U.S. patent application number 14/054253 was filed with the patent office on 2014-02-13 for method of supercritical fluid fractionation of oil seed extraction materials.
This patent application is currently assigned to MOR Supercritical, LLC. The applicant listed for this patent is MOR Supercritical, LLC. Invention is credited to Rodger T. Marentis.
Application Number | 20140046080 14/054253 |
Document ID | / |
Family ID | 40221652 |
Filed Date | 2014-02-13 |
United States Patent
Application |
20140046080 |
Kind Code |
A1 |
Marentis; Rodger T. |
February 13, 2014 |
Method Of Supercritical Fluid Fractionation Of Oil Seed Extraction
Materials
Abstract
Generally, a method of pressure regulated supercritical fluid
fractionation of oil seed extraction materials which can be
utilized to refine oil seed extraction material established in an
amount of supercritical fluid. Specifically, a method of pressure
regulated supercritical fluid fractionation of corn germ extraction
material to produce a refined corn oil extraction material.
Inventors: |
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: |
40221652 |
Appl. No.: |
14/054253 |
Filed: |
October 15, 2013 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
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13428612 |
Mar 23, 2012 |
8557318 |
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14054253 |
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12217497 |
Jul 5, 2008 |
8142830 |
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13428612 |
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60958472 |
Jul 6, 2007 |
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Current U.S.
Class: |
554/78 |
Current CPC
Class: |
A23L 5/20 20160801; Y02P
20/54 20151101; C11B 3/00 20130101; Y02P 20/544 20151101; C11B
1/104 20130101 |
Class at
Publication: |
554/78 |
International
Class: |
C11B 3/00 20060101
C11B003/00 |
Claims
1-19. (canceled)
20. A method of fractionating oil seed extraction material,
comprising the steps of: a) establishing an amount of oil seed
extraction material in an amount of supercritical carbon dioxide in
a first oil seed extraction material separation zone at a
temperature of between about 60.degree. C. and about 110.degree.
C.; b) adjusting pressure of said amount of oil seed extraction
material in said amount of supercritical carbon dioxide in said
first oil seed extraction material separation zone to between about
200 bar and about 400 bar to achieve a density of said
supercritical fluid of between about 0.75 g/mL and about 0.85 g/mL;
and c) separating a phosphatide fraction from said oil seed
extraction material in said amount of supercritical carbon dioxide
resulting in a triglyceride fraction and a fatty acid fraction
remaining in said amount of supercritical carbon dioxide.
21. The method of fractionating oil seed extraction material as
described in claim 20, further comprising the steps of: a)
delivering said amount of oil seed extraction material in said
amount of supercritical carbon dioxide having said phosphatide
fraction separated in said first oil seed extraction material
separation zone to a second oil seed extraction material separation
zone; b) maintaining said amount of oil seed extraction material in
said amount of supercritical carbon dioxide having said phosphatid
fraction separated in said first oil seed extraction material
separation zone at a temperature of between about 60.degree. C. and
about 100.degree. C.; c) adjusting pressure of said amount of oil
seed extraction material in said amount of supercritical carbon
dioxide having said phosphatid fraction separated in said first oil
seed extraction material separation zone to between about 150 bar
and about 300 bar to achieve a density of said supercritical fluid
of between about 0.65 g/mL and about 0.75 g/mL; and d) separating a
triglyceride fraction from said oil seed extraction material in
said amount of supercritical carbon dioxide having said phosphatide
fraction separated in said first oil seed extraction material
separation zone.
22. The method of fractionating oil seed extraction material as
described in claim 21, further comprising the steps of: a)
delivering said amount of oil seed extraction material in said
amount of supercritical oil seed having said phosphatide fraction
separated in said first oil seed extraction material separation
zone and said triglyceride fraction separated in said second oil
seed extraction material separation zone to a third oil seed
extraction material separation zone; b) maintaining said amount of
oil seed extraction material in said amount of supercritical carbon
dioxide having said phosphatid fraction separated in said first oil
seed extraction material separation zone and said triglyceride
fraction separated in said second oil seed extraction material
separation zone at a temperature of between about 40.degree. C. and
about 70.degree. C.; c) adjusting pressure of said amount of oil
seed extraction material in said amount of supercritical carbon
dioxide having said phosphatid fraction separated in said first oil
seed extraction material separation zone and said triglyceride
fraction separated in said second oil seed extraction material
separation zone to between about 75 bar and about 100 bar to
achieve a density of said supercritical fluid of between about 0.10
g/mL and about 0.30 g/mL; and d) separating an free fatty acid
fraction from said oil seed extraction material in said amount of
supercritical carbon dioxide having said phosphatid fraction
separated in said first oil seed extraction material separation
zone and said triglyceride fraction separated in said second oil
seed extraction material separation zone.
23. The method of fractionating oil seed extraction material as
described in claim 22, wherein said step of maintaining said amount
of oil seed extraction material in said amount of supercritical
carbon dioxide in said first oil seed extraction material
separation zone at a temperature of between about 60.degree. C. and
about 110.degree. C. comprises the step of maintaining said amount
of oil seed extraction material in said amount of supercritical
carbon dioxide in said first oil seed extraction material
separation zone at a temperature of between about 70.degree. C. and
about 90.degree. C.
24. The method of fractionating oil seed extraction material as
described in claim 23, wherein said step of adjusting pressure of
said amount of oil seed extraction material in said amount of
supercritical carbon dioxide in said first oil seed extraction
material separation zone to between about 200 bar and about 400 bar
to achieve a density of said supercritical fluid of between about
0.75 g/mL and about 0.85 g/mL comprises the step of adjusting
pressure of said amount of oil seed extraction material in said
amount of supercritical carbon dioxide in said first oil seed
extraction material separation zone to between about 250 bar and
about 350 bar to achieve a density of said supercritical fluid of
between about 0.75 g/mL and about 0.85 g/mL.
25. The method of fractionating oil seed extraction material as
described in claim 24, wherein said step of maintaining said amount
of oil seed extraction material in said amount of supercritical
carbon dioxide having said phosphatid fraction separated in said
first oil seed extraction material separation zone at a temperature
of between about 60.degree. C. and about 100.degree. C. comprises
the step of maintaining said amount of oil seed extraction material
in said amount of supercritical carbon dioxide having said
phosphatid fraction separated in said first oil seed extraction
material separation zone at a temperature of between about
70.degree. C. and about 90.degree. C.
26. The method of fractionating oil seed extraction material as
described in claim 25, wherein said step of adjusting pressure of
said amount of oil seed extraction material in said amount of
supercritical carbon dioxide having said phosphatid fraction
separated in said first oil seed extraction material separation
zone to between about 150 bar and about 300 bar to achieve a
density of said supercritical fluid of between about 0.65 g/mL and
about 0.75 g/mL comprises the step of adjusting pressure of said
amount of oil seed extraction material in said amount of
supercritical carbon dioxide having said phosphatid fraction
separated in said first oil seed extraction material separation
zone to between about 175 bar and about 250 bar to achieve a
density of said supercritical fluid of between about 0.65 g/mL and
about 0.75 g/mL.
27. The method of fractionating oil seed extraction material as
described in claim 26, wherein said step of maintaining said amount
of oil seed extraction material in said amount of supercritical
carbon dioxide having said phosphatid fraction separated in said
first oil seed extraction material separation zone and said
triglyceride fraction separated in said second oil seed extraction
material separation zone at a temperature of between about
40.degree. C. and about 70.degree. C. comprises the step of
maintaining said amount of oil seed extraction material in said
amount of supercritical carbon dioxide having said phosphatid
fraction separated in said first oil seed extraction material
separation zone and said triglyceride fraction separated in said
second oil seed extraction material separation zone at a
temperature of between about 45.degree. C. and about 65.degree.
C.
28. The method of fractionating oil seed extraction material as
described in claim 27, wherein said step of adjusting pressure of
said amount of oil seed extraction material in said amount of
supercritical carbon dioxide having said phosphatid fraction
separated in said first oil seed extraction material separation
zone and said triglyceride fraction separated in said second oil
seed extraction material separation zone to between about 75 bar
and about 100 bar to achieve a density of said supercritical fluid
of between about 0.10 g/mL and about 0.30 g/mL comprises the step
of adjusting pressure of said amount of oil seed extraction
material in said amount of supercritical carbon dioxide having said
phosphatid fraction separated in said first oil seed extraction
material separation zone and said triglyceride fraction separated
in said second oil seed extraction material separation zone to
between about 80 bar and about 95 bar to achieve a density of said
supercritical fluid of between about 0.10 g/mL and about 0.30
g/mL.
29. The method of fractionating oil seed extraction material as
described in claim 28, wherein said step of maintaining said amount
of oil seed extraction material in said amount of supercritical
carbon dioxide in said first oil seed extraction material
separation zone at a temperature of between about 70.degree. C. and
about 90.degree. C. comprises the step of maintaining said amount
of oil seed extraction material in said amount of supercritical
carbon dioxide in said first oil seed extraction material
separation zone at a temperature of between about 75.degree. C. and
about 85.degree. C.
30. The method of fractionating oil seed extraction material as
described in claim 29, wherein said step of adjusting pressure of
said amount of oil seed extraction material in said amount of
supercritical carbon dioxide in said first oil seed extraction
material separation zone to between about 250 bar and about 350 bar
to achieve a density of said supercritical fluid of between about
0.75 g/mL and about 0.85 g/mL comprises the step of adjusting
pressure of said amount of oil seed extraction material in said
amount of supercritical carbon dioxide in said first oil seed
extraction material separation zone to between about 275 bar and
about 325 bar to achieve a density of said supercritical fluid of
between about 0.75 g/mL and about 0.85 g/mL.
31. The method of fractionating oil seed extraction material as
described in claim 30, wherein said step of maintaining said amount
of oil seed extraction material in said amount of supercritical
carbon dioxide having said phosphatid fraction separated in said
first oil seed extraction material separation zone at a temperature
of between about 70.degree. C. and about 90.degree. C. comprises
the step of maintaining said amount of oil seed extraction material
in said amount of supercritical carbon dioxide having said
phosphatid fraction separated in said first oil seed extraction
material separation zone at a temperature of between about
75.degree. C. and about 85.degree. C.
32. The method of fractionating oil seed extraction material as
described in claim 31, wherein said step of adjusting pressure of
said amount of oil seed extraction material in said amount of
supercritical carbon dioxide having said phosphatid fraction
separated in said first oil seed extraction material separation
zone to between about 175 bar and about 250 bar to achieve a
density of said supercritical fluid of between about 0.65 g/mL and
about 0.75 g/mL comprises the step of adjusting pressure of said
amount of oil seed extraction material in said amount of
supercritical carbon dioxide having said phosphatid fraction
separated in said first oil seed extraction material separation
zone to between about 195 bar and about 230 bar to achieve a
density of said supercritical fluid of between about 0.65 g/mL and
about 0.75 g/mL.
33. The method of fractionating oil seed extraction material as
described in claim 32, wherein said step of maintaining said amount
of oil seed extraction material in said amount of supercritical
carbon dioxide having said phosphatid fraction separated in said
first oil seed extraction material separation zone and said
triglyceride fraction separated in said second oil seed extraction
material separation zone at a temperature of between about
45.degree. C. and about 65.degree. C. comprises the step of
maintaining said amount of oil seed extraction material in said
amount of supercritical carbon dioxide having said phosphatid
fraction separated in said first oil seed extraction material
separation zone and said triglyceride fraction separated in said
second oil seed extraction material separation zone at a
temperature of between about 50.degree. C. and about 60.degree.
C.
34. The method of fractionating oil seed extraction material as
described in claim 33, wherein said step of adjusting pressure of
said amount of oil seed extraction material in said amount of
supercritical carbon dioxide having said phosphatid fraction
separated in said first oil seed extraction material separation
zone and said triglyceride fraction separated in said second oil
seed extraction material separation zone to between about 80 bar
and about 95 bar to achieve a density of said supercritical fluid
of between about 0.10 g/mL and about 0.30 g/mL comprises the step
of adjusting pressure of said amount of oil seed extraction
material in said amount of supercritical carbon dioxide having said
phosphatid fraction separated in said first oil seed extraction
material separation zone and said triglyceride fraction separated
in said second oil seed extraction material separation zone to
between about 80 bar and about 90 bar to achieve a density of said
supercritical fluid of between about 0.10 g/mL and about 0.30
g/mL.
35. The method of fractionating oil seed extraction material as
described in claim 34, wherein oil seed extraction material
comprises corn germ extraction material.
Description
[0001] This United States Patent application is a continuation of
U.S. patent application Ser. No. 13/428,612, filed Mar. 23, 2012,
which is a continuation of U.S. patent application Ser. No.
12/217,497, filed Jul. 5, 2008, now U.S. Pat. No. 8,142,830, issued
Mar. 27, 2012, which claims the benefit of U.S. Provisional Patent
Application No. 60/958,472, filed Jul. 6, 2007, each hereby
incorporated by reference herein.
I. BACKGROUND
[0002] Generally, a method of pressure regulated supercritical
fluid fractionation of oil seed extraction materials which can be
utilized to refine oil seed extraction material established in an
amount of supercritical fluid. Specifically, a method of pressure
regulated supercritical fluid fractionation of corn germ extraction
material to produce a refined corn oil extraction material.
[0003] Oil Seed extraction materials which include materials
extracted from the entirety or parts of various seeds such as corn
(typically the corn germ), cotton, rape, safflower, sunflower,
flax, or the like, can be generated by a wide variety of extraction
methods, such as, solvent extraction, hydraulic pressing, expeller
pressing, or the like. Useful solvents for solvent extraction can
include hexane, n-hexane, isopropyl alcohol, supercritical fluids,
supercritical carbon dioxide, and other similar solvents.
[0004] There is a large commercial market for oil seed extraction
materials suitably refined to meet the varying standards for direct
use as fuels, the production of fuels, the processing of foods,
addition to foods, and food. The oil seed extraction materials
obtained by these extraction methods exhibit a correspondingly wide
range of compositions as mixtures of neutral extraction oils, fatty
acids, and a greater or lesser amount of undesired impurities. For
example, the undesired impurities in the corn germ extraction
material can include one or more of: free fatty acids (FFA) from
the degradation of corn germ oil by hydrolysis, phosphatides
(hydratable and non-hydratable), organic compounds which contribute
certain colors, flavors or odors, particulates entrained by the
extracted corn germ extraction material, or the like.
[0005] A significant problem with the refining of oil seed
extraction material including corn germ extraction material may be
that while a wide variety of methods for the extraction of oil seed
extraction material from oil seeds have developed over the past
decades, relatively few methods of refining oil seed extraction
material have developed over the same period. For example, corn
germ extraction material continues to be refined by addition of a
base such as sodium hydroxide, soda ash, sodium bicarbonate,
potassium hydroxide, or the like, which reacts with FFA to produce
an emulsion of neutral corn germ extraction oils, a soap mass
(often referred to as the "soap stock"), and residual base. The
emulsion can centrifuged to separate the neutral corn germ oils
from the soap stock and the residual base. The neutral corn germ
oils are typically combined with an amount of silica to trap
residue soap stock, residual phosphorus, and trace metals. The
silica being removed from the neutral corn germ extraction oils by
filtration. The resulting neutral corn germ oils may be bleached to
reduce color. The corn oil generated may be suitable for a wide
variety of uses depending on the exact manner of applying the
above-described general steps of the corn germ extraction material
refining process.
[0006] While this centrifugal refining process is typically
suitable for processing oil seed extraction materials and
specifically suitable across the wide range of corn germ extraction
material compositions generated by the various corn germ extraction
material extraction techniques, it has certain disadvantages in
that the centrifugal refining process involves the utilization of
equipment costly to purchase and maintain, the various extraction
processes and the centrifugal refining process may operate separate
from one another without significant feed back from the refining
process to the extraction process, and without limiting the
disadvantages of the centrifugal refining process, may be more
costly per unit of refined corn germ extraction material than
necessary based upon the higher quality of corn germ extract
materials being generated by more recently developed corn germ
extraction material extraction processes.
[0007] Interestingly, due to the prevalence and overall suitability
of conventional centrifugal refining process, developments in the
refining of oil seed extraction materials and specifically corn
germ extraction materials may not have addressed refining of oil
seed extraction materials or corn germ extract materials in bulk by
any alternate non-centrifugal extraction material refining process,
but rather focus on the production of oil seed extraction material
or corn germ extraction material fractions enriched in certain
compounds. For example, U.S. Pat. No. 5,932,261 describes a process
for production of a carotene rich refined oil fraction from a corn
germ extraction material.
[0008] To address the unresolved problems associated with the
utilization of conventional oil seed and corn germ extraction
equipment and methods of refining oil seed extraction materials and
specifically corn germ extraction materials, the instant invention
provides devices and methods for the pressure regulated
supercritical fluid fractionation of oil seed extraction materials
and specifically of corn germ extraction materials.
II. SUMMARY OF THE INVENTION
[0009] Accordingly, a broad object of embodiments of the invention
can be to provide a oil seed material production system which
utilizes an amount of a supercritical fluid to remove an amount of
oil seed extraction material from ground whole or ground parts of
oil seeds and subsequently fractionates the amount of oil seed
extraction materials established in the amount of supercritical
fluid (also referred herein as the effluent) by passage through a
series of oil seed extraction material separation zones each having
an adjustable pressure within a fixed temperature range each
producing a corresponding oil seed extraction material fraction
separable from the effluent in each oil seed extraction material
separation zone.
[0010] A second broad object of embodiments of the invention can be
to provide an oil seed extraction material separator which
generates at least one oil seed extraction material fraction
suitable for the production of biodiesel or utilization as food
grade oil without utilization of conventional productions steps
involving generation of soap stock and centrifugation.
[0011] A third broad object of embodiments of the invention can be
to provide a oil seed extraction material separator which provides
three oil seed extraction material separation zones: a first
providing an adjustable pressure within a fixed temperature range
to generate a phosphatide fraction from an amount of effluent, a
second providing an adjustable pressure within a fixed temperature
range to generate a triglyceride fraction from an amount of
effluent having the phosphatide fraction separated in the first
extraction material separation zone, and a third providing an
adjustable pressure within a fixed temperature range to generate an
FFA fraction from the effluent having the phosphatide fraction
separated in the first extraction material separation zone and
having the triglyceride fraction separated in the second extraction
material separation zone.
[0012] A fourth broad object of the invention can be to provide a
corn germ extraction material separator which provides three corn
germ extraction material separation zones: a first providing an
adjustable pressure within a fixed temperature range to generate a
phosphatide fraction from an amount of effluent, a second providing
an adjustable pressure within a fixed temperature range to generate
a triglyceride fraction from an amount of effluent having the
phosphatide fraction separated in the first extraction material
separation zone, and a third providing an adjustable pressure
within a fixed temperature range to generate an FFA fraction from
the effluent having the phosphatide fraction separated in the first
extraction material separation zone and having the triglyceride
fraction separated in the second extraction material separation
zone.
[0013] Naturally, further objects of the invention are disclosed
throughout other areas of the specification, drawings, photographs,
and claims.
III. A BRIEF DESCRIPTION OF THE DRAWINGS
[0014] FIG. 1 provides a flow diagram of a particular embodiment of
an oil seed extraction and oil seed extraction material
fractionation system.
[0015] FIG. 2 provides an enlarged portion of the flow diagram
shown in FIG. 1 further providing a cut away of a part of an
extraction vessel showing the oil seed extraction zone containing
an amount of oil seed material.
[0016] FIG. 3 provides an enlarged portion of the flow diagram
shown in FIG. 1 further providing cut away views of the separator
vessels included in the oil seed extraction material separator.
[0017] FIG. 4 provides a graph which plots density of supercritical
carbon dioxide against temperature for each of a plurality of
supercritical carbon dioxide pressures and provides for each of a
first separator vessel (S-1), a second separator vessel (S-2), and
a third separator vessel (S-3) a corresponding window which bounds
the separation parameters in which one of a phosphatide fraction, a
triglyceride fraction, or a fatty acid fraction can be separated
from an amount of supercritical carbon dioxide in which an amount
of corn germ extraction material is established.
IV. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
[0018] Generally, a method of pressure regulated supercritical
fluid fractionation of oil seed extraction materials which can be
utilized to refine oil seed extraction material established in an
amount of supercritical fluid. Specifically, a method of pressure
regulated supercritical fluid fractionation of corn germ extraction
material to produce a refined corn oil extraction material.
[0019] First referring primarily to FIGS. 1 and 2, a non-limiting
example of an oil seed extraction material production system (1) is
shown. For the purposes of this invention the term "oil seed" or
"oil seeds" means the seed of corn, cotton, flax, sunflower,
canola, sesame, linseed, soybean, peanuts, copra, safflower,
mustard, brassica, rapeseed, or the like, whether in whole or
comminuted to provide sufficiently small pieces of seed or
sufficiently small pieces of a part of the seed compatible with a
method of oil extraction and specifically includes as non-limiting
example corn germ isolated from whole corn seed. The term "oil seed
extraction material" for the purposes of this invention means the
materials extracted from the entirety or parts of the various oil
seeds by any device or method of removal or extraction, such as,
solvent extraction, hydraulic pressing, expeller pressing,
including the correspondingly wide range of compositions of neutral
extraction oils, fatty acids, and a greater or lesser amount of
undesired impurities. The undesired impurities in the oil seed
extraction material can include one or more of: free fatty acids
(FFA) from the degradation of corn germ oil by hydrolysis,
phosphatids (hydratable and non-hydratable), organic compounds
which contribute certain colors, flavors or odors, particulates
entrained by the extracted corn germ extraction material, or the
like.
[0020] A non-limiting example of an oil seed extraction material
production system (1) which can be used to produce an amount of
corn germ extraction material (11)(see FIG. 2) can include a corn
germ extractor (2)(for example, the cascade extractor shown in FIG.
1 which provides one or a plurality of corn germ extractor vessels
(3) each of which defines a corn germ extraction zone (4)(see FIG.
2) inside of which an amount of corn germ (5) comminuted to provide
a plurality of corn germ particles (6) can be located for fluidic
engagement with an amount of supercritical carbon dioxide (7) to
perform a corn germ extraction event to produce an amount corn germ
extraction material (11). Each of the corn germ extractor vessels
(3) can independently perform an extraction event on an amount of
corn germ (5) in manner which allows at least one extractor vessel
(3A)(shown in broken lines) to come off line for a period of time
after the extraction event sufficient for removal of an amount of
extracted corn germ (8) and introduce an amount of corn germ (5)
for a subsequent extraction event.
[0021] While the embodiment of the corn germ extraction material
production system (1) shown in FIG. 1 utilizes a cascade extractor
with an amount of supercritical carbon dioxide (7) as the
extractant, as more fully described in U.S. patent application Ser.
No. 11/716,838, hereby incorporated by reference in the entirety
herein, this is not intended to limit the manner in which an amount
of corn germ extract material (11) can be obtained from an amount
of corn germ (5) or the manner in which an amount of oil seed
extract material can be obtain from an amount of oil seed. Rather,
it is intended that the description of the corn germ extractor (2)
be illustrative with respect to the numerous and varied oil seed
extractors and oil seed extraction processes which can be utilized
to obtain oil seed extraction material(s) including corn germ
extraction materials (11) having the correspondingly wide range of
compositions as above-described which can be received by the oil
seed extraction material separator (14)(also referred to in the
context of the non-limiting example which follows as a corn germ
extraction material separator) and processed as further described
below.
[0022] Again referring primarily to FIGS. 1 and 2, each of the
plurality of corn germ extractor vessels (3) can be coupled to a
heat source (9) which generates an amount of heat sufficient to
maintain the amount of supercritical carbon dioxide (7) at a
temperature of between about 70.degree. C. and about 120.degree. C.
during fluidic engagement with the amount of corn germ (5) located
inside said corn germ extraction zone (4). The heat source (9) can
be coupled to a temperature adjustment element (10) which can
monitor temperature of the amount of supercritical carbon dioxide
(7) in the corn germ extraction zone (4) or can monitor other
conditions outside of the corn germ extraction zone such as the
amount of corn germ extraction material (11) established (whether
solubilized, carried, or entrained) in the amount of supercritical
carbon dioxide (7) (the "effluent" (12)) which flows from the corn
germ extraction zone (4), or other measure of the efficiency of the
extraction event to allow continuous adjustment of the temperature
of the amount of supercritical carbon dioxide (7) in the corn germ
extraction zone (4) to maintain a preselected temperature, a
preselected temperature profile, or a preselected corn germ
extraction efficiency profile based on monitoring the effluent (12)
from the corn germ extraction zone (4). The corn germ extractor (2)
further includes a plurality of conduits and valves (13) configured
to allow transfer of the amount of supercritical carbon dioxide (7)
into and away from the corn germ extraction zone (4).
[0023] Now referring primarily to FIG. 1, the oil seed extraction
material production system (1) can further include an oil seed
extraction material separator (14)(also referred to as a corn germ
extraction material separator in the context of examples of
fractionating corn germ extraction material (11)). As one
non-limiting example in the context of refining an amount of corn
germ extraction material (11), the oil seed extraction material
separator (14) can include at least one separator vessel (15) which
defines at least one corn oil separation zone (16) in which the
amount of corn germ extraction material (11) extracted from the
amount of corn germ (5) and established in the amount of
supercritical carbon dioxide (or other solvent depending on the
extraction method utilized) can be separated from the amount of
supercritical carbon dioxide (7)(or other solvent) by establishing
one or a plurality of corn germ extraction material separation
conditions in the at least one corn germ extraction material
separation zone (16). The at least one separator vessel (15)
further includes a plurality of separator conduits and valves (17)
configured to allow serial transfer of the amount of effluent (12)
into or between the at least one corn oil separation zone (16) and
transfer of a separated corn germ extraction material fraction (18)
and the separated amount of supercritical carbon dioxide (7) away
from the at least one corn oil separation zone (16).
[0024] Now referring primarily to FIG. 3, a non-limiting example of
a corn germ extraction material separator (14) includes a first
separator vessel (19) the configuration of the internal surfaces
defining within a first corn germ extraction material separation
zone (20), a second separator vessel (21) the configuration of the
internal surfaces defining within a second corn germ extraction
material separation zone (22), and a third separator vessel (23)
the configuration of the internal surfaces defining within a third
corn germ extraction material separation zone (24).
[0025] Now referring primarily to FIGS. 1, 2, and 3, the effluent
(12) exiting the corn germ extractor (2) passes serially through
each of the first separator vessel (19), the second separator
vessel (21), and the third separator vessel (23) each configured to
establish conditions in the respective corn germ extraction
material separation zones (20)(22)(24) which allow adjustable
pressure of the effluent (12) of between about 200 bar to about 400
bar, 150 bar and 300 bar, and about 75 bar to about 100 bar
respectively at temperatures respectively fixed at between about
60.degree. C. to about 110.degree. C., about 60.degree. C. to about
100.degree. C. and about 40.degree. C. to about 70.degree. C.
[0026] Operation of a main pressure reduction generator (26)
coupled to conduit (27), in part controls the pressure in the corn
germ extraction material separation zones (20)(22)(24) at the same
time the conduit valve (28) controls the flow of effluent (12) to
the separator vessels (19)(21)(23). The auxiliary pressure
reduction generators (29)(30)(31) downstream of each separator
vessel (19)(22)(23) and heat exchangers (32)(33)(34) upstream of
each separator vessel (19)(22)(23) operate to control the
conditions in each such separator vessel (19)(22)(23). To obtain
separated corn germ extraction material fractions (18) from the
effluent (12), the effluent (12) flows by operation of the main
pressure reduction generator (26) in conduit (27) through a heat
exchanger (32) in conduit (35) and into the first separator vessel
(19).
[0027] For the purposes of describing the present invention, ranges
may be expressed as from "about" one particular value to "about"
another particular value. When such a range is expressed, another
embodiment includes from the one particular value to the other
particular value. Similarly, when values are expressed as
approximations, by use of the antecedent "about," it will be
understood that the particular value forms another embodiment. It
will be further understood that the endpoints of each of the ranges
are significant both in relation to the other endpoint, and
independently of the other endpoint. Moreover, for the purposes of
the present invention, the term "a" or "an" entity refers to one or
more of that entity. As such, the terms "a" or "an", "one or more"
and "at least one" can be used interchangeably herein. Furthermore,
an element "selected from the group consisting of" refers to one or
more of the elements in the list that follows, including
combinations of two or more of the elements.
[0028] Now referring primarily to FIGS. 3 and 4, the effluent (12)
entering the first corn germ extraction material separation zone
(20) in the first separator vessel (19) can be maintained at a
fixed temperature in the range of about 60.degree. C. to about
110.degree. C. and the pressure of the effluent (12) can be
variably adjusted between about 200 bar and about 400 bar to
achieve a density of the supercritical fluid (typically
supercritical carbon dioxide) of between about 0.75 g/mL and about
0.85 g/mL to produce a phosphatide fraction (36)(see conditions
bounded by block S-1 in FIG. 4). The phosphatide fraction (36)
which separates out of the effluent (12) in the first separator
vessel (19) can accumulate as a solid material whether at the
bottom of the first separator which can be periodically removed or
exits through the first separator vessel drain line (37) entrained
in an amount of the effluent. This phosphatide fraction (36)
comprises any one of or a mixture of various phosphorous containing
lipids (or phospholipids) commonly referred to as lecithin which
can serve as crystallization nuclei for condensation of flocculants
in biodiesel.
[0029] Now referring primarily to FIG. 4 and Table 1, an increase
in the total amount of the phosphatide fraction (36) can be
achieved by fixing the temperature within a narrower temperature
range of between about 70.degree. C. and about 90.degree. C. and
adjusting pressure of the effluent (12) between about 250 bar and
about 350 bar to achieve a density of the supercritical fluid of
between about 0.75 g/mL and about 0.85 g/mL. Specifically in the
non-limiting context of an amount of corn germ extraction material
established in an amount of supercritical carbon dioxide, an even
greater increase in total amount of the phosphatide fraction (36)
can be achieved within a fixed range of temperature of between
about 60.degree. C. and about 70.degree. C. and adjusting pressure
of the effluent (12) between about 325 bar and about 350 bar to
achieve a density of the supercritical carbon dioxide of between
about 0.75 g/mL and about 0.85 g/mL (total phospholipid increases
with reduced density to about 0.75 g/mL).
TABLE-US-00001 TABLE 1 1st Separator Data CO.sub.2 Pressure Temp.
Density Total Phospholipids Experiment # MPa .degree. C. g/mL Wt.
Percent Feedstock N/A N/A 0.52 SM 70723 34.474 70 0.823 0.65 SM
70724 27.579 55 0.832 0.26 SM 70725 34.474 60 0.860 0.52 SM 70731
41.369 65 0.881 0.12 SM 707801 48.263 70 0.897 0.12 SM 707802
55.158 80 0.898 0.14 SM 707809 51.711 75 0.897 0.10 SM 707810
44.816 70 0.881 0.10 MPa = Megapascals 1 Megapascal = 10 bar
[0030] Again referring to Table 1 and in particular referring to
Feedstock SM70725 as a non-limiting example, a crude corn oil
feedstock can be obtained from ConAgra Foods Inc., Memphis, Tenn.
having a phospholipid concentration of 0.52 mg/g. 500 mL of the
crude corn oil feedstock was fed through a first separator by a
high pressure diaphragm pump enabling countercurrent contact
between the crude corn oil feedstock and supercritical carbon
dioxide (also referred to as "supercritical CO.sub.2"). The
temperature in the separator was set at 60.degree. C. in all the
sections. The supercritical CO.sub.2 supply pressure was maintained
at about 34.474 MPa by a CO.sub.2 pump. This temperature and
pressure provided a pure super critical carbon dioxide density of
0.960 mg/mL. The crude corn oil feedstock was fed into the
separator at an average rate of approximately 2.6 mL/min; the
supercritical carbon dioxide flow rate was kept at 3 SLPM. Every
ten minutes, readings were taken of the pressure inside the first
separator, at the CO.sub.2 pump and the high pressure diaphragm
pump, also the temperatures at the top, center, and bottom of the
separator were monitored. Finally the temperatures of supercritical
CO.sub.2 entering and exiting the column were also recorded. The
separator was operated in the manner described above for 120
minutes. A bottom valve of the separator was opened every ten
minutes and a sample of liquid that condensed during the previous
ten minute period was drawn from the column. After reaching
steady-state of pressures, temperatures and flow rates within the
column, six samples from the bottom of the extractor were combined
and analyzed for phospholipid content. The phospholipid
concentration of the crude corn oil feed stock was unchanged by
fractionation at these processing conditions and remained at 0.52
mg/g in the separator. Fractionation continued utilizing the same
procedure at processing conditions representing both higher and
lower pure carbon dioxide densities as shown in Table 1. As can be
seen from the table the phospholipid concentrations or amounts
begin to selectively concentrate in the first separator below a
pure carbon dioxide density of about 825 kg/m.sup.3.
[0031] Again referring primarily to FIGS. 3 and 4, the resulting
effluent (12) proceeds from the first separator vessel (19) through
the conduit (38), the auxiliary pressure reduction generator (29)
and the heat exchanger (33) into the second separator vessel (21).
The temperature of the effluent (12) can be adjusted in the heat
exchanger (33), and the pressure of the fluid in the second
separator vessel (21) can be adjusted by the downstream pressure
reduction generator (30). Fractionation conditions in the second
corn germ extraction material separation zone (22) of the second
separator vessel (21) can be established to provide a fixed
temperature in the range of about 60.degree. C. to about
100.degree. C. and a pressure adjusted within range of about 150
bar to about 300 bar to achieve a density of the supercritical
fluid (typically supercritical carbon dioxide) of between about
0.62 g/mL and about 0.75 g/mL to produce a triglyceride fraction
(38)(see conditions bounded by block S-2 in FIG. 4). The
triglyceride fraction (38) which separates out of the effluent (12)
in the second separator vessel (21) exits through the second
separator vessel drain line (39). This triglyceride fraction (38)
comprises glyceride in which the glycerol is esterified with three
fatty acids. It is the main constituent of the corn germ extraction
material (11) established in the effluent (12).
[0032] Now referring primarily to FIG. 4 and Table 2, conditions
can be established in the second corn germ extraction material
separation zone (22) which allows the separation of the
triglyceride fraction (36) while the free fatty acids remain
soluble in the effluent (12). Specifically in the non-limiting
context of an amount of corn germ extraction material having the
phospholipid fraction removed the triglyceride fraction (36) can be
separated while the FFAs remain soluble in the effluent (12) by
fixing the temperature within a temperature range of between about
70.degree. C. and about 90.degree. C. and adjusting pressure of the
effluent (12) between about 175 bar and about 250 bar to achieve a
density of the supercritical fluid of between about 0.62 g/mL and
about 0.75 g/mL. Specifically in the non-limiting context of an
amount of corn germ extraction material established in an amount of
supercritical carbon dioxide, an even greater increase in free
fatty acid in the effluent transferred from the second corn germ
extraction material separation zone (22) can be achieved within a
fixed range of temperature of between about 60.degree. C. and about
65.degree. C. and adjusting pressure of the effluent (12) between
about 195 bar and about 250 bar to achieve a density of the
supercritical carbon dioxide of between about 0.72 g/mL and about
0.76 g/mL. As to certain embodiments of the invention, even a
greater amount of FFAs remain soluble in the effluent (12) at a
fixed temperature of about 60.degree. C. and adjusting the pressure
to about 0.72 g/mL.
TABLE-US-00002 TABLE 2 2.sup.nd Separator Data CO.sub.2 Pressure
Temp. Density Free Fatty Acid in Experiment # MPa .degree. C. g/mL
Effluent mg/g Feedstock N/A N/A 1.74 SM 70613-1 19.926 60 0.722
18.82 SM 70614-1 25.028 65 0.762 16.26 SM 70615-1 20.684 55 0.764
10.99 SM 70618-1 19.995 45 0.813 9.63 SM 70618-2 23.994 75 0.698
11.70 SM 70619-1 17.995 45 0.789 11.58 MPa = Megapascals 1
Megapascal = 10 bar
[0033] Again referring to Table 2, crude corn oil feedstock was
obtained from ConAgra Foods Inc., Memphis, Tenn. with a free fatty
acid concentration of 1.74 mg/g. 500 ml of crude corn oil feedstock
was fed through the second separator by a high pressure diaphragm
pump to enable the countercurrent contact between the feedstock and
supercritical CO.sub.2. The temperature in the separator column was
set at 60.degree. C. in all the sections. The supercritical
CO.sub.2 supply pressure was 19.926 MPa. This temperature and
pressure represented a pure carbon dioxide density of 0.722 g/mL.
The feedstock was fed into the column at an average of rate of
approximately 2.6 mL/min; the carbon dioxide flow rate was kept at
3 SLPM. Every ten minutes, readings were taken of the pressure
inside the column, at the CO.sub.2 pump and the diaphragm feedstock
pump, also the temperatures at the top, center, and bottom of the
fractionation column were monitored. Finally the temperatures of
the supercritical CO.sub.2 entering and exiting the column were
also recorded. The second separator was operated in the manner
described above for 120 minutes. After reaching steady-state of
pressures, temperatures and flow rates within the column a sample
was obtained of the effluent exiting the second separator under
steady-state operating conditions and analyzed for FFA composition.
The FFA concentration was folded by fractionation at these
processing conditions by a factor of about 10.82 from 1.74 mg/g to
18.82 mg/g (see Table 2, SM 70613-1). Fractionation continued
utilizing the same procedure at processing conditions representing
both higher and lower pure carbon dioxide densities as shown in
Table 2. As can be seen from the table the FFA concentrations begin
to selectively concentrate approaching 19% in the third separator
below a pure carbon dioxide density of about 725 kg/m.sup.3.
[0034] Now referring primarily to FIGS. 3 and 4, the resulting
effluent (12) proceeds from the second separator vessel (21)
through the conduit (40), the auxiliary pressure reduction
generator (30) and the heat exchanger (34) into the third separator
vessel (23). The temperature of the effluent (12) can be adjusted
in the heat exchanger (34), and the pressure of the fluid in the
third separator vessel (23) can be adjusted by the downstream
pressure reduction generator (31). Fractionation conditions in the
third corn germ extraction material separation zone (24) of the
third separator vessel (23) establish a fixed temperature in the
range of about 40.degree. C. to about 70.degree. C. and the
pressure can be adjusted within the range of about 75 bar to about
100 bar to achieve a density of the supercritical fluid (typically
supercritical carbon dioxide) of between about 0.1 g/mL and about
0.3 g/mL which allows separation of the FFA fraction (41) from the
effluent (see conditions bounded by block S-3 in FIG. 4). The FFA
fraction (41) which separates out of the effluent (12) in the third
separator vessel (23) exits through the third separator vessel
drain line (42). This FFA fraction (41) comprises a carboxylic acid
often with a long unbranched aliphatic tail (chain), which is
either saturated or unsaturated. Carboxylic acids as short as
butyric acid (4 carbon atoms) are considered to be fatty acids,
while fatty acids derived from natural fats and oils may be assumed
to have at least 8 carbon atoms, such as caprylic acid (octanoic
acid). In regard to biodiesel production, if the free fatty acid
level is too high it may cause problems with soap formation and the
separation of the glycerin by-product downstream. It is also known
that high free fatty acids levels may not be good for human
health.
[0035] Now referring primarily to FIG. 4, in increase in total
amount of free fatty acids in the FFA fraction (41) can be achieved
by fixing the temperature within a narrower temperature range of
between about 45.degree. C. and about 65.degree. C. and adjusting
pressure of the effluent (12) between about 85 bar and about 95 bar
to achieve a density of the supercritical fluid of between about
0.1 g/mL and about 0.3 g/mL. Specifically in the non-limiting
context of an amount of corn germ extraction material established
in an amount of supercritical carbon dioxide, an even greater
increase in total phospholipids in the phosphatide fraction (36)
can be achieved within a fixed range of temperature of between
about 50.degree. C. and about 60.degree. C. and adjusting pressure
of the effluent (12) between about 80 bar and about 90 bar to
achieve a density of the supercritical carbon dioxide of between
about 0.1 g/mL and about 0.3 g/mL.
[0036] It can be appreciated that the corn germ extraction material
separator (14) shown in FIG. 3 may be operated with additional
separator vessels to re-fractionate any of separated corn germ
extraction material fractions (18) to further isolate additional
extraction material fractions, or may be operated with additional
separator vessels in series to isolate additional extraction
material fractions, or may be operated to by-pass the first
separator vessel (19) or the second separator vessel (21) or both.
Also, a two step fractionation of corn germ extraction material
(11) entrained in the effluent (12) can be carried out between the
first separator vessel (19) and the second separator vessel
(21).
[0037] Use of the corn germ extraction material separator (14) as
shown in FIG. 3 and utilized as above-describe can yield a quality
of food grade corn germ extraction material which exhibits the
characteristics set out in Table I.
TABLE-US-00003 TABLE I ATTRIBUTE DESCRIPTOR MIN MAX UOM Free Fatty
n/a 0.01 0.06 % Acids Free Fatty n/a 0.01 0.05 % Acids PV n/a 0.0
0.5 meq/kg PV n/a 0.0 1.0 meq/kg OSI @110 deg F. 6.5 n/a hours AOM
n/a 15 n/a hours Flavor Fresh tbd tbd Hedonic Lovibond Red Color
n/a 3.0 n/a Moisture n/a n/a 0.03 % Fatty Acid Palmitic Acid 9.0
15.0 % Composition Fatty Acid Stearic Acid 1.0 4.0 % Composition
Fatty Acid Oleic 24.0 29.0 % Composition Fatty Acid Linoleic Acid
55.0 63.0 % Composition Fatty Acid Linoleic Acid n/a <2 %
Composition para- n/a n/a 6.0 avu Anisidine Phosphorous n/a n/a 5.0
ppm
[0038] Again referring to FIG. 1, the resulting amount of carbon
dioxide (43) proceeds from the third separator vessel (23) through
the conduit (44) under the influence of the auxiliary pressure
reduction generator (31) to the carbon dioxide recycle assembly
(45)(see FIG. 1) which further include a condenser (46) which
provides condensing conditions to establish the amount of carbon
dioxide (43) in a phase compatible with a pressure generator (47)
which establishes and maintains the amount of supercritical carbon
dioxide (7) at pressures between about 7,000 psi and about 12,000
psi in the corn germ extraction zone (4). The pressure generator
(47) can be coupled to a pressure adjustment element (48) which can
monitor the pressure of the amount supercritical carbon dioxide (7)
in the corn germ extraction zone (4) or can monitor other
conditions outside of the corn germ extraction zone (4) such as the
amount of corn oil solubilized in the effluent (12), or other
measure of the efficiency of the extraction event to allow
continuous adjustment of the pressure of the amount of
supercritical carbon dioxide (7) in the corn germ extraction zone
(4) to establish or maintain a preselected pressure, a preselected
pressure profile, or a preselected corn germ extraction efficiency
profile based on monitoring the effluent (12) from the corn germ
extraction zone (4).
[0039] Now again referring primarily to FIG. 1, it can be
understood that if the flow rate of the supercritical carbon
dioxide (7) in the corn germ extraction zone (4) 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 (7) 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 germ extraction material
(11) of about twenty percent of the amount of the corn germ (5)
(wt./wt.). For example, if the solvent to feed ratio is about 20 to
1 to obtain an amount of corn germ extraction material (11) of
twenty percent of the weight of the amount of the corn germ (16)
extracted, then for each ton of corn germ extraction material (11)
extracted about twenty tons of supercritical carbon dioxide (7)
would be utilized. If the solvent to feed ration is about 2 to 1,
then for each ton of an amount of corn germ extraction material
(11) extracted two tons of supercritical carbon dioxide (7) would
be utilized and so forth. If the corn germ extraction material
production system (1) processes 300 tons of corn germ (5) per day
at a solvent to feed ratio of about 20 to 1 then about 6,000 tons
of supercritical carbon dioxide (7) would pass through the corn
germ extraction zone (4) of the corn germ extractor (2) and be
recovered by the carbon dioxide recycle assembly (45) per day.
However, if the corn germ extraction material production system (1)
processes the same 300 tons of corn germ (5) per day at a solvent
to feed ratio of about 2 to 1 then only 600 tons of supercritical
carbon dioxide (7) would pass through the corn germ extraction zone
(4) of the corn germ extractor (2) and be recovered by the carbon
dioxide recycle assembly (45) per day. Accordingly, the corn germ
extractor (2) can be configured to allow for processing of the
corresponding amount of effluent (12). Even if the configuration of
the corn germ extractor (2) remains substantially the same
regardless of the solvent to feed ratio because the mass of the
amount of corn germ (5) extracted remains constant, it can be
understood that at least the components of the a corn germ
extraction material separator (14) and the carbon dioxide recycle
assembly (45) would be necessarily scaled upward or downward as
solvent to feed ratio increases or decreases.
[0040] As can be easily understood from the foregoing, the basic
concepts of the present invention may be embodied in a variety of
ways. The invention involves numerous and varied embodiments of
corn germ extraction material production system and methods of
making and using such corn germ extraction material production
system and making and using corn germ extraction material. As such,
the particular embodiments or elements of the invention disclosed
by the description or shown in the figures 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.
[0041] 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 a "corn oil separator" should be
understood to encompass disclosure of the act of "separating corn
oil" whether explicitly discussed or not and, conversely, were
there effectively disclosure of the act of "separating corn oil",
such a disclosure should be understood to encompass disclosure of a
"corn oil separator" and even a "means for separating corn oil."
Such alternative terms for each element or step are to be
understood to be explicitly included in the description.
[0042] 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 be 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.
[0043] Thus, the applicant(s) should be understood to claim at
least: i) each of the corn germ extraction material production
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.
[0044] 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.
[0045] The claims set forth in this specification, if any, 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 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.
[0046] The claims set forth below, if any, are intended 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.
* * * * *