U.S. patent application number 14/623793 was filed with the patent office on 2015-06-11 for method of drying biomass.
This patent application is currently assigned to River Basin Energy, Inc.. The applicant listed for this patent is Clinton B. Camper, Vijay Sethi. Invention is credited to Clinton B. Camper, Vijay Sethi.
Application Number | 20150159105 14/623793 |
Document ID | / |
Family ID | 53270530 |
Filed Date | 2015-06-11 |
United States Patent
Application |
20150159105 |
Kind Code |
A1 |
Sethi; Vijay ; et
al. |
June 11, 2015 |
METHOD OF DRYING BIOMASS
Abstract
A process for torrefaction of biomass is provided in which
biomass are passed into a fluidized bed reactor and heated to a
predetermined temperature in an oxidizing environment. The dried
biomass is then fed to a cooler where the temperature of the
product is reduced to approximately 100 degrees Fahrenheit.
Inventors: |
Sethi; Vijay; (Laramie,
WY) ; Camper; Clinton B.; (Billings, MT) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
Sethi; Vijay
Camper; Clinton B. |
Laramie
Billings |
WY
MT |
US
US |
|
|
Assignee: |
River Basin Energy, Inc.
Highlands Ranch
CO
|
Family ID: |
53270530 |
Appl. No.: |
14/623793 |
Filed: |
February 17, 2015 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
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13084697 |
Apr 12, 2011 |
8956426 |
|
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14623793 |
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12763355 |
Apr 20, 2010 |
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13084697 |
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Current U.S.
Class: |
44/590 ; 44/589;
44/605; 44/606 |
Current CPC
Class: |
Y02E 50/14 20130101;
C10L 9/083 20130101; C10B 53/02 20130101; C10L 2290/30 20130101;
F26B 2200/02 20130101; C10L 2290/52 20130101; Y02P 20/145 20151101;
C10L 5/44 20130101; Y02E 50/10 20130101; C10L 2290/50 20130101;
C10L 5/361 20130101; C10L 2290/08 20130101; C10L 2290/06 20130101;
Y02E 50/15 20130101; C10B 49/10 20130101; C10L 5/363 20130101; C10L
2290/145 20130101; C10L 5/30 20130101; F26B 3/084 20130101; C10L
5/447 20130101; C10L 2290/10 20130101; Y02E 50/30 20130101 |
International
Class: |
C10L 5/44 20060101
C10L005/44; C10L 5/30 20060101 C10L005/30; C10L 5/40 20060101
C10L005/40; C10L 5/36 20060101 C10L005/36 |
Claims
1. A process for drying a biomass, comprising: directing said
biomass to a fluidized bed reactor; heating said biomass in said
fluidized bed reactor with a first heat source, which provides heat
energy into said fluidized bed reactor, to a temperature sufficient
to evaporate water and convert a portion of said biomass to
vaporized organic compounds, such that a dry biomass is produced
that contains less than about 10 wt % moisture; and further heating
said biomass with said first heat source and with a second heat
source that is associated with a combustion of said vaporized
organic compounds, heat from said first heat source and said second
heat source each intermingling to directly provide heat energy to
said biomass.
2. The process of claim 1, further comprising adding air to said
fluidized bed reactor to adjust an oxygen content of the first heat
source and the second heat source within said fluidized bed
reactor.
3. The process of claim 1, wherein said biomass is combined with a
coal, and wherein the coal and biomass are directed to said
fluidized bed reactor.
4. The process of claim 1, wherein said fluidized bed reactor has
an aspect ratio is no greater than about 2.
5. The process of claim 1, further comprising directing heated air
to said fluidized bed reactor with a startup heater.
6. The process of claim 1, wherein said temperature does not
initiate a torrefaction reaction.
7. The process of claim 1, wherein dried biomass is cooled in a
mixer or a hollow flight screw cooler.
8. The process of claim 1, wherein dried biomass is consolidated
into pellets or briquettes before cooling.
Description
CROSS REFERENCE TO RELATED APPLICATION
[0001] This application is a Continuation In Part of U.S. patent
application Ser. No. 13/084,697 filed on Apr. 12, 2011, which
issued as U.S. Pat. No. 8,956,426 on Feb. 17, 2015, which is a
Continuation In Part of U.S. patent application Ser. No.
12/763,355, filed Apr. 20, 2010, the entire disclosures of which
are incorporated by reference herein.
FIELD OF THE INVENTION
[0002] Embodiments of the present invention generally relate to
thermal processing of biomass "torrefaction" so that it can be used
instead of, or in addition to, coal for energy production. In one
embodiment of the present invention, the biomass is "roasted" in
the presence of oxygen wherein heat generated by the combustion of
biomass and hot gases associated with biomass combustion provide
the heat required to support the torrefaction process, all in a
single reactor.
BACKGROUND OF THE INVENTION
[0003] Many states have adopted Renewable Portfolio Standards (RPS)
that require electricity supply companies to increase energy
production that is attributed to renewable energy sources. The
federal government may soon implement a renewable electricity
standard (RES) that would be similar to the "renewables obligation"
imposed in the United Kingdom. These standards place an obligation
on electricity supply companies to produce a specified fraction of
their electricity from renewable energy sources, such as wind,
solar, hydroelectric, geothermal, biofuels, and biomass.
[0004] "Biomass" refers to renewable organic materials such as
wood, forestry waste, energy crops, municipal waste, plant
materials, or agricultural waste. Biomass often contains about 10
to about 50 weight percent moisture. The trapped moisture cannot be
used as fuel and increases costs associated with transportation of
the biomass. Thus biomass is a low grade, high cost fuel that
cannot compete economically with the fuel most commonly used to
generate electricity--coal. Further, biomass has a low bulk
density, is very hydrophilic, is seasonal, is variable, and has a
limited shelf life.
[0005] "Torrefaction" refers to the processing of biomass at
temperatures between about 200.degree. C. to about 350.degree. C.
(400.degree.-660.degree. F.) at atmospheric pressure wherein water
and light volatile organic chemicals associated with the raw
biomass material (i.e., "feed stock") are vaporized. In addition,
during the torrefaction process, molecules of biopolymers
(cellulose, hemicelluloses and lignin) contained in the biomass
decompose. After torrefaction, the biomass is a solid, dry,
blackened material that is often referred to as "torrefied biomass"
or "biocoal" that is easier to grind, which allows it to be used in
coal burning power plants. Further, the torrefied biomass possesses
a lower oxygen content, has a significantly reduced moisture
content (less than about 3%), and has higher fixed carbon levels,
which is directly proportional to heating value.
[0006] Fluid bed reactors are commonly used to carry out multiphase
reactions. In this type of reactor, gas or liquid is passed through
a granular solid material at high enough velocity to suspend the
solid and cause it to behave as though it were a fluid. This
process, known as "fluidization" imparts many important advantages
to the reactor. As a result, the fluidized bed reactor is now used
in many industrial applications, such as coal drying. Commonly coal
drying is performed in an inert gas, i.e., oxygen-free environment.
Drying coal in a non-oxidizing environment requires external heat
sources to maintain the temperature of the reactor. However, coal
has been dried in an oxidizing environment where the heat used to
support the process is at least partially drawn from the burning
coal. The temperature of the fluid bed reactor used to dry and
otherwise process the coal is controlled by balancing the rate at
which the coal is fed into the reactor against the amount of heat
generated by the combustion process. Drying of coal increases the
heating value of low rank coals, reduces the particle size of the
feed stock, and partially decarboxylizes and desulfurizes the coal.
After the coal is dried, it must be rehydrated to raise the
moisture content up to about 5-9% to reduce its spontaneous
combustion characteristics so that it is similar to native
coal.
[0007] The table provided below illustrates the differences between
raw coal and processed coal. One of skill in the art will
appreciate that processed coal possesses a higher fixed carbon and
heating values correspond to raw coal and the moisture content is
drastically reduced.
TABLE-US-00001 Raw Coal Product 1 Product 2 Product 2 Proximate
Analysis: Moisture 20.16% 8.00% 8.00% 8.00% Ash 8.16% 7.93% 8.69%
8.67% Volatile Matter 31.70% 35.33% 34.90% 35.05% Fixed Carbon
39.98% 48.74% 48.42% 42.48% Ultimate Analysis: Moisture 20.16%
8.00% 8.00% 8.00% Hydrogen 2.87% 3.32% 3.19% 3.14% Carbon 55.50%
63.15% 62.65% 62.74% Nitrogen 0.75% 0.99% 1.12% 0.81% Sulfur 0.77%
0.52% 0.54% 0.48% Oxygen 11.79% 16.09% 15.82% 16.16% Ash 8.16%
7.93% 8.69% 8.67% Heating Value, 9,444 10,460 10,315 10,165
Btu/lb
SUMMARY OF THE INVENTION
[0008] It is one aspect of the present invention to process biomass
by torrefaction. More specifically, torrefying biomass is an
efficient way to achieve the goal of producing a biomass material
that can be handled and burned like coal. Thus one embodiment of
the present invention is a torrefaction process that is suited for
biomass that reduces the moisture content, increases the heating
value (HHV), and improves grindability and handling characteristics
of the biomass. Hydrophobicity, shelf life, energy density, and
homogeneity are all also improved. In addition, mass recovery of
55-65% of the feed as salable product is achieved. Further, energy
recovery in the range of about 80-85% of the feed energy content of
product is provided where nearly all sulphur is removed. In the
process of one embodiment of the present invention, about 70% of
the chlorine in the feed is also removed. One advantage to the
contemplated process and related systems is that the processed
biomass can be used in existing coal burning power plants alone or
in combination with coal. That is, little or no modifications are
needed to existing power producing systems or processes, and
generating capacity was not decreased (derated).
[0009] It is another aspect of the present invention to employ a
fluid bed reactor to torrefy the biomass. In one embodiment, the
fluid bed reactor uses a combination of air and gas drawn from the
fluid bed exhaust, i.e., "offgas" as a primary heating and
fluidizing gas. The rate of fluidizing gas introduction into the
fluid bed reactor would be as required to produce a gas velocity
within the fluid bed reactor between about 4 and 8 feet per second.
At this velocity, the bed temperature of the reactor would be
maintained between about 230 to 350.degree. C. (450 to 670.degree.
F.).
[0010] It is still yet another aspect of the present invention to
torrefy biomass in the presence of oxygen. More specifically, as
those skilled in the art are aware, torrefaction processes of
biomass and coal, have generally been performed in an inert
environment, usually in the presence of nitrogen, argon, water
vapor, or some other inert or reducing gas. Those of skill in the
art are also familiar with the fact that the rate at which
volatiles associated with the feed stock are converted to vapor is
a function of the amount of volatile organic and inorganic
chemicals, processing temperature, and the residence time at the
processing temperature. In general, reaction rates for volatile
evolution, thermal cracking of larger organic compounds, and
oxidation of the biomass increase with the increasing temperatures
and increased residence time. However, because it takes time to dry
the material before torrefaction reactions can occur, if the
biomass is predried, preferably using heat from other sources in
the system, residence times can be reduced.
[0011] Torrefying in an oxygen rich environment adds to the
conversion of solid mass to gaseous mass and generates energy to
drive the torrefaction process. The combustion of vaporized
volatiles driven from the biomass generates heat to help maintain
the torrefaction process. Traditionally, the heat associated with
torrefaction predominately originates from outside sources. In
contrast, the system of one embodiment of the present invention
employs a fluid bed reactor that is heated internally by the
burning of vapors from biomass and biomass itself. This reduces the
amount of energy required from outside sources and allows the
biomass to be "roasted" economically and in a controlled
manner.
[0012] The primary reason that torrefaction processes of the prior
art are performed in an inert environment is that burning of the
biomass is believed to be uncontrollable and could lead to an
explosion. Embodiments of the present invention, however, control
the oxygen level in the reactor to prevent excess combustion rates
and possible explosion. Temperature control is achieved by
controlling the amount of biomass feed and the amount of available
oxygen to the reactor and one embodiment of the invention,
combustion rate within the reactor is also controlled by
selectively adding water to the reactor.
[0013] It is another aspect to provide a scalable system. As
traditional systems depend primarily on external heat sources,
increase in reactor size translates to reduced external surface
area to volume ratios, thereby requiring increased heat transfer
rates or reduced capacity. As one skilled in the art will
appreciate, in the case of a large reactor, external heating
sources cannot efficiently raise the temperature of the inner
portions of the larger reactors to heat the biomass efficiently.
The reactors of embodiments of the present invention, however, can
be increased in size because the heat needed for torrefaction is
internally generated. Ideally, a large reactor having an increased
diameter is desired because it provides a bed with a large surface
area to evenly expose the biomass to the heat.
[0014] It is still yet another aspect of the present invention to
provide a process where pre-drying is used. As briefly mentioned
above, biomass is often wet having a moisture content of about
10-50%. Thus to decrease residence time within the fluid bed
reactor that is associated with vaporizing such moisture, some
embodiments of the present invention pre-dry the feed stock.
Pre-drying can be achieved by simply allowing the biomass to dry
under ambient conditions. More preferably, however, a controlled
pre-drying process is used wherein excess heat from the fluid bed
reactor, or other processing stations of the system, is used to
pre-dry the biomass.
[0015] It is still yet another aspect of the present invention to
provide a process for starting combustion in the fluid bed reactor.
More specifically, one embodiment of the present invention uses
excess heat to initially start combustion of a predetermined amount
of biomass positioned within the fluid bed reactor. After
combustion has begun, the heat within the fluid bed reactor will
increase due to the combustion of the biomass product. Once the
temperature in the fluid bed reactor reaches a predetermined level,
the amount of external heat added to the fluid bed reactor can be
decreased and additional biomass is added to the reactor to
maintain the temperature of the fluid bed reactor.
[0016] It is another aspect of the present invention to provide a
new processing environment where torrefaction is performed at about
290.degree. C. (550.degree. F.) and wherein the biomass has a 15-20
minute residence time. One embodiment of the present invention has
a minimum auto reaction temperature of about 260.degree. C.
(500.degree. F.) and produces off gases of about 10 to 17 volume
percent water vapor and about 4 to 5 volume percent carbon dioxide.
The pressure in the fluid bed reactor is near atmospheric.
[0017] It is yet another aspect of the present invention to employ
water sprays and a mixing device, such as a mixing screw, a
hollow-flight screw cooler or rotary drum, to cool the processed
biomass. Hot torrefied product would be discharged directly from
the reactor into the cooler and water would be sprayed onto the hot
product through the use of a multiplicity of sprays to provide
cooling through evaporation of water. The total amount of water
added would be that to provide cooling to approximately the boiling
point of water (100.degree. C. at sea level) without raising the
moisture content of the cooled product above approximately 3 weight
percent. The mixing/tumbling action of the cooler would provide
particle to particle contact to enhance distribution of the water
added for cooling. The direct application of water may be achieved
by methods disclosed in U.S. patent application Ser. No.
12/566,174, which is incorporated by reference in its entirety
herein.
[0018] In an alternative embodiment of the present invention, an
indirect cooler to reduce the temperature of the torrified biomass
is employed in the event that a minimum moisture content is
required. For example, an indirect cooler with cooling surfaces
such as a hollow flight screw cooler or a rotary tube cooler may be
employed to achieve this goal.
[0019] It is another aspect of the present invention to provide a
single stage process for biomass torrefaction, comprising charging
biomass to a fluidized bed reactor, charging air to the fluidized
bed reactor at a velocity of from about 4 to about 8 feet per
second, subjecting the biomass to a temperature of from about 230
and 350.degree. C. (450 to 670.degree. F.), and removing the water
from the biomass by torrefying the biomass. The biomass charged to
the fluidized bed reactor of this embodiment has an average
moisture content from about 10 to about 50 percent. The reactor of
this example may be comprised of a fluidized bed with a fluidized
bed density up to about 50 pounds per cubic foot. In one
contemplated process wood chips having a density of about 10 to 13
pounds per cubic foot are used. At fluidization, the bed density
would be no more than half of the density of the feed stock.
[0020] It is another aspect of the present invention to provided a
process for biomass torrefaction, comprising: adding biomass to a
reactor; adding enriched gas to said reactor; controlling the
oxygen content of the enriched gas; initiating heating of said
biomass by increasing the temperature of said reactor; heating said
biomass; maintaining said biomass within said reactor for a
predetermined time; removing water from said biomass; vaporizing
volatile organic compounds associated with said biomass; torrefying
said biomass; and combusting said volatile organic compounds to
help maintain the temperature of said fluidized bed reactor.
[0021] It is still yet another aspect of the present invention to
provide a process for drying a material, comprising: directing the
material to a reactor; pre-drying the material with gasses
exhausted from the fluidized bed reactor; and subjecting said
material within the reactor to a temperature sufficient to
evaporate water; and combusting the vaporized organic compounds to
provide heat needed to help maintain said temperature.
[0022] The Summary of the Invention is neither intended nor should
it be construed as being representative of the full extent and
scope of the present invention. Moreover, references made herein to
"the present invention" or aspects thereof should be understood to
mean certain embodiments of the present invention and should not
necessarily be construed as limiting all embodiments to a
particular description. The present invention is set forth in
various levels of detail in the Summary of the Invention as well as
in the attached drawings and the Detailed Description of the
Invention and no limitation as to the scope of the present
invention is intended by either the inclusion or non-inclusion of
elements, components, etc. in this Summary of the Invention.
Additional aspects of the present invention will become more
readily apparent from the Detail Description, particularly when
taken together with the drawings.
BRIEF DESCRIPTION OF THE DRAWINGS
[0023] The accompanying drawings, which are incorporated in and
constitute a part of the specification, illustrate embodiments of
the invention and together with the general description of the
invention given above and the detailed description of the drawings
given below, serve to explain the principles of these
inventions.
[0024] FIG. 1 is a schematic representation showing the
relationship between biomass, coal, and charcoal torrefaction;
[0025] FIG. 2 is a schematic of a biomass torrefaction process of
one embodiment of the present invention;
[0026] FIG. 3 is a detailed view of FIG. 2 showing a fluid bed
reactor used in the process of one embodiment of the present
invention;
[0027] FIG. 4 is a table showing wood biomass data; and
[0028] FIG. 5 is a table showing bio-coal data.
[0029] To assist in the understanding of one embodiment of the
present invention, the following list of components and associated
numbering found in the drawings is provided below: [0030] #
Component [0031] 2 Biomass torrefaction system [0032] 6 Fluid bed
reactor [0033] 10 Hopper [0034] 14 Conveyor [0035] 18 Surge bin
[0036] 22 Feeder [0037] 26 Feed screw [0038] 34 Plate [0039] 46 Off
gas [0040] 50 Startup heater combustion air fan [0041] 54 Recycle
fan [0042] 58 Recycle Gas line [0043] 62 Recycle Gas line [0044] 66
Recycle Gas line [0045] 70 Heated Fluidizing Gas line [0046] 74
Heated Fluidizing Gas line [0047] 78 Heated Fluidizing Gas line
[0048] 82 Offgas line [0049] 86 Recycled Gas line [0050] 90
Recycled Gas line [0051] 94 Fresh air fan [0052] 98 Valve [0053]
102 Emissions control device [0054] 106 Particulate removable
device [0055] 110 Startup heating system [0056] 114 Valve [0057]
118 Cooler [0058] 122 Dump valve [0059] 126 Conveyor [0060] 130
Storage system
[0061] It should be understood that the drawings are not
necessarily to scale. In certain instances, details that are not
necessary for an understanding of the invention or that render
other details difficult to perceive may have been omitted. It
should be understood, of course, that the invention is not
necessarily limited to the particular embodiments illustrated
herein.
DETAILED DESCRIPTION
[0062] FIG. 1 is a schematic representation showing the
relationship between biomass, coal, and charcoal. It is one goal of
embodiments of the present invention to provide a system and
process suited for altering biomass, regardless of its source, such
that it behaves like coal. One advantage of providing biomass that
behaves like coal is that existing coal burning electrical power
plants can use the processed biomass without substantial
modifications. To make biomass a viable alternative, moisture
content must be reduced, heating value must be increased,
grindability and handling must be improved, hydrophobicity must be
imparted, shelf life must be increased, energy density must be
increased, and homogeneity must be improved. To achieve these
objectives, embodiments of the present invention treat biomass by
torrefaction wherein water, carbon dioxide, carbon monoxide, light
volatile organic chemicals, sulphur dioxides, and hydrochlorides
are driven out of the raw biomass. The end result is a coal like
product that can be used in coal burning electricity generation
plants of current design.
[0063] More specifically, the torrefaction contemplated by
embodiments of the present invention include thermally processing
biomass at temperatures of about 250-325.degree. C.
(480-620.degree. F.) under near atmospheric pressure and in the
presence of oxygen. This process will remove water and light
volatiles from biomass and will reduce the oxygen content of the
biomass. Importantly, the amount of fixed carbon in the biomass is
increased and the biopolymers, cellulose, hemicelluloses, and
lignin, are decomposed.
[0064] Referring now to FIG. 2, the biomass torrefaction system 2
of one embodiment of the present invention employs a fluidized bed
reactor 6. The biomass may be wood that has been reduced in size by
a commercially available wood chipper. The size of the biomass will
vary, but the smallest dimension is typically about 3 mm to 10 mm.
In one embodiment, biomass having about 10 to 50 weight percent
moisture is processed. The biomass is initially fed into a hopper
10 that in one embodiment is a feed hopper equipped with a screw
conveyor or paddle screw feeder that is adapted to controllably
feed biomass to a feed conveyor 14. In another embodiment, the
biomass is fed directly into a surge bin 18.
[0065] A feeder 22 positioned beneath the feed hopper 10 empties
biomass onto the conveyor 14. In one embodiment, the feed conveyor
14 provides up to 6000 pounds (2721.6 kg) of biomass per hour to
the surge bin 18. The surge bin 18 is equipped with a controllable
feed screw 26 that supplies the desired amount of feed at the
desired rate to the fluid bed reactor 6. In another embodiment, a
rotary valve or lock hoppers may be used if the surge bin is
located above the reactor 6. In one embodiment, the surge bin 18
employs low level and high level sensors that automatically control
a rotary valve and/or associated feeder 22 located underneath the
feed hopper 10 in order to maintain a predetermined amount of feed
biomass in the surge bin 18. In another embodiment, the level of
biomass in the surge bin 18 is controlled using a continuous level
sensor such as, e.g., an ultrasonic level sensing unit. A feed
screw 26 directs biomass to the fluid bed reactor 6. The fluid bed
reactor 6 may be a custom design or a commercially available
design.
[0066] The biomass is dried to a moisture content of less than
about 40 weight percent before introduction to the reactor 6. The
biomass may be pre-dried by conventional means including, e.g., air
drying, rotary kilns, cascaded whirling bed dryers, elongated slot
dryers, hopper dryers, traveling bed dryers, vibrating fluidized
bed dryers, and other methods that do not employ a fluidized bed
reactor. Those of skill in the art will appreciate that
fluidized-bed dryers or reactors may also be used. The heat source
for pre-drying the biomass may be of the form of waste heat, other
available heat sources, or auxiliary fuels. The waste heat may be
drawn from the reactor 6 or an emissions control device 102. In one
embodiment, the biomass is pre-dried to a moisture content of about
5 to about 20 weight percent. In another embodiment, two or more
biomass materials, each with different moisture contents, are
blended together to provide a raw feed with an average moisture
content of less than about 40 weight percent.
[0067] FIG. 3 is a schematic of an integrated fluid bed reactor 6
and pre-dryer system of one embodiment of the invention. Off-gases
46 from the fluidized bed 6 contact and pre-dry the feed material
before it reaches a plate 34. The fluidized bed reactor 6 is
cylindrical and has an aspect ratio (bed height divided by
diameter) of about 2 or less, in one embodiment, the aspect ratio
ranges from about 2 to about 1/3. The bed is positioned within the
cylindrical fluidized bed reactor at a depth of from about 1 to
about 8 feet and, more preferably, from about 2 to about 5 feet.
Non-cylindrical fluidized beds also may be used, but in one
embodiment, the aspect ratio thereof (the ratio of the bed height
to the maximum cross sectional dimension) ranges from about 2 to
about 1/3. Bed fluidization is achieved by directing fluidizing gas
through the perforated plate 34. A mixture of fresh air and
recycled gas, i.e., gas taken from the fluidized bed reactor 6, is
used as the fluidizing gas. It is preferred to use a blower to
control the amount and composition of the fluidizing gas. In other
embodiments, multiple blowers may be used.
[0068] A startup heater system 110 is used to provide the heat
needed for preheating the fluidizing gas during startup for flame
stabilization during normal operation. In addition, a recycle fan
54 is used to move the fluidized gas in a loop comprised of lines
58, 62, 66, 70, 74, 78, 82, 86 and 90 during startup and shutdown
of the system.
[0069] A fresh air fan 94 is used to add fresh air to the
fluidizing gas in order to adjust the oxygen content thereof. In
another embodiment, the fan 94 may be replaced with a control valve
and a suitable control valve added to line 86. During startup and
shutdown, as fresh air is added to the fluidizing gas, a vent valve
98 is used to release an equal amount of gas to the emissions
control device 102 to maintain a consistent flow of fluidizing gas
through the reactor 6.
[0070] Gases exiting the reactor 6 enter a particulate removal
device 106 where fines are separated. Multiple fines removal
devices may be employed to allow coarser particulate to be
recovered as additional product or as a separate product. Cleaned
gas passes a vent valve 98 where an appropriate amount of gas is
vented to an emissions control device 102. The purpose of the
emissions control device 102 is to destroy any carbonaceous
components in the offgas after removal of particulate. The
emissions control device could be, e.g., a thermal oxidizer.
[0071] In one embodiment, a typical startup procedure involves,
e.g., starting the heater system 110 and the recycle fan 54.
Recycle fan speed is selected to ensure sufficient gas flow to
achieve bed fluidization, preferably the apparent gas velocity in
the reactor is in the range of about 4 to 8 feet per second. The
temperature of the fluidizing gas is slowly increased using the
heater system. When the biomass in the reactor 6 reaches a
temperature within the range of about 446 to 482.degree. F. (230 to
250.degree. C.), biomass is fed to the reactor to fill the reactor
bed. When the biomass reaches a temperature of approximately
250.degree. C. (480.degree. F.), it begins to release heat as it
consumes oxygen present in the fluidizing gas. Small amounts of
biomass are then added to the reactor 6 to maintain a steady rise
in the temperature of the fluidized bed. It is preferred that the
temperature of the fluidized bed be maintained at about 230 and
350.degree. C. (450 to 670.degree. F.) and, more preferably, about
270 to about 300.degree. C. (520 to about 570.degree. F.).
[0072] As biomass is processed it exits reactor 6 through valve 114
into a cooler 118. A dump valve 122 can be used to remove material
buildup in the bed, or in case of emergency, be actuated to quickly
empty the reactor 6 contents into the cooler 118. As the process
reaches steady state, the temperature of the recycle gas in line 66
increases and the burner system 110 controls automatically reduces
the firing rate. In one embodiment, hot gasses taken from the
emissions control device 106 are used to preheat the fluidizing gas
(for example, by the process of FIG. 3) to reduce the amount of
combustion of biomass required to maintain the temperature of the
fluidized bed as well as the amount of fuel required by the burner
system 110. The reactor 6 is preferably equipped with several water
spray nozzles (not shown) to assist in the control the temperature
of the fluidized bed. The reactor 6 is also preferably equipped
with several temperature sensors to monitor the temperature of the
fluidized bed.
[0073] At steady state, reactor 6 operation is a balance between
biomass particle size, the reactor temperature, the residence time
required for decomposition of biomass polymers, the residence time
required for moisture and volatile organics to diffuse from the
interior of the biomass particles, the reaction rate of oxygen with
the volatile organics, and the gas velocity required for
maintaining proper levels of fluidization. In one embodiment, the
smallest biomass particle dimension is from about 3 mm to about 10
mm, the fluidizing gas velocity is from about 4 to about 8 feet per
second, the temperature of the fluidized bed is maintained at about
230 and 350.degree. C. (450 to 670.degree. F.) and, more
preferably, at about 270 to about 300 degrees .degree. C. (520 to
about 570.degree. F.), and the average biomass particle residence
time is from about 5 minutes to about 30 minutes.
[0074] The gases leaving the reactor 6 via line 82 have an oxygen
content of less than about 8 volume percent, whereas the oxygen
content of the fluidizing gas is maintained at greater than about
10 volume percent (and, more preferably, closer to that of fresh
air) to maximize the rate of biomass processing. At the preferred
steady state conditions, the amount of heat released via the
combustion of the biomass is balanced by the amount of heat
required to accomplish torrefaction and dry the biomass added to
the reactor 6.
[0075] The off gas from reactor 6 is run through a particle
separation step to remove particles entrained in the reactor
offgas. In one embodiment, this step consists of a single unit such
as bag house (not shown) or a cyclone 106. In another embodiment,
the particle separation step includes multiple devices to
facilitate recovery of entrained particles on the basis of particle
size or density. Larger particles may be directed to the cooler for
recovery as product.
[0076] The biomass produced in reactor 6 is typically at a
temperature of about 275 to about 330 degrees Centigrade, and it
typically contains about 0 to about 1 weight percent of moisture.
This product is discharged through valve 114 which may be, e.g., a
rotary valve, lock hoppers, etc. to a cooling apparatus 118.
[0077] The preferred method for cooling, rehydration, and
stabilization occurs in one process piece of process equipment.
This could be a screw conveyor, a mixing screw conveyor, a rotary
drum, rotary tube cooler or any other device that would provide
cooling through the application of water as well as mixing. The
cooler 118 would be equipped with a multiplicity of water sprays
and temperature sensors to allow water to be applied to the product
for either progressively lowering the temperature of the product to
less than the ambient boiling point of water (100 degrees
Centigrade at sea level) and/or adding up to about 3 percent
moisture to the product. The application of water may be continuous
or intermittent. The control of water application could be on the
basis of temperature, the mass flow rate of product and/or a
combination thereof.
[0078] In one embodiment, the cooling device would be a mixing
screw. In another embodiment, the cooling device could be a hollow
flight screw cooler. The screw cooler assembly is also comprised of
a multiplicity of water sprays and temperature sensors to control
the application of water on the basis of product temperature. For
example, if the rate of temperature decrease in the cooler is too
low, and/or too high, the rate may be modified by modifying the
biomass feed rate into the system, and/or by modifying flow rate or
temperature of the water in the screw jackets and/or the rate at
which water is applied using the sprays. The water spray may be
continuous, and/or it may be intermittent.
[0079] In yet another embodiment, torrefied biomass is consolidated
into briquettes or pellets and then cooled.
[0080] The cooled biomass from cooler 118 is discharged 70 to a
conveyor 126. The conveyor 126 conveys the cooled biomass product
to a storage system 130, a load out system for trucks or railcars
(not shown), or directly to the end user. Any gases emitted in the
cooler are directed to the emissions control device 106.
[0081] Referring now to FIG. 4 shows a Proximate and Ultimate
analysis for an example woody biomass feed. FIG. 5 shows a
Proximate and Ultimate analysis for the torrefied product produced
from the woody biomass feed of FIG. 4.
[0082] While various embodiments of the present invention have been
described in detail, it is apparent that modifications and
alterations of those embodiments will occur to those skilled in the
art. However, it is to be expressly understood that such
modifications and alterations are within the scope and spirit of
the present invention, as set forth in the following claims.
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