SYSTEM AND METHOD FOR IMPROVING THE WET AND DRY GRINDING PROCESS OF CORN

Description

1 / 71 “SYSTEM AND METHOD FOR IMPROVING THE WET AND DRY GRINDING PROCESS OF CORN CROSS-REFERENCE TO RELATED ORDER(S)

[0001] This application is a continuation in part of copending U.S. Patent Application No. 17 / 581,434, filed January 21, 2022, and entitled “SYSTEM AND METHOD FOR IMPROVING THE CORN WET MILL AND DRY MILL PROCESS,” which will be issued as U.S. Patent No. 11,623,966 and claims priority over U.S. Provisional Patent Application No. 63 / 140,342, entitled “System and Method for Improving the Corn Wet Mill and Dry Mill Process,” filed January 22, 2021, both incorporated by reference in their entirety for all purposes. FIELD OF THE INVENTION

[0002] The present invention relates to wet and dry milling processes of corn and produces high-purity starch as a raw material for synthetic biology, alcohols and oils as biofuels, and other co-products such as protein-rich animal feed. The present invention also relates to soybean processing. BACKGROUND

[0003] The wet milling process of corn, over the last fifty years, has been used to produce starch pastes that are then converted into corn syrup for human consumption. This low-cost corn syrup has been used to replace sugar in many products. There is evidence that excessive consumption of high-fructose corn syrup negatively affects human health. At the same time, the consumption of petroleum-based products by the world's population has created a global warming problem. Petition 870250092067, dated 08 / 10 / 2025, p. 5 / 119 2 / 71 Wet corn mills are exploring ways to use their existing infrastructure to produce products other than corn syrup that are more beneficial to human health and the environment.

[0004] Many companies use corn as a feedstock to replace fossil-based hydrocarbon fuels. Over 200 dry milling ethanol plants have been built and produce over 15.8 billion gallons of fuel ethanol in the U.S. annually. The dry milling process represents a 2,000-year-old technology for converting grain starch into alcohol. There have been some improvements, but these are just the beginning. More new green technology processes will emerge in the future, such as the production of butanol from starch.

[0005] Figure 1 illustrates a typical dry milling process 100. A supply of corn is fed through a hammer mill (grinding) Step 109 to reduce the particle size. The sieve size in the hammer mill is typically 2 mm to 3.6 mm. The corn flour produced in the hammer mill particle size reduction Step 109 typically contains a very wide bell-shaped particle size distribution, ranging from less than 50 microns to as small as 2 to 3 mm. The grinding step 109 is followed by a liquefaction step (steps 101, 102, 103A and 103B), where the ground cornmeal is mixed with cooking water to create a paste in a paste tank (step 101), and an enzyme such as alpha-amylase is typically added, followed by a steam injection stove (step 102) (optional) to heat the liquefied starch to a higher temperature if necessary. The pH is adjusted. Petition 870250092067, dated 08 / 10 / 2025, page 6 / 119 3 / 71 to approximately 5.0 to 6, and the temperature is maintained between 50 °C and 105 °C to convert the insoluble starch in the paste into soluble starch in two liquefaction tanks (steps 103A and 103B).

[0006] The current after the liquefaction stages 103A and B contain approximately 26 to 38% dry solids (DS), with all the components found in corn kernels, including sugars, proteins, fiber, starch, germ, coarse sand, oil, and salts, for example. Generally, there are three types of insoluble solid particles in the liquefaction stream: fiber, germ, and grain, with all three solids exhibiting approximately the same particle size distribution.

[0007] Liquefaction Steps 103A and B are followed by a simultaneous saccharification and fermentation step, Step 104. This simultaneous step is referred to in the industry as Simultaneous Saccharification and Fermentation (SSF). In some commercial dry-mill ethanol processes, saccharification and fermentation occur separately (not shown). Both individual saccharification and SSF can take 50 to 60 hours. Fermentation converts sugar into alcohol using a fermenter. After saccharification and fermentation, in Step 104, distillation (and dehydration) Step 105 occurs, which uses a still to recover the alcohol produced in Step 104.

[0008] Finally, the final stage of the Process Step 100, which occurs after distillation (and dehydration) Step 105, includes a centrifugation Step 106 using a decanter. This involves centrifuging the residues, the whole vinasse, produced in distillation Step 104 and dehydration Step 105, to separate the... Petition 870250092067, dated 08 / 10 / 2025, page 7 / 119 4 / 71 insoluble solids (wet cake) of the liquid (fine vinasse). The wet cake includes fibers, of which there are three types: (1) pericarp, with average particle sizes typically around 1 mm to 3 mm; (2) capsule tip, with average particle sizes around 500 microns; (3) and fine fibers, with average particle sizes around 250 microns. The centrifuge liquid contains about 6% to 8% dry solids (DS).

[0009] The fine vinasse enters the evaporators in Evaporation Step 107 to evaporate the water. This leaves a thick syrup containing the soluble (dissolved), fine suspended solids (usually less than 50 μm), and floating solids from Fermentation Step 104. This generally equates to about 25% to 40% dry solids. The concentrated paste may undergo an optional oil recovery step (not shown), where the paste can be centrifuged to separate the oil from the syrup. The oil can be sold as a high-value separate product. The oil yield is typically about 0.4 lb / Bu of high-free-fat corn. This oil yield recovers only about M of the corn oil. About half of the oil contained in the corn kernel remains within the germ after distillation step 105 and cannot be separated in the typical dry milling process using centrifuges. The free-fat content, created when the oil is held in the fermenter for approximately 50 hours, reduces its value.The centrifugation (deoiling) stage removes less than 50% of the oil present in the thickened syrup, because the protein and oil form an emulsion that cannot be satisfactorily separated by centrifugation alone, as is currently practiced. Petition 870250092067, dated 08 / 10 / 2025, page 8 / 119 5 / 71

[0010] The centrifuged wet cake and de-oiled syrup, which still contains more than 10% (dry matter concentration) of oil, can be mixed and the mixture can be sold to feedlots and dairies as Wet Distillers Grain with Soluble (WDGS). Alternatively, the syrup can be mixed with the wet cake and then the concentrated syrup mixture can be dried using the drying in Step 108 and sold as Dried Distillers Grain with Soluble (DDGS) to feedlots and dairies. This DDGS contains all the protein and 75% of the oil from the corn. However, the value of the DDGS is low due to the high percentage of fiber and, in some cases, the oil is an obstacle to animal digestion. The percentage of starch in DDGS is typically as low as 5 to 6%.

[0011] The typical dry milling process can also produce a clean sugar solution through a filtration method to remove all insoluble solids (e.g., fiber and protein) from the liquefied starch solution. However, this clean sugar solution still contains all soluble solids, such as ash from the interior of the corn, as well as small amounts of corn oil. Many new green technology processes require much purer starch, free of oil and soluble solids, as feedstock.

[0012] A typical corn kernel 1400 is illustrated in Figure 14. The kernel 1400 includes a husk 1410, a mealy endosperm 1420, a corn-like endosperm 1430, with cells filled with starch granules in a protein matrix, a germ 1440 and a tip capsule 1450. A typical corn composition is illustrated in Table 1 below. Petition 870250092067, dated 08 / 10 / 2025, page 9 / 119 6 / 71 Table 1 Composition of Yellow Dent corn Dry base Percentage in grain Starch Protein Oil Ash Sugar Fiber Endosperm 82.90% 88.40% 8% 0.80% 0.30% 0.60% 1.90% Germ 11% 11.90% 18.40% 29.60% 10.50% 10.80% 18.80% Pericarp 5.30% 7.30% 3.70% 1% 0.80% 0.30% 86.90% Tip Coverage 0.80% 5.30% 9.10% 3.80% 1.60% 1.60% 78.60% Whole Grain 100.00% 75% 8.90% 4% 1.50% 1.70% 8.90% of body weight in lb. / Bu 47 35.25 4.183 1.88 0.705 0.799 4.183 Endosperm 38.963 34.44329 3.11704 0.311704 0.116889 0.233778 0.740297 Germ 5.17 0.61523 0.95128 1.53032 0.54285 0.55836 0.97196 Pericarp 2.491 0.181843 0.092167 0.02491 0.019928 0.007473 2.164679 Tip Cover 0.376 0.019928 0.034216 0.014288 0.006016 0.006016 0.295536 pericap+tipcap 2.867 0.201771 0.126383 0.039198 0.025944 0.013489 2.460215 % comp 100.00% 7.04% 4.41% 1.37% 0.90% 0.47% 85.81% change after promotion -32.648 0.375 0.42 Byproduct Total 15.127 0.602 4.558 1.88 1.105 2.799 4.183 % laboratory analysis 100 3.979639 30.13155 12.42811 7.304819 18.50334 27.65254 % in grain Starch Protein Oil Ash Sugar Fiber Soluble solids 3.904 1.105 2.799 Yeast 0.83333333 0.375 0.458333 Germ 3.45356 0.95128 1.53032 0.97196 Corn protein 4.169041 3.11704 0.311704 0.740297 Pericap + Tipcap 2.827567 0.201771 0.126383 0.039198 2.460215 Total 15.1875013 0.201771 4.569703 1.881222 1.105 2.799 4.630805. Petition 870250092067, dated 08 / 10 / 2025, page 10 / 119 7 / 71 SUMMARY OF THE INVENTION

[0013] This new wet corn milling process includes a continuous steeping approach / system, an early starch separation process for easy access, fine milling to ensure germ protein without the use of solvents or heat, and phase separation to collect the fermentation product.

[0014] The process can produce high-purity sugar as a raw material for synthetic biology, various biofuels, highly digestible animal feed, and other valuable co-products. A new continuous maceration tank with probiotic-infused liquid reduces the total maceration time with a lower capital investment.

[0015] After the first milling of the corn kernels, the easily accessible starch from the mealy endosperm of the corn kernel is separated from the corn endosperm and the germ. The easily accessible starch can be thoroughly washed to a high level of purity. On the other hand, the corn endosperm includes more difficult-to-access starch bound to protein and oil. The more difficult-to-access starch, protein, and oil are processed separately.

[0016] New components of this process can be used separately or in different combinations to produce multiple possible co-products in addition to the traditional DDGS and gluten meal produced in most current wet mills. Co-product options include pure starch, pure sugar, yeast / germ protein meal, ethanol, and butanol. This process can Petition 870250092067, dated 08 / 10 / 2025, page 11 / 119 8 / 71 efficiently produce a high yield of sustainable aviation fuel (e.g., an alcohol biofuel created by mixing sugar and culture), which is then combined with a small amount of oil; phase separation is then used to remove the biofuel from the culture mixture, keeping the alcohol concentration low enough to preserve the health of the culture.

[0017] Improvement No. 1: Continuous maceration tank design

[0018] A typical wet mill system uses 6 to 8 batch tanks. In contrast, as shown in Figure 18, according to some embodiments, this system includes one large tank with 6 to 12 internal chambers. Each chamber has 4 to 8 paddles that move the corn kernels progressively through the chambers, pushing them outwards and downwards to the next chamber, or inwards and downwards to the next chamber, alternating the directions of movement in each chamber.

[0019] The blades are controlled by a variable speed motor connected to a central shaft. A tank with more chambers is used in applications that require longer maceration times.

[0020] The steeping liquid flows from the bottom of the tank, in countercurrent. For a wet mill that processes corn, the steeping fluid includes four probiotic microorganisms (Lactobacillus plantarum, Lactobacillus amylovorus, Lactobacillus mucosae and Lactobacillus fermentum) known to improve digestion and the immune system of animals. Petition 870250092067, dated 08 / 10 / 2025, p. 12 / 119 9 / 71

[0021] In less than 24 hours, the steeping fluid increases the concentration of probiotics by 10⁹ CFU, and the concentration of lactic acid increases by 20% (dry basis). Due to the higher concentration of lactic acid, the steeping time can be reduced from 50 hours to 30 hours, increasing the moisture content of the corn from 10% to 50%.

[0022] Improvement No. 2: A process for maximizing the purity of starch obtained from a typical wet corn mill

[0023] In a typical wet corn mill system, the starch from all parts of the corn kernel is processed through a 12-stage countercurrent washing system, with a water to starch paste ratio of 1:1, to produce starch that includes many soluble proteins.

[0024] In contrast to a typical process, in some embodiments, after the first milling, the easily accessible starch of the farinaceous endosperm of the corn grain is separated from the corneous endosperm and the germ. The germ includes difficult-to-access starch, bound to proteins and oil.

[0025] As shown in Figure 19A, only the readily accessible starch from the farinaceous endosperm starch is then processed through the 12-stage countercurrent washing system. The amount of water used is similar to that of the typical process, resulting in a higher water-to-starch ratio (i.e., more than 1:1, 2:1, 3:1 or higher) than in the typical process. As a result, more soluble protein is removed, resulting in a higher purity starch paste. This pure starch can then be used as Petition 870250092067, dated 08 / 10 / 2025, page 13 / 119 10 / 71 Carbohydrate raw material for the growing synthetic biology, biochemistry and renewable chemistry industries.

[0026] Improvement #3: Addition of yeast to the germ to create a higher value feed product for aquaculture

[0027] As shown in Figure 19A, after the germ is separated (but still moist), it is combined with yeast, which propagates using the small amount of starch present in the germ. The resulting mixture is then dehydrated to produce a feed product that includes germ protein and yeast. This product can improve wet milling margins compared to typical gluten meal production for chickens.

[0028] Enhancement No. 4: A process for separating the protein from the germ, preserving the protein structure without denaturing it.

[0029] In the typical wet milling process of corn, solvents and heat are used to separate the germ protein and oil. However, the solvents commonly used in wet milling of corn are toxic to humans. In addition, the heat used denatures the germ protein, making it difficult for animals or humans to digest.

[0030] In contrast to the typical process, in some embodiments, as shown in Figure 20A, the germ is ground to < 50 microns without creating an emulsion, and then the fine fiber cake, starch and protein are separated. The resulting protein is therefore produced without the use of toxic solvents and is more nutritious, whether for use in animal feed or for human consumption. Petition 870250092067, dated 08 / 10 / 2025, page 14 / 119 11 / 71

[0031] Improvement No. 5: A process for saccharification of starch paste in a high-purity sugar solution

[0032] Typical wet corn mills that seek to produce a high-purity corn-based sugar solution utilize an expensive membrane separation process.

[0033] In contrast to the typical process, in some embodiments, as shown in Figures 19B and 20B, an alternative process exists whereby pure starch paste, derived primarily from starch found in the hard-to-reach horny endosperm, is converted into a sugar solution with less than 0.0001% soluble protein (compared to the 0.05-0.1% soluble protein in typical current wet mills). This sugar solution can then be used as a carbohydrate feedstock in the synthetic biology, biochemistry, renewable chemistry, and food industries, with a smaller carbon footprint than traditional sugar processes. It can also be fermented into ethanol, butanol, or other biofuels.

[0034] Enhancement No. 6: A process for converting hard-to-find corn starch into ethanol

[0035] In a typical wet mill, the starch from all parts of the corn kernel is processed into high-fructose corn syrup.

[0036] In contrast to the typical process, in some embodiments, as shown in Figures 19C and 20C, this process converts only a portion of the starch—the starch of the endosperm and germ—into ethanol. Petition 870250092067, dated 08 / 10 / 2025, p. 15 / 119 12 / 71

[0037] Enhancement No. 7: A process for converting hard-to-obtain corn starch into sustainable aviation fuel or other alcoholic biofuels such as butanol.

[0038] Ethanol production involves the fermentation of a starch paste to produce ethanol. As shown in Figures 19E and 20E, according to some embodiments, the liquefied and saccharified solution can be combined with different crops (both naturally occurring and bioprospected or custom-designed) to produce different biofuel products, including butanol or other alcohols, for use as sustainable aviation fuel or feedstock for sustainable aviation fuel.

[0039] Enhancement No. 8: A process that uses phase separation to remove the product of fermentation, preserving the health of the culture and maximizing the yield of an alcohol, including butanol.

[0040] Different cultures of microorganisms ferment sugars to produce different types of alcohol, including ethanol and butanol. As fermentation progresses, the concentration of alcohol in the mixture increases. At some point, the alcohol concentration causes the death of the microorganism(s), limiting the alcohol yield of the process.

[0041] In typical corn milling processes that produce ethanol, yeast can survive in a solution containing up to 14% ethanol; distillation towers are then used to evaporate and condense the alcohol. However, microorganisms that produce butanol do not Petition 870250092067, dated 08 / 10 / 2025, page 16 / 119 13 / 71 can survive in solutions with a concentration greater than 2% butanol.

[0042] To overcome this challenge and maintain the continued health of the culture, as shown in Figures 19E and 20E, according to some embodiments, the sugar-alcohol culture mixture is combined with a small amount of oil. The fermentation product (e.g., butanol) is attracted by the oil, liquid-liquid phase separation occurs, and the butanol-oil mixture can be separated from the aqueous sugar and culture solution. The oil incorporated to promote phase separation can be corn oil previously extracted from corn kernels, any other vegetable oil, an oil of animal origin such as tallow, or a petroleum-derived oil.

[0043] Improvement #9: Limit the water in the sugar solution to reduce energy consumption in the process.

[0044] Different microorganism cultures require different sugar concentration levels. For example, ethanol needs a 24% sugar solution, while butanol needs a 6-8% sugar solution. As shown in Figures 19E and 20E, the process manages the amount of water added so that the solution does not exceed the desired sugar concentration. The wet milling plant can therefore conserve water and avoid using additional energy to evaporate water or further concentrate the solution.

[0045] Improvement #10: Use soybeans other than corn in this process and with this equipment to produce Petition 870250092067, dated 08 / 10 / 2025, page 17 / 119 14 / 71 soy-based foods for human consumption without the use of carcinogenic solvents

[0046] To produce soybean oil, most soybean processors currently grind the beans and mix them with the solvent hexane before pressing the beans to extract the oil. However, hexane is carcinogenic and can cause nerve damage. In addition, the resulting soybean meal has lower nutritional value because the soy protein has been denatured.

[0047] In some embodiments, the process, as shown in Figure 21A, allows the extraction of soybean oil and other soy-based products without the use of toxic solvents. BRIEF DESCRIPTION OF THE DRAWINGS

[0048] Figure 1 illustrates a typical dry grinding process.

[0049] Figure 2 illustrates a degerming process using a germ cyclone (e.g., germ separation) according to some embodiments.

[0050] Figure 3 illustrates a fiber washing process (e.g., fiber separation) with countercurrent washing using a multi-stage pressure screen, according to some embodiments.

[0051] Figure 4 illustrates a starch / gluten separation process (e.g., starch and protein separation) according to some embodiments.

[0052] Figure 5 illustrates a starch washing process (e.g., starch washing and purification) according to some embodiments. Petition 870250092067, dated 08 / 10 / 2025, p. 18 / 119 15 / 71

[0053] Figure 6 illustrates an enhanced dry milling process to produce pure starch for biotechnological processes and to separate fiber and germ before fermentation, according to some embodiments.

[0054] Figure 7 illustrates an enhanced dry milling process to produce pure starch for biotechnological processes and to produce pure fiber before fermentation, according to some embodiments.

[0055] Figure 8 illustrates an enhanced dry milling process to produce pure starch for biotechnological processes and to produce pure fiber and organic oil before fermentation, according to some embodiments.

[0056] Figure 9 illustrates an enhanced dry milling process to produce pure starch for biotechnological processes and to produce pure fiber and organic oil before fermentation, and animal feed after fermentation, according to some embodiments.

[0057] Figure 10 illustrates a flow diagram of a wet mill according to some embodiments.

[0058] Figure 11 illustrates an improved wet mill process for producing fuel alcohol according to some embodiments.

[0059] Figure 12 illustrates a two-stage double germ cyclone process for recovering germ after liquefaction in an enhanced dry mill process according to some embodiments.

[0060] Figure 13 illustrates a process for using partially husked brown rice to produce alcohol and pure starch for biotechnological processes, as well as products Petition 870250092067, dated 08 / 10 / 2025, page 19 / 119 16 / 71 as organic oil, rice protein and yeast protein for human consumption according to some embodiments.

[0061] Figure 14 illustrates a corn kernel according to some modalities.

[0062] Figure 15 illustrates the particle size analysis of corn flour after hammer milling, with different sieve sizes according to some methods.

[0063] Figure 16 illustrates the size distribution of corn flour according to some modalities.

[0064] Figure 17 illustrates the protein x particle size relationship of corn flour after hammer milling according to some methods.

[0065] Figure 18 illustrates a continuous maceration tank according to some embodiments.

[0066] Figure 19A illustrates an enhanced wet milling process that produces maximum pure starch and high-value germ and yeast protein flour, according to some embodiments.

[0067] Figure 19B illustrates an enhanced wet milling process that produces pure starch, germ / yeast protein flour and pure sugar, according to some embodiments.

[0068] Figure 19C illustrates an enhanced wet milling process that produces pure starch, germ / yeast, protein flour and alcohol, according to some embodiments.

[0069] Figure 19D illustrates an improved wet milling process that produces pure starch, flour Petition 870250092067, dated 08 / 10 / 2025, page 20 / 119 17 / 71 protein from germ / yeast and additional pure starch, according to some variations.

[0070] Figure 19E illustrates an enhanced wet milling process that produces pure starch, germ / yeast protein flour, lactic acid, and a sustainable aviation fuel (SAF) alcohol, such as butanol, according to some embodiments.

[0071] Figure 20A illustrates a wet milling process that produces pure starch, gluten flour feed, and yeast / germ protein flour, according to some embodiments.

[0072] Figure 20B illustrates a wet milling process that produces pure starch, sugar solution, gluten flour ration, and yeast / germ protein flour, according to some embodiments.

[0073] Figure 20C illustrates a wet milling process that produces pure starch, alcohol, gluten flour feed and yeast / germ protein flour, according to some embodiments.

[0074] Figure 20D illustrates a wet milling process that produces additional pure starch, gluten flour feed, and yeast / germ protein flour, according to some embodiments.

[0075] Figure 20E illustrates a wet milling process that produces pure starch, sustainable aviation fuel (SAF, such as butanol or other alcohol), gluten flour, lactic acid, and yeast / germ protein flour, according to some embodiments. Petition 870250092067, dated 08 / 10 / 2025, page 21 / 119 18 / 71

[0076] Figure 21A illustrates a soybean processing method for producing probiotic foods for human consumption, according to several modalities. DETAILED DESCRIPTION OF PREFERRED MODALITIES

[0077] A Yellow Dent corn kernel is illustrated in Figure 14 and its composition is illustrated in Table 1. There are 34.4 pounds of starch per bushel of corn. Most of the starch is contained in two types of endosperm: farinaceous endosperm and corneous endosperm. The starch within the farinaceous endosperm is loosely packed within the endosperm and fairly easy to separate (e.g., easy-to-separate starch). It can be used to produce pure starch as a raw material for green technology processes. The starch in the corneous endosperm (e.g., difficult-to-separate starch) is contained within cells filled with granular starch in a protein matrix. The starch in the corneous endosperm is not easy to separate as it is bound to protein.

[0078] In some embodiments, a process is illustrated that combines starch (in the purest form of the farinaceous endosperm) and all other corn compounds (pericarp, husk, fine fiber, corn protein, germ and coarse sand) as raw material for a dry milling process to produce alcohol and by-products such as organic oil for human consumption, corn oil for biodiesel, animal feed for cows, chickens, pigs, fish and domestic animals, etc. A similar wet milling system is illustrated in Process 1000 of Figure 10.

[0079] In some embodiments, a process separates only about half (e.g., 15 lb / bu) of the free starch from the farinaceous endosperm with a process of Petition 870250092067, dated 08 / 10 / 2025, page 22 / 119 19 / 71 Improved wet milling is simple and low-cost. The process utilizes the remaining corn as feedstock to produce alcohol and higher value-added byproducts with an improved dry milling process, described in detail below. In comparison, a typical dry milling process converts all the starch from the corn into alcohol and uses technology that is over 2,000 years old.

[0080] In some embodiments, a process provides an effective way to separate the starch from the farinaceous endosperm first and use the remainder of the corn as feedstock for the production of alcohol and high-value co-products with an enhanced dry milling process.

[0081] A) Improved wet milling process according to some embodiments

[0082] As illustrated in Process 1100 of Figure 11 shows that corn undergoes five stages to produce a pure starch paste as a raw material for green technology processes. The remaining corn is used as feedstock for the dry milling process to produce alcohol and byproducts such as animal feed. The five-stage process includes: a) the immersion / soaking process 1600 is used to soften and hydrate the corn so that it has more than 45% moisture; b) the degerming process 200, which uses a Baumé starch paste of approximately 12°C as a liquid medium to separate the germ from the coarse sand and fiber, utilizing density differences through the use of two different sets of double degerming cyclone processes 200; c) the use of a novel three-section paddle sieving process 300 to remove the starch from the coarse sand and fiber before it is used as a raw material for Petition 870250092067, dated 08 / 10 / 2025, page 23 / 119 20 / 71 to produce alcohol and valuable by-products, such as animal feed; d) use of a starch / gluten separation process 400 with a double-nozzle centrifuge to remove gluten from starch and produce by-products, including gluten flour, as chicken feed; ee) purification of starch paste in a 12-stage starch washing process 500 with a 10 mm starch washing cyclone network and a countercurrent washing configuration.

[0083] In Figure 11, process 11A illustrates a part of the process for the production of pure starch, liquid starch or pure corn sugar (e.g., for biotechnological feedstock) according to some embodiments. Process 11B illustrates the other part of the alcohol production process according to some embodiments.

[0084] The following are brief descriptions of each step in more detail:

[0085] 1) 1600 Soaking / Soaking Process in Figure 11: Corn kernels are soaked / soaked in an aqueous solution of sulfur dioxide at 100 to 600 ppm at approximately 50 °C (just below the temperature of starch gelatin) for 5 to 60 hours to macerate and soften the corn kernels. The soaking / soaking time depends on the desired starch yield and purity requirements. Longer soaking / soaking times provide higher starch yields as well as higher purity starch. The 1600 soaking / soaking process can be a continuous or batch system. Larger plants or existing wet milling plants can use the typical batch system. New and small plants can use a new continuous soaking / soaking system. The process water used for the Petition 870250092067, dated 08 / 10 / 2025, page 24 / 119 21 / 71 maceration / soaking process 1600 comes from the overflow of the gluten nozzle centrifuge in a system like Process 400 in Figure 4. Lactic acid-producing cultures can be added to the process water to produce lactic acid before being sent to the maceration tank to accelerate this process.

[0086] The soaking / maceration process 1600 is normally set up in countercurrent mode to maximize the extraction of soluble solids (e.g., ash) from the corn. The soaking / maceration corn kernels fully absorb the water and reach more than 45% moisture in less than 10 hours. The maceration liquid from this soaking / maceration step has about 8 to 10% solids and is then sent to evaporator 3 in Step 1106 to concentrate the flow to about 30 to 40% DS syrup (dry matter). This syrup contains most of the plant nutrients (K+ and P+), as well as a large amount of lactic acid (up to 10% on a dry basis), which can be used as a natural organic insect repellent to keep them away from young plants. The concentrated syrup can also be mixed with fiber from a screw press in Step 1107 and then dried in a dryer in Step 108 to produce DDGS as feed for livestock.

[0087] 2) The degerming process 200 in Figure 11 after Process 1600, which may be the same as or similar to Process 200 in Figure 2: Soaked / soaked corn kernels with more than 45% moisture are fed into the degerming process 200 in Figure 2. The soaked / soaked corn is fed into the grinding stage in Step 201 of Figure 2 to open the corn and release the starch, which is Petition 870250092067, dated 08 / 10 / 2025, p. 25 / 119 22 / 71 is poured into tank 1astage in Stage 202 to form a Baumé starch paste of approximately 12°C. A grinding mill or roller mill can be used to open corn kernels. This 12° Baumé starch paste is used as a liquid medium to float the germ in two double germ cyclone processes, which include a 23 cm degerming cyclone followed by a 20 cm degerming cyclone. Optionally, a 15 cm cyclone process (one cyclone) Cyclone A (15 cm) followed by another cyclone B (15 cm) can also be used on a small plant.

[0088] In Step 205, Baumé starch paste 12° containing germ particles, coarse sand, and fiber is fed to a first set of twin germ cyclones for the first germ / grain separation. Since the germ particles are lighter than the liquid, they are released at the top of the first germ cyclone (23 cm) as an overflow, then sent to dewatering and washing in Step 208 to produce pure germ for subsequent corn oil extraction. Also in Step 205, the underflow from the first cyclone (23 cm) is fed to a second cyclone (20 cm). Still in Step 205, the excess from the second cyclone (8 inches) is sent back to the 1st stage tank, adjusted in Step 202. The coarse sand and fiber, heavier than the liquid, exit the bottom of the second cyclone as an underflow, followed by dewatering and grinding in Step 203 and sent to a 2nd stage tank in Step 204.The 12° Baumé starch paste with residual germ particles that are not removed during the 1st germ / grain separation in Step 205 are fed to the 2nd germ / grain separation in Step 206 with the other set of. Petition 870250092067, dated 08 / 10 / 2025, page 26 / 119 23 / 71 double degerming cyclone processes in Step 206 to recover more germ.

[0089] In the second double germ cyclone process, the excess from the first germ cyclone is recycled back to the 1st stage tank in Step 202. The underflow from the first cyclone is fed to the second cyclone and the excess from the second cyclone is recycled back to the 2nd stage tank in Step 204. The underflow from the second cyclone is fed to a three-section paddle screen in Step 300 (continue to Process 300 in Figure 3) to wash the free starch from the coarse sand / fiber before sending it to produce alcohol and by-products such as animal feed.

[0090] 3) Liquid / Solid Separation and Washing in Process 300 in Process 1100 of Figure 11: The novel three-section paddle sieve described in U.S. Provisional Patent Application 63 / 131,035 is incorporated herein by reference, which can be used to separate coarse sand and fibers from starch paste as a bottom flow of the degerming process 200. This novel paddle sieve has a three-section sieve: a) a first sieve with 50-micron open slots, for example, parallel to the flow; b) 2nd and 3rd sieve sections with 75-micron open slots, for example, parallel to the flow. The bottom stream from the last degerming cycle contains a 12° Baumé starch paste with coarse sand, fibers, and larger solid particles that is fed to this three-section paddle sieve in Step 300. The overflow from the gluten centrifuge in Step 402 of Figure 4 can be used as wash water in this step.The filtrate from the first sieve section can be fed into the starch / gluten separation section of Process 400. The filtrate... Petition 870250092067, dated 08 / 10 / 2025, page 27 / 119 24 / 71 of the 2nd and 3rd sieve sections can be fed into the 1st stage tank in Stage 201 to mix with the ground corn from Stage 201 and form a Baumé 12° starch paste in the 1st stage tank in Stage 201.

[0091] 4) The wet milling process 1100 of Figure 11 includes the starch / gluten separation process 400 of Figure 4: The Baumé starch paste 12° from the first filtration of the three-section paddle sieve in Process 300 is sent for starch / gluten separation in Process 400. The Baumé starch paste 12° is sent to a primary centrifuge in Step 401 to separate the gluten from the starch in the starch / gluten separation process 400 in Process 400 of Figure 4.

[0092] In Step 401, the starch paste (around 22° Baumé) exits as the heavy phase from a centrifuge with a primary nozzle. The wash water from the first starch washing step in Process 500 of Figure 11 is fed from the bottom of the centrifuge with the primary nozzle in Step 401 as replacement wash water at the outer edge of the inner container of the primary centrifuge in Step 401 to remove gluten from the starch before it exits as the heavy phase from the nozzle of the centrifuge with the primary nozzle in Step 401. The gluten, which is lighter than the starch, will exit as the light phase from the top of the primary centrifuge in Step 401. It is then fed to a gluten thickening centrifuge in Step 402 to further concentrate the paste to more than 30% by volume of gluten as residual flow.

[0093] In Step 402, clean process water exits as the light phase from the top of the centrifuge with the gluten nozzle. The clean water is used as process water for degerming in Process 200, sand separation and washing. Petition 870250092067, dated 08 / 10 / 2025, page 28 / 119 25 / 71 coarse and fibers in Process 300 and steeping water for steeping in Process 1600. The residual flow from the gluten thickening centrifuge in Step 402 is sent to a vacuum drum filter to further dehydrate the gluten, producing a gluten cake with approximately 40% dry solids. The cake is subsequently dried in a dryer to produce gluten flour, which can be used as chicken feed.

[0094] 5) Starch washing - Process 500 of Process 1100 of Figure 11, which may be the same or similar as described in more detail in Figure 5. A Baumé starch paste of approximately 20° to 22°, from the bottom stream of the primary centrifuge, is mixed with the top stream of the 2nd stage of a multi-stage (typically 12) 10 mm starch washing cyclone network. The paste is then fed into the 10 mm starch washing cyclone network of the 1st stage to perform dilute washing and to separate and purify the starch paste, removing soluble and insoluble proteins from the starch paste with a countercurrent washing configuration. The starch paste flows downstream from the 1st stage to a 2nd stage, continuing to a 3rd stage and so on until it exits as a final (12th) stage starch washing cyclone, as a pure Baumé starch paste of 23° with less than 0.35% protein on a dry basis.The clean water used as wash water enters the last (12th) stage and flows upstream to perform the dilution washing / separation from stage 12 to stage 11. The water then continues to flow countercurrently to stage 10 and so on until it exits the overflow of the starch washing cyclone from the 1st stage, which will be used. Petition 870250092067, dated 08 / 10 / 2025, page 29 / 119 26 / 71 as wash water in the primary centrifuge for starch / gluten separation in process 400 (described in detail in Figure 4).

[0095] The starch paste flows through the Fiber Washing Process 300, the Gluten / Starch Separation Process 400, and the Starch Washing Process 500 to maximize starch yield and purity. When this high starch yield and purity in the starch paste is not required, some of the starch purification steps can be eliminated to meet the starch purity specification for any specific green technology process.

[0096] The solid phase of the liquid / solid separation in Process 300 of Figure 11 contains much less starch than corn. This can be taken into consideration when using it as a raw material for alcohol production. It is important to remove the fiber and germ in the initial phase (before fermentation and during liquefaction) to produce a high alcohol content in the beer.

[0097] The solid phase (coarse sand and fiber) of the liquid / solid separation in Process 300 of Figure 11 may undergo another optional particle size reduction in Step 1114 before going to the pulp tank in Step 101, followed by a steam injection stove in Step 102 and a liquefaction tank 1 (above 26° Baumé) in Step 103 to liquefy the starch. The pulp is then fed to the liquid / solid separation in Step 701 to separate the solid (coarse sand and fiber) from the liquid (liquefied starch). The solid (coarse sand and fiber) from the liquid / solid separation in Step 701 is sent to the liquefaction tank 2 in Step 103. 604 (below 5° Baumé) to further liquefy the starch. Petition 870250092067, dated 08 / 10 / 2025, page 30 / 119 27 / 71 at a much lower Baumé setting. This is followed by liquid / solid separation in Step 605, followed by grinding in Step 606 to further fragment the solid (coarse sand). The slurry is then fed to liquid / solid separation and washing in Step 702.

[0098] The cooking water is used to wash away any starch / coarse sand / protein from the fiber to produce pure fiber before fermentation. The washed fiber goes to the sieve press in Step 1107 to produce 43% DS cake. It is then mixed with the evaporator syrup in Step 1106 and fed to the dryer in Step 108 to produce DDGS. The steeping liquid from the steeping / mashing in Process 1600 mainly contains soluble solids from the interior of the corn. It is sent to evaporator 3 in Step 1106 to concentrate the liquid to 30-40% DS syrup. It is then mixed with the fiber to produce DDGS.

[0099] The liquefaction tanks above, with high Baumé liquefaction (> 26° Be) in Stage 103 and low Baumé liquefaction (< 5° Be) in Stage 604, are connected to the new three-section paddle screen with high washing capacity in Stage 701, according to some embodiments. The 1st section screen can be 75 microns (can be 50 to 200 microns depending on oil and alcohol yield), with the screen slots parallel to the flow direction. The 2nd and 3rd section screens can be 200 microns (100 to 600 microns depending on oil and alcohol yield) with the screen slots open parallel to the fluid flow. The filtrate from the first section of the screen can be sent to fermentation in Stage 104. The filtrate (washing liquid) from the 2nd and 3rd sections of the screen can be recycled back to the tank. Petition 870250092067, dated 08 / 10 / 2025, page 31 / 119 28 / 71 of pulp in Step 101 of Figure 11. The liquid from the three-section paddle screen in Step 702 can be used as wash water to remove germs, coarse sand, and fine fiber particles smaller than 200 microns. The filtrate with these medium-sized solid particles is recycled back to the pulp tank.

[00100] All vinasse, after fermentation in Step 104, followed by distillation in Step 105, is sent to a nozzle centrifuge in Step 1130 to separate the oil from the protein. The oil stream exits as the light phase of the clarifier as feedstock for biodiesel production. The protein stream exits as the heavy phase of the clarifier in Step 1130 and is sent to the protein decanter in Step 1140 for dehydration, producing a wet yeast protein cake. The cake is subsequently dried in a ring dryer in Step 1120 to produce high-quality protein for pets and fish farms. The excess from the protein decanter in Step 1140 is recycled as a return stream.

[00101] B) Improved dry milling process

[00102] As illustrated in Figure 14 and Table 1, there are approximately 34 lb / bu of starch within the corn kernels. The starch in the farinaceous endosperm is free starch, internally compacted and very easy to separate into granules of pure free starch. Thus, the coarse sand of free starch disclosed in this disclosure is termed free starch or liberated starch when such starch is released from the kernels.

[00103] The starch in the farinaceous endosperm is in the form of starch granules in a protein matrix (called Petition 870250092067, dated 08 / 10 / 2025, page 32 / 119 29 / 71 coarse sand), which is not easily fragmented to release the starch. One objective of this disclosure is to provide a simple and effective way to separate the starch from the farinaceous endosperm (e.g., free starch) and produce a purer form of corn sugar for biotechnological processes. Then, all other components of the corn grain (pericarp, head tip, germ, e.g., coarse sand) are used as feedstock for an improved dry milling process in order to produce alcohol and high-value byproducts (oil and animal feed). Thus, when termed free starch or released starch, this starch is primarily or in more than a substantial portion (e.g., more than 50%, 75%, or 99%) originally contained in the farinaceous endosperm of the corn.

[00104] As illustrated in Figure 15, graph 1-1 shows the particle size distribution of corn after hammer milling with various sieve sizes. It shows that about 50% of the corn flour particles are larger than 500 microns and most of the particles are composed of pericarp, head tip, germ and coarse sand.

[00105] With reference to Figure 16, graph 12 shows the average particle size of corn flour in dry milling plants in the USA. This shows that approximately 10% of the corn flour has a particle size smaller than 125 microns, 20% of the corn flour is smaller than 240 microns, 30% of the corn flour is smaller than 375 microns, and 40% of the corn flour is smaller than 500 microns. These small particles are primarily starch from the farinaceous endosperm and the corneous endosperm. Petition 870250092067, dated 08 / 10 / 2025, page 33 / 119 30 / 71

[00106] The percentage of protein in these small corn flour particles is shown in Figure 17, graph 1-3. This shows that the smaller particles are starch from the farinaceous endosperm with a lower protein content. Therefore, it is possible to separate and produce free starch or starch released from the farinaceous endosperm. This yield and purity of free starch (% protein) can be controlled by the size of the sieve used in the separation in Step 703 of Figure 7. Any sieve separation method, such as a vibrating sieve, can be used in this screening step. Particles smaller than the sieve openings pass through the sieve in Step 703, for liquefaction in Step 704 and saccharification in Step 705, to produce corn syrup.Next, they are sent to the slurry centrifuge in Step 706 to separate any oil / germ from the light phase (slurry), followed by the pre-coat drum filter in Step 707 to remove any fine solids and produce pure, clean corn syrup for biotechnological processes.

[00107] In some embodiments, grinding the larger particles one or more times increases the yield of pure starch or improves the purity of the pure starch. Any solid particle size reducer, such as a roller mill or pin mill, can be used. Larger particles remain at the top of the sieve in Step 703 and can be used as feedstock for an enhanced dry grinding process to produce various by-products.

[00108] Next, some improvements in the dry milling process, according to some modalities. Petition 870250092067, dated 08 / 10 / 2025, p. 34 / 119 31 / 71

[00109] 1) Process 700 of Figure 7: Improved dry milling process with fiber removal before fermentation.

[00110] The larger solid particles from the sieve separation in Step 703 are sent to the pulp tank in Step 101 with filtrate from the liquid / solid separation in Step 701, which are used as cooking water as a starting point for the liquefaction process, followed by jet cooking in Step 102 and liquefaction 1 in Step 103 to liquefy most of the starch at a higher temperature (above 110°C) and higher Baumé pulp. The liquefied starch paste with a high Baumé content, containing coarse sand, germ, and fibers, is sent for liquid / solid separation and washing in Step 701. The new three-section paddle sieve is used to separate a liquefied starch paste with a high Baumé content, containing small particles of coarse sand and germ (depending on the sieve size used in this sieve) from the first section of the sieve and sent for fermentation in Step 104.The excess liquefaction from Step 604 can be used as wash water for the second and third sections of the three-section paddle sieve in order to remove liquefied starch from the solid particles (coarse sand, germ and fibers).

[00111] In Figure 7, Process 700A illustrates one part of the process for the production of pure starch, liquid starch, or pure corn sugar (e.g., for biotechnological feedback) according to some embodiments. Process 700B illustrates the other part of the process for the production of alcohol according to some embodiments. Petition 870250092067, dated 08 / 10 / 2025, page 35 / 119 32 / 71

[00112] In Step 604, the output is a washed and moist cake, sent to Liquefaction 2. The solids will continue to be soaked / cooked in a paste with low Baumé content (e.g., less than 5 Be) to further soften the coarse sand germ particles. This is followed by liquid / solid separation and dehydration in Step 605, followed by grinding for particle size reduction in Step 606 to fragment the coarse sand and germ particles and release more starch and oil. This is followed by liquid / solid separation and washing in Step 702 to produce pure fiber (less than 3% starch, less than 4% oil, and less than 15% protein) with a yield of approximately 3 lb. / bu. This pure fiber is an ideal raw material for the production of secondary alcohol and use in the paper industry. It can also be followed by a screw press in Step 708 to produce a 43% DS cake. The cake can be mixed with de-oiled syrup in Step 110 and then dried in Step 108 to produce 20-30% pro-fat feed for livestock, according to market needs. The protein-rich cake from the decanter in Step 106 can be added wholly or partially to the dryer in Step 108 to increase the pro-fat content in the DDGS by up to 30%.

[00113] All the vinasse, after fermentation in Step 104 and distillation in Step 105, is sent to the decanter in Step 106 to remove solids (mainly protein and fine fiber). The excess (fine vinasse from the decanter in Step 106) is sent for evaporation in Step 107 to concentrate the fluid to 30-35% DS syrup, followed by oil recovery in Step 110 to recover oil for biodiesel production. The recovery Petition 870250092067, dated 08 / 10 / 2025, page 36 / 119 33 / 71 of the oil in Step 110 occurs after fermentation, being dark in color and rich in fatty acids (up to 10%), and is not ideal for human consumption. The oil must be recovered before fermentation if it is intended for human consumption, as described below.

[00114] 2) Process 600 of Figure 6: An improved dry milling process with fiber and germ removal prior to fermentation.

[00115] Corn flour, after the hammer mill in Step 109, is sent to the sieve separation in Step 703 to separate fine solid particles (mainly starch from the farinaceous endosperm) from coarse solids (mainly germ, coarse sand, and fiber). The fine solid portion proceeds to liquefaction in Step 704 and saccharification in Step 705 to produce corn syrup. It is then sent to a slurry centrifuge in Step 706 to separate any oil / germ as light phase slurry. The light slurry then goes to a pre-coat drum filter in Step 707 to remove any fine solids and produce clean, pure corn syrup for biotechnology processes.

[00116] The larger solid particles from the sieve separation in Step 703 are sent to a pulp tank in Step 101, with the filtrate from the liquid / solid separation in Step 701 being used as cooking water to initiate liquefaction. The jet cooker in Step 102 and liquefaction 1 in Step 103 are used to liquefy most of the starch at higher temperatures (above 110°C), resulting in a pulp with a high Baumé content. The liquefied starch pulp with a high Baumé content, containing coarse sand, germ, and fiber, is sent to the Petition 870250092067, dated 08 / 10 / 2025, page 37 / 119 34 / 71 degerming in Step 609 (as shown in Figure 12) to separate the germ from the coarse sand and fiber by density difference, using liquefied starch pulp as the liquid medium. A two-stage double germ cyclone can be used for this degerming process. A 9-inch cyclone can be followed by a 6-inch cyclone, or a 6-inch cyclone A followed by a 6-inch cyclone B, as is commonly used in the industry.

[00117] Process 1200 of Figure 12: The liquefied starch paste with germ particles, coarse sand, and fiber is pumped to a first set of double germ cyclones in Step 1205, to separate the germ from the coarse sand and fiber by density differential. The germ particles lighter than the liquefied starch paste will exit as the light phase from the top of the first germ cyclone. The germ is then washed and dehydrated in Step 1208 to produce germ for corn oil production.

[00118] Coarse sand and fiber particles heavier than the liquefied starch paste exit from the bottom of the second double germ cyclone in Step 1206. The coarse sand and fiber are then subjected to a second grinding in Step 1203 to fragment the coarse sand (corneous endosperm) and release more starch. The ground coarse sand and fiber are then sent to the second-stage tank in Step 1204. The heavy liquefied starch paste with fragmented coarse sand from the second-stage tank in Step 1204 is fed to the second double germ cyclone in Step 1206. The light phase of the first germ cyclone contains the liquefied starch paste with any germ particles. Petition 870250092067, dated 08 / 10 / 2025, page 38 / 119 35 / 71 not recovered from the first double germ cyclone is recycled back to the first stage tank. The heavy phase from the bottom of the second germ cyclone is discharged to the liquid / solid separation in Process 300 (new three-section paddle screen) to separate fine particles (less than 50 microns) of starch and gluten from larger particles (coarse sand and fiber). The stream of fine particles with liquefied starch is recycled back to a second stage tank in Stage 1204. The return stream used as wash water in the three-section paddle screen is used to wash the liquefied starch from the coarse sand and fiber particles in sections 2 and 3 of the screens. The wash liquid is recycled back to the first stage tank in Stage 1202.

[00119] Coarse sand and fiber particles washed from the three-section paddle sieve in the Process 300 are sent to the low Baumé 2 liquefaction in Step 604 to continue soaking / cooking to soften the coarse sand. The degerming operation can occur after the high Baumé 1 liquefaction in Step 103 of the Figure. 6, or between liquefaction with high Baumé content 1 in Step 103 and liquefaction with low Baumé 2 content in Step 604, or after liquefaction with low Baumé 2 content in Step 604.

[00120] The softened coarse sand from liquefaction 2 in Step 604, along with the liquefied starch paste with low Baumé content, is fed to the liquid / solid separation in Step 605 for dewatering, followed by grinding in Step 606 to fragment the coarse sand particles and release more starch. The paste is then sent to the liquid / solid separation and washing in Step 702 to produce fiber. Petition 870250092067, dated 08 / 10 / 2025, page 39 / 119 36 / 71 pure as raw material for secondary alcohol production and use in the paper industry, or sent to the sieve press in Step 708 for dehydration. It is then mixed with the evaporator syrup in Step 107 and sent to the dryer in Step 108 to produce low-protein DDGS for cattle feed.

[00121] All the vinasse, after fermentation in Step 104 and distillation in Step 105, is sent to the decanter in Step 106 for recovery of the protein-rich flour. The germ from the degerming process 1200 in Step 609 of Figure 6 can be subsequently extracted by combining the helical press in Step 607 and solvent extraction in Step 608. The oil quality is better (light color and low free fatty acid content). The oil yield can reach 1.6 lb / bu, but the germ protein denatures at the high temperatures (above 1000°F) used in this oil extraction, resulting in a product with lower nutritional value. Ethanol can be used as a solvent, and an extremely high shear device, such as a Supraton, can be used to break down the protein wall of oil cells, producing good quality oil with high yield (up to 1.4 lb / bu), as well as high-value germ protein meal for fish farming.

[00122] 3) Process 800 in Figure 8 illustrates an enhanced dry milling process with removal of fiber and organic oil prior to fermentation in Step 104, according to some embodiments.

[00123] The corn flour, after the hammer mill in Step 109, is sent to the sieve separation in Step 703, to separate the fine solids (mainly Petition 870250092067, dated 08 / 10 / 2025, page 40 / 119 37 / 71 starch from the farinaceous endosperm) of the coarse solids (mainly germ, coarse sand and fiber). The fine solids portion is sent for liquefaction in Step 704 and saccharification in Step 705 to produce corn syrup, then sent to a slurry centrifuge in Step 706 to separate any oil / germ as a light phase (slurry). Next comes the pre-coating drum filter in Step 707 to remove any fine solids and produce pure, clean corn syrup for biotechnological processes. Larger solid particles are separated by sieving in Step 703 is sent to the pulp tank in Step 101, along with the filtrate from the liquid / solid separation in Step 702 as cooking water to initiate the liquefaction steps, followed by jet cooking in Step 102 and liquefaction 1 in Step 103 to liquefy most of the starch at higher temperatures (above 110 °C) and pulp. Baumé is taller.

[00124] The liquefied starch paste with a high Baumé content, containing coarse sand particles, germ, and fibers, is sent for liquid / solid separation and washing in Step 701. The new three-section sieve with small sieve openings (e.g., 100 microns (can be 50 to 400 microns)) is used to separate and wash any larger solid particles (coarse sand, germ, and fibers) for liquefaction 2 with a low Baumé content in Step 604. After immersion / cooking, the coarse sand, germ, and fiber particles will become softer and easier to fragment. The coarse sand and germ particles, after immersion / cooking in liquefaction 2 in Step 604, are sent for liquid / solid separation in Step 605 for dehydration. Then, Petition 870250092067, dated 08 / 10 / 2025, page 41 / 119 38 / 71 Grinding occurs in Step 606 to further fragment the coarse sand and germ particles, releasing starch and oil. The broken coarse sand and germ particles are sent for further solids-liquid separation and washing in Step 702 to produce pure fiber for secondary alcohol production or use in the paper industry, or further dewatering by screw press in Step 708. These are then mixed with evaporator syrup in Step 107 to produce low-fat DDGS after drying in Step 108. The cooking water is used to wash the liquefied starch from the fiber in the 2nd and 3rd screening sections of the three-section paddle screening apparatus before exiting as wet fiber cake.

[00125] The filtrate from the 2nd and 3rd sections of the sieve is recycled back to liquefaction 2 in Step 604. The filtrate from the 1st section of the sieve with small germ particles and coarse sand is sent to the pulp tank in Step 101. The liquefied starch with a high Baumé content (filtrate from the first section of the paddle sieve in Step 701) is sent to the slurry centrifuge in Step 801 to remove the slurry (oil / germ / protein phase) before being sent to fermentation.

[00126] All vinasse after fermentation in Step 104 and distillation in Step 105 is sent to the decanter in Step 106 to produce protein-rich cake for animal feed, and a portion is mixed with fiber to form protein-rich WDGS or DDGS. The excess from the decanter in Step 106 is sent to the evaporator in Step 107 to concentrate to 30-35% DS syrup and mixed with Petition 870250092067, dated 08 / 10 / 2025, page 42 / 119 39 / 71 fiber from the screw press in Step 708 to produce DDGS. Excess from the decanter in Step 106 is replenished.

[00127] The slurry phase, from both the slurry centrifuge in Step 801 and Step 706, is sent to a high-shear grinding device in Step 802, such as a Supraton, to further break down the oil cell wall within the germ and release more oil. The broken-down germ (germ protein) and oil is fed to a three-phase decanter in Step 803 to perform germ oil / protein separation and produce organic oil as a light phase for human consumption. The germ protein, as the heavy phase from the decanter, is sent for fermentation in Step 104. A non-toxic solvent, such as hexane, butanol, and even ethanol, can be added to the decanter in Step 803 to increase the oil yield, but this increases the need for more equipment (solvent recovery system) and the cost. If ethanol is used, the solvent recovery system can be incorporated into the distillation process to save on equipment and operational costs.

[00128] 4) Process 900 in Figure 9 illustrates an enhanced dry milling process that produces pure corn syrup for biotechnological processes, in addition to removing pure fibers and organic oil produced before fermentation, yielding valuable products for animal feed from the post-fermentation process, according to some embodiments.

[00129] After the hammer mill in Step 109, the corn flour is fed to the sieving separation in Step 703 to separate the fine solids, Petition 870250092067, dated 08 / 10 / 2025, page 43 / 119 40 / 71 mainly starch from the farinaceous endosperm, of the coarse solids, which are mainly germ, coarse sand and fiber.

[00130] The fine solid portion is sent for liquefaction in Step 704 and saccharification in Step 705 to produce corn syrup. It is then sent to a slurry centrifuge in Step 706 to separate the oil from the germ as the light phase (slurry), followed by a pre-coat drum filter in Step 707 to remove any fine solids and produce pure, clean corn syrup, which can be used in biotechnological processes. The larger solid particles from the sieve separation in Step 703 are sent to a pulp tank in Step 101, with the filtrate from the liquid / solid separation in Step 702 being used as cooking water to start the liquefaction step, followed by a jet cooking in Step 102 and liquefaction 1 in Step 103 to liquefy most of the starch at higher temperatures (above 110 °C) and higher Baumé pulp.The liquefied starch paste with a high Baumé content, containing coarse sand particles, germ, and fibers, is sent for liquid / solid separation and washing in Step 701. The three-section sieve with small openings, for example, 100 microns (which can be from 50 to 400 microns), separates and washes any larger solid particles (e.g., coarse sand, germ, and fibers) from the low Baumé liquefaction 2 in Step 604. The separated coarse sand, germ, and fiber particles are subjected to further soaking and cooking to become softer and easier to fragment. The coarse sand and germ particles, after soaking and cooking in liquefaction 2 in Step 604, are sent for liquid / solid separation in Step 605 for dehydration and then... Petition 870250092067, dated 08 / 10 / 2025, page 44 / 119 41 / 71 for grinding in Step 606 to further fragment the coarse sand and germ particles and release starch and oil.

[00131] Broken germ and coarse sand particles are sent for liquid / solid separation and washing in Step 702 to produce pure fiber for secondary alcohol production or for the paper industry. They may undergo further dewatering by screw press in Step 708 to produce low-fat DDGS after drying in Step 108.

[00132] The cooking water can be used to wash the liquefied starch from the fiber in sections 2 and 3 of the three-section paddle sieve, before exiting as wet fiber cake. The filtrate from the 2nd and 3rd sieving sections is recycled back to liquefaction 2 in Step 604. The filtrate from the 1st sieving section, with small germ particles and coarse sand, is sent to the pulp tank in Step 101. The liquefied starch with a high Baumé content, as filtrate from the paddle sieve of the first section in Step 701, is sent to the slurry centrifuge in Step 801 to remove the slurry (e.g., the oil / germ / protein phase) before being sent to fermentation.

[00133] The slurry phase from both slurry centrifuges in Steps 801 and 706 is sent to a high-shear grinding device in Step 802, such as a Supraton, to further break down the oil cell wall within the germ particles and release more oil. The broken germ particles, containing germ protein and oil, are fed to a two- or three-phase decanter in Step 803 to perform an oil / germ protein separation and produce organic oil as a light phase for Petition 870250092067, dated 08 / 10 / 2025, page 45 / 119 42 / 71 human consumption. The germ protein, as the heavy phase of the decanter in Step 803, is sent for fermentation in Step 104. A solvent such as hexane, butanol, or ethanol can be added to the decanter in Step 803 to increase the oil yield. However, this increases the need for more equipment (solvent recovery system) and increases costs. If ethanol is used, the solvent recovery system can be part of the distillation process to save on equipment costs.

[00134] All vinasse, after fermentation in Step 104 and distillation in Step 105, is sent to liquid / solid separation in Step 901 to separate any larger particles of coarse sand and germs and dehydrate the paste before being sent to milling in Step 902. The subsequently fragmented coarse sand and germ particles from milling in Steps 606 and 902, in addition to the return stream, are sent to liquid / solid separation in Step 702 and to a washing step, being recycled back to the paste tank in Step 101 for higher oil and alcohol yield. The filtrate from liquid / solid separation in Step 901 is sent to a decanter in Step 903 to produce a protein-rich wet flour cake, followed by a dryer in Step 109 to produce gluten meal for chicken and pig feed.The excess from the decanter in Step 903 is sent to a nozzle centrifuge in Step 904 to separate an oil-rich stream as the light phase and a protein-rich stream as the heavy phase. The protein-rich heavy phase is sent to the protein decanter in Step 906 to produce a high-value yeast / germ protein wet cake. Petition 870250092067, dated 08 / 10 / 2025, page 46 / 119 43 / 71 followed by a ring dryer in Step 907 to produce high-value HP50 protein meal for domestic pet food and fish farming feed. The excess from the decanter in Step 906 is reset. The oil-rich light phase from the nozzle centrifuge in Step 904 is sent to evaporator 1 in Step 107 to concentrate the liquid to 30-35% DS syrup. To recover the oil, this 30% DS syrup is sent to enrich the syrup in Step 108. 908 to convert resident sugar into lactic acid by adding lactic acid-producing probiotic cultures such as Lactobacillus plantarum ZJ316, Lactobacillus amylovorus, Lactobacillus fermentum, or Lactobacillus mucosae. This secondary fermentation produces up to 20% (by DB) of lactic acid and 109 probiotic units CFU.

[00135] This enriched syrup can be concentrated to 85% DS syrup by a low-temperature vacuum evaporator 2 in Step 905 to avoid high temperatures that could destroy the nutritional value within the syrup. Alternatively, a waste heat recovery system (not shown) can be used to recover waste heat from the dryer to help evaporate the syrup to 85% DS. This high-concentration syrup can also bypass the dryer and be added to super-dry feed to maintain 10% moisture in feed products. This 85% DS enriched syrup can also be used as an animal feed supplement or part of puppy milk or as a binding agent in the production of probiotic pellet feed. The syrup can be added to animal drinking water formula. Petition 870250092067, dated 08 / 10 / 2025, page 47 / 119 44 / 71

[00136] The improved dry milling processes above are examples of many possible ways to use the larger particles of coarse sand, germ and fiber as feedstock to produce alcohol and some by-products for animal feed. The selection of the specific process depends on the quality and quantity of pure starch required, as well as the required alcohol yield and quality and the quality of the by-products.

[00137] Many particle size reduction devices can be used for grinding in Steps 60 and 90, such as a grinding mill (some shear force and some cutting); a roller mill (low energy and no cutting); a pin mill (no cutting, but impact force to fragment the particles); or a Supraton (highly intensive shear grinding). The choice will depend on the quality and quantity of by-products desired, as well as the desired alcohol yield.

[00138] The three-section paddle sieve with high-rate washing should be used for liquid / solid separation in Step 605 and particle size separation and washing in Steps 701, 702, and 901. The three sieve sections can have openings of different sieve sizes, as well as different sieve designs and orientations (vertical or parallel wedge wire slot opening, round hole plate sieve or wire sieve, etc.). Therefore, this device can be used for very efficient solid classification by shape and size. For example, the device can separate fine fibers and germ particles with a wedge wire, with openings parallel to the fluid flow, to receive the particles. Petition 870250092067, dated 08 / 10 / 2025, page 48 / 119 45 / 71 fine and long fibers. This device also provides an extremely high wash liquid / solid ratio (> 1), replenishment wash, and ease in selecting the positioning location of the wash liquid source.

[00139] 5) Process 1300 in Figure 13 illustrates the use of partially husked brown rice to produce alcohol and pure starch, organic oil, rice protein and yeast protein for human consumption.

[00140] A raw material of rice grains is fed to a partial husking device in Step 1301 to partially husk the grains. The husk is not completely removed in this step. Some of the husk may be left with the grain, which contains starch. The removed husk is sent to a boiler as a fuel source.

[00141] The starch and remaining husk particles are sent to Step 1302 for bran and embryo separation. Bran and embryo are the portions containing protein and oil, respectively. To produce pure starch, the protein and oil-containing portions need to be removed. The protein- and oil-free starch is sent to a hammer mill in Step 1306. The milled rice starch is then sent to Step 704 for liquefaction, then to Step 705 for saccharification, and finally to Step 1303 to remove the pure starch for biotechnological applications. The bran and embryo separated in Step 1302 are combined with fine fibers from Step 1303 and sent to Step 109 for milling. The rice flour, milled in a hammer mill in Step 109, is sent to a pulp tank in Step 101 and, in Petition 870250092067, dated 08 / 10 / 2025, page 49 / 119 46 / 71 followed, for liquefaction in Step 103. After liquefaction 1 of Step 103, the pulp is sent to Step 701. The backfreezing residue is also added to Step 701.

[00142] The separated portions containing oil and protein are sent to a slurry centrifuge in Step 801 to separate any oil / germ as a light phase (slurry), followed by a pre-coat drum filter in Step 802 to remove any fine solids.

[00143] Protein and oil-containing particles are fed to a two- or three-phase decanter in Step 803 to separate the oil from the protein and produce organic oil as a light phase for human consumption. The germ protein exits as the heavy phase of the decanter in Step 803 and is sent for protein purification in Step 804. After the pure protein is removed, the liquid stream is sent for fermentation in Step 104. After fermentation in Step 104, the alcohol is sent to Step 105 for distillation to recover alcohol. The distillation vinasse is sent for yeast concentration in Step 1304. The concentrated yeast is dehydrated in Step 1305 for organic yeast recovery for human consumption. The rejected water is used as countercurrent.A solvent (such as hexane, butanol, or even ethanol) can optionally be fed to the decanter in Step 802 to increase oil yield, but more equipment is required (solvent recovery system). If ethanol is used, the solvent recovery system can be part of the ethanol distillation process to save equipment and operating costs. This step can produce pure, clean corn syrup for biotechnology processes. The particles. Petition 870250092067, dated 08 / 10 / 2025, page 50 / 119 Larger solids from the sieve separation in Stage Ί01 are sent to the pulp tank in Stage 101, along with the filtrate from the liquid / solid separation in Stage Ί02. The liquefied starch pulp with a high Baumé content, containing coarse sand particles, germ, and fiber, is sent for liquid / solid separation and washing in Stage Ί01.

[00144] A three-section paddle sieve, with small openings in the first section (e.g., 100 microns or between 50 and 400 microns), should be used to separate and wash any larger solid particles (coarse sand, germ, and fiber). These particles can be added to the low Baumé liquefaction 2 in Step 604. Further soaking and cooking of the coarse sand, germ, and fiber particles makes them softer and easier to fragment. The coarse sand and germ particles, after soaking and cooking in liquefaction 2 in Step 604, are sent to liquid / solid separation in Step 605 for dehydration and then to grinding in Step 606 for further breaking down the coarse sand and germ particles, releasing starch and oil. This breakdown of germ and coarse sand particles is sent to another liquid-solid separation and washing in Step 602.The broken particles are combined with the stream after the evaporator in Step 10 and sent to the dryer in Step 10 to produce DDDS. The cooking water is used to wash the liquefied starch from the fiber in the 2nd and 3rd sieve sections in the three-section paddle sieving device, before exiting as wet fiber cake. The filtrate from the 2nd and 3rd sieving sections is recycled back to liquefaction 2 in Step 60. The filtrate from the 1st sieving section, with... Petition 870250092067, dated 08 / 10 / 2025, page 51 / 119 48 / 71 small germ particles and coarse sand are sent to the pulp tank in Step 101. The liquefied starch with a high Baumé content, as filtrate from the first section of the paddle sieve in Step 701, is sent to a slurry centrifuge in Step 801 to remove the slurry (oil / germ / protein phase) before being sent to fermentation.

[00145] The slurry phase from both slurry centrifuges in Steps 801 and 706 is sent to a high shear grinding device in Step 802, such as a Supraton, to further break down the oil cell wall within the germ and release more oil.

[00146] This invention can be applied to all types of grains, such as sorghum, wheat, barley, millet and rice, etc., in addition to corn. Process Variations

[00147] Figure 18 illustrates a continuous steeping tank according to some embodiments. In some embodiments, this large steeping tank has approximately equivalent height and diameter. The steeping tank contains horizontal divisions that separate the larger tank into multiple chambers. Each chamber has opening(s) near the tank wall or in the center. The type of opening for each chamber is the opposite of the type in the chamber above it, creating an alternating pattern. Each chamber contains paddles that move the corn towards the openings, with a different design depending on whether the corn is moving towards the edge openings or the central opening. The paddles are connected to a central shaft which, in turn, is connected to a variable speed motor that controls the timing of Petition 870250092067, dated 08 / 10 / 2025, page 52 / 119 49 / 71 corn soaking by adjusting the amount of time the corn remains in each chamber.

[00148] Figure 19A illustrates a wet milling process 1900A producing starch paste with maximum purity, high-value germ and yeast protein flour according to some embodiments.

[00149] The 1900 Process improves a typical wet mill process with the following changes, including (1) replacing the current 6-8 batch steeping tanks with a continuous steeping tank to cut capital costs and simplify operations, (2) installing a multi-section paddle sieve to wash starch from the fiber and produce low-starch fiber, (3) installing a solid ring design grinding mill to grind wet germ particles to less than 50 microns to release oil and produce germ protein, (4) producing a pure starch paste from the starch in the farinaceous endosperm with very poorly soluble proteins, suitable for use in many new green technology processes, (5) converting the starch from the endosperm, which is bound with fiber and protein, into a sugar solution and using this low-sugar Baumé solution to produce yeast cells as aquatic feed,(6) increase lactic acid in the steeping liquid by adding probiotic cultures to reduce steeping time and produce probiotic feed, and (7) produce a high-nutrient DDGS with low oil and starch content for livestock feed. Detailed steps of the 1900 Process

[00150] In the continuous maceration Step 1911A, the corn kernels enter the process and are immersed in liquid. Petition 870250092067, dated 08 / 10 / 2025, page 53 / 119 50 / 71 in a continuous steeping process, illustrated in the system of Figure 18. (A batch steeping process is the alternative normally used.) The corn starts with 10% moisture and increases to 45% to 50% moisture by weight at the end of this stage.

[00151] In Step 1912A of dehydration, free water is separated from the swollen corn kernels.

[00152] In Stage 1913A of a grinding mill for the first grinding, a grinding mill or other grinding device separates the grains to release the starch only from the farinaceous endosperm. LeeTech's patented solid ring grinding mill (US Patent No. 9352326) is suitable for this stage as it allows greater control over the grinding level and is incorporated by reference for all purposes.

[00153] In Step 1914A of germ separation, a germ cyclone (such as the most commonly used) or other separation device separates the germ from the starch paste.

[00154] In Step 1915A of a paddle sieve for liquid / solid separation, a paddle sieve or other separation device separates the mixture, which contains starch from the farinaceous endosperm, coarse sand, and germ with 90% moisture, into two streams: one stream with liquid and starch, and the other stream containing germ and coarse sand with 80% moisture and no free starch. LeeTech's patented paddle sieve (US Patent No. 9718006) is suitable for this step and is incorporated by reference for all purposes.

[00155] In Step 1916A of starch concentration, a cyclone concentrator creates two streams of starch paste. The incoming starch paste contains 10-13° Baumé starch. Petition 870250092067, dated 08 / 10 / 2025, page 54 / 119 51 / 71 After the cyclone concentrator, the lower stream contains 23° Baumé starch and the upper stream contains 5-7° Baumé starch. The use of a cyclone concentrator reduces the capacity required for the primary centrifuge in the subsequent starch processing step (Step 1919A), saving energy consumption compared to using a centrifuge alone.

[00156] In Stage 1917A of a grinding mill for the second grinding, a grinding mill or other mill fragments the remaining germ and coarse sand from the endosperm, which contains protein-bound starch, oil, and fiber. LeeTech's patented solid ring design grinding mill (US Patent No. 9352326) is suitable for this stage, which is incorporated by reference for all purposes.

[00157] In Step 1918A of coarse fiber separation / washing, a paddle sieve or other screen separation device with different screen sizes washes the fiber (from the pericarp and capsule tip) to remove starch, protein, and oil. LeeTech's patented paddle sieve (US Patent No. 9718006) is suitable for this step and is incorporated by reference for all purposes.

[00158] In Step 1919A of starch separation, a primary centrifuge separates the starch from the protein. The starch in the underflow is directed to the 12-stage starch washing system and the protein in the overflow is directed to the clarifying centrifuge (see step 1951A).

[00159] In Step 1920A of the 12-stage starch washing process, a countercurrent washing system reduces the protein content of the paste from 4% to less than 0.4% protein. Petition 870250092067, dated 08 / 10 / 2025, page 55 / 119 52 / 71 (including only 0.1% soluble protein), creating a pure starch paste.

[00160] In Step 1921A of germ washing, after germ separation (Step 1914A), the germ is washed to separate any remaining starch. This starch is directed to the cyclone concentrator (Step 1916A), while the germ proceeds to milling (Step 1922A).

[00161] In Step 1922A of a grinding mill for germ particle size reduction, a grinding mill or other grinding device reduces the germ particle size to less than 50 microns by breaking the bonds between the oil, protein, and starch. The LeeTech patented solid ring design grinding mill (US Patent No. 9352326) is suitable for this step and is incorporated by reference for all purposes.

[00162] In Step 1923A of liquefaction and saccharification, the starch in the germ is converted into shorter chains and then converted into sugar (glucose).

[00163] In Step 1924A of yeast propagation, the yeast may consume some sugar to propagate, but not enough to produce significant amounts of alcohol.

[00164] In Step 1925A of three-phase separation, a three-phase decanter is used to separate the mixture into 3 phases. The oily phase produces corn oil suitable for biodiesel (but less suitable for human consumption due to the high concentration of free fatty acids). The solid phase contains a yeast protein and germ cake. The liquid phase includes water and solubles, with minimal levels of oil, alcohol, and protein. Petition 870250092067, dated 08 / 10 / 2025, page 56 / 119 53 / 71

[00165] In Step 1901A of probiotic propagation, the probiotics present in this aqueous mixture are propagated and the resulting liquid is then used as part of the original steeping liquid for the corn in the first step of the process (Step 1911A).

[00166] In Step 1926A of yeast / germ dehydration, the solid phase, which contains yeast protein and germ in a cake, is dehydrated to reduce the moisture content from 75% to 65% using a vacuum drum filter, plate and frame filter, press, filtration device, or other dehydration equipment.

[00167] In Step 1927A of yeast / germ drying, a dryer reduces the moisture content of the mixture to 10% to produce a yeast / germ protein meal that is a high-value aquatic feed.

[00168] In Step 1941A of the fine vinasse concentration, after the initial dehydration (Step 1912A), a nozzle centrifuge concentrates the dehydrated liquid into a clear, fine vinasse syrup (70% or more dry solids). The probiotic syrup can be used as a binding agent to produce enriched probiotic DDGS tablets.

[00169] In Step 1942A of fiber pressing, one fiber pressing reduces the cake moisture from 80% to 60%.

[00170] In Step 1943A of DDGS drying, a dryer further dries the cake, which is then combined with the probiotic syrup from Step 1941A, to create probiotic DDGS tablets for livestock feed. Petition 870250092067, dated 08 / 10 / 2025, page 57 / 119 54 / 71

[00171] In Step 1951A of protein separation, after the primary centrifuge (Step 1919A), the protein and overflow water go to the clarifying centrifuge or other separation device that separates the water from the protein. The overflow water can be used for germ washing (Step 1921A) and fiber washing (Step 1918A).

[00172] In Step 1952A of protein dehydration, the protein is further dehydrated using vacuum filtration or a plate and frame filter to produce 40% dry solids (DS) or a decanter to produce 35% dry solids.

[00173] In Step 1953A of gluten flour drying, a dryer (e.g., usually a rotary dryer) is used to further reduce moisture and create a gluten flour feed with 50-60% protein content.

[00174] For the sake of brevity, the remaining steps already provided in the figure are not described in further detail and can be performed using common processes.

[00175] Figure 19B illustrates an enhanced wet milling process 1900B, producing pure starch, yeast / germ protein flour and a sugar solution, according to some embodiments. This variation further enhances the typical wet milling process, going beyond the changes shown in Process 1900A of Figure 19A, producing a sugar solution with a higher content of soluble protein from the starch bound to the protein in the endosperm. The main variation processes are illustrated below. Petition 870250092067, dated 08 / 10 / 2025, page 58 / 119 55 / 71

[00176] In the liquefaction and saccharification Step 1932B, after the second milling (Step 1931B) and before the separation of the coarse fibers (Step 1933B), the starch from the endosperm is liquefied and converted into sugars.

[00177] In the oil recovery Step 1934B, after the separation of coarse fibers (Step 1933B), a centrifuge is used to separate the corn oil from the liquefied starch.

[00178] In Step 1961B of the sugar solution purification, a centrifuge, filtration device or desorbing centrifuge separates the sugar solution from the fine fiber cake (which is directed to the gluten flour dryer (Step 1953B).

[00179] For the sake of brevity, the other steps already shown in the figure are not described in further detail and can be performed using common processes or the process described in 1900A.

[00180] Figure 19C illustrates an improved wet milling process 1900C, producing pure starch, yeast / germ protein flour and alcohol, according to some embodiments.

[00181] This variation further enhances the typical wet milling process, going beyond the changes shown in Figure 19A, producing alcohol (typically ethanol, but possibly a high-carbon alcohol such as propanol) from the starch bound to protein and fiber in the endosperm (instead of the sugar solution in Figure 19B). The main variation processes are illustrated below. Petition 870250092067, dated 08 / 10 / 2025, page 59 / 119 56 / 71

[00182] In Step 1933C of fermentation, after the starch in the endosperm has been liquefied and saccharified (for example, in Step 1932C), yeast is added. The yeast converts the sugar solution into alcohol.

[00183] In Step 1934C / 1971C of distillation, a distillation tower or other distillation method collects the alcohol. The remaining oil and fiber (e.g., whole vinasse) are directed to the coarse fiber separation / washing stage (Step 1934C).

[00184] For the sake of brevity, the other steps already shown in the figure are not described in further detail and can be performed using common processes or the process described in 1900A.

[00185] Figure 19D illustrates an improved wet milling process 1900D, producing pure starch, yeast / germ protein flour and other starch according to some embodiments.

[00186] This variation further enhances the typical wet milling process, in addition to the changes shown in Figure 19A, by producing additional pure starch from the starch bound to protein and fiber in the endosperm (instead of the sugar solution in Figure 19B or the alcohol in Figure 19C). The main variation processes are illustrated below.

[00187] After the grinding mill in Step 1931D, the pulp goes directly to the separation and washing of coarse fibers (Step 1932D), instead of first going through liquefaction, saccharification and fermentation.

[00188] In the 1933D / 1981D starch concentration steps, after the separation and washing of coarse fibers, the Petition 870250092067, dated 08 / 10 / 2025, pp. 60 / 119 57 / 71 filtrate is directed to a cyclone concentrator that separates another starch paste (underflow) from the oil (overflow).

[00189] In Step 1934D of oil separation, the oil is separated from the fine fiber to produce corn oil.

[00190] For the sake of brevity, the other steps already shown in the figure are not described in further detail and can be performed using common processes or the process described in 1900A.

[00191] Figure 19E illustrates an enhanced wet milling process 1900E, producing pure starch, yeast / germ protein flour, lactic acid and sustainable aviation fuel (SAF, such as butanol or other alcohol) according to some embodiments.

[00192] This variation further enhances the typical wet milling process, going beyond the changes shown in Figure 19A, converting the sugar solution of all the starch bound to protein and fiber in the endosperm into an alcohol that can be a sustainable bio-based aviation fuel through fermentation and phase separation. The main variation processes are illustrated below.

[00193] In the liquefaction and saccharification Step 1992E, after grinding the endosperm corneum, the starch is liquefied and saccharified.

[00194] In Step 1993E of fermentation, a culture is added. The culture converts the sugar solution into an alcohol, such as butanol. Petition 870250092067, dated 08 / 10 / 2025, pp. 61 / 119 58 / 71

[00195] In Stage 1994E of phase separation, a separation device, such as a gravity inclined plate, separates the sustainable aviation fuel (e.g., butanol) from the water, which remains in the fermenter. (e.g., butanol, with 4 carbons, does not dissolve in water, remaining in the oil.)

[00196] In Step 1910E, after the probiotic propagation step, the resulting lactic acid can become a co-product, usable as a non-toxic, bio-based insecticide.

[00197] In Step 1954E of fine fiber recovery, after separation and washing of coarse fibers, the fine fiber is recovered from the fine vinasse and the cake is added to the gluten flour dryer (Step 1955E).

[00198] For the sake of brevity, the other steps already shown in the figure are not described in further detail and can be performed using common processes or the process described in 1900A.

[00199] Figure 20A illustrates a wet milling process 2000A producing the maximum amount of pure starch and yeast / germ protein meal according to some embodiments. The 2000A process includes features to reduce the capital investment required for a new wet mill, simplify operations, and produce corn oil without toxic solvents, while also producing high-value yeast / germ protein as aquaculture feed. The main variation processes are illustrated below.

[00200] In Step 2011A of maceration, the corn enters the process and is macerated in a maceration process. Petition 870250092067, dated 08 / 10 / 2025, page 62 / 119 59 / 71 in batch or continuous. The corn starts with 10% moisture and increases to 50% moisture by weight.

[00201] In Step 2012A of dehydration, free water is separated from the swollen corn kernels.

[00202] In Stage 2013A of a grinding mill for initial grinding, a grinding mill or other grinding device separates the grains to release the starch only from the farinaceous endosperm. LeeTech's patented solid ring design grinding mill (US Patent No. 9352326) is suitable for this stage as it allows greater control over the grinding level and is incorporated by reference for all purposes.

[00203] In Step 2014 of a paddle sieve for liquid / solid separation, a paddle sieve or other separation device separates the mixture (containing starch from the farinaceous endosperm, coarse sand, and germ with 90% moisture) into two streams: one with liquid and starch, and the other with germ and coarse sand with 80% moisture (and no free starch). LeeTech's patented paddle sieve (US Patent No. 9718006) would be suitable for this step and is incorporated by reference for all purposes.

[00204] In the starch concentration Step 2015A, a cyclone concentrator creates two starch paste streams. The incoming starch paste contains 10-13° Baumé starch. After the cyclone concentrator, the lower stream contains 23° Baumé starch and is directed to a primary centrifuge (Step 2018A). The upper stream contains 5-7° Baumé starch with germ protein; a portion of this stream is directed back to the paddle sieve (Step 2014A) and a portion to the yeast / germ protein flour production stream and Petition 870250092067, dated 08 / 10 / 2025, page 63 / 119 60 / 71 corn oil, specifically for yeast propagation (Step 2021). The use of a cyclone concentrator reduces the capacity required for the primary centrifuge in the subsequent starch processing step (Step 2018A), saving energy consumption compared to using a centrifuge alone.

[00205] In Step 2016A of a grinding mill for a second grinding, a grinding mill or other mill fragments the remaining germ and coarse sand from the endosperm (which contains protein-bound starch, oil, and fiber). LeeTech's patented grinding mill (US Patent No. 9352326) is suitable for this step and is incorporated by reference for all purposes.

[00206] In Step 2017A of coarse fiber separation and washing, a paddle sieve or other screen separation device with different screen sizes washes the coarse fiber (from the pericarp and tip cap) to remove starch, protein, and oil. LeeTech's patented paddle sieve (US Patent No. 9718006) is suitable for this step and is incorporated by reference for all purposes.

[00207] In the starch / protein separation Step 2018A, the input for this step comes from both the coarse fiber separation and washing paddle screen (Step 2017A) and the starch concentrator cyclone (Step 2015A). A primary centrifuge separates the protein from the starch. The starch in the downstream is directed to the 12-stage starch washing system, and the protein in the overflow is directed to the clarifying centrifuge (see Step 2051A). Petition 870250092067, dated 08 / 10 / 2025, page 64 / 119 61 / 71

[00208] In Step 2019A, 12-stage starch washing: countercurrent washing reduces the protein content of the paste from 4% to less than 0.4% protein (including only 0.1% soluble protein), creating a pure starch paste. The excess containing protein is directed back to the primary centrifuge (Step 2018A).

[00209] In Step 2021A of yeast propagation, the excess starch concentrator, which contains protein and starch after separation of pure starch (Step 2015A), together with germ / fiber wash water containing some germ after protein separation (Step 2051A), or another low-sugar solution (a readily available byproduct from other parts of the process), are combined with a yeast culture, which propagates but stops before fermentation.

[00210] In Step 2022A / 2031A of the three-phase separation, a three-phase decanter is used to separate the mixture into 3 phases. The oily phase produces corn oil suitable for biodiesel (but less suitable for human consumption due to the high content of free fatty acids). The solid phase contains a yeast protein and germ cake. The liquid phase includes water and solubles, with minimal oil, alcohol, and protein content.

[00211] In Step 2001A of probiotic propagation, the probiotics in the liquid phase of Step 2022A / 2031A are propagated and the resulting liquid is then used as part of the original steeping liquid for the corn in the first step of the process, Step 2011A. Petition 870250092067, dated 08 / 10 / 2025, page 65 / 119 62 / 71

[00212] In Step 2023A of yeast / germ dehydration: the solid phase containing yeast and germ protein in a cake is dehydrated to reduce the moisture content from 75% to 65% using a vacuum drum filter, plate and frame filter, press, filtration device or other dehydration equipment.

[00213] In Step 2024A of yeast / germ drying, a dryer reduces the moisture content of the mixture to 10% to produce a yeast / germ protein meal that is a high-value aquaculture feed.

[00214] In Step 2041A of the fine vinasse concentration, after initial dehydration (Step 2012A), a nozzle centrifuge concentrates the dehydrated liquid into a clear, fine vinasse syrup (70% or more dry solids). The probiotic syrup can be used as a binding agent to produce enriched probiotic DDGS tablets.

[00215] In Step 2042A of fiber pressing, the cake from the separation / washing of coarse fibers (Step 2017A) is subjected to a fiber press that reduces the cake moisture from 80% to 60%.

[00216] In Step 2043A of DDGS drying, the fiber press cake is combined with the evaporator syrup (Step 2041A); a dryer dries the syrup / cake mixture into probiotic DDGS for animal feed.

[00217] In Step 2051A of protein separation, after the primary centrifuge (Step 2018A), the protein and overflow water go to the clarifying centrifuge or other separation device that separates Petition 870250092067, dated 08 / 10 / 2025, page 66 / 119 63 / 71 the water from the protein. The overflow water, which contains some germ, is directed to the corn germ and oil production process (starting in Step 2021A).

[00218] In Step 2052A of protein dehydration, the water in the mixture is further reduced.

[00219] In Step 2053A of gluten flour drying, a dryer is used to further reduce moisture and create a gluten flour feed with 50-60% protein content. For brevity, the remaining Steps already shown in the figure are not described in further detail and can be performed using common processes.

[00220] Figure 20B illustrates a wet milling process producing pure starch, yeast / germ protein flour, and sugar solution according to some embodiments. This variation is based on the characteristics of Figure 20A and also produces a sugar solution with a higher content of soluble protein from the starch bound to the protein in the endosperm. The main variation processes are illustrated below.

[00221] In the liquefaction and saccharification Step 2032B, after the second grinding (Step 2031B) and before the separation of coarse fibers (Step 2033B), the starch is liquefied.

[00222] In the coarse fiber separation / washing step 2033B, part of the fiber washing liquid, a low-sugar solution, is directed to the yeast propagation step (Step 2021B) in the yeast / germ protein flour and corn oil process.

[00223] In Step 2034B of three-phase separation, after the separation of coarse fibers (step 2033B), a Petition 870250092067, dated 08 / 10 / 2025, page 67 / 119 A 64 / 71 three-phase decanter or other three-phase separation equipment is used to separate corn oil from liquefied starch.

[00224] In Step 2061B of sugar solution purification, a centrifuge, filtration device or desorbing centrifuge separates the pure sugar solution from the fine fiber cake, which is directed to the gluten flour drying step.

[00225] In Step 2022B / 2031B of the two-phase separation, the germ oil was captured elsewhere in the process, therefore this step is a two-phase separation, not a three-phase separation.

[00226] For the sake of brevity, the other steps already shown in the figure are not described in further detail and can be performed using common processes or the process described in 1900A.

[00227] Figure 20C illustrates a wet milling process 2000C producing pure starch, yeast / germ protein flour and alcohol according to some embodiments. This variation is based on the significant features of Figure 20A and also produces alcohol (ethanol) from all the starch bound to protein and fiber in the endosperm (instead of the sugar solution in Figure 20B). The main variation processes are illustrated below.

[00228] In Step 2073C of fermentation, after the starch in the endosperm has been liquefied and saccharified, yeast is added. The yeast ferments the sugar solution into alcohol. Petition 870250092067, dated 08 / 10 / 2025, pp. 68 / 119 65 / 71

[00229] In Step 2074C of distillation, a distillation tower or other distillation method collects the alcohol. The alcohol breaks the oil emulsion. The remaining oil and fiber are separated and directed to de-oiling (Step 2031C) and to coarse fiber separation / washing (Step 2041C).

[00230] In Step 2031C of deoiling, the fiber is separated from the corn oil.

[00231] In Step 2053C of the liquid / solid filtration, the filtrate from the coarse fiber separation / washing (Step 2041C) is filtered. The resulting liquid, a low-sugar solution, is combined with the excess starch concentration (Step 2015C) and directed to the yeast propagation step in the yeast / germ protein flour process. The resulting solid is combined with the protein dehydration cake (Step 2052C) in the gluten flour dryer (Step 2054C).

[00232] For the sake of brevity, the other steps already shown in the figure are not described in further detail and can be performed using common processes or the process described in 1900A.

[00233] Figure 20D illustrates a wet milling process 2000D producing pure starch, yeast / germ protein flour, and additional starch, according to some embodiments. This variation builds on the significant changes in Figure 20A and also produces a starch paste with 40% from the starch bound to protein and fiber in the endosperm corneum (instead of the sugar solution in Figure 20B or the alcohol in Figure 20C). The main variation processes are illustrated below. Petition 870250092067, dated 08 / 10 / 2025, pp. 69 / 119 66 / 71

[00234] After the second milling with the LeeTech Milling Mill in Step 2042D, the pulp goes directly to the separation and washing of coarse fibers (Step 2043D), instead of first going through liquefaction, saccharification and fermentation.

[00235] In the starch concentration step 2081D, after separation and washing of the coarse fibers (Step 2043D), the filtrate is directed to a cyclone concentrator, which produces another starch paste. The excess, which contains protein and water, is a low-sugar solution that can be added to the yeast propagation step (2021D) in the yeast / germ protein flour process.

[00236] For the sake of brevity, the other steps already shown in the figure are not described in further detail and can be performed using common processes or the process described in 1900A.

[00237] Figure 20E illustrates a wet milling process 2000E producing pure starch, yeast / germ protein flour, lactic acid, and an alcohol suitable for use as sustainable aviation fuel (SAF), according to some embodiments. This variation builds on the significant changes in 20A and also converts the sugar solution of all the starch bound to proteins and fibers in the endosperm into a bio-based alcohol that can be used as sustainable aviation fuel, through fermentation and phase separation. The following illustrates the main variation processes that differ from the 2000D process of Figure 20D.

[00238] In the liquefaction and saccharification step 2032E, after the horny endosperm has been ground in Petition 870250092067, dated 08 / 10 / 2025, pp. 70 / 119 67 / 71 In the LeeTech Grind mill, during the second grinding process, the starch is liquefied and saccharified (This step is similar to the process at 2000C in Figure 20C).

[00239] In Step 2033E of fermentation, a culture is added. The culture ferments the sugar solution into an alcohol, such as butanol. (This step is similar to the process in 2000C, although a different culture is used.) Oil is also added. This oil may be corn oil from a different part of the process, another vegetable oil, an oil of animal origin such as tallow, or a petroleum-derived oil.

[00240] In Stage 2034E of phase separation, a separation device, such as a gravity inclined plate, separates the alcohol for sustainable aviation fuel (e.g., butanol) from the water, which remains in the fermenter. Butanol, with 4 carbons, does not dissolve in water, remaining with the oil.

[00241] In Step 2001E, after the probiotic propagation step, the resulting lactic acid can become a co-product, usable as a non-toxic, bio-based insecticide.

[00242] For the sake of brevity, the other steps already shown in the figure are not described in further detail and can be performed using common processes or the process described in 1900A.

[00243] Figure 21A illustrates a 2100A soybean process producing probiotic food products for human consumption according to some embodiments. This variation uses a process similar to that described above to significantly improve the current process of Petition 870250092067, dated 08 / 10 / 2025, pp. 71 / 119 68 / 71 soybean oil extraction. This soybean process avoids the use of the carcinogenic solvent hexane, maintains the protein structure for greater digestibility, and creates options for the production of a variety of safe probiotic foods for human consumption. The main variation processes are illustrated below.

[00244] In Step 2111A, the soybeans enter the process and are soaked in a batch or continuous maceration process.

[00245] In Dehydration Step 2112A, free water is separated from the swollen soybeans.

[00246] In Stage 2113A of a grinding mill for initial grinding, a grinding mill or other grinding device reduces soybeans into smaller particles (less than 35 microns). LeeTech's patented solid ring grinding mill (US Patent No. 9352326) is suitable for this stage as it allows greater control over the grinding level and is incorporated by reference for all purposes.

[00247] In Step 2114A of a paddle sieve for liquid / solid separation, a paddle sieve or other separation device separates the mixture (containing protein, fiber, and water) into two streams: one with liquid, protein, and starch, and the other with soybean hull fiber with 80% moisture (and no starch). LeeTech's patented paddle sieve (US Patent No. 9718006) would be ideal for this step and is incorporated by reference for all purposes.

[00248] In Step 2115A of fiber pressing, a fiber press reduces the cake moisture from 80% to 60%. Petition 870250092067, dated 08 / 10 / 2025, pp. 72 / 119 69 / 71

[00249] In Step 2116A of drying with DDGS, a dryer dries the cake even further.

[00250] In Step 2117A of probiotic enrichment, the dehydration water (Step 2112A) is combined with a probiotic culture and added to the cake to produce a probiotic DDGS for cattle feed.

[00251] In Step 2121A of pasteurization, the filtrate from the paddle sieve (step 2114A) is pasteurized.

[00252] In Steps 2122A / 2131A of probiotic enrichment, a probiotic culture is added to produce probiotic soy milk.

[00253] In Step 2123A of fermentation, yeast can be added to the mixture and fermented to create a lightly alcoholic probiotic beverage.

[00254] In Step 2141A of the three-phase separation, after pasteurization, a three-phase decanter or other separation device separates the mixture into an oil phase, a solid phase, and a liquid phase. The liquid can be diverted back to the sieve (Step 2114A).

[00255] In Step 2142A of oil refining, the oil phase from the three-phase separation is further refined to create hexane-free soybean oil.

[00256] In Step 2151A of tofu pressing, the solid phase from the three-phase separation (Step 2141A), consisting mainly of soy curd, is pressed to produce tofu.

[00257] In Step 2161A of spray drying, a spray dryer can also convert the solid phase of the three-phase separation (Step 2141A) into a powder. Petition 870250092067, dated 08 / 10 / 2025, pp. 73 / 119 70 / 71 soy-based protein is a rich source of long-lasting protein for smoothies.

[00258] In Step 2171A of probiotic enrichment, the solid phase of the triphasic separation (Step 2141A) can be combined with a culture to produce a non-dairy probiotic yogurt. Abbreviations:

[00259] The meanings of the abbreviations may be used throughout the Specification or in selected parts thereof or of the drawings. U / F — underflow; O / F - overflow.

[00260] The advantageous features and aspects of the processes disclosed here include: (1) using a continuous steeping tank design (Figure 18) to provide a less energy-intensive approach compared to the current batch operation typically used in US wet corn mills, (2) decreasing steeping time from 50 to 30 hours due to increased lactic acid concentration in the steeping liquid, (3) increasing production efficiency by separately separating and processing the easily accessible starch in the endosperm of the flour from the more difficult-to-access starch in the endosperm corneum, (4) creating a higher-value additional co-product that includes yeast protein and germ that can be used as aquaculture feed, (5) creating a pure sugar solution that can be used as feedstock for synthetic biology or other bio-based processes, (6) creating a more efficient process for transforming starch into ethanol,(7) avoid the use of solvent germ extraction, thus preventing the problem of solvent toxicity and maintaining digestible protein (no, Petition 870250092067, dated 08 / 10 / 2025, pp. 74 / 119 71 / 71 denatured) so that the germ protein can be used in aquaculture feed, (8) using less energy compared to the traditional wet milling process to produce more valuable co-products, (9) requiring less capital investment compared to the traditional wet milling process to produce more valuable co-products, (10) producing starch and sugar with higher purity and therefore better as carbohydrate feedstock for biochemical, synthetic biology, renewal chemistry and other green technologies, (11) producing a syrup with a high lactic acid content that can be used as a natural insecticide and (12) producing alcohol that can be used to fragment an oil / protein emulsion.

[00261] In operation, continuous maceration is carried out, the corn kernels and their parts are ground twice, liquefaction and saccharification are performed, the starch in the different parts of the corn is separated for different purposes with different processes, and co-products are generated, including starch, sugar, animal feed, oil, ethanol and other alcohols, such as butanol.

[00262] In use, pure starch is used in a biotechnological process as a raw material. When the starch paste contains less than 0.2% soluble protein, it is a better raw material for biochemical processes, synthetic biology, renewable chemicals and other green technologies. Petition 870250092067, dated 08 / 10 / 2025, pp. 75 / 119

Claims

1 / 10 CLAIMS 1. Continuous maceration tank, characterized in that it comprises: a) a tank body; b) multiple internal chambers within the tank body; c) one or more paddles in each of the multiple internal chambers configured to move the grains progressively through and between the chambers; d) a maceration liquid inlet coupled to the tank body.

2. Continuous maceration tank, according to claim 1, characterized in that one or more paddles move the grains outwards.

3. Continuous maceration tank, according to claim 1, characterized in that one or more paddles move the grains in different directions in an alternating pattern in each of the multiple internal chambers.

4. Continuous maceration tank, according to claim 1, characterized in that one or more paddles comprise from 4 to 8 paddles.

5. Continuous maceration tank, according to claim 1, characterized in that the 4 to 8 paddles are controlled by a variable speed motor connected to a central shaft.

6. Continuous maceration tank, according to claim 1, characterized in that the multiple internal chambers comprise from 6 to 12 internal chambers.

7. Continuous maceration tank, according to claim 1, characterized in that the inlet of the maceration liquid is located at the bottom of the tank body, configured to have a maceration liquid flowing from the bottom of the tank in a countercurrent flow containing multiple probiotic microorganisms at a predetermined concentration to reduce maceration time.

8. Wet milling process for generating purified starch, characterized in that it comprises: a) performing continuous maceration of corn kernels using a continuous maceration tank; b) milling the corn kernels to generate corn components, including starch, mainly from the farinaceous endosperm of the corn kernels; c) performing the separation of the corn components to obtain the starch, mainly from the farinaceous endosperm of the corn kernels; d) processing the starch using a 12-stage countercurrent washing system; e) washing the soluble protein from the starch, resulting in purified starch.

9. Wet milling process according to claim 8, characterized in that the 12-stage countercurrent washing system uses a water-to-starch ratio greater than 1:1, which allows more protein to be removed from the starch by washing.

10. Wet milling process according to claim 8, characterized in that it further comprises reducing the protein content of the starch paste from about 4% to less than 0.4%.

11. Wet milling process, according to Petition 870250092067, dated 10 / 08 / 2025, page 77 / 119 3 / 10 claim 9, characterized in that the starch paste contains less than 0.2% soluble protein.

12. Wet milling process for generating a high-protein feed product with yeast and germ protein, characterized in that it comprises: a) performing continuous mashing of corn kernels using a continuous mashing tank; b) milling the corn kernels to generate corn components; c) performing separation of the corn components to obtain the germ; d) adding yeast to the germ and allowing the yeast to propagate; e) producing a feed product that includes yeast and germ protein.

13. Wet milling process according to claim 12, characterized in that it further comprises reducing the particle size of the germ to less than 50 microns using a milling mill.

14. Wet milling process, according to claim 12, characterized in that it further comprises the propagation of yeast using starch present in the germ.

15. Wet milling process, according to claim 12, characterized in that it further comprises separating the protein from the yeast and germ without the use of solvent to avoid toxicity and denaturing the protein to maintain digestibility for an animal.

16. Wet milling process, according to claim 12, characterized in that it further comprises the separation of yeast protein and germ using a water-based solution.

17. Wet milling process for producing a sugar solution mainly from the protein-bound starch in the endosperm, characterized in that it comprises: a) performing continuous maceration of corn kernels using a continuous maceration tank; b) performing a first milling of the corn kernels to generate corn components; c) performing the separation of the corn components to obtain the endosperm of the corn kernels; d) performing a second milling of the corn kernel components to release the protein-bound starch in the endosperm of the corn kernels; e) liquefying and saccharifying the starch to produce a sugar solution.

18. Wet milling process, according to claim 17, characterized in that it further comprises carrying out the separation and washing of coarse fibers.

19. Wet milling process, according to claim 17, characterized in that it further comprises carrying out oil recovery by separating corn oil from liquefied starch using a centrifuge, decanter or other separation equipment.

20. Wet milling process, according to claim 17, characterized in that it further comprises purifying the sugar solution using a centrifuge, filtration device or desorbing centrifuge to separate the sugar solution from a cake of fine fibers.

21. Wet milling process, according to claim 17, characterized in that it further comprises processing the starch from the endosperm corneum part of the corn grain separately from the starch from the endosperm farinaceous part.

22. Wet milling process according to claim 17, characterized in that the wet milling process for producing a sugar solution does not use a membrane separation process.

23. Wet milling process for the production of ethanol mainly from starch bound to proteins and fibers in the endosperm of corn kernels, characterized in that it comprises: a) performing continuous maceration of corn kernels using a continuous maceration tank; b) performing a first milling of the corn kernels to produce corn components; c) performing the separation of the corn components to obtain the endosperm; d) performing a second milling of the corn kernel components to release the starch bound to protein in the endosperm of the corn kernels; e) performing liquefaction and saccharification of the corn kernels to form a sugar solution; f) fermenting the sugar solution to form ethanol; g) distilling the ethanol.

24. Wet milling process, according to claim 23, characterized in that it also includes deodorization to separate the fiber from the corn oil.

25. Wet milling process according to claim 23, characterized in that it further comprises breaking an oil / protein emulsion using ethanol.

26. Wet milling process for producing butanol or other predetermined alcohol mainly from starch bound to proteins and fibers in the endosperm of corn kernels, characterized in that it comprises: h) performing continuous maceration of corn kernels using a continuous maceration tank; i) performing a first milling of the corn kernels to produce corn components; j) performing separation of the corn components to obtain the endosperm; k) performing a second milling of the corn kernel components to release the starch bound to protein in the endosperm of the corn kernels; l) performing liquefaction and saccharification of the corn kernels to form a sugar solution; m) fermenting the sugar solution to form alcohol; n) using phase separation to separate the alcohol.

27. Wet milling process according to claim 26, characterized in that it further comprises the addition of different microorganisms to produce different types of alcohol for fermentation.

28. Wet milling process, according to claim 26, characterized in that it further comprises the addition of oil with the culture to the fermentation to facilitate phase separation. Petition 870250092067, dated 08 / 10 / 2025, page 81 / 119 7 / 10 29. Wet milling process, according to claim 26, characterized in that the alcohol has a main chain with 3 or more carbons.

30. Wet milling process according to claim 29, characterized in that the alcohol comprises a sustainable aviation fuel.

31. Wet milling process, according to claim 26, characterized in that it further comprises the use of a minimum amount of water in the sugar solution necessary to produce a target concentration for crop health and thus reduces energy consumption in a subsequent process to concentrate the sugar solution.

32. Wet milling process according to claim 26, characterized in that it further comprises carrying out a phase separation to separate a first liquid phase containing alcohol and oil from a second liquid phase containing an aqueous solution of sugar and culture to maintain the health of the culture in the sugar and culture solution and increase the alcohol yield.

33. Wet milling process, according to claim 32, characterized in that it further comprises the separation of alcohol from oil in the first liquid phase.

34. Wet milling process according to claim 33, characterized in that the recovered oil is recycled back as feedstock for phase separation.

35. Wet milling process, according to claim 23, characterized in that the alcohol is produced without distillation.

36. Grain milling process to produce soy-based foods for human consumption without the use of a carcinogenic solvent, characterized in that it comprises: a. performing continuous maceration of soybeans using a continuous maceration tank; b. milling the soybeans to generate soy components; c. separating the soy components; d. selecting and combining a portion of the soy components with probiotics; and e. processing the components into soy-based products for human consumption.

37. Grain milling process according to claim 36, characterized in that it further comprises carrying out multiple soy milk extraction steps to produce a predetermined concentration of soy milk for the production of the respective soy-based products.

38. Grain milling process according to claim 36, characterized in that the soy-based products for human consumption comprise soybean oil, tofu or soy milk.

39. Grain milling process according to claim 36, characterized in that it further comprises separation by sieving with paddles.

40. Grain milling process according to claim 38, characterized in that it further comprises pasteurization.

41. Grain milling process according to claim 39, characterized in that it further comprises carrying out a three-phase separation. Petition 870250092067, dated 08 / 10 / 2025, page 83 / 119 9 / 10 42. Grain milling process according to claim 38, characterized in that soy-based products for human consumption are produced without the use of organic solvents.

43. Grain milling process according to claim 38, characterized in that the soy-based products for human consumption include a soy-based bacon substitute, rich in protein and oil; a probiotic non-dairy yogurt substitute; and a soy-based meat substitute, rich in fine fiber and protein.

44. Wet milling process for generating lactic acid for use as a biologically based insecticide, characterized in that it comprises: a) performing continuous maceration of corn kernels using a continuous maceration tank; b) milling the corn kernels to generate corn components, including germ, fiber, and pure starch paste; c) combining wet germ and wet fiber cake containing bound starch, forming a first mixture; d) milling the first mixture to form a second mixture; e) liquefying and saccharifying the second mixture to form a sugar solution; f) adding a lactic acid-producing culture to the sugar solution to convert sugar into lactic acid; g) using the lactic acid syrup as part of a maceration liquid; eh) producing a lactic acid spray as a biologically based insecticide. Petition 870250092067, dated 10 / 08 / 2025, page 84 / 119 10 / 10 45. Wet milling process according to claim 44, characterized in that it further comprises carrying out a liquid-solid separation to form a liquid phase and a cake after yeast propagation.

46. ​​Wet milling process according to claim 45, characterized in that it further comprises the propagation of probiotics in the liquid phase to form lactic acid.

47. Wet milling process, according to claim 45, characterized in that the cake forms a yeast / germ protein flour. Petition 870250092067, dated 08 / 10 / 2025, pp. 85 / 119

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