Abstract:
A process of producing ethanol from whole stillage, includes obtaining a supply of whole stillage from an ethanol production facility after ethanol has been extracted therefrom; pre-treating the whole stillage to convert hemicellulose portions of the whole stillage into sugars; adding enzymes to the whole stillage to convert cellulose portions of the whole stillage to sugars; fermenting the whole stillage to create a beer mixture; and distilling the beer mixture to separate ethanol therefrom. The pre-treating step may include adding acid to the whole stillage to decrease its pH level; heating and pressurizing the whole stillage; holding the whole stillage under pressure and heat for a dwell time; removing pressure from the whole stillage to cause flashing; and cooling the whole stillage before the enzymes are added.

Description:
BACKGROUND 
     The present invention relates to ethanol production processes and systems. More particularly, the invention relates to processes and systems for producing additional ethanol from byproducts of an ethanol production facility. 
     The production of ethanol for use as a gasoline additive or a straight liquid fuel continues to increase as petroleum costs rise and environmental concerns become more pronounced. Ethanol may be produced in a dry milling process by grinding corn or other grains into a powder or flour and then liquefying, fermenting, and distilling it to produce alcohol, carbon dioxide, and byproducts. Conventional ethanol production processes produce ethanol from the starch portion of the grain but do not produce any usable ethanol from the fiber portions of the grain, which are primarily found in the byproducts. Instead, the byproducts are typically dehydrated and used as animal feed. Moreover, because the byproducts are high in fiber content, the resultant animal feed is difficult for monogastrics to digest. 
     SUMMARY 
     The present invention solves the above-described problems and provides a distinct advance in the art of ethanol production processes. More particularly, the present invention provides processes and systems for producing additional ethanol from byproducts of an ethanol production facility. The processes and systems of the present invention also improve the nutritional content and value of the animal feed produced from the byproducts of the process. 
     An embodiment of the invention is a process of producing additional ethanol from whole stillage that comprises obtaining a supply of whole stillage from an ethanol production facility after ethanol has been extracted therefrom; pre-treating the whole stillage to convert hemicellulose portions of the whole stillage into sugars; adding enzymes to the whole stillage to convert cellulose portions of the whole stillage to sugars; fermenting the whole stillage to create a beer mixture; and distilling the beer mixture to separate ethanol therefrom. 
     The pre-treating steps may comprise adding acid to the whole stillage to decrease its pH level; heating and pressurizing the whole stillage; holding the whole stillage under pressure and heat for a dwell time; removing pressure from the whole stillage to cause flashing; and cooling the whole stillage before the enzymes are added. 
     The process may further comprise removing the whole stillage byproducts of the distilling step, separating the solids from the whole stillage, and drying the solids to form dried distillers grains. 
     The processes of the present invention advantageously produce additional ethanol from the byproducts of an ethanol production facility rather than just using the byproducts as animal feed. The processes of the present invention also result in a final byproduct that is higher in protein and lower in fiber and thus easier for monogastrics to digest. 
     This summary is provided to introduce a selection of concepts in a simplified form that are further described in the detailed description below. This summary is not intended to identify key features or essential features of the claimed subject matter, nor is it intended to be used to limit the scope of the claimed subject matter. Other aspects and advantages of the present invention will be apparent from the following detailed description of the embodiments and the accompanying drawing figures. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWING FIGURES 
       Embodiments of the present invention are described in detail below with reference to the attached drawing figures, wherein: 
         FIG. 1  is a schematic diagram of a prior art ethanol production facility. 
         FIG. 2  is a flow diagram depicting a process of producing additional ethanol from byproducts of the ethanol production facility of  FIG. 1 . 
         FIG. 3  is a schematic diagram of a system that may be used to implement the process of  FIG. 2 . 
         FIG. 4  is a schematic diagram depicting parts of the system of  FIG. 3  in more detail. 
     
    
    
     The drawing figures do not limit the present invention to the specific embodiments disclosed and described herein. The drawings are not necessarily to scale, emphasis instead being placed upon clearly illustrating the principles of the invention. 
     DETAILED DESCRIPTION 
     The following detailed description of embodiments of the invention references the accompanying drawings. The embodiments are intended to describe aspects of the invention in sufficient detail to enable those skilled in the art to practice the invention. Other embodiments can be utilized and changes can be made without departing from the scope of the claims. The following detailed description is, therefore, not to be taken in a limiting sense. The scope of the present invention is defined only by the appended claims, along with the full scope of equivalents to which such claims are entitled. 
     In this description, references to “one embodiment”, “an embodiment”, or “embodiments” mean that the feature or features being referred to are included in at least one embodiment of the technology. Separate references to “one embodiment”, “an embodiment”, or “embodiments” in this description do not necessarily refer to the same embodiment and are also not mutually exclusive unless so stated and/or except as will be readily apparent to those skilled in the art from the description. For example, a feature, structure, act, etc. described in one embodiment may also be included in other embodiments, but is not necessarily included. Thus, the present technology can include a variety of combinations and/or integrations of the embodiments described herein. 
       FIG. 1  is a schematic illustration of the primary components of a conventional ethanol production facility  10 . The facility  10  is shown for purposes of describing aspects of the present invention and can be replaced, in whole or part, by other ethanol production facilities or components without departing from the scope of the present invention. Other ethanol production facilities and processes are described and illustrated in U.S. Pat. Nos. 6,660,506 and 7,527,941 and U.S. Patent Application No. 2004/0023349, all of which are incorporated in their entireties into the present application by reference. 
     Returning to  FIG. 1 , grain  12  such as corn is first delivered to the ethanol production facility  10  by railcars, trucks, or other means. The grain may also be barley, rye, wheat, oats, sorghum, milo, canola, or soybeans. A sufficient supply of the grain to operate the production facility may be stored in one or more grain elevators  14 , bins, or other storage vessels. 
     Ethanol production begins by milling or otherwise processing the grain into a fine powder or flour by a hammer mill or other milling machine  16 . The milled grain is then mixed with water and enzymes in one or more slurry tanks  18  and held in these tanks or liquefaction tanks  20  for a sufficient amount of time to enable the enzymes to begin to breakdown the starch in the mixture into fermentable sugars. 
     The mixture is then passed to one or more fermentation tanks  22  where yeast is added. The fermenting process creates a mixture that contains alcohol, solids, and liquids and that is commonly referred to as “beer.” 
     The beer is then transferred to one or more distillation columns  24 , also often referred to as “beer strippers”, which separate the alcohol from the solids and the liquids. The alcohol exits the top of these columns  24  and is transferred to one or more rectifiers  26  to remove moisture from the alcohol. The alcohol may also be passed to one or more molecular sieves  28  to remove even more moisture. The final alcohol is then transferred to one or more ethanol holding tanks  30  where it may be denatured before use as a fuel or fuel additive. 
     The liquid and solid mixture that remains in the distillation columns  24  after the alcohol has been removed is commonly referred to as “whole stillage” or simply “stillage”. The whole stillage falls to the bottom of the distillation columns  24  and is then transferred to one or more whole stillage holding tanks  32 . The whole stillage may then be passed through one or more centrifuges  34  which separate it into a stream of “thin stillage” and a stream of “wet distillers grain”. The thin stillage is mostly liquid but may also contain a small amount of solid materials. The thin stillage may be held in one or more tanks and is typically returned to the slurry tanks  18  or some other part of the ethanol production facility  10  that requires water. Some or all of the thin stillage may also be transferred to one or more evaporators  38  to produce evaporated thin stillage, which is commonly referred to as “syrup”. The syrup may be held in one or more tanks  40  and be used as an animal feed additive. 
     The wet distillers grain, which is often referred to as “wetcake”, may be held in storage facilities  42 ,  43  and sold as a livestock feed. Some of the wet distillers grain may also be transferred to one or more dryers  44  to remove liquid therefrom to produce dried distillers grain, which may also be stored in one or more tanks  46  and used as livestock feed. In addition, some of the syrup can be dried with the wet distillers grains to produce dried distillers grains with solubles (DDGS). 
     The above described ethanol production facility  10  does not attempt to produce ethanol from the whole stillage removed from the distillation columns  24 . Instead, the whole stillage is just a byproduct of the ethanol production process and is either used as livestock feed, make-up water, and/or is discarded. The processes of the present invention produce additional useable ethanol from the fiber portions of the whole stillage and any leftover starch after the main ethanol extraction is complete. The processes of the present invention also increase the protein content of the final byproducts, thus improving their nutrient value when used as livestock feed. 
     Since whole stillage is the byproduct of the fermentation of corn or other cereal grain, it contains a sizable fraction of fiber. All fiber is made up of hemicellulose, cellulose, and lignin. Lignin is a binder and is not fermentable into ethanol. Cellulose consists of glucose molecules, the same as in starch, but the linkages in cellulose make it more difficult to break down into individual glucose molecules than in starch. Hemicellulose contains a mixture of sugars and is generally easier to breakdown than cellulose. The processes of the present invention include steps for converting both the hemicellulose and cellulose portions of the whole stillage into sugars that may be fermented into ethanol. 
     The flow chart of  FIG. 2  shows the steps in a process  200  for producing ethanol from whole stillage in accordance with embodiments of the invention. The functions noted in the various blocks may occur out of the order depicted in  FIG. 2 . For example, two blocks shown in succession in  FIG. 2  may in fact be performed substantially concurrently, or the blocks may sometimes be performed in the reverse order depending upon the functionality involved. 
     Moreover, other embodiments of the process  200  may include additional steps not shown in  FIG. 2  and/or may omit some of the steps shown in  FIG. 2 . The schematic diagrams of  FIGS. 3 and 4  depict equipment that may be used to implement the process  200  and other embodiments of the process. The illustrated equipment may be replaced with other equipment without departing from the scope of the invention. 
     The process  200  starts by obtaining whole stillage as depicted in block  202 . The whole stillage may be obtained from the distillation columns  24  or the whole stillage tanks  32  shown in  FIG. 1  or elsewhere in the ethanol production facility  10  and may be held in one or more tanks  48  as depicted in  FIG. 3 . At this point in the process, the whole stillage has already been subjected to: 1) a long soak time in the liquefaction tanks  20  and fermenting tanks  22 , 2) heating in the distillation steps, and 3) chemical reactions from the chemicals added throughout the ethanol production process. These steps help to facilitate the breakdown of the fiber in the whole stillage. The whole stillage is further treated in the process  200  of the present invention to continue the breakdown of the fiber for extracting additional ethanol. 
     The whole stillage may also be concentrated prior to further processing. One way of concentrating the fiber in the whole stillage is to employ a separation step prior to pretreatment and fermentation. This would entail processing a portion of the whole stillage through a machine such as press or a centrifuge to separate the supernatant (thin stillage) and the solids portion (wet distiller&#39;s grains) then reintroduce the wet distiller&#39;s grains into the unprocessed portion of the whole stillage. This has the tendency to reduce the volume of liquid thereby reducing chemical and energy costs, as well as reducing the required fermentation volume. The vast majority of the fiber is contained in the solids within the wet distiller&#39;s grain and therefore the final product yield is virtually unchanged. The thin stillage from this process would either be used as recycle in the facility  10 , or evaporated to form syrup. This syrup could either be sold separately, or dried in with the DDGS from the whole stillage fermentation process. 
     The whole stillage is then subjected to a pre-treatment process as depicted in block  204  of  FIG. 2 . In one embodiment, the pre-treatment process may be implemented with the equipment  50  generally illustrated in  FIG. 3  and shown in more detail in  FIG. 4 . Referring to  FIG. 4 , the whole stillage is first transferred to a surge tank  52  or other vessel. Sulfuric acid or another acid is then added to the surge tank  52  to decrease the pH level of the whole stillage to promote dilute acid hydrolysis. Sufficient acid is supplied to decrease the pH of the whole stillage to 1.0 to 4.5 and preferably to 1.8. Some evidence suggests that lower pH values aid in oil recovery. 
     The pre-treatment portion of the process  200  continues by heating and pressurizing the whole stillage mixture. In one embodiment, the heating is performed in a hydro-heater  54  shown in  FIG. 4  where high pressure steam is injected into the mixture to increase its temperature to 215° F. to 260° F., with the best results at 260° F. Higher temperatures up to 300° F. may be even more beneficial, but temperatures above 260° F. may be difficult to achieve economically. Heating by steam injection is beneficial because it results in cavitation of the mixture which further disrupts the structure of the fiber in the whole stillage which aids in subsequent processing of the whole stillage. 
     During the heating process, the whole stillage is also pressurized in the hydro-heater  54 , a cook tube  56 , or other vessel to a pressure in excess of the vapor pressure to prevent the mixture from boiling. The heated mixture is then held at the elevated temperature and pressure for 2-20 minutes. Applicant has discovered that retention times beyond 20 minutes don&#39;t provide substantial additional benefits. 
     Another method of heating the whole stillage is to use a heat exchanger where the steam, or other heating medium, does not come in contact with the whole stillage. This heating method produces very similar results to steam injection, but seems to require more residence time and is difficult to perform without fouling of the heat exchanger. This heating method also does not result in any cavitation of the whole stillage. 
     The pre-treatment portion of the process  200  continues by transferring the whole stillage mixture to a flash tank  58  where its pressure is rapidly dropped, causing the mixture to boil and flash off steam. This rapid boiling causes further rupturing of the fiber structure of the whole stillage to further expose the cellulose and hemicellulose of the whole stillage. The steam from the flash tank  58  may be captured in a flash condensor  60  and used as make-up water in the slurry tanks or elsewhere in the ethanol production facility  10  as depicted in  FIG. 4 . 
     Afterward, the whole stillage is cooled in one or more heat exchanges  62  to a temperature appropriate for the subsequent enzymatic hydrolysis process. Pentose sugars, such as xylose, may be produced from the hemicellulose by this portion of the method. Generally 75 to 100% of the final hemicellulose breakdown is achieved during the pre-treatment portion of the process  200  process. The enzymatic process that follows releases a bit more sugars from the hemicellulose. 
     The mixture is then subjected to an enzymatic hydrolysis process as depicted in block  212  of  FIG. 2 . In one embodiment, the enzymatic hydrolysis process may be implemented with the equipment  64  shown generally in  FIG. 3  and shown in more detail in  FIG. 4 . The enzymatic hydrolysis primarily converts the cellulose portions of the fiber to usable sugars but also converts some of the hemicellulose to sugars. The whole stillage is first transferred to one or more tanks  66  shown in  FIG. 4  where enzymes are added. Ammonia may also be added to increase the pH to a level conducive to the activity of the enzymes. In one embodiment, the whole stillage is held at a temp of 150° F.-160° F., with a preferred temp of 158° F. and a pH level of approximately 4.5. The whole stillage is then cooled in one or more heat exchangers  68  and, if necessary, pH corrected to a level of 4.8 to avoid denaturing the enzymes. Hexose sugars, such as glucose, may be produced from the cellulose by the enzymatic hydrolysis. 
     Depending on the nature of the enzyme used, the enzymatic hydrolysis can either be carried out during the fermentation steps described below where the temperature is held at a point that is conducive to fermentation, or as a separate step as described above in a separate tank where the temperature is held higher so the activity level of the enzymes is greater. The choice of a separate step or a simultaneous enzymatic and fermentation step depends on the activity of the enzymes used and on viscosity requirements. The whole stillage can become very viscous during the pretreatment steps, especially when cooled to fermentation temperature. It may therefore be necessary to cool the whole stillage to an intermediate temperature where the viscosity is lower and then add enzymes to breakdown the mixture further. The whole stillage can then be cooled to fermentation temperatures without excessive viscosity issues. 
     Different enzymes may be used to hydrolyze the hemicellulose and cellulose portions of the fiber. Hemicellulose composition varies from one fiber source to another, but all contain a variety of sugars with xylose generally being the most abundant. In corn fiber, xylose and arabinose are present in the highest concentrations. Mannose, glucose and other sugars are also present, but to a much smaller degree. 
     Hemicellulose can be broken down with enzymes that are currently commercially available, and by combining appropriate chemical and physical pretreatment methods the hydrolysis is quite effective. The enzymes used to hydrolyze hemicellulose are somewhat generically termed ‘xylanases.’ Xylanases contain several different enzymes that hydrolyze specific bonds in hemicellulose, but due to the fact that hemicellulose contains varying amounts of each of the sugars, varying amounts of each of the activities is required for an optimized hydrolyzation of all of the components. Xylanases are generally most effective at temperatures in the range of 155° F. to 185° F., with reduced activity at fermentation temperatures of 90° F. to 95° F. 
     Cellulose is more difficult to convert to sugars because of it crystalline structure. The glucose is linked to form chains, with cross linking between the chains. This cross linking of the chains creates much of the difficulty in hydrolyzing cellulose; in effect it creates a crystal structure with a relatively small surface area to volume ratio. The most effective way of hydrolyzing cellulose is to pretreat it as described above to rupture the fiber structure thereby creating more surface area. The cellulases are then introduced to continue the breakdown of the cellulose to glucose. 
     The enzymatic hydrolysis of the pretreated cellulose is usually accomplished in three steps. The first step is to cleave long chains of glucose from the cellulose using a whole cellulase, which randomly hydrolyzes links in the cellulose. Since this action is random in its attack it can create anything from a single glucose unit to a chain that is few thousand glucose units long. This is generally the cheapest portion of a cellulase formulation, but since it is random it does not produce free glucose units at a reliable rate. It does however create more chains for the next enzymes to act upon. 
     The second step is carried out by cellobiohydrolase. This enzyme hydrolyzes two units of glucose, termed cellobiose, from the end of a cellulose chain. Since this is not a random attack the rate of production of cellobiose is reliable. 
     The third enzyme used is beta-glucosidase. This enzyme acts on the end of a cellulose chain to hydrolyze single units of glucose. The chain can be of any length from two units to thousands of units long. 
     The best way to cost effectively hydrolyze cellulose is to balance the use of each one of these enzymes. For the cellobiohydrolase and beta-glucosidase to be effective they need ends to work on. The production of more ends is the job of the whole cellulase. 
     To further complicate matters, the temperature optimum for each of these enzymes is slightly different. The whole cellulase generally operates best at temperatures from 150° F. to 185° F., while beta-glucosidase operates in temperatures below 130° F., and is denatured at the optimum temperatures of the whole cellulase. 
     In light of this, it can be most cost effective to perform the above described pretreatment steps at a temperature near 160° F. and the add the cellulase alone in the enzymatic hydrolysis step. This can reduce the viscosity of the fluid and provide more ends for the cellobiohydrolase and beta-glucosidase to work on in fermentation. This step can also utilize the whole cellulase working in tandem with the xylanase, which is usually a higher temperature enzyme. 
     If viscosity is not an issue, it can be more cost effective to perform all of the enzymatic hydrolysis in fermentation rather than in a separate step. This provides a less capital intensive up-front investment. Additionally, many of the most cost effective enzymes available today contain all three of these enzyme activities in one mixture. Currently the decision on using an enzymatic pretreatment is solely based on viscosity. 
     The whole stillage is next fermented as depicted by block  208  in  FIG. 2  and equipment  70  in  FIG. 3 . The fermentation of the mixed sugars produced in the pre-treatment and enzymatic hydrolysis steps described above requires an organism different than the yeast used in the fermentation step of the main ethanol production facility  10 . Saccharomyces cerevisiae is only able to ferment hexose sugars, and therefore cannot use the pentose sugars unlocked from the hemicelluloses. Another yeast or bacteria is needed to perform this step. 
       Saccharomyces cerevisiae  can be used, but two outcomes occur. Either an infectious organism begins to consume the pentose and some of the hexose sugars, or no infection occurs and the pentose sugars remain in solution. In the first case, the final acid detergent fiber content of the whole stillage byproduct of the process  200  is reduced and protein content is increased, with a slight change in amino acid profile. In the second case, the acid detergent fiber levels of the whole stillage byproduct remain higher with a resultant reduction in the percentage of protein. 
     The two front runners for the mixed sugar fermentation are both yeasts. The two strains are very similar in most respects. The first strain,  Pichia Stipitis , is the most likely candidate because it is readily available.  Candida Shehatae  is the second candidate, but it is similar in most respects to  Pichia Stipitis  except that it is less readily available. 
     These yeasts are able to ferment both the glucose and the xylose contained in the mixture. This is a trait which greatly enhances the process  200 . Fermentation times appear rather long, with 70 to 100 hours as the range found in other publications. The upper final ethanol concentrations these yeasts can survive is around 3.5 to 5 wt %. This is not an issue as the whole stillage is dilute enough to only produce final ethanol concentrations of around 1.5 to 3 wt %. If either of these yeasts are used, the entire fermentation would be carried out by the  Pichia Stipitis  or  Candida Shehatae . No co-fermentation with  Saccharomyces cerevisiae  would be required, but could be done. 
     The fermentation step of the process  200  enhances the nutrient value of the final byproduct of the process  200 . The yeasts are rich in proteins and are used to enhance the protein levels and the amino acid profiles of the whole stillage byproduct of the process  200 . It would therefore be conceivable that someone could want to produce only yeast during this process, without the production of additional ethanol. This could remove the requirement for the distillation  72  and enhance the feed produced from the whole stillage byproduct even further. 
     A total fermentation time of ˜20 hours can be used to ferment ˜80% of the available sugars. This gives reasonable results to the process  200 . However, additional time allows more fiber to be hydrolyzed and fermented, improving yields and feed composition. Generally, by 90 to 100 hours, the fermentation is nearly halted due to exhaustion of the feedstock. If fermentation is further extended beyond this point, the yeast will go through autolysis and begin to consume their own structural carbohydrates. This step increases the protein levels of the whole stillage byproduct but does little to nothing for final ethanol yields. 
     After fermentation, whole stillage is distilled and separated as depicted by block  210  in  FIG. 2  to remove ethanol from the whole stillage. The distillation may be performed in one or more distillation columns  72  depicted in  FIG. 3 . The distillation portion of the process  200  is similar to the distillation that occurs in the distillation columns  24  of the main ethanol production facility  10 . The ethanol or alcohol exits the top of the columns  72  and is transferred to one or more rectifiers to remove moisture from the alcohol. The alcohol may also be passed to one or more molecular sieves to remove even more moisture. The final alcohol is then transferred to one or more ethanol holding tanks where it may be denatured before use as a fuel or fuel additive. The alcohol from the distillation columns  72  may be transferred to the rectifiers  26  and sieves  28  of the main ethanol production facility  10  where it is co-mingled with the ethanol from the distillation columns  24  or it may be purified by its own dedicated rectifiers and sieves. 
     The whole stillage that remains in the distillation columns  72  after the alcohol has been removed falls to the bottom of the distillation columns and is then transferred to one or more whole stillage holding tanks  74 . The whole stillage at this point is similar to the whole stillage obtained at the beginning of the process  200  except that it has less solids and higher protein. The whole stillage may then be passed through one or more centrifuges  76  which separate the whole stillage into a stream of thin stillage and a stream of wet distillers grain. The thin stillage may be held in one or more tanks  78  and is typically returned to the slurry tanks  18  or some other part of the ethanol production facility  10  that requires water. Some or all of the thin stillage may also be transferred to one or more evaporators  80  to produce evaporated thin stillage, which is commonly referred to as “syrup”. The syrup may be held in one or more tanks  82  and be used as an animal feed additive. 
     The wet distillers grain, which is often referred to as “wetcake”, may be held in storage facilities  84 ,  86  and also sold as a livestock feed. Some of the wet distillers grain may be passed through one or more dryers  88  to remove liquid therefrom to produce dried distillers grain, which may be stored in one or more tanks  90  and used as dry livestock feed. The syrup from the tanks  82  may also be dehydrated in the dryers  88  forming dried distillers grain with solubles (DDGS). 
     The process  200  and systems described above provide numerous benefits. For example, the process  200  recovers additional ethanol from the whole stillage byproduct of the primary ethanol production facility  10 , thus increasing the ethanol yield of the facility. Moreover, the process  200  also improves the quality of the final whole stillage byproducts. The dried distillers grain produced by the main ethanol production facility  10  has a high fiber content that is difficult for monogastrics to digest. The process  200  of the present invention uses that fiber as a carbohydrate that is metabolized by the fermentation step. During the initial stages of fermentation, the added yeast goes through a growth phase where the carbohydrates and available nitrogen are used to produce more yeast cells. The yeast are high in protein content and also produce essential amino acids. The reduction of fiber and increase of protein content produces a feed that is more digestable for monogastrics, and therefore much higher in value. 
     A conventional corn to ethanol process produces the following from one bushel of corn: 
     
       
         
               
               
               
               
             
               
               
               
               
             
           
               
                   
                   
               
               
                   
                 Product 
                 Yield 
               
               
                   
                   
               
             
             
               
                   
               
             
          
           
               
                   
                 Ethanol 
                 2.75 
                 Gallons per Bushel 
               
               
                   
                 DDGS 
                 16.4 
                 Pounds per Bushel 
               
               
                   
                 Corn Oil 
                 0.45 
                 Pounds per Bushel 
               
               
                   
                   
               
             
          
         
       
     
     In contrast, an embodiment of the process  200  of the present invention produces the following from one bushel of corn: 
     
       
         
               
               
               
               
             
               
               
               
               
             
           
               
                   
                   
               
               
                   
                 Product 
                 Yield 
               
               
                   
                   
               
             
             
               
                   
               
             
          
           
               
                   
                 Ethanol 
                 3.02 
                 Gallons per Bushel 
               
               
                   
                 DDGS 
                 11.3 
                 Pounds per Bushel 
               
               
                   
                 Corn Oil 
                 1.5 
                 Pounds per Bushel 
               
               
                   
                   
               
             
          
         
       
     
     Moreover, the process  200  improves the nutrient content of the final DDGS byproduct as follows: 
     
       
         
               
               
               
               
               
             
               
               
               
               
               
             
           
               
                   
                   
               
               
                   
                 Type 
                 Protein 
                 Fat 
                 Crude Fiber 
               
               
                   
                   
               
             
             
               
                   
               
             
          
           
               
                   
                 Prior Art 
                 30% 
                 10% 
                 7% 
               
               
                   
                 Process 200 
                 50% 
                 3% 
                 2% 
               
               
                   
                   
               
             
          
         
       
     
     Embodiments of the invention may also be used to ferment whole stillage to other products. The sugars produced through the process  200  are relatively low in concentration as compared to traditional starch fermentations. This low concentration of fermentable sugars translates into low final concentrations of products. This allows fermentations with products that are toxic to the fermentation organism to be carried with low residual sugars. 
     One example of such a fermentation would be acetone, butanol, ethanol (ABE) fermentation. In this fermentation, butanol is toxic to the host organism at concentrations around 2%. If whole stillage is not concentrated prior to the fermentation, sugar concentrations of 3 to 4 wt % are expected. This would translate to final butanol concentrations of less than 2%. While ABE fermentation is used as the example many other types of fermentations would be well suited to this process. 
     The process  200  also improves corn oil recovery by breaking down and fermenting the fiber in the fat rich germ portion of the kernel. In prior art processes, the oil tends to become trapped within the fiber matrix of the germ, making it difficult to remove. Most reports of oil recovery in corn to ethanol plants with oil removal report yields of 15 to 35% of the total oil. By breaking down the fiber this number can increase to nearly 100% of total oil. 
     Although the invention has been described with reference to the embodiments illustrated in the attached drawing figures, it is noted that equivalents may be employed and substitutions made herein. For example, the particular equipment shown in  FIGS. 1 ,  3  and  4  may be replaced with other equipment without departing from the scope of the invention as recited in the claims.