ALCOHOL PRODUCTION PROCESS

专利摘要:
processes for producing ethanol by dry milling and its production system a process and system for producing ethanol by dry milling, with a front-end milling method, is provided to improve the yield of alcohol and/or by-products, such as oil and/or protein yields. in one example, the process includes milling corn kernels into particles, then mixing the corn particles with a liquid to produce a paste, including oil, protein, starch, fiber, germ and grain. thereafter, the pulp is subjected to a front end milling method, which includes separating the pulp into a solids part, including fibers, grains and germ, and a liquid part, which includes oil, protein, starch and then , grind the separated solids part to reduce the germ and grain size and release bound starch, oil and protein from the solids part. Starch is converted to sugar and alcohol is produced from it, then recovered. in addition, the fiber can be separated and recovered. oil and protein can also be separated and recovered.
公开号:BR112013024366B1
申请号:R112013024366-0
申请日:2012-03-23
公开日:2021-06-29
发明作者:Chie Ying Lee
申请人:Lee Tech Llc；
IPC主号:

专利说明:

DESCRIPTIVE REPORT Reference to Related Orders
[001] This Application claims the benefit of United States Provisional Application No. 61/466,985, filed March 24, 2011, and United States Provisional Application No. 61/501.041, filed June 24, 2011, the descriptions of which are incorporated by reference herein in their entirety. Technical Field
[002] The present invention generally relates to dry milling alcohol production and more specifically to improved milling systems and methods for dry milling ethanol plants to increase alcohol and/or by-product productions. Background
[003] An alcohol of great interest today is ethanol. The majority of ethanol fuel in the United States is produced from a wet mill process or a dry mill ethanol process. Although virtually any type and quality of grain can be used to produce ethanol, the feedstock for these processes is typically corn.
[004] Conventional processes for the production of various types of grain alcohol generally follow similar procedures. Wet mill corn processing plants convert corn kernels into a number of different co-products, such as germ (for oil extraction), gluten feed (high fiber animal feed), gluten meal (high fiber animal feed). high protein content), and starch-based products such as ethanol, high fructose corn syrup, or industrial and food starch. Dry milling ethanol plants generally convert corn into two products, ie ethanol and distiller grains with solubles. If sold as wet animal feed, wet distiller grains with solubles are referred to as DWGS. If dried for animal feed, distiller dried grains with solubles are referred to as DDGS. In the standard dry mill ethanol process, a bushel of corn produces approximately 8.2 kg (approximately 17 lbs.) of DDGS in addition to approximately 10.5 liters (approximately 2.8 gal) of ethanol. This co-product provides a critical secondary yield stream that offsets a portion of the total ethanol production cost.
[005] With respect to the dry milling process, Figure 1 is a flowchart of a typical dry milling ethanol production process 10. As a general reference point, the dry milling ethanol process 10 can be divided at a front end and a rear end. The part of process 10 that takes place before distillation and dehydration 24 is considered the “front end”, and the part of process 10 that takes place after distillation and dehydration 24 (hereinafter “dehydration”) is considered the “rear end”. To that end, the front end of the process 10 begins with a milling step 12 in which dry whole corn kernels are passed through hammer mills for milling into flour or a fine powder. Screen openings in hammer mills are typically of a size 7/64, or about 2.78 mm, with a resulting particle distribution producing a very wide spread bell curve that includes particle sizes as small as 45 microns and as large as 2-3 mm.
[006] The milling step 12 is followed by a liquefaction step 16 in which the milled bran is mixed with cooking water to create a suspension and a commercial enzyme called alpha-amylase is typically added (not shown). The pH is adjusted here to about 5.8 to 6 and the temperature maintained between about 50°C to 105°C in order to convert the insoluble starch in the suspension to soluble starch. Several typical liquefaction processes, which take place in this liquefaction step 16, are also described in greater detail below. The stream after the liquefaction step 16 has about 30% dry solid content (DS) with all components contained in the corn kernels, including sugars, protein, fiber, starch, germ, grain, and oil and salts, by example. There are generally three types of solids in the liquefaction stream: fiber, germ, and grain, with all three solids having approximately the same particle size distribution.
[007] The liquefaction step 16 is followed by a simultaneous saccharification and fermentation step 18. This simultaneous step is referred to in the industry as "Simultaneous Saccharification and Fermentation" (SSF). In some conventional dry milling ethanol processes, saccharification and fermentation take place separately (not shown). Both individual saccharification and SSF can take around 50 to 60 hours. Fermentation converts sugar to alcohol using a fermenter. Subsequent to the saccharification and fermentation step 18 is the distillation (and dehydration) step 24, which uses a distillery to recover the alcohol.
[008] Finally, the rear end of process 10, which follows distillation 24, includes a centrifugation step 26, which involves centrifugation of the residues, i.e., "complete vinasse", produced with distillation step 24 to separate the insoluble solids (“wet mass”) of the liquid (“thin vinasse”). “Wet mass” includes fiber, of which there are three types: (1) pericarp, with average particle sizes typically from about 1 mm to 3 mm; (2) tricap, with average particle sizes of about 500 microns; (3) and fine fiber, with average particle sizes of about 250 microns. Centrifuge liquid contains about 6% to 8% DS.
[009] The fine vinasse enters the evaporators in an evaporation step 28 to evaporate the moisture, leaving a thick syrup that contains the soluble (dissolved) solids from the fermentation (25% to 40% dry solids). The concentrated suspension can be subjected to an optional oil recovery step 29 in which the suspension can be centrifuged to separate the oil from the syrup. Oil can be sold as a separate high value product. The oil product is typically about 0.4 lb./bu of corn with the high free fatty acid content. This oil product only recovers about / as much oil in corn. About half of the oil inside the corn kernel remains inside the germ after distillation step 24, which cannot be separated in the typical dry milling process using centrifuges. The free fatty acid content, which is created when the oil is kept in the fermenter for approximately 50 hours, reduces the value of the oil. The (de-oil) centrifuge only removes less than 50% because the protein and oil make an emulsion, which cannot be satisfactorily separated.
[0010] The syrup and centrifuged wet mass, which is more than 10% oil, can be blended and the mixture can be sold to dairy and beef cattle feedlots as Soluble Moist Grain Distillers (DWGS). Alternatively, the syrup can be mixed with the wet mass, then the concentrated syrup mixture can be dried in a drying step 30 and sold as Soluble Dry Grain Distillers (DDGS) for feedlots for beef cattle and milk. These DDGS have all the protein and 75% of the oil in corn. However, the DDGS value is low due to the high percentage of fiber, and in some cases oil is an obstacle to animal digestion.
[0011] Also with respect to liquefaction step 16, Figure 2 is a flowchart of several typical liquefaction processes that define liquefaction step 16 in the dry milling ethanol production process 10. Again, the front end of the process 10 starts with a milling step 12 in which the dry whole corn kernels are passed through hammer mills to mill bran or a fine powder. Milling step 12 is followed by liquefaction step 16, which alone includes multiple steps as will be described below.
[0012] Each of the various liquefaction processes generally starts with the ground bran being mixed with cooking, or in reverse, water, which can be sent from evaporation step 28 (Figure 1), to create a suspension in suspension tank 32 in the to which a commercial enzyme called alpha-amylase is typically added (not shown). The pH is adjusted here, as is known in the art, to about 5.8 to 6 and the temperature maintained between about 50°C to 105°C so as to allow enzyme activity to begin converting the insoluble starch into the suspension. for soluble starch.
[0013] After suspension tank 32, there are typically three optional pre-storage tank steps, identified in Figure 2 as systems A, B, and C, which can be selected depending generally on the desired storage time and temperature of suspension. With system A, the suspension from suspension tank 32 is subjected to a jet cooking step 34 in which the suspension is fed by a jet cooker, heated to 120°C, maintained in a U tube for about 5 to 30 minutes then forwarded to a flash tank. The jet cooker creates a shear force that breaks the starch granules to help the enzyme react with the starch inside the granule. With system B, the suspension is subjected to a secondary suspension tank step 36 in which steam is injected directly into the secondary suspension tank and the suspension is maintained at a temperature of about 90°C to 100°C during about 30 minutes to an hour. With system C, the suspension from suspension tank 32 is subjected to a secondary suspension tank - no steam stage 38, in which the suspension from suspension tank 32 is sent to a secondary suspension tank, without any steam injection , and maintained at a temperature of about 80°C to 90°C for 1 to 2 hours. Therefore, the suspension from each of systems A, B, and C is routed, in series, to the first and second storage tanks 40 and 42 for a total storage time of about 2 to 4 hours at temperatures of about from 80°C to 90°C to complete liquefaction step 16, which is then followed by saccharification and fermentation step 18, along with the remainder of process 10 of Figure 1. At the same time two holding tanks are shown here, it should be understood that one conservation tank or more than two conservation tanks can be used.
[0014] To increase alcohol production, and generate additional income, for example, from oil and/or protein productions in the typical dry milling process, it would be beneficial to develop a process(es) to further break down grain particles and initially ground germ particles, which mainly include starch, to release more starch, oil and/or protein from them. Such a process could provide increased alcohol, oil, and/or protein production, and produce much higher purity fiber (with less protein, starch, and oil), which can be used as a raw feed material for the food industry. paper and cellulosic for secondary alcohol processes.
[0015] Several dry milling systems have tried to increase alcohol yields, for example, focusing on the milling aspect in the dry milling process 10. However, such systems are known to have not produced very good results. For example, with the grinding systems on the market today, these systems tend to downsize on all particles (fiber, germ, and grain) at the same time and at the same rate. The resulting corn components can be difficult to separate, particularly if all the particles, including the fiber, are ground to very small sizes, eg less than 300 microns. While alcohol production can improve with smaller particle sizes, this can also produce a very wet decanter mass and dirty constant flow, i.e. dirty fine vinasse. And this dirty constant flow can create scale and result in lower syrup concentrations during evaporation step 28. Lower syrup concentrations and wetter masses also produce increased drier loads increasing DDGS drying costs. In contrast, if the resulting corn components are much larger in size, for example, greater than 1,000 microns, the particles will not adequately convert to sugar during liquefaction step 16 and the production of alcohol, for example, will decrease .
[0016] Such conventional systems also tend to focus either on grinding the entire stream or a partially separated stream into a very wet suspension form, without any dehydration prior to grinding. For solid particle grinding, the food that is sent to the grinding mill should be as dry as possible to produce maximum grinding results. Current systems will also fail to remove fine solid particle before feeding the particles to the cutting/grinding device. As such, the fine solid particles become smaller particles, i.e., very small, creating problems at the rear end of the process producing very wet masses and dirty excess, as described above.
[0017] It would thus be beneficial to provide an improved milling system and method for dry milling ethanol plants that can improve alcohol, oil and/or protein productions, and generate additional income from oil and/or productions protein, for example, while avoiding and/or overcoming the aforementioned disadvantages. summary
[0018] The present invention relates to improved milling systems and methods for dry milling ethanol plants to increase the production of alcohol and/or by-products. Such an improved milling system and method for dry milling ethanol plants can improve alcohol, oil and/or protein productions, and generate additional income from oil and/or protein productions.
[0019] In one embodiment, a dry milling ethanol production process is provided which includes milling the corn kernels into particles then mixing the corn particles with a liquid to produce a suspension including oil, protein, starch, fiber, germ, and grain. Therefore the suspension is subjected to an end milling method, which includes separating the suspension into a solid part, including fiber, grain and germ, and a liquid part, including oil, protein, and starch, then grinding the part. separated from solids to reduce germ and grain size and release bound starch, oil, and protein from the solids portion. Starch is converted to sugar, and alcohol is produced from it, then recovered. Furthermore, fiber can be separated and recovered, and oil and protein can be separated and recovered as well.
[0020] In another embodiment, a dry milling ethanol production process is provided which includes milling the corn kernels into corn particles, then mixing the corn particles with a liquid to form a suspension. Therefore, an amount of the liquid is reduced from the suspension to form a wet mass then the wet mass is milled. Alcohol, fiber, oil and protein can be separated and recovered in this process as well.
[0021] In yet another embodiment, a system for producing ethanol by dry milling is provided, which includes a milling device, which grinds the corn kernels into particles, and a suspension tank in which the corn particles mix with a liquid to produce a suspension including oil, protein, starch, fiber, germ and grain. The system also includes a first dehydration device, which separates the suspension into a solids part, including fiber, grain, and germ, and a liquid part, including oil, protein and starch. A size reduction device, which follows the first dehydration device, reduces the germ and grain size from the solids part and releases bound starch, oil and protein from the solids part. And at least one storage tank, which helps in converting starch to sugar, is provided. The system also includes a fermenter to produce alcohol from sugar and an alembic to recover the alcohol as well as a second dehydration device, which separates and recovers the fiber. Brief Description of Drawings
[0022] The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and, with a detailed description of the embodiments given below, serve to explain the principles of the invention.
[0023] FIG. 1 is a flowchart of a typical dry milling ethanol production process;
[0024] FIG. 2 is a flowchart of several typical liquefaction processes that define the liquefaction step in a dry milling ethanol production process;
[0025] FIG. 3 is a flowchart showing a dry milling ethanol production system and process with a front end milling method in accordance with an embodiment of the invention;
[0026] FIG. 3A is a simplified flowchart of the dry milling ethanol production system and process of Figure 3;
[0027] FIGS. 3B-3D are simplified flowcharts showing a variation of the dry milling ethanol production system and process with the front end milling method of Figure 3A in accordance with embodiments of the invention;
[0028] FIG. 4 is a flowchart showing a dry milling ethanol production system and process with the front end milling method in accordance with another embodiment of the invention;
[0029] FIG. 5 is a flowchart showing a dry milling ethanol production system and process with front end milling method in accordance with another embodiment of the invention;
[0030] FIG. 6 is a flowchart showing a dry milling ethanol production system and process with a front end milling method in accordance with another embodiment of the invention;
[0031] FIG. 7 is a flowchart showing a dry milling ethanol production system and process with the front end milling method in accordance with another embodiment of the invention;
[0032] FIG. 7A is a flowchart showing a variation of the dry milling ethanol production system and process with the front end milling method of Figure 7 in accordance with an embodiment of the invention;
[0033] FIG. 7B is a flowchart showing a variation of the dry milling ethanol production system and process with the front end milling method of Figure 7A in accordance with an embodiment of the invention;
[0034] FIG. 8 is a flowchart showing a dry milling ethanol production system and process with the front end milling method in accordance with another embodiment of the invention;
[0035] FIG. 9 is a flowchart showing a dry milling ethanol production system and process with the front end milling method in accordance with another embodiment of the invention;
[0036] FIG. 9A is the flowchart showing a variation of the dry milling ethanol production system and process with the front end milling method of Figure 9 in accordance with another embodiment of the invention; and
[0037] FIG. 9B is the flowchart showing a variation of the dry milling ethanol production system and process with the front milling method of Figure 9A in accordance with another embodiment of this invention. Detailed Description of Specific Modalities
[0038] Figures 1 and 2 have been described above and represent a flowchart of a typical dry milling ethanol production process and several typical liquefaction processes that define the liquefaction step in a dry milling ethanol production process, respectively.
[0039] Figures 3-9B illustrate various modalities of a dry milling ethanol production system and process with the front end milling method to improve alcohol, oil and/or protein productions, and to produce a higher fiber. pure, more desirable for secondary alcohol production, for example. These processes and systems are described in detail here below.
[0040] First, with reference to Figure 3, this figure depicts a flowchart of an embodiment of a dry milling ethanol production system and process with a front end milling method to improve alcohol and/or by-product productions , for example, oil and/or protein productions. In this process 100, the corn is first subjected to a milling step 102, which involves the use of a hammer mill, or the like, to grind corn to particle sizes less than about 0.28 centimeter (7/64 inch). ) and allows the release of oil from it. In one example, the screen size for separating particles can decrease from about 0.28 centimeters (7/64) to about 0.24 centimeters (6/64 inches). In another example, particle sizes are from about 50 microns to 3 mm. Grinding helps to break the bonds between fiber, protein, starch, and germ.
[0041] Next, the ground cornmeal is mixed with water, referred to as cooking water, in suspension tank 104 to create a suspension and begin liquefaction. An enzyme(s), such as alpha amylase, optionally can be added to slurry tank 104. The slurry can be heated in slurry tank 104 to about 65.56°C (150°F) to about 93.33°C (200 °F) for about 30 minutes to about 120 minutes. Suspension tank stream 104 contains about 1 lb/bu of free oil and about 1.5 lb/bu of germ (particle size ranges from about 50 microns to about 3 mm), 1.8 lb/bu grain bu (particle size ranges from about 50 microns to about 3 mm), and 4.2 lb/bu fiber (particle size ranges from about 50 microns to about 3 mm).
[0042] The feed from the suspension tank 104 is then subjected to a liquid/solid separation step 106, which defines the start of the front end milling method. While the front end milling method begins after suspension tank 104 in Figure 3, it should be understood that it can be located anywhere along the liquefaction process, including from suspension tank 104 to the fermentation step 11 1. The liquid/solid separation step 106 separates a generally liquefied solution (about 60-80% by volume), which includes free oil, protein, and fine solids (which do not require grinding), of heavy weight solids (about 20-40% by volume), which includes the heaviest fiber, grain, and germ, which may include bound oil, protein, and/or starch. The liquid/solid separation step 106 uses dewatering equipment, for example, a paddle screen, a vibrating screen, screen decanter centrifuge or conical screen centrifuge, a pressure screen, a pre-concentrator, and similar to carry out the separation of solids from the liquid part. Fine solids are no larger than 200 microns. In another example, fine solids are no larger than 500 microns, which is generally dependent on the screen size apertures used in the liquid/solid separation device.
[0043] In one example, the dewatering equipment is a paddle screen, which includes a stationary cylinder screen with a high-speed rake paddle. Multiple paddles on the paddle screen can be in the range of 1 paddle by 10.16 to 20.32 centimeters (4 to 8 inches) of screen diameter. In another example, the dewatering equipment is a pre-concentrator, which includes a stationary cylinder screen with a low speed conveyor belt. The conveyor pitch in the pre-concentrator can be about 1/6 to 1/2 the screen diameter. Various paddles on the paddle screen and conveyor pitch in the pre-concentrator can be modified depending on the amount of solids in the food. The gap between the paddle screen and the paddle can range from about 0.1 to 0.51 centimeter (0.04 to 0.2 inch). A smaller gap produces a drier mass with purer fiber and higher capacity, but loses more fiber when filtering. A larger gap produces a wetter mass with a purer liquid and a lower capacity (less insoluble solid). Blade speed can range from 400 to 1200 RPM. In another example, paddle speed can range from 800 to 900 RPM. A higher speed provides more capacity but consumes more power. A suitable type of paddle screen is the FQ-PS32 paddle screen, which is available from Fluid-Quip, Inc. of Springfield, Ohio.
[0044] The screen for the dewatering equipment may include a type of slotted wedge wire or a thin plate, round hole screen. Round hole screen can help prevent long fine fiber from passing through the screen better than wedge wire grooving, however, round hole capacity is smaller, so more equipment may be required to use. the round hole screens. The size of the screen openings can range from about 45 microns to 500 microns. In another example, screen apertures can range from 100 to 300 microns. In yet another example, screen apertures can range from 200 to 250 microns. Smaller screen openings tend to increase protein/oil/alcohol production with higher operating cost and equipment, while larger screen openings tend to reduce protein/oil/alcohol production with lower operating cost and equipment.
[0045] The new separated liquefied starch solution can be subjected to an optional oil separation step 108, which can use any type of oil separator, such as a slurry centrifuge, three-stage settler, disc settler, centrifuge three-phase disc, and the like, to separate the oil from the liquefied starch solution by taking advantage of differences in density. In particular, the liquefied starch solution is used as a heavy medium liquid to float the oil particle/emulsion/fine germ. The liquefied starch solution has densities of about 1.1 to 1.2 grams/cc and 0.9 to 0.92 grams/cc for oil and 1 to 1.05 grams/cc for germ.
[0046] There may be three phases discharged from oil separation step 108. The first is a light phase, which includes oil or an oil/emulsion layer. The second is a heavy phase, which includes the liquefied starch solution, possibly with some small germ particles. The third phase is the solid phase, which contains fine fiber, grain particles, and starch. Solid phase and heavy underflow phase can be combined as illustrated in Figure 3; otherwise, they can remain separate and be sent to different locations to refine the results.
[0047] The oil/emulsion/fine germ layer and can be routed to an oil polishing step 109 while the layer can be subjected to centrifugation, including a three-stage decanter, three-stage disc centrifuge, or similar to separate the pure oil from the emulsion and fine germ particle. From the oil polishing step 109, the emulsion and fine germ particle can be discharged as a heavy phase and optionally subjected to a solvent extraction step 110 to recover additional oil, or rejoined with the heavy phase/ combined starch solution from oil separation step 108. In oil polishing step 109, alcohol, such as 200 resistant alcohol from a distillation tower of distillation step 118, can be added to the emulsion and fine germ particles so to break the emulsion and extract oil from the fine germ particle, which is normally less than 100 microns. The remaining fine germ particles are sent to fermentation step 111 as indicated.
[0048] The oil that is recovered in step 110 has a much more desirable quality in terms of color and free fatty acid content (less than 7% and, in another example, less than 5%) when compared to oil which is recovered downstream, particularly oil recovered after fermentation 111. In particular, the color of oil recovered from pre-fermentation is lighter and lower in free fatty acid content. Oil production in step 108 can reach about 0.9 lb/bu while current oil recovery from the evaporator streams averages below 0.5 lb/bu. With oil polishing step 109 and solvent extraction step 110, oil production can increase as high as 1.4 lb/bu.
[0049] Returning now to the liquid/solid separation step 106, the wet mass or parts of dewatered solid from the stream in the liquid/solid separation step 106 (about 60 to 65% water) continues through the method of front end milling and is then subjected to a dehydrated milling step 112, while the solids, particularly the germ and grain, are reduced in size by the size reduction equipment. The size reduction equipment can include a hammer mill, a pin or impact mill, and a grinding mill, and the like. In one example, the size reduction equipment is a pin mill or grinding mill. This dehydrated milling step 112 is intended to break the germ and grain particles and the bonds between fiber and starch, as well as oil and protein, without cutting the fiber too fine, thereby producing a sharper separation between fiber and protein /starch/oil.
[0050] In a dehydrated form, the germ and grain particles are able to separate more easily than the fiber as a result of the increased frictional action in which less fine fiber is created, however, the germ and grain are more thoroughly ground. This results in a relatively non-uniform particle size among the ground solids. For example, the germ and grain particles can be ground to a particle size between about 300 to 800 microns, while a majority of the fiber remains within a particle size range of 500 to 2000 microns. In one example, more than 75% of the fiber remains in a particle size range of 500 to 2000 microns. In another example, no more than 80% by weight of the total particles after the dehydrated milling step 112 has a particle size less than 800 microns. In another example, no more than 75% by weight of the total particles after the dehydrated milling step 112 has a particle size of less than 800 microns. In yet another example, no more than 65% by weight of the total particles after the dehydrated milling step 112 has a particle size of less than 800 microns. In another example, about 30% to about 50% by weight of the total particles after the dehydrated milling step 112 has a particle size of about 100 microns to about 800 microns. In yet another example, about 40% to about 50% by weight of the total particles after the dehydrated milling step 112 has a particle size of about 100 microns to about 800 microns. In yet another example, no more than 50% by weight of the total particles after the dehydrated milling step 112 has a particle size of about 100 microns to about 800 microns. The % protein in solid particles that are larger than 300 microns is about 29.5%. After milling and if washing techniques are used, the % protein in the fiber may decrease from about 29.5% to about 21.1%. The % oil in fiber can decrease from about 9.6% to about 6.4%, and the % starch in fiber can decrease from about 5.5% to about 3%.
[0051] If a grinding mill is used for particle size reduction in the dehydrated grinding step 112, the design of the grain plates (not shown) for the grinding mill can be varied to perform the germ and grain grinding , while tending to avoid fiber grinding. Historically, grain plates, which are generally opposite, typically define a group of about 6 grinding plate segments that form an annular ring when combined together and secured to the surface of a grinding disc. Each segment of the grinding plate, and hence the grinding plate itself, contains “tooth” designs placed in rows of annular rings or bars of various widths that extend from the inner diameter to the outer diameter of the grinding plate. With bar-style grinding plates, the width and depth can be varied to provide more effective grinding of the germ and grain, while tending to avoid fiber. In one example, the bar is 50.8 centimeters (20 inches) long. Different combinations, numbers, and shapes and sizes of “tooth” or bar designs can be provided to more effectively grind the germ and grain, while tending to avoid fiber. Furthermore, the gap between the grinding plates as well as the RPMs can be adjusted for energy efficiency and desired performance. In an example, the gap might be 0.03 to 0.76 centimeters (0.01 to 0.3 inches). In another example, the plate gap is about 0.05 to 0.38 centimeters (0.020 to 0.15 inches). Also, in an example, the RPM could be 900 to 3000 for one or more grinding plates. In another example, the RPM is around 1800.
[0052] The grinding plate can be composed of white iron, which has high abrasion resistance with approximately 25% chromium content to increase corrosion resistance, however, it can be formed from any suitable metal or alloy, plastic, composite and the like. Also tooth size (width, height and length), tooth shape, distance between teeth, and number of teeth in each row can vary to achieve the desirable germ and grain grinding, while tending to avoid fiber grinding.
[0053] One type of milling mill having a suitable type of milling plate is the FQ-136 milling mill, which is available from Fluid-Quip, Inc. of Springfield, Ohio. This type of grinding mill has a stationary disk 91.44 centimeters (36” inches) in diameter and a rotating disk 91.44 centimeters (36” inches) in diameter. Grinding plate segments defining the grinding plate are installed on each disc, and the gap between the two discs can be varied to produce an effective grinding result. Grinding mills can be made with larger or smaller diameter discs. The FQ-152 grinding mill also available from Fluid-Quip, Inc. of Springfield, Ohio, has disks 132.08 centimeters (52 inches) in diameter. Larger diameter discs can provide higher tangential speed at the outer edge of the discs compared to smaller discs, which can provide greater impact and shear and grinding effect if run at the same rotary speeds. Grinding mills can also be made with two rotating discs, which can vary in diameter. In this case, the disks rotate in opposite directions, producing an effective disk-to-disk net speed twice that of a single spinning disk. The increased speed will increase the number of tooth or bar crossings that will effect the impact and/or shear effect on the medium passing through the grinding mill.
[0054] If a pin/impact mill is used for particle size reduction, different types and sizes of pin, eg round, triangular, hexagonal, and the like, can be used depending on operating requirements to improve the dehydrated milling step 112. In one example, pin sizes might include round pins, which can be approximately 6.67 centimeters (21/8 inches) in height and 4.76 centimeters (15/8 inches) in diameter. In addition, the RPM for the pin/impact mill can be 2000 to 3000. The pins can be made of stainless steel or other suitable corrosion resistant metal or metal alloy, plastic, composite and the like. A suitable type of pin/impact mill, which uses an impact force to help break the germ and grain, while tending to prevent fiber grinding, is the FQ-IM40, which is available from Fluid- Quip, Inc. of Springfield, Ohio.
[0055] After milling, which alone defines the end of the front end milling method, the solids can be mixed with the liquefied starch solution either from the optional oil separation step 108 or from the liquid/solid separation step 106 , as shown, to form a heavy suspension then subjected to one of the three optional pre-storage tank systems in the pre-storage tank step 113, i.e. generally one of systems A, B, and C of Figure 2 In addition, if the emulsion and fine germ particle from the oil polishing step 109 are not optionally subjected to the solvent extraction step 110, the underflow (mainly liquefied starch) joins with the underflow solution from the separation step of oil 108, which is joined with the solids from the dehydrated milling step 112 to form the heavy suspension, and sent to the pre-storage tank step 113.
[0056] In the pre-preservation tank step 113 and as generally described above with respect to Figure 2, the heavy suspension may be subjected to system A or a pressurized jet cooker and heated to about 101°C to about 130°C for about 3 to 30 minutes at a pressure of about 20 psi to about 150 psi, held in a U-tube for about 5 to 15 minutes, then routed to a flash tank and held at above temperature at 95°C for about 3 to 30 minutes to help solubilize the starch. Alternatively, the heavy suspension can be subjected to system B or fed to a secondary suspension tank whereas steam is injected directly into the secondary suspension tank and the suspension is maintained at a temperature of about 95°C for about 60°C. to 120 minutes. Alternatively, the heavy suspension can also be subjected to system C or fed to a secondary suspension tank, without steam injection, and maintained at a temperature of about 60°C to 85°C for 1 to 4 hours.
[0057] Therefore, the suspension from the stage of the pre-preservation tank 113 is forwarded, in series, to the first of the second storage tanks 114 and 115 for a total storage time of about 2 to 4 hours at temperatures and about 60°C to 85°C to also solubilize the starch component in the slurry stream and complete liquefaction before sending to fermentation step 111. While two holding tanks are shown here, it should be understood that one conservation tank or more than two conservation tanks can be used.
[0058] Various enzymes (and types thereof) such as amylase or glucoamylase, fungal, cellulose, cellobiose, protease, and the like can optionally be added during and/or after the dehydrated milling step 112, pre-preservation tank step 113, or preservation tanks 114 and 115 to enhance component separation, such as to help break the bonds between protein, starch and fiber.
[0059] After the second holding tank 115, the stream from the optional solvent extraction step 110 can be joined with the liquefied suspension solution and sent to the fermentation step 111 while fermentation takes place.
[0060] When compared to current dry milling processes, the front end milling method, which includes the liquid/solid separation step 106 and the dehydrated milling step 112, produces a more complete starch conversion. In addition, an increase of about 1.0% alcohol production, about 0.05 lb/bu oil production, and 0.3 lb/bu protein production can be realized.
[0061] The starch solution liquefied in fermentation step 111, which now includes fiber, reduced germ and grain particles, as well as protein and oil, is subjected to fermentation to convert the sugar to alcohol, followed by a step of 118 distillation, which recovers the alcohol. In distillation step 118, the fermented solution (commonly referred to herein as “beer”) is separated from the total vinasse, which includes fiber, protein, oil, and germ and grain particles, to produce the alcohol. Alcohol production is about 2.78 gal/bu, which is about a 1% increase over conventional productions, due at least in part to the dehydrated milling step 112 while the starch in the grain particle is germ is released and eventually converted to sugar to produce more alcohol.
[0062] With continued reference to Figure 3, the tail end of process 100, which alone is optional in that a typical tail end process may be used here, may include a total vinasse separation step 120 while the dewatering equipment, for example, a paddle screen, vibrating screen, filter centrifuge, pressure screen, screen bowl decanter and the like, is used to carry out the separation of insoluble solids or "total vinasse", which includes fiber , from the liquid “fine vinasse” part. Screen openings can range in size here from about 45 to 400 microns, depending on the purity of fiber and protein desired here. In one example, the screen of the dewatering equipment has openings of a size of about 75 to 800 microns. And, in another example, the size of the openings ranges from about 150 to 500 microns.
[0063] The thin stillage from the total vinasse separation step 120 can be sent to a protein recovery step 122, which uses, for example, a decanter, a centrifuge with a nozzle, or a disc decanter to recover the protein and thin germ (corn gluten as well as spent yeast). These recovered components are sent to a drying step 124, which uses a dryer, such as a rotary or ring dryer, to produce a gluten/germ (protein bran) mixture.
[0064] The insoluble solids (total vinasse), or the wet mass fiber part, from the total vinasse separation step 120 is sent to a washing and dehydrating step 126, which uses a filtration device such as a centrifuge of fiber, to separate the different types of fiber depending on a screen(s) having different size openings. An exemplary filtration device for wet mass washing and dehydrating step 126 is shown and described in Lee U.S. Patent Application Publication No. 2010/0012596, the contents of which are incorporated herein by reference. Screen openings for the fiber centrifuge will typically be about 500 microns to capture amounts of tip cap, pericarp, as well as fine fiber, however, it can range from about 400 microns to about 1500 microns. The residual liquid from the centrifuge can rejoin the fine vinasse before the protein recovery step 122. The centrifuged fiber contains less than 3% starch compared to normal dry mill fiber, which is 4 to 6 % starch in fiber. The % protein in fiber also decreases from a conventional 29% to 21% and the % oil decreases from a conventional 9% to about 6%.
[0065] The overflow current from the protein recovery step 122 can move to a fine protein recovery step 130, which uses, for example, a clarifier followed by a high-speed settler or disc settler, and the like, to separate the liquid portion of the stream, which includes oil, from the remaining heavier components, including the residual protein. The centrifuged protein is then sent to drying step 124, along with protein recovered from protein recovery step 122, to produce the gluten/germ (protein bran) mixture, which is about 50% protein. The total protein production of the process is more than 4 lb./bu.
[0066] The liquid superflow from the fine protein recovery step 130 moves to the evaporators in an evaporation step 136 so as to separate any oil from it by boiling off moisture, leaving a thick syrup. High concentrated syrup (more than 60% DS) can be used, among other things, as (a) nutrition for secondary alcohol production, (b) animal feed raw material, (c) plant feed , (d) and/or anaerobic digestion to produce biogas. The concentrated suspension can optionally be sent to a centrifuge, for example, to separate the oil from the syrup. Oil can be sold as a separate high value product.
[0067] The syrup can be mixed with the centrifuged wet mass from the washing and dehydration step 126, and the mixture can be sold to feedlots of beef and dairy cattle as Soluble Moist Grain Distillers (DWGS). The mixture of wet mass and concentrated syrup can also optionally be dried in a drying step 140 and sold as Soluble Dry Grain Distillers (DDGS) for feedlots for beef cattle and milk. This DDGS has less than 25% protein and 8% oil.
[0068] Referring now to Figure 3A, this figure depicts a simplified flowchart of the dry milling ethanol production system and process 100 of Figure 3, and particularly the front end milling method, which includes in its simplest form the liquid/solid separation step 106 and the dehydrated milling step 112. As described in detail below, more than one liquid/solid separation step 106 and the dehydrated milling step 112 can be used here, for example, to production of alcohol, oil, protein, and/or fiber, with purity and/or desirable production.
[0069] With continued reference to Figure 3A, to accomplish the desirable production of alcohol, oil, protein, and/or fiber, corn is first ground to particle sizes less than about 0.28 centimeter (7/64 inches). ). Milling helps to break the bonds between fiber, protein, starch, and germ and allows the release of oil from the corn. The ground cornmeal is mixed with cooking water in slurry tank 104 to create a slurry and begin liquefaction. An enzyme(s), such as alpha amylase, optionally can be added to suspension tank 104 to help convert the insoluble starch in the suspension to soluble starch. Suspension tank stream 104, which contains, for example, sugars, protein, oil, germ particle (particle size ranges from about 50 microns to about 3 mm), grain (particle size ranges from about 50 microns to about 3 mm), and fiber (particle size ranges from about 50 microns to about 3 mm), is routed to the liquid/solid separation step 106. The liquid/solid separation step 106, which again defines the beginning of the front end milling method, separates a generally liquefied solution (about 60-80% by volume), which includes oil, protein, and fine solids (which do not require milling), from the mass of solids. heavy (about 20 to 40% by volume), which includes heavier fiber, grain, and germ. The oil in the liquid portion optionally can be subjected to a front end oil separation step 108 to recover free oil in the stream.
[0070] The dewatered solid part of the stream (about 60 to 65% water) is subjected to the dewatered milling step 112, which defines the end of the front end milling method. Here, solids, particularly germ and grain, are reduced in size through size reduction equipment, which breaks down germ and grain particles and the bonds between fiber and starch, as well as oil and protein, without cutting the very fine fiber, thereby determining sharper separation between fiber and protein/starch/oil. The germ and grain particles are ground to a particle size between about 300 to 800 microns, whereas a majority of the fiber remains in a particle size range of 500 to 2000 microns. Various enzymes (and types thereof) such as amylase or glucoamylase, fungi, cellulose, cellobiose, protease, and the like can optionally be added to enhance component separation, such as to aid in breaking the bonds between protein, starch and fiber. . The heavy suspension from the dehydrated milling step 112 is subjected to the pre-preservation tank stage 113, followed by the first and second preservation tanks 114 and 115 to also solubilize the starch component in the suspension and complete liquefaction stream before sending to the fermentation step 111. Therefore, alcohol and optionally fiber, oil, and/or protein are recovered from process 100.
[0071] Referring now to Figures 3B-3D, these figures depict a simplified flowchart showing variations of the dry milling ethanol production system and process with the front end milling method of Figure 3A according to the embodiments of the invention. In particular, each of Figures 3B-3D generally depicts optional locations of the initial cooking water and optional enzyme addition, as well as the incorporation of additional optional solid/liquid separation steps 302, 402 and dehydrated milling steps 502, 702. Along with additional optional solid/liquid separation steps 302, 402, oil recovery can optionally be implemented by following additional solid/liquid separation steps 302, 402. And Figure 3D, depicts fiber tip recovery optional front. These simplified processes with their additional optional steps are described in more detail below, and can be used to recover alcohol, oil, protein, and/or fiber, with desirable purity and/or yields.
[0072] Referring now to Figure 4, this figure depicts a flowchart of a dry milling ethanol production system and process 200 with the front end milling method according to another embodiment of the invention to improve alcohol productions and/or by-product, for example oil and/or protein productions. In a way, this process 200 is a variation of the dry milling ethanol production process 100 with the front end milling method of Figure 3. Here, in Figure 4, the front end milling method, which includes the liquid/solid separation step 106 and dehydrated milling step 112, is situated after the second holding tank 115 and before the fermentation step 111, as a way to increase oil recovery, rather than after the tank of suspension 104. As a result, the feed that is sent to the oil separation step 108 has a lower viscosity and a higher Brix, which is understood to make oil recovery more efficient. In contrast, process 100 of Figure 3 is intended to increase alcohol production by allowing for greater starch release.
[0073] Due to the location of the front end milling method, as shown in Figure 4, the food from the suspension tank 104 is sent directly to the pre-preservation tank step 113 (instead of the liquid/separation step/ solid 106 as shown in Figure 3), whereas the suspension is subjected to one of systems A, B or C as described above. Therefore, the suspension is sent to the first and second holding tanks 114 and 115 to also solubilize the starch component in the suspension stream.
[0074] The suspension stream of the second preservation tank 115 is then subjected to the liquid/solid separation step 106, which defines the start of the front end milling method. The liquid/solid separation step 106 again separates the liquefied solution (about 65-85% by volume), which includes oil, protein, and fine solids (which do not require grinding), from the mass of heavy solids (about 15 to 35% by volume), which includes the heaviest fiber, grain and germ. The now separated liquefied starch solution can move to optional oil separation step 108 to separate oil from the liquefied starch solution taking advantage of density differences, and an oil/emulsion/germ layer can also be routed to the oil polishing step 109.
[0075] The dehydrated solids portion of the stream in the liquid/solid separation step 106 (about 60 to 65% water) continues through the front end milling method and is then subjected to the dehydrated milling step 112 , while solids, particularly germ and grain, are reduced in size through size reduction equipment. After milling, which defines the end of the front end milling method, the solids are mixed with the liquefied starch solution from either the optional oil separation step 108 or the liquid/solid separation step 106 to form a heavy suspension. and subjected to the fermentation step 111. Also, if the emulsion and fine germ particle from the oil polishing step 109 are not optionally subjected to the solvent extraction step 110, the subflow (mainly liquefied starch) is joined with the solution of subflow from the oil separation step 108, which is joined with the solids from the dehydrated milling step 112 to form the heavy suspension, and sent to the fermentation step 111. The remainder of the dry milling ethanol production process 200 is generally the same as the one in Figure 3.
[0076] While not intending to be limiting, it should also be understood that the front end milling method can also be used between the pre-preservation tank step 113 and the first conservation tank 114, or the first conservation tank 114 and second conservation tank 115, and the like, for example.
[0077] Referring now to Figure 5, this figure depicts a flowchart of a dry milling ethanol production system and process 300 with the front end milling method according to another embodiment of the invention to improve alcohol productions and/or by-product, for example oil and/or protein productions. To some extent, this process 300 is a variation of the dry milling ethanol production process 100 with the front end milling method of Figure 3. In this process 300, at the front end, as compared to process 100 of Figure 3 , there is an additional liquid/solid separation step 302, which is situated between the pre-preservation tank step 113 and the first preservation tank 114 and is considered as an addition to the front end milling method. In an effort to maximize the production of alcohol, protein, and/or oil, the backwash also that is set up in this process 300 where filtrate, which includes liquefied starch plus medium sized solids, is removed from the slurry stream in the second step of liquid/solid separation 302. This filtrate is recycled again to mix with the ground corn bran just before the suspension tank 104 creates a suspension and starts liquefaction, and replaces the initial cooking water which is used in the modality shown in Figure 3. As such, cooking water is now initially added after dehydrated milling step 112, as compared to just after milling step 102, in process 300 of Figure 5. This backwash configuration allows for the liquefied starch additional and medium sized solids are recycled back to the dehydrated milling step 112 one or more times, without the need for dehydrated milling equipment. the additional. The recycled liquefied starch revisits the first liquid/solid separation step 106 whereas it can be separated by traveling through the screen, then it can be sent to the first conservation tank 114.
[0078] With continuous reference now to Figure 5, the feed from the suspension tank 104 is subjected to the first liquid/solid separation step 106, which defines the start of the front end milling method. The liquid/solid separation step 106 again separates the liquefied solution (about 60-80% by volume), which includes oil, protein, and fine solids (which do not require grinding), from the mass of heavy solids (about 20 to 40% by volume), which includes the heaviest fiber, grain and germ. The now separated liquefied starch solution can move to the optional oil separation step 108, to separate oil from the liquefied starch solution by taking advantage of density differences, and then the oil/emulsion/germ layer can also be forwarded to oil polishing step 109.
[0079] The dehydrated solids portion of the stream in the liquid/solid separation step 106 (about 60 to 65% water) continues through the front end milling method and is then subjected to the dehydrated milling step 112 , while solids, particularly germ and grain, are reduced in size through size reduction equipment. After milling, the solids are mixed with the cooking water to form a heavy suspension and subjected to one of the three optional pre-storage tank systems at pre-storage tank step 113, i.e. generally one of systems A , B, and C of Figure 2. The addition of cooking water after the dehydrated milling step 112 helps with washing and separating starch, oil, and liquefied medium size solids.
[0080] The suspension from the pre-preservation tank step 113 is then forwarded to the second liquid/solid separation step 302. And as in the case of the first liquid/solid separation step 106, the second separation step liquid/solid 302 uses dewatering equipment, for example, a paddle screen, a vibrating screen, a filtration, scroll screen, or conical screen centrifuge, a pressure screen, a preconcentrator, and the like, to perform the separation of solids from the liquid part. In one example, the dewatering equipment is a paddle screen or a preconcentrator, as described above. With the second liquid/solid separation step 302, the actual screen openings can be larger in size than those in the first liquid/solid separation step 106, which can provide greater alcohol and oil production. In one example, the size of the screen used in the first liquid/solid separation step 106 can range from 45 microns to 300 microns, and the size of the screen used in the second liquid/solid separation step 302 can range from about 300 to 800 microns in size. The filtrate, which is removed from the second liquid/solid separation step 302 and joined with the ground corn meal before the suspension tank 104, contains about 6 to 10 Brix of liquefied starch solution as well as solid particles (germ, grain and protein) having sizes smaller than the screen size apertures used in the second liquid/solid separation step 302. Using a smaller screen in the first liquid/solid separation step 106 and a larger screen in the second separation step of liquid/solid 302, the countercurrent configuration allows to achieve the grinding of grain and germ particles larger than the screen size in the first liquid/solid separation step and smaller than the screen size in the second separation step. liquid/solid 302. Particles larger than screen size in the second liquid/solid separation step 302 tend to be mostly fiber and contain less starch, so they do not need to be recycled for milling additional in the dehydrated milling step 112.
[0081] The dehydrated solids part of the stream is then routed, in series, to the first and second storage tanks 114 and 115 for a total storage time of about 2 to 4 hours at temperatures of about 66°C at 85°C to further solubilize the starch component in the suspension stream and complete liquefaction before sending to the fermentation step 111. In this process 300, the liquefied starch solution from the optional oil separation step 108 and optionally the emulsion and Fine germ particle from the oil polishing step 109 can be joined with the heavy solids from the second liquid/solid separation step 302 in the first holding tank 114. In addition, the liquefied starch solution from the first liquid separation step /solid 106 can be combined with the solids here in the first holding tank 114 if the optional oil separation step 108 is not used. The rest of the dry milling ethanol production process 300 is generally the same as that in Figure 3.
[0082] The backwash configuration in this process 300 is understood to create a desirable way to control the temperature, brix, pH, and enzyme concentration profile of the suspension throughout the liquefaction process, i.e., from the suspension tank 104 to the second holding tank 115. For example, when cooking water and fresh enzyme, as shown in Figure 5, are added near the rear end of liquefaction and subjected to the first and second stages of holding tank 114, 115, the conditions slurry (eg pH, temperature and Brix) can be controlled by adjusting the amount of cooking water and the source of cooking water, which typically includes very cold fresh water and hot condensate from the evaporator and CO2 rubber. These cooking water sources, which have different temperatures, pH, etc., can be manipulated to provide optimal results for the liquefaction process, including helping to minimize the formation of non-convertible starch, and minimizing retrograde starch during saccharification .
[0083] In addition, the combination of the first and second liquid/solids separation step 106, 302 and the dehydrated milling step 112 helps to provide an additional increased production of 1.5% alcohol, about 0.1 lb. /bu of more oil, and 0.5 lb/bu of more protein. And the amount of backwash water for backwashing is only a part of the total cooking water flow, for example about 50%. As such, the heavy mass content in the suspension which is subjected to the first and second holding tanks 114, 115 approximately doubles, which in turn doubles the average hold time that is required to produce a more complete liquefaction, for example.
[0084] Referring now to Figure 6, this figure depicts a flowchart of a dry milling ethanol production system and process 400 with the front end milling method according to another embodiment of the invention to improve alcohol productions and/or by-product, for example oil and/or protein productions. To some extent, this process 400 is a variation of the dry milling ethanol production process 300 with the front end milling method of Figure 5. Here, in Figure 6, at the front end of process 400 as compared to the In process 300 of Figure 5, there is a third liquid/solid separation step 402, which is situated between the second holding tank 115 and the fermentation step 111, and is considered as an addition to the front end milling method.
[0085] As shown in Figure 6, the feed from the suspension tank 104 is subjected to the first liquid/solid separation step 106, which defines the start of the front end milling method. The first liquid/solid separation step 106 again separates the liquefied solution (about 60-80% by volume), which includes oil, protein, and fine solids (which do not require grinding), from the heavy solids mass. (about 20 to 40% by volume), which includes the heaviest fiber, grain and germ. Instead of moving to the optional oil separation step 108 as shown in Figure 5, the now separated liquefied starch solution is routed to join with the dehydrated solids from the second liquid/solid separation step 302. dehydrated solids are subjected to the first followed by second holding tanks 114, 115 for a hold time of about 2 to 4 hours at temperatures of about 66°C to 85°C to further solubilize the starch component in the slurry stream. before sending the suspension to the third step of liquid/solid separation 402. Various enzymes (and types thereof) such as amylase or glycoamylase, fungi, cellulose, cellobiose, protease and the like can optionally be added to the dehydrated solids of the second step of liquid/solid separation 302 before the first holding tank 114 to enhance component separation, such as to help break the bonds between the protein, the wet and fiber.
[0086] As in the case of the first and second liquid/solid separation step 106 and 302, the third liquid/solid separation step 402 uses dewatering equipment, for example, a paddle screen, a vibrating screen, a filtration, scroll screen, or conical screen centrifuge, a pressure screen, a pre-concentrator, and the like, to carry out the separation of solids from the liquid part. In one example, the dewatering equipment is a paddle screen or a pre-concentrator, as described above. With the second liquid/solid separation step 302, actual screen openings may be larger in size than those in the first and/or third liquid/solid separation step 106, 402.
[0087] In the third liquid/solid separation step 402, the liquefied solution (about 70-85% by volume), which includes oil, protein, and fine solids, is separated from the heavy solids mass (about 15- 30% by volume), which includes the heaviest fiber, grain, and germ. The now separated liquefied starch solution can move to the oil separation step 108, to separate the oil from the liquefied starch solution taking advantage of density differences, and an oil/emulsion/germ layer can also be routed to the oil polishing step 109. If the oil recovery centrifuge in the oil separation step 108 is specifically a three-stage decanter, the third liquid/solid separation step 402 can be eliminated. However, the performance of the three-phase decanter can be improved by keeping the third liquid/solid separation step 402.
[0088] With further reference to Figure 6, the heavy subflow and solid phase from the third liquid/solid separation step 402 can be combined and routed to join with the liquefied starch solution from the oil separation step 108, and optionally with the emulsion and fine germ particle from the oil polishing step 109 and the remaining fine germ particle from the solvent extraction step 110, then directly subjected to fermentation 111. Although not described in Figure 6, if the step of oil separation 108 is not optionally used here, the third liquid/solid separation step 402 can be eliminated and the liquefied starch suspension solution sent directly from the second holding tank 115 to the fermentation step 111. dry milling ethanol production process 300 is generally the same as that of Figure 5.
[0089] Although not illustrated, it should be understood that processes 300 and 400 of Figure 5 and Figure 6, respectively, can be rearranged so that the food that goes to the oil separation step 108, for example, can be sent from the pre-preservation tank step 113, to the first conservation tank 114, or the like. With respect to increasing alcohol production, process 300 in Figure 5 is understood to be desirable for releasing more starch, whereas process 400 in Figure 6 is understood to be more desirable for oil recovery as the feed for step oil separator 108 of Figure 6 will have lower viscosity and higher Brix.
[0090] Referring now to Figure 7, this figure depicts a flowchart of a dry milling ethanol production system and process 500 with the front end milling method according to another embodiment of the invention to improve alcohol productions and/or by-product, for example oil and/or protein productions. To some extent, this process 500 is a variation of the dry milling ethanol production process 400 with the front end milling method of Figure 6. Here, in Figure 7, at the front end of the process 500, when compared to the In process 400 of Figure 6, in this regard a second dehydrated milling stage 502 is added, which is situated between the second liquid/solid separation stage 302 and the first holding tank 114, and is considered as an addition to the milling method. of front end. Thus, with this process 500, in that regard three liquid/solid separation steps 106, 302, 402 and two dehydrated milling steps 112 and 502 in the front end milling method are provided. It is noted that to release starch from the germ and grain particles, the particle size must be less than about 300 to 400 microns, whereas to release oil from the germ particles, the particle size must be less than about 75 to 150 microns. To increase alcohol production, while two dehydrated milling steps 112, 502 in a series are desirable, one will suffice. However, to increase oil production, two dehydrated milling steps 112, 502 are desirable.
[0091] With continuous reference to Figure 7, the dehydrated solids portion of the stream in the second liquid/solid separation step 302 continues along the front end grinding method and is subjected to the second dehydrated grinding step 502, at step that solids, particularly germ and grain, are also reduced in size through size reduction equipment. The size reduction equipment can include a hammer mill, a pin or impact mill, a grinding mill, and the like. In one example, the size reduction equipment is a pin mill or grinding mill. This second dehydrated milling step 502 is also intended to break the germ and grain particles and the bonds between fiber and starch, as well as oil and protein, without cutting the fiber too fine, thereby producing a sharper separation between the fiber and the protein/starch/oil. In a dehydrated form, germ and grain particles are able to separate more easily than fiber as a result of the increased frictional action in which less fine fiber is created, however, the germ and grain are more thoroughly ground. . This results in a relatively non-uniform particle size among the ground solids. For example, germ and grain particles can be ground here to particle sizes between about 75 to 150 microns, whereas a majority of the fiber remains in a particle size range of 300 to 800 microns. In one example, more than 75% of the fiber remains in a particle size range of 300 to 1000 microns. In another example, about 30% to about 60% by weight of the total particles after the second dewatered milling step 502 has a particle size of about 100 microns to about 800 microns. In yet another example, about 40% to about 50% by weight of the total particles after the second dewatered milling step 502 has a particle size of about 100 microns to about 800 microns. In yet another example, no more than 60% by weight of the total particles after the second dehydrated milling step 502 has a particle size of about 100 microns to about 800 microns. In yet another example, no more than 50% by weight of the total particles after the second dewatered milling step 502 has a particle size of about 100 microns to about 800 microns. The rest of the 500 dry mill ethanol production process is generally the same as the one in Figure 6.
[0092] The combination of the three liquid/solid separation steps 106, 302, 402, and two dehydrated milling steps 112 and 502 in the front end milling method of Figure 7 helps to provide an additional increased production of 2% of alcohol, about 0.15 lb/bu more oil, and 0.8 lb/bu more protein.
[0093] Referring now to Figure 7A, this figure depicts a flowchart showing a variation of the dry milling ethanol production system and process 500 with the front end milling method of Figure 7 according to another embodiment of the invention for improve alcohol and/or by-product productions, eg oil and/or protein productions. In this process 500A, the countercurrent washing of Figure 7, which includes removing and recycling back liquefied starch plus medium sized solids from the suspension stream in the second liquid/solid separation step 302 so that the mixture with the flour ground corn just before the suspension tank 104 is disposed of. Instead, the ground cornmeal is again mixed with the initial cooking water in the suspension tank 104 to create a suspension and begin liquefaction, as in Figure 3. Successively, the filtrate from the second liquid/solid separation step 302 is bonded with the ground solids from the second dehydrated milling step 502 instead of the liquefied solution separated from the first liquid/solid separation step 106. In addition, the liquefied solution from the first liquid/solid separation step 106 is similarly bonded with the ground solids from the first dehydrated milling step 1 12. And the rest of the 500A dry milling ethanol production process is generally the same as that of Figure 7.
[0094] Referring now to Figure 7B, this figure depicts a flowchart showing a variation of the dry milling ethanol production system and process 500A with the front end milling method of Figure 7A according to another embodiment of the invention to improve alcohol and/or by-product productions, for example oil and/or protein productions. Instead of subjecting the suspension formed from the filtrate from the second liquid/solid separation step 302 and the ground solids from the second dehydrated grinding step 502 to the first followed by the second holding tank 114, 115, the suspension from the first holding tank 114 is subjected to the third liquid/solid separation step 402. Again, the third liquid/solid separation step 402 uses dewatering equipment to perform the separation of the solids from the liquid portion. The liquefied solution (about 70-85% by volume), which includes oil, protein, and fine solids, is separated from the mass of heavy solids (about 15-30% by volume), which includes fiber, grain, and heavier germs.
[0095] The now separated liquefied starch solution can move to the optional oil separation step 108, and the subflow heavy phase and solid phase can be routed to join with the liquefied starch solution from the oil separation step optional 108, and optionally the emulsion and fine germ particle from the oil polishing step 109 and the remaining fine germ particle from the solvent extraction step 110, then subjected to the second holding tank 115. Therefore, the suspension is shipped and subjected to fermentation step 111. The total storage time in the first and second storage tanks is about 2 to 4 hours at temperatures of about 66°C to 85°C to also solubilize the starch component in the stream of suspension and complete liquefaction before sending to fermentation step 111. The rest of the 500B dry milling ethanol production process is generally the same as that of Figure 7A.
[0096] Referring now to Figure 8, this figure depicts a flowchart of a system and process for producing ethanol by dry milling 600 with the front end milling method according to another embodiment of the invention to improve alcohol productions and/or by-product, for example oil and/or protein productions. To some extent, this process 600 is a variation of the dry milling ethanol production process 500 with the front end milling method of Figure 7. Here, in Figure 8, at the front end of the 600 process, when compared to the process 500 of Figure 7, the liquefied solution (about 60-80% by volume) from the first liquid/solid separation step 106 is sent to the oil separation step 108 (and an oil/emulsion/germ layer can be also routed to the oil polishing step 109), rather than routed to collecting the ground solids after the second dewatered milling step 502. The dewatered solids portion of the stream in the first liquid/solid separation step 106 (about from 60 to 65% water) continues through the front end milling method and is then subjected to the first dehydrated milling step 112, while the solids are reduced in size by the size reduction equipment.
[0097] To that end and in an additional effort to maximize the production of alcohol, protein, and/or oil, additional backwash is configured in this 600 process where the filtrate, which includes liquefied starch plus medium size solids (2 to 6 Brix of liquefied starch solution) is removed from the slurry stream in the third liquid/solid separation step 402. This filtrate, similar to the filtrate from the second liquid/solid separation step 302, is recycled back to mix with the ground solids after the first dewatered milling step 112. The weighed suspension is then subjected to one of the three optional pre-storage tank systems in the pre-storage tank step 113, i.e. generally one of systems A, B, and C of Figure 2, whereas the suspension is kept for about 0.5 to 1 hour of shelf life before being sent to the second liquid/solid separation step 302. The recycled filtrate from the third step of separation of liquid/solid 402 replaces the cooking water that is used in process 500 of Figure 7, which combines with the ground solids after the first dehydrated milling step 112. In view of this, the cooking water in process 600 is now initially added after the second dehydrated milling step 112, together with optional enzymes as previously described. The backwash configuration allows released oil and smaller starch/converted sugar particles to flow through the screens and wash forward again as larger grains and starch particles continue to wash downstream for further treatment and milling prior to fermentation. . Oil recovery is understood to be successful due to the high concentration of sugars and oil recycling back to the initial suspension, which mixes with the initial free oil for later recovery. Although not described in Figure 8, if the oil separation step 108 is not optionally used here, the liquefied starch solution from the first liquid/solid separation step 106 can be joined with the solids portion of the third oil separation step. liquid/solid 402 and sent directly to fermentation step 111. The rest of the dry milling ethanol production process 600 is generally the same as that in Figure 7.
[0098] With continued reference to Figure 8, the screen size for the liquid/solids separation step 106, 302, 402 can be selected so that certain sized solid particles are recycled back to one or more of the steps of dehydrated milling 112, 502 in order to be subjected to further milling. For example, a screen size of 75 microns can be used in the first liquid/solid separation step 106, a screen size of 150 microns in the second liquid/solid separation step 302, and a screen size of 300 microns in the third liquid/solid separation step 402. With the backwash configuration, the grain and germ particles can be selectively ground to the desired particle sizes. In one example, the grain size must be less than about 300 microns for increased alcohol yields. In another example, the germ size must be less than about 150 microns to increase the increased oil yields. In another example, the germ size must be less than 45 microns to increase the increased oil yields. The combination of the first, second, and third liquid/solids separation steps 106, 302, and 402 and the first and second dehydrated milling steps 112 and 502 arranged in this backwash configuration helps to provide an additional increased production of 2% of alcohol, about 0.15 lb/bu more oil, and 0.8 lb/bu more protein.
[0099] Referring now to Figure 9, this figure depicts a flowchart of another modality of an ethanol production system and process by dry milling 700 with the front end milling method to improve alcohol and/or by-product productions , for example, oil and/or protein productions. To some extent, this process 700 is a variation of the dry milling ethanol production process 600 with the front end milling method of Figure 8. Here, in Figure 9, at the front end of process 700, when compared to process 600 of Figure 8, there is a third dehydrated milling step 702, which is situated between the third liquid/solid separation step 402 and the second holding tank 115, and is considered as an addition to the front end milling method. Furthermore, instead of subjecting the ground solids from the second dewatering milling step 502 to the first followed by the second holding tank 114, 115, the suspension from the first holding tank 114 is first subjected to the third liquid/solid separation step 402 to carry out the separation of solids from the liquid part. In addition, the filtrate from a fiber separation step 704, similar to the filtrate from the second liquid/solid separation step 302, is recycled back into a countercurrent configuration for mixing with the ground solids after the second dehydrated milling step 502 to form a heavy suspension. This heavy suspension is sent to the first holding tank 114 and held for about 1 to 3 hours at a temperature of about 50°C to 85°C.
[00100] In addition, with respect to the third liquid/solid separation step 402, the liquefied solution (about 80-90% by volume), which includes oil, protein and fine solids, is separated from the heavy solids mass ( about 10-20% by volume), which includes heavier grain, fiber and germ. The dehydrated solids portion of the stream in the third liquid/solid separation step 402 continues through the front end milling method and is then subjected to the third dehydrated milling step 702 while the solids, particularly the germ and grain , are also reduced in size by the size reduction equipment, then subjected to the second preservation tank 115. In the second preservation tank 115, the suspension is mixed with the filtrate (less than 1 Brix of liquefied starch solution) of a fiber washing and dewatering step 706 and held for about 1 to 3 hours at a temperature of about 50°C to 85°C.
[00101] The size reduction equipment used in the third step of dewatered milling 702 may include a hammer mill, a pin or impact mill, a milling mill, and the like. In one example, the size reduction equipment is a pin mill or grinding mill. This third step of dehydrated milling 702 is also intended to break the germ and grain particles and the bonds between fiber and starch, as well as oil and protein, without cutting the fiber too fine, thereby determining a sharper separation between the fiber and the protein/starch/oil. In a dehydrated form, germ and grain particles are able to separate more easily than fiber as a result of the increased frictional action in which less fine fiber is created, however, the germ and grain are more thoroughly ground. This results in a relatively non-uniform particle size among the ground solids. For example, germ and grain particles can be ground here to particle sizes between about 75 to 150 microns, whereas a majority of the fiber remains within a particle size range of 300 to 800 microns. In one example, more than 75% of the fiber remains within a particle size range of 300 to 1000 microns. In another example, about 30% to about 75% by weight of the total particles after the third dehydrated milling step 702 has a particle size of about 100 microns to about 800 microns. In yet another example, about 40% to about 60% by weight of the total particles after the third dehydrated milling step 702 have a particle size of about 100 microns to about 800 microns. In another example, no more than 75% by weight of the total particles after the third dehydrated milling step 702 have a particle size of about 100 microns to about 800 microns. In yet another example, no more than 60% by weight of the total particles after the third dehydrated milling step 702 has a particle size of about 100 microns to about 800 microns. In yet another example, no more than 50% by weight of the total particles after the third dehydrated milling step 702 has a particle size of about 100 microns to about 800 microns.
[00102] Various enzymes (and types thereof) such as amylase or glucoamylase, fungi, cellulose, cellobiose, protease, and the like may optionally be added after the third step of dehydrated milling 702 to enhance component separation, such as to help to break the bonds between protein, starch, and fiber in the second holding tank 115, for example.
[00103] With continuous reference to Figure 9, after the second conservation tank 115, the suspension is sent and subjected to a fiber separation step 704, which helps to produce the desired fiber for secondary alcohol feedstock. Dewatering equipment, for example, a paddle screen, vibrating screen, filter centrifuge, pressure screen, screen bowl decanter, and the like, is used in fiber separation step 704 to perform fiber separation from solution of liquefied starch. Again, the separated liquefied starch solution is recycled back and joined with the milled solids from the second dehydrated milling step 502 while the germ and grain particles can be milled to particle sizes between about 45 to 300 microns. The separated fiber part is forwarded, mixed with cooking water, then sent to fiber washing and dehydration step 706 while the fiber is washed and separated from the liquefied starch solution. The fiber washing and dewatering step 706 can use dewatering equipment, for example, a paddle screen, vibrating screen, fiber centrifuge, scroll screen, or conical screen centrifuge, pressure screen, pre-concentrator, and the like, to effect the separation of solids from the liquid part. In one example, the dewatering equipment is a paddle screen or a fiber centrifuge.
[00104] The washed/dehydrated fiber from the fiber washing and dewatering step 706 can be used as a feedstock for secondary alcohol production. The resulting cellulosic material, which includes pericarp and tip cap and has more than 35% DS, less than 10% protein, less than 2% oil, and less than 1% starch/sugar, can be shipped to a second secondary alcohol system, as is known in the art, as a feedstock without any further treatment. Pulp production is about 3 lb/bu.
[00105] The subflow from the oil separation step 108, and optionally from the oil polishing step 109 and the solvent extraction step 110, can be joined and routed to the fermentation step 111. Although not described in Figure 9, if the oil separation step 108 is not optionally used here, the subflow from the liquid/solid separation step 106 can be routed directly to the fermentation step 111. Because of the fiber washing and dehydrating step 706 located at the end Front of the process, the fermenter size in fermentation step 111 can be decreased because it no longer needs to accommodate the volume of fiber component in the stream. Therefore, in distillation step 118, the sugar solution is separated from the "total vinasse", which includes protein, oil, and germ and grain particles and significantly excludes fiber (less than 20% fiber), to produce alcohol. The total stillage from the still tower includes only the fine fiber because the coarser fiber was removed in the 706 fiber washing and dehydration step. The starch alcohol production is about 2.82 gal/Bu, which is an increase of about 2.25% above conventional productions, due at least in part to the dehydrated milling steps 112, 502, 702 while the starch in the grain and germ is released and eventually converted to sugar to produce more alcohol.
[00106] As also shown in Figure 9, the rear end of process 700 may include a fiber/fine protein separation step 708, which receives the stream from distillation step 118. This stream is subjected to a special graded decanter or fine mesh pressure screen, for example, to separate the fine fiber from the liquid “fine vinasse” part, which includes the protein. The separated fine fiber optionally can be sent to a caustic treatment step 710 while the fine fiber is treated with caustic, which includes a weak alkali solution (such as sodium, calcium or potassium hydroxide, sodium carbonate, and the like ), to adjust the pH from about 8.5 to 9.5 and separate residual bound proteins from the fine fiber. The treated fine fiber stream is routed to a fine fiber washing and dewatering step 712 while the dewatering equipment, for example, a paddle screen, vibrating screen, filter centrifuge, pressure screen, basin decanter screen and the like, is used to perform the separation of the fine fiber from the protein part. The washed/dehydrated fine fiber can be used as a feedstock for the production of secondary alcohol without any further treatment. Fine fiber production is about 1 lb/bu, with less than 10% protein and less than 2% oil.
[00107] The filtrate from the fine fiber/protein 708 separation step, which includes the protein, can be joined with the residual protein separated in the fine fiber washing and dehydration step 712, then subjected to similar protein recovery and steps dryings like those shown in Figure 8. Also for this purpose, it is noted here that fine protein recovery step 130 in process 700 of Figure 9 is optional. In addition, the heavier components from the optional fine protein recovery step 130 can optionally be subjected to centrifugation before being sent to a separate drying step (not shown), which uses a dryer, eg, a ring dryer or similar, to produce a gluten/yeast (protein bran) mixture having about 55% protein. In addition, in drying step 124, a gluten/germ/fine fiber blend (protein bran) can be produced having about 40% protein, which can be combined with the optional gluten/yeast blend (protein bran) ) having about 55% protein to produce a blended protein bran having about 50% protein content and a yield of about 5.5 to 6 lb./Bu protein bran.
[00108] The liquid superflow from the optional fine protein recovery step 130 or the superflow from the protein recovery step 122 can move to the evaporators in the evaporation step 136 to separate any oil there by boiling the moisture, leaving a thick syrup . In addition, if the separated fine fiber is not subjected to optional caustic treatment step 710 to produce cellulose for secondary alcohol, the centrifuged wet mass from washing and dehydration step 126 may be mixed with the syrup after evaporation step 136 and sold as DWGS, or further dried in drying step 140 and sold as DDGS.
[00109] The high concentrated syrup (more than 60% DS) from evaporation step 136 can be used, among other things, as (a) nutrition for the production of secondary alcohol, (b) raw material for feeding animal, (c) plant food, (d) and/or anaerobic digestion to produce biogas. The concentrated suspension can optionally be sent to a centrifuge, for example, to separate oil from syrup in an oil recovery step. Oil can be sold as a separate high value product. In this process, a maximum oil production of up to 1.2 lb/bu can be produced (about 0.8 lb/bu of front end oil production, and about 0.4 lb/bu of front end oil production. rear end). In yet another example, the concentrated syrup optionally can be mixed with the resulting protein and germ fines (as well as spent yeast) recovered from protein recovery step 122, then sent to drying step 124 to produce a gluten/ germ/yeast (protein bran) now including syrup.
[00110] Referring now to Figure 9A, this figure depicts a flowchart showing a variation of the system and process of producing ethanol by dry milling 700 with the front end milling method of Figure 9 according to another embodiment of the invention for improve alcohol and/or by-product productions, eg oil and/or protein productions. In this process 700A, at the front end, when compared to process 700 of Figure 9, the liquefied solution from the third liquid/solid separation step 402 is optionally sent to the oil separation step 108, instead of being routed to join the ground solids after the first dewatered milling step 112. Successively, the filtrate from the fiber separation step 704 is recycled back into a countercurrent configuration to join with the ground solids from the first dewatered milling step 112. In addition, the solution liquefied (20 to 25 Brix) from the first liquid/solid separation step 106 is joined with the ground solids from the second dehydrated grinding step 502 and sent to the first conservation tank 114, instead of being routed to the separation step. optional oil 108. Although not described in Figure 9A, if the oil separation step 108 is not optionally used here, the liquefied solution from the third liquid separation step/ Solid 402 can be joined with the fiber portion (fiber mass) from fiber separation step 704 then subjected to fermentation step 111.
[00111] With continuous reference to Figure 9A, the fiber portion (fiber mass) of fiber separation step 704 joins with the heavy phase of optional oil recovery step 108, and optionally oil polishing step 109 and the stream from optional solvent extraction step 110, then subjected to fermentation step 111. As such, fiber washing and dehydrating step 706 of Figure 9 is eliminated. And the cooking water that was added to the fiber portion from the fiber separation step 704 in Figure 9 is now added to the ground solids from the third dewatered milling step 702 in process 700A of Figure 9A. The rest of the front end of the 700A process is generally the same as that of Figure 9.
[00112] With further reference to Figure 9A, the rear end of the 700A process may include, after the distillation step 118, the total vinasse separation step 120 while the dehydration equipment, for example, a paddle screen, vibrating screen, filter centrifuge, pressure screen, screen basin decanter and the like, is used to perform the separation of insoluble solids or “total vinasse”, which includes fiber, from the liquid “fine vinasse” portion. The separated fiber optionally can be sent to caustic treatment step 710 while the fiber is treated with caustic, which includes a weak alkali solution (such as sodium, calcium, and potassium hydroxide, or sodium carbonate, and the like ), to adjust the pH to about 8.5 to 9.5 and separate residual bound proteins from the fiber. A high shear jet cooker or dehydrated milling device can optionally be used in caustic treatment step 710.
[00113] The treated fiber stream is forwarded to a fiber/protein separation step 802 while the dewatering equipment, for example, a paddle screen, vibration screen, filtration centrifuge, pressure screen, decanter screen bowl and the like, is used to perform the separation of fiber from protein part. The separated fiber is then subjected to a fiber washing step 804, and the washed fiber can be used as a feedstock for secondary alcohol production, without any further treatment. This production of secondary alcohol from cellulose is intended to meet government requirements during 2014 for alcohol produced from starch, which must mix 10% of alcohol produced from cellulose.
[00114] The filtrate from the 802 fiber/protein separation step and the 804 fiber washing step is mixed together and the pH adjusted to 5 to 6 by treating the filtrate with sulfuric acid, hydrochloric acid, phosphoric acid, or similar . The filtrate is then joined with the liquid "fine vinasse" portion of the total vinasse separation step 120, and subjected to the protein recovery step 122, followed by the fine protein recovery step 130, like the one in Figure 9. 50% of the protein is made up in the dryer step 124. The concentrate from the fine protein recovery step 130 is sent to the evaporator 136 while the water is removed to produce 60% DS syrup. The DDGS 140 dryer step is eliminated in process 700A of Figure 9A.
[00115] Referring now to Figure 9B, this figure depicts a flowchart showing a variation of the 700A dry milling ethanol production system and process with the front end milling method of Figure 9A according to another embodiment of the invention for improve alcohol and/or by-product productions, eg oil and/or protein productions. In this process 700B, the countercurrent wash of Figure 9A, which includes removing and recycling back into process 700A the liquefied starch plus certain sized solids from the suspension stream in the second liquid/solid separation step 302, in the third step of separation of liquid/solid 402, and in fiber separation step 704, is eliminated. Instead, the milled cornmeal in process 700B is again mixed with initial cooking water in suspension tank 104 to create a suspension and begin liquefaction, as in Figure 3. Successively, the filtrate from the third liquid separation step /solid 402 is joined with the ground solids from the third dehydrated milling step 702 rather than forwarded to the oil separation step 108.
[00116] In addition, the filtrate from the fiber separation step 704 is now sent to the oil separation step 108 instead of recycled back to join with the ground solids from the first dehydrated milling step 112. the filtrate from the second liquid/solid separation step 302 is joined with the ground solids from the second dehydrated milling step 502 instead of mixed with the ground cornmeal just before the slurry tank 104. And the liquefied solution from the first step of liquid/solid separation 106 is similarly joined with the ground solids from the first dewatered milling step 112. Although not described in Figure 9A, if the oil separation step 108 is not optionally used here, the fiber separation step 704 can be discarded and the liquefied starch suspension solution is sent directly from the second holding tank 115 to the fermentation step 111. The rest of the 700B dry milling ethanol production process is ge basically the same as that of Figure 9A.
[00117] The processes of the present invention as shown in Figures 3-9B may include, for example, up to three dehydrated milling steps depending on the production of alcohol, oil, protein, and fiber and the level of purity desired. And with the current dry milling process, the germ and grain particles still exist after distillation and then combine together as a low value DDGS by-product, which includes about 30% protein, 10% oil, and 5% of starch. However, the dry milling ethanol production process, with the front end milling method, breaks the bonds between fiber, protein, oil, and starch in the grain, germ and fiber (pericarp and tip cap) to produce valuable by-products such as oil, protein, extra starch alcohol and cellulose. In fact, instead of low-value DDGS, the processes in Figures 3-9B can be used to produce desirable by-products, including oil, protein, and cellulose.
[00118] While the present invention has been illustrated by a description of various embodiments and while these embodiments have been described in considerable detail, it is not the Applicant's intention to restrict or in any way limit the scope of the Claims attached to such detail. For example, although the various systems and methods described herein 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. In addition, for example, for the optional oil separation step 108, food can be taken from the suspension tank 104, the pre-preservation tank step 113, or the first or second preservation tank step 114, 115. And more broadly speaking, it should be understood that flowcharts can be modified, for example, to include or exclude front end backwashing and oil recovery, to vary the location of the dehydrated milling step, to produce fiber for alcohol production secondary (front end or rear end), and to separate protein from fiber and produce high-protein bran. Furthermore, alcohol recovery and production can be considered to be optional steps and can be excluded from the process. Additional modifications and advantages will easily come to those skilled in the art. Thus, the invention in its broadest aspects is therefore not limited to specific details, representative method and mechanism, and illustrative example shown and described. Consequently, divergences may be made from such details without departing from the spirit or scope of the Applicant's general inventive concept.

权利要求:
Claims (17)
[0001]
1. Alcohol Production Process, characterized in that the process comprises: (A) grinding corn kernels into particles; (B) mixing a ground grain and/or grain component flour with a liquid to produce a paste, including oil, protein, free starch and fiber particles, germ and grain; (C) subjecting the slurry from step (B) to the initiation of liquefaction which includes adding an enzyme to the slurry; (D) after step (C), separate the slurry by particle sizes into a part of solids, including the fiber, grain and germ particles of the slurry and a part of liquid, including oil, protein and starch free from the slurry ; (E) grinding the separated solids part of step (D) to reduce the size of the fiber, grain and germ particles and release the starch, oil and protein therefrom; (F) recombining at least the starch from the liquid portion separated from step (D) with at least the starch released from step (E) to form a second paste; (G) converting starches in the second slurry of step (F) into sugar; (H) produce alcohol from the sugar of step (G) through fermentation; and (I) recover the alcohol after fermentation.
[0002]
2. Alcohol Production Process, according to Claim 1, characterized in that it further comprises separating and recovering the fiber from any of the steps (A) to (I).
[0003]
3. Alcohol Production Process, according to Claim 2, characterized in that the fiber from any of the steps (A) to (G) is separated and recovered before step (H).
[0004]
Alcohol Production Process according to Claim 2, characterized in that separating the remaining fiber after step (H) further comprises subjecting said remaining fiber to a caustic treatment and recovering the treated fiber.
[0005]
5. Alcohol Production Process according to Claim 1, characterized in that it further comprises, before producing alcohol from sugar and recovering the alcohol, separating and recovering the free oil from the liquid part of step (D ).
[0006]
6. Alcohol Production Process according to Claim 5, characterized in that separating and recovering the free oil from the liquid part of step (D) includes extracting the oil from the liquid part of step (D) through the solvent extraction.
[0007]
Process for the Production of Alcohol, according to Claim 1, characterized in that said process comprises washing against the current.
[0008]
8. Alcohol Production Process according to Claim 1, characterized in that step (E) further comprises the following: (E1) separating the ground solids part of step (E) into a second solids part, including particles of fibers, grains and germ from the ground solids part of step (E) and a second part of liquid including the oil, protein and starch released from the ground solids part of step (E).
[0009]
9. Alcohol Production Process according to Claim 8, characterized in that step (E1) further comprises the following: (E2) after separating the ground solids part of step (E) into the second solids part and in the second part liquid, further separate the second part solids into an additional part solids including the fiber, grain and germ particles from the second part solids and an additional part liquid including oil, protein and starch released from the second part of solids.
[0010]
Alcohol Production Process, according to Claim 9, characterized in that it further comprises separating and recovering the released oil from the additional part of liquid before producing alcohol from the sugar and recovering the alcohol.
[0011]
11. Alcohol Production Process according to Claim 8, characterized in that step (E1) further comprises the following: (E3) grinding the second part of solids from step (E1) to reduce the size of the fiber particles , grains and germ and release starch, oil and protein from them.
[0012]
12. Alcohol Production Process according to Claim 11, characterized in that step (E3) further comprises the following: (E4) separating the second part of ground solids of step (E3) into a third part of solids, including fiber, grain and germ particles from the second part of the ground solids of step (E3) and a third part of liquid, including the oil, protein and starch released from the second part of the ground solids of step (E3).
[0013]
13. Alcohol Production Process according to Claim 12, characterized in that step (E4) further comprises the following: (E5) grinding the third part of solids from step (E4) to reduce the size of the fiber particles , grains and germ and release starch, oil and protein from them.
[0014]
Alcohol Production Process according to Claim 1, characterized in that it further comprises separating and recovering the protein from the liquid part of step (D) and/or the protein from the ground solids part of the step (AND).
[0015]
15. Alcohol Production Process according to Claim 14, characterized in that the protein from the liquid part of step (D) and/or the protein from the ground solids part of step (E) is separated and recovered after step (I).
[0016]
16. Alcohol Production Process according to Claim 1, characterized in that the grains and/or grain components are selected from corn, wheat, barley, sorghum, rye, rice and/or oats.
[0017]
17. Alcohol Production Process, according to Claim 1, characterized in that the alcohol is ethanol.

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同族专利:

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公开号 | 公开日

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CA2831268A1|2012-09-27|

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US20120244590A1|2012-09-27|

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CN103597064B|2016-09-28|

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WO2012129500A3|2012-11-15|

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EP2689003A4|2014-12-17|

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EP2689003B1|2020-09-23|

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BR112013024366A2|2016-08-23|

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ES2831861T3|2021-06-09|

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CA2831268C|2017-11-14|

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PL2689003T3|2021-04-06|

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US9689003B2|2017-06-27|

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CN103597064A|2014-02-19|

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US9012191B2|2015-04-21|

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EP2689003A2|2014-01-29|

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HUE052980T2|2021-05-28|

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US20150240266A1|2015-08-27|

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WO2012129500A2|2012-09-27|

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法律状态:
2018-04-03| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|

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2019-06-25| B06T| Formal requirements before examination [chapter 6.20 patent gazette]|

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2020-09-15| B07A| Technical examination (opinion): publication of technical examination (opinion) [chapter 7.1 patent gazette]|

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2021-02-02| B06G| Technical and formal requirements: other requirements [chapter 6.7 patent gazette]|

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2021-02-23| B06I| Publication of requirement cancelled [chapter 6.9 patent gazette]|Free format text: ANULADA A PUBLICACAO CODIGO 6.7 NA RPI NO 2613 DE 02/02/2021 POR TER SIDO INDEVIDA. |

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2021-05-04| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|

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2021-06-08| B350| Update of information on the portal [chapter 15.35 patent gazette]|

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2021-06-29| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 23/03/2012, 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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US201161466985P| true| 2011-03-24|2011-03-24|

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US61/466,985|2011-03-24|

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US201161501041P| true| 2011-06-24|2011-06-24|

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US61/501,041|2011-06-24|

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PCT/US2012/030337|WO2012129500A2|2011-03-24|2012-03-23|Dry grind ethanol production process and system with front end milling method|

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