METHOD AND SYSTEM FOR PRODUCING VALUABLE OIL AND BY-PRODUCTS FROM GRAIN IN DRY GRINDING SYSTEMS WITH

专利摘要:
METHOD AND SYSTEM FOR PRODUCING VALUABLE OIL AND BY-PRODUCTS FROM GRAIN IN DRY GRINDING SYSTEMS WITH BACK-END DEHYDRATION GRINDING UNIT. A method and system for producing oil and valuable by-products from grain in a dry milling unit are disclosed. The method and system include a dehydration milling process after fermentation. Furthermore, the method and system are capable of producing oil without evaporation. Furthermore, the method and system includes one or more of the germ processing units, emulsion processing units, fiber processing units, high value protein production units and inorganic salt and glycerol production units, so that high-value by-products can be generated.
公开号:BR112015003793B1
申请号:R112015003793-3
申请日:2013-08-20
公开日:2021-09-08
发明作者:Chie Ying Lee
申请人:Lee Tech Llc；
IPC主号:

专利说明:

CROSS REFERENCE TO RELATED ORDERS
[0001] This application claims priority from US Provisional Patent Application No. of Serial 61/692 593, filed on August 23, 2012 and entitled "SYSTEM AND METHOD FOR SEPARATING OIL AND PROTEIN FROM GRAINS USED FOR ACOL PRODUCTION", and US patent application No. of Serial 61/822 053, filed on May 10, 2013 and entitled "SYSTEM AND METHOD FOR SEPARATING OIL AND PROTEIN FROM GRAIN USED FOR ALCOHOL PRODUCTION", which are hereby incorporated in their entirety by way of reference for all the purposes. FIELD OF INVENTION
[0002] The present invention relates to methods and apparatus for a dry milling alcohol production system. More specifically, the present invention relates to methods and systems for increasing alcohol, oil by-product and protein yields for dry milling ethanol plants. BACKGROUND OF THE INVENTION
[0003] Figure 1 is a wet grinding process for alcohol production. Figure 2 is a typical dry milling process with a back-end oil recovery system. Figure 3 is a typical dry milling process with a back-end oil and protein recovery system.
[0004] Conventional methods to produce alcohols from grain generally use two procedures. One of the procedures is triggered in a wet condition and the other is triggered in a dry condition, which are referred to as wet grinding process and dry grinding process, respectively. Wet mill corn processing plants convert corn kernels into several different co-products such as germs (for oil extraction), gluten feed (high animal fiber feed), gluten meal (high animal protein feed) and starch-based products such as ethanol, high fructose corn syrup and food) and industrial starch. Dry-mill ethanol plants convert corn into two products that include ethanol and soluble distillers grains. Wet distillers grains with soluble are referred to as DWGS if they are sold as wet animal feed. Distillery dried grains with soluble are referred to as DDGS if they are dried for use as animal feed.
[0005] In the typical dry milling process for ethanol production, one bushel of corn yields approximately 8.2 kg of DDGS in addition to approximately 10.3 liters of ethanol. These co-products provide an essential secondary income stream that offsets a portion of the total ethanol production costs. DDGS is typically sold as a low value animal feed although DDGS contains 11% oil and 33% protein. Some plants begin to modify the typical processes by separating the valuable oil and protein from the DDGS.
[0006] It is reported that there are about 40 mills using a back-end oil recovery system, one mill having a protein recovery system and one mill having a front milling device and an oil recovery system front. These improved processes have the same objective, which is to increase the mills' alcohol yield as well as recover valuable oil from the front-end process. Generally, a front-end process refers to steps and/or procedures that are performed before fermentation and a back-end processing refers to steps and procedures that are performed after fermentation.
[0007] The following are some typical wet grinding processes. Figure 1 is a flow diagram of a typical wet milled ethanol production process 100. Process 100 begins with an infusion 111, in which the corns, (corn seeds that contain mainly starch, fiber, protein and oil) are soaked for 24 to 48 hours in a solution of water and sulfur oxide to soften the seeds. for grinding. In infusion 111, the soluble components are leached into the infused water and the protein matrix and endosperm are loosened. Then, the infused corn, after infusion 11 with about 50% DS, is introduced into a determination grind 112 (first grind) in a grinding mill in which the corn is ground in a way that the seeds tear open. and releases the germ so as to obtain a heavy density slurry (from 8 to 9.5 Be) of the milled components, which is basically a starch slurry.
[0008] Then, germ separation 113 is performed by floating the germs and a hydro-cyclone is used to separate the germ from the rest of the slurry. Germs contain oil, which is inside the seed. Germs separated in a chain (separated as a germ by-product) contain some parts of starch, protein and fiber. The separated germs are sent to a 113A germ wash so that the starch and protein can be removed. The germ stream is then sent to a dryer. 1.134 to 1.361 kg (dry basis) of germs are generated per bushel (25.4 kg) of corn. Dry germs have about 50% oil content on a dry basis.
[0009] The slurry remaining from the germ separation 13, which is now devoid of germs containing fibers, gluten (eg protein) and starch, is subjected to fine grinding 14 (second grinding) in a fine grinding mill where the complete rupture of the endosperm occurs. The components of the endosperm (which include gluten and starch are released from the fiber).
[0010] Next, a fiber separation 115 is performed. In fiber separation 115, the slurry passes through a series of screens for separating fibers from starch and gluten. Fibers are washed clean of gluten and starch. Fiber separation 115 typically uses static pressure screens or rotating paddles mounted on a cylindrical screen (paddle screens). Even after washing, the fibers of a typical wet mill mill still contain 15%-20% starch. This starch can be sold with the fibers as animal feed. The remaining slurry, which is now defibered, is subjected to a gluten separation 116, in which centrifugations separate the starch from the gluten. The gluten stream (in 16A gluten filtering and drying) goes to a vacuum filter followed by a drying step in a dryer to produce gluten (protein) flour.
[0011] Then liquefaction/saccharification 117, fermentation 118, distillation/dehydration 119 are performed. In liquefaction/saccharification 117, the starch from the starch/gluten separation 116 passes through a jet cooker to start the process that converts starch to sugar. Jet cooking refers to a cooking process that is carried out at elevated temperatures and pressures. Elevated temperatures and pressures can vary widely. Typically, jet cooking takes place at a temperature of about 120° to 150°C and a pressure of about 8.4 kg/cm2 to 10.5 kg/cm2, although the temperature can be as low as about 104°C to 107°C when a pressure of about 8.4 kg/cm2 is used. Liquefaction occurs when the mixture or “pure” is kept at 90°C to 95°C. In this condition, alpha-amylase hydrolyzes gelatinized starch to maltodextrins and oligosaccharides (glucose sugar molecule chains) to produce a puree or liquefied slurry. The saccharification process is accomplished by cooling the liquefied puree to about 50°C and adding a commercially available enzyme known as glyco-amylase. Glycoamylase hydrolyzes maltodextrins and short chain oligosaccharides into single glucose sugar molecules to produce a liquified puree.
[0012] In fermentation 118, a common variety of yeast (crevasse Saccharomyces) is added to metabolize glucose sugars to ethanol and CO2. Upon completion, the fermented puree (“beer”) contains approximately 17% to 18% ethanol (volume/basis by volume). Following fermentation 18 there is distillation and dehydration 19 in which beer is pumped into distillation columns where it is brought to a boil in order to evaporate the ethanol. Ethanol vapor is compensated in the distillation columns, and liquid alcohol (ethanol, for example) exits the top of the distillation columns at a purity of about 95% (190 proof). Next, the 190 proof of ethanol passes through a molecular sieve dehydration column, which removes the remaining waste water from the ethanol so that a final product of essentially 100% ethanol is produced (199.5 proof) . This anhydrous ethanol is ready to be used for motor fuel purposes. The solids and some liquid that remain after the distillation go to evaporation 20 where the yeast can be recovered as a by-product. Yeast can optionally be recycled back to fermentation 18. In some embodiments, CO2 is recovered and sold as a commodity product. The “distillation product” produced after distillation and dehydration 19 in the wet milling process 10 is generally called “syrup”.
[0013] The wet milling process 100 is capable of producing a high quality starch product that can be converted to alcohol as well as separate germ, fiber and protein streams that can be sold as by-products to generate additional income streams. However, the wet grinding process is complicated and expensive, requiring high capital investment as well as high energy costs to run.
[0014] Since the capital costs of wet grinding mills are so prohibitive, some alcohol mills prefer to use a simple dry grinding process. Figure 2 is a digital of flows from a typical dry milling ethanol production process 200. As a general point of reference, the 200 dry mill ethanol process can be divided into a front-end and a back-end process. The part of process 200 that occurs before fermentation 223 is considered the "front-end" process, and the part of process 20 that occurs after fermentation 223 is considered the "back-end" process.
[0015] The front-end process of Process 200 begins with milling 221, in which whole corn seeds are passed through hydraulic hammers to be ground into a corn flour or fine powder. Screen openings in hydraulic hammers are typically of size 7, or about 2.70 mm, with the resulting particle distribution yielding a very wide spread and a bell-like curved particle size distribution, which includes sizes of particle as small as 45 microns and as large as 2-3 mm. The milled flour is mixed with water to produce a slurry, and a commercial enzyme called alpha-amylase (not shown) is added. This slurry is then heated to approximately 120°C for about 0.5 to three (3 minutes) in a pressurized jet cooking process so as to gelatinize (make soluble) the starch in the milled flour. It is noted that in some processes a jet cooker is not used and a longer retention time is used instead.
Milling 221 is followed by liquefaction 222, in which the milled flour is mixed with cooking water to produce a slurry, and a commercial enzyme called alpha-amylase is typically added. The pH is adjusted here to about 5.8 to 6 and the temperature is maintained between 50°C and 105°C so as to convert insoluble starch into the slurry to become a soluble starch. The stream after liquefaction 222 has a load detection circuit content of 30% dry solids (DS) with all components contained in corn seeds, including sugars, protein, fiber, starch, germ, grain and oil and salt. There are thus three types of solid bodies (fiber, germ and grain) with similar particle size distribution in the liquefaction flow.
[0017] Liquefaction 222 is followed by simultaneous saccharification and fermentation 223. This simultaneous process is referred to in the industry as Simultaneous Sacarification and Fermentation (SSF). In some commercial dry-mill ethanol processes, saccharification and fermentation take place separately (not shown). Each of individual saccharification and SSF can take as long as about 50 to 60 hours. In fermentation 223, sugar is converted to alcohol using a fermenter. Then, distillation and dehydration 224 are carried out, using an alembic to recover the alcohol.
[0018] In the back-end process of process 200, which follows the distillation and dehydration 224, the separation of fibers 225 (centrifugation of the "full distillation product" produced in the distillation and dehydration 224, so that the insoluble solid bodies (“wet cake”) can be separated from the liquid (“fine distillation product”)) and evaporation 227.
[0019] The “wet cake” of distillation and dehydration 224 includes fiber (by cap, tip, cap and fine fiber), grain, germ particles and some protein. Centrifuge liquid contains about 6% to 8% DS, which mainly contain oil, germs, fine fiber, fine grain, protein, soluble fermenter solid and corn ash. The full distillate in any plant that has 12 to 14% DS that is fed to preconcentration 228 from a first staged evaporator to concentrate the full distillate to 15 to 25% DS before being fed to the integral distillation product for fiber separation step 225.
[0020] In fiber separation 225, a centrifuge with decanter is used to divide the full distillation product into two streams (a cake stream and a liquid stream). Cake stream mainly contains fiber and protein, grain and germ particles. The liquid flux, which is commonly called a fine distillation product, contains insoluble solid (such as protein, germ and fine fiber) and soluble corn solid. Then the fine distillation product is split into two streams. One stream includes about 30% ~ 40% of stream that is recycled again (as a “retro-stabilized” stream) to be mixed with corn kernels in a slurry tank at the start of liquefaction 222. The other stream, which contains the rest of the flux (load sensing circuit 60 to 70% of the total flux) enters evaporators at evaporation 227 so as to boil off moisture, leaving a thick syrup which contains mostly fine solid (protein, germ and fine fiber) and soluble (dissolved) solids from fermentation (25% to 40% of dry solids).
[0021] The back-stabilized water is used as part of the cooking water of the liquefaction 222 to reduce fresh water consumption as well as energy and evaporation equipment costs.
[0022] The concentrated slurry from evaporation 227 can be subjected to back-end oil recovery 226, where the slurry can be centrifuged to separate the oil from the syrup. Recovered oil can be sold as a separate high value product. The oil yield is normally about 0.181 kg of corn with a high free fatty acid content. This oil yield only accounts for about ^ of the oil in corn. About half of the corn seed oil remains inside the germ after distillation 224, which cannot be separated in a typical dry milling process using centrifuges. Free fatty acids, which are produced when oil is held in the fermenter for approximately 50 hours, reduce the oil value.
[0023] Centrifuges (oil extraction) can only remove less than 50% oil from the syrup as the protein and oil make an emulsion, which cannot be satisfactorily separated. Although the addition of chemicals, such as an emulsion breaker, is able to improve separation efficiency to some degree, the chemicals are expensive and the DDGS product can be contaminated by the added chemicals. In some cases, heat is supplied or the feed temperature is raised in the centrifuge to break the emulsion, but the method affects the color and quality of the DDGS. In some other cases, alcohol is added to break the emulsion, which can also improve separation and increase oil yield. However, the addition of alcohol requires exploration-proof equipment and costly operations. All of these improvements only increase the oil yield from an average of 0.181 kg/(25.4 kg of corn) to about 0.772 kg/(25.4 kg of corn), although the “free” oil (extractable oil ) in the full distillation product is about 0.454 kg/(25.4 kg of corn). The main reason for having such low oil yield in the back-end of the typical method is that oil and protein emulsify during the entire dry milling process, which makes oil recovery difficult.
[0024] An oil and protein recovery process is developed by separating oil/protein which is area added to break this oil/protein emulsion from a full distillation product. As shown in process 300 of Figure 3, the front-end process is similar to the typical dry milling process. The process changes its procedures after fiber separation 225 (figure 2) from the back-end process. This oil/protein separation 31 can be added between fiber separation 25 and evaporation 27. Nozzle centrifuges, other types of disc centrifuges or decanters are commonly used for this case.
[0025] The fine distillation product from fiber separation 325 is fed to the oil/protein separation 331. The oil/protein emulsion is broken down at a higher G-force inside the centrifuge. Oil is in a light phase discharge (overflow) and protein is in a heavy phase discharge (underflow) because of the density difference between oil (0.9 g/ml) density and protein (1 .2 g/ml).
[0026] The light phase (overflow) from the oil/protein separation 331 is fed to evaporation 327 to be concentrated to contain 25%~40% DS (forming a semi-concentrated syrup). The semi-concentrate syrup is then sent to back-end oil recovery 26 to recover the oil in the back-end process. Light phase flux contains less protein, so it is less likely to form an oil/protein emulsion. The oil yield with this system can be as high as 0.454 kg/(25.4 kg of corn). The 326 backend oil recovery oil-free syrup can also be concentrated in an evaporator to a much higher syrup concentration as high as 60% DS. Low protein oil-free syrup can prevent dirt in the evaporator.
[0027] The underflow from the oil/protein 331 separation is sent to a protein dehydration 332 so that the protein can be recovered. Protein cake separated from protein dehydration 332, with a content that is less than 3% oil, is sent to protein 333 drying in a first instruction dryer in order to produce a high value protein flour, which has 50% protein. The 332 protein dehydration liquid is sent back to the front end as a back-set stream which is used as part of the cooking water in the 322 liquefaction.
[0028] All oil that is recovered from the back-end oil recovery system has poor quality, dark color and high fatty acid (about 15 to 20%), since the oil is in the fermenter for more than 50 hours. Back-end oil separation can also be difficult to perform as the oil and protein emulsify throughout the entire dry milling process. Every step of the entire dry milling process, such as pumping and separating, produces some oil/protein emulsion. In order to obtain good quality oil and avoid formation of oil/protein emulsion during the entire dry milling process, front-end oil recovery can be a good solution.
[0029] The three decanter stages that are used to recover oil from the liquefied starch stream in liquefaction are tested. But since the high viscosity in the liquefied starch solution plus most of the oil is still in germ form, the oil yield is typically low, at about 0.091 kg/(25.4 kg of corn). However, the quality of the oil is much better than the oil obtained from the backend which is much lighter in color with about 5-9% free fatty acid. SUMMARY OF THE INVENTION
[0030] An improved front-end oil recovery system is developed to improve oil yield as well as to increase alcohol yield. As shown in center hole 400 of Figure 7, the liquid/solid separation of two stages 442 and 444 is followed by a milling with two stage dehydration 443 and 445 in series respectively with the establishment of countercurrent, in which a part of the cooking water is added to holding tank 446 (such as from solid/liquid separation 449, for example) instead of addition to slurry tank 441.
[0031] In process 400, cooking water (from fiber separation 425) is mixed with a cake from the second dehydration mill 445 to form a mixture. The mixture is introduced into a third solid/liquid separation 449 to recover liquid that is about 7 to 10° Brix. The liquid from the solid/liquid separation 449 is mixed with the cake from the first dewatering mill 443 in holding tank 446 for about 4 to 6 hours. The contents of holding tank 446 are introduced into the second solid/liquid separation 444 to separate liquid from solid. The liquid separated in the second solid/liquid separation 444 is about 15 to 20 Brix, and is used as part of the cooking water so as to be mixed with corn grain from the hydraulic hammer 421, to be sent to the semi-slurry tank. 441 fluid with jet cooking. Using this counter-current washing device, the germ joint has about twice the retention time in holding tank 446, resulting in a much lower Brix liquefied starch solution (approximately 7 to 10 Brix in instead of 25 to 30 Brix). The germ that is soaked in a lower Brix environment and has double retention time in liquefaction can be softened more easily, so the germ can be broken down and can release the oil in the second dehydration grind 35. This washing step countercurrent 444A of process 400 also leads to intermediate sized germ particles from the second dehydration mill 445, which are recycled back to the first dehydration mill 443 so as to ensure that the germ particles are milled to become a pre-set size of the germ particles less than 150 microns) to release more oil. Furthermore, all solid grain/germ/fiber particles have a wide particle size range from less than 45 microns to as large as 2-3 mm. By softening the germ particle in a lower Brix solution with a longer holding tank time, the germ is much softer and easier to break down than the fibers. Therefore, the dehydrated milling process is capable of breaking down more germ particles than fibers. However, each dehydrated grind is only capable of reducing the germ particle size to about half its original size at best. For example, a 1,000 micron germ particle becomes about 600 microns on average after a dehydrated milling pass. In order for the germ particles to release oil, it is preferable that the germ particle size be less than 150 microns. Therefore, normally dehydrated mills of at least two/three stages in series are needed to release more oil from the germ particles.
[0032] The 444A backwash arrangement allows medium sized germs after the second dehydration grind 444 to be recycled back into the first dehydration grind 442 to break down the germ particles once more. The screen size openings in the first and second solid/liquid separations 442 and 444 are selected to obtain a predetermined degree of sizes so that the germ particles can be recycled back into the semi-slurry tank. fluid.
[0033] After the slurry tank 441, the mixture is sent to jet cooking, the second slurry tank or one or more holding tanks. Then, the slurry is sent to the first solid/liquid separation 442, so that the liquid is separated from the solid.
[0034] In solid/liquid separation 442, the liquid containing oil into small solid particles (germ, protein and fine fiber) in liquefied starch solution is sent to front-end oil recovery systems that include the separation of oil 447 and oil purification 448. The dehydrated solid stream (cake) in the solid/liquid separation 442, which contains mostly grain/germ/fiber, is sent to the first dehydration mill 443 to break down the solid particles (grain/germ/fiber) so that the starch and oil from the solid grain/germ/fiber particles are released. Then, the solid from the dehydration mill 443 is mixed with the liquid from the third solid/liquid separation 449 to be sent to holding tank 446. The back-stabilized liquid has only less than half of the total cooking water, so that the solid (grain/germ/fiber) is able to remain in the holding tank more than twice the typical hold time and at a much lower Brix. Solid grain/germ particles can be quickly and easily softened/broken so that the starch is liquefied and the oil is released from the germ particles. After holding tank 446, the slurry is sent to the second solid/liquid separation 444 to dehydrate/remove the water. The liquid from the solid/liquid separation 444 is recycled back into the slurry tank 441 with larger germ particles as part of the cooking water. The cake from the second solid/liquid separation 444 is sent to the second dehydration mill 445. The cake from the second dehydration mill 445 is then mixed with the back-stabilized water from the protein separation 425 for the solid/liquid separation 449. The liquid from the third solid/liquid separation 449 is sent to holding tank 446. The cake from the solid/liquid separation 449 is sent to the fermenter for fermentation 423.
[0035] The liquid from the first solid/liquid 442 separation that contains most of the oil in the front-end is sent to a front-end oil recovery system (eg, the 447AA oil recovery process) which includes oil separation 447 and oil purification 448. In oil separation 447, the three-stage nozzle centrifuge can be used to separate the small oil/emulsion germ particles from the liquefied starch solution. The light phase of the three-phase nozzle centrifuge (which contains most of the oil/emulsion/germ particles with a small amount of liquefied starch solution) is sent to a small three-phase separation centrifuge (decanter or disk centrifuge ) to polish and purify the oil in oil purification 448. The heavy phase and sub-flow/cake phase of either a 447 three-stage oil separation centrifuge or a 447 three-stage separation centrifuge of oil 448 are sent to fermentation 423 so that they are first converted to a sugar and then to an alcohol.
[0036] The “beer” from the fermentation that contains about 15% to 17% alcohol goes to the 424 distillation for alcohol recovery. The full distillation product from the bottom of the 424 distillation can be sent to a first staged evaporator for the 446A preconcentration of a normal concentration of 12% ~ 14% DS to 15% ~ 25% DS. The germs in the 446B germ removal are then separated using a germ cyclone to float any larger germs that are still in the full distillate. The use of the germ cyclone can increase the oil yield by about 0.0921 kg/(25.4 kg of corn) depending on the forward grinding system and the concentration of the concentrated full distillate and the operation of the germ cyclone of germ removal 446B. The germ free fiber stream discharged from the bottom of the germ cyclone or the integral still discharging from the bottom of the still is sent to a decanter centrifuge at fiber separation 425 to recover the fibers as DDG. The defibrated stream from the fiber separation decanter 425 is divided into two streams. One of the streams that contains 30% ~ 40% of the stream is used as a back-stabilized stream/water. The other stream consisting of 60% ~ 70% of the stream is sent to evaporation 427 to be concentrated to about 45% DS as a syrup by-product.
[0037] Oil recovery in a front-end system leads to obtaining a lower and lighter colored fatty acid oil (about 5 to 9%). Front-end oil yield is affected by the number of dehydration grinds on the front-end and the number of germ extraction systems on the back-end. With a dehydration grinding system, the oil yield is about 0.362/(25.4 kg corn) ~ 0.454 kg/(25.4 kg corn). With two dehydration mills in series, the oil yield is about 0.408 kg/(25.4 kg corn) ~ 0.499 kg/(25.4 kg corn). With an additional germ extraction system on the back end, the oil yield is about 0.454 kg/(25.4 kg of corn). Not all oil can be obtained in the front-end oil recovery system, as the germ particulate oil can only be released in less than half of the oil in the front-end process.
[0038] Process 400A of Figure 4A shows a dry milling process with front milling mill and front-end oil recovery system for oil production according to some embodiment of the present invention. The 400A process includes 445A dehydration milling and 449A solid/liquid separation in the back-end process to break down germ particles that completely absorb the water so that more oil can be released. The 445A Dehydration Mill and the 449A Solid/Liquid Separation is referred to as the “Backend Germ Particle Breaking Process”.
[0039] The germ particles in the liquefaction stage do not completely absorb water and are not easy to break down in dehydration milling. Since the germ particle size normally decreases by half after dehydration milling, more than half of the oil inside the corn seed is still retained inside the germ (protection of the oil droplets by a protein cell wall ) and is not released with forward dehydration milling.
[0040] The germ particles after 423A fermentation and 424A distillation completely absorb water and become easy to break down by the grinding mill. Therefore, the 400A process includes a 445A dehydration mill and a 449A solid/liquid separation in the back-end (after the 423A fermentation) to break down the germ particles so that more oil can be released.
[0041] In addition, more oils can be released from the germ particles in the back-end process by having an alcohol presented in the back-end, which acts as a solvent to extract more oil during 423A fermentation, 424A distillation or even the evaporation 427A. In some cases, more than half (60% ~ 70%) of the shredded stream is sent to 427A evaporation, so the oil in this stream cannot be recovered at the front end. Furthermore, if the corns that are used are old or are dried in a high temperature environment, the softening process of germ particles becomes very slow during the softening process in the holding tank. Therefore, in some embodiments more enzymes and a larger holding tank are used (in order to obtain a longer retention time to soften the germs).
[0042] The methods and apparatus for recovering corn oil according to some embodiments of the present invention are capable of generating an oil that has a yield of 0.635 kg/(25.4 kg of corn). The methods and systems disclosed here also provide valuable by-products such as white fiber (for secondary alcohol production and in the papermaking industry), high-value protein flour (gluten flour, spent yeast and germ protein), glycerol, organic plant food and dietary food with animal nutrients.
[0043] Some features of the systems according to some embodiments of the present invention are described below. Dehydration separation/recovery and milling processes are included in some systems, which facilitate the separation of the germ particles from the fiber and their breakdown so that the protein cell oil can be released to produce pure corn oil.
[0044] Figure 5A shows a 500A back-end oil recovery system that has a protein and white fiber recovery process. System 500A includes a liquid/solid separation 572, a dehydration mill 551A and a germ/fiber separation 552A. Likewise, Figure 6A shows a 600A front-end oil recovery system that has a protein and white fiber recovery process. The 600A system includes 672A liquid/solid separation and 652A germ/fiber separation processes. Processes 500A in Figure 5A and 600A in Figure 6 have advantageous features. For example, both 500A and 600A processes include a 553A/653A fiber purification to separate the protein and oil from the fiber so that pure white fibers can be produced for secondary alcohol production or the papermaking industry.
[0045] An oil emulsion and a protein blend are formed in an integral dry milling process, which affects oil yield and protein purity. In some modalities. An oil/protein emulsion breaking process is included so that oil yield and protein purity can be increased. In process 500 of Figure 5 and 500A of Figure 5A, for example, a backend oil recovery system contains an oil/protein pre-separation 555A, an oil/protein emulsion break 556A, an oil purification 554A, and a 547A syrup polish included to break the bonds between the oil and the protein by using a centrifugal force so that pure corn oil flours and higher protein are produced after the 523A fermentation. Likewise, in processes 600 of Figure 6 and 600A of Figure 6A, a front-end oil recovery system (647 oil recovery and 648 oil polish before fermentation 623) is included to break the bonds between the oil. and the protein using a centrifugal force so that pure corn oil flours and higher protein are produced. The 600 and 600A processes also include a 655/655A oil/protein pre-separation, a 656/656A oil/protein emulsion break and a 657/657A syrup polish in the back-end processes.
In some embodiments (processes 500 of Figure, 500A of Figure 5A, 600A of Figure 6 and 600A of Figure 6A), recovery of glycerol and inorganic salt, which is referred to as the Inorganic Process, is included. There is about 0.680/(25.4 kg of corn) of glycerin and 0.227 kg/(25.4 kg of corn) of inorganic salt (rich in potassium and phosphate) in the syrup. In some embodiments, a 658/658A glycerol recovery and a 659/659A inorganic salt recovery are included to separate/recover glycerol and inorganic salt (as food for organic plants) from the high concentration syrup.
[0047] Further details according to the embodiments of the present invention are described below. There are generally two ways to recover oil. One of the two processes includes recovering oil in a front-end system prior to fermentation, such as processes 600 in Figure 6 and 600A in Figure 6A. The other process includes a back-end oil recovery system, such as processes 500 in Figure 5 and process 500A in Figure 5A. The front-end oil recovery system is capable of providing higher oil quality (lighter color and lower FFA) and yields a higher % alcohol. However, the front-end oil recovery system receives a higher capital investment.
[0048] In contrast, the back-end oil recovery system has a lower oil quality (dark color and high FFA) and has a lower alcohol percentage yield. However, a lower capital investment is required for the back-end oil recovery system.
[0049] Four exemplary processes are disclosed, according to some modalities, which can be used individually, separated or combined in any way and any sequences in typical dry milling plants, so that valuable products such as oil can be produced , protein, white fiber, glycerin, inorganic salt and highly concentrated nutritious syrup with different qualities and quantities.
[0050] In the back-end oil recovery process 500 of Figure 5, an oil/protein emulsion break and a recovery of glycerin and inorganic salt and highly concentrated oil-free and protein-free syrup are included in the back process -end. The 500A back-end oil recovery process of Figure 5A includes all four processes, including (1) oil/protein emulsion breaking, (2) glycerin and inorganic salt recovery, (3) germ recovery and milling dehydration and (4) fiber purification in the back-end oil recovery system.
[0051] In the front-end oil recovery process, such as process 60 of Figure 6, oil/protein emulsion recovery and the recovery of glycerin and inorganic salt from the highly concentrated oil-free and protein-free syrup are included. in the front-end process. The 60A front-end recovery of Figure 6A includes all four processes, including (1) oil/protein emulsion breaking, (2) glycerin and inorganic salt recovery, (3) germ recovery and dehydration milling, and ( 4) fiber purification in the front-end oil recovery process.
[0052] Selective yields are disclosed below. Typically, a dry milling process is capable of having a yield of 7.076 kg/(25.4 kg corn) of DDGS. With the use of dry milling processes with a back-end oil recovery system according to some embodiments of the present invention, yields of 0.227 kg/(25.4 kg of corn) of oil and 6, 85 kg/(25.4 kg of corn) of DDGS. In addition, a back-end oil recovery system with oil/protein emulsion breakage, according to some modalities, is capable of yields of 0.362 kg/(25.4 kg of corn), 1.36 kg/ (25.4 kg of corn) of protein flour and 5.35 kg/(25.4 kg of corn) of DDGS. Furthermore, a back-end oil recovery system with separation of glycerin and organic salt, according to some modalities is capable of yields of 0.363 kg/(25.4 kg of corn) of oil, 1.36 kg /(25.4 kg of corn) of protein flour, 0.680 kg/(25.4 kg of corn) of glycerin, 0.227 kg/(25.4 kg of corn) of inorganic salt and 4.445 kg/(25.4 kg of corn) of DDGS. In addition, a back-end oil recovery system, with germ recovery and dehydration grinding, according to some modalities, is capable of yielding 0.454 kg/(25.4 kg of corn) of oil, 2.275 kg/(25.4 kg of corn) of protein flour, 0.680 kg/(25.4 kg of corn) of glycerin, 0.23 kg/(25.4 kg of corn) of inorganic salt, 3.45 kg /(25.4 kg of corn) of DDGS. In addition, a back-end oil recovery system with a fiber purification process according to some modalities has yields of 0.544 kg/(25.4 kg corn) oil, 2.721 kg/(25.4 kg of corn), 0.680 kg/(25.4 kg of corn) of glycerin, 1.361 kg/(25.4 kg of corn) of inorganic salt, 1.542 kg/(25.4 kg of corn) of syrup and 1.542 kg/ (25.4 kg of corn) of white fibers.
[0053] A front milling system of front oil recovery of a dry milling system and front oil recovery of a dry milling system according to some modalities, is capable of generating 0.227 kg/(25.4 kg of corn) of oil, 6,622 kg/(25.4 kg of corn) of DDGS and a 2% increase in alcohol yield. Furthermore, a prior milling system and prior oil recovery from a dry milling system with an emulsion break, according to some modalities, is capable of having yields of 0.454 kg/(25.4 kg of corn) of oil, 1.361 kg/(25.4 kg corn) protein flour, 5.039 kg/(25.4 kg corn) DDGS and a 2% increase in alcohol yield, In addition, a front milling system and forward oil recovery from a dry milling system with oil/protein emulsion breakage, according to some modalities, is capable of yields of 0.454 kg/(25.4 kg of corn) of oil, 1.361 kg /(25.4 kg of corn) of protein flour, 5.039 kg/(25.4 kg of corn) of DDGS and a 2% increase in alcohol yield. Furthermore, a front milling system and a front oil recovery system of a dry milling system, with a glycerin and inorganic salt separation process, according to some modalities, is capable of having yields of 0.453 kg / (25.4 kg of corn) of oil, 1.361 kg / (25.4 kg of corn) of protein flour, 0.680 kg / (25.4 kg of corn) of glycerin, 0.227 kg / (25.4 kg of corn) of inorganic salt, 4.128 kg/(25.4 kg of corn) of DDS and a 2% increase in oil yield. In addition, a front milling and front oil recovery system of a dry milling system, with germ recovery and dehydration milling, according to some modalities, is capable of yields of 0.544 kg/(25.4 kg of corn) of oil, 2.268 kg/(25.4 kg of corn) of protein flour, 0.680 kg/(25.4 kg of corn) of glycerin, 0.227 kg/(25.4 kg of corn) of salt inorganic, 3.13 kg/(25.4 kg of corn) of DDGS and a 2% increase in alcohol yield. Furthermore, a forward milling and forward oil recovery system of a dry milling system with fiber purification, according to some modalities, is capable of having yields of 0.635 kg/(25.4 kg of corn) of oil, 2.722 kg/(25.4 kg of corn) of protein flour, 0.680 kg/(25.4 kg of corn) of glycerin, 0.227 kg/(25.4 kg of corn) of inorganic salt, 1.13 kg /(25.4 kg of corn) of syrup and 1.361 kg/(25.4 kg of corn) of white fiber and a 3% increase in alcohol yield. In the following, some other aspects of the invention are disclosed.
[0054] In one aspect, a method for producing oil using a dry milling system comprises separating an integral distillate into a solid part and a liquid part after fermentation and grinding the solid part after separation to release oil from germs in grain seeds. In some embodiments, grinding comprises dehydration grinding. In other embodiments the oil is recovered in oil recovery after fermentation. In some other embodiments, the liquid portion contains protein, oil, soluble solid, or a combination thereof. In some embodiments, the method also comprises separation of oil and protein. In other embodiments, the oil and protein separation separates the liquid part into an oily part and a protein part. In some other embodiments, the method also comprises dehydrating fibers and proteins which generate DDG from the protein part. In some embodiments, the method also comprises recovering oil from the oily portion from the oil and protein separation. In other modalities, oil recovery is carried out without evaporation. In some other modes, oil recovery is carried out before evaporation. In some embodiments, the method also comprises generating syrup with a dry solids content higher than 60%. In other embodiments, the grain comprises corn. In some other embodiments, the oil comprises corn oil.
[0055] In another aspect, a method for producing oil that uses a dry grinding system, comprises releasing oil from germs by dehydrating grinding of the germs after fermentation and recovering the oil after fermentation. In some embodiments, the method also comprises grinding with a mechanical hammer prior to fermentation. In other embodiments, the method also comprises liquefaction prior to fermentation. In some other embodiments, the method also comprises separating solids and liquids after fermentation and before dehydration milling. And in some embodiments, the method also comprises dehydration of fibers and proteins after dehydration milling. In other embodiments, the dehydration of fibers and proteins will receive an input from both the dehydration mill and the separation of oil and protein. In some other embodiments, the method also comprises separating oil and protein. In some other embodiments, the method also comprises imparting an oil-containing stream from the oil and protein separation. In other modalities, oil recovery is carried out without evaporation after fermentation. In some other modes, oil recovery is carried out before evaporation.
[0056] In another aspect, a method for producing grain oil comprises separating oil and protein in the fine distillation product in an oil-rich stream and a protein-rich stream after fermentation, breaking the emulsion formed by oil and protein in the stream rich in oil and concentrate the oil in the oil rich stream of less than 2% to more than 20% oil.
[0057] In some other modalities the concentration is carried out using one or more three-phase disc centrifuges. In other embodiments, the disk centrifuge comprises a nozzle centrifuge, a disk decanter, or a combination thereof. In some other embodiments, the method also comprises purifying the oil using a three-stage centrifuge.
[0058] In another aspect, a method for separating proteins from a syrup comprises separating a light phase from a cake phase by the difference in density of a first syrup containing 10% ~ 40% dry solids, wherein the light phase contains an emulsion that has oil, proteins, and germ particles and where the cake phase contains proteins that include spent yeast and germ protein, generate a second oil-free, protein-free syrup and concentrate the second syrup to form a third syrup that contains 80% dry solids.
[0059] In some modalities, the concentration is carried out using one or more three-phase centrifuges. In other embodiments, the three-phase centrifuge or centrifuges comprise decanters, disk centrifuges, centrifuges with disk settlers, or a combination thereof. In some other embodiments, the proteins comprise spent yeast, germ protein, or a combination thereof.
[0060] In another aspect, a method for separating glycerin and inorganic salt from a high concentration syrup comprises obtaining glycerin and inorganic salt from a syrup containing 60% ~ 80% dry solids and forming animal feed with the syrup.
[0061] In another aspect, dry milling system comprises a germ crushing unit that couples with a fermentation unit and after the fermentation unit in a processing sequence and an oil recovery unit that couples with the germ crushing unit.
[0062] In some embodiments, the system also comprises an emulsion processing unit. In other embodiments, the emulsion processing unit comprises breaking down oil and protein emulsions. In other embodiments, the system also comprises a fiber processing unit. In some other embodiments, the fiber processing unit comprises a caustic treatment unit. In some embodiments, the fiber processing unit produces white fiber. In other embodiments, the system also comprises a glycerol recovery unit. In some other embodiments, the system also comprises an organic salt recovery unit. In some embodiments, the system also comprises a backwash system. In other embodiments, the oil recovery unit sits before the fermentation unit in a processing sequence. In some other embodiments, the oil recovery unit sits after the fermentation unit in a processing sequence. In some embodiments, the system also comprises one or more dehydration milling units prior to the fermentation unit. In other embodiments, the system also comprises several dehydration milling units coupled in series before the fermentation unit. In some other embodiments, the germ crushing unit comprises several crushing mills in series after the fermentation unit. BRIEF DESCRIPTION OF THE DRAWINGS
[0063] Modalities will now be described by way of examples, with reference to the attached drawings which are intended to be exemplary and not limiting. For all figures mentioned here, the same numbered elements refer to the same elements everywhere.
[0064] Figure 1 is a flow diagram of a wet milling process to produce ethanol and grain distilled with soluble.
[0065] Figure 2 is a flow diagram of a typical dry milling process for ethanol production and back-end oil recovery.
[0066] Figure 3 is a flow diagram of a typical dry milling process for ethanol production and back-end oil and protein recovery.
[0067] Figures 4 and 4A are flow diagrams of dry milling processes with forward crushing and forward oil recovery according to some embodiments of the present invention.
[0068] Figure 5 is a flow diagram of a dry milling process with back-end oil and protein recovery according to some embodiments of the present invention.
[0069] Figures 5A, 5B and 5C are flow diagrams of dry milling processes with back-end oil recovery, protein recovery and white fiber recovery according to some embodiments of the present invention.
[0070] Figure 6 is a flow diagram of a dry milling process with oil recovery and front-end protein recovery according to some embodiments of the present invention.
[0071] Figure 6A is a flow diagram of a dry milling process with oil recovery and front-end protein recovery, and white fiber recovery according to some embodiments of the present invention.
[0072] Figures 7 and 7A are flow diagrams of dry milling processes with back-end oil recovery and back-end milling according to some embodiments of the present invention.
[0073] Figures 8 and 8A are flow diagrams of dry milling processes with back-end milling processes and back-end oil recovery according to some embodiments of the present invention.
[0074] Figures 9 and 9A are flow diagrams of dry milling processes with various counter-current washes according to some embodiments of the present invention. DETAILED DESCRIPTION OF THE PREFERRED MODALITY
[0075] A typical dry milling alcohol plant produces only one by-product, which is called DDGS, which contains about 29% ~ 31% protein, 11% ~ 13% oil and 4% ~ 6% starch . The yield of DDGS is about 7.076 kg/(25.4 kg of corn) which has about 2.132 kg/(25.4 kg of corn) of protein, 0.907 kg/(25.4 kg of corn) of oil and 0.363 kg/(25.4 kg of corn) of starch. The DDGS generated in the typical milling plant has a low selling price, although it has a high protein and oil content. The low selling price of DDGS generated in the typical dry milling plant is due to the fact that too much fiber is found in the DDGS, which is only good as feed for animals like cows and not good for chicken or fish.
[0076] In some embodiments the processes or apparatus of the present invention are capable of separating the individual compounds/components in the DDGS in order to present themselves in a purer form and become a more valuable product, such as white fiber (less than 10 % protein, less than 3% oil and less than 2% starch) for secondary alcohol feed, raw material water resistant pulp in the paper manufacturing industry, protein flour (more than 45% protein, less than 3% oil and less than 2&% starch), corn oil, glycerin, inorganic salt and syrup (as a nutrient for animal feed). Some embodiments of the present invention separate the DDGS into five parts which include: (1) larger solid particles (which have particle sizes greater than 300 microns) which are a combination of fiber (by cap and tip-cap) bonded with some protein and starch, grain (fine fiber bound with protein) and germ particles, contained in an oil droplet protected by a protein cell wall inside the germ (The yield of larger solid particles is about 2.722 kg/(25.4 kg of corn) with a composition of 28% protein, 8% oil and 4% starch); (2) a protein part that mainly contains protein (gluten, spent yeast and germ particle) with some fine fibers, which is bound with starch and absorbs oil in the fine fiber, (the protein part is an insoluble solid that has a density of 1.1 and has a particle size ranging from 5 microns to 300 microns; the yield for the protein part is about 1.814 kg/(25.4 kg of corn) and the protein part has a composition of 45% protein, 5% oil and 2% starch); (3) a very fine germ paste and an oil/protein emulsion, which has a density of about 1 and a particle size of 1 µm sub-micron to 5 microns (very fine germ paste and oil/emulsion protein that has a yield of about 0.726 kg/(25.4 kg of corn) with a composition of 35% protein, 30% oil and 2% starch; (4) a soluble solid that contains inorganic salt in corn , sugar, fermentation by-products (such as lactic acid, glycerol) and acetic acid (yield is about 1.814 kg/(25.4 kg corn) with a composition of about 8% protein, 7% oil and 5% starch; (5) "free" oil, which is oil that can be recovered by a centrifuge (yield is about 0.454 kg/(25.4 kg of corn).
[0077] Next, four processes are disclosed according to some embodiments of the present invention. These processes can be added to typical dry milling processes/systems so that sharper separations between fibre, proteins and oil can be obtained and purer valuable products such as white fiber, proteins (gluten, spent yeast and germ) , oil, glycerin, inorganic salts and feed nutrient can be produced.
[0078] Process 500A of Figure 5A and process 600A of Figure 6A include milling processes with germ recovery/dehydration according to some embodiments of the present invention. The processes described above are capable of releasing and recovering more than 0.908 kg/(25.4 kg of corn) of germs in the full distillation product. The 500A and 600A processes include a solid/liquid separation 572A/672A, a dehydration mill 551/51A and a germ/fiber separation 552/652A so that the germs from the fibers can be separated and the germ particles can be separated. be broken down to release oil from the protein cells and produce pure corn oil.
[0079] In addition, process 500A of Figure 5A and process 600A of Figure 6A include fiber purification processes according to some modalities. The fiber can be purified to produce white fibers, which can be used in the production of secondary alcohol or be used in the papermaking industry. There is more than 20% protein and 8% oil bound with fiber in DDG. The inclusion of fiber purification 53 is able to separate the protein and oil from the fiber, so as to produce a pure white fiber for secondary alcohol production or in the paper manufacturing industry and also increase the oil and protein yield when Same time.
[0080] In addition, processes 500 of Figure 5, 500A of Figure 5A, 600A of Figure 6 and 600A of Figure 6A include processes of breaking down oil/protein emulsions in a total dry milling system, which is capable of increase oil yield and protein purity. In the back-end oil recovery system (oil recovery after fermentation), such as the 500 and 500A process, oil/protein 555/555A pre-separation, the breaking of oil/protein 556 emulsions are included. /556A, oil purification 554/554A and syrup polish 557/557A. The 556/556A oil/protein emulsion breaking and 554/554A oil purification processes in the backend are used to break the bonds between oil and protein using centrifugal force to produce corn oil can use and flours of protein. Likewise, in the front-end oil recovery system, such as 600 and 600A processes, 655/655A oil/protein pre-separation, breaking of oil/protein emulsions, 632 protein dehydration are included. /623A and the 657/657A syrup polish. 647/647A oil recovery and 648/648A oil polish on the front end are used to break the bonds between oil and protein using centrifugal force to produce pure corn oil and protein flours.
[0081] Furthermore, processes 500 of Figure 5, 500A of Figure 5A, 60 of Figure 6 and 600A of Figure 6A include processes for recovering glycerol and inorganic salt according to some embodiments of the present invention. There are about 0.680 kg/(25.4 kg of corn) of glycerin and 0.227 kg/(25.4 kg of corn) and inorganic salt in the syrup. The glycerol and inorganic salt recovery processes disclosed herein are capable of separating/recovering glycerol and inorganic salt (as organic plant feed) from high concentration syrup.
[0082] Further details of the exemplary modalities are described below. The embodiments disclosed herein primarily include a front crushing and front oil recovery system, such as processes 600 of Figure 6 and 600A of Figure 6A, and a back-end oil recovery system, such as processes 500 of Figure 5 and 500A of Figure 5a.
[0083] In some embodiments, process 500 includes breaking oil/protein emulsions 556, recovering glycerol 558 and recovering inorganic salt 559 from a concentrated syrup. The 500A process includes 556A oil/protein emulsion breaking, 558A glycerol recovery and 559A inorganic salt recovery, 552A germ/fiber separation, 551A dehydration milling and 553A fiber purification.
[0084] In some embodiments, process 600 (Figure 6) adds breaking oil/protein emulsions, forward milling and recovery of glycerol and inorganic salt stages, and forward oil recovery to a system that is described in process 400 (Figure 4). In some embodiments, the 600A process (Figure 6A) adds oil/protein emulsion breaking, glycerol and inorganic salt recovery, germ recovery/dehydration grinding and fiber purification in a forward grinding system to a system of process oil recovery 400 (Figure 4). The processes will be described in more detail in the following sections.
[0085] There is generally about 1.361 kg/(25.4 kg of corn) of gluten protein and 0.454 kg/(25.4 kg of corn) of germ protein in the corn seed. There is also about 0.363 kg/(25.4 kg of corn) of yeast protein from the fermentation. Thus there is a total of about 2.177 kg/(25.4 kg of corn) of total protein within the whole distillation product. A protein recovery process is capable of producing a protein flour with a protein purity of 50% by including oil/protein separation, protein dehydration and protein drying in addition to the processes that are performed in a protein recovery system. Typical dry milling. With the process described above, the protein yield is still only about 1.361 kg/(25.4 kg of corn) of protein meal at a protein content of about 50%, so that only 33% of protein inside the whole distillation product are recovered. Although there is about 0.907 kg/(25.4 kg of corn) in the corn seed, both the back-end oil recovery technique (such as process 20) and the front-end oil recovery system ( like process 40) are only able to have a yield of 0.226 kg/(25.4 kg of corn), which shows that only about 25% of oil is recovered.
[0086] In some embodiments, the processes of the present invention increase oil and protein yields by separating/recovering oil from germs and by separating/recovering oil and protein from fibers that are bound with protein and oil within the DDGS. In addition, some embodiments of the present invention increase fiber purity by separating/recovering protein and oil so that more valuable white fibers can be produced in place of DDGS.
[0087] Process 500 of Figure 5 is capable of a) increasing protein yield and purity as well as separating more valuable proteins (spent yeast and germ protein from gluten protein), b) increasing oil yield, c ) produce two other valuable by-products including glycerin and inorganic salt. Process 500 of Figure 5 includes the additional processes of solid/liquid separation 572, oil/protein pre-separation 555, breaking oil/protein emulsions 556, oil purification 554, and syrup polishing 557 when process 500 is compared to the dry milling process that is described in process 200 of Figure 2.
[0088] In process 500, the full distillation product from distillation 524 can be optionally pre-concentrated to pre-concentration 528, so that the solid content can be increased from about 13 DS to 15% ~ 25% DS before from sending the substance to solid/liquid separation 572 for separating the solid (mainly fiber, germ and grain) from the liquid (mainly protein, fine fiber, small germ particles, starch, oil and soluble solid).
[0089] The solid phase of this solid/liquid separation 572 of process 500 can be mixed with the sub-flow (protein rich stream without oil) of breaking down oil/protein emulsions 556 to form a mixing stream . Then the mix stream is sent to fiber/protein separation 525 so that 525 so that fibers and proteins can be removed to produce a DDG cake. The DDG cake can be mixed with the 527 evaporation syrup to produce DDGS as a by-product. The fine distillation product from the fiber/protein separation step 525 can be returned to the evaporation step 527 or the oil/protein pre-separation step 555 or the back-stabilized liquid.
[0090] The liquid phase of the solid/liquid separation 572 of process 500 can be optionally mixed with the fine distillation product of the fiber/protein separation 525, forming a mixture, which can be sent to the oil pre-separation /protein 555, so that the oil slurry and the protein slurry can be separated into two streams, which include an oil-rich stream and a protein-rich stream.
[0091] The oil and protein slurry in the 555 oil/protein pre-separation of the 500 process contain about 2% insoluble protein and 1% oil, which can be separated into two layers in a water tank. simple retention with several hours of retention times. The light layer (oil-rich flux) contains more oil (about 1.3% to 1.7% oil) and less protein (1.3% to 1.7%). The heavy phase (protein-rich flux), which contains less oil (0.3 to 0.7%) and more protein (2.3 to 2.7%), sits at the bottom of a settling tank. The heavy phase (protein rich flow) of oil/protein pre-separation 55 can be sent to the front-end with a back-stabilized flow, which is used as a part of the cooking water or can optionally be sent to protein dehydration 32 in order to produce a protein meal. The protein 32 dehydration overflow can be sent to the front-end as a back-stabilized stream that is used as part of the cooking water. The light phase (oil rich flow) of the oil/protein 555 separation can go to the breakdown of oil/protein 556 emulsion.
[0092] In some embodiments, the plant includes a large fine distillation retention tank so that a retention time greater than four hours can be used for this oil/protein 555 pre-separation of the 50 process. In some embodiments, an inclined plate settler is used to increase the separation area with a smaller holding/sedimentation tank. In some embodiments, a gas (air or CO2) in the form of fine bubbles is used to accelerate this oil/protein 555 pre-separation. Coagulated agents and commercial air flotation units are used in some embodiments.
[0093] In a typical dry milling process, the fine distillation product is typically split into two streams by a simple volume splitting process. Each of the streams contains the same concentration of oil (about 1% oil in the fine distillation product). About 30%~50% of flux is recycled again as cooking water in the slurry tank in order to cut fresh water usage and save evaporation energy. Another 50% ~ 60% of the flux is sent to an evaporator to be concentrated to about 30% ~ 40% DS as a syrup. Both streams have the same proportion of oil and protein content. Oil in syrup is not recovered unless another back-end oil recovery system is installed. The syrup also cannot be concentrated to be more than 40% DS, as too much of the protein in the solution can foul the evaporator.
[0094] In breaking the oil/protein emulsion 556 of process 550, higher speed disc centrifuges are used, such as a two- or three-stage nozzle centrifuge to break the bonds between oil and protein by the difference in density (oil is 0.9 gram/ml and protein is 1.15 gram/ml. All oil, oil/protein emulsion, germ particles (depending on the density of both liquid and germ particles) that are lighter than the liquid are separated from proteins and fine fibers.The liquid phase stream contains more oil, oil/protein emulsion, and the germ particles in the liquid stream are discharged from the breakdown of oil/protein emulsion 556. In oil/protein emulsion breakdown 556, the heavy phase stream (which contains more protein and fine fibers) that is heavier than the liquid is separated from the oil/emulsion/germ stream as heavy phase discharge stream. top layer of light liquid phase flux (about 30 to 70% liquid ido) contains mainly oil, oil/emulsion and fine germ particles. Liquid phase heavy flux (about 30 to 70% liquid) contains mostly proteins and fine fibers and sometimes with germ particles, depending on the size of the germs and the density of the liquid. Those skilled in the art will understand that the liquid split ratio can be any ratio from 5:95, 10:90, 30:70, 50:50 to 80:20.
[0095] The liquid phase of the oil/protein emulsion breakdown 556 contains about 30 to 70% of oil which is sent to oil purification 554 to produce pure corn oil. The heavy phase of the oil/protein emulsion breakdown 556 can optionally be sent to protein dehydration 532 for protein recovery or sent directly to evaporation 527 when protein dehydration 532 is not installed.
[0096] When using a three-stage decanter in breaking down oil/protein emulsion 556 of process 556, a three-stage disc decanter can be used. The cake phase of three-stage centrifuges/decanter may contain mostly corn gluten with some germs and spent yeast. The protein cake can be sent to a protein drier (not shown) to produce a protein flour (with 50% protein and less than 3% oil) or it can be sent to a DDGS drier in order to produce DDGS as a by-product.
[0097] When a three-stage nozzle centrifuge is used in breaking down the 556 oil/protein emulsion of the 550 process, the sub-flow is a heavy protein slurry rather than the cake. The heavy protein slurry is mixed with solid phase from solid/liquid separation 572 in fiber/protein separation decanter 525 to produce a DDG cake, which is then mixed with syrup to produce a by-product of DDGS. The overflow from the fiber/protein separation 525 can optionally be sent to the oil/protein emulsion break 556 to the front-end as a back-stabilized stream and/or to evaporation 527.
[0098] The heavy phase discharge of oil/protein emulsion breaking 556 and oil purification 554 of process 5005 with overflow from fiber/protein separation 525 can be optionally sent to evaporation 527 to be concentrated to about 20% to 40% total solid before the content is sent to Syrup Polish 557. The light phase flow of Syrup Polish 557 (which mainly contains emulsion and fine germ particles with high oil content (plus 30% of oil)) can go through any emulsion breaking process (such as using heat, chemicals or alcohol to break the emulsion) to recover more oil or is sent to a DDGS dryer to become part of the DDGS. The heavy phase stream of polishing syrup 55 (which contains mainly soluble corn solid and fermentation by-products such as glycerol) is sent to evaporation 527 to be concentrated to about 50% ~ 80% DS and so as to be produce syrup as a by-product. The 557 syrup polish cake sub-flow/flow contains mainly spent yeast and germ protein, which can be mixed with the protein cake (mostly gluten) from the 532 protein dehydration or optionally sold as high value protein flour. for fish. Alternatively, the underflow/cake from the syrup polish 557 is mixed with the fibercake that is received from the fiber/protein separation 525 to produce DDGS byproducts.
The oil-free and protein-free syrup from the syrup polish 557 of process 500 can also be concentrated to contain 80% DS since the protein (which scales in the evaporator) is removed. This high percentage of DS syrup with very high free oil and insoluble protein content is ideal for making organic plant food. Syrup polish 557 can be replaced several times during a series of evaporation processes in order to recover more protein and oil emulsion as long as the protein content in the syrup is kept low so that the viscosity of the syrup is kept low. and do not dirty the evaporator. The syrup can then be concentrated to be as high as 80% DS with a low/or lower oil and protein content. In one example, after the second stage evaporator (a second evaporation process) the syrup is fed to a centrifuge and generates a liquid phase and a protein cake. The liquid phase contains oil/emulsion/germ with 11.3% protein, 61.5% oil and 0.79% starch. The protein cake contains 38.9% protein, 0.85% oil and 2.79% starch. The separate oil-free and protein-free syrup has 22% DS. The syrup is then sent to a 527 third stage evaporation to remove more water, followed by the 557 syrup polish. The liquid phase contains 22.5% protein, 42.4% oil and 1.68% starch. The protein cake phase contains 31.4% protein, 0.14% oil and 4.08% starch. The oil-free, protein-free syrup has 29.7% DS.
[0100] The liquid phase of the 557 syrup polish contains oil, emulsion, small germ particles and cake (which mainly contains yeast and low oil germ protein). In some embodiments, a three-stage decanter or a disc centrifuge is used in syrup polishing 557, because of the high viscosity of the syrup which requires a much higher G-force (such as a disc decanter with a arrangement of two discs in a series design, which can be used to provide better separation). In some other embodiments, the 557 syrup polish uses a microfiltration apparatus. Light phase discharge (oil, emulsion, small germ paste) of 557 Syrup Polish contains 30% ~ 50% oil depending on syrup concentration and centrifuge operation. The oil is sent to the 556 emulsion breaker for emulsion breaking and further oil recovery.
[0101] Protein cake from protein dehydration 532 and syrup polish 557 of process 500, which contains less than 3% oil, can be combined to produce a highly valuable flour with high protein content (about 50% protein) or sold separately as gluten flour and yeast/germ protein.
[0102] After fiber/protein separation 525 from process 500, another factor that affects oil yield is how to effectively break the bonds between oil and protein in the syrup. Product content can be adjusted based on pre-determined factors and factory needs. Minimizing the oil in the syrup is selected when the dry milling plant only produces DDGS as a by-product. Minimizing the percentage of oil in both syrup and protein is selected when the dry milling plant produces both DDGS and protein flour. The breakdown of 556 oil/protein emulsions can be primarily to break the bonds between oil and protein and reduce oil loss in the syrup. Syrup 557 polish is primarily to reduce oil loss in both the syrup and the protein stream.
{0103] The oil-free, protein-free syrup after polishing syrup 557 can be concentrated to up to 80% DS without fouling the evaporator. The highly concentrated syrup (free of oil and protein) contains about 15% ~ 20% organic salt, 35% ~ 45% sugar (such as a sugar that remains without fermentation, maltose, glucose and fructose) and 35% ~ 45% fermentation by-products (such as lactic acid and glycerol) that can be recovered by going through glycerol recovery 558 and inorganic salt recovery 559 for glycerol recovery/removal and inorganic salt separation. Glycerol is a chemical in industry and inorganic salt can be used as food for organic plants. Vacuum distillation or a combination of micro-filtration and ultra-filtration can be used in the recovery of glycerol 558. Any liquid/solid separation apparatus, such as a decanter centrifuge with a cross-linked basin, can be used in the salt separation. Inorganic 559. Retaining the concentrated syrup in a cold place for a longer duration can help the inorganic salt crystal grow to a larger size and make the separation of inorganic salt 559 much easier.
[0104] The syrup, after glycerol recovery 558 and inorganic salt separation 559, mainly contains animal ripple material which is commonly called "unknown growth factor", which can be used as an animal dietary supplement or mixed with DDG fibers and be sold as DDGS. In some modalities, the syrup can also be recycled again at the front-end in order to increase the alcohol yield, since the sugar inside it can still be used in the production of additional alcohol.
[0105] The processes/steps described in process 500 are optional and all processes/steps can be run in different orders. Additional steps/processes can be added. In some embodiments, for example, the system does not include the separation of glycerol 558 when glycerin and inorganic salt will not be recovered. In another example, the system does not include syrup polishing 557, so the system can produce 1.361 kg/(25.4 kg corn) of gluten flour. In some other embodiments, oil/protein pre-separation, breaking of oil/protein emulsions 556 and oil purification 554 are included, so that the oil yield can be about 0.272 kg ~ 0.363 kg/ (25.4 kg of corn) With the addition of oil/protein pre-separation 555 or the breakdown of oil/protein emulsions 556 (with a back-end oil recovery system or with the 557 syrup polish) , the oil yield can be about 0.363 kg ~ 0.453kg/(25.4 kg of corn).
[0106] In some embodiments of the present invention, germ separation and dehydration milling (liquid/solid separation 572, dehydration milling 551 and germ/fiber separation 552) with fiber purification (purification of fibers 553) can also be included in process 550 of Figure 5 for germ and germ recovery from dehydration milling so that the protein cell wall can be broken down and thus the oil can be released. In addition, fiber purification 553 can be added to process 500 in order to produce white fiber.
[0107] In some embodiments, process 500A includes process 500 processes with liquid/solid separation 572A, dehydration milling 551A, germ/fiber separation 552 and additional fiber purification 553. The additional processes of the 500A process take place after the 523A fermentation and before the 525A fiber/protein separation. In the 500A process, the corns go through 521A hydraulic hammers, 522A liquefaction, 523A fermentation and 524A distillation and 528A pre-concentration, which are processes that are also included in the 500 process. The bottom layer of the 524A distillation (product full distillation) of the 500A process contains fiber and germ particles, corn protein, yeast and fermentation by-products, and corn ash. The full distillation product with 12% ~ 14% DS can be optionally passed through the first evaporator (the 528A preconcentration) to be concentrated to 15% ~ 25% DS. Then, the whole distillation product or concentrated whole distillation product is sent to liquid/solid separation 572A for separation of the solid (mainly fiber, germ and grain) from the liquid (mainly protein, fine germ and starch particles, oil, fine fiber and soluble solid).
[0108] The liquid phase from the 572A liquid/solid separation is sent to the 551A dehydration mill to break down the germ and grain particles and release the oil and starches. The solid phase from the 551A dehydration mill is mixed with the liquid phase from the 525A fiber/protein separation and sent to the 552A germ/fiber separation. The light phase of the 552A germ/fiber separation which mainly contains germ particles with liquid can be sent back to the front-end as part of the cooking water (back-stabilized flow). The heavy phase from the 552A germ/fiber separation is mixed with the sub-flow from the 556A oil/protein emulsion breakdown and sent to the 525A fiber/protein separation. The solid phase from the 525A fiber/protein separation is sent to the DDGS dryer to produce a DDGS by-product (not shown in the figure for clarity) or continuously passes through the 553A fiber purification to produce white fibers for the production of secondary oil or water resistant paste.
[0109] In some embodiments, the liquid phase from solid/liquid separation 572A is sent to oil/protein pre-separation 555A, then the remaining processes can be identical to process 500. For example, the slurry of Oil/Protein 555A can be split into two streams, which include an oil-rich stream and a protein-rich stream. The protein-rich stream with optional 532A protein dehydration can produce protein cake or it can be sent back to the front-end as a back-stabilized cooking water stream. The oil-rich flux can undergo breaking 556A oil/protein emulsions and purifying 554A oil to produce pure corn oil.
[0110] The heavy phase of oil/protein emulsion 556A and oil purification 554A can be sent to evaporation 527A to be concentrated to contain 20%~40% DS. The concentrated syrup is sent to the 557A Syrup Polish to recover emulsion/germ as a light phase, fine protein (spent yeast and germ protein) as a cake phase, and the oil-free and protein-free syrup as a heavy phase. The oil-free and protein-free syrup can be concentrated up to 80% DS. Then, separation of glycerol 558A (after evaporation 527A) is able to recover glycerol, followed by separation of inorganic salt 559A for recovery of the inorganic salt.
[0111] Germ recovery/dehydration milling ("germ process") in some embodiments of the present invention may include solid/liquid separation 572A, dehydration milling 551A and germ/fiber separation 552A.
[0112] Process 500B may be similar to process 500A. In some embodiments, the germ/fiber separation 552A is replaced by the solid/liquid separation in the 500B process. The process using the 575B solid/liquid separation in the 500B process has an oil yield of about 0.045 KG/(25.4 kg of corn) lower than the oil yield of the 500A process, since the separation of germs/fiber is not used.
[0113] Process 500C of Figure 5C shows modalities that have solid/liquid separation 572C, dehydration milling 551C and germ/fiber separation 552C that are set up differently than process 500A. The full distillation product can be sent to solid/liquid separation 572C. The solid phase can be sent to the 551C dehydration mill in order to release oil from the germs. In the 551C dehydration mill, the crushed solid is mixed with a liquid from the 525C fiber/protein separation and can be sent to the 552C germ/fiber separation. The light phase of the 552C germ/fiber separation which contains unbroken germ particles can be sent back to the 572C liquid/solid separation for separation of the germs from the liquid. Then, the germs separated in the solid/liquid separation 572C can go to the dehydration mill 551C one or more times, so that the germ particles can continue to be recycled again and for repeated grinding until the germ particles are smaller than the cell size aperture that is used in solid/liquid separation 572C. Then, the heavy phase from the 552C germ/fiber separation mixes with the sub-flow from the 556C oil/protein breakdown breakdown and is sent to the 525C fiber/protein separation to produce a DDG cake. The 525C fiber/protein separation liquid is sent back to be mixed with the crushed solid from the 551C dehydration mill, and the mixture is then sent to the 552C germ/fiber separation. In some embodiments, the 552C germ/fiber separation process is not included, and the crushed cake from the 551C dehydration mill can be mixed with the 556C oil/protein emulsion breaking down stream and sent to the fiber/ 525C protein in order to produce DDG cake and fine distillation.
[0114] The process 600A of Figure 6A shows some other processes of recovery/dehydration of germs according to some embodiments of the present invention. In the 600A process, the 652A germ/fiber separation occurs before the 6A72 solid/liquid separation and the germ is recycled in the front-end. In some other embodiments, the germ is crushed in the 643A dehydration mill. In some other embodiments, the germs are crushed to break the germs using a small grinding arrangement with high shear conical crushing.
[0115] In some embodiments, the inclusion of 651A back-end crushing milling is able to increase the oil yield by 0.091 kg/(25.4 kg of corn). Any screen separation apparatus, such as a pressure screen and a roller screen, can be used in the 672A solid/liquid separation. In some embodiments, a disk grinding mill (such as fluid device 36) can be used when dehydration grinding 651A is followed by germ/fiber separation 652A. In some other embodiments, the conical mill techniques can be used when the 652A germ/fiber separation is followed by the 651A dehydration mill (not shown). A hydro-cyclone (germ cyclone) can be used in the 652A germ/fiber separation and in conjunction with a classification design decanter used in the 625A fiber/protein separation for the recovery of more germs. However, the clarified decanter design can be used if more protein with fiber is required to be recovered. A multi-stage germ cyclone in series can be used when a higher oil yield is required.
[0116] The fiber from the 625A fiber/protein separation of the 600A process can contain 25% protein, 8% oil and 40% starch. The fiber can be sent to 653A fiber purification for white fiber production.
[0117] In some embodiments, the crushed cake from the 651A dehydration mill can bypass the 652A germ/fiber separation and the wash water is added to the washed protein, oil, and starch from the fiber using a series of processes. solid/liquid separation with a counter-current arrangement for white fiber production. An additional dehydration grind can be added to the above process.
[0118] In some embodiments, the pH is adjusted to be in the range of 7~9 during the purification of 653A fibers in order to speed up the purification process. In some embodiments, the 600A process is capable of generating 0.454 ~ 0.635 kg/(25.4 kg of corn) of oil, 1.814 kg/(25.4 kg of corn) of gluten flour, 0.907 kg/(25.4 kg of corn) of spent yeast and germ protein, 0.680 kg/(25.4 kg of corn) of glycerol and 0.226 kg/(25.4 kg of corn) of inorganic salt.
[0119] Some of the exemplary results are revealed below. Process 500, which has the oil/protein pre-separation process 550, the breaking of oil/protein emulsions 556, the oil purification 554 and the syrup polishing 557, is capable of producing 0.363 kg/(25, 4 kg of corn) of oil and 1,814 kg/(25.4 kg of corn) of protein. The 500A process (which has a 552A backend germ/fiber separation process, the 551A dehydration mill and the 553A fiber purification) is capable of producing 0.544 kg/(25.4 kg of corn) of oil (with a less ideal quality) on the back end, 2,722 kg/(25.4 kg of corn) of protein, a protein purity of 50% and about a 2% increase in alcohol yield.
[0120] The systems/processes described above, such as 50, 500A, 500B and 500C, mainly recover oil in the back-end, with production with less ideal quality oil (dark color and about 13% FFA). Process 400 in Figure 4 recovers oil at the front end, which can generate an oil that has a better quality (light color and about 7% FFA). However, the front-end oil recovery system has a lower oil yield (0.227 kg/(25.4 kg of corn)) which is lower than the oil yield (0.635 kg/(25.4 kg) of corn)) of oil yield (from the back-end oil recovery system, since, in the front-end oil recovery system, more than half of the oil is still trapped inside the germ and cannot be released during the liquefaction stage. Most of the oil is released in 423 fermentation and 424 distillation, as the alcohol in the fermenter acts as a solvent that is able to extract oil from the germ particles. temperature in the 424 distillation is able to “cook” the germ, so that the oil can be released.
[0121] In some modalities, the yield of the front-end oil recovery system can be increased by recovering the oil that is released during fermentation and distillation. The method to increase the oil yield includes a) sending the oily flow from the backend to the frontend and recovering oil using the frontend oil system; b) recover germs in the back-end and send the germs back to the front-end to be crushed one or more times in order to release the oil and recover the oil in the front-end oil recovery system; c) add the back-end dehydration grind 51 to release the oil from germs and then send the oil/protein emulsion back to the front-end for oil recovery in the front oil recovery system. Further details of the front-end oil recovery system according to some embodiments of the present invention are disclosed below.
[0122] The F6A 600A process is a front-end oil recovery system according to some embodiments of the present invention. After 641A jet cooking in the slurry tank, two solid/liquid separations 642A and 644A and 643A dehydration milling are performed with a 644A countercurrent arrangement, where the corn grain of a 621A hydraulic hammer is mixed with a liquid from the 644A solid/liquid separation in a 641A slurry tank so that the grain/germ particles can be broken down and the starch can be liquefied to release oil from the grains and germs. In some embodiments, a cross-current wash (a wash process is added at each stage/process/step, for example) is used in place of the counter-current wash. In some embodiments, a jet cooker is added to the 641A slurry tank. Partial liquefied starch slurry with about 30% ~ 35% DS from the 641A jet cooking slurry tank is sent to the first solid/liquid separation 642A. The liquid from the first 642A solid/liquid separation which contains most of the oil with some protein in the liquefied starch solution is sent to a 647A oil recovery (which includes oil separation) for recovery of the oil as a light phase. The light phase which mainly contains 10%~50% oil with some oil/emulsion/germ in the liquefied starch solution is sent to 648A oil polish so as to produce pure oil, which has light color and low fatty acid (about 5%~9% free fatty acid).
[0123] The 648A oil polishing subflow/cake discharge of the 60A process (in an oil polishing centrifuge) which mainly contains liquefied starch with solid (protein/fine fiber) is combined with the heavy phase and the sub -flow/cake from the 647A oil separation step to be sent to the fermenter for 623A fermentation. The 648A oil polish heavy phase discharge contains an emulsion/germ layer (a combination of oil, germ, protein and starch solution liquefied with some solid). In some embodiments, the emulsion (usually about 50% oil) in the heavy discharge is also broken down by passing through the 671A emulsion breaker so that more oil can be recovered. In some modalities, emulsion breaking can be done using an emulsion breaking technology, such as a) heating to a higher temperature (100°C to 130°C), b) addition of chemicals (breaker emulsions) or c) addition of an alcohol.
[0124] The 600A process 648A oil polish removes most of the oil in the light phase and protein solids in the cake phase. The heavy phase contains only emulsion. After passing through 648A oil polish, the emulsion volume is reduced to only 10%~30%. This small volume of emulsion is mixed with 200 proof alcohol to form a solution containing about 20% alcohol so that the emulsion can be broken down. The mixture is then sent to the fermenter for 623A fermentation and the oil can be recovered after 624A distillation using either the front-end or back-end oil recovery system.
[0125] In some embodiments, a disc centrifuge with a three-stage nozzle and/or other types of disc centrifuge are used in the recovery of 647A oil from the 600A process for separating the oil/emulsion layer from the liquefied solution. In some embodiments, 648A oil polishing is accomplished using a three-stage decanter or a three-stage disc centrifuge to separate pure oil from other substances (emulsion/germ layer and liquefied starch solution).
[0126] In some embodiments, the solid phase from the first solid/liquid separation 642A is introduced into the dehydration mill 643A to break up the germ and grain particles so that the starch can be released from the grain and the oil is released from the germ particles. The crushed solid, mixed with the cooking water, forms a very thick semi-fluid paste. The slurry is mixed with a fresh enzyme in order to lower the Brix (about 15 to 20 Brix) of the slurry in several holding tanks (2 or 3, for example) for about 3 to 6 hours at a predetermined liquefied temperature (about 180°F ). Then, slurry is sent to solid/liquid separation 644A for separation of liquid from solid. The liquid contains 15 to 20 Brix of liquid starch solution with some oil or protein, which is sent to a slurry tank as cooking water.
[0127] The solid from the 644A solid/liquid separation is mixed with the heavy phase and the sub-flow/cake phase discharge from the 647A oil recovery and the oil polish 48 to be sent to the fermenter in the 623A fermentation. In some embodiments, a caster screen (and other dewatering apparatus such as pressure screens and vibrating screens) is used in solid/liquid separation 642A and 644A. In the 643A dehydration mill, the germ and grain particles are broken down into smaller particles without breaking down the fiber. In some embodiments, the grinding uses a disk grinding mill in the 643A dehydration grinding. Those skilled in the art will understand that other crushing mills are applicable, such as pin mills. The starch in the grain and germ can be exposed to an enzyme and is liquefied before it is sent to the fermenter in 623A fermentation. The single dehydration milling stage with a backwash set up in the 600A process of Figure 6A is disclosed as an example. Those skilled in the art will understand that the front oil recovery system can have 2 or 3 stages of milling by crushing in series with or without a counter-current arrangement.
[0128] In some embodiments, a dehydration grind is used to cut the germ particles down to half their size. For example, a 1 mm germ particle can be reduced to about 500 to 600 microns after passing through a dewatering mill stage. In some embodiments, a 2 or 3 stage cordless dehydration mill is used to reduce the germ particles to smaller sizes and to extract more oil so that the highest oil yield can be obtained. Although the existence of several dehydration mills can have a higher oil yield, the related costs are also higher.
[0129] According to some embodiments, there are at least two ways to reduce the number of milling stages: a) mount a counter-current wash to recycle the medium-sized germ particles back to the forward dewatering mill; and b) add the germ extraction system in the front-end or back-end to recycle the germ particles in the forward milling stage. The proportion of oil that is released into the front-end mill can be affected by a) particle size, b) retention time in liquefaction, c) liquefaction conditions, temperature, type and proportion of enzyme used, and Brix. With the processes revealed above, the oil is released and extracted in fermentation. In addition, oil yield in the fermentation process can be affected a) by enzyme type and ratio, b) by fermenter conditions such as temperature, alcohol ratio/percentage and retention time, and c) by particle sizes . Therefore, by optimizing the above conditions, the oil yield can be increased.
[0130] After fermentation, distillation and fiber separation, the fiber can contain 9% ~ 11% oil without going through any forward mills, 6% to 9% oil when using a crushing mill, 3% to 6 % oil when two crushing mills are used in series and 1% to 3% oil when three crushing mills are used in series. The lower proportion of oil in the fiber reduces oil loss, so oil yield is increased.
[0131] After 623A fermentation and 624A distillation, the bottom layer of the distillation (full distillation product) contains fiber and germ particles, corn proteins, yeast and fermenter by-product, and corn ash. The full distillation product still has about 0.227 kg to 1.134 kg/(25.4 kg of corn) of germs and 1.814 kg to 2.268 kg/(25.4 kg of corn) of fiber. Both solids have the same particle sizes, ranging from less than 50 microns to over 1 mm.
[0132] Germ particles on the front end that do not completely absorb water are much harder and harder to break up using a crushing mill. The germ particles after fermentation and cooking in the bottom of a distillation apparatus completely absorb water and are much softer to be broken down by grinding mills. Therefore, in some embodiments the combination of germ cyclone and sorting decanter is used to separate the germs from the fiber in the back-end after distillation, and the germs are recycled back into the 643A dehydration mill in the front-end or in the mill. of 673A germs in the backend. In some modalities, two dehydration grinds are used (but not used in series in the front-end), including one in the front-end (first dehydration grind 643A) to increase the oil yield and another in the back-end ( 673A) germ grinding to increase oil yield.
[0133] In the 600A process of Figure 6A, the full distillation product from the 624A distillation goes to the 628A preconcentration in order to increase the solid concentration from 12% ~ 14% DS to 15% ~ 25% DS using a first evaporator. Then, the full distillation product is mixed with the overflow from the 625A fiber/protein separation and is sent to the 652A germ/fiber separation for separation of the germ particles from the fiber using density difference. In the 652A germ/fiber separation, the germ particles, (about 1 density) are lighter than the fiber (about 1.15 density) so the germ particles can be in the overflow stream from the top of the cyclone and the fiber is in the sub-flow of the cyclone bottom.
[0134} In some embodiments, the overflow from the 652A germ/fiber separation of the 600A process is sent to a 672A solid/liquid separation for germ particle recovery. The germ particles are then sent to the 643A dehydration mill on the front-end to be further broken down into smaller particles until the particles are smaller than the open screen size in the 642A solid/liquid separation. In some embodiments, the separated germs are sent to a high-shear crushing mill, such as the 673A conical crushing mill, before the germs are sent back to the front-end for front-end oil recovery.
[0135] In some embodiments, the 652A germ/fiber separation sub-flow is mixed with the 656A oil/protein emulsion breakdown sub-flow and goes to the 625A fiber/protein separation to produce DDG . In some embodiments, wash water 625A is added to the fiber/protein separation 625A to wash the protein from the fiber. Then, the protein-free fiber is sent to a 653A fiber purification in order to produce white fiber as a raw material for secondary alcohol production or for the papermaking industry. In some embodiments, purification of 653A fibers is not performed and the protein free fiber is used to produce DDGS. The 653A Fiber Purification Protein and Starch Wash Liquid can be recycled back into the front-end as part of the cooking water.
[0136] The oil recovery system such as back-end crushing mill, such as the 651A dehydrating mill is capable of increasing the oil yield by about 0.091 kg/(25.4 kg of corn). In some embodiments, the 672A solid/liquid separation utilizes screen type apparatus such as a roller screen and a pressure screen. In some embodiments, the 625A fiber/protein separation utilizes a decanter, a fiber centrifuge, a roller screen followed by a press, or a combination of these to remove/protein from the fiber. Filtrations such as the fiber centrifuge are able to separate fiber germs by particle size and backwash the fibers to recover more protein. Likewise, decanters are capable of classifying and separating the germs from the fibers by density.
[0137] The cake, (fiber part) of the centrifuge in solid/liquid separation 672A forms a by-product of DDGS. The 672A solid/liquid separation liquid is primarily a defibered protein solution, which is different from the fine distillation product of the decanter of a typical dry milling process. The defibrated protein solution from the solid/liquid separation 672A of the 600A process of Figure 6A contains 70% more protein in the full distillate, which has a much higher protein percentage compared to the fine distillate from the decanter. a typical dry milling plant (only 20 to 30% protein in the full distillates, for example).
[0138] In some embodiments, the defibrated protein and oil slurry from the 672A solid/liquid separation is sent to the 655A oil/protein pre-separation so that the oil/protein slurry can be separated into two streams. One of the streams is an oil-rich stream and the other stream is a protein-rich stream. The oil/protein slurry can contain about 2% insoluble protein and 1% oil, which can be separated into two layers using a simple holding tank with several hours of hold time. One of the two layers includes the light layer, which is an oil-rich flux that contains more oil (about 1.3% to 1.7% oil) and less protein (1.3% to 1.7%) in the top of the settling tank. The other layer is a heavy layer, which is a protein-rich stream that contains less oil (0.3% to 0.7%) and more protein (2.4% to 2.7%) at the bottom of the settling tank . In some embodiments, the heavy (protein-rich flow) layer of the 655A oil/protein pre-separation is sent to the breakdown of 656A oil/protein emulsions. The light layer (oil rich stream) from the 655A oil/protein separation is sent to the front-end as a back-stabilized stream, which is used as part of the cooking water. The heavy phase of the 656A oil/protein emulsion breakdown is sent to a 627A evaporator for evaporation with the option of being sent to 632A protein dehydration to produce a protein cake. Then, the overflow from the 632A protein dehydration is sent to the 627A evaporator for evaporation.
[0139] In some embodiments, three-stage centrifuges (such as decanter types to produce dry cake) are used in breaking down 656A oil/protein emulsions. The cake phase of the three-stage decanter or disk decanter can produce a protein cake without the dehydration of 632A protein. In some other embodiments, three-stage disc centrifuges are used. The underflow/sludge phase is capable of producing wet cake using 632A protein dehydration or by bringing the underflow back to 625A fiber/protein separation. In some embodiments, the light phase of the 656A oil/protein emulsion break is sent to the front-end so that the oil can be recovered using a front-end oil recovery system (the 647A and oil recovery 648A oil polishing, for example). In some embodiments, oil purification can be added, such as oil purification 654A is added after the oil/protein breakdown step 656A, as shown in process 500A of Figure 5A.
[0140] In some embodiments, a large fine distillation holding tank is used and more than four hours of hold time are used for the 655A oil/protein separation. In some embodiments, an inclined plate settler is used to increase the separation area with a smaller holding/sedimentation tank. In some embodiments, a gas (air or CO2) in the form of fine bubbles is added to accelerate the 655A oil/protein separation. In some other embodiments, a coagulating agent and a commercial air flotation unit are used.
[0141] In some embodiments, the breaking of 656A oil/protein emulsions uses high-speed centrifuges, such as a two- or three-stage nozzle centrifuge, to break the bonds between oil and protein by the difference in density (the oil is 0.9 gram/ml and protein is 1.15 gram/ml). In breaking down oil/protein 46 emulsions, the light phase flux (about 10%~30% liquid) mainly contains oil, oil/emulsion and fine germ particles. Heavy phase flux (about 50% ~ 80%) contains mostly white protein and fibers and sometimes with germ particles depending on germ size and liquid density. The sub-flow/cake phase stream mainly contains gluten flour (5% ~ 10%). The light phase of the 656A oil/protein emulsion breakage contains about 3% ~ 6% oil, which is sent back to the front end as a back-stabilized fluid. In some embodiments, the 654A oil purification is added to produce pure oil in the back-end, as shown in process 50A in Figure 5A.
[0142] In some embodiments, the heavy phase discharged from breaking 656A oil/protein emulsions is sent to an evaporator for 627A evaporation. The sub-flow/cake phase of the three-stage centrifuges contains mostly corn gluten with some germ and spent yeast. The proportion of germ and yeast spent in the sub-flow/cake stage is variable/controllable depending on the control of the operating conditions of the three-stage centrifuge.
[0146] In some embodiments, three-phase settlers or three-phase disc settlers are used in breaking down 656A oil/protein emulsions. The cake phase from the three-stage settlers can be sent to a drier in 632A protein dehydration in order to produce a protein flour (which has 50% protein and less than 3% oil). In some embodiments, the cake phase is mixed with DDGS to be a part of DDGS by-products.
[0144] In other modalities, three-phase disc centrifuges (Desludgr or nozzle centrifuge) are used in breaking down 656A oil/protein emulsions. The underflow of the three-stage disc centrifuge may contain a soapy cake. In some embodiments, 632A protein dehydration and/or 625A fiber/protein separation are used to further dehydrate the soapy cake prior to sending the cake to a dryer.
[0145] In some embodiments, the heavy phase discharged from breaking 656A oil/protein emulsions and the overflow from 632A protein dehydration are sent to an evaporator for 627A evaporation to be concentrated to have 20% ~ 40% of total solid before the heavy phase is sent to the 657A syrup polish.
[0146] Light phase flux of 657A syrup polish mainly contains emulsion and fine germ particles with a high oil content (plus 30% oil), which can go through various emulsion-breaking processes, such as heat, chemicals added alcohol to break the emulsion and recover more oil. In some embodiments the emulsion is sent to a DDGS dryer to become part of the DDGS.
[0147] The heavy liquid stream from the syrup polish 57 which mainly contains soluble corn solid and fermentation by-products such as glycerin, is sent to the evaporator for 627A evaporation so as to be concentrated to about 50% ~ 80 % DS and produce syrup as a by-product. The sub-flow/cake flow of the 657A syrup polish mainly contains germ particle and spent yeast, which can be mixed with a protein cake (mostly gluten) from the 632A protein dehydration. In some embodiments, the sub-flow/cake can be used to produce a high value fish protein meal. In some other embodiments, the sub-stream/cake is sent to be mixed with the fiber cake received from fiber separation 625A so as to produce a DDGS by-product.
[0148] In some embodiments, 657A syrup polish is used between multi-stage evaporation to separate small germ particles (more than 30% oil) from spent yeast and germ protein. The concentrated syrup (with a higher density) floats the lighter germ particles (because of the oil) to the top so that they join with the oil/emulsion layer and does not sink to the bottom (which has the yeast spent and the germ protein (heavier because of the low oil content)).
[0149] Dry milling according to some modalities may contain from three to six evaporators in series. The syrup generated by dry milling can have a concentration of about 4% DS to 40% DS or more. In some embodiments, the 657A syrup polish is operated with 20% DS syrup as a feed, which generates a higher protein yield with a higher oil content in the protein cake, resulting in an oil yield. lower. In some other embodiments, the 657A syrup polish is powered with 40% DS syrup as a feed, which generates a lower protein yield with a lower oil content in the protein cake, resulting in a yield of higher oil. In some embodiments, the oil-free, protein-free syrup is also concentrated to have up to 80% DS without creating an evaporator fouling problem. The high concentration oil-free and protein-free syrup can also be sent to 658A glycerol separation and 659A inorganic salt separation to recover the high value glycerin and inorganic salt.
[0150] The process 600A of Figure 6A is directed to a dry milling process with a front-end oil recovery system according to some embodiments of the present invention. The 600A process includes four beneficial features. These four features can be selectively added to a typical dry milling process to produce high quality by-products that are valuable in quantity. The four features include 653A fiber purification, 652A germ/fiber separation, 672A solid/liquid separation and 73 germ milling. 6% oil in the DDGS, process 600 in Figure 6 can be used.
[0151] Some exemplary results are revealed below. In some embodiments, the 600A process is capable of generating 0.653 kg/(25.4 kg of corn) of oil, 2.72 kg/(25.4 kg of corn) of protein flour, 0.680 kg/(25.4 kg of corn) of glycerin, 0.227 kg/(25.4 kg of corn) of inorganic salt, 1.113 kg/(25.4 kg of corn) of syrup and 1.361 kg/(25.4 kg of corn) of white fiber and 3% increase in alcohol yield. In some embodiments, the 600A process without 653A fiber purification is capable of generating 0.544 kg/(25.4 kg corn) oil, 2.49 kg/(25.4 kg corn) protein flour, 0.680 kg/(25.4 kg of corn) of glycerin, 0.227 kg/(25.4 kg of corn) of inorganic salt, 2.858 kg/(25.4 kg of corn) of DDGS and 3% increase in alcohol yield . In some embodiments, the 600A process without the glycerin 58 separation and the 659A inorganic salt separation is capable of generating 0.544 kg/(25.4 kg corn) oil, 2.49 kg/(25.4 kg corn) ) of protein flour, 3.719 kg/(25.4 kg of corn) of DDGS and 3% increase in alcohol yield. In some embodiments, the 600A process without germ/fiber separation 652A, solid/liquid separation 672A, and germ milling 673A is capable of generating 0.454 kg/(25.4 kg corn) of oil, 2.04 kg/(25.4 kg of corn) of protein flour, 9.6 lb/Bu of DDGS and 2% increase in oil yield. In some embodiments, the 600A process without the 657A syrup polish is capable of generating 0.363 kg/(25.4 kg corn) oil, 1.588 kg/(25.4 kg corn) protein function, 4.899 kg/ (25.4 kg of corn) of DDGS and 2% increase in alcohol yield. In some embodiments, the 600A process without breaking 656A oil/protein emulsions (with front-end crushing and a front-end recovery system) is capable of generating 0.227 kg/(25.4 kg of corn) of oil, 6.849 kg/(25.4 kg of corn) of DDGS and 2% increase in oil yield. In some embodiments, the 600A process without protein recovery and protein dehydration is capable of generating 0.227 kg/(25.4 kg corn) of oil, 6.622 kg/(25.4 kg of corn) of DDGS and 2 % increase in oil yield. In some embodiments, the 60A process without the front-end crushing and without the front-end oil recovery system is capable of generating 7,076 kg/(25.4 kg of corn) of DDGS.
[0152] Process 700 of Figure 7 shows a back-end oil recovery system with back-end crushing according to some embodiments of the present invention. In the 700 process, the germ particles that go through the 723 fermentation and the 724 distillation can completely absorb the water and become much easier to break down and release oil in the 775 dehydration mill in the backend.
[0153] Process 700 includes grinding with hydraulic hammers 721, a liquefaction 722, a fermentation 723, a distillation 724, a pre-concentration 728 and a solid/liquid separation 772 which are processes that are also included in process 500 of Figure 5.
[0154] The solid phase of solid/liquid separation 772, mainly contains larger solid particles such as fiber, germ and hard endosperm, which are sent to dehydration mill 775 to break down germ and grain particles and to release oil and starch . The liquid phase of the liquid/solid separation 772 contains mainly white fiber, protein solid and all soluble solids from the interior of the corn. The liquid is sent to the 756 Oil/Protein Breakdown Emulsions to be separated into a light phase (rich oil stream), a heavy phase, low oil and protein stream) and a sub stream (the highly concentrated protein stream). ) in a three-stage nozzle centrifuge (or other types of three-stage separation centrifuge). In some embodiments, the underflow from breaking 756 oil/protein emulsions is sent to protein dehydration 732 to recover protein prior to immission with the solid phase from dehydration mill 775. DDG 725 for recovery of the fiber and protein mixture as a solid phase (a by-product of DDG). DDG 725 recovery liquid which contains germ, germ protein and fine protein solid is sent back to the front-end as part of the back-stabilized fluid.
[0155] Light phase from breaking down oil/protein emulsions is sent to oil purification 754 for back-end oil recovery. The heavy phase of oil purification 754 and the breaking of oil/oil protein/protein 756 emulsions, which contain less oil and protein, is sent to an evaporator at evaporation 727. Then, the polishing of syrup 756 is carried out to recover the emulsion layer as a light phase and the germ/yeast protein layer as the solid phase, which is similar to the process described in process 500 of Figure 5. In some embodiments, the concentrated syrup is sent to glycerol recovery 758 and inorganic salt recovery 759, which is similar to the process described in process 500 of Figure 5.
[0156] In some embodiments, process 700 of Figure 7 contains a three-stage nozzle centrifuge, which is used in breaking down oil/protein 756 emulsions. In some other embodiments, process 70A of Figure 7A includes a centrifuge with Two-phase nozzle which is used in breaking down oil/protein emulsions 756. In the 700A process, the light phase (rich oil flow) is combined with the heavy phase (low oil and protein flow) of breaking oil emulsions /protein 756 and is sent to the evaporator for evaporation 727 to concentrate the solution to contain 25%-30% DS.
[0157] Next, the 757 syrup polish is used to recover germ/yeast protein in the solid phase, oil paste/emulsion/germ in the light phase and clear syrup (free of oil and protein) in the heavy phase. Clean syrup can also be concentrated to a value as high as 80% DS. In some embodiments, the clean syrup is sent to 758 glycerol recovery and 759 organic salt recovery. The light phase of the 757 syrup polish, which includes the oil/emulsion/germ paste, is sent to the front-end as part of a back-stabilized flow. In some embodiments, the germ paste is also treated to break down/extract emulsions (such as added alcohol) so that more oil can be recovered.
[0158] The underflow from the breakdown of 756 oil/protein emulsions, which contains mostly protein stream, is sent to the 732 protein dehydration for protein flour recovery. The overflow from protein dehydration 732 is mixed with the crushed cake from dehydration mill 775 and sent to a decanter (from fiber/protein separation 725) for fiber separation (DDG). In some embodiments, fiber is also purified in fiber purification 753 after dehydration milling 775 and backwashing with optional caustic treatment (such as a pH of 7~9) depends on the desired fiber purity.
[0159] In some embodiments, the breaking of oil/protein emulsions 556/556A/656/656A in 500, 500A, 600 and 600A processes use centrifuges with high-speed nozzles to break the bonds between oil and protein (with some fine fibers) and separate the solution into two streams, which include an oil-rich stream and a protein-rich stream. The “free oil” in the oil rich stream (from the oil/protein emulsion in a high speed centrifuge) can be recovered using either the front-end recovery system (such as 647A oil recovery and polishing of oil 648A from process 600A of Figure 6A) or back-end oil purification 754 (such as process 700 of Figure 7). In some modalities, the protein-rich flux produces a high-protein flour (more than 50% protein) while also undergoing protein dehydration 32.
[0160] The differences between the exemplary processes include the fact that the light phase (oil rich flow) of the 500 and 500A processes of the oil/protein 555 pre-separation is introduced in the breakdown of oil/protein 556 emulsions. In 600 and 600A processes, the heavy phase of the 655/655A oil/protein pre-separation is introduced into the breakdown of 656/656A oil/protein emulsions.
[0161] By the existence of oil/protein pre-separation, breaking of oil/protein emulsions, syrup polishing, glycerin separation, inorganic salt separation, back-end dehydration milling and purification of fibre, in some embodiment of the present invention valuable by-products such as oil, proteins (gluten, spent yeast and germ protein) white fibers and glycerol and organic plant foods can be generated. Those skilled in the art will understand that the above processes and systems can be selectively/optionally combined in any way and in any order.
[0162] Figures 8 and 8A are flow diagrams of dry grinding systems with back-end grinding processes and 800 and 800A back-end oil recovery according to some embodiments of the present invention.
[0163] In Figure 8, the full distillation product, after fermentation 804, is sent to solid/liquid separation 806. Optional intermediate processes of the preparation of 802 corn through fermentation 804 to solid/liquid separation 806 no are described here for the sake of brevity. In some embodiments, the solid/liquid separation 806 uses a rotating screen. The solid phase (which mainly contains fibers) from the solid/liquid separation 806 is sent to the dehydration mill 810. The liquid phase (which mainly contains protein, oil and soluble solid) is sent to the oil/protein separation 814.
[0164] In the 810 dehydration mill the germs are crushed so that the oil can be released from the germs. Advantageously, the process/system with the dehydration mill 810 is capable of producing more oil than typical dry mill systems since the germ particles in process 800 of the present invention completely absorb water in and before fermentation 804 Corn seed becomes soft and easy to break after fermentation 804, so more oil and germs can be released from the seed. In some modalities, the released oil is sent to the processes/apparatus for oil recovery in the back-end.
[0165] In some embodiments, the crushed mixture from the dehydration mill 810 is sent to the fiber/protein dehydration 812. In some embodiments, a decanter is used in the fiber/protein dehydration 802. In some embodiments, the solid from the dehydration of 812 fiber/protein is sent for DDG production. The fiber/protein dehydration liquid 812 can be used as a back-stable process/step flow that requires the addition of water.
[0166] In the separation of oil/protein 814, a stream of protein (gluten protein) can be sent to the dehydration of fibers/proteins 812. In some embodiments, the gluten produced in the separation of oil/protein 804 is sent to production of gluten flours. The oil/protein oily stream (which contains oil and fine protein) is sent to a back-end oil recovery apparatus for oil recovery. Advantageously, process 800 described above is capable of recovering oil in the back-end process without using any evaporator or evaporation steps. In some embodiments, Process 800 recovers oil without condensing/evaporating the oily stream to form the syrup from the oil/protein separation 814. In some embodiments, the oil/protein separation uses a two-three-nozzle centrifuge phases.
[0167] The 800A process of Figure 8A is similar to the 800 process. The 800A process can include the 800 process/steps. In addition, the oil stream from the 814A oil/protein separation can be sent to an evaporator for evaporation 816A. In 816A evaporation, a part of the 816B yeast protein/germ output, another part can be used for 816C oil recovery. And another part of the output contains highly concentrated 816D syrup (with 80% DS, for example) which can be processed in order to recover the glycerol and the inorganic salt.
[0168] Figure 9 shows a dry milling process with several countercurrent washes 900 according to some embodiments of the present invention.
[0169] Process 900 of Figure 1 includes a four-stage countercurrent wash 991A, 994A, 993A and 997A on the front-end. Each of the backwash arrangements is capable of lowering the Brix level to a predetermined degree. The first backwash arrangement 991A includes receiving crushed corn from the hammer 921 into a slurry tank 991. The output of slurry tank 991 is sent to the first solid/liquid separation 992 for separation of the slurry. liquid solid. The solid part is sent to fermentation 923 in a fermenter. The liquid part of the first solid/liquid separation is split into two streams. One of the streams from the first solid/liquid separation is sent back to slurry tank 991 forming the first backwash. The other stream from the first solid/liquid separation is sent to a first holding tank 993. The first holding tank 993 and the second solid/liquid separation 995 form the second countercurrent wash 993A.
[0170] In the second counter-current wash 993, the liquid from the second solid/liquid separation 995 is sent back to the first holding tank 993 so as to form a counter-current wash flow. The solid from the solid/liquid separation 993A is sent to the second holding tank 994.
[0171] In the third countercurrent wash 994A, the contents of the second holding tank 994 are sent to the third solid/liquid separation 996 after a predetermined period, such as a four hour period. The solid portion of the solid/liquid separation 996 is sent to a third holding tank 997 and the liquid portion is sent back to the second holding tank 994 as a backwash flow.
[0172] In the third backwash 997A, the third holding tank 997 receives solid from the third solid/liquid separation 996. The contents of the third holding tank 997 are mixed with a stream of cooking water. The mixture is sent to a fourth solid/liquid separation 998. The liquid from the solid/liquid separation 998 is sent back to holding tank 997 as a backwash flow. The solid from the fourth solid/liquid separation 998 is sent to fermentation 923.
[0173] With the various stages of backwash, the Brix degree in three holding tanks can be 15 ~ 20 Brix in the first holding tank, 7 ~ 15 Brix in the second holding tank and 2 ~ 6 Brix in the holding tank third holding tank. The countercurrent washing arrangement in the liquefaction stage with a lower Brix is able to prevent the formation of non-fermentable starch and increase the liquefaction efficiency. So that the liquefaction time can be shortened. The backwash can also be divided into three liquefaction zones, so that different types of enzyme, a different proportion of enzymes and different liquefaction conditions (such as temperature and pH) can be applied to the different liquefaction zones of in order to obtain an optimized result.
[0174] Backwash can also be used to increase the retention time of solids inside the three holding tanks. The number of stages of the backwash can vary. The back-end processes of process 90 of Figure 9 can be identical to process 70 of Figure 7 or 70A of Figure 7A.
[0175] Figure 9 shows processes 900A and 900B, which are processes derived from process 900 of Figure 9. Process 900A shows a process without the use of dehydration milling 975 of process 900. The solid from solid/liquid separation 972A is sent to DDG 925A oil recovery without using the dehydration mill 975 of Figure 9. The solid/liquid separation process 972A can receive an input of 928A (eg, similar to the 928 preconcentration of the 900 process) and output to 956A (e.g., similar to the breakdown of the 956 oil/protein emulsion of process 900). Process 90B shows another process that uses various solid/liquid separation processes to replace the dehydration mill 975 of process 900. The solid from solid/liquid separation 972B is sent to another solid/liquid separation 972C. The liquid from 972D solid/liquid 972C separation can be sent back to 972 or 972A as a backwash flow. Solid from solid/liquid separation 972C can be sent to DDG or white fiber 925B recovery. Various 925B liquid/solid separations, such as 1, 2, 5 and 10, can be used, depending on the purity of the white fiber that is predetermined.
[0176] Generally, throughout the present invention, the processes/steps that occur before fermentation are part of the front-end process and the processes/steps that occur after fermentation are part of the back-end process. Although the present invention has been illustrated by a description of several embodiments, and although these embodiments have been described in considerable detail, it is not the applicant's intention to restrict or limit in any way the scope of the claims appended to such details. For example, although the various systems and methods described here have focused on corn, virtually any type of grain, including but not limited to wheat, barley, sorghum, rye, rice, oats, and the like, can be used. The embodiments of the present invention can be used to produce white fiber for the papermaking industry and used as a feed stock for the production of secondary alcohol, clean sugar solution for the production of butanol, lysine and plastic.
[0177] When in use, the methods and apparatus disclosed here are able to improve oil yield and recover valuable by-products from corn. In operation, the fiber process, the germ process, the inorganic salt and glycerol recovery process and the oil emulsion process can be used either before or after fermentation. Advantageously, the methods and apparatus disclosed herein are capable of producing high quality corn oil and pure corn by-products.
[0178] Thus, the invention, under its broader aspects, is not limited, therefore, to specific details, to the representative equipment and method and to the illustrative example shown and described. Therefore, variations may be introduced in such details without departing from the spirit or scope of the applicant's general concept of invention.

权利要求:
Claims (28)
[0001]
1. Method for producing oil using a dry milling system characterized by comprising: a) separating an integral distillation product (806) into a solid and a liquid part after fermentation (804); and b) grinding the solid portion (810) after separation to release a first oil from the germs and release the starch from the grain into grain cores; and c) separating a second oil and protein (814) in the liquid part.
[0002]
2. Method according to claim 1, characterized in that the grinding comprises dehydration grinding (810).
[0003]
3. Method according to claim 2, characterized in that the first oil is recovered in oil recovery after fermentation.
[0004]
4. Method according to claim 1, characterized in that the liquid part contains the protein, the second oil, soluble solid or a combination of them.
[0005]
5. Method according to claim 1, characterized in that the separation of the second oil and the protein separates the liquid part into an oily part and a protein part.
[0006]
The method of claim 5, further comprising protein dehydration (932) which generates protein meal from the protein part.
[0007]
The method of claim 5, further comprising dehydrating fiber and protein (975) which generates DDG (925) from the protein part.
[0008]
The method of claim 7, further comprising recycling the overflow from the fiber/protein dehydration as part of a back-stabilized fluid (922).
[0009]
The method of claim 5, further comprising recovering the second oil from the oily portion of the oil and protein separation (814).
[0010]
10. Method according to claim 9, characterized in that the oil recovery is carried out without evaporation.
[0011]
11. Method according to claim 9, characterized in that the oil recovery is carried out before evaporation (927).
[0012]
A method according to claim 9, characterized in that it further comprises generating a syrup (816D) which has a dry solid content greater than 60%.
[0013]
13. Method according to claim 1, characterized by the fact that the grains comprise corn.
[0014]
14. Method according to claim 1, characterized in that the first or second oil comprises corn oil.
[0015]
15. A dry milling system characterized by comprising: a) a germ crushing unit (810) coupled with a fermentation unit (804) and after the fermentation unit in a processing sequence; and b) an oil recovery unit (814) coupled with the liquid and solid separation unit (806) after the fermentation unit.
[0016]
The system of claim 15, further comprising an emulsion processing unit (956).
[0017]
17. System according to claim 16, characterized in that the emulsion processing unit (956) comprises breaking down oil and protein emulsions.
[0018]
The system of claim 15, further comprising a fiber processing unit (925).
[0019]
19. System according to claim 18, characterized in that the fiber processing unit (925) comprises a caustic treatment unit.
[0020]
20. System according to claim 18, characterized in that the fiber processing unit (925) produces white fiber.
[0021]
The system of claim 15, further comprising a glycerol recovery unit (958).
[0022]
The system of claim 15, further comprising an inorganic salt recovery unit (959).
[0023]
The system of claim 15, further comprising a backwash system (922).
[0024]
24. System according to claim 15, characterized in that the oil recovery unit is before the fermentation unit in a processing sequence.
[0025]
25. System according to claim 15, characterized in that the oil recovery unit (816C) is located after the fermentation unit in a processing sequence.
[0026]
The system of claim 15, characterized in that it further comprises one or more dehydration milling units before the fermentation unit.
[0027]
A system according to claim 15, characterized in that it further comprises multiple dehydration milling units coupled in series before the fermentation unit.
[0028]
28. System according to claim 15, characterized in that the germ crushing unit comprises multiple crushing mills in series after the fermentation unit.

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同族专利:

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公开号 | 公开日

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CA2882173A1|2014-02-27|

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US20140053829A1|2014-02-27|

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BR112015003793A2|2019-12-17|

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US9388475B2|2016-07-12|

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WO2014031700A2|2014-02-27|

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WO2014031700A3|2014-05-08|

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CA2882173C|2020-08-04|

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法律状态:
2018-03-06| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|

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2018-03-13| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|

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2018-03-20| B06I| Publication of requirement cancelled [chapter 6.9 patent gazette]|Free format text: ANULADA A PUBLICACAO CODIGO 6.6.1 NA RPI NO 2462 DE 13/03/2018 POR TER SIDO INDEVIDA. |

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2018-03-27| B15K| Others concerning applications: alteration of classification|Ipc: C13K 13/00 (2006.01) |

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2019-07-23| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|

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2019-12-24| B15I| Others concerning applications: loss of priority|Free format text: PERDA DAS PRIORIDADES US 61/692,593, DE 23/08/2012, E US 61/822,053, DE 10/05/2013, PORAUSENCIA DE CUMPRIMENTO DA EXIGENCIA PUBLICADA NA RPI NO 2536, DE 13/08/2019, UMA VEZ QUENAO FOI APRESENTADA CESSAO ESPECIFICA PARA AS PRIORIDADES |

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2020-03-10| B12F| Other appeals [chapter 12.6 patent gazette]|

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2021-02-02| B06A| Patent application procedure suspended [chapter 6.1 patent gazette]|

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2021-06-22| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|

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2021-09-08| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 20/08/2013, OBSERVADAS AS CONDICOES LEGAIS. |

优先权:

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申请号 | 申请日 | 专利标题

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US201261692593P| true| 2012-08-23|2012-08-23|

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US61/692,593|2012-08-23|

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US201361822053P| true| 2013-05-10|2013-05-10|

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US61/822,053|2013-05-10|

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PCT/US2013/055881|WO2014031700A2|2012-08-23|2013-08-20|A method of and system for producing oil and valuable byproducts from grains in dry milling systems with a back-end dewater milling unit|

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