EA040968B1 - METHOD FOR INCREASING THE EFFICIENCY OF CARBON CONVERSION - Google Patents

Description

Technical field

The present invention relates to processes and methods for improving carbon conversion efficiency. In particular, the present invention relates to a combination of a carbon monoxide consuming process with an industrial process, wherein the gas generated from the industrial process is purified and converted, and the carbon dioxide generated from the carbon monoxide consuming process is recycled to increase product yield.

State of the art

Carbon dioxide (CO2) accounts for approximately 76% of global human-caused greenhouse gas emissions, with the remainder being methane (16%), nitrous oxide (6%) and fluorinated gases (2%) (according to the Environmental Protection Agency USA). Reducing greenhouse gas emissions, in particular CO2, is vital to prevent the progression of global warming and the accompanying changes in climate and weather.

It has long been known that catalytic processes such as the Fischer-Tropsch process can be used to convert gases containing CO ₂ , carbon monoxide (CO) and/or hydrogen (H ₂ ) into various fuels and chemicals. Recently, however, gas fermentation has been developed as an alternative platform for the biological capture of such gases. In particular, d-scavenging microorganisms have been shown to convert gases containing CO2, CO, CH ₄ and/or H ₂ into products such as ethanol and 2,3-butanediol.

Such gases may be produced, for example, from industrial processes, including emissions from carbohydrate fermentation, gas fermentation, cement production, pulp and paper production, steel making, petroleum refining and related processes, petrochemical production, coke production, anaerobic or aerobic decomposition. gasification, natural gas extraction, oil extraction, metallurgical processes, production and/or purification of aluminum, copper and/or iron alloys, geological deposits, Fischer-Tropsch processes, methanol production, pyrolysis, methane steam reforming, dry methane reforming, partial oxidation biogas or natural gas; and autothermal reforming of biogas or natural gas.

To optimize the use of these gases in CO consuming processes, such as C1 adsorption fermentation processes, a combination of purification and industrial gas shift may be required. Accordingly, there remains a need for improved integration of industrial processes with CO-consuming processes, including industrial gas purification and conversion processes to optimize carbon conversion efficiency.

Brief description of the essence of the invention

Against this background, the present invention provides certain advantages and advances over the prior art.

Although the present invention described herein is not limited to particular advantages or functionalities, the present invention provides a method for improving carbon conversion efficiency, said method comprising supplying a CO2-containing gaseous substrate from an industrial process to a first purification module to remove at least at least one component of the CO ₂ -containing gaseous substrate to obtain a first purified CO ₂ gas stream, supplying the first purified CO ₂ gas stream to the CO ₂ electrolysis module to convert at least a portion of the first purified CO ₂ gas stream to obtain a stream with an increased content of CO and a first O ₂ rich stream and feeding at least a portion of the CO rich stream to a CO consuming process.

In some aspects of the method described herein, a CO2-containing gaseous substrate from an industrial process is first fed into a pressure modulation module to produce a compressed CO2-containing gas stream, and the compressed CO2-containing gas stream is fed into the first purification module.

In some aspects of the method described herein, the proposed method further comprises one or more of feeding at least a portion of the first O ₂ enriched stream directly to an industrial process and supplying at least a portion of the first O ₂ enriched stream to a recovery module O ₂ to obtain a second stream with a high content of O ₂ and a stream with a reduced content of O ₂ .

In some aspects of the method described herein, the proposed method further comprises one or more of supplying at least a portion of the second O2 enriched stream to an industrial process, supplying at least a portion of the O2 reduced stream to a CO2 electrolysis module, and supplying at least a portion of the O2-reduced stream to the CO-consuming process.

In some aspects of the method described herein, the proposed method further includes supplying at least a portion of the CO2-containing gaseous substrate from the industrial process and/or at least a portion of the first purified CO2 gas stream to the first CO ₂ concentration module to obtain a first concentrated stream CO ₂ and the first stream with a reduced content of CO ₂ .

- 1 040968

In some aspects of the method described herein, the proposed method further includes feeding at least a portion of the first concentrated CO2 stream to one or more of the first purification module and the CO2 electrolysis module.

In some aspects of the process described herein, the first CO2 reduced stream contains CO and/or H2, and the proposed method further comprises feeding at least a portion of the first _CO2 reduced stream to a CO consuming process.

In some aspects of the method described herein, the proposed method includes feeding at least a portion of the CO enriched stream to a pressure modulation module to produce a compressed CO stream and feeding at least a portion of the compressed CO stream to a CO consuming process.

In some aspects of the method described herein, the proposed method further comprises supplying an aqueous substrate to an H2 electrolysis module to produce an H2 rich stream and feeding at least a portion of the H2 rich stream to a CO consuming process.

In some aspects of the process described herein, the CO consuming process produces a tail gas containing CO ₂ .

In some aspects of the method described herein, the proposed method further includes one or more of supplying at least a portion of the tail gas containing CO ₂ to the first cleaning module or to the second cleaning module to remove at least one component from the tail gas with obtaining a second purified CO ₂ gas stream and supplying at least a portion of the tail gas containing CO 2 to the second CO 2 concentration module to obtain a second concentrated CO 2 stream and a second stream with a reduced CO 2 content.

In some aspects of the process described herein, at least a portion of the tail gas containing CO2 is supplied to a pressure modulation module to form a compressed tail gas stream, and the compressed tail gas stream is supplied to a first purification module and/or a second purification module.

In some aspects of the method described herein, the proposed method further includes feeding at least a portion of the second stream of concentrated CO ₂ to the first purification module or to the second purification module to remove at least one component from the tail gas to obtain a second purified CO gas stream ₂ .

In some aspects of the method described herein, the proposed method further includes supplying at least a portion of the second purified CO2 gas stream to the CO2 electrolysis module.

In some aspects of the process described herein, the gaseous CO2 containing substrate from the industrial process further comprises one or more of CO, H2 and CH ₄ .

In some aspects of the process described herein, the industrial process is selected from the group consisting of carbohydrate fermentation, gas fermentation, cement production, pulp and paper production, steel making, petroleum refining and related processes, petrochemical production, coke production, anaerobic or aerobic decomposition. , gasification, natural gas extraction, oil extraction, metallurgical processes, production and/or refining of aluminium, copper and/or iron alloys, geological deposits, Fischer-Tropsch processes, methanol production, pyrolysis, methane steam reforming, methane dry reforming, partial oxidation biogas or natural gas; and autothermal reforming of biogas or natural gas.

In some aspects of the process described herein, the CO2-containing gaseous substrate is obtained from a mixture of at least two or more sources.

In some aspects of the process described herein, the first purification module is selected from the group consisting of a hydrolysis module, an acid gas removal module, a deoxygenation module, a catalytic hydrogenation module, a solids removal module, a chloride removal module, a tar removal module, and a hydrogen cyanide post-treatment module. .

In some aspects of the process described herein, at least one component removed from the CO ₂ containing gaseous substrate is selected from the group consisting of sulfur compounds, aromatics, alkynes, alkenes, alkanes, olefins, nitrogen compounds, oxygen, phosphorus compounds, fine particles, solids, oxygen, halogenated compounds, silicon compounds, carbonyls, metals, alcohols, esters, ketones, peroxides, aldehydes, ethers, tar and naphthalene.

In some aspects of the method described herein, the CO-consuming process is a fermentation process comprising growing at least one caroboxidotrophic microorganism. The carboxydotrophic microorganism may be a carboxydotrophic bacterium.

In some aspects of the method described herein, the carboxydotrophic bacteria are selected from the group consisting of Moorella, Closthdium, Ruminococcus, Acetobacterium, Eubacterium, Butyribacterium, Oxobacter, Methanosarcina, and Desulfotomaculum. In some aspects of the method described

- 2 040968 in this document, carboxydotrophic bacteria are Closthdium autoethanogenum.

In certain aspects of the process described herein, the fermentation process provides a fermentation product selected from the group consisting of ethanol, butyrate, 2,3butanediol, lactate, butene, butadiene, methyl ethyl ketone, ethylene, acetone, isopropanol, lipids, 3hydroxypropionate, terpenes , fatty acids, 2-butanol, 1,2-propanediol and 1-propanol.

Brief description of graphic materials

In FIG. 1A, 1B and 1C are an integration flow diagram showing the integration of a purification module, a CO ₂ electrolysis module, and an optional H ₂ electrolysis module with a CO consuming process. In FIG. 1B additionally shows a pressure change module installed before the cleaning module. In FIG. 1C additionally shows a pressure change module installed before the process using CO.

In FIG. 2 is an integration flow diagram showing the integration of a purification module, a CO2 electrolysis module, an optional O2 recovery module, and an optional H2 electrolysis module with a CO consuming process.

In FIG. 3 is an integration flow diagram showing the integration of an optional CO ₂ concentration module upstream of the purification module, a CO ₂ electrolysis module, an optional H ₂ electrolysis module, and an optional O ₂ recovery module with a CO consuming process.

In FIG. 4 is an integration flow diagram showing the integration of an optional CO ₂ concentration module downstream of a purification module, a CO2 electrolysis module, an optional H2 electrolysis module, and an optional O2 recovery module with a CO consuming process.

In FIG. 5 is an integration flow diagram showing the integration of an H2 electrolysis module downstream of the optional pressure modulation module, where a portion of the gas from the H ₂ electrolysis module is mixed with the gas from the CO ₂ electrolysis module prior to being fed into the CO consuming process.

In FIG. 6 is an integration flow chart showing the integration of an additional purification module installed after the CO ₂ electrolysis module.

Detailed description of the invention

The inventors of the present invention have found that the integration of an industrial process that generates CO ₂ with a process that consumes CO, as well as a purification process that is carried out before the process of electrolysis of CO2, provides a significant advantage for the industrial process that produces CO2, and for a process that consumes CO, which may be a fermentation process with absorption of C1.

The term industrial process refers to a process for obtaining, converting, purifying, reforming, extracting or oxidizing a substrate, including chemical, physical, electrical and/or mechanical steps. Exemplary industrial processes include, but are not limited to, carbohydrate fermentation, gas fermentation, cement production, pulp and paper production, steelmaking, petroleum refining and related processes, petrochemical production, coke production, anaerobic or aerobic decomposition, gasification (such as biomass gasification). , liquid waste streams, solid waste streams, domestic effluents, fossil resources including natural gas, coal and oil), natural gas extraction, oil extraction, metallurgical processes, production and/or refining of aluminium, copper and/or iron alloys, geological deposits , Fischer-Tropsch processes, methanol production, pyrolysis, steam methane reforming, dry methane reforming, partial oxidation of biogas or natural gas, and autothermal reforming of biogas or natural gas. In such embodiments, the substrate and/or source of N-carbon can be captured from the industrial process prior to its release to the atmosphere using any standard method.

The terms industrial process gas, industrial process gas source, and industrial process gaseous substrate can be used interchangeably to refer to industrial process off-gas, industrial process by-product, industrial process co-product, industrial process recycle gas, and/or gas used in an industrial plant for energy recovery. In some embodiments, the gas from the industrial process is a pressure swing adsorption (PSA) tail gas. In some embodiments, the industrial process gas is a gas obtained from a CO2 extraction process, which may include amine scrubbing or the use of a carbonic anhydrase solution.

C1 refers to a molecule containing one carbon atom, such as CO, CO ₂ , methane (CP ₄ ) or methanol (CH3OH). d-oxygenate refers to a molecule containing one carbon atom, which also contains at least one oxygen atom, such as CO, CO ₂ or CH 3 OH. A C1 carbon source refers to a molecule containing one carbon atom that serves as a partial or sole carbon source for a microorganism according to the present invention. For example

- 3 040968 measures, the source of Cl-carbon may contain one or more of CO, CO2, CH ₄ , CH ₃ OH or formic acid (CH2O2). Preferably the O-carbon source contains one or both of CO and CO2. A C1 scavenging microorganism is a microorganism that can produce one or more products from an O-carbon source. Typically, the microorganism of the present invention is a C1-absorbing bacteria.

The substrate refers to a source of carbon and/or energy. Typically, the substrate is gaseous and contains a source of O-carbon, such as CO, CO2 and/or CH ₄ . Preferably the substrate contains an O-carbon source which is CO or CO and CO2. The substrate may additionally contain other non-carbon components such as H2, N2 or electrons. In this context, a substrate may refer to a source of carbon and/or energy for a microorganism according to the present invention.

The term co-substrate refers to a substrate which, while not necessarily the primary source of energy and material for product synthesis, can be used to synthesize a product when combined with another substrate such as the primary substrate.

The CO2-containing gaseous substrate, CO2-containing gas, or CO2-containing gaseous source may include any gas containing CO2. The gaseous substrate typically contains a significant portion of CO2, preferably at least about 5 to about 100% CO2 by volume. In addition, the gaseous substrate may contain one or more of hydrogen (H ₂ ), oxygen (O ₂ ), nitrogen (N ₂ ) and/or CH ₄ . In this context, CO, H ₂ and CH ₄ may be referred to as high energy gases.

The term carbon capture in this context refers to the absorption of carbon compounds, including CO2 and/or CO, from a stream containing CO2 and/or CO, and either a) conversion of CO2 and/or CO to products, b) conversion of CO2 and/or CO into substances suitable for long-term storage, c) capturing CO2 and/or CO with substances suitable for long-term storage, or d) a combination of these processes.

Terms efficiency improvement, increased efficiency, etc. refer to an increase in the rate and/or yield of a reaction, for example an increase in the rate of conversion of CO ₂ and/or CO to products, and/or an increase in product concentration. When used in relation to a fermentation process, efficiency enhancement includes, but is not limited to, an increase in one or more of the growth rate of microorganisms catalyzing the fermentation, the rate of growth and/or production of product at higher product concentrations, the volume of product desired produced per unit volume consumed the substrate, the rate of production or degree of production of the desired product, and the relative content of the desired product produced compared to other fermentation by-products.

A reactant in this context refers to a substrate that is present in a chemical reaction and is consumed during the reaction to form a product. A reagent is a starting material that undergoes change during a chemical reaction. In specific embodiments, the reagent includes, but is not limited to, CO and/or H ₂ . In specific embodiments, the reagent is CO ₂ .

A CO-consuming process refers to a process in which CO is the reactant; CO is consumed to form a product. A non-limiting example of a process that consumes CO is a gas fermentation process that absorbs C1. A process that consumes CO may include a reaction to form CO2. For example, a process that consumes CO may result in the formation of at least one product, such as a fermentation product, as well as CO2. In another example, a process that consumes CO is the production of acetic acid, in which CO is brought into contact with methanol under pressure.

Gas flow refers to any substrate flow that can be fed, for example, from one module to another, from one module to a CO consuming process, and/or from one module to a carbon capture device.

The gas streams are usually not a pure CO ₂ stream and have some content of at least one other component. For example, each source may have a different content of CO ₂ , CO, H ₂ and different components.

Due to the variability of their content, the gas stream must be treated before it is fed into a process that consumes CO. The processing of the gas stream includes the removal and/or conversion of various components that may be microbial inhibitors and/or catalyst inhibitors. Preferably the catalyst inhibitors are removed and/or converted prior to being fed to the electrolysis module and the microbial inhibitors are removed and/or converted prior to being fed to the CO consuming process. In addition, it may be necessary to treat the gas stream in one or more concentration steps that increase the concentration of CO and/or CO2. Preferably, the gas stream is subjected to a concentration step to increase the CO2 concentration before being fed into the electrolysis module. It has been found that higher concentrations of CO ₂ fed into the electrolysis module provide higher concentrations of CO leaving the electrolysis module.

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Purification module, impurity removal module, preparation module, processing module, etc. include technologies that can convert and/or remove at least one component from a gas stream. Non-limiting examples of purification modules include hydrolysis modules, acid gas removal modules, deoxygenation modules, catalytic hydrogenation modules, particulate removal modules, chloride removal modules, tar removal modules, and hydrogen cyanide post-treatment modules.

Terms components, impurities, etc. in this context refers to inhibitors of microbes and/or inhibitors of the catalyst, which may be in the gas stream. In specific embodiments, such components include, but are not limited to, sulfur compounds, aromatics, alkynes, alkenes, alkanes, olefins, nitrogen compounds, phosphorus compounds, fine particles, solids, oxygen, halogenated compounds, silicon compounds, carbonyls, metals , alcohols, esters, ketones, peroxides, aldehydes, ethers, tars and naphthalene. Preferably, the component removed in the cleaning module does not contain CO2.

Microbial inhibitors in this context refer to one or more components that slow down or interfere with a specific chemical reaction or other process involving microbes. In specific embodiments, microbial inhibitors include, but are not limited to, oxygen (O2), hydrogen cyanide (HCN), acetylene (C2H2), and BTEX (benzene, toluene, ethylbenzene, xylene).

Catalyst inhibitor, adsorbent inhibitor, and the like. in this context refer to one or more substances that slow down or interfere with a chemical reaction. In specific embodiments, catalyst inhibitors may include, but are not limited to, hydrogen sulfide (H2S) and carbonyl sulfide (COS).

In some cases, the fermentation step produces, introduces and/or concentrates at least one removable component. One or more of these components may be present in the gaseous substrate after fermentation. For example, the fermentation step can produce, introduce and/or concentrate sulfur in the form of H2S. In specific embodiments, hydrogen sulfide is introduced during the fermentation step. In various embodiments, the gaseous substrate after fermentation contains at least a portion of hydrogen sulfide. Hydrogen sulfide may be a catalyst inhibitor. Therefore, hydrogen sulfide can slow down the action of certain electrolysis modules. In order to supply a non-inhibitory post-fermentation substrate gas to the electrolytic cell, at least a portion of the hydrogen sulfide or other component present in the post-fermentation substrate gas may need to be removed by one or more purification modules. In another embodiment, acetone may be produced in the fermentation step and charcoal may be used as a purification module.

The terms purified gas and purified gas stream refer to a gas stream passed through at least one purification module from which one or more components have been removed and/or modified. For example, a CO2 purified gas stream refers to a CO2-containing gas passed through one or more purification modules.

Concentration modulus and similar terms refer to technology that can increase the content of a particular component in a gas stream. In particular embodiments, the concentration module is a CO2 concentration module, wherein the CO2 content of the gas stream exiting the CO ₂ concentration module is higher than the CO ₂ content of the gas stream prior to its entry into the CO ₂ concentration module. In some embodiments, the concentration module uses deoxygenation technology to remove O2 from a gas stream and increase the CO2 content of said gas stream. In some embodiments, the CO2 concentration module uses pressure swing adsorption (PSA) technology to remove H2 from a gas stream and increase the CO2 content of said gas stream. In some cases, the fermentation process acts as a CO2 concentration module. In some embodiments, the gas stream from the concentration module is fed to a carbon capture and storage (CCS) or enhanced oil recovery (EOR) unit.

The terms electrolysis module and cell can be used interchangeably to refer to a plant that uses electricity to carry out a non-spontaneous reaction. Electrolysis technologies are known in the art. Illustrative processes include alkaline aqueous solution electrolysis, proton or anion exchange membrane electrolysis (PEM, AEM), and solid oxide electrolysis (SOE) (Ursua et al., Proceedings of the IEEE 100(2):410-426, 2012; Jhong et al. ., Current Opinion in Chemical Engineering 2:191-199, 2013). The term Faraday efficiency is a value that refers to the number of electrons passed through the cell and transferred to the reduced product, and not involved in side processes. SOE modules operate at elevated temperatures. Below the thermoneutral voltage of the electrolysis module, the electrolysis reaction is endothermic. Above the thermoneutral voltage of the electrolysis module, the electrolysis reaction is exothermic. In some embodiments, the electrolysis module is operated without excess pressure. In some embodiments, the electrolysis module is operated at a pressure of 5-10 bar.

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The CO2 electrolysis module refers to a plant that can split CO2 into CO and _O2 , and operates according to the following stoichiometric reaction: 2CO2+electricity^2CO+O2. The use of different catalysts for CO ₂ reduction affects the final product. Catalysts, including but not limited to those based on Au, Ag, Zn, Pd and Ga, have been shown to be effective in producing CO from CO ₂ . In some embodiments, the pressure of the gas stream exiting the CO ₂ electrolysis module is about 5-7 barg.

H ₂ electrolysis module, water electrolysis module and H ₂ O electrolysis module refers to a plant that can split H ₂ O in the form of steam into H ₂ and O ₂ , and operates according to the following stoichiometric reaction: 2H ₂ O + electricity ^ 2H ₂ +O ₂ . The H ₂ O electrolysis module ensures the reduction of protons to H ₂ and the oxidation of O ^2- to O ₂ . The H ₂ produced by electrolysis can be mixed with a d-containing gaseous substrate as a way to provide additional feedstock and improve the composition of the substrate.

H2 and CO2 electrolysis modules have 2 gas outlets. One side of the electrolysis module, the anode, contains H ₂ or CO (and other gases such as unreacted water vapor or unreacted CO ₂ ). The second side, the cathode, contains O ₂ (and possibly other gases). The composition of the feedstock passed through the electrolysis process can determine the presence of various components in the CO stream. For example, the presence of inert components such as CH ₄ and/or N 2 in the feed may result in the presence of one or more of these components in the CO rich stream. In addition, in some electrolyzers, O ₂ generated at the cathode passes through the anode side where CO is produced and/or CO is passed through the anode side resulting in cross-contamination of the desired gaseous products.

The term release modulus is used to describe a technology that can separate a substance into two or more components. For example, an O ₂ separation module can be used to separate an O 2 -containing gaseous substrate into a stream containing primarily O ₂ (also referred to as an O ₂ rich stream or an O ₂ rich gas) and a stream which, in essentially no O2, no O2, or only trace amounts of O ₂ (also referred to as an O ₂ depleted or O ₂ depleted stream).

As used herein, the terms rich stream, rich gas, high purity gas, and similar terms refer to a gas stream having a higher content of a particular component after passing through a module such as an electrolysis module, compared to the content of said component in the stream entering the this module. For example, a CO rich stream can be obtained by passing a CO ₂ containing gaseous substrate through a CO ₂ electrolysis module. An H ₂ rich stream can be obtained by passing an aqueous gaseous substrate through an H ₂ electrolysis module. A stream with a high content of O ₂ is automatically formed at the anode in the CO ₂ or H ₂ electrolysis module; an O2 rich stream can also be obtained by passing an O2-containing gaseous substrate through an O ₂ separation module. A CO ₂ rich stream can be obtained by passing a CO 2 -containing gaseous substrate through a CO 2 concentration module.

As used herein, the terms depleted stream, lean gas, and similar terms refer to a gas stream having a lower content of a particular component after passing through a module such as a concentration module or a separation module, compared to the content of said component in the stream entering the given module. For example, an O ₂ reduced stream can be obtained by passing an O ₂ -containing gaseous substrate through an O ₂ separation module. The O ₂ reduced stream may contain unreacted CO ₂ from the CO ₂ electrolysis module. The O ₂ reduced stream may contain trace amounts of O ₂ or may contain no O ₂ . A _CO2 reduced stream can be obtained by passing a CO2 containing gaseous substrate through a CO2 concentration module. The CO2 reduced stream may contain CO, H2 and/or a component such as a microbial inhibitor or a catalyst inhibitor. The CO2 reduced stream may contain trace amounts of CO2 or may not contain CO2.

In particular embodiments of the present invention, an integrated process is provided in which the pressure of the gas stream can be increased and/or decreased. The term pressure modulus refers to technology that can create (ie increase) or decrease the pressure of a gas stream. The pressure of the gas may be increased and/or decreased by any suitable means, for example by means of one or more compressors and/or valves. In some cases, the gas stream may have a sub-optimal pressure, or the pressure of the gas stream may be higher than the optimum pressure and, therefore, a valve may be used to reduce the pressure. The pressure modulation module may be located before or after any of the modules described herein. For example, a pressure modulation module may be used prior to a purification module, prior to a concentration module, prior to an electrolysis module, and/or prior to a CO-consuming process.

Compressed gas flow refers to the gaseous substrate passed through the measuring module

- 6 040968 pressure gauge. The compressed gas stream can also be used to describe a gas stream that meets the operating pressure requirements of a particular module.

Terms gaseous substrate after the CO-consuming process, tail gas after the CO-consuming process, tail gas, etc. can be used interchangeably to describe a gas that has gone through a CO-consuming process. The gaseous substrate after the CO consuming process may contain unreacted CO, unreacted H2 and/or CO2 formed (or concurrently not consumed) in the CO consuming process. The gaseous substrate from the CO consuming process may be further supplied to one or more of a pressure change module, a purification module, a CO2 concentration module, and/or an electrolysis module. In some embodiments, the gaseous substrate after the CO-consuming process is the gaseous substrate after fermentation.

The term required composition is used to indicate the required content and type of components in a substance, such as, for example, a gas stream. More specifically, a gas is considered to have the required composition if it contains a certain component (i.e. CO, H2 and/or CO2) and/or contains a certain component in a certain amount, and/or does not contain a certain component (i.e. an impurity harmful to microorganisms) and/or does not contain a certain component in a certain amount. More than one component may be considered in determining whether a gas stream has the desired composition.

Although the substrate does not necessarily contain H2, the presence of H2 should not adversely affect the formation of the product in accordance with the methods of the present invention. In specific embodiments of the invention, the presence of H2 leads to an improvement in the overall efficiency of alcohol production. In one embodiment, the substrate contains about 30% or less H2 by volume, 20% or less _H2 by volume, about 15% or less _H2 by volume, or about 10% or less H2 by volume. In other embodiments, the substrate stream contains low concentrations of H ₂ , such as less than 5%, or less than 4%, or less than 3%, or less than 2%, or less than 1%, or essentially no H ₂ .

The substrate may also contain some CO, such as from about 1 to about 80% CO by volume, or from 15 to about 30% CO by volume. In one embodiment, the substrate contains less than or exactly about 20% CO by volume. In specific embodiments, the substrate contains less than or exactly about 15% CO by volume, less than or exactly about 10% CO by volume, less than or exactly about 5% CO by volume, or substantially no CO.

The composition of the substrate can be improved to provide the desired or optimal ratio of H ₂ :CO:CO ₂ . The required ratio of H ₂ :CO:CO ₂ depends on the desired fermentation product in the fermentation process. For ethanol, the optimal ratio of H ₂ :CO:CO ₂ is

where x>2y, to meet the ethanol production stoichiometry

U)// ₃ + (y)CO + f^^CO ₃ -> f^)c ₃ ^OH+

Operating the fermentation process in the presence of H ₂ has the added benefit of reducing the amount of CO 2 generated during the fermentation process. For example, a gaseous substrate containing a minimal amount of H ₂ usually turns into ethanol and CO ₂ with the following stoichiometry: 6CO+3H ₂ O^C ₂ H ₅ OH+4CO ₂ . As the amount of H ₂ used by C1-consuming bacteria increases, the amount of CO ₂ produced decreases, i.e. 2CO'4n2 >C2H5OH'H2O.

If CO is the only source of carbon and energy for the production of ethanol, then part of the carbon is lost to the formation of CO ₂ according to the equation

CO + 3 H ₂ O -> C ₂ H ₅ OH + 4 CO ₂ (AG ⁰ \u003d -224.90 kJ / mol of ethanol)

With an increase in the amount of H ₂ available in the substrate, the amount of CO ₂ formed decreases. With a stoichiometric ratio of 1:2 (CO/H ₂ ), the formation of CO ₂ is completely excluded.

CO + 1 H ₂ + 2 H ₂ O -> 1 C ₂ H ₅ OH + 3 CO ₂ (AG ⁰ \u003d -204.80 kJ / mol of ethanol)

CO + 2 H ₂ + 1 H ₂ O -> 1 C ₂ H ₅ OH + 2 CO ₂ (AG ⁰ \u003d -184.70 kJ / mol of ethanol)

CO + 3 H ₂ -> 1 C ₂ H ₅ OH + 1 CO ₂ (AG ⁰ \u003d -164.60 kJ / mol of ethanol)

The composition of the substrate can significantly affect the efficiency and/or cost of the reaction. For example, the presence of O2 can reduce the efficiency of an anaerobic fermentation process. Depending on the composition of the substrate, it may be necessary to treat, clean or filter the substrate to remove undesirable contaminants such as toxins, unwanted components or dust particles, and/or to

- 7 040968 increasing the concentration of the required components. In addition, carbon capture can be increased by recycling the CO2 generated in the CO consuming process to the CO2 electrolysis module to increase the yield of the CO consuming process. The CO2 generated in the CO2 consuming process can be purified before being fed into the _CO2 electrolysis module.

In some embodiments, the CO consuming process is carried out in a bioreactor. The term bioreactor includes a fermentation apparatus consisting of one or more vessels and/or towers or pipelines, which include a continuous stirred cell reactor (CSTR), an immobilized cell reactor (ICR), a trickled bed reactor (TBR), a bubble column, a gas lift a fermenter, a static mixer, a circulating loop reactor, a membrane reactor such as a hollow fiber membrane bioreactor (HFM BR), or other container or other device suitable for gas-liquid contact. The reactor is preferably configured to receive a gaseous substrate containing CO, CO2, H2 or mixtures thereof. The reactor may contain several reactors (stages) arranged in parallel or in series. For example, the reactor may comprise a first growth reactor in which bacteria are grown and a second fermentation reactor into which fermentation broth can be fed from the growth reactor and where most of the fermentation products can be obtained. Operation of the bioreactor at elevated pressure makes it possible to increase the rate of gas mass transfer from the gas phase to the liquid phase. Accordingly, it is generally preferred to carry out the cultivation/fermentation at a pressure above atmospheric pressure. In addition, since this gas conversion rate is partly dependent on the residence time of the substrate in the reactor, and achieving the required residence time determines the required volume of the bioreactor, the use of pressurized systems can significantly reduce the required volume of the bioreactor and, therefore, the capital cost of the growth/fermentation equipment. . This in turn means that the residence time, defined as the volume of liquid in the bioreactor divided by the gas flow rate, can be reduced if the bioreactors are maintained at elevated pressure rather than at atmospheric pressure. Optimum reaction conditions depend in part on the particular microorganism used. However, it is generally preferred to carry out the fermentation at a pressure above atmospheric pressure. In addition, since this gas shift rate depends in part on the residence time of the substrate in the reactor, and the achievement of the required retention time in turn determines the required volume of the bioreactor, the use of pressurized systems can significantly reduce the required volume of the bioreactor and, therefore, capital costs for enzymatic equipment.

Unless the context implies otherwise, the expressions fermentation, fermentation process, fermentation reaction, etc. in this context, both the growth phase and the gaseous substrate biosynthesis phase are included. In some embodiments, the fermentation is carried out without carbohydrate substrates such as sugar, starch, lignin, cellulose, or hemicellulose.

The culture is usually maintained in an aqueous culture medium which contains sufficient nutrients, vitamins and/or minerals to allow the growth of microorganisms. Culture medium growth medium and culture medium are used to describe a medium for growing bacteria. Preferably, the aqueous culture medium is an anaerobic microorganism growth medium, such as a minimal anaerobic microbial growth medium. Suitable media are well known in the art. The term nutrient includes any substance that can be used for the metabolism of a microorganism. Exemplary nutrients include potassium, B vitamins, trace metals, and amino acids.

The terms fermentation broth and broth include a mixture of components, including a growth medium and a culture, or one or more microorganisms. It should be noted that the term microorganism and the term bacterium are used interchangeably in this context.

The microorganism of the present invention can be grown using the gas stream to produce one or more products.

For example, the microorganism according to the present invention can produce or can be created to produce ethanol (WO 2007/117157), acetate (WO 2007/117157), butanol (WO 2008/115080 and WO 2012/053905), butyrate (WO 2008/115080) , 2,3-butanediol (WO 2009/151342 and WO 2016/094334), lactate (WO 2011/112103), butene (WO 2012/024522), butadiene (WO 2012/024522), methyl ethyl ketone (2 butanone) (WO 2012/ 024522 and WO 2013/185123), ethylene (WO 2012/026833), acetone (WO 2012/115527), isopropanol (WO 2012/115527), lipids (WO 2013/036147), 3-hydroxypropionate (3-HP) (WO 2013/180581), terpenes including isoprene (WO 2013/180584), fatty acids (WO 2013/191567), 2-butanol (WO 2013/185123), 1,2-propanediol (WO 2014/036152), 1-propanol (WO 2014/0369152), products from chorismate (WO 2016/191625), 3-hydroxybutyrate (WO 2017/066498) and 1,3-butanediol (WO 2017/0066498). In addition to one or more target products, the microorganism according to the present invention can also produce ethanol, acetate and/or 2,3-butanediol. In some embodiments, the microbial biomass itself may be considered a product. Such products can be subjected to additional conversion to obtain at least one component from a diesel, aviation

- 8 040968 fuel and/or gasoline. In addition, microbial biomass can be further processed to produce a single cell protein (SCP).

A microorganism is a microscopic organism, such as bacteria, archaea, viruses, or fungi. The microorganism according to the present invention is usually a bacterium. In this context, reference to a microorganism includes bacteria.

The parent microorganism is the microorganism used to produce the microorganism according to the present invention. The parent microorganism may be a naturally occurring microorganism (ie, a wild-type microorganism) or a microorganism previously modified (ie, a mutant or recombinant microorganism). The microorganism of the present invention may be modified to express or overexpress one or more enzymes that are not expressed or overexpressed in the parent microorganism. Likewise, the microorganism of the present invention may be modified such that it contains one or more genes that are not contained in the parent microorganism. The microorganism according to the present invention can also be modified so that it does not express or expresses a smaller amount of one or more enzymes that are expressed in the original microorganism. In one embodiment, the parent microorganism is Clostridium autoethanogenum, Clostridium ljungdahlii, or Clostridium ragsdalei. In a preferred embodiment, the parent microorganism is Clostridium autoethanogenum LZ1561, introduced June 7, 2010 to the German Collection of Microorganisms and Cell Cultures (Deutsche Sammlung von Mikroorganismen und Zellkulturen GmbH (DSMZ)), located at Inhoffenstrae 7B, D-38124 Braunschweig, Germany , June 7, 2010 under the Budapest Treaty on the International Recognition of the Deposit of Microorganisms for the Purposes of Patent Procedure under accession number DSM23693. This strain is described in International Patent Application No. PCT/NZ 2011/000144 published as WO 2012/015317.

The term derived from means that a nucleic acid, protein, or microorganism is modified or adapted from another (i.e., parental or wild-type) nucleic acid, protein, or microorganism to form a new nucleic acid, protein, or microorganism. Such modifications or adaptations typically include the insertion, deletion, mutation, or substitution of nucleic acids or genes. In general, the microorganism according to the present invention is obtained from the parent microorganism. In one embodiment, the microorganism of the present invention is derived from Clostridium autoethanogenum, Clostridium ljungdahlii, or Clostridium ragsdalei. In a preferred embodiment, the microorganism of the present invention is derived from Clostridium autoethanogenum LZ1561, which is listed in the DSMZ collection under accession number DSM23693.

The microorganism according to the present invention can be further classified according to functional characteristics. For example, the microorganism of the present invention may be or may be derived from a C1-absorbing microorganism, anachrob, acetogen, ethanologen, carboxydotroph and/or methanotroph.

Wood-Ljungdahl refers to the Wood-Ljungdahl carbon sequestration cascade as described, for example, in Ragsdale, Biochim Biophys Acta, 1784: 1873-1898, 2008. Wood-Ljungdahl microorganisms refer, as might be expected, to microorganisms having a Wood-Ljungdahl cascade. Typically, the microorganism of the present invention has a native Wood-Ljungdahl cascade. In this context, the Wood-Ljungdahl cascade may be a native, unmodified Wood-Ljungdahl cascade, or it may be a Wood-Ljungdahl cascade with some degree of genetic modification (i.e., overexpression, heterologous expression, knockout, etc.), provided that it still acts to convert CO, CO ₂ and/or H ₂ to acetyl-CoA.

Anaerobe is a microorganism that does not require O ₂ for growth. The anaerobe can react negatively or even die if the O2 content exceeds a certain limit. However, some anaerobes can tolerate low concentrations of O ₂ (ie 0.000001-5% O ₂ ). As a rule, the microorganism according to the present invention is an anaerobe.

Acetogens are obligate anaerobic bacteria that use the Wood-Ljungdahl cascade as the main energy storage mechanism and for the synthesis of acetyl-CoA and acetyl-CoA derivatives such as acetate (Ragsdale, Biochim Biophys Acta, 1784: 1873-1898, 2008). In particular, acetogens use the Wood-Ljungdahl cascade as (1) a mechanism for the reductive synthesis of acetyl-CoA from CO ₂ , (2) for accepting a terminal electron, an energy conservation process, (3) a mechanism for the assimilation (assimilation) of CO ₂ in the synthesis of cellular carbon (Drake, Acetogenic Prokaryotes, in The Prokaryotes, 3rd ed., p. 354, New York, NY, 2006). All natural acetogens are C1-scavenging, anaerobic, autotrophic, and non-methanotrophic. Typically, the microorganism of the present invention is an acetogen.

An ethanologen is a microorganism that produces or can produce ethanol. Typically, the microorganism according to the present invention is an ethanologen.

An autotroph is a microorganism that can grow in the absence of organic carbon.

- 9 040968 kind. Instead, autotrophs use inorganic carbon sources such as CO and/or CO ₂ . Typically, the microorganism according to the present invention is an autotroph.

A carboxydotroph is a microorganism capable of using CO2 as its sole source of carbon and energy. Typically, the microorganism according to the present invention is a carboxydotroph.

A methanotroph is a microorganism capable of using methane as its sole source of carbon and energy. In some embodiments, the microorganism of the present invention is a methanotroph or derived from a methanotroph. In other embodiments, the microorganism of the present invention is not a methanotroph or derived from a methanotroph.

The table provides an illustrative list of microorganisms and indicates their functional characteristics.

Wuda-Ljungdal Cl absorption Anaerobe Acetogen Ethanologen W o CL ΙΟ 1- Carboxidotroph Acetobacterium woodii + + + + +/- ¹ + Alkalibaculum bacchii + + + + + + + Blautia producta + + + + - + + Butyribacterium methylotrophicum + + + + + + + Clostridium aceticum + + + + - + + Clostridium autoethanogenum + + + + + + + Clostridium carboxidivorans + + + + + + + Clostridium coskatii + + + + + + + Clostridium drakei + + + + - + + Clostridium formicoaceticum + + + + - + + Clostridium Ijungdahlii + + + + + + + Clostridium magnum + + + + + +/- ² Clostridium ragsdalei + + + + + + + Clostridium scatologenes + + + + - + + Eubacterium limosum + + + + - + + Moorella thermautotrophica + + + + + + + Moorella thermoacetica (former Clostridium thermoaceticum) + + + + _ 3 + + Oxobacter pfennigii + + + + - + + Sporomus ovata + + + + + +/- ⁴ Sporomusa silvacetica + + + + + +/- ⁵ Sporomusa sphaeroides + + + + + +/- ⁱⁿ Thermoanaerobacter kiuvi + + + + - + -

Acetobacterium woodi can produce ethanol from fructose, but not from gas.

² It has not been studied whether Closthdium magnum can grow on CO.

³ It is described that one strain of Moorella thermoacetica, Moorella sp. HUC22-1, produces ethanol from gas.

⁴ It has not been studied whether Sporomusa ovata can grow on CO.

⁵ Whether Sporomusa silvacetica can grow on CO has not been studied.

⁶ It has not been studied whether Sporomusa sphaeroides can grow on CO.

A native product is a product produced by a non-genetically modified microorganism. For example, ethanol, acetate and 2,3-butanediol are native products of Clostridium autoethanogenum, Clostridium Ijungdahlii and Closthdium ragsdalei. Non-native product before

- 10040968 is a product produced by a genetically modified microorganism, but which is not produced by the non-genetically modified microorganism from which the genetically modified microorganism is derived.

Selectivity refers to the ratio of the production of the target product to the production of all fermentation products produced by the microorganism. The microorganism according to the present invention can be designed to produce products with a certain selectivity or with a minimum selectivity. In one embodiment, the target product is at least about 5%, 10%, 15%, 20%, 30%, 50%, or 75% of all fermentation products produced by the microorganism of the present invention. In one embodiment, the proportion of the desired product is at least 10% of all fermentation products produced by the microorganism of the present invention, such that the microorganism of the present invention has a selectivity for the desired product of at least 10%. In another embodiment, the proportion of the desired product is at least 30% of all fermentation products produced by the microorganism according to the present invention, so that the microorganism according to the present invention has a selectivity for the desired product of at least 30%.

Cultivation/fermentation is preferably carried out under suitable conditions for the production of the target product. As a rule, cultivation/fermentation is carried out under anaerobic conditions. Reaction conditions to be considered include pressure (or partial pressure), temperature, gas flow rate, liquid flow rate, medium pH, medium redox potential, agitation rate (when using a continuous mixing reactor), inoculum content, maximum gaseous substrate concentrations , so that the gas content in the liquid phase does not become limiting, and the maximum concentrations of the product in order to avoid inhibition of the process. In particular, the rate of introduction of the substrate can be controlled so that the gas concentration in the liquid phase does not become limiting, since the products can be consumed by the culture under conditions of limited gas content.

Target products can be isolated or purified from the fermentation broth by any method or combination of methods known in the art, including, for example, fractional distillation, evaporation, evaporation through a semi-permeable membrane, gas stripping, phase separation, and extractive fermentation, including, for example, liquid- liquid extraction. In some embodiments, the target products are isolated from the fermentation broth by continuously removing a portion of the broth from the bioreactor, isolating the microbial cells from the broth (typically by filtration), and isolating one or more target products from the broth. Alcohols and/or acetone can be isolated, for example, by distillation. Acids can be isolated, for example, by adsorption on activated charcoal. The isolated microbial cells are preferably returned to the bioreactor. The cell-free filtrate that remains after removal of the desired products is also preferably returned to the bioreactor. Additional nutrients (such as B vitamins) can be added to the cell-free filtrate to replenish the medium before it is returned to the bioreactor.

In FIG. 1A shows a method for integrating an industrial process 110, one or more purification modules 120, a CO ₂ electrolysis process 130, an optional H ₂ electrolysis process 160, and a CO consuming process 140. CO ₂ -containing gas from industrial process 110 is fed through pipe 112 to one or more purification modules 120 to remove and/or convert one or more components 128. The purified gas from one or more purification modules 120 is then fed through pipe 122 to electrolysis module 130 CO2 to convert at least a portion of the gas stream. In some embodiments, CO ₂ -containing gas from industrial process 110 is directly fed through conduit 114 to CO ₂ electrolysis module 130 to convert at least a portion of the gas stream; in this embodiment, the sulfur component may be removed before it is passed through the industrial process. Optionally, at least a portion of the O ₂ may be supplied from CO ₂ electrolysis module 130 to industrial process 110 via conduit 136. At least a portion of the converted gas stream is passed via conduit 132 from CO ₂ electrolysis module 130 to CO consuming process 140. In some embodiments, the aqueous substrate is fed through conduit 162 to the H ₂ electrolysis module 160 to convert at least a portion of the aqueous substrate, and the H ₂ rich stream is fed through conduit 164 to the CO-consuming process 140. Optionally, at least a portion of the O ₂ may be supplied from the H ₂ electrolysis module 160 to the industrial process 110 via conduit 166. The CO consuming process 140 provides at least one product 146 and a gaseous substrate after the CO consuming process.

The CO consuming process 140 shown in FIG. 1A may be a gas fermentation process and may take place in an inoculator and/or in one or more bioreactors. For example, CO consuming process 140 may be a gas fermentation process in a bioreactor containing a culture of at least one O-absorbing microorganism. In those embodiments in which the CO-consuming process 140 is a gas fermentation process, the culture can be fermented to produce one or more fermentation products 146 and a post-fermentation gaseous substrate (substrate gas from the CO-consuming process).

- 11 040968

In some embodiments, the CO consuming process 140 illustrated in FIG. 1A includes a reaction step to produce CO2. In those embodiments where the CO-consuming process substrate gas contains CO2, at least a portion of said CO-consuming process substrate gas is fed through conduit 142 to one or more purification modules 150 to remove and/or convert one or more components 158. The purified gas stream containing CO ₂ is then fed through pipe 152 to the CO ₂ electrolysis module 130 to convert at least a portion of the gas stream. In particular embodiments, the gaseous substrate after the CO-consuming process is fed through conduit 142 to the same one or more purification modules 120 that are supplied with CO2-containing gas from the industrial process 110. In various embodiments, the gaseous substrate after the CO-consuming process, may be fed to one or more purification modules 120, which are supplied with CO2-containing gas from the industrial process 110, and to one or more purification modules 150. This process of purifying and electrolyzing the gaseous substrate after the CO consuming process has been found to increase the efficiency of carbon capture.

In specific embodiments, the at least one component removed in the cleaning module 150 shown in FIG. 1A is produced, injected and/or concentrated in a CO consuming process 140, such as a gas fermentation process. In various embodiments, one or more components obtained, introduced and/or concentrated during the fermentation step contain sulfur. In some cases, sulfur, such as hydrogen sulfide, is introduced into the CO-consuming process 140. Found that such sulfur reduces the efficiency of the module 130 electrolysis of CO ₂ . The purification module 150 has been found to be effective in reducing the amount of sulfur in the gaseous substrate after the CO-consuming process before supplying the gaseous substrate after the CO-consuming process to the CO ₂ electrolysis module 130 . It has been found that the use of the purification module 150 prior to the CO ₂ electrolysis module 130 increases the efficiency of the CO ₂ electrolysis module 130 .

The present inventors have found that a by-product of the electrolysis of CO ₂ and H ₂ , oxygen O 2 can provide an additional benefit to the commercial C 1 production process. Although the fermentation processes of the present invention are anaerobic processes, the present inventors have found that a by-product of the CO production process, oxygen O ₂ , such as O ₂ , passing through conduit 136 in FIG. 1A can be used in an industrial process for making C1. A by-product of the CO ₂ electrolysis process, high purity oxygen O ₂ can be integrated into the industrial process and advantageously recover costs and in some cases provide synergies that further reduce the costs of said industrial process as well as subsequent gas fermentation.

Generally, the industrial processes described herein provide the required O2 by air separation. The production of O2 by air separation is an energy-intensive process involving the cryogenic separation of _O2 from N2 to achieve the highest purity. Production of O ₂ by electrolysis of CO 2 and/or H 2 and replacement of O 2 produced by air separation can recover up to 5% of electricity costs in an industrial process.

Some industrial processes that produce C1 involving partial oxidation reactions require the supply of O ₂ . Exemplary industrial processes include basic steel furnace (BOF) reactions, COREX or FINEX steelmaking processes, blast furnace (BF) processes, ferroalloy processes, titanium dioxide processes, and gasification processes. Gasification processes include, but are not limited to, solid waste gasification, biomass gasification, petroleum coke gasification, and coal gasification. In one or more of these industrial processes, the O2 from the CO2 electrolysis process can be used to replace or completely replace the O2 normally provided by air separation.

As shown in FIG. 1B and 1C, the method for integrating an industrial process, one or more purification modules, a CO2 electrolysis process, an optional H2 electrolysis process, and a CO consuming process may further include integrating one or more pressure change modules 170. For example, as shown in FIG. 1B, at least a portion of the CO ₂ -containing gas from industrial process 110 is supplied through conduit 112 to pressure modulation module 170 to form a compressed CO ₂ -containing gas stream. Then, at least part of the compressed CO ₂ -containing gas stream is fed through the pipe 172 to the cleaning module 120. At least a portion of the gaseous substrate from the CO consuming process may also be fed through conduit 142 to pressure modulation module 170 to produce pressurized tail gas. Then, at least a portion of the compressed tail gas is fed through pipe 172 to a purification module 150 and/or a purification module 120. As shown in FIG. 1C, at least a portion of the converted gas stream is fed through conduit 132 from CO ₂ electrolysis module 130 to pressure modulation module 170 to form a compressed CO-containing gas stream, which is fed via conduit 172 to CO consuming process 140.

In FIG. 2 shows a method for integrating an industrial process 210, a purification module 220, a CO ₂ electrolysis module 230, an optional H ₂ electrolysis process 270, a CO consuming process 240, and an optional O ₂ recovery module 260. CO ₂ -containing gas from industrial process 210 is fed through pipe 212 to one or more purification modules 220 to remove and/or convert one or

- 12 040968 more components 228. Then, the purified gas from one or more purification modules 220 is fed through pipe 222 to the CO ₂ electrolysis module 230 to convert at least a portion of the gas stream. Optionally _, at least a portion of the O ₂ may be supplied from the CO ₂ module 230 to the industrial process 210 via conduit 236. 246 and the gaseous substrate after the CO-consuming process. In some embodiments, the aqueous substrate is fed through conduit 272 to the H ₂ electrolysis module 270 to convert at least a portion of the aqueous substrate, and the H ₂ rich stream is fed through conduit 274 to the CO-consuming process 240. Optionally, at least a portion of the O2 may be supplied from the H2 electrolysis module 270 to the industrial process 210 via conduit 276.

In specific embodiments, the proposed process includes an O2 separation module 260 after a CO ₂ electrolysis module 230 to separate at least a portion of the O ₂ from the gas stream. In those embodiments that use an O ₂ recovery module 260 downstream of the CO ₂ electrolysis module 230, at least a portion of the gas stream is fed from the CO ₂ electrolysis module 230 to the O ₂ recovery module 260 via conduit 234. In those embodiments that contain O ₂ separation module 260, at least a portion of the O ₂ separated from the gas stream from the O ₂ separation module 260 (the O ₂ enriched stream) can be fed into the industrial process 210 via conduit 264. In those embodiments in which the module is used 260 O ₂ recovery after CO ₂ electrolysis module 230, at least a portion of the O ₂ depleted stream is fed from O ₂ recovery module 260 to CO consuming process 240 through conduit 262. In some embodiments that use recovery module 260 O ₂ after CO ₂ electrolysis module 230, at least a portion of the O ₂ reduced stream is fed from O ₂ separation module 260 back to CO ₂ electrolysis module 230 via pipe 266. In implementations that do not use the O2 recovery module 260, a portion of the gas stream may be supplied from the _CO2 electrolysis module 230 to the industrial process 210 via conduit 236.

In some embodiments, the CO consuming process 240 illustrated in FIG. 2 includes a reaction step for producing CO ₂ . In those embodiments in which the gaseous substrate after the CO-consuming process contains CO ₂ , at least a portion of said gaseous substrate after the CO-consuming process is fed through pipe 242 to one or more purification modules 250 to remove and/or convert one or more components 258. The purified gas stream is then fed through pipe 252 to the CO ₂ electrolysis module 230 to convert at least a portion of the gas stream. In specific embodiments, the gaseous substrate after the CO-consuming process is fed through conduit 242 to the same one or more purification modules 220 that are supplied with CO2-containing gas from the industrial process 210. In various embodiments, the gaseous substrate after the CO-consuming process, can be fed to one or more purification modules 220, which are supplied with CO ₂ -containing gas from the industrial process 210, and one or more purification modules 250.

The CO consuming process 240 shown in FIG. 2 may be a gas fermentation process and may take place in an inoculator and/or in one or more bioreactors. For example, CO consuming process 240 may be a gas fermentation process in a bioreactor containing a culture of at least one d-captive microorganism. In those embodiments where the CO-consuming process 240 is a gas fermentation process, the culture can be fermented to produce one or more fermentation products 246 and a post-fermentation gaseous substrate (CO-consuming process substrate gas).

It has been found that a high purity condition of the CO ₂ stream (CO ₂ enriched stream) fed to the CO2 electrolysis process increases the efficiency (carbon capture) of the CO consuming process. To increase the CO ₂ concentration in the stream, one or more CO 2 concentration modules can be introduced into said process. Preferably the stream after electrolysis has a CO concentration of 20-90%.

In FIG. 3 shows a method for integrating an industrial process 310 with an optional CO ₂ concentration module 370, a purification module 320, a CO ₂ electrolysis module 330, an optional H ₂ electrolysis module 380, a CO consuming process 340, and an optional O ₂ recovery module 360, in accordance with one aspect of the present invention. In those implementations that do not include the module 370 concentration of CO ₂ , CO ₂ -containing gas from the industrial process 310 is fed through the pipe 312 to the module 320 cleaning. In those embodiments in which CO ₂ concentration module 370 is included, CO ₂ -containing gas from industrial process 310 is fed through pipe 314 to CO 2 concentration module 370 to increase the concentration of CO 2 in the gas stream and to remove one or more components 374. Gas stream concentrated CO ₂ is fed through pipe 372 to one or more purification modules 320 to remove and/or convert one or more components 328. The purified gas from one or more purification modules 320 is then fed through pipe 322 to CO2 electrolysis module 330 for conversion of at least parts of the gas stream. At least a portion of the converted gas stream is supplied from CO ₂ electrolysis module 330 to CO consuming process 340 via conduit 332. In some embodiments, component 374 is CO and/or H ₂ that is supplied via conduit 376 to CO consuming process 340. CO. In some embodiments, the aqueous substrate

- 13 040968 served through the pipe 382 in the module 380 electrolysis H ₂ for the conversion of at least part of the aqueous substrate, and the stream with a high content of H ₂ served through the pipe 384 in the process 340, consuming CO. Optionally, at least a portion of the O ₂ may be supplied from the H ₂ electrolysis module 380 to the industrial process 310 via conduit 386.

At least a portion of the gas stream from the CO ₂ electrolysis module 330 may be supplied to the industrial process 310 through conduit 336. In specific embodiments, the proposed process includes an O ₂ separation module 360 after the CO ₂ electrolysis module 330, where the gas stream is supplied from the CO 2 electrolysis module 330 ₂ to an O ₂ separation module 360 through conduit 334 to separate at least a portion of the O ₂ from the gas stream. In those embodiments that use an O ₂ recovery module 360 after the CO ₂ electrolysis module 330, at least a portion of the removed O ₂ (O ₂ enriched stream) is fed from the O ₂ recovery module 360 to the industrial process 310 via conduit 364. In those embodiments that use O ₂ recovery module 360 after CO ₂ electrolysis module 330, at least a portion of the O ₂ reduced stream is fed from O ₂ recovery module 360 to CO consuming process 340 through conduit 362. In some embodiments that use O ₂ recovery module 360 downstream of CO ₂ electrolysis module 330, at least a portion of the O ₂ reduced stream is fed from O 2 recovery module 260 back to CO ₂ electrolysis module ₃₃₀ via conduit 366. In those embodiments, , which do not use the O ₂ separation module 360, a portion of the gas stream can be supplied from the CO ₂ electrolysis module 330 to the industrial process 310 through pipe 336.

The process of concentrating CO ₂ in a gas stream to one or more purification modules 320 has been found to reduce unwanted gases, increasing the efficiency of a CO consuming process, such as a fermentation process. The amount of O ₂ generated at the anode side of the electrolysis module is 50% of the amount of CO ₂ generated at the cathode of the electrolysis module. The produced O ₂ can be used to improve the efficiency of industrial process 310, wherein at least a portion of the electrolysis gas stream is fed to industrial process 310.

In some embodiments, the CO consuming process 340 illustrated in FIG. 3 includes a reaction step for producing CO ₂ . In those implementations in which the gaseous substrate after the CO-consuming process contains CO ₂ , said gaseous substrate after the CO-consuming process is fed through pipe 342 to one or more purification modules 350 to remove and/or convert one or more components 358 The purified gas stream is then fed through conduit 352 to CO ₂ electrolysis module 330 to convert at least a portion of the gas stream. In particular embodiments, the gaseous substrate after the CO-consuming process is fed through conduit 342 to one or more purification modules 320, which are supplied with CO ₂ -containing gas from industrial process 310. In various embodiments, the gaseous substrate after the CO-consuming process can be be fed to one or more purification modules 320, which are supplied with CO2-containing gas from the industrial process 310, and to one or more purification modules 350.

The CO consuming process 340 shown in FIG. 3 may be a gas fermentation process and may take place in an inoculator and/or in one or more bioreactors. For example, the CO consuming process may be a gas fermentation process in a bioreactor containing a culture of at least one d-absorbing microorganism. In the CO consuming process 340, the culture is fermented to produce one or more fermentation products 346 and a gaseous substrate after the CO consuming process.

In particular embodiments, the CO2 concentration module may be located after the purification module. In FIG. 4 shows a method for integrating an industrial process 410 with a purification module 420, an optional CO ₂ concentration module 470, a CO ₂ electrolysis module 430, an optional H2 electrolysis module 480, a CO-consuming process 440, and an optional O2 recovery module 460, in accordance with one aspect of the present invention. inventions. In those embodiments that do not include the optional CO2 concentration module 470, the CO2-containing gas from the industrial process 410 is supplied from the purification module 420 to the CO ₂ electrolysis module 430 via conduit 422. In those embodiments that include the optional concentration module 470 CO ₂ , CO ₂ containing gas from industrial process 410 is fed through pipe 412 to one or more purification modules 420 to remove and/or convert one or more components 428. The purified stream is then fed through pipe 424 to an optional CO ₂ concentration module 470 to increase concentration of CO ₂ in the gas stream and to remove one or more components 474. The concentrated CO 2 gas stream is then fed through pipe 472 to the CO 2 electrolysis module 430 to convert at least a portion of the gas stream. At least a portion of the converted gas stream may be supplied from the CO ₂ electrolysis module 430 to the CO consuming process 440 via conduit 432. In some embodiments, component 474 is CO and/or H2, which is supplied via conduit 476 to the CO CO. In some embodiments, the aqueous substrate is fed through conduit 482 to the H ₂ electrolysis module 480 to convert at least a portion of the aqueous substrate, and the H ₂ rich stream is fed through conduit 484 to the CO-consuming process 440. Optionally, at least a portion of the O ₂ may be supplied from the H ₂ electrolysis module 480 to the industrial process 410 through conduit 486.

- 14 040968

At least a portion of the gas stream from CO2 electrolysis module 430 may be supplied to industrial process 410 via conduit 436. In particular embodiments, said process includes an O ₂ recovery module 460 downstream of CO 2 electrolysis module ₄₃₀ to separate at least a portion of the O ₂ from the gas stream. . In those embodiments that include an O2 recovery module 460 downstream of the CO2 electrolysis module 430, the gas stream is fed through conduit 434 from the CO2 electrolysis module 430 to the O ₂ recovery module 460 . In those implementations that use the O ₂ recovery module 460 after the CO 2 electrolysis module 430, at least a portion of the gas stream is fed from the O 2 recovery module 460 to the industrial process 410 through pipe 464. In those implementations that use the O 2 recovery module 460 after the CO2 electrolysis module 430, at least a portion of the O2 reduced stream is fed from the O2 recovery module 460 to the CO consuming process via conduit 462. In some embodiments that use an _O2 recovery module 460 after the _CO2 electrolysis module 430 , at least a portion of the O ₂ depleted stream is fed from O ₂ recovery module 460 back to CO ₂ electrolysis module 430 via conduit 466. In those embodiments that do not use O ₂ recovery module 460, a portion of the gas stream may be fed from CO ₂ electrolysis module 430 into industrial process 410 through pipe 436.

In some embodiments, the CO consuming process 440 illustrated in FIG. 4 includes a reaction step for producing CO ₂ . In those embodiments where the CO-consuming process substrate gas contains CO ₂ , at least a portion of said CO-consuming process substrate gas is fed through conduit 442 to one or more purification modules 450 to remove and/or convert one or more components 458. The purified gas stream is then fed through pipe 452 to the CO ₂ electrolysis module 430 to convert at least a portion of the gas stream. In particular embodiments, the gaseous substrate after the CO-consuming process is fed through conduit 442 to the same one or more purification modules 420, which are supplied with CO2-containing gas from the industrial process 410. In various implementations, the gaseous substrate after the CO-consuming process, may be fed to one or more purification modules 420, which are supplied with CO ₂ -containing gas from the industrial process 410, and to one or more purification modules 450.

The CO consuming process 440 shown in FIG. 4 may be a gas fermentation process and may take place in an inoculator and/or in one or more bioreactors. For example, CO consuming process 440 may be a gas fermentation process in a bioreactor containing a culture of at least one d-captive microorganism. In those embodiments in which the CO-consuming process 440 is a gas fermentation process, the culture can be fermented to produce one or more fermentation products 446 and a post-fermentation gaseous substrate (CO-consuming process substrate gas).

In FIG. 5 shows a method for integrating an industrial process 510 with a purification module 520, an optional CO ₂ concentration module 570, a CO ₂ electrolysis module 530, a CO consuming process 540, an optional O ₂ recovery module 560, an optional pressure change module 580, and an optional H2 electrolysis module 1500. in accordance with one aspect of the present invention. The CO ₂ -containing gas from industrial process 510 is fed through conduit 512 to one or more purification modules 520 to remove and/or convert one or more components 528. The purified gas from one or more purification modules 520 is then fed via conduit 522 to electrolysis module 530 CO ₂ to convert at least a portion of the gas stream. In embodiments where H ₂ mixing is performed, hydrolysis-electrolysis module 1500 may provide an H2 rich gas stream through conduit 1502 to be mixed with the converted gas stream prior to being fed to CO consuming process 540.

In particular embodiments of the present invention, one or more pressure change modules 580 are provided to pressurize the converted gas from the CO2 electrolysis module 530. In those implementations that use a pressure change module 580 downstream of the CO ₂ electrolysis module 530, at least a portion of the gas stream is fed from the CO ₂ electrolysis module 530 to the pressure change module 580 through conduit 532. The pressure change module 580 provides pressurization of the gas stream and supplying the gas stream to the CO consuming process 540 via conduit 582.

In various embodiments, the H ₂ electrolysis module 1500 is embedded in the O ₂ evolution module 560 and/or in the pressure change module 580. In various embodiments, the water substrate is fed through conduit 1506 to the H ₂ electrolysis module 1500, and the H ₂ electrolysis module 1500 may provide an H ₂ enriched gas stream through conduit 1502 to be mixed with the converted gas stream prior to introducing said gas stream into the process. 540 consuming CO. In particular embodiments, H2 rich gas stream supply conduit 1502 is connected to CO enriched compressed stream conduit 582 to allow mixing of said streams. In various embodiments, the H2 electrolysis module 1500 provides an H2 rich gas stream directly to the _CO consuming process 540 through conduit 1504. .

In some embodiments, the present invention provides for the integration of industrial

- 15 040968 optional process 510, optional CO2 concentration module 570, purification module 520, CO ₂ electrolysis module 530, optional O ₂ recovery module 560, optional pressure change module 580, H ₂ electrolysis module 1500, and CO consuming process 540, according to with one aspect of the present invention. CO ₂ -containing gas from industrial process 510 is supplied through pipe 514 to an optional CO ₂ concentration module 570 to increase the concentration of CO ₂ in the gas stream and to remove one or more components 574. The optional CO ₂ concentration module 570 provides gas supply to the purification module 520 through conduit 572 to remove and/or convert one or more components 528. The purified stream is then fed through conduit 524 to an optional CO2 concentration module 570 to increase the concentration of CO2 in the gas stream and to remove one or more components 574. The optional CO2 concentration module 570 provides supplying gas through conduit 572 to CO ₂ electrolysis module 530 to convert at least a portion of the gas stream. At least a portion of the converted gas stream may be supplied to the optional O ₂ separation module 560 via conduit 534 to separate at least a portion of the O ₂ from the gas stream. At least a portion of the O2 enriched gas stream may be supplied from the optional _O2 recovery module 560 to industrial process 510 via conduit 564. At least a portion of the _O2 enriched gas stream may be supplied from _CO2 electrolysis module 530 to industrial process 510 through conduit 536. At least a portion of the O ₂ reduced gas stream may be fed from the optional O ₂ recovery module 560 to the optional pressure change module 580 through conduit 562. The gas stream from the optional pressure change module 580 through conduit 582 is fed to process 540, consumable CO. This gas stream may be mixed with the H2 rich gas stream prior to being fed to the CO-consuming process 540. Preferably, the H2 rich gas stream is supplied from the H2 electrolysis module 1500 via conduit 1502.

The CO consuming process 540 shown in FIG. 5 provides product 546. The CO consuming process may be a gas fermentation process and may take place in an inoculator and/or one or more bioreactors. For example, a CO-consuming process may include fermenting a culture to produce one or more fermentation products 546 and a post-fermentation gaseous substrate (substrate gas from the CO-consuming process). The gaseous substrate from the CO consuming process may be fed through conduit 542 to purification module 550 to remove and/or convert _one or more components 558. the substrate after the CO2-consuming process may be fed through pipe 544 to an optional CO2 concentration module 570 to increase the concentration of CO2 in the gas stream and to remove one or more components 574. The optional CO2 concentration module 570 may supply gaseous substrate after the CO2-consuming process, to a purification module 550 via conduit 572 to remove and/or convert one or more components 558. The purified gas stream may then be fed via conduit 552 to CO ₂ electrolysis module 530 to convert at least a portion of the gas stream. In specific embodiments, the gaseous substrate after the CO-consuming process is fed through conduit 542 to the same one or more purification modules 520, which are supplied with CO ₂ containing gas from the industrial process 510. In various implementations, the gaseous substrate after the CO-consuming process, may be fed to one or more purification modules 520, which are supplied with CO ₂ -containing gas from the industrial process 510, and to one or more purification modules 550.

The present invention generally provides the ability to remove components from the gas stream that may adversely affect the following processes, such as the next fermentation process, and/or the following modules. In particular embodiments of the present invention, one or more additional cleaning modules are provided between the various modules to prevent such adverse effects from occurring.

In various cases, the conversion of the CO2-containing gaseous substrate in the CO2 electrolysis module results in one or more components passing through the CO ₂ electrolysis module. In various embodiments, this results in the presence of one or more components in the CO rich stream. In some cases, the specified component contains parts of the converted O ₂ . In various embodiments, the additional purification module is a deoxygenation module to remove O ₂ from the CO rich stream.

In FIG. 6 shows the integration of a CO ₂ electrolysis module 630, an optional O ₂ recovery module 660, an optional pressure change module 680 with an additional purification module 690. In some cases, an additional purification module 690 is used after the CO ₂ electrolysis module 630. In those implementations that use an additional purification module 690 after the CO ₂ electrolysis module 630, at least a portion of the gas stream is supplied from the CO ₂ electrolysis module 630 to the additional purification module 690 through pipe 632. The additional purification module 690 provides removal and / or the conversion of one or more components 698 in the gas stream. In addition, when using the optional O ₂ recovery module 660, said O ₂ recovery module 660 provides a gas stream through pipe 662 to an additional purification module 690 for removal and / or converter

- 16 040968 these one or more components 698. Then the purified stream is fed through the pipe 692 to the optional module 680 pressure changes.

In some embodiments, the present invention integrates an industrial process 610, an optional CO ₂ concentration module 670, a purification module 620, a CO ₂ electrolysis module 630, an additional purification module 690, an optional O ₂ recovery module 660, an optional pressure change module 680, an optional module 1600 electrolysis H ₂ and the process 640, consuming CO, in accordance with one aspect of the present invention. In those embodiments that do not include an optional CO ₂ concentration module 670 between industrial process 610 and purification module 620, CO2-containing gas from industrial process 610 is fed through pipe 612 to purification module 620. In those embodiments that include an optional CO2 concentration module 670 between industrial process 610 and purification module 620, CO2 containing gas from industrial process 610 is fed through pipe 614 to an optional CO2 concentration module 670 to increase the concentration of CO2 in the gas stream and to remove one or more components 674. An optional CO2 concentration module 670 provides gas to purification module 620 via pipe 672 to remove and/or convert one or more components 628. In those embodiments that do not include CO ₂ concentration module 670, between purification module 620 and module 630 electrolysis of CO ₂ , the purified stream is fed through pipe 622 from the purification module 620 to the CO ₂ electrolysis module 630 . In those implementations that include a CO ₂ concentration module 670 between the purification module 620 and the CO ₂ electrolysis module 630, the purified stream is then fed through pipe 624 to an optional CO 2 concentration module ₆₇₀ to increase the concentration of CO ₂ in the gas stream and to remove one or more components 674. An optional CO ₂ concentration module 670 provides gas through conduit 672 to CO ₂ electrolysis module 630 to convert at least a portion of the gas stream. At least a portion of the O ₂ enriched gas stream may be supplied from CO ₂ electrolysis module 630 to industrial process 610 via conduit 636. /or conversion of one or more components 698. At least a portion of the purified gas stream can be fed through pipe 634 to an optional O ₂ separation module 660 to separate at least a portion of the O ₂ from the gas stream. At least a portion of the O ₂ enriched gas stream may be fed through pipe 664 from optional O ₂ recovery module 660 to industrial process 610. At least a portion of the gas stream may be fed from optional O ₂ recovery module 660 through pipe 662 to additional module 690 purifying to remove and/or convert one or more components 698. At least a portion of the gas stream may be supplied from the optional purifying module 690 through conduit 692 to an optional pressure change module 680. The gas stream from the optional pressure change module 680 is fed through conduit 682 to a CO-consuming process 640. This gas stream may be mixed with the H2 rich gas stream prior to being fed to the CO consuming process 640. Preferably, the aqueous substrate is supplied via conduit 1606 to the H2 electrolysis module 1600, and the _H2 enriched gas stream is supplied from the _H2 electrolysis module 1600 via conduit 1602. In various embodiments, the _H2 electrolysis module 1600 provides an H2 enriched gas stream. ₂ directly to the CO-consuming process 640 via conduit 1604. In some embodiments, O ₂ produced in H ₂ electrolysis module 1600 is fed via conduit 1608 to industrial process 610.

The CO consuming process 640 shown in FIG. 6 may produce product 646. The CO consuming process may be a gas fermentation process and may take place in an inoculator and/or one or more bioreactors. For example, a CO-consuming process may include fermenting a culture to produce one or more fermentation products 646 and a post-fermentation gaseous substrate (substrate gas from the CO-consuming process). The gaseous substrate after the CO consuming process is fed through pipe 644 to an optional CO ₂ concentration module 670 to increase the concentration of CO ₂ in the gas stream and to remove one or more components 674. The optional CO ₂ concentration module 670 provides a supply of gaseous substrate after the process consuming CO, to purification module 650 through conduit 672 to remove and/or convert one or more components 658. The purified gas stream is then fed via conduit 652 to CO ₂ electrolysis module 630 to convert at least a portion of the gas stream. In specific embodiments, the gaseous substrate after the CO-consuming process is fed through conduit 642 to the same one or more purification modules 620, which are supplied with CO2-containing gas from the industrial process 610. In various implementations, the gaseous substrate after the CO-consuming process, may be fed to one or more purification modules 620, which are supplied with CO2-containing gas from the industrial process 610, and to one or more purification modules 650.

In various embodiments of the present invention, an integrated process is provided that includes electrolysis, wherein the energy supplied to the electrolysis process is at least partially derived from a renewable energy source.

Although the substrate is usually gaseous, the substrate can also be provided

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Claims (16)

in alternative forms. For example, the substrate can be dissolved in a liquid saturated with a CO-containing gas using a microbubble dispersion generator. As a further example, the substrate may be adsorbed onto a solid support. The d-absorbing microorganism in the bioreactor is typically a carboxydotrophic bacterium. In specific embodiments, the carboxydotrophic bacteria are selected from the group consisting of Moorella, Clostridium, Ruminococcus, Acetobacterium, Eubacterium, Butyribacterium, Oxobacter, Methanosarcina, Methanosarcina, and Desulfotomaculum. In various embodiments, the carboxydotrophic bacteria is Clostridium autoethanogenum. All references, including publications, patent applications, and patents cited herein, are incorporated herein by reference to the same extent as if each reference were individually and specifically indicated to be incorporated by reference and are herein incorporated in their entirety. . The mention of any prior art in this specification is not and should not be construed as an admission that the prior art forms part of the generally known general knowledge of science. Terms in the singular used in the context of the description of the present invention (especially in the context of the following claims) should be interpreted as including the singular and plural, unless otherwise indicated herein, or clearly refuted by the context. The terms including, having, and containing are to be construed as non-limiting terms (i.e., meaning including, but not limited to), unless otherwise indicated. The term consisting essentially of limits the scope of a composition, process, or method to specific materials or steps, or to those materials and steps that do not significantly affect the basic and new characteristics of the composition, process, or method. The use of an alternative (i.e., or) should be understood to mean one, both, or any combination of the proposed options. As used herein, the term approximately means ±20% of the specified range, value, or structure, unless otherwise indicated. The listing of ranges of values in this document is only intended to be concise and separate reference to each individual value within the specified range, unless otherwise noted, and each individual value is included in this description as if it were specifically listed in this document. For example, any concentration range, percentage range, ratio range, integer range, size range, or thickness range should be understood to include the value of any integer within the specified range and, if appropriate, its fractions (e.g., one tenth and one hundredth of an integer ), unless otherwise specified. All of the methods described herein may be performed in any suitable order, unless otherwise indicated herein, or unless the context clearly refutes. The use of any or all of the examples or illustrative language (i.e., such as) provided herein is intended only to better illuminate the present invention and is not intended to limit the scope of the present invention, unless otherwise stated. Nothing in this specification should be construed as indicating an unclaimed element essential to the practice of this invention. This document describes the preferred embodiments of the present invention. Variations on these preferred embodiments will become apparent to those skilled in the art upon reading the above description. The present inventors expect those skilled in the art to make such variations appropriately, and the inventors believe that the present invention may be practiced in a manner other than specifically described herein. Accordingly, the present invention includes all modifications and equivalents of the subject matter set forth in the claims appended to this document, to the extent permitted by applicable law. In addition, any combination of the above elements in all their possible variations is covered by the invention, unless otherwise specified in this document or clearly contrary to the context. CLAIM 1. A method for improving the efficiency of carbon conversion, including: a) supplying a CO ₂ containing gaseous substrate from the industrial process to a first purification module to remove at least one component from the CO ₂ containing gaseous substrate to obtain a first purified CO ₂ gas stream; b) supplying a first purified CO2 gas stream to a CO2 concentration module to obtain a first concentrated CO2 gas stream and a first CO2 reduced stream containing CO and/or H ₂ ; c) supplying a first concentrated CO ₂ gas stream to a CO ₂ electrolysis module to convert at least a portion of the first concentrated CO ₂ gas stream to obtain a first CO rich stream and a first O ₂ rich stream; - 18 040968 d) feeding at least a portion of the first CO-rich stream to a bioreactor containing a culture of at least one d-absorbing microorganism; e) feeding at least a portion of the first CO2 reduced stream to the bioreactor; f) fermenting the culture to produce one or more fermentation products and a tail gas stream containing CO ₂ ; g) feeding at least a portion of the tail gas stream to the first purification module or to the second purification module to remove at least one component selected from H2S, acetone and mixtures thereof, to obtain a purified tail gas stream containing CO ₂ ; h) feeding at least a portion of the cleaned tail gas stream to a carbon dioxide electrolysis module to convert at least a portion of the carbon dioxide to form a second CO rich stream and an O2 rich stream; And i) feeding at least a portion of the second CO rich stream to the bioreactor. 2. The method of claim 1, further comprising supplying a CO ₂ -containing gaseous substrate from the industrial process to the pressure modulation module to obtain a compressed CO 2 -containing gas stream and then supplying the compressed CO ₂ -containing gas stream to the first purification module. 3. The method of claim 1 further comprising feeding at least a portion of the first O ₂ rich stream directly into the industrial process. 4. The method of claim 1, wherein the first CO ₂ reduced stream contains CO and/or H ₂ , and said method further comprises feeding at least a portion of the first CO ₂ reduced stream to the bioreactor. 5. The method of claim 1, comprising feeding at least a portion of the CO enriched stream to a pressure modulation module to form a compressed CO stream and feeding at least a portion of the compressed CO stream to the bioreactor. 6. The method of claim 1, further comprising supplying an aqueous substrate to the H ₂ electrolysis module to produce an H 2 rich stream and feeding at least a portion of the H ₂ rich stream to a CO consuming process. 7. The method according to claim 1, characterized in that at least a part of the tail gas containing CO ₂ is supplied to the pressure change module to obtain a compressed tail gas stream, and the compressed tail gas stream is supplied to the first purification module. 8. The method according to claim 1, characterized in that the CO ₂ -containing gaseous substrate from the industrial process additionally contains one or more of CO, H ₂ and CH ₄ . 9. The method according to claim 1, characterized in that the industrial process is selected from the group containing carbohydrate fermentation, cement production, pulp and paper production, steel making, oil refining, petrochemical production, coke production, anaerobic or aerobic decomposition, gasification, mining natural gas, oil extraction, metallurgical processes, production and/or refining of aluminium, copper and/or iron alloys, Fischer-Tropsch processes, methanol production, pyrolysis, steam methane reforming, dry methane reforming, partial oxidation of biogas or natural gas and autothermal reforming biogas or natural gas. 10. The method of claim 1, wherein the first purification module is selected from the group consisting of a hydrolysis module, an acid gas removal module, a deoxygenation module, a catalytic hydrogenation module, a solids removal module, a chloride removal module, a tar removal module, and a purification of hydrogen cyanide. 11. The method according to claim 1, characterized in that at least one component removed from the CO2-containing gaseous substrate is selected from the group consisting of sulfur compounds, aromatic compounds, alkynes, alkenes, alkanes, olefins, nitrogen compounds, oxygen, phosphorus-containing compounds, fine particles, solids, halogenated compounds, silicon compounds, carbonyls, metals, alcohols, esters, ketones, peroxides, aldehydes, ethers, tar and naphthalene. 12. The method according to claim 1, characterized in that the fermentation product is selected from the group consisting of ethanol, butyrate, 2,3-butanediol, lactate, butene, butadiene, methyl ethyl ketone, ethylene, acetone, isopropanol, lipids, 3-hydroxypropionate, terpenes, fatty acids, 2-butanol, 1,2-propanediol and 1-propanol. 13. The method according to claim 1, characterized in that the first and/or second CO-rich stream contains at least a portion of oxygen, and at least a portion of the CO-enriched stream is fed to a deoxygenation module to remove at least a portion of the oxygen from a stream with a high content of carbon monoxide. 14. The method according to claim 1, characterized in that the d-absorbing microorganism is a carboxydotrophic bacterium. 15. The method according to claim 14, wherein the carboxydotrophic bacterium is selected from the group consisting of Moorella, Clostridium, Ruminococcus, Acetobacterium, Eubacterium, Butyribacterium, Oxobacter, Methanosarcina and Desulfotomaculum. 16. The method according to claim 15, characterized in that the carboxydotrophic bacterium is Clos -