U.S. patent application number 15/955418 was filed with the patent office on 2018-08-23 for processing biomass.
The applicant listed for this patent is XYLECO, INC.. Invention is credited to Marshall Medoff.
Application Number | 20180236427 15/955418 |
Document ID | / |
Family ID | 43974444 |
Filed Date | 2018-08-23 |
United States Patent
Application |
20180236427 |
Kind Code |
A1 |
Medoff; Marshall |
August 23, 2018 |
PROCESSING BIOMASS
Abstract
Biomass (e.g., plant biomass, animal biomass, and municipal
waste biomass) is processed to produce useful products, such as
fuels. For example, systems can use feedstock materials, such as
cellulosic and/or lignocellulosic materials and/or starchy or
sugary materials, to produce ethanol and/or butanol, e.g., by
fermentation.
Inventors: |
Medoff; Marshall;
(Wakefield, MA) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
XYLECO, INC. |
Wakefield |
MA |
US |
|
|
Family ID: |
43974444 |
Appl. No.: |
15/955418 |
Filed: |
April 17, 2018 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
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15048455 |
Feb 19, 2016 |
9968905 |
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15955418 |
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14963064 |
Dec 8, 2015 |
9278896 |
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15048455 |
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14919221 |
Oct 21, 2015 |
9283537 |
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14963064 |
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14810158 |
Jul 27, 2015 |
9187769 |
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14919221 |
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14704733 |
May 5, 2015 |
9132407 |
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14810158 |
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14580100 |
Dec 22, 2014 |
9062328 |
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14704733 |
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14215105 |
Mar 17, 2014 |
8946489 |
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14580100 |
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13656892 |
Oct 22, 2012 |
8716537 |
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14215105 |
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12719776 |
Mar 8, 2010 |
8497366 |
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13656892 |
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12417880 |
Apr 3, 2009 |
8212087 |
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12719776 |
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61049404 |
Apr 30, 2008 |
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61049413 |
Apr 30, 2008 |
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61049415 |
Apr 30, 2008 |
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61049419 |
Apr 30, 2008 |
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61073496 |
Jun 18, 2008 |
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Current U.S.
Class: |
1/1 |
Current CPC
Class: |
B01J 19/121 20130101;
C12M 45/00 20130101; Y02E 50/16 20130101; D21B 1/10 20130101; B01J
2219/0879 20130101; B02C 23/18 20130101; C10L 2290/26 20130101;
C12P 7/10 20130101; Y02E 50/10 20130101; C07C 27/04 20130101; B01J
19/123 20130101; H01J 37/3002 20130101; B01J 19/126 20130101; C07C
27/00 20130101; C10L 1/02 20130101; C12P 2201/00 20130101; D21B
1/02 20130101; C13K 1/02 20130101; B01J 2219/00006 20130101; B01J
19/085 20130101; D21B 1/063 20130101; C12P 19/00 20130101; B01J
2219/089 20130101; B01J 2219/0871 20130101; C07C 27/24 20130101;
B01J 19/081 20130101; C08B 1/00 20130101; C12P 19/02 20130101; C12P
19/14 20130101; G21K 5/00 20130101; B01J 2219/08 20130101; B01J
2219/0869 20130101; C10L 2200/0469 20130101 |
International
Class: |
B01J 19/08 20060101
B01J019/08; C08B 1/00 20060101 C08B001/00; B01J 19/12 20060101
B01J019/12; B02C 23/18 20060101 B02C023/18; C07C 27/04 20060101
C07C027/04; C07C 27/24 20060101 C07C027/24; C12M 1/00 20060101
C12M001/00; C12P 7/10 20060101 C12P007/10; H01J 37/30 20060101
H01J037/30; G21K 5/00 20060101 G21K005/00; D21B 1/06 20060101
D21B001/06; D21B 1/02 20060101 D21B001/02; C13K 1/02 20060101
C13K001/02; C12P 19/14 20060101 C12P019/14; C12P 19/02 20060101
C12P019/02; C12P 19/00 20060101 C12P019/00 |
Claims
1. A method of converting an intermediate to a product, the method
comprising treating an irradiated intermediate product with a
microorganism, the intermediate having been prepared by irradiating
a starchy material and treating the starchy material with an
enzyme.
2. The method of claim 1 wherein the product comprises a
combustible fuel.
3. The method of claim 1 wherein the starchy material is selected
from the group consisting of corn starch, wheat starch, potato
starch, rice starch, derivatives thereof, and mixtures thereof.
4. The method of claim 3, wherein the starchy material consists
essentially of corn starch.
5. The method of claim 1 wherein the starchy material is selected
from the group consisting of arracacha, buckwheat, banana, rice,
arrowroot, barley, cassava, kudzu, oca, sago, sorghum, potatoes,
sweet potato, taro, yams, beans, lentils, peas and mixtures
thereof.
6. The method of claim 1 wherein the starchy material comprises
corn.
7. The method of claim 1, wherein when irradiating the starchy
material, the radiation is applied at a total dosage of between
about 10 MRad and about 50 MRad.
8. The method of claim 1, wherein treating the intermediate product
with the microorganism comprises fermentation.
9. The method of claim 1, wherein the intermediate product
comprises one or more sugars selected from the group consisting of
cellobiose, lactose, sucrose, glucose and xylose.
10. The method of claim 1, wherein irradiating is performed with an
electron beam.
11. The method of claim 1, wherein the enzyme comprises
amylase.
12. The method of claim 1, wherein irradiating is conducted under
conditions selected to alter the functionalization of the starchy
material.
Description
RELATED APPLICATIONS
[0001] This application is a continuation of pending U.S.
application Ser. No. 15/048,455, filed Feb. 19, 2016, which is a
continuation of U.S. application Ser. No. 14/963,064, filed Dec. 8,
2015, now U.S. Pat. No. 9,278,896, issued on Mar. 8, 2016, which is
a continuation of U.S. application Ser. No. 14/919,221, filed Oct.
21, 2015, now U.S. Pat. No. 9,283,537, issued on Mar. 15, 2016,
which is a continuation of U.S. application Ser. No. 14/810,158,
filed Jul. 27, 2015, now U.S. Pat. No. 9,187,769, issued on Nov.
17, 2015, which is a continuation of U.S. application Ser. No.
14/704,733, filed May 5, 2015, now U.S. Pat. No. 9,132,407, issued
on Sep. 15, 2015, which is a continuation of U.S. application Ser.
No. 14/580,100, filed Dec. 22, 2014, now U.S. Pat. No. 9,062,328,
issued on Jun. 23, 2015, which is a continuation of U.S.
application Ser. No. 14/215,105, filed Mar. 17, 2014, now U.S. Pat.
No. 8,946,489, issued on Feb. 3, 2015, which is a continuation of
U.S. application Ser. No. 13/656,892, filed Oct. 22, 2012, now U.S.
Pat. No. 8,716,537, issued on May 6, 2014, which is a continuation
of U.S. application Ser. No. 12/719,776, filed Mar. 8, 2010, now
U.S. Pat. No. 8,497,366, issued on Jul. 30, 2013, which is a
continuation of U.S. application Ser. No. 12/417,880, filed Apr. 3,
2009, now U.S. Pat. No. 8,212,087, issued on Jul. 3, 2012, which
claims benefit of U.S. provisional App. Nos. 61/049,404, filed Apr.
30, 2008, 61/049,413, filed Apr. 30, 2008, 61/049,415, filed Apr.
30, 2008, 61/049,419, filed Apr. 30, 2008, and 61/073,496, filed
Jun. 18, 2008. The entire contents of all of these applications are
incorporated by reference herein.
TECHNICAL FIELD
[0002] This invention relates to processing biomass, such as
methods and systems for processing biomass.
BACKGROUND
[0003] Various carbohydrates, such as cellulosic and
lignocellulosic materials, e.g., in fibrous form, are produced,
processed, and used in large quantities in a number of
applications. Often such materials are used once, and then
discarded as waste, or are simply considered to be waste materials,
e.g., sewage, bagasse, sawdust, and stover.
SUMMARY
[0004] Biomass can be processed to alter its structure at one or
more levels. The processed biomass can then be used, for example as
a source of materials and/or fuel.
[0005] In general, the invention pertains to methods of changing a
molecular and/or a supramolecular structure of a biomass feedstock.
As will be discussed below, in some implementations, the methods
include irradiating and quenching the biomass feedstock. In other
implementations, the methods include irradiating the feedstock,
cooling the feedstock, and again irradiating the feedstock.
[0006] Carbohydrate-containing materials (e.g., biomass materials
or biomass-derived materials, such as starchy materials, cellulosic
materials, lignocellulosic materials, or biomass materials) that
are or that include significant amounts of low molecular weight
sugars (e.g., monosaccharides, disaccharides, or trisaccharides),
can be processed to change their structure, and products can be
made from the structurally changed materials. For example, many of
the methods described herein can provide cellulosic and/or
lignocellulosic materials that have a lower molecular weight and/or
crystallinity relative to a native material. Many of the methods
provide materials that can be more readily utilized by a variety of
microorganisms to produce useful products, such as hydrogen,
alcohols (e.g., ethanol or butanol), organic acids (e.g., acetic
acid), hydrocarbons, co-products (e.g., proteins) or mixtures of
any of these. Many of the products obtained, such as ethanol or
n-butanol, can be utilized as a fuel for powering cars, trucks,
tractors, ships or trains, e.g., as an internal combustion fuel or
as a fuel cell feedstock. Many of the products obtained can also be
utilized to power aircraft, such as planes, e.g., having jet
engines or helicopters. In addition, the products described herein
can be utilized for electrical power generation, e.g., in a
conventional steam generating plant or in a fuel cell plant.
[0007] In one aspect, the invention features methods that include
quenching a biomass feedstock that has been irradiated to ionize
the biomass feedstock so that the feedstock has a first level of
radicals which are detectable with an electron spin resonance
spectrometer, to an extent that the radicals are at a second level
lower than the first level. Some methods further include processing
the irradiated and quenched biomass feedstock to produce a
product.
[0008] Some implementations include one or more of the following
features.
[0009] Quenching can include quenching the radicals to a level that
is no longer detectable with the electron spin resonance
spectrometer, e.g., less than about 10.sup.14 spins. Quenching can
include applying pressure to the biomass, e.g., a pressure of
greater than about 1000 psi. Pressure can be applied together with
the application of heat. Quenching can include contacting the
biomass with a gas capable of reacting with the radicals, e.g.,
contacting the biomass with a fluid capable of penetrating into the
biomass and reacting with the radicals. Quenching can also, or
alternatively, include contacting the biomass with an antioxidant.
In some cases, the biomass feedstock includes an antioxidant
dispersed therein, and quenching includes contacting the
antioxidant dispersed in the biomass feedstock with the
radicals.
[0010] In another aspect, the invention features a method including
irradiating a biomass feedstock that has been prepared by reducing
one or more dimensions of individual pieces of the biomass
feedstock, using an apparatus comprising an accelerator configured
to accelerate particles, such as electrons or ions, wherein the
apparatus is capable of processing greater than 1,000 tons of
biomass material per year, e.g., greater than 10,000, 25,000,
50,000, 100,000, or even greater than 1,000,000 tons of biomass per
year.
[0011] In a further aspect, the invention features irradiating a
biomass feedstock, e.g., with ionizing radiation of electrons or
ions, to change a molecular and/or supramolecular structure of the
biomass feedstock, cooling the biomass feedstock, and then
re-irradiating the biomass feedstock. The two applications of
radiation can be the same or different, e.g., the same kind, such
as electrons at the same level.
[0012] The invention also features products formed by these
methods, and systems for performing the methods.
[0013] Some implementations of these methods include one or more of
the following features.
[0014] The biomass feedstock can be cooled to an extent that after
cooling, the biomass is at a temperature below its initial
temperature prior to irradiation. Cooling of the biomass can
include contacting the biomass with a fluid at a temperature below
the initial temperature of the biomass or below the temperature of
the biomass after irradiation.
[0015] Each irradiation of the biomass feedstock can be performed
as the biomass feedstock is being pneumatically conveyed in a
fluid. Radiation can be applied as the biomass feedstock falls
under the influence of gravity. For example, the biomass can be
conveyed from a first belt at a first height and captured by a
second belt at a second level, lower than the first level, the
trailing edge of the first belt and the leading edge of the second
belt defining a gap, and ionizing radiation can be applied to the
biomass feedstock in the defined gap. During irradiation the
biomass can be conveyed past a particle gun and through a beam of
charged particles. The biomass feedstock may have a bulk density of
less than about 0.25 g/cm.sup.3 in a region under and/or above the
beam.
[0016] In another aspect, the invention features methods of
changing a molecular structure and/or a supramolecular structure of
a starchy material or of a low molecular weight sugar, such as
sucrose, in a biomass feedstock comprising at least about 10
percent by weight of the low molecular weight sugar. The methods
include processing a treated biomass feedstock to produce a
product, the treated biomass feedstock having been prepared by
pretreating a biomass feedstock using a pretreatment method that
changes the molecular structure and/or supramolecular structure of
the starchy material or of the low molecular weight sugar portion,
selected from radiation, sonication, pyrolysis, and oxidation.
[0017] Any of the above aspects of the invention can, in some
implementations, include one or more of the following features.
[0018] The method can further include treating the biomass
feedstock with one or more other pretreatment methods, wherein the
other pretreatment methods are selected from sonication, pyrolysis,
and oxidation.
[0019] Radiation can be in the form of an electron beam, which can
be applied, for example, at a total dosage of between about 10 MRad
and about 50 MRad. The radiation can be ionizing radiation.
[0020] Processing can include making a combustible fuel. In some
cases, processing includes converting the irradiated material
utilizing a microorganism having the ability to convert at least
about 1 percent by weight of the biomass to the fuel.
[0021] In some implementations, processing comprises fermenting the
feedstock, aerobically or anaerobically, to produce a product such
as a fuel, e.g., ethanol. For example, processing may comprise
contacting the feedstock with a microorganism having the ability to
convert at least a portion, e.g., at least about 1 percent by
weight, of the feedstock to the product. The microorganism can be a
natural microorganism or an engineered microorganism. For example,
the microorganism can be a bacterium, e.g., a cellulolytic
bacterium, a fungus, e.g., a yeast, a plant or a protist, e.g., an
algae, a protozoa or a fungus-like protist, e.g., a slime mold.
When the organisms are compatible, mixtures may be utilized.
[0022] The product can include one or more of hydrogen, organic
acids, proteins, hydrocarbons, and alcohols, e.g., ethanol,
n-propanol, isopropanol, n-butanol, and mixtures thereof. Other
examples of products that may be produced by the methods disclosed
herein include mono- and polyfunctional C1-C6 alkyl alcohols, mono-
and poly-functional carboxylic acids, C1-C6 hydrocarbons, and
combinations thereof. Other examples of alcohols include methanol,
ethylene glycol, propylene glycol, 1,4-butane diol, glycerin, and
combinations thereof. Carboxylic acids include formic acid, acetic
acid, propionic acid, butyric acid, valeric acid, caproic acid,
palmitic acid, stearic acid, oxalic acid, malonic acid, succinic
acid, glutaric acid, oleic acid, linoleic acid, glycolic acid,
lactic acid, .gamma.-hydroxybutyric acid, and combinations thereof.
Hydrocarbons include methane, ethane, propane, pentane, n-hexane,
and combinations thereof. Many of these products may be used as
fuels.
[0023] The method can further include preparing the biomass
feedstock by reducing one or more dimensions of individual pieces
of the biomass feedstock.
[0024] In some cases, the biomass feedstock has internal fibers,
and the biomass feedstock has been sheared to an extent that its
internal fibers are substantially exposed. The biomass feedstock
can in some cases include or be made up of discrete fibers and/or
particles having a maximum dimension of not more than about 0.5
mm.
[0025] The biomass feedstock can be prepared and then pretreated,
or pretreated and then prepared. The pretreatment method can be
selected from, e.g., radiation, such as radiation from a beam of
electrons or ions, sonication, pyrolysis, and oxidation. In some
embodiments, at least one of the pretreatment methods, e.g.,
radiation, is performed on the biomass feedstock while the biomass
feedstock is exposed to air, nitrogen, oxygen, helium, or argon. In
some embodiments, pretreatment can include pretreating the biomass
feedstock with steam explosion.
[0026] In some embodiments, reducing one or more dimensions of
individual pieces of biomass includes shearing, wet or dry
grinding, cutting, squeezing, compressing or mixtures of any of
these processes. For example, shearing can be performed with a
rotary knife cutter. The shearing can produce fibers having an
average length-to-diameter ratio of greater than 5/1. In some
embodiments, the prepared biomass can have a BET surface area of
greater than 0.25 m.sup.2/g. The biomass can be sheared to an
extent that internal fibers of the biomass are substantially
exposed. The biomass can be sheared to an extent that it has a bulk
density of less than about 0.35 g/cm.sup.3.
[0027] In some embodiments, two or more pretreatment methods can be
applied to the biomass feedstock, for example radiation and
sonication, radiation and oxidation, radiation and pyrolization,
sonication and oxidation, sonication and pyrolization, or oxidation
and pyrolization. The two or more processes can be performed in any
order or at or about the same time.
[0028] In some embodiments, the change in molecular structure
and/or change in supramolecular structure of the biomass, e.g., the
cellulosic or lignocellulosic material or low molecular weight
sugar or starchy material, can include a change in any one or more
of an average molecular weight, average crystallinity, surface
area, degree of polymerization, porosity, branching, grafting,
domain size or number, a change in kind or number of chemical
functional groups, and a change in formula weight. For example, the
change in molecular structure and/or supramolecular structure can
include a decrease in either one or both of an average molecular
weight and average crystallinity or an increase in either one or
both of surface area and porosity.
[0029] In some instances, functionalized biomass (biomass in which
the number and/or kind of functional groups has been changed) is
more soluble and more readily utilized by microorganisms in
comparison to un-functionalized biomass. In addition, many of the
functionalized materials described herein are less prone to
oxidation and can have enhanced long-term stability under ambient
conditions.
[0030] In some embodiments, at least one pretreatment method can be
performed on biomass in which less than about 25 percent by weight
of the biomass is in a swollen state, the swollen state being
characterized as having a volume of more than about 2.5 percent
higher than an unswollen state. In other embodiments, the biomass
is mixed with or includes a swelling agent. For example, in any
method described herein, the biomass can be mixed with or and
include a swelling agent, and the biomass can receive a dose of
less than about 10 Mrad of radiation.
[0031] The pretreated biomass material can further include,
optionally, a buffer, such as sodium bicarbonate or ammonium
chloride, an electrolyte, such as potassium chloride or sodium
chloride, a growth factor, such as biotin, and/or a base pair such
as uracil, a surfactant, a mineral, or a chelating agent.
[0032] In some cases, pretreatment is performed while the biomass
feedstock is exposed to air, nitrogen, oxygen, helium or argon.
Pretreatment may be performed under pressure, e.g., under a
pressure of greater than about 2.5 atmospheres. The methods
described herein may further include oxidizing the biomass prior to
pretreatment.
[0033] The biomass feedstock may include, for example, paper, paper
products, paper waste, wood, particle board, sawdust, agricultural
waste, sewage, silage, grasses, rice hulls, bagasse, cotton, jute,
hemp, flax, bamboo, sisal, abaca, straw, corn cobs, corn stover,
switchgrass, alfalfa, hay, rice hulls, coconut hair, cotton,
synthetic celluloses, seaweed, algae, and mixtures thereof. The
biomass may in some cases include a synthetic material.
[0034] The biomass can in some cases include a carbohydrate that
includes one or more .beta.-1,4-linkages and has a number average
molecular weight between about 3,000 and 50,000.
[0035] In some implementations, the biomass material includes a
starch, e.g., corn starch, wheat starch, potato starch or rice
starch, a derivative of starch, or a material that includes starch,
such as an edible food product or a crop. For example, the starchy
material can be arracacha, buckwheat, banana, barley, cassava,
kudzu, ocra, sago, sorghum, regular household potatoes, sweet
potato, taro, yams, or one or more beans, such as fava beans,
lentils, or peas.
[0036] In other implementations, the biomass material is or
includes a low molecular weight sugar. For example, the biomass
materials can include at least about 0.5 percent by weight of a low
molecular weight sugar, e.g., at least about 2, 3, 4, 5, 6, 7, 8,
9, 10, 12.5, 25, 35, 50, 60, 70, 80, 90 or even at least about 95
percent by weight of the low molecular weight sugar. In some
instances, the biomass is composed substantially of the low
molecular weight sugar, e.g., greater than 95 percent by weight,
such as 96, 97, 98, 99 or substantially 100 percent by weight of
the low molecular weight sugar. Biomass materials that include low
molecular weight sugars can be agricultural products or food
products, such as sugarcane and sugar beets, or an extract
therefrom, e.g., juice from sugarcane or sugar beets. Specific
examples of low molecular weight sugars include cellobiose,
lactose, sucrose, glucose and xylose, along with derivatives
thereof. Processing low molecular weight sugars by any of the
methods described herein can make the resulting products more
soluble and/or easier to utilize by microbes.
[0037] In any of the methods disclosed herein, radiation may be
applied from a device that is in a vault.
[0038] The term "fibrous material," as used herein, is a material
that includes numerous loose, discrete and separable fibers. For
example, a fibrous material can be prepared from a bleached Kraft
paper fiber source by shearing, e.g., with a rotary knife
cutter.
[0039] The term "screen," as used herein, means a member capable of
sieving material according to size. Examples of screens include a
perforated plate, cylinder or the like, or a wire mesh or cloth
fabric.
[0040] The term "pyrolysis," as used herein, means to break bonds
in a material by the application of heat energy. Pyrolysis can
occur while the subject material is under vacuum, or immersed in a
gaseous material, such as an oxidizing gas, e.g., air or oxygen, or
a reducing gas, such as hydrogen.
[0041] Oxygen content is measured by elemental analysis by
pyrolyzing a sample in a furnace operating at 1300.degree. C. or
above.
[0042] The terms "biomass" refers to any non-fossilized, i.e.,
renewable, organic matter. The various types of biomass include
plant biomass (defined below), microbial biomass, animal biomass
(any animal by-product, animal waste, etc.) and municipal waste
biomass (residential and light commercial refuse with recyclables
such as metal and glass removed).
[0043] The term "plant biomass" and "lignocellulosic biomass" refer
to virtually any plant-derived organic matter (woody or non-woody).
Plant biomass can include, but is not limited to, agricultural or
food crops (e.g., sugarcane, sugar beets or corn kernels) or an
extract therefrom (e.g., sugar from sugarcane and corn starch from
corn), agricultural crop wastes and residues such as corn stover,
wheat straw, rice straw, sugar cane bagasse, and the like. Plant
biomass further includes, but is not limited to, trees, woody
energy crops, wood wastes and residues such as softwood forest
thinnings, barky wastes, sawdust, paper and pulp industry waste
streams, wood fiber, and the like. Additionally, grass crops, such
as switchgrass and the like have potential to be produced on a
large-scale as another plant biomass source. For urban areas, the
best potential plant biomass feedstock includes yard waste (e.g.,
grass clippings, leaves, tree clippings, and brush) and vegetable
processing waste.
[0044] "Lignocellulosic feedstock," is any type of plant biomass
such as, but not limited to, non-woody plant biomass, cultivated
crops, such as, but not limited to, grasses, for example, but not
limited to, C4 grasses, such as switchgrass, cord grass, rye grass,
miscanthus, reed canary grass, or a combination thereof, or sugar
processing residues such as bagasse, or beet pulp, agricultural
residues, for example, soybean stover, corn stover, rice straw,
rice hulls, barley straw, corn cobs, wheat straw, canola straw,
rice straw, oat straw, oat hulls, corn fiber, recycled wood pulp
fiber, sawdust, hardwood, for example aspen wood and sawdust,
softwood, or a combination thereof. Further, the lignocellulosic
feedstock may include cellulosic waste material such as, but not
limited to, newsprint, cardboard, sawdust, and the like.
[0045] Lignocellulosic feedstock may include one species of fiber
or alternatively, lignocellulosic feedstock may include a mixture
of fibers that originate from different lignocellulosic feedstocks.
Furthermore, the lignocellulosic feedstock may comprise fresh
lignocellulosic feedstock, partially dried lignocellulosic
feedstock, fully dried lignocellulosic feedstock or a combination
thereof.
[0046] For the purposes of this disclosure, carbohydrates are
materials that are composed entirely of one or more saccharide
units or that include one or more saccharide units. The saccharide
units can be functionalized about the ring with one or more
functional groups, such as carboxylic acid groups, amino groups,
nitro groups, nitroso groups or nitrile groups and still be
considered carbohydrates. Carbohydrates can be polymeric (e.g.,
equal to or greater than 10-mer, 100-mer, 1,000-mer, 10,000-mer, or
100,000-mer), oligomeric (e.g., equal to or greater than a 4-mer,
5-mer, 6-mer, 7-mer, 8-mer, 9-mer or 10-mer), trimeric, dimeric, or
monomeric. When the carbohydrates are formed of more than a single
repeat unit, each repeat unit can be the same or different.
[0047] Examples of polymeric carbohydrates include cellulose,
xylan, pectin, and starch, while cellobiose and lactose are
examples of dimeric carbohydrates. Examples of monomeric
carbohydrates include glucose and xylose.
[0048] Carbohydrates can be part of a supramolecular structure,
e.g., covalently bonded into the structure. Examples of such
materials include lignocellulosic materials, such as those found in
wood.
[0049] A starchy material is one that is or includes significant
amounts of starch or a starch derivative, such as greater than
about 5 percent by weight starch or starch derivative. For purposes
of this disclosure, a starch is a material that is or includes an
amylose, an amylopectin, or a physical and/or chemical mixture
thereof, e.g., a 20:80 or 30:70 percent by weight mixture of
amylose to amylopectin. For example, rice, corn, and mixtures
thereof are starchy materials. Starch derivatives include, e.g.,
maltodextrin, acid-modified starch, base-modified starch, bleached
starch, oxidized starch, acetylated starch, acetylated and oxidized
starch, phosphate-modified starch, genetically-modified starch and
starch that is resistant to digestion.
[0050] For purposes of this disclosure, a low molecular weight
sugar is a carbohydrate or a derivative thereof that has a formula
weight (excluding moisture) that is less than about 2,000, e.g.,
less than about 1,800, 1,600, less than about 1,000, less than
about 500, less than about 350 or less than about 250. For example,
the low molecular weight sugar can be a monosaccharide, e.g.,
glucose or xylose, a disaccharide, e.g., cellobiose or sucrose, or
a trisaccharide.
[0051] A combustible fuel is a material capable of burning in the
presence of oxygen. Examples of combustible fuels include ethanol,
n-propanol, n-butanol, hydrogen and mixtures of any two or more of
these.
[0052] Swelling agents as used herein are materials that cause a
discernable swelling, e.g., a 2.5 percent increase in volume over
an unswollen state of cellulosic and/or lignocellulosic materials,
when applied to such materials as a solution, e.g., a water
solution. Examples include alkaline substances, such as sodium
hydroxide, potassium hydroxide, lithium hydroxide and ammonium
hydroxides, acidifying agents, such as mineral acids (e.g.,
sulfuric acid, hydrochloric acid and phosphoric acid), salts, such
as zinc chloride, calcium carbonate, sodium carbonate,
benzyltrimethylammonium sulfate, and basic organic amines, such as
ethylene diamine.
[0053] A "sheared material," as used herein, is a material that
includes discrete fibers in which at least about 50% of the
discrete fibers have a length/diameter (L/D) ratio of at least
about 5, and that has an uncompressed bulk density of less than
about 0.6 g/cm.sup.3. A sheared material is thus different from a
material that has been cut, chopped or ground.
[0054] Changing a molecular structure of a biomass feedstock, as
used herein, means to change the chemical bonding arrangement, such
as the type and quantity of functional groups, or conformation of
the structure. For example, the change in the molecular structure
can include changing the supramolecular structure of the material,
oxidation of the material, changing an average molecular weight,
changing an average crystallinity, changing a surface area,
changing a degree of polymerization, changing a porosity, changing
a degree of branching, grafting on other materials, changing a
crystalline domain size, or an changing an overall domain size.
[0055] This application incorporates by reference herein the entire
contents of International Application No. PCT/US2007/022719, filed
on Oct. 26, 2007. The full disclosures of each of the following
U.S. patent applications, which are being filed concurrently
herewith, are hereby incorporated by reference herein: U.S.
application Ser. No. 12/417,707, now U.S. Pat. No. 7,867,358,
issued on Jan. 11, 2011, U.S. application Ser. No. 12/417,720, now
U.S. Pat. No. 7,846,295, issued on Dec. 7, 2010, U.S. patent
application Ser. No. 12/417,699, now U.S. Pat. No. 7,931,784,
issued on Apr. 26, 2011, U.S. application Ser. No. 12/417,840, now
U.S. Pat. No. 8,236,535, issued on Aug. 7, 2012, U.S. application
Ser. No. 12/417,900, U.S. application Ser. No. 12/417,880, now U.S.
Pat. No. 8,212,087, issued on Jul. 3, 2012, U.S. application Ser.
No. 12/417,723, U.S. application Ser. No. 12/417,786, now U.S. Pat.
No. 8,025,098, issued on Sep. 27, 2011, U.S. application Ser. No.
12/417,904, now U.S. Pat. No. 7,867,359, issued on Jan. 11,
2011.
[0056] Unless otherwise defined, all technical and scientific terms
used herein have the same meaning as commonly understood by one of
ordinary skill in the art to which this invention belongs. Although
methods and materials similar or equivalent to those described
herein can be used in the practice or testing of the present
invention, suitable methods and materials are described below. All
publications, Appendices, patent applications, patents, and other
references mentioned herein or attached hereto are incorporated by
reference in their entirety for all that they contain. In case of
conflict, the present specification, including definitions, will
control. In addition, the materials, methods, and examples are
illustrative only and not intended to be limiting.
[0057] Other features and advantages of the invention will be
apparent from the following detailed description, and from the
claims.
DESCRIPTION OF DRAWINGS
[0058] FIG. 1 is a block diagram illustrating conversion of biomass
into products and co-products.
[0059] FIG. 2 is block diagram illustrating conversion of a fiber
source into a first and second fibrous material.
[0060] FIG. 3 is a cross-sectional view of a rotary knife
cutter.
[0061] FIG. 4 is block diagram illustrating conversion of a fiber
source into a first, second and third fibrous material.
[0062] FIG. 5 is block diagram illustrating densification of a
material.
[0063] FIG. 6 is a perspective view of a pellet mill.
[0064] FIG. 7A is a densified fibrous material in pellet form.
[0065] FIG. 7B is a transverse cross-section of a hollow pellet in
which a center of the hollow is in-line with a center of the
pellet.
[0066] FIG. 7C is a transverse cross-section of a hollow pellet in
which a center of the hollow is out of line with the center of the
pellet.
[0067] FIG. 7D is a transverse cross-section of a tri-lobal
pellet.
[0068] FIG. 8 is a block diagram illustrating a treatment sequence
for processing feedstock.
[0069] FIG. 9 is a perspective, cut-away view of a gamma irradiator
housed in a concrete vault.
[0070] FIG. 10 is an enlarged perspective view of region R of FIG.
9.
[0071] FIG. 11 is a block diagram illustrating an electron beam
irradiation feedstock pretreatment sequence.
[0072] FIG. 11A is a schematic representation of biomass being
ionized, and then oxidized or quenched.
[0073] FIG. 11B is a schematic side view of a system for
irradiating a low bulk density material, while FIG. 11C is
cross-sectional of the system taken along 11C-11C.
[0074] FIG. 11D is a schematic cross-sectional view of a fluidized
bed system for irradiating a low bulk density material.
[0075] FIG. 11E is a schematic side-view of another system for
irradiating a low bulk density material.
[0076] FIG. 12 is a schematic view of a system for sonicating a
process stream of cellulosic material in a liquid medium.
[0077] FIG. 13 is a schematic view of a sonicator having two
transducers coupled to a single horn.
[0078] FIG. 14 is a block diagram illustrating a pyrolytic
feedstock pretreatment system.
[0079] FIG. 15 is a cross-sectional side view of a pyrolysis
chamber.
[0080] FIG. 16 is a cross-sectional side view of a pyrolysis
chamber.
[0081] FIG. 17 is a cross-sectional side view of a pyrolyzer that
includes a heated filament.
[0082] FIG. 18 is a schematic cross-sectional side view of a
Curie-Point pyrolyzer.
[0083] FIG. 19 is a schematic cross-sectional side view of a
furnace pyrolyzer.
[0084] FIG. 20 is a schematic cross-sectional top view of a laser
pyrolysis apparatus.
[0085] FIG. 21 is a schematic cross-sectional top view of a
tungsten filament flash pyrolyzer.
[0086] FIG. 22 is a block diagram illustrating an oxidative
feedstock pretreatment system.
[0087] FIG. 23 is block diagram illustrating a general overview of
the process of converting a fiber source into a product, e.g.,
ethanol.
[0088] FIG. 24 is a cross-sectional view of a steam explosion
apparatus.
[0089] FIG. 25 is a schematic cross-sectional side view of a hybrid
electron beam/sonication device.
[0090] FIG. 26 is a block diagram illustrating a dry milling
process for corn kernels.
[0091] FIG. 27 is a block diagram illustrating a wet milling
process for corn kernels.
[0092] FIG. 28 is a scanning electron micrograph of a fibrous
material produced from polycoated paper at 25.times. magnification.
The fibrous material was produced on a rotary knife cutter
utilizing a screen with 1/8 inch openings.
[0093] FIG. 29 is a scanning electron micrograph of a fibrous
material produced from bleached Kraft board paper at 25.times.
magnification. The fibrous material was produced on a rotary knife
cutter utilizing a screen with 1/8 inch openings.
[0094] FIG. 30 is a scanning electron micrograph of a fibrous
material produced from bleached Kraft board paper at 25.times.
magnification. The fibrous material was twice sheared on a rotary
knife cutter utilizing a screen with 1/16 inch openings during each
shearing.
[0095] FIG. 31 is a scanning electron micrograph of a fibrous
material produced from bleached Kraft board paper at 25.times.
magnification. The fibrous material was thrice sheared on a rotary
knife cutter. During the first shearing, a 1/8 inch screen was
used; during the second shearing, a 1/16 inch screen was used, and
during the third shearing a 1/32 inch screen was used.
[0096] FIG. 32 is a schematic side view of a sonication apparatus,
while FIG. 33 is a cross-sectional view through the processing cell
of FIG. 32.
[0097] FIG. 34 is a scanning electron micrograph at 1000.times.
magnification of a fibrous material produced from shearing
switchgrass on a rotary knife cutter, and then passing the sheared
material through a 1/32 inch screen.
[0098] FIGS. 35 and 36 are scanning electron micrographs of the
fibrous material of FIG. 34 after irradiation with 10 Mrad and 100
Mrad gamma rays, respectively, at 1000.times. magnification.
[0099] FIG. 37 is a scanning electron micrographs of the fibrous
material of FIG. 34 after irradiation with 10 Mrad and sonication
at 1000.times. magnification.
[0100] FIG. 38 is a scanning electron micrographs of the fibrous
material of FIG. 34 after irradiation with 100 Mrad and sonication
at 1000.times. magnification.
[0101] FIG. 39 is an infrared spectrum of Kraft board paper sheared
on a rotary knife cutter.
[0102] FIG. 40 is an infrared spectrum of the Kraft paper of FIG.
39 after irradiation with 100 Mrad of gamma radiation.
[0103] FIG. 41 is a schematic view of a process for biomass
conversion.
[0104] FIG. 42 is schematic view of another process for biomass
conversion.
DETAILED DESCRIPTION
[0105] Systems and processes are described herein that can use
various biomass materials, such as cellulosic materials,
lignocellulosic materials, starchy materials or materials that are
or that include low molecular weight sugars, as feedstock
materials. Such materials are often readily available, but can be
difficult to process, e.g., by fermentation, or can gives
sub-optimal yields at a slow rate. In some cases, the difficulty in
processing stems at least in part from the recalcitrance of the
feedstock. Processing steps are described herein that can reduce
this recalcitrance and thereby facilitate conversion of the biomass
feedstock to a desired product.
[0106] In the processes described herein, feedstock materials are
first physically prepared for processing, often by size reduction
of raw feedstock materials. Physically prepared feedstock can then
be pretreated or processed using one or more of radiation (which
may in some cases be under controlled thermal conditions),
sonication, oxidation, pyrolysis, and steam explosion. The various
pretreatment systems and methods can be used in combinations of
two, three, or even four of these technologies. Other techniques
which may be used to enhance the processing of the feedstock are
described herein, for example cooling the feedstock between
irradiating steps and quenching the biomass feedstock after
irradiation.
[0107] Functionalized materials are also disclosed herein, having
desired types and amounts of functionality, such as carboxylic acid
groups, enol groups, aldehyde groups, ketone groups, nitrile
groups, nitro groups, or nitroso groups, which can be prepared
using the methods described herein. Such functionalized materials
can be, e.g., more soluble, easier to utilize by various
microorganisms or can be more stable over the long term, e.g., less
prone to oxidation.
[0108] In some cases, the feedstock can include low molecular
weight sugars or starchy materials, as will be discussed in detail
herein.
Types of Biomass
[0109] Generally, any biomass material that is or includes
carbohydrates composed entirely of one or more saccharide units or
that include one or more saccharide units can be processed by any
of the methods described herein. For example, the biomass material
can be cellulosic or lignocellulosic materials, starchy materials,
such as kernels of corn, grains of rice or other foods, or
materials that are or that include one or more low molecular weight
sugars, such as sucrose or cellobiose.
[0110] For example, such materials can include paper, paper
products, wood, wood-related materials, particle board, grasses,
rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal,
abaca, straw, corn cobs, rice hulls, coconut hair, algae, seaweed,
cotton, synthetic celluloses, or mixtures of any of these. Suitable
materials include those listed in the Summary section, above.
[0111] Fiber sources include cellulosic fiber sources, including
paper and paper products (e.g., polycoated paper and Kraft paper),
and lignocellulosic fiber sources, including wood, and wood-related
materials, e.g., particle board. Other suitable fiber sources
include natural fiber sources, e.g., grasses, rice hulls, bagasse,
cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs,
rice hulls, coconut hair; fiber sources high in .alpha.-cellulose
content, e.g., cotton; and synthetic fiber sources, e.g., extruded
yarn (oriented yarn or un-oriented yarn). Natural or synthetic
fiber sources can be obtained from virgin scrap textile materials,
e.g., remnants or they can be post consumer waste, e.g., rags. When
paper products are used as fiber sources, they can be virgin
materials, e.g., scrap virgin materials, or they can be
post-consumer waste. Aside from virgin raw materials,
post-consumer, industrial (e.g., offal), and processing waste
(e.g., effluent from paper processing) can also be used as fiber
sources. Also, the fiber source can be obtained or derived from
human (e.g., sewage), animal or plant wastes. Additional fiber
sources have been described in U.S. Pat. Nos. 6,448,307, 6,258,876,
6,207,729, 5,973,035 and 5,952,105.
[0112] Microbial biomass includes biomass derived from naturally
occurring or genetically modified unicellular organisms and/or
multicellular organisms, e.g., organisms from the ocean, lakes,
bodies of water, e.g., salt water or fresh water, or on land, and
that contains a source of carbohydrate (e.g., cellulose). Microbial
biomass can include, but is not limited to, for example protists
(e.g., animal (e.g., protozoa such as flagellates, amoeboids,
ciliates, and sporozoa) and plant (e.g., algae such alveolates,
chlorarachniophytes, cryptomonads, euglenids, glaucophytes,
haptophytes, red algae, stramenopiles, and viridaeplantae)),
seaweed, plankton (e.g., macroplankton, mesoplankton,
microplankton, nanoplankton, picoplankton, and femptoplankton),
phytoplankton, bacteria (e.g., gram positive bacteria, gram
negative bacteria, and extremophiles), yeast and/or mixtures of
these. In some instances, microbial biomass can be obtained from
natural sources, e.g., the ocean, lakes, bodies of water, e.g.,
salt water or fresh water, or on land. Alternatively or in
addition, microbial biomass can be obtained from culture systems,
e.g., large scale dry and wet culture systems.
[0113] Animal biomass includes any organic waste material such as
animal-derived waste material or excrement or human waste material
or excrement (e.g., manure and sewage).
[0114] In some embodiments, the carbohydrate is or includes a
material having one or more .beta.-1,4-linkages and having a number
average molecular weight between about 3,000 and 50,000. Such a
carbohydrate is or includes cellulose (I), which is derived from
(.beta.-glucose 1) through condensation of
(.beta.(1.fwdarw.4)-glycosidic bonds. This linkage contrasts itself
with that for .alpha.(1.fwdarw.4)-glycosidic bonds present in
starch and other carbohydrates.
##STR00001##
Starchy Materials
[0115] Starchy materials include starch itself, e.g., corn starch,
wheat starch, potato starch or rice starch, a derivative of starch,
or a material that includes starch, such as an edible food product
or a crop. For example, the starchy material can be arracacha,
buckwheat, banana, barley, cassava, kudzu, ocra, sago, sorghum,
regular household potatoes, sweet potato, taro, yams, or one or
more beans, such as favas, lentils or peas. A blend of any two or
more starchy materials is also a starchy material. Starch sources
include, e.g., wheat, barley, corn and potatoes. In particular
embodiments, the starchy material is derived from corn. Various
corn starches and derivatives are described in "Corn Starch," Corn
Refiners Association (11.sup.th Edition, 2006), which is included
as Appendix A in U.S. Pat. No. 8,212,087.
[0116] A starch (e.g., CAS#9005-25-8 and chemical formula
(C.sub.6H.sub.10O.sub.5).sub.n) generally comprises a mixture of
amylose and amylopectin (usually in 20:80 or 30:70 ratios) and
generally exists as a homopolymer of repeating anhydroglucose units
joined by an .alpha.-glucosidic on the next starch unit through
hemiacetal linkages. Starch molecules typically are made up of
1,4-linkages are referred to as amylose while 1,6-linkages serve as
the branching point in branched starch molecules called
amylopectin.
Granular Structure
TABLE-US-00001 [0117] TABLE 1 Granule Size of Various Starches
Granule Size Range (.mu.m) Average size Starch Species (Coulter
Counter) (.mu.m) Waxy Rice 2-13 5.5 High Amylose Corn 4-22 9.8 Corn
5-25 14.3 Cassava 3-28 14 Sorghum 3-27 16 Wheat 3-34 6.5, 19.5
Sweet Potato 4-40 18.5 Arrowroot 9-40 23 Sago 15-50 33 Potato 10-70
36 Canna (Aust. Arrowroot) 22-85 53
[0118] Plants store starch within specialized organelles called
amyloplasts where they are deposited to form granules. These
granules are comprised of newly-synthesized starch layered around a
hilum nucleus, and vary in diameter from 2 to 130 microns. The size
and shape of the granule is characteristic of the plant's origin
and serves as a way of identifying the source of a particular
starch (Table 1). The structure of the granule of grain is
crystalline with the starch molecules orienting in such a way as to
form radially oriented crystals giving rise to the phenomenon of
birefringence. When a beam of polarized light is directed through a
starch granule, the granule is divided by dark lines into four
wedge-shaped sections. This cross-hatching or cross is
characteristic of spherocrystalline structures.
Amylose
##STR00002##
[0120] Amylose molecules consist of single mostly-unbranched chains
with 500-20,000 .alpha.-(1,4)-D-glucose units depending on the
source. The .alpha.(1,4) bonds promote the formation of a helix
structure. The structural formula of amylose is pictured in II
where the number of repeated glucose subunits (n) can be many
thousands (usually in the range of 300 to 3000). Amylose starch is
less readily digested than amylopectin; however, it takes up less
space so is preferred for storage in plants. Amylose makes up about
30% of the stored starch in plants. The digestive enzyme amylase
works on the ends of the starch molecule, breaking it down into
sugars.
[0121] Amylose molecules contribute to gel formation because the
linear chains can orient parallel to each other, moving close
enough together to bond. Probably due to the ease with which
amylose molecules slip past each other in the cooked paste, they do
not contribute significantly to viscosity.
Amylopectin
##STR00003##
[0123] Amylopectin is formed by non-random .alpha.-(1,6)-branching
of the amylose-type .alpha.-(1,4)-D-glucose structure. As can be
seen in III, glucose units are linked in a linear way with .alpha.
(1,4) bonds. Branching takes place with .alpha. (1,6) bonds
occurring every 24 to 30 glucose units and is determined by
br\anching enzymes. Each amylopectin molecule contains a million or
so residues, about 5% of which form the branch points.
[0124] The branched amylopectin molecules give viscosity to the
cooked paste due to the role it serves in maintaining the swollen
granule. Their side chains and bulky shape keep amylopectin
molecules from orienting closely enough to hydrogen bond together,
so they do not usually contribute to gel formation.
Source
[0125] Plants hydrolyze starch releasing the glucose subunits when
energy is required. By far the largest source of starch is corn
(maize) with other commonly used sources being wheat, potato,
tapioca and rice. The relative proportions of amylose to
amylopectin and 1,6-linkage branch-points are established
genetically and are relatively constant for each species of starch.
For example, amylomaizes contain over 50% amylase, whereas "waxy"
maize has almost none (.about.3%).
Unprocessed Starch
[0126] Starch that is produced by the corn wet milling process and
then dried is referred to as common, regular, or unmodified corn
starch. Various forms of corn starch exist including, fine or
coarse powders, flakes, pearls or even larger particles. Unmodified
starch can be minimally processed by adjusting the pH, by mild heat
treatment, or by adding small quantities of chemicals or adjuvants
before or after drying in order to optimize performance. As an
example, enzyme conversion of starch to sugars can be accelerated
by adjusting the pH of the starch.
[0127] By far the most consumed polysaccharide in the human diet is
starch. Starch (in particular cornstarch) is used in cooking for
thickening foods such as sauces. In industry, it is used in the
manufacturing of adhesives, paper, textiles, and as a mold in the
manufacture of sweets such as wine gums and jelly beans.
Papermaking is the largest non-food application for starches
globally, consuming millions of metric tons annually. In a typical
sheet of copy paper for example, the starch content may be as high
as 8%. Both chemically modified and unmodified starches are used in
papermaking.
[0128] The chemical composition of starch, highly oxygenated carbon
molecules, makes starch an excellent product for use as a chemical
feedstock.
Genetically Modified Starch
[0129] Genetically modified starch, which refers to starch from
genetically engineered plants, has been modified to reduce the need
for chemical processing (reducing cost, toxicity, or
environmentally hazardous processes), or in order to produce novel
carbohydrates which might not naturally occur in the plant species
being harvested. The modification in this sense refers to the
genetic engineering of the plant DNA, and not the later processing
or treatment of the starch or starch granules.
[0130] Genetically modified starch is of particular interest in the
manufacture of biodegradable polymers and non-cellulose feedstock
in the paper industry, as well as the creation of new food
additives. For example, waxy maize was studied extensively in the
1950's for its desirable properties. Waxy maize starch, which is
essentially 100% amylopectin, yields pastes that are almost clear
when cool, non-congealing, and when dried in thin films, yields a
translucent, water-soluble coating often used for thickening a wide
variety of prepared foods. Genetic modification of this starch to
try and increase the amylose content could potentially result in an
excellent film former and might be spun into a fiber. Research in
this area resulted in the commercial development of two corn
hybrids, one containing about 55%, the other about 70% amylose, and
recently research has resulted in developing a starch with 80%
amylose.
Modified Starch
[0131] Modified starch is a food additive which is prepared by
treating starch or starch granules, causing the starch to be
partially degraded. Modified starch is used as a thickening agent,
stabilizer, or an emulsifier. Apart from food products, modified
starch is also found in pharmaceuticals. Starches are modified for
a number of reasons including, to increase their stability to
excessive heat, acid, and freezing; to change their texture; or to
lengthen or shorten gelatinization time.
Acid-Modified Starch
[0132] Acid-treated starch, usually simply referred to as "modified
starch", is prepared by treating starch or starch granules with
inorganic acids. The primary reaction taking place during acid
treatment is hydrolysis of glucosidic bonds in starch molecules.
Acid modification reduces the chain length of the starch, but does
not substantially change the molecular configuration. In this
method, a starch-water suspension is agitated while being subjected
to mild treatment with dilute mineral acid at temperatures elevated
but below the starch gelatinization temperature. Upon achieving the
desired viscosity, the acid is neutralized with sodium carbonate
and the starch is filtered, washed, and dried.
Oxidized Corn Starch
[0133] Another method for reducing viscosity is oxidation. Although
oxidizing agents such as chlorine, hydrogen peroxide and potassium
permanganate can be used, oxidized starches produced by the wet
milling process are almost always made using sodium hypochlorite as
the oxidizing agent. Aqueous starch suspensions under agitation are
treated with dilute sodium hypochlorite containing a small excess
of sodium hydroxide (NaOH) and heated to 120.degree. F. When the
desired viscosity is achieved, the oxidized starch slurry is
treated with a reducing agent such as sodium bisulfite to remove
excess hypochlorite, the pH is adjusted, and the starch is
filtered, washed and finally dried. Treatment of starch with an
oxidizing agent randomly converts hydroxyl groups to carboxyl or
carbonyl groups, which results in the cleavage of the adjacent
glucosidic bond. Oxidized starches are used in batters and breading
as they adhere quite well to meats.
Dextrins
[0134] Dextrins are a group of low molecular weight carbohydrates
produced by the dry heating or roasting of unmodified starch, with
or without an acid or alkaline catalyst. Other dextrinization
methods utilize a fluid bed, in which unmodified starch is placed
in a reactor and suspended or "fluidized" in a stream of heated
air. The starch is then acidified and heated until the desired end
product is obtained. During dextrinization, the granule is not
destroyed but granule integrity is disrupted. When dextrins are
suspended in water and heated, the granules swell and separate into
layers that eventually break free and disperse. Dextrins are
mixtures of linear .alpha.-(1,4)-linked D-glucose polymers starting
with an .alpha.-(1,6) bond. Industrial production is, in general,
performed by acidic hydrolysis of potato starch. Dextrins are
water-soluble, white to slightly yellow solids that are optically
active. Under analysis, dextrins can be detected with iodine
solution, giving a red coloration.
[0135] There are three major types of dextrins: white, yellow, and
British gums. White dextrins have a white color and have reduced
viscosities, and cold water solubilities ranging from 5 to over
90%. White dextrins are used to make very soft gels. Yellow
dextrins (produced with less acid, higher temperatures, and more
time) are yellow in color and have higher water solubility. Yellow
dextrins are used for making high solids pastes that are very tacky
and, when applied in thin films, dry rapidly. Finally, British gums
are produced by adding little or no acid to very dry starch and
then roasting while gradually increasing the temperature. They are
tan to light brown in color and are used to prepare nearly solid
gels through very soft gels to viscous liquids.
Cyclodextrins
[0136] Cyclodextrins are non-reducing cyclic glucose
oligosaccharides resulting from the cyclomaltodextrin
glucanotransferase catalyzed degradation of starch. There are three
common cyclodextrins with 6, 7 or 8 D-glucopyranonsyl residues
(.alpha.-, .beta.-, and .gamma.-cyclodextrin, respectively) linked
by .alpha.-1,4 glycosidic bonds (FIG. 4). All three cyclodextrins
have similar structures (bond lengths and orientations) apart from
the structural necessities of accommodating a different number of
glucose residues. They present a bottomless bowl-shaped (truncated
cone) molecule stiffened by hydrogen bonding between the 3-OH and
2-OH groups around the outer rim. Cyclodextrins are used for
encapsulation for controlled flavor release, masking odors and
tastes, stabilizing emulsions, increasing foaming power, and
controlling or masking color.
Starch Derivatives (Crosslinked and Stabilization)
[0137] Starch can be chemically derivatized at the primary and
secondary hydroxyl positions, which imparts different properties
than those found in the parent starch. This is presumably due to
disruption of hydrogen bonds. Two types of derivatives are prepared
commercially, crosslinked/inhibited and stabilization. Crosslinked
starches, sometimes referred to as inhibited starches, are made by
reacting hydroxyl groups on two different molecules within a
granule with a bifunctional agent. Reagents such as phosphorus
oxychloride or sodium trimetaphosphate may be used as crosslinking
agents. Very small amounts of these agents can exert a marked
effect on the behavior of the cooked starch.
[0138] Starch can be stabilized against gelling using
monofunctional reagents. These reagents react with hydroxyl groups
on the starch to introduce substituent groups that interfere with
hydrogen bonding effects thereby increasing their water combining
capacity or viscosity, or imparting a positive charge to the starch
molecule. Reagents used in the stabilization of starch through
disruption of hydrogen bonding include, ethylene oxide to produce
hydroxyethyl starch, acetic anhydride to produce starch acetates,
succinic anhydride to produce starch succinates, monosodium
orthophosphate or sodium tripolyphosphate to produce starch
phosphates, and propylene oxide to produce hydroxypropyl starches.
Reagents that impart a positive charge to the starch molecule
include tertiary or quaternary amines to produce cationic
starches.
Pregelatinized Starch
[0139] Suspensions of many starches and starch derivatives can be
gelatinized and dried to yield a broad variety of pregelatinized
starches. This is done on a single drum dryer with applicator
rolls. The starch slurry is heated to gelatinize it,
instantaneously dried and ground to desired granulation
requirement. Pregelatinized starch is used to thicken instant
desserts such as puddings, allowing the food to thicken with the
addition of cold water or milk. Similarly, cheese sauce granules
(such as in Macaroni and Cheese or lasagna) or gravy granules may
be thickened with boiling water without the product going lumpy.
Commercial pizza toppings containing modified starch will thicken
when heated in the oven, keeping them on top of the pizza, and then
become runny when cooled.
Bleached Starches
[0140] Bleaching by very light oxidation is carried out using
sodium hypochlorite, sodium chlorite, hydrogen peroxide, potassium
permanganate, peracetic acid, or ammonium persulfate with sulfur
dioxide. Interaction with the starch molecules must be very small
since no change occurs in the physical properties of the starch or
its solution except in its color. Theoretically, there will be
production of a few aldehyde or carboxyl groups. Only trace amounts
of sodium chloride, sodium sulfate or sodium acetate remain in the
final product. The bleached starch is recovered on continuous
filters or centrifuges using copious amounts of water to remove
trace amounts of inorganic salts formed from the bleaching agent,
dried and packaged.
Low Molecular Weight Sugars
[0141] Biomass materials that include low molecular weight sugars
can, e.g., include at least about 0.5 percent by weight of the low
molecular sugar, e.g., at least about 2, 3, 4, 5, 6, 7, 8, 9, 10,
12.5, 25, 35, 50, 60, 70, 80, 90 or even at least about 95 percent
by weight of the low molecular weight sugar. In some instances, the
biomass is composed substantially of the low molecular weight
sugar, e.g., greater than 95 percent by weight, such as 96, 97, 98,
99 or substantially 100 percent by weight of the low molecular
weight sugar.
[0142] Biomass materials that include low molecular weight sugars
can be agricultural products or food products, such as sugarcane
and sugar beets or an extract therefrom, e.g., juice from
sugarcane, or juice from sugar beets. Biomass materials that
include low molecular weight sugars can be substantially pure
extracts, such as raw or crystallized table sugar (sucrose). Low
molecular weight sugars include sugar derivatives. For example, the
low molecular weight sugars can be oligomeric (e.g., equal to or
greater than a 4-mer, 5-mer, 6-mer, 7-mer, 8-mer, 9-mer or 10-mer),
trimeric, dimeric, or monomeric. When the carbohydrates are formed
of more than a single repeat unit, each repeat unit can be the same
or different.
[0143] Specific examples of low molecular weight sugars include
cellobiose, lactose, sucrose, glucose and xylose, along with
derivatives thereof. In some instances, sugar derivatives are more
rapidly dissolved in solution or utilized by microbes to provide a
useful material, such as ethanol or butanol. Several such sugars
and sugar derivatives are shown below.
##STR00004##
Ethanol from Low Molecular Weight Sugars
[0144] More than half of world ethanol production is produced from
sugar and sugar byproducts, with Brazil being by far the world
leader. Currently, there is no commercial production of ethanol
from sugarcane or sugar beets in the United States, where 97
percent of ethanol is produced from corn.
[0145] Technologically, the process of producing ethanol from sugar
is simpler than converting corn into ethanol. Converting corn into
ethanol requires additional cooking (wet milling process) and the
application of enzymes, whereas the conversion of sugar requires
only a yeast fermentation process. The energy requirement for
converting sugar into ethanol is about half that for corn. However,
the technology and direct energy costs are but one of several
factors that determine the feasibility of ethanol production. Other
factors include relative production costs (including feedstocks),
conversion rates, proximity to processing facilities, alternative
prices and government policies, facility construction and
processing costs. As other countries have shown that it can be
economically feasible to produce ethanol from sugar and other new
feedstocks are researched, interest in the United States in ethanol
production from sugar has increased.
[0146] In response to the growing interest around sugar and
ethanol, USDA released a study in July 2006 titled: "The Economic
Feasibility of Ethanol Production from Sugar in the United States"
which is incorporated herein by reference in its entirety. The
report found that at the current market prices for ethanol,
converting sugarcane, sugar beets and molasses to ethanol would be
profitable (see Table 1).
TABLE-US-00002 TABLE 1 Current Market Prices for Ethanol Feedstock
Total Costs* Processing Costs* Corn (wet milling/dry milling):
$1.03/1.05 $0.63/0.52 Raw Sugarcane $2.40 $0.92 Raw Sugar beets
$2.35 $0.77 Molasses** $1.27 $0.36 Raw Sugar** $3.48 $0.36 Refined
sugar** $3.97 $0.36 *Per gallon **Excludes transportation costs
Sugar Beets
[0147] Sugar beets are an annual crop grown in 11 states across a
variety of climatic conditions, from the hot climate of the
Imperial Valley of California to the colder climates of Montana and
North Dakota. Sugar beet byproducts include beet pulp, which can be
sold for animal feed, and molasses, which is also sold for animal
feed or further processed to extract more sugar.
[0148] Sugar beet processing facilities convert raw sugar beets
directly into refined sugar in a 1-step process. While planted
sugar beet acreage has fallen slightly since the 1990s, sugar
production actually increased due to investments in new processing
equipment, the adoption of new technologies, improved crop
varieties and enhanced technologies for the de-sugaring of
molasses. Sugar beets are very bulky and relatively expensive to
transport and must be processed fairly quickly before the sucrose
deteriorates. Therefore, all sugar beet processing plants are
located in the production areas.
Sugarcane
[0149] Sugarcane is a perennial tropical crop produced in four
states: Florida, Hawaii, Louisiana and Texas. Byproducts of
sugarcane processing include molasses and bagasse, the fibrous
material that remains after sugar is pressed from the sugarcane.
Bagasse is often burned as fuel to help power the sugarcane mills.
Sugarcane is initially processed into raw sugar at mills near the
cane fields. Like beets, cane is bulky and relatively expensive to
transport and must be processed as soon as possible to minimize
sucrose deterioration. The raw sugar is then shipped to refineries
to produce refined sugar.
[0150] Sugar beets have gained a greater share of U.S. sugar
production over the past decade, now accounting for 58.8 percent of
the nation's sugar output while sugarcane fell to 41.2 percent.
Molasses
[0151] The most widely used sugar for ethanol fermentation is
blackstrap molasses which contains about 35-40 wt. % sucrose, 15-20
wt. % invert sugars such as glucose and fructose, and 28-35 wt. %
of non-sugar solids. Blackstrap (syrup) is collected as a
by-product of cane sugar manufacture. The molasses is diluted to a
mash containing ca 10-20 wt. % sugar. After the pH of the mash is
adjusted to about 4-5 with mineral acid, it is inoculated with the
yeast, and the fermentation is carried out non-aseptically at
20-32.degree. C. for about 1-3 days. The fermented beer, which
typically contains approximately 6-10 wt. % ethanol, is then set to
the product recovery in purification section of the plant.
[0152] Ethanol production (using 141 gallons per ton of sucrose
conversion factor) was calculated for sugarcane, sugar beets and
molasses below.
Sugarcane:
[0153] 12.24% raw sugar recovery rate, plus 41.6 pounds of sucrose
from cane molasses
[0153] 1 ton of sugarcane = 235.0 pounds of sucrose from raw sugar
and 41.6 lbs of sucrose from molasses = 276.6 pounds ( 0.1383 tons
) sucrose = 19.5 gallons of ethanol ##EQU00001## [0154] or 0.051
tons of sugarcane per gallon of ethanol produced Sugar beets:
[0155] 15.58% refined sugar recovery rate, plus 40.0 pounds of
sucrose from beet molasses
[0155] 1 ton of sugar beets = 311.6 pounds of sucrose from refined
sugar and 40.0 pounds of sucrose from beet molasses = 351.6 pounds
( 0.1758 tons ) of sucrose = 24.8 gallons of ethanol ##EQU00002##
[0156] or 0.040 tons of sugar beets per gallon of ethanol
produced
Molasses:
[0156] [0157] 49.2% total sugars as sucrose
[0157] 1 ton of molasses = 984 pounds ( 0.492 tons ) of sucrose =
69.4 gallons of ethanol ##EQU00003## [0158] or 28.8 pounds of
molasses per gallon of ethanol produced [0159] or 2.45 gallons of
molasses per gallon of ethanol produced (using a conversion of 1.0
gallon of molasses=11.74 pounds of weight) Raw sugar: [0160] 96.0%
totals sugars as sucrose
[0160] 1 ton of raw sugar = 1920 pounds ( 0.96 tons ) of sucrose =
135.4 gallons of ethanol ##EQU00004## [0161] or 14.77 pounds of raw
sugar per gallon of ethanol produced Refined beet sugar: [0162]
100.0% total sugars as sucrose
[0162] 1 ton of refined sugar = 2000 pounds ( 1.0 ton ) of sucrose
= 141.0 gallons of ethanol ##EQU00005## [0163] or 14.18 pounds of
refined sugar per gallon of ethanol produced
[0164] Results from this study have several important implications
concerning the production of ethanol from sugar crops in the United
States. First, under existing fermentation technology, corn is
currently the cheapest feedstock available for use in the
production of ethanol in the United States. Second, given current
and future projected sugar and ethanol market prices, it appears
that the production of sugar is the most profitable use of
sugarcane or sugar beets. Third, cellulosic conversion of biomass
into ethanol offers the potential for a wide variety of feedstocks
to be used in ethanol production. Systems and processes are
described herein that can utilize these low molecular weight to
produce ethanol more rapidly and more cost effectively.
[0165] Blends of any biomass materials described herein can be
utilized for making any of the products described herein, such as
ethanol. For example, blends of cellulosic materials and starchy
materials can be utilized for making any product described
herein.
Systems for Treating Biomass
[0166] FIG. 1 shows a system 100 for converting biomass,
particularly biomass with significant cellulosic and
lignocellulosic components and/or starchy components, into useful
products and co-products. System 100 includes a feed preparation
subsystem 110, a pretreatment subsystem 114, a primary process
subsystem 118, and a post-processing subsystem 122. Feed
preparation subsystem 110 receives biomass in its raw form,
physically prepares the biomass for use as feedstock by downstream
processes (e.g., reduces the size of and homogenizes the biomass),
and stores the biomass both in its raw and feedstock forms. Biomass
feedstock with significant cellulosic and/or lignocellulosic
components, or starchy components can have a high average molecular
weight and crystallinity that can make processing the feedstock
into useful products (e.g., fermenting the feedstock to produce
ethanol) difficult. For example, others have used acids, bases and
enzymes to process cellulosic, lignocellulosic or starchy
feedstocks. As described herein, in some embodiments, such
treatments are unnecessary, or are necessary only in small or
catalytic amounts.
[0167] Pretreatment subsystem 114 receives feedstock from the feed
preparation subsystem 110 and prepares the feedstock for use in
primary production processes by, for example, reducing the average
molecular weight and crystallinity of the feedstock. Primary
process subsystem 118 receives pretreated feedstock from
pretreatment subsystem 114 and produces useful products (e.g.,
ethanol, other alcohols, pharmaceuticals, and/or food products). In
some cases, the output of primary process subsystem 118 is directly
useful but, in other cases, requires further processing provided by
post-processing subsystem 122. Post-processing subsystem 122
provides further processing to product streams from primary process
system 118 which require it (e.g., distillation and denaturation of
ethanol) as well as treatment for waste streams from the other
subsystems. In some cases, the co-products of subsystems 114, 118,
122 can also be directly or indirectly useful as secondary products
and/or in increasing the overall efficiency of system 100. For
example, post-processing subsystem 122 can produce treated water to
be recycled for use as process water in other subsystems and/or can
produce burnable waste which can be used as fuel for boilers
producing steam and/or electricity.
[0168] The optimum size for biomass conversion plants is affected
by factors including economies of scale and the type and
availability of biomass used as feedstock. Increasing plant size
tends to increase economies of scale associated with plant
processes. However, increasing plant size also tends to increase
the costs (e.g., transportation costs) per unit of feedstock.
Studies analyzing these factors suggest that the appropriate size
for biomass conversion plants can range from 1000 to 10,000 or more
dried tons of feedstock per day depending at least in part on the
type of feedstock used. The type of feedstock can also impact plant
storage requirements with plants designed primarily for processing
feedstock whose availability varies seasonally (e.g., corn stover)
requiring more on- or of-site feedstock storage than plants
designed to process feedstock whose availability is relatively
steady (e.g., waste paper).
Physical Preparation
[0169] In some cases, methods of processing begin with a physical
preparation of the feedstock, e.g., size reduction of raw feedstock
materials, such as by cutting, grinding, shearing, ball milling,
nip-roll processing, or chopping. In some cases, the material can
be reduced into particles using a hammermill, disk-refiner, or
flaker. In some cases, loose feedstock (e.g., recycled paper,
starchy materials, or switchgrass) is prepared by shearing or
shredding. Screens and/or magnets can be used to remove oversized
or undesirable objects such as, for example, rocks or nails from
the feed stream.
[0170] Feed preparation systems can be configured to produce feed
streams with specific characteristics such as, for example,
specific maximum sizes, specific length-to-width, or specific
surface areas ratios. As a part of feed preparation, the bulk
density of feedstocks can be controlled (e.g., increased or
decreased).
Size Reduction
[0171] In some embodiments, the material to be processed is in the
form of a fibrous material that includes fibers provided by
shearing a fiber source. For example, the shearing can be performed
with a rotary knife cutter.
[0172] For example, and by reference to FIG. 2, a fiber source 210
is sheared, e.g., in a rotary knife cutter, to provide a first
fibrous material 212. The first fibrous material 212 is passed
through a first screen 214 having an average opening size of 1.59
mm or less ( 1/16 inch, 0.0625 inch) to provide a second fibrous
material 216. If desired, fiber source can be cut prior to the
shearing, e.g., with a shredder. For example, when a paper is used
as the fiber source, the paper can be first cut into strips that
are, e.g., 1/4- to 1/2-inch wide, using a shredder, e.g., a
counter-rotating screw shredder, such as those manufactured by
Munson (Utica, N.Y.). As an alternative to shredding, the paper can
be reduced in size by cutting to a desired size using a guillotine
cutter. For example, the guillotine cutter can be used to cut the
paper into sheets that are, e.g., 10 inches wide by 12 inches
long.
[0173] In some embodiments, the shearing of the fiber source and
the passing of the resulting first fibrous material through the
first screen are performed concurrently. The shearing and the
passing can also be performed sequentially, e.g., in a batch-type
process.
[0174] For example, a rotary knife cutter can be used to
concurrently shear the fiber source and screen the first fibrous
material. Referring to FIG. 3, a rotary knife cutter 220 includes a
hopper 222 that can be loaded with a shredded fiber source 224
prepared by shredding the fiber source. Shredded fiber source is
sheared between stationary blades 230 and rotating blades 232 to
provide a first fibrous material 240. First fibrous material 240
passes through screen 242, and the resulting second fibrous
material 244 is captured in bin 250. To aid in the collection of
the second fibrous material, the bin can have a pressure below
nominal atmospheric pressure, e.g., at least 10 percent below
nominal atmospheric pressure, e.g., at least 25 percent below
nominal atmospheric pressure, at least 50 percent below nominal
atmospheric pressure, or at least 75 percent below nominal
atmospheric pressure. In some embodiments, a vacuum source 252 is
utilized to maintain the bin below nominal atmospheric
pressure.
[0175] Shearing can be advantageous for "opening up," "stressing,"
or even reducing the molecular weight of the fibrous materials,
making the cellulose of the materials more susceptible to chain
scission and/or reduction of crystallinity. The open materials can
also be more susceptible to oxidation when irradiated.
[0176] The fiber source can be sheared in a dry state, a hydrated
state (e.g., having up to ten percent by weight absorbed water), or
in a wet state, e.g., having between about 10 percent and about 75
percent by weight water. The fiber source can even be sheared while
partially or fully submerged under a liquid, such as water,
ethanol, or isopropanol.
[0177] The fiber source can also be sheared in a gas (such as a
stream or atmosphere of gas other than air), e.g., oxygen or
nitrogen, or steam.
[0178] Other methods of making the fibrous materials include, e.g.,
stone grinding, mechanical ripping or tearing, pin grinding, ball
milling, nip-roll processing, or air attrition milling.
[0179] If desired, the fibrous materials can be separated, e.g.,
continuously or in batches, into fractions according to their
length, width, density, material type, or some combination of these
attributes.
[0180] For example, ferrous materials can be separated from any of
the fibrous materials by passing a fibrous material that includes a
ferrous material past a magnet, e.g., an electromagnet, and then
passing the resulting fibrous material through a series of screens,
each screen having different sized apertures.
[0181] The fibrous materials can also be separated, e.g., by using
a high velocity gas, e.g., air. In such an approach, the fibrous
materials are separated by drawing off different fractions, which
can be characterized photonically, if desired. Such a separation
apparatus is discussed, e.g., in Lindsey et al, U.S. Pat. No.
6,883,667.
[0182] The fibrous materials can have a low moisture content, e.g.,
less than about 7.5, 5, 3, 2.5, 2, 1.5, 1, or 0.5% by weight before
processing. This material can be irradiated with a beam of
particles, such as electrons or protons. The irradiation can be
immediately following preparation of the material, or after a
moisture reduction step, e.g., drying at approximately 105.degree.
C. for 4-18 hours, so that the moisture content is, e.g., less than
about 0.5% before use.
[0183] If desired, lignin can be removed from any of the fibrous
materials that include lignin. Also, to aid in the breakdown of the
materials that include the cellulose, the material can be treated
prior to irradiation with heat, a chemical (e.g., mineral acid,
base or a strong oxidizer such as sodium hypochlorite) and/or an
enzyme.
[0184] In some embodiments, the average opening size of the first
screen is less than 0.79 mm ( 1/32 inch, 0.03125 inch), e.g., less
than 0.51 mm ( 1/50 inch, 0.02000 inch), less than 0.40 mm ( 1/64
inch, 0.015625 inch), less than 0.23 mm (0.009 inch), less than
0.20 mm ( 1/128 inch, 0.0078125 inch), less than 0.18 mm (0.007
inch), less than 0.13 mm (0.005 inch), or even less than less than
0.10 mm ( 1/256 inch, 0.00390625 inch). The screen is prepared by
interweaving monofilaments having an appropriate diameter to give
the desired opening size. For example, the monofilaments can be
made of a metal, e.g., stainless steel. As the opening sizes get
smaller, structural demands on the monofilaments may become
greater. For example, for opening sizes less than 0.40 mm, it can
be advantageous to make the screens from monofilaments made from a
material other than stainless steel, e.g., titanium, titanium
alloys, amorphous metals, nickel, tungsten, rhodium, rhenium,
ceramics, or glass. In some embodiments, the screen is made from a
plate, e.g., a metal plate, having apertures, e.g., cut into the
plate using a laser. In some embodiments, the open area of the mesh
is less than 52%, e.g., less than 41%, less than 36%, less than
31%, less than 30%.
[0185] In some embodiments, the second fibrous material is sheared
and passed through the first screen, or a different sized screen.
In some embodiments, the second fibrous material is passed through
a second screen having an average opening size equal to or less
than that of first screen.
[0186] Referring to FIG. 4, a third fibrous material 220 can be
prepared from the second fibrous material 216 by shearing the
second fibrous material 216 and passing the resulting material
through a second screen 222 having an average opening size less
than the first screen 214.
[0187] Generally, the fibers of the fibrous materials can have a
relatively large average length-to-diameter ratio (e.g., greater
than 20-to-1), even if they have been sheared more than once. In
addition, the fibers of the fibrous materials described herein may
have a relatively narrow length and/or length-to-diameter ratio
distribution.
[0188] As used herein, average fiber widths (i.e., diameters) are
those determined optically by randomly selecting approximately
5,000 fibers. Average fiber lengths are corrected length-weighted
lengths. BET (Brunauer, Emmet and Teller) surface areas are
multi-point surface areas, and porosities are those determined by
mercury porosimetry.
[0189] The average length-to-diameter ratio of the second fibrous
material 14 can be, e.g., greater than 8/1, 10/1, 15/1, 20/1, 25/1,
or even greater than 50/1. An average length of the second fibrous
material 14 can be, e.g., between about 0.5 mm and 2.5 mm, e.g.,
between about 0.75 mm and 1.0 mm, and an average width (i.e.,
diameter) of the second fibrous material 14 can be, e.g., between
about 5 .mu.m and 50 .mu.m, e.g., between about 10 .mu.m and 30
.mu.m.
[0190] In some embodiments, a standard deviation of the length of
the second fibrous material 14 is less than 60 percent of an
average length of the second fibrous material 14, e.g., less than
50 percent of the average length, less than 40 percent of the
average length, less than 25 percent of the average length, less
than 10 percent of the average length, less than 5 percent of the
average length, or even less than 1 percent of the average
length.
[0191] In some embodiments, a BET surface area of the second
fibrous material is greater than 0.1 m.sup.2/g, e.g., greater than
0.25 m.sup.2/g, greater than 0.5 m.sup.2/g, greater than 1.0
m.sup.2/g, greater than 1.5 m.sup.2/g, greater than 1.75 m.sup.2/g,
greater than 5.0 m.sup.2/g, greater than 10 m.sup.2/g, greater than
25 m.sup.2/g, greater than 35 m.sup.2/g, greater than 50 m.sup.2/g,
greater than 60 m.sup.2/g, greater than 75 m.sup.2/g, greater than
100 m.sup.2/g, greater than 150 m.sup.2/g, greater than 200
m.sup.2/g, or even greater than 250 m.sup.2/g. A porosity of the
second fibrous material 14 can be, e.g., greater than 20 percent,
greater than 25 percent, greater than 35 percent, greater than 50
percent, greater than 60 percent, greater than 70 percent, e.g.,
greater than 80 percent, greater than 85 percent, greater than 90
percent, greater than 92 percent, greater than 94 percent, greater
than 95 percent, greater than 97.5 percent, greater than 99
percent, or even greater than 99.5 percent.
[0192] In some embodiments, a ratio of the average
length-to-diameter ratio of the first fibrous material to the
average length-to-diameter ratio of the second fibrous material is,
e.g., less than 1.5, e.g., less than 1.4, less than 1.25, less than
1.1, less than 1.075, less than 1.05, less than 1.025, or even
substantially equal to 1.
[0193] In particular embodiments, the second fibrous material is
sheared again and the resulting fibrous material passed through a
second screen having an average opening size less than the first
screen to provide a third fibrous material. In such instances, a
ratio of the average length-to-diameter ratio of the second fibrous
material to the average length-to-diameter ratio of the third
fibrous material can be, e.g., less than 1.5, e.g., less than 1.4,
less than 1.25, or even less than 1.1.
[0194] In some embodiments, the third fibrous material is passed
through a third screen to produce a fourth fibrous material. The
fourth fibrous material can be, e.g., passed through a fourth
screen to produce a fifth material. Similar screening processes can
be repeated as many times as desired to produce the desired fibrous
material having the desired properties.
Densification
[0195] Densified materials can be processed by any of the methods
described herein, or any material described herein, e.g., any
fibrous material described herein, can be processed by any one or
more methods described herein, and then densified as described
herein.
[0196] A material, e.g., a fibrous material, having a low bulk
density can be densified to a product having a higher bulk density.
For example, a material composition having a bulk density of 0.05
g/cm.sup.3 can be densified by sealing the fibrous material in a
relatively gas impermeable structure, e.g., a bag made of
polyethylene or a bag made of alternating layers of polyethylene
and a nylon, and then evacuating the entrapped gas, e.g., air, from
the structure. After evacuation of the air from the structure, the
fibrous material can have, e.g., a bulk density of greater than 0.3
g/cm.sup.3, e.g., 0.5 g/cm.sup.3, 0.6 g/cm.sup.3, 0.7 g/cm.sup.3 or
more, e.g., 0.85 g/cm.sup.3. After densification, the product can
processed by any of the methods described herein, e.g., irradiated,
e.g., with gamma radiation. This can be advantageous when it is
desirable to transport the material to another location, e.g., a
remote manufacturing plant, where the fibrous material composition
can be added to a solution, e.g., to produce ethanol. After
piercing the substantially gas impermeable structure, the densified
fibrous material can revert to nearly its initial bulk density,
e.g., greater than 60 percent of its initial bulk density, e.g., 70
percent, 80 percent, 85 percent or more, e.g., 95 percent of its
initial bulk density. To reduce static electricity in the fibrous
material, an anti-static agent can be added to the material.
[0197] In some embodiments, the structure, e.g., bag, is formed of
a material that dissolves in a liquid, such as water. For example,
the structure can be formed from a polyvinyl alcohol so that it
dissolves when in contact with a water-based system. Such
embodiments allow densified structures to be added directly to
solutions that include a microorganism, without first releasing the
contents of the structure, e.g., by cutting.
[0198] Referring to FIG. 5, a biomass material can be combined with
any desired additives and a binder, and subsequently densified by
application of pressure, e.g., by passing the material through a
nip defined between counter-rotating pressure rolls or by passing
the material through a pellet mill. During the application of
pressure, heat can optionally be applied to aid in the
densification of the fibrous material. The densified material can
then be irradiated.
[0199] In some embodiments, the material prior to densification has
a bulk density of less than 0.25 g/cm.sup.3, e.g., 0.20 g/cm.sup.3,
0.15 g/cm.sup.3, 0.10 g/cm.sup.3, 0.05 g/cm.sup.3 or less, e.g.,
0.025 g/cm.sup.3. Bulk density is determined using ASTM D1895B.
Briefly, the method involves filling a measuring cylinder of known
volume with a sample and obtaining a weight of the sample. The bulk
density is calculated by dividing the weight of the sample in grams
by the known volume of the cylinder in cubic centimeters.
[0200] The preferred binders include binders that are soluble in
water, swollen by water, or that has a glass transition temperature
of less 25.degree. C., as determined by differential scanning
calorimetry. By water-soluble binders, we mean binders having a
solubility of at least about 0.05 weight percent in water. By water
swellable binders, we mean binders that increase in volume by more
than 0.5 percent upon exposure to water.
[0201] In some embodiments, the binders that are soluble or swollen
by water include a functional group that is capable of forming a
bond, e.g., a hydrogen bond, with the fibers of the fibrous
material, e.g., cellulosic fibrous material. For example, the
functional group can be a carboxylic acid group, a carboxylate
group, a carbonyl group, e.g., of an aldehyde or a ketone, a
sulfonic acid group, a sulfonate group, a phosphoric acid group, a
phosphate group, an amide group, an amine group, a hydroxyl group,
e.g., of an alcohol, and combinations of these groups, e.g., a
carboxylic acid group and a hydroxyl group. Specific monomeric
examples include glycerin, glyoxal, ascorbic acid, urea, glycine,
pentaerythritol, a monosaccharide or a disaccharide, citric acid,
and tartaric acid. Suitable saccharides include glucose, sucrose,
lactose, ribose, fructose, mannose, arabinose and erythrose.
Polymeric examples include polyglycols, polyethylene oxide,
polycarboxylic acids, polyamides, polyamines and polysulfonic acids
polysulfonates. Specific polymeric examples include polypropylene
glycol (PPG), polyethylene glycol (PEG), polyethylene oxide, e.g.,
POLYOX.RTM., copolymers of ethylene oxide and propylene oxide,
polyacrylic acid (PAA), polyacrylamide, polypeptides,
polyethylenimine, polyvinylpyridine,
poly(sodium-4-styrenesulfonate) and
poly(2-acrylamido-methyl-1-propanesulfonic acid).
[0202] In some embodiments, the binder includes a polymer that has
a glass transition temperature less than 25.degree. C. Examples of
such polymers include thermoplastic elastomers (TPEs). Examples of
TPEs include polyether block amides, such as those available under
the tradename PEBAX.RTM., polyester elastomers, such as those
available under the tradename HYTREL.RTM., and styrenic block
copolymers, such as those available under the tradename
KRATON.RTM.. Other suitable polymers having a glass transition
temperature less than 25.degree. C. include ethylene vinyl acetate
copolymer (EVA), polyolefins, e.g., polyethylene, polypropylene,
ethylene-propylene copolymers, and copolymers of ethylene and alpha
olefins, e.g., 1-octene, such as those available under the
tradename ENGAGE.RTM.. In some embodiments, e.g., when the material
is a fiberized polycoated paper, the material is densified without
the addition of a separate low glass transition temperature
polymer.
[0203] In a particular embodiment, the binder is a lignin, e.g., a
natural or synthetically modified lignin.
[0204] A suitable amount of binder added to the material,
calculated on a dry weight basis, is, e.g., from about 0.01 percent
to about 50 percent, e.g., 0.03 percent, 0.05 percent, 0.1 percent,
0.25 percent, 0.5 percent, 1.0 percent, 5 percent, 10 percent or
more, e.g., 25 percent, based on a total weight of the densified
material. The binder can be added to the material as a neat, pure
liquid, as a liquid having the binder dissolved therein, as a dry
powder of the binder, or as pellets of the binder.
[0205] The densified fibrous material can be made in a pellet mill.
Referring to FIG. 6, a pellet mill 300 has a hopper 301 for holding
undensified material 310 that includes carbohydrate-containing
materials, such as cellulose. The hopper communicates with an auger
312 that is driven by variable speed motor 314 so that undensified
material can be transported to a conditioner 320 that stirs the
undensified material with paddles 322 that are rotated by
conditioner motor 330. Other ingredients, e.g., any of the
additives and/or fillers described herein, can be added at inlet
332. If desired, heat may be added while the fibrous material is in
the conditioner. After being conditioned, the material passes from
the conditioner through a dump chute 340, and to another auger 342.
The dump chute, as controlled by actuator 344, allows for
unobstructed passage of the material from conditioner to auger.
Auger is rotated by motor 346, and controls the feeding of the
fibrous material into die and roller assembly 350. Specifically,
the material is introduced into a hollow, cylindrical die 352,
which rotates about a horizontal axis and which has radially
extending die holes 250. Die 352 is rotated about the axis by motor
360, which includes a horsepower gauge, indicating total power
consumed by the motor. Densified material 370, e.g., in the form of
pellets, drops from chute 372 and are captured and processed, such
as by irradiation.
[0206] The material, after densification, can be conveniently in
the form of pellets or chips having a variety of shapes. The
pellets can then be irradiated. In some embodiments, the pellets or
chips are cylindrical in shape, e.g., having a maximum transverse
dimension of, e.g., 1 mm or more, e.g., 2 mm, 3 mm, 5 mm, 8 mm, 10
mm, 15 mm or more, e.g., 25 mm. Other convenient shapes include
pellets or chips that are plate-like in form, e.g., having a
thickness of 1 mm or more, e.g., 2 mm, 3 mm, 5 mm, 8 mm, 10 mm or
more, e.g., 25 mm; a width of, e.g., 5 mm or more, e.g., 10 mm, 15
mm, 25 mm, 30 mm or more, e.g., 50 mm; and a length of 5 mm or
more, e.g., 10 mm, 15 mm, 25 mm, 30 mm or more, e.g., 50 mm.
[0207] Referring now FIG. 7A-7D, pellets can be made so that they
have a hollow inside. As shown, the hollow can be generally in-line
with the center of the pellet (FIG. 7B), or out of line with the
center of the pellet (FIG. 7C). Making the pellet hollow inside can
increase the rate of dissolution in a liquid after irradiation.
[0208] Referring now to FIG. 7D, the pellet can have, e.g., a
transverse shape that is multi-lobal, e.g., tri-lobal as shown, or
tetra-lobal, penta-lobal, hexa-lobal or deca-lobal. Making the
pellets in such transverse shapes can also increase the rate of
dissolution in a solution after irradiation.
[0209] Alternatively, the densified material can be in any other
desired form, e.g., the densified material can be in the form of a
mat, roll or bale.
EXAMPLES
[0210] In one example, half-gallon juice cartons made of un-printed
white Kraft board having a bulk density of 20 lb/ft.sup.3 can be
used as a feedstock. Cartons can be folded flat and then fed into a
shredder to produce a confetti-like material having a width of
between 0.1 inch and 0.5 inch, a length of between 0.25 inch and 1
inch and a thickness equivalent to that of the starting material
(about 0.075 inch). The confetti-like material can be fed to a
rotary knife cutter, which shears the confetti-like pieces, tearing
the pieces apart and releasing fibrous material.
[0211] In some cases, multiple shredder-shearer trains can be
arranged in series with output. In one embodiment, two
shredder-shearer trains can be arranged in series with output from
the first shearer fed as input to the second shredder. In another
embodiment, three shredder-shearer trains can be arranged in series
with output from the first shearer fed as input to the second
shredder and output from the second shearer fed as input to the
third shredder. Multiple passes through shredder-shearer trains are
anticipated to decrease particle size and increase overall surface
area within the feedstream.
[0212] In another example, fibrous material produced from shredding
and shearing juice cartons can be treated to increase its bulk
density. In some cases, the fibrous material can be sprayed with
water or a dilute stock solution of POLYOX.TM. WSR N10
(polyethylene oxide) prepared in water. The wetted fibrous material
can then be processed through a pellet mill operating at room
temperature. The pellet mill can increase the bulk density of the
feedstream by more than an order of magnitude.
Pretreatment
[0213] Physically prepared feedstock can be pretreated for use in
primary production processes by, for example, reducing the average
molecular weight and crystallinity of the feedstock and/or
increasing the surface area and/or porosity of the feedstock.
[0214] In some embodiments, the cellulosic and/or lignocellulosic
material includes a first cellulose having a first number average
molecular weight and the resulting carbohydrate includes a second
cellulose having a second number average molecular weight lower
than the first number average molecular weight. For example, the
second number average molecular weight is lower than the first
number average molecular weight by more than about twenty-five
percent, e.g., 2.times., 3.times., 5.times., 7.times., 10.times.,
25.times., even 100.times. reduction.
[0215] In some embodiments, the first cellulose has a first
crystallinity and the second cellulose has a second crystallinity
lower than the first crystallinity, such as lower than about two,
three, five, ten, fifteen or twenty-five percent lower.
[0216] In some embodiments, the first cellulose has a first level
of oxidation and the second cellulose has a second level of
oxidation higher than the first level of oxidation, such as two,
three, four, five, ten or even twenty-five percent higher.
[0217] Pretreatment processes can include one or more of
irradiation, sonication, oxidation, pyrolysis, and steam explosion.
The various pretreatment systems and methods can be used in
combinations of two, three, or even four of these technologies.
Pretreatment Combinations
[0218] In some embodiments, biomass can be processed by applying
two or more of any of the processes described herein, such as two,
three, four or more of radiation, sonication (or any other
disruption technique described herein, e.g., treatment with a
rotor-stator disruptor), oxidation, pyrolysis, and steam explosion
either with or without prior, intermediate, or subsequent feedstock
preparation as described herein. The processes can be applied to
the biomass in any order or concurrently. For example, a
carbohydrate can be prepared by applying radiation, sonication,
oxidation, pyrolysis, and, optionally, steam explosion to a
cellulosic and/or lignocellulosic material (in any order or
concurrently). The provided carbohydrate-containing material can
then be converted by one or more microorganisms, such as bacteria,
yeast, or mixtures of yeast and bacteria, to a number of desirable
products, as described herein. Multiple processes can provide
materials that can be more readily utilized by a variety of
microorganisms because of their lower molecular weight, lower
crystallinity, and/or enhanced solubility. Multiple processes can
provide synergies and can reduce overall energy input required in
comparison to any single process.
[0219] For example, in some embodiments, feedstocks are provided
that include a carbohydrate that is produced by a process that
includes irradiating and sonicating, irradiating and oxidizing,
irradiating and pyrolyzing, or irradiating and steam-exploding (in
either order or concurrently) a cellulosic and/or a lignocellulosic
material. The provided feedstock can then be contacted with a
microorganism having the ability to convert at least a portion,
e.g., at least about 1 percent by weight, of the feedstock to the
product, such as the combustible fuel.
Pretreatment Conditions
[0220] In some embodiments, the process does not include
hydrolyzing the cellulosic and/or lignocellulosic material, such as
with an acid, e.g., a mineral acid, such as hydrochloric or
sulfuric acid, an enzyme or a base. If desired, some or none of the
feedstock can include a hydrolyzed material. For example, in some
embodiments, at least about seventy percent by weight of the
feedstock is an unhydrolyzed material, e.g., at least at 95 percent
by weight of the feedstock is an unhydrolyzed material. In some
embodiments, substantially all of the feedstock is an unhydrolyzed
material. For example, treatment with alkali can be avoided.
[0221] Any feedstock or any reactor or fermentor charged with a
feedstock can include a buffer, such as sodium bicarbonate,
ammonium chloride or Tris; an electrolyte, such as potassium
chloride, sodium chloride, or calcium chloride; a growth factor,
such as biotin and/or a base pair such as uracil or an equivalent
thereof; a surfactant, such as Tween.RTM. or polyethylene glycol; a
mineral, such as such as calcium, chromium, copper, iodine, iron,
selenium, or zinc; or a chelating agent, such as ethylene diamine,
ethylene diamine tetraacetic acid (EDTA) (or its salt form, e.g.,
sodium or potassium EDTA), or dimercaprol.
[0222] When radiation is utilized, it can be applied to any sample
that is dry or wet, or even dispersed in a liquid, such as water.
For example, irradiation can be performed on cellulosic and/or
lignocellulosic material in which less than about 25 percent by
weight of the cellulosic and/or lignocellulosic material has
surfaces wetted with a liquid, such as water. In some embodiments,
irradiating is performed on cellulosic and/or lignocellulosic
material in which substantially none of the cellulosic and/or
lignocellulosic material is wetted with a liquid, such as
water.
[0223] In some embodiments, any processing described herein occurs
with the cellulosic and/or lignocellulosic material remaining dry
as acquired or after the material has been dried, e.g., using heat
and/or reduced pressure. For example, in some embodiments, the
cellulosic and/or lignocellulosic material has less than about five
percent by weight retained water, measured at 25.degree. C. and at
fifty percent relative humidity.
[0224] The feedstock can be treated so that it has a low moisture
content, e.g., less than about 7.5, 5, 3, 2.5, 2, 1.5, 1, or 0.5%
by weight. This material can be irradiated with a beam of
particles, such as electrons or protons. The irradiation can be
immediately following preparation of the material or after a
moisture reduction step, e.g., drying at approximately 105.degree.
C. for 4-18 hours.
[0225] If desired, a swelling agent, as defined herein, can be
utilized in any process described herein. In some embodiments, when
a cellulosic and/or lignocellulosic material is processed using
radiation, less than about 25 percent by weight of the cellulosic
and/or lignocellulosic material is in a swollen state, the swollen
state being characterized as having a volume of more than about 2.5
percent higher than an unswollen state, e.g., more than 5.0, 7.5,
10, or 15 percent higher than the unswollen state. In specific
embodiments when radiation is utilized, the cellulosic and/or
lignocellulosic material includes a swelling agent, and swollen
cellulosic and/or lignocellulosic receives a dose of less than
about 10 Mrad. In other embodiments, when radiation is utilized on
a cellulosic and/or lignocellulosic material, substantially none of
the cellulosic and/or lignocellulosic material is in a swollen
state.
[0226] In some embodiments, no chemicals, e.g., no swelling agents,
are added to the biomass prior to irradiation. For example, in some
of these embodiments no alkaline substances (such as sodium
hydroxide, potassium hydroxide, lithium hydroxide and ammonium
hydroxides), acidifying agents (such as mineral acids (e.g.,
sulfuric acid, hydrochloric acid and phosphoric acid)), salts, such
as zinc chloride, calcium carbonate, sodium carbonate,
benzyltrimethylammonium sulfate, or basic organic amines, such as
ethylene diamine, are added prior to irradiation or other
processing. In some cases, no additional water is added. For
example, the biomass prior to processing can have less than 0.5
percent by weight added chemicals, e.g., less than 0.4, 0.25, 0.15
or 0.1 percent by weight added chemicals. In some instances, the
biomass has no more than a trace, e.g., less than 0.05 percent by
weight added chemicals, prior to irradiation. In other instances,
the biomass prior to irradiation has substantially no added
chemicals or swelling agents. Avoiding the use of such chemicals
can also be extended throughout processing, e.g., at all times
prior to fermentation, or at all times.
[0227] When radiation is utilized in any process, it can be applied
while the cellulosic and/or lignocellulosic is exposed to air,
oxygen-enriched air, or even oxygen itself, or blanketed by an
inert gas such as nitrogen, argon, or helium. When maximum
oxidation is desired, an oxidizing environment is utilized, such as
air or oxygen. The distance from the radiation source can also be
optimized to maximize reactive gas formation, e.g., ozone and/or
oxides of nitrogen.
[0228] When radiation is utilized, it may be applied to biomass,
such as cellulosic and/or lignocellulosic material, under a
pressure of greater than about 2.5 atmospheres, such as greater
than 5, 10, 15, 20 or even greater than about 50 atmospheres.
[0229] When the process includes radiation, the irradiating can be
performed utilizing an ionizing radiation, such as gamma rays,
x-rays, energetic ultraviolet radiation, such as ultraviolet C
radiation having a wavelength of from about 100 nm to about 280 nm,
a beam of particles, such as a beam of electrons, slow neutrons or
alpha particles. In some embodiments, irradiating includes two or
more radiation sources, such as gamma rays and a beam of electrons,
which can be applied in either order or concurrently.
[0230] Any processing technique described herein can be used at a
pressure above or below normal, earth-bound atmospheric pressure.
For example, any process that utilizes radiation, sonication,
oxidation, pyrolysis, steam explosion, or combinations of any of
these processes to provide materials that include a carbohydrate
can be performed under high pressure, which can increase reaction
rates. For example, any process or combination of processes can be
performed at a pressure greater than about normal atmospheric
pressure, e.g., at a pressure of greater than about 25 MPa, e.g.,
greater than 50 MPa, 75 MPa, 100 MPa, 150 MPa, 200 MPa, 250 MPa,
350 MPa, 500 MPa, 750 MPa, 1,000 MPa, or greater than 1,500
MPa.
Radiation Treatment
[0231] One or more irradiation processing sequences can be used to
process raw feedstock from a wide variety of different sources to
extract useful substances from the feedstock, and to provide
partially degraded organic material which functions as input to
further processing steps and/or sequences. Irradiation can reduce
the molecular weight and/or crystallinity of feedstock. In some
embodiments, energy deposited in a material that releases an
electron from its atomic orbital is used to irradiate the
materials. The radiation may be provided by 1) heavy charged
particles, such as alpha particles or protons, 2) electrons,
produced, for example, in beta decay or electron beam accelerators,
or 3) electromagnetic radiation, for example, gamma rays, x rays,
or ultraviolet rays. In one approach, radiation produced by
radioactive substances can be used to irradiate the feedstock. In
some embodiments, any combination in any order or concurrently of
(1) through (3) may be utilized. In another approach,
electromagnetic radiation (e.g., produced using electron beam
emitters) can be used to irradiate the feedstock. The doses applied
depend on the desired effect and the particular feedstock. For
example, high doses of radiation can break chemical bonds within
feedstock components and low doses of radiation can increase
chemical bonding (e.g., cross-linking) within feedstock components.
In some instances when chain scission is desirable and/or polymer
chain functionalization is desirable, particles heavier than
electrons, such as protons, helium nuclei, argon ions, silicon
ions, neon ions carbon ions, phoshorus ions, oxygen ions or
nitrogen ions can be utilized. When ring-opening chain scission is
desired, positively charged particles can be utilized for their
Lewis acid properties for enhanced ring-opening chain scission. For
example, when oxygen-containing functional groups are desired,
irradiation in the presence of oxygen or even irradiation with
oxygen ions can be performed. For example, when nitrogen-containing
functional groups are desirable, irradiation in the presence of
nitrogen or even irradiation with nitrogen ions can be
performed.
[0232] Referring to FIG. 8, in one method, a first material 2 that
is or includes cellulose having a first number average molecular
weight (.sup.TM.sub.N1) is irradiated, e.g., by treatment with
ionizing radiation (e.g., in the form of gamma radiation, X-ray
radiation, 100 nm to 280 nm ultraviolet (UV) light, a beam of
electrons or other charged particles) to provide a second material
3 that includes cellulose having a second number average molecular
weight (.sup.TM.sub.N2) lower than the first number average
molecular weight. The second material (or the first and second
material) can be combined with a microorganism (e.g., a bacterium
or a yeast) that can utilize the second and/or first material to
produce a product, e.g., a fuel 5 that is or includes hydrogen, an
alcohol (e.g., ethanol or butanol, such as n-, sec- or t-butanol),
an organic acid, a hydrocarbon or mixtures of any of these.
[0233] Since the second material 3 has cellulose having a reduced
molecular weight relative to the first material, and in some
instances, a reduced crystallinity as well, the second material is
generally more dispersible, swellable and/or soluble in a solution
containing a microorganism. These properties make the second
material 3 more susceptible to chemical, enzymatic and/or
biological attack relative to the first material 2, which can
greatly improve the production rate and/or production level of a
desired product, e.g., ethanol. Radiation can also sterilize the
materials.
[0234] In some embodiments, the second number average molecular
weight (M.sub.n2) is lower than the first number average molecular
weight (.sup.TM.sub.n1) by more than about 10 percent, e.g., 15,
20, 25, 30, 35, 40, 50 percent, 60 percent, or even more than about
75 percent.
[0235] In some instances, the second material has cellulose that
has as crystallinity (.sup.TC.sub.2) that is lower than the
crystallinity (.sup.TC.sub.1) of the cellulose of the first
material. For example, (.sup.TC.sub.2) can be lower than
(.sup.TC.sub.1) by more than about 10 percent, e.g., 15, 20, 25,
30, 35, 40, or even more than about 50 percent.
[0236] In some embodiments, the starting crystallinity index (prior
to irradiation) is from about 40 to about 87.5 percent, e.g., from
about 50 to about 75 percent or from about 60 to about 70 percent,
and the crystallinity index after irradiation is from about 10 to
about 50 percent, e.g., from about 15 to about 45 percent or from
about 20 to about 40 percent. However, in some embodiments, e.g.,
after extensive irradiation, it is possible to have a crystallinity
index of lower than 5 percent. In some embodiments, the material
after irradiation is substantially amorphous.
[0237] In some embodiments, the starting number average molecular
weight (prior to irradiation) is from about 200,000 to about
3,200,000, e.g., from about 250,000 to about 1,000,000 or from
about 250,000 to about 700,000, and the number average molecular
weight after irradiation is from about 50,000 to about 200,000,
e.g., from about 60,000 to about 150,000 or from about 70,000 to
about 125,000. However, in some embodiments, e.g., after extensive
irradiation, it is possible to have a number average molecular
weight of less than about 10,000 or even less than about 5,000.
[0238] In some embodiments, the second material can have a level of
oxidation (.sup.TO.sub.2) that is higher than the level of
oxidation (.sup.TO.sub.1) of the first material. A higher level of
oxidation of the material can aid in its dispersibility,
swellability and/or solubility, further enhancing the materials
susceptibility to chemical, enzymatic or biological attack. In some
embodiments, to increase the level of the oxidation of the second
material relative to the first material, the irradiation is
performed under an oxidizing environment, e.g., under a blanket of
air or oxygen, producing a second material that is more oxidized
than the first material. For example, the second material can have
more hydroxyl groups, aldehyde groups, ketone groups, ester groups
or carboxylic acid groups, which can increase its
hydrophilicity.
Ionizing Radiation
[0239] Each form of radiation ionizes the biomass via particular
interactions, as determined by the energy of the radiation. Heavy
charged particles primarily ionize matter via Coulomb scattering;
furthermore, these interactions produce energetic electrons that
may further ionize matter. Alpha particles are identical to the
nucleus of a helium atom and are produced by the alpha decay of
various radioactive nuclei, such as isotopes of bismuth, polonium,
astatine, radon, francium, radium, several actinides, such as
actinium, thorium, uranium, neptunium, curium, californium,
americium, and plutonium.
[0240] When particles are utilized, they can be neutral
(uncharged), positively charged or negatively charged. When
charged, the charged particles can bear a single positive or
negative charge, or multiple charges, e.g., one, two, three or even
four or more charges. In instances in which chain scission is
desired, positively charged particles may be desirable, in part,
due to their acidic nature. When particles are utilized, the
particles can have the mass of a resting electron, or greater,
e.g., 500, 1000, 1500, or 2000 or more times the mass of a resting
electron. For example, the particles can have a mass of from about
1 atomic unit to about 150 atomic units, e.g., from about 1 atomic
unit to about 50 atomic units, or from about 1 to about 25, e.g.,
1, 2, 3, 4, 5, 10, 12 or 15 amu. Accelerators used to accelerate
the particles can be electrostatic DC, electrodynamic DC, RF
linear, magnetic induction linear or continuous wave. For example,
cyclotron type accelerators are available from IBA, Belgium, such
as the Rhodotron.RTM. system, while DC type accelerators are
available from RDI, now IBA Industrial, such as the
Dynamitron.RTM.. Ions and ion accelerators are discussed in
Introductory Nuclear Physics, Kenneth S. Krane, John Wiley &
Sons, Inc. (1988), Krsto Prelec, FIZIKA B 6 (1997) 4, 177-206, a
copy of which is included as Appendix B of U.S. Pat. No. 8,212,087;
Chu, William T., "Overview of Light-Ion Beam Therapy",
Columbus-Ohio, ICRU-IAEA Meeting, 18-20 March 2006, a copy of which
is included as Appendix C of U.S. Pat. No. 8,212,087; Iwata, Y. et
al., "Alternating-Phase-Focused IH-DTL for Heavy-Ion Medical
Accelerators", Proceedings of EPAC 2006, Edinburgh, Scotland, a
copy of which is included as Appendix D of U.S. Pat. No. 8,212,087,
and Leitner, C. M. et al., "Status of the Superconducting ECR Ion
Source Venus", Proceedings of EPAC 2000, Vienna, Austria, a copy of
which is included as Appendix E of U.S. Pat. No. 8,212,087.
[0241] Electrons interact via Coulomb scattering and bremsstrahlung
radiation produced by changes in the velocity of electrons.
Electrons may be produced by radioactive nuclei that undergo beta
decay, such as isotopes of iodine, cesium, technetium, and iridium.
Alternatively, an electron gun can be used as an electron source
via thermionic emission.
[0242] Electromagnetic radiation interacts via three processes:
photoelectric absorption, Compton scattering, and pair production.
The dominating interaction is determined by the energy of the
incident radiation and the atomic number of the material. The
summation of interactions contributing to the absorbed radiation in
cellulosic material can be expressed by the mass absorption
coefficient.
[0243] Electromagnetic radiation is subclassified as gamma rays, x
rays, ultraviolet rays, infrared rays, microwaves, or radiowaves,
depending on its wavelength.
[0244] For example, gamma radiation can be employed to irradiate
the materials. Referring to FIGS. 9 and 10 (an enlarged view of
region R), a gamma irradiator 10 includes gamma radiation sources
408, e.g., .sup.60Co pellets, a working table 14 for holding the
materials to be irradiated and storage 16, e.g., made of a
plurality iron plates, all of which are housed in a concrete
containment chamber (vault) 20 that includes a maze entranceway 22
beyond a lead-lined door 26. Storage 16 includes a plurality of
channels 30, e.g., sixteen or more channels, allowing the gamma
radiation sources to pass through storage on their way proximate
the working table.
[0245] In operation, the sample to be irradiated is placed on a
working table. The irradiator is configured to deliver the desired
dose rate and monitoring equipment is connected to an experimental
block 31. The operator then leaves the containment chamber, passing
through the maze entranceway and through the lead-lined door. The
operator mans a control panel 32, instructing a computer 33 to lift
the radiation sources 12 into working position using cylinder 36
attached to a hydraulic pump 40.
[0246] Gamma radiation has the advantage of a significant
penetration depth into a variety of material in the sample. Sources
of gamma rays include radioactive nuclei, such as isotopes of
cobalt, calcium, technicium, chromium, gallium, indium, iodine,
iron, krypton, samarium, selenium, sodium, thalium, and xenon.
[0247] Sources of x rays include electron beam collision with metal
targets, such as tungsten or molybdenum or alloys, or compact light
sources, such as those produced commercially by Lyncean.
[0248] Sources for ultraviolet radiation include deuterium or
cadmium lamps.
[0249] Sources for infrared radiation include sapphire, zinc, or
selenide window ceramic lamps.
[0250] Sources for microwaves include klystrons, Slevin type RF
sources, or atom beam sources that employ hydrogen, oxygen, or
nitrogen gases.
[0251] Various other irradiating devices may be used in the methods
disclosed herein, including field ionization sources, electrostatic
ion separators, field ionization generators, thermionic emission
sources, microwave discharge ion sources, recirculating or static
accelerators, dynamic linear accelerators, van de Graaff
accelerators, and folded tandem accelerators. Such devices are
disclosed, for example, in U.S. Provisional Application Ser. No.
61/073,665, the complete disclosure of which is incorporated herein
by reference.
Electron Beam
[0252] In some embodiments, a beam of electrons is used as the
radiation source. A beam of electrons has the advantages of high
dose rates (e.g., 1, 5, or even 10 Mrad per second), high
throughput, less containment, and less confinement equipment.
Electron beams can also have up to 80 percent electrical
efficiency, allowing for a low energy usage, which can translate
into a low cost of operation and low greenhouse gas emissions
corresponding to the small amount of energy used. Electrons can
also be more efficient at causing chain scission. In addition,
electrons having energies of 4-10 MeV can have a penetration depth
of 5 to 30 mm or more, such as 40 mm. In low bulk density
materials, such as many of the materials described herein, e.g.,
materials having a bulk density of less than about 0.5 g/cm.sup.3,
electrons having energies in the 4-10 MeV range can penetrate 4-8
inches or even more.
[0253] Electron beams can be generated, e.g., by electrostatic
generators, cascade generators, transformer generators, low energy
accelerators with a scanning system, low energy accelerators with a
linear cathode, linear accelerators, and pulsed accelerators.
Electrons as an ionizing radiation source can be useful, e.g., for
relatively thin piles of materials, e.g., less than 0.5 inch, e.g.,
less than 0.4 inch, 0.3 inch, 0.2 inch, or less than 0.1 inch. In
some embodiments, the energy of each electron of the electron beam
is from about 0.3 MeV to about 2.0 MeV (million electron volts),
e.g., from about 0.5 MeV to about 1.5 MeV, or from about 0.7 MeV to
about 1.25 MeV.
[0254] FIG. 11 shows a process flow diagram 3000 that includes
various steps in an electron beam irradiation feedstock
pretreatment sequence. In first step 3010, a supply of dry
feedstock is received from a feed source. As discussed above, the
dry feedstock from the feed source may be pre-processed prior to
delivery to the electron beam irradiation devices. For example, if
the feedstock is derived from plant sources, certain portions of
the plant material may be removed prior to collection of the plant
material and/or before the plant material is delivered by the
feedstock transport device. Alternatively, or in addition, as
expressed in optional step 3020, the biomass feedstock can be
subjected to mechanical processing (e.g., to reduce the average
length of fibers in the feedstock) prior to delivery to the
electron beam irradiation devices.
[0255] In step 3030, the dry feedstock is transferred to a
feedstock transport device (e.g., a conveyor belt) and is
distributed over the cross-sectional width of the feedstock
transport device approximately uniformly by volume. This can be
accomplished, for example, manually or by inducing a localized
vibration motion at some point in the feedstock transport device
prior to the electron beam irradiation processing.
[0256] In some embodiments, a mixing system introduces a chemical
agent 3045 into the feedstock in an optional process 3040 that
produces a slurry. Combining water with the processed feedstock in
mixing step 3040 creates an aqueous feedstock slurry that may be
transported through, for example, piping rather than using, for
example, a conveyor belt.
[0257] The next step 3050 is a loop that encompasses exposing the
feedstock (in dry or slurry form) to electron beam radiation via
one or more (say, N) electron beam irradiation devices. The
feedstock slurry is moved through each of the N "showers" of
electron beams at step 3052. The movement may either be at a
continuous speed through and between the showers, or there may be a
pause through each shower, followed by a sudden movement to the
next shower. A small slice of the feedstock slurry is exposed to
each shower for some predetermined exposure time at step 3053.
[0258] Electron beam irradiation devices may be procured
commercially from Ion Beam Applications, Louvain-la-Neuve, Belgium
or the Titan Corporation, San Diego, Calif. Typical electron
energies can be 1 MeV, 2 MeV, 4.5 MeV, 7.5 MeV, or 10 MeV. Typical
electron beam irradiation device power can be 1 kW, 5 kW, 10 kW, 20
kW, 50 kW, 100 kW, 250 kW, or 500 kW. Effectiveness of
depolymerization of the feedstock slurry depends on the electron
energy used and the dose applied, while exposure time depends on
the power and dose. Typical doses may take values of 1 kGy, 5 kGy,
10 kGy, 20 kGy, 50 kGy, 100 kGy, or 200 kGy.
[0259] Tradeoffs in considering electron beam irradiation device
power specifications include cost to operate, capital costs,
depreciation, and device footprint. Tradeoffs in considering
exposure dose levels of electron beam irradiation would be energy
costs and environment, safety, and health (ESH) concerns.
Typically, generators are housed in a vault, e.g., of lead or
concrete. Tradeoffs in considering electron energies include energy
costs; here, a lower electron energy may be advantageous in
encouraging depolymerization of certain feedstock slurry (see, for
example, Bouchard, et al, Cellulose (2006) 13: 601-610).
[0260] It may be advantageous to provide a double-pass of electron
beam irradiation in order to provide a more effective
depolymerization process. For example, the feedstock transport
device could direct the feedstock (in dry or slurry form)
underneath and in a reverse direction to its initial transport
direction. Double-pass systems can allow thicker feedstock slurries
to be processed and can provide a more uniform depolymerization
through the thickness of the feedstock slurry.
[0261] The electron beam irradiation device can produce either a
fixed beam or a scanning beam. A scanning beam may be advantageous
with large scan sweep length and high scan speeds, as this would
effectively replace a large, fixed beam width. Further, available
sweep widths of 0.5 m, 1 m, 2 m or more are available.
[0262] Once a portion of feedstock slurry has been transported
through the N electron beam irradiation devices, it may be
necessary in some embodiments, as in step 3060, to mechanically
separate the liquid and solid components of the feedstock slurry.
In these embodiments, a liquid portion of the feedstock slurry is
filtered for residual solid particles and recycled back to the
slurry preparation step 3040. A solid portion of the feedstock
slurry is then advanced on to the next processing step 3070 via the
feedstock transport device. In other embodiments, the feedstock is
maintained in slurry form for further processing.
Heavy Ion Particle Beams
[0263] Particles heavier than electrons can be utilized to
irradiate carbohydrates or materials that include carbohydrates,
e.g., cellulosic materials, lignocellulosic materials, starchy
materials, or mixtures of any of these and others described herein.
For example, protons, helium nuclei, argon ions, silicon ions, neon
ions carbon ions, phoshorus ions, oxygen ions or nitrogen ions can
be utilized. In some embodiments, particles heavier than electrons
can induce higher amounts of chain scission. In some instances,
positively charged particles can induce higher amounts of chain
scission than negatively charged particles due to their
acidity.
[0264] Heavier particle beams can be generated, e.g., using linear
accelerators or cyclotrons. In some embodiments, the energy of each
particle of the beam is from about 1.0 MeV/atomic unit to about
6,000 MeV/atomic unit, e.g., from about 3 MeV/atomic unit to about
4,800 MeV/atomic unit, or from about 10 MeV/atomic unit to about
1,000 MeV/atomic unit.
Electromagnetic Radiation
[0265] In embodiments in which the irradiating is performed with
electromagnetic radiation, the electromagnetic radiation can have,
e.g., energy per photon (in electron volts) of greater than
10.sup.2 eV, e.g., greater than 10.sup.3, 10.sup.4, 10.sup.5,
10.sup.6, or even greater than 10.sup.7 eV. In some embodiments,
the electromagnetic radiation has energy per photon of between
10.sup.4 and 10.sup.7, e.g., between 10.sup.5 and 10.sup.6 eV. The
electromagnetic radiation can have a frequency of, e.g., greater
than 10.sup.16 hz, greater than 10.sup.17 hz, 10.sup.18, 10.sup.19,
10.sup.20, or even greater than 10.sup.21 hz. In some embodiments,
the electromagnetic radiation has a frequency of between 10.sup.18
and 10.sup.22 hz, e.g., between 10.sup.19 to 10.sup.21 hz.
Doses
[0266] In some embodiments, the irradiating (with any radiation
source or a combination of sources) is performed until the material
receives a dose of at least 0.05 Mrad, e.g., at least 0.1, 0.25,
1.0, 2.5, 5.0, or 10.0 Mrad. In some embodiments, the irradiating
is performed until the material receives a dose of between 1.0 Mrad
and 6.0 Mrad, e.g., between 1.5 Mrad and 4.0 Mrad. In other
embodiments, irradiating is performed at a dose between about 0.1
MRad and about 10 MRad, e.g., between about 0.25 MRad and about 9
MRad, between about 0.5 MRad and about 7.5 MRad or between about
0.75 MRad and about 5 MRad.
[0267] In some embodiments, the irradiating is performed at a dose
rate of between 5.0 and 1500.0 kilorads/hour, e.g., between 10.0
and 750.0 kilorads/hour or between 50.0 and 350.0
kilorads/hours.
[0268] In some embodiments, two or more radiation sources are used,
such as two or more ionizing radiations. For example, samples can
be treated, in any order, with a beam of electrons, followed by
gamma radiation and UV light having wavelengths from about 100 nm
to about 280 nm. In some embodiments, samples are treated with
three ionizing radiation sources, such as a beam of electrons,
gamma radiation, and energetic UV light.
[0269] In one example of the use of radiation as a pretreatment,
half-gallon juice cartons made of un-printed polycoated white Kraft
board having a bulk density of 20 lb/ft.sup.3 are used as a
feedstock. Cartons are folded flat and then fed into a sequence of
three shredder-shearer trains arranged in series with output from
the first shearer fed as input to the second shredder, and output
from the second shearer fed as input to the third shredder. The
fibrous material produced by the shredder-shearer train can be
sprayed with water and processed through a pellet mill operating at
room temperature. The densified pellets can be placed in a glass
ampoule which is evacuated under high vacuum and then back-filled
with argon gas. The ampoule is sealed under argon. Alternatively,
in another example, the ampoule is sealed under an atmosphere of
air. The pellets in the ampoule are irradiated with gamma radiation
for about 3 hours at a dose rate of about 1 Mrad per hour to
provide an irradiated material in which the cellulose has a lower
molecular weight than the starting material.
Additives to Enhance Molecular Weight Breakdown During
Irradiation
[0270] In some embodiments, prior to irradiation, various
materials, e.g., solids or liquids, can be added to the biomass to
enhance molecular weight reduction. In those instances in which a
liquid is utilized, the liquid can be in contact with outer
surfaces of the biomass and/or the liquid can be in interior
portions of the biomass, e.g., infused into the biomass.
[0271] For example, the material can be a neutral weak base, such
as alanine, ammonia, ammonia/water mixture, e.g., 25 percent by
weight ammonia in water, water, methyl amine, dimethyl amine,
trimethyl amine, pyridine, or a anionic base, such as a salt of
acetic acid (e.g., sodium acetate), sodium carbonate, sodium
bicarbonate or a salt of an ion of hydrogen sulfide (e.g., sodium
hydrosulfide).
[0272] Alternatively, the material can be a neutral weak acid, such
as formic acid, acetic acid, trichloroacetic acid, water, hydrogen
sulfide or a cationic acid, such as an ammonium salt.
Quenching and Controlled Functionalization of Biomass
[0273] After treatment with one or more ionizing radiations, such
as photonic radiation (e.g., X-rays or gamma-rays), e-beam
radiation or particles heavier than electrons that are positively
or negatively charged (e.g., protons or carbon ions), any of the
carbohydrate-containing materials or mixtures described herein
become ionized; that is, they include radicals at levels that are
detectable with an electron spin resonance spectrometer. The
current limit of detection of the radicals is about 10.sup.14 spins
at room temperature. After ionization, any biomass material that
has been ionized can be quenched to reduce the level of radicals in
the ionized biomass, e.g., such that the radicals are no longer
detectable with the electron spin resonance spectrometer. For
example, the radicals can be quenched by the application of a
sufficient pressure to the biomass and/or by utilizing a fluid in
contact with the ionized biomass, such as a gas or liquid, that
reacts with (quenches) the radicals. Using a gas or liquid to at
least aid in the quenching of the radicals can be used to
functionalize the ionized biomass with a desired amount and kind of
functional groups, such as carboxylic acid groups, enol groups,
aldehyde groups, nitro groups, nitrile groups, amino groups, alkyl
amino groups, alkyl groups, chloroalkyl groups or chlorofluoroalkyl
groups. In some instances, such quenching can improve the stability
of some of the ionized biomass materials. For example, quenching
can improve the resistance of the biomass to oxidation.
Functionalization by quenching can also improve the solubility of
any biomass described herein, can improve its thermal stability,
and can improve material utilization by various microorganisms. For
example, the functional groups imparted to the biomass material by
the quenching can act as receptor sites for attachment by
microorganisms, e.g., to enhance cellulose hydrolysis by various
microorganisms.
[0274] FIG. 11A illustrates changing a molecular and/or a
supramolecular structure of a biomass feedstock by pretreating the
biomass feedstock with ionizing radiation, such as with electrons
or ions of sufficient energy to ionize the biomass feedstock, to
provide a first level of radicals. As shown in FIG. 11A, if ionized
biomass remains in the atmosphere, it will be oxidized, such as to
an extent that carboxylic acid groups are generated by reacting
with the atmospheric oxygen. In some instances with some materials,
such oxidation is desired because it can aid in the further
breakdown in molecular weight of the carbohydrate-containing
biomass, and the oxidation groups, e.g., carboxylic acid groups can
be helpful for solubility and microorganism utilization in some
instances. However, since the radicals can "live" for some time
after irradiation, e.g., longer than 1 day, 5 days, 30 days, 3
months, 6 months or even longer than 1 year, materials properties
can continue to change over time, which in some instances, can be
undesirable. Detecting radicals in irradiated samples by electron
spin resonance spectroscopy and radical lifetimes in such samples
is discussed in Bartolotta et al., Physics in Medicine and Biology,
46 (2001), 461-471 and in Bartolotta et al., Radiation Protection
Dosimetry, Vol. 84, Nos. 1-4, pp. 293-296 (1999) which are included
as Appendix F and Appendix G, respectively, in U.S. Pat. No.
8,212,087. As shown in FIG. 11A, the ionized biomass can be
quenched to functionalize and/or to stabilize the ionized biomass.
At any point, e.g., when the material is "alive", "partially alive"
or fully quenched, the pretreated biomass can be converted into a
product, e.g., a fuel, a food, or a composite.
[0275] In some embodiments, the quenching includes an application
of pressure to the biomass, such as by mechanically deforming the
biomass, e.g., directly mechanically compressing the biomass in
one, two, or three dimensions, or applying pressure to a fluid in
which the biomass is immersed, e.g., isostatic pressing. In such
instances, the deformation of the material itself brings radicals,
which are often trapped in crystalline domains, in close enough
proximity so that the radicals can recombine, or react with another
group. In some instances, the pressure is applied together with the
application of heat, such as a sufficient quantity of heat to
elevate the temperature of the biomass to above a melting point or
softening point of a component of the biomass, such as lignin,
cellulose or hemicellulose. Heat can improve molecular mobility in
the polymeric material, which can aid in the quenching of the
radicals. When pressure is utilized to quench, the pressure can be
greater than about 1000 psi, such as greater than about 1250 psi,
1450 psi, 3625 psi, 5075 psi, 7250 psi, 10000 psi or even greater
than 15000 psi.
[0276] In some embodiments, quenching includes contacting the
biomass with a fluid, such as a liquid or gas, e.g., a gas capable
of reacting with the radicals, such as acetylene or a mixture of
acetylene in nitrogen, ethylene, chlorinated ethylenes or
chlorofluoroethylenes, propylene or mixtures of these gases. In
other particular embodiments, quenching includes contacting the
biomass with a liquid, e.g., a liquid soluble in, or at least
capable of penetrating into the biomass and reacting with the
radicals, such as a diene, such as 1,5-cyclooctadiene. In some
specific embodiments, the quenching includes contacting the biomass
with an antioxidant, such as Vitamin E. If desired, the biomass
feedstock can include an antioxidant dispersed therein, and the
quenching can come from contacting the antioxidant dispersed in the
biomass feedstock with the radicals.
[0277] Other methods for quenching are possible. For example, any
method for quenching radicals in polymeric materials described in
Muratoglu et al., U.S. Patent Application Publication No.
2008/0067724 and Muratoglu et al., U.S. Pat. No. 7,166,650, which
are included as Appendix H and Appendix I, respectively, in U.S.
Pat. No. 8,212,087, can be utilized for quenching any ionized
biomass material described herein. Furthermore any quenching agent
(described as a "sensitizing agent" in the above-noted Muratoglu
disclosures) and/or any antioxidant described in either Muratoglu
reference can be utilized to quench any ionized biomass
material.
[0278] Functionalization can be enhanced by utilizing heavy charged
ions, such as any of the heavier ions described herein. For
example, if it is desired to enhance oxidation, charged oxygen ions
can be utilized for the irradiation. If nitrogen functional groups
are desired, nitrogen ions or anions that includes nitrogen can be
utilized. Likewise, if sulfur or phosphorus groups are desired,
sulfur or phosphorus ions can be used in the irradiation.
[0279] In some embodiments, after quenching any of the quenched
ionized materials described herein can be further treated with one
or more of radiation, such as ionizing or non-ionizing radiation,
sonication, pyrolysis, and oxidation for additional molecular
and/or supramolecular structure change.
Particle Beam Exposure in Fluids
[0280] In some cases, the cellulosic or lignocellulosic materials
can be exposed to a particle beam in the presence of one or more
additional fluids (e.g., gases and/or liquids). Exposure of a
material to a particle beam in the presence of one or more
additional fluids can increase the efficiency of the treatment.
[0281] In some embodiments, the material is exposed to a particle
beam in the presence of a fluid such as air. Particles accelerated
in any one or more of the types of accelerators disclosed herein
(or another type of accelerator) are coupled out of the accelerator
via an output port (e.g., a thin membrane such as a metal foil),
pass through a volume of space occupied by the fluid, and are then
incident on the material. In addition to directly treating the
material, some of the particles generate additional chemical
species by interacting with fluid particles (e.g., ions and/or
radicals generated from various constituents of air, such as ozone
and oxides of nitrogen). These generated chemical species can also
interact with the material, and can act as initiators for a variety
of different chemical bond-breaking reactions in the material. For
example, any oxidant produced can oxidize the material, which can
result in molecular weight reduction.
[0282] In certain embodiments, additional fluids can be selectively
introduced into the path of a particle beam before the beam is
incident on the material. As discussed above, reactions between the
particles of the beam and the particles of the introduced fluids
can generate additional chemical species, which react with the
material and can assist in functionalizing the material, and/or
otherwise selectively altering certain properties of the material.
The one or more additional fluids can be directed into the path of
the beam from a supply tube, for example. The direction and flow
rate of the fluid(s) that is/are introduced can be selected
according to a desired exposure rate and/or direction to control
the efficiency of the overall treatment, including effects that
result from both particle-based treatment and effects that are due
to the interaction of dynamically generated species from the
introduced fluid with the material. In addition to air, exemplary
fluids that can be introduced into the ion beam include oxygen,
nitrogen, one or more noble gases, one or more halogens, and
hydrogen.
Irradiating Low Bulk Density Biomass Materials and Cooling
Irradiated Biomass
[0283] During treatment of biomass materials with ionizing
radiation, especially at high dose rates, such as at rates greater
than 0.15 Mrad per second, e.g., 0.25 Mrad/s, 0.35 Mrad/s, 0.5
Mrad/s, 0.75 Mrad/s or even greater than 1 Mrad/sec, biomass
materials can retain significant quantities of heat so that the
temperature of the biomass materials becomes elevated. While higher
temperatures can, in some embodiments, be advantageous, e.g., when
a faster reaction rate is desired, it is advantageous to control
the heating of the biomass to retain control over the chemical
reactions initiated by the ionizing radiation, such as
crosslinking, chain scission and/or grafting, e.g., to maintain
process control. Low bulk density materials, such as those having a
bulk density of less than about 0.4 g/cm.sup.3, e.g., less than
about 0.35, 0.25 or less about 0.15 g/cm.sup.3, especially when
combined with materials that have thin cross-sections, such as
fibers having small transverse dimensions, are generally easier to
cool. In addition, photons and particles can generally penetrate
further into and through materials having a relatively low bulk
density, which can allow for the processing of larger volumes of
materials at higher rates, and can allow for the use of photons and
particles that having lower energies, e.g., 0.25 Mev, 0.5 MeV, 0.75
MeV or 1.0 MeV, which can reduce safety shielding requirements.
Many of the biomass materials described herein can be processed in
one or more of the systems shown in FIGS. 11B, 11C, 11D and 11E,
which are described below. The systems shown allow one or more
types of ionizing radiation, such as relativistic electrons or
electrons in combination with X-rays, to be applied to low bulk
density biomass materials at high dose rates, such as at a rate
greater than 1.0, 1.5, 2.5 Mrad/s or even greater than about 5.0
Mrad/s, and then to allow for cooling of the biomass prior to
applying radiation for a second, third, fourth, fifth, sixth,
seventh, eighth, ninth or even a tenth time.
[0284] For example, in one method of changing a molecular and/or a
supramolecular structure of a biomass feedstock, the biomass is
pretreated at a first temperature with ionizing radiation, such as
photons, electrons or ions (e.g., singularly or multiply charged
cations or anions), for a sufficient time and/or a sufficient dose
to elevate the biomass feedstock to a second temperature higher
than the first temperature. The pretreated biomass is then cooled
to a third temperature below the second temperature. Finally, if
desired, the cooled biomass can be treated one or more times with
radiation, e.g., with ionizing radiation. If desired, cooling can
be applied to the biomass after and/or during each radiation
treatment.
[0285] The biomass feedstock can be physically prepared as
discussed above, e.g., by reducing one or more dimensions of
individual pieces of the biomass feedstock so that the feedstock
can be more efficiently processed, e.g., more easily cooled and/or
more easily penetrated by an ionizing radiation.
[0286] In some implementations, the ionizing radiation is applied
at a total dose of less than 25 Mrad or less than 10 Mrad, such as
less than 5 Mrad or less than 2.5 Mrad, and at a rate of more than
0.25 Mrad per second, such as more than 0.5, 0.75 or greater than
1.0 Mrad/s, prior to cooling the biomass.
[0287] The pretreating of the biomass feedstock with ionizing
radiation can be performed as the biomass feedstock is being
pneumatically conveyed in a fluid, such as a in a gas, e.g.,
nitrogen or air. To aid in molecular weight breakdown and/or
functionalization of the materials, the gas can be saturated with
any swelling agent described herein and/or water vapor. For
example, acidic water vapor can be utilized. To aid in molecular
weight breakdown, the water can be acidified with an organic acid,
such as formic, or acetic acid, or a mineral acid, such as sulfuric
or hydrochloric acid.
[0288] The pretreating of the biomass feedstock with ionizing
radiation can be performed as the biomass feedstock falls under the
influence of gravity. This procedure can effectively reduce the
bulk density of the biomass feedstock as it is being processed and
can aid in the cooling of the biomass feedstock. For example, the
biomass can be conveyed from a first belt at a first height above
the ground and then can be captured by a second belt at a second
level above the ground lower than the first level. For example, in
some embodiments, the trailing edge of the first belt and the
leading edge of the second belt define a gap. Advantageously, the
ionizing radiation, such as a beam of electrons, protons, or other
ions, can be applied at the gap to prevent damage to the biomass
conveyance system.
[0289] Cooling of the biomass can include contacting the biomass
with a fluid, such as a gas, at a temperature below the first or
second temperature, such as gaseous nitrogen at or about 77 K. Even
water, such as water at a temperature below nominal room
temperature (e.g., 25 degrees Celsius) can be utilized.
[0290] Often advantageously, the biomass feedstock has internal
fibers, and prior to irradiation with the ionizing radiation, the
biomass feedstock has been sheared to an extent that its internal
fibers are substantially exposed. This shearing can provide a low
bulk density material having small cross-sectional dimensions,
which can aid in the breakdown and/or functionalization of the
biomass. For example, in some embodiments, the biomass is or
includes discrete fibers and/or particles having a maximum
dimension of not more than about 0.5 mm, such as not more than
about 0.25 mm, not more than about 0.1 mm or not more than about
0.05 mm.
[0291] In some embodiments, the biomass feedstock to which the
ionizing radiation is applied has a bulk density of less than about
0.35 g/cm.sup.3, such as less than about 0.3, 0.25, 0.20, or less
than about 0.15 g/cm.sup.3 during the application of the ionizing
radiation. In such embodiments, the biomass feedstock can be
cooled, and then ionizing radiation can be applied to the cooled
biomass. In some advantageous embodiments, the biomass feedstock is
or includes discrete fibers and/or particles having a maximum
dimension of not more than about 0.5 mm, such as not more than
about 0.25 mm, not more than about 0.1 mm, not more than about 0.05
mm, or not more than about 0.025 mm.
[0292] FIGS. 11B and 11C show a fibrous material generating,
treating, conveying and irradiating device 1170 (shielding not
illustrated in the drawings). In operation, paper sheet 1173, e.g.,
scrap bleached Kraft paper sheet, is supplied from a roll 1172 and
delivered to a fiberizing apparatus 1174, such as a rotary shearer.
The sheet 1173 is converted into fibrous material 1112 and is
delivered to a fiber-loading zone 1180 by conveyer 1178. If
desired, the fibers of the fibrous material can be separated, e.g.,
by screening, into fractions having different L/D ratios. In some
embodiments, the fibrous material 1112 of generally a low bulk
density and advantageously thin cross-section, is delivered
continuously to zone 1180; in other embodiments, the fibrous
material is delivered in batches. A blower 1182 in loop 1184 is
positioned adjacent to the fiber-loading zone 1180 and is capable
of moving a fluid medium, e.g., air, at a velocity and volume
sufficient to pneumatically circulate the fibrous material 1112 in
a direction indicated by arrow 1188 through loop 1184.
[0293] In some embodiments, the velocity of air traveling in the
loop is sufficient to uniformly disperse and transport the fibrous
material around the entire loop 1184. In some embodiments, the
velocity of flow is greater than 2,500 feet/minute, e.g., 5,000
feet/minute, 6,000 feet/minute or more, e.g., 7,500 feet/minute or
8,500 feet/minute.
[0294] The entrained fibrous material 1112 traversing the loop
passes an application zone 1190, which forms part of loop 1184.
Here, any desired additives described herein are applied, such as a
liquid, such as water, which may be acidified or made basic. In
operation, application zone 1190 applies an additive, such as a
liquid solution 1196, to the circulating fibrous material via
nozzles 98, 99 and 11100. When a liquid is applied, the nozzles
produce an atomized spray or mist, which impacts the fibers as the
fibers pass in proximity to the nozzles. Valve 11102 is operated to
control the flow of liquid to the respective nozzles 1198, 1199,
and 11100. After a desired quantity of additive is applied, the
valve 11102 is closed.
[0295] In some embodiments, the application zone 1190 is two to one
hundred feet long or more, e.g., 125 feet, 150 feet, 250 feet long
or more, e.g., 500 feet long. Longer application zones allow for
application of liquid over a longer period of time during passage
of fibrous material through application zone 1190. In some
embodiments, the nozzles are spaced apart, e.g., by from about
three to about four feet, along the length of loop 1184.
[0296] As the fibrous material moves in loop 1184 and through the
irradiating portion of the loop 11107 that includes a horn 11109
for delivering ionizing radiation, ionizing radiation is applied to
the fibrous material (shielding is not shown).
[0297] As the irradiated fibrous material moves around loop 1184,
it cools by the action of gases, such as air, circulating at high
speeds in the loop. The material is bathed in reactive gases, such
as ozone and/or oxides of nitrogen that are produced from the
action of the ionizing radiation on the circulating gases, such as
air. After passing through the irradiating portion 11107, a cooling
fluid, such as a liquid (e.g., water) or a gas, such as liquid
nitrogen at 77 K, can be injected into loop 1184 to aid in the
cooling of the fibrous material. This process can be repeated more
than one time if desired, e.g., 2, 3, 4, 5, 6, 7, 8, 9, 10 times or
more, e.g., 15 times, to deliver the desired dose to the fibrous
material. While, as shown, the long axis of the horn is along the
direction of flow, in some implementations, the long axis of the
horn is transverse to the direction of the flow. In some
implementations, a beam of electrons is utilized as a principal
ionizing radiation source and X-rays as a secondary ionizing
radiation source. X-rays can be generated by having a metal target,
such as a tantalum target 11111, on the inside of loop 1184 such
that when electrons strike the target, X-rays are emitted.
[0298] After a desired dose is delivered to the fibrous material,
the fibrous material can be removed from loop 1184 via a separator
11112, which is selectively connected to loop 1184 by section 11114
and gate valve 11116. When valve 11116 is opened, another valve is
also opened to allow air to enter the loop 1184 to compensate for
air exiting through separator 11112.
[0299] FIG. 11D shows a fluidized bed fibrous irradiating device
11121 with shielding. Fibrous material in a fluid, such as a gas,
such as air under pressure, is delivered to a shielded containment
vessel 11123 via piping 11125 and into a shielded fluidized bed
portion 11127. Counter-current streams 11131 of fluid, such as a
gas, and transverse streams 11133 of fluid, such as a gas, that can
be the same as or different from the fluid delivered
counter-currently, combine to cause turbulence in the bed portion.
Ionizing radiation is applied to the fluidized bed portion as the
fibrous material is conveyed through the bed portion. For example,
as shown, three beams of electrons from three Rhodotron.RTM.
machines 11135, 11136 and 11137 can be utilized. Advantageously,
each beam can penetrate into the fluidized bed a different depth
and/or each beam can emit electrons of a different energy, such as
1, 3, and 5 MeV. As the irradiated fibrous material moves through
the system, it cools by the action of gases, such as air,
circulating at high speeds in the system and it is bathed in
reactive gases, such as ozone and/or oxides of nitrogen, that are
produced from the action of the ionizing radiation on the
circulating gases, such as air. If desired, the process can be
repeated a desired number of times until the fibrous material has
received a desired dose. While the fluidized bed has been
illustrated such that its long axis is horizontal with the ground,
in other implementations, the long axis of the bed is perpendicular
to the ground so that the fibrous material falls under the
influence of gravity.
[0300] FIG. 11E shows another fibrous material conveying and
irradiating device 11140 without shielding. Fibrous material 11144
is delivered from a bin 11142 to a first conveyer 11150 at a first
level above the ground and then the material is transferred to a
second conveyer 11152 at a lower height than the first conveyer.
The trailing edge 11160 of the first conveyer and the leading edge
11161 of the second conveyer 11152 define a gap with a spacing S.
For example, the spacing S can be between 4 inches and about 24
inches. Material 11144 has enough momentum to free fall under
gravity and then to be captured by the second conveyer 11152
without falling into the gap. During the free fall, ionizing
radiation is applied to the material. This arrangement can be
advantageous in that the ionizing radiation is less likely to
damage the conveying system because the conveying system is not
directly contacted by the radiation.
[0301] After the material passes through the irradiating portion, a
cooling fluid, such as a liquid (e.g., water) or a gas, such as
liquid nitrogen at 77 K, can be applied to the material to aid in
the cooling of the fibrous material. This process can be repeated
more than one time if desired, e.g., 2, 3, 4, 5, 6, 7, 8, 9, 10
times or more, e.g., 15 times, to deliver the desired dose to the
fibrous material. While, as shown, the long axis of the horn is
transverse to the direction of the material flow, other beam
arrangements are possible. In some implementations, a beam of
electrons is utilized as a principal ionizing radiation source and
X-rays as a secondary ionizing radiation source. X-rays can be
generated by having a metal target, such as a tantalum target, in
the gap on the opposite side of the material, such that as the
electrons that pass through the material they strike the target,
generating X-rays.
Sonication and other Biomass Disruption Processes
[0302] One or more sonication processing sequences can be used to
process raw feedstock from a wide variety of different sources to
extract useful substances from the feedstock, and to provide
partially degraded organic material which functions as input to
further processing steps and/or sequences. Sonication can reduce
the molecular weight and/or crystallinity of feedstock, such as one
or more of any of the biomass materials described herein, e.g., one
or more carbohydrate sources, such as cellulosic or lignocellulosic
materials, or starchy materials.
[0303] Referring again to FIG. 8, in one method, a first material 2
that includes cellulose having a first number average molecular
weight (.sup.TM.sub.n1) is dispersed in a medium, such as water,
and sonicated and/or otherwise cavitated, to provide a second
material 3 that includes cellulose having a second number average
molecular weight (.sup.TM.sub.n2) lower than the first number
average molecular weight. The second material (or the first and
second material in certain embodiments) can be combined with a
microorganism (e.g., a bacterium or a yeast) that can utilize the
second and/or first material to produce a fuel 5 that is or
includes hydrogen, an alcohol, an organic acid, a hydrocarbon or
mixtures of any of these.
[0304] Since the second material has cellulose having a reduced
molecular weight relative to the first material, and in some
instances, a reduced crystallinity as well, the second material is
generally more dispersible, swellable, and/or soluble in a solution
containing the microorganism, e.g., at a concentration of greater
than 10.sup.6 microorganisms/mL. These properties make the second
material 3 more susceptible to chemical, enzymatic, and/or
microbial attack relative to the first material 2, which can
greatly improve the production rate and/or production level of a
desired product, e.g., ethanol. Sonication can also sterilize the
materials, but should not be used while the microorganisms are
supposed to be alive.
[0305] In some embodiments, the second number average molecular
weight (.sup.TM.sub.n2) is lower than the first number average
molecular weight (.sup.TM.sub.n1) by more than about 10 percent,
e.g., 15, 20, 25, 30, 35, 40, 50 percent, 60 percent, or even more
than about 75 percent.
[0306] In some instances, the second material has cellulose that
has as crystallinity (.sup.TC.sub.2) that is lower than the
crystallinity (.sup.TC.sub.1) of the cellulose of the first
material. For example, (.sup.TC.sub.2) can be lower than
(.sup.TC.sub.1) by more than about 10 percent, e.g., 15, 20, 25,
30, 35, 40, or even more than about 50 percent.
[0307] In some embodiments, the starting crystallinity index (prior
to sonication) is from about 40 to about 87.5 percent, e.g., from
about 50 to about 75 percent or from about 60 to about 70 percent,
and the crystallinity index after sonication is from about 10 to
about 50 percent, e.g., from about 15 to about 45 percent or from
about 20 to about 40 percent. However, in certain embodiments,
e.g., after extensive sonication, it is possible to have a
crystallinity index of lower than 5 percent. In some embodiments,
the material after sonication is substantially amorphous.
[0308] In some embodiments, the starting number average molecular
weight (prior to sonication) is from about 200,000 to about
3,200,000, e.g., from about 250,000 to about 1,000,000 or from
about 250,000 to about 700,000, and the number average molecular
weight after sonication is from about 50,000 to about 200,000,
e.g., from about 60,000 to about 150,000 or from about 70,000 to
about 125,000. However, in some embodiments, e.g., after extensive
sonication, it is possible to have a number average molecular
weight of less than about 10,000 or even less than about 5,000.
[0309] In some embodiments, the second material can have a level of
oxidation (.sup.TO.sub.2) that is higher than the level of
oxidation (.sup.TO.sub.1) of the first material. A higher level of
oxidation of the material can aid in its dispersibility,
swellability and/or solubility, further enhancing the materials
susceptibility to chemical, enzymatic or microbial attack. In some
embodiments, to increase the level of the oxidation of the second
material relative to the first material, the sonication is
performed in an oxidizing medium, producing a second material that
is more oxidized than the first material. For example, the second
material can have more hydroxyl groups, aldehyde groups, ketone
groups, ester groups or carboxylic acid groups, which can increase
its hydrophilicity.
[0310] In some embodiments, the sonication medium is an aqueous
medium. If desired, the medium can include an oxidant, such as a
peroxide (e.g., hydrogen peroxide), a dispersing agent and/or a
buffer. Examples of dispersing agents include ionic dispersing
agents, e.g., sodium lauryl sulfate, and non-ionic dispersing
agents, e.g., poly(ethylene glycol).
[0311] In other embodiments, the sonication medium is non-aqueous.
For example, the sonication can be performed in a hydrocarbon,
e.g., toluene or heptane, an ether, e.g., diethyl ether or
tetrahydrofuran, or even in a liquefied gas such as argon, xenon,
or nitrogen.
[0312] Without wishing to be bound by any particular theory, it is
believed that sonication breaks bonds in the cellulose by creating
bubbles in the medium containing the cellulose, which grow and then
violently collapse. During the collapse of the bubble, which can
take place in less than a nanosecond, the implosive force raises
the local temperature within the bubble to about 5100 K (even
higher in some instance; see, e.g., Suslick et al., Nature 434,
52-55) and generates pressures of from a few hundred atmospheres to
over 1000 atmospheres or more. It is these high temperatures and
pressures that break the bonds. In addition, without wishing to be
bound by any particular theory, it is believed that reduced
crystallinity arises, at least in part, from the extremely high
cooling rates during collapse of the bubbles, which can be greater
than about 10.sup.11 K/second. The high cooling rates generally do
not allow the cellulose to organize and crystallize, resulting in
materials that have reduced crystallinity. Ultrasonic systems and
sonochemistry are discussed in, e.g., Olli et al., U.S. Pat. No.
5,766,764; Roberts, U.S. Pat. No. 5,828,156; Mason, Chemistry with
Ultrasound, Elsevier, Oxford, (1990); Suslick (editor), Ultrasound:
its Chemical, Physical and Biological Effects, VCH, Weinheim,
(1988); Price, "Current Trends in Sonochemistry" Royal Society of
Chemistry, Cambridge, (1992); Suslick et al., Ann. Rev. Mater. Sci.
29, 295, (1999); Suslick et al., Nature 353, 414 (1991); Hiller et
al., Phys. Rev. Lett. 69, 1182 (1992); Barber et al., Nature, 352,
414 (1991); Suslick et al., J. Am. Chem. Soc., 108, 5641 (1986);
Tang et al., Chem. Comm., 2119 (2000); Wang et al., Advanced
Mater., 12, 1137 (2000); Landau et al., J. of Catalysis, 201, 22
(2001); Perkas et al., Chem. Comm., 988 (2001); Nikitenko et al.,
Angew. Chem. Inter. Ed. (December 2001); Shafi et al., J. Phys.
Chem B 103, 3358 (1999); Avivi et al., J. Amer. Chem. Soc. 121,
4196 (1999); and Avivi et al., J. Amer. Chem. Soc. 122, 4331
(2000).
Sonication Systems
[0313] FIG. 12 shows a general system in which a cellulosic
material stream 1210 is mixed with a water stream 1212 in a
reservoir 1214 to form a process stream 1216. A first pump 1218
draws process stream 1216 from reservoir 1214 and toward a flow
cell 1224. Ultrasonic transducer 1226 transmits ultrasonic energy
into process stream 1216 as the process stream flows through flow
cell 1224. A second pump 1230 draws process stream 1216 from flow
cell 1224 and toward subsequent processing.
[0314] Reservoir 1214 includes a first intake 1232 and a second
intake 1234 in fluid communication with a volume 1236. A conveyor
(not shown) delivers cellulosic material stream 1210 to reservoir
1214 through first intake 1232. Water stream 1212 enters reservoir
1214 through second intake 1234. In some embodiments, water stream
1212 enters volume 1236 along a tangent establishing a swirling
flow within volume 1236. In certain embodiments, cellulosic
material stream 1210 and water stream 1212 can be introduced into
volume 1236 along opposing axes to enhance mixing within the
volume.
[0315] Valve 1238 controls the flow of water stream 1212 through
second intake 1232 to produce a desired ratio of cellulosic
material to water (e.g., approximately 10% cellulosic material,
weight by volume). For example, 2000 tons/day of cellulosic
material can be combined with 1 million to 1.5 million gallons/day,
e.g., 1.25 million gallons/day, of water.
[0316] Mixing of cellulosic material and water in reservoir 1214 is
controlled by the size of volume 1236 and the flow rates of
cellulosic material and water into the volume. In some embodiments,
volume 1236 is sized to create a minimum mixing residence time for
the cellulosic material and water. For example, when 2000 tons/day
of cellulosic material and 1.25 million gallons/day of water are
flowing through reservoir 1214, volume 1236 can be about 32,000
gallons to produce a minimum mixing residence time of about 15
minutes.
[0317] Reservoir 1214 includes a mixer 1240 in fluid communication
with volume 1236. Mixer 1240 agitates the contents of volume 1236
to disperse cellulosic material throughout the water in the volume.
For example, mixer 1240 can be a rotating vane disposed in
reservoir 1214. In some embodiments, mixer 1240 disperses the
cellulosic material substantially uniformly throughout the
water.
[0318] Reservoir 1214 further includes an exit 1242 in fluid
communication with volume 1236 and process stream 1216. The mixture
of cellulosic material and water in volume 1236 flows out of
reservoir 1214 via exit 1242. Exit 1242 is arranged near the bottom
of reservoir 1214 to allow gravity to pull the mixture of
cellulosic material and water out of reservoir 1214 and into
process stream 1216.
[0319] First pump 1218 (e.g., any of several recessed impeller
vortex pumps made by Essco Pumps & Controls, Los Angeles,
Calif.) moves the contents of process stream 1216 toward flow cell
1224. In some embodiments, first pump 1218 agitates the contents of
process stream 1216 such that the mixture of cellulosic material
and water is substantially uniform at inlet 1220 of flow cell 1224.
For example, first pump 1218 agitates process stream 1216 to create
a turbulent flow that persists along the process stream between the
first pump and inlet 1220 of flow cell 1224.
[0320] Flow cell 1224 includes a reactor volume 1244 in fluid
communication with inlet 1220 and outlet 1222. In some embodiments,
reactor volume 1244 is a stainless steel tube capable of
withstanding elevated pressures (e.g., 10 bars). In addition or in
the alternative, reactor volume 1244 includes a rectangular cross
section.
[0321] Flow cell 1224 further includes a heat exchanger 1246 in
thermal communication with at least a portion of reactor volume
1244. Cooling fluid 1248 (e.g., water) flows into heat exchanger
1246 and absorbs heat generated when process stream 1216 is
sonicated in reactor volume 1244. In some embodiments, the flow
rate and/or the temperature of cooling fluid 1248 into heat
exchanger 1246 is controlled to maintain an approximately constant
temperature in reactor volume 1244. In some embodiments, the
temperature of reactor volume 1244 is maintained at 20 to
50.degree. C., e.g., 25, 30, 35, 40, or 45.degree. C. Additionally
or alternatively, heat transferred to cooling fluid 1248 from
reactor volume 1244 can be used in other parts of the overall
process.
[0322] An adapter section 1226 creates fluid communication between
reactor volume 1244 and a booster 1250 coupled (e.g., mechanically
coupled using a flange) to ultrasonic transducer 1226. For example,
adapter section 1226 can include a flange and O-ring assembly
arranged to create a leak tight connection between reactor volume
1244 and booster 1250. In some embodiments, ultrasonic transducer
1226 is a high-powered ultrasonic transducer made by Hielscher
Ultrasonics of Teltow, Germany.
[0323] In operation, a generator 1252 delivers electricity to
ultrasonic transducer 1252. Ultrasonic transducer 1226 includes a
piezoelectric element that converts the electrical energy into
sound in the ultrasonic range. In some embodiments, the materials
are sonicated using sound having a frequency of from about 16 kHz
to about 110 kHz, e.g., from about 18 kHz to about 75 kHz or from
about 20 kHz to about 40 kHz. (e.g., sound having a frequency of 20
kHz to 40 kHz). In some implementations, sonication is performed,
for example, at a frequency of between about 15 kHz and about 25
kHz, such as between about 18 kHz and 22 kHz. In specific
embodiments, sonicating can be performed utilizing a 1 KW or larger
horn, e.g., a 2, 3, 4, 5, or even a 10 KW horn.
[0324] The ultrasonic energy is then delivered to the working
medium through booster 1248. The ultrasonic energy traveling
through booster 1248 in reactor volume 1244 creates a series of
compressions and rarefactions in process stream 1216 with an
intensity sufficient to create cavitation in process stream 1216.
Cavitation disaggregates the cellulosic material dispersed in
process stream 1216. Cavitation also produces free radicals in the
water of process stream 1216. These free radicals act to further
break down the cellulosic material in process stream 1216.
[0325] In general, 5 to 4000 MJ/m.sup.3, e.g., 10, 25, 50, 100,
250, 500, 750, 1000, 2000, or 3000 MJ/m.sup.3, of ultrasonic energy
is applied to process stream 16 flowing at a rate of about 0.2
m.sup.3/s (about 3200 gallons/min). After exposure to ultrasonic
energy in reactor volume 1244, process stream 1216 exits flow cell
1224 through outlet 1222. Second pump 1230 moves process stream
1216 to subsequent processing (e.g., any of several recessed
impeller vortex pumps made by Essco Pumps & Controls, Los
Angeles, Calif.).
[0326] While certain embodiments have been described, other
embodiments are possible.
[0327] As an example, while process stream 1216 has been described
as a single flow path, other arrangements are possible. In some
embodiments, for example, process stream 1216 includes multiple
parallel flow paths (e.g., flowing at a rate of 10 gallon/min). In
addition or in the alternative, the multiple parallel flow paths of
process stream 1216 flow into separate flow cells and are sonicated
in parallel (e.g., using a plurality of 16 kW ultrasonic
transducers).
[0328] As another example, while a single ultrasonic transducer
1226 has been described as being coupled to flow cell 1224, other
arrangements are possible. In some embodiments, a plurality of
ultrasonic transducers 1226 are arranged in flow cell 1224 (e.g.,
ten ultrasonic transducers can be arranged in a flow cell 1224). In
some embodiments, the sound waves generated by each of the
plurality of ultrasonic transducers 1226 are timed (e.g.,
synchronized out of phase with one another) to enhance the
cavitation acting upon process stream 1216.
[0329] As another example, while a single flow cell 1224 has been
described, other arrangements are possible. In some embodiments,
second pump 1230 moves process stream to a second flow cell where a
second booster and ultrasonic transducer further sonicate process
stream 1216.
[0330] As still another example, while reactor volume 1244 has been
described as a closed volume, reactor volume 1244 is open to
ambient conditions in certain embodiments. In such embodiments,
sonication pretreatment can be performed substantially
simultaneously with other pretreatment techniques. For example,
ultrasonic energy can be applied to process stream 1216 in reactor
volume 1244 while electron beams are simultaneously introduced into
process stream 1216.
[0331] As another example, while a flow-through process has been
described, other arrangements are possible. In some embodiments,
sonication can be performed in a batch process. For example, a
volume can be filled with a 10% (weight by volume) mixture of
cellulosic material in water and exposed to sound with intensity
from about 50 W/cm.sup.2 to about 600 W/cm.sup.2, e.g., from about
75 W/cm.sup.2 to about 300 W/cm.sup.2 or from about 95 W/cm.sup.2
to about 200 W/cm.sup.2. Additionally or alternatively, the mixture
in the volume can be sonicated from about 1 hour to about 24 hours,
e.g., from about 1.5 hours to about 12 hours, or from about 2 hours
to about 10 hours. In certain embodiments, the material is
sonicated for a pre-determined time, and then allowed to stand for
a second pre-determined time before sonicating again.
[0332] Referring now to FIG. 13, in some embodiments, two
electroacoustic transducers are mechanically coupled to a single
horn. As shown, a pair of piezoelectric transducers 60 and 62 is
coupled to a slotted bar horn 64 by respective intermediate
coupling horns 70 and 72, the latter also being known as booster
horns. The mechanical vibrations provided by the transducers,
responsive to high frequency electrical energy applied thereto, are
transmitted to the respective coupling horns, which may be
constructed to provide a mechanical gain, such as a ratio of 1 to
1.2. The horns are provided with a respective mounting flange 74
and 76 for supporting the transducer and horn assembly in a
stationary housing.
[0333] The vibrations transmitted from the transducers through the
coupling or booster horns are coupled to the input surface 78 of
the horn and are transmitted through the horn to the oppositely
disposed output surface 80, which, during operation, is in forced
engagement with a workpiece (not shown) to which the vibrations are
applied.
[0334] The high frequency electrical energy provided by the power
supply 82 is fed to each of the transducers, electrically connected
in parallel, via a balancing transformer 84 and a respective series
connected capacitor 86 and 90, one capacitor connected in series
with the electrical connection to each of the transducers. The
balancing transformer is known also as "balun" standing for
"balancing unit." The balancing transformer includes a magnetic
core 92 and a pair of identical windings 94 and 96, also termed the
primary winding and secondary winding, respectively.
[0335] In some embodiments, the transducers include commercially
available piezoelectric transducers, such as Branson Ultrasonics
Corporation models 105 or 502, each designed for operation at 20
kHz and a maximum power rating of 3 kW. The energizing voltage for
providing maximum motional excursion at the output surface of the
transducer is 930 volt rms. The current flow through a transducer
may vary between zero and 3.5 ampere depending on the load
impedance. At 930 volt rms the output motion is approximately 20
microns. The maximum difference in terminal voltage for the same
motional amplitude, therefore, can be 186 volt. Such a voltage
difference can give rise to large circulating currents flowing
between the transducers. The balancing unit 430 assures a balanced
condition by providing equal current flow through the transducers,
hence eliminating the possibility of circulating currents. The wire
size of the windings must be selected for the full load current
noted above and the maximum voltage appearing across a winding
input is 93 volt.
[0336] While ultrasonic transducer 1226 has been described as
including one or more piezoelectric active elements to create
ultrasonic energy, other arrangements are possible. In some
embodiments, ultrasonic transducer 1226 includes active elements
made of other types of magnetostrictive materials (e.g., ferrous
metals). Design and operation of such a high-powered ultrasonic
transducer is discussed in Hansen et al., U.S. Pat. No. 6,624,539.
In some embodiments, ultrasonic energy is transferred to process
stream 16 through an electrohydraulic system.
[0337] While ultrasonic transducer 1226 has been described as using
the electromagnetic response of magnetorestrictive materials to
produce ultrasonic energy, other arrangements are possible. In some
embodiments, acoustic energy in the form of an intense shock wave
can be applied directly to process stream 16 using an underwater
spark. In some embodiments, ultrasonic energy is transferred to
process stream 16 through a thermohydraulic system. For example,
acoustic waves of high energy density can be produced by applying
power across an enclosed volume of electrolyte, thereby heating the
enclosed volume and producing a pressure rise that is subsequently
transmitted through a sound propagation medium (e.g., process
stream 1216). Design and operation of such a thermohydraulic
transducer is discussed in Hartmann et al., U.S. Pat. No.
6,383,152.
[0338] Some embodiments use a high frequency, rotor-stator device.
This type of device produces high-shear, microcavitation forces,
which can disintegrate biomass in contact with such forces. Two
commercially available high-frequency, rotor-stator dispersion
devices are the SUPRATON.TM. devices manufactured by Krupp
Industrietechnik GmbH and marketed by Dorr-Oliver Deutschland GmbH
of Connecticut, and the DISPAX.TM. devices manufactured and
marketed by Ika-Works, Inc. of Cincinnati, Ohio. Operation of such
a microcavitation device is discussed in Stuart, U.S. Pat. No.
5,370,999.
[0339] In another biomass disruption technique, microwave or
radiowave energy is applied to a treated or untreated biomass
material, such as a lignocellulosic material, in a manner that
water within the biomass material is vaporized, but overall the
biomass material undergoes little bulk heating. For example, a
frequency of from about 10 MHz to about 300,000 MHz can be applied
to the biomass material. In some instances the microwave or
radiowave energy is applied in short pulses, e.g., having a
duration of less than 0.1 seconds, e.g., less than 0.05 seconds,
less than 0.03 seconds, less than 0.01 seconds or even less, e.g.,
0.005 seconds. Without wishing to be bound by any particular
theory, it is believed when the microwave or radiowave energy is
applied in this manner, water is vaporized within the biomass
material with explosive force, which disrupts the lignin and
"peels" it away from the cellulose. At the same time, since
application of such energy does not heat the bulk material, the
lignin does not tend to re-apply onto the cellulose, which could
block access to the cellulose, e.g., by an enzyme or microbe. Many
of the properties of lignin are described Carter Fox in a thesis
entitled "Chemical and Thermal Characterization of Three Industrial
Lignin and Their Corresponding Esters (May 2006, University of
Idaho).
[0340] In another biomass disruption technique, treated (e.g.,
using any treatment method described herein) or untreated biomass
material is subjected to a hot, compressed fluid, such as water. In
such a method, the biomass is placed in a pressure vessel
containing a fluid, such as water, at an elevated temperature,
e.g., above 50, 60, 70, 80, 90, 100, 110, 120, 130, 140, 150, 160,
170, or above 180.degree. C. The pressure vessel is placed under
gas pressure, such as under argon, nitrogen or air, and then
stirred, e.g., with a two blade turbine propeller for a period of
time, e.g., 10 minutes, 20 minutes, 30 minutes, 45 minutes, 60
minutes or 90 minutes. In some embodiments, the pressure is between
about 500 psig and 2000 psig, e.g., between about 650 psig and
about 1500 psig or between about 700 psig and about 1200 psig. In
some embodiments, the temperature is at or 5 or 10.degree. C. above
a glass transition temperature for the lignin. Without wishing to
be bound by any particular theory, it is believed that when the
temperature is above the glass transition temperature of the
lignin, the conditions in the pressure vessel cause the lignin to
"peel" away from the cellulose, making the cellulose more exposed
for breakdown, e.g., by an enzyme.
[0341] In another biomass disruption technique, treated, e.g.,
irradiated, or untreated biomass material is delivered to a nip
defined between two counter rotating pressure rolls, which can be
optionally heated. Pressure in the nip can be adjusted by the
amount of biomass material fed into the nip and the spacing between
the pressure rolls. In some embodiments, the pressure in the nip
can be greater than 1,000 psi per linear inch, e.g., greater than
2,500 psi, greater than 5,000 psi, greater than 7,500 psi, greater
than 10,000 psi, or even greater than 15,000 psi per linear inch.
In some embodiments, the pressure rolls are operated at an elevated
temperature, e.g., above 50, 60, 70, 80, 90, 100, 110, 120, 130,
140, 150, 160, 170, or above 180.degree. C. In some embodiments,
the rolls are operated at a temperature above a glass transition
temperature of the lignin. Without wishing to be bound by any
particular theory, it is believed that the pressure and heat in the
nip can disrupt any lignin of the biomass material, making the
cellulose more accessible and available to an enzyme.
Pyrolysis
[0342] One or more pyrolysis processing sequences can be used to
process raw feedstock from a wide variety of different sources to
extract useful substances from the feedstock, and to provide
partially degraded organic material which functions as input to
further processing steps and/or sequences.
[0343] Referring again to the general schematic in FIG. 8, a first
material 2 that includes cellulose having a first number average
molecular weight (.sup.TM.sub.n1) is pyrolyzed, e.g., by heating
the first material in a tube furnace, to provide a second material
3 that includes cellulose having a second number average molecular
weight (.sup.TM.sub.n2) lower than the first number average
molecular weight. The second material (or the first and second
material in certain embodiments) is/are combined with a
microorganism (e.g., a bacterium or a yeast) that can utilize the
second and/or first material to produce a fuel 5 that is or
includes hydrogen, an alcohol (e.g., ethanol or butanol, such as
n-, sec or t-butanol), an organic acid, a hydrocarbon or mixtures
of any of these.
[0344] Since the second material has cellulose having a reduced
molecular weight relative to the first material, and in some
instances, a reduced crystallinity as well, the second material is
generally more dispersible, swellable and/or soluble in a solution
containing the microorganism, e.g., at a concentration of greater
than 10.sup.6 microorganisms/mL. These properties make the second
material 3 more susceptible to chemical, enzymatic and/or microbial
attack relative to the first material 2, which can greatly improve
the production rate and/or production level of a desired product,
e.g., ethanol. Pyrolysis can also sterilize the first and second
materials.
[0345] In some embodiments, the second number average molecular
weight (.sup.TM.sub.n2) is lower than the first number average
molecular weight (.sup.TM.sub.n1) by more than about 10 percent,
e.g., 15, 20, 25, 30, 35, 40, 50 percent, 60 percent, or even more
than about 75 percent.
[0346] In some instances, the second material has cellulose that
has as crystallinity (.sup.TC.sub.2) that is lower than the
crystallinity (.sup.TC.sub.1) of the cellulose of the first
material. For example, (.sup.TC.sub.2) can be lower than
(.sup.TC.sub.1) by more than about 10 percent, e.g., 15, 20, 25,
30, 35, 40, or even more than about 50 percent.
[0347] In some embodiments, the starting crystallinity (prior to
pyrolysis) is from about 40 to about 87.5 percent, e.g., from about
50 to about 75 percent or from about 60 to about 70 percent, and
the crystallinity index after pyrolysis is from about 10 to about
50 percent, e.g., from about 15 to about 45 percent or from about
20 to about 40 percent. However, in certain embodiments, e.g.,
after extensive pyrolysis, it is possible to have a crystallinity
index of lower than 5 percent. In some embodiments, the material
after pyrolysis is substantially amorphous.
[0348] In some embodiments, the starting number average molecular
weight (prior to pyrolysis) is from about 200,000 to about
3,200,000, e.g., from about 250,000 to about 1,000,000 or from
about 250,000 to about 700,000, and the number average molecular
weight after pyrolysis is from about 50,000 to about 200,000, e.g.,
from about 60,000 to about 150,000 or from about 70,000 to about
125,000. However, in some embodiments, e.g., after extensive
pyrolysis, it is possible to have a number average molecular weight
of less than about 10,000 or even less than about 5,000.
[0349] In some embodiments, the second material can have a level of
oxidation (.sup.TO.sub.2) that is higher than the level of
oxidation (.sup.TO.sub.1) of the first material. A higher level of
oxidation of the material can aid in its dispersibility,
swellability and/or solubility, further enhancing the materials
susceptibility to chemical, enzymatic or microbial attack. In some
embodiments, to increase the level of the oxidation of the second
material relative to the first material, the pyrolysis is performed
in an oxidizing environment, producing a second material that is
more oxidized than the first material. For example, the second
material can have more hydroxyl groups, aldehyde groups, ketone
groups, ester groups or carboxylic acid groups, which can increase
its hydrophilicity.
[0350] In some embodiments, the pyrolysis of the materials is
continuous. In other embodiments, the material is pyrolyzed for a
pre-determined time, and then allowed to cool for a second
pre-determined time before pyrolyzing again.
Pyrolysis Systems
[0351] FIG. 14 shows a process flow diagram 6000 that includes
various steps in a pyrolytic feedstock pretreatment system. In
first step 6010, a supply of dry feedstock is received from a feed
source.
[0352] As described above, the dry feedstock from the feed source
may be pre-processed prior to delivery to the pyrolysis chamber.
For example, if the feedstock is derived from plant sources,
certain portions of the plant material may be removed prior to
collection of the plant material and/or before the plant material
is delivered by the feedstock transport device. Alternatively, or
in addition, the biomass feedstock can be subjected to mechanical
processing 6020 (e.g., to reduce the average length of fibers in
the feedstock) prior to delivery to the pyrolysis chamber.
[0353] Following mechanical processing, the feedstock undergoes a
moisture adjustment step 6030. The nature of the moisture
adjustment step depends upon the moisture content of the
mechanically processed feedstock. Typically, pyrolysis of feedstock
occurs most efficiently when the moisture content of the feedstock
is between about 10% and about 30% (e.g., between 15% and 25%) by
weight of the feedstock. If the moisture content of the feedstock
is larger than about 40% by weight, the extra thermal load
presented by the water content of the feedstock increases the
energy consumption of subsequent pyrolysis steps.
[0354] In some embodiments, if the feedstock has a moisture content
which is larger than about 30% by weight, drier feedstock material
6220, which has a low moisture content, can be blended in, creating
a feedstock mixture in step 6030 with an average moisture content
that is within the limits discussed above. In certain embodiments,
feedstock with a high moisture content can simply be dried by
dispersing the feedstock material on a moving conveyor that cycles
the feedstock through an in-line heating unit. The heating unit
evaporates a portion of the water present in the feedstock.
[0355] In some embodiments, if the feedstock from step 6020 has a
moisture content which is too low (e.g., lower than about 10% by
weight), the mechanically processed feedstock can be combined with
wetter feedstock material 6230 with a higher moisture content, such
as sewage sludge. Alternatively, or in addition, water 6240 can be
added to the dry feedstock from step 6020 to increase its moisture
content.
[0356] In step 6040, the feedstock--now with its moisture content
adjusted to fall within suitable limits--can be preheated in an
optional preheating step 6040. Preheating step 6040 can be used to
increase the temperature of the feedstock to between 75.degree. C.
and 150.degree. C. in preparation for subsequent pyrolysis of the
feedstock. Depending upon the nature of the feedstock and the
particular design of the pyrolysis chamber, preheating the
feedstock can ensure that heat distribution within the feedstock
remains more uniform during pyrolysis, and can reduce the thermal
load on the pyrolysis chamber.
[0357] The feedstock is then transported to a pyrolysis chamber to
undergo pyrolysis in step 6050. In some embodiments, transport of
the feedstock is assisted by adding one or more pressurized gases
6210 to the feedstock stream. The gases create a pressure gradient
in a feedstock transport conduit, propelling the feedstock into the
pyrolysis chamber (and even through the pyrolysis chamber). In
certain embodiments, transport of the feedstock occurs
mechanically; that is, a transport system that includes a conveyor
such as an auger transports the feedstock to the pyrolysis
chamber.
[0358] Other gases 6210 can also be added to the feedstock prior to
the pyrolysis chamber. In some embodiments, for example, one or
more catalyst gases can be added to the feedstock to assist
decomposition of the feedstock during pyrolysis. In certain
embodiments, one or more scavenging agents can be added to the
feedstock to trap volatile materials released during pyrolysis. For
example, various sulfur-based compounds such as sulfides can be
liberated during pyrolysis, and an agent such as hydrogen gas can
be added to the feedstock to cause desulfurization of the pyrolysis
products. Hydrogen combines with sulfides to form hydrogen sulfide
gas, which can be removed from the pyrolyzed feedstock.
[0359] Pyrolysis of the feedstock within the chamber can include
heating the feedstock to relatively high temperatures to cause
partial decomposition of the feedstock. Typically, the feedstock is
heated to a temperature in a range from 150.degree. C. to
1100.degree. C. The temperature to which the feedstock is heated
depends upon a number of factors, including the composition of the
feedstock, the feedstock average particle size, the moisture
content, and the desired pyrolysis products. For many types of
biomass feedstock, for example, pyrolysis temperatures between
300.degree. C. and 550.degree. C. are used.
[0360] The residence time of the feedstock within the pyrolysis
chamber generally depends upon a number of factors, including the
pyrolysis temperature, the composition of the feedstock, the
feedstock average particle size, the moisture content, and the
desired pyrolysis products. In some embodiments, feedstock
materials are pyrolyzed at a temperature just above the
decomposition temperature for the material in an inert atmosphere,
e.g., from about 2.degree. C. above to about 10.degree. C. above
the decomposition temperature or from about 3.degree. C. above to
about 7.degree. C. above the decomposition temperature. In such
embodiments, the material is generally kept at this temperature for
greater than 0.5 hours, e.g., greater than 1.0 hour or greater than
about 2.0 hours. In other embodiments, the materials are pyrolyzed
at a temperature well above the decomposition temperature for the
material in an inert atmosphere, e.g., from about 75.degree. C.
above to about 175.degree. C. above the decomposition temperature
or from about 85.degree. C. above to about 150.degree. C. above the
decomposition temperature. In such embodiments, the material is
generally kept at this temperature for less than 0.5 hour, e.g.,
less 20 minutes, less than 10 minutes, less than 5 minutes or less
than 2 minutes. In still other embodiments, the materials are
pyrolyzed at an extreme temperature, e.g., from about 200.degree.
C. above to about 500.degree. C. above the decomposition
temperature of the material in an inert environment or from about
250.degree. C. above to about 400.degree. C. above the
decomposition temperature. In such embodiments, the material is
generally kept at this temperature for less than 1 minute, e.g.,
less than 30 seconds, 15 seconds, 10 seconds, 5 seconds, 1 second
or less than 500 ms. Such embodiments are typically referred to as
flash pyrolysis.
[0361] In some embodiments, the feedstock is heated relatively
rapidly to the selected pyrolysis temperature within the chamber.
For example, the chamber can be designed to heat the feedstock at a
rate of between 500.degree. C./s and 11,000.degree. C./s, for
example, from 500.degree. C./s to 1000.degree. C./s.
[0362] A turbulent flow of feedstock material within the pyrolysis
chamber is usually advantageous, as it ensures relatively efficient
heat transfer to the feedstock material from the heating
sub-system. Turbulent flow can be achieved, for example, by blowing
the feedstock material through the chamber using one or more
injected carrier gases 6210. In general, the carrier gases are
relatively inert towards the feedstock material, even at the high
temperatures in the pyrolysis chamber. Exemplary carrier gases
include, for example, nitrogen, argon, methane, carbon monoxide,
and carbon dioxide. Alternatively, or in addition, mechanical
transport systems such as augers can transport and circulate the
feedstock within the pyrolysis chamber to create a turbulent
feedstock flow.
[0363] In some embodiments, pyrolysis of the feedstock occurs
substantially in the absence of oxygen and other reactive gases.
Oxygen can be removed from the pyrolysis chamber by periodic
purging of the chamber with high pressure nitrogen (e.g., at
nitrogen pressures of 2 bar or more). Following purging of the
chamber, a gas mixture present in the pyrolysis chamber (e.g.,
during pyrolysis of the feedstock) can include less than 4 mole %
oxygen (e.g., less than 1 mole % oxygen, and even less than 0.5
mole % oxygen). The absence of oxygen ensures that ignition of the
feedstock does not occur at the elevated pyrolysis
temperatures.
[0364] In certain embodiments, relatively small amounts of oxygen
can be introduced into the feedstock and are present during
pyrolysis. This technique is referred to as oxidative pyrolysis.
Typically, oxidative pyrolysis occurs in multiple heating stages.
For example, in a first heating stage, the feedstock is heated in
the presence of oxygen to cause partial oxidation of the feedstock.
This stage consumes the available oxygen in the pyrolysis chamber.
Then, in subsequent heating stages, the feedstock temperature is
further elevated. With all of the oxygen in the chamber consumed,
however, feedstock combustion does not occur, and combustion-free
pyrolytic decomposition of the feedstock (e.g., to generate
hydrocarbon products) occurs. In general, the process of heating
feedstock in the pyrolysis chamber to initiate decomposition is
endothermic. However, in oxidative pyrolysis, formation of carbon
dioxide by oxidation of the feedstock is an exothermic process. The
heat released from carbon dioxide formation can assist further
pyrolysis heating stages, thereby lessening the thermal load
presented by the feedstock.
[0365] In some embodiments, pyrolysis occurs in an inert
environment, such as while feedstock materials are bathed in argon
or nitrogen gas. In certain embodiments, pyrolysis can occur in an
oxidizing environment, such as in air or argon enriched in air. In
some embodiments, pyrolysis can take place in a reducing
environment, such as while feedstock materials are bathed in
hydrogen gas. To aid pyrolysis, various chemical agents, such as
oxidants, reductants, acids or bases can be added to the material
prior to or during pyrolysis. For example, sulfuric acid can be
added, or a peroxide (e.g., benzoyl peroxide) can be added.
[0366] As discussed above, a variety of different processing
conditions can be used, depending upon factors such as the
feedstock composition and the desired pyrolysis products. For
example, for cellulose-containing feedstock material, relatively
mild pyrolysis conditions can be employed, including flash
pyrolysis temperatures between 375.degree. C. and 450.degree. C.,
and residence times of less than 1 second. As another example, for
organic solid waste material such as sewage sludge, flash pyrolysis
temperatures between 500.degree. C. and 650.degree. C. are
typically used, with residence times of between 0.5 and 3 seconds.
In general, many of the pyrolysis process parameters, including
residence time, pyrolysis temperature, feedstock turbulence,
moisture content, feedstock composition, pyrolysis product
composition, and additive gas composition can be regulated
automatically by a system of regulators and an automated control
system.
[0367] Following pyrolysis step 6050, the pyrolysis products
undergo a quenching step 6250 to reduce the temperature of the
products prior to further processing. Typically, quenching step
6250 includes spraying the pyrolysis products with streams of
cooling water 6260. The cooling water also forms a slurry that
includes solid, undissolved product material and various dissolved
products. Also present in the product stream is a mixture that
includes various gases, including product gases, carrier gases, and
other types of process gases.
[0368] The product stream is transported via in-line piping to a
gas separator that performs a gas separation step 6060, in which
product gases and other gases are separated from the slurry formed
by quenching the pyrolysis products. The separated gas mixture is
optionally directed to a blower 6130, which increases the gas
pressure by blowing air into the mixture. The gas mixture can be
subjected to a filtration step 6140, in which the gas mixture
passes through one or more filters (e.g., activated charcoal
filters) to remove particulates and other impurities. In a
subsequent step 6150, the filtered gas can be compressed and stored
for further use. Alternatively, the filtered gas can be subjected
to further processing steps 6160. For example, in some embodiments,
the filtered gas can be condensed to separate different gaseous
compounds within the gas mixture. The different compounds can
include, for example, various hydrocarbon products (e.g., alcohols,
alkanes, alkenes, alkynes, ethers) produced during pyrolysis. In
certain embodiments, the filtered gas containing a mixture of
hydrocarbon components can be combined with steam gas 6170 (e.g., a
mixture of water vapor and oxygen) and subjected to a cracking
process to reduce molecular weights of the hydrocarbon
components.
[0369] In some embodiments, the pyrolysis chamber includes heat
sources that burn hydrocarbon gases such as methane, propane,
and/or butane to heat the feedstock. A portion 6270 of the
separated gases can be recirculated into the pyrolysis chamber for
combustion, to generate process heat to sustain the pyrolysis
process.
[0370] In certain embodiments, the pyrolysis chamber can receive
process heat that can be used to increase the temperature of
feedstock materials. For example, irradiating feedstock with
radiation (e.g., gamma radiation, electron beam radiation, or other
types of radiation) can heat the feedstock materials to relatively
high temperatures. The heated feedstock materials can be cooled by
a heat exchange system that removes some of the excess heat from
the irradiated feedstock. The heat exchange system can be
configured to transport some of the heat energy to the pyrolysis
chamber to heat (or pre-heat) feedstock material, thereby reducing
energy cost for the pyrolysis process.
[0371] The slurry containing liquid and solid pyrolysis products
can undergo an optional de-watering step 6070, in which excess
water can be removed from the slurry via processes such as
mechanical pressing and evaporation. The excess water 6280 can be
filtered and then recirculated for further use in quenching the
pyrolysis decomposition products in step 6250.
[0372] The de-watered slurry then undergoes a mechanical separation
step 6080, in which solid product material 6110 is separated from
liquid product material 6090 by a series of increasingly fine
filters. In step 6100, the liquid product material 6090 can then be
condensed (e.g., via evaporation) to remove waste water 6190, and
purified by processes such as extraction. Extraction can include
the addition of one or more organic solvents 6180, for example, to
separate products such as oils from products such as alcohols.
Suitable organic solvents include, for example, various
hydrocarbons and halo-hydrocarbons. The purified liquid products
6200 can then be subjected to further processing steps. Waste water
6190 can be filtered if necessary, and recirculated for further use
in quenching the pyrolysis decomposition products in step 6250.
[0373] After separation in step 6080, the solid product material
6110 is optionally subjected to a drying step 6120 that can include
evaporation of water. Solid material 6110 can then be stored for
later use, or subjected to further processing steps, as
appropriate.
[0374] The pyrolysis process parameters discussed above are
exemplary. In general, values of these parameters can vary widely
according to the nature of the feedstock and the desired products.
Moreover, a wide variety of different pyrolysis techniques,
including using heat sources such as hydrocarbon flames and/or
furnaces, infrared lasers, microwave heaters, induction heaters,
resistive heaters, and other heating devices and configurations can
be used.
[0375] A wide variety of different pyrolysis chambers can be used
to decompose the feedstock. In some embodiments, for example,
pyrolyzing feedstock can include heating the material using a
resistive heating member, such as a metal filament or metal ribbon.
The heating can occur by direct contact between the resistive
heating member and the material.
[0376] In certain embodiments, pyrolyzing can include heating the
material by induction, such as by using a Curie-Point pyrolyzer. In
some embodiments, pyrolyzing can include heating the material by
the application of radiation, such as infrared radiation. The
radiation can be generated by a laser, such as an infrared
laser.
[0377] In certain embodiments, pyrolyzing can include heating the
material with a convective heat. The convective heat can be
generated by a flowing stream of heated gas. The heated gas can be
maintained at a temperature of less than about 1200.degree. C.,
such as less than 1000.degree. C., less than 750.degree. C., less
than 600.degree. C., less than 400.degree. C. or even less than
300.degree. C. The heated gas can be maintained at a temperature of
greater than about 250.degree. C. The convective heat can be
generated by a hot body surrounding the first material, such as in
a furnace.
[0378] In some embodiments, pyrolyzing can include heating the
material with steam at a temperature above about 250.degree. C.
[0379] An embodiment of a pyrolysis chamber is shown in FIG. 15.
Chamber 6500 includes an insulated chamber wall 6510 with a vent
6600 for exhaust gases, a plurality of burners 6520 that generate
heat for the pyrolysis process, a transport duct 6530 for
transporting the feedstock through chamber 6500, augers 6590 for
moving the feedstock through duct 6530 in a turbulent flow, and a
quenching system 6540 that includes an auger 6610 for moving the
pyrolysis products, water jets 6550 for spraying the pyrolysis
products with cooling water, and a gas separator for separating
gaseous products 6580 from a slurry 6570 containing solid and
liquid products.
[0380] Another embodiment of a pyrolysis chamber is shown in FIG.
16. Chamber 6700 includes an insulated chamber wall 6710, a
feedstock supply duct 6720, a sloped inner chamber wall 6730,
burners 6740 that generate heat for the pyrolysis process, a vent
6750 for exhaust gases, and a gas separator 6760 for separating
gaseous products 6770 from liquid and solid products 6780. Chamber
6700 is configured to rotate in the direction shown by arrow 6790
to ensure adequate mixing and turbulent flow of the feedstock
within the chamber.
[0381] A further embodiment of a pyrolysis chamber is shown in FIG.
17. Filament pyrolyzer 1712 includes a sample holder 1713 with
resistive heating element 1714 in the form of a wire winding
through the open space defined by the sample holder 1713.
Optionally, the heated element can be spun about axis 1715 (as
indicated by arrow 1716) to tumble the material that includes the
cellulosic material in sample holder 1713. The space 1718 defined
by enclosure 1719 is maintained at a temperature above room
temperature, e.g., 200 to 250.degree. C. In a typical usage, a
carrier gas, e.g., an inert gas, or an oxidizing or reducing gas,
traverses through the sample holder 1713 while the resistive
heating element is rotated and heated to a desired temperature,
e.g., 325.degree. C. After an appropriate time, e.g., 5 to 10
minutes, the pyrolyzed material is emptied from the sample holder.
The system shown in FIG. 17 can be scaled and made continuous. For
example, rather than a wire as the heating member, the heating
member can be an auger screw. Material can continuously fall into
the sample holder, striking a heated screw that pyrolizes the
material. At the same time, the screw can push the pyrolyzed
material out of the sample holder to allow for the entry of fresh,
unpyrolyzed material.
[0382] Another embodiment of a pyrolysis chamber is shown in FIG.
18, which features a Curie-Point pyrolyzer 1820 that includes a
sample chamber 1821 housing a ferromagnetic foil 1822. Surrounding
the sample chamber 1821 is an RF coil 1823. The space 1824 defined
by enclosure 1825 is maintained at a temperature above room
temperature, e.g., 200 to 250.degree. C. In a typical usage, a
carrier gas traverses through the sample chamber 1821 while the
foil 1822 is inductively heated by an applied RF field to pyrolize
the material at a desired temperature.
[0383] Yet another embodiment of a pyrolysis chamber is shown in
FIG. 19. Furnace pyrolyzer 130 includes a movable sample holder 131
and a furnace 132. In a typical usage, the sample is lowered (as
indicated by arrow 137) into a hot zone 135 of furnace 132, while a
carrier gas fills the housing 136 and traverses through the sample
holder 131. The sample is heated to the desired temperature for a
desired time to provide a pyrolyzed product. The pyrolyzed product
is removed from the pyrolyzer by raising the sample holder (as
indicated by arrow 134).
[0384] In certain embodiments, as shown in FIG. 20, a cellulosic
target 140 can be pyrolyzed by treating the target, which is housed
in a vacuum chamber 141, with laser light, e.g., light having a
wavelength of from about 225 nm to about 1500 nm. For example, the
target can be ablated at 266 nm, using the fourth harmonic of a
Nd-YAG laser (Spectra Physics, GCR170, San Jose, Calif.). The
optical configuration shown allows the nearly monochromatic light
143 generated by the laser 142 to be directed using mirrors 144 and
145 onto the target after passing through a lens 146 in the vacuum
chamber 141. Typically, the pressure in the vacuum chamber is
maintained at less than about 10.sup.-6 mm Hg. In some embodiments,
infrared radiation is used, e.g., 1.06 micron radiation from an
Nd-YAG laser. In such embodiments, an infrared sensitive dye can be
combined with the cellulosic material to produce a cellulosic
target. The infrared dye can enhance the heating of the cellulosic
material. Laser ablation is described by Blanchet-Fincher et al.,
in U.S. Pat. No. 5,942,649.
[0385] Referring to FIG. 21, in some embodiments, a cellulosic
material can be flash pyrolyzed by coating a tungsten filament 150,
such as a 5 to 25 mil tungsten filament, with the desired
cellulosic material while the material is housed in a vacuum
chamber 151. To affect pyrolysis, current is passed through the
filament, which causes a rapid heating of the filament for a
desired time. Typically, the heating is continued for seconds
before allowing the filament to cool. In some embodiments, the
heating is performed a number of times to effect the desired amount
of pyrolysis.
[0386] In certain embodiments, carbohydrate-containing biomass
material can be heated in an absence of oxygen in a fluidized bed
reactor. If desired, the carbohydrate containing biomass can have
relatively thin cross-sections, and can include any of the fibrous
materials described herein, for efficient heat transfer. The
material can be heated by thermal transfer from a hot metal or
ceramic, such as glass beads or sand in the reactor, and the
resulting pyrolysis liquid or oil can be transported to a central
refinery for making combustible fuels or other useful products.
[0387] In some embodiments, irradiating the biomass material, e.g.,
with a beam of particles, such as electrons, prior to pyrolysis can
lower the pyrolysis temperature, resulting in less energy being
consumed during pyrolysis.
Oxidation
[0388] One or more oxidative processing sequences can be used to
process raw feedstock from a wide variety of different sources to
extract useful substances from the feedstock, and to provide
partially degraded organic material which functions as input to
further processing steps and/or sequences.
[0389] Referring again to FIG. 8, a first material 2 that includes
cellulose having a first number average molecular weight
(.sup.TM.sub.n1) and having a first oxygen content (.sup.TO.sub.1)
is oxidized, e.g., by heating the first material in a tube furnace
in stream of air or oxygen-enriched air, to provide a second
material 3 that includes cellulose having a second number average
molecular weight (.sup.TM.sub.n2) and having a second oxygen
content (.sup.TO.sub.2) higher than the first oxygen content
(.sup.TO.sub.1). The second material (or the first and second
material in certain embodiments) can be, e.g., combined with a
resin, such as a molten thermoplastic resin or a microorganism, to
provide a composite 4 having desirable mechanical properties, or a
fuel 5
[0390] Such materials can also be combined with a solid and/or a
liquid. For example, the liquid can be in the form of a solution
and the solid can be particulate in form. The liquid and/or solid
can include a microorganism, e.g., a bacterium, and/or an enzyme.
For example, the bacterium and/or enzyme can work on the cellulosic
or lignocellulosic material to produce a fuel, such as ethanol, or
a coproduct, such as a protein. Fuels and coproducts are described
in FIBROUS MATERIALS AND COMPOSITES," U.S. Ser. No. 11/453,951,
filed Jun. 15, 2006. The entire contents of each of the foregoing
applications are incorporated herein by reference.
[0391] In some embodiments, the second number average molecular
weight is not more than 97 percent lower than the first number
average molecular weight, e.g., not more than 95 percent, 90, 85,
80, 75, 70, 65, 60, 55, 50, 45, 40, 30, 20, 12.5, 10.0, 7.5, 5.0,
4.0, 3.0, 2.5, 2.0 or not more than 1.0 percent lower than the
first number average molecular weight. The amount of reduction of
molecular weight will depend upon the application.
[0392] In some embodiments in which the materials are used to make
a fuel or a coproduct, the starting number average molecular weight
(prior to oxidation) is from about 200,000 to about 3,200,000,
e.g., from about 250,000 to about 1,000,000 or from about 250,000
to about 700,000, and the number average molecular weight after
oxidation is from about 50,000 to about 200,000, e.g., from about
60,000 to about 150,000 or from about 70,000 to about 125,000.
However, in some embodiments, e.g., after extensive oxidation, it
is possible to have a number average molecular weight of less than
about 10,000 or even less than about 5,000.
[0393] In some embodiments, the second oxygen content is at least
about five percent higher than the first oxygen content, e.g., 7.5
percent higher, 10.0 percent higher, 12.5 percent higher, 15.0
percent higher or 17.5 percent higher. In some preferred
embodiments, the second oxygen content is at least about 20.0
percent higher than the oxygen content of the first material.
Oxygen content is measured by elemental analysis by pyrolyzing a
sample in a furnace operating 1300.degree. C. or higher. A suitable
elemental analyzer is the LECO CHNS-932 analyzer with a VTF-900
high temperature pyrolysis furnace.
[0394] In some embodiments, oxidation of first material 200 does
not result in a substantial change in the crystallinity of the
cellulose. However, in some instances, e.g., after extreme
oxidation, the second material has cellulose that has as
crystallinity (.sup.TC.sub.2) that is lower than the crystallinity
(.sup.TC.sub.1) of the cellulose of the first material. For
example, (.sup.TC.sub.2) can be lower than (.sup.TC.sub.1) by more
than about 5 percent, e.g., 10, 15, 20, or even 25 percent. This
can be desirable to enhance solubility of the materials in a
liquid, such as a liquid that includes a bacterium and/or an
enzyme.
[0395] In some embodiments, the starting crystallinity index (prior
to oxidation) is from about 40 to about 87.5 percent, e.g., from
about 50 to about 75 percent or from about 60 to about 70 percent,
and the crystallinity index after oxidation is from about 30 to
about 75.0 percent, e.g., from about 35.0 to about 70.0 percent or
from about 37.5 to about 65.0 percent. However, in certain
embodiments, e.g., after extensive oxidation, it is possible to
have a crystallinity index of lower than 5 percent. In some
embodiments, the material after oxidation is substantially
amorphous.
[0396] Without wishing to be bound by any particular theory, it is
believed that oxidation increases the number of hydrogen-bonding
groups on the cellulose, such as hydroxyl groups, aldehyde groups,
ketone groups carboxylic acid groups or anhydride groups, which can
increase its dispersibility and/or its solubility (e.g., in a
liquid). To further improve dispersibility in a resin, the resin
can include a component that includes hydrogen-bonding groups, such
as one or more anhydride groups, carboxylic acid groups, hydroxyl
groups, amide groups, amine groups or mixtures of any of these
groups. In some preferred embodiments, the component includes a
polymer copolymerized with and/or grafted with maleic anhydride.
Such materials are available from Dupont under the tradename
FUSABOND.RTM..
[0397] Generally, oxidation of first material 200 occurs in an
oxidizing environment. For example, the oxidation can be effected
or aided by pyrolysis in an oxidizing environment, such as in air
or argon enriched in air. To aid in the oxidation, various chemical
agents, such as oxidants, acids or bases can be added to the
material prior to or during oxidation. For example, a peroxide
(e.g., benzoyl peroxide) can be added prior to oxidation.
Oxidation Systems
[0398] FIG. 22 shows a process flow diagram 5000 that includes
various steps in an oxidative feedstock pretreatment system. In
first step 5010, a supply of dry feedstock is received from a feed
source. The feed source can include, for example, a storage bed or
container that is connected to an in-line oxidation reactor via a
conveyor belt or another feedstock transport device.
[0399] As described above, the dry feedstock from the feed source
may be pre-processed prior to delivery to the oxidation reactor.
For example, if the feedstock is derived from plant sources,
certain portions of the plant material may be removed prior to
collection of the plant material and/or before the plant material
is delivered by the feedstock transport device. Alternatively, or
in addition, the biomass feedstock can be subjected to mechanical
processing (e.g., to reduce the average length of fibers in the
feedstock) prior to delivery to the oxidation reactor.
[0400] Following mechanical processing 5020, feedstock 5030 is
transported to a mixing system which introduces water 5150 into the
feedstock in a mechanical mixing process. Combining water with the
processed feedstock in mixing step 5040 creates an aqueous
feedstock slurry 5050, which can then be treated with one or more
oxidizing agents.
[0401] Typically, one liter of water is added to the mixture for
every 0.02 kg to 1.0 kg of dry feedstock. The ratio of feedstock to
water in the mixture depends upon the source of the feedstock and
the specific oxidizing agents used further downstream in the
overall process. For example, in typical industrial processing
sequences for lignocellulosic biomass, aqueous feedstock slurry
5050 includes from about 0.5 kg to about 1.0 kg of dry biomass per
liter of water.
[0402] In some embodiments, one or more fiber-protecting additives
5170 can also be added to the feedstock slurry in feedstock mixing
step 5040. Fiber-protecting additives help to reduce degradation of
certain types of biomass fibers (e.g., cellulose fibers) during
oxidation of the feedstock. Fiber-protecting additives can be used,
for example, if a desired product from processing a lignocellulosic
feedstock includes cellulose fibers. Exemplary fiber-protecting
additives include magnesium compounds such as magnesium hydroxide.
Concentrations of fiber-protecting additives in feedstock slurry
5050 can be from 0.1% to 0.4% of the dry weight of the biomass
feedstock, for example.
[0403] In certain embodiments, aqueous feedstock slurry 5050 can be
subjected to an optional extraction 5180 with an organic solvent to
remove water-insoluble substances from the slurry. For example,
extraction of slurry 5050 with one or more organic solvents yields
a purified slurry and an organic waste stream 5210 that includes
water-insoluble materials such as fats, oils, and other non-polar,
hydrocarbon-based substances. Suitable solvents for performing
extraction of slurry 5050 include various alcohols, hydrocarbons,
and halo-hydrocarbons, for example.
[0404] In some embodiments, aqueous feedstock slurry 5050 can be
subjected to an optional thermal treatment 5190 to further prepare
the feedstock for oxidation. An example of a thermal treatment
includes heating the feedstock slurry in the presence of
pressurized steam. In fibrous biomass feedstock, the pressurized
steam swells the fibers, exposing a larger fraction of fiber
surfaces to the aqueous solvent and to oxidizing agents that are
introduced in subsequent processing steps.
[0405] In certain embodiments, aqueous feedstock slurry 5050 can be
subjected to an optional treatment with basic agents 5200.
Treatment with one or more basic agents can help to separate lignin
from cellulose in lignocellulosic biomass feedstock, thereby
improving subsequent oxidation of the feedstock. Exemplary basic
agents include alkali and alkaline earth hydroxides such as sodium
hydroxide, potassium hydroxide, and calcium hydroxide. In general,
a variety of basic agents can be used, typically in concentrations
from about 0.01% to about 0.5% of the dry weight of the
feedstock.
[0406] Aqueous feedstock slurry 5050 is transported (e.g., by an
in-line piping system) to a chamber, which can be an oxidation
preprocessing chamber or an oxidation reactor. In oxidation
preprocessing step 5060, one or more oxidizing agents 5160 are
added to feedstock slurry 5050 to form an oxidizing medium. In some
embodiments, for example, oxidizing agents 5160 can include
hydrogen peroxide. Hydrogen peroxide can be added to slurry 5050 as
an aqueous solution, and in proportions ranging from 3% to between
30% and 35% by weight of slurry 5050. Hydrogen peroxide has a
number of advantages as an oxidizing agent. For example, aqueous
hydrogen peroxide solution is relatively inexpensive, is relatively
chemically stable, and is not particularly hazardous relative to
other oxidizing agents (and therefore does not require burdensome
handling procedures and expensive safety equipment). Moreover,
hydrogen peroxide decomposes to form water during oxidation of
feedstock, so that waste stream cleanup is relatively
straightforward and inexpensive.
[0407] In certain embodiments, oxidizing agents 5160 can include
oxygen (e.g., oxygen gas) either alone, or in combination with
hydrogen peroxide. Oxygen gas can be bubbled into slurry 5050 in
proportions ranging from 0.5% to 10% by weight of slurry 5050.
Alternatively, or in addition, oxygen gas can also be introduced
into a gaseous phase in equilibrium with slurry 5050 (e.g., a vapor
head above slurry 5050). The oxygen gas can be introduced into
either an oxidation preprocessing chamber or into an oxidation
reactor (or into both), depending upon the configuration of the
oxidative processing system. Typically, for example, the partial
pressure of oxygen in the vapor above slurry 5050 is larger than
the ambient pressure of oxygen, and ranges from 0.5 bar to 35 bar,
depending upon the nature of the feedstock.
[0408] The oxygen gas can be introduced in pure form, or can be
mixed with one or more carrier gases. For example, in some
embodiments, high-pressure air provides the oxygen in the vapor. In
certain embodiments, oxygen gas can be supplied continuously to the
vapor phase to ensure that a concentration of oxygen in the vapor
remains within certain predetermined limits during processing of
the feedstock. In some embodiments, oxygen gas can be introduced
initially in sufficient concentration to oxidize the feedstock, and
then the feedstock can be transported to a closed, pressurized
vessel (e.g., an oxidation reactor) for processing.
[0409] In certain embodiments, oxidizing agents 5160 can include
nascent oxygen (e.g., oxygen radicals). Typically, nascent oxygen
is produced as needed in an oxidation reactor or in a chamber in
fluid communication with an oxidation reactor by one or more
decomposition reactions. For example, in some embodiments, nascent
oxygen can be produced from a reaction between NO and O.sub.2 in a
gas mixture or in solution. In certain embodiments, nascent oxygen
can be produced from decomposition of HOCl in solution. Other
methods by which nascent oxygen can be produced include via
electrochemical generation in electrolyte solution, for
example.
[0410] In general, nascent oxygen is an efficient oxidizing agent
due to the relatively high reactivity of the oxygen radical.
However, nascent oxygen can also be a relatively selective
oxidizing agent. For example, when lignocellulosic feedstock is
treated with nascent oxygen, selective oxidation of lignin occurs
in preference to the other components of the feedstock such as
cellulose. As a result, oxidation of feedstock with nascent oxygen
provides a method for selective removal of the lignin fraction in
certain feedstocks. Typically, nascent oxygen concentrations of
between about 0.5% and 5% of the dry weight of the feedstock are
used to effect efficient oxidation.
[0411] Without wishing to be bound by theory, it is believed that
nascent oxygen reacts with lignocellulosic feedstock according to
at least two different mechanisms. In a first mechanism, nascent
oxygen undergoes an addition reaction with the lignin, resulting in
partial oxidation of the lignin, which solubilizes the lignin in
aqueous solution. As a result, the solubilized lignin can be
removed from the rest of the feedstock via washing. In a second
mechanism, nascent oxygen disrupts butane cross-links and/or opens
aromatic rings that are connected via the butane cross-links. As a
result, solubility of the lignin in aqueous solution increases,
facilitating separation of the lignin fraction from the remainder
of the feedstock via washing.
[0412] In some embodiments, oxidizing agents 5160 include ozone
(03). The use of ozone can introduce several chemical handling
considerations in the oxidation processing sequence. If heated too
vigorously, an aqueous solution of ozone can decompose violently,
with potentially adverse consequences for both human system
operators and system equipment. Accordingly, ozone is typically
generated in a thermally isolated, thick-walled vessel separate
from the vessel that contains the feedstock slurry, and transported
thereto at the appropriate process stage.
[0413] Without wishing to be bound by theory, it is believed that
ozone decomposes into oxygen and oxygen radicals, and that the
oxygen radicals (e.g., nascent oxygen) are responsible for the
oxidizing properties of ozone in the manner discussed above. Ozone
typically preferentially oxidizes the lignin fraction in
lignocellulosic materials, leaving the cellulose fraction
relatively undisturbed.
[0414] Conditions for ozone-based oxidation of biomass feedstock
generally depend upon the nature of the biomass. For example, for
cellulosic and/or lignocellulosic feedstocks, ozone concentrations
of from 0.1 g/m.sup.3 to 20 g/m.sup.3 of dry feedstock provide for
efficient feedstock oxidation. Typically, the water content in
slurry 5050 is between 10% by weight and 80% by weight (e.g.,
between 40% by weight and 60% by weight). During ozone-based
oxidation, the temperature of slurry 5050 can be maintained between
0.degree. C. and 100.degree. C. to avoid violent decomposition of
the ozone.
[0415] In some embodiments, feedstock slurry 5050 can be treated
with an aqueous, alkaline solution that includes one or more alkali
and alkaline earth hydroxides such as sodium hydroxide, potassium
hydroxide, and calcium hydroxide, and then treated thereafter with
an ozone-containing gas in an oxidation reactor. This process has
been observed to significantly increase decomposition of the
biomass in slurry 5050. Typically, for example, a concentration of
hydroxide ions in the alkaline solution is between 0.001% and 10%
by weight of slurry 5050. After the feedstock has been wetted via
contact with the alkaline solution, the ozone-containing gas is
introduced into the oxidation reactor, where it contacts and
oxidizes the feedstock.
[0416] Oxidizing agents 5160 can also include other substances. In
some embodiments, for example, halogen-based oxidizing agents such
as chlorine and oxychlorine agents (e.g., hypochlorite) can be
introduced into slurry 5050. In certain embodiments,
nitrogen-containing oxidizing substances can be introduced into
slurry 5050. Exemplary nitrogen-containing oxidizing substances
include NO and NO.sub.2, for example. Nitrogen-containing agents
can also be combined with oxygen in slurry 5050 to create
additional oxidizing agents. For example, NO and NO.sub.2 both
combine with oxygen in slurry 5050 to form nitrate compounds, which
are effective oxidizing agents for biomass feedstock. Halogen- and
nitrogen-based oxidizing agents can, in some embodiments, cause
bleaching of the biomass feedstock, depending upon the nature of
the feedstock. The bleaching may be desirable for certain
biomass-derived products that are extracted in subsequent
processing steps.
[0417] Other oxidizing agents can include, for example, various
peroxyacids, peroxyacetic acids, persulfates, percarbonates,
permanganates, osmium tetroxide, and chromium oxides.
[0418] Following oxidation preprocessing step 5060, feedstock
slurry 5050 is oxidized in step 5070. If oxidizing agents 5160 were
added to slurry 5050 in an oxidation reactor, then oxidation
proceeds in the same reactor. Alternatively, if oxidizing agents
5160 were added to slurry 5050 in a preprocessing chamber, then
slurry 5050 is transported to an oxidation reactor via an in-line
piping system. Once inside the oxidation reactor, oxidation of the
biomass feedstock proceeds under a controlled set of environmental
conditions. Typically, for example, the oxidation reactor is a
cylindrical vessel that is closed to the external environment and
pressurized. Both batch and continuous operation is possible,
although environmental conditions are typically easier to control
in in-line batch processing operations.
[0419] Oxidation of feedstock slurry 5050 typically occurs at
elevated temperatures in the oxidation reactor. For example, the
temperature of slurry 5050 in the oxidation reactor is typically
maintained above 100.degree. C., e.g., in a range from 120.degree.
C. to 240.degree. C. For many types of biomass feedstock, oxidation
is particularly efficient if the temperature of slurry 5050 is
maintained between 150.degree. C. and 220.degree. C. Slurry 5050
can be heating using a variety of thermal transfer devices. For
example, in some embodiments, the oxidation reactor contacts a
heating bath that includes oil or molten salts. In certain
embodiments, a series of heat exchange pipes surround and contact
the oxidation reactor, and circulation of hot fluid within the
pipes heats slurry 5050 in the reactor. Other heating devices that
can be used to heat slurry 5050 include resistive heating elements,
induction heaters, and microwave sources, for example.
[0420] The residence time of feedstock slurry 5050 in the oxidation
reactor can be varied as desired to process the feedstock.
Typically, slurry 5050 spends from 1 minute to 60 minutes
undergoing oxidation in the reactor. For relatively soft biomass
material such as lignocellulosic matter, the residence time in the
oxidation reactor can be from 5 minutes to 30 minutes, for example,
at an oxygen pressure of between 3 and 12 bars in the reactor, and
at a slurry temperature of between 160.degree. C. and 210.degree.
C. For other types of feedstock, however, residence times in the
oxidation reactor can be longer, e.g., as long 48 hours. To
determine appropriate residence times for slurry 5050 in the
oxidation reactor, aliquots of the slurry can be extracted from the
reactor at specific intervals and analyzed to determine
concentrations of particular products of interest such as complex
saccharides. Information about the increase in concentrations of
certain products in slurry 5050 as a function of time can be used
to determine residence times for particular classes of feedstock
material.
[0421] In some embodiments, during oxidation of feedstock slurry
5050, adjustment of the slurry pH may be performed by introducing
one or more chemical agents into the oxidation reactor. For
example, in certain embodiments, oxidation occurs most efficiently
in a pH range of about 9-11. To maintain a pH in this range, agents
such as alkali and alkaline earth hydroxides, carbonates, ammonia,
and alkaline buffer solutions can be introduced into the oxidation
reactor.
[0422] Circulation of slurry 5050 during oxidation can be important
to ensure sufficient contact between oxidizing agents 5160 and the
feedstock. Circulation of the slurry can be achieved using a
variety of techniques. For example, in some embodiments, a
mechanical stirring apparatus that includes impeller blades or a
paddle wheel can be implemented in the oxidation reactor. In
certain embodiments, the oxidation reactor can be a loop reactor,
in which the aqueous solvent in which the feedstock is suspended is
simultaneously drained from the bottom of the reactor and
recirculated into the top of the reactor via pumping, thereby
ensuring that the slurry is continually re-mixed and does not
stagnate within the reactor.
[0423] After oxidation of the feedstock is complete, the slurry is
transported to a separation apparatus where a mechanical separation
step 5080 occurs. Typically, mechanical separation step 5080
includes one or more stages of increasingly fine filtering of the
slurry to mechanically separate the solid and liquid
constituents.
[0424] Liquid phase 5090 is separated from solid phase 5100, and
the two phases are processed independently thereafter. Solid phase
5100 can optionally undergo a drying step 5120 in a drying
apparatus, for example. Drying step 5120 can include, for example,
mechanically dispersing the solid material onto a drying surface,
and evaporating water from solid phase 5100 by gentle heating of
the solid material. Following drying step 5120 (or, alternatively,
without undergoing drying step 5120), solid phase 5100 is
transported for further processing steps 5140.
[0425] Liquid phase 5090 can optionally undergo a drying step 5110
to reduce the concentration of water in the liquid phase. In some
embodiments, for example, drying step 5110 can include evaporation
and/or distillation and/or extraction of water from liquid phase
5090 by gentle heating of the liquid. Alternatively, or in
addition, one or more chemical drying agents can be used to remove
water from liquid phase 5090. Following drying step 5110 (or
alternatively, without undergoing drying step 5110), liquid phase
5090 is transported for further processing steps 5130, which can
include a variety of chemical and biological treatment steps such
as chemical and/or enzymatic hydrolysis.
[0426] Drying step 5110 creates waste stream 5220, an aqueous
solution that can include dissolved chemical agents such as acids
and bases in relatively low concentrations. Treatment of waste
stream 5220 can include, for example, pH neutralization with one or
more mineral acids or bases. Depending upon the concentration of
dissolved salts in waste stream 5220, the solution may be partially
de-ionized (e.g., by passing the waste stream through an ion
exchange system). Then, the waste stream--which includes primarily
water--can be re-circulated into the overall process (e.g., as
water 5150), diverted to another process, or discharged.
[0427] Typically, for lignocellulosic biomass feedstocks following
separation step 5070, liquid phase 5090 includes a variety of
soluble poly- and oligosaccharides, which can then be separated
and/or reduced to smaller-chain saccharides via further processing
steps. Solid phase 5100 typically includes primarily cellulose, for
example, with smaller amounts of hemicellulose- and lignin-derived
products.
[0428] In some embodiments, oxidation can be carried out at
elevated temperature in a reactor such as a pyrolysis chamber. For
example, referring again to FIG. 17, feedstock materials can be
oxidized in filament pyrolyzer 1712. In a typical usage, an
oxidizing carrier gas, e.g., air or an air/argon blend, traverses
through the sample holder 1713 while the resistive heating element
is rotated and heated to a desired temperature, e.g., 325.degree.
C. After an appropriate time, e.g., 5 to 10 minutes, the oxidized
material is emptied from the sample holder. The system shown in
FIG. 17 can be scaled and made continuous. For example, rather than
a wire as the heating member, the heating member can be an auger
screw. Material can continuously fall into the sample holder,
striking a heated screw that pyrolizes the material. At the same
time, the screw can push the oxidized material out of the sample
holder to allow for the entry of fresh, unoxidized material.
[0429] Feedstock materials can also be oxidized in any of the
pyrolysis systems shown in FIGS. 18-20 and described above in the
Pyrolysis Systems section.
[0430] Referring again to FIG. 21, feedstock materials can be
rapidly oxidized by coating a tungsten filament 150, together with
an oxidant, such as a peroxide, with the desired cellulosic
material while the material is housed in a vacuum chamber 151. To
affect oxidation, current is passed through the filament, which
causes a rapid heating of the filament for a desired time.
Typically, the heating is continued for seconds before allowing the
filament to cool. In some embodiments, the heating is performed a
number of times to effect the desired amount of oxidation.
[0431] Referring again to FIG. 12, in some embodiments, feedstock
materials can be oxidized with the aid of sound and/or cavitation.
Generally, to effect oxidation, the materials are sonicated in an
oxidizing environment, such as water saturated with oxygen or
another chemical oxidant, such as hydrogen peroxide.
[0432] Referring again to FIGS. 9 and 10, in certain embodiments,
ionizing radiation is used to aid in the oxidation of feedstock
materials. Generally, to effect oxidation, the materials are
irradiated in an oxidizing environment, such as air or oxygen. For
example, gamma radiation and/or electron beam radiation can be
employed to irradiate the materials.
Other Processes
[0433] Steam explosion can be used alone without any of the
processes described herein, or in combination with any one or more
of the processes described herein.
[0434] FIG. 23 shows an overview of the entire process of
converting a fiber source or feedstock 400 into a product 450, such
as ethanol, by a process that includes shearing and steam explosion
to produce a fibrous material 401, which is then hydrolyzed and
converted, e.g., fermented, to produce the product. The fiber
source can be transformed into the fibrous material 401 through a
number of possible methods, including at least one shearing process
and at least one steam explosion process.
[0435] For example, one option includes shearing the fiber source,
followed by optional screening step(s) and optional additional
shearing step(s) to produce a sheared fiber source 402, which can
then be steam exploded to produce the fibrous material 401. The
steam explosion process is optionally followed by a fiber recovery
process to remove liquids or the "liquor" 404, resulting from the
steam exploding process. The material resulting from steam
exploding the sheared fiber source may be further sheared by
optional additional shearing step(s) and/or optional screening
step(s).
[0436] In another method, the fibrous material 401 is first steam
exploded to produce a steam exploded fiber source 410. The
resulting steam exploded fiber source is then subjected to an
optional fiber recovery process to remove liquids, or the liquor.
The resulting steam exploded fiber source can then be sheared to
produce the fibrous material. The steam exploded fiber source can
also be subject to one or more optional screening steps and/or one
or more optional additional shearing steps. The process of shearing
and steam exploding the fiber source to produce the sheared and
steam exploded fibrous material will be further discussed
below.
[0437] The fiber source can be cut into pieces or strips of
confetti material prior to shearing or steam explosion. The
shearing processes can take place with the material in a dry state
(e.g., having less than 0.25 percent by weight absorbed water), a
hydrated state, or even while the material is partially or fully
submerged in a liquid, such as water or isopropanol. The process
can also optimally include steps of drying the output after steam
exploding or shearing to allow for additional steps of dry shearing
or steam exploding. The steps of shearing, screening, and steam
explosion can take place with or without the presence of various
chemical solutions.
[0438] In a steam explosion process, the fiber source or the
sheared fiber source is contacted with steam under high pressure,
and the steam diffuses into the structures of the fiber source
(e.g., the lignocellulosic structures). The steam then condenses
under high pressure thereby "wetting" the fiber source. The
moisture in the fiber source can hydrolyze any acetyl groups in the
fiber source (e.g., the acetyl groups in the hemicellulose
fractions), forming organic acids such as acetic and uronic acids.
The acids, in turn, can catalyze the depolymerization of
hemicellulose, releasing xylan and limited amounts of glucan. The
"wet" fiber source (or sheared fiber source, etc.) is then
"exploded" when the pressure is released. The condensed moisture
instantaneously evaporates due to the sudden decrease in pressure
and the expansion of the water vapor exerts a shear force upon the
fiber source (or sheared fiber source, etc.). A sufficient shear
force will cause the mechanical breakdown of the internal
structures (e.g., the lignocellulosic structures) of the fiber
source.
[0439] The sheared and steam exploded fibrous material is then
converted into a useful product, such as ethanol. In some
embodiments, the fibrous material is converted into a fuel. One
method of converting the fibrous material into a fuel is by
hydrolysis to produce fermentable sugars, 412, which are then
fermented to produce the product. Other methods of converting
fibrous materials into fuels may also be used.
[0440] In some embodiments, prior to combining with the
microorganism, the sheared and steam exploded fibrous material 401
is sterilized to kill any competing microorganisms that may be on
the fibrous material. For example, the fibrous material can be
sterilized by exposing the fibrous material to radiation, such as
infrared radiation, ultraviolet radiation, or an ionizing
radiation, such as gamma radiation. The microorganisms can also be
killed using chemical sterilants, such as bleach (e.g., sodium
hypochlorite), chlorhexidine, or ethylene oxide.
[0441] One method to hydrolyze the sheared and steam exploded
fibrous material is by the use of cellulases. Cellulases are a
group of enzymes that act synergistically to hydrolyze cellulose.
Commercially available Accellerase.RTM. 1000 enzyme complex, which
contains a complex of enzymes that reduces lignocellulosic biomass
into fermentable sugars, can also be used.
[0442] According to current understanding, the components of
cellulase include endoglucanases, exoglucanases
(cellobiohydrolases), and b-glucosidases (cellobiases). Synergism
between the cellulase components exists when hydrolysis by a
combination of two or more components exceeds the sum of the
activities expressed by the individual components. The generally
accepted mechanism of action of a cellulase system (particularly of
T. longibrachiatum) on crystalline cellulose is that endoglucanase
hydrolyzes internal .beta.-1,4-glycosidic bonds of the amorphous
regions, thereby increasing the number of exposed non-reducing
ends. Exoglucanases then cleave off cellobiose units from the
non-reducing ends, which in turn are hydrolyzed to individual
glucose units by b-glucosidases. There are several configurations
of both endo- and exoglucanases differing in stereospecificities.
In general, the synergistic action of the components in various
configurations is required for optimum cellulose hydrolysis.
Cellulases, however, are more inclined to hydrolyze the amorphous
regions of cellulose. A linear relationship between crystallinity
and hydrolysis rates exists whereby higher crystallinity indices
correspond to slower enzyme hydrolysis rates. Amorphous regions of
cellulose hydrolyze at twice the rate of crystalline regions. The
hydrolysis of the sheared and steam exploded fibrous material may
be performed by any hydrolyzing biomass process.
[0443] Steam explosion of biomass sometimes causes the formation of
by-products, e.g., toxicants, that are inhibitory to microbial and
enzymatic activities. The process of converting the sheared and
steam exploded fibrous material into a fuel can therefore
optionally include an overliming step prior to fermentation to
precipitate some of the toxicants. For example, the pH of the
sheared and steam exploded fibrous material may be raised to exceed
the pH of 10 by adding calcium hydroxide (Ca(OH).sub.2) followed by
a step of lowering the pH to about 5 by adding H.sub.2SO.sub.4. The
overlimed fibrous material may then be used as is without the
removal of precipitates. As shown in FIG. 23, the optional
overliming step occurs just prior to the step of hydrolysis of the
sheared and steam exploded fibrous material, but it is also
contemplated to perform the overliming step after the hydrolysis
step and prior to the fermenting step.
[0444] FIG. 24 depicts an example of a steam explosion apparatus
460. The steam explosion apparatus 460 includes a reaction chamber
462, in which the fiber source and/or the fibrous material is
placed through a fiber source inlet 464. The reaction chamber is
sealed by closing fiber source inlet valve 465. The reaction
chamber further includes a pressurized steam inlet 466 that
includes a steam valve 467. The reaction chamber further includes
an explosive depressurization outlet 468 that includes an outlet
valve 469 in communication with the cyclone 470 through the
connecting pipe 472. Once the reaction chamber contains the fiber
source and/or sheared fiber source and is sealed by closing valves
465, 467 and 469, steam is delivered into the reaction chamber 462
by opening the steam inlet valve 467 allowing steam to travel
through steam inlet 466. Once the reaction chamber reaches target
temperature, which can take about 20-60 seconds, the holding time
begins. The reaction chamber is held at the target temperature for
the desired holding time, which typically lasts from about 10
seconds to 5 minutes. At the end of the holding time period, outlet
valve is opened to allow for explosive depressurization to occur.
The process of explosive depressurization propels the contents of
the reaction chamber 462 out of the explosive depressurization
outlet 468, through the connecting pipe 472, and into the cyclone
470. The steam exploded fiber source or fibrous material then exits
the cyclone in a sludge form into the collection bin 474 as much of
the remaining steam exits the cyclone into the atmosphere through
vent 476. The steam explosion apparatus further includes wash
outlet 478 with wash outlet valve 479 in communication with
connecting pipe 472. The wash outlet valve 479 is closed during the
use of the steam explosion apparatus 460 for steam explosion, but
opened during the washing of the reaction chamber 462.
[0445] The target temperature of the reaction chamber 462 is
preferably between 180 and 240 degrees Celsius or between 200 and
220 degrees Celsius. The holding time is preferably between 10
seconds and 30 minutes, or between 30 seconds and 10 minutes, or
between 1 minute and 5 minutes.
[0446] Because the steam explosion process results in a sludge of
steam exploded fibrous material, the steam exploded fibrous
material may optionally include a fiber recovery process where the
"liquor" is separated from the steam exploded fibrous material.
This fiber recovery step is helpful in that it enables further
shearing and/or screening processes and can allow for the
conversion of the fibrous material into fuel. The fiber recovery
process occurs through the use of a mesh cloth to separate the
fibers from the liquor. Further drying processes can also be
included to prepare the fibrous material or steam exploded fiber
source for subsequent processing.
Combined Irradiating, Pyrolyzing, Sonicating, and/or Oxidizing
Devices
[0447] In some embodiments, it may be advantageous to combine two
or more separate irradiation, sonication, pyrolization, and/or
oxidation devices into a single hybrid machine. Using such a hybrid
machine, multiple processes may be performed in close juxtaposition
or even simultaneously, with the benefit of increasing pretreatment
throughput and potential cost savings.
[0448] For example, consider the electron beam irradiation and
sonication processes. Each separate process is effective in
lowering the mean molecular weight of cellulosic material by an
order of magnitude or more, and by several orders of magnitude when
performed serially.
[0449] Both irradiation and sonication processes can be applied
using a hybrid electron beam/sonication device as is illustrated in
FIG. 25. Hybrid electron beam/sonication device 2500 is pictured
above a shallow pool (depth .about.3-5 cm) of a slurry of
cellulosic material 2550 dispersed in an aqueous, oxidant medium,
such as hydrogen peroxide or carbamide peroxide. Hybrid device 2500
has an energy source 2510, which powers both electron beam emitter
2540 and sonication horns 2530.
[0450] Electron beam emitter 2540 generates electron beams, which
pass through an electron beam aiming device 2545 to impact the
slurry 2550 containing cellulosic material. The electron beam
aiming device can be a scanner that sweeps a beam over a range of
up to about 6 feet in a direction approximately parallel to the
surface of the slurry 2550.
[0451] On either side of the electron beam emitter 2540 are
sonication horns 2530, which deliver ultrasonic wave energy to the
slurry 2550. The sonication horns 2530 end in a detachable endpiece
2535 that is in contact with the slurry 2550.
[0452] The sonication horns 2530 are at risk of damage from
long-term residual exposure to the electron beam radiation. Thus,
the horns can be protected with a standard shield 2520, e.g., made
of lead or a heavy-metal-containing alloy such as Lipowitz metal,
which is impervious to electron beam radiation. Precautions must be
taken, however, to ensure that the ultrasonic energy is not
affected by the presence of the shield. The detachable endpieces
2535, which are constructed of the same material and attached to
the horns 2530, are in contact with the cellulosic material 2550
during processing and are expected to be damaged. Accordingly, the
detachable endpieces 2535 are constructed to be easily
replaceable.
[0453] A further benefit of such a simultaneous electron beam and
ultrasound process is that the two processes have complementary
results. With electron beam irradiation alone, an insufficient dose
may result in cross-linking of some of the polymers in the
cellulosic material, which lowers the efficiency of the overall
depolymerization process. Lower doses of electron beam irradiation
and/or ultrasound radiation may also be used to achieve a similar
degree of depolymerization as that achieved using electron beam
irradiation and sonication separately. An electron beam device can
also be combined with one or more of high frequency, rotor-stator
devices, which can be used as an alternative to ultrasonic
sonication devices.
[0454] Further combinations of devices are also possible. For
example, an ionizing radiation device that produces gamma radiation
emitted from, e.g., .sup.60Co pellets, can be combined with an
electron beam source and/or an ultrasonic wave source. Shielding
requirements may be more stringent in this case.
[0455] The radiation devices for pretreating biomass discussed
above can also be combined with one or more devices that perform
one or more pyrolysis processing sequences. Such a combination may
again have the advantage of higher throughput. Nevertheless,
caution must be observed, as there may be conflicting requirements
between some radiation processes and pyrolysis. For example,
ultrasonic radiation devices may require the feedstock be immersed
in a liquid oxidizing medium. On the other hand, as discussed
previously, it may be advantageous for a sample of feedstock
undergoing pyrolysis to be of a particular moisture content. In
this case, the new systems automatically measure and monitor for a
particular moisture content and regulate the same. Further, some or
all of the above devices, especially the pyrolysis device, can be
combined with an oxidation device as discussed previously.
Primary Processes
Fermentation
[0456] Generally, various microorganisms can produce a number of
useful products, such as a fuel, by operating on, e.g., fermenting
the pretreated biomass materials. For example, alcohols, organic
acids, hydrocarbons, hydrogen, proteins or mixtures of any of these
materials can be produced by fermentation or other processes.
[0457] The microorganism can be a natural microorganism or an
engineered microorganism. For example, the microorganism can be a
bacterium, e.g., a cellulolytic bacterium, a fungus, e.g., a yeast,
a plant or a protist, e.g., an algae, a protozoa or a fungus-like
protist, e.g., a slime mold. When the organisms are compatible,
mixtures of organisms can be utilized.
[0458] To aid in the breakdown of the materials that include the
cellulose, one or more enzymes, e.g., a cellulolytic enzyme can be
utilized. In some embodiments, the materials that include the
cellulose are first treated with the enzyme, e.g., by combining the
material and the enzyme in an aqueous solution. This material can
then be combined with the microorganism. In other embodiments, the
materials that include the cellulose, the one or more enzymes and
the microorganism are combined at the concurrently, e.g., by
combining in an aqueous solution.
[0459] Also, to aid in the breakdown of the materials that include
the cellulose, the materials can be treated post irradiation with
heat, a chemical (e.g., mineral acid, base or a strong oxidizer
such as sodium hypochlorite), and/or an enzyme.
[0460] During the fermentation, sugars released from cellulolytic
hydrolysis or the saccharification step, are fermented to, e.g.,
ethanol, by a fermenting microorganism such as yeast. Suitable
fermenting microorganisms have the ability to convert
carbohydrates, such as glucose, xylose, arabinose, mannose,
galactose, oligosaccharides or polysaccharides into fermentation
products. Fermenting microorganisms include strains of the genus
Saccharomyces spp. e.g., Saccharomyces cerevisiae (baker's yeast),
Saccharomyces distaticus, Saccharomyces uvarum; the genus
Kluyveromyces, e.g., species Kluyveromyces marxianus, Kluyveromyces
fragilis; the genus Candida, e.g., Candida pseudotropicalis, and
Candida brassicae, Pichia stipitis (a relative of Candida shehatae,
the genus Clavispora, e.g., species Clavispora lusitaniae and
Clavispora opuntiae the genus Pachysolen, e.g., species Pachysolen
tannophilus, the genus Bretannomyces, e.g., species Bretannomyces
clausenii (Philippidis, G. P., 1996, Cellulose bioconversion
technology, in Handbook on Bioethanol: Production and Utilization,
Wyman, C. E., ed., Taylor & Francis, Washington, D.C.,
179-212). In particular embodiments, such as when xylose is
present, Pichia stipitis (ATCC 66278) is utilized in
fermentation.
[0461] Commercially available yeast include, for example, Red
Star.RTM./Lesaffre Ethanol Red (available from Red Star/Lesaffre,
USA) FALI.RTM. (available from Fleischmann's Yeast, a division of
Burns Philip Food Inc., USA), SUPERSTART.RTM. (available from
Alltech, now Lallemand), GERT STRAND.RTM. (available from Gert
Strand AB, Sweden) and FERMOL.RTM. (available from DSM
Specialties).
[0462] Bacteria that can ferment biomass to ethanol and other
products include, e.g., Zymomonas mobilis and Clostridium
thermocellum (Philippidis, 1996, supra). Leschine et al.
(International Journal of Systematic and Evolutionary Microbiology
2002, 52, 1155-1160) isolated an anaerobic, mesophilic,
cellulolytic bacterium from forest soil, Clostridium
phytofermentans sp. nov., which converts cellulose to ethanol.
[0463] Fermentation of biomass to ethanol and other products may be
carried out using certain types of thermophilic or genetically
engineered microorganisms, such Thermoanaerobacter species,
including T. mathranii, and yeast species such as Pichia species.
An example of a strain of T. mathranii is A3M4 described in
Sonne-Hansen et al. (Applied Microbiology and Biotechnology 1993,
38, 537-541) or Ahring et al. (Arch. Microbiol. 1997, 168,
114-119). Other genetically engineered microorganisms are discussed
in U.S. Pat. No. 7,192,772.
[0464] Yeast and Zymomonas bacteria can be used for fermentation or
conversion. The optimum pH for yeast is from about pH 4 to 5, while
the optimum pH for Zymomonas is from about pH 5 to 6. Typical
fermentation times are about 24 to 96 hours with temperatures in
the range of 26.degree. C. to 40.degree. C., however thermophilic
microorganisms prefer higher temperatures.
[0465] Enzymes which break down biomass, such as cellulose, to
lower molecular weight carbohydrate-containing materials, such as
glucose, during saccharification are referred to as cellulolytic
enzymes or cellulase. These enzymes may be a complex of enzymes
that act synergistically to degrade crystalline cellulose. Examples
of cellulolytic enzymes include: endoglucanases,
cellobiohydrolases, and cellobiases (.beta.-glucosidases). A
cellulosic substrate is initially hydrolyzed by endoglucanases at
random locations producing oligomeric intermediates. These
intermediates are then substrates for exo-splitting glucanases such
as cellobiohydrolase to produce cellobiose from the ends of the
cellulose polymer. Cellobiose is a water-soluble .beta.-1,4-linked
dimer of glucose. Finally cellobiase cleaves cellobiose to yield
glucose.
[0466] A cellulase is capable of degrading biomass and may be of
fungal or bacterial origin. Suitable enzymes include cellulases
from the genera Bacillus, Pseudomonas, Humicola, Fusarium,
Thielavia, Acremonium, Chrysosporium and Trichoderma, and include
species of Humicola, Coprinus, Thielavia, Fusarium, Myceliophthora,
Acremonium, Cephalosporium, Scytalidium, Penicillium or Aspergillus
(see, e.g., EP 458162), especially those produced by a strain
selected from the species Humicola insolens (reclassified as
Scytalidium thermophilum, see, e.g., U.S. Pat. No. 4,435,307),
Coprinus cinereus, Fusarium oxysporum, Myceliophthora thermophila,
Meripilus giganteus, Thielavia terrestris, Acremonium sp.,
Acremonium persicinum, Acremonium acremonium, Acremonium
brachypenium, Acremonium dichromosporum, Acremonium obclavatum,
Acremonium pinkertoniae, Acremonium roseogriseum, Acremonium
incoloratum, and Acremonium furatum; preferably from the species
Humicola insolens DSM 1800, Fusarium oxysporum DSM 2672,
Myceliophthora thermophila CBS 117.65, Cephalosporium sp. RYM-202,
Acremonium sp. CBS 478.94, Acremonium sp. CBS 265.95, Acremonium
persicinum CBS 169.65, Acremonium acremonium AHU 9519,
Cephalosporium sp. CBS 535.71, Acremonium brachypenium CBS 866.73,
Acremonium dichromosporum CBS 683.73, Acremonium obclavatum CBS
311.74, Acremonium pinkertoniae CBS 157.70, Acremonium roseogriseum
CBS 134.56, Acremonium incoloratum CBS 146.62, and Acremonium
furatum CBS 299.70H. Cellulolytic enzymes may also be obtained from
Chrysosporium, preferably a strain of Chrysosporium lucknowense.
Additionally, Trichoderma (particularly Trichoderma viride,
Trichoderma reesei, and Trichoderma koningii), alkalophilic
Bacillus (see, for example, U.S. Pat. No. 3,844,890 and EP 458162),
and Streptomyces (see, e.g., EP 458162) may be used. The bacterium,
Saccharophagus degradans, produces a mixture of enzymes capable of
degrading a range of cellulosic materials and may also be used in
this process.
[0467] Anaerobic cellulolytic bacteria have also been isolated from
soil, e.g., a novel cellulolytic species of Clostiridium,
Clostridium phytofermentans sp. nov. (see Leschine et. al,
International Journal of Systematic and Evolutionary Microbiology
(2002), 52, 1155-1160).
[0468] Cellulolytic enzymes using recombinant technology can also
be used (see, e.g., WO 2007/071818 and WO 2006/110891).
[0469] Other enzyme and enzyme formulations that can be used are
discussed in U.S. Publication Nos. 2006/0008885 and 2006/0068475,
and in PCT Application No. WO 2006/128304.
[0470] The cellulolytic enzymes used can be produced by
fermentation of the above-noted microbial strains on a nutrient
medium containing suitable carbon and nitrogen sources and
inorganic salts, using procedures known in the art (see, e.g.,
Bennett, J. W. and LaSure, L. (eds.), More Gene Manipulations in
Fungi, Academic Press, C A 1991). Suitable media are available from
commercial suppliers or may be prepared according to published
compositions (e.g., in catalogues of the American Type Culture
Collection). Temperature ranges and other conditions suitable for
growth and cellulase production are known in the art (see, e.g.,
Bailey, J. E., and Ollis, D. F., Biochemical Engineering
Fundamentals, McGraw-Hill Book Company, N Y, 1986).
[0471] Treatment of cellulose with cellulase is usually carried out
at temperatures between 30.degree. C. and 65.degree. C. Cellulases
are active over a range of pH of about 3 to 7. A saccharification
step may last up to 120 hours. The cellulase enzyme dosage achieves
a sufficiently high level of cellulose conversion. For example, an
appropriate cellulase dosage is typically between 5.0 and 50 Filter
Paper Units (FPU or IU) per gram of cellulose. The FPU is a
standard measurement and is defined and measured according to Ghose
(1987, Pure and Appl. Chem. 59:257-268).
[0472] In particular embodimements, ACCELERASE.RTM. 1000 enzyme
complex (Genencor) is utilized as the enzyme system at a loading of
0.25 mL per gram of substrate. ACCELERASE.RTM. 1000 enzyme complex
is a multiple enzyme cocktail with multiple activities, mainly
exoglucanase, endoglucanase, hemicellulase and beta-glucosidase.
The cocktail has a minimum endoglucanase activity of 2500 CMC U/g
and a minimum beta-glucosidase activity of 400 pNPG U/g. The pH of
the cocktail is from about 4.8 to about 5.2. In other particular
embodiments, the enzyme system utilized is a blend of
CELLUCLAST.RTM. 1.5 L and Novozyme 188. For example, 0.5 mL of
CELLUCLAST.RTM. 1.5 L and 0.1 mL of Novozyme 188 can be used for
each gram of substrate. When a higher hemicellulase (xylanase)
activity is desired, OPTIMASH.TM. BG can be utilized.
[0473] Mobile fermentors can be utilized, as described in U.S.
Provisional Patent Application Ser. 60/832,735, now Published
International Application No. WO 2008/011598.
Ethanol Fermentation
[0474] Ethanol is a product of fermentation. Fermentation is a
sequence of reactions which release energy from organic molecules
in the absence of oxygen. In this application of fermentation,
energy is obtained when sugar is changed to ethanol and carbon
dioxide. All beverage ethanol, and more than half of industrial
ethanol, is made by this process. Changing corn to ethanol by
fermentation takes many steps. Starch in corn must be broken down
into simple sugars before fermentation can occur. This can be
achieved, for example, by cooking the corn and adding the enzymes
alpha amylase and gluco amylase. These enzymes function as
catalysts to speed up the chemical changes. Once a simple sugar is
obtained, yeast is added. Yeast is a single-celled fungus, which
feeds on the sugar and causes the fermentation. As the fungi feeds
on the sugar, it produces alcohol (ethanol) and carbon dioxide. In
fermentation, the ethanol retains much of the energy that was
originally in the sugar, which explains why ethanol is an excellent
fuel.
[0475] The fermentation reaction is represented by the simple
equation:
C.sub.6H.sub.12O.sub.6.fwdarw.2CH.sub.3CH.sub.2OH+2CO.sub.2
[0476] Ethanol can be made from a wide variety of available
feedstocks. Fuel ethanol can be made from crops which contain
starch such as feed grains, food grains, such as corn, and tubers,
such as potatoes and sweet potatoes. Crops containing sugar, such
as sugar beets, sugarcane, and sweet sorghum also could be used for
the production of ethanol. In addition, food processing byproducts,
such as molasses, cheese whey, and cellulosic materials including
grass and wood, as well as agricultural and forestry residues, can
be processed to ethanol. As discussed above, these and other
feedstocks can be treated as discussed herein to facilitate
production of ethanol.
Conversion of Starchy Materials
[0477] FIGS. 26 and 27 show block diagrams for a dry and wet
milling process, respectively, and illustrate the conversion, e.g.,
fermentation, of corn kernels to ethanol and other valuable
co-products.
[0478] Referring particularly now to FIG. 26, in some
implementations, a dry milling process for the conversion of corn
kernels to ethanol, e.g., anhydrous ethanol, that can be utilized
as a fuel, e.g., automobile or aviation fuel, can begin with
pretreating the dried corn kernels with any one or more
pretreatments described herein, such as radiation, e.g., any one or
more types of radiation described herein (e.g., a beam of electrons
in which each electron has an energy of about 5 MeV or a beam of
protons in which the energy of each proton is about 3-100 MeV).
After pre-treatment, the corn kernels can be ground and/or sheared
into a powder. Although any one or more pretreatments described
herein can be applied after grinding and/or at any time during the
dry milling process outlined in FIG. 26, pretreating prior to
grinding and/or shearing can be advantageous in that the kernels
are generally more brittle after pretreatment and, as a result, are
easier and can require less energy to grind and/or shear. In some
embodiments, a selected pretreatment can be applied more than once
during conversion, e.g., prior to milling and then after
milling.
[0479] After grinding and/or shearing, the milled, dry kernels can
be optionally hydrated by adding the milled material to a vessel
containing water and, optionally, hydrating agents, such as
surfactants. Optionally, this reaction vessel can also include one
or more enzymes, such as amylase, to aid in further breakdown of
starchy biomass, or the reaction vessel may contain one or more
acids, such as a mineral acid, e.g., dilute sulfuric acid. If a
hydration vessel is utilized, its contents are emptied into a
conversion vessel, e.g., a fermentation vessel, which includes one
or more conversion microbes, such as one or more yeasts, bacteria
or mixtures of yeasts and/or bacteria. If a hydration vessel is not
utilized, the milled material can be directly charged to the
conversion vessel, e.g., for fermentation.
[0480] After conversion, the remaining solids are removed and dried
to give distillers dry grains (DDG), while the ethanol is distilled
off. In some embodiments, a thermophilic microbe is utilized for
the conversion and the ethanol is continuously removed by
evaporation as it is produced. If desired, the distilled ethanol
can be fully dehydrated, such as by passing the wet ethanol through
a zeolite bed, or distilling with benzene.
[0481] Referring particularly now to FIG. 27, in some
implementations, the wet milling process for the conversion of corn
kernels to anhydrous ethanol begins with pretreating the dried corn
kernels with any one or more pretreatments described herein, such
as radiation, e.g., any one or more types of radiation described
herein (e.g., a beam of electrons in which each electron has an
energy of about 5 MeV). After pre-treatment, the corn kernels are
steeped in dilute sulfuric acid and gently stirred to break the
corn kernels into its constituents. After steeping, the fiber, oil
and germ portions are fractionated and dried, and then combined
with any solids remaining after distillation to give corn gluten
feed (CGF). After removing germ and fiber, in some embodiments, the
gluten is separated to give corn gluten meal (CGM). The remaining
starch can be pretreated again (or for the first time) by any
pretreatment described herein, e.g., to reduce its molecular weight
and/or to functionalize the starch so that it is more soluble. In
some embodiments, the starch is then charged to a reaction vessel
containing water and, optionally, hydrating agents, such as
surfactants. Optionally, this reaction vessel can also include one
or more enzymes, such as amylase, to aid in further breakdown of
starch, or the reaction vessel may contain one or more acids, such
as a mineral acid, e.g., dilute sulfuric acid. As shown,
saccharification can occur in several vessels and then the contents
of the final vessel can be emptied into a conversion vessel, e.g.,
a fermentation vessel, which includes one or more conversion
microbes, such as one or more yeasts or bacteria.
[0482] After conversion, the ethanol is distilled off. In some
embodiments, a thermophilic microbe is utilized for the conversion
and the ethanol is continuously removed by evaporation as it is
produced. If desired, the distilled ethanol can be fully
dehydrated, such as by passing the wet ethanol through a zeolite
bed.
Gasification
[0483] In addition to using pyrolysis for pre-treatment of
feedstock, pyrolysis can also be used to process pre-treated
feedstock to extract useful materials. In particular, a form of
pyrolysis known as gasification can be employed to generate fuel
gases along with various other gaseous, liquid, and solid products.
To perform gasification, the pre-treated feedstock is introduced
into a pyrolysis chamber and heated to a high temperature,
typically 700.degree. C. or more. The temperature used depends upon
a number of factors, including the nature of the feedstock and the
desired products.
[0484] Quantities of oxygen (e.g., as pure oxygen gas and/or as
air) and steam (e.g., superheated steam) are also added to the
pyrolysis chamber to facilitate gasification. These compounds react
with carbon-containing feedstock material in a multiple-step
reaction to generate a gas mixture called synthesis gas (or
"syngas"). Essentially, during gasification, a limited amount of
oxygen is introduced into the pyrolysis chamber to allow some
feedstock material to combust to form carbon monoxide and generate
process heat. The process heat can then be used to promote a second
reaction that converts additional feedstock material to hydrogen
and carbon monoxide.
[0485] In a first step of the overall reaction, heating the
feedstock material produces a char that can include a wide variety
of different hydrocarbon-based species. Certain volatile materials
can be produced (e.g., certain gaseous hydrocarbon materials),
resulting in a reduction of the overall weight of the feedstock
material. Then, in a second step of the reaction, some of the
volatile material that is produced in the first step reacts with
oxygen in a combustion reaction to produce both carbon monoxide and
carbon dioxide. The combustion reaction releases heat, which
promotes the third step of the reaction. In the third step, carbon
dioxide and steam (e.g., water) react with the char generated in
the first step to form carbon monoxide and hydrogen gas. Carbon
monoxide can also react with steam, in a water gas shift reaction,
to form carbon dioxide and further hydrogen gas.
[0486] Gasification can be used as a primary process to generate
products directly from pre-treated feedstock for subsequent
transport and/or sale, for example. Alternatively, or in addition,
gasification can be used as an auxiliary process for generating
fuel for an overall processing system. The hydrogen-rich syngas
that is generated via the gasification process can be burned, for
example, to generate electricity and/or process heat that can be
directed for use at other locations in the processing system. As a
result, the overall processing system can be at least partially
self-sustaining. A number of other products, including pyrolysis
oils and gaseous hydrocarbon-based substances, can also be obtained
during and/or following gasification; these can be separated and
stored or transported as desired.
[0487] A variety of different pyrolysis chambers are suitable for
gasification of pre-treated feedstock, including the pyrolysis
chambers disclosed herein. In particular, fluidized bed reactor
systems, in which the pre-treated feedstock is fluidized in steam
and oxygen/air, provide relatively high throughput and
straightforward recovery of products. Solid char that remains
following gasification in a fluidized bed system (or in other
pyrolysis chambers) can be burned to generate additional process
heat to promote subsequent gasification reactions.
[0488] Syngas can be reformed using a Fischer-Tropsch process,
which is a catalyzed chemical reaction in which the synthesis gas
is converted into liquid alcohols and hydrocarbons. The most common
catalysts are based on iron and cobalt, although nickel and
ruthenium have also been used.
[0489] In an alternative process, a biofilm can be used to reform
the syngas to produce the liquid fuel instead of a chemical
catalyst. Such a process has been described by Coskata, Inc. Any of
the biomass materials described herein can be used in Coskata's
process.
[0490] In some embodiments, irradiating the biomass material, e.g.,
with a beam of particles, such as electrons, prior to gasification
can lower the gasification temperature, resulting in less energy
being consumed during gasification, and can result in less char and
tar formation, resulting in enhanced syngas yield.
Post-Processing
Distillation
[0491] After fermentation, the resulting fluids can be distilled
using, for example, a "beer column" to separate ethanol and other
alcohols from the majority of water and residual solids. The vapor
exiting the beer column can be, e.g., 35% by weight ethanol, and
can be fed to a rectification column. A mixture of nearly
azeotropic (92.5%) ethanol and water from the rectification column
can be purified to pure (99.5%) ethanol using vapor-phase molecular
sieves. The beer column bottoms can be sent to the first effect of
a three-effect evaporator. The rectification column reflux
condenser can provide heat for this first effect. After the first
effect, solids can be separated using a centrifuge and dried in a
rotary dryer. A portion (25%) of the centrifuge effluent can be
recycled to fermentation and the rest sent to the second and third
evaporator effects. Most of the evaporator condensate can be
returned to the process as fairly clean condensate with a small
portion split off to waste water treatment to prevent build-up of
low-boiling compounds.
Waste Water Treatment
[0492] Wastewater treatment is used to minimize makeup water
requirements of the plant by treating process water for reuse
within the plant. Wastewater treatment can also produce fuel (e.g.,
sludge and biogas) that can be used to improve the overall
efficiency of the ethanol production process. For example, as
described in further detail below, sludge and biogas can be used to
create steam and electricity that can be used in various plant
processes.
[0493] Wastewater is initially pumped through a screen (e.g., a bar
screen) to remove large particles, which are collected in a hopper.
In some embodiments, the large particles are sent to a landfill.
Additionally or alternatively, the large particles are burned to
create steam and/or electricity as described in further detail
below. In general, the spacing on the bar screen is between 1/4
inch to 1 inch spacing (e.g., 1/2 inch spacing).
[0494] The wastewater then flows to an equalization tank, where the
organic concentration of the wastewater is equalized during a
retention time. In general, the retention time is between 8 hours
and 36 hours (e.g., 24 hours). A mixer is disposed within the tank
to stir the contents of the tank. In some embodiments, mixers
disposed throughout the tank are used to stir the contents of the
tank. In certain embodiments, the mixer substantially mixes the
contents of the equalization tank such that conditions (e.g.,
wastewater concentration and temperature) throughout the tank are
uniform.
[0495] A first pump moves water from the equalization tank through
a liquid-to-liquid heat exchanger. The heat exchanger is controlled
(e.g., by controlling the flow rate of fluid through the heat
exchanger) such that wastewater exiting the heat exchanger is at a
desired temperature for anaerobic treatment. For example, the
desired temperature for anaerobic treatment can be between
40.degree. C. to 60.degree. C.
[0496] After exiting the heat exchanger, the wastewater enters one
or more anaerobic reactors. In some embodiments, the concentration
of sludge in each anaerobic reactor is the same as the overall
concentration of sludge in the wastewater. In other embodiments,
the anaerobic reactor has a higher concentration of sludge than the
overall concentration of sludge in the wastewater.
[0497] A nutrient solution containing nitrogen and phosphorus is
metered into each anaerobic reactor containing wastewater. The
nutrient solution reacts with the sludge in the anaerobic reactor
to produce biogas which can contain 50% methane and have a heating
value of approximately 12,000 British thermal units, or Btu, per
pound). The biogas exits each anaerobic reactor through a vent and
flows into a manifold, where several biogas streams are combined
into a single stream. A compressor moves the stream of biogas to a
boiler or a combustion engine as described in further detail below.
In some embodiments, the compressor also moves the single stream of
biogas through a desulphurization catalyst. Additionally or
alternatively, the compressor can move the single stream of biogas
through a sediment trap.
[0498] A second pump moves anaerobic effluent from the anaerobic
reactors to one or more aerobic reactors (e.g., activated sludge
reactors). An aerator is disposed within each aerobic reactor to
mix the anaerobic effluent, sludge, and oxygen (e.g., oxygen
contained in air). Within each aerobic reactor, oxidation of
cellular material in the anaerobic effluent produces carbon
dioxide, water, and ammonia.
[0499] Aerobic effluent moves (e.g., via gravity) to a separator,
where sludge is separated from treated water. Some of the sludge is
returned to the one or more aerobic reactors to create an elevated
sludge concentration in the aerobic reactors, thereby facilitating
the aerobic breakdown of cellular material in the wastewater. A
conveyor removes excess sludge from the separator. As described in
further detail below, the excess sludge is used as fuel to create
steam and/or electricity.
[0500] The treated water is pumped from the separator to a settling
tank. Solids dispersed throughout the treated water settle to the
bottom of the settling tank and are subsequently removed. After a
settling period, treated water is pumped from the settling tank
through a fine filter to remove any additional solids remaining in
the water. In some embodiments, chlorine is added to the treated
water to kill pathogenic bacteria. In some embodiments, one or more
physical-chemical separation techniques are used to further purify
the treated water. For example, treated water can be pumped through
a carbon adsorption reactor. As another example, treated water can
pumped through a reverse osmosis reactor.
[0501] In the processes disclosed herein, whenever water is used in
any process, it may be grey water, e.g., municipal grey water, or
black water. In some embodiments, the grey or black water is
sterilized prior to use. Sterilization may be accomplished by any
desired technique, for example, by irradiation, steam, or chemical
sterilization.
Waste Combustion
[0502] The production of alcohol from biomass can result in the
production of various by-product streams useful for generating
steam and electricity to be used in other parts of the plant. For
example, steam generated from burning by-product streams can be
used in the distillation process. As another example, electricity
generated from burning by-product streams can be used to power
electron beam generators and ultrasonic transducers used in
pretreatment.
[0503] The by-products used to generate steam and electricity are
derived from a number of sources throughout the process. For
example, anaerobic digestion of wastewater produces a biogas high
in methane and a small amount of waste biomass (sludge). As another
example, post-distillate solids (e.g., unconverted lignin,
cellulose, and hemicellulose remaining from the pretreatment and
primary processes) can be used as a fuel.
[0504] The biogas is diverted to a combustion engine connected to
an electric generator to produce electricity. For example, the
biogas can be used as a fuel source for a spark-ignited natural gas
engine. As another example, the biogas can be used as a fuel source
for a direct-injection natural gas engine. As another example, the
biogas can be used as a fuel source for a combustion turbine.
Additionally or alternatively, the combustion engine can be
configured in a cogeneration configuration. For example, waste heat
from the combustion engines can be used to provide hot water or
steam throughout the plant.
[0505] The sludge, and post-distillate solids are burned to heat
water flowing through a heat exchanger. In some embodiments, the
water flowing through the heat exchanger is evaporated and
superheated to steam. In certain embodiments, the steam is used in
the pretreatment rector and in heat exchange in the distillation
and evaporation processes. Additionally or alternatively, the steam
expands to power a multi-stage steam turbine connected to an
electric generator. Steam exiting the steam turbine is condensed
with cooling water and returned to the heat exchanger for reheating
to steam. In some embodiments, the flow rate of water through the
heat exchanger is controlled to obtain a target electricity output
from the steam turbine connected to an electric generator. For
example, water can be added to the heat exchanger to ensure that
the steam turbine is operating above a threshold condition (e.g.,
the turbine is spinning fast enough to turn the electric
generator).
[0506] While certain embodiments have been described, other
embodiments are possible. As an example, while the biogas is
described as being diverted to a combustion engine connected to an
electric generator, in certain embodiments, the biogas can be
passed through a fuel reformer to produce hydrogen. The hydrogen is
then converted to electricity through a fuel cell.
[0507] As another example, while the biogas is described as being
burned apart from the sludge and post-distillate solids, in certain
embodiments, all of the waste by-products can be burned together to
produce steam.
Products/Co-Products
Alcohols
[0508] The alcohol produced can be a monohydroxy alcohol, e.g.,
ethanol, or a polyhydroxy alcohol, e.g., ethylene glycol or
glycerin. Examples of alcohols that can be produced include
methanol, ethanol, propanol, isopropanol, butanol, e.g., n-, sec-
or t-butanol, ethylene glycol, propylene glycol, 1, 4-butane diol,
glycerin or mixtures of these alcohols.
[0509] Each of the alcohols produced by the plant have commercial
value as industrial feedstock. For example, ethanol can be used in
the manufacture of varnishes and perfume. As another example,
methanol can be used as a solvent used as a component in windshield
wiper fluid. As still another example, butanol can be used in
plasticizers, resins, lacquers, and brake fluids.
[0510] Bioethanol produced by the plant is valuable as an
ingredient used in the food and beverage industry. For example, the
ethanol produced by the plant can be purified to food grade alcohol
and used as a primary ingredient in the alcoholic beverages.
Bioethanol produced by the plant also has commercial value as a
transportation fuel. The use of ethanol as a transportation fuel
can be implemented with relatively little capital investment from
spark ignition engine manufacturers and owners (e.g., changes to
injection timing, fuel-to-air ratio, and components of the fuel
injection system). Many automotive manufacturers currently offer
flex-fuel vehicles capable of operation on ethanol/gasoline blends
up to 85% ethanol by volume (e.g., standard equipment on a Chevy
Tahoe 4.times.4).
[0511] Bioethanol produced by this plant can be used as an engine
fuel to improve environmental and economic conditions beyond the
location of the plant. For example, ethanol produced by this plant
and used as a fuel can reduce greenhouse gas emissions from manmade
sources (e.g., transportation sources). As another example, ethanol
produced by this plant and used as an engine fuel can also displace
consumption of gasoline refined from oil.
[0512] Bioethanol has a greater octane number than conventional
gasoline and, thus, can be used to improve the performance (e.g.,
allow for higher compression ratios) of spark ignition engines. For
example, small amounts (e.g., 10% by volume) of ethanol can be
blended with gasoline to act as an octane enhancer for fuels used
in spark ignition engines. As another example, larger amounts
(e.g., 85% by volume) of ethanol can be blended with gasoline to
further increase the fuel octane number and displace larger volumes
of gasoline.
[0513] Bioethanol strategies are discussed, e.g., by DiPardo in
Journal of Outlook for Biomass Ethanol Production and Demand (EIA
Forecasts), 2002; Sheehan in Biotechnology Progress, 15:8179, 1999;
Martin in Enzyme Microbes Technology, 31:274, 2002; Greer in
BioCycle, 61-65, April 2005; Lynd in Microbiology and Molecular
Biology Reviews, 66:3, 506-577, 2002; Ljungdahl et al., in U.S.
Pat. No. 4,292,406; and Bellamy, in U.S. Pat. No. 4,094,742.
Organic Acids
[0514] The organic acids produced can include monocarboxylic acids
or polycarboxylic acids. Examples of organic acids include formic
acid, acetic acid, propionic acid, butyric acid, valeric acid,
caproic, palmitic acid, stearic acid, oxalic acid, malonic acid,
succinic acid, glutaric acid, oleic acid, linoleic acid, glycolic
acid, lactic acid, .gamma.-hydroxybutyric acid or mixtures of these
acids.
Co-Products
Lignin Residue
[0515] As described above, lignin-containing residues from primary
and pretreatment processes has value as a high/medium energy fuel
and can be used to generate power and steam for use in plant
processes. However, such lignin residues are a new type of solids
fuel and there is little demand for it outside of the plant
boundaries, and the costs of drying it for transportation only
subtract from its potential value. In some cases, gasification of
the lignin residues can convert it to a higher-value product with
lower cost.
Other Co-Products
[0516] Cell matter, furfural, and acetic acid have been identified
as potential co-products of biomass-to-fuel processing facilities.
Interstitial cell matter could be valuable, but might require
significant purification. Markets for furfural and acetic acid are
in place, although it is unlikely that they are large enough to
consume the output of a fully commercialized
lignocellulose-to-ethanol industry.
EXAMPLES
[0517] The following Examples are intended to illustrate, and do
not limit the teachings of this disclosure.
Example 1--Preparation of Fibrous Material from Polycoated
Paper
[0518] A 1500 pound skid of virgin, half-gallon juice cartons made
of un-printed polycoated white Kraft board having a bulk density of
20 lb/ft.sup.3 was obtained from International Paper. Each carton
was folded flat, and then fed into a 3 hp Flinch Baugh shredder at
a rate of approximately 15 to 20 pounds per hour. The shredder was
equipped with two 12 inch rotary blades, two fixed blades and a
0.30 inch discharge screen. The gap between the rotary and fixed
blades was adjusted to 0.10 inch. The output from the shredder
resembled confetti having a width of between 0.1 inch and 0.5 inch,
a length of between 0.25 inch and 1 inch and a thickness equivalent
to that of the starting material (about 0.075 inch).
[0519] The confetti-like material was fed to a Munson rotary knife
cutter, Model SC30. Model SC30 is equipped with four rotary blades,
four fixed blades, and a discharge screen having 1/8 inch openings.
The gap between the rotary and fixed blades was set to
approximately 0.020 inch. The rotary knife cutter sheared the
confetti-like pieces across the knife-edges, tearing the pieces
apart and releasing a fibrous material at a rate of about one pound
per hour. The fibrous material had a BET surface area of 0.9748
m.sup.2/g+/-0.0167 m.sup.2/g, a porosity of 89.0437 percent and a
bulk density (@0.53 psia) of 0.1260 g/mL. An average length of the
fibers was 1.141 mm and an average width of the fibers was 0.027
mm, giving an average L/D of 42:1. A scanning electron micrograph
of the fibrous material is shown in FIG. 28 at 25.times.
magnification.
Example 2--Preparation of Fibrous Material from Bleached Kraft
Board
[0520] A 1500 pound skid of virgin bleached white Kraft board
having a bulk density of 30 lb/ft.sup.3 was obtained from
International Paper. The material was folded flat, and then fed
into a 3 hp Flinch Baugh shredder at a rate of approximately 15 to
20 pounds per hour. The shredder was equipped with two 12 inch
rotary blades, two fixed blades and a 0.30 inch discharge screen.
The gap between the rotary and fixed blades was adjusted to 0.10
inch. The output from the shredder resembled confetti having a
width of between 0.1 inch and 0.5 inch, a length of between 0.25
inch and 1 inch and a thickness equivalent to that of the starting
material (about 0.075 inch). The confetti-like material was fed to
a Munson rotary knife cutter, Model SC30. The discharge screen had
1/8 inch openings. The gap between the rotary and fixed blades was
set to approximately 0.020 inch. The rotary knife cutter sheared
the confetti-like pieces, releasing a fibrous material at a rate of
about one pound per hour. The fibrous material had a BET surface
area of 1.1316 m.sup.2/g+/-0.0103 m.sup.2/g, a porosity of 88.3285
percent and a bulk density (@0.53 psia) of 0.1497 g/mL. An average
length of the fibers was 1.063 mm and an average width of the
fibers was 0.0245 mm, giving an average L/D of 43:1. A scanning
electron micrograph of the fibrous material is shown in FIG. 29 at
25.times. magnification.
Example 3--Preparation of Twice Sheared Fibrous Material from
Bleached Kraft Board
[0521] A 1500 pound skid of virgin bleached white Kraft board
having a bulk density of 30 lb/ft.sup.3 was obtained from
International Paper. The material was folded flat, and then fed
into a 3 hp Flinch Baugh shredder at a rate of approximately 15 to
20 pounds per hour. The shredder was equipped with two 12 inch
rotary blades, two fixed blades and a 0.30 inch discharge screen.
The gap between the rotary and fixed blades was adjusted to 0.10
inch. The output from the shredder resembled confetti (as above).
The confetti-like material was fed to a Munson rotary knife cutter,
Model SC30. The discharge screen had 1/16 inch openings. The gap
between the rotary and fixed blades was set to approximately 0.020
inch. The rotary knife cutter the confetti-like pieces, releasing a
fibrous material at a rate of about one pound per hour. The
material resulting from the first shearing was fed back into the
same setup described above and sheared again. The resulting fibrous
material had a BET surface area of 1.4408 m.sup.2/g+/-0.0156
m.sup.2/g, a porosity of 90.8998 percent and a bulk density (@0.53
psia) of 0.1298 g/mL. An average length of the fibers was 0.891 mm
and an average width of the fibers was 0.026 mm, giving an average
L/D of 34:1. A scanning electron micrograph of the fibrous material
is shown in FIG. 30 at 25.times. magnification.
Example 4--Preparation of Thrice Sheared Fibrous Material from
Bleached Kraft Board
[0522] A 1500 pound skid of virgin bleached white Kraft board
having a bulk density of 30 lb/ft.sup.3 was obtained from
International Paper. The material was folded flat, and then fed
into a 3 hp Flinch Baugh shredder at a rate of approximately 15 to
20 pounds per hour. The shredder was equipped with two 12 inch
rotary blades, two fixed blades and a 0.30 inch discharge screen.
The gap between the rotary and fixed blades was adjusted to 0.10
inch. The output from the shredder resembled confetti (as above).
The confetti-like material was fed to a Munson rotary knife cutter,
Model SC30. The discharge screen had 1/8 inch openings. The gap
between the rotary and fixed blades was set to approximately 0.020
inch. The rotary knife cutter sheared the confetti-like pieces
across the knife-edges. The material resulting from the first
shearing was fed back into the same setup and the screen was
replaced with a 1/16 inch screen. This material was sheared. The
material resulting from the second shearing was fed back into the
same setup and the screen was replaced with a 1/32 inch screen.
This material was sheared. The resulting fibrous material had a BET
surface area of 1.6897 m.sup.2/g+/-0.0155 m.sup.2/g, a porosity of
87.7163 percent and a bulk density (@0.53 psia) of 0.1448 g/mL. An
average length of the fibers was 0.824 mm and an average width of
the fibers was 0.0262 mm, giving an average L/D of 32:1. A scanning
electron micrograph of the fibrous material is shown in FIG. 31 at
25.times. magnification.
Example 5--Preparation of Densified Fibrous Material from Bleached
Kraft Board without Added Binder
[0523] Fibrous material was prepared according to Example 2.
Approximately 1 lb of water was sprayed onto each 10 lb of fibrous
material. The fibrous material was densified using a California
Pellet Mill 1100 operating at 75.degree. C. Pellets were obtained
having a bulk density ranging from about 7 lb/ft.sup.3 to about 15
lb/ft.sup.3.
Example 6--Preparation of Densified Fibrous Material from Bleached
Kraft Board with Binder
[0524] Fibrous material was prepared according to Example 2.
[0525] A 2 weight percent stock solution of POLYOX.TM. WSR N10
(polyethylene oxide) was prepared in water.
[0526] Approximately 1 lb of the stock solution was sprayed onto
each 10 lb of fibrous material. The fibrous material was densified
using a California Pellet Mill 1100 operating at 75.degree. C.
Pellets were obtained having a bulk density ranging from about 15
lb/ft.sup.3 to about 40 lb/ft.sup.3.
Example 7--Reducing the Molecular Weight of Cellulose in Fibrous
Kraft Paper by Gamma Radiation with Minimum Oxidation
[0527] Fibrous material is prepared according to Example 4. The
fibrous Kraft paper is densified according to Example 5.
[0528] The densified pellets are placed in a glass ampoule having a
maximum capacity of 250 mL. The glass ampoule is evacuated under
high vacuum (10.sup.-5 torr) for 30 minutes, and then back-filled
with argon gas. The ampoule is sealed under argon. The pellets in
the ampoule are irradiated with gamma radiation for about 3 hours
at a dose rate of about 1 Mrad per hour to provide an irradiated
material in which the cellulose has a lower molecular weight than
the fibrous Kraft starting material.
Example 8--Reducing the Molecular Weight of Cellulose in Fibrous
Kraft Paper by Gamma Radiation with Maximum Oxidation
[0529] Fibrous material is prepared according to Example 4. The
fibrous Kraft paper is densified according to Example 5.
[0530] The densified pellets are placed in a glass ampoule having a
maximum capacity of 250 mL. The glass ampoule is sealed under an
atmosphere of air. The pellets in the ampoule are irradiated with
gamma radiation for about 3 hours at a dose rate of about 1 Mrad
per hour to provide an irradiated material in which the cellulose
has a lower molecular weight than the fibrous Kraft starting
material.
Example 9--Methods of Determining Molecular Weight of Cellulosic
and Lignocellulosic
Materials by Gel Permeation Chromatography
[0531] Cellulosic and lignocellulosic materials for analysis were
treated according to Example 4. Sample materials presented in the
following tables include Kraft paper (P), wheat straw (WS), alfalfa
(A), and switchgrass (SG). The number "132" of the Sample ID refers
to the particle size of the material after shearing through a 1/32
inch screen. The number after the dash refers to the dosage of
radiation (MRad) and "US" refers to ultrasonic treatment. For
example, a sample ID "P132-10" refers to Kraft paper that has been
sheared to a particle size of 132 mesh and has been irradiated with
10 MRad.
TABLE-US-00003 TABLE 1 Peak Average Molecular Weight of Irradiated
Kraft Paper Sample Sample Dosage.sup.1 Average MW .+-. Source ID
(MRad) Ultrasound.sup.2 Std Dev. Kraft Paper P132 0 No 32853 .+-.
10006 P132-10 10 '' 61398 .+-. 2468** P132-100 100 '' 8444 .+-. 580
P132-181 181 '' 6668 .+-. 77 P132-US 0 Yes 3095 .+-. 1013 **Low
doses of radiation appear to increase the molecular weight of some
materials .sup.1Dosage Rate = 1 MRad/hour .sup.2Treatment for 30
minutes with 20 kHz ultrasound using a 1000 W horn under
re-circulating conditions with the material dispersed in water.
TABLE-US-00004 TABLE 2 Peak Average Molecular Weight of Irradiated
Materials Sample Peak Dosage.sup.1 Average MW .+-. ID # (MRad)
Ultrasound.sup.2 Std Dev. WS132 1 0 No 1407411 .+-. 175191 2 '' ''
39145 .+-. 3425 3 '' '' 2886 .+-. 177 WS132-10* 1 10 '' 26040 .+-.
3240 WS132-100* 1 100 '' 23620 .+-. 453 A132 1 0 '' 1604886 .+-.
151701 2 '' '' 37525 .+-. 3751 3 '' '' 2853 .+-. 490 A132-10* 1 10
'' 50853 .+-. 1665 2 '' '' 2461 .+-. 17 A132-100* 1 100 '' 38291
.+-. 2235 2 '' '' 2487 .+-. 15 SG132 1 0 '' 1557360 .+-. 83693 2 ''
'' 42594 .+-. 4414 3 '' '' 3268 .+-. 249 SG132-10* 1 10 '' 60888
.+-. 9131 SG132-100* 1 100 '' 22345 .+-. 3797 SG132-10-US 1 10 Yes
86086 .+-. 43518 2 '' '' 2247 .+-. 468 SG132-100-US 1 100 '' 4696
.+-. 1465 *Peaks coalesce after treatment **Low doses of radiation
appear to increase the molecular weight of some materials
.sup.1Dosage Rate = 1 MRad/hour .sup.2Treatment for 30 minutes with
20 kHz ultrasound using a 1000 W horn under re-circulating
conditions with the material dispersed in water.
[0532] Gel Permeation Chromatography (GPC) is used to determine the
molecular weight distribution of polymers. During GPC analysis, a
solution of the polymer sample is passed through a column packed
with a porous gel trapping small molecules. The sample is separated
based on molecular size with larger molecules eluting sooner than
smaller molecules. The retention time of each component is most
often detected by refractive index (RI), evaporative light
scattering (ELS), or ultraviolet (UV) and compared to a calibration
curve. The resulting data is then used to calculate the molecular
weight distribution for the sample.
[0533] A distribution of molecular weights rather than a unique
molecular weight is used to characterize synthetic polymers. To
characterize this distribution, statistical averages are utilized.
The most common of these averages are the "number average molecular
weight" (M.sub.n) and the "weight average molecular weight"
(M.sub.w). Methods of calculating these values are described in the
art, e.g., in Example 9 of WO 2008/073186.
[0534] The polydispersity index or PI is defined as the ratio of
M.sub.w/M.sub.n. The larger the PI, the broader or more disperse
the distribution. The lowest value that a PI can be is 1. This
represents a monodisperse sample; that is, a polymer with all of
the molecules in the distribution being the same molecular
weight.
[0535] The peak molecular weight value (M.sub.P) is another
descriptor defined as the mode of the molecular weight
distribution. It signifies the molecular weight that is most
abundant in the distribution. This value also gives insight to the
molecular weight distribution.
[0536] Most GPC measurements are made relative to a different
polymer standard. The accuracy of the results depends on how
closely the characteristics of the polymer being analyzed match
those of the standard used. The expected error in reproducibility
between different series of determinations, calibrated separately,
is ca. 5-10% and is characteristic to the limited precision of GPC
determinations. Therefore, GPC results are most useful when a
comparison between the molecular weight distributions of different
samples is made during the same series of determinations.
[0537] The lignocellulosic samples required sample preparation
prior to GPC analysis. First, a saturated solution (8.4% by weight)
of lithium chloride (LiCl) was prepared in dimethyl acetamide
(DMAc). Approximately 100 mg of each sample was added to
approximately 10 g of a freshly prepared saturated LiCl/DMAc
solution, and each mixture was heated to approximately 150.degree.
C.-170.degree. C. with stirring for 1 hour. The resulting solutions
were generally light- to dark-yellow in color. The temperature of
the solutions was decreased to approximately 100.degree. C. and the
solutions were heated for an additional 2 hours. The temperature of
the solutions was then decreased to approximately 50.degree. C. and
each sample solution was heated for approximately 48 to 60 hours.
Of note, samples irradiated at 100 MRad were more easily
solubilized as compared to their untreated counterpart.
Additionally, the sheared samples (denoted by the number 132) had
slightly lower average molecular weights as compared with uncut
samples.
[0538] The resulting sample solutions were diluted 1:1 using DMAc
as solvent and were filtered through a 0.45 .mu.m PTFE filter. The
filtered sample solutions were then analyzed by GPC. The peak
average molecular weight (Mp) of the samples, as determined by Gel
Permeation Chromatography (GPC), are summarized in Tables 1 and 2.
Each sample was prepared in duplicate and each preparation of the
sample was analyzed in duplicate (two injections) for a total of
four injections per sample. The EasiCal polystyrene standards PS1A
and PS1B were used to generate a calibration curve for the
molecular weight scale from about 580 to 7,500,00 Daltons.
TABLE-US-00005 TABLE 3 GPC Analysis Conditions Instrument: Waters
Alliance GPC 2000 Plgel 10.mu. Mixed-B Columns (3): S/N's:
10M-MB-148-83; 10M-MB-148-84; 10M-MB-174-129 Mobile Phase
(solvent): 0.5% LiCl in DMAc (1.0 mL/min.) Column/Detector
Temperature: 70.degree. C. Injector Temperature: 70.degree. C.
Sample Loop Size: 323.5 .mu.L
Example 10--Determining Crystallinity of Irradiated Material by
X-Ray Diffraction
[0539] X-ray diffraction (XRD) is a method by which a crystalline
sample is irradiated with monoenergetic x-rays. The interaction of
the lattice structure of the sample with these x-rays is recorded
and provides information about the crystalline structure being
irradiated. The resulting characteristic "fingerprint" allows for
the identification of the crystalline compounds present in the
sample. Using a whole-pattern fitting analysis (the Rietvelt
Refinement), it is possible to perform quantitative analyses on
samples containing more than one crystalline compound.
TABLE-US-00006 TABLE 4 XRD Data Including Domain Size and %
Crystallinity Sample Domain Size % ID (.ANG.) Crystallinity P132 55
55 P132-10 46 58 P132-100 50 55 P132-181 48 52 P132-US 26 40 A132
28 42 A132-10 26 40 A132-100 28 35 WS132 30 36 WS132-10 27 37
WS132-100 30 41 SG132 29 40 SG132-10 28 38 SG132-100 28 37
SG132-10-US 25 42 SG132-100-US 21 34
[0540] Each sample was placed on a zero background holder and
placed in a Phillips PW1800 diffractometer using Cu radiation.
Scans were then run over the range of 5.degree. to 50.degree. with
a step size of 0.05.degree. and a counting time of 2 hours
each.
[0541] Once the diffraction patterns were obtained, the phases were
identified with the aid of the Powder Diffraction File published by
the International Centre for Diffraction Data. In all samples the
crystalline phase identified was cellulose--Ia, which has a
triclinic structure.
[0542] The distinguishing feature among the 20 samples is the peak
breadth, which is related to the crystallite domain size. The
experimental peak breadth was used to compute the domain size and
percent crystallinity, which are reported in Table 4.
[0543] Percent crystallinity (X.sub.c %) is measured as a ratio of
the crystalline area to the total area under the x-ray diffraction
peaks,
X c % = A C { A a + A C } .times. 100 % ##EQU00006##
where, [0544] A.sub.c=Area of crystalline phase [0545] A.sub.a=Area
of amorphous phase [0546] X.sub.c=Percent of crystallinity
[0547] To determine the percent crystallinity for each sample it
was necessary to first extract the amount of the amorphous phase.
This is done by estimating the area of each diffraction pattern
that can be attributed to the crystalline phase (represented by the
sharper peaks) and the non-crystalline phase (represented by the
broad humps beneath the pattern and centered at 22.degree. and
38.degree.).
[0548] A systematic process was used to minimize error in these
calculations due to broad crystalline peaks as well as high
background intensity. First, a linear background was applied and
then removed. Second, two Gaussian peaks centered at 22.degree. and
38.degree. with widths of 10-12.degree. each were fitted to the
humps beneath the crystalline peaks. Third, the area beneath the
two broad Gaussian peaks and the rest of the pattern were
determined. Finally, percent crystallinity was calculated by
dividing the area beneath the crystalline peak by the total
intensity (after background subtraction). Domain size and %
crystallinity of the samples as determined by X-ray diffraction
(XRD) are presented in Table 4.
Example 11--Porosimetry Analysis of Irradiated Materials
[0549] Mercury pore size and pore volume analysis (Table 5) is
based on forcing mercury (a non-wetting liquid) into a porous
structure under tightly controlled pressures. Since mercury does
not wet most substances and will not spontaneously penetrate pores
by capillary action, it must be forced into the voids of the sample
by applying external pressure. The pressure required to fill the
voids is inversely proportional to the size of the pores. Only a
small amount of force or pressure is required to fill large voids,
whereas much greater pressure is required to fill voids of very
small pores.
TABLE-US-00007 TABLE 5 Pore Size and Volume Distribution by Mercury
Porosimetry Median Median Average Bulk Total Total Pore Pore Pore
Density Apparent Intrusion Pore Diameter Diameter Diameter @ 0.50
(skeletal) (Volume) (Area) Volume Area (4 V/A) psia Density
Porosity Sample ID (mL/g) (m.sup.2/g) (.mu.m) (.mu.m) (.mu.m)
(g/mL) (g/mL) (%) P132 6.0594 1.228 36.2250 13.7278 19.7415 0.1448
1.1785 87.7163 P132-10 5.5436 1.211 46.3463 4.5646 18.3106 0.1614
1.5355 89.4875 P132-100 5.3985 0.998 34.5235 18.2005 21.6422 0.1612
1.2413 87.0151 P132-181 3.2866 0.868 25.3448 12.2410 15.1509 0.2497
1.3916 82.0577 P132-US 6.0005 14.787 98.3459 0.0055 1.6231 0.1404
0.8894 84.2199 A132 2.0037 11.759 64.6308 0.0113 0.6816 0.3683
1.4058 73.7990 A132-10 1.9514 10.326 53.2706 0.0105 0.7560 0.3768
1.4231 73.5241 A132-100 1.9394 10.205 43.8966 0.0118 0.7602 0.3760
1.3889 72.9264 SG132 2.5267 8.265 57.6958 0.0141 1.2229 0.3119
1.4708 78.7961 SG132-10 2.1414 8.643 26.4666 0.0103 0.9910 0.3457
1.3315 74.0340 SG132-100 2.5142 10.766 32.7118 0.0098 0.9342 0.3077
1.3590 77.3593 SG132-10-US 4.4043 1.722 71.5734 1.1016 10.2319
0.1930 1.2883 85.0169 SG132-100-US 4.9665 7.358 24.8462 0.0089
2.6998 0.1695 1.0731 84.2010 WS132 2.9920 5.447 76.3675 0.0516
2.1971 0.2773 1.6279 82.9664 WS132-10 3.1138 2.901 57.4727 0.3630
4.2940 0.2763 1.9808 86.0484 WS132-100 3.2077 3.114 52.3284 0.2876
4.1199 0.2599 1.5611 83.3538
[0550] The AutoPore 9520 can attain a maximum pressure of 414 MPa
or 60,000 psia. There are four low-pressure stations for sample
preparation and collection of macropore data from 0.2 psia to 50
psia. There are two high-pressure chambers, which collect data from
25 psia to 60,000 psia. The sample is placed in a bowl-like
apparatus called a penetrometer, which is bonded to a glass
capillary stem with a metal coating. As mercury invades the voids
in and around the sample, it moves down the capillary stem. The
loss of mercury from the capillary stem results in a change in the
electrical capacitance. The change in capacitance during the
experiment is converted to volume of mercury by knowing the stem
volume of the penetrometer in use. A variety of penetrometers with
different bowl (sample) sizes and capillaries are available to
accommodate most sample sizes and configurations. Table 6 below
defines some of the key parameters calculated for each sample.
TABLE-US-00008 TABLE 6 Definition of Parameters Parameter
Description Total Intrusion The total volume of mercury intruded
during Volume: an experiment. This can include interstitial filling
between small particles, porosity of sample, and compression volume
of sample. Total Pore Area: The total intrusion volume converted to
an area assuming cylindrical shaped pores. Median Pore The size at
the 50.sup.th percentile on the Diameter (volume): cumulative
volume graph. Median Pore The size at the 50.sup.th percentile on
the Diameter (area): cumulative area graph. Average Pore The total
pore volume divided by the total Diameter: pore area (4 V/A). Bulk
Density: The mass of the sample divided by the bulk volume. Bulk
volume is determined at the filling pressure, typically 0.5 psia.
Apparent The mass of sample divided by the volume of Density:
sample measured at highest pressure, typically 60,000 psia.
Porosity: (Bulk Density/Apparent Density) .times. 100%
Example 12--Particle Size Analysis of Irradiated Materials
[0551] The technique of particle sizing by static light scattering
is based on Mie theory (which also encompasses Fraunhofer theory).
Mie theory predicts the intensity vs. angle relationship as a
function of the size for spherical scattering particles provided
that other system variables are known and held constant. These
variables are the wavelength of incident light and the relative
refractive index of the sample material. Application of Mie theory
provides the detailed particle size information. Table 7 summarizes
particle size using median diameter, mean diameter, and modal
diameter as parameters.
TABLE-US-00009 TABLE 7 Particle Size by Laser Light Scattering (Dry
Sample Dispersion) Sample Median Diameter Mean Diameter Modal
Diameter ID (.mu.m) (.mu.m) (.mu.m) A132 380.695 418.778 442.258
A132-10 321.742 366.231 410.156 A132-100 301.786 348.633 444.169
SG132 369.400 411.790 455.508 SG132-10 278.793 325.497 426.717
SG132-100 242.757 298.686 390.097 WS132 407.335 445.618 467.978
WS132-10 194.237 226.604 297.941 WS132-100 201.975 236.037
307.304
[0552] Particle size was determined by Laser Light Scattering (Dry
Sample Dispersion) using a Malvern Mastersizer 2000 using the
following conditions: [0553] Feed Rate: 35% [0554] Disperser
Pressure: 4 Bar [0555] Optical Model: (2.610, 1.000i), 1.000
[0556] An appropriate amount of sample was introduced onto a
vibratory tray. The feed rate and air pressure were adjusted to
ensure that the particles were properly dispersed. The key
component is selecting an air pressure that will break up
agglomerations, but does not compromise the sample integrity. The
amount of sample needed varies depending on the size of the
particles. In general, samples with fine particles require less
material than samples with coarse particles.
Example 13--Surface Area Analysis of Irradiated Materials
TABLE-US-00010 [0557] TABLE 8 Summary of Surface Area by Gas
Adsorption Sample Single point surface area BET Surface Area ID
(m.sup.2/g) (m.sup.2/g) P132 @ P/Po = 0.250387771 1.5253 1.6897
P132-10 @ P/Po = 0.239496722 1.0212 1.2782 P132-100 @ P/Po =
0.240538100 1.0338 1.2622 P132-181 @ P/Po = 0.239166091 0.5102
0.6448 P132-US @ P/Po = 0.217359072 1.0983 1.6793 A132 @ P/Po =
0.240040610 0.5400 0.7614 A132-10 @ P/Po = 0.211218936 0.5383
0.7212 A132-100 @ P/Po = 0.238791097 0.4258 0.5538 SG132 @ P/Po =
0.237989353 0.6359 0.8350 SG132-10 @ P/Po = 0.238576905 0.6794
0.8689 SG132-100 @ P/Po = 0.241960361 0.5518 0.7034 SG132-10-US @
P/Po = 0.225692889 0.5693 0.7510 SG132-100-US @ P/Po = 0.225935246
1.0983 1.4963 WS132 @ P/Po = 0.237823664 0.6582 0.8663 WS132-10 @
P/Po = 0.238612476 0.6191 0.7912 WS132-100 @ P/Po = 0.238398832
0.6255 0.8143
[0558] Surface area of each sample was analyzed using a
Micromeritics ASAP 2420 Accelerated Surface Area and Porosimetry
System. The samples were prepared by first degassing for 16 hours
at 40.degree. C. Next, free space (both warm and cold) with helium
is calculated and then the sample tube is evacuated again to remove
the helium. Data collection begins after this second evacuation and
consists of defining target pressures, which controls how much gas
is dosed onto the sample. At each target pressure, the quantity of
gas adsorbed and the actual pressure are determined and recorded.
The pressure inside the sample tube is measured with a pressure
transducer. Additional doses of gas will continue until the target
pressure is achieved and allowed to equilibrate. The quantity of
gas adsorbed is determined by summing multiple doses onto the
sample. The pressure and quantity define a gas adsorption isotherm
and are used to calculate a number of parameters, including BET
surface area (Table 8).
[0559] The BET model for isotherms is a widely used theory for
calculating the specific surface area. The analysis involves
determining the monolayer capacity of the sample surface by
calculating the amount required to cover the entire surface with a
single densely packed layer of krypton. The monolayer capacity is
multiplied by the cross sectional area of a molecule of probe gas
to determine the total surface area. Specific surface area is the
surface area of the sample aliquot divided by the mass of the
sample.
Example 14--Fiber Length Determination of Irradiated Materials
[0560] Fiber length distribution testing was performed in
triplicate on the samples submitted using the Techpap MorFi LB01
system. The average length and width are reported in Table 9.
TABLE-US-00011 TABLE 9 Summary of Lignocellulosic Fiber Length and
Width Data Statistically Corrected Arith- Average Length Average
Length Width metic Weighted Weighted (microm- Sample Average in
Length in Length eters) ID (mm) (mm) (mm) (.mu.m) P132-10 0.484
0.615 0.773 24.7 P132-100 0.369 0.423 0.496 23.8 P132-181 0.312
0.342 0.392 24.4 A132-10 0.382 0.423 0.650 43.2 A132-100 0.362
0.435 0.592 29.9 SG132-10 0.328 0.363 0.521 44.0 SG132-100 0.325
0.351 0.466 43.8 WS132-10 0.353 0.381 0.565 44.7 WS132-100 0.354
0.371 0.536 45.4
Example 15--Ultrasonic Treatment of Irradiated and Un-irradiated
Switchgrass
[0561] Switchgrass was sheared according to Example 4. The
switchgrass was treated by ultrasound alone or irradiation with 10
Mrad or 100 Mrad of gamma rays, and then sonicated. The resulting
materials correspond to G132-BR (un-irradiated), G132-10-BR (10
Mrad and sonication) and G132-100-BR (100 Mrad and sonication), as
presented in Table 1. Sonication was performed on each sample for
30 minutes using 20 kHz ultrasound from a 1000 W horn under
re-circulating conditions. Each sample was dispersed in water at a
concentration of about 0.10 g/mL.
[0562] FIGS. 32 and 33 show the apparatus used for sonication.
Apparatus 500 includes a converter 502 connected to booster 504
communicating with a horn 506 fabricated from titanium or an alloy
of titanium. The horn, which has a seal 510 made from VITON.RTM.
about its perimeter on its processing side, forms a liquid tight
seal with a processing cell 508. The processing side of the horn is
immersed in a liquid, such as water, that has dispersed therein the
sample to be sonicated. Pressure in the cell is monitored with a
pressure gauge 512. In operation, each sample is moved by pump 517
from tank 516 through the processing cell and is sonicated. After,
sonication, the sample is captured in tank 520. The process can be
reversed in that the contents of tank 520 can be sent through the
processing cell and captured in tank 516. This process can be
repeated a number of times until a desired level of processing is
delivered to the sample.
Example 16--Scanning Electron Micrographs of Un-irradiated
Switchgrass in Comparison to Irradiated and Irradiated and
Sonicated Switchgrass
[0563] Switchgrass samples for the scanning electron micrographs
were applied to carbon tape and gold sputter coated (70 seconds).
Images were taken with a JEOL 6500 field emission scanning electron
microscope.
[0564] FIG. 34 is a scanning electron micrograph at 1000.times.
magnification of a fibrous material produced from shearing
switchgrass on a rotary knife cutter, and then passing the sheared
material through a 1/32 inch screen.
[0565] FIGS. 35 and 36 are scanning electron micrographs of the
fibrous material of FIG. 34 after irradiation with 10 Mrad and 100
Mrad gamma rays, respectively, at 1000.times. magnification.
[0566] FIG. 37 is a scanning electron micrographs of the fibrous
material of FIG. 34 after irradiation with 10 Mrad and sonication
at 1000.times. magnification.
[0567] FIG. 38 is a scanning electron micrographs of the fibrous
material of FIG. 34 after irradiation with 100 Mrad and sonication
at 1000.times. magnification.
Example 17--Infrared Spectrum of Irradiated Kraft Paper in
Comparison to Un-irradiated Kraft Paper
[0568] The FT-IR analysis was performed on a Nicolet/Impact 400.
The results indicate that all samples reported in Table 1 are
consistent with a cellulose-based material.
[0569] FIG. 39 is an infrared spectrum of Kraft board paper sheared
according to Example 4, while FIG. 40 is an infrared spectrum of
the Kraft paper of FIG. 39 after irradiation with 100 Mrad of gamma
radiation. The irradiated sample shows an additional peak in region
A (centered about 1730 cm.sup.-1) that is not found in the
un-irradiated material.
Example 18--Combination of Electron Beam and Sonication
Pretreatment
[0570] Switchgrass is used as the feedstock and is sheared with a
Munson rotary knife cutter into a fibrous material. The fibrous
material is then evenly distributed onto an open tray composed of
tin with an area of greater than about 500 in.sup.2. The fibrous
material is distributed so that it has a depth of about 1-2 inches
in the open tray. The fibrous material may be distributed in
plastic bags at lower doses of irradiation (under 10 MRad), and
left uncovered on the metal tray at higher doses of radiation.
[0571] Separate samples of the fibrous material are then exposed to
successive doses of electron beam radiation to achieve a total dose
of 1 Mrad, 2 Mrad, 3, Mrad, 5 Mrad, 10 Mrad, 50 Mrad, and 100 Mrad.
Some samples are maintained under the same conditions as the
remaining samples, but are not irradiated, to serve as controls.
After cooling, the irradiated fibrous material is sent on for
further processing through a sonication device.
[0572] The sonication device includes a converter connected to
booster communicating with a horn fabricated from titanium or an
alloy of titanium. The horn, which has a seal made from VITON.RTM.
about its perimeter on its processing side, forms a liquid tight
seal with a processing cell. The processing side of the horn is
immersed in a liquid, such as water, into which the irradiated
fibrous material to be sonicated is immersed. Pressure in the cell
is monitored with a pressure gauge. In operation, each sample is
moved by pump through the processing cell and is sonicated.
[0573] To prepare the irradiated fibrous material for sonication,
the irradiated fibrous material is removed from any container
(e.g., plastic bags) and is dispersed in water at a concentration
of about 0.10 g/mL. Sonication is performed on each sample for 30
minutes using 20 kHz ultrasound from a 1000 W horn under
re-circulating conditions. After sonication, the irradiated fibrous
material is captured in a tank. This process can be repeated a
number of times until a desired level of processing is achieved
based on monitoring the structural changes in the switchgrass.
Again, some irradiated samples are kept under the same conditions
as the remaining samples, but are not sonicated, to serve as
controls. In addition, some samples that were not irradiated are
sonicated, again to serve as controls. Thus, some controls are not
processed, some are only irradiated, and some are only
sonicated.
Example 19--Microbial Testing of Pretreated Biomass
[0574] Specific lignocellulosic materials pretreated as described
herein are analyzed for toxicity to common strains of yeast and
bacteria used in the biofuel industry for the fermentation step in
ethanol production. Additionally, sugar content and compatibility
with cellulase enzymes are examined to determine the viability of
the treatment process. Testing of the pretreated materials is
carried out in two phases as follows.
[0575] I. Toxicity and Sugar Content
[0576] Toxicity of the pretreated grasses and paper feedstocks is
measured in yeast Saccharomyces cerevisiae (wine yeast) and Pichia
stipitis (ATCC 66278) as well as the bacteria Zymomonas mobilis
(ATCC 31821) and Clostridium thermocellum (ATCC 31924). A growt.h
study is performed with each of the organisms to determine the
optimal time of incubation and sampling.
[0577] Each of the feedstocks is then incubated, in duplicate, with
S. cerevisiae, P. stipitis, Z. mobilis, and C. thermocellum in a
standard microbiological medium for each organism. YM broth is used
for the two yeast strains, S. cerevisiae and P. stipitis. RM medium
is used for Z. mobilis and CM4 medium for C. thermocellum. A
positive control, with pure sugar added, but no feedstock, is used
for comparison. During the incubation, a total of five samples is
taken over a 12 hour period at time 0, 3, 6, 9, and 12 hours and
analyzed for viability (plate counts for Z. mobilis and direct
counts for S. cerevisiae) and ethanol concentration.
[0578] Sugar content of the feedstocks is measured using High
Performance Liquid Chromatography (HPLC) equipped with either a
Shodex.RTM. sugar SP0810 or Biorad Aminex.RTM. HPX-87P column. Each
of the feedstocks (approx. 5 g) is mixed with reverse osmosis (RO)
water for 1 hour. The liquid portion of the mixture is removed and
analyzed for glucose, galactose, xylose, mannose, arabinose, and
cellobiose content. The analysis is performed according to National
Bioenergy Center protocol Determination of Structural Carbohydrates
and Lignin in Biomass.
[0579] II. Cellulase Compatibility
[0580] Feedstocks are tested, in duplicate, with commercially
available Accellerase.RTM. 1000 enzyme complex, which contains a
complex of enzymes that reduces lignocellulosic biomass into
fermentable sugars, at the recommended temperature and
concentration in an Erlenmeyer flask. The flasks are incubated with
moderate shaking at around 200 rpm for 12 hours. During that time,
samples are taken every three hours at time 0, 3, 6, 9, and 12
hours to determine the concentration of reducing sugars (Hope and
Dean, Biotech J., 1974, 144:403) in the liquid portion of the
flasks.
Example 20--Alcohol Production Using Irradiation-Sonication
Pretreatment
[0581] The optimum size for biomass conversion plants is affected
by factors including economies of scale and the type and
availability of biomass used as feedstock. Increasing plant size
tends to increase economies of scale associated with plant
processes. However, increasing plant size also tends to increase
the costs (e.g., transportation costs) per unit of biomass
feedstock. Studies analyzing these factors suggest that the
appropriate size for biomass conversion plants can range from 2000
to 10,000 dried tons of biomass feedstock per day. The plant
described below is sized to process 2000 tons of dry biomass
feedstock per day.
[0582] FIG. 41 shows a process schematic of a biomass conversion
system configured to process switchgrass. The feed preparation
subsystem processes raw biomass feedstock to remove foreign objects
and provide consistently sized particles for further processing.
The pretreatment subsystem changes the molecular structure (e.g.,
reduces the average molecular weight and the crystallinity) of the
biomass feedstock by irradiating the biomass feedstock, mixing the
irradiated the biomass feedstock with water to form a slurry, and
applying ultrasonic energy to the slurry. The irradiation and
sonication convert the cellulosic and lignocellulosic components of
the biomass feedstock into fermentable materials. The primary
process subsystem ferments the glucose and other low weight sugars
present after pretreatment to form alcohols.
Example 21--Electron Beam Processing of Table Sugar (Sucrose)
[0583] Sucrose was treated with a beam of electrons using a vaulted
Rhodotron.RTM. TT200 continuous wave accelerator delivering 5 MeV
electrons at 80 kW output power. The table below describes the
nominal parameters for the TT200. The nominal doses (in MRad) and
actual doses (in kgy) delivered to the samples are also given
below.
Rhodotron.RTM. TT 200 Parameters
TABLE-US-00012 [0584] Beam Beam Produced: Accelerated electrons
Beam energy: Nominal (maximum): 10 MeV (+0 keV-250 keV Energy
dispersion at 10 Mev: Full width half maximum (FWHM) 300 keV Beam
power at 10 MeV: Guaranteed Operating Range 1 to 80 kW Power
Consumption Stand-by condition <15 kW (vacuum and cooling ON):
At 50 kW beam power: <210 kW At 80 kW beam power: <260 kW RF
System Frequency: .sup. 107.5 .+-. 1 MHz Tetrode type: Thomson
TH781 Scanning Horn Nominal Scanning Length 120 cm (measured at
25-35 cm from window): Scanning Range: From 30% to 100% of Nominal
Scanning Length Nominal Scanning Frequency 100 Hz .+-. 5% (at max.
scanning length): Scanning Uniformity (across 90% .+-.5% of Nominal
Scanning Length)
Dosages Delivered to the Sucrose Samples
TABLE-US-00013 [0585] Total Dosage (MRad) Delivered Dose (Number
Associated with Sample ID (kgy).sup.1 1 9.9 3 29.0 5 50.4 7 69.2 10
100.0 15 150.3 20 198.3 30 330.9 50 529.0 70 695.9 100 993.6
.sup.1For example, 9.9 kgy was delivered in 11 seconds at a beam
current of 5 mA and a line speed of 12.9 feet/minute. Cool time
between 1 MRad treatments was about 2 minutes.
The solubility of the sucrose samples treated above 30 Mrad was
enhanced, and at or above 30 Mrad, the sucrose appeared visually to
be devoid of crystallinity. Above 70 Mrad, the sucrose was
converted into a solid mass of material.
Feed Preparation
[0586] The selected design feed rate for the plant is 2,000 dry
tons per day of switchgrass biomass. The design feed is chopped
and/or sheared switchgrass.
[0587] Biomass feedstock, in the form of bales of switchgrass, is
received by the plant on truck trailers. As the trucks are
received, they are weighed and unloaded by forklifts. Some bales
are sent to on-site storage while others are taken directly to the
conveyors. From there, the bales are conveyed to an automatic
unwrapping system that cuts away the plastic wrapping and/or net
surrounding the bales. The biomass feedstock is then conveyed past
a magnetic separator to remove tramp metal, after which it is
introduced to shredder-shearer trains where the material is reduced
in size. Finally, the biomass feedstock is conveyed to the
pretreatment subsystem.
[0588] In some cases, the switchgrass bales are wrapped with
plastic net to ensure they don't break apart when handled, and may
also be wrapped in plastic film to protect the bale from weather.
The bales are either square or round. The bales are received at the
plant from off-site storage on large truck trailers.
[0589] Since switchgrass is only seasonally available, long-term
storage is required to provide feed to the plant year-round.
Long-term storage will likely consist of 400-500 acres of uncovered
piled rows of bales at a location (or multiple locations)
reasonably close to the ethanol plant. On-site short-term storage
is provided equivalent to 72 hours of production at an outside
storage area. Bales and surrounding access ways as well as the
transport conveyors will be on a concrete slab. A concrete slab is
used because of the volume of traffic required to deliver the large
amount of biomass feedstock required. A concrete slab will minimize
the amount of standing water in the storage area, as well as reduce
the biomass feedstock's exposure to dirt. The stored material
provides a short-term supply for weekends, holidays, and when
normal direct delivery of material into the process is
interrupted.
[0590] The bales are off-loaded by forklifts and are placed
directly onto bale transport conveyors or in the short-term storage
area. Bales are also reclaimed from short-term storage by forklifts
and loaded onto the bale transport conveyors.
[0591] Bales travel to one of two bale unwrapping stations.
Unwrapped bales are broken up using a spreader bar and then
discharged onto a conveyor that passes a magnetic separator to
remove metal prior to shredding. A tramp iron magnet is provided to
catch stray magnetic metal and a scalping screen removes gross
oversize and foreign material ahead of multiple shredder-shearer
trains, which reduce the biomass feedstock to the proper size for
pretreatment. The shredder-shearer trains include shredders and
rotary knife cutters. The shredders reduce the size of the raw
biomass feedstock and feed the resulting material to the rotary
knife cutters. The rotary knife cutters concurrently shear the
biomass feedstock and screen the resulting material.
[0592] Three storage silos are provided to limit overall system
downtime due to required maintenance on and/or breakdowns of feed
preparation subsystem equipment. Each silo can hold approximately
55,000 cubic feet of biomass feedstock (.about.3 hours of plant
operation).
Pretreatment
[0593] A conveyor belt carries the biomass feedstock from the feed
preparation subsystem 110 to the pretreatment subsystem 114. As
shown in FIG. 42, in the pretreatment subsystem 114, the biomass
feedstock is irradiated using electron beam emitters, mixed with
water to form a slurry, and subjected to the application of
ultrasonic energy. As discussed above, irradiation of the biomass
feedstock changes the molecular structure (e.g., reduces the
average molecular weight and the crystallinity) of the biomass
feedstock. Mixing the irradiated biomass feedstock into a slurry
and applying ultrasonic energy to the slurry further changes the
molecular structure of the biomass feedstock. Application of the
radiation and sonication in sequence may have synergistic effects
in that the combination of techniques appears to achieve greater
changes to the molecular structure (e.g., reduces the average
molecular weight and the crystallinity) than either technique can
efficiently achieve on its own. Without wishing to be bound by
theory, in addition to reducing the polymerization of the biomass
feedstock by breaking intramolecular bonds between segments of
cellulosic and lignocellulosic components of the biomass feedstock,
the irradiation may make the overall physical structure of the
biomass feedstock more brittle. After the brittle biomass feedstock
is mixed into a slurry, the application of ultrasonic energy
further changes the molecular structure (e.g., reduces the average
molecular weight and the crystallinity) and also can reduce the
size of biomass feedstock particles.
Electron Beam Irradiation
[0594] The conveyor belt 491 carrying the biomass feedstock into
the pretreatment subsystem distributes the biomass feedstock into
multiple feed streams (e.g., 50 feed streams) each leading to
separate electron beam emitters 492. In this embodiment, the
biomass feedstock is irradiated while it is dry. Each feed stream
is carried on a separate conveyor belt to an associated electron
beam emitter. Each irradiation feed conveyor belt can be
approximately one meter wide. Before reaching the electron beam
emitter, a localized vibration is induced in each conveyor belt to
evenly distribute the dry biomass feedstock over the
cross-sectional width of the conveyor belt.
[0595] Electron beam emitter 492 (e.g., electron beam irradiation
devices commercially available from Titan Corporation, San Diego,
Calif.) are configured to apply a 100 kilo-Gray dose of electrons
applied at a power of 300 kW. The electron beam emitters are
scanning beam devices with a sweep width of 1 meter to correspond
to the width of the conveyor belt. In some embodiments, electron
beam emitters with large, fixed beam widths are used. Factors
including belt/beam width, desired dose, biomass feedstock density,
and power applied govern the number of electron beam emitters
required for the plant to process 2,000 tons per day of dry
feed.
Sonication
[0596] The irradiated biomass feedstock is mixed with water to form
a slurry before ultrasonic energy is applied. There can be a
separate sonication system associated with each electron beam feed
stream or several electron beam streams can be aggregated as feed
for a single sonication system.
[0597] In each sonication system, the irradiated biomass feedstock
is fed into a reservoir 1214 through a first intake 1232 and water
is fed into the reservoir 1214 through second intake 1234.
Appropriate valves (manual or automated) control the flow of
biomass feedstock and the flow of water to produce a desired ratio
of biomass feedstock to water (e.g., 10% cellulosic material,
weight by volume). Each reservoir 1214 includes a mixer 1240 to
agitate the contents of volume 1236 and disperse biomass feedstock
throughout the water.
[0598] In each sonication system, the slurry is pumped (e.g., using
a recessed impeller vortex pump 1218) from reservoir 1214 to and
through a flow cell 1224 including an ultrasonic transducer 1226.
In some embodiments, pump 1218 is configured to agitate the slurry
1216 such that the mixture of biomass feedstock and water is
substantially uniform at inlet 1220 of the flow cell 1224. For
example, the pump 1218 can agitate the slurry 1216 to create a
turbulent flow that persists throughout the piping between the
first pump and inlet 1220 of flow cell 1224.
[0599] Within the flow cell 1224, ultrasonic transducer 1226
transmits ultrasonic energy into slurry 1216 as the slurry flows
through flow cell 1224. Ultrasonic transducer 1226 converts
electrical energy into high frequency mechanical energy (e.g.,
ultrasonic energy), which is then delivered to the slurry through
booster 48. Ultrasonic transducers are commercially available
(e.g., from Hielscher USA, Inc. of Ringwood, N.J.) that are capable
of delivering a continuous power of 16 kilowatts.
[0600] The ultrasonic energy traveling through booster 1248 in
reactor volume 1244 creates a series of compressions and
rarefactions in process stream 1216 with an intensity sufficient to
create cavitation in process stream 1216. Cavitation disaggregates
components of the biomass feedstock including, for example,
cellulosic and lignocellulosic material dispersed in process stream
1216 (e.g., slurry). Cavitation also produces free radicals in the
water of process stream 1216 (e.g., slurry). These free radicals
act to further break down the cellulosic material in process stream
1216. In general, about 250 MJ/m.sup.3 of ultrasonic energy is
applied to process stream 1216 containing fragments of poplar
chips. Other levels of ultrasonic energy (between about 5 and about
4000 MJ/m.sup.3, e.g., 10, 25, 50, 100, 250, 500, 750, 1000, 2000,
or 3000) can be applied to other biomass feedstocks After exposure
to ultrasonic energy in reactor volume 1244, process stream 1216
exits flow cell 24 through outlet 1222.
[0601] Flow cell 1224 also includes a heat exchanger 1246 in
thermal communication with at least a portion of reactor volume
1244. Cooling fluid 1248 (e.g., water) flows into heat exchanger
1246 and absorbs heat generated when process stream 1216 (e.g.,
slurry) is sonicated in reactor volume 1244. In some embodiments,
the flow of cooling fluid 1248 into heat exchanger 1246 is
controlled to maintain an approximately constant temperature in
reactor volume 1244. In addition or in the alternative, the
temperature of cooling fluid 1248 flowing into heat exchanger 1246
is controlled to maintain an approximately constant temperature in
reactor volume 1244.
[0602] The outlet 1242 of flow cell 1224 is arranged near the
bottom of reservoir 1214 to induce a gravity feed of process stream
1216 (e.g., slurry) out of reservoir 1214 towards the inlet of a
second pump 1230 which pumps process stream 1216 (e.g., slurry)
towards the primary process subsystem.
[0603] Sonication systems can include a single flow path (as
described above) or multiple parallel flow paths each with an
associated individual sonication unit. Multiple sonication units
can also be arranged to series to increase the amount of sonic
energy applied to the slurry.
Primary Processes
[0604] A vacuum rotary drum type filter removes solids from the
slurry before fermentation. Liquid from the filter is pumped cooled
prior to entering the fermentors. Filtered solids are passed to the
post-processing subsystem for further processing.
[0605] The fermentation tanks are large, low pressure, stainless
steel vessels with conical bottoms and slow speed agitators.
Multiple first stage fermentation tanks can be arranged in series.
The temperature in the first stage fermentation tanks is controlled
to 30 degrees centigrade using external heat exchangers. Yeast is
added to the first stage fermentation tank at the head of each
series of tanks and carries through to the other tanks in the
series.
[0606] Second stage fermentation consists of two continuous
fermentors in series. Both fermentors are continuously agitated
with slow speed mechanical mixers. Temperature is controlled with
chilled water in external exchangers with continuous recirculation.
Recirculation pumps are of the progressive cavity type because of
the high solids concentration.
[0607] Off gas from the fermentation tanks and fermentors is
combined and washed in a counter-current water column before being
vented to the atmosphere. The off gas is washed to recover ethanol
rather than for air emissions control.
Post-Processing
Distillation
[0608] Distillation and molecular sieve adsorption are used to
recover ethanol from the raw fermentation beer and produce 99.5%
ethanol. Distillation is accomplished in two columns--the first,
called the beer column, removes the dissolved CO2 and most of the
water, and the second concentrates the ethanol to a near azeotropic
composition.
[0609] All the water from the nearly azeotropic mixture is removed
by vapor phase molecular sieve adsorption. Regeneration of the
adsorption columns requires that an ethanol water mixture be
recycled to distillation for recovery.
[0610] Fermentation vents (containing mostly CO2, but also some
ethanol) as well as the beer column vent are scrubbed in a water
scrubber, recovering nearly all of the ethanol. The scrubber
effluent is fed to the first distillation column along with the
fermentation beer.
[0611] The bottoms from the first distillation contain all the
unconverted insoluble and dissolved solids. The insoluble solids
are dewatered by a pressure filter and sent to a combustor. The
liquid from the pressure filter that is not recycled is
concentrated in a multiple effect evaporator using waste heat from
the distillation. The concentrated syrup from the evaporator is
mixed with the solids being sent to the combustor, and the
evaporated condensate is used as relatively clean recycle water to
the process.
[0612] Because the amount of stillage water that can be recycled is
limited, an evaporator is included in the process. The total amount
of the water from the pressure filter that is directly recycled is
set at 25%. Organic salts like ammonium acetate or lactate, steep
liquor components not utilized by the organism, or inorganic
compounds in the biomass end up in this stream. Recycling too much
of this material can result in levels of ionic strength and osmotic
pressures that can be detrimental to the fermenting organism's
efficiency. For the water that is not recycled, the evaporator
concentrates the dissolved solids into a syrup that can be sent to
the combustor, minimizing the load to wastewater treatment.
Wastewater Treatment
[0613] The wastewater treatment section treats process water for
reuse to reduce plant makeup water requirements. Wastewater is
initially screened to remove large particles, which are collected
in a hopper and sent to a landfill. Screening is followed by
anaerobic digestion and aerobic digestion to digest organic matter
in the stream. Anaerobic digestion produces a biogas stream that is
rich in methane that is fed to the combustor. Aerobic digestion
produces a relatively clean water stream for reuse in the process
as well as a sludge that is primarily composed of cell mass. The
sludge is also burned in the combustor. This screening/anaerobic
digestion/aerobic digestion scheme is standard within the current
ethanol industry and facilities in the 1-5 million gallons per day
range can be obtained as "off-the-shelf" units from vendors.
Combustor, Boiler, and Turbogenerator
[0614] The purpose of the combustor, boiler, and turbogenerator
subsystem is to burn various by-product streams for steam and
electricity generation. For example, some lignin, cellulose, and
hemicellulose remains unconverted through the pretreatment and
primary processes. The majority of wastewater from the process is
concentrated to a syrup high in soluble solids. Anaerobic digestion
of the remaining wastewater produces a biogas high in methane.
Aerobic digestion produces a small amount of waste biomass
(sludge). Burning these by-product streams to generate steam and
electricity allows the plant to be self-sufficient in energy,
reduces solid waste disposal costs, and generates additional
revenue through sales of excess electricity.
[0615] Three primary fuel streams (post-distillate solids, biogas,
and evaporator syrup) are fed to a circulating fluidized bed
combustor. The small amount of waste biomass (sludge) from
wastewater treatment is also sent to the combustor. A fan moves air
into the combustion chamber. Treated water enters the heat
exchanger circuit in the combustor and is evaporated and
superheated to 510.degree. C. (950.degree. F.) and 86 atm (1265
psia) steam. Flue gas from the combustor preheats the entering
combustion air then enters a baghouse to remove particulates, which
are landfilled. The gas is exhausted through a stack.
[0616] A multistage turbine and generator are used to generate
electricity. Steam is extracted from the turbine at three different
conditions for injection into the pretreatment reactor and heat
exchange in distillation and evaporation. The remaining steam is
condensed with cooling water and returned to the boiler feedwater
system along with condensate from the various heat exchangers in
the process. Treated well water is used as makeup to replace steam
used in direct injection.
Other Embodiments
[0617] A number of embodiments of the invention have been
described. Nevertheless, it will be understood that various
modifications may be made without departing from the spirit and
scope of the invention. Accordingly, other embodiments are within
the scope of the following claims.
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