U.S. patent application number 14/102398 was filed with the patent office on 2014-05-15 for carbon dioxide corn germ oil extraction system.
This patent application is currently assigned to MOR Supercritical, LLC. The applicant listed for this patent is MOR Supercritical, LLC. Invention is credited to Daniel L. Claycamp, Kenneth E. DeLine, Daniel Fetherston, Rodger T. Marentis.
Application Number | 20140134069 14/102398 |
Document ID | / |
Family ID | 39082301 |
Filed Date | 2014-05-15 |
United States Patent
Application |
20140134069 |
Kind Code |
A1 |
DeLine; Kenneth E. ; et
al. |
May 15, 2014 |
Carbon Dioxide Corn Germ Oil Extraction System
Abstract
Supercritical carbon dioxide extraction of corn germ oil from
corn germ utilizing extraction conditions adapted to a dry corn
fractionation ethanol production process.
Inventors: |
DeLine; Kenneth E.; (Avon,
CO) ; Claycamp; Daniel L.; (West Frankfort, IL)
; Fetherston; Daniel; (Cape Girardeau, MO) ;
Marentis; Rodger T.; (Macungie, PA) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
MOR Supercritical, LLC |
Macungie |
PA |
US |
|
|
Assignee: |
MOR Supercritical, LLC
Macungie
PA
|
Family ID: |
39082301 |
Appl. No.: |
14/102398 |
Filed: |
December 10, 2013 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
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12589816 |
Oct 28, 2009 |
8603328 |
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14102398 |
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11716838 |
Mar 12, 2007 |
7612220 |
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12589816 |
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60858107 |
Nov 10, 2006 |
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60838642 |
Aug 18, 2006 |
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Current U.S.
Class: |
422/284 |
Current CPC
Class: |
Y02E 50/17 20130101;
Y02E 50/10 20130101; C12P 7/06 20130101; Y02P 20/544 20151101; C11B
1/104 20130101; Y02P 20/54 20151101 |
Class at
Publication: |
422/284 |
International
Class: |
C11B 1/10 20060101
C11B001/10 |
Claims
1. A corn oil extraction system, comprising: an amount of corn germ
having a substantially fixed location inside of at least one
extractor vessel; an amount of supercritical carbon dioxide fluidly
engaged to said amount of corn germ inside said at least one
extractor vessel; a heat source which maintains said amount of
supercritical carbon dioxide at a temperature in a range of about
85.degree. C. to about 120.degree. C.; a pressure generator which
maintains said amount of supercritical carbon dioxide at a pressure
in a range of about 8500 psi and about 12,000 psi; and an amount of
corn oil extracted from said amount of corn germ with said amount
of supercritical carbon dioxide.
2. The corn oil extraction system of claim 1, further comprising an
effluent monitor which monitors an amount of corn oil solubilized
in said amount of supercritical carbon dioxide.
3. The corn oil extraction system of claim 2, further comprising: a
temperature adjustment element coupled to said heat source; and a
pressure adjustment element coupled to said pressure generator,
said temperature adjustment element responsive to said effluent
monitor, said temperature adjustment element and said pressure
adjustment element adjusting said temperature or said pressure
based on monitoring of said amount of corn oil solubilized in said
amount of supercritical carbon dioxide to achieve a preselected
corn germ extraction efficiency profile.
4. The corn oil extraction system of claim 1, wherein a ratio of
said amount of supercritical carbon dioxide to said amount of corn
is between about 2:1 to about 6:1 (wt/wt)
5. The corn oil extraction system of claim 4, wherein said ratio
comprises about 2:1 to about 5:1 (wt/wt).
6. The corn oil extraction system of claim 5, further comprising a
duration of time of between about 10 and about 30 minutes.
7. The corn oil extraction system of claim 6, further comprising a
yield of said corn oil from said amount of corn germ of greater
than 18 percent of the weight.
8. The corn oil extraction system of claim 1, further comprising a
comminutor which reduces particle size of said amount of corn germ
fluidically engaged to said amount of supercritical carbon dioxide
in said corn germ extraction zone to less than about 30 mesh.
9. The corn oil extraction system of claim 1, further comprising a
water removal element coupled to said amount of supercritical
carbon dioxide which reduces an amount of water in said amount of
supercritical carbon dioxide which fluidically engages said amount
of corn germ inside of said corn germ extraction zone to between
about one percent by weight to about seven percent by weight.
10. The corn oil extraction system of claim 9, wherein said amount
of corn germ located inside said corn germ extraction zone contains
an amount of water in the range of about ten percent by weight to
about fourteen percent by weight prior to fluidic engagement with
said amount of supercritical carbon dioxide inside said corn germ
extraction zone.
11. The corn oil extraction system of claim 10, further comprising
an amount of extracted corn germ generated by fluidic engagement
with said amount of supercritical carbon dioxide inside said corn
germ extraction zone, wherein said amount of extracted corn germ
contains an amount of water in the range of about one percent by
weight to about seven percent by weight.
12. The corn oil extraction system of claim 10, further comprising
an amount of distillation soluble having an amount of solids in the
range of about 20 percent by weight to about 60 percent by weight
mixed with said amount of extracted corn germ containing an amount
of water in the range of about one percent by weight to about seven
percent by weight sufficient to increase said amount of water
contained by said amount of extracted corn germ to between eight
percent by weight to about fourteen percent by weight.
13. The corn oil extraction system of claim 12, further comprising
an amount of distillation soluble having an amount of solids in the
range of about 20 percent by weight to about 60 percent by weight
mixed with said amount of extracted corn germ containing an amount
of water in the range of about one percent by weight to about seven
percent by weight sufficient to increase said amount of water
contained by said amount of extracted corn germ to greater than
fourteen percent by weight, and further comprising a dryer capable
of reducing the amount of water contained by said amount of corn
germ mixed with said amount of distillation soluble having said
amount of solids in the range of about 30 percent by weight to
about 60 percent by weight to between about eight percent by weight
to about fourteen percent by weight.
Description
[0001] This United States patent application is a continuation of
U.S. patent application Ser. No. 12/589,816, filed Oct. 28, 2009,
which is a division of U.S. patent application Ser. No. 11/716,838,
filed Mar. 12, 2007, now U.S. Pat. No. 7,612,220, issued Nov. 3,
2009, which claims the benefit of U.S. Provisional Patent
Application No. 60/858,107, filed Nov. 10, 2006 and U.S.
Provisional Patent Application No. 60/838,642, filed Aug. 18, 2006,
each hereby incorporated by reference herein.
I. BACKGROUND
[0002] Specifically, supercritical carbon dioxide extraction of
corn germ oil from corn germ utilizing extraction conditions
adapted to a dry corn fractionation ethanol production process.
Generally, inventive supercritical carbon dioxide extraction
conditions which can be applied to corn germ.
[0003] As shown in FIG. 1, conventional ethanol production systems
(1) may mill whole corn (2) into a mixture of corn particles (3)
(referred to hereinafter as "milled corn") the mixture of particles
including corn bran, corn endosperm and corn germ. The milled corn
(3) can be transferred to the ethanol production process (4) which
includes the conventional steps of fermentation, distillation, and
dehydration to generate an amount of ethanol (5). In the
fermentation step, the milled corn (3) may be combined with an
amount of water and an amount of alpha-amylase (or other enzyme
capable of liquefying corn starch) to generate a mash in which the
starch of the corn endosperm is liquefied. The mash may be held for
a period of time at a temperature of between about 120 degrees
Celsius (.degree. C.) and about 150.degree. C. to kill bacteria in
the mash. The mash may then be held at a temperature of between
about 90.degree. C. and about 100.degree. C. for a duration of time
sufficient to achieve a desired level of liquefication of the
starch. An amount of gluco-amylase (or other enzyme capable of
generating fermentable sugars from the liquefied starch) added to
the mash converts the liquefied starch to fermentable sugars, such
as dextrose, in a process referred to as saccharification. Yeast
can then be added to the mash to convert the sugars to an amount of
ethanol (5) and an amount of carbon dioxide (6) (also referred to
as "CO2") along with other volatile organics. The amount of carbon
dioxide (6) can be placed in a storage unit (18) or sold in the
marketplace. For sale into certain markets or for certain
applications, the amount of carbon dioxide (6) can be stripped of
the other volatile organics and captured as an amount of purified
carbon dioxide (9). The fermented mash often referred to as "beer"
comprises an amount of ethanol (5) in a concentration of about
eight percent to about eighteen percent by weight, other liquids,
and non-fermentable solids. The amount of ethanol (5) in the beer
can be separated and concentrated to about 190 proof by
conventional distillation techniques and dehydrated by application
to molecular sieve to produce a dehydrated ethanol of about 200
proof. The about 200 proof ethanol may be combined with up to about
five percent denaturant to generate an amount of fuel grade ethanol
(10) which can be placed in the storage unit (18) and subsequently
sold.
[0004] The stillage which remains after distillation of the beer
can comprise an amount of liquid typically referred to as "thin
stillage" and an amount of remaining solids typically referred to
as the "distillers grains". The thin stillage can be separated from
the distillers grains (for example by centrifugation). The
distillers grains can be dried by evaporation of the remaining thin
stillage. The thin stillage can be concentrated by evaporation of
water to generate a syrup containing about twenty percent solids to
about sixty percent solids (also referred to as "condensed
distiller soluble"). The syrup can be recombined with the dried
distillers grains to generate an amount of distillers dried grain
with solubles (7) ("DDGS"). The DDGS can be sold as animal feed
(8).
[0005] Even though there is an increasing demand for fuel ethanol
(10) worldwide and an increasing amount of research in ethanol
production, there remain substantial unresolved problems with
respect to conventional ethanol production.
[0006] A first substantial problem with the conventional ethanol
production process above-described and referring again to FIG. 1
can be that the amount of thermal energy (11) (or energy Btus or
Btus) utilized by the conventional ethanol production process (4),
including the steps of fermentation, distillation and dehydration,
and by-product handling, which results in about a gallon of fuel
ethanol (5), and a corresponding amount of DDGS (7) and carbon
dioxide (6) may utilize an amount of thermal energy (11) of between
about 30,000 and 40,000 British thermal units (hereinafter "Btu").
This amount of thermal energy (11) is typically generated by
burning a corresponding amount of fossil fuel (12) such as oil,
coal oil, coal or natural gas.
[0007] To reduce the amount of fossil fuels (12) utilized to
provide the amount of thermal energy (11) required for the ethanol
production process (4), an amount of the DDGS (7) may be burned to
produce a part of the amount of thermal energy (11) required as
described by United States Patent Application No.
2003/0019736A1.
[0008] Alternately, referring to FIG. 2, U.S. Patent Application
No. 60/838,642, hereby incorporated by reference, inventive dry
mill kernel fractionation processes (17) which fracture kernels of
grain (13), such as cleaned conditioned corn, and isolate process
fractions which include the pericarp (also referred to as "bran"),
the germ, and the endosperm can be utilized to reduce the amount of
thermal energy (11) required by the ethanol production system (4)
or to generate an amount of thermal energy (11) without the use of
fossil fuels (12). As shown in FIG. 2, the isolated endosperm
fraction (14) can be introduced into the ethanol production process
(4) without substantial amounts of the germ fraction (16) or the
bran fraction (15). By introducing only the endosperm fraction (14)
into the ethanol production process (4) an increased amount of
ethanol (5) and fuel ethanol (10) can be generated per unit of
fermented material. As the amount of ethanol (5) per unit of
fermented material increases, the amount of thermal energy (11)
required to produce an amount of ethanol (5) decreases. However,
use of the inventive dry mill kernel fractionation processes (17)
described also generates an isolated germ fraction (16) and the
isolated bran fraction (15) which must be further processed, placed
in the storage unit (18), sold, or disposed.
[0009] Referring now to FIGS. 3 and 4, various embodiments of the
inventive dry mill corn fractionation process (17) as described by
U.S. Patent Application No. 60/858,107 and International Patent
Cooperation Treaty Patent Application No. PCT/US06/45193, each
hereby incorporated by reference, can utilize the isolated germ
fraction (16) and the isolated bran fraction (15) (or isolated
components thereof whether in whole or in part or separately or in
various combinations) to generate an amount of thermal energy (11)
to replace in whole or in part the amount of thermal energy (11)
conventionally produced by burning fossil fuels (12). With respect
to the corn germ fraction (16), extraction of the corn germ
fraction (16) with an amount of supercritical carbon dioxide (28)
can generate an amount of corn oil (23) which can be placed in the
storage unit (18), sold, burned to produce thermal energy (11) or
can be converted to biodiesel (27) which can placed in the storage
unit (18), sold or burned as a fuel (33) to produce an amount of
thermal energy (11) separately or in combination with an amount of
any one or more of condensed distiller soluble (30), fusel oil
(29), ethanol (5), or fractionated corn gluten meal (31). As to
certain embodiments of the invention, the amount of thermal energy
(11) can be transferred to a boiler (34) which can produce steam
which coupled to a turbine (36) can generate an amount of
electricity (37).
[0010] A substantial problem with respect to corn germ oil
extraction (21) of the corn germ fraction (16) to produce an amount
of corn germ oil (23) can be that conventional carbon dioxide
extraction methods whether performed with carbon dioxide or with
supercritical carbon dioxide utilize extraction conditions which:
may not extract (21) a substantial portion of the amount of the
corn oil (23) contained in the corn germ fraction (16), or may
extract the amount of corn oil (23) contained in the corn germ
fraction (15) at a rate which requires greater than about thirty
minutes (the term "about" means greater or lesser than the value or
range of values stated by 10 percent, but not does not limit any
value or range of values to this broader definition and each value
or range of values preceded by the term "about" also includes in
the alternative the absolute value or range of values stated), or
may not extract an amount of corn oil (23) from the corn germ
fraction (16) of between about 18 weight percent to about 30 weight
percent (such weight percent including any processing of the corn
germ to remove a part of the oil prior to extraction with carbon
dioxide or supercritical carbon dioxide), or may not extract 90
percent or more of the extractable amount of corn oil (23) in the
amount of corn germ fraction (16)), or requires utilization of an
amount of supercritical carbon dioxide (28) to the amount of corn
germ fraction (16) extracted of greater than about 5 to 1 (wt./wt.)
(as a non-limiting example, ratios of 5 to 1 or less may be
preferred in certain embodiments of a dry mill corn fractionation
process (17) in the context of ethanol production), or of greater
than about 7 to 1 (as a non-limiting example, ratios of 7 to 1 or
less may be preferred in other embodiments of the dry mill corn
fractionation process (17) in the context of ethanol production),
or may greater than about than 12 to 1 (as a non-limiting example,
12 to 1 or less may be preferred in yet other embodiments of the
dry mill corn fractionation process (17) in the context of ethanol
production).
[0011] As such, conventional carbon dioxide extraction methods may
be in whole or in part impracticable or incompatible with the
process rates or efficiency rates required in the context of a dry
mill kernel fractionation ethanol production process (17), or may
not be competitive or commercially feasible relative to other
conventional methods, or are simply less desirable to extraction
conditions which allow between about 18 weight percent to about 30
weight percent of the corn germ fraction (16) (or greater weight
percents for corn germ having greater weight percentage extractable
corn oil such as about 45 weight percent corn germ oil) to be
extracted as corn oil (23) utilizing a ratio of supercritical
carbon dioxide (28) to corn germ fraction (16) of not greater than
about 12.0 to 1 (wt./wt.), or not greater than 7 to 1, or not
greater than 5 to 1, or of greater than 2 to 1 depending on the
application. Understandably, the inventive corn germ fraction (16)
extraction conditions described herein may confer an advantage in
other applications outside of ethanol production systems (17)
described herein or incorporated by reference and the invention is
not so limited.
[0012] Now referring primarily to FIG. 4, another substantial
problem with conventional methods of corn germ oil extraction (21)
may be that the extracted corn germ fraction (22) (also referred to
as "germ cake") may contain an amount of water (25) subsequent to
corn oil extraction (21), a portion of which may require
evaporation or otherwise removed before the germ cake (22) prior to
placement in the storage unit (18) or sold, or which increases the
number steps to process the germ cake (22) into a particular germ
cake byproduct (27) (such as a germ cake animal feed) or makes the
steps to produce a particular germ cake byproduct (27) more costly.
As an example, further described below, the condensed distiller
soluble (24) above-described can be mixed with the germ cake (22)
but the amount of water (25) contained by the germ cake (22)
subsequent to mixing which is in excess of about fourteen percent
by weight (or in excess of a pre-selected or desired amount of
water) must be removed. As such, any reduction in the amount of
water (25) contained by the germ cake (22) subsequent to corn oil
extraction (21) can reduce the amount of water (25) that must be
removed from the germ cake (22) or removed from a mixture of germ
cake (22) and condensed distiller soluble (24) to achieve an amount
of water in a germ cake animal feed (27) of less than fourteen
percent by weight or other water content desirable based upon the
application.
[0013] The present inventive supercritical carbon dioxide
extraction conditions of the corn germ fraction (16) described
herein address each of the above-mentioned problems related to
conventional corn germ oil extraction from corn germ (16).
II. SUMMARY OF THE INVENTION
[0014] Accordingly, a broad object of the invention can be to
provide supercritical carbon dioxide extraction of corn germ oil
from corn germ utilizing extraction conditions adapted to a dry
corn fractionation ethanol production process.
[0015] A second broad object of the invention can be to provide
inventive supercritical carbon dioxide extraction of corn germ oil
from corn germ. The inventive supercritical carbon dioxide
extraction conditions as to certain embodiments of the invention
can extract greater amounts of corn oil from the same amount of
corn germ fraction compared with conventional corn germ extraction
conditions. Additionally, the inventive supercritical carbon
dioxide extraction conditions can extract the same or greater
amounts of corn oil from the corn germ fraction in a lesser
duration of time, or can extract an amount of corn oil from an
amount of corn germ fraction of between about 18 percent by weight
to about 30 percent by weight (or greater weight percentage for
corn germ containing for example 45 percent corn oil by weight)
which as to certain embodiments of the invention can be in a lesser
duration of time. An additional advantage of utilizing the
inventive supercritical carbon dioxide extraction conditions can be
a reduction in the amount of supercritical carbon dioxide utilized
to extract the same or greater amount of corn oil from the corn
germ fraction which as to certain embodiments of the invention can
provide a ratio of supercritical carbon dioxide to corn germ
fraction extracted of not greater than about 12 to 1 (wt./wt.), or
as to certain embodiments of the invention not greater than about
7.0 to 1, or as to certain embodiments of the invention not greater
than about 5.0 to 1.0, or as to certain embodiments of the
invention between about 2.0-5.0 to 1.0.
[0016] A third broad object of the invention can be to provide an
extracted corn germ fraction containing an amount of water which
can be less than the amount of water contained by conventional corn
germ oil extraction processes.
[0017] A fourth broad object of the invention can be to provide a
corn germ animal feed which includes the germ cake extracted with
supercritical carbon dioxide (whether by conventional conditions or
the inventive conditions described herein) mixed with an amount of
condensed distiller soluble and a method of manufacturing such
animal feed which can utilize less thermal energy to bring the
mixture to a desired amount of water.
[0018] Naturally, further objects of the invention are disclosed
throughout other areas of the specification, drawings, and
claims.
III. A BRIEF DESCRIPTION OF THE DRAWINGS
[0019] FIG. 1 provides a flow diagram of the conventional fuel
ethanol production technology.
[0020] FIG. 2 provides a flow diagram of a particular embodiment of
an inventive fuel ethanol production technology utilizing grain
fractionation products.
[0021] FIG. 3 provides a flow diagram of a particular embodiment of
the inventive fuel ethanol production technology utilizing grain
fractionation products.
[0022] FIG. 4 provides a flow diagram of a particular embodiment of
the inventive fuel ethanol production technology utilizing grain
fractionation products.
[0023] FIG. 5 provides a flow diagram of a particular embodiment of
a corn germ extraction system.
[0024] FIG. 6 provides an enlarged portion of the flow diagram
shown in FIG. 5 further providing a cut away of a part of an
extraction vessel showing the corn germ extraction zone containing
an amount of corn germ.
[0025] FIG. 6A provides an enlargement of one of the plurality of
particles included in the amount of corn germ contained in the corn
germ extraction zone further illustrating the corn germ matrix.
[0026] FIG. 7 provides a graph which plots solvent to feed ratio
against percent weight of feedstock (weight of corn germ) extracted
for certain embodiments of the inventive corn germ extraction
conditions.
[0027] FIG. 8 provides a graph which plots solvent to feed ratio
against percent weight of feedstock (weight of corn germ) extracted
for certain embodiments of the inventive corn germ extraction
conditions.
[0028] FIG. 9 provides a graph which plots solvent to feed ratio
against percent weight of feedstock (weight of corn germ) extracted
for certain embodiments of the inventive corn germ extraction
conditions.
[0029] FIG. 10 provides a graph which plots solvent to feed ratio
against percent weight of feedstock (weight of corn germ) extracted
for certain embodiments of the inventive corn germ extraction
conditions.
[0030] FIG. 11 provides a graph which plots solvent to feed ratio
against percent weight of feedstock (weight of corn germ) extracted
for certain embodiments of the inventive corn germ extraction
conditions.
IV. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
[0031] Specifically, supercritical carbon dioxide extraction of
corn germ oil from corn germ utilizing extraction conditions
adapted to a dry mill corn fractionation ethanol production
process. Generally, inventive supercritical carbon dioxide
extraction conditions which can be applied to corn germ to achieve
at least one of: greater amounts of corn oil from the same amount
of corn germ, generate the same amount of corn oil or greater
amounts of corn oil from an amount of corn germ in a lesser
duration of time, utilize lesser amounts of supercritical carbon
dioxide to generate the same or greater amounts of corn oil from an
amount of corn germ.
[0032] Now referring primarily to FIGS. 2-4, a corn germ fraction
(16) (also referred to in part as "an amount of corn germ") can be
generated as above-described or can be generated by any
conventional milling process or other corn germ production means.
While certain aspects of the inventive supercritical carbon dioxide
extraction conditions described herein were adapted for use with
the corn fractionation ethanol production systems (17) shown by
FIGS. 2-4, the invention is not so limited and the inventive
supercritical carbon dioxide extraction conditions can be adapted
for use in a wide variety applications which extract an amount of
corn germ oil (23) from an amount of corn germ (16).
[0033] Now referring primarily to FIGS. 3 and 4, the amount of corn
germ (16) can pass through a comminutor (38) to be reduced to a
plurality of corn germ particles (39) having a particle
configuration (whether by size, range of size, or shape or in
various permutations and combinations thereof) suitable for use
with the inventive extraction conditions described herein. The
particle configuration of the plurality of corn germ particles (39)
obtained (whether by sieving, sifting, independent of or in
combination with use of a comminutor (38)) allows the amount of
supercritical carbon dioxide (9) to fluidically engage the amount
of corn germ (16) in a manner which allows the amount of corn oil
(23) (or the extractable portion of corn oil (23)) contained in the
amount corn germ (16) to be solubilized and removed from the amount
of corn germ (16) at a particular combination of: a temperature, a
pressure, a ratio of supercritical carbon dioxide (9) to the amount
of corn germ (16) (wt./wt.), and pre-selected duration of time (the
"extraction event"). The inventive extraction conditions can be
utilized to overcome the un predictability of a number of factors
which affect the extraction event including without limitation
differences in the corn germ matrix (40) (see FIG. 6) presented by
the amount corn germ (16) which can vary in terms of the porosity,
the void volume, the pore configuration or range of pore
configurations, resistance to alteration of the corn germ matrix
(40) to pressure, resistance to alteration of the corn germ matrix
(40) to temperature, the amount of corn germ oil (23) contained by
the amount of corn germ (16), the solubility of the corn germ oil
(23) or components of the amount of corn germ oil (23) in the
amount supercritical carbon dioxide (9), or the like.
[0034] Now referring primarily to FIGS. 5 and 6, the plurality of
corn germ particles (40) generated from the amount of corn germ
(16) must be compatible with a given corn germ oil extraction
system (41). A first configuration of the plurality of particles
(40) which comprise the amount of corn germ (16) may be compatible
with a particular configuration of a corn germ oil extraction
system (41) under a first set of extraction conditions and
incompatible with the same corn germ oil extraction system (41)
under a second set of extraction conditions. For example, under a
first set of extraction conditions, the plurality of particles (39)
may allow sufficient flow of the amount of supercritical carbon
dioxide (9) through one or a plurality of extractor vessels (42)
(further described below) while under a second set of extraction
conditions, the plurality of particles may restrict flow through
one or more of the plurality of extractor vessels (42) such as by
reduction of flow of the amount of supercritical carbon dioxide
through fits which may be used to retain the plurality of particles
(39) in the plurality of extractor vessels (42).
[0035] With respect to certain embodiments of the invention
utilized with the above-described corn fractionation ethanol
production systems (17) (or other corn germ production means), the
comminutor (38) can be utilized to reduce the amount of corn germ
(16) to the plurality of corn germ particles (39) having a
configuration suitable for use with the inventive corn germ oil
extraction conditions described herein. The comminutor (38) can
operate to reduce the amount of corn germ (16) to the plurality of
particles (39) suitable for use with the invention. As to certain
non-limiting embodiments of the invention the comminuator (38) can
provide a particle configuration which can pass through a 20 mesh
screen each opening having a width of opening of about 0.33 inches
or about 850 .mu.M but not through a 100 mesh screen each opening
having a width of opening of about 0.0060 inches or about 150 or
can operate to reduce the amount of corn germ (16) to a plurality
of particles (39) which pass through about a 30 mesh sieve each
opening having a width of opening of about 0.21 inches or about 540
.mu.M but not through a 100 mesh screen. As too certain embodiments
of the invention the comminutor (38) can operate to reduce the
amount of corn germ (16) to a plurality of particles (39) which
pass through a 20 mesh sieve or a 30 mesh sieve without any
limitation as to a lower limit on particle size. A non-limiting
example of a comminutor (38) suitable for use with the invention
can be a hammermill adjusted to generate the plurality of particles
(39) of one or more of the above-described configurations. As but
one example, a hammermill available from Bliss Industries, Inc.,
Ponca City, Okla. can be utilized. With respect to certain
embodiments of the invention, one or more sifters, or separators,
or air lifts can be utilized separately or in combination with the
comminutor (38) to generate the plurality of particles (39) which
are not within the defined particle configuration. Each of the
trials set out by Example 1 included that portion of an amount corn
germ which was ground and passed through a 30 mesh sieve. It is not
intended that the above described particle configurations be
limiting with respect to the broader range of particle
configurations which can be utilized with the inventive extraction
conditions further described below.
[0036] Now referring primarily to FIGS. 5 and 6, the corn germ oil
extraction system (41) can include an extractor assembly (43) such
as the cascade extractor shown in the Figure which provides one or
a plurality of extractor vessels (42) each of which define a corn
germ extraction zone (43) inside of which the amount of corn germ
(16) which can be comminuted to provide a plurality of particles
(39) as above-described can be located for fluidic engagement with
an amount of supercritical carbon dioxide (9) to perform the
extraction event. Each of the extraction vessels (42) can
independently perform an extraction event on the amount of corn
germ (16) in manner which allows at least one extractor vessel
(42A) (shown in broken lines) to come off line for a duration of
time after the extraction event sufficient to remove the amount of
extracted corn germ (22) and introduce an amount of corn germ (16)
for a subsequent extraction event. Each of the plurality of
extractor vessels (42) can be coupled to a heat source (45) which
generates an amount of heat sufficient to maintain the amount of
supercritical carbon dioxide (9) at a temperature of between about
70.degree. C. and about 120.degree. C. during fluidic engagement
with the amount of corn germ (16) located inside said corn germ
extraction zone. The heat source (45) can be coupled to a
temperature adjustment element (46) which can monitor temperature
of the amount of supercritical carbon dioxide (9) in the corn germ
extraction zone (43) or can monitor other conditions outside of the
corn germ extraction zone such as the amount of corn oil (23)
solubilized in the amount of supercritical carbon dioxide (9) (the
"effluent"(46)) flowing from the corn germ extraction zone (43), or
other measure of the efficiency of the extraction event to allow
continuous adjustment of the temperature of the amount of
supercritical carbon dioxide (9) in the corn germ extraction zone
(43) to maintain a preselected temperature, a preselected
temperature profile, or a preselected corn germ extraction
efficiency profile based on monitoring the effluent (46) from the
corn germ extraction zone. The extractor assembly further includes
a plurality of conduits and valves (47) configured to allow
transfer of the amount of supercritical carbon dioxide (9) into and
away from the corn germ extraction zone (43). While a particular
example of a cascade extractor is shown in FIG. 5, it is not
intended that this configuration of cascade extractor be limiting
with respect to the numerous and varied configurations of cascade
extractors which could be utilized or made compatible with the
inventive supercritical carbon dioxide extraction conditions herein
described or utilized with or made compatible with other
configurations of extractor assemblies such as a continuous feed
extractor which continuously introduces an amount of corn germ (16)
into at least one extraction vessel (42) counter current to the
continuous introduction of an amount of supercritical carbon
dioxide (9).
[0037] The corn oil extraction system (41) can further include a
carbon dioxide recycle assembly (48) which can include at least one
separator (49) having at least one separator vessel (50) which
defines at least one corn oil separation zone (51) in which the
amount of corn oil (23) extracted from the amount of corn germ (16)
can be separated from the amount of supercritical carbon dioxide
(9) by establishing one or a plurality of corn oil separation
conditions in the at least one corn oil separation zone (51). The
at least one separator (49) further includes a plurality of
separator conduits and valves (52) configured to allow transfer of
the amount of supercritical carbon dioxide (9) into and away from
the at least one corn oil separation zone (50 and transfer of the
separated amount of corn oil (23) away from the at least one corn
oil separation zone (51).
[0038] The carbon dioxide recycle assembly (48) can further include
a condenser (52) which provides condensing conditions to establish
the separated amount of carbon dioxide (9) in a phase compatible
with a pressure generator (53) which establishes and maintains the
amount of supercritical carbon dioxide at pressure between about
7,000 psi and about 12,000 psi in the corn germ extraction zone
(43). The pressure generator (53) can be coupled to a pressure
adjustment element (54) which can monitor the pressure of the
amount supercritical carbon dioxide (9) in the corn germ extraction
zone (43) or can monitor other conditions outside of the corn germ
extraction zone (43) such as the amount of corn oil solubilized in
the effluent (46), or other measure of the efficiency of the
extraction event to allow continuous adjustment of the pressure of
the amount of supercritical carbon dioxide (9) in the corn germ
extraction zone (43) to establish or maintain a preselected
pressure, a preselected pressure profile, or a preselected corn
germ extraction efficiency profile based on monitoring the effluent
(46) from the corn germ extraction zone (43).
[0039] Now referring primarily to FIG. 5 and Table 1 set out below,
it can be understood that if the flow rate of the supercritical
carbon dioxide (9) in the corn germ extraction zone (43) has a
constant velocity (although in practice the velocity can also be
varied) then the effects of the alteration of the supercritical
carbon dioxide extraction conditions as to a temperature and a
pressure can be evaluated as to effect on a ratio of the amount of
supercritical carbon dioxide (9) at a given temperature and
pressure to the amount of corn germ (16) (wt./wt.) (also referred
to as the "solvent to feed ratio") to reach a particular extraction
event end point such as an amount of corn oil (23) of about twenty
percent of the amount of the corn germ (16) (wt./wt.). For example,
if the solvent to feed ratio is about 20 to 1 to obtain extraction
of an amount of corn germ oil (23) of twenty percent of the weight
of the amount of the corn germ (16) extracted, then for each ton of
corn germ oil (23) extracted about twenty tons of supercritical
carbon dioxide (9) would be utilized. If the solvent to feed ration
is about 2 to 1, then for each ton of corn germ oil (23) extracted
two tons of supercritical carbon dioxide (9) would be utilized and
so forth. The inventive dry corn fractionation plants
above-described as a non-limiting example can process between about
3,000 tons and 5,000 tons of whole corn (2) per day to generate
about 250 tons to about 400 tons of corn germ fraction (16). If the
corn oil extraction system (41) processes 300 tons of corn germ
fraction (16) per day at a solvent to feed ratio of about 20 to 1
then about 6,000 tons of supercritical carbon dioxide (9) would
pass through the corn germ extraction zone (43) of the extractor
assembly and be recovered by the carbon dioxide recycle assembly
(48) per day. However, if the corn oil extraction system (41)
processes the same 300 tons of corn germ fraction (16) per day at a
solvent to feed ratio of about 2 to 1 then only 600 tons of
supercritical carbon dioxide (9) would pass through the corn germ
extraction zone (43) of the extractor assembly (43) and be
recovered by the carbon dioxide recycle assembly (48) per day.
[0040] Even if the configuration of the extractor assembly (43)
remains substantially the same regardless of the solvent to feed
ratio because the mass of the amount of corn germ (16) extracted
remains constant, it can be understood that at least the components
of the carbon dioxide recycle assembly (48) would be necessarily
scaled upward as solvent to feed ratio increases over the 10 fold
range shown in Table 1. As the solvent to feed ratio increases both
the capital costs and the cost to operate the corn germ oil
extraction system (41) also increase. Corn germ oil extraction
systems (41) which adapted to or built to utilize the inventive
solvent to feed ratios in the range of about 2 to 1 to about 6.5 to
1 can be extremely economically operate with respect to both
capital cost and operating costs while corn oil extraction systems
(41) which are adapted to or utilize the inventive solvent to feed
ratios in the range of about 7.0 to 1 to about 18.5 to 1 are likely
be only marginally economical to operate, and corn oil extraction
systems (41) which utilize solvent to feed ratios of greater than
20 to 1 are likely to be impractical to build or uneconomical to
operate.
TABLE-US-00001 TABLE 1 Effect of Pressure and Temperature on
Extraction Efficiency as Represented by Solvent/Feed Ration to
Reach 20% of Feedstock wt/wt Extraction. Temper- Solvent/Feed
Ration to ature Reach 20% of Feedstock Pressure (.degree. C.) wt/wt
Extraction 9300 110 ~2.0 9000 100 ~2.5 9000 80 ~3.5 9300 80 ~4.5
9580 87.3 ~5.0 8000 95 ~5.5 7500 100 ~5.5 8000 85 ~6.0 8500 90 ~6.5
7500 90 ~7.0 7000 80 ~8.0 6000 85 ~10 5800 57 ~13.5 5000 80 >20
6000 70 ~23 5000 100 >25 1600 20 >30
[0041] Now referring primarily to FIG. 7 and Table 1, certain
extraction events are plotted to show the solvent to feed ratio as
a function of the percent of the weight of the amount of the corn
germ (16) extracted for corn germ extraction conditions which
result in solvent to feed ratios of less than about 5 to 1 to
achieve extraction of an amount of corn oil (23) of about twenty
percent of the weight of the amount of corn germ (16) extracted. It
is not intended that the examples shown in Table 1 be limiting with
respect to the weight percent of the amount of corn oil which can
be achieved utilizing the stated solvent to feed ratios, and
significantly greater weight percent corn germ oil may be extracted
from an amount of corn germ having significantly greater amounts of
extractable corn germ oil (23), as a non-limiting example forty
five percent extractable corn oil by weight. Similarly, these
examples are not intended to preclude applications to an amount of
corn germ oil (23) having a part of the extractable corn germ oil
(23) removed prior to extraction with an amount of supercritical
carbon dioxide in which case the remaining extractable amount of
corn germ oil may be less than twenty percent by weight. As such
the term "an amount of corn germ" is intended to include any source
of corn germ or pre-processed corn germ whether or not a part of
the corn germ oil (23) has been prior removed by another
process(es) prior to extraction with the invention extraction
conditions described herein.
[0042] As can be understood from the plots shown, fluidically
engaging an amount of supercritical carbon dioxide (9) with an
amount of corn germ (16) at a pressure of between about 9,000 psi
and about 10,000 psi and at temperatures of between about
80.degree. C. and about 110.degree. C. (even greater pressures of
up to 12,000 psi and even greater temperatures of up to about
120.degree. C. can be utilized) can achieve solvent to feed ratios
of less than about 5 to 1 and even about 2 to 1 or even less than
about 2 to 1 as shown by the examples performed at 9,300 psi and
110.degree. C. (about 1.75 to 1) (see also Examples below).
Additionally, dramatic reduction of solvent to feed ratios can be
achieved by increasing temperature when the pressure is established
at between about 9,000 psi to about 10,000 psi (or even greater
pressure up to about 12,000). It is believed that these inventive
solvent to feed ratios of less than about 5 to 1, or about 2 to 1,
or less that about 2 to 1 and the corn germ extraction conditions
utilized to achieve these solvent to feed ratios of between about
9,000 psi and about 10,000 psi and between about 85.degree. C. and
about 110.degree. C. (or up to about 12,000 psi and up to about
120.degree. C.) have not been taught prior to the invention.
[0043] Now referring primarily to FIG. 8 and Table 1, certain
extraction events are plotted to show solvent to feed ratio as a
function of the percent of the weight of the amount of the corn
germ (16) extracted for corn germ extraction conditions which
result in solvent to feed ratios of about 5 to 1 to about 7.0 to 1
to achieve extraction of an amount of corn oil (23) of about twenty
percent of the weight of the amount of corn germ (16) extracted. As
can be understood from the plots shown, fluidically engaging
supercritical carbon dioxide with an amount of corn germ at a
pressure of between about 7,500 and about 8,500 psi at temperatures
of between about 90.degree. C. and about 100.degree. C. can achieve
solvent to feed ratios of between about 5 to 1 to about 7 to 1. It
is believed that these advantageous solvent to feed ratios of
between 5 to 1 to about and 7 to 1 and the particular corn germ
extraction conditions utilized to achieve these solvent to feed
ratios of between about 7,500 psi and about 8,500 psi and between
about 85.degree. C. and about 100.degree. C. have not been taught
prior to the invention.
[0044] Now referring primarily FIG. 9 and Table 1, certain
extraction events are plotted to show the solvent to feed ratio as
a function of the percent of the weight of the amount of the corn
germ extracted for corn germ extraction conditions which result in
solvent to feed ratios of between about 7.0 to 1 and about 10 to 1
to achieve extraction of an amount of corn oil of about twenty
percent of the weight of the amount of corn germ extracted. As can
be understood fluidically engaging supercritical carbon dioxide
with an amount of corn germ at a pressure of between about 6,000
psi and about 7,500 psi at temperatures of between about 80.degree.
C. and about 90.degree. C. can achieve solvent to feed ratios of
between about 7 to 1 to about 10 to 1. It is believed that these
advantageous solvent to feed ratios of between 7 to 1 to about and
10 to 1 and the particular corn germ extraction conditions utilized
to achieve these solvent to feed ratios of between about 6,000 psi
and about 7,500 psi and between about 80.degree. C. and about
90.degree. C. have not been taught prior to the invention.
[0045] Now referring primarily to FIG. 10 and Table 1, certain
extraction events are plotted to show the solvent to feed ratio as
a function of the percent of the weight of the amount of the corn
germ extracted for corn germ extraction conditions which show that
pressure lower than about 6,000 psi and temperatures of about
60.degree. C. result in solvent to feed ratios of greater than
about 10 to 1 to achieve extraction of an amount of corn oil of
about twenty percent of the weight of the amount of corn germ
extracted. Solvent to feed ratios greater than about 10:1 are
likely to be impractical or uneconomic in the context of corn
fractionation production systems as above-described.
[0046] Now referring primarily to FIG. 11 and Table 1, certain
extraction events are plotted to show the solvent to feed ratio as
a function of the percent of the weight of the amount of the corn
germ (16) extracted for corn germ extraction conditions which
result in solvent to feed ratios of greater than about 20 to 1 to
achieve extraction of an amount of corn oil of about twenty percent
of the weight of the amount of corn germ extracted. Solvent to feed
ratios greater than about 10:1 are likely to be impractical or
uneconomic in the context of corn fractionation production systems
as above-described.
[0047] Also, as can be seen by the trials run at 5,000 psi that a
substantial increase temperature from about 80.degree. C. to
100.degree. C. can actually operate to adversely increase the
solvent to feed ratio. This teaches away from the inventive corn
germ extraction conditions above described which show substantial
reductions in solvent to feed ratio as temperature increases and
may account for higher temperatures and pressures not being prior
discovered.
[0048] Again referring primarily to FIG. 5, the corn oil extraction
system (41) can further provide a water removal element (55) which
operates to remove an amount of water from the amount of
supercritical carbon dioxide (9) prior to fluidic engagement with
the amount of corn germ (16) in the corn germ extraction zone (43)
to establish an amount of water (56) contained by the amount of
supercritical carbon dioxide (9) of about one percent to about
seven percent by weight or an amount of water (56) by weight which
upon fluidic engagement with the amount of corn germ (16) in the
corn germ extraction zone (43) reduces the amount of water (57)
contained by the amount of extracted corn germ (22) (see FIGS. 3
and 4) to between about one percent to about fourteen percent by
weight.
[0049] Again referring primarily to FIG. 4, a corn germ animal feed
(58) can be produced by mixing (59) the amount of extracted corn
germ (22) having the amount of water (57) reduced to between about
one percent to about seven percent by weight with an amount of
condensed distiller soluble (30) having a solids content of between
about thirty percent to about sixty percent by weight. In one
embodiment of the inventive method of producing the corn germ
animal feed (58) above described, the amount of condensed distiller
soluble (30) mixed (59) with the amount of extracted corn germ (22)
increases the amount of water (57) contained by the amount of
extracted corn germ to an amount of water (57) by weight which does
not exceed about fourteen percent water or does not exceed an
amount of water (57) by weight which requires the additional step
of drying (60) the animal feed prior to placement in the storage
unit (18) or sold. In an alternate embodiment of the inventive
method of producing the corn germ animal feed above described, the
amount of condensed distiller soluble (30) mixed with the amount of
extracted corn germ (22) to introduce the desired amount of solids
increases the amount of water (57) contained by the amount of
extracted corn germ (22) above fourteen percent by weight or above
an amount of water by weight which requires removal of an amount of
the water (57) then contained by the amount of extracted corn germ
(22). However, this process still confers an advantage because less
water needs to be removed (60) than would conventionally be
required if the condensed distiller soluble (30) was mixed (59)
with an amount of corn germ (16) or with an amount of extracted
corn germ (22) which typically contains an amount of water (57) of
between about seven percent to about fourteen percent by weight or
containing a greater amount of water (57) than between about one
percent and about seven percent by weight. By avoiding any removal
(60) of the amount of water (57), or by reducing the amount of
water (57) to be removed (60), contained by the amount of extracted
corn germ (22) subsequent to mixing (59) with the amount of
condensed distiller soluble (30), a lesser amount of fuel (33) or
thermal energy (11) can be consumed to produce the same amount of
corn germ animal feed (58) as above-described. As to those
embodiments of the animal feed which require removal of a part of
the amount of water (27) contained by the extracted corn germ (22)
after mixing (59) with the amount of condensed distiller soluble
(30), embodiments of the invention can further include a dryer (60)
capable of reducing the amount of water (57) contained by the
amount of corn germ (22) mixed (59) with said amount of condensed
distillation soluble (30) having the amount of solids in the range
of about 20 percent by weight to about 60 percent by weight to
between about eight percent by weight to about fourteen percent by
weight. Because the amount of water to be removed can be less when
the animal feed is prepared by the above-described method, the
dryer (60) can be a less expensive type of dryer (60) such as a
rotary dryer. A rotary dryer suitable for use with the invention
can be obtained for example from FMC Corporation or ICM, Inc.
Example 1
[0050] A series of trials were conducted to assess the effect of
temperature and pressure on the carbon dioxide extraction (21) of
corn oil (23) from the corn germ fraction (16) obtained from the
corn fractionation process (13).
Trial 1: 100 ml Extraction of Corn Germ:
[0051] 9200 psi and 90.degree. C. 35.55 g of corn germ feedstock
was ground and sieved, and placed in a 100 ml extraction vessel and
extracted with pure carbon dioxide at a pressure of 9200 psi and a
temperature of 90.degree. C. The flow rate was 4 liters/minute. A
total of 8.33 g of yellow corn oil was extracted (23.43% by weight
of feedstock). The solvent to feedstock ratio was <8
(S/F<8).
Trial 2: 100 ml Extraction of Corn Germ:
[0052] 7500 psi and 80.degree. C. 35.55 g of corn germ feedstock
was ground and sieved, and placed in a 100 ml extraction vessel and
extracted with pure carbon dioxide at a pressure of 7500 psi and a
temperature of 80.degree. C. The flow rate was 4 liters/minute. A
total of 6.26 g of yellow corn oil was extracted (17.60% by weight
of feedstock).
Trial 3: 100 ml Extraction of Corn Germ:
[0053] 6000 psi and 70.degree. C. 35.55 g of corn germ feedstock
was ground and sieved, and placed in a 100 ml extraction vessel and
extracted with pure carbon dioxide at a pressure of 6000 psi and a
temperature of 70.degree. C. The flow rate was 4 liters/minute. A
total of 7.33 g of yellow corn oil was extracted (20.61% by weight
of feedstock). Solvent/feed ratio of about 15/1.
Trial 4: 100 ml Extraction of Corn Germ:
[0054] 5000 psi and 60.degree. C. 35.55 g of corn germ feedstock
was ground and sieved, and placed in a 100 ml extraction vessel and
extracted with pure carbon dioxide at a pressure of 5000 psi and a
temperature of 60.degree. C. The flow rate was 4 liters/minute. A
total of 7.38 g of yellow corn oil was extracted (20.75% by weight
of feedstock). Solvent/feed ratio of about 25/1.
Trial 5: 100 ml Extraction of Corn Germ:
[0055] 8000 psi and 85.degree. C. 35.55 g of corn germ feedstock
was ground and sieved, and placed in a 100 ml extraction vessel and
extracted with pure carbon dioxide at a pressure of 8000 psi and a
temperature of 85.degree. C. The flow rate was 4 liters/minute. A
total of 7.57 g of yellow corn oil was extracted (21.29% by weight
of feedstock). Solvent/feed ratio of about 10/1.
Trial 6: 100 ml Extraction of Corn Germ: 8500 Psi and 90.degree.
C.
[0056] 35.55 g of corn germ feedstock was ground and sieved, and
placed in a 100 ml extraction vessel and extracted with pure carbon
dioxide at a pressure of 8500 psi and a temperature of 90.degree.
C. The flow rate was 4 liters/minute. A total of 7.62 g of yellow
corn oil was extracted (21.43% by weight of feedstock).
Solvent/feed ratio of about 12/1.
Trial 7: 100 ml Extraction of Corn Germ/7500 Psi and 90.degree.
C.
[0057] 35.55 g of corn germ feedstock was ground and sieved, and
placed in a 100 ml extraction vessel and extracted with pure carbon
dioxide at a pressure of 7500 psi and a temperature of 90.degree.
C. The flow rate was 4 liters/minute. A total of 7.50 g of yellow
corn oil was extracted (21.09% by weight of feedstock).
Solvent/feed ratio of about 12/1.
Trail 8: 100 ml Extraction of Corn Germ:
[0058] 7000 psi and 80.degree. C. 35.55 g of corn germ feedstock
was ground and sieved, and placed in a 100 ml extraction vessel and
extracted with pure carbon dioxide at a pressure of 7000 psi and a
temperature of 80.degree. C. The flow rate was 4 liters/minute. A
total of 7.40 g of yellow corn oil was extracted (20.81% by weight
of feedstock). Solvent/feed ratio of about 12/1.
Trial 9: 100 ml Extraction of Corn Germ:
[0059] 6,000 psi and 85.degree. C. 35.55 g of corn germ feedstock
was ground and sieved, and placed in a 100 ml extraction vessel and
extracted with pure carbon dioxide at a pressure of 6000 psi and a
temperature of 85.degree. C. The flow rate was 4 liters/minute. A
total of 7.52 g of yellow corn oil was extracted (21.15% by weight
of feedstock). Solvent/feed ratio of about 18/1.
Trial 10: 100 ml Extraction of Corn Germ 1600 Psi and 20.degree.
C.
[0060] 35.55 g of corn germ feedstock was ground and sieved, and
placed in a 100 ml extraction vessel and extracted with pure carbon
dioxide at a pressure of 1600 psi and an ambient temperature of
20.degree. C. The flow rate was 4 liters/minute. A total of 4.22 g
of yellow corn oil was extracted (11.87% by weight of feedstock).
Solvent/feed ratio is >65/1.
[0061] The plots shown in the Figures are the result of these
trials or trails similarly performed.
[0062] As can be easily understood from the foregoing, the basic
concepts of the present invention may be embodied in a variety of
ways which includes the best mode of the invention. The invention
involves numerous and varied corn germ oil extraction devices and
methods of extracting corn oil from corn germ whether derived from
conventional corn milling processes, from the kernel fractionation
processes incorporated by reference, or otherwise. While certain
examples are provided in the context of dry corn fractionation
processes, it is not intended that these examples limit the use of
the invention to corn germ derived solely from these inventive dry
corn fractionation process (17), but rather are intended to be
illustrative such that a person of ordinary skill in the art can
make and use the invention in the context of the numerous and
varied processes that produce an amount of corn germ from which
corn germ oil (23) can be extracted.
[0063] As such, the particular embodiments or elements of the
invention disclosed by the description or shown in the figures or
tables accompanying this application are not intended to be
limiting, but rather exemplary of the numerous and varied
embodiments generically encompassed by the invention or equivalents
encompassed with respect to any particular element thereof. In
addition, the specific description of a single embodiment or
element of the invention may not explicitly describe all
embodiments or elements possible; many alternatives are implicitly
disclosed by the description and figures.
[0064] It should be understood that each element of an apparatus or
each step of a method may be described by an apparatus term or
method term. Such terms can be substituted where desired to make
explicit the implicitly broad coverage to which this invention is
entitled. As but one example, it should be understood that all
steps of a method may be disclosed as an action, a means for taking
that action, or as an element which causes that action. Similarly,
each element of an apparatus may be disclosed as the physical
element or the action which that physical element facilitates. As
but one example, the disclosure of an "extractor" should be
understood to encompass disclosure of the act of
"extracting"--whether explicitly discussed or not--and, conversely,
were there effectively disclosure of the act of "extracting", such
a disclosure should be understood to encompass disclosure of a
"extractor" and even a "means for extracting." Such alternative
terms for each element or step are to be understood to be
explicitly included in the description.
[0065] In addition, as to each term used it should be understood
that unless its utilization in this application is inconsistent
with such interpretation, common dictionary definitions should be
understood to included in the description for each term as
contained in the Random House Webster's Unabridged Dictionary,
second edition, each definition hereby incorporated by
reference.
[0066] Thus, the applicant(s) should be understood to claim at
least: i) each of the kernel fractionation devices or systems
herein disclosed and described, ii) the related methods disclosed
and described, iii) similar, equivalent, and even implicit
variations of each of these devices and methods, iv) those
alternative embodiments which accomplish each of the functions
shown, disclosed, or described, v) those alternative designs and
methods which accomplish each of the functions shown as are
implicit to accomplish that which is disclosed and described, vi)
each feature, component, and step shown as separate and independent
inventions, vii) the applications enhanced by the various systems
or components disclosed, viii) the resulting products produced by
such systems or components, ix) methods and apparatuses
substantially as described hereinbefore and with reference to any
of the accompanying examples, x) the various combinations and
permutations of each of the previous elements disclosed.
[0067] The background section of this patent application provides a
statement of the field of endeavor to which the invention pertains.
This section may also incorporate or contain paraphrasing of
certain United States patents, patent applications, publications,
or subject matter of the claimed invention useful in relating
information, problems, or concerns about the state of technology to
which the invention is drawn toward. It is not intended that any
United States patent, patent application, publication, statement or
other information cited or incorporated herein be interpreted,
construed or deemed to be admitted as prior art with respect to the
invention.
[0068] The claims set forth in this specification are hereby
incorporated by reference as part of this description of the
invention, and the applicant expressly reserves the right to use
all of or a portion of such incorporated content of such claims as
additional description to support any of or all of the claims or
any element or component thereof, and the applicant further
expressly reserves the right to move any portion of or all of the
incorporated content of such claims or any element or component
thereof from the description into the claims or vice-versa as
necessary to define the matter for which protection is sought by
this application or by any subsequent application or continuation,
division, or continuation-in-part application thereof, or to obtain
any benefit of, reduction in fees pursuant to, or to comply with
the patent laws, rules, or regulations of any country or treaty,
and such content incorporated by reference shall survive during the
entire pendency of this application including any subsequent
continuation, division, or continuation-in-part application thereof
or any reissue or extension thereon.
[0069] The claims set forth below are intended to describe the
metes and bounds of a limited number of the preferred embodiments
of the invention and are not to be construed as the broadest
embodiment of the invention or a complete listing of embodiments of
the invention that may be claimed. The applicant does not waive any
right to develop further claims based upon the description set
forth above as a part of any continuation, division, or
continuation-in-part, or similar application.
* * * * *