US20100159549A1 - System for production of ethanol and co-products with separation and solvent washing of fermentation product - Google Patents

Abstract

A system for the production of ethanol and co-products is provided. The system facilitates an overall reduction in the use of energy, for example, by reducing the mass of wet solids supplied to a distillation system. The system also reduces the amount of energy used to dry the wet solids component of a fermentation product, for example, by increasing the ethanol concentration of the wet solids. The system also facilitates the recovery of co-products including bioproducts and other biochemicals extracted from components of the fermentation product. The solids component of the fermentation product may be dried and constituted into a meal that may be used for animal feed, among other uses.

Description

CROSS REFERENCE TO RELATED APPLICATIONS
• This application claims priority from and the benefit of and incorporates by reference, each of the following: (a) U.S. Provisional Application Ser. No. 61/140,454, entitled FORMING DRIED SOLID FROM A FERMENTATION PROCESS, filed Dec. 23, 2008; (b) U.S. Provisional Application Ser. No. 61/161,342, entitled PROCESS FOR LOW ENERGY DRYING OF ETHANOL FERMENTATION SOLIDS, filed Mar. 18, 2009; (c) U.S. Provisional Application Ser. No. 61/161,622, entitled PROCESS FOR LOW ENERGY DRYING OF ETHANOL FERMENTATION SOLIDS, filed Mar. 19, 2009; (d) U.S. Provisional Application Ser. No. 61/161,684, entitled LOW ENERGY DRYING OF ETHANOL FERMENTATION SOLIDS WITH REDUCTION OF NON-FERMENTABLE INPUTS, filed Mar. 19, 2009; (e) U.S. Provisional Application Ser. No. 61/162,097, entitled LOW ENERGY DRYING OF ETHANOL FERMENTATION SOLIDS WITH MULTIPLE ETHANOL FEEDS, filed Mar. 20, 2009; (f) U.S. Provisional Application Ser. No. 61/168,331, entitled PROCESS FOR PRODUCING ETHANOL, filed Apr. 10, 2009; (g) U.S. Provisional Application Ser. No. 61/179,347, entitled PROCESS FOR PRODUCING ETHANOL, filed May 18, 2009; and (h) U.S. Provisional Application Ser. No. 61/179,348, entitled PROCESS FOR PRODUCING ETHANOL, filed May 18, 2009.
BACKGROUND
• Ethanol can be produced from grain-based feedstocks (such as corn), cellulosic feedstocks (such as switchgrass or corn cobs), or other plant material (such as sugar cane).
• In a conventional ethanol plant producing ethanol from corn, corn kernels are processed to separate the starch-containing material (e.g. endosperm) from other matter (such as fiber and germ). The starch-containing material is then slurried with water and liquefied to facilitate saccharification where the starch is converted into sugar (i.e. glucose) and fermentation where the sugar is converted by an ethanologen (i.e. yeast) into ethanol. The product of fermentation is beer, which comprises a liquid component containing ethanol and water (among other things) and a solids component containing unfermented particulate matter (among other things).
• According to the process typically used at a conventional ethanol plant, the liquefaction of the starch-containing material is done by “cooking” the slurry at temperature at or near boiling point of water. According to an alternative process (that has been developed and implemented by the assignee of the present application), for example, as described in U.S. Patent Application Publication No. 2005/0239181, raw starch may be converted and fermented without “cooking” or liquefication.
• In a conventional ethanol plant, the liquid component and solids component of the fermentation product is sent to a distillation system. In distillation, the fermentation product is processed into, among other things, ethanol and stillage containing wet solids (i.e. the solids component of the beer with substantially all ethanol removed) formed into a wet cake which can be dried into distillers dried grains (DDG) and sold as an animal feed product. Other co-products, for example, syrup (and oil contained in the syrup) can also be recovered from the stillage. Water removed from the fermentation product in distillation can be treated for re-use at the plant.
• In a conventional ethanol plant, certain plant operations are conducted at elevated temperatures over ambient temperature with the resultant consumption of energy. For example, the liquefaction of the starch-containing slurry is typically done with a jet cooker (using natural gas as a fuel to elevate the temperature of the slurry to a boil). The amount of energy used in the distillation process (another operation performed at an elevated temperature, with heat typically provided by steam from an on-site boiler) is a function, among other things, the volume/mass of material supplied to the distillation system. And the drying of wet solids into distillers dried grains, an operation in which water is removed from the solids typically in a dryer (such as a ring dryer) heated by natural gas, will consume energy as a function of the properties (e.g. heat capacity, heat of vaporization and boiling point) of the water to be removed from the solids.
• It would be advantageous provide for a system for producing ethanol that facilitates an overall reduction in the use of energy at the plant, for example, by reducing the mass of wet solids supplied to the distillation system. It would also be advantageous to provide for a system for producing ethanol that reduced the amount of energy used to dry the wet solids component of the fermentation product. It would further be advantageous to provide for a system for producing ethanol that facilitated the recovery of co-products including bioproducts and other biochemicals extracted from components of the fermentation product. It would further be advantageous to provide for a system for producing ethanol in which the solids component of the fermentation product would be dried and constituted into a meal that could be used for animal feed, among other uses.
SUMMARY
• The present invention relates to a system and method for processing a fermentation product of a fermentation process in a biorefinery that performs distillation of ethanol, the fermentation product comprising a liquid component and a solids component, the method comprising the steps of: (a) separating the liquid component from the solids component prior to distillation of the liquid component, (b) applying a solvent to the solids component to alter the composition of the solids component, and (c) drying the solids component, wherein the solids component is not exposed to heat added to the liquid phase product during the distillation process.
DRAWINGS
• FIG. 1 is a process flow diagram of an exemplary embodiment of a biorefinery.
• FIG. 2 is a process flow diagram of an exemplary embodiment of the biorefinery ofFIG. 1.
• FIG. 3 is a process flow diagram of an exemplary embodiment of the biorefinery ofFIG. 1.
• FIG. 4 is a process flow diagram of an exemplary embodiment of the biorefinery ofFIG. 1.
• FIG. 5 is a process flow diagram of an exemplary embodiment of the biorefinery ofFIG. 1.
• FIG. 6 is a block flow diagram of an exemplary embodiment of the biorefinery.
• FIG. 7 is a block flow diagram of an exemplary embodiment of the biorefinery.
• FIG. 8 is a block flow diagram of an exemplary embodiment of the biorefinery.
• FIG. 9 is a block flow diagram of an exemplary embodiment of the biorefinery.
• FIG. 10 is a block flow diagram of an exemplary embodiment of the biorefinery.
• FIG. 11 is a block flow diagram of an exemplary embodiment of the biorefinery.
• FIG. 12 is a block flow diagram of an exemplary embodiment of the biorefinery.
• FIG. 13 is a block flow diagram of an exemplary embodiment of solids washing processes.
• FIG. 14 is a process flow diagram of an exemplary embodiment of the solids washing processes.
• FIG. 15 is an exemplary graphical representation of energy for drying wet solids vs. the ethanol concentration of the wet solids.
• FIG. 16 is a block flow diagram of an exemplary embodiment of the solids washing processes.
• FIG. 17 is a process flow diagram of an exemplary embodiment of the solids washing processes.
• FIGS. 18A and 18B are cross-sectional views of an exemplary embodiment of a wash process capable of implementing multiple wash stages.
• FIGS. 19 through 23 are cross-sectional views at various locations along the filter belt ofFIGS. 18A and 18B.
• FIG. 24 is a perspective view of an exemplary embodiment of the ethanol wash process.
• FIG. 25 is a flow chart of the exemplary embodiment of the solids washing processes.
• FIG. 26 is a flow chart of the exemplary embodiment of multiple solids washing processes.
• FIG. 27 is a process flow diagram of an exemplary embodiment of the fractionation process.
• FIG. 28 is a block flow diagram of an exemplary embodiment of the saccharification process.
• FIG. 29 is a block flow diagram of an exemplary embodiment of the fermentation process.
• FIG. 30 illustrates exemplary embodiments of the separation process.
DETAILED DESCRIPTION
• FIG. 1 is a process flow diagram of an exemplary embodiment of abiorefinery10. Biorefinery10 receives a feedstock, illustrated ascorn12, and processes the feedstock to produce several usable products for consumption, principally ethanol. Although illustrated ascorn12, other types of feedstock such as sorghum, wheat, barley, potatoes, sugar cane, switchgrass, and corn cobs, may be processed bybiorefinery10. Additional inputs such as enzymes, yeast, water, and energy (e.g., heat energy) may be added to the feedstock to facilitate production of the usable products. The usable products frombiorefinery10 may includebioproducts14, such as corn oil, corn syrup, bran, flour, proteins (e.g., zein), and other suitable bioproducts,ethanol16, and ananimal feed18 shown as distillers dried grain (DDG).
• Ethanol16 is an alcohol produced fromcorn12 or other starch-based crop.Ethanol16 has many uses, and of particular interest is its capacity to be blended with gasoline for use inmotor vehicles20.Ethanol16 is a relatively clean-burning, high-octane fuel that may be produced domestically in the United States from renewable sources, reducing the dependence on foreign sources of energy.Ethanol16 also delivers economic vitality to agricultural regions where the feedstocks are produced. Ethanol blends increase fuel octane ratings, decrease harmful fossil fuel emissions, reduce fuel costs, and extend the overall supply of gasoline.
• FIG. 2 is a process flow diagram of an exemplary embodiment ofbiorefinery10 ofFIG. 1.Corn12 may be directed into a preparation/fractionation process24, where corn kernels ofcorn12 may be separated into non-fermentable solids (e.g., germ and fiber) and fermentable solids (e.g., endosperm). Once the endosperm has been separated from the non-fermentable solids, the endosperm may be ground into ground endosperm, which may be directed into asaccharification process26. Separation and grinding of endosperm may also be conducted in an integrated process.Saccharification process26 may also receive additional inputs (e.g., heat, water, and enzymes) and may convert starches within the ground endosperm into sugars, which may be suitable for fermenting. A fermentation slurry may be directed fromsaccharification process26 into afermentation process28.
• Fermentation process28 may also receive additional inputs (e.g., yeast and enzymes) and may ferment the sugars within the fermentation slurry to produce a certain concentration of ethanol within the fermentation slurry.Fermentation process28 may produce a certain amount of carbon dioxide (CO₂) and other gases, which may be processed through the use of ascrubber30 or other suitable equipment. The main product offermentation process28 is a fermentation product shown asbeer32 comprises a liquid component and a solids component and is generally a mixture of ethanol, water, syrup, particulate matter, and dissolved solids.Saccharification process26 andfermentation process28 may be performed separately, or according to certain embodiments, may be combined into a substantially integrated process (e.g., called simultaneous saccharification and fermentation (SSF)).
• Beer32 may be directed intosolids processing system34, which may washbeer32 with ethanol (or other solvent).Solids processing system34 ofFIG. 2 include a separation/wash process36, aseparation process38, and adesolventizing process40.Beer32 may be separated into a liquid component and a solids component by separation/wash process36. The liquid component from separation/wash process36 may be processed by a series ofdistillation system42, which primarily produceethanol16.Distillation system42 may include adistillation pre-treatment process44, adistillation process46, and a dehydration/filtration process48.Distillation pre-treatment process44 may remove wet solids components from the liquid component beforedistillation process46 produces ethanol, which may be dried within dehydration/filtration process48 to remove any remainingwater49. Dehydration/filtration process48 may include any suitable type of dehydration, such as dessication.Water49 removed fromdistillation system42 may be used as make-up water, as a slurry water source, or as a source of water for other processes internal or external to biorefinery10.
• The solids component comprises ethanol, water, syrup, meal, zein, lutein, lysine, various proteins (having different attributes and nutritional values), yeast, fiber, and other particulate matter and dissolved solids. The solids component may be processed throughsolids processing system34, which primarily producesmeal18 and several biochemicals, such as zein and xanthophylls.Ethanol16 fromdistillation process46 and/or dehydration/filtration process48 may be used in separation/wash process36 to wash the solids component with ethanol, increasing the ethanol concentration of the solids component and reducing the energy required to desolventize the solids component in thedesolventizing process40 to producemeal18. Liquids removed byseparation process38 anddesolventizing process40 may be directed to separation/wash process36.
• FIG. 3 is a process flow diagram of an exemplary embodiment ofbiorefinery10 ofFIG. 1. The processes are substantially similar to those ofFIG. 2 through the production ofbeer32.Beer32 may be directed into aseparation process50, which separates thebeer32 into a liquid component and a solids component. The liquid component fromseparation process50 may be processed by distillation processes operating throughdistillation system42 to produceethanol16.
• The solids component may be directed into awash process52, which washes the solids component withethanol16 fromdistillation process46 and/or dehydration/filtration process48. Biochemicals removed bywash process52 may be extracted by a biochemical extraction process. Certain components fromwash process52 may be directed into distillation system42 (e.g., distillation pre-treatment process44). Ethanol-washed solids fromwash process52 may be directed intoseparation process38, where a certain amount of water and ethanol may be removed before the ethanol (e.g., solvent) is removed bydesolventizing process40 to producemeal18. Liquids removed byseparation process38 anddesolventizing process40 may be directed to washprocess52.
• FIG. 4 is a process flow diagram of an exemplary embodiment ofbiorefinery10 ofFIG. 1. The processes are substantially similar to those ofFIGS. 2 and 3 through the production ofbeer32.Beer32 may be directed intodistillation process46, with ethanol fromdistillation process46 being directed to dehydration/filtration process48, and the liquid/solids mixture (e.g., stillage) fromdistillation process46 being directed into separation/wash process36. Separation/wash process36 may receive ethanol fromdistillation process46 and/or dehydration/filtration process48 and wash the liquid/solids mixture (e.g., stillage) fromdistillation process46 with the ethanol, increasing the ethanol concentration of the liquid/solids mixture (e.g., stillage). The ethanol-washed liquid/solids mixture (e.g., stillage) may be directed intoseparation process38, where a certain amount of water and ethanol may be removed before the ethanol (e.g., solvent) is removed bydesolventizing process40 to produce distillers dried grain (DDG)54. Liquids removed byseparation process38 anddesolventizing process40 may be re-cycled back through separation/wash process36. Biochemicals and stillage may be extracted from separation/wash process36.
• FIG. 5 is a process flow diagram of an exemplary embodiment ofbiorefinery10 ofFIG. 1. The processes are substantially similar to those ofFIGS. 2 through 4 through the production ofbeer32.Beer32 may be directed intowash process52, which may washbeer32 with ethanol fromdistillation process46 and/or dehydration/filtration process48. The ethanol-washedbeer32 may be directed intoseparation process38, where a certain amount of water and ethanol may be removed before the ethanol (e.g., solvent) is removed bydesolventizing process40 to producemeal18. Liquid removed byseparation process38 anddesolventizing process40 may be re-cycled back throughwash process52. Ethanol and water fromwash process52,separation process38, anddesolventizing process40 may also be directed into distillation system42 (e.g., distillation pre-treatment process44).
• FIG. 6 is a block flow diagram of an exemplary embodiment ofbiorefinery10.Corn12 may first be directed into preparation/fractionation process24, where it is prepared for saccharification and fermentation. Non-fermentable solids incorn12 may be separated (e.g., fractionated) from fermentable solids. Corn kernels generally comprise endosperm, germ, and fiber. Endosperm comprises most of the starches and proteins available in a corn kernel and, therefore, is used infermentation process28 to generate ethanol. In other words, endosperm represents the fermentable solids of a corn kernel; germ and fiber represent the non-fermentable solids, which may be withheld fromfermentation process28. Endosperm comprises approximately 80-85% of a corn kernel, germ comprises approximately 10-15% of a corn kernel, and fiber comprises approximately 5-10% of a corn kernel, all by mass.
• Non-fermentable solids56 may be directed into various bioproduct processes, which may produceusable bioproducts14.Non-fermentable solids56 may include the germ and fiber ofcorn12, which may be processed into bioproducts such as corn oil, corn syrup, bran, flour, and proteins (e.g., zein). Fermentable solids58 (e.g., endosperm of corn12) from preparation/fractionation process24 may be directed into a saccharification/fermentation process60, which may includesaccharification process26 andfermentation process28.Saccharification process26 andfermentation process28 may be conducted separately (e.g., in separate stages) or may be conducted concurrently (e.g., in an integrated stage). It should be noted thatfermentable solids58 may contain small portions of non-fermentable components (e.g., germ and fiber) not intended for the fermentation process.
• Preparation/fractionation process24 may include passingcorn12 through mills, such as hammer mills and pins mills, to grindfermentable solids58 into a fine powder (e.g., flour), further facilitating saccharification/fermentation process60. Fermentable solids58 (e.g., endosperm) include a high proportion of starches suitable for fermenting to produceethanol16. Saccharification/fermentation process60 may include saccharifyingfermentable solids58 to convert the starches withinfermentable solids58 into sugars. The process of saccharifyingfermentable solids58 may include adding heat, water, and enzymes to fermentablesolids58 to produce a fermentation slurry.
• Saccharification/fermentation process60 may also include adding yeast to the fermentation slurry. The yeast helps convert the sugars within the fermentation slurry intoethanol16 and carbon dioxide. The fermentation slurry may be agitated and cooled until the concentration ofethanol16 has been maximized. The output from saccharification/fermentation process60 may be referred to asfermentation product32, which may generally includeethanol16, but may also include a certain amount of water, as well as syrup, particulate matter, and dissolved solids.
• Fermentation product may be separated byseparation process50 into a liquid component and a solids component, both of which may be processed in respective processing paths. The liquid component may include liquid62, which containsethanol16, a certain amount of water and other non-ethanol liquids, as well as fine solids, which may be removed fromliquid62.Distillation system42 may remove most of the water, other non-ethanol liquids, and fine solids to produceethanol16.Ethanol16 leavingdistillation system42 may contain various target concentrations of ethanol, such as from approximately 95% (e.g., 190 proof) to approximately 100% (e.g., 200 proof). Stillage66 (e.g., comprising liquid and wet solids) fromdistillation system42 may be processed and/or combined into bioproducts14 (e.g., animal feed, oils, syrup, and other biochemicals).
• The solids component may includewet solids64, which may include a certain amount of ethanol, a certain amount of water, syrup, particulate matter, and dissolved solids. It should be noted that when reference is made to “solids,” the solids may include particulate matter and dissolved solids, which may be associated with a certain amount of liquids (e.g., “wet solids”).Solids processing system34 anddesolventizing process40 may remove most of the water and ethanol fromwet solids64 to producemeal18.Solids processing system34 may include washingwet solids64 with ethanol or a liquid with a desired ethanol content to decrease the boiling point, specific heat, and enthalpy (heat) of vaporization of thewet solids64, reducing the energy required to dry (e.g., desolventize)wet solids64 to producemeal18. The ethanol may be directed tosolids processing system34.
• FIG. 7 is a block flow diagram of an exemplary embodiment ofbiorefinery10. The processes are substantially similar to those ofFIG. 6 through the production ofbeer32. The fermentation product shown asbeer32 may be directed intodistillation system42, wherebeer32 is distilled to produceethanol16.Stillage66 fromdistillation system42 may be directed into solids processing system34 (e.g., including separation and washing), wherestillage66 may be washed with ethanol fromdistillation system42 and/ordesolventizing process40 to increase the ethanol concentration ofstillage66, reducing the amount of energy required bydesolventizing process40 to remove liquids fromstillage66 to produceDDG54. Thin stillage may be removed fromsolids processing system34 asbioproducts14.
• FIG. 8 is a block flow diagram of an exemplary embodiment ofbiorefinery10. The processes are substantially similar to those ofFIGS. 6 and 7 through the production of the fermentation product shown asbeer32.Beer32 may be separated byseparation process50 into a liquid component shown as comprisingliquid62 and a solids component shown as comprisingwet solids64.Ethanol16 may be recovered fromliquid62 bydistillation system42;wet solids64 may be directed intosolids processing system34, where solids may be washed with a solvent68 (e.g., hexane) other than ethanol.Solvent68 may be received bysolids processing system34 from asolvent conditioning process70, which may in turn receive spent solvent fromsolids processing system34, forming a closed-loop cycle of solvent68 throughsolids processing system34. Solvent from solvent-washedwet solids64 may be removed bydesolventizing process40 to producemeal18.Solvent conditioning process70 may also remove a ethanol/water mixture71 and direct the ethanol/water mixture71 todistillation system42.Solvent conditioning process70 may further removewater72 and extracted co-products74 fromwet solids64.
• FIG. 9 is a block flow diagram of an exemplary embodiment ofbiorefinery10. The processes are substantially similar to those ofFIGS. 6 through 8 through the production of the fermentation product shown asbeer32.Beer32 may be directed intodistillation system42, wherebeer32 is distilled to produceethanol16.Stillage66 fromdistillation system42 may be directed into solids processing system34 (e.g., separation and washing), wherestillage66 may be washed with solvent68 (e.g., hexane).Solvent68 may be received bysolids processing system34 fromsolvent conditioning process70, which may in turn receive spent solvent fromsolids processing system34, forming a closed-loop cycle of solvent68 throughsolids processing system34. Solvent from solvent-washedwet solids64 may be removed bydesolventizing process40 to produceDDG54.Solvent conditioning process70 may further removewater72 and extracted co-products74 fromstillage66. Thin stillage may be removed fromsolids processing system34 asbioproducts14.
• FIG. 10 is a block flow diagram of an exemplary embodiment ofbiorefinery10.Biorefinery10 begins with preparation/fractionation process24, which may include apreparation process76 and/or afractionation process78. Preparation/fractionation process24 preparescorn12 for saccharification and fermentation insaccharification process26 andfermentation process28.
• Preparation process76 may include a cleaning stage to remove impurities that may be present in the corn, such as stalks, cobs, stone, sand, and other fine particles. Clean corn output from the cleaning stage may be directed into a water tempering stage, wherecorn12 may be tempered with a water concentration for a period of time. In the water tempering stage, the water penetrates the germ and fiber ofcorn12, facilitating subsequent removal of the germ and fiber fromcorn12, as well as increasing resistance of the germ and fiber to physical breakage during subsequent stages (e.g., further separation).
• Temperedwhole corn12 frompreparation process76 may then be directed intofractionation process78.Corn12 may be fractionated into non-fermentable solids56 (e.g., primarily germ and fiber) and fermentable solids58 (e.g., primarily endosperm) withfermentable solids58 being milled to reduce the particle size offermentable solids58. The downstream processes ofbiorefinery10 may not require thatcorn12 be fractionated into endosperm, germ, and fiber. For example,separation process50 andsolids processing system34 do not require fractionatedcorn12 to lead to beneficial results, although such fractionation may enhance the benefits.
• The ground endosperm fromfractionation process78 may be directed intosaccharification process26, in which starch within the endosperm may be converted into sugars that can be fermented by a microorganism, such as yeast. The conversion may be accomplished by saccharifying the endosperm with a number of additional inputs, such as saccharifying enzyme compositions, without cooking the endosperm. The downstream processes ofbiorefinery10 may not require thatcorn12 be saccharified prior tofermentation process28, although certain benefits and co-products may be enhanced bysaccharification process26.
• The output ofsaccharification process26 may be described as a fermentation slurry, which may be directed intofermentation process28, in which sugars within the fermentation slurry are fermented to produceethanol16. Additional inputs (e.g., microorganisms such as yeast) may be introduced intofermentation process28 to facilitate the fermenting. The output offermentation process28 may includefermentation product32, such as a mixture of ethanol, water, syrup, particulate matter (e.g., fiber, germ, yeast, etc.), and dissolved solids.
• Fermentation product32 fromfermentation process28 may be directed intoseparation process50, in whichfermentation product32 is separated into a liquid component (e.g., liquid62) and a solids component (e.g., wet solids64). The equipment used forseparation process50 may vary and may include, for example, centrifuges, decanters, hydroclones, sedimentation tanks, and filter presses.
• Liquid62 (e.g., water/ethanol mixture) and wet solids64 (e.g., wet solids) may then be directed into separate processing paths.Liquid62 may be directed intodistillation system42;wet solids64 may be processed throughsolids processing system34. An end product of the liquids processing path isethanol16; an end product of the solids processing path is meal18 (and possibly other bioproducts such as biochemicals).
• Liquid62 (e.g., water/ethanol mixture) fromseparation process50 may first be directed intodistillation pre-treatment process44, in whichliquid62 is prepared for further distillation.Distillation pre-treatment process44 may includeheating liquid62 prior to distillation.Distillation pre-treatment process44 may also include removing the remaining fractions of germ and fiber fromliquid62 asbioproducts14. Onceliquid62 has been pre-treated bydistillation pre-treatment process44, thepre-treated liquid62 may be directed intodistillation process46, in which water may be removed fromethanol16.Ethanol16 fromdistillation process46 may be approximately 190 proof (e.g., approximately 95% alcohol).Ethanol16 fromdistillation process46 may then be directed into dehydration/filtration process48, in whichethanol16 is further dried and filtered.Ethanol16 from dehydration/filtration process48 may be approximately 200 proof (e.g., approximately 100% alcohol).Ethanol16 from dehydration/filtration process48 may be sold for use as a fuel.
• Wet solids64 fromseparation process50 may first be directed into awash process52, in whichwet solids64 are washed with various concentrations ofethanol16 to increase the ethanol concentration ofwet solids64. Thewet solids64 may then be directed intoseparation process38 anddesolventizing process40, in which thewet solids64 may be deliquified, separated, and desolventized to generatemeal18. By increasing the ethanol concentration ofwet solids64 inwash process52, the boiling point of the liquid component of the wet solids will be decreased, as will its specific heat and enthalpy (heat) of vaporization, reducing the energy required to dry (e.g., desolventize) the wet solids indesolventizing process40.Wash process52 andseparation process38 may be integrated or separate, such that each stage throughwash process52 andseparation process38 progressively increases the ethanol content in the wet solids.Ethanol16 fromseparation process38 anddesolventizing process40 may be used to increase the ethanol concentration ofwet solids64 inwash process52.
• FIG. 11 is a block flow diagram of an exemplary embodiment ofbiorefinery10. The processes are substantially similar to those ofFIG. 10 throughfermentation process28.Fermentation product32 fromfermentation process28 may be directed into distillation system42 (e.g.,distillation pre-treatment process44,distillation process46, and dehydration/filtration process48), wherefermentation product32 is distilled to produceethanol16.Stillage66 fromdistillation process46 may be directed intosolids processing system34, wherestillage66 may be washed with ethanol to increase the ethanol concentration ofstillage66, reducing the amount of energy required bydesolventizing process40 to remove liquids fromstillage66 to produceDDG54.Solids processing system34 may receive the ethanol fromdistillation process46 and/or dehydration/filtration process48. A certain amount of ethanol fromdesolventizing process40 may be directed back tosolids processing system34 for further use. Anextraction process79 may also extractbioproducts14 fromsolids processing system34. Some biochemicals may be extracted fromsolids processing system34 and directed intodistillation pre-treatment44 for further processing.
• FIG. 12 is a block flow diagram of an exemplary embodiment ofbiorefinery10. The processes are substantially similar to those ofFIGS. 10 and 11 throughfermentation process28.Fermentation product32 fromfermentation process28 may be separated byseparation process50 into a liquid component shown as comprisingliquid62 and a solids component shown as comprisingwet solids64.Liquid62 may be converted intoethanol16 by distillation system42 (e.g.,distillation pre-treatment process44,distillation process46, and dehydration/filtration process48);wet solids64 may be directed intowash process52, where solids may be washed with a solvent68 (e.g., hexane) other than ethanol.Solvent68 may be received bywash process52 fromsolvent conditioning process70, which may in turn receive spent solvent fromwash process52, forming a closed-loop cycle of solvent68 throughwash process52. Solvent from solvent-washedwet solids64 may be removed byseparation process38 anddesolventizing process40 to producemeal18. Some of the solvent removed fromseparation process38 anddesolventizing process40 may be directed to washprocess52 for further use.Solvent conditioning process70 may also remove an ethanol/water mixture71 and direct the ethanol/water mixture71 to distillation system42 (e.g., distillation pre-treatment process44).Solvent conditioning process70 may further removewater72;extraction process79 may extract co-products74. Bothpre-treatment process44 and washprocess52 may facilitate the recovery ofbioproducts14 available from thefermentation product32.
• The individual processes ofbiorefinery10 may be highly synergistic, with each process contributing to efficiencies and other benefits of other processes. For example, by fractionating and milling the feedstock into primarily ground endosperm infractionation process78, the downstream processes ofbiorefinery10 may be indirectly enhanced. Because primarily fermentable endosperm is directed intosaccharification process26, only enough energy to saccharify the endosperm will be required bysaccharification process26. Energy need not be expended processing the non-fermentable solids (e.g., germ and fiber) insaccharification process26 or in other processes, such as the operation ofdistillation system42. Because the fermentation slurry fromsaccharification process26 consists of primarily fermentable solids, water, and enzymes,fermentation process28 may also be generally more efficient.
• By saccharifying the ground endosperm insaccharification process26 without cooking, the amount of heat input into the ground endosperm may be lower as compared to conventional cooking processes. Saccharifying the ground endosperm without “cooking” (e.g., using “raw starch” hydrolysis) may lead tomeal18 having a different quality thanDDG54 produced by conventional biorefineries. For example,meal18 may be higher in protein values, as well as higher in amino acids (e.g., lysine) and other biochemicals having different attributes and qualities, thantypical DDG54.
• Separating a liquid component comprising liquid62 from a solids component comprisingwet solids64 inseparation process50 may lead to several benefits downstream ofseparation process50. Because wet solids64 (e.g., a certain amount of ethanol, a certain amount of water, syrup, particulate matter, and dissolved solids) have been substantially removed from liquid62 (e.g., a water/ethanol mixture), the distillation equipment ofdistillation process46 will be much less likely to encounter fouling fromwet solids64, which may otherwise impair the performance of the distillation equipment, render it less efficient, and/or require cleaning. The distillation equipment ofdistillation process46 may also be sized smaller because the added mass ofwet solids64 need not be processed through the distillation equipment. The removal ofwet solids64 may also lead to the distillation equipment ofdistillation process46 requiring less energy than conventional distillation equipment.
• The combination of the processes ofbiorefinery10 may lead to overall energy reduction ofbiorefinery10, as well as reducing the temperature to which the products ofbiorefinery10 are exposed.Wet solids64,stillage66,meal18, andDDG54 may all be processed bybiorefinery10 without ever experiencing temperatures above approximately 150° C. Maintaining the temperature below 150° C. has been shown to reduce the possibility of degradation of the resultingmeal18 orDDG54. Reduced degradation may include color transformation and significant oxidation of residual starches downstream offermentation process28. Using measurements of the resultingmeal18 orDDG54, such as neutral detergent fiber (NDF) measurements, it has been found that maintaining the temperatures experienced bymeal18 orDDG54 withinbiorefinery10 under approximately 150° C. significantly reduces the possibility of degrading theresultant meal18 orDDG54. Using these same measurements, it has been found that maintaining the temperatures experienced bymeal18 orDDG54 withinbiorefinery10 under approximately 100° C. may further reduce the possibility of degrading themeal18 orDDG54.
• FIGS. 13 and 14 are a block flow diagram and a process flow diagram of an exemplary embodiment ofsolids processing system34. Wet solids components80 (e.g.,wet solids64 or stillage66) may be washed withethanol16 to increase the ethanol concentration, facilitating the reduction of energy required for drying.Wet solids components80 may generally comprise wet solids or wet beer solids. Washing with ethanol may lead to lower drying energy consumption regardless of whether a liquid component (e.g., liquid62) and a solids component (e.g., wet solids64) have been separated byseparation process50. The ethanol wash may also be used with wet solids exiting a distillation process, as in existing plants.
• A stream ofethanol16 may be introduced intowet solids components80. The stream ofethanol16 may be received fromdistillation system42 or may be received from other sources internal or external to biorefinery10. The stream ofethanol16 may be fed through ethanolfeed flow lines82 into anethanol distribution system84, which applies (e.g., sprays, mists, drips, deposits, or pours over)ethanol16 towet solids components80 to increase the ethanol concentration ofwet solids components80. Althoughethanol distribution system84 is illustrated as a series of spray nozzles, other means of applyingethanol16 may be used. For example,ethanol16 may be poured overwet solids components80.Wet solids components80 will remain generally unperturbed by the application ofethanol16. Oncewet solids components80 have been washed withethanol16, liquid86 (e.g., a mixture of water and ethanol) fromwet solids components80 may be collected by aliquid collection88, such as a tank or collection tray. Co-products (e.g., zein and xanthophylls) may be extracted fromliquid86, and liquid86 collected byliquid collection88 may be directed intodistillation system42 for further processing.
• Wet solids components80 washed withethanol16 may be transformed intowet solids components90, which contain an increased concentration ofethanol16 to water as compared to the initialwet solids components80. Less energy may be required by adesolventizer40 to dry (i.e., desolventize) wet solids components90 (e.g., after ethanol washing) than would be required bydesolventizer40 to dry (i.e., desolventize) wet solids components80 (e.g., before ethanol washing). The reduction in energy required to desolventize/drywet solids components90 to producemeal18 may be due at least in part to the fact thatwet solids components90 contain an increased concentration ofethanol16 to water as compared towet solids components80.
• FIG. 15 is an exemplarygraphical representation92 of energy for drying wet solids as it relates to the amount of ethanol present in the liquid portion of those wet solids. The horizontal axis inFIG. 15 represents the volume of ethanol present in the liquid portion of the wet solids as a percent of the total liquid volume portion of the wet solids. The vertical axis inFIG. 15 represents the amount of energy that it would take to dry (e.g., by vaporization) all liquid from wet solids. The graphical representation inFIG. 15 represents the relationship of the amount of energy to dry the solids within the liquid portion as the concentration of ethanol changes in the liquid portion of the wet solids. In a conventional drying process, the wet solids may contain no ethanol and may require ε₀amount of energy to remove the liquid from wet solids. By processing the wet solids to contain 20% by volume of ethanol, the amount of energy required to remove the liquid from wet solids would decrease to ε₂₀as depicted inFIG. 15. This trend continues as the ethanol concentration is increased, as seen when the ethanol concentration is increased to 90% by volume and the new amount of energy required to remove the liquid portion is drastically reduced to ε₉₀. The lowest amount of energy required to remove the liquid from wet solids can be achieved when the liquid is 100% ethanol.
• Returning toFIGS. 13 and 14, increasing the ethanol concentration ofwet solids components90 decreases the amount of energy required to drywet solids components90 at least partially because water has a relatively high boiling point, heat capacity, and enthalpy (heat) of vaporization as compared to ethanol. A relatively high amount of energy is required to heat water to a temperature sufficient to vaporize the water; a relatively low amount of energy is required to heat ethanol to a temperature sufficient to vaporize ethanol. For example, the boiling point of ethanol is approximately 173° F. at atmospheric pressure; the boiling point of water is approximately 212° F. at atmospheric pressure. The heat capacity of ethanol is approximately 0.58 BTU/lb-° F.; the heat capacity of water is 1.0 BTU/lb-° F. The enthalpy (heat) of vaporization of ethanol is approximately 362 BTU/lb; the enthalpy (heat) of vaporization of water is approximately 980 BTU/lb. Ethanol may be heated with less energy input, reaching its boiling point at a lower temperature, and once at the boiling point, vaporizes with less energy input.
• Increasing the ethanol concentration ofwet solids components90 helps to decrease the amount of energy required bydesolventizer40 to dry/desolventizewet solids components90.FIGS. 13 and 14 include one stage of ethanol washing.FIGS. 16 and 17 are a block flow diagram and a process flow diagram of exemplary embodiments ofsolids processing system34, comprising multiple ethanol wash stages.Separation process50 may separate a liquid component shown as liquid62 (e.g., a water/ethanol mixture) from a solids component shown as wet solids64 (e.g., a certain amount of ethanol, a certain amount of water, syrup, particulate matter, and dissolved solids).Liquid62 may be directed intodistillation process46, which may produceethanol16.
• Ethanol94 fromdistillation system42 may be directed into afirst stage wash96, which also receiveswet solids64 fromseparation process50.Wet solids64 fromseparation process50 are washed withethanol94 to increase the ethanol concentration ofwet solids64. It should be noted that when reference is made to “ethanol” in the discussions of the wash process, the fluid used may, and in many cases will, be an ethanol-containing fluid, such as a mixture of water and ethanol. Any other suitable solvent (e.g., hexane) may also be used. The “wash” fluid will generally have a higher concentration of ethanol (or other solvent) than the wet solids receiving the wash, displacing water in the wet solids with ethanol (or other solvent).
• First stage wash96 is configured to mixwet solids64 withethanol94. Ethanol-washedsolids98 fromfirst stage wash96 may be directed into afirst stage separation100, which separatesfirst stage solids102 fromfirst stage liquid104.First stage liquid104 may consist of a water/ethanol mixture, which may be directed back todistillation system42 for further processing.First stage liquid104 washes away a certain amount of the water fromwet solids64.First stage solids102 output fromfirst stage separation100 will have a higher ethanol concentration thanwet solids64 input intofirst stage wash96.
• A second stream ofethanol106 may be directed into asecond stage wash108, which also receivesfirst stage solids102 fromfirst stage separation100.First stage solids102 fromfirst stage separation100 may be washed withethanol106 to further increase the ethanol concentration offirst stage solids102.Second stage wash108 may be configured to mixfirst stage solids102 withethanol106.Ethanol106 may be received fromdistillation system42 or may be received from other processes withinbiorefinery10.
• Ethanol-washedsolids110 fromsecond stage wash108 may be directed into asecond stage separation112, which may separatesecond stage solids114 fromsecond stage liquid116.Second stage liquid116 may consist of a water/ethanol mixture, which may be directed back tofirst stage wash96.Second stage liquid116 may supplement or replaceethanol94 fromdistillation system42 to washwet solids64 infirst stage wash96.Second stage liquid116 washes away a certain amount of the water fromfirst stage solids102.Second stage solids114 output fromsecond stage separation112 will have a higher ethanol concentration thanfirst stage solids102 input intosecond stage wash108.
• The ethanol wash cycles (e.g., washing and separating) may be repeated multiple times. A last stream ofethanol118 may be directed into afinal stage wash120, which also receives the previous stage solids from a previous stage separator. The previous stage solids may be washed withethanol118 to further increase the ethanol concentration of the previous stage solids. Final stage wash120 may be configured to mix the previous stage solids withethanol118.Ethanol118 may be received fromdistillation system42 or may be received from other processes withinbiorefinery10.
• Ethanol-washedsolids122 fromfinal stage wash120 may be directed into afinal stage separation124, which may separatefinal stage solids126 fromfinal stage liquid128. Final stage liquid128 will consist of a water/ethanol mixture, which may be directed back to the previous stage wash. Final stage liquid128 may wash away a certain amount of the water from the previous stage solids.Final stage solids126 output fromfinal stage separation124 will have a higher ethanol concentration than the previous stage solids input intofinal stage wash120.
• Final stage solids126 may then be directed into anevaporation stage130, in which the remaining liquid may be evaporated fromfinal stage solids126, leaving dry or substantiallydry meal18.Ethanol vapor132 recovered fromevaporation stage130 may be condensed by acondenser134 and added to thefinal stage ethanol118 in the final stage ethanol wash cycle, as shown byline136. In order to effect the condensation ofethanol vapor132 fromevaporation stage130, a heat exchanger may be used to recover waste heat from any available source, and direct the heat intoevaporation stage130.
• FIG. 17 is substantially similar toFIG. 16 with additional wash stages illustrated. A third stream ofethanol138 may be directed into athird stage wash140, which also receivessecond stage solids114 fromsecond stage separation112.Second stage solids114 fromsecond stage separation112 may be washed withethanol138 to further increase the ethanol concentration ofsecond stage solids114.Third stage wash140 may be configured to mixsecond stage solids114 withethanol138.Ethanol138 may be received fromdistillation system42 or may be received from other processes withinbiorefinery10.
• Ethanol-washedsolids142 fromthird stage wash140 may be directed into athird stage separation144, which may separatethird stage solids146 fromthird stage liquid148.Third stage liquid148 may consist of a water/ethanol mixture, which may be directed back tosecond stage wash108.Third stage liquid148 may supplement or replaceethanol106 fromdistillation system42 to washfirst stage solids102 insecond stage wash108.Third stage liquid148 washes away a certain amount of the water fromsecond stage solids114.Third stage solids146 output fromthird stage separation144 will have a higher ethanol concentration thansecond stage solids114 input intothird stage wash140.
• This process continues with a fourth stream ofethanol150 being used by a next-to-final stage wash152 to generate ethanol-washedsolids154, which may be separated by a next-to-final stage separation156. Similar to the other wash stages,solids158 from next-to-final stage separation156 may be directed intofinal stage wash120; liquid from next-to-final stage separation156 may be directed to the previous wash stage.
• The ethanol wash stages ofFIGS. 16 and 17 may be repeated multiple times such that the wet solids contain a low concentration of water and a high concentration of ethanol. The number of ethanol wash stages may be chosen to achieve a particular concentration of ethanol in the resultant wet solids prior to drying. The concentration of the resultant wet solids prior to drying may be selectively adjusted. In each ethanol wash stage, the washes receive a quantity of ethanol wash containing a higher ethanol concentration than the concentration present in the wet solids. For each ethanol wash stage, a water/ethanol mixture may be received from a subsequent ethanol wash stage as an ethanol wash source. The water/ethanol mixture from a subsequent ethanol wash stage may be suitable for a previous ethanol wash stage because the water/ethanol mixture from the subsequent ethanol wash stage may generally contain more ethanol than the wet solids of the previous ethanol wash stage. Using ethanol from a subsequent ethanol wash stage allows the same stream ofethanol94 brought into the initial ethanol wash stage to be used over and over again until the final ethanol wash stage. If enough ethanol wash stages are used, the composition of the resulting wet solids will have an ethanol concentration approximately equal to the ethanol concentration of ethanol used in the initial ethanol wash stage. After the multiple ethanol wash stages, the resultantfinal stage solids126 contain a liquid component with a higher concentration of ethanol thanwet solids64 fromseparation process50. In certain embodiments,ethanol stream118 may be the only stream of ethanol used; ethanol streams94,106,138, and150 may be used as make-up ethanol, to selectively control the concentration of ethanol in the other wash stages, or may be omitted.
• Returning toFIG. 15, to minimize the energy to drymeal18, the ethanol concentration of the resultantfinal stage solids126 may be at or above the azeotropic ratio for water and ethanol (e.g., point A), which is approximately 96% ethanol-to-water. At concentration levels at or above the azeotropic ratio, ethanol in wet solids will vaporize at substantially the same rate as the remaining water in the wet solids, leavingmeal18 while using the least amount of energy for drying. With a ratio of ethanol-to-water below the azeotropic ratio, drying of wet solids will be less efficient than when the ratio is at or above the azeotropic ratio. The process may bring the ethanol content of the wet solids to any point along the concentration line with consequent benefits to drying. In an effort to achieve certain benefits, the wet solids will be brought to an ethanol concentration above the azeotropic ratio.
• Returning now toFIGS. 16 and 17,evaporation stage130 may employ a dryer for drying the resultantfinal stage solids126, otherwise referred to as wet cake. The drying process may exposemeal18 to temperatures just high enough to vaporizeethanol vapor132 frommeal18.Meal18 may be altered and change color when exposed to high temperatures. By limiting the temperature thatfinal stage solids126 experience by using a low-energy drying process, the possibility of altering themeal18 duringevaporation stage130 may be substantially reduced. Becausefinal stage solids126 may be dried at much lower temperatures and with less energy input than in conventional processes, a large volume of air may not be required duringevaporation stage130. Because a lower volume of air may be used inevaporation stage130 for low-energy drying, the concentration of liquid in the resultingethanol vapor132 may be relatively high.Ethanol vapor132 may also be condensed and re-used withinbiorefinery10, reducing emissions frombiorefinery10. Because water used inevaporation stage130 may be re-circulated, more of the water initially injected into the saccharification (if used) and fermentation processes ofbiorefinery10 may be sent back todistillation system42, where it may be captured and re-used, significantly reducing the overall water consumption ofbiorefinery10. The specific equipment ofFIGS. 16 and 17 are merely illustrative. Other specific equipment and processes may be used to implement multiple ethanol wash stages to increase the ethanol concentration of wet solids for the purpose of reducing the energy required to dry the wet solids.
• Each stage of the solids processing (including steps in the wash/separation process) may be conducted on a single apparatus or (as indicated inFIGS. 16-18, for example) may be conducted on separate apparatus of the same type or including different types of apparatus (e.g., a filter belt system, separator, centrifuge, decanter, etc.); different stages of the processing of the solids component may be conducted on the same or on different/separate apparatus. In the processing of the wet solids (e.g. wet cake), additional operations to the wash/separation process, including operations such as soaking, re-mixing, slurrying, or other processing of the solids component may be conducted in various sequences, before, during or after washing and separating operations.
• According to an exemplary embodiment, at least a portion of the solids processing can be conducted on a filter belt system shown as including filter belt162 (see, e.g.,FIGS. 18 through 24). The filter belt system may include one or more belts (e.g., for conveying material), some of which may be comprised of a filter media (e.g., to allow the filtration of material on and through the belt), bulk handling systems for loading and unloading the material into and from the system, controls and other instrumentation. The filter belt system may be segmented into stages or chambers (some of which may be configured to operate at differential pressure, including vacuum or positive pressure). According to other embodiments, other combinations of systems may be used for solids processing of the solids component (e.g., wet solids or wet cake).
• FIGS. 18A and 18B are cross-sectional views of an exemplary embodiment of anethanol wash process160 capable of implementing multiple ethanol wash stages.Ethanol wash process160 comprises an apparatus shown as afilter belt162 conveyed by a pair ofrollers164,166.Rollers164,166 are configured to rotate in a clockwise fashion, as shown byarrow168, causingfilter belt162 to move in a left-to-right direction from the top ofroller164 to the top ofroller166, as shown byarrow170, and in a right-to-left direction from the bottom ofroller166 to the bottom ofroller164, as shown byarrow172. The specific relative movement offilter belt162 androllers164,166 may vary among specific implementations.
• Wet solids64 may be loaded onto the top offilter belt162 and may move in a left-to-right direction. The left-hand end offilter belt162 may be referred to as the upstream end; the right-hand end offilter belt162 may be referred to as the downstream end.Ethanol wash process160 utilizes a counterflow ethanol wash process. Ethanol may flow throughethanol wash process160 from the downstream end offilter belt162 to the upstream end offilter belt162;wet solids64 may flow throughethanol wash process160 from the upstream end offilter belt162 to the downstream end offilter belt162. The ethanol used forethanol wash process160 generally flows in a direction opposite from the flow ofwet solids64. The ethanol used forethanol wash process160 may alternatively flow in the same direction aswet solids64.
• Ethanol may be introduced intoethanol wash process160 toward the downstream end offilter belt162. A first stream ofethanol174 may be applied to (e.g., poured over, sprayed onto, or deposited onto)wet solids64 byethanol distribution system84 above a firstdownstream collection vessel176. A mixture of water and ethanol may be drawn throughfilter belt162 by gravity and/or vacuum intocollection vessel176 or the flow of the mixture of water and ethanol throughfilter belt162 and intocollection vessel176 may be facilitated by positive differential pressure abovefilter belt162. The water/ethanol mixture178 fromcollection vessel176 may then be combined with a second stream ofethanol180, with the combination being applied to (e.g., poured over, sprayed onto, or deposited onto)wet solids64 byethanol distribution system84 above a seconddownstream collection vessel182, which is upstream ofcollection vessel176. The first stream ofethanol174 may have a higher, lower, or substantially similar concentration of ethanol than the second stream ofethanol180. In other embodiments, the second stream ofethanol180 may not be combined with the water/ethanol mixture178 fromcollection vessel176, but rather only the water/ethanol mixture178 may be applied towet solids64. A mixture of water and ethanol may be drawn throughfilter belt162 by gravity and/or vacuum intocollection vessel182 or the flow of the mixture of water and ethanol throughfilter belt162 and intocollection vessel182 may be facilitated by positive differential pressure abovefilter belt162. The water/ethanol mixture184 fromcollection vessel182 may then be applied to (e.g., poured over, sprayed onto, or deposited onto)wet solids64 byethanol distribution system84 above a thirddownstream collection vessel186, which is upstream ofcollection vessel182.
• Water/ethanol mixture188 fromcollection vessel186 may be directed toward other upstreamethanol distribution systems84. Ultimately, water/ethanol mixture190 may be applied to (e.g., poured over, sprayed onto, or deposited onto)wet solids64 byethanol distribution system84 above a firstupstream collection vessel192. Water/ethanol mixture194 fromcollection vessel192 may be directed back todistillation system42 to recapture some of the ethanol. A secondupstream collection vessel196 upstream ofcollection vessel192 may collect water/ethanol mixture198, which may also be directed back todistillation system42 to recapture some of the ethanol. A finaldownstream collection vessel200 downstream ofcollection vessel176 may collect water/ethanol mixture200, which may also be directed back todistillation system42 to recapture some of the ethanol.Collection vessel200 may also act as an evaporation stage, whereby the last remaining water/ethanol mixture202 may be removed or joined with the water/ethanol mixture178 fromcollection vessel176. A separate drying process, such asevaporation stage130 ofFIGS. 16 and 17 and/ordesolventizer40 ofFIGS. 13 and 14 may also be used downstream ofethanol wash process160.
• More or less pure ethanol may be applied to wash the wet solids at the various locations along thefilter belt162. Such concentrations, along with the flow rates of the wash fluid and the speed of thefilter belt162, may serve to control the rate of displacement of water in the wet solids by ethanol. Such factors may regulate the relative difference in ethanol content at each wash stage, as well as the ultimate ethanol content of the wet solids just before final drying.
• FIGS. 19 through 23 are cross-sectional views at various locations alongfilter belt162 ofFIGS. 18A and 18B. For example,FIG. 19 is a cross-sectional view offilter belt162 ofFIGS. 18A and 18B upstream of the location wherewet solids64 are placed ontofilter belt162 shown byarrow204 inFIGS. 18A and 18B. Although any filter belt technology may be employed,filter belt162 may have a substantially perforated or porous structure such that a liquid component ofwet solids64 onfilter belt162 may be drawn throughfilter belt162 or the flow of the mixture of water and ethanol throughfilter belt162 may be facilitated by positive differential pressure abovefilter belt162.Filter belt162 may also include acollection tray206, which may facilitate the collection of water/ethanol mixtures collected throughfilter belt162.Collection tray206 may include acollection opening208, through which water/ethanol mixtures may be collected into collection vessels.FIG. 20 is a cross-sectional view offilter belt162 ofFIGS. 18A and 18B at a location wherewet solids64 are placed ontofilter belt162 shown byarrow210 ofFIGS. 18A and 18B. A vacuum or gravity beneathfilter belt162 may draw a water/ethanol mixture212 fromwet solids64 ontocollection tray206 and intocollection vessel196, as shown byarrows214.FIG. 21 is a cross-sectional view offilter belt162 ofFIGS. 18A and 18B upstream ofethanol distribution system84 shown byarrow216. At this point onfilter belt162,wet solids64 will contain a certain concentration of ethanol.FIG. 22A is a cross-sectional view offilter belt162 ofFIGS. 18A and 18B at a location nearethanol distribution system84 shown byarrow218. At this point, ethanol is introduced intowet solids64 byethanol distribution system84, transformingwet solids64 into a mixture of liquids220 (e.g., a water/ethanol mixture) andsolids222. A vacuum or gravity beneathfilter belt162 may draw a water/ethanol mixture212 fromwet solids64 ontocollection tray206 and into a collection vessel, as shown byarrows214.FIG. 22B is a cross-sectional view offilter belt162 ofFIGS. 18A and 18B at a location nearethanol distribution system84 shown byarrow218. Apressure chamber223 may be used to create a differential pressure between the top and bottom offilter belt162. Pressure may be applied withinpressure chamber223 to facilitate washing by effectively facilitating the flow of the ethanol throughwet solids64.Wet solids64 downstream oflocation218 offilter belt162 will have a higher ethanol concentration thanwet solids64 upstream oflocation218 offilter belt162.FIG. 23 is a cross-sectional view offilter belt162 ofFIGS. 18A and 18B at a location nearcollection vessel200, as shown byarrow224.Collection vessel200 may be used as an evaporation stage.Heated gas226 may be applied towet solids64 abovefilter belt162. A vacuum or gravity beneathfilter belt162 may drawheated gas226 throughwet solids64 and anethanol vapor228 may be collected and further processed to recover ethanol and other desirable components present inethanol vapor228.
• FIG. 24 is a perspective view of another exemplary embodiment ofethanol wash process160.Wet solids64 may be placed onfilter belt162 at an upstream location withmeal18 exiting at a downstream location offilter belt162. Aninitial collection vessel196 may collect water/ethanol mixture198 without washing, which may be directed back todistillation pre-treatment process44. The first stream ofethanol174 may be applied towet solids64 abovecollection vessel176. A mixture of water and ethanol may be drawn throughfilter belt162 by gravity and/or vacuum intocollection vessel176 or the flow of the mixture of water and ethanol throughfilter belt162 and intocollection vessel176 may be facilitated by positive differential pressure abovefilter belt162. The water/ethanol mixture fromcollection vessel176 may be directed into afirst conditioning process230, which may filter and condition the water/ethanol mixture. A portion of the ethanol/water mixture may be directed to co-product processing, as shown byarrow232; filtered/conditioned ethanol fromconditioning process230 may be applied towet solids64 abovecollection vessel182.
• A mixture of water and ethanol may be drawn throughfilter belt162 by gravity and/or vacuum intocollection vessel182 or the flow of the mixture of water and ethanol throughfilter belt162 and intocollection vessel182 may be facilitated by positive differential pressure abovefilter belt162. The water/ethanol mixture fromcollection vessel182 may be directed into asecond conditioning process234, which may filter and condition the water/ethanol mixture. A portion of the ethanol/water mixture may be directed to co-product processing, as shown byarrow236; filtered/conditioned ethanol fromconditioning process234 may be applied towet solids64 above previous upstream collection vessels. Ultimately, a mixture of water and ethanol may be drawn throughfilter belt162 by gravity and/or vacuum intocollection vessel192 or the flow of the mixture of water and ethanol throughfilter belt162 and intocollection vessel192 may be facilitated by positive differential pressure abovefilter belt162. The water/ethanol mixture194 fromcollection vessel192 may be directed todistillation pre-treatment process44.
• In certain embodiments, the apparatus comprising a filter belt may include two or more such belts. For example, a first belt may be used for a first stage of washing with ethanol (or another solvent), while further filter belts may be used for subsequent stages. The material conveyed with the belts may be transferred from one belt to the other as the process progresses. Some embodiments may include intermediate equipment between filter belts, such as mixers for creating a slurry with the solvent or solvent mixture, centrifuges or other separators for performing some degree of moisture removal, and so forth. The filter belts themselves may be of any suitable type, including arrangements in which a semi-permeable belt serves as a substrate used to receive the solids component, and apparatuses with multiple layers of belts, support structures, and so forth.
• FIG. 25 is a flow chart of an exemplary embodiment ofsolids processing system34.Separation process50 may be performed to separate a liquid component shown as liquid62 (e.g., a water/ethanol mixture) from a solids component shown as wet solids64 (e.g., a certain amount of ethanol, a certain amount of water, syrup, particulate matter, and dissolved solids).Wet solids64 may then be washed with ethanol (e.g., wash process52). For example, a solvent (e.g., ethanol) may be added towet solids64, as shown byblock238. Once ethanol has been added towet solids64,wet solids64 may be separated to remove a mixture of water and ethanol from wet solids64 (e.g., separation process38).Wet solids64 will contain a higher concentration of ethanol than beforewash process52 andseparation process38.Wet solids64 may then be desolventized to remove remaining liquids fromwet solids64 to produce meal18 (e.g., desolventizing process40). In each ofseparation process38 anddesolventizing process40, liquid and vapor may be captured, as shown byblock240. The liquid and vapor may be distilled and used as a source of ethanol inwash process52, as shown byblock242. The liquid and vapor may be re-used bywash process52.
• FIG. 26 is a flow chart of an exemplary embodiment of multiplesolids processing system34 stages.Separation process50 may be performed to separate a liquid component shown as comprising liquid62 (e.g., a water/ethanol mixture) from a solids component shown as comprising wet solids64 (e.g., a certain amount of ethanol, a certain amount of water, syrup, particulate matter, and dissolved solids).Wet solids64 may then be washed with ethanol (e.g., wash process52). Once ethanol has been added towet solids64,wet solids64 may be separated to remove a mixture of water and ethanol from wet solids64 (e.g., separation process38).Wet solids64 will contain a higher concentration of ethanol than beforewash process52 andseparation process38. Subsequent ethanol wash stages may be used to further increase the ethanol concentration ofwet solids64 beforedesolventizing process40. For example,wet solids64 may be washed again with concentrated ethanol (e.g., wash process52). For example, a solvent (e.g., ethanol) may again be added towet solids64, as shown byblock238. Once ethanol has again been added towet solids64,wet solids64 may be separated again to remove a mixture of water and ethanol from wet solids64 (e.g., separation process38).Wet solids64 may contain an even higher concentration of ethanol than before ethanol wash processes52 and separation processes38.Wet solids64 may then be desolventized to remove remaining liquids fromwet solids64 to produce meal18 (e.g., desolventizing process40). In each of separation processes38 anddesolventizing process40, liquid and vapor may be captured, as shown byblocks240. The liquid and vapor may be re-distilled and used in other processes internal and/or external to biorefinery10, as shown byblock242. The liquid and vapor may be re-used by previous wash processes52.
• Various processes upstream ofsolids processing system34 may also lead to significant tangible benefits. For example,FIG. 27 is a process flow diagram of an exemplary embodiment offractionation process78. Exemplary processes are described in U.S. Patent Application Publication No. 2005/0233030, U.S. Patent Application Publication No. 2007/0037267, U.S. Patent Application Publication No. 2007/0178567, and U.S. Patent Application Publication No. 2007/0202214, each of which is incorporated by reference.Corn12 may initially be processed intoindividual corn kernels244, which may be fractionated withinfractionation process78. Eachcorn kernel244 may be comprised ofendosperm246,fiber248,germ250, and atip cap252.Endosperm246 comprises most of the starches and proteins available incorn kernel244 and is used infermentation process28 to generateethanol16.Endosperm246 represents thefermentable solids58 ofcorn kernel244; germ and fiber represent thenon-fermentable solids56 ofcorn kernel244, which may be withheld fromfermentation process28.Endosperm246 comprises approximately 80-85% ofcorn kernel244 by mass,germ250 comprises approximately 10-15% ofcorn kernel244 by mass, andfiber248 comprises approximately 5-10% ofcorn kernel244 by mass.
• Fractionation process78 preparescorn kernels244 for saccharification and fermentation insaccharification process26 andfermentation process28.Fractionation process78 reducescorn kernel244 to make starches and proteins withincorn kernel244 more readily available for saccharification and fermentation. For example,corn kernel244 may first be fractionated into its component parts, such asgerm250,fiber248, andendosperm246. Tempered whole corn may be fed into aprimary separation stage254, which substantially separatescorn kernel244 into components (e.g., fractions) ofendosperm germ250,fiber248, andendosperm246.Primary separation stage254 may also separate out fiber248 (e.g., bran) and flour (e.g., comprising a fine powder of endosperm246) and may direct the remaining components ofcorn kernel244 into asecondary separation stage256.Fiber248 fromprimary separation stage254 may be processed through a secondary starch recovery process. The secondary starch recovery process may include a milling stage, a separation stage, and a mechanical fiber dusting stage. The milling stage may utilize a pin mill, a hammer mill, a roller mill, or other suitable mill technology.
• Secondary separation stage256 may further removegerm250 fromendosperm246.Germ250 fromsecondary separation stage256 may pass through a secondary refining (or purification) process, which may include a milling stage and a separation stage. The milling stage may utilize a roller mill. Grits (e.g., endosperm246) from the secondary refining process may be passed to a mechanism for reducing their size, such as a hammer mill, prior to fermentation.
• Fractionatingcorn kernel244 to separate endosperm246 (e.g., fermentable solids) fromgerm250 and fiber248 (e.g., non-fermentable solids) may provide several benefits to processes downstream offractionation process78. For example, using primarily endosperm246 insaccharification process26 may enhance the efficiency ofsaccharification process26 becausenon-fermentable solids56 are generally not involved insaccharification process26. The fact that the fermentation slurry fromsaccharification process26 includes primarily endosperm246, water, and enzymes may also lead tofermentation process28 being more efficient becausenon-fermentable solids56 are generally not involved infermentation process28.
• By fractionatingcorn kernel244 prior to fermentation, the levels of proteins (e.g., zein) may be increased. For example, removinggerm250 andfiber248 fractions prior tofermentation process28 may concentrate proteins in the fermentation slurry delivered tofermentation process28. Proteins are generally isolated inendosperm246 ofcorn kernel244 and fractionation of protein-enrichedendosperm246 results in concentration of proteins in residuals fromfermentation process28.
• Endosperm246 fromsecondary separation stage256 may be directed into a milling process, whereendosperm246 may be milled and reduced in particle size to prepare the ground endosperm forsaccharification process26 andfermentation process28.Endosperm246 may be reduced using any suitable method, including grinding, to make starches withinendosperm246 more readily available forsaccharification process26 andfermentation process28. The specific equipment used to grindendosperm246 may include, for example, a ball mill, a roller mill, a hammer mill, or any other type of mill capable of grindingendosperm246 for the purpose of particle size reduction. The use of emulsion technology, sonic pulsation, rotary pulsation, and other particle size reduction methods may be utilized to increase the surface area ofendosperm246, while also raising the effectiveness of flowing the liquefied media (e.g., decreased viscosity). Theground endosperm246 may be referred to as being or including “raw starch.” Grindingendosperm246 exposes more surface area ofendosperm246 and may facilitatesaccharification process26 andfermentation process28.
• Ground endosperm246 fromfractionation process78 may be directed intosaccharification process26, in which starches withinground endosperm246 may be converted into sugars that may be fermented infermentation process28.FIG. 28 is a block flow diagram of an exemplary embodiment ofsaccharification process26.Endosperm246 may be combined in areaction tank258 with asaccharifying enzyme composition260,water262, andheat264 to facilitate the conversion. Thesaccharifying enzyme composition260 may include an amylase, such as an alpha amylase (e.g., an acid fungal amylase). Thesaccharifying enzyme composition260 may also include glucoamylase. Thesaccharifying enzyme composition260 may also include acid fungal amylase for hydrolyzing raw starch withinground endosperm246.
• The term “saccharifying” refers to the process of converting starches withinground endosperm246 into smaller polysaccharides and eventually to monosaccharides, such as glucose. Conventional saccharification methods use liquefaction of gelatinized starch to create soluble dextrinized substrates that hydrolyze into glucose.Saccharification process26 may be conducted without cooking. The phrase “without cooking” generally refers to a process for converting starch to sugars without heat treatment for gelatinization and dextrinization of starches withinground endosperm246. “Without cooking” (e.g., a “raw starch” process) refers to maintaining a temperature below starch gelatinization temperatures ofground endosperm246 such that saccharification occurs directly from the raw native insoluble starch to soluble glucose, while bypassing conventional starch gelatinization conditions. Starch gelatinization temperatures are typically in a range of 57-93° C., depending on the starch source and polymer type.Saccharification process26 may be conducted in a temperature range of approximately 25-40° C. Exemplary processes are described in U.S. Patent Application Publication No. 2004/0234649, U.S. Patent Application Publication No. 2005/0233030, U.S. Patent Application Publication No. 2005/0239181, U.S. Patent Application Publication No. 2007/0037267, U.S. Patent Application Publication No. 2007/0178567, U.S. Patent Application Publication No. 2007/0196907, and U.S. Patent Application Publication No. 2007/0202214, each of which is incorporated by reference.
• Saccharification process26 may include mixingground endosperm246 with a liquid (e.g., water262), which may form a slurry or suspension, and adding asaccharifying enzyme composition260 to the slurry. The addition of thesaccharifying enzyme composition260 may occur before or during mixing ofground endosperm246 withwater262.Saccharification process26 may convert raw or native starch to sugars at a faster rate as compared to conventional saccharification methods that utilize cooking. The percentage ofground endosperm246 towater262 may be higher as compared to conventional saccharification methods that utilize cooking because, unlike conventional processes, saccharifyingground endosperm246 without cooking does not include gelatinization, which increases viscosity.
• Saccharification process26 may utilize any enzyme sources suitable for saccharifying starches withinground endosperm246 to produce fermentable sugars without cooking. Thesaccharifying enzyme composition260 may include an amylase, such as an alpha amylase (e.g., an acid fungal amylase) or a glucoamylase. The initial pH ofsaccharification process26 may be adjusted by the addition of, for example, ammonia, sulfuric acid, phosphoric acid, or process waters (e.g., stillage or backset, evaporator condensate or distillate, side stripper bottoms).
• The ability ofsaccharification process26 to convert starches withinground endosperm246 to produce fermentable sugars without cookingground endosperm246 may provide several tangible benefits. For example,meal18 that is ultimately produced bybiorefinery10 may generally be of higher quality becauseground endosperm246 is not cooked.Meal18 produced bybiorefinery10 may include elevated levels of protein as compared toconventional DDG54.Meal18 produced bybiorefinery10 may also include elevated levels of B vitamins, vitamin C, vitamin E, folic acid, amino acids (e.g., lysine), and/or vitamin A as compared toconventional DDG54.Meal18 produced bybiorefinery10 may also have improved physical characteristics, such as decreased caking or compaction and increased ability to flow.
• Fermentation slurry266 fromsaccharification process26 may be directed intofermentation process28, in which the sugars within thefermentation slurry266 are fermented to produceethanol16.FIG. 29 is a block flow diagram of an exemplary embodiment offermentation process28. Exemplary processes are described in U.S. Patent Application Publication No. 2004/0234649, U.S. Patent Application Publication No. 2005/0233030, U.S. Patent Application Publication No. 2005/0239181, U.S. Patent Application Publication No. 2007/0037267, U.S. Patent Application Publication No. 2007/0178567, U.S. Patent Application Publication No. 2007/0196907, and U.S. Patent Application Publication No. 2007/0202214, each of which is incorporated by reference.Fermentation slurry266 may be combined in fermentation tank(s)268 withenzymes270 andyeast272 to facilitate fermentation.Fermentation process28 may be facilitated by mixing theyeast272 withfermentation slurry266 under conditions suitable for growth of theyeast272 and production ofethanol16.Fermentation slurry266 contains sugars that have been converted from starches without cooking.
• Any of a variety ofyeasts272 may be utilized as the yeast starter infermentation process28.Yeast272 may be selected to provide rapid growth and fermentation rates in the presence of high temperature and high ethanol levels. The amount of yeast starter utilized is selected to effectively produce a commercially significant quantity ofethanol16 within a suitable time from (e.g., less than 72 or 144 hours).Yeast272 may be added tofermentation slurry266 by any of a variety of methods known for addingyeast272 to fermentation processes. Yeast starter may be added as a dry batch, or by conditioning/propagating. Yeast starter may also be added as a single inoculation.
• Fermentation process28 may be conducted as either a continuous process or a batch process. As a continuous process,fermentation slurry266 fromsaccharification process26 may be moved (e.g., pumped) through a series of vessels (e.g., tanks) to provide a sufficient duration forfermentation process28.Fermentation process28 may also include multiple stages of vessels. For example,fermentation slurry266 fromsaccharification process26 may be fed into the top of a first vessel stage, partially fermented slurry drawn out of the bottom of the first vessel stage may be fed into the top of a second vessel stage, and partially fermented slurry drawn out of the bottom of the second vessel stage may be fed into the top of a third vessel stage. As a batch process,fermentation slurry266 may be directed into a vessel, where the fermentation cycle may be completed before the vessel is emptied.
• Output fromfermentation process28 may include the fermentation product shown asbeer32.Ethanol16 may be recovered from liquids inbeer32,meal18 may be recovered from solids inbeer32, and other various by-products (e.g., proteins and corn syrup) may be separated frombeer32.Fermentation process28 may generate a relatively large amount of carbon dioxide (CO₂) and other gases. A system may be installed atbiorefinery10 to capture, re-use, and/or otherwise dispose (e.g., via sequestration) of the gases.
• Fermentation product32 (e.g., beer) may be separated byseparation process50 into a liquid component (e.g., liquid62) and a solids component (e.g., wet solids64).FIG. 30 illustrates exemplary embodiments ofseparation process50.Liquid62 may be directed intodistillation system42, whereethanol16 may be produced. By directing primarily liquid62 todistillation system42, equipment ofdistillation system42 may be less susceptible to fouling, which is usually caused by solids present when fermented beer is distilled directly, such as in conventional methods. Becauseliquid62 has substantially fewer solids, occurrences of fouling may be substantially reduced. With a reduced susceptibility to fouling, complicated anti-fouling provisions may be unnecessary, reducing the complexity and cost ofdistillation system42. Becauseliquid62 is substantially free of solids components, heat energy applied todistillation system42 may only have to heat those minimal solids dissolved inliquid62, reducing heat energy requirements ofdistillation system42 compared to conventional distillation systems, which must heat both the solids and liquid components of fermented beer.
• Wet solids64 may be directed intosolids processing system34, where ethanol (or other solvents) may be added towet solids64 to decrease the boiling point, heat capacity, and enthalpy (heat) of vaporization ofwet solids64. The ethanol concentration ofwet solids64 fromseparation process50 may generally be determined byfermentation process28, and may typically fall within a range of 10-20% by volume, although ethanol concentrations above and below this range may also be used. A substantial portion of water will be removed frombeer32 asliquid62 and, as such, the boiling point, heat capacity, and enthalpy (heat) of vaporization ofwet solids64 may be reduced downstream ofseparation process50 as compared tobeer32 upstream ofseparation process50. The amount of energy required to dry/desolventize wet solids64 (i.e., having a lower boiling point, heat capacity, and enthalpy (heat) of vaporization) may be substantially reduced compared to conventional deliquification/drying systems, which must deliquify and dry stillage containing higher concentrations of water (i.e., having a higher boiling point, heat capacity, and enthalpy (heat) of vaporization).
• By separating liquid components (e.g., liquid62) from the solids components (e.g., wet solids64) ofbeer32 prior todistillation system42, the favorable physical characteristics of ethanol may be exploited (particularly the low boiling point, low specific heat, and low enthalpy (heat) of vaporization of ethanol) to evaporate liquid matter fromwet solids64, producingmeal18. Rather than drying stillage that has been processed in a distillation system and contains little to no ethanol, ethanol-containingwet solids64 may be dried using lower amounts of energy as compared to conventional methods.Separation process50 may be performed by any suitable separation means including, but not limited to, a disk-type centrifuge274, adecanter centrifuge276, ahydroclone278, asedimentation tank280, or afilter press282. Indeed, any type of separator capable of separating liquid62 fromwet solids64 may be used.
• Meal18 produced bybiorefinery10 may also be reconstituted into feed at a desired composition to differentiate the product for various markets. For example, some protein and any extracted biochemicals or other bioproducts may be re-applied to the resulting meal to constitute the desired end product. Levels of protein and other amino acids could be selectively adjusted. For example, proteins, fats, syrup, oils, lutein, lysine, zein, and other bioproducts and biochemicals may be selectively combined with the meal. According to preferred embodiment, processing of the meal may take place at temperatures that avoid degradation of the meal itself. The use of such reduced temperatures at all stages of processing (through the plant) results in a meal that is of a different quality than conventional DDG (i.e., resulting from a process employing “cooked” liquefaction). For example, maintaining the processing temperatures below about 150° C. is believed to produce a product that is quite distinct from conventionally processed DDG, and even lower temperatures, on the order of 100° C. (or even lower, at 93° C., 180° F., or 130° F.) are particularly helpful in creating a unique meal.
• Depending upon the processing, the meal may be referred to as “corn meal” (particularly when corn is the feedstock), “distillers meal”, “distillers dried meal”, “dried distillers meal”, “protein-containing meal”, and “corn distillers meal”, among others. When the solids component is subject to the distillation process, the resulting product may be different still, somewhat more akin to conventional DDG, although certain benefits of the processing are nevertheless realized, such as the reduction in energy utilization in the biorefinery.
• The meal may also be further transformed for particular product categories and markets. For example, the meal may be mechanically pressed or extruded into pellets configured for packaging, transportation, durability, and digestibility. Such processing may be well suited for producing animal feeds. Within this category of product, a number of varieties may be formulated including different ingredients, protein qualities, additives, sizes, and configurations.
• While only certain features and embodiments of the invention have been illustrated and described, many modifications and changes may occur to those skilled in the art (e.g., variations in sizes, dimensions, structures, shapes and proportions of the various elements, values of parameters (e.g., temperatures, pressures, etc.), mounting arrangements, use of materials, colors, orientations, etc.) without materially departing from the novel teachings and advantages of the subject matter recited in the claims. The order or sequence of any process or method steps may be varied or re-sequenced according to alternative embodiments. It is, therefore, to be understood that the appended claims are intended to cover all such modifications and changes as fall within the true spirit of the invention. Furthermore, in an effort to provide a concise description of the exemplary embodiments, all features of an actual implementation may not have been described (i.e., those unrelated to the presently contemplated best mode of carrying out the invention, or those unrelated to enabling the claimed invention). It should be appreciated that in the development of any such actual implementation, as in any engineering or design project, numerous implementation specific decisions may be made. Such a development effort might be complex and time consuming, but would nevertheless be a routine undertaking of design, fabrication, and manufacture for those of ordinary skill having the benefit of this disclosure, without undue experimentation.

Claims (20)

1. A method for processing a fermentation product of a fermentation process in a biorefinery that performs distillation of ethanol, the fermentation product comprising a liquid component and a solids component, the method comprising the steps of:

(a) separating the liquid component from the solids component prior to distillation of the liquid component;

(b) applying a solvent to the solids component to alter the composition of the solids component; and

(c) drying the solids component, wherein the solids component is not exposed to heat added to the liquid phase product during the distillation process.

2. The method ofclaim 1 wherein the solids component comprises particulate matter, the particulate matter being separated from the liquid component prior to distillation of the liquid component.

3. The method ofclaim 1 wherein the solids component is separated from the liquid component by centrifuging.

4. The method ofclaim 1 wherein the solids component comprises proteins derived from corn.

5. The method ofclaim 1 wherein the solvent comprises hexane.

6. The method ofclaim 1 wherein the solvent comprises ethanol.

7. The method ofclaim 6 wherein the solids component comprises a moisture content comprising an ethanol component and a water component, and wherein the composition of the solids component is altered by decreasing the water component.

8. The method ofclaim 7 wherein the composition of the solids component is altered by increasing the ethanol component.

9. The method ofclaim 7 comprising collecting liquid and/or gas from the solids component, and increasing ethanol content of the liquid and/or gas collected from the solids component to obtain a higher ethanol-content liquid, and wherein the higher ethanol-content liquid is applied to the solids component.

10. The method ofclaim 9 wherein the liquid and/or gas is collected from the solids component by application of at least one of a positive pressure, a vacuum pressure, and heat to the solids component.

11. The method ofclaim 7 comprising performing step (b) at least twice to drive the components of the moisture content towards the water/ethanol azeotropic point.

12. The method ofclaim 11 wherein performance of step (b) is stopped, and the solids component is dried prior to reaching the water/ethanol azeotropic point.

13. The method ofclaim 7 comprising performing step (b) up to or beyond the water/ethanol azeotropic point.

14. The method ofclaim 13 comprising performing step (b) until the moisture content is substantially entirely ethanol.

15. The method ofclaim 7 wherein the ethanol is produced by distillation of the liquid component of the fermentation products.

16. The method ofclaim 1 comprising removing a portion of the solids component bioproduct from the solids component prior to drying.

17. The method ofclaim 1 wherein the solids component comprises meal.

18. The method ofclaim 1 wherein in steps (b) and (c) the average temperature of the solids component is maintained below a temperature that will result in degradation of the solids component.

19. The method ofclaim 18 wherein in steps (b) and (c) the average temperature of the wet solid fermentation product is maintained below 150° C.

20. The method ofclaim 19 wherein in step (b) and (c) the average temperature of the wet solid fermentation product is maintained below 100° C.

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