Syngas generation process and carbon monoxide electrolysis

Abstract

Disclosed herein are methods and systems related to the use of electrolysis to enhance synthesis gas production. Methods disclosed herein include harvesting a volume of carbon monoxide from a syngas production system operated using a volume of natural gas, feeding the volume of carbon monoxide to a cathode region of an electrolyzer, and generating a volume of the generated chemical using the volume of carbon monoxide and the electrolyzer. The volume of the generated chemical is at least one of a volume of a hydrocarbon, a volume of an olefin, a volume of an organic acid, a volume of an alcohol, and a volume of an N-rich organic compound.

Description

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS

[0002] This application claims priority to U.S. Patent Application No. 17 / 980,912 filed on November 4, 2022 (which application claims the benefit of U.S. Provisional Patent Application No. 63 / 322,638 filed on March 22, 2022) and U.S. Provisional Patent Application No. 63 / 351,442 filed on June 13, 2022, all of which are incorporated herein by reference in their entirety for all purposes. Background Art

[0003] There is an urgent need to reduce emissions associated with the production of useful fuels and chemicals in our society. In addition, clean-burning (i.e., burning without producing gaseous carbon) fuels need to be widely adopted to replace fossil fuels used throughout society. Therefore, processes for generating dihydrogen gas (hereinafter also referred to as "hydrogen gas") and syngas with low carbon dioxide (CO2) emissions are key technologies for building future sustainable fuel and chemical production platforms.

[0004] Hydrogen can be used as an energy source in various reactors, including fuel cells and dihydrogen combustion systems. It can also be used in a variety of industrial processes, and particularly chemical processes. Dihydrogen gas burns cleanly, but first requires a large amount of energy to generate. The process required to generate this large amount of energy may involve the generation of carbon byproducts in a counterintuitive way. Dihydrogen gas can be classified according to the impact of producing dihydrogen gas on the environment. Gray hydrogen is dihydrogen produced using a process that emits carbon byproducts into the atmosphere, thereby offsetting the benefits of using dihydrogen as a hydrocarbon fuel substitute to a certain extent. Blue hydrogen is dihydrogen produced using a process that generates carbon byproducts, but captures and sequesters the carbon byproducts instead of emitting them into the atmosphere. Green hydrogen is dihydrogen produced without or with very limited carbon byproducts, such as by using renewable energy to power a process that generates dihydrogen by water electrolysis.

[0005] Synthesis gas is a mixture of dihydrogen (H2) and carbon monoxide (CO) in various ratios. The gas usually also includes CO2 and methane (CH4). Synthesis gas can be used as a raw material for the production of dihydrogen gas or as a raw material for the production of chemicals or synthetic fuels. Synthesis gas can also be used directly as a fuel for power generation or as a raw material for internal combustion engines.

[0006] Different technologies can be used to produce dihydrogen and synthesis gas. Synthesis gas can be generated by processing various raw materials containing carbon and hydrogen atoms (such as natural gas, hydrocarbons, biomass or certain waste products). The process for generating synthesis gas from these raw materials can be called a synthesis gas generation process. For example, natural gas can be processed to separate dihydrogen from methane and other hydrocarbons in natural gas. The remaining carbon bonds with oxygen and produces carbon monoxide and carbon dioxide, collectively referred to as carbon oxides. Synthesis gas can be produced with various ratios of dihydrogen gas and carbon oxides, depending on the application in which the synthesis gas will be used. In specific applications, when all carbon oxides are removed to produce pure dihydrogen gas, the ratio is zero. In these applications, a synthesis gas generation process can be used to generate blue hydrogen from synthesis gas, which first generates synthesis gas in a way that captures carbon, and further separates and captures carbon oxides from the synthesis gas to separate pure dihydrogen gas.

[0007] Currently, blue hydrogen has advantages over green hydrogen from an economic perspective and the maturity of related technologies. Blue hydrogen also has significant advantages over gray hydrogen in terms of environmental impact. Therefore, blue hydrogen is expected to play an important role in the scale-up of the global hydrogen power infrastructure due to its scalability and relatively low cost. However, the unresolved issue of using blue hydrogen is the cost of carbon capture and the low likelihood that such costs will decrease over time. It is reported that capturing carbon dioxide from the blue hydrogen process increases the final cost of hydrogen by 30% to 100%, with a total cost of about $1.40 to $2.40 per kilogram of blue hydrogen compared to gray hydrogen, which can cost as little as $1.00 per kilogram. As a result, there are many facilities that produce syngas or generate syngas specifically for hydrogen production that are not equipped with carbon capture and storage facilities, but simply emit the produced carbon dioxide into the atmosphere. Summary of the invention

[0008] Disclosed herein are methods and systems related to enhancing syngas generation processes using electrolysis. In specific embodiments, carbon monoxide generated from a syngas production system is harvested directly or indirectly for use in an electrolyzer to produce at least one of hydrocarbons, olefins, organic acids, alcohols, or N-rich organic compounds.

[0009] In a specific embodiment of the present invention, a method is provided. The method includes harvesting a certain volume of carbon monoxide from a synthesis gas production system, supplying the certain volume of carbon monoxide to the cathode region of an electrolyzer, and using the certain volume of carbon monoxide and the electrolyzer to generate a certain volume of generated chemicals. In a specific embodiment of the present invention, the electrolyzer is a dedicated electrolyzer, which is designed for electrochemical reduction of carbon monoxide, as described in the following specific embodiments. The certain volume of generated chemicals is at least one of the following: a certain volume of hydrocarbons, a certain volume of organic acids, a certain volume of alcohols, a certain volume of olefins, and a certain volume of N-rich organic compounds.

[0010] In a specific embodiment of the present invention, a system is provided. The system includes: a syngas production system configured to produce a certain volume of syngas; a first connector, which is fluidly connected to the syngas output of the syngas production system; a separation system, which is fluidly connected to the first connector and configured to separate a certain volume of carbon monoxide from the certain volume of syngas; a second connector, which is fluidly connected to the carbon monoxide output of the separation system; and an electrolyzer having a cathode input fluidly connected to the second connector and configured to generate a certain volume of generated chemicals from the certain volume of carbon monoxide. The certain volume of generated chemicals is at least one of the following: a certain volume of hydrocarbons, a certain volume of organic acids, a certain volume of alcohols, a certain volume of olefins, and a certain volume of N-rich organic compounds.

[0011] In a specific embodiment of the invention, a method is provided. The method includes supplying a volume of carbon dioxide and a volume of natural gas to a reforming process. The method also includes harvesting a volume of carbon monoxide from the reforming process. The method also includes supplying the volume of carbon monoxide to a cathode region of an electrolyzer and using the volume of carbon monoxide and the electrolyzer to generate a volume of generated chemicals. BRIEF DESCRIPTION OF THE DRAWINGS

[0012] Figure 1 A flow chart showing a set of methods for enhancing a syngas production system according to specific embodiments of the invention disclosed herein.

[0013] Figure 2A A system for enhancing a syngas production system according to specific embodiments of the invention disclosed herein is shown.

[0014] Figure 2B A system for enhancing a syngas production system using recycled dihydrogen gas according to specific embodiments of the invention disclosed herein is shown.

[0015] Figure 3A A system for enhancing a syngas production system according to a specific embodiment of the invention disclosed herein is shown, comprising a water-gas shift reactor.

[0016] Figure 3B Another system for enhancing a syngas production system according to specific embodiments of the invention disclosed herein is shown and includes a water-gas shift reactor.

[0017] Figure 4A A system for enhancing a syngas production system using a reforming reactor according to specific embodiments of the invention disclosed herein is shown.

[0018] Figure 4BA system for enhancing a syngas production system using a gasification reactor is shown in accordance with specific embodiments of the invention disclosed herein.

[0019] Figure 4C A system for enhancing a syngas production system using oxygen collected from the output of an electrolyzer as an input to a partial oxidation reactor is shown in accordance with specific embodiments of the invention disclosed herein.

[0020] Figure 4D A system for enhancing a syngas production system according to a specific embodiment of the invention disclosed herein is shown that uses parasitic hydrogen collected from the output of an electrolyzer to increase dihydrogen production of the system.

[0021] Figure 5 Shown is an exploded view of an electrolyzer that may be used in accordance with specific embodiments of the invention disclosed herein.

[0022] Figure 6 Shown is a set of electrolyzer reactions that may be used in accordance with specific embodiments of the invention disclosed herein.

[0023] Figure 7 A second set of electrolyzer reactions that may be used in accordance with specific embodiments of the invention disclosed herein are shown.

[0024] Figure 8 An electrolyzer using a diaphragm as a separator element according to a specific embodiment of the invention disclosed herein is shown. DETAILED DESCRIPTION

[0025] Disclosed herein in detail are methods and systems related to enhancing the synthesis gas generation process using electrolysis according to the above overview. The methods and systems disclosed in this section are non-limiting embodiments of the present invention, are provided for explanation purposes only, and should not be used to limit the full scope of the present invention. It should be understood that the disclosed embodiments may or may not overlap with each other. Therefore, an embodiment or a portion of its specific embodiment may or may not fall within the scope of another embodiment or its specific embodiment, and vice versa. Different embodiments from different aspects may be combined or practiced separately. Many different combinations and sub-combinations of the representative embodiments shown within the broad framework of the present invention may be obvious to those skilled in the art but are not explicitly shown or described and should not be interpreted as being excluded.

[0026] The production of synthesis gas or pure dihydrogen gas can involve a synthesis gas generation process that results in the generation of carbon monoxide. Carbon monoxide can be generated in a synthesis gas generation reaction, wherein a mixture of dihydrogen, carbon monoxide and possible other chemicals is generated. Other chemicals may include carbon dioxide and other carbon-containing chemicals. The term "synthesis gas generation reaction" is used with reference to the fact that the raw material has been at least partially generated as synthesis gas. The reaction can be part of a further reaction, wherein the final composition of dihydrogen and carbon monoxide is reached, or all dihydrogen has been separated out to form pure dihydrogen gas. According to specific embodiments of the present invention disclosed herein, the carbon monoxide product generated during this synthesis gas generation reaction can be harvested for specific purposes.

[0027] Harvesting carbon monoxide from synthesis gas generation reaction can be direct harvest or indirect harvest.In indirect harvest, the carbon monoxide from synthesis gas generation reaction can be piped to storage tank, then sealed.Then, the tank can be transported to the location where carbon monoxide will be utilized or stored locally for later use.On the contrary, in direct harvest, the carbon monoxide generated from synthesis gas can be directly piped to the electrolyzer or other systems (for example, one or more intermediate steps can be performed before carbon monoxide is transported to electrolyzer) where carbon monoxide will be utilized from the reactor or other systems where synthesis gas generation reaction occurs therein.In a specific embodiment of the present invention, two systems (for example, reactor and electrolyzer) can be located in a single industrial facility.In fact, in a specific embodiment of the present invention, existing synthesis gas or dihydrogen production facilities can be enhanced using system disclosed herein, so that carbon monoxide can be directly harvested, otherwise carbon monoxide will be directly discharged into the atmosphere or first converted into carbon dioxide and then discharged into the atmosphere from those facilities.

[0028] Figure 1 A flow chart 100 is included for a group of methods for enhancing a synthesis gas production system according to a specific embodiment of the present invention disclosed herein. Flow chart 100 includes a step 101 of harvesting a certain volume of carbon monoxide from a synthesis gas production system. The synthesis gas production system can be operated using a certain volume of natural gas, biomass, waste (e.g., biowaste, plastic, waste mixture) or other raw materials. Natural gas can be in liquefied or gaseous form, and the term "gas" used in this phrase is not meant to limit the state of natural gas to gaseous form. As known to those of ordinary skill in the art, natural gas can be transported and processed in liquefied form, while still using the term "natural gas" to refer to natural gas (i.e., liquefied natural gas). In this disclosure, the term "fluid" will be used to refer to a substance describing any physical form, including liquid, gaseous, supercritical, or a combination of liquid and gaseous forms.

[0029] The synthesis gas production system can be a part of the dihydrogen production line 110 utilizing the synthesis gas generation process. The synthesis gas production system may include a synthesis gas generation process, which generates a certain volume of dihydrogen (such as dihydrogen gas) and a certain volume of carbon monoxide. Harvesting may involve harvesting the entire volume of carbon monoxide generated by the synthesis gas production system or a part of the certain volume of carbon monoxide generated by the synthesis gas production system. The certain volume of carbon monoxide can be harvested as a part of a stream containing carbon monoxide, wherein the certain volume of carbon monoxide is mixed with other chemicals or impurities. As described elsewhere herein, the "volume" of the term substance (e.g., the volume of carbon monoxide) is not meant to indicate a separate, different and purified physical volume, but means to refer to a collection of substances in the same sense, a cup of coffee containing one tablespoon of milk contains "a certain volume" of milk, wherein the volume is one tablespoon.

[0030] The harvest of carbon monoxide can be direct harvest and all steps of flow chart 100 can be performed in a single facility. The collection of carbon monoxide can be performed according to the synthesis gas production system. For example, the dihydrogen production line 110 can be in the same facility with the electrolyzer 120, and the carbon monoxide generated by the dihydrogen production line 110 can be harvested and provided directly to the electrolyzer 120, or one or more intermediate steps between 110 and 120 can be used to pre-treat it before the stream containing CO is fed into the electrolyzer. The synthesis gas production system can be fluidly connected to a separation system for harvesting carbon monoxide from synthesis gas. Fluid connection can be provided by one or more valves, one or more seals, and / or one or more regulators or other instruments in the pipeline or by coupling the output of the synthesis gas production system to other connectors in the area where carbon monoxide will be used. Alternatively, the harvest of carbon monoxide can be indirect harvesting, wherein the regional fluid for generating the process of this certain volume of carbon monoxide is connected to one or more storage tanks, and these storage tanks store carbon monoxide for transportation and / or use at a later time. In either case, the machinery in which the syngas generation process is performed and the machinery in which the carbon monoxide is utilized in the electrolysis process can be in a single industrial facility such as a refinery, biorefinery, chemical plant, industrial laboratory, waste treatment plant or other facility. Carbon monoxide can be harvested from the process in a variety of ways as described below.

[0031] In a specific embodiment of the invention, carbon monoxide can be separated from the synthesis gas generated by the synthesis gas production system. Carbon monoxide can be separated from the synthesis gas using a variety of methods, such as separation using membranes, cryogenic separation, separation methods based on the different physical or chemical properties of the synthesis gas components, separation based on pressure swing adsorption, temperature swing adsorption, vacuum or vacuum pressure swing adsorption, or separation based on absorption. For example, a separation system can be used for the synthesis gas, first cooling the synthesis gas to remove impurities, and then heating the synthesis gas to evaporate the purified dihydrogen through a membrane that filters out carbon monoxide.

[0032] The system for performing the above-mentioned separation steps and processes can take various forms. The separation system can perform one or more of the multiple separation / purification steps, including any technology that can be used for the target purification / separation. The separation system may include a separation unit based on but not limited to the following technologies: membrane technology, including but not limited to dense polymer membranes, ultrafiltration and nanofiltration membranes, facilitated transport membranes, metal membranes, hollow fiber pervaporation membranes; cryogenic technology; adsorption technology, including but not limited to physical adsorption and chemical adsorption technology; absorption technology, including physical absorption technology and chemical absorption technology; its operation technology such as but not limited to vacuum voltage swing, temperature swing, voltage swing, dry voltage swing, voltage and temperature swing coupling, electric swing. The chemical adsorbents that can be used include but are not limited to amine-based adsorbents (amine-grafted or impregnated solids), metal oxides, metal salts, complex salts and hydrotalcites. The physical adsorbents that can be used include but are not limited to materials such as carbon-based materials, mesoporous silica, zeolites, zeolite imidazolate frameworks (ZIFs), metal organic frameworks (MOFs), and mixed adsorbents.

[0033] The crude synthesis gas may have a ratio of dihydrogen to carbon monoxide of 1 to 5, depending on the feedstock and the process for generating synthesis gas. The method for changing the ratio can be used to produce a concentrated stream of dihydrogen and carbon monoxide. In a specific embodiment of the present invention, the process for generating carbon monoxide does not need to extract all carbon monoxide from the synthesis gas and only leave pure dihydrogen. In fact, if the purpose of the overall process is to produce a synthesis gas with a certain ratio of carbon monoxide to dihydrogen, the harvest and separation steps disclosed herein can be calibrated to remove only a portion of carbon monoxide in the synthesis gas product. In these methods, the process of harvesting this certain volume of carbon monoxide may include supplying a certain volume of synthesis gas from a synthesis gas production system to a separation system, and using a separation system to separate a certain volume of dihydrogen and this certain volume of carbon monoxide from this certain volume of synthesis gas, to leave a second volume of synthesis gas. The separation system may be configured to separate this certain volume of carbon monoxide from this certain volume of synthesis gas, to achieve a target ratio of carbon monoxide to hydrogen in the second volume of synthesis gas.

[0034] In a specific embodiment of the present invention, the synthesis gas generation process that generates a certain volume of carbon monoxide can take various forms.Synthesis gas can be produced using various raw materials and various processes.The process for generating synthesis gas includes reforming technology, oxidation or partial oxidation (POX) technology and gasification of biomass or waste (e.g., biowaste, plastics or any waste containing rich carbon molecules).Reforming technology can be further subdivided into steam reforming, such as steam methane reforming (SMR), autothermal reforming (ATR) and dry reforming technology.Some reforming technologies that are in less advanced development stages also involve the use of plasma.The raw materials for reforming and partial oxidation technology can be natural gas including methane, or any carbon raw materials including naphtha and other hydrocarbon fuels.Carbon dioxide can also be used as a co-reactant of the above-mentioned technology.The raw materials for gasification technology can include biomass and / or waste, such as biowaste, plastics or any waste containing rich carbon molecules, or any of the above-mentioned raw materials.

[0035] The technology and feedstock selected will have an impact on the ratio of carbon to dihydrogen gas ultimately produced. If the goal is to produce dihydrogen gas, SMR is an advantageous process because it generates the highest ratio of dihydrogen to carbon in the output with methane as input. Throughout this disclosure, examples of natural gas and methane are used as examples of feedstocks for the synthesis gas generation process described herein. However, other feedstocks described above may be used in place of them.

[0036] The equations for the various technologies described in the previous paragraphs are provided below, where methane from natural gas serves as a feedstock in each example. Specifically with respect to natural gas and methane, the above-mentioned reforming technologies may be referred to as SMR, autothermal reforming, and dry methane reforming (DMR). In SMR, methane from natural gas is heated with steam, and usually with a catalyst, to produce a mixture of carbon monoxide and dihydrogen. Blue hydrogen may be produced using a process involving the generation of synthesis gas, using a synthesis gas generation process in the form of an SMR. SMR may be performed with methane gas as a feedstock, followed by a water-gas shift reaction (WGSR), in which carbon monoxide from the synthesis gas reacts with water to produce additional dihydrogen gas and carbon dioxide gas. The equations for SMR and WGSR are as follows:

[0037] SMR: CH4 + H2O ->3H2 + CO (1)

[0038] WGS: CO + H2O <-> CO2 + H2 (2)

[0039] ATR can be performed with water or CO2 as a co-reactant. The ATR equation with CO2 as a co-reactant and water as a co-reactant is:

[0040] ATR (using CO2): 2CH4 + O2 + CO2 -> 3H2 + 3CO + H2O (3)

[0041] ATR (using H2O): 4CH4 + O2 + 2H2O -> 10H2 + 4CO (4)

[0042] Dry methane reforming also utilizes carbon dioxide as a co-reactant and can be performed according to the following equation:

[0043] CH4 + CO2 → 2CO + 2H2 (5)

[0044] In the case of POX with methane as feedstock, the partial oxidation of methane is performed according to the following equation:

[0045] CH4 + 0.5O2 → CO + 2H2 (6)

[0046] The choice of syngas generation process for a given production line depends on the available fossil feedstock and the target syngas ratio. For example, SMR is used to produce a hydrogen-rich syngas stream with a typical H2 / CO ratio of 3:1 to 5:1. ATR is used to produce a hydrogen-rich syngas stream with a typical H2 / CO ratio of 1:1 to 2.5:1. POX is used to produce a syngas stream with a typical H2 / CO ratio of 1.6 to 1.8.

[0047] Gasification involves the thermal treatment of feedstock materials at high temperatures without complete combustion, particularly via the controlled introduction of oxygen or steam. Gasification for the production of dihydrogen in the synthesis gas production process can be represented by the following equation:

[0048] Energy-rich substrate for gasification → x H2 + y CO(7)

[0049] Figure 2AA system 200 for enhancing a synthesis gas generation process according to a specific embodiment of the present invention disclosed herein is shown. The system includes a synthesis gas production system 201, which is configured to produce a certain volume of synthesis gas using a synthesis gas generation process. Raw material 202 can be natural gas, biomass, biowaste, carbon-rich waste or other raw materials for synthesis gas production as described herein. In an embodiment in which the raw material 202 for the synthesis gas production process is at least one of biomass, biowaste or any carbon-rich waste, the synthesis gas production system 201 can be a gasification system and the synthesis gas generation process performed by the synthesis gas production system can be a gasification process. In an embodiment in which the raw material 202 is natural gas, the synthesis gas production system 201 can be a reforming system such as a steam methane reforming system, a dry reforming system or an autothermal reforming, or an oxidation system such as a partial oxidation system. The synthesis gas production system 201 can be configured to convert the raw material 202 into synthesis gas 203 using any of the above processes. The syngas 203 may then be passed through a first connector 204 and delivered to a separation system 205, which may be used to harvest carbon monoxide 206 from the syngas 203, such as in step 101 as described above. The first connector 204 may also carry carbon dioxide and other impurities with the syngas 203. The carbon monoxide 206 may be provided to a second connector 207 from the carbon monoxide output of the separation system 205. The separation system may be designed to separate at least a portion of the carbon monoxide from the syngas and deliver the low-carbon syngas or pure dihydrogen gas 208 out of a different pipeline or manifold. In the example shown, pure dihydrogen gas is generated and delivered out of a separate pipeline or connector 211.

[0050] Figure 2A Represents a system that can perform a specific implementation, wherein the harvest of the certain volume of carbon monoxide as in step 101 can include a step 251 of supplying a certain volume of synthesis gas from a synthesis gas production system to a separation system, and a step 252 of separating a certain volume of dihydrogen and the certain volume of carbon monoxide from the certain volume of synthesis gas using the separation system. In the illustrated case, the certain volume of dihydrogen is pure dihydrogen gas 208 collected on a separate pipeline or connection 211. However, in alternative embodiments, depending on the raw materials used for the system, the synthesis gas generation process and the separation system, the certain volume of dihydrogen gas can alternatively be dihydrogen with a low carbon content, including low carbon dihydrogen gas (i.e., dihydrogen gas and a remaining amount of carbon). The low carbon dihydrogen gas can then be used as synthesis gas for a specific process requiring a ratio of the obtained carbon to dihydrogen or for further purification.

[0051] Flowchart 100 also includes a step 102 of supplying the volume of carbon monoxide to the cathode region of the electrolyzer. This step may involve supplying a volume of carbon monoxide to the cathode input of the electrolyzer at the cathode input of the electrolyzer. The volume of carbon monoxide may be mixed with another fluid to form the cathode input fluid, or may remain pure so that the cathode input fluid is pure carbon monoxide. This step may involve transporting a carbon monoxide tank from an area where the carbon monoxide is harvested and connecting it to a connector or pipeline connected to the cathode region of the electrolyzer. This step may also involve temporarily storing the carbon monoxide in the tank until the price of electricity drops, and then doing so when it becomes more economical to supply the stored carbon monoxide to the electrolyzer. Alternatively, this step may involve conveying the carbon monoxide directly from the syngas production system to the electrolyzer in the same industrial facility via a connector or pipeline. The electrolyzer may have the following reference Figures 5 to 7 The features described. The connector or pipeline may include seals and valves that allow carbon monoxide to be controllably delivered to the electrolyzer as a cathode input fluid. The connector or pipeline may allow alternative fluids (such as water or other raw materials or impurities from the synthesis gas production process) to be mixed with carbon monoxide to form a cathode input fluid for the electrolyzer. This is illustrated by the connector 218 that carries the alternative chemical 217 to the electrolyzer assembly 209. In Figures 2 to 4, the top of the electrolyzer represents the cathode input to the cathode region of the electrolyzer, and the left side of the electrolyzer represents the anode input to the anode region of the electrolyzer. In a specific embodiment of the present invention, the contents of connector 218 and connector 207 can be mixed before being provided to the electrolyzer assembly. The connector or pipeline may allow carbon monoxide to be alternatively delivered to other systems, such as other electrolyzers or water-gas shift systems. Valves and seals and any other necessary instruments may be configured to deliver carbon monoxide to one system at a first time, and then deliver carbon monoxide to a second system at a second time. A connection or conduit may be coupled to an accumulation tank or set of tanks located between the electrolyzer and the syngas production system to accumulate excess carbon monoxide in the event of any difference between the rates of the syngas production system and the electrolyzer. Such an accumulation tank or set of tanks may also be used to temporarily store carbon monoxide during periods of high electricity costs.

[0052] Flowchart 100 also includes a step 103 of using the volume of carbon monoxide and the electrolyzer to generate a volume of generated chemicals. For example, electrolyzer 209 can use carbon monoxide 206 to produce generated chemicals 216. The volume of generated chemicals can be at least one of the following: a volume of hydrocarbons, a volume of organic acids, a volume of alcohols, and a volume of N-rich organic compounds. Using the process shown, the carbon content of the syngas can be reduced, optionally until pure dihydrogen gas is produced from the syngas, and the carbon monoxide can be value-added to produce useful chemicals that can be used as raw materials in other industrial processes or other useful applications. The disclosed method and system can be used to enhance existing syngas production facilities, including those facilities that would otherwise emit any excess carbon monoxide or would use carbon monoxide to obtain additional dihydrogen gas through the water-gas shift reaction and thereby emit carbon dioxide. Using these processes, the generation of blue hydrogen can be more economically competitive than the production of gray hydrogen, because the market value of the generated chemicals can offset the operating costs of the electrolyzer, and the use of carbon monoxide to generate these chemicals can eliminate the cost of carbon storage. In a specific embodiment of the invention, the electrolyzer can be operated using dihydrogen gas as an input without the need for external energy or with the addition of only a small amount of external energy. In a specific embodiment of the invention, the dihydrogen gas used for this purpose can be dihydrogen gas separated from synthesis gas. In an alternative embodiment, as described below, the dihydrogen gas can be dihydrogen gas that is parasitically generated by the electrolyzer and then circulated from the cathode output of the electrolyzer to the anode input of the electrolyzer. For example, Figure 2B The system 220 in FIG. 1 shows the circulation of dihydrogen 221 on a connection 222 that connects the cathode output to the anode input, so that the dihydrogen parasitically generated at the cathode output is circulated by supplying it at the anode input to be used as an oxidation substrate. In an alternative embodiment, a portion of the dihydrogen 208 would have been supplied alternatively to serve as an oxidation substrate.

[0053] Although Figure 2A The system shown in includes a single separation system and a single electrolyzer, but many different variations are possible. For example, multiple separation systems can be connected in series to separate a volume of low-carbon dihydrogen synthesis gas with increasing purity levels, and one or more of the multiple separation systems can be coupled to a single electrolyzer to deliver carbon monoxide. As another example, multiple such separation systems can be coupled to a group of electrolyzers that are configured to accept cathode inputs with different levels of carbon monoxide volume or concentration.

[0054] System 200 includes electrolyzer 209, which has a cathode input connected to second connector 207 for receiving a certain volume of carbon monoxide 206. The electrolyzer represents the cathode input with the top line of the block, and uses the left line of the block as the anode input. In a specific embodiment, the electrolyzer may also include a cathode output and an anode output to receive output fluids from the cathode region and the anode region. In a specific embodiment, the electrolyzer may also include a separation region output from the separation region of the electrolyzer, which is arranged between the cathode region and the anode region and provides a way to capture other generated chemicals. In a specific embodiment, chemicals will be captured from both the separation region output and the anode or cathode output. In a specific embodiment, multiple chemicals can be captured in both liquid and gaseous forms from any of these outputs. For example, the generated chemicals of this certain volume may include a certain volume of gaseous hydrocarbons and a certain volume of liquid products, and the liquid products include at least one of liquid organic acids and liquid alcohols. This certain volume of gaseous hydrocarbons can be captured from the cathode output of the electrolyzer. This volume of liquid product may then be captured by a trap on the cathode output, or if the electrolyser includes a separation region, may be captured via the separation region output.

[0055] The electrolyzer may receive a volume of fluid at a cathode input and a separate volume of fluid at an anode input. The electrolyzer may convert the carbon monoxide received at the cathode input into beneficial and valuable chemicals by electrolysis. In specific embodiments of the invention disclosed below, additional chemicals, such as nitrogen-containing reactants such as ammonia, water, electrolyte water, or steam, may be provided to the cathode input along with the carbon monoxide. For example, these additional chemicals may be provided via connector 218 or combined with the carbon monoxide in connector 207 before being provided to the electrolyzer assembly 209. In specific embodiments of the invention disclosed below, different chemicals, including one or more of water, electrolyte, oxidation substrate, and dihydrogen gas, may be provided to the anode region. The dihydrogen gas may be dihydrogen gas taken from a syngas generation process or dihydrogen gas supplied separately. The dihydrogen gas may also be parasitic dihydrogen produced in the cathode region that is circulated from the cathode output of the electrolyzer back to the anode input of the electrolyzer. In Figure 2A In the embodiment of the present invention, the electrolyzer 209 receives water 212 from a connection 213 at the anode input and receives an oxidized substrate 214 from a connection 215 at the anode input. In a specific embodiment of the present invention, additional chemicals (such as water) and the oxidized substrate can be combined and provided to the electrolyzer assembly via a single connection. The water provided to the anode input or the cathode input can be provided by a water source. The water source can provide a fluid flow including water. The water from the water source can be pure deionized water, electrolyte water, or water mixed with any other chemicals.

[0056] The generated chemicals can be removed from the electrolyzer in liquid or gaseous form from the generated chemical output. The generated chemical output can be fluidly coupled to a separate region of the electrolyzer. Figure 2A In the embodiment, useful chemicals 216 are removed from the electrolyzer via an output collected from the cathode output stream from the cathode region. In alternative embodiments disclosed below, useful chemicals may be collected via a separate region between the anode region and the cathode region of the electrolyzer.

[0057] It is noteworthy that the step of performing water gas shift to harvest more dihydrogen using carbon monoxide is missing in flow chart 100. In fact, although some processes represented by flow chart 100 can be used in combination with processes utilizing water gas shift as described below, these processes do not need to use water gas shift, and alternatively using carbon monoxide as a raw material for the electrolysis process rather than as a raw material for the water gas shift reaction is a key aspect of the specific embodiments of the present invention disclosed herein. In these specific embodiments of the present invention, carbon monoxide in the total volume of natural gas used as a raw material for the synthesis gas generation process is not used in the water gas shift reaction. For example, raw material 202 can be a certain volume of natural gas, and carbon monoxide derived from the certain volume of natural gas will not be used in the water gas shift reactor. On the contrary, all carbon monoxide can be used as a certain volume of carbon monoxide 206. In these embodiments, the synthesis gas production system (e.g., synthesis gas production system 201) can be an SMR reactor and can perform an SMR process on a certain volume of natural gas. In these embodiments, pure dihydrogen can be the desired output of the system. However, according to the specific embodiments disclosed below, the carbon monoxide can be used in the electrolyzer instead of in the water gas shift reactor to produce more dihydrogen. As described below, in alternative embodiments, at least a portion of the carbon monoxide in the connector 204 can be used for the WGS reaction, and another portion of the carbon monoxide in the connector 204 can be provided to the electrolyzer component.

[0058] Particular benefits arise from methods where the WGS reaction operated using carbon monoxide from the syngas generation process is replaced with an electrolyzer operated using carbon monoxide from the syngas generation process. In such systems where the syngas generation system is used to ultimately produce dihydrogen, it is of interest to also increase the ratio of dihydrogen gas to carbon monoxide compared to that produced by the syngas generation production driven via the first SMR. To this end, a WGS reaction step is added for producing additional H2 from CO according to the following reaction:

[0059] WGS: CO + H2O → CO2 + H2 (8)

[0060] In the case of SMR coupled with WGS, the overall equation is:

[0061] SMR + WGS: CH4 + 2H2O → 4H2 + CO2 (9)

[0062] This combined process allows four moles of dihydrogen gas to be produced for every mole of methane, rather than just three moles of dihydrogen gas without the WGS step. However, this step comes at the cost of producing one mole of carbon dioxide for every additional mole of dihydrogen produced. Therefore, in order for this dihydrogen to become blue hydrogen, the carbon dioxide must be captured and permanently stored, which is expensive. Assuming the process of Equation 9 is used and all carbon dioxide is emitted, the cost of gray hydrogen (C 灰H2 ) is $1,000 per ton of dihydrogen gas. The mass of carbon dioxide to be captured (m(CO2)) is a function of the mass of H2 produced by reaction 9:

[0063]

[0064] Where m(CO2) is the mass of carbon dioxide produced in reaction 9, n(CO2) is the corresponding number of moles of carbon dioxide, and M(CO2) is the molar mass of carbon dioxide (44 g.mol -1 ), m(H2) is the mass of dihydrogen gas produced in reaction 9, n(H2) is the number of moles of the corresponding dihydrogen gas, and M(H2) is the molar mass of dihydrogen gas (2 g.mol -1 ). Therefore, the mass of carbon dioxide that needs to be captured for each ton of dihydrogen gas produced is equal to:

[0065]

[0066] Therefore, assuming a CO2 capture cost of $30 per tonne and an additional storage cost of $110 per tonne of CO2 for geological storage, the cost of producing blue hydrogen using SMRs and WGS (C 蓝H2 ) is expressed as the cost per ton of dihydrogen gas and one ton of gray hydrogen:

[0067] C 蓝H2 = C 灰H2 + $140 × 5.5 = $1000 + $770 = $1770 (12)

[0068] By suppressing the WGS step, and by advantageously coupling the SMR step with the CO electrolysis step to produce valuable carbon-based products, we can counterintuitively reduce the cost of equivalent low-carbon dihydrogen. This is counterintuitive because by suppressing the WGS step, the cost of dihydrogen gas increases to $1,333 per ton of dihydrogen gas. This is because we are now only producing 3 moles of dihydrogen gas at the same cost as 4 moles of dihydrogen gas. The costs are actually the same because most of the process costs come from the SMR step compared to the WGS step. However, in a specific embodiment, the WGS step is purposefully replaced by a carbon monoxide capture step that is intended to capture the carbon monoxide generated during the SMR step and provide it to a carbon monoxide electrolyzer to produce high value-added carbon-based products. From an economic perspective, this translates into the following analysis. The mass of carbon monoxide (m(CO)) to be captured is a function of the mass of dihydrogen gas produced by the SMR (without the WGS reaction), provided by the following relationship:

[0069]

[0070] Where m(CO) is the mass of carbon monoxide produced in reaction 1, n(CO) is the corresponding number of moles of carbon monoxide, and M(CO) is the molar mass of carbon dioxide (28 g.mol -1 ), m(H2) is the mass of dihydrogen gas produced in reaction 1, n(H2) is the number of moles of the corresponding dihydrogen gas, and M(H2) is the molar mass of dihydrogen gas (2 g.mol -1 ).

[0071] Each production t H2 The mass of CO that needs to be captured is equal to:

[0072]

[0073] Therefore, assuming that the capture cost of CO is $30 per ton, similar to the capture cost of CO2, the cost of low-carbon dihydrogen is:

[0074] C 低碳H2 = $1333 + $30 × 4.7 = $1474 (15)

[0075] Therefore, by replacing WGS with a downstream carbon monoxide value-added carbon capture step, the economic benefits of producing low-carbon dihydrogen gas equals $1770-$1474=$296, while the carbon monoxide fed to the electrolyzer can be value-added by selling a certain volume of chemicals produced. Using this system, the price of low-carbon dihydrogen gas is not only lower than the target cost of green hydrogen ($2000 per ton of dihydrogen gas), but also provides valuable carbon feedstock for the production of valuable products (particularly hydrocarbons, alcohols and organic acids), such as but not limited to ethylene, ethanol, acetic acid, propylene and propanol.

[0076] Another advantage of a specific embodiment of the present invention is that existing facilities for producing dihydrogen gas and synthesis gas already include separate reactors for the above-mentioned synthesis gas generation process, so that installing a separation system and electrolyzer assembly to harvest and separate carbon monoxide can be as simple as connecting a new machine to an existing output on a connection that would otherwise be delivered to the WGS reactor. In typical synthesis gas generation and WGS systems, the synthesis gas generation process is an endothermic reaction. In the case of an SMR, it is typically performed at 800°C-1000°C and 20-30 bar in the presence of a nickel-based catalyst. However, the WGS process is exothermic, requires optimization of different conditions, and is therefore preferably carried out in a separate reactor. Due to its exothermic nature, the formation of dihydrogen gas by WGS is thermodynamically unfavorable at high temperatures, although the reaction is kinetically favorable when the temperature is increased. Therefore, in order to benefit from both thermodynamic and kinetic advantages, WGS is usually carried out in a two-step process, a first high-temperature shift step (usually carried out at 300°C-450°C using an iron oxide-based catalyst) and a low-temperature process (usually carried out at 200°C-250°C using a copper or copper oxide-based catalyst supported on a mixture of aluminum oxide and zinc oxide). In the present system, the reactors usually used to carry out the two-step water gas shift (i.e., low-temperature and high-temperature shift) are inhibited and replaced with a separation system that allows separation of dihydrogen from carbon monoxide, which can then be used in the carbon monoxide electrolysis step using the electrolyzer discussed herein. Therefore, two independent WGS systems can be replaced with a separation system and a single electrolyzer, which can maintain or reduce the fixed costs of the production line.

[0077] In a specific embodiment of the invention, some of the carbon monoxide from the raw feedstock is sent to the electrolyser and some of it is sent to the water gas shift reactor. Figure 3ASystem 300 is shown where a feedstock 301 (e.g., natural gas) is provided to a syngas production system in the form of a reforming reactor 302. Subsequently, a portion of the carbon monoxide 303 is provided via a third connection 211 to a water-gas shift reactor 304 which will produce additional dihydrogen gas and carbon dioxide 305 from the carbon monoxide 303 and water 306. While the process will produce carbon dioxide, specific embodiments of the invention discussed below may utilize this carbon dioxide as described below, eliminating the need to capture and sequester it.

[0078] In a specific embodiment of the invention, the carbon monoxide originating from the raw feedstock is sent directly to a water-gas shift reactor, and the output of the water-gas shift reactor is sent to a separation system where the remaining carbon monoxide can be separated and fed to an electrolyser. Figure 3B System 310 is shown in which feedstock 301 is provided to a syngas production system in the form of a reforming reactor 302. Subsequently, any syngas produced by the reforming reactor 302 is fed to a water gas shift reactor 311 which also receives a volume of water 316. The output 313 of the WGS reactor 311 is in the form of dihydrogen gas mixed with carbon dioxide and carbon monoxide. The output 313 can then be applied to a separation system 312 which provides carbon monoxide 314 along a connection 315 to an electrolyzer 209 where it can be converted into a useful feedstock, as described in reference to Figure 2A In a specific embodiment of the present invention, the reforming reactor may perform a DMR or ATR reaction using carbon dioxide as an input, and the carbon dioxide generated by the water-gas shift reactor 311 may be separated and fed back as an input to the reforming reactor 302, as described below.

[0079] In a specific embodiment of the present invention, the synthesis gas generation process can be a reforming process, such as an autothermal or dry reforming process, such as a DMR process performed on natural gas. From an environmental point of view, these processes have additional advantages, that is, using carbon dioxide as an input, so that the process is used to capture carbon dioxide and provide the environmental benefits described above. These processes can be referred to as carbon dioxide consuming reforming processes and related systems can be referred to as carbon dioxide consuming reforming systems. In a specific embodiment of the present invention, the synthesis gas production system can be a dry methane reforming system and a dry methane reforming process can be performed on a certain volume of natural gas and a certain volume of carbon dioxide. The synthesis gas production system can be configured to use both the certain volume of natural gas and the certain volume of carbon dioxide to produce a certain volume of synthesis gas.

[0080] exist Figure 4AIn the system 400, the synthesis gas production system is a reforming reactor 401, such as a dry methane reforming reactor or an autothermal reforming reactor. Figure 4A Also included is a step 410 of supplying a volume of carbon dioxide for use by the syngas production system, which may be performed prior to the start of the steps of flow chart 100. For example, feedstock 402 may be methane, and reforming reactor 401 may be a DMR reactor that receives both feedstock 402 and carbon dioxide from carbon dioxide source 403 on connection 404.

[0081] The carbon dioxide used in the dry reforming process can be provided by a variety of carbon dioxide sources. For example, the carbon dioxide source can be captured from a carbon emission process in another industrial process that occurs in the same single industrial facility as the dihydrogen or syngas production line for which it is desired to capture carbon dioxide. As another example, the dihydrogen production line may include, for example, Figure 4A In the water-gas shift reactor, and the carbon dioxide produced by the reaction can be fed back as at least a portion of a carbon dioxide source 403. In these embodiments, both the harvesting step 101 and the supply step 410 can occur in a single industrial facility. These processes may include a connector, such as a connector 404, which connects the carbon dioxide output fluid of a carbon dioxide emission source (represented by carbon source 403) to a synthesis gas production system (e.g., a reforming reactor 401). In these embodiments, the existing connector for discharging carbon dioxide can be reused to provide carbon dioxide to the synthesis gas production system, although this can only be completed to some extent depending on the target H2:CO ratio. In alternative embodiments, the carbon dioxide of a certain volume can come from a carbon dioxide storage tank (represented by carbon source 403) stored in carbon dioxide discharged at different times or at different facilities. For example, the carbon dioxide source 403 can be a storage tank or a carbon dioxide transport pipeline.

[0082] exist Figure 4B In the system 420 in FIG. 4 , the syngas production system is a partial oxidation reactor 453 and the feedstock is a suitable feedstock for a gasification reactor, such as biomass or carbonaceous waste 422 . Figure 4B The remaining components of the system can be Figure 2A , Figure 3 and Figure 4A Similar to those cited. In an alternative embodiment, the water gas shift reactor 302 can be replaced with a Fischer-Tropsch reactor, followed by an upgrading reactor to upgrade the crude product to a usable fuel. Such a system can enable the production of sustainable aviation fuel. In particular, the carbon dioxide produced by the WGS reactor 302 shown can be fed back as input to the partial oxidation reactor 453.

[0083] exist Figure 4CIn the system 450 in, the synthesis gas production system is an oxidation reactor 421 and the raw material is a suitable raw material for the oxidation reactor, such as methane 451 and oxygen 452. In system 450, oxygen 452 can be the oxygen from electrolyzer 209 harvested on the anode output of the electrolyzer. As shown in the figure, oxygen can include other oxygen provided from a separate source, because the oxygen harvested is usually not enough to continue to fully supply the oxidation reactor. When the electrolyzer oxidation is supplied to the water of the anode input of the electrolyzer, oxygen can be generated. The oxidation reactor can perform a partial oxidation process. In an alternative embodiment, the oxygen generated by the water supplied to the anode input by the electrolyzer oxidation can be value-added in a separate process, or it can be separated and stored. Then, the stored oxygen can be sold as, for example, purified oxygen.

[0084] exist Figure 4D In the system 460 in FIG. 2 , the synthesis gas production system can use the parasitic output of the electrolyzer to have an increased concentration of dihydrogen in the synthesis gas produced, or a larger volume of purified dihydrogen. As shown, the electrolyzer 209 can produce parasitic dihydrogen 461 in the cathode region of the electrolyzer, and output it to the cathode output of the electrolyzer and transmit it via connector 462 to enhance the production of dihydrogen by the WGS reactor 302 or any other system for producing dihydrogen in the entire system to which the electrolyzer belongs. Dihydrogen can be separated from useful products 216, which are also output on the cathode output produced on 216. For example, if the useful products are fluids, they can be separated via a trap on connector 462, while gaseous dihydrogen remains in the connector.

[0085] In a specific embodiment of the present invention, the synthesis gas production device is advantageously integrated with a carbon monoxide electrolyzer, which includes a cathode region where carbon monoxide reduction according to the following equation 16 occurs and an anode region where an oxidation reaction of an oxidized substrate occurs at the anode. The oxidized substrate can be water, dihydrogen gas, a halide, organic waste, or any other oxidized substrate. For example, the oxidation can involve water oxidation or dihydrogen oxidation according to the following equations 17 and 18, respectively.

[0086] xCO+(x+yz)H2O+(2x+y-2z)e - →C x H y O z +(2x+y-2z)OH - (16)

[0087] 2H2O→4H + +4e - +O2 (17)

[0088] H2→2H + +2e- (18)

[0089] Both the carbon monoxide and the oxidized substrate may be mixed with additional chemicals to change the characteristics of the reactor and to change the characteristics of the chemicals produced by the electrolyzer. Figure 2A , water (not shown) and carbon monoxide 206 may be combined to form a cathode input fluid for the electrolyzer assembly, while an oxidized substrate 214 (such as dihydrogen) is provided on another connection 215 coupled to the anode input of the electrolyzer.

[0090] Chemicals produced by the electrolyzer can vary in different embodiments of the present invention. Chemicals can be separated using a separator, such as a trap for liquid chemicals on the anode or cathode output of the electrolyzer, or a separator between the cathode region and the anode region, which has its own output output from the electrolyzer. The produced chemical can be removed from the electrolyzer in solid or gaseous form, and can be removed from the cathode or anode output stream on the cathode or anode output of the electrolyzer, or removed from a separate output from a separation layer. The example of such a separation layer is provided below. A single electrolyzer can produce chemicals in gaseous and liquid forms simultaneously. Therefore, a certain volume of chemicals generated in a step such as step 103 can include at least one of a certain volume of hydrocarbons, a certain volume of organic acids, a certain volume of alcohols, a certain volume of olefins and a certain volume of rich N organic compounds, wherein the chemical is in gaseous or liquid form. For example, the certain volume of chemicals generated can include a certain volume of gaseous hydrocarbons and a certain volume of liquid alcohols. As another example, the certain volume of chemicals generated can include a certain volume of gaseous hydrocarbons and a certain volume of organic acids. In one embodiment, the primary desired products are ethylene (in the gaseous product stream) and acetic acid / acetate (in the liquid product stream).

[0091] Such a system is particularly advantageous in situations such as the production of low-carbon dihydrogen gas (which would otherwise undergo a water-gas shift reaction) because it is able to valorize carbon monoxide prior to its conversion to carbon dioxide, which otherwise occurs during the water-gas shift reaction. Thus, the system unlocks the production of low-carbon SMR-derived dihydrogen (similar to blue hydrogen) without the need for carbon capture and storage facilities. In addition, it is able to co-produce valuable carbon-based feedstocks with a low carbon footprint compared to those traditionally produced by petroleum-derived processes such as, but not limited to, naphtha cracking and ethane dehydration.

[0092] In a specific embodiment of the present invention, the oxidation substrate is dihydrogen gas, and the dihydrogen gas is supplied by a synthesis gas production process. The system may include a second output from a separation system that separates dihydrogen from the synthesis gas, and a connector that connects the second output fluid of the separation system to the anode region of the electrolyzer. For example, the second output may be taken from the separation system 205 and connected to the anode region of the electrolyzer. Figure 2A The process performed by the system may then include separating a second volume of dihydrogen from the volume of syngas. Then, using the volume of carbon monoxide by the electrolyzer to generate useful chemicals may include supplying the volume of carbon monoxide as a cathode input fluid to a cathode region of the electrolyzer, and supplying the second volume of dihydrogen as an anode input fluid to an anode region of the electrolyzer.

[0093] The carbon monoxide electrolyzer used according to the present disclosure may include one or more electrocatalytic cells arranged on top or adjacent to each other to increase the surface available for reaction. They can be stacked together up and down, and such stacking can be parallelized. These cells can be connected in series or in parallel. Many different cell and stack configurations can be used for electrolyzers according to the present disclosure. Figure 5 A schematic diagram of electrolyzer 500 is provided for purposes of explanation. The methods and systems disclosed herein are broadly applicable to electrolyzers generally capable of receiving a carbon input, such as carbon monoxide, and electrolyzer 500 is provided as a non-limiting example of one such electrolyzer.

[0094] Figure 5 Included is an illustration of an electrolyzer 500 in a stacked form according to a specific embodiment of the invention disclosed herein. The electrolyzer assembly 500 includes end plates such as 502, unipolar plates such as 504, rigid rods such as 506, a membrane electrode assembly (MEA) such as 508 or any form of catalytic core, a flow field such as 510, and a bipolar plate such as 512. Again, although an example of an MEA is provided, this is merely an example, and an electrolyzer with any form of catalytic core may be used in accordance with the embodiments disclosed herein. In addition, the stack 500 includes an inlet 514 and an outlet 516 for an anode flow, as well as an inlet 518 for a cathode flow and an outlet 520 for a cathode flow. The plates (such as the unipolar plate 504 and the bipolar plate 512) may be part of a slot in the stack. The stack may also include gaskets, seals of any shape and material, which are not shown in the illustrations for clarity. Figure 5 Shown in.

[0095] In the electrolysis stack, subsequent cells can be connected by bipolar plates (BPP) (such as Figure 5The bipolar plates 512 in the stack are physically separated, which ensures mechanical support for each electrolyzer on each side of the BPP. The BPP also ensures electrical series connection between subsequent electrolyzers and separate introduction / removal of reactants / products. At the end of the stack, only one side of the plate may be in contact with the terminal cell; it is then called a monopolar plate, such as Figure 5 The stack may be assembled in a stack housing to allow mechanical support and compression thereof, as well as to provide reactants to the stack and transport product streams from the stack. The stack housing may include end plates that ensure electrical isolation of the stack and provide inlets and outlets for reactant and product streams. Alternatively, an insulating plate may be placed between an end plate such as 502 and a monopolar plate such as 504 to ensure electrical insulation of the stack from the stack housing, depending on the material of the end plate.

[0096] The carbon monoxide electrolyzer can take a cathode input stream (e.g., a stream rich in carbon monoxide) and an anode input stream as inputs. The cathode input stream can be provided to an inlet, such as inlet 518. The anode input stream can be provided to an inlet, such as inlet 514. The cathode stream and the anode stream can flow from the inlet through the stack to the outlet, and are distributed to each cathode and anode region respectively through flow channels (such as flow channels 510 of each tank). The anode stream and the cathode stream will flow through separate channels on each side of the tank. Alternatively, at least one of the cathode stream and the anode stream can be provided to each tank separately, rather than through connectors passing through all plates. In this case, each tank has a dedicated fluid inlet and outlet for the cathode and / or anode stream. The properties of the anode stream can be determined by the properties of the target oxidation reaction (such as, but not limited to, water oxidation, dihydrogenation, chloride oxidation, halide oxidation, hydrocarbon oxidation, waste organic oxidation). When powered, the carbon monoxide electrolyzer simultaneously performs reduction of carbon monoxide and oxidation of a selected oxidation substrate to produce value-added chemicals (such as hydrocarbons, organic acids and / or alcohols and / or N-containing organic products) in an output cathode stream separate from an anode stream in which the oxidation products are exclusively collected. For example, using carbon monoxide and the electrolyzer to generate chemicals in step 103 may involve supplying a volume of carbon monoxide as a cathode input fluid to a cathode region of the electrolyzer, and supplying a volume of water as an anode input fluid to an anode region of the electrolyzer.

[0097] In a specific embodiment of the present invention, the anode region may include an anode catalyst layer capable of oxidizing a substance to produce a product and a proton. The catalyst may include one or more of: a molecular substance, a single metal site heterogeneous compound, a metal compound, a carbon-based compound, a polymer electrolyte (also referred to as an ionomer), a metal organic framework, a metal-doped covalent organic framework, or any other additive. The molecular substance may be selected from a metal porphyrin, a metal phthalocyanine, or a metal bipyridine complex. The metal compound may be in the form of a metal nanoparticle, a nanowire, a nanopowder, a nanoarray, a nanosheet, a nanocube, a dendrite, a film, a layer, or a mesoporous structure. The single metal site compound may include a metal-doped carbon-based material or a metal-NC-based compound. Anode catalyst materials for this purpose may include, but are not limited to, the following metals and / or ions: Ir, Co, Cu, Ni, Fe, Pt, Rh, Re, Ru, Pd, Os, Mo, and mixtures and / or alloys thereof. For example, the anode catalyst may be Ni, so that the electrolyzer assembly includes a nickel-based anode. The polymer electrolyte may be selected from the same material as that used for the membrane. The carbon-based compound may include carbon nanofibers, carbon nanotubes, carbon black, graphite, boron-doped diamond powder, diamond nanopowder, boron nitride, or a combination thereof. The additive may be a halide-based compound, including F, Br, I, and Cl. Such additives may be specifically used to modify the hydrophobicity, such as treatment with polytetrafluoroethylene (PTFE) or carbon black.

[0098] The anode catalyst may be deposited on a gas diffusion layer or porous transport layer or any other support that facilitates diffusion of gas from the anode interface to the purified gas stream separated from the cathode stream. The anode region may also include a gas diffusion layer with one or more separators on its boundaries, such as but not limited to membranes, polymeric materials, diaphragms, inorganic materials, as described below.

[0099] In a specific embodiment of the present invention, the cathode region may include a catalyst layer capable of reducing a substance (e.g., carbon monoxide) to generate additional hydrocarbons / alcohols / organic acids. The catalyst may include one or more of: a molecular substance, a single metal site heterogeneous compound, a metal compound, a carbon-based compound, a polymer electrolyte (also known as an ionomer), a metal organic framework, or a metal-doped covalent organic framework, or any other additive. The molecular substance may be selected from a metal porphyrin, a metal phthalocyanine, or a metal bipyridine complex. The metal compound may be in the form of a metal nanoparticle, a nanowire, a nanopowder, a nanoarray, a nanosheet, a nanocube, a dendrite, a film, a layer, or a mesoporous structure. The single metal site compound may include a metal-doped carbon-based material or a metal-NC-based compound. The cathode catalyst may be made of a metal or a metal ion from a metal, such as, but not limited to, Cu, Ag, Au, Zn, Sn, Bi, Ni, Fe, Co, Pd, Ir, Pt, Mn, Re, Ru, La, Tb, Ce, Dy or other lanthanides and mixtures and / or alloys thereof. For example, the cathode catalyst may include Cu so that the electrolyzer assembly includes a copper-based cathode. The polymer electrolyte may be selected from the same material as that used for the membrane. The carbon-based compound may include carbon nanofibers, carbon nanotubes, carbon black, graphite, boron-doped diamond powder, diamond nanopowder, boron nitride or a combination thereof. The additive may be a halide-based compound, including F, Br, I, Cl. Such additives may be specifically used to change the hydrophobicity, such as by treating with PTFE or carbon black. The cathode may also include a catalyst layer on a gas diffusion layer, a porous transport layer or any other support, which promotes gas diffusion from the flow to the surface of the catalyst, and allows the release of non-reactive / product gases. The cathode region may also include a gas diffusion layer having one or more separators on its border, such as but not limited to a membrane, a polymer material, a diaphragm, an inorganic material, as described below.

[0100] In a specific embodiment of the invention, the porous support for the anode region, the cathode region or both can be selected from a carbon-based porous support or a metal-based porous material or a combination. The carbon-based porous support can be based on carbon fiber, carbon cloth, carbon felt, carbon fabric, carbon paper, molded graphite laminate, etc. or a mixture thereof. The carbon-based porous support can be a gas diffusion layer with or without a microporous layer. Such carbon-based supports can in particular be selected from the following list: Sigracet 39AA, Sigracet 39BC, Sigracet 39BB, Sigracet 39BA, Sigracet 36AA, Sigracet 36BB, Sigracet 35BC, Sigracet 35BA, Sigracet 29BA, Sigracet 28BB, Sigracet 28AA, Sigracet 28BC, Sigracet 25BC, Sigracet 22BB, Sigracet 35BI, Toray paper, Toray THP-H-030, Toray TGP-H-060, Toray TGP-H-090, Toray TGP-H-120, Freudenberg H23C6, Freudenberg H15C13, Freudenberg H15C14, Freudenberg H14C10, Freudenberg H14CX483, FreudenbergH14CX653, Freudenberg H23C2, Freudenberg H23CX653, Freudenberg H24CX483, Freudenberg H23C6, Freudenberg H23C8, Freudenberg H24C5, Freudenberg H23C3, Avcarb MB-30, Avcarb GDS5130, Avcarb GDS2130, Avcarb GDS3250, Avcarb GDS3260, Avcarb GDS2230, Avcarb GDS2240, Avcarb GDS2255, Avcarb GDS2185, AvCar 1071, AvCarb1698, AvCarbon1209, AvCarb 1185、AvCarb1186、AvCarb 7497, AvCarb T1819, AvCarbT1820, AvCarb T1824, AvCarbon 1071, AvCarb 1698, AvCarb 1209, AvCarb1185, AvCarb1186, AvCarb 1186, AvCarb T1819, AvCarbAvCarb T1820, AvCarb T1824, AvCarb EP40, AvCarb P75, AvCarb EP55, AvCarbon EP40T, AvCarb P75T, AvCarb EP55T, AvCarb MGL190, AvCarb MGL280, AvCarb MGL370. The metal-based porous support may be selected from titanium, stainless steel, Ni, Cu or any other suitable metal, and may be in the form of a mesh, glass frit, foam or plate of any thickness or porosity.

[0101] In a specific embodiment of the present invention, the electrolyzer may include a separator to separate the specific generated chemical from other substances. The separator may be one or more traps on the cathode and / or anode output of the electrolyzer, which separates the liquid output from the gaseous output. For the purpose of effective product separation, it may also be a more complex system known to those skilled in the art. The separator may be a separation region between the anode region and the cathode region, which is configured to separate the generated chemical of this certain volume from the electrolyzer. The separation region may be a separation layer. The effective physical separation of the anode region and the cathode region may allow for easier separation of the gas released from each part of the reactor. The separator may be an ion-conducting polymer separator, a non-ion-conducting polymer separator, a diaphragm, a ceramic material, a non-charged separator support, a mixed ceramic-organic compound separator, or any other separator. The separation may be carried out by using: a diffusion ion exchange membrane that is conducive to anions (in anion exchange membranes) or cations (in cation exchange membranes), or a bipolar membrane (comprising a mixture of cations and anion exchange membranes) or other types of separators, such as a diaphragm, a ceramic material (particularly a mixed ceramic / organic compound) or a non-charged separator support. Anion exchange membranes may include organic polymers with positively charged functionality (such as, but not limited to, imidazolium, pyridinium, or tertiary amines). This allows negatively charged hydroxide ions (OH-) produced during carbon monoxide reduction to easily migrate from the cathode to the anode. The use of this layer also prevents other gases from penetrating the separation layer from the cathode. Cation exchange membranes may include organic polymers with negatively charged functionality (such as, but not limited to, sulfonate groups). The diaphragm or uncharged separator may be a material derived from an insulating material that can be charged with an ion-conducting electrolyte to facilitate charge transfer between the electrodes. The ceramic-containing material may be pure ceramic or a mixed polymer and ceramic material. Ceramic polymer mixtures can reach higher temperatures than pure organic polymers, and the ion exchange functionality in the polymer can be used to transfer charge between the electrodes.

[0102] In a particular embodiment of the invention, the system may include an electrolyte that will promote the transport of ions and provide ions that promote the reaction. In particular, the electrolyte may be a concentrated alkaline solution, such as a hydroxide-containing salt such as, but not limited to, a solution of potassium hydroxide, sodium hydroxide or cesium hydroxide, with a concentration such as (0.01 molar concentration (M), 0.05M, 0.1M, 0.2M, 0.5M, 1M, 2M, 3M, 4M, 5M, 6M, 7M, 8M, 9M and 10M). The use of concentrated alkaline solutions reduces the energy requirement of the overall reaction. Alkali metal cations (such as Li, Na, K, Cs, Rb) may be used as counter cations.

[0103] In specific embodiments of the present invention, the flow field may include ladders, single or multiple serpentine structures, interdigitated patterns, pillars, biomimetic leaf-like shapes, or combinations thereof. The electrolyzer may also include plates, as further discussed in this disclosure.

[0104] Figure 6 and Figure 7 An example of a reaction that can be performed according to the electrolyzer assembly described herein is shown. In the schematic diagram, for clarity, only a single tank is shown, but these tanks can be easily assembled into multiple tanks, such as stacking. In the schematic diagram, the carbon monoxide electrolyzer includes a cathode containing a gas diffusion layer and a copper-based catalyst, and the anode includes a nickel material of any shape (such as but not limited to foam, mesh, deposited on a conductive porous transport layer (PTL), etc.). In this case, the carbon monoxide reduction product includes one or more of the following: ethylene (C2H4), ethanol (C2H5OH), acetic acid (CH3COOH), propylene (C3H6), propanol (C3H8O), oxalic acid (COOH-COOH), acrylic acid (C2H3COOH), glyoxylic acid (COH-COOH), which is produced according to the following carbon monoxide reduction reaction:

[0105] Under neutral / alkaline conditions:

[0106] 2CO+6H2O+8e - →CH2CH2+8OH - (19)

[0107] 2CO+7H2O+8e - →CH3CH2OH+8OH - (20)

[0108] 2CO+4H2O+4e-→CH3COOH+4OH - (twenty one)

[0109] 3CO+5H2O+6e - →C2H3COOH+6OH - (twenty two)

[0110] 3CO+9H2O+12e-→C3H6+12OH - (twenty three)

[0111] 3CO+10H2O+12e-→C3H8O+12OH - (twenty four)

[0112] Under acidic conditions:

[0113] 2CO+8H + +8e - →CH2CH2+2H2O (25)

[0114] 2CO+8H + +8e - →CH3CH2OH+H2O (26)

[0115] 2CO+4H + +4e - →CH3COOH (27)

[0116] 3CO+6H + +6e - →C2H3COOH+H2O (28)

[0117] 3CO+12H + +12e - →C3H6+3H2O (29)

[0118] 3CO+12H + +12e - →C3H8O+2H2O (30)

[0119] In specific embodiments, the CO stream is mixed with other gaseous or liquid compounds to produce higher value-added products at the cathode. In one such embodiment, imines, amines, nitrogen oxides or ammonia are added to react with CO or intermediates formed during its reduction to form amide bonds or N-rich organic compounds, such as amino acids or urea. Examples of such reactions are:

[0120] Under neutral / alkaline conditions, 2CO+3H2O+NH3+4e - →CH3CONH2+4OH - (31)

[0121] Under acidic conditions, 2CO+4H + +NH3+4e - →CH3CONH2+H2O (32)

[0122] In specific embodiments, the oxidation reaction at the anode is selected from the group consisting of reactions conducted in an acidic environment and reactions conducted in an alkaline environment, such as but not limited to anode reactions in an acidic environment, such as:

[0123] 2H2O→O2+4H + +4e - (33)

[0124] H2→2H + +2e - (34)

[0125] Cl - →Cl2+2e - (35)

[0126] Br - →Br2+2e - (36)

[0127] I - →I2+2e - (37)

[0128] C3H8O3(glycerol)→C3H6O3(glyceraldehyde)+2H + +2e - (38)

[0129] C3H8O3(glycerol)+H2O→C3H5O4 - (Glyceraldehyde)+5H + +4e - (39)

[0130] C3H8O3(glycerol)+3 / 2H2O→3 / 2C2H3O3 - +13 / 2H + +5e - (40)

[0131] C3H8O3(glycerol)+3H2O→3HCOO - (Formate)+11H + +8e - (41)

[0132] C3H8O3(glycerol)+3H2O→3 / 2C2O4 2- +14H + +11e - (42)

[0133] and anodic reactions in neutral / alkaline environments, such as:

[0134] 4OH - →O2+2H2O+4e- (43)

[0135] H2+2OH - →2H2O+2e - (44)

[0136] Cl - →Cl2+2e - (45)

[0137] Br - →Br2+2e - (46)

[0138] I - →I2+2e - (47)

[0139] C3H8O3(glycerol)+2OH - →C3H6O3(glyceraldehyde)+2H2O+2e - (48)

[0140] C3H8O3(glycerol)+5OH - →C3H5O4 - (Glyceraldehyde)+4H2O+4e - (49)

[0141] C3H8O3(glycerol)+13 / 2OH - →3 / 2C2H3O3 - +5H2O+5e - (50)

[0142] C3H8O3(glycerol)+11OH - →3HCOO - (Formate)+8H2O+8e - (51)

[0143] C3H8O3(glycerol)+14OH - →3 / 2C2O4 2- +11H2O+11e - (52)

[0144] In a specific embodiment of the present invention, the carbon monoxide electrolyzer comprises an anion exchange membrane selected from the group consisting of, but not limited to, commercially available Ionomer anion exchange membranes), proton exchange membranes (such as but not limited to or commercially available membranes), bipolar membranes (such as but not limited to FBM and ) one or more membranes. In a specific embodiment of the present invention, the membrane in the anion exchange membrane is prepared using N-containing monomers. In the example of reactor 600, the electrolyzer includes an anion exchange membrane and hydroxide moves from the cathode to the anode. The oxidation product depends on the oxidation substrate, and the product harvested from the cathode output can be any of the above-mentioned chemicals generated. In the example of schematic diagram 602, the electrolyzer includes a cation exchange membrane and protons move from the anode to the cathode. The oxidation product once again depends on the oxidation substrate, and the product harvested from the cathode output can be any of the above-mentioned chemicals generated.

[0145] In a specific embodiment of the present invention, the electrolyzer may include a separation layer. In the example of reactor 601, the carbon monoxide electrolyzer includes a central separation layer, in which the electrolyte fluid circulates, thereby allowing the collection of liquid carbon monoxide reduction products that migrate from the cathode toward the central separation layer. In a specific embodiment, the central separation layer is either separated from the cathode by an anion exchange membrane, or separated from the anode by a cation exchange membrane, or both membranes exist. In the example of reactor 601, both membranes exist. In this example, useful products can be harvested from both the liquid stream from the separation layer and the gaseous stream output from the cathode. For example, the electrolyzer can use carbon monoxide to produce one or more of the following: ethylene (C2H4), ethanol (C2H5OH), acetic acid (CH3COOH), propylene (C3H6), propanol (C3H8O). In a specific embodiment, the main target product is ethylene (in the gaseous product stream). In another specific embodiment, the main target product is ethylene (in the gaseous product stream) and ethanol (in the liquid product stream). In another specific embodiment, the main target product is ethylene (in gaseous product stream) and acetic acid / acetate (in liquid product stream). For example, in reactor 602, the trap is located at the cathode output, which separates the liquid product from the gaseous product so that they can be collected. In these examples, the oxidation occurring at the anode can be water / hydroxide oxidation, dihydroxide or chloride oxidation. It should be noted that in the physical system, the trap is located on the connector with the cathode outlet, such as on the connector with the pipeline connected to the cathode, and the trap is drawn as being connected to the cathode region for schematic purposes only.

[0146] Figure 7 The examples shown in the figure are similar in general theory to the reactor Figure 6 However, Figure 7The method in is not operated using an exchange membrane, but rather using a separation layer that achieves a similar effect. Reactor 700 is similar to reactor 600 in that hydroxide ions move from the cathode to the anode and the generated products can be harvested from the cathode output. Reactor 701 is similar to reactor 601 in that the separation layer includes a liquid electrolyte, and useful products can be harvested in liquid form from the output of the separation layer and in fluid form from the output of the cathode region. Reactor 702 is similar to reactor 602 in that protons migrate through the separation layer and useful products can be harvested from the output of the cathode.

[0147] In a specific embodiment of the present invention, a porous membrane may be used as a separation element in an electrolyzer to achieve separation. The membrane may be saturated with electrolyte, thereby allowing ions to pass between the cathode and the anode. Figure 8 Reactor 800 is shown in which the separation element is a membrane that allows ions to pass from the anode to the cathode and / or from the cathode to the anode.

[0148] In a specific embodiment of the present invention, the synthesis gas production system is a biomass gasification device for producing low-carbon dihydrogen. Carbon monoxide is then separated from the produced dihydrogen and fed into a carbon monoxide electrolyzer to produce one or more of the following: ethylene (C2H4); ethanol (C2H5OH); acetic acid (CH3COOH); propylene (C3H6), propanol (C3H8O); or products containing carbon-nitrogen bonds, such as amino acids and / or urea and / or amide-containing organic substances, provided that N-containing substances (such as imines, amines, ammonia, nitrogen oxides) and CO are used as inputs to the cathode stream at the same time. In a specific embodiment, the main target product is ethylene (in the gaseous product stream). In a specific embodiment, the main target products are ethylene (in the gaseous product stream) and ethanol (in the liquid product stream). The oxidation occurring at the anode is water / hydroxide oxidation, dihydroxide oxidation or chloride oxidation.

[0149] In a specific embodiment of the present invention, the carbon monoxide stream is mixed with at least one other chemical such as other gas or liquid compound to generate a higher value-added product at the cathode of the electrolyzer. When carbon monoxide is supplied to the electrolyzer, the carbon monoxide stream can be mixed with such additive chemicals. In one such embodiment, imines, amines, nitrogen oxides or ammonia are added to react with carbon monoxide or the intermediate formed during its reduction to form amide bonds or nitrogen-rich organic compounds, such as amino acids. In another embodiment, aromatic or fatty acid / aldehyde / alcohol is added to react with carbon monoxide or the intermediate formed during its reduction to form hydrocarbons, alcohols or organic acids. In another embodiment, olefins or hydrocarbons are added to react with carbon monoxide or the intermediate formed during its reduction to form hydrocarbons, alcohols or organic acids. These reactions can be combined with any one of the above-mentioned reactors. For example, the oxidation occurring at the anode can be water oxidation, hydroxide oxidation, dihydrogenation or halide oxidation.

[0150] Although this specification has been described in detail with respect to specific embodiments of the present invention, it should be understood that those skilled in the art, after understanding the foregoing, can easily think of changes, variations and equivalents of these embodiments of the present invention. The chemical volume disclosed in this disclosure is not meant to refer to physically isolated volumes, because a certain volume of dihydrogen can exist in a single physical volume with a certain volume of carbon dioxide in the form of a certain volume of synthesis gas. Although the examples in this disclosure generally relate to the production of dihydrogen, the same method can be used in other industrial processes in which carbon monoxide can be obtained, such as in the steel industry. In addition, although the examples in this disclosure are generally applied to industrial chemical processes, the same method is also applicable to chemical processing of any scale and scope. In addition, although the examples in this disclosure are generally applied to transporting carbon monoxide to an electrolyzer, the method disclosed herein is more widely applicable to transporting any member of the oxygen-containing carbon compound family to an electrolyzer for the purpose of generating useful chemicals therefrom. Without departing from the spirit and scope of the present invention, those skilled in the art can implement these and other modifications and changes to the present invention, and the scope of the present invention is more specifically set forth in the appended claims.

Claims

1. A method (100), comprising: harvesting (101) a volume of carbon monoxide (206) from a synthesis gas production system (201); supplying (102) the volume of carbon monoxide (206) to a cathode region of an electrolyser (209; 500); as well as generating (103) a volume of a generated chemical (216) using the volume of carbon monoxide (206) and the electrolyzer (209; 500); The volume of generated chemicals (216) is at least one of: a volume of hydrocarbons, a volume of organic acids, a volume of alcohols, a volume of olefins, and a volume of N-rich organic compounds.

2. The method (100) according to claim 1, wherein: The raw material (202; 301; 402) used in the synthesis gas production system (201) is a certain volume of natural gas.

3. The method (100) of claim 1, wherein: The synthesis gas production system (201) includes a gasification process; and The raw material (202; 301; 402) used in the gasification process is at least one of biomass and waste (422).

4. The method (100) of claim 1, wherein harvesting (101) a volume of carbon monoxide (206) comprises: supplying (251) a volume of syngas from the syngas production system (201) to a separation system (205); as well as A volume of dihydrogen (208) and a volume of carbon monoxide (206) are separated (252) from the volume of syngas (203) using the separation system (205).

5. The method (100) of claim 2, wherein: The synthesis gas production system (201) performs a steam methane reforming process on a certain volume of natural gas to produce a certain volume of synthesis gas; and The carbon monoxide (206) from the volume of syngas (203) is not used in the water gas shift reaction.

6. The method (100) of claim 1, further comprising: A volume of carbon dioxide is supplied (401) to be used in the synthesis gas production system (201).

7. The method (100) of claim 6, wherein: The volume of carbon dioxide is obtained from a water-gas shift reaction performed on a second volume of carbon monoxide (206) from the synthesis gas production system (201).

8. The method (100) of claim 1, wherein said generating (103) using said volume of carbon monoxide (206) and said electrolyzer (209; 500) comprises: supplying (102) the volume of carbon monoxide (206) to the cathode region of the electrolyzer (209; 500) as a cathode input fluid; as well as A volume of electrolyte is supplied to the anode region of the electrolyser (209; 500) as an anode input fluid.

9. The method (100) of claim 8, further comprising: supplying a volume of oxygen (452) generated by the electrolyser (209; 500) from an anode output to the synthesis gas production system (201); and The synthesis gas production system (201) performs one of an oxidation process and a partial oxidation process.

10. The method (100) of claim 1, further comprising: Providing a volume of dihydrogen (208); and wherein said generating (103) a volume of a generated chemical (216) comprises: supplying (103) the volume of carbon monoxide (206) to the cathode region of the electrolyzer (209; 500) as a cathode input fluid; as well as The volume of dihydrogen (208) is supplied to the anode region of the electrolyser (209; 500) as an anode input fluid.

11. The method (100) of claim 10, wherein: The volume of dihydrogen (208) includes parasitic dihydrogen (208) (461) output from the cathode region; and The parasitic dihydrogen (208)(461) output is circulated from the cathode output of the electrolyzer (209; 500) to the anode input of the electrolyzer (209; 500).

12. The method (100) of claim 10, wherein: wherein harvesting (101) a volume of carbon monoxide (206) comprises: (i) supplying (251) a volume of syngas from the syngas production system (201) to a separation system (205); and (ii) separating (252) the volume of dihydrogen (208) and the volume of carbon monoxide (206) from the volume of synthesis gas (203) using the separation system (205).

13. The method (100) of claim 1, further comprising: Supplying a volume of water (212) to the anode region of the electrolyzer (209; 500) as an anode input fluid; and The electrolyser (209; 500) comprises a cathode region having a copper-based catalyst.

14. The method (100) of claim 1, wherein: The electrolyzer (209; 500) includes at least one separator element selected from the group consisting of an ion-conducting polymer separator, a non-ion-conducting polymer separator, a diaphragm, a ceramic-containing material, an uncharged separator support, and a hybrid ceramic-organic compound separator.

15. The method (100) of claim 1, wherein: The volume of generated chemicals (216) includes a volume of gaseous hydrocarbons and a volume of liquid alcohol.

16. The method (100) of claim 1, wherein: The volume of generated chemicals (216) includes a volume of gaseous hydrocarbons and a volume of organic acids.

17. The method (100) of claim 1, further comprising: mixing the volume of carbon monoxide (206) with a volume of at least one additive chemical; and wherein when the volume of carbon monoxide (206) is supplied to the electrolyser (209; 500), the volume of carbon monoxide (206) has been mixed with the volume of at least one additive chemical.

18. The method (100) of claim 17, wherein: The volume of at least one additive chemical includes water (212).

19. The method (100) of claim 17, wherein: The volume of the additive chemical is one of an imine, an amine, a nitrogen oxide, and ammonia; and The volume of generated chemical (216) is a volume of amino acids.

20. A system (200), comprising: A syngas production system (201) configured to produce a volume of syngas; a first connection (204) fluidly connected to a syngas output of the syngas production system (201); a separation system (205) fluidly connected to the first connection (204) and configured to separate a volume of carbon monoxide (206) from the volume of syngas (203); a second connection (207) fluidly connected to a carbon monoxide (206) output of the separation system (205); an electrolyser (209; 500) having a cathode input fluidly connected to the second connection (207) and configured to generate a volume of a generated chemical (216) from the volume of carbon monoxide (206); and The volume of generated chemicals (216) is at least one of: a volume of hydrocarbons, a volume of organic acids, a volume of alcohols, and a volume of N-rich organic compounds.

21. The system (200; 300; 400) according to claim 20, wherein: The synthesis gas production system (201) is a gasification system; and The raw material (202; 301; 402) for the gasification system is at least one of biomass and waste (422).

22. The system (200; 300; 400) according to claim 20, wherein: The synthesis gas production system (201) is one of a methane (451) reforming system and a partial oxidation system; and The synthesis gas production system (201) is configured to operate using a volume of natural gas.

23. The system (200; 300; 400) according to claim 20, wherein: The syngas production system (201) is configured to produce the volume of syngas (203) using a volume of carbon dioxide.

24. The system (200; 300; 400) according to claim 20, further comprising: Water source; as well as A third connection (211) connects the water (212) source fluid to the anode region of the electrolyzer (209; 500) as an anode input fluid.

25. The system (200; 300; 400) according to claim 24, further comprising: an anode region of the electrolyzer (209; 500) having an anode output and configured to generate a volume of oxygen (452) while oxidizing the anode input fluid; a third connection (211) connecting the anode output fluid of the anode region to the synthesis gas production system (201); and The synthesis gas production system (201) is configured to perform one of an oxidation process and a partial oxidation process.

26. The system (200; 300; 400) according to claim 20, further comprising: An anode region of the electrolyzer (209; 500) is configured to receive a volume of dihydrogen (208) from the separation system.

27. The system (200; 300; 400) according to claim 20, further comprising: a third connection (211) fluidly connected to a cathode output of the cathode region; as well as An anode region of the electrolyzer (209; 500) has an anode input fluidly connected to the third connection (211) and is configured to receive a volume of dihydrogen (208) from a cathode output via the third connection (211).

28. The system (200; 300; 400) of claim 20, wherein the electrolyzer (209; 500) also includes: a cathode region having a copper-based catalyst; as well as An anode region having at least one of an iridium-based catalyst and a nickel-based catalyst.

29. The system (200; 300; 400) of claim 20, wherein the electrolyzer (209; 500) further comprises: At least one separator element selected from the group consisting of an ion-conducting polymer separator, a non-ion-conducting polymer separator, a membrane, a ceramic-containing material, an uncharged separator support, and a hybrid ceramic-organic compound separator.

30. A method (100) comprising: supplying (401) a volume of carbon dioxide and a volume of natural gas to a reforming process; harvesting (101) a volume of carbon monoxide (206) from the reforming process; supplying (102) the volume of carbon monoxide (206) to a cathode region of an electrolyser (209; 500); as well as A volume of a produced chemical (216) is produced (103) using the volume of carbon monoxide (206) and the electrolyzer (209; 500).

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