method for frontal separation of oil by-products from grains used in alcohol production process

专利摘要:
Continuous method and systems for separating by-products from grains used in alcohol production. The present invention relates to systems and methods for separating high quality by-products, such as oil and / or germs, from grains used in the production of alcohol. In one embodiment, a method for separating by-products from grains used in the production of alcohol includes subjecting ground grains to liquefaction to obtain a liquefied starch solution that includes fibers, proteins and germs. The germs are separated from the liquefied starch solution. The separated germs are crushed, for example, to a particle size of less than 50 microns, to release, thus obtaining a germ / oil mixture. Then, before fermentation, the oil is separated from the germ / oil mixture to produce an oil by-product. It is possible to adjust the pH of the germ / oil mixture by about 8 to about 10.5 and / or to add enzymes or chemicals that break the cell wall to the germ / oil mixture to help release oil from the germs. In one example, oil production exceeds 1.0 Ib / bu.
公开号:BR112013013552B1
申请号:R112013013552-2
申请日:2011-12-05
公开日:2020-11-10
发明作者:Chie Ying Lee
申请人:Chie Ying Lee；
IPC主号:

专利说明:

DESCRIPTIVE REPORT Reference to Related Orders
[0001] This Application claims the benefit of United States Provisional Patent Application No. 61 / 419,426, filed on December 3, 2010, the disclosure of which is hereby incorporated by reference in its entirety. Technical Field
[0002] In general terms, the present invention relates to a system and method for separating by-products from grains used in the production of alcohol. Background
[0003] An alcohol of great interest today is ethanol, which can be produced from almost any type of grain, but which is most often produced from corn. Most fuel ethanol in the United States is produced by a wet grinding or dry milling process. Although it is possible to use practically any type and quality of grains to produce ethanol, the raw material for these processes is usually corn known as “yellow toothed corn ne 2”. “Na 2” refers to a quality of corn with certain characteristics, as defined by the United States National Grain Inspection Association, as is known in the art. “Yellow toothing” refers to a specific type of corn, as is known in the art.
[0004] In general terms, conventional methods for producing various types of alcohol from grains follow similar procedures, depending on whether the process is carried out dry or wet. Wet milling plants convert corn kernels into several different by-products, such as germs (for oil extraction), gluten feed (animal feed with high fiber content), gluten meal (animal feed with high content of proteins) and starch products such as ethanol, high fructose corn syrup or food and industrial starch. Dry milling ethanol plants convert corn into two products, namely ethanol and distillery grains with soluble. If sold as wet animal feed, moist distillers with soluble grains are called DWGS. If dried for animal feed, they are called DDGS. In the standard process of ethanol production by dry milling, a bushel of corn yields about 8.2 kg of dry distillery grains with soluble, in addition to about 10.5 liters of ethanol. This co-product provides an important secondary revenue stream that offset part of the total cost for ethanol production.
[0005] With regard to the wet milling process, Figure 1 illustrates a flow chart of a typical wet mill ethanol production process 10. Process 10 begins with a maceration step 12, in which the corn is left soak for 24 to 48 hours in a solution of water and sulfur dioxide in order to soften the grains for crushing, leach components soluble in the maceration water and untie the protein matrix with the endoperm. Corn kernels contain starch, fiber, protein and oil. Then, the mixture of macerated corn with water is fed to a grinding stage for degermination (first crushing) 14, when the corn is crushed in order to tear the grains and release the germs in order to produce a specific pasta paste weight (from 8.5 to 9.5 Be) of the crushed components, essentially a starch paste. The germ separation step 16 follows, which occurs by flotation and the use of hydrocyclones to separate the germs from the rest of the paste. The germ is the part of the grain that contains the oil found in corn. The stream of separate germs, which contains some portion of starch, proteins and fibers, passes to washing the germs to remove the starch and proteins and then to a dryer to produce about 2.7 to 3.2 pounds (in dry basis) of germs per bushel of corn. Dry germs contain about 50% dry oil content.
[0006] Next, the remaining paste, now free from germs, but containing fibers, gluten (that is, protein) and starch, is subjected to a stage of fine crushing (second crushing) 20, when there is a complete rupture of the endoperm and the release of endoperm components, namely gluten and starch, in relation to fibers. There follows a step of separating the fibers 22, in which the paste is passed through a series of sieves in order to separate the fibers from the starch and gluten and wash them from gluten and starch. The fiber separation stage 22 normally makes use of static pressure sieves or rotating spatulas installed in a cylindrical sieve (sieves with spatulas). Even after washing, the fibers from a typical wet grinding mill contain 15% to 20% starch. This starch is sold together with the fibers as animal feed. The remaining paste, now free from fibers, is subjected to a gluten separation step 24, in which centrifuges or hydrocyclones separate the starch from the gluten. The gluten stream passes through a vacuum filter and dryer to produce gluten flour (protein).
[0007] Thereafter, the resulting purified starch by-product is subjected to a continuous pretreatment step 26 to begin the process of converting the starch to sugar. Continuous pretreatment refers to a cooking process carried out at elevated temperatures and pressures, although specific temperatures and pressures vary widely. Most often, continuous pretreatment takes place at a temperature of about 120 ° to 150 ° C and a pressure of about 8.4 to 10.5 kg / cm2, although the temperature can be as low as 104 ° to 107 ° C when using pressures of about 8.4 kg / cm2. This is followed by liquefaction 28, saccharification 30, fermentation 32, recycling of yeast 34 and distillation / dehydration 36. Liquefaction occurs while the mixture, or “mass”, is maintained at 90 ° to 95 ° C in order for the alpha -amylase hydrolysis gelatinized starch in maltodextrins and oligosaccharides (chains of glucose sugar molecules) produce a liquefied mass or paste. In saccharification step 30, the liquefied mass is cooled to about 50 ° C and a commercial enzyme known as glycoamylase is added. Glycoamylase hydrolyzes maltodextrins and short chain oligosaccharides into simple glucose sugar molecules to produce a liquefied mass. In fermentation step 32, a common yeast strain (Saccharomyces cerevisiae) is added to metabolize glucose sugars into ethanol and CO2.
[0008] Upon completion, the fermented mass (“beer”) contains about 17% to 18% ethanol (basic volume / volume) plus soluble and insoluble solids of all the remaining components of the grains. The solids and some liquid remaining after fermentation pass to an evaporation stage, in which it is possible to recover the yeast as a by-product. As an option, it is possible to recycle yeast in a yeast 34 recycling step. In some cases, CO2 is recovered and sold as a primary product. After the fermentation stage 32, there is the distillation and dehydration stage 36, in which the beer is pumped into distillation columns where it is boiled in order to vaporize the ethanol. The ethanol vapor is condensed in the distillation columns, and the liquid alcohol (in this case, ethanol) leaves the top of the distillation columns with a purity of about 95% (190 proofs). Then, the ethanol with 190 proofs is passed through a dehydration column with a molecular sieve, which removes the residual water remaining from the ethanol to produce a final product consisting essentially of 100% ethanol (199.5 proofs). This anhydrous ethanol is now ready for use as a motor fuel.
[0009] A centrifugation step is not necessary at the end of the wet mill ethanol production process 10 since the germs, fibers and gluten have already been removed in the separation steps 16, 22 and 24 above. The “stillage” produced after distillation and dehydration 36 in the wet milling process 10 is generally called “complete stillage”, although it is not technically the same type of complete stillage produced by the dry milling process described in Figure 2 below, as seen that there are no insoluble solids present. Some producers of alcohol by wet grinding call this type of vinasse “diluted”.
[0010] The wet milling process 10 generates a high quality starch product for conversion to alcohol, in addition to separate streams of germs, fibers and proteins, which can be sold as by-products to generate additional revenue streams. However, the total production of the various by-products may be less than desirable; and the wet grinding process is complicated and costly, requiring high capital investment in addition to high energy costs for operation.
[0011] Because the capital cost of wet grinding mills is so prohibitive, some alcohol mills prefer to use the simpler dry milling process. Figure 2 illustrates a flow chart of a typical ethanol production process by dry grinding 100. Process 100 begins with a grinding step 102, in which dry, whole corn kernels pass through hammer mills to crush them. in flour or fine powder. The crushed flour is mixed with water, thus forming a paste, and a commercial enzyme called alpha-amylase (not shown) is added. Then, this paste is heated to about 120 ° C for about 0.5 to 3 minutes in a pressurized continuous pretreatment process 104 in order to gelatinize (solubilize) the starch in the crushed flour. It is worth noting that some processes exclude continuous pretreatment and, instead, make use of a longer storage time of the pulp in a pulp tank at a temperature of about 50 ° C to 95 ° C.
[0012] There follows a step of liquefaction 106, when it is possible to add more alpha-amylase. The flow after this liquefaction step contains a content of about 30% dry solids (DS) with all the components contained in the corn kernels, including sugars, proteins, fibers, starch, germs, oil and salts. There follow separate steps of saccharification 108 and fermentation 110, although in most commercial processes of ethanol production by dry milling, saccharification and fermentation occur at the same time. This step is called in the industry “simultaneous saccharification and fermentation” (SSF). Both saccharification and SSF can take up to 50 to 60 hours. Fermentation converts sugar to alcohol. As an option, yeast can be recycled in a yeast 112 recycling step. After fermentation step 110, there is a distillation and dehydration step 114, as in the wet grinding process, to recover the alcohol.
[0013] Finally, a centrifugation stage 116 involves centrifuging the residues produced in the distillation and dehydration stage 114, that is, the “complete vinasse”, in order to separate the insoluble solids (“wet mass”) from the liquid (“ diluted vinasse ”). The liquid that leaves the centrifuge contains about 8% to 10% dry solids. The diluted vinasse enters evaporators in an evaporation stage 118 in order to remove moisture by boiling, thus obtaining a thick syrup that contains soluble (dissolved) solids from fermentation (from 25% to 35% dry solids). The concentrated paste can be sent to a centrifuge to separate the oil from the syrup. The oil can be sold as a separate high quality product. Oil production is usually about 6.427 g / L (0.5 lb / bu) of corn with a high content of free fatty acids. Free fatty acids are generated when the oil is kept in the fermenter for about 50 hours. The fatty acid content in books decreases the quality of the oil. The oil removal centrifuge removes less than 50% because proteins and oil form an emulsion that cannot be separated satisfactorily.
[0014] The syrup, which contains more than 10% oil, can be mixed with the wet centrifuged mass, and the mixture sold to beef and dairy farms in the form of wet distillers with soluble grains (DWGS). Alternatively, mixing the wet dough with the concentrated syrup can be dried in one step 120 and sold as dry soluble distillery grains (DDGS) to beef and dairy farms. These dry soluble distillery grains contain all protein and 75% of the oil in corn. However, the quality of dry distillery grains with soluble is low due to the high percentage of fibers and, in some cases, oil is an obstacle to the digestion of animals.
[0015] As the dry milling process 100 only produces ethanol and dry distillery grains with low quality soluble, many companies have started to develop a dry fractionation process. In it, the corn goes through a pre-treatment stage, such as steam treatment, and then various types of mechanical separation equipment are used to separate dry fractions from corn, including fibers, starch and an oil fraction. / germs. Although these separation processes produce a certain level of separation of the components, it is often incomplete. For example, the fiber fraction typically contains more than 30% dry starch, and germs contain more than 25% starch and 35% dry oil. Furthermore, in these processes, less than 30% of the total oil is recovered in the corn kernels and the germ and fiber fractions must undergo purification stages before being sold at a reasonable price.
[0016] After dry fractionation, the starch (with proteins) goes through another crushing stage, then through liquefaction, fermentation, distillation and evaporation, to produce alcohol and syrup, as in the dry crushing process 100. However, the production of alcohol is usually a mere 0.2467 L / L (2.3 gal / bu) of corn due to the loss of starch to the fractions of germs and fibers. In addition, the aforementioned purification steps for germs and fibers are complex and costly. As can be seen, the dry fractionation process does not provide a good separation and generates low-purity by-products, which complicates the downstream purification steps. Due to high costs and low production, these dry fractionation processes ended up not being widely accepted by the industry.
[0017] Other attempts have been made in the dry milling industry to desirably recover by-products, such as high quality oil. However, attempts to separate the oil from the “hammer-ground” paste have failed because of the high concentration of solids and because the oil is not released from the solid particles. Some success has been achieved with processes that recover oil in the evaporation stages of the dry grinding process. However, production is relatively low, and the oil must go through the entire process, including fermentation, before evaporation. The presence of oil in these stages of the process can be detrimental to the efficiency of the other parts of the process. An attempt was made to recover the oil directly after fermentation. However, the mixing and fermentation process emulsifies the oil, which makes it extremely difficult to remove. Other attempts have been made to recover oil directly from corn by extracting the solvents, but the cost, for example, is too high for commercial use.
[0018] It would therefore be advantageous to develop an improved system and method for separating by-products from grains used in the production of alcohol that overcome the various disadvantages mentioned above in order to generate high-quality by-products with desirable yield. Summary of the Invention
[0019] The present invention relates to a system and method for separating by-products from grains used in the production of alcohol. Said system and method offer a better separation between oil, proteins, fibers and / or starch and generate a purer by-product thanks to several changes along the alcohol production route.
[0020] In one embodiment, a method for separating by-products from grains used in the production of alcohol includes subjecting ground grains used in the production of alcohol to liquefaction in order to obtain a solution of liquefied starch that includes fibers, proteins and germs. The germs are separated from the liquefied starch solution and then ground, for example, to a particle size of less than 150 microns (or less than 50 microns) to release oil in order to obtain a germ / oil mixture. Before fermentation, the oil is separated from the germ / oil mixture to produce an oil by-product. It is possible to adjust the pH of the germ / oil mixture by about 8 to about 10.5 and / or to add enzymes to the mixture to help release the oil. It is also possible to subject the germ / oil mixture to a temperature of about 180 ° F to about 200 ° F. In one example, oil production exceeds 12.85 g / L (1.0 lb / bu).
[0021] In another embodiment, a method for separating by-products from grains used in alcohol production includes subjecting ground grains used in alcohol production to liquefaction to obtain a liquefied starch solution that includes fibers, proteins, germs and oil. The germs and oil are individually separated from the liquefied starch solution to produce an oil by-product. Then, the separated germs are crushed to release oil in order to obtain a germ / oil mixture. Before fermentation, the oil is separated from the germ / oil mixture to produce an oil by-product.
[0022] In yet another embodiment, a method for separating by-products from grains used in alcohol production includes subjecting ground grains used in alcohol production to liquefaction to obtain a liquefied starch solution that includes fibers, proteins, germs and oil. The solids, which include fibers and germs, are separated from the liquefied starch solution. After and before fermentation, the oil is separated from the germ / oil mixture to produce an oil by-product.
[0023] In another embodiment, a continuous system for separating by-products from grains used in the production of alcohol includes a grinding device, which grinds the grains used in the production of alcohol, and a liquefaction apparatus, which helps to convert the starch of the grains ground in sugar to obtain a solution of liquefied starch, which includes fibers, proteins and germs. The system also includes a germ separator, which separates the germs from the liquefied starch solution, and a germ crusher, which grinds the separated germs to release oil in order to obtain a germ / oil mixture. A germ / oil separator separates the oil from the germ / oil mixture to produce an oil by-product. After that, a fermenter and a distiller ferment and distill, respectively, the liquefied starch solution to produce alcohol.
[0024] In yet another embodiment, a continuous system for separating by-products from grains used in the production of alcohol includes a grinding device, which grinds the grains used in the production of alcohol, and a liquefaction apparatus, which helps to convert the starch of the grains ground in sugar to obtain a solution of liquefied starch, which includes fibers, proteins, germ and oil. The system also includes a separator, which separately separates the germs and oil from the liquefied starch solution to produce a by-product of the oil, and a germ crusher, which grinds the separated germs to release the oil in order to obtain a mixture of germs / oil. A germ / oil separator separates the oil from the germs to produce an oil by-product. After that, a fermenter and a distiller ferment and distill, respectively, a mixture that includes the separated germs and the liquefied starch solution to produce alcohol.
[0025] In yet another embodiment, a continuous system for separating by-products from grains used in the production of alcohol includes a grinding device, which separates the grains used in the production of alcohol, and a liquefaction apparatus, which helps to convert the starch of the grains ground in sugar to obtain a solution of liquefied starch, which includes fibers, proteins, germs and oil. The system also includes a solids / liquids separator, which separates solids, which include fibers and germs, from the liquefied starch solution. After that, an oil separator separates the oil from the liquefied starch solution to produce an oil by-product. Then, a fermenter and a distiller ferment and distill, respectively, a mixture that includes the liquefied starch solution, which includes proteins and solids, which include fibers and germs, to produce alcohol.
[0026] In this context, an improved system and method is provided to separate by-products from grains used in the production of alcohol; system and method that produce high quality by-products with desirable yield. Brief Description of Drawings
[0027] The attached drawings, which are incorporated and constitute part of this Descriptive Report, illustrate embodiments of the invention and, together with the detailed description of the embodiments presented below, serve to explain the principles of the invention.
[0028] Fig. 1 illustrates a flow chart of a typical process of ethanol production by wet grinding;
[0029] Fig. 2 illustrates a flow chart of a typical ethanol production process by dry grinding;
[0030] Fig. 3 illustrates a flow chart of a system and method for separating high-quality by-products from grains used in the production of alcohol according to an embodiment of the invention;
[0031] Fig. 3A illustrates a flow chart of a variation of the system and method of Figure 3;
[0032] Fig. 4 illustrates a flow chart of a system and method for separating high-quality by-products from grains used in the production of alcohol according to another embodiment of the invention;
[0033] Fig. 4A illustrates a flow chart of a variation of the system and method of Figure 4;
[0034] Fig. 5 illustrates a flow chart of a system and method for separating high-quality by-products from grains used in the production of alcohol according to another embodiment of the invention;
[0035] Fig. 5A illustrates a flow chart of a variation of the system and method of Figure 5; and
[0036] Fig. 5B illustrates a flow chart of another variation of the system and method of Figure 5. Detailed Description of Specific Embodiments
[0037] Figures 1 and 2 were discussed above and represent flowcharts of typical processes of ethanol production by wet grinding and dry grinding, respectively.
[0038] Figures 3 to 5B illustrate several embodiments of a system and method for separating high-quality oil, collagen fibers and protein flour from grains used in the production of alcohol; system and method that constitute advances in relation to typical and other procedures. From now on, these systems and methods will be discussed in detail.
[0039] As an overview of the embodiments illustrated in Figures 3 to 5B, each system and process includes, after milling the corn and before fermenting, the separation of the germs from a liquefied starch solution thanks to specific mass differences between the different components of that solution. The liquefied starch solution contains, after liquefaction, oil, germs, granules, proteins and fiber particles with particle sizes ranging from less than 50 microns to more than 2 mm. The specific mass of the oil is usually about 0.9 g / cm3, of a germ particle of about 1 g / cm3 and of the granules, proteins and fibers of about 1.1 to 1.15 g / cm3. During soaking / cooking and liquefaction, the liquid solution has a specific gravity of about 10.5 to 1.12 g / cm3 (for example, about 15 to 28 Brix of sugar solution). This heavy specific mass of the liquefied starch solution can serve to separate the germs and oil from the granules, proteins and fibers. In addition, the pH of the paste when liquefying is about 5 to 6.
[0040] There are two main ways to prepare the germs before separating them from the liquefied starch solution. The first one, as shown in Figures 3 and 3A, involves soaking and boiling the corn and then tearing the corn kernels using a grinding mill or roller mill, followed by liquefaction. Alternatively, as shown in Figures 4 to 5B, the soaking and cooking step is eliminated and, as in the dry milling process existing today, the corn is subjected directly to a hammer mill, for example, to which liquefaction follows.
[0041] The crushing step aims to tear apart the germs and granules and to break the bonds between starch and proteins without cutting the fibers so that they become very thin. There are three types of fiber: (1) the pericarp, with average particle sizes generally between about 1 mm and 5 mm; (2) the tip, with average particle sizes of about 500 microns; (3) and fine fiber, with average particle sizes of about 250 microns. A filtering device, such as a fiber centrifuge, can be used to separate the different types of fiber using one or more sieves with openings of different sizes. The pericarp and the tip are kept in sizes greater than 300 microns, while the germs and granules are smaller than that. In addition, fine fibers can cause problems with the separation of fibers / proteins downstream and can produce a very moist mass of fibers (dry distillery grains), which is very expensive to dry. As an option, it is also possible to add enzymes, such as an enzyme that degrades the cell wall, including amylase, protease or combinations thereof, during the crushing / impact milling step, for example, to help break the bonds between proteins, starch and fibers. During or after soaking / cooking or liquefaction, the liquefied starch solution passes through the most diverse separation devices possible, such as a cyclone or three-phase decanter, to separate, for example, the germs and oil from it, which can be further processed as will be discussed in more detail below, such as to produce a desirable oil and / or fiber by-product.
[0042] Referring now to Figure 3, a system and method 200 is illustrated, which substantially correspond to a system and process of the wet type, system and method which separate by-products, such as high quality germs and proteins, from grains used in the production of alcohol in order to produce, for example, desirable collagen fibers (for example, pericarps) for industrial use and high quality oil. In this specific system and method 200, the corn is subjected to a soaking / cooking step 202, in which the corn is soaked for 4 to 12 hours in soaking tanks filled with water with a temperature around 55 ° to 95 ° C. As an option, an enzyme, such as alpha-emylase, can be included in the soaking tanks, as well as about 50 to 100 ppm of sodium sulfite, sulfur dioxide or the like. Then, the soaked corn is subjected to a crushing step 204 using one or more crushing mills and / or roller mills to grind the corn kernels and release the germs. As an option, an enzyme, such as alpha-amylase, can be added before or during the crushing step 204. After that, the paste, which includes starch, is subjected to a 206 liquefaction step, which generates a liquefied starch solution with a specific gravity of about 1.05 g / cm3 to 1.15 g / cm3. In the 206 liquefaction step, the starch begins to convert into a liquefied starch solution. It is possible to use any suitable liquefying apparatus that is familiar in the art.
[0043] Then, in a step of separating the germs 208, the germs are separated from the liquefied starch solution, as well as from the fibers, proteins and granules, taking advantage of the differences in specific mass between the different components in the starch solution liquefied using, for example, a biphasic germ cyclone or a disc centrifuge or decanter designed for this purpose, in series. More specifically, the liquefied starch solution is used as a heavy liquid medium to suspend the germs, which are then separated from it. After that, the germs are fed to a shredding device in a shredding step 209 to shred them to a particle size of less than 150 microns (or, in another example, less than 50 microns) without creating fine fibers and to release the oil from the germs, thus obtaining an oil / germ mixture.
[0044] The crushed germs (or oil / germ mixture) are transported to a germ storage tank 210, where the pH of the germs is adjusted from about 8 to about 10.5 (or about 8 to about 9.5), such as adding chemicals, for example, sodium hydroxide, calcium oxide, sodium carbonate, trisodium phosphate or the like, to help release oil from the germs. In addition, enzymes that disrupt the cell wall, for example, protease or the like, and / or chemicals that also disrupt the cell wall, for example, sodium sulfite or the like, can be added here to help release oil of the germs. In one example, the germs are kept in the tank for about 1 hour at a temperature of about 140 ° F to about 200 ° F (or from about 180 ° F to about 200 ° F).
[0045] Then, the oil / fine germ mixture is subjected to an oil / germ 211 separation step, in which the oil is separated from the fine germs, taking advantage of the specific mass differences between the different components in the solution of residual liquefied starch using, for example, a three-phase decanter or a three-phase disc centrifuge. The oil recovered at this stage of the process has a much more desirable quality in terms of color and content of free fatty acids (from about 2% to about 5%) compared to the oil recovered downstream, more specifically the oil recovered after fermentation. More specifically, the oil recovered before fermentation is lighter and has a lower fatty acid content. Oil production can include 12.85 g / L (1.0 lb / bu) or more. In one example, oil production is about 12.85 to about 15.42 g / L (1.0 to about 1.2 lb / bu). In addition to, or as an alternative to, oil recovery operations before fermentation, it is possible to perform similar methods of oil recovery after fermentation.
[0046] The remaining liquefied starch solution from the germ separation step 208, which includes fibers, proteins and granules, is subjected to a size reduction step 212 using a grinding mill, pin mill or high stove pressure, for example, to further break the connection between fibers, starch and proteins. Although not specifically illustrated, as an option, various enzymes (and types of enzymes), such as glycoamylase, fungal, cellulose, cellobiosis, protease and the like, can be added during the 212 size reduction step and afterwards, even during fermentation , to intensify the separation of the components.
[0047] In the fermentation step 213, the solids, which include the separated fine germs (from which oil has been removed), and the residual liquefied starch solution from the oil / germ separation step 211, come together with the liquefied starch solution from the size reduction step 212. The fine germs can be separated from the fiber and protein components downstream in the form of high quality fine germs. In an alternative example, the separate germs sent to the grinding step 209 can be ground to a particle size of less than 500 microns, but not so small as to release oil from them and without producing fine fibers. In one example, the particle size of the germs is 50 to 500 microns, with an average size of 250 microns. After that, the fine germs would return to the liquefied starch solution after the size reduction step 212 and before the fermentation step 213 for the downstream separation in the form of high quality fine germs. In this alternative example, the germ storage tank 210 and / or the oil / germ separation step 211 would be removed from the method.
[0048] Alternatively, it is possible to replace the oil / germ separation step 211 with a solvent extraction step 214, the alcohol / germ separation step 215 and the alcohol evaporation step 216 to recover oil from the oil / fine germ mixture in the storage tank 210. More specifically, the oil / fine germ mixture can pass from storage tank 210 to the solvent extraction step 214, in which the alcohol recovered in the distillation step 217 is added to the oil / fine germ mixture to extract this oil. Then, the alcohol / oil / germ mixture is sent to the alcohol / germ separation step 215 to separate the alcohol, which includes the extracted oil, from the fine germs using, for example, a decanter or disk centrifuge. In the fermentation step 213, the solids (or heavy phase), which include the separated fine germs (from which oil has been removed), and the residual liquefied starch solution from the alcohol / germ separation step 214, are added to the solution of liquefied starch from the size reduction step 212. In addition, the separate alcohol / oil solution (or light phase) is sent to the alcohol evaporation step 214, in which an evaporator separates the oil and the alcohol to recover both . A small evaporator can be included as part of the distillation tower. The germs from which oil has been removed usually contain about 10% to 20% oil. However, with solvent extraction step 214, the germs from which oil was removed include about 4% to 10% oil. Oil production can include 12.85 g / L (1.0 lb / bu) or more. In one example, oil production is about 12.85 g / L (1.0 lb / bu) to about 17.99 g / L (1.4 lb / bu) (or 15.42 g / L (1.2 lb / bu) to about 17.99 g / L (1.4 lb / bu)).
[0049] In the fermentation stage 213, the liquefied starch solution, which includes fibers, proteins, granules and, now, fine germ particles, is subjected to fermentation, followed by distillation in the distillation stage 217. The Fine germs will have their oil partially removed during fermentation, which can assist in the later separation and production of high quality oil with little or no germ protein. In the distillation tower, the sugars in the liquefied starch solution are separated from the vinasse, which includes fibers, proteins and fine germ particles, to produce alcohol.
[0050] Fibers are separated from fine germs, fine fibers and proteins (gluten) in a fiber / protein separation step 218 thanks to differences in particle sizes by means of a sieving device, such as a sieve with spatulas / filtration centrifuge, to remove the collagen fiber, that is, the pericarp, from them. Here, the sieve openings are usually about 1 mm, but can vary from about 0.3 mm to 1.5 mm. Still regarding the particle sizes, the average particle size of the proteins is about 1 to 5 microns, of the fine germs of about 10 to 500 microns and of the various fibers of about 50 microns to 3 mm. The separated fibers are washed and dried to produce high quality collagen fibers for industrial use with a yield of about 25.70 g / L (2.0 lb / bu). The separated fibers can also be used as a raw material in the secondary production of alcohol with a yield of about 38.55 g / L (3.0 lb / bu). Collagen fibers are mainly composed of pericarp and contain less than 10% protein, less than 2% oil and less than 2% starch. In one example, collagen fibers include 85% or more pericarp, in another example, 90% or more pericarp and, in another example, 95% or more pericarp.
[0051] With continuous reference to Figure 3, the filtrate of the filtration centrifuge, which includes fine residual fibers and tips with sizes from about 30 microns to 300 microns and from about 300 microns to 500 microns, in addition to fine and gluten (protein), passes to a stage of separation of fine germs and fibers 219, in which fine germs and fibers are removed from the gluten solution by a fine sieving device, such as a sieve with spatulas or a pressure sieve with a size of opening of about 45 microns. Fine germs and fine fibers are transported to a fine germ / fiber storage tank 220, where the pH of the fine germs / fibers is adjusted from about 8 to about 10.5 (or about 8 to about 9.5), such as adding chemicals, for example, sodium hydroxide, calcium oxide, sodium carbonate, trisodium phosphate or the like, to help release more oil from the germs. In addition, enzymes that disrupt the cell wall, for example, protease or the like, and / or chemicals that also disrupt the cell wall, for example, sodium sulfite or the like, can be added here to help release more oil of the germs. Then, the fine germ / fiber mixture is subjected to a step of separating the fine fibers 221, in which the fine fibers are separated from the fine germs by a decanter, for example, and dried to produce dry distillery grains. In one example, fine fibers include less than 15% protein and 4% oil.
[0052] The center from the step of separating the fine germs and fibers 219 and the center from the step of separating the fine fibers 221 come together and go through a step of recovery / dehydration of the proteins 222, which uses, for example, a decanter, a centrifuge with discharge piping or a disc decanter to recover fine germs and proteins (as well as used yeast). Alternatively, the centering from the fine fiber separation step 221 can be dehydrated using, for example, a decanter, a centrifuge with discharge pipe or a disc decanter and sent back to the germ crushing step 209 for extract more oil. Components from recovery / dehydration step 222 are sent to a dryer 223 to produce a high quality gluten / germ / yeast mixture (protein flour) with about 60% gluten and about 40% germ / yeast . The remaining flow from the protein dehydration step 222 passes to an evaporator 226 to separate oil from it and produce syrup, which can be mixed with dry and dry distillery grains, as represented by number 228, to produce dry distillery grains with soluble with low protein content (about 20%) / low oil content (about 7%), such as for cattle and pigs. In one example, proteins do not exceed 20% and oil does not exceed 7%. In another example, it is possible to add sodium sulfite, sulfur dioxide or the like at any stage in the process between soaking / cooking step 202 and drying step 228. As can be seen, in this system and method 200, recovery most of the by-product after fermentation.
[0053] Regarding oil recovery, whenever there is oil recovery, there is usually a tendency for an emulsion layer to form in the collection tanks. In tanks where oil is stored, it floats naturally and the emulsion layer settles on the bottom, along with any other solids. There is a significant content of xanthophyll in the emulsion layer, and this is good for making chicken egg yolks yellow. With an optional centrifugation step (not shown), it is possible to recover the xanthophyll content in the emulsion layer and mix it with the protein flour by-product before drying the proteins in order to increase the quality of the feed. It is possible to add sodium sulfite, sulfur dioxide and the like to the wet protein mass, for example, in order to maintain more than 20 ppm of sulfur dioxide level, before sending it to the 223 protein dryer. Dioxide sulfur prevents the xanthophylls from decomposing in the 223 protein dryer. The oil (light phase) that leaves the centrifuge can return to the oil storage tanks.
[0054] With reference now to Figure 3A, this illustrates a flow chart of a variation of the system and method 200 of Figure 3. In this system and method 200a, the gluten flour (protein) and collagen fibers (this is removed) ie, the pericarp) before fermentation 213. Briefly, as an extra information, it is worth mentioning that there are from 0.221 to 0.442 g / kg (100 to 200 mg / lb) in xanthophyll in the gluten flour originating from a typical wet grinding process. corn. The recovery of gluten flour before fermentation 213 reduces the loss of xanthophyll during fermentation 213 and the subsequent stages of distillation 217 and recovery of proteins 222. Furthermore, it is worth noting that the particle size of the pericarp is important for industrial uses , as in the paper industry. Larger pericarp particles, such as about 1 mm to about 5 mm, can clog the heat exchanger used during fermentation. Therefore, removal of the pericarp before fermentation 213 avoids these clogging problems and increases the fermentation capacity by about 15% thanks to the previous removal of the pericarp.
[0055] As shown in Figure 3A, after the separation of the germs and the subsequent step of reducing the size 212, the liquefied starch solution, along with the fibers, proteins and granules, is subjected to a step of gluten / fiber separation 230 using a sieving device, such as a filtering centrifuge, to remove collagen fibers, that is, the pericarp, from it. The sieve openings are usually about 1.5 mm, but can vary from about 1 mm to 2 mm. The separated fibers are washed and dried, as represented by number 232, to produce high quality collagen fibers for industrial use with a yield of about 25.70 g / L (2 lb / bu). The separated fibers can also be used as a raw material in the secondary production of alcohol. In the case of collagen fibers used as raw material in the paper industry, for example, they are composed mainly of pericarp, whereas, in the case of secondary alcohol production, they are composed mainly of pericarps, ends and fine fibers, have a yield of 38.55 to 51.40 g / L (3 to 4 lb / bu) and contain less than 14% protein and less than 5% oil. In one example, collagen fibers include 85% or more pericarp, in another example, 90% or more pericarp and, in another example, 95% or more pericarp.
[0056] As an option, the proteins in the excess flow of the liquefied starch solution resulting from the gluten / fiber separation step 230 can be separated by methods known in the art in which the gluten goes through a washing and drying step 234 to produce flour. high quality gluten with a desirable percentage of xanthophyll, that is, from about 0.221 g / kg (100 mg / lb) to about 0.442 g / kg (200 mg / lb). Otherwise, the excess flow fraction of the liquefied starch solution meets the fine germ particles in the fermentation step 213. The rest of the process is substantially the same as in Figure 3, except that the gluten flour and fibers collagen were recovered at the beginning of the process, before fermentation 213. More specifically, when collagen fibers are previously separated from proteins, fine fibers and fine germ particles and recovered in system and method 200 of Figure 3, the fine fibers and fine germ particles larger than 50 microns are separated from the residual protein (gluten) in the step of separating fine germs and fibers 219 using a fine sieving device, such as a sieve with spatulas or a pressure sieve with an opening size of about 45 microns.
[0057] Then, the fine germs and fibers are transported to the fine germs / fibers 220 storage tank, where the pH of the fine germs / fibers is adjusted from about 8 to about 10.5 (or about 8 to about 9.5), such as adding chemicals, for example, sodium hydroxide, calcium oxide, sodium carbonate, trisodium phosphate or the like, to help release oil from the germs. In addition, enzymes that disrupt the cell wall, for example, protease or the like, and / or chemicals that also disrupt the cell wall, for example, sodium sulfite or the like, can be added here to help release oil from germs. Then, the germ / fiber mixture is subjected to a step of separating the fine fibers 221, in which the fine fibers are separated from the fine germs by a decanter, for example, and dried to produce dry distillery grains. In one example, fine fibers include less than 15% protein and 4% oil in order to produce dry distillery grains. The center from the separation of fine germs and fibers 219 and the center from the separation stage of fine fibers 221 come together and go through a recovery / dehydration stage of proteins 222, which uses, for example, a decanter, a centrifuge with discharge pipe or a disc decanter to recover fine germs and residual proteins, as well as the yeast used. Alternatively, the centering from the fine fiber separation step 221 can be dehydrated using, for example, a decanter, a discharge tube centrifuge or a disc decanter and sent back to the germ crushing step 209 to extract more oil. The components from the protein recovery / dehydration step 222 are sent to a dryer 223 to essentially produce a germ / yeast mixture with about 60% gluten and about 40% germ / yeast.
[0058] Referring now to Figure 4, this illustrates a flowchart of another embodiment of a system and method 300 for separating high quality by-products from grains used in the production of alcohol. This system and method 300, which substantially correspond to a dry crushing ethanol production system and process, separates various by-products to produce, for example, cellulosic material for the secondary production of high quality alcohol and oil. For this purpose, in this specific process and method 300, firstly, the corn is subjected to a hammer mill 302, for example, which can be used to crush the corn in particle sizes below about 2.78 mm ( 7/64 in.) And help release oil from it. In one example, the particle size is about 50 microns to 3 mm. Crushing helps to break the bonds between fibers, proteins, starch and germs. In another example, a fraction of germs, such as from a dry fractionation process, can replace the initially un-ground corn here. The crushed corn is mixed with water and sent to a 304 liquefaction stage, which provides a solution of liquefied starch with a specific gravity of about 1.05 to 1.15 g / cm3. In the 304 liquefaction step, the starch begins to convert into a liquefied starch solution. Enzymes, such as alpha-amylase, can be added to liquefaction step 304. It is possible to use any suitable liquefaction apparatus that is familiar in the art.
[0059] The flow from the 304 liquefaction step contains about 12.85 g / L (1 lb / bu) oil-free and about 19.27 g / L (1.5 lb / bu) of germ particles (size ranges from less than about 50 microns to about 1 mm), 12.85 g / L (1 lb / bu) of granules (size ranges from about 50 microns to about 1 mm) and 64, 25 g / L (5 lb / bu) of fibers (particle size ranges from about 50 microns to about 3 mm). This flow passes to a germ / oil separation step 306, which uses three-phase separation equipment (for example, a three-phase decanter, a three-phase disc centrifuge, a hydrocyclone and the like) to individually separate the oil and germs from the solution of liquefied starch, which includes heavier fibers, proteins and granules, taking advantage of the specific mass differences between the different components in it. More specifically, the liquefied starch solution is used as a heavy liquid medium to suspend the germs and oil, which have specific masses of about 1.0 to 1.05 g / cm3 and 0.9 to 0.92 g / cm3, respectively. It should be borne in mind that if a three-phase disk centrifuge is used in the germ / oil separation step 306, a pre-screening step (not shown) may be required to remove large fiber particles, as with more than 750 microns, for example. If this pre-sorting step is used, the solids fraction deviates from the germ / oil separation step 306 and moves directly to a crushing step 310, which we will discuss in more detail below. The oil recovered at this stage of the process, that is, in the germ / oil separation step 306, has a much more desirable quality in terms of color and free fatty acid content (from about 2% to about 5%) in comparison to the oil recovered downstream, more specifically to the oil recovered after fermentation. More specifically, the oil recovered before fermentation is lighter and has a lower fatty acid content. Oil production can include 12.85 g / L (1 lb / bu) or more. In one example, oil production is from about 12.85 g / L (1 lb / bu) to about 15.42 g / L (1.2 lb / bu).
[0060] After that, the separated germs are fed to a grinding device in a grinding step 307 to fine grind them to a particle size between about 10 and 300 microns to help release more oil, obtaining, thus, an oil / germ mixture. In another example, the particle size is less than 50 microns. The crushed germs (or oil / germ mixture) are transported to a 308 germ storage tank, where their pH is adjusted from about 8 to about 10.5 (or about 8 to about 9.5) ), such as adding chemicals, for example, sodium hydroxide, calcium oxide, sodium carbonate, trisodium phosphate or the like, to help release oil from the germs. In addition, enzymes that disrupt the cell wall, for example, protease or the like, and / or chemicals that also disrupt the cell wall, for example, sodium sulfite or the like, can be added here to help release oil from germs. In one example, fine germs are kept in the tank for about 1 hour at a temperature of about 60 ° C (140 ° F) to about 93.33 ° C (200 ° F) (or about 82, 22 ° C (180 ° F) to about 93.33 ° C (200 ° F)).
[0061] Next, the oil / germ mixture is subjected to an oil / germ 309 separation step, in which the oil is separated from the fine germs, taking advantage of the specific mass differences between the different components in the solution of residual liquefied starch using, for example, a three-phase decanter or a three-phase disc centrifuge. The oil recovered at this stage of the process has a much more desirable quality in terms of color and content of free fatty acids (from about 2% to about 5%) compared to the oil recovered downstream, more specifically the oil recovered after fermentation. In addition to, or as an alternative to, oil recovery operations before fermentation, it is possible to perform similar methods of oil recovery after fermentation.
[0062] The remaining liquefied starch solution from the germ separation step 306, which includes fibers, proteins and granules, goes through a 310 grinding step, such as a grinding mill, to further break the connection between fibers, starch and proteins. Although not specifically illustrated, as an option, various enzymes (and types of enzymes), such as glycoamylase, fungal, cellulose, cellobiosis, protease and the like, can be added during the crushing step 310 and thereafter, even during fermentation, to intensify the separation of components.
[0063] The solids, which include the separated fine germs, and the residual liquefied starch solution from the oil / germ 309 separation step, join the liquefied starch solution from the 310 size reduction step and are then subjected to the fermentation step 311. The fine germ particles can be separated from the fiber and protein components downstream in the form of fine high quality germ particles (from which the oil has been partially removed). In an alternative example, the separated germs are sent to the crushing step 307 and then the fine germ particles are returned to the liquefied starch solution after the size reduction step 310 in the fermentation step 311 for separation a downstream in the form of fine particles of high quality germ. In this alternative example, the germ storage tank 308 and / or the oil / germ separation step 309 would be removed from the method.
[0064] Alternatively, it is possible to replace the oil / germ separation step 309 with a solvent extraction step 312, the alcohol / germ separation step 313 and the alcohol evaporation step 314 to recover oil from the oil / fine germ mixture in the storage tank 308. More specifically, the oil / fine germ mixture can be sent from storage tank 308 to the solvent extraction step 312, in which the alcohol recovered in the distillation step 315 is added to the oil / fine germ mixture for extract oil from it. Then the alcohol / oil / germ mixture is sent to the alcohol / germ separation step 313 to separate the alcohol, which includes the extracted oil, from the fine germs using, for example, a decanter or disk centrifuge. The solids (or heavy phase), which include the separated fine germs (from which oil has been removed), and the residual liquefied starch solution from the alcohol / germ separation step 313, join the liquefied starch solution from the reduction in size 310 in fermentation step 311. In addition, the separated alcohol / oil solution (or light phase) is sent to the alcohol evaporation step 314, in which an evaporator separates the oil and the alcohol for the recovery of both. A small evaporator can be included as part of the distillation tower. The germs from which oil has been removed usually contain about 10% to 20% oil. However, with solvent extraction step 312, the germs from which oil has been removed include about 4% to 10% oil. Oil production can include 12.85 g / L (1 lb / bu) or more. In one example, oil production is about 12.85 g / L (1 lb / bu) to about 17.99 g / L (1.4 lb / bu) (or 15.42 g / L (1.2 lb / bu) to about 17.99 g / L (1.4 lb / bu)).
[0065] In fermentation step 311, the liquefied starch solution, which includes fibers, proteins, granules and, now, fine germ particles, is subjected to fermentation, followed by distillation in the 315 distillation step. distillation tower, the fermented solution (also called beer) is separated from the vinasse, which includes fibers, proteins and fine particles of germ, to produce alcohol. The fibers can be separated from the fine particles of germ and proteins (gluten) in a fiber / protein separation step 316 thanks to differences in particle sizes using a sieving device, such as a sifter with spatulas, a filtering centrifuge or a decanter, to remove fibers from them. The sieve openings are usually about 500 microns to capture sums of tips, pericarps, as well as fine fibers, but can range from about 300 microns to about 700 microns. The separated fibers are washed and, optionally, dried to produce cellulose for the secondary production of alcohol, which is a lower quality fiber than the collagen fibers produced by the process of Figure 3, for example. The resulting cellulosic material, which includes pericarps and tips (and may include fine fibers) and contains less than about 15% protein, less than about 5% oil and less than about 4% starch, can be sent to a secondary alcohol system, as is known in the art, as a raw material without any additional treatment.
[0066] With continuous reference to Figure 4, the centering arising from the fiber / protein separation step 316, which includes residual fine fibers and ends with sizes from 30 microns to 300 microns and from 300 microns to 500 microns, as well as fine and gluten, passes to a stage of separation of the fine germs and fibers 317, in which the fine germs and fine fibers are removed from the gluten solution by a fine sieving device, such as a sieve with spatulas or pressure sieve with an opening size of about 45 microns. The fine germs and fine fibers are transported to a fine germ / fiber storage tank 318, where the pH of the fine germs / fibers is adjusted from about 8 to about 10.5 (or about 8 to about of 9.5), such as adding chemicals, for example, sodium hydroxide, calcium oxide, sodium carbonate, trisodium phosphate or the like, to help release more oil from the germs. In addition, enzymes that disrupt the cell wall, for example, protease or the like, and / or chemicals that also disrupt the cell wall, for example, sodium sulfite or the like, can be added here to help release more oil of the germs. Then, the germ / fiber mixture is subjected to a step of separating the fine fibers 319, in which the fine fibers are separated from the fine germs by a decanter, for example. The fine fibers are recombined to the vinasse from the distillation so that they can be again submitted to the fiber / protein separation step 316.
[0067] The centering arising from the separation stage of fine germs and fibers 317 and the excess flow arising from the separation stage of fine fibers 319 come together and pass to a stage of recovery / dehydration of the proteins 320, which it uses, for example , a decanter, a centrifuge with discharge piping or a disc decanter to recover fine germs and proteins (as well as used yeast). Alternatively, the excess flow from the step of separating the fine fibers 319 can be dehydrated using, for example, a decanter, a centrifuge with discharge pipe or a disc decanter and sent back to the germ crushing step 310 to extract more oil. The components from the recovery / dehydration step 320 are sent to a dryer 321 to produce a high quality gluten / germ / yeast mixture (protein flour) with about 60% gluten and about 40% germ / yeast . The excess flow from the protein dehydration step passes to an evaporator 324 to separate any oil from it and produce a highly concentrated syrup (more than 65% dry solids), which can be used, among other things, (a) as a nutrient for secondary production of alcohol, (b) as animal feed, (c) as fertilizer and / or (d) in anaerobic digestion to produce biogas.
[0068] In addition, it is possible to include an optional centrifugation step (not shown) to recover the xanthophyll content in the emulsion layer of the recovered oils, both before and after fermentation 311, and to mix it with the flour by-product. protein before drying the proteins in order to increase the quality of the feed. Sodium sulfite, sulfur dioxide and the like can be added to the wet protein mass, for example, in order to maintain more than 20 ppm of sulfur dioxide level, before sending it to the 321 protein dryer. sulfur dioxide prevents xanthophylls from decomposing in the 321 protein dryer. Excess flow from centrifuges can return to the oil storage tanks.
[0069] Referring now to Figure 4A, this illustrates a flow chart of a variation of the system and method 300 of Figure 4. In this system and method 300a, cellulosic material and gluten (protein) flour are removed before fermentation 311. The recovery of gluten flour before fermentation 311 reduces the loss of xanthophyll during fermentation 311 and the subsequent stages of distillation 315 and recovery of proteins 320. In addition, larger pericarp particles, such as about 1 mm around of 4 mm, can clog the heat exchangers used during fermentation 311. Therefore, removing the pericarp before fermentation 311 avoids these clogging problems and increases the fermentation capacity by about 15% compared to conventional processes.
[0070] As Figure 4A illustrates, after the germ / oil separation step 306, the liquefied starch solution, together with the granules, fibers and proteins, is subjected to the crushing step 310, followed by a separation step gluten / fibers 326 using a sieving device, such as a filtering centrifuge, to remove collagen fibers from it. The sieve openings are usually about 500 microns to capture sums of tips, pericarps, as well as fine fibers, but can range from about 300 microns to about 700 microns. The separated fibers are washed and, optionally, dried, as represented by number 328, to produce cellulose for the secondary production of alcohol. The resulting cellulosic material, which includes pericarps and tips and contains up to about 15% protein, up to about 5% oil and up to about 4% starch, can be sent to a secondary alcohol system as raw material. without any additional treatment.
[0071] The protein fraction of the center of the liquefied starch solution after the 326 gluten / fiber separation step can, as an option, be separated, as represented by the number 330, using a centrifuge, as a disc decanter, or a centrifugal combination with discharge pipe / decanter. The separated proteins are additionally subjected to a 332 washing step and produce high-quality protein flour with a desirable percentage of xanthophyll, that is, from about 0.221 g / kg (100 mg / lb) to about 0.442 g / kg (200 mg / lb), which can be further combined with separate residual proteins downstream, as we will discuss in detail below. Otherwise, the center of the liquefied starch solution meets the fine germ particles in the fermentation step 311. Also, as an option, the fine germ particles from the oil / germ separation step 309 can be further processed to separate and produce germ proteins before adding to the liquefied starch solution in fermentation step 311.
[0072] The rest of the process is substantially the same as in Figure 4, except that the gluten flour and fibers were recovered at the beginning of the process, before fermentation 311. More specifically, when the fibers are previously separated from proteins, from fine particles of germ and fine fibers, there is no separation step 316 (Figure 4). Instead, fine fibers and fine germs larger than 50 microns are separated from residual proteins (gluten) in the step of separating fine germs and fibers 317. Here, fine germs and fine fibers are separated using a device fine sifting, such as a sieve with spatulas or by pressure with an opening size of about 45 microns.
[0073] The fine germs and fibers are transported to the fine germs / fibers storage tank 318, where the pH of the fine germs / fibers is adjusted from about 8 to about 10.5 (or about 8 to about 9.5), such as adding chemicals, for example, sodium hydroxide, calcium oxide, sodium carbonate, trisodium phosphate or the like, to help release more oil from the germs. In addition, enzymes that disrupt the cell wall, for example, protease or the like, and / or chemicals that also disrupt the cell wall, for example, sodium sulfite or the like, can be added here to help release more oil of the germs. Then, the germ / fiber mixture is subjected to a step of separating the fine fibers 319, in which the fine fibers are separated from the fine germs by a decanter, for example. Then, the fine fibers can be combined with the separated fibers that have been washed and, optionally, dried, as represented by number 328, to produce cellulose for the secondary production of alcohol. In one example, fine fibers include less than 15% protein and 4% oil.
[0074] The centering from the step of separating fine germs and fibers 317, the excess flow from the step of separating fine fibers 319 and the excess flow from the optional previous step of washing gluten 332 come together and pass to a protein recovery / dehydration step 320, which uses, for example, a decanter, a discharge tube centrifuge or a disc decanter to recover fine germs and proteins (as well as used yeast). Alternatively, the excess flow from the fine fiber separation step 319 can be dehydrated using, for example, a decanter, a discharge tube centrifuge or a disc decanter and sent back to the germ crushing step 307 to extract more oil. The components from the recovery / dehydration step 320 are sent to dryer 321 and combined with the optionally separated gluten from the front end to produce a high quality gluten / germ / yeast mixture (protein flour) with about 60% gluten and about 40% germs / yeast. The excess flow from the protein dehydration step 320 passes to the evaporator 324 to separate any oil from it and produce the highly concentrated syrup (more than 65% dry solids), which can be used again, among other things, (a ) as a nutrient for the secondary production of alcohol, (b) as animal feed, (c) as fertilizer and / or (d) in anaerobic digestion to produce biogas.
[0075] Referring now to Figure 5, this illustrates a flowchart of another embodiment of a system and method 400 for separating high quality by-products from grains used in the production of alcohol. This 400 system and method, which substantially correspond to a dry milling ethanol production system and process, separates various by-products to produce, for example, dry distillery grains with low protein content (less than 20%) / low content oil (less than 8%), as for cattle and pigs, and high quality oil. For this purpose, in this specific process and method 400, first, the corn is subjected to a hammer mill 402, for example, which can be used to crush the corn in particle sizes below about 2.78 mm ( 7/64 in.) And help release oil from it. In one example, the particle size is 50 microns to 3 mm. Crushing helps to break the bonds between fibers, proteins, starch and germs. In another example, a fraction of germs, such as from a dry fractionation process, can replace the initially un-ground corn here. The crushed corn is mixed with water and sent to a 404 liquefaction step, which produces a solution of liquefied starch with a specific gravity of about 1.05 to 1.15 g / cm3. In the 404 liquefaction step, the starch begins to convert into a liquefied starch solution. Enzymes, such as alpha-amylase, can be added to the 404 liquefaction step. You can use any suitable liquefaction apparatus that is familiar in the art.
[0076] The flow from the 404 liquefaction step contains about 12.85 g / L (1 lb / bu) oil-free and about 19.27 g / L (1.5 lb / bu) of germ particles (size ranges from less than about 50 microns to about 1 mm), 12.85 g / L (1 lb / bu) of granules (size ranges from about 50 microns to about 1 mm) and 64, 25 g / L (5 lb / bu) of fibers (particle size ranges from about 50 microns to about 3 mm). This flow passes to a solid / liquid separation step 406, which uses any suitable filtering device, for example, a pre-concentrator, a sieve with spatulas, a pressure sieve, a fiber centrifuge or something like that, to separate the liquid material of the solid material. The sieve openings can vary from about 50 microns to about 500 microns and are selected to desirably separate the fibers, granules and germ particles from the liquid, which essentially includes the liquefied starch solution with low amounts of oil, free proteins (mainly gluten) and starch. In one example, the sieve openings are about 50 microns.
[0077] The liquid fraction passes to an oil / liquefied starch solution 408 separation step, in which the liquid fraction is subjected to a centrifuge, such as a disk centrifuge, to separate the oil before sending the starch solution liquefied to join the fraction of treated solids before fermentation, which we will discuss below. In the oil / liquefied starch solution 408 separation step, the liquefied starch solution is used as a heavy liquid medium to suspend the oil, the density of which is about 1.05 to 1.15 g / cm3. The oil recovered at this stage of the process has a much more desirable quality in terms of color and content of free fatty acids (from about 2% to about 5%) compared to the oil recovered downstream, more specifically the oil recovered after fermentation. More specifically, the oil recovered before fermentation is lighter and has a lower fatty acid content. Oil production can include 10.28 g / L (0.8 lb / bu) or more. In one example, oil production is from about 10.28 g / L (0.8 lb / bu) to about 12.85 g / L (1 lb / bu).
[0078] The fraction of separated solids from the solid / liquid separation step 406 is subjected to a size reduction step 410 using a crushing mill, pin mill or high pressure cooker, for example, to additionally break the connection between fibers, starch and proteins. As an option, various enzymes (and types of enzymes), such as glycoamylse, fungal, cellulose, cellobiose, protease and the like, can also be added to improve separation. Then, the fraction of treated solids from the 410 size reduction step and the liquefied starch solution from the oil / liquefied starch 408 separation step are combined. The liquefied starch solution, which now includes fibers , granules, germs and proteins, is subjected to a fermentation stage 412, followed by distillation 414. In the distillation tower, the fermented vinasse solution, which includes fibers, proteins and germ particles, is separated to produce alcohol. The fibers can be separated from the germ and protein (gluten) particles in a fiber / protein 416 separation step thanks to differences in particle sizes using a sieving device, such as a filtering centrifuge, to remove the fibers from them. The sieve openings are usually about 500 microns to capture sums of tips, pericarps, as well as fine fibers, but can range from about 300 microns to about 700 microns. The separated fibers are used to produce dry distillery grains with a low protein content (less than 20%) / low oil content (less than 8%).
[0079] If a low protein and oil content in the fibers is necessary or desired, they can be sent to a storage tank (not shown), for example, where their pH is adjusted from about 8 to about 10, 5 (or about 8 to about 9.5), such as adding chemicals, for example, sodium hydroxide, calcium oxide, sodium carbonate, trisodium phosphate or the like, to help release more oil of the germs. In addition, enzymes that disrupt the cell wall, for example, protease or the like, and / or chemicals that also disrupt the cell wall, for example, sodium sulfite or the like, can be added here to help release more oil of the germs. In one example, the fibers are kept in the tank for about 1 hour at a temperature of about 140 ° F to about 200 ° F (or from about 180 ° F to about 200 ° F). After that, the fibers can be subjected to a crushing step to release more oil and proteins from them. The fibers produced by these additional treatment steps produce much less oil (less than 2%) and protein (less than 10%) and can be used in secondary alcohol production.
[0080] The centering resulting from the fiber / protein separation step 416 goes on to a recovery / dehydration step of the 418 proteins, which uses, for example, a decanter, a centrifuge with a nozzle or a disc decanter to recover the fine and proteins (as well as the yeast used). These components are sent to a dryer 420 to produce a high quality gluten / germ / yeast mixture (protein flour) with about 60% gluten and about 40% germ / yeast. This system and method 400 provides a protein yield of 70.68 g / L (5.5 lb / bu) with a protein purity of about 45%. Alternatively, prior to the recovery / dehydration step of proteins 418, the centering from the fiber / protein separation step 416 can be sent to a germ / gluten separation step 422, in which the gluten germs are separated using, for example, a sifter with spatulas or by pressure. The germs are sent back to the crushing stage of the germs 410 to extract more oil. The gluten is sent to the 418 protein recovery / dehydration stage and then to the 420 protein dryer.
[0081] The excess flow from the dehydration step of proteins 418 passes to an evaporator 424 to separate any oil from it and produce syrup, which can be mixed with dry and dry distillery grains, as represented by the number 426, to produce grains of dry distillery with solubles with a low protein content (less than 20%) / low oil content (less than 8%), such as for cattle and pigs, especially dairy cattle. Dry soluble distillery grains contain less than about 20% protein, less than about 8% oil and less than 4% starch.
[0082] In addition, it is possible to include an optional centrifugation step (not shown) to recover the xanthophyll content in the emulsion layer of the recovered oils, both before and after fermentation 412, and mix it with the protein by-product before drying in order to increase the quality of the feed. Sodium sulfite, sulfur dioxide and the like can be added to the wet protein mass, for example, in order to maintain more than 20 ppm of sulfur dioxide level, before sending it to the 420 protein dryer. sulfur dioxide prevents the xanthophylls from decomposing in the 420 protein dryer. The excess flow from the centrifuges can return to the oil storage tanks. In addition, although not illustrated, it should be borne in mind that the fibers, proteins, fine germs and fine fibers of vinasse from distillation can be treated in the manner illustrated at the end of methods 300 and 400 of Figures 3 and 4.
[0083] Referring now to Figure 5A, this illustrates a flowchart of a variation of the system and method 400 of Figure 5. In this system and method 400a, the gluten flour is removed prior to fermentation 412. The recovery of the gluten before fermentation 412 reduces the loss of xanthophyll during fermentation 412 and the subsequent stages of distillation 414 and recovery of proteins 418.
[0084] As shown in Figure 5A, after the solid / liquid separation step 406, the liquid fraction passes to a separation stage of oil / liquefied starch / gluten solution 428, in which it is subjected to a disc centrifuge or decanter centrifuge. disc to separate the oil and gluten individually from the liquefied starch solution, which is sent to join the fraction of treated solids prior to fermentation 412. In the oil / liquefied starch / gluten 428 separation step, the liquefied starch solution as a heavy liquid medium to suspend and separate the oil, whose specific mass is about 0.9 to 0.92 g / cm3. The gluten is discharged in the form of a mass from separation step 428 and passes to a gluten washing step 430, followed by a gluten drying step 432, to produce high quality gluten flour with a desired percentage of xanthophyll, i.e., from about 0.221 g / kg (100 mg / lb) to about 0.442 g / kg (200 mg / lb).
[0085] The rest of the process is substantially the same as in Figure 5, except that the gluten flour was recovered at the beginning of the process, before fermentation 412. More specifically, the optional germ / gluten separation step 422 (Figure 5) , now, it becomes an optional dehydration step for germs 423, which uses, for example, a sifter with spatulas or pressure sifter to recover the fine germs. The germs are sent back to the crushing stage of the germs 410 to extract more oil. The centered material is sent to the 418 protein recovery / dehydration stage and then the recovered components are sent to the protein dryer 420. The resulting gluten / germ / yeast mixture (protein flour) contains a lower percentage of gluten. The excess flow from the protein recovery / dehydration step 418 still passes through the evaporator 424 to separate any oil from it and produce syrup, which can be mixed with dry distillery grains and dried to obtain dry distillery grains with low soluble solids. protein (less than 20%) / low oil content (less than 8%).
[0086] Referring now to Figure 5B, this illustrates a flow chart of a variation of the system and method 400 of Figure 5. In this system and method 400b, the fraction of treated solids from the size reduction step 410 is sent first to a storage tank 434 and then to a solid / liquid separation step 436 before combining it, in fermentation step 412, with the liquefied starch solution from the oil / solution separation step of liquefied starch 408.
[0087] More specifically, as illustrated in Figure 5B, the fraction of solids treated with cooking water is mixed in storage tank 434, where the connections between fibers, starch, proteins and oil from fine germs and fine fibers can be additionally broken. In addition, the pH of fine germs is adjusted from about 8 to about 10.5 (or about 8 to about 9.5), such as adding chemicals, for example, sodium hydroxide, sodium oxide calcium, sodium carbonate, trisodium phosphate or something like that, to help release oil from the germs. In addition, enzymes that disrupt the cell wall, for example, protease or the like, and / or chemicals that also disrupt the cell wall, for example, sodium sulfite or the like, can be added here to help release oil from germs. In one example, fine germs are kept in the tank for about 1 hour at a temperature of about 140 ° F to about 200 ° F (or from about 180 ° F to about 200 ° F).
[0088] After the storage tank 434, the paste is sent to the solid / liquid separation step 436, in which the solids and liquids are separated using, for example, a sieve with spatulas or by pressure. The size of the sieve openings is larger than in the sieves used in the 406 solid / liquid separation step. In one example, the openings range from about 100 microns to 400 mm. In another example, they are about 250 microns. The liquid center, which includes fine germ particles and fine fibers smaller than the size of the sieve openings, returns in order to mix with the milled grains after the hammer mill 402 and before the liquefaction step 404 to form a paste and for processing additional, such as to recover additional by-products. Then, the solid fraction from the solid / liquid separation step 436 and the liquefied starch solution from the oil / liquefied starch solution 408 are combined and subjected to fermentation step 412, followed by distillation 414. O The rest of the process is substantially the same as in Figure 5, including, optionally, sending the fine germs from the germ / gluten separation step 422 back to the germ crushing step 410 to extract more oil, which will additionally be submitted to the tank storage 434 and the solid / liquid separation step 436. With this system and method 400b, the oil production from the oil / liquefied starch solution separation step 408 is 12.85 g / L (1 lb / bu) or more. In one example, oil production is about 15.42 g / L (1.2 lb / bu) to about 17.99 g / L (1.4 lb / bu). In addition, it should be kept in mind that additional steps 434 and 436 can be implemented in the processes as shown in Figures 3 to 5A.
[0089] Therefore, an improved system and method is provided to separate high quality by-products, such as oil, collagen fibers and protein flour from grains used in the production of alcohol; These systems and methods represent an advance in relation to typical and other processes, in addition to overcoming the disadvantages of current systems and methods.
[0090] Although the present invention has been illustrated by describing various embodiments and although those embodiments have been described in considerable detail, the Applicant does not intend to restrict or limit in any way the scope of the claims attached to such details. For example, although the description of the various systems and methods in this document has focused on corn, almost any type of grain can be used, including, but not limited to, wheat, barley, sorghum, rye, rice, oats and the like. The use of any by-product is also contemplated, such as fiber proteins from the current wet corn milling processes or germ fractions or fiber from the current dry fractionation processes. Other advantages and modifications will be readily apparent to those skilled in the art. Therefore, the invention, in its broadest aspects, is not limited to specific details, representative apparatus and methods, or illustrated and described illustrative examples. Therefore, it is possible to diverge from these details without diverging, however, from the scope or the essence of the Applicant's general inventive concept.

权利要求:
Claims (7)
[0001]
1. Method for Frontal Separation of Oil By-Products from Grains Used in Alcohol Production Process, characterized by the fact that the method comprises: grinding the grains into grains particles to release oil from the grains; mixing the grain particles with a liquid to form a paste that includes starch, fiber, protein, germ and the oil released defining free oil in the paste; submit the liquefaction paste to provide a liquefied starch solution including sugars and free fiber, protein, germ and oil; separating solids including fiber and germ from liquefied starch solution including free oil and sugars; subsequently and before fermentation, separate the free oil from the liquefied starch solution to produce the oil by-product; and after separating the free oil from the liquefied starch solution, grout the liquefied starch solution including the sugars with the solids separated, then subjecting the mixture to fermentation to produce alcohol.
[0002]
2. Method for Frontal Separation of Oil By-Products from Grains Used in the Alcohol Production Process, according to Claim 1, characterized by the fact that the oil production is 10.28 g / L (0.8 lb / bu) to 12.85 g / L (1 lb / bu).
[0003]
3. Method for Frontal Separation of Oil By-Products from Grains Used in the Alcohol Production Process, according to Claim 1, characterized by the fact that separating the free oil from the liquefied starch solution further comprises separately separating the gluten and the oil free of the liquefied starch solution to produce the oil and a gluten by-product.
[0004]
4. Method for Frontal Separation of Oil By-Products from Grains Used in the Alcohol Production Process, according to Claim 1, characterized by the fact that it also grinds the solids separated from the liquefied starch solution to produce fine fiber and fine germ, separate the fine fiber and fine germ from the ground solids before fermentation and subject the fine fiber and fine germ to liquefaction with the ground grains used for the production of alcohol to provide the liquefied starch solution including fiber, protein, germ and free oil.
[0005]
5. Method for Frontal Separation of Oil By-Products from Grains Used in the Alcohol Production Process, according to Claim 4, characterized by the fact that it also comprises combining fine germ recovered after distillation with the separated solids, including fiber and germ of the liquefied starch solution and grind the solids separated from the liquefied starch solution and the fine germ recovered after distillation to produce the fine fiber and fine germ.
[0006]
6. Method for Frontal Separation of Oil By-Products from Grains Used in the Alcohol Production Process, according to Claim 1, characterized by the fact that the alcohol is ethanol.
[0007]
7. Method for Frontal Separation of Oil By-Products from Grains Used in the Alcohol Production Process, according to Claim 1, characterized by the fact that the grains include at least one of corn, wheat, barley, sorghum, rye , rice or oats.

类似技术:

---

公开号 | 公开日 | 专利标题

---

BR112013013552B1|2020-11-10|method for frontal separation of oil by-products from grains used in alcohol production process

---

US9388475B2|2016-07-12|Method of and system for producing oil and valuable byproducts from grains in dry milling systems with a back-end dewater milling unit

---

US11034987B2|2021-06-15|Systems and methods for producing a sugar stream

---

BR112013024366B1|2021-06-29|ALCOHOL PRODUCTION PROCESS

---

US20160222135A1|2016-08-04|System for and method of separating pure starch from grains for alcohol production using a dry mill process

---

EP3556222A1|2019-10-23|System and method for producing a sugar stream

---

US20210324489A1|2021-10-21|System and method for producing a sugar stream using membrane filtration

---

US20130288376A1|2013-10-31|System for and method of separating germ from grains used for alcohol production

---

BR102019006714A2|2020-02-04|system and method for producing sugar stream

---

EP3539394A1|2019-09-18|System and method for producing a sugar stream with front end oil separation

---

US20170166835A1|2017-06-15|Systems and Methods To Improve Co-Product Recovery From Grains And/Or Grain Components Used For Biochemical And/Or Biofuel Production Using Emulsion-Disrupting Agents

同族专利:

---

公开号 | 公开日

---

CA2819842C|2021-01-19|

---

US9732302B2|2017-08-15|

---

US20130236936A1|2013-09-12|

---

CN103347615A|2013-10-09|

---

WO2012075481A1|2012-06-07|

---

EP2646164A4|2015-10-07|

---

EP2646164A1|2013-10-09|

---

CN107034240A|2017-08-11|

---

CN103347615B|2017-04-12|

---

PL2646164T3|2020-01-31|

---

CA2819842A1|2012-06-07|

---

EP2646164B1|2019-08-07|

---

BR112013013552A2|2016-10-11|

引用文献:

---

公开号 | 申请日 | 公开日 | 申请人 | 专利标题

---

---

US2282797A|1939-12-22|1942-05-12|Musher Foundation Inc|Manufacture of cereal germ oil|

---

US3236740A|1961-05-26|1966-02-22|Grain Processing Corp|Process for producing starch and alcohol|

---

CA1012408A|1972-11-14|1977-06-21|Dieter Schwengers|Method for degreasing crushed highly starchy fatty vegetable material|

---

US3909288A|1973-11-05|1975-09-30|American Maize Prod Co|Process for recovery of starch and corn oil from corn|

---

US4126707A|1976-10-04|1978-11-21|Hart Edwin R|Method of processing grain|

---

US4181748A|1978-05-11|1980-01-01|Cpc International Inc.|Combined dry-wet milling process for refining corn|

---

US4501814A|1978-10-26|1985-02-26|The Amalgamated Sugar Company|Process for producing a high fructose sweetener, high protein meal, and cereal germ oils|

---

GB2074183B|1980-04-18|1983-10-05|Cpc International Inc|Process for obtaining corn oil from corn germs and corn oil thus obtained|

---

US4361651A|1980-07-18|1982-11-30|Keim Carroll R|Process for making fermentable sugars and high-protein products|

---

US6254914B1|1999-07-02|2001-07-03|The Board Of Trustees Of The University Of Illinois|Process for recovery of corn coarse fiber |

---

US20040028775A1|2000-06-28|2004-02-12|Olsen Hans Sejr|Process for providing a starch product, treating milled or grinded crop kernels with an aqueous solution with an acidiic protease activity|

---

US7297236B1|2001-06-30|2007-11-20|Icm, Inc.|Ethanol distillation process|

---

US6648978B2|2001-10-15|2003-11-18|A. E. Staley Manufacturing Co.|Membrane filtration for thickening and starch washing in corn wet milling|

---

US6962722B2|2001-12-04|2005-11-08|Dawley Larry J|High protein corn product production and use|

---

US20060057251A1|2001-12-04|2006-03-16|Larry Dawley|Mid-level protein distillers dried grains with solubles - production and use|

---

ITBO20020047A1|2002-01-30|2003-07-30|Mario Menegatto|METHOD AND PLANT FOR THE PROCESSING OF GRAINS|

---

ITBO20020148A1|2002-03-22|2003-09-22|Mario Menegatto|APPARATUS AND METHOD FOR GERM TRANSFORMATION|

---

US20040023349A1|2002-06-13|2004-02-05|Novozymes A/S|Processes for making ethanol|

---

WO2004007083A2|2002-07-16|2004-01-22|United States Filter Corporation|System and method of processing mixed-phase streams|

---

US20050255190A1|2002-07-23|2005-11-17|Mehra Suhas K|Method for processing cereal material|

---

EP2534961A1|2003-03-10|2012-12-19|POET Research, Inc.|Method for producing ethanol using raw starch|

---

US7488390B2|2003-03-25|2009-02-10|Langhauser Associates, Inc.|Corn and fiber refining|

---

US20040187863A1|2003-03-25|2004-09-30|Langhauser Associates Inc.|Biomilling and grain fractionation|

---

US7452425B1|2003-03-25|2008-11-18|Langhauser Associates, Inc.|Corn refining process|

---

US6899910B2|2003-06-12|2005-05-31|The United States Of America As Represented By The Secretary Of Agriculture|Processes for recovery of corn germ and optionally corn coarse fiber |

---

US20070014905A1|2003-06-30|2007-01-18|Purdue Research Foundation|Starchy material processed to produce one or more products comprising starch, ethanol, sugar syrup, oil, protein, fiber, gluten meal, and mixtures thereof|

---

CN1212377C|2003-08-22|2005-07-27|吉林省石油化工设计研究院|Improved wet method for producing fuel ethanol|

---

CN1950514B|2004-03-10|2010-05-05|布罗因联合公司|Methods and systems for producing ethanol using raw starch and fractionation|

---

WO2006004748A2|2004-06-25|2006-01-12|Grainvalue, Llc|Improved corn fractionation method|

---

WO2006017712A2|2004-08-05|2006-02-16|The Board Of Trustees Of The University Of Illinois|Corn oil and dextrose extraction apparatus and method|

---

US7601858B2|2004-08-17|2009-10-13|Gs Cleantech Corporation|Method of processing ethanol byproducts and related subsystems|

---

US8518467B2|2004-08-23|2013-08-27|Mississippi State University|Fiber separation from grain using elusieve process|

---

US7670633B2|2004-08-23|2010-03-02|The Board Of Trustees Of The University Of Illinois|Removal of fiber from grain products including distillers dried grains with solubles|

---

US7569671B2|2005-01-06|2009-08-04|The Board Of Trustees Of The University Of Illinois|Method and system for corn fractionation|

---

NZ562363A|2005-04-19|2011-02-25|Archer Daniels Midland Co|Process for the production of animal feed and ethanol and novel animal feed|

---

WO2007092131A2|2006-02-06|2007-08-16|Corn Value Products|Process for recovery and separation of grain pericarp from endosperm|

---

BRPI0707942A2|2006-02-16|2011-05-17|Gs Ind Design Inc|method and system for recovering oil from distillation residues|

---

US7524522B2|2006-08-18|2009-04-28|Mor Technology, Llc|Kernel fractionation system|

---

US7829680B1|2006-08-18|2010-11-09|ProGold Plus, Inc.|System and method for isolation of gluten as a co-product of ethanol production|

---

US7659098B2|2006-09-12|2010-02-09|Masahiro Yamamoto|Method of treating waste from alcohol production|

---

US20090017164A1|2007-02-13|2009-01-15|Renessen Llc|Fermentation process for the preparation of ethanol from a corn fraction having low oil content|

---

US20080026101A1|2007-06-14|2008-01-31|Gary Nickel|Food products|

---

WO2009015333A1|2007-07-25|2009-01-29|Archer-Daniels-Midland Company|Dry fractionation of corn|

---

US20090186136A1|2008-01-18|2009-07-23|Saponin Inc.|Process for seed and grain fractionation and recovery of bio-products|

---

WO2009134869A1|2008-04-29|2009-11-05|Icm, Inc.|Pretreatment of grain slurry with alpha-amylase and a hemicellulase blend prior to liquefaction|

---

US20090311397A1|2008-06-17|2009-12-17|Icm, Inc.|Process for edible protein extraction from corn germ|

---

EP2329033A4|2008-08-27|2012-05-16|Edeniq Inc|Materials and methods for converting biomass to biofuel|

---

CN101348816B|2008-09-13|2011-09-28|天明（沈阳）酒精有限公司|Use of low temperature boiling technology in alcohol production|

---

US20100166913A1|2008-12-19|2010-07-01|Stewart David A|Cellulosic ethanol distillers residues|

---

CN102307485B|2008-12-23|2013-11-06|波伊特研究股份有限公司|System for production of ethanol and co-products|

---

US9567612B2|2009-04-01|2017-02-14|Hui Wang|Corn degerming ethanol fermentation processes|

---

EP2729501A2|2011-07-07|2014-05-14|Life Technologies Corporation|Polymer particles, nucleic acid polymer particles and methods of making and using the same|CA2882246C|2012-08-13|2019-03-26|Lee Tech, Llc|Multi-zoned screening apparatus|

---

US9388475B2|2012-08-23|2016-07-12|Lee Tech Llc|Method of and system for producing oil and valuable byproducts from grains in dry milling systems with a back-end dewater milling unit|

---

US9376504B2|2012-09-17|2016-06-28|Icm, Inc.|Hybrid separation|

---

US9352326B2|2012-10-23|2016-05-31|Lee Tech Llc|Grind mill for dry mill industry|

---

US9695381B2|2012-11-26|2017-07-04|Lee Tech, Llc|Two stage high speed centrifuges in series used to recover oil and protein from a whole stillage in a dry mill process|

---

ITPD20130176A1|2013-06-25|2014-12-26|Menegatto & Menegatto Tecnologie S R L|PROCEDURE FOR SEPARATION OF COMPONENTS OF CORN AND WHEAT GERMS AND OIL SEEDS|

---

WO2015055562A1|2013-10-15|2015-04-23|Dsm Ip Assets B.V.|Method for preparing oil from grain material|

---

ITMI20131993A1|2013-11-28|2015-05-29|Ferruccio Beniamino Gilberti|EXTRACTION METHOD OF CELLULOSE, STARCH, SUGARS, PROTEINS AND VEGETABLE HORMONES FROM CORN PLANT|

---

US20160222135A1|2015-01-29|2016-08-04|Lee Tech LLC.|System for and method of separating pure starch from grains for alcohol production using a dry mill process|

---

US11166478B2|2016-06-20|2021-11-09|Lee Tech Llc|Method of making animal feeds from whole stillage|

---

US9777303B2|2015-07-23|2017-10-03|Fluid Quip Process Technologies, Llc|Systems and methods for producing a sugar stream|

---

US11220663B2|2015-10-23|2022-01-11|Fluid Quip Technologies, Llc|System and process for clarifying thin stillage|

---

WO2017223029A1|2016-06-21|2017-12-28|Cellulosic Ethanol Technologies, Llc|Process and system for separation of a starch rich flow|

---

US10400201B2|2016-08-19|2019-09-03|Kiwi Green Technologies, Llc|Method and structure for comprehensive utilization of co-products of alcohol production from grains|

---

CN106819357A|2017-01-23|2017-06-13|信阳山信生物食品科技有限公司|A kind of cereal chaff cake protein extraction process|

---

US20190284593A1|2018-03-15|2019-09-19|Fluid Quip Process Technologies, Llc|System and method for producing a sugar stream with front end oil separation|

---

US11053557B2|2018-03-15|2021-07-06|Fluid Quip Technologies, Llc|System and method for producing a sugar stream using membrane filtration|

---

US20190309377A1|2018-04-05|2019-10-10|Fluid Quip Process Technologies, Llc|System and method for producing a sugar stream|

---

US10480038B2|2018-04-19|2019-11-19|Fluid Quip Technologies, Llc|System and method for producing a sugar stream|

---

US10995351B1|2020-09-14|2021-05-04|Fluid Quip Technologies, Llc|System and method for producing a carbohydrate stream from a cellulosic feedstock|

法律状态:
2018-04-03| B06F| Objections, documents and/or translations needed after an examination request according art. 34 industrial property law|

---

2019-06-04| B06T| Formal requirements before examination|

---

2020-03-24| B06A| Notification to applicant to reply to the report for non-patentability or inadequacy of the application according art. 36 industrial patent law|

---

2020-08-04| B09A| Decision: intention to grant|

---

2020-11-10| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 05/12/2011, OBSERVADAS AS CONDICOES LEGAIS. |

优先权:

---

申请号 | 申请日 | 专利标题

---

US41942610P| true| 2010-12-03|2010-12-03|

---

US61/419,426|2010-12-03|

---

PCT/US2011/063228|WO2012075481A1|2010-12-03|2011-12-05|A system and method for separating high value by-products from grains used for alcohol production|

---