US20040087808A1

US20040087808A1 - Substantially fat free products from whole stillage resulting from the production of ethanol from oil-bearing agricultural products

Info

Publication number: US20040087808A1
Application number: US10/619,833
Authority: US
Inventors: John Prevost; Neal Hammond
Original assignee: Individual
Current assignee: FARMERS FIRST GROUP LLC
Priority date: 2002-10-28
Filing date: 2003-07-15
Publication date: 2004-05-06
Also published as: AU2003284371A1; US8257951B2; AU2003284371A8; US20120283422A1; US20040082044A1; US8524473B2; US20060194296A1; WO2004039959A3; WO2004039959A2

Abstract

A process for obtaining substantially fat free products from whole stillage produced during ethanol production from agricultural products, such as cereal grains. More particularly, at least a portion of the fat is removed from both the thin stillage stream and the wet distillers grains that result from whole stillage.

Description

CROSS-REFERENCE TO RELATED APPLICATION

This application is a continuation-in-part of U.S. Ser. No. 10/281,490 filed Oct. 28, 2002.[0001]

BACKGROUND OF THE INVENTION

1. Field of the Invention

This invention relates a process for obtaining substantially fat free products from whole stillage produced during ethanol production from agricultural products, such as cereal grains. More particularly, at least a portion of the fat is removed from both the thin stillage stream and the wet distillers grains that result from whole stillage.

2. Description of Related Art

In a conventional ethanol production process utilizing corn as the starch containing feedstock, the corn is ground to produce a milled corn. This is typically achieved by the use of a hammer mill or other suitable milling equipment. Water and enzymes are added to the milled corn and heated to form a mash. The mash is then mixed in a fermentation vessel with water, yeast and optionally minerals and nutrients to enhance the fermentation of the mash. The resulting fermented product, commonly referred to as the “beer”, is then distilled to produce an ethanol rich stream (about 95% ethanol and 5% water by weight) and whole stillage. The whole stillage comprises water, as well as the solids left over from the fermentation. The whole stillag is typically centrifuged to remove a substantial portion of the water to form a solids rich fraction commonly referred to as wet distillers grains and a substantially liquid fraction commonly referred to as thin stillage. The wet distillers grains fraction includes most of the protein-containing solids from the whole stillage. It also contains about 8 to 12 wt. % fat. The thin stillage fraction, after evaporation to form a syrup, will typically contain from about 8 to 15 wt. % a fat. This syrup is also referred to as condensed distillers solubles (CDS), and is typically combined with the wet distillers grains and sent to a dryer to produce a dry protein containing animal feed called distiller dried grain solubles (DDGS).

Conventional ethanol processes have several significant problems. One problem is the energy costs to remove water from the whole stillage to produce a low economic value DDGS. A second problem is the environmentally unacceptable amount of volatile organic compounds (VOC), air toxics, and combustion pollutants, such as CO, NO _x, and particulate matter, released into the atmosphere during conventional drying methods. To achieve an acceptable levels VOC, air toxics, and combustion pollutants release amount requires large capital investments in thermal oxidizers and other equipment to capture the VOC, air toxics, and combustion pollutants released during conventional drying methods, as well as expensive equipment maintenance. Another problem, depending on the end use of the stream, is that the fat content for both the thin stillage fraction and the wet distillers grains fraction can be considered too high. These problems have hampered the commercial success of ethanol production processes that have to date, remained economically viable due only to governmental subsidies.

OBJECTS AND SUMMARY OF THE INVENTION

One object of the present invention is to provide an improved ethanol production process that results in value added flavor enhancing, nutritional, nutraceutical, and/or pharmaceutical by products.

Another object of the present invention is to provide an improved ethanol production process that minimizes the amount of VOC and other pollutants released to the atmosphere during the treatment of the whole stillage.

Still another object of the present invention is to provide an improved ethanol production process resulting in an oil stream, which oil stream is obtained from dried distillers grains, thin stillage, syrup resulting from thin stillage, or a mixture thereof.

Other objects and advantages of this invention shall become apparent from the ensuing descriptions of the invention.

Accordingly, an improved ethanol producing process is disclosed wherein a starch-containing feedstock, preferably a cereal grain such as corn, is processed to produce ethanol and whole stillage. The whole stillage comprises solids, nutrients, yeast and water remaining after the ethanol has been distilled off. The whole stillage is centrifuged, filtered or otherwise separated by any suitable technique to produce a substantially solids stream and a substantially liquid stream. The substantially solids stream is referred to as wet distillers grains and contains most of the protein-containing solids, from about 8 to about 12 wt. % fat or oil, and water. The substantially liquid stream, referred to as the thin stillage will comprise the nutrients, yeast and most of the water from the whole stillage. The thin stillage is typically subjected to an evaporation step remove water and produce a syrup that will contain about 7 to about 15 wt. % oil or fat. It is to be understood that no distinction is made herein between the terms “oil” and “fat” and the words can be used interchangeably herein.

The wet distillers grains are dried under conditions that do not denature the proteins contained in the distillers grains, and more preferably, under conditions that minimize volutizing organic components in the wet distillers grains. The drying conditions used will depend on a variety of factors. For example, when utilizing spray drying, these factors include the ease at which the wet distillers grains can be atomized, the humidity of the air in the drying environment, the temperature of the hot air used to dry the wet distillers grains, the temperature of the wet distillers grains when they enter the spray drier, and the contact time between the hot air and the atomized wet distillers grain. In a preferred embodiment, these factors are controlled to produce a protein-rich product having a water content of less than about 15% by weight. More preferably a protein-rich product is produced that is substantially free of oil, but that will require an oil removal step. It has been found that setting the temperature and contact time to achieve a hot air exhaust temperature between about 140° F. and about 170° F. will result in a protein-rich product containing less than about 15% water by weight and whose proteins have not been denatured. Under normal humidity conditions and using conventional spray drying technology an exhaust temperature in the above range should result in an inlet hot air temperature of less than about 450° F., and a contact time of less than about three minutes. Utilization of the above drying conditions will also reduce the VOC emissions to the atmosphere. In a preferred embodiment the drying conditions are set to maintain the temperature of the wet distillers grains at an effective temperature that is low enough so that the amount of VOCs emitted will be less than the environmental regulations permit. It is preferred that a temperature be used wherein substantially no VOCs are emitted. It is further preferred that any VOC that is volatized pass through a cold trap and then filtered to remove water to produce a VOC product. The VOC product can then be utilized as a supplement to flavor enhance other products.

The dried distillers grains can be subjected to an oil removal step. It is preferred that an oil removal technique be used that will remove substantially all of the oil from the dried distillers grains. Non-limiting examples of oil removal techniques that can be used include centrifugation, pressing with and without the use of a solvent, and solvent extraction without the use of pressing. The preferred solvent for solvent extraction is a normally gaseous solvent, more preferably butane, propane, or mixtures thereof. By normally gaseous we mean a solvent in which the oil is soluble and being in the gas phase at atmospheric pressure and at room temperature (approximately 75° F.).

The syrup can be added to the wet distillers grain prior to the drying step and be processed under the same conditions as the wet distillers grains as described above. An oil removal step can be performed on either the thin stillage before evaporation or on the syrup after evaporation. If performed prior to evaporation, an oil removal process such as centrifugation is preferred whereas after evaporation a solvent extraction process is preferred to extract at least a portion of the oil from the syrup.

In another alternate embodiment the thin stillage stream is not subjected to oil removal and is passed through a microfiltration unit utilizing a filter size to form a carotenoid containing retentate and a nutrient rich permeate. A filter having a pore size of about 0.1 to 1.0 micron can be used. The carotenoid containing retentate is then dried to produce a carotenoid rich product having less than about 15% water by weight. It has been found that setting the temperature and contact time to achieve a hot air exhaust temperature between about 140° F. and about 170°F. will result in a carotenoid rich product containing less than about 15% water by weight. Under normal humidity conditions and using a conventional spray dryer an exhaust temperature in the above range should result in an inlet hot air temperature of less than about 450° F., and a contact time of less than about three minutes. In a preferred embodiment any volatized VOC is passed through a cold trap and filter to produce a liquefied VOC product.

In yet another alternate embodiment the nutrient rich permeate is passed through an ultrafiltration unit utilizing a filter size to form a protein and yeast containing retentate and vitamin and mineral containing permeate. A filter having a pore size of less than about 0. I microns is preferred. The protein and yeast containing retentate is dried to produce a protein and yeast rich product having less than 15% water by weight. It has been found that setting the temperature and contact time to achieve a hot air exhaust temperature between about 140° F. and about 170° F. will result in a protein and yeast rich product containing less than about 15% water by weight and whose proteins have not been denatured. Under normal humidity conditions and using a conventional spray dryer an exhaust temperature in the above range should result in an inlet hot air temperature of less than about 450° F., and a contact time of less than about three minutes. The vitamin and mineral containing permeate can also be dried under the same conditions as the protein and yeast containing retentate to produce a vitamin and mineral rich product having less than 15% water by weight. It is preferred that any volatized VOC's be passed to a cold trap and filter to produce a liquid VOC product.

BRIEF DESCRIPTION OF THE DRAWINGS

The accompanying drawings illustrate a preferred embodiment of this invention. However, it is to be understood that this embodiment is not intended to be exhaustive, nor limiting of the invention. They are but examples of some of the forms in which the invention may be practiced. [0017]
FIG. 1 is a schematic illustrating a conventional ethanol production process, but with oil removal steps on products resulting after centrifugation of the whole stillage. [0018]
FIG. 2 is a schematic illustrating a preferred embodiment of this invention to treat the wet distillers grain to produce a non-denatured protein rich product. [0019]
FIG. 3 is a schematic illustrating a preferred embodiment of this invention to treat the thin stillage through use of microfiltration to produce a carotenoid rich product. [0020]
FIG. 4 is a schematic illustrating a preferred embodiment of this invention to treat the permeate stream from the microfiltration through use of ultrafiltration to produce a protein/yeast rich product and/or a vitamin/mineral rich product.[0021]

DETAILED DESCRIPTION OF THE INVENTION

Without any intent to limit the scope of this invention, reference is made to the figures in describing the preferred embodiments of the invention utilizing corn as the starch containing feedstock. The process described herein can also be used with other starch containing feedstocks such as bagasse, sugar cane, grains, and other oil-bearing starch or sugar based materials. [0022]
In a typical ethanol production process as illustrated in FIG. 1, a starch-containing feedstock [0023] 1, such as corn, is fed to a grinder 2 to produce a milled corn 3. The milled corn 3 is then sent to a mixer 4 where water 5, as well as enzymes 6, are added to produce a liquid mash 7. The liquid mash 7 is then sent to a fermentation vessel 8 where the desired yeast and additional enzymes 9, as well as the minerals and nutrients 10 if necessary for efficient fermentation, are added. After an effective amount of fermentation time a “beer” is produced and is sent to distillation unit 12 where an ethanol rich (about 95% ethanol by weight) stream 13 is separated from the remaining fermented solids and water. The remaining fermented solids and water is generally known as the whole stillage 14. The whole stillage 14 is processed to produce an animal feed commonly known as DDGS. The conventional method of treating whole stillage 14 is conduct it to a centrifuge 15 to form two separate streams, a substantially solids stream and a substantially liquid stream. The substantially solids stream is referred to as the wet distillers grains fraction 16. The substantially liquid stream is referred to as the thin stillage fraction 17. The wet distillers grains fraction 16 is comprised of most of the solids, protein, water, and about 8 to 12 wt. % oil. The thin stillage stream 17 is substantially all water with some oil and up to about 10 wt. % solids. It includes the minerals, nutrients, yeast and the remaining water that was found in the whole stillage 14. In a typical process, the thin stillage stream 17 is sent to evaporator 18 where water 19 is removed and the remaining solids or syrup 20 are combined with the wet distillers grain 16 and sent to a dryer 21. In the improved process of the present invention oil can removed at various stages of the process. For example, the wet distillers grains can be passed to oil removal step 16A wherein at least a portion of the oil is removed. Since the wet distillers grains still contain a significant amount of water, it is preferred to remove the oil by a centrifugation process wherein the wet distillers grains are introduced into a centrifuge apparatus and centrifuged at an effective speed and amount of time to cause oil to be removed from the wet distillers grains. The resulting liquid products from centrifugation will be predominantly comprised of water and oil, which can be separated from each other by any suitable oil/water separation technique. For example, the oil/water mixture can be conducted to a decanting tank and allowed to sit for an effective amount of time to allow phase separation to occur. That is for an oil phase and a water phase to form. The oil phase can then be easily decanted. It is also within the scope of this invention that the oil/water mixture be passed through a countercurrent vessel containing one or more suitable vertically disposed distribution trays wherein a solvent, such a C₂to C₆alkane is passed counter to the flow of the oil/water mixture. The oil will be taken up in the solvent and be carried with the solvent to a separation vessel wherein the solvent can be flashed or distilled from the oil and recycled.
The wet distillers grains can also be dried via [0024] dryer 21 to produce a dried distillers grains fraction which can then be subjected to oil removal via 24A. Oil removal step 24A can be any suitable oil removal process including centrifugation, but solvent extraction is preferred. The dried distillers grains can be first pressed before solvent extraction. That is, the dried distillers grains can be put in a suitable press and a substantial amount of oil removed via pressing. At least a portion of the remaining oil can be removed by subjecting the pressed grains to a suitable solvent, preferably a normally gaseous solvent, more preferably one selected from butane, propane and mixtures thereof. Since the solids of the wet distillers grains originate from the milling of the cereal grain, it is unlikely that pressing will be needed to remove the oil.
[0025] Dryer 21 is typically operated with hot air having an inlet temperature at about 1000° F.-1200° F. The hot air will remain in contact with the wet distillers grain 16 and syrup 20 for an effective amount of time, which will typically be from about 3 to 10 minutes, more preferably from about 4 to 6 minutes before exiting the dryer 20 having an exhaust temperature at about 200° F.-225° F. At these conditions the protein contained in the dried solids 24 are denatured and are only good for use in animal feed known as DDSG. In addition any water vapor 22 and VOC 23 in the wet distillers grain 16 and syrup 20 is volatized and either released to the atmosphere or passed through expensive conventional thermal oxidizers (not shown).
Both the thin stillage and syrup can each be individually, or a mixture thereof, conducted to an oil removal step, [0026] 17A and 20A. For example, the thin stillage can be centrifuged in a similar manner as the wet distillers grains and the resulting oil/water mixture sent to a separation zone wherein the water is separated from the oil. As mentioned previously, separation can be done by simple decanting, by distilling the water from the oil, or by passing a solvent, in which the oil is at least partially soluble or misible, can be run counter current with the flow of mixture, which solvent will pickup the oil and carry it in the opposite direction than the water. If using solvent extraction it is preferred that the material being oil-extracted be substantially dry. For example, it is preferred to dry the syrup by any suitable means, preferably by spray drying, before subjecting it to a solvent.
As previously mentioned, the preferred solvent for solvent extraction is a normally gaseous solvent. As previously mentioned, butane, propane, and mixtures thereof are preferred with propane being the more preferred. Non-limiting examples of other solvents that can be used include: methane, ethane, ethylene, propylene, butylene, sulfur dioxide, carbon dioxide, CHF[0027] ₃, CClF₃, CFBr₃, CF₂═CH₂, CF₃—CF₂—CF₃, CF₄, CF₄, CH₃—CF₃, CHCl₂, ammonia, methane, dimethylether, methyl fluoride, and halogenated hydrocarbons that are normally gaseous as indicated.
If solvent extraction is used it can be conducted in either batch, semi-batch or continuous mode, with continuous mode being preferred. By semi-batch we mean that the process unit will contain several extraction vessels, wherein there will always be one extraction vessel off line and being emptied of treated product while the other one or more extraction vessels will remain on line. When it is time to unload treated product from one of the reactors on line, such extraction vessel will be taken off line and the extraction vessel that was off line will take its place on line. In one preferred method for practicing batch solvent extraction, the material to be extracted is introduced into a suitable extraction vessel. Air is removed from the vessel and a normally gaseous solvent is introduced wherein it is pressurized, preferably by continuing to introduce solvent into the closed vessel until the normally gaseous solvent is converted to the liquid state. The oil will then dissolve in the liquid solvent and the solution of oil and solvent will be conducted from the extraction vessel to a separation vessel where the solvent will be removed from the oil by flashing or distillation. It is preferred that the oil in solvent solution be passed from the extraction vessel to the separation vessel while the solvent is still in the liquid state. It is also preferred that a vacuum be used to remove remaining solvent from the deoiled material as well as being used to aid in the removal of air from the extraction vessel prior to introduction of solvent. [0028]
Any suitable continuous solvent extraction mode can be used in the practice of the present invention. For example, the material (syrup) to be extracted can continuously be fed at an effective rate, into a pressure sealed extraction vessel by any suitable means, such as by use of an auger feeding mechanism. Solvent can continuously be added to contact fresh syrup to be extracted and the resulting oil in solvent solution can continuously be removed and the solvent separated from the oil as previously mentioned. [0029]
In one preferred embodiment, the process of this invention involves improved treatment of the [0030] whole stillage 14 to produce products each having greater economic value than DDGS, as well as significantly reduce the costs of treatment of the emissions from the process. In particular the amount of VOC emissions can be reduced while at the same time producing a flavor enhancement supplement product. Turning now to FIG. 2, the whole stillage 14 is again separated into two product streams by centrifuge 15. Other known separating equipment such as filters could be used. These two streams include the wet distillers grains 16 containing oil and most of the protein compounds found in the whole stillage 14 and the thin stillage stream 17 also containing oil, as well as most of the carotenoid, yeast, vitamin, mineral, and remaining protein compounds.
The [0031] wet distillers grain 16 is sent to a drying step 21 that is operated at conditions controlled to produce a protein rich product having a water content of less than about 15% by weight. Non-limiting examples of suitable drying means include spray drying, fluidized bed drying, single and double drum dehydrating, use of ring drier or other suitable means to produce a substantially free flowing solid. It is preferred that the drier can be a spray drier. It has been found that setting the temperatures of the hot air and the wet distiller grain 16, as well as their contact time to achieve a hot air exhaust temperature of between about 140° F. and about 170° F. will result in the production of a protein rich product 23 having a water content of less than about 15% by weight. Under normal humidity conditions a hot air exhaust temperature in the above range would likely require an inlet hot air temperature of less than about 450° F., and a contact time of less than about three minutes. Within these drying conditions the wet distillers grain temperature should remain below the temperature to volatize most, if not all, of the VOC contained in the wet distillers grain. Thus, a significant portion of the VOC will remain in the protein rich product 23. This has the result of not only reducing the VOC that are volutized, but maintaining more of the flavor enhancing compounds in the protein rich product 23. It is also preferred that the protein rich product 23 be cooled upon leaving dryer 21 to prevent any further volutization of the VOC that is contained in the protein rich product 23. One method of cooling the protein rich product 23 is through the use of a fluidized bed wherein cool or ambient temperature air is used to fluidize the bed. Other known cooling techniques could be employed. This protein rich product 23 can also be subjected to an oil removal step (not shown) as previously mentioned.
The water and any [0032] VOC vapor 22 removed during drying can be recycled to the mixer 4. Depending on the dryer operating conditions some VOC may be volatized. Because the volume of the volutized VOC is substantially less than in a conventional whole stillage treatment process, the water and VOC vapor 22 can be sent through a conventional and less expensive cold trap 24 to produce a liquid VOC product 25. Water 26 in the liquid VOC product 25 can be removed, such as by filter 26 or other known separating equipment, to produce a dry VOC product 28 that can be sold as a flavor enhancing additive.
Turning now to FIG. 3 in another preferred embodiment the [0033] thin stillage 17, without oil removal, is passed through a microfiltration unit 29 having a filter size of about 0.1 to 1.0 micron to form a retentate stream 30 and a permeate stream 31. In a more preferred embodiment the filter size is set to capture in the retentate stream 30 the carotenoid compounds. Carotenoid compounds, particularly Lutien and Zeaxantin, have been found useful in reducing various serious eye diseases such as age related macular degeneration and cataracts. The retentate stream 30 containing the carotenoid compounds is sent to dryer 32. If desired, this carotenoid rich product can also be subjected to an oil removal step (not shown) as previously mentioned. In a preferred embodiment dryer 32 will be operated at a temperature to minimize the denaturing of any protein contained in the retentate stream 30, as well as to prevent volatization of the VOC's in the retentate stream 30 during the period that the retentate stream 30 is contained in the dryer 32. This can be achieved if the retentate stream 30 is retained in dryer 32 for a period of less than about three minutes, and the dryer 32 is operated with a hot air exhaust temperature less than about 170° F. to remove the water. Operated in this manner sufficient water can be removed to form a carotenoid rich product 34 having less than 15% water by weight. Depending on the dryer operating conditions and the retention time of the retentate stream 30 in the dryer 32 some VOC may be volatized. Because the volume of the VOC is substantially less than in a conventional whole stillage treatment process, the water and VOC vapor 33 can be sent through a conventional and less expensive cold trap 35 to produce a liquid VOC stream 36. Stream 36 can be recycled to mixer 4 or preferably the liquid VOC can be separated from the water 38 in stream 36 by a filter 37 to produce VOC product 39 that can be sold as a flavor enhancing additive.
Turning now to FIG. 4 in another preferred embodiment the [0034] permeate 31 is passed through an ultrafiltration unit 40. The filter size is selected to be less than about 100,000 molecular weight to produce a protein and yeast rich retentate 41 and a vitamin and mineral rich permeate 42. By less than 100,000 molecular weight we mean that the filter is one that components less than about 100,000 molecular weight will pass. The protein and yeast rich retentate 41 is sent to dryer 43 to remove at least a substantial portion of the water from the retentate 41. It is preferred that the dryer 43 be operated to minimize the volalization of any VOC's in the retentate 41. This can be achieved by utilizing the same operating conditions as described above for dryer 32. Operated in this manner sufficient water can be removed to form a protein and yeast rich product 45 having less than 15% water by weight. Depending on the dryer operating conditions and the retention time of the protein and yeast retentate 41 in the dryer 43 some VOC may be volatized. Because the volume of the VOC is substantially less than in a conventional whole stillage treatment process, the water and VOC vapor 44 can be sent through a conventional and less expensive cold trap 48 to produce a liquid VOC stream 49. Stream 49 can be recycled to mixer 4 or preferably the water 51 in stream 41 can be separated by filter 50 to form a VOC product 52 that can be sold as a flavor enhancing additive.
In another preferred embodiment the vitamin and mineral rich permeate [0035] 42 is sent to the dryer 46 to remove at least a substantial portion of the water in permeate 42. It is preferred that the dryer 46 be operated to minimize the volalization of any VOC's in the permeate 42. This can be achieved by operating dryer 46 under the same conditions as dryer 43. Operated in this manner sufficient water can be removed to form a vitamin and mineral rich byproduct 47 having less than 15% water by weight. Depending on the dryer operating conditions and the retention time of the permeate 42 in the dryer 46 some VOC may be volatized. Because the volume of the VOC is substantially less than in a conventional stillage treatment process, the water and VOC vapor can be sent through a conventional and less expensive cold trap 48 to produce a liquid VOC stream similar to stream 49. This stream can also be recycled to mixer 4 or passed through a filter, such as filter 50, to form a VOC product that can be sold as a flavor enhancing additive.
Thus, as shown in the FIGS. [0036] 2-4, the whole stillage 14 can be processed to produce a protein rich product 23, a carotenoid rich product 34, a protein and yeast rich product 45, and a vitamin and mineral rich product 47 with minimum or no VOC's released to the atmosphere. The VOC's produced do not have to be treated by expensive thermal oxidizers or similar equipment, but can be sent to a less expensive cold trap and filter to produce yet another value added product, liquid VOC's. Each of these five product streams has significantly greater commercial value than the currently produced animal feed DDGS.
It is not necessary that separate cold traps be used for each of the product streams. Depending on the amount of VOC volatized, the different VOC streams volatized can be combined and sent to one or more of the cold traps, thus further reducing capital expense. Depending on the product desired it is also possible to direct various streams to a common dryer. There are of course other alternate embodiments that are obvious from the foregoing descriptions of the invention which are intended to be included within the scope of the invention as defined by the following claims. [0037]
In another preferred embodiment of the present invention the thin stillage is dried to a substantially free flowing powder by any suitable drying means. Non-limiting examples of suitable drying means include spray drying, fluidized bed drying, single and double drum dehydrating, use of ring drier or other suitable means to produce a substantially free flowing solid. It is preferred that the drier can be a spray drier. It is preferred that the water content of the thin stillage be first reduced by one or more dewatering steps, such as evaporation, prior to being subjected to the drying means. The dewatering step(s) is distinguished from the drying step since the drying step is performed at elevated temperatures and the dewatering is done by lower temperature operations that include gross water separation, such as by pressing, evaporation, etc. After drying, the resulting free flowing powder will contain 15 wt. % or less water, based on the total weight of the final dried product. It is preferred that the water content of the final product be from about 10 wt. % to about 15 wt. %. It is also preferred that the drying be done at an effective temperature and for an effective amount of time. By effective temperature we mean that temperature that is effectively low so that desirable ingredients, such as proteins, are not destroyed but not so low that drying takes an uneconomical amount to time. Such temperatures will be less than about 170° F., typically from about 140° F. to about [0038] 170° F. An effective amount of an additive can be introduced into the thin stillage stream prior to drying or it can be introduced into the drying means simultaneously with the thin stillage. The additive can be any ingredient in an amount that is needed to produce a final dried product having the desired properties for its intended end use. Non-limiting end uses can be an ingredient for a pet food or for human consumption. Non-limiting examples of such additives are selected from vitamins, minerals, amino acids, proteins, flavors, phytochemicals, pharmaceuticals, nutraceuticals, binders and fillers, other streams resulting from the treatment of cereal grains, and mixtures thereof. It is to be understood that the free flowing syrup powder can also be subjected to an oil removal step as previously described.

Claims

What is claimed is:

1. A process for recovering an oil stream from the whole stillage produced in the production of ethanol from an oil-bearing agricultural product, which process comprises:

separating the whole stillage in a solids rich stream referred to as the wet distillers grains stream and a water rich stream referred to as the thin stillage stream, both streams containing oil from the cereal grains;

conducting the wet distillers grains stream, the thin stillage stream, or both, to an oil removal stage wherein at least a portion of the oil is removed from the one or both streams, and wherein the oil is removed by centrifugation or solvent extraction.

2. The process of claim 1 wherein centrifugation is used to separate the oil from the one or more streams, thereby resulting in an oil and water stream, which oil and water stream is sent to a separation zone.

3. The process of claim 2 wherein the separation zone is a distillation stage wherein water is distilled from the oil.

4. The process of claim 2 wherein the separation zone is a decanting stage wherein the oil and water stream is allowed to sit in a suitable vessel until a two phase system develops, an oil phase and a water phase.

5. The process of claim 4 wherein the oil phase is decanted from the water phase.

6. The process of claim 1 wherein only the thin stillage stream is subjected to oil removal.

7. The process of claim 6 wherein centrifugation is used to remove oil from the thin stillage stream.

8. A process for recovering an oil stream from the thin stillage that results in the production of ethanol from cereal grains, which process comprises:

drying the thin stillages stream so that its water content is less than about 15 wt. %;

passing the dried thin stillage into an extraction zone;

contacting said dried thin stillage with a normally gaseous solvent for in effective amount of time thereby extracting oil from said dried thin stillage and resulting in a substantially oil free dry thin stillage and an oil in solvent solution;

conducting said oil in solvent solution to a separation zone wherein the solvent is evaporated from the oil;

collecting the substantially oil free thin stillage and the oil.

9. The process of claim 8 wherein the solvent is selected from the group consisting of butane, propane, and mixtures thereof.

10. The process of claim 8 wherein the oil removal is performed in batch mode.

11. The process of claim 8 wherein the oil removal is performed in continuous mode.

12. In a process wherein a cereal grain is milled, formed into a mash and fermented to produce an ethanol stream and a whole stillage stream, which whole stillage stream is centrifuged to produce: a) a wet distiller grains stream, which is dried to produce a dried distiller grains stream; and b) a thin stillage stream, which is evaporated to produce a syrup stream; and wherein all of said streams contain oil from the cereal grain, the improvement which comprises removing at least a portion of the oil from one or more of the stream selected from the wet distiller grains stream, the dried distiller grains stream, the thin stillage stream, and the syrup stream.

13. The process of claim 12 wherein only the thin stillage stream is subjected to oil removal.

14. The process of claim 13 wherein the oil is removed from the thin stillage stream by centrifugation.

15. The process of claim 14 wherein centrifugation results in a stream containing a mixture of oil and water.

16. The process of claim 15 wherein the mixture of oil and water stream is conducted to a decanting vessel wherein the mixture is allowed to sit until an oil phase is formed on top of a water phase.

17. The process of claim 16 wherein the oil phase is decanted from the water phase.

18. The process of claim 15 wherein the mixture of oil and water stream is conduced to a distillation stage wherein the water is distilled from the oil.

19. The process of claim 12 wherein the thin stillage stream is conducted to an evaporator to produce a syrup stream containing less than about 15 wt. % water, which syrup stream is itself conducted to an oil removal stage wherein at least of the oil is removed from the syrup.

20. The process of claim 19 wherein the oil is removed from the syrup by centrifugation to produce a mixture of oil and water stream.

21. The process of claim 20 wherein the mixture of oil and water stream is conducted to a decanting vessel wherein the mixture is allowed to sit until an oil phase is formed on top of a water phase.

22. The process of claim 21 wherein the oil phase is decanted from the water phase.

23. The process of claim 20 wherein the mixture of oil and water stream is conduced to a distillation stage wherein the water is distilled from the oil.

24. The process of claim 12 wherein the thin stillage is conducted to an evaporator to produce a solids rich syrup stream, then to a drier to produce a free-flowing solids stream, which free-flowing solids stream is conducted to an oil removal zone wherein at least a portion of its oil is removed by use of solvent extraction.

25. The process of claim 24 wherein the free-flowing solids stream is subjected to oil removal process comprising: introducing the free-flowing solids into an evaporation vessel; removing air from the extraction vessel; introducing a normally gaseous solvent into the extraction vessel at a rate and under a pressure to cause the normally gaseous solvent to convert to a liquid; causing the free-flowing solids and solvent to have an effective residence time to allow at least a portion of the oil to dissolve in the solvent; passing the oil and solvent to a separation zone wherein the solvent is separated from the oil.

26. The process of claim 25 which is a continuous process.

27. The process of claim 25 which is a batch process.

28. The process of claim 25 wherein the normally gaseous solvent is selected from butane, propane, and mixtures thereof.