PROCESS FOR PRODUCING RENEWABLE FUELS FROM ALCOHOLS

Abstract

Disclosed are systems, methods, and compositions for producing renewable alcohols, conversion of C1-C5 alcohols to a mixture of C2-C7 olefins to generate stream for recycle to the alcohol conversion step to create or separate oligomerization conversion to generate a predominantly C4+ stream, oligomerizing stream into fuel range olefins to create a stream, separating stream into fractions appropriate for use as gasoline, jet, and diesel fuels. The disclosure also provides systems, methods, and compositions of bio-based ethanol that can be converted to ethylene and subsequently to mixtures of C3-C8 olefins in a single-step.

Description

1 / 81 PROCESS FOR PRODUCING RENEWABLE FUELS FROM ALCOHOLS RELATED DEPOSIT REQUESTS

[001] The present invention claims priority for the Application of US Provisional Patent Serial Number 63 / 490,708, entitled "Process for the production of renewable fuels from alcohols," filed March 16, 2023, the description of which is incorporated herein by reference as if defined in its entirety. FIELD

[002] The present invention relates to systems and methods for producing renewable alcohols, hydrocarbons and further processing them to produce transportation fuels such as gasoline, jet fuel and diesel. The description also relates to processes for converting C1-C5 alcohols to a mixture of C2-C7 olefins for use in the production of transportation fuels. Processes for converting ethanol of biological origin into ethylene and subsequently into mixtures of C3-C8 olefins in a single step are also disclosed. BACKGROUND OF THE INVENTION

[003] Petroleum is a non-renewable resource and its combustion results in the release of carbon into the environment. There is a growing demand for the use of biomass sources to replace petroleum as a starting point for the synthesis of fuels, specifically transportation fuels such as gasoline, aviation kerosene and diesel fuel (generically referred to as fuels or transportation fuels in this application). With the increased availability and reduced cost of biomass-derived alcohols, they have become inexpensive and a renewable feedstock for the production of various olefins for use in downstream hydrocarbon production. Petition 870250080789, dated 09 / 09 / 2025, page 8 / 122 2 / 81

[004] Current biogas production and spent grain processing technologies produce byproducts, such as proteins that could be used to produce other products, for example, animal feed, and are therefore not fully efficient technologies. Furthermore, current technologies fail to address the problems created by high nitrogen concentrations in anaerobic digestion systems. Current integrated systems and processes for improving alcohol production yield and efficiency also suffer from inefficiencies and limitations. For example, there is a need for systems that produce vinasse specifications that have fully efficient and low-cost anaerobic digestion. There is also a need for the production of high-energy-density fuels, such as hydrocarbon fuels or transportation fuels, especially those with low or no carbon footprint (i.e., carbon neutral).Furthermore, there is also a need for an improved method for processing renewable alcohols and hydrocarbons to produce transportation fuels.

[005] Current technologies employing petroleum fuels have an inherently high carbon footprint, in part because they are produced by recovering petroleum from the earth, which ends up in the atmosphere when the fuel is burned, such as in an engine. The use of biodiesel can also pose a problem because it is not a hydrocarbon, and its chemical properties make its fuel properties inferior and its blending limits low. Renewable diesel is a commonly used hydrocarbon, but it is produced from fats, greases, and oils derived from animals and plants, the supply of which is relatively low considering the high global demand for transportation fuels. Furthermore, the co-products produced from sources such as renewable diesel and pro-renewable diesel... Petition 870250080789, dated 09 / 09 / 2025, page 9 / 122 3 / 81 cloth has a low octane rating and high vapor pressure and therefore very little value for recycling in transport fuel markets, such as the gasoline market or the SAF (sustainable aviation fuel) market, to reduce the net carbon footprint or net energy use.

[006] Today, there is a demand for zero or low carbon footprint (i.e., carbon neutral) and negative carbon footprint (i.e., carbon sequestration) high-energy-density transportation fuels such as jet fuel (SAF), diesel oil, marine fuel oil (bunker), or gasoline. These fuels can be used in existing assets and blended at high levels with conventional fuels, or they can be used directly without blending. Fuels such as ethanol have low energy density and blending limitations due to incompatibility with existing assets. Currently existing ethanol production assets were not designed to be carbon neutral.Renewable diesel is an example of a high-energy, low-carbon fuel, but its carbon footprint is much greater than zero. Renewable diesel only serves the diesel oil market, and the quantities of renewable raw materials needed for its production are low compared to the market size and demand.

[007] To date, the steps necessary to provide a commercially viable, carbon-neutral, high-energy-density transportation fuel made from carbohydrates have not been identified. As can be seen in the California Low Carbon Fuel System reports, there are no viable high-energy-density carbohydrate-based fuels (i.e., greater than 110,000 BTU / gallon), nor zero-carbon-score hydrocarbon fuels.

[008] Current commercial ethanol processes depend on Petition 870250080789, dated 09 / 09 / 2025, page 10 / 122 4 / 81 Distillation and evaporation, as recovery operations for fermentation products, require large amounts of energy, even when heat is integrated to minimize energy. For example, according to the Renewable Fuels Association (RFA), in a 2016 publication, a typical ethanol plant uses approximately 26,700 BTU / gallon of process energy (thermal energy plus electrical energy) from external energy sources (hereinafter referred to as external energy). External energy, as used in this application, refers to energy sources brought in from outside the boundaries of the ethanol plant. Ethanol has a low energy density of 76,300 BTU / gallon, meaning that production process energy accounts for approximately 35% of the energy output. This process energy, natural gas and grid electricity, represents a large carbon footprint and therefore prevents processes from achieving carbon neutrality.Furthermore, ethanol has an energy density of approximately 65% ​​of petroleum gasoline (116,000 BTU / gallon). Therefore, ethanol imposes a limit on the range it can carry in a vehicle, and it cannot be used as aviation fuel, diesel fuel, or bunker fuel. Additionally, its blending ratio in gasoline is limited.

[009] The processes for converting alcohol into hydrocarbon fuels have not been commercially deployed for various reasons, with varying degrees of success. The desire for renewable fuels with high energy density is a recent phenomenon. The ability to convert alcohols into transportation fuels that meet fuel specifications, which requires control over the molecular architecture of the products, has not yet been developed. Therefore, there is an unmet need for a supply of renewable alcohols with a carbon footprint low enough to allow the resulting hydrocarbon to have an attractive carbon footprint and be Petition 870250080789, dated 09 / 09 / 2025, page 11 / 122 5 / 81 commercially viable for use as transportation fuel.

[0010] Bio-based alcohol is a significant basic chemical. With the increasing availability and reduced cost of bioethanol, researchers have explored bioethanol as a feedstock for the production of a variety of hydrocarbons, including aviation fuel and / or diesel oil. Researchers at Gevo Inc. have developed a fermentation process that facilitates the production of bioisobutanol and have provided a new route for biofuels based on bio-based alcohols and subsequent conversions thereof.

[0011] The process of oligomerizing gaseous monoolefins to form gasoline-like hydrocarbons is known and has been described in the patent literature (US Patents No. 4,613,719 and 9,688,590). However, there is a constant need to develop new oligomerization processes employing more efficient and / or less expensive methods.

[0012] The oligomerization process of olefins was carried out using acid catalysts, such as phosphoric acid on a solid support, and olefin dimers were generally obtained for gasoline additive after hydrogenation of the dimers (US Patent Nos. 6,689,927 and 6,284,938).

[0013] There are reported examples using cation exchange resins for oligomerization. It has been claimed that a cation exchange resin can be used in a dimerization (USP 20050119111A1). US Patent No. 5,789,643 taught that oligomerization could be catalyzed by zeolites, aluminas, and ion exchange resins. Tetramers or pentamers can be obtained by oligomerization of preformed dimers with ion exchange resins (US Patent No. 6,239,321).

[0014] Oligomerization of lower olefins (e.g., C2-C8) for aviation fuel and / or diesel fuel from alcohol Petition 870250080789, dated 09 / 09 / 2025, page 12 / 122 6 / 81 bio-based materials employing catalytic conversion processes using a first catalyst, such as zirconium-tungsten, zirconium-molybdenum or a combination thereof, and a second catalyst, such as a ZSM-5 acid catalyst, was recently disclosed in U.S. Patent No. 11,078,433 (Gevo Inc.), which is incorporated herein by reference in its entirety.

[0015] This application provides, among other things, solutions to the above-mentioned and other problems in the field of the invention. SUMMARY OF THE INVENTION

[0016] The present invention describes, among other things, a system for the production of renewable hydrocarbons. The system includes a fractionation subsystem for processing a biomass containing a carbohydrate; a fermentation subsystem for converting the carbohydrate into a fermentation product; a water treatment subsystem for receiving a first portion of the fermentation product; an alcohol enrichment subsystem for receiving a second portion of the fermentation product; a hydrocarbon production subsystem for receiving renewable alcohols and producing the renewable hydrocarbons; processing the alcohols and renewable hydrocarbons for the production of transportation fuel; and a power management subsystem for receiving a fuel stream from the system and supplying power to the system.

[0017] In some embodiments, one or more of the following features may be included in any feasible combination. For example, the fractionation subsystem may include at least one of the following: a storage vessel for storing the biomass; a shredder for breaking up the biomass; a pretreatment vessel for pretreating the biomass; a treatment vessel for treating the biomass to produce the carbohydrate; and a container Petition 870250080789, dated 09 / 09 / 2025, page 13 / 122 7 / 81 high temperature short time (HTST) to pasteurize the carbohydrate.

[0018] In some embodiments, the fermentation subsystem may include at least one of the following: a fermenter to convert carbohydrate into the fermentation product; a nutrient addition subsystem; a pH adjustment subsystem; and an inoculum propagation subsystem.

[0019] In some embodiments, the water treatment subsystem may include at least one of the following: a fermented wort surge tank to receive the first portion of the fermentation product; a microorganism separation device to remove microorganisms from the first portion of the fermentation product; a first distillation column to separate the first portion of the fermentation product into an alcohol and a bottoms product; a digester to receive a portion of the bottoms product and produce a biogas; and a biogas removal subsystem to remove a pollutant from the biogas.

[0020] In some embodiments, the alcohol enrichment subsystem may include at least one of the following: a flash tank to separate a condensate from the second portion of the fermentation product; a separation vessel to separate the condensate into a light phase and a heavy phase; an ion exchange vessel to purify the light phase; a membrane separator to separate the light phase into a high-alcohol retentate and a water-rich permeate; a second distillation column to separate the water from the high-alcohol retentate; and an alcohol storage vessel.

[0021] In some embodiments, the hydrocarbon production subsystem may include at least one of the following: a denitrogenation subsystem to separate nitrogen from the alcohol; a sub Petition 870250080789, dated 09 / 09 / 2025, page 14 / 122 8 / 81 dehydration system to convert alcohol into an olefin; a hydrocarbon pretreatment subsystem to condition an olefin feed; a hydrogen supply subsystem to supply hydrogen; and a hydrocarbon processing subsystem to convert the olefin feed into at least an iso-octane fraction, a C12 alkane fraction and / or a C16 alkane fraction.

[0022] In some embodiments, the hydrocarbon processing subsystem may include at least one of the following: a first reactor; a debutanizer; a second reactor; a separator; a first splitter; and / or a second splitter.

[0023] In some embodiments, the energy management subsystem may include at least one of the following: a fuel gas system to distribute fuel gas received from the hydrocarbon processing subsystem; a low-pressure boiler to generate steam; a high-pressure boiler to generate steam; a combined heat and power unit to generate steam and electricity; a wind turbine to generate electricity; an electric boiler to receive renewable electricity and heat water to produce steam; a biomass boiler to burn biomass to heat water to produce steam; and / or a steam turbine to generate electricity.

[0024] In some embodiments, the biomass is corn, wheat, and / or sorghum. In some embodiments, the biomass has a negative carbon footprint. In some embodiments, the biomass is grown using strip tillage or no-till farming. In some embodiments, the shredder is a mill. In some embodiments, the biomass is grown using agricultural practices to increase soil organic carbon. In some embodiments, the pre-treatment tank may include a recycled water intake. In some embodiments, the biomass is grown using agricultural practices to increase soil organic carbon. Petition 870250080789, dated 09 / 09 / 2025, page 15 / 122 9 / 81 In some embodiments, biomass pretreatment may include pretreatment of biomass with an enzyme. In some embodiments, the treatment vessel may include an outlet for non-fermentable solids. In some embodiments, the non-fermentable solids outlet may include an outlet for dried distillery grains and / or an outlet for corn oil. In some embodiments, a portion of the corn oil production may be used as fuel for a boiler.

[0025] In some embodiments, the fermenter is a continuous fermenter. In some embodiments, the fermentation product may include an alcohol. In some embodiments, the alcohol is isobutanol.

[0026] In some embodiments, the inoculum propagation subsystem is configured to provide a microorganism to the fermenter. In some embodiments, the microorganism is yeast. In some embodiments, the first portion of the fermentation product may include an alcohol. In some embodiments, the first portion of the fermentation product may include isobutanol. In some embodiments, the first portion of the fermentation product may include water. In some embodiments, the microorganism separation device may include a centrifuge. In some embodiments, the microorganism separation device may include a filter. In some embodiments, the microorganism separation device may include a settling tank. In some embodiments, the microorganisms are yeasts.

[0027] In one aspect of the present invention, the first distillation column includes at least one vapor recompression subsystem. In another aspect of the present invention, the first distillation column includes at least one mechanical vapor recompression (MVR). In another aspect of the present invention, the first distillation column includes at least one thermal vapor recompression (TVR). Petition 870250080789, dated 09 / 09 / 2025, p. 16 / 122 10 / 81

[0028] In one aspect of the present invention, the base product may include vinasse. In some embodiments, the digester is an anaerobic digester. In another aspect of the present invention, the digester is a continuous digester. In another aspect of the present invention, the biogas removal subsystem may include a scrubbing column. In another aspect of the present invention, the pollutant is hydrogen sulfide.

[0029] In some embodiments, the flash tank receives the second portion of the fermentation product from the fermentation subsystem and returns part of the second portion of the fermentation product back to the fermentation subsystem. In some embodiments, the second portion of the fermentation product is a broth, and a broth low in isobutanol is returned to the fermentation subsystem. In some embodiments, the flash tank operates at atmospheric pressure. In some embodiments, the flash tank operates under vacuum at a reduced pressure below atmospheric pressure. In some embodiments, the flash tank operates at a temperature below the temperature of the second portion of the fermentation product received from the fermentation subsystem. In some embodiments, the separation vessel is a liquid / liquid separator to separate the condensate into the light phase and the heavy phase. In some embodiments, the light phase contains a higher amount of alcohol than the heavy phase.In some embodiments, the alcohol is isobutanol and the liquid / liquid separator forms a two-phase system. In some embodiments, the ion exchange vessel contains an ion exchange resin and receives the light phase from the separation vessel and removes impurities from the light phase by trapping ions in the ion exchange resin. In some embodiments, the ion exchange vessel receives a caustic solution to regenerate the ion exchange resin, discharging the impurities into a surge tank for fermented wort. Petition 870250080789, dated 09 / 09 / 2025, page 17 / 122 11 / 81

[0030] In some embodiments, the hydrocarbon production subsystem also includes at least one of the following: an oil-water separator to separate wastewater from the hydrocarbon processing subsystem; and a hydrocarbon storage vessel to store at least one of the following: iso-octane, C12 blend, or C16 blend from the hydrocarbon processing subsystem.

[0031] In some embodiments, the denitrogenation subsystem receives alcohol from the alcohol enrichment subsystem. In some embodiments, the alcohol is a fuel-grade isobutanol. In some embodiments, the dehydration subsystem receives alcohol from the denitrogenation subsystem and sends water and / or purge products to a fermented wort lung tank. In some embodiments, the olefin is a four-carbon olefin.

[0032] In some embodiments, the hydrocarbon pretreatment subsystem may include at least one of the following: a coalescer to receive the olefin from the dehydration subsystem; an adsorbent to remove unreacted alcohols, water, and nitrogen; and a feed receiver.

[0033] In some embodiments, the coalescer also receives wash water and sends wastewater to an equalization tank and / or dehydration unit. In some embodiments, the coalescer also receives wash water and sends wastewater to an equalization tank and / or dehydration unit. In some embodiments, the olefin is a C4 olefin. In some embodiments, the unreacted alcohol is isobutanol.

[0034] In some embodiments, the feed receiver receives the olefin from the adsorbent. In some embodiments, the first reactor is a solid acid-catalyzed oligomerization reactor (e.g., Polynaptha™ as a commercial example). In some Petition 870250080789, dated 09 / 09 / 2025, p. 18 / 122 In some embodiments, the first reactor receives the olefin from the feed receiver and oligomerizes the olefin into a polyolefin. In some embodiments, the debutanizer receives a polyolefin from the first reactor. In some embodiments, the debutanizer recycles an unreacted olefin and / or paraffin to the first reactor. In some embodiments, the second reactor is a hydrogenation reactor. In some embodiments, the second reactor receives a polyolefin from the debutanizer. In some embodiments, the second reactor also receives hydrogen from a hydrogen supply subsystem and hydrogenates the polyolefin to form a C8-C16 alkane. In some embodiments, the separator removes an unreacted olefin and / or paraffin from the C8-C16 alkane. In some embodiments, the unreacted olefins and / or paraffins include C4 products. In some configurations, the separator recycles a portion of the C8-C16 alkane to the second reactor.In some forms, the first dividing line separates the iso-octane fraction from the C8-C16 alkane.

[0035] In some embodiments, the iso-octane fraction may include about 85%, 90%, 91%, 92%, 93%, 94%, 95%, 96%, 97%, 98%, 99% or 100% by weight of C8 alkanes, about 1%, 2%, 3%, 4% or 5% by volume of olefins and / or about 2 ppm, 4 ppm, 6 ppm, 8 ppm or 10 ppm of sulfur.

[0036] In other embodiments, the isooctane fraction may include more than 95% by weight of C8 alkanes, less than 5% by volume of olefins and / or less than 10 ppm of sulfur. In some embodiments, the first divider separates an unreacted olefin and / or paraffin from the C8C16 alkane. In some embodiments, the unreacted olefins and / or paraffins include C4 products. In some embodiments, the second divider separates the C12 alkane fraction from the C18 fraction.

[0037] In some embodiments, the fuel gas system supplies fuel gas to the low-pressure boiler. In some Petition 870250080789, dated 09 / 09 / 2025, page 19 / 122 13 / 81 In some embodiments, the fuel gas system supplies fuel gas to the high-pressure boiler. In some embodiments, the fuel gas system supplies fuel gas to a direct-flame heater. In some embodiments, the low-pressure boiler is further configured to receive natural gas and / or biogas from an anaerobic digester. In some embodiments, the combined heat and power unit is further configured to receive natural gas and / or biogas from an anaerobic digester. In some embodiments, the low-pressure boiler in the fuel gas system is configured to receive corn oil, biomass, or biomass pyrolysis products as low-carbon intensity fuels.

[0038] In one embodiment, a process is provided for producing renewable transport fuels, such as gasoline, jet fuel (SAF) and diesel oil from renewable C1-C5 alcohols, comprising: a) converting C1-C5 alcohols to a mixture of C2-C7 olefins to generate stream A; b) optionally separating a predominantly C2 olefin fraction from stream A for recycling in the alcohol conversion step to create or separating the oligomerization conversion to generate a predominantly C4+ stream B; c) optionally purifying stream A and / or stream B and combining them to create a stream C suitable for oligomerization into fuel-range olefins; d) oligomerizing stream C into fuel-range olefins to create stream D; e) optionally hydrogenating stream D to create a predominantly paraffinic stream E;ef) to separate the current E into fractions suitable for use as gasoline, aviation fuel and diesel.;

[0039] In another embodiment, a process is provided for producing a renewable alkylate from renewable C1-C5 alcohols, comprising: a) converting C1-C5 alcohols to a mixture of C2-C7 olefins to generate stream A; b) optionally separating a Petition 870250080789, dated 09 / 09 / 2025, p. 20 / 122 14 / 81 predominantly C2 olefin fraction from stream A for recycling in the alcohol conversion step to create or separate oligomerization conversion to generate a predominantly C4+ stream B; c) optionally purify stream A and / or stream B and combine with renewable or petrochemical isobutane to create a stream C suitable for alkylation; d) subject stream C to an alkylation process to produce a crude renewable alkylate stream D; ee) optionally purify stream D so that it is suitable for direct use as renewable gasoline.

[0040] In yet another embodiment, a process is provided for converting ethanol of biological origin into higher octane gasoline and aviation fuel fractions, comprising: a) converting ethanol into ethylene and subsequently into C3-C8 olefin mixtures in a single step; and b) C3-C8 olefins, linear butenes and / or fractions thereof are cooligomerized with isobutylene, thereby increasing branching and providing higher octane gasoline and aviation fuel fractions.

[0041] It should be understood that all combinations of the foregoing concepts and additional concepts discussed in greater detail below (provided that such concepts are not mutually inconsistent) are contemplated as part of the inventive object described in this application. In particular, all combinations of the claimed subject matter of the present invention are contemplated as part of the embodiments disclosed in this application. It should also be taken into consideration that the terminology explicitly employed in this application, which may also appear in any description incorporated by reference, should be given a meaning more consistent with the specific concepts described in this application. BRIEF DESCRIPTION OF THE DRAWINGS

[0042] Figure 1 is a flowchart that illustrates a process of Petition 870250080789, dated 09 / 09 / 2025, page 21 / 122 15 / 81 low energy production consistent with the modalities of the current description.

[0043] Figure 2 is a flowchart illustrating a process for converting carbohydrates into hydrocarbons consistent with the embodiments of the present description.

[0044] Figure 3 is a flowchart illustrating an ethanol pretreatment and processing system consistent with the embodiments of the present description.

[0045] Figure 4 is a diagram illustrating the integration of waste heat from alcohol into hydrocarbons with biomass processing consistent with the embodiments of the present description.

[0046] Figure 5 is a process flow diagram illustrating a typical ethanol distillation system.

[0047] Figure 6 is a process flow diagram illustrating a conventional triple-effect evaporator used in ethanol purification.

[0048] Figure 7 is a process flow diagram illustrating the use of multiple MVR fans in ethanol purification consistent with the embodiments of the present description.

[0049] Figure 8 is a diagram illustrating the evaporator system integrated with Figure 7 consistent with embodiments of the present description.

[0050] Figure 9 is a graph showing a comparison of carbon intensities for different petroleum-based fuels, as well as the reductions in carbon intensity by employing various aspects of the low-energy process to produce biofuels.

[0051] Figure 10 is a flowchart illustrating an isobutanol production process consistent with embodiments of the present description. Petition 870250080789, dated 09 / 09 / 2025, page 22 / 122 16 / 81

[0052] Figure 11 is a flowchart illustrating a carbon-neutral, net-zero energy isobutanol process consistent with embodiments of the present description.

[0053] Figure 12 is a flowchart that illustrates a continuation of the process in Figure 11 consistent with the modalities of the current description.

[0054] Figure 13 is a flowchart illustrating a hydrocarbon pretreatment and processing system consistent with the embodiments of the present description.

[0055] Figure 14 is a diagram that illustrates the ETO recycling process with C2 to supply products consistent with the embodiments of the current description.

[0056] Figure 15 is a diagram illustrating the ETO dimerization process with C2 to supply products consistent with the embodiments of the present description.

[0057] Figure 16 is a diagram illustrating the process of dehydrating ethanol and alkylating a solid acid to alkylate the product consistent with embodiments of the present description.

[0058] Figure 17 is a diagram illustrating the process involving ETO with alkylation with liquid acid or with ionic liquid to alkylate the product consistent with embodiments of the present description.

[0059] Figure 18 is a graph depicting the increase in octane rating as a result of the cooligomerization of isobutylene with linear butenes versus iso-octane mixture. DETAILED DESCRIPTION

[0060] This application describes a process for producing high-energy-density, zero-carbon-footprint hydrocarbon fuels using a globally abundant and carbon-neutral feedstock: carbohydrates Petition 870250080789, dated 09 / 09 / 2025, page 23 / 122 17 / 81 tos. In the systems and processes described in this application, carbohydrates (e.g., corn, wheat, and / or sorghum) are converted into hydrocarbons. In general, the systems and processes achieve net-zero energy use and a zero carbon footprint by using a low-carbon carbohydrate-based feedstock, a feedstock fractionation process that can be employed before or after fermentation to remove most proteins and water-insoluble solids, a fermentation process, a biogas generation process using fermentation vinasse, and a process for converting alcohol into hydrocarbons.

[0061] In the systems and processes described in this application, the total external process energy requirements are less than approximately 20,000 BTU / gallon, 15,000 BTU / gallon, 10,000 BTU / gallon, 8,000 BTU / gallon, 6,000 BTU / gallon, 4,000 BTU / gallon, 2,000 BTU / gallon; The product is a hydrocarbon with an energy density of at least 100,000 BTU / gallon, 105,000 BTU / gallon, 110,000 BTU / gallon, 115,000 BTU / gallon, 120,000 BTU / gallon, 125,000 BTU / gallon, 130,000 BTU / gallon, 135,000 BTU / gallon, 140,000 BTU / gallon, 145,000 BTU / gallon, or 150,000 BTU / gallon. Therefore, the external process energy does not represent more than 6%, 8%, 10%, or 12% of the product energy. Achieving a zero carbon footprint, i.e., carbon neutrality, is possible due to this low external process energy requirement plus the appropriate selection of carbohydrate raw materials.Achieving this with ethanol or any other low-energy-density fuel is easier than with other fuels, given the lower energy density of the low-energy-density fuel. However, there is demand for a fuel that has an energy density closer to that of petroleum fuels, for example, an energy density of at least 65%, 70%, 75%, 80% or 85% of petroleum gasoline or gasoline. Petition 870250080789, dated 09 / 09 / 2025, page 24 / 122 18 / 81 aviation fuel.

[0062] In the hydrocarbon processes described in this application, any hydrocarbon product from the gasoline distillation range provides an octane rating of at least 50, 55, 60, 65, 70, 75 or 80 to ensure economical blending with other components to produce gasoline. This contrasts with current renewable diesel production, which generates a co-product (propane) with an octane rating lower than 50, 55, 60, 65, 70, 75 or 80.

[0063] In the processes described in this application, carbon intensity (CI) (gCO2e / MJ) is used as a measure of a high-energy-density carbohydrate-derived fuel using feedstock from reduced-crop maize, vinasse biogas and wind energy.

[0064] Carbon Intensity (CI), as described in this application, is calculated based on the industry-standard GREET® (Greenhouse gases, Regulated Emissions, and Energy use in Technologies) model from Argonne National Laboratory. However, other CI frameworks, while not used to calculate the CI values ​​in this application, may also be used, including but not limited to: the California Low Carbon Fuel Standard (CA-GREET3).0, The California LowCarbon Fuel Standard); the Carbon Offsetting and Reduction Scheme for International Aviation by the UN International Civil Aviation Organization (ICAO CORSIA); the Environmental Protection Agency's Renewable Fuel Standard (EPA RFS); the European Renewable Energy Directive (EU REDII); the Canadian Clean Fuel Standard (CFS). Petition 870250080789, dated 09 / 09 / 2025, page 25 / 122 The Argonne GREET® model was developed by Argonne with support from the U.S. Department of Energy (DOE) to consider the carbon intensity related to the energy and environmental effects of fuels and vehicle technologies. The Argonne GREET® model can be applied to all aspects of the fuel supply chain, enabling a true peer-to-peer comparison of greenhouse gas emissions among suppliers, consumers, industry, and regulators. The Argonne GREET® model quantifies emissions throughout the life cycle and is considered superior to other life cycle analysis (LCA) tools currently available. (Note: The text also mentions the 19 / 81 Canadian Clean Fuel Standard and the carbon reduction regulation used by Brazil (RenovaBio).)The Argonne GREET® model includes the Feedstock Carbon Intensity Calculator (FD-CIC) and the Carbon Calculator for Land Use Change from Biofuels (CCLUB). These models can be downloaded from https: / / greet.es.anl.gov / .

[0065] Carbon-neutral and net-zero energy systems, equipment, processes, resources, and functions for addressing problems in current systems are described and illustrated in this application. In the following description, certain specific details are presented to provide a complete understanding of various embodiments. In some cases, well-known structures have not been shown or described in detail to avoid unnecessarily obscuring the descriptions of the embodiments. Unless the context requires otherwise, throughout the descriptive report and claims that follow, the word "comprise" and variations thereof, such as "comprises" and "comprising," shall be interpreted in an open and inclusive sense, that is, as including but not limited to. Furthermore, the headings Petition 870250080789, dated 09 / 09 / 2025, page 26 / 122 20 / 81 provided in this application are for convenience only and do not interpret the scope or meaning of the claimed description.

[0066] The reference throughout this descriptive report to some modalities, a modality, or the modality means that a particular feature, structure, or resource described in connection with the modality is included in at least one modality. Thus, the appearance of the phrases in some modalities, in a modality, or in the modality in various places throughout this descriptive report does not necessarily refer to the same modality. Furthermore, particular features, structures, or characteristics may be combined in any suitable manner in one or more modalities. Additionally, as used in this descriptive report and the attached claims, the singular forms a, an, or include plural referents unless the content clearly indicates otherwise. It should also be noted that the term or is generally employed in its including and / or sense unless the content clearly indicates otherwise.

[0067] The word about, when immediately preceding a numerical value, means an interval of plus or minus 10% of that value, for example, about 50 means 45 to 55, about 25,000 means 22,500 to 27,500, etc. In addition, the phrases less than about a value or greater than about a value should be understood in light of the definition of the term about provided in this application.

[0068] C12 oligomers can be used directly for the production of renewable diesel fuel and renewable aviation fuel post-hydrogenation, for example, for the isobutanol / iC4 process. Process scheme for a low-energy production process for biofuel production.

[0069] A schematic of a low-energy production process 100 is shown in Figure 1. The low-energy production process Petition 870250080789, dated 09 / 09 / 2025, page 27 / 122 21 / 81 energy 100 is sometimes called a net zero carbon footprint process (sometimes Net Zero or NZ). Regarding raw materials and raw material selection, it is now known that certain farming practices allow for carbohydrates with a zero or lower carbon footprint. For example, maize grown with reduced tillage, reasonable yields, and no or low irrigation has been estimated to have a low or zero carbon footprint.

[0070] Referring to Step 1 of Figure 1, the low-energy production process 100 begins with the preparation of a fermentation feedstock. The fermentation feedstock is a biomass source containing carbohydrates and, optionally, water-insoluble solids and reducing proteins when the feedstock is introduced into water to form a paste. It has been determined that a carbohydrate source (e.g., high-sugar corn) can affect the ability to ultimately achieve a net-zero energy and carbon neutrality target. As mentioned in Figure 1, the feedstock is fractionated as needed for the process.

[0071] Step 2 in Figure 1 involves carrying out a fermentation to convert the carbohydrate into fermentation product. Alternatively, Step 1 can be carried out after the process in Step 2.

[0072] Step 3 of Figure 1 involves subjecting the fermentation broth containing a fermentation product to one or more fermentation product separation processes, which produces a first stream containing the fermentation product and a second stream consisting of the exhausted fermentation broth. The fermentation product is purified so that it can meet product specifications using one or more energy-efficient processes consistent with the technology described in this application. Optionally, the fermentation product is subjected to one or more transformations. Petition 870250080789, dated 09 / 09 / 2025, page 28 / 122 22 / 81 chemical processes that result in one or more hydrocarbons which, in certain embodiments described in this application, meet the specifications for use in fuels and / or chemicals. A unit with low thermal energy demand operates to recover the product of fermentation, including, as described in this application, distillation processes and equipment fitted with mechanical vapor recompression (MVR) and / or membranes, filters or centrifuges, which allow for an overall thermal energy production process lower than the zero-carbon energy generated by the fuel gas system.

[0073] In step 4 of Figure 1, the fermentation product is converted into a hydrocarbon product with an energy density of at least 100,000 BTU / gallon, 105,000 BTU / gallon, 110,000 BTU / gallon, 115,000 BTU / gallon, 120,000 BTU / gallon, 125,000 BTU / gallon, 130,000 BTU / gallon, 135,000 BTU / gallon, 140,000 BTU / gallon, 145,000 BTU / gallon, or 150,000 BTU / gallon using a combination of dehydration and oligomerization followed by hydrogenation. The heat output from the oligomerization step can be integrated into the first conversion step, which includes dehydration, so that the overall net energy required to convert alcohol to hydrocarbon is minimized to achieve a low-energy process.

[0074] In step 5 of Figure 1, the hydrocarbon product is separated into transportation fuels such as aviation fuel, diesel oil, bunker fuel and / or hydrocarbons from the gasoline distillation range. The hydrocarbon product, produced from the fermented product, generally consists of a range of C6 to C20 hydrocarbons that are useful for gasoline, aviation fuels, diesel and / or bunker fuels.

[0075] In step 6 of Figure 1, the vinasse has a composition substantially free of proteins and suspended solids, allowing Petition 870250080789, dated 09 / 09 / 2025, page 29 / 122 23 / 81 thus an efficient and low-cost water treatment system. Specifically, the composition of vinasse presents the following characteristics: greater than 40,000 COD, 45,000 COD, 50,000 COD, 55,000 COD, 60,000 COD, 65,000 COD, 70,000 COD, 75,000 COD, 80,000 COD, 85,000 COD or 90,000 COD; less than 0.2%, 0.4%, 0.8%, 1%, 1.2% or 1.4% of total suspended solids (TSS); less than 1000 ppm, 1300 ppm, 1600 ppm, 1900 ppm, 2200 ppm or 2500 ppm of total Kjeldahl nitrogen (TKN); less than 2000 ppm, 4000 ppm, 6000 ppm, 8000 ppm, 10,000 ppm or 12,000 ppm of protein.

[0076] Step 7 of Figure 1 may include subjecting the vinasse to one or more filtration processes to reduce suspended solids and proteins in order to meet these specifications. In certain embodiments, step 7 may be optional depending on the compositions.

[0077] In step 8 of Figure 1, the exhausted fermentation broth is subjected to an anaerobic digestion process which, in certain embodiments, produces at least 6,000 BTU, 8,000 BTU, 10,000 BTU, 12,000 BTU, 18,000 BTU, 22,000 BTU, 25,000 BTU, 30,000 BTU, 35,000 BTU or 40,000 BTU of methane per gallon of hydrocarbon product. This represents at least 6%, 8%, 10%, 12%, 18%, 22%, 25%, 30%, 35% or 40% of the energy content of the product being produced. In some embodiments, the anaerobic digestion process can produce at least 20,000 BTU of methane per gallon of hydrocarbon product, which can represent at least 20% of the energy content of the product being produced. In some embodiments, the amount of methane generated is at least as large as the external energy required by the process.As an alternative to using the methane produced in step 8 as an energy source, at least some of the oils produced during biomass fractionation (Step 1) can be used as an energy source for propulsion. Petition 870250080789, dated 09 / 09 / 2025, page 30 / 122 24 / 81 ionize the entire production process, or at least a part of the production process, so that fewer external energy sources are needed, which reduces the overall carbon footprint, at least in part.

[0078] The subsequent use of at least some of this methane as an energy source to power the entire production process, whether in whole or in part, results in the need for fewer external energy sources. For example, with a COD of 82,000 mg / L in a 58 MMGPY isobutanol plant, there would be approximately 233 MMBTU / h, or 500 MMBTU / day, of methane generated in an anaerobic digester. This equates to approximately 2 million MMBTU / year, considering 24 hours a day and 350 days a year. The total thermal energy required for the process is ~3300 MMBTU / day, not including the energy required to dry any of the solids streams, and approximately 5500 MMBTU / day if 90% of the solids are dried to approximately 88% dry matter, with the remainder being supplied to the feed market on a wet basis.

[0079] In step 9 of Figure 1, water treatment processes are used to produce water. The recovered water can be recycled back to the beginning of the process.

[0080] In step 10 of Figure 1, one or more boilers can accept the gas output from the anaerobic digester (AD) system. The heat or energy from the AD system, in certain embodiments, produces steam that drives part of the process. The use of heat / energy from the AD system also serves to reduce the overall external energy requirements of the process.

[0081] Referring to Figure 2, a flowchart is shown illustrating a process of converting carbohydrates into hydrocarbons via isobutanol 1000. A carbohydrate, such as corn 1001, undergoes fractionation 1005. Fractionation generally refers to the conversion of carbohydrates into hydrocarbons via isobutanol 1000. A carbohydrate, such as corn 1001, undergoes fractionation 1005. Fractionation generally refers to the conversion of carbohydrates into hydrocarbons. Petition 870250080789, dated 09 / 09 / 2025, page 31 / 122 25 / 81 version of the carbohydrate in constituent components. The fractionation products 1005 are then used for feed and raw material 1010, for example, although other alternative uses 1010 may be available for different biomasses, or used in the production of isobutanol 1015. Although described as isobutanol, isobutanol is an example of a possible alcohol that can be used in the overall process. The products of isobutanol production 1015 can be used for hydrocarbon production 1020 or water treatment 1030. The products of isobutanol production 1015 used for hydrocarbon production 1020 become iso-octane aviation fuel 1025. The product of isobutanol production 1015 used for water treatment 1030 becomes, in part, biogas 1035. Biogas 1035 and / or natural gas 1055 can be used to create an energy supply 1040. Optionally, corn oil and / or biomass can also be used as part of the energy supply 1040.In certain embodiments, any corn oil by-products may be sold or otherwise disposed of. Energy supply 1040 includes aggregated biogas, natural gas, corn oil, and biomass. Energy 1040, in certain embodiments, produces electricity 1050 and steam 1045, which optionally utilize wind power, CHP, electric boilers, combinations thereof, and similar systems. Process scheme for an energy-efficient hydrocarbon production process using ethanol as an alcoholic intermediate.

[0082] A schematic of a low-energy production process well-suited for jet fuels and diesel derived from an ethanol intermediate is shown in Figure 3. The selection of the feedstock is crucial to ensure that the input feedstock has a zero or negative carbon footprint.

[0083] Figure 3 is a process diagram and equipment 50. Petition 870250080789, dated 09 / 09 / 2025, page 32 / 122 26 / 81 The process diagram and equipment 50 show a fractionation and fermentation unit 51 that receives a carbohydrate 52, such as corn 52. The fractionation and fermentation unit 51 produces a fermentation broth 53 which is received by a distillation unit 54. The fractionation and fermentation unit 51 also produces corn fiber 55 and corn oil 56. The corn fiber 55 can be fed to an anaerobic digester (explained elsewhere in this application). The corn oil 56 can be used as fuel or otherwise disposed of. The distillation unit 54 produces an alcohol 57, such as ethanol 57, which is received by the dehydration unit 58. The distillation unit 54 produces fusel oils 59 which are combined with other fuels and sent to a boiler or similar. Distillation unit 54 also produces a feed co-product 60 and wastewater 61. Dehydration unit 58 dehydrates alcohol 57 and produces ethylene 62 which is received by a dimerization unit 63.The dehydration unit 58 also produces ethane 64 which is combined with fusel oils 59 and other fuels and additional wastewater 61. The dimerization unit 63 receives ethylene 62, catalysts and / or chemicals 65 to facilitate the operation of the dimerization unit 63 and water 66 to produce C4-C6 olefins 67 and C8 olefins 67. C4-C6 olefins 67 are received by an oligomerization unit 68. The dimerization unit 63 emits purge light 69 which is combined with the other fuels. The dimerization unit 63 also generates by-products which include spent caustic agents 70 and additional wastewater 61. The oligomerization unit 68 receives C4-C6 olefins 67 to produce C6 olefins 71 which are received by a hydrogenation and fractionation unit 72. The oligomerization unit 68 also produces additional light purge 69 which is combined with other fuels.The hydrogenation and fractionation unit 72 receives C4-C6 olefins 67 and C8 olefins 67 for processing. Petition 870250080789, dated 09 / 09 / 2025, page 33 / 122 27 / 81 produce fuels for transport 73. The hydrogenation and fractionation unit 72 also emits light purge 69 which is combined with other fuels.

[0084] As described in this application, low-carbon intensity (LC) maize or some other low-carbon intensity, carbohydrate-rich feedstock is fed into the process, as shown in Figure 3. In the case of maize, for example, the feedstock is simply ground into a flour with the desired particle size before being fed in. The flour is mixed with warm water and enzymes (e.g., alpha amylase and / or other suitable enzymes) before being fed into a liquefaction system that provides sufficient residence time for the starch in the maize flour to liquefy into polysaccharides. In some respects, enzymes such as cellulolytic enzymes, cellulase, protease, pectinase, xylanase, α-l-arabinofuranosidase and / or phytase may be used.In conventional dry milling plants for corn-based ethanol, heating the corn flour / water mixture prior to liquefaction is an energy-intensive process, as large quantities of steam are injected directly into the slurry tank to achieve a target temperature. To help minimize steam and freshwater use, warm water from the ethanol distillation system, warm water from the evaporator system, and fine, warm vinasse (called backset) are recycled to the downstream slurry tank. Additional water is often required to achieve the target percentage of total solids in the slurry tank. The bottom of the CO2 scrubbing column is a common stream of cold water that is fed into the slurry tank. If anaerobic digestion is being used in the design, treated DA effluent water can also be fed to the slurry tank. In some cases, fresh makeup water, such as city water, can also be introduced into the slurry tank. Petition 870250080789, dated 09 / 09 / 2025, page 34 / 122 28 / 81 at their sources, these water streams are relatively cold and increase the steam load required in the slurry tank. To enable this low-energy process to produce biofuels, design features are being incorporated to utilize excess heat from other parts of the NZ plant to heat the cold water streams feeding the slurry tank, thus reducing steam usage to the point where it is only needed during start-up. Figure 4 shows an example of the heat integration scheme being used to preheat the water feeding the slurry tank. Other configurations from Figure 4 to integrate heat generated from one part of the NZ plant to another are possible and are within the scope of this application.

[0085] Figure 4 shows a process and equipment diagram for integrating cooking water heating. Diagram 75 shows one possible equipment and process configuration, and others are possible and within the spirit and scope of current technology. The liquid, heated by other processes associated with the plant with a net-zero carbon footprint to produce transportation fuels and described elsewhere in this application, is received by a process water tank 76. The process water tank 76 contains heated water 77 or process water 77 for reuse by the plant, thus conserving thermal energy. The process water 77 can be used directly from the process water tank 76 or can be heated and pressurized by one or more heat exchangers 78, described further on as exemplary exchangers, where the heat exchangers 78 heat the process water 77 to superheated process water 79.For safe storage, a pulp heat exchanger 80 uses the heat from superheated process water 79 to heat the pulp 81 in the pulp tank 82. The pulp heat exchanger 80 cools and depressurizes the process water. Petition 870250080789, dated 09 / 09 / 2025, p. 35 / 122 29 / 81 superheated 70 for cooking water 83 which is stored in the cooking water tank 84. A pulp mixer 85 uses the cooking water to combine cooking water 83, corn flour (or similar), backset (described elsewhere in this application) and enzymes to produce pulp 81.

[0086] The anaerobic digester (AD) described elsewhere in this application is optional. Because the AD is optional, it may not be available to produce an effluent water stream as shown. An ethanol reactor creates an ethanol-to-ethylene purge water stream, this reactor being optional. The ethanol reactor converts ethanol into ethylene and water. This stream can be used to offset the freshwater fed into the CO2 scrubbing column or can be fed directly into the process water tank, as shown in Figure 4. A scrubbing water for ethylene dimerization is generated from the washing of butenes formed from the dimerization of ethylene in preparation for sending the butenes to the oligomerization process that produces C8, C12, and C16 olefins. The ethanol-to-ethylene conversion process receives 190 proof ethanol as feed and, for safety reasons, is cooled before going to intermediate storage by a water cooler.In this example, other heat exchangers could be used. Hot 190-proof ethanol undergoes cross-heat exchange with cold makeup water, which is heated by the hot 190-proof ethanol, thus conserving the heat removed from the hot 190-proof ethanol. The heated water is supplied to the process water tank. The bottoms of the stripper column constitute a relatively clean water stream, generated in the production of 190-proof ethanol. It is hot when it comes from the ethanol distillation and is fed directly into the process water tank. The evaporator condensate water is generated in the process of removing water from fine vinasse to produce syrup. The syrup. Petition 870250080789, dated 09 / 09 / 2025, page 36 / 122 30 / 81 sq.ft is finally mixed with the wet cake and sold as is for animal feed or, optionally, fed to a dryer to produce DDGS (dried distillers grains with solubles). The condensed water from the evaporator is hot and contains low levels of impurities, such as organic acids. It is fed directly into the process water tank.

[0087] The combined water streams in the process water tank are hot, but additional heat may be required to achieve the desired temperature in the slurry tank. A wide range of cooling operations in the ethanol-to-aviation kerosene conversion process were evaluated, in which the heat removed by a cooling water-cooled heat exchanger or an air-cooled heat exchanger would instead be used to heat the water exiting the process water tank. The cooling services were evaluated based on cooling load, temperature, operability, and safety. Although there were other operations with higher cooling loads or useful temperature ranges, the three operations that met all criteria, including operability and safety, are shown in Figure 4.Cooling operations related to the exothermic heat of reaction generated by ethylene dimerization and butene oligomerization were evaluated, but were ultimately eliminated as heat sources for cooking water because they were too cold or presented safety / operability problems in managing reaction temperatures. The three cooling operations shown in Figure 4 are arranged to allow the process water to be heated from approximately 67 °C to approximately 112 °C in three stages. The process water exiting the cross-heat exchanger with saturated recycling from hydrogenation is above the boiling point of water at atmospheric pressure. The process water will be backpressure controlled at this point. Petition 870250080789, dated 09 / 09 / 2025, page 37 / 122 31 / 81 making it superheated. It is necessary to accumulate the hot process water in an equalization tank to manage process fluctuations, but water cannot be safely or economically stored superheated and some of it will vaporize if stored at atmospheric pressure. For this reason, the superheated process water is exchanged through a pulp tank circulation circuit to lower the process water temperature to below the atmospheric boiling point before being fed to the cooking water tank, which is at atmospheric pressure. The cooking water tank, as shown in Figure 4, will operate at approximately 95°C. The cooking water is fed into the pulp tank where it is combined with corn flour, backset, and enzymes. In total, the heat integration scheme, as shown in Figure 4, saves at least 33 MMBTU / h of steam for an ethanol capacity of 100 million gallons per year (anhydrous basis, 8).000 hours of annual operation), which is equivalent to 39 MMBTU / h of natural gas, assuming a boiler efficiency of 85%.

[0088] Optionally, the stream exiting the liquefaction can undergo further processing to reduce the size of the corn particles before being fed downstream. This is advantageous because it helps to release more corn oil from the corn particles, making more corn oil available for further recovery, although energy recovery through corn oil is optional, as corn oil can be used in other ways to reduce carbon. In the case of this low-energy process for biofuel production, the corn oil will be recovered and used as fuel for the boiler system, which helps to reduce the carbon intensity of the final aviation product, as well as the naphtha and diesel byproducts.

[0089] The stream that comes out of the liquefaction feeds the tanks of Petition 870250080789, dated 09 / 09 / 2025, p. 38 / 122 32 / 81 fermenter, where it combines with additional enzymes and yeast. Fermentation is carried out conventionally. The liquefied starch is simultaneously saccharified to form monosaccharides which are then consumed by the yeast to form ethanol and CO2 gas. The CO2 gas is released from the fermenters to a washing system that uses water to purify any ethanol or other water-soluble impurities that may have been carried along with the CO2 vapor. Fermentations are carried out in batches. When a batch of fermentation is complete, the monosaccharides are almost gone, leaving only a small amount of residual sugars. The ethanol concentration is approximately 13.0% by weight, 13.5% by weight, 14.0% by weight, 14.5% by weight, 15.0% by weight, or 15.5% by weight.In general, the yeast does not consume the corn fiber, corn oil, corn protein, ash, and other corn-based components present in the fermenter broth, except for a small amount of nutrients consumed as the yeast continues to multiply during fermentation. Ethanol-based components, water, yeast, and corn are transferred to a large equalization tank called the fermented wort lung tank. A stream of fermented wort is continuously fed out of the fermented wort lung tank, downstream of the ethanol distillation, where the ethanol is recovered, while most of the water, corn components, yeast, and enzymes are sent downstream in what is called full vinasse.

[0090] Ethanol distillation can be carried out in several ways. In dry corn milling plants that produce fuel-grade ethanol, the ethanol distillation system is almost always thermally integrated with the evaporator system in some way to reduce the amount of fresh steam needed to run the process. Figure 5 shows an example of a technology. Petition 870250080789, dated 09 / 09 / 2025, page 39 / 122 33 / 81 commercially available gia for distilling fuel-grade ethanol.

[0091] Like all available technologies, the one in Figure 5 has features to facilitate operation. The fermented wort from the fermented wort surge tank is almost always exchanged in the exchanger 101, with the stream exiting the liquefaction to preheat the fermented wort on its way to distillation in the fermented wort stripping column 102 (or fermented wort distillation tower 102) and to save on cooling water demand by cooling the liquefied wort before fermentation. Figure 5 shows the wet ethanol vapor 103 removed at the top of the fermented wort separator 102 and being condensed in a first evaporator of a multi-effect evaporator system 104, shown in Figure 6. The heat removed from the wet ethanol vapor is used to remove water vapor from the fine vinasse in the first evaporator, as shown in Figure 6.The water removed in the first evaporator is used to power the separation in the second-effect evaporator, and so on. Evaporation is a process that consumes a lot of energy, but the scheme shown in Figures 5 and 6 is such that the evaporator system does not require fresh steam. Figure 6 shows a typical triple-effect evaporator configuration that can be used. Figure 6 shows additional distillation components, including a fermented wort reboiler 105, a rectifier column 106 (rectifier distillation tower 106), where the condensed wet ethanol 103 is revaporized by the rectifier column 106 and used to provide heat to the fermented wort reboiler 105. A top condenser of the rectifier column 107 uses the outlet of the fermented wort reboiler cooler 105 to further condense the output to a 190 proof ethanol 108. A fusel oil washing and separation unit 109 is used by the rectifier column 106. Petition 870250080789, dated 09 / 09 / 2025, page 40 / 122 34 / 81 and provides fusel output 110 which is combined, in this example, with proof ethanol 108. A side stripping column 111 (side distillation tower 111) is driven by fresh steam 112 in a side stripping column reboiler 113 to provide additional energy to the system 114.

[0092] Figure 7 shows an exemplary embodiment of the multiple-effect evaporation system 104 in more detail. The multiple-effect evaporation 104 receives wet ethanol vapor 103 and a fine vinasse from a vinasse separation, which is explained elsewhere in this application. Although the multiple-effect evaporation system 104 is shown with three (3) evaporators 120, 121 and 122, more or fewer evaporators are possible depending on cost, design and recovery constraints. The condensed wet ethanol 103 is fed to the rectifier column 106. An improvement in the energy conservation of the distillation system shown in Figure 5 consistent with the technology of the present application is shown in Figure 7 below. In particular, it has been found that condensation of the vapor from the top of the rectifier column 106 allows the pressure and temperature of the vapor / liquid from the top to be heated using one or more pumps, such as the mechanical vapor recompression fans shown.The pressure can be such that the condensed steam from the top of the rectifier column 106 operates at a higher pressure and temperature, so that the ethanol 190 proof can power the fermented wort reboiler 105. The fermented wort reboiler 105 has a substantial function, so this heat integration saves fresh steam and reduces the total external energy required for the NZ plant. The problem with condensing the steam at the top of the fermented wort extraction column 102 before feeding into the rectifier column 106 is that most of the feed to the rectifier now needs to be re-vaporized to get the ethanol to the top of the rectifier column 106. A. Petition 870250080789, dated 09 / 09 / 2025, page 41 / 122 35 / 81 energy for revaporization comes from a large quantity of fresh steam 112 used in the reboiler of the side stripping column 113.

[0093] For this lower energy consumption process to produce biofuels, it is desirable to minimize the use of fresh steam and natural gas, so that even a scheme like that in Figures 5 and 6 has opportunities for energy reduction. For this lower energy process to produce biofuels, a scheme like that shown in Figure 7 can be implemented. Figure 7 shows one possible configuration, although other configurations are within the spirit and scope of the present application.

[0094] Figure 7 shows the distillation system with fans. MVR, refer to the fermented wort column with MVR 3195 fans in Figure 11 below. The MVR fans shown in Figure 7 can be considered a mechanical vapor recompression (MVR) system 123. Figure 7 has some components similar to the distillation system of Figure 5, and the similarities will not be explained again. As shown in Figure 7, wet ethanol 103 is fed directly to the rectifier column 106. The vapor from the top of the rectifier column 106 is fed into the MVR system 123, which has a series of MVR 1241-I fans, of which the MVR system 123 has five (5) MVR 1241-5 fans. The MVR 124 fans increase the pressure and temperature of the steam from the top of the rectifier column 106 to drive the fermented wort reboiler 105. The discharge from the fermented wort reboiler is fed into a multi-effect finishing evaporator 125, which replaces the multi-effect evaporation system 104 above.A collection well (not shown) in rectifier column 106 is used to extract 190 proof 108 ethanol directly from rectifier column 106, which removes fermentation byproducts from the 190 proof 108 ethanol stream that would present problems in the dehydration and purification reaction. Petition 870250080789, dated 09 / 09 / 2025, page 42 / 122 36 / 81 ethanol. The 190 proof 108 ethanol is drawn from an extraction tray one or more stages below the top of the rectifier column (note that the columns used in the context of the present application may be distillation towers). This allows acetaldehyde to accumulate in the top rectifier, away from the 190 proof, and be purged in the light purge stream shown in Figure 7. Acetaldehyde can form undesirable byproducts such as CO2 during the ethanol dehydration reaction, therefore it is desirable to keep it out of the 190 proof ethanol. As shown in Figure 7, the fusel oil stream is not recombined with the 190 proof 108 ethanol stream as occurs in a conventional corn milling plant producing fuel-grade ethanol. The fusel oil stream contains high concentrations of C4 and C5 alcohols. These C4 and C5 alcohols react in the dehydration reaction of ethanol to form their respective monoolefins.These olefins are ultimately removed from the ethylene produced along with other oxygenated byproducts and then burned as fuel to offset other heating demands of the process. Fossil fuels have a higher calorific value as fuel before being converted into olefins, therefore, for this low-energy process to produce biofuels, they are not combined with 190 proof ethanol. Table 1 below shows examples of the composition of the fusel oil stream and the composition of the light purge shown in Figure 7. Table 1. Component % by weight of light purge % by weight of fusels Ethanol 70.8905 25.6346 Water 3.6641 27.6144 Carbon dioxide 8.2980 Acetaldehyde 14.6326 0.0032 Acetal 0.0950 0.0089 Petition 870250080789, dated 09 / 09 / 2025, page 43 / 122 37 / 81 Ethyl acetate 2.0928 0.0012 Methanol 0.1249 0.0010 N-propanol 0.0897 N-butanol 0.9071 2-butanol 0.0696 Isobutanol 7.8546 Isoamyl alcohol 22.7177 Amyl alcohol 15.0954 Acetone 0.1096 0.0003 Isopropanol 0.0001 0.0001 1-pentanol 0.0011 Diethyl ether 0.0916 Tert-butanol 0.0008 0.0012 Total 100.0000 100.0000

[0095] The combined light purge and fusels are capable of offsetting up to 27 MMBTU / h (higher calorific value) of the project’s thermal demand. Burning corn oil as fuel provides another 62 MMBTU / h (higher calorific value) for steam production.

[0096] Ethanol distillation for this lower energy consumption process to produce biofuels differs from what a conventional corn ethanol plant can do in several ways. A clear distinction, as shown in Figure 7, is the addition of the MVR 123 system, centered around five (5) MVR 124 fans placed in series between the upper steam rectifier column 106 and the fermented wort reboiler 105. The MVR 123 system mechanically compresses a vapor that simultaneously increases its temperature to a more useful range and increases the pressure so that the vapor condenses at a higher temperature.This effect makes the latent heat of condensation of the steam available to power something like the reboiler of the fermented wort column, as shown in Figure 7. At least three, four, and five or more. Petition 870250080789, dated 09 / 09 / 2025, page 44 / 122 38 / 81 MVR fans are shown because the temperature and pressure rise in an MVR fan is in the range of 11 °C and 6.5 psi, respectively. A total pressure rise of 20 psi, 25 psi, 30 psi, 35 psi, 40 psi, 45 psi, 50 psi or more is believed to be preferable in the fans so that the vapor has a condensation range with a higher temperature than that in which the bottom of the fermented wort column will be operating. The temperature rise in the fans is controlled by injecting high-resistance liquid from the rectifier pump into the feed of each fan. In one embodiment, the total number of MVR fans is preferably five. A single MVR fan brings benefits. In general, certain embodiments of the present technology will include at least three (3) MVR fans. Other embodiments of this technology will include a maximum of five (5) MVR fans.In other embodiments of the present technology, three (3) to five (5) MVR fans are provided.

[0097] The exemplary system configuration shown in Figure 7 provides five (5) MVR fans to increase the pressure and temperature of the steam from the top of the rectifier column to a useful range where it can be used to operate the reboiler of the fermented wort stripping column.

[0098] The five (5) stage MVR, for example, as illustrated in Figure 7, is considered the most economical to obtain the necessary thermal energy savings, for the following reasons, for example: i. MVRs use fuel ethanol to power the reboiler in the fermented wort column, ii. More MVRs increased the cost, iii. Fewer MVRs did not provide energy at the preferred pressure, Petition 870250080789, dated 09 / 09 / 2025, page 45 / 122 39 / 81 iv. One compressor costs almost three times the cost of five MVRs and v. The thermal energy savings are at least about 7,327 BTU / gal of ethanol, or at least approximately 11,780 BTU / gal of hydrocarbon (based on 100 MMGPY of ETOH and 62.2 MMGPY of hydrocarbon).

[0099] An additional water remover absorbs the hydraulic load from the bottom of the rectifier column and reduces the hydraulic load on the wort stripping column. This reduces the size (diameter) of the wort stripping column and allows the column to be manufactured in the workshop and transported to the field. This provides significant cost savings compared to a field-manufactured column.

[00100] Another way is to generate low-pressure steam from evaporator condensate or boiler water to power an auxiliary reboiler for the water stripping column, which reduces the natural gas thermal load by about 1,884 BTU / gal of ethanol, or about 3,028 BTU / gal of hydrocarbon.

[00101] The vapor from the top of the rectifier column 106 is partially condensed in the fermented wort reboiler 105. Additional heat can be recovered after the fermented wort reboiler 105 by the multi-effect finishing evaporator 125, which is shown in more detail in an exemplary configuration in Figure 8.

[00102] Figure 8 also shows fine vinasse being concentrated into syrup. A mechanical vapor recompression evaporator (MVR) 126 uses a single fan MVR 127 to increase the pressure and temperature of water vapor from an extraction of the MVR 126 evaporator to produce the heat necessary to expel the water from the fine vinasse being fed to it. The discharge from the single fan MVR 126 is used for reflux in a distillation system. Petition 870250080789, dated 09 / 09 / 2025, page 46 / 122 40 / 81 tion. The multi-effect finishing evaporator 125 is shown with three (3) finishing evaporators 127, 128, 129. The first finishing evaporator 127 receives the output from the fermented wort reboiler 105. As can be seen in Figure 8, the steam and condensate configuration of the MVR evaporator 126 and the multi-effect finishing evaporator 125 is to recover / conserve as much energy as possible to reduce the overall carbon footprint of the NZ plant in which it is incorporated.

[00103] The intermediate vinasse produced by the MVR 126 evaporator contains approximately 35% to 45% solids by weight and is sent to a corn oil separation system 130, where the corn oil is removed by centrifugation. Optionally, the distilled corn oil generated by the corn oil separation can be consumed by the NZ plant as energy to reduce the plant's footprint. Alternatively, the distilled corn oil can be disposed of in other ways that reduce carbon emissions.

[00104] The intermediate vinasse is then sent to the finishing evaporators 127 and 128 in this exemplary configuration, where the output of the fermented must reboiler 105 is used to provide the heat to remove the remaining water to achieve a syrup solids content of approximately 45% by weight or 45% by weight.

[00105] The outlet of the fermented wort reboiler 105 is used by the finishing evaporators 127 and 128 to increase the syrup solids. This allows for better wet solids for transport and sales, as well as reducing energy in a rotary dryer by approximately 1.8 MMBTU / h.

[00106] The condensed steam from the top of the rectifier column is then sent back to an upper tank of the rectifier column 131. The contents of the upper tank of the rectifier column 11 can be used as a reflux injection in the rectifier column 106 to facilitate the Petition 870250080789, dated 09 / 09 / 2025, page 47 / 122 41 / 81 distillation process.

[00107] Heat integration in ethanol and hydrocarbon results in energy reduction of approximately 3,446 BTU / gal of ethanol, or approximately 5,540 BTU / gal of hydrocarbon.

[00108] Another evident feature of Figures 7 and 8 is that the described scheme improves efficiency because the steam from the fermented wort remover 103, whether ethanol steam 103 in this exemplary embodiment, is not condensed before feeding the rectifier. With this feature, high rates of fresh steam 112 are not required for the side stripping column reboiler 113 to re-vaporize the feed to the rectifier column 106. The scheme in Figure 7 incorporates the evaporator system in a heat integration strategy. After the fermented wort reboiler 105, a portion of the top vapors from the rectifier column 10 still remains in the vapor phase. The condensation load of this remaining vapor is used to drive the multi-effect finishing evaporator 125, which is part of the evaporator system that produces syrup.Figure 8 shows an exemplary configuration of the multi-effect finishing evaporator 125, which integrates the top vapors from the rectifier column 106 in Figure 7 into the multi-effect finishing evaporator 125.

[00109] The scheme in Figure 8 uses an MVR127 fan to drive the MVR 126 evaporator to remove some of the water in the fine vinasse. A benefit of the MVR 127 fan is that it increases the overall efficiency of the evaporator and eliminates the need for fresh steam in exchange for electricity from a renewable source such as wind. The fine vinasse feeding the evaporator system, as shown in Figure 8, originates at the bottom of the fermented must column 102, as shown in Figure 7, as complete vinasse. All the vinasse is processed through a system to remove most of the Petition 870250080789, dated 09 / 09 / 2025, page 48 / 122 42 / 81 insoluble solids (also known as suspended solids) from the liquid. Some type of centrifugation is normally employed for this. The two streams resulting from the separation of the complete vinasse are called fine vinasse and wet cake. An example of the streams and compositions of complete vinasse, fine vinasse, and wet cake are shown in Table 2. This corresponds to a capacity of over 100 million gallons of anhydrous ethanol per year (8,000 operating hours per year). Table 2. Components: Complete Vinasse, Fine Vinasse, Wet Cake, Large Fibers + Ash, lb / h 16,482 2,472 14,010, Fine Fibers + Ash, lb / h 12,034 4,212 7,822, Sugar (dextrose), lb / h 778 597 181, Fine Starch, lb / h 3,328 1,165 2,163, Fine Protein, lb / h 22,423 7,848 14,575, Large Protein, lb / h 0 - -, Corn Glycerides, lb / h 10,606 6,576 4,030, Corn Fat, lb / h 442 274 168, Water, lb / h 354,949 272,477 82,472 Lactic acid, lb / h 78 60 18 Glycerol, lb / h 2,969 2,279 690 Protein amylase, lb / h 9 7 2 Yeast, lb / h 3176 476 2,700 Urea, lb / h 134 103 31 Total, lb / h 427,410 298,547 128,862

[00110] Often, a portion of the fine vinasse is recycled back into the pulp tank to be mixed with cornmeal, cooking water, and enzymes. This recycled fine vinasse is called Petition 870250080789, dated 09 / 09 / 2025, page 49 / 122 43 / 81 backset (fine vinasse recirculation stream). The backset has multiple functions. It helps reduce freshwater use in the plant and reduces the size and utilities associated with the evaporator system. It also provides nutrients that are used by the yeast during fermentation, ensuring that it is healthy and performs quickly and efficiently.

[00111] The diagram in Figure 8 shows thin vinasse feeding an MVR 126 evaporator. A constant circulation of thickened vinasse is pumped from the bottom of the evaporator to the top. The thin vinasse mixes with this recirculation stream as it travels to the top of the evaporator. This type of evaporator is called a falling film evaporator because the feed to the top is distributed through a series of tubes. The vinasse flows as a film through the inside of the tubes and is heated by the hot steam flowing over the outside of the tubes. Water vapor evaporates from the thin vinasse as it descends through the tubes and detaches from the liquid at the bottom of the evaporator. In Figure 8, the water vapor that separates from the vinasse at the bottom is fed to the MVR 127 fan which compresses the water vapor and forces it through the outside of the tubes, where most of it condenses as it heats the vinasse inside the tubes.With the MVR 127 fan, it is believed that fresh steam is not required to operate the multi-effect finisher evaporator 125. The vinasse stream produced in the MVR 126 evaporator contains approximately 35% or approximately 45% total solids by weight. This concentration is necessary to remove the corn oil from the stills in the vinasse stream between the MVR 125 evaporator and the finisher evaporators 127, 128, and 129. The process of removing the corn oil from the distillery typically involves adding a chemical to the vinasse that acts as a demulsifier, followed by centrifugation. The oil... Petition 870250080789, dated 09 / 09 / 2025, page 50 / 122 44 / 81 Corn, being less dense than water, can be separated quickly and efficiently under the high relative centrifugal forces imposed by centrifugation.

[00112] In the case of this lower energy consumption process for producing biofuels, distillery corn oil is used as fuel to power the boiler system.

[00113] The de-oiled intermediate vinasse from the oil separation block in Figure 8 is sent to the finishing evaporators 127, 128, 129. The heat to power the first finishing evaporator 127 is supplied by the outlet of the fermented wort reboiler 105. The vinasse is circulated to the top and back down through the tubes in the same manner as the MVR evaporator 126 above, except that in this case the high-resistance rectifier steam fed to the side of the casing of the first finishing evaporator 127 condenses as it transfers heat through the tube walls to the vinasse. The separated water vapor at the bottom of the first finishing evaporator 127 is used to power the second finishing evaporator 128. The concentrated vinasse produced by the second finishing evaporator 128 is called syrup and is mixed with the wet cake from the whole vinasse separation.The wet cake can be sold as is as animal feed and is called wet distillers grains with solubles (WDGS). The wet cake can also be dried and then sold as animal feed, known as dried distillers grains with solubles (DDGS). The water vapor from the second finishing evaporator 128 is condensed and mixed with other cooking water streams to be used in the pulp tank, see Figure 4. Table 3 below compares the energy use for a conventional ethanol distillation and evaporation system, as shown in Figures 5 and 6, versus the system with energy reductions shown in Figures 7 and 8. Petition 870250080789, dated 09 / 09 / 2025, page 51 / 122 45 / 81 Table 3a. Parameter Case 1b Conventional Case 2c Low Energy MVR Fan Power, Megawatts 0 6.4 MVR Fan Power, MMBtu / h 0 21.8 Steam Consumption, MMBtu / h 117 15.8 Natural Gas Equivalent, MMBtu / h 137.6 18.6 All figures are based on a capacity of 100 million gallons of anhydrous ethanol per year and 8,000 hours of operation; bFor Figures 5 and 6; For Figures 7 and 8; assume a boiler efficiency of approximately 85%.

[00114] As evident from Table 3, the steam demand drops dramatically when using the MVR-based system by approximately 86.5%. Furthermore, by placing the energy requirement of the MVR in the same units as the steam, it is not a one-to-one exchange from steam to electricity. The MVR provides an energy reduction of approximately 67% compared to conventional systems, regardless of the heat source.

[00115] In the described lowest energy consumption process for producing biofuels, all electrical demands are met with renewable wind energy. It is also possible to use other forms of renewable electricity, such as solar, nuclear or hydroelectric. For the described lowest energy consumption process for producing biofuels, the thermal loads that would normally be met by natural gas can be met with fuel streams generated in situ by the process itself or by a mixture of natural gas and renewable natural gas with a net carbon intensity of zero.

[00116] The low-energy process described for producing bio Petition 870250080789, dated 09 / 09 / 2025, page 52 / 122 46 / 81 fuels, for aviation fuel, naphtha, and renewable diesel products, are marketable and valuable as renewable fuels since their carbon intensity is low compared to their conventional petroleum-based equivalents. This low-energy process for producing biofuels is designed to produce liquid transportation fuels with a carbon intensity of about 45 or less, using the methodologies defined by the California Air Resources Board's (CARB) Low Carbon Fuel Standard (LCFS). Figure 9 shows a comparison of carbon intensities for different petroleum-based fuels, as well as the carbon intensity reductions achieved by employing various aspects of this low-energy process for producing biofuels designed to ultimately achieve a carbon intensity of about 45 or less for the liquid transportation fuel products.

[00117] Figure 10 shows an isobutanol process and system 2000. At the beginning of the isobutanol process and system 2000, a storage container 2001, for example, corn silos, contains a carbohydrate, for example, corn or high-sugar corn, which can be sent to a crusher, such as a hammer mill 2005, or alternatively, the fine carbohydrate vinasse 2040 can undergo high-temperature short-time (HTST) fine vinasse processing 2045. Referring to the carbohydrate that is sent to the crusher, it then goes to a pulp tank 2010, followed by liquid tanks 2015 and subsequently by treatment tanks 2020. The product from the treatment tanks 2020 undergoes separation, such as feed and oil separation 2025, to produce final products such as corn oil and animal feed. 2030 for storage, and residual products that are recycled in the process, such as via Mash HTST 2035. Petition 870250080789, dated 09 / 09 / 2025, p. 53 / 122 47 / 81

[00118] Referring to fine vinasse 2040, it undergoes HTST fine vinasse 2045 before use in isobutanol yeast propagation 2050. The isobutanol yeast propagation product 2050 then goes to a fermentation unit, such as the isobutanol fermenter 2055, along with the HTST mash products 2060. The products from the isobutanol fermenters 2055 are sent to modified GIFT columns 2065, and a portion is recycled back to the isobutanol fermenters 2055 or sent to a fermented wort surge tank 2090. What is not recycled from the modified GIFT columns 2065 returns to the isobutanol fermenters 2055 / fermented wort surge tank 290 and is sent to a liquid / liquid separator 2070. The products from the tank Lung fermentation of wort 2090 is sent to a first distillation column 2085, as is the fermentation wort column 2085.A product from distillation column 2085 is fed into liquid / liquid separator 2070, and a product from distillation column 2085 is fed into a filter unit 2115. Liquid / liquid separator 2070 produces heavy phase liquid 2075 and light phase liquid 2080. The heavy phase liquid 2075 is sent back to the fermented wort column 2085, as in a reflux operation. The light phase liquid 2080 is sent to the descaling unit 2095, through membranes 2100 for filtration and the like, and to a descaling unit 2105. The light descaling unit 2105 produces fuel-grade isobutanol 2110 for hydrocarbon storage or processing. The product from the fermented wort column 2085 fed to the filtration unit 2115 is combined with the product from the light removal unit 2105 and filtered in the filtration unit 2115; optionally, a filter before the fermented wort column 2085 can be provided.The output from filter 2115 is sent to an anaerobic digester 2120. The products are rich in protein. Petition 870250080789, dated 09 / 09 / 2025, page 54 / 122 48 / 81 of the 2125 filter 2115 can be used for animal feed, recycled as fermentation nutrients, or otherwise disposed of. The anaerobic digester 2120 produces biogas 2130 which can be sent to the boiler of another subsystem and recycles water 2135, which is recycled in other subsystems.

[00119] Figure 11 is a flowchart illustrating an isobutanol production process and a 3000 system consistent with a net-zero production plant consistent with the technology of the present application that produces, in certain embodiments, transportation fuels. The isobutanol production process and the 3000 system flowcharts include systems and subsystems that have particular structures which, together, describe an NZ plant consistent with the technology of the application represented. Although certain structures, processes, and features of the NZ plant are described in relation to one or more of the identified subsystems, the specific structures, processes, and features may be scattered or contained in other subsystems of the NZ plant without departing from the scope of the present technology.The isobutanol 3000 production process and system includes a fractionation subsystem 3002, a fermentation subsystem 3003, a water treatment subsystem 3004, and an alcohol enrichment system 3006. Products from these subsystems, along with the subsystems shown in Figure 12, are combined to create a carbon-neutral, net-zero energy overall production plant that utilizes the processes and equipment described.

[00120] In the fractionation subsystem 3002, recycled water 3001 goes through cooking 3005 to create cooking water 3010. Additionally, a carbohydrate such as corn 3030 goes through a receiving and storage system 3035 and subsequently through grinding 3025 to produce ground corn 3020. Ground corn 3020 and water Petition 870250080789, dated 09 / 09 / 2025, page 55 / 122 49 / 81 of cooking 3010, together with the added enzyme 3045, are placed in the pulp pre-treatment 3015. The resulting pulp 3050, together with the biogas 3035, goes to the clean sugar process 3055. The clean sugar process 3055 has a dryer vent to the atmosphere 3060 and generates products 3070, such as dried distillers grains (DDG) and corn oil for storage and shipping 3075, as well as sugar / pulp 3080 destined for the HTST pulp processor 3085, which treats the sugar / pulp 3080. The sterilized mash 3090 from the HTST Mash 3085 is then placed in the fermentation subsystem 3003.

[00121] In the fermentation subsystem 3003, there is sterile air 3135 and, additionally, air from a CO2-rich exhaust collector 3095. The CO2-rich air is washed by a scrubbing column of the CO2-rich exhaust system 3100, and the resulting air is released to the atmosphere 3105.

[00122] The sterilized must 3090, received from the fractionation subsystem 3002, together with nutrients 3115 and a pH adjusting agent 3120, are placed in the fermentation structure 3110. In addition, the recycle water 3250 is directed to the vinasse sterilization 3255, and the resulting sterile vinasse 3260, together with nutrients 3280, a pH adjusting agent 3290, and a microorganism 3275, such as yeast cream 3275, from a microorganism propagation unit 3270, such as the yeast seed system 3270, are placed in the propagation 3265. The propagation 3265 produces an inoculum 3285. The inoculum 3285 is fed to the fermentation 3110, together with the constituent parts mentioned above. Fermentation unit 3110 produces at least one first portion and one second portion. The second portion of fermentation unit 3110 includes at least one fermentation broth 3125. The first portion of fermentation unit 3110 Petition 870250080789, dated 09 / 09 / 2025, p. 56 / 122 50 / 81 includes at least one diluted fermented wort 3165 (or one alcohol 3165), such as isobutanol fermented wort 3265. The fermentation broth 3125 is supplied to the modified / enhanced GIFT 3140 of the alcohol enrichment subsystem 3006, described below.

[00123] A portion of the diluted fermented wort 3165, such as, for example, a diluted isobutanol fermented wort 3165, from fermentation 3110 may be used for water recovery in the water treatment subsystem 3004, described below. A portion of the diluted fermented wort 316 may be used by the alcohol enrichment system 3006, as described below. Before water recovery or alcohol enrichment, however, the fermented wort surge tank 3170 receives the diluted fermented wort 3165. HC water from a DHYD unit 3175 and the intermittent purge of heavy components from the DHYD unit 3180 are fed into the fermented wort surge tank 3170 to create the fermented wort 3185 (or undiluted fermented wort 3185). The fermented wort 3185 passes through the yeast separation unit 3190 of a fermented wort column with MVR 3195, such as, for example, an isobutanol (IBA) fermented wort column with MVR 3195.The fermented must column with MVR 3195 receives a pH adjusting agent 3205. The resulting fermented must column with the condensate from MVR 3195 goes to the alcohol enrichment subsystem 3006 via a light / light separation unit 3215, such as, for example, an IBA light / light separation unit 3215. The heavy phase 3210 from the light / light separation unit 3210 is recycled back to the fermented must column with MVR 3195. The fermented must column with MVR 3195 produces the bottoms of the fermented must column 3245, which are used in the sterilization of vinasse 3255. A portion of the bottoms of the fermented must column 3245 is used in the water treatment subsystem 3004, as explained. Petition 870250080789, dated 09 / 09 / 2025, page 57 / 122 51 / 81 below.

[00124] The alcohol enrichment system 3004 receives the fermentation broth 3125 from the fermentation subsystem 3003. An enhanced GIFT 3140 receives the fermentation broth 3125. The enhanced GIFT passes chilled water 3145 and hot water 3150 back and forth between the GIFT coolers 3155. The enhanced GIFT 3140 produces a lean wort 313, such as the IBA lean wort 3130, which is fed to the fermentation 3110 of the fermentation subsystem described above, as well as a GIFT condensate 3160. A separation unit 3125, such as the IBA light / light separation unit 3215, receives the GIFT condensate 3160 to produce, among other things, a light IBA phase 3220 that goes to the ion exchange 3225, as well as the heavy phase 3210 received by the column. of fermented must with MVR 3195 described above. The ion exchange 3225 may be upstream or downstream of the drying membranes 3300, such as membranes for IBA 3300.Caustic agents 3230 are added to the ion exchange 3225, and the resulting impurities 3235 are optionally recycled to the fermented wort surge tank 3170. IBA 3240 from the ion exchange 3225 also moves through the membranes of IBA 3300 to create water-rich permeate 3306 which is recycled to the light / light separation of IBA 3215 and the IBA-rich retentate 3305 which is sent to a light column of IBA 3310. The light column of IBA 3310 creates fuel IBA 3315, which can be sent to storage of IBA 3340 before being sent to the HC unit as fuel of IBA 3345. The top of the light column 3320, originating from the light column of IBA 3310, is fed to the anaerobic digester. (DA) 3350 of the water treatment subsystem 3004, described below. The alcohol enrichment subsystem 3006 may include a poor CO2 exhaust collector 3325, which is released to the atmosphere 3335 through a scrubbing column of the exhaust system. Petition 870250080789, dated 09 / 09 / 2025, page 58 / 122 52 / 81 CO2 poor 3330.

[00125] The water treatment subsystem 3004, as described above, receives the bottom of the fermented wort column 3245 from the fermentation subsystem 3003 and the top of the light column 3320 from the alcohol enrichment subsystem 3006, at DA 3350. DA 3350 also uses reject water from the HC unit 3375 and creates raw biogas 3355, reclaimed water 3380 and rejected waste products 3370. The rejects are disposed of, for example, by being sent to wetlands or soil applications. Raw biogas 3355 is sent to the biogas H2S removal unit 3360 in order to generate biogas 3365, which can be sent to the low-pressure (LP) boiler, to the cogeneration unit (CHP), to the DDG dryer, to a combination thereof, or to similar equipment. Reclaimed water 3380 is sent to the recycled water treatment 3385 to create recycle water 3390.

[00126] Figure 12 shows a hydrocarbon production process 4000. The hydrocarbon production process 4000 includes a hydrocarbon production subsystem 4002 and an energy management subsystem 4003. The hydrocarbon production process and system 4000 also provides certain auxiliary components and processes that may or may not be specifically incorporated into the hydrocarbon production subsystem 4002 and the energy management subsystem 4003. The hydrocarbon production process and system 4000 are coupled to the isobutanol process and system 3000 to form part of a carbon-neutral, net-zero energy overall process and plant. The hydrocarbon production subsystem 4002 receives a water supply 4001, which includes recycled water from other subsystems, such as the recycle water 3390 described above, in a hydrogen supply system 4005 to form hydrogen 4010. Furthermore, the IBA Petition 870250080789, dated 09 / 09 / 2025, p. 59 / 122 Fuel grade 4050, which includes IBA from another subsystem, such as fuel grade 3345 IBA described above, undergoes nitrogen removal 4045 to produce IBA 4040. A dehydration unit 4035 receives the IBA 4040 and produces water with hydrocarbons 4055 and intermittent purge of heavy materials 4060 to be sent to the fermented wort surge tank, such as fermented wort surge tank 3170, as described above. The dehydration unit 4035 also produces a feed 4030, such as C4 olefins 4030, for hydrocarbon pretreatment 4025. The hydrocarbon pretreatment derives olefin feed 4020 and wash water 4065, which may optionally be used in various systems described in this application. The olefin feed 4020, together with the hydrogen 4010 described above, are sent to a hydrocarbon processing unit 4015.The hydrocarbon processing unit 4015 produces hydrocarbon wastewater 4120, which is sent to a hydrocarbon oily water separator 4130 to create hydrocarbon reject water 4135 to be sent to the DA 3350 described above. The hydrocarbon processing unit 4015 also produces hydrocarbon exhaust products 4070, which leave the hydrocarbon production subsystem 4002 via a fuel gas system 4075 in order to generate fuel gas 4080, as described below, and the exhaust products may further be directed to a safety valve header (PSV) 4095 and subsequently received in a flare system 4100. In addition, the hydrocarbon processing unit 4015 produces isooctane 4115 and C12-C16 aviation fuel 4110, both of which are sent for hydrocarbon storage and shipping 4125.Isooctane 4140 and C12-C16 aviation fuel 4145 can then be obtained from hydrocarbon storage and shipping 4125. Petition 870250080789, dated 09 / 09 / 2025, page 60 / 122 54 / 81

[00127] The fuel gas system 4075, described above, also supplies fuel gas 4080 to a direct flame heater 4085 and a high-pressure boiler 4090, where fuel gas 400 is used.

[00128] Excess fuel gas 4105 from fuel system 4075, to the extent that there is excess fuel gas, may be supplied to the energy management subsystem 4003 by means of an LPG boiler 4155. The LPG boiler 4155 also absorbs, as needed, renewable natural gas 4150, biogas 4160 from DA 3355, described above, and natural gas 4165 from a utility system, again as needed. A cogeneration unit 4170 receives biogas 4160, natural gas 4165, as needed, and optionally, corn oil from fractionation. The output of the low-pressure boiler (LP) 4175 and the CHP unit 4170 generates low-pressure steam (LP) 4175. The steam collector LP 4170, which may be a steam collector, may receive feed from a biomass boiler / turbine 4195 and an electric boiler 4180, which may use renewable energy sources for its operation.Renewable energy sources include wind power 4190, photovoltaic panels (not shown), or energy generated by the boiler turbine / biomass turbine 4195. The hydrocarbon production process and system 4000 also includes some auxiliary systems and processes. For example, the hydrocarbon production process and system 4000 includes, among other elements, an exhaust gas collection and volatile organic compound (VOC) reduction unit 4210, which receives streams from IBA exhaust 4200 and dryer exhaust 4205. Other components of the hydrocarbon production process and system 4000 include a flammable vapor holding tank 4215, nitrogen 4220, plant and instrument air 4225, raw water treatment 4230, and reverse osmosis water. Petition 870250080789, dated 09 / 09 / 2025, page 61 / 122 55 / 81 reverse (RO) 4235, cooling water 4240, sewage and pumps 4245, a cleaning in situ (CIP) unit 4250, wash water 4255, chemicals 4260 and fire fighting water 4265. The hydrocarbon pretreatment 4025 and the hydrocarbon processing unit 4015 are described in more detail in Figure 13.

[00129] Figure 13 illustrates further details of the hydrocarbon pretreatment and processing unit 4025 and hydrocarbon processing unit 4015 as a hydrocarbon pretreatment and processing scheme 5000, which describes features, processes and structure. Initially, a wash / coalescer water column 5010 receives wash water 5001 and a C4 olefin feed 5005. The wash / coalescer water column 5010 feeds a hydrocarbon wastewater equalization tank or dewatering unit (TBC) 5015 and water and nitrogen adsorbents IBA 5020. The water and nitrogen adsorbents IBA 5020 feed a feed receiver 5025 before combining with a C4 olefin recycle 5045, a debutanizer recycle 5040, and a splitter bottom recycle 5120. Polynaphtha reactors 5030 receive the aforementioned combination and feed the product into a debutanizer 5035.The products of the debutanizer 5035 enter the recycle of the debutanizer 5040 or combine with the recycle of refined C4 for the RVP control 5055, 99.999 mol% H2 compound hydrogen 5060 and recycle of hydrogenated liquid 5080 to enter total hydrogenation reactors 5065.

[00130] The total hydrogenation reactors 5065 feed a separator 5070 which produces a purge from reactor 5075 and a recycle of the hydrogenated liquid 5080, part of which is supplied to the total hydrogenation reactors 5065 (above) and part of which is supplied to the splitter 5085. The purge from reactor 5075, an outlet from the splitter 5085 and the recycle of Petition 870250080789, dated 09 / 09 / 2025, page 62 / 122 56 / 81 C4 olefins 5045 combine to produce a refined C4 product for fuel gas 5050. The output of the separator 5070 not used as hydrogenated liquid recycle 5080 is received by the splitter 5085 which creates a bottom recycle of the splitter 5120, which feeds back into the debutanizer recycle 5040 and feeds the C12-C16 splitter 5090 and isooctane 5110. The C12-C16 splitter 5090 creates a mixture of C12 or aviation fuel 5105 or C12 / C16 aviation fuel 5115. In addition, a first mixture of C12 5095 can be created from isooctane 5110 and the mixture of C12 or jet fuel 5105 and a second mixture of C12 5100 can be created from the mixture of C12 or aviation fuel 5105 and C12 / C16 aviation fuel 5115. ETO with C2 Recycling for fuel products

[00131] Figure 14 is a process and equipment flow diagram 135, which shows equipment, processes, features and functions according to certain aspects of current technology. Referring to Step 1 of Figure 14, ethanol, fusel oils or a combination thereof is fed into the ETO dehydration unit 136. The ETO dehydration unit 136 processes the feed to convert ethanol and / or fusel oils into ethylene and other light olefins. Then, an ethylene distillation tower 137 distills the ethylene. The ethylene is recycled as shown, and the C3 olefins are fed into the aromatics distillation tower 138, although alternatively propylene can be distilled as a chemical and the C4 olefins fed to aromatics distillation 138.Alternatively, all C2 and C4 olefins can be recycled to the ETO 136 dehydration unit to produce propylene with a higher yield, in which case Steps 3 and 4 below would not be present in Figure 14. Ethane is purged from the ethylene recycle stream and used as a low carbon intensity (IC) fuel gas. The process. Petition 870250080789, dated 09 / 09 / 2025, page 63 / 122 57 / 81 ETO inherently maximizes thermal efficiency and reduces the energy requirements of auxiliary systems by combining dehydration (endothermic) and conversion to light olefins (exothermic) in a single unit process, thus reducing the total energy requirement compared to a conventional two-step process of ethanol dehydration to ethylene, followed by ethylene dimerization to butenes. This, combined with the high exothermicity of hydrogenation, results in a net thermal energy surplus with low CI for the ETJ process, which can be used to meet part of the thermal energy demand of ethanol production and replace the use of natural gas.

[00132] In Step 2 of Figure 14, aromatics and heavy olefins are removed from the light olefins stream as a purification step prior to oligomerization. The aromatics stream is then marketed as a base blend for gasoline, and the top stream from the aromatics distillation, composed mainly of C3+ olefins, is fed into an oligomerization unit 139.

[00133] In Step 3 of Figure 14, C3+ olefins are fed into the oligomerization unit 139 and converted mainly into C6+ olefins by a column reactor 140. The light olefins in the effluent stream from the column reactor 140 are recycled and the C6+ olefins are fed into a hydrogenation unit 141. A split tower 142 purges light paraffins from the recycle stream and uses them as low IC fuel gas. Optionally, to increase the octane rating of the gasoline product, linear butenes can be separated before oligomerization and isomerized into isobutene and then fed for oligomerization or dimerized separately into iso-octene.

[00134] In Step 4 of Figure 14, mixed olefins are fed into hydrogenation 141 along with hydrogen and converted into paraffins. Petition 870250080789, dated 09 / 09 / 2025, page 64 / 122 58 / 81 Hydrogen is produced by electrolysis powered by electricity generated by wind turbines and / or solar panels. Split tower 142 purges light paraffins and excess hydrogen from the recycle stream and uses it as a low IC fuel gas. The paraffin mixture is split by distillation in split tower 142 into light fuels, gasoline, sustainable aviation fuel (SAF), and diesel products. This separation can occur before hydrogenation if certain olefinic products are desired.

[00135] System-wide measures to further reduce the system's IC score include: using electricity produced by wind turbines and / or solar panels, using surplus thermal energy and / or fuel gas produced for upstream process heating and / or utilities. Ethanol Specification for HC in the ETJ NZ1 Process

[00136] HC ethanol was developed to reduce the production costs of pure ethanol to feed the HC unit. The process requires an additional 2 to 3 distillation columns (approximately US$10 to 20 million) and approximately 3,000 to 4,000 BTU / gal of ethanol.

[00137] The process allows for the removal of dehydration and energy equipment.

[00138] The appropriate ethanol concentration (e.g., containing a minimum of about 85% by weight, 86% by weight, 87% by weight, 88% by weight, 89% by weight, or 90% by weight ethanol content and a maximum of about 10% by weight, 11% by weight, 12% by weight, 13% by weight, 14% by weight, or 15% by weight water content) was developed through testing to find the most energy-efficient concentration for the HC plant and to allow the removal of contaminants that would create catalyst lifespan and product quality problems, such as: i. Lower level of contaminants to prevent formation Petition 870250080789, dated 09 / 09 / 2025, page 65 / 122 59 / 81 of acids in the HC process, which would lead to serious corrosion problems or require more expensive metallurgy (costing 2 to 3 times more), ii. Lower level of contaminants to avoid loss of catalyst activity, iii. Lower level of contaminants to form byproducts that would cause loss of catalyst activity and possible product quality problems, and iv. This includes choosing the correct ethanol concentration to avoid nitrogen concentrations in the ethanol that would damage the catalyst; a. The concentration of water affects the levels of contaminants in ethanol.

[00139] In addition, pure ethanol increases the IC. ETO with C2 dimerization for fuel products

[00140] Figure 15 is a process and equipment flow diagram 145, showing equipment, processes, features and functions according to certain aspects of current technology. Referring to Step 1 of Figure 15, ethanol is fed to an ETO dehydration unit 146 which converts ethanol, fusel oils or a combination thereof into ethylene and other light olefins. An ethylene distillation tower 147 distills the ethylene that fed the dimerization unit 148 while the C3 olefins are fed into the aromatics distillation unit 149, although alternatively propylene could be distilled as a chemical and the C4 olefins fed to the aromatics distillation. Ethane is purged from the distilled ethylene stream and used as a low IC fuel gas.The ETO process inherently maximizes thermal efficiency and reduces the energy requirements of auxiliary systems by combining dehydration (endothermic) and conversion into light olefins. Petition 870250080789, dated 09 / 09 / 2025, page 66 / 122 60 / 81 (exothermic) in a single unit process, thus reducing the total energy requirement compared to a conventional two-stage process of ethanol dehydration to ethylene, followed by ethylene dimerization to butenes. This, combined with the high exothermicity of hydrogenation, results in a net thermal energy surplus of low CI for the ETJ process, which can be used to meet part of the thermal energy demand of ethanol production and replace the use of natural gas.

[00141] In Step 2 of Figure 15, the distilled ethylene stream is fed into dimerization unit 148 and converted primarily into C4 olefins. The light paraffins are purged and used as low IC fuel gas. The C4 olefin stream is distilled and an oligomerization unit 150 receives the C4 olefin stream. The C8+ stream is fed directly into a hydrogenation unit 151 with the lighter C6 olefin stream from oligomerization unit 150. The C4 olefins are combined with the C3 olefins described below.

[00142] In Step 3 of Figure 15, the C3 olefins from the ethylene distillation tower 147 are distilled by the aromatics distillation tower 149. The heavy olefins are removed from the light olefins stream in this step. The aromatics distillation tower 149 feeds the light olefins stream, which is available as a gasoline mixture, composed mainly of C3 olefins, which are fed into the oligomerization unit 150 along with the C4 olefins described above.

[00143] In Step 4 of Figure 15, C3 olefins from the aromatic distillation tower 149 and olefins from the dimerization unit 148 are fed into the oligomerization unit 150 and converted mainly into C6 olefins by the reactor tower 152. The light olefins in the stream from reactor tower 152 are recycled and C6 olefins are there Petition 870250080789, dated 09 / 09 / 2025, page 67 / 122 61 / 81 are treated in a hydrogenation unit 151. The splitting tower 153 receives the output from the hydrogenation unit 151 and the light paraffins are purged from the recycle stream and used as low IC fuel gas. Optionally, to increase the octane rating of the gasoline product, the linear butenes can be separated before oligomerization and isomerized to isobutene and then fed for oligomerization or dimerized separately to iso-octene.

[00144] In Step 5 of Figure 15, mixed olefins are fed into hydrogenation unit 151 along with hydrogen and converted into paraffins. Hydrogen can be produced by electrolysis powered by electricity generated by wind turbines and / or solar panels. Light paraffins and excess hydrogen are purged from the recycle stream by splitting tower 153 and used as low IC fuel gas. The paraffin mixture is also separated by splitting tower 153 into light, gasoline, SAF, and diesel. This separation can occur before hydrogenation if certain olefin products are desired.

[00145] System-wide measures to further reduce the system's IC score include: using electricity produced by wind turbines and / or solar panels, using surplus thermal energy and / or fuel gas produced for upstream process heating and / or utilities. Dehydration of ethanol and alkylation with solid acid to obtain an alkylate product.

[00146] Figure 16 is a process and equipment flow diagram 155, which shows equipment, processes, resources and functions according to certain aspects of current technology. Referring to Step 1 of Figure 16, ethanol, fusel oils or a combination thereof may be fed to a first dehydration unit 156 to convert the ethanol, fusel oils or the combination into Petition 870250080789, dated 09 / 09 / 2025, page 68 / 122 62 / 81 ethylene and other light olefins, such as C2 olefins. Simultaneously, isobutanol is fed into a second dehydration unit 157 which emits an olefin stream that an aromatic distillation tower 158 receives to produce isobutylene. A hydrogenation unit 159 produces isobutane where C2 light olefins from the first dehydration unit 156 and isobutane are combined. An alkylation unit 160 receives C2 light olefins and isobutane. The stream of C2+ light olefins and isobutane is available as a base blend for gasoline, and the top stream from the aromatic distillation, composed mainly of C2+ olefins, is fed into an alkylation unit 160.

[00147] In Step 2 of Figure 16, isobutane is produced from the low IC isobutanol (IBA) production described in this application, followed by dehydration to isoethylene and then hydrogenation to isobutane. It is important to note that renewable isobutane can also be produced from a variety of feedstocks, including ethanol. Alternatively, fossil-derived isobutane can be used, although it typically has a higher IC score.

[00148] In Step 3 of Figure 16, the alkylation unit 160 produces alkylated gasoline product. A final distillation tower 161 separates the light paraffins from the alkylated gasoline. The light paraffins are purged and used as low IC fuel gas, and the isobutane is recycled in the process.

[00149] System-wide measures to further reduce the system's IC score include: using electricity produced by wind turbines and / or solar panels, using surplus thermal energy and / or fuel gas produced for upstream process heating and / or utilities. ETO with alkylation by liquid acid or ionic liquid to obtain an alkylate product. Petition 870250080789, dated 09 / 09 / 2025, page 69 / 122 63 / 81

[00150] Figure 17 is a process and equipment flow diagram 165, which shows equipment, processes, features and functions according to certain aspects of current technology. Referring to Step 1 of Figure 17, ethanol, fusel oils or a combination thereof are fed into the ETO dehydration unit 166 which converts ethanol, fusel oils or a combination into ethylene and other light olefins. An ethylene distillation tower 167 distills the output of the ETO dehydration unit 16 to ethylene and C3 olefins. A first aromatic distillation tower 168 receives the C3 olefins. Optionally, the ethylene can be dimerized into butenes predominantly and mixed with the C3 olefins stream after the first aromatic distillation tower 168.

[00151] In Step 2 of Figure 17, the first aromatic distillation tower 168 removes aromatics and heavy olefins from the light olefin stream, such as C3 olefin vapor. The aromatic stream is available as a base blend for gasoline, and the top stream from the aromatic distillation, composed mainly of C3+ olefins, is fed into an alkylation unit 169, as described below.

[00152] In Step 3 of Figure 17, isobutane is produced from the low IC IBA production described in this application and is received by an isobutanol dehydration unit 170. A second aromatic distillation tower 171 produces isobutene which is received by a hydrogenation unit 172 to produce isobutane. It is important to note that renewable isobutane can also be produced from a variety of feedstocks, including ethanol. Alternatively, fossil-derived isobutane can be used, although it typically has a higher IC score.

[00153] In Step 4 of Figure 17, C3 olefins (light olefins from aromatic distillation tower 168) are combined with isobutane from Petition 870250080789, dated 09 / 09 / 2025, p. 70 / 122 64 / 81 hydrogenation unit 172 and an alkylation unit 169 receive the combination to produce an alkylated gasoline product. A reactor tower 173 produces light paraffins, which are purged and used as low IC fuel gas, and isobutane is recycled in the process. Reactor tower 173 also produces alkylated gasoline.

[00154] System-wide measures to further reduce the system's IC score include: using electricity produced by wind turbines and / or solar panels, using surplus thermal energy and / or fuel gas produced for upstream process heating and / or utilities. High-Octane Gasoline and Aviation Fuel Fractions

[00155] Bio-based ethanol can be converted to ethylene and subsequently to C3-C8 olefin blends in a single step. The resulting C3-C8 olefins, linear butenes and / or fractions thereof, can be cooligomerized with isobutylene derived from bio-based isobutanol in proportions that increase branching to such an extent that blends of high-octane fractions and aviation fuel are maximized. While it is well known that increased branching results in higher octane fuels, it was surprising to find that the addition of large amounts of isobutylene resulted in significantly higher octane values ​​compared to simply blending more branched paraffinic compounds after oligomerization. Figure 18 illustrates the increase in octane as a result of cooligomerization of isobutylene with linear butenes versus iso-octane blending.

[00156] Thus, the oligomerization of mixtures of isobutylene and / or linear butenes, derived from isobutanol and ethanol, respectively, results in gasoline and aviation fuel fractions with higher octane ratings compared to the oligomerization of linear butenes followed by the addition of iso-octane to increase the octane values. Petition 870250080789, dated 09 / 09 / 2025, page 71 / 122 65 / 81 octane rating. Furthermore, parallel, or colocalized, fermentation of isobutanol and ethanol results in surprising synergies and cost savings in terms of reduced nutrients, dilution of toxic impurities, and energy savings. The exemplary oligomerization reaction step involves the oligomerization of a mixture of isobutylene and a linear olefin stream over appropriate acid catalysts between 80 °C and 260 °C and pressures between 250 psig and 500 psig.

[00157] Single-stage oligomerization conditions: T=175 °C in the reactor, WHSV = 1.7, Feed: 14% isobutylene, 55% linear butenes (n-butene, cis / trans-2-butene), 31% pentene mixture; P=250 psig; Catalyst mixture: Tungsten Zirconia + Zeolite ZSM5 (Si / Al=55).

[00158] The selectivity of the oligomers is shown in Table 4. Table 4. % C4 % C5C7 % C8 % C9C11 % C12 % C13C15 % C16 % C20 % C24 WZr+5524_50iC4, 50nC4 + C5's; 175C; 250psi; T = 0 to 1h40' 17.25 7.95 25.26 7.93 22.17 4.09 9.56 3.65 2.14 WZr+5524_50iC4, 50nC4 + C5's; 175C; 250 psi; T = 1h40' to 2h40' 9.79 9.21 21.21 10.07 22.80 5.53 13.26 5.14 2.99 WZr+5524_50iC4, 50nC4 + C5's; 175C; 250 psi; T = 6h2' to 21h10' 18.41 9.53 24.15 9.57 21.71 4.69 8.78 2.38 0.78 WZr+5524_50iC4, 50nC4 + C5's; 175°C; 250 psi; T = 21:10' to 22:10' 15.58 9.24 27.05 9.99 23.88 4.75 7.39 1.69 0.44

[00159] Isobutylene / C4 linear + C5 linear ratio = 0.16.

[00160] Actual RON measurement of hydrogenated C8 fraction = 96.6.

[00161] Without isobutylene; linear C4 + linear C5 oligomerization. Petition 870250080789, dated 09 / 09 / 2025, page 72 / 122 66 / 81

[00162] Actual RON measurement of hydrogenated C8 fraction = 72.7.

[00163] The specific examples given in this application are intended to be illustrative and should not be construed as limiting the scope of the claims.

[00164] The above detailed description was provided for clarity of understanding only, and no unnecessary limitations should be inferred from it, as modifications will be obvious to those skilled in the art.

[00165] Although described in connection with its specific embodiments, it should be understood that the principles described in this application are capable of further modifications and this application is intended to cover any variations, uses or adaptations following, in general, the principles described in this application and including such deviations from the present invention as they fall within known or customary practice within the art to which the technology belongs and as they may be applied to the essential features set forth above and as follows within the scope of the appended claims.

[00166] The disclosures, including the claims, figures and / or drawings, of each patent, patent application and publication cited in this application are incorporated by reference in their entirety. Exemplary Aspects / Modalities

[00167] Certain aspects, including embodiments / aspects of the present subject described above, may be beneficial alone or in combination with one or more aspects described below. Furthermore, although the present subject has been described with reference to certain aspects cited below and in the claims, numerous modifications, alterations, and changes to the described aspects / embodiments are possible without departing from the scope and sphere of the present invention. Consequently, it is intended that the present invention is not limited to the embodiments, aspects, and claims described, but Petition 870250080789, dated 09 / 09 / 2025, p. 73 / 122 67 / 81 having the full scope defined by the language of the present invention and equivalents thereof. Although the present technology has been described with reference to its specific aspects / embodiments, it should be understood by those skilled in the art that various alterations may be made and equivalents may be substituted without departing from the true spirit and scope of the description. Furthermore, many modifications may be made to adapt a specific situation, material, composition of matter, process and / or step or steps of the process, to the objective, spirit and scope of the present invention. All such modifications must be within the scope of the appended claims.

[00168] Below are some examples of aspects of current technology.

[00169] 1. A system for the production of renewable hydrocarbons, comprising: a fractionation subsystem for processing biomass containing a carbohydrate; a fermentation subsystem to convert carbohydrate into a fermentation product; an alcohol enrichment subsystem to receive a second portion of the fermentation product; A hydrocarbon production subsystem to receive alcohol and produce renewable hydrocarbons; an energy management subsystem to receive the fuel stream from the system and supply energy to the system; and further comprising at least one of the following to reduce the energy demand or IC of ethanol and / or fuels: a) a water treatment subsystem to receive an initial portion of the fermentation product; b) combustion of light oxygenates, fusel oil, Petition 870250080789, dated 09 / 09 / 2025, page 74 / 122 68 / 81 vegetable oil, biomass or derivatives and / or hydrocarbon by-products; c) use of hot water sources and waste heat from fermentation and hydrocarbon production systems for biomass processing at moderate temperatures; d) utilize an alcohol purification system that employs a mechanical vapor recompression (MVR) system to pressurize the top vapors of the rectifier column, whose condensation provides heat to the reboiler of the fermented wort column, in addition to producing purified alcohol suitable for conversion into hydrocarbons; and (e) a fine vinasse evaporation system that utilizes heat from a partially condensed ethanol stream from the top vapors of the rectifier column, as well as from the MVR system, to produce a syrup with a dry solids content of at least about 35% to about 45%, without any additional application of steam.

[00170] 2. The system of aspect 1, in which the fractionation subsystem also comprises at least one of the following: a storage container for storing biomass; a shredder for breaking up biomass; a pre-treatment container for pre-treating biomass; a treatment vessel for processing the biomass to produce the carbohydrate; and a high-temperature short-time (HTST) vessel for pasteurizing the carbohydrate. Petition 870250080789, dated 09 / 09 / 2025, page 75 / 122 69 / 81

[00171] 3. The system in aspect 2, where the biomass is corn.

[00172] 4. The system in aspect 2, where biomass has a negative carbon footprint.

[00173] 5. The system in aspect 2, in which biomass is cultivated using strip tillage or no-till farming.

[00174] 6. The system in aspect 2, where the crusher is a mill.

[00175] 7. The system in aspect 2, where the pretreatment tank includes a recycled water inlet.

[00176] 8. The system of aspect 2, in which the biomass pretreatment includes pretreatment of the biomass with an enzyme.

[00177] 9. The system of aspect 2, in which the treatment vessel includes an outlet for non-fermentable solids.

[00178] 10. The system of aspect 9, in which the output of non-fermentable solids includes the output of dried distillery grains and / or the output of corn oil.

[00179] 11. The system of any of the above aspects, in which the fermentation subsystem comprises at least one of the following: a fermenter to convert the carbohydrate into the fermentation product; a nutrient addition subsystem; a pH adjustment subsystem; and an inoculum propagation subsystem.

[00180] 12. The system of aspect 11, where the fermenter is a continuous fermenter.

[00181] 13. The system of aspect 11, in which the fermentation product includes an alcohol.

[00182] 14. The system of aspect 13, in which the alcohol is isobutyric. Petition 870250080789, dated 09 / 09 / 2025, page 76 / 122 70 / 81 ethanol.

[00183] 15. The system of aspect 11, in which the inoculum propagation subsystem is configured to supply a microorganism to the fermenter.

[00184] 16. The system of aspect 15, in which the microorganism is yeast.

[00185] 17. The system of any of the above aspects, in which the water treatment subsystem comprises at least one of the following: a fermented wort surge tank to receive the first portion of the fermentation product; a device for separating microorganisms to remove microorganisms from the first portion of the fermentation product; a first distillation column to separate the first portion of the fermentation product into an alcohol and a bottom product; a digester to receive a portion of the bottom product and to produce biogas; and a biogas removal subsystem to remove a pollutant from the biogas.

[00186] 18. The system of aspect 17, in which the first portion of the fermentation product includes an alcohol.

[00187] 19. The aspect ratio 17 system, in which the first portion of the fermentation product includes isobutanol.

[00188] 20. The aspect 17 system, in which the first portion of the fermentation product includes water.

[00189] 21. The system of aspect 17, in which the microorganism separation device includes a centrifuge.

[00190] 22. The system of aspect 17, in which the device of Petition 870250080789, dated 09 / 09 / 2025, p. 77 / 122 71 / 81 separation of microorganisms includes a filter.

[00191] 23. The system of aspect 17, in which the microorganism separation device includes a settling tank.

[00192] 24. The system of aspect 17, in which the microorganisms are yeasts.

[00193] 25. The system of aspect 17, in which the first distillation column includes a vapor recompression subsystem.

[00194] 26. The system of aspect 17, in which the first distillation column includes mechanical vapor recompression (MVR).

[00195] 27. The system of aspect 17, in which the first distillation column includes thermal vapor recompression (TVR).

[00196] 28. The system of aspect 17, in which the inferior product includes vinasse.

[00197] 29. The system of aspect 17, in which the digester is an anaerobic digester.

[00198] 30. The system of aspect 17, in which the digester is a continuous digester.

[00199] 31. The system of aspect 17, in which the biogas removal subsystem includes a scrubbing column.

[00200] 32. The system of aspect 17, in which the pollutant is hydrogen sulfide.

[00201] 33. The system of any of the preceding aspects, in which the alcohol enrichment subsystem comprises at least one of the following: a flash tank to separate condensate from the second portion of the fermentation product; a separating vessel to separate the condensate into a light phase and a heavy phase; an ion exchange vessel for purifying the light phase; a membrane separator to separate the light phase into Petition 870250080789, dated 09 / 09 / 2025, page 78 / 122 72 / 81 an alcohol-rich retentate and a water-rich permeate; a second distillation column to separate the water from the high-alcohol retentate; and a container for storing alcohol.

[00202] 34. The system of aspect 33, in which the flash tank receives the second portion of the fermentation product from the fermentation subsystem and returns part of the second portion of the fermentation product to the fermentation subsystem.

[00203] 35. The system of aspect 33, in which the second portion of the fermentation product is a broth and a broth poor in isobutanol is returned to the fermentation subsystem.

[00204] 36. The system of aspect 33, in which the flash tank operates at atmospheric pressure.

[00205] 37. The system of aspect 33, in which the flash tank operates under vacuum at a reduced pressure below atmospheric pressure.

[00206] 38. The system of aspect 33, in which the flash tank operates at a temperature below the temperature of the second portion of the fermentation product received from the fermentation subsystem.

[00207] 39. The system of aspect 33, in which the separation vessel is a liquid / liquid separator to separate the condensate into the light phase and the heavy phase.

[00208] 40. The aspect 39 system, in which the light phase contains a greater quantity of alcohol than the heavy phase.

[00209] 41. The system of aspect 40, in which the alcohol is isobutanol and the liquid / liquid separator forms a two-phase system.

[00210] 42. The system of aspect 33, in which the ion exchange vessel contains an ion exchange resin and receives the light phase received from the separation vessel and removes impurities from the light phase by trapping ions in the ion exchange resin. Petition 870250080789, dated 09 / 09 / 2025, page 79 / 122 73 / 81

[00211] 43. The system of aspect 42, in which the ion exchange vessel receives a caustic solution to regenerate the ion exchange resin by discharging impurities into a fermented wort surge tank.

[00212] 44. The system of aspect 33, in which the hydrocarbon production subsystem comprises at least one of the following: a denitrogenation subsystem to separate nitrogen from alcohol; a dehydration subsystem to convert the alcohol into an olefin; a hydrocarbon pretreatment subsystem for conditioning an olefin feed; a hydrogen supply subsystem to provide hydrogen; and a hydrocarbon processing subsystem to convert the olefin feed into at least an isooctane fraction, a C12 alkane fraction and / or a C16 alkane fraction.

[00213] 45. The system of aspect 44, in which the hydrocarbon production subsystem further comprises at least one of the following: an oil-water separator to separate wastewater from the hydrocarbon processing subsystem; and a hydrocarbon storage vessel to store at least one of the following iso-octane: C12 blend, or C16 blend from the hydrocarbon processing subsystem.

[00214] 46. The aspect ratio 44 system, in which the denitrogenation subsystem receives alcohol from the alcohol enrichment subsystem. Petition 870250080789, dated 09 / 09 / 2025, p. 80 / 122 74 / 81

[00215] 47. The system of aspect 46, where the alcohol is a fuel-grade isobutanol.

[00216] 48. The system of aspect 44, in which the dehydration subsystem receives alcohol from the denitrogenation subsystem and sends water and / or purge products to a fermented wort surge tank.

[00217] 49. The aspect ratio system 44, where the olefin is a four-carbon olefin.

[00218] 50. The aspect 44 system, wherein the hydrocarbon pretreatment subsystem comprises at least one of the following: a coalescer to receive the olefin from the dehydration subsystem; an adsorbent to remove unreacted alcohols, water, and nitrogen; and a feed receptor.

[00219] 51. The system of aspect 50, in which the coalescer also receives wash water and sends wastewater to an equalization tank and / or a dewatering unit.

[00220] 52. The system of aspect 50, in which the coalescer also receives wash water and sends wastewater to an equalization tank and / or a dewatering unit.

[00221] 53. The aspect 50 system, where the olefin is a C4 olefin.

[00222] 54. The aspect ratio 50 system, in which the unreacted alcohol is isobutanol.

[00223] 55. The system of aspect 50, in which the feed receptor receives the olefin from the adsorber.

[00224] 56. The aspect 44 system, in which the hydrocarbon processing subsystem comprises at least one of Petition 870250080789, dated 09 / 09 / 2025, p. 81 / 122 75 / 81 following: a first reactor; a debutante; a second reactor; a separator; a first divisor; and / or a second divisor.

[00225] 57. The system with aspect 56, where the first reactor is a polynaphtha reactor.

[00226] 58. The system of aspect 56, in which the first reactor receives the olefin from the feed receiver and oligomerizes the olefin into a polyolefin.

[00227] 59. The system of aspect 56, in which the debutanizer receives a polyolefin from the first reactor.

[00228] 60. The aspect ratio 56 system, in which the debutanizer recycles an unreacted olefin and / or paraffin to the first reactor.

[00229] 61. The system with aspect ratio 56, where the second reactor is a hydrogenation reactor.

[00230] 62. The aspect ratio 56 system, in which the second reactor receives a polyolefin from the debutanizer.

[00231] 63. The system of aspect 56, in which the second reactor also receives hydrogen from a hydrogen supply subsystem and hydrogenates the polyolefin to a C8-C16 alkane.

[00232] 64. The system of aspect 56, in which the separator removes an unreacted olefin and / or paraffin from the C8-C16 alkane.

[00233] 65. The aspect ratio 64 system, in which unreacted olefins and / or paraffins include C4 products.

[00234] 66. The aspect ratio system 56, in which the separator recycles a portion of the C8-C16 alkane to the second reactor.

[00235] 67. The aspect ratio system 56, in which the first divisor Petition 870250080789, dated 09 / 09 / 2025, p. 82 / 122 76 / 81 separates the iso-octane fraction from the C8-C16 alkane.

[00236] 68. The system of aspect 67, wherein the isooctane fraction comprises about 85%, 90%, 91%, 92%, 93%, 94%, 95%, 96%, 97%, 98%, 99% or 100% by weight of C8 alkanes, about 1%, 2%, 3%, 4% or 5% by volume of olefins and / or about 2 ppm, 4 ppm, 6 ppm, 8 ppm or 10 ppm of sulfur.

[00237] 68. The aspect ratio 67 system, in which the isooctane fraction comprises more than 95% by weight of C8 alkanes, less than 5% by volume of olefins and / or less than 10 ppm of sulfur.

[00238] 70. The aspect ratio 56 system, in which the first divider separates an unreacted olefin and / or paraffin from the C8-C16 alkane.

[00239] 71. The aspect ratio 70 system, in which unreacted olefins and / or paraffins include C4 products.

[00240] 72. The aspect ratio 56 system, in which the second divisor separates the C12 alkane fraction from the C18 alkane fraction.

[00241] 73. The system of any of the above aspects, in which the energy management subsystem comprises at least one of the following: a fuel gas system for distributing fuel gas received from the hydrocarbon processing subsystem; a low-pressure boiler for steam generation; a high-pressure boiler for steam generation; a combined heat and power unit for generating steam and electricity; a wind turbine for generating electricity; an electric boiler to receive renewable electricity and heat water to produce steam; a biomass boiler for burning biomass to heat water and produce steam; and / or Petition 870250080789, dated 09 / 09 / 2025, page 83 / 122 77 / 81 a steam turbine to generate electricity.

[00242] 74. The system of aspect 73, in which the fuel gas system supplies fuel gas to the low-pressure boiler.

[00243] 75. The system of aspect 73, in which the fuel gas system supplies fuel gas to the high-pressure boiler.

[00244] 76. The system of aspect 73, in which the fuel gas system supplies fuel gas to a direct flame heater.

[00245] 77. The system in aspect 73, in which the low-pressure boiler is further configured to receive natural gas and / or biogas from an anaerobic digester.

[00246] 78. The system of aspect 73, in which the combined heat and power unit is further configured to receive natural gas and / or biogas from an anaerobic digester.

[00247] 79. A system for the production of renewable alcohols, comprising: a fractionation subsystem for processing biomass containing a carbohydrate; a fermentation subsystem to convert carbohydrate into a fermentation product; an alcohol enrichment subsystem to receive at least a portion of the fermentation product; an energy management subsystem to receive the fuel stream from the system and supply power to the system; and at least one of the following to reduce the energy demand or IC of the alcohol: a) a water treatment subsystem to receive an initial portion of the fermentation product; b) combustion of light oxygenates, fusel oil, vegetable oil, biomass or derivatives and / or co-products; Petition 870250080789, dated 09 / 09 / 2025, page 84 / 122 78 / 81 c) to use an alcohol purification system that employs a mechanical vapor recompression system to pressurize the top vapors of the rectifier column, whose condensation provides heat to the reboiler of the fermented wort column; and (d) a fine vinasse evaporation system that utilizes heat from a partially condensed ethanol stream from the top vapors of the rectifier column, as well as from the mechanical vapor recompression system, to produce a syrup with a dry solids content of at least about 35% to about 45%, without any additional application of steam.

[00248] 80. A process for producing renewable transport fuels, such as gasoline, aviation kerosene and diesel oil, from renewable C1-C5 alcohols, comprising: a) conversion of C1-C5 alcohols to a mixture of C2-C7 olefins to generate stream A; b) optional separation of a predominantly C2 olefin fraction from stream A for recycling in the alcohol conversion step to create or separate oligomerization conversion to generate a predominantly C4+ B stream; c. optional purification of stream A and / or stream B and combining to create a stream C suitable for oligomerization into fuel-grade olefins; d. oligomerization of the C stream into fuel band olefins to create a D stream; e. optional hydrogenation of the D stream to create a predominantly paraffinic E stream; and f. separation of the E stream into fractions suitable for use as gasoline, aviation fuel, and diesel.

[00249] 81. The process of aspect 80 comprising the separation Petition 870250080789, dated 09 / 09 / 2025, page 85 / 122 79 / 81 ration of a predominantly C2 olefin fraction from stream A for recycling in the alcohol conversion step to create or separate oligomerization conversion to generate a predominantly C4+ stream B.

[00250] 82. The process of aspect 80 comprises the purification of stream A and / or stream B and the combination to create a stream C suitable for oligomerization into fuel range olefins.

[00251] 83. The process of aspect 80 comprising the hydrogenation of stream D to create a predominantly paraffinic stream E.

[00252] 84. Process for producing a renewable alkylate from C1-C5 renewable alcohols, characterized by comprising: a) conversion of C1-C5 alcohols to a mixture of C2-C7 olefins to generate stream A; b) optional separation of a predominantly C2 olefin fraction from stream A for recycling in the alcohol conversion step to create or separate oligomerization conversion to generate a predominantly C4+ B stream; c) optional purification of stream A and / or stream B and combination with renewable or petrochemical isobutane to create a stream C suitable for alkylation; d) subjecting stream C to an alkylation process to produce a crude renewable alkylate stream D; and (e) Optional purification of the D stream so that it is suitable for direct use as renewable gasoline.

[00253] 85. The process of aspect 84 comprises separating a predominantly C2 olefin fraction from stream A for recycling in the alcohol conversion step to create or separate the oligomerization conversion to generate a predominantly olefin C2 stream. Petition 870250080789, dated 09 / 09 / 2025, page 86 / 122 80 / 81 te C4+ B.

[00254] 86. The process of aspect 84 comprising optional purification of stream A and / or stream B and combination with renewable or petrochemical isobutane to create a stream C suitable for alkylation.

[00255] 87. The process in aspect 84 comprises purifying the D stream so that it is suitable for direct use as renewable gasoline.

[00256] 88. Process for converting ethanol of biological origin into higher octane gasoline and aviation fuel fractions, characterized by comprising: a) conversion of ethanol into ethylene and subsequently into C3-C8 olefin mixtures in a single step; and b) C3-C8 olefins, linear butenes and / or fractions thereof are cooligomerized with isobutylene, thereby increasing branching and providing gasoline and aviation fuel fractions with higher octane ratings.

[00257] 89. The process of aspect 88, in which isobutylene is cooligomerized with linear butenes.

[00258] 90. The process of aspect 88, in which a mixture of isobutylene and a linear olefin are cooligomerized with one or more suitable acid catalysts at a temperature between 80 °C and 260 °C and under pressures between 250 and 500 psig.

[00259] 91. The process of aspect 90, in which mixtures of isobutylene and linear butenes are derived from isobutanol and ethanol, respectively.

[00260] 92. The process of aspect 90, in which the catalysts are selected from a group consisting of: tungsten zirconia catalysts, nickel- and / or cobalt-doped tungsten zirconia catalysts, zeolites or metal-doped zeolites from Groups Petition 870250080789, dated 09 / 09 / 2025, p. 87 / 122 81 / 81 pos IB to VIIB, and / or any combination thereof.

[00261] 93. The process of aspect 90, in which the catalysts are a mixture of catalysts comprising: Zirconia Tungstate + Zeolite ZSM5 (Si / Al=55).

[00262] 94. The process of aspect 88, in which oligomerization is carried out under conditions of T=175 °C in a reactor, WHSV = 1.7, with 14% isobutylene, 55% linear butenes (n-butene, cis / trans2-butene), 31% pentene mixture and under a pressure of about 250 psig.

[00263] 95. The process of any of claims 80 or 88, wherein the alcohols comprise a minimum of about 85% by weight to 90% by weight of ethanol content and a maximum of 10% by weight to 15% by weight of water content.

[00264] 96. The process of claim 95, wherein the alcohols comprise a minimum of about 85% by weight, 86% by weight, 87% by weight, 88% by weight, 89% by weight or 90% by weight of ethanol content.

[00265] 97. The process of claim 95 or 96, wherein the alcohols comprise a maximum of about 10% by weight, 11% by weight, 12% by weight, 13% by weight, 14% by weight or 15% by weight of water content.

[00266] 98. The process of any of the claims 80 or 88, wherein the alcohols comprise a minimum of about 88% by weight of ethanol content and a maximum of 12% by weight of water content. Petition 870250080789, dated 09 / 09 / 2025, p. 88 / 122

Claims

1 / 3 CLAIMS 1. Process for producing renewable transportation fuels from renewable C1-C5 alcohols, characterized by comprising: a. converting C1-C5 alcohols to a mixture of C2-C7 olefins to generate stream A; b. optionally separating a predominantly C2 olefin fraction from stream A for recycling in an alcohol conversion step to create or separating the oligomerization conversion to generate a predominantly C4+ stream B; c. optionally purifying stream A and / or stream B and combining the purified stream A and / or stream B to create a stream C suitable for oligomerization into fuel band olefins; d. oligomerizing stream C into fuel band olefins to create a stream D; e. optionally hydrogenating stream D to create a predominantly paraffinic stream E; and f. separating stream E into fractions suitable for use as transportation fuels.

2. Process, according to claim 1, characterized by comprising the optional separation of a predominantly C2 olefin fraction from stream A for recycling in the alcohol conversion step to create or separating the oligomerization conversion to generate a predominantly C4+ stream B.

3. Process according to claim 1, characterized by comprising the purification of stream A and / or stream B and the combination to create a stream C suitable for oligomerization into fuel range olefins.

4. Process, according to claim 1, characterized by comprising the hydrogenation stream D to create a predominantly paraffin stream E.

5. Process for producing a renewable alkylate from C1-C5 renewable alcohols, characterized by comprising: a. converting C1-C5 alcohols to a mixture of C2-C7 olefins to generate stream A; b. optionally separating a predominantly C2 olefin fraction from stream A for recycling in the alcohol conversion step to create or separating the oligomerization conversion to generate a predominantly C4 + B stream; c. purifying stream A and / or stream B and combining it with renewable or petrochemical isobutane to create a stream C suitable for alkylation; d. subjecting stream C to an alkylation process to produce a crude renewable alkyl stream D; and e. optionally purifying stream D so that it is suitable for direct use as renewable gasoline.

6. Process according to claim 5, characterized by comprising the optional separation of a predominantly C2 olefin fraction from stream A for recycling in the alcohol conversion step to create or separating the oligomerization conversion to generate a predominantly C4+ stream B.

7. Process according to claim 5, characterized by comprising optional purification of stream A and / or stream B and combination with renewable or petrochemical isobutane to create a stream C suitable for alkylation.

8. Process, according to claim 5, characterized by comprising the purification of stream D so that it is suitable for direct use as renewable gasoline.

9. Process for converting ethanol of biological origin (Petition 870250080789, dated 09 / 09 / 2025, page 90 / 122 3 / 3) into higher octane gasoline and aviation fuel fractions, characterized by comprising: a. converting ethanol into ethylene and subsequently into C3-C8 olefin mixtures in a single step; and b. C3-C8 olefins, linear butenes and / or fractions thereof are cooligomerized with isobutylene, thus increasing branching and providing higher octane gasoline and aviation fuel fractions.

10. Process according to claim 9, characterized by comprising the oligomerization being carried out under conditions of T=175 °C in a reactor, WHSV = 1.7, with 14% isobutylene, 55% linear butenes (n-butene, cis / trans-2-butene), 31% pentene mixture and under a pressure of about 250 psig.

11. Process, according to claim 1, 5 or 9, characterized by comprising alcohols comprising a minimum of about 85% by weight to 90% by weight of ethanol content and a maximum of 10% by weight to 15% by weight of water content.

12. Process according to claim 11, characterized by comprising alcohols comprising a minimum of about 85% by weight, 86% by weight, 87% by weight, 88% by weight, 89% by weight or 90% by weight of ethanol content.

13. Process according to claim 11 or 12, characterized in comprising alcohols comprising a maximum of about 10% by weight, 11% by weight, 12% by weight, 13% by weight, 14% by weight or 15% by weight of water content.

14. Process, according to claim 1, 5 or 9, characterized by comprising alcohols comprising a minimum of about 88% by weight of ethanol content and a maximum of 12% by weight of water content. Petition 870250080789, dated 09 / 09 / 2025, pp. 91 / 122

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