Method for producing carbon oxide reduction product and method for producing synthesis gas used in said production method

Abstract

A method for producing a carbon oxide-containing gas according to an embodiment of the present disclosure includes a gas production step and a gas reforming step. The gas reforming step is performed using a gas reforming device equipped with a reactor for converting at least a portion of carbon dioxide and hydrogen into carbon monoxide and water vapor by being brought into contact with a catalyst, the reactor having a high-temperature part for heating a reaction field and a cooling part for condensing at least a portion of the reaction product. Waste heat in the gas production step is utilized as a heat source of the high-temperature part.

Description

Method for producing carbon oxide reduction products and method for producing synthesis gas used in the said production method.

[0001] This disclosure relates to a method for producing carbon oxide reduction products.

[0002] In a technology that produces carbon oxide reduction products via carbon oxide through hydrocarbon conversion reactions, the synthesis gas supplied to the converter may be reformed and / or its components adjusted. As a process for such reforming and / or adjusting the components, for example, a reformer that reduces carbon dioxide using a reverse shift reaction, as described in Patent Document 1, may be used.

[0003] Japanese Patent Application Publication No. 2015-77120

[0004] In the reformer described above, the reverse shift reaction is an endothermic reaction, so a lot of energy is required to heat the reformer.

[0005] One aspect of this disclosure aims to realize a method for producing carbon oxide reduction products with excellent energy efficiency.

[0006] A method for producing a carbon oxide-containing gas according to one aspect of the present disclosure is a method for producing a carbon oxide-containing gas used in a method for producing a carbon oxide reduction product, comprising: a gas production step of producing a first synthesis gas containing carbon oxide by steam reforming and / or oxidation of a carbon-containing raw material; and a gas reforming step of producing a second synthesis gas by reforming a first supply gas containing carbon dioxide and hydrogen, wherein the carbon oxide-containing gas comprises at least a portion of the first synthesis gas and at least a portion of the second synthesis gas, and the gas reforming step is carried out using a gas reforming apparatus equipped with a reactor that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas into carbon monoxide and steam by contacting it with a catalyst, the reactor having a high-temperature section for heating the reaction field and a cooling section for condensing at least a portion of the gas in the reactor, and the waste heat from the gas production step is used as the heat source for the high-temperature section.

[0007] A method for producing a carbon oxide reduction product according to one aspect of this disclosure involves reducing the carbon oxide contained in the carbon oxide-containing gas obtained from the above-mentioned method for producing a carbon oxide-containing gas to obtain a carbon oxide reduction product.

[0008] A method for producing a carbon oxide reduction product according to one aspect of this disclosure involves synthesizing hydrocarbons and / or alcohols from a carbon oxide-containing gas obtained from the above-mentioned method for producing a carbon oxide-containing gas by an inversion reaction.

[0009] According to one aspect of this disclosure, it is possible to realize a method for producing carbon oxide-containing gases and carbon oxide-reduced products that are highly energy-efficient.

[0010] This is a schematic diagram showing the configuration of an alcohol production apparatus according to Embodiment 1 of the present disclosure. This is a cross-sectional view of an exemplary gas reforming apparatus according to the present disclosure, when cut by a plane perpendicular to the bottom surface. This is a schematic diagram showing the configuration of a hydrocarbon production apparatus according to Embodiment 2 of the present disclosure. This is a schematic diagram showing the configuration of a hydrocarbon and alcohol production apparatus according to Embodiment 3 of the present disclosure. This is a schematic diagram showing the configuration of a carbon oxide reduction product production apparatus according to Embodiment 4 of the present disclosure.

[0011] The carbon oxide reduction products relating to this disclosure may be, for example, alcohols such as methanol or ethanol, hydrocarbons such as methane, carbon monoxide, aldehydes such as dimethyl ether or formaldehyde, ketones such as acetone or methyl ethyl ketone, diols such as ethylene glycol or 1,3-propanediol, carboxylic acids or their esters such as formic acid, acetic acid, methyl formate, or methyl acetate, or elemental carbon such as carbon powder. In the following embodiments, as examples of methods for producing carbon oxide reduction products, methods for producing alcohol, methods for producing hydrocarbons, methods for producing hydrocarbons and alcohols, and methods for producing carbon oxide reduction products will be described in detail.

[0012] [Embodiment 1] Hereinafter, an alcohol manufacturing method, which is one embodiment of the present disclosure, will be described in detail with reference to the drawings, along with the manufacturing apparatus used therein. Note that the attached drawings are for illustrative purposes only and may differ from the actual dimensions. In this specification, "A to B" indicates a range of A or greater and B or less.

[0013] The method for producing alcohol according to the present disclosure is a method for producing alcohol from a carbon-containing raw material via carbon oxide, which comprises a gas production step, a gas reforming step, and a conversion step, and is characterized in that waste heat from the gas production step is used as a heat source for the gas reforming step. Each step is described in detail below.

[0014] In the present embodiment, a production apparatus 100 that implements the method for producing alcohol according to the present disclosure will be described. However, the system described in the present specification and drawings is merely a typical example, and does not limit the scope of the present disclosure in any way. This also applies to other embodiments described below.

[0015] (Configuration of Alcohol Production Apparatus) A production apparatus 100, which is an example of the alcohol production apparatus according to the present disclosure, will be described. The production apparatus 100 is an apparatus that produces alcohol from a carbon-containing raw material.

[0016] The carbon-containing raw material in the present disclosure is not particularly limited, and may be, for example, fossil fuel, waste plastic, or biomass waste. The biomass waste only needs to be a material containing an organic substance from which a gas containing hydrogen and carbon oxide can be obtained in the gas production step described later. Examples of such waste include garbage, paper waste, textile waste, plastic waste, sewage sludge, human waste, livestock waste, waste oil, rubber tires, black liquor, waste molasses, or mixtures thereof.

[0017] FIG. 1 is a system diagram schematically showing the configuration of the production apparatus 100 according to Embodiment 1. As shown in FIG. 1, the production apparatus 100 includes a gas production apparatus 20, a gas cleaning apparatus 30, a gas reforming apparatus 40, a CO ２ separation apparatus 50, an alcohol conversion apparatus 60, and an alcohol purification apparatus 70, and has a general configuration. The gas reforming apparatus 40 and the CO ２ separation apparatus 50 can be used for adjusting the composition of a supply gas to be supplied to the alcohol conversion apparatus 60.

[0018] The gas production apparatus 20 is an apparatus for carrying out a gas production step of obtaining a first syngas G1 by steam reforming and / or partial oxidation of a carbon-containing raw material. The first syngas G1 comprises carbon monoxide (CO), carbon dioxide (CO ２ ), and hydrogen (H ２ ).

[0019] The gas production apparatus 20 may be an apparatus comprising a reforming furnace that performs steam reforming by reacting a carbon-containing raw material with steam in the presence of a catalyst. The reaction temperature of the steam reforming may generally be carried out at 700°C to 1000°C. Alternatively, the gas production apparatus 20 may be an apparatus comprising a partial oxidation furnace that performs partial oxidation by reacting a carbon-containing raw material with oxygen. The reaction temperature of the partial oxidation may generally be carried out at 800°C to 1000°C. Alternatively, the gas production apparatus 20 may be an apparatus comprising an incinerator that performs partial oxidation by reacting a carbon-containing raw material with oxygen. The reaction temperature of the partial oxidation may generally be carried out at 800°C to 1000°C. The gas production apparatus 20 may comprise either one of a steam reforming apparatus and a partial oxidation apparatus, or may comprise both of them.

[0020] Alternatively or additionally, the gas production apparatus 20 may be an apparatus for carrying out a gas production step of obtaining a first syngas G1 containing carbon oxides by oxidizing a carbon-containing raw material. In this case, the first syngas G1 contains carbon oxides such as carbon monoxide (CO) and carbon dioxide (CO ２ ), and may have a composition that does not contain hydrogen (H ２ ). The gas production apparatus 20 may be an apparatus comprising a blast furnace that performs oxidation by reacting a carbon-containing raw material with oxygen. Oxidation in a blast furnace may include complete oxidation and partial oxidation. The reaction temperature of the oxidation in a blast furnace may generally be carried out at 1000°C to 2200°C. The gas production apparatus 20 may comprise only an oxidation apparatus, or may comprise an oxidation apparatus in addition to one or both of a steam reforming apparatus and a partial oxidation apparatus.

[0021] The gas scrubber 30 is an apparatus that performs a gas scrubbing step of scrubbing gas by removing impurities from the first synthesis gas G1. The gas scrubbing step can be carried out by a known method, and as the gas scrubber 30, a known apparatus such as a wet scrubbing tower or an electrostatic precipitator can be used.

[0022] The gas reformer 40 is an apparatus that performs a gas reforming step of producing the second synthesis gas G2 by reforming the first supply gas GE1 containing carbon dioxide and hydrogen. The first supply gas GE1 supplied to the gas reformer 40 may contain at least a part of the first synthesis gas G1 produced by the gas production apparatus 20. Further, the first supply gas GE1 is CO described later ２ separated from the separation apparatus 50 ２ may be contained. The first supply gas GE1 contains CO ２ and H ２ . In the gas reformer 40, at least part of CO ２ and H ２ in the first supply gas GE1 is reformed into CO and water vapor through a reverse shift reaction. Thereby, the CO ２ concentration and H ２ concentration in the synthesis gas are reduced, and the CO concentration can be increased.

[0023] In the present disclosure, the gas reformer 40 uses an apparatus that shifts the chemical equilibrium toward the product side and promotes the reaction by condensing the product and recovering it from the inside of the reactor. FIG. 2 is a cross-sectional view of the exemplary gas reformer 40 according to the present disclosure, taken along a plane perpendicular to the bottom surface.

[0024] In the gas reformer 40, reactions represented by the following formulas (1) to (3) can proceed. By adjusting the temperature conditions and the catalyst used, and taking out the generated water vapor out of the system as a condensed liquid, the reaction proceeding in the right direction of formula (1) (reverse shift reaction) can be promoted predominantly.

[0025] CO ２ +H ２ →CO+H ２ O (reversible reaction)...(1) CO+2H ２ →CH ３OH (reversible reaction) ... (2) CO ２ +3H ２ →CH ３ OH + H ２ O (Reversible reaction) ... (3) As shown in Figure 2, the gas reformer 40 includes a reactor 401, a first heat exchange section 422, a catalyst layer 402 in contact with the first heat exchange section 422, a permeable wall 440, and a second heat exchange section 452 separated from the permeable wall 440 by a space 404. In the gas reformer 40, the catalyst layer 402 corresponds to the reaction field according to this disclosure. The permeable wall 440 is provided on the side of the catalyst layer 402 opposite to the side where the first heat exchange section 422 is located. The reactor 401 is, for example, a pressure-resistant stainless steel metal container.

[0026] The first heat exchange section 422 is an example of a high-temperature section according to the present disclosure, and is a heat exchanger composed of the inner wall surface of the reactor 401 and the first heat exchange wall 420. The first heat exchange section 422 can maintain a high temperature in the reaction field where the endothermic reaction proceeds by circulating the first heat transfer medium 421. In the gas reforming apparatus 40, the temperature of the reaction field may be 200°C or more and 500°C or less, preferably 250°C or more and 400°C or less.

[0027] To maintain the reaction field at the above temperature, the first heat transfer medium 421 can be, for example, high-pressure boiler water (e.g., saturated water with a pressure of 2.2 MPaG to 5.0 MPaG), molten metal salt (e.g., a mixture of sodium nitrite and potassium nitrate), or heat transfer oil, all at a temperature of 250°C to 500°C, preferably 270°C to 350°C. The waste heat from the gas production process described above is used to heat the first heat transfer medium 421. The dashed arrows in Figure 1 indicate the heat supply.

[0028] Since the reaction temperature in the gas production process is 700°C to 1000°C, and the temperature of the first heat transfer medium 421 circulating through the first heat exchange section 422 is 250°C to 500°C, by utilizing the waste heat from the gas production process, the first heat transfer medium 421 can be heated to a temperature suitable for the reaction without further heating by combustion or other means.

[0029] Furthermore, although these are external devices to the manufacturing apparatus 100, the waste heat temperature of devices such as heavy oil combustion furnaces, high-pressure boilers, or waste incinerators is also between 700°C and 1000°C. Since the temperature of the first heat medium 421 that flows through the first heat exchange section 422 is between 250°C and 500°C, even when utilizing waste heat from these devices, the first heat medium 421 can be heated to a temperature suitable for the reaction without further heating by combustion or other means.

[0030] The second heat exchange section 452 is an example of a cooling section according to the present disclosure and is a heat exchanger composed of the inner wall surface of the reactor 401 and the second heat exchange wall 450. The second heat exchange section 452 can maintain the temperature of the second heat exchange wall 450 below the dew point of the reaction gas 432 by circulating the second heat transfer medium 451. In the reverse shift reaction, the product includes water and methanol. In this case, in the gas reformer 40, the temperature of the cooling section (second heat exchange wall 450) may be 0°C or more and 180°C or less, preferably 5°C or more and 100°C or less.

[0031] To maintain the second heat exchange wall 450 at the above temperature, the second heat transfer medium 451 can be, for example, low-pressure boiler water at 80 to 150°C (e.g., saturated water at -0.05 to 0.4 MPaG), industrial water, aqueous ammonia solution, hydrocarbon compounds such as pentane, or fluorocarbon compounds such as 1,1,1,3,3-pentafluoropropane.

[0032] The catalyst layer 402 is filled with a catalyst suitable for the reaction. The catalyst layer 402 is a reaction field where the first supply gas GE1 and the catalyst come into contact and the reaction proceeds. As the catalyst, for example, a catalyst containing a transition metal can be used.

[0033] Catalysts containing transition metals are known to exhibit high activity and selectivity in reverse shift reactions, contributing to improved reaction yields. Examples of transition metal-containing catalysts include those containing copper, iron, nickel, cobalt, molybdenum, and manganese. These transition metals can be appropriately selected depending on the reaction conditions or the desired product.

[0034] The catalyst may be a copper-containing catalyst. Among transition metals, copper is inexpensive, readily available, and widely used industrially. Therefore, it is particularly preferred as a catalyst component that improves the reaction rate while keeping costs down.

[0035] As a catalyst containing transition metals, alloy catalysts combining two or more transition metal components or composite oxide catalysts combining two or more transition metal oxide components can also be used. For example, multi-component catalysts combining copper and nickel, iron and cobalt, or copper and manganese can also be suitably used. Furthermore, one or more metals selected from the group consisting of alkali metals (sodium, potassium, cesium, etc.), alkaline earth metals (calcium, barium, etc.), rare earth metals (lanthanum, cerium, etc.), and precious metals (palladium, rhodium, platinum, ruthenium, etc.) may be included in the catalyst as an additive or promoter.

[0036] Catalysts containing transition metals may be supported catalysts in which the transition metal component or transition metal oxide component is supported on a support, or they may be unsupported catalysts (metal powders, alloys, oxides, etc.) without a support. Examples of support materials include silica, alumina, zeolite, titania, and activated carbon. Known methods such as impregnation, coprecipitation, and ion exchange can be applied to support the transition metal component or transition metal oxide component on these support materials.

[0037] The permeable wall 440 is constructed using a porous material that allows gas to pass through. The permeable wall 440 is made of a material that allows the reaction gas 432 to pass through but prevents the catalyst from passing through, such as a metal mesh with an appropriate pore size.

[0038] Space 404 is a space formed between the permeable wall 440 and the second heat exchange wall 450. Below space 404, a condensate storage section is formed that can store the condensed and liquefied product (condensate) that condenses on the surface of the second heat exchange wall 450 facing space 404. The condensate can be recovered through a condensate recovery port provided at the bottom of the condensate storage section.

[0039] (Reaction Flow) The first supply gas GE1 supplied to the gas reformer 40 reacts with the catalyst filling the catalyst layer 402. The reaction gas 432 generated by the reaction passes through the permeable wall 440 and proceeds to the space 404. Subsequently, the reaction gas 432 is cooled below the dew point by the second heat exchange wall 450, causing the product to condense. The condensed and liquefied product is recovered as a condensate. In this embodiment, the condensed product contains water and methanol.

[0040] The reaction gas 432 passing through the permeate wall 440 from the catalyst layer 402 side also contains unreacted first supply gas GE1. However, the main components of the unreacted first supply gas GE1 are not condensed at the second heat exchange wall 450. The unreacted raw material gas returns to the catalyst layer 402 and comes into contact with the catalyst again.

[0041] As described above, the reverse shift reaction proceeds predominantly in reactor 401, and therefore, compared to the first feed gas GE1, CO ２ and H ２ A second synthesis gas G2 can be obtained in which the concentration of is reduced and the CO concentration increases. At least a portion of the second synthesis gas G2 can be supplied to the alcohol converter 60 as at least a portion of the second supply gas GE2.

[0042] At least a portion of the second synthesis gas G2 obtained by the gas reforming unit 40 is CO ２ It may also be used in the separation device 50. ２ The separation unit 50 extracts CO from the second synthesis gas G2 obtained from the gas reforming unit 40. ２ Selectively separate CO to obtain the adjusted second synthesis gas G2X. ２ This is a device that performs the separation process. ２ CO ２ An emission path is provided, CO ２ CO can be discharged. ２ As the separation device 50, known devices such as pressure swing adsorption devices, absorption and desorption towers, cryogenic carbon dioxide separation devices, and carbon dioxide separation membrane equipment can be used. The adjusted second synthesis gas G2X has a CO2 content that is lower than that of the second synthesis gas G2. ２This is a gas with a reduced concentration.

[0043] CO ２ CO separated from the separation device 50 ２ As shown in Figure 1, CO is produced by the waste heat of the gas production equipment. ２ It may be preheated and supplied to the gas reformer 40 as part of the first supply gas GE1.

[0044] The alcohol converter 60 uses CO, CO2 supplied as the second supply gas GE2. ２ , and H ２ This apparatus performs a conversion process in which a gas containing CO (carbon oxide-containing gas) is reacted with a catalyst to convert it into an alcohol. ２ It can also be said that this is a reduction process that reduces CO. The alcohol in this disclosure may include ethanol or methanol. The second supply gas GE2 includes at least a portion of the first synthesis gas G1 produced by the gas production apparatus 20 and at least a portion of the second synthesis gas G2 obtained by the gas reformer 40. The second supply gas GE2 is further supplied by the gas reformer 40 and CO ２ It may contain a modified second synthesis gas G2X whose components have been adjusted by the separation device 50.

[0045] The alcohol converter 60 can use known alcohol synthesis reactors such as a quench-type multi-stage adiabatic reactor, a heat exchange isothermal reactor, an internal condensation reactor, a membrane reactor, or a gas fermentation reactor. When using the heat exchange isothermal reactor, heat generated by the reaction in the catalyst layer can be recovered via a heat transfer medium. Furthermore, the alcohol converter 60 may be a combination of multiple reactors, and the alcohol production rate can be improved by connecting reactors of the same type or different structures in series.

[0046] Although not shown in the diagram, a condenser may be provided between the alcohol converter 60 and the alcohol purification device 70. The condenser cools the gas discharged from the alcohol converter 60 and can separate it into unreacted residual gas and a condensate containing alcohol and water. Known devices such as water-cooled condensers, air-cooled condensers, and evaporative condensers can be used as the condenser.

[0047] The alcohol purification apparatus 70 is a device that performs a purification process to purify alcohol by purifying the condensate and separating water and impurities. The condensate obtained from the condenser is obtained as a liquid mixture containing alcohol and water, which are the products. The method for extracting alcohol from the mixture in the alcohol purification apparatus 70 is not particularly limited, but for example, water and impurities may be removed and alcohol obtained by dehydration and purification treatment using known methods. Examples of dehydration and purification treatment methods include distillation or membrane separation.

[0048] (Summary of Embodiment 1) The alcohol production method according to this embodiment includes: a gas production step of producing a first synthesis gas G1 containing carbon monoxide, carbon dioxide and hydrogen by steam reforming and / or partial oxidation of a carbon-containing raw material; a gas reforming step of producing a second synthesis gas G2 by reforming and / or adjusting the composition of a first supply gas GE1 containing carbon dioxide and hydrogen; and a conversion step of synthesizing alcohol by a conversion reaction from a second supply gas GE2 containing at least a portion of the first synthesis gas G1 and at least a portion of the second synthesis gas G2, wherein the gas reforming step is carried out using a gas reforming apparatus 40, which includes a reactor 401 that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas GE1 into carbon monoxide and water vapor by contacting it with a catalyst, and the reactor has a high-temperature section (first heat exchange section 422) for heating the reaction field and a cooling section (second heat exchange section 452) for condensing at least a portion of the reaction product. The waste heat from the gas production process is used as the heat source for the high-temperature section (first heat exchange section 422). The conversion process for synthesizing alcohol from the second supply gas GE2 can also be said to include a reduction process for reducing carbon oxide.

[0049] Generally, CO ２ The reverse shift reaction that converts to CO is an equilibrium endothermic reaction, and when carried out using conventional (non-internal condensation) fixed-bed reactors, fluidized-bed reactors, etc., a large amount of heat supply is required to improve the equilibrium conversion rate.

[0050] This disclosure uses a so-called internal condensation reactor, which has a cooling section that condenses at least a portion of the reaction products in the gas reforming process. This enables gas reforming with a high conversion rate at lower temperatures compared to conventional fixed-bed reactors. Although waste heat from the gas production process is used to supply heat to the gas reforming process, the heating of the reaction field in the gas reforming process can be set lower than in conventional methods, so the waste heat from the gas production process can be used without further heating. This makes it possible to realize an alcohol production method with excellent energy efficiency.

[0051] [Embodiment 2] Hereinafter, a hydrocarbon production method, which is one embodiment of the present disclosure, will be described in detail with reference to the drawings, along with the production apparatus used therein.

[0052] The hydrocarbon production method of this disclosure is a method for producing hydrocarbons from carbon-containing raw materials via carbon oxide, and includes a gas production step, a gas reforming step, and a conversion step, characterized in that the waste heat from the gas production step is used as a heat source for the gas reforming step. The differences from the alcohol production method described in Embodiment 1 are described in detail below.

[0053] (Configuration of the hydrocarbon manufacturing apparatus) An example of a hydrocarbon manufacturing apparatus according to this disclosure, manufacturing apparatus 101, will be described. Manufacturing apparatus 101 is an apparatus for manufacturing hydrocarbons from carbon-containing raw materials.

[0054] Figure 3 is a schematic diagram showing the configuration of the manufacturing apparatus 101 according to Embodiment 2. As shown in Figure 3, the manufacturing apparatus 101 includes a gas production apparatus 20, a gas cleaning apparatus 30, a gas reforming apparatus 40, and CO ２ The system is generally configured to include a separation device 50, a hydrocarbon converter 61, and a hydrocarbon purification device 71. ２ The separation device 50 may be used to adjust the composition of the feed gas supplied to the hydrocarbon converter 61. At least a portion of the second synthesis gas G2 may be supplied to the hydrocarbon converter 61 as at least a portion of the second feed gas GE2.

[0055] The hydrocarbon converter 61 receives CO, CO as the second supply gas GE2. ２, and H ２ This apparatus performs a conversion process in which a gas containing CO (carbon oxide-containing gas) is reacted with a catalyst to convert it into hydrocarbons. ２ It can also be said that this is a reduction process that reduces CO2. The hydrocarbon converter 61 may be a device that carries out a thermochemical reaction using, for example, the Fischer-Tropsch process. The hydrocarbons according to this disclosure may include liquid fuels containing light oils of C6 to C16 or heavy oils of C17 or higher. The second supply gas GE2 includes at least a portion of the first synthesis gas G1 produced by the gas production device 20 and at least a portion of the second synthesis gas G2 obtained by the gas reformer 40. The second supply gas GE2 is further supplied by the gas reformer 40 and CO2 ２ It may contain a modified second synthesis gas G2X whose components have been adjusted by the separation device 50.

[0056] The hydrocarbon converter 61 can include known reactors such as fixed-bed reactors, fluidized-bed reactors, and slurry-bed reactors. Alternatively, the hydrocarbon converter 61 may be a combination of multiple reactors.

[0057] The hydrocarbon purification apparatus 71 is a device that performs a purification process to separate and purify the hydrocarbons produced by the hydrocarbon converter 61. The hydrocarbons produced by the hydrocarbon converter 61 can be separated in the hydrocarbon purification apparatus 71 into liquid fuels with various carbon numbers, waxes, gaseous components, etc. For example, a distillation column can be used as the hydrocarbon purification apparatus 71.

[0058] (Summary of Embodiment 2) The hydrocarbon production method according to this embodiment includes: a gas production step of producing a first synthesis gas G1 containing carbon monoxide, carbon dioxide and hydrogen by steam reforming and / or partial oxidation of a carbon-containing raw material; a gas reforming step of producing a second synthesis gas G2 by reforming and / or adjusting the composition of a first supply gas GE1 containing carbon dioxide and hydrogen; and a conversion step of synthesizing hydrocarbons by a conversion reaction from a second supply gas GE2 containing at least a portion of the first synthesis gas G1 and at least a portion of the second synthesis gas G2, wherein the gas reforming step is carried out using a gas reforming apparatus 40, which includes a reactor 401 that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas GE1 into carbon monoxide and steam by contacting it with a catalyst, and the reactor has a high-temperature section (first heat exchange section 422) for heating the reaction field and a cooling section (second heat exchange section 452) for condensing at least a portion of the reaction products. The waste heat from the gas production process is used as the heat source for the high-temperature section (first heat exchange section 422). The conversion process for synthesizing hydrocarbons from the second supply gas GE2 can also be said to include a reduction process for reducing carbon oxide.

[0059] This disclosure describes the use of a so-called internal condensation reactor, which has a cooling section that condenses at least a portion of the reaction products in the gas reforming process. This enables gas reforming with a high conversion rate at lower temperatures compared to conventional fixed-bed reactors. Although waste heat from the gas production process is used to supply heat to the gas reforming process, the heating of the reaction field in the gas reforming process can be set lower than in conventional methods, so the waste heat from the gas production process can be used without further heating. This makes it possible to realize an energy-efficient hydrocarbon production method.

[0060] [Embodiment 3] Hereinafter, a hydrocarbon and alcohol production method, which is one embodiment of the present disclosure, will be described in detail with reference to the drawings, along with the production apparatus used therein.

[0061] The hydrocarbon and alcohol production method of this disclosure is a method for producing hydrocarbons and alcohols from carbon-containing raw materials via carbon oxide, and includes a gas production step, a gas reforming step, a conversion to alcohol step (first conversion step), and a conversion to hydrocarbon step (second conversion step), characterized in that waste heat from the gas production step is used as a heat source for the gas reforming step. Differences from the alcohol production method described above in Embodiment 1 are described in detail below.

[0062] (Configuration of Hydrocarbon and Alcohol Production Apparatus) An example of a hydrocarbon and alcohol production apparatus according to this disclosure, production apparatus 102, will be described. Production apparatus 102 is an apparatus for producing hydrocarbons and alcohols from carbon-containing raw materials. Production apparatus 102 differs from production apparatus 100 shown in Figure 1 in that it is equipped with a hydrocarbon converter 61 and a hydrocarbon purifier 71.

[0063] Figure 4 is a schematic diagram showing the configuration of the manufacturing apparatus 102 according to Embodiment 3. As shown in Figure 4, the manufacturing apparatus 102 includes a gas production apparatus 20, a gas cleaning apparatus 30, a gas reforming apparatus 40, and CO ２ The system is generally configured to include a separation device 50, an alcohol converter 60, an alcohol purifying device 70, a hydrocarbon converter 61, and a hydrocarbon purifying device 71. ２ The separation unit 50 can be used to adjust the composition of the feed gas supplied to the alcohol converter 60, as well as to adjust the composition of the feed gas supplied to the hydrocarbon converter 61. A portion of the second synthesis gas G2 can be supplied to the alcohol converter 60 as at least a portion of the second feed gas GE2. Another portion of the second synthesis gas G2 can be supplied to the hydrocarbon converter 61 as at least a portion of the third feed gas GE3.

[0064] The hydrocarbon converter 61 receives CO, CO as the third supply gas GE3. ２ , and H ２ This apparatus performs a conversion process in which a gas containing CO (carbon oxide-containing gas) is reacted with a catalyst to convert it into hydrocarbons. ２It can also be said that this is a reduction process that reduces CO2. The hydrocarbon converter 61 may be a device that carries out a thermochemical reaction using, for example, the Fischer-Tropsch process. The hydrocarbons in this disclosure may include liquid fuels containing light oils of C6 to C16 or heavy oils of C17 or higher. The third feed gas GE3 supplied to the hydrocarbon converter 61 includes a portion of the first synthesis gas G1 produced by the gas production device 20 and a portion of the second synthesis gas G2 obtained by the gas reformer 40. The third feed gas GE3 is further supplied to the gas reformer 40 and CO2. ２ It may contain a portion of the adjusted second synthesis gas G2X whose components have been adjusted by the separation device 50.

[0065] (Summary of Embodiment 3) The hydrocarbon and alcohol production method according to this embodiment includes: a gas production step of producing a first synthesis gas G1 containing carbon monoxide, carbon dioxide and hydrogen by steam reforming and / or partial oxidation of a carbon-containing raw material; a gas reforming step of producing a second synthesis gas G2 by reforming and / or adjusting the composition of a first supply gas GE1 containing carbon dioxide and hydrogen; a first conversion step of synthesizing alcohol by a conversion reaction from a second supply gas GE2 (carbon oxide-containing gas) containing a portion of the first synthesis gas G1 and a portion of the second synthesis gas G2; and a second conversion step of synthesizing hydrocarbon by a conversion reaction from a third supply gas GE3 (carbon oxide-containing gas) containing another portion of the first synthesis gas G1 and another portion of the second synthesis gas G2. The gas reforming process is carried out using a gas reforming apparatus 40, which includes a reactor 401 that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas GE1 into carbon monoxide and water vapor by contacting it with a catalyst, and a reactor having a high-temperature section (first heat exchange section 422) for heating the reaction field and a cooling section (second heat exchange section 452) for condensing at least a portion of the reaction products, and the waste heat from the gas production process is used as the heat source for the high-temperature section (first heat exchange section 422). Both the first conversion step for synthesizing alcohol from the second supply gas GE2 and the second conversion step for synthesizing hydrocarbons from the third supply gas GE3 can also be said to include a reduction step for reducing carbon oxide.

[0066] This disclosure uses a so-called internal condensation reactor, which has a cooling section that condenses at least a portion of the reaction products in the gas reforming process. This enables gas reforming with a high conversion rate at lower temperatures compared to conventional fixed-bed reactors. Although waste heat from the gas production process is used to supply heat to the gas reforming process, the heating of the reaction field in the gas reforming process can be set lower than in conventional methods, so the waste heat from the gas production process can be used without further heating. This makes it possible to realize an energy-efficient method for producing hydrocarbons and alcohols.

[0067] [Embodiment 4] Hereinafter, a method for producing a carbon oxide reduction product, which is one embodiment of the present disclosure, will be described in detail with reference to the drawings, along with the manufacturing apparatus used therefor.

[0068] The present disclosure is a method for producing a carbon oxide reduction product from a carbon-containing raw material via carbon oxide, comprising a gas production step, a gas reforming step, and a reduction step, characterized in that the waste heat from the gas production step is used as a heat source for the gas reforming step. The differences from the alcohol production method described in Embodiment 1 are described in detail below.

[0069] The carbon oxide reduction product produced by the method according to Embodiment 4 may be an alcohol, a hydrocarbon, carbon monoxide, dimethyl ether, formaldehyde, a ketone such as acetone or methyl ethyl ketone, a diol such as ethylene glycol or 1,3-propanediol, a carboxylic acid or ester thereof such as formic acid, acetic acid, methyl formate, or methyl acetate, or elemental carbon. Elemental carbon may be obtained by further reduction of carbon monoxide, or by thermal or catalytic decomposition of an alcohol, hydrocarbon, or carbon monoxide. The obtained carbon may be used as a raw material for a reaction in a blast furnace included in the gas production apparatus 20, or in another blast furnace.

[0070] (Configuration of the carbon oxide reduction product manufacturing apparatus) An example of a carbon oxide reduction product manufacturing apparatus according to this disclosure, manufacturing apparatus 103, will be described. Manufacturing apparatus 103 is an apparatus that produces carbon oxide reduction products from carbon-containing raw materials.

[0071] Figure 5 is a schematic diagram showing the configuration of the manufacturing apparatus 103 according to Embodiment 4. As shown in Figure 5, the manufacturing apparatus 103 includes a gas production apparatus 20, a gas cleaning apparatus 30, a gas reforming apparatus 40, and CO ２ The system is generally configured to include a separation device 50, a carbon oxide reduction device 62, and a reduced product purification device 72. ２ The separation device 50 may be used to adjust the composition of the supply gas supplied to the carbon oxide reduction device 62. At least a portion of the second synthesis gas G2 may be supplied to the carbon oxide reduction device 62 as at least a portion of the second supply gas GE2.

[0072] The carbon oxide reduction device 62 uses CO, CO2 supplied as the second supply gas GE2. ２ Carbon dioxide and H ２ This apparatus performs a reduction process in which a gas containing carbon dioxide is reacted in the presence of a catalyst to obtain a reduced product of carbon dioxide. When reducing to an alcohol, the aforementioned alcohol converter 60 can be used as the carbon dioxide reduction apparatus 62. When reducing to a hydrocarbon, the aforementioned hydrocarbon converter 61 can be used as the carbon dioxide reduction apparatus 62. When reducing to carbon monoxide, a carbon monoxide converter that produces carbon monoxide from carbon dioxide can be used as the carbon dioxide reduction apparatus 62. When reducing to an aldehyde, the carbon dioxide can be reduced to an alcohol or hydrocarbon, and then the alcohol or hydrocarbon can be oxidized or partially oxidized to reach the aldehyde. In this case, the aforementioned alcohol converter 60 or hydrocarbon converter 61 can be combined with an aldehyde converter that produces aldehyde from alcohol or hydrocarbon and used as the carbon dioxide reduction apparatus 62.

[0073] When reducing to carbon, carbon oxide can be reached by first reducing it to an alcohol, hydrocarbon, or carbon monoxide, and then further reducing or decomposing the alcohol, hydrocarbon, or carbon monoxide. In this case, the aforementioned alcohol converter 60, hydrocarbon converter 61, or carbon monoxide converter can be combined with a carbon converter that produces carbon from alcohol, hydrocarbon, or carbon monoxide to form a carbon oxide reduction device 62.

[0074] The second supply gas GE2 includes at least a portion of the first synthesis gas G1 produced by the gas production unit 20 and at least a portion of the second synthesis gas G2 obtained by the gas reformer 40. The second supply gas GE2 is further supplied by the gas reformer 40 and CO ２ It may contain a modified second synthesis gas G2X whose components have been adjusted by the separation device 50.

[0075] The carbon monoxide converter may be a device that carries out thermochemical reactions using, for example, a reverse shift reaction, dry reforming of methane, thermal decomposition, or catalytic decomposition. In dry reforming of methane, methane and carbon dioxide react to produce carbon monoxide and hydrogen. At least a portion of the hydrogen obtained by the carbon monoxide converter may be supplied to the gas reformer 40.

[0076] The aldehyde conversion apparatus may be a device that carries out a thermochemical reaction, for example, using a catalytic oxidation method for alcohols. Hydrogen may be generated in this thermochemical reaction. At least a portion of the hydrogen obtained by the aldehyde conversion apparatus may be supplied to the gas reforming apparatus 40. The aldehyde conversion apparatus may be a device that carries out partial oxidation of hydrocarbons, for example.

[0077] The carbon converter may be, for example, a device that performs thermal or catalytic decomposition of alcohol, methane, or carbon monoxide. Hydrogen may be generated by this thermal or catalytic decomposition. At least a portion of the hydrogen obtained by the carbon converter may be supplied to the gas reformer 40.

[0078] The aldehyde conversion apparatus can include known reactors such as fixed-bed reactors, fluidized-bed reactors, and slurry-bed reactors. The carbon conversion apparatus can include known reactors such as pyrolysis furnaces, fluidized-bed reactors, and plasma reactors. Furthermore, the aldehyde conversion apparatus and the carbon conversion apparatus may be a combination of multiple reactors.

[0079] The reduced product purification apparatus 72 is a device that performs a purification process to separate and purify the reduced products generated by the carbon oxide reduction apparatus 62. When purifying alcohol, the aforementioned alcohol purification apparatus 70 can be used in the reduced product purification apparatus 72. When purifying hydrocarbons from reduced products, the aforementioned hydrocarbon purification apparatus 71 can be used in the reduced product purification apparatus 72. When purifying aldehydes, for example, a distillation column, adsorption column, membrane separation apparatus, dehydration column, etc., can be used in the reduced product purification apparatus 72. When purifying elemental carbon, for example, a cyclone separator, filter apparatus, and dust collector, etc., can be used in the reduced product purification apparatus 72.

[0080] (Summary of Embodiment 4) The method for producing a carbon oxide reduction product according to this embodiment includes: a gas production step of producing a first synthesis gas G1 containing carbon oxide such as carbon monoxide and carbon dioxide by steam reforming and / or oxidation of a carbon-containing raw material; a gas reforming step of producing a second synthesis gas G2 by reforming and / or adjusting the composition of a first supply gas GE1 containing carbon dioxide and hydrogen; and a reduction step of reducing carbon oxide contained in a second supply gas GE2 which includes at least a portion of the first synthesis gas G1 and at least a portion of the second synthesis gas G2. The gas reforming step is carried out using a gas reforming apparatus 40, which includes a reactor 401 that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas GE1 into carbon monoxide and steam by contacting it with a catalyst, and a reactor having a high-temperature section (first heat exchange section 422) for heating the reaction field and a cooling section (second heat exchange section 452) for condensing at least a portion of the reaction product. The waste heat from the gas production process is used as the heat source for the high-temperature section (first heat exchange section 422). The oxidation in the gas production process may be complete oxidation and / or partial oxidation. In the gas production process, if the gas production apparatus 20 includes a blast furnace, a large amount of waste heat is generated because the reaction temperature is very high. Therefore, a large amount of thermal energy that can be used as a heat source for the high-temperature section can be obtained.

[0081] This disclosure uses a so-called internal condensation reactor, which has a cooling section that condenses at least a portion of the reaction products in the gas reforming process. This enables gas reforming with a high conversion rate at lower temperatures compared to conventional fixed-bed reactors. Although waste heat from the gas production process is used to supply heat to the gas reforming process, the heating of the reaction field in the gas reforming process can be set lower than in conventional methods, so the waste heat from the gas production process can be used without further heating. This makes it possible to realize an energy-efficient method for producing carbon oxide reduction products.

[0082] The scope of this disclosure is not limited to the embodiments 1 to 4 described above. For example, an alcohol production method according to one embodiment of this disclosure may include a gas production step, a gas reforming step, a first conversion step for synthesizing alcohol from a second supply gas GE2, and a second conversion step for synthesizing alcohol from a third supply gas GE3. The alcohol synthesized in the second conversion step may be the same as or different from the alcohol synthesized in the first conversion step. For example, a hydrocarbon production method according to one embodiment of this disclosure may include a gas production step, a gas reforming step, a first conversion step for synthesizing hydrocarbon from a second supply gas GE2, and a second conversion step for synthesizing hydrocarbon from a third supply gas GE3. The hydrocarbon synthesized in the second conversion step may be the same as or different from the hydrocarbon synthesized in the first conversion step. For example, a hydrocarbon production method according to one embodiment of the present disclosure may include a gas production step, a gas reforming step, a first conversion step for synthesizing hydrocarbons from a second feed gas GE2, and a second conversion step for synthesizing alcohols from a third feed gas GE3. For example, a carbon oxide reduction method according to one embodiment of the present disclosure may include a first reduction step for reducing carbon oxide to obtain any of alcohols, hydrocarbons, carbon monoxide, aldehydes, and carbon, and a second reduction step for reducing carbon oxide to obtain any of alcohols, hydrocarbons, carbon monoxide, aldehydes, and carbon. Furthermore, a method for producing hydrocarbons and / or alcohols and a carbon oxide reduction method according to one embodiment of the present disclosure may include three or more conversion steps.

[0083] [Summary] (A1) A method for producing a carbon oxide reduction product according to embodiment A1 of the present disclosure includes: a gas production step of producing a first synthesis gas containing carbon monoxide, carbon dioxide and hydrogen by steam reforming and / or partial oxidation of a carbon-containing raw material; a gas reforming step of producing a second synthesis gas by reforming a first supply gas containing carbon dioxide and hydrogen; and a conversion step of synthesizing hydrocarbons and / or alcohols by a conversion reaction from a second supply gas containing at least a portion of the first synthesis gas and at least a portion of the second synthesis gas, wherein the gas reforming step is carried out using a gas reforming apparatus that includes a reactor that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas into carbon monoxide and steam by contacting it with a catalyst, and the reactor has a high-temperature section for heating the reaction field and a cooling section for condensing at least a portion of the reaction products, and the waste heat from the gas production step is used as the heat source for the high-temperature section.

[0084] (A2) The method for producing a carbon oxide reduction product according to embodiment A2 of the present disclosure is, in embodiment A1, wherein the alcohol comprises ethanol or methanol.

[0085] (A3) In the method for producing a carbon oxide reduction product according to embodiment A3 of the present disclosure, in embodiment A1 or A2, the temperature of the reaction field in the gas reformer is 500°C or less.

[0086] (A4) In the method for producing a carbon oxide reduction product according to embodiment A4 of the present disclosure, in any of embodiments A1 to A3, the temperature of the cooling section is 0°C or higher and 180°C or lower.

[0087] (A5) The method for producing a carbon oxide reduction product according to embodiment A5 of the present disclosure is, in any of embodiments A1 to A4 above, wherein the catalyst is a catalyst containing a transition metal.

[0088] (A6) The method for producing a carbon oxide reduction product according to embodiment A6 of the present disclosure is, in any of embodiments A1 to A5 above, wherein the catalyst is a copper-containing catalyst.

[0089] (B1) A method for producing a carbon oxide reduction product according to embodiment B1 of the present disclosure includes: a gas production step of producing a first synthesis gas containing carbon oxide by steam reforming and / or oxidation of a carbon-containing raw material; a gas reforming step of producing a second synthesis gas by reforming a first supply gas containing carbon dioxide and hydrogen; and a reduction step of reducing carbon oxide contained in a second supply gas which includes at least a portion of the first synthesis gas and at least a portion of the second synthesis gas, wherein the gas reforming step is carried out using a gas reforming apparatus which includes a reactor that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas into carbon monoxide and steam by contacting it with a catalyst, and the reactor has a high-temperature section for heating the reaction field and a cooling section for condensing at least a portion of the reaction products, and the waste heat from the gas production step is used as the heat source for the high-temperature section.

[0090] (B2) A method for producing a carbon oxide reduction product according to embodiment B2 of the present disclosure, wherein, in embodiment B1, the carbon oxide reduction product comprises an alcohol, a hydrocarbon, carbon monoxide, an aldehyde, or carbon.

[0091] (B3) In the method for producing a carbon oxide reduction product according to embodiment B3 of the present disclosure, the temperature of the reaction field in the gas reformer is 500°C or less, in embodiment B1 or B2.

[0092] (B4) In the method for producing a carbon oxide reduction product according to embodiment B4 of the present disclosure, in any of embodiments B1 to B3, the temperature of the cooling section is 0°C or higher and 180°C or lower.

[0093] (B5) The method for producing a carbon oxide reduction product according to embodiment B5 of the present disclosure is, in any of embodiments B1 to B4 above, wherein the catalyst is a catalyst containing a transition metal.

[0094] (B6) The method for producing a carbon oxide reduction product according to embodiment B6 of the present disclosure is, in any of embodiments B1 to B5 above, wherein the catalyst is a copper-containing catalyst.

[0095] (C1) A method for producing a carbon oxide-containing gas according to embodiment C1 of the present disclosure is a method for producing a carbon oxide-containing gas used in a method for producing a carbon oxide reduction product, comprising: a gas production step of producing a first synthesis gas containing carbon oxide by steam reforming and / or oxidation of a carbon-containing raw material; and a gas reforming step of producing a second synthesis gas by reforming a first supply gas containing carbon dioxide and hydrogen, wherein the carbon oxide-containing gas comprises at least a portion of the first synthesis gas and at least a portion of the second synthesis gas, and the gas reforming step is carried out using a gas reforming apparatus equipped with a reactor that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas into carbon monoxide and steam by contacting it with a catalyst, the reactor having a high-temperature section for heating the reaction field and a cooling section for condensing at least a portion of the gas in the reactor, and the waste heat from the gas production step is used as the heat source for the high-temperature section.

[0096] (C2) A method for producing a carbon oxide reduction product according to embodiment C2 of the present disclosure involves reducing the carbon oxide contained in the carbon oxide-containing gas obtained from the method for producing a carbon oxide-containing gas described in embodiment C1 to obtain a carbon oxide reduction product.

[0097] (C3) A method for producing a carbon oxide reduction product according to embodiment C3 of the present disclosure involves synthesizing hydrocarbons and / or alcohols by an inversion reaction from a carbon oxide-containing gas obtained from the method for producing a carbon oxide-containing gas described in embodiment C1.

[0098] (C4) The method for producing a carbon oxide reduction product according to embodiment C4 of the present disclosure is wherein, in embodiment C3, the alcohol comprises ethanol or methanol.

[0099] (C5) In the method for producing a carbon oxide-containing gas according to embodiment C5 of the present disclosure, the temperature of the reaction field in the gas reformer is 500°C or less, in embodiment C1.

[0100] (C6) In the method for producing a carbon oxide-containing gas according to embodiment C6 of the present disclosure, the temperature of the cooling section is 0°C or higher and 180°C or lower, in embodiment C1.

[0101] (C7) The method for producing a carbon oxide-containing gas according to embodiment C7 of the present disclosure is, in embodiment C1, wherein the catalyst is a catalyst containing a transition metal.

[0102] (C8) The method for producing a carbon oxide-containing gas according to embodiment C8 of the present disclosure is, in embodiment C1, wherein the catalyst is a copper-containing catalyst.

[0103] (C9) A method for producing a first synthesis gas according to embodiment C9 of the present disclosure, comprising: a gas production step of producing a first synthesis gas containing carbon oxide by steam reforming and / or oxidation of a carbon-containing raw material; and a gas reforming step of producing a second synthesis gas by reforming a first supply gas containing carbon dioxide and hydrogen, wherein the gas reforming step is carried out using a gas reforming apparatus equipped with a reactor that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas into carbon monoxide and steam by contacting it with a catalyst, the reactor having a high-temperature section for heating the reaction field and a cooling section for condensing at least a portion of the gas in the reactor, and the waste heat from the gas production step is used as the heat source for the high-temperature section, the method for producing a first synthesis gas used in a method for producing a carbon oxide reduction product, comprising a gas production step of producing the first synthesis gas used as at least a portion of the second supply gas by steam reforming and / or oxidation of a carbon-containing raw material.

[0104] (C10) A method for producing a second synthesis gas according to embodiment C10 of the present disclosure, comprising: a gas production step of producing a first synthesis gas containing carbon oxide by steam reforming and / or oxidation of a carbon-containing raw material; and a gas reforming step of producing a second synthesis gas by reforming a first supply gas containing carbon dioxide and hydrogen, wherein the gas reforming step is carried out using a gas reforming apparatus equipped with a reactor that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas into carbon monoxide and steam by contacting it with a catalyst, the reactor having a high-temperature section for heating the reaction field and a cooling section for condensing at least a portion of the gas in the reactor, and the waste heat from the gas production step is used as the heat source for the high-temperature section, the method for producing a second synthesis gas used as at least a portion of the second supply gas.

[0105] [Additional Notes] This disclosure is not limited to the embodiments described above, and various modifications are possible within the scope of the claims. Embodiments obtained by appropriately combining the technical means disclosed in different embodiments are also included in the technical scope of this disclosure.

[0106] 100 Manufacturing equipment (alcohol manufacturing equipment) 101 Manufacturing equipment (hydrocarbon manufacturing equipment) 102 Manufacturing equipment (hydrocarbon and alcohol manufacturing equipment) 103 Manufacturing equipment (carbon oxide reduction product manufacturing equipment) 20 Gas manufacturing equipment 30 Gas cleaning equipment 40 Gas reforming equipment 401 Reactor 402 Catalyst layer 422 First heat exchange section (high temperature section) 452 Second heat exchange section (cooling section) 50 CO ２ Separation unit 60 Alcohol converter 61 Hydrocarbon converter 62 Carbon oxide reduction unit 70 Alcohol purification unit 71 Hydrocarbon purification unit 72 Reduced product purification unit G1 First synthesis gas G2 Second synthesis gas G2X Adjusted second synthesis gas GE1 First supply gas GE2 Second supply gas (carbon oxide-containing gas) GE3 Third supply gas (carbon oxide-containing gas)

Claims

1. A method for producing a carbon oxide-containing gas used in the production of carbon oxide reduction products, comprising: a gas production step of producing a first synthesis gas containing carbon oxide by steam reforming and / or oxidation of a carbon-containing raw material; and a gas reforming step of producing a second synthesis gas by reforming a first supply gas containing carbon dioxide and hydrogen, wherein the carbon oxide-containing gas comprises at least a portion of the first synthesis gas and at least a portion of the second synthesis gas; the gas reforming step is carried out using a gas reforming apparatus equipped with a reactor that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas into carbon monoxide and steam by contacting it with a catalyst, the reactor having a high-temperature section for heating the reaction field and a cooling section for condensing at least a portion of the gas in the reactor, and the waste heat from the gas production step is used as the heat source for the high-temperature section.

2. A method for producing a carbon oxide-reduced product, comprising reducing the carbon oxide contained in the carbon oxide-containing gas obtained from the method for producing a carbon oxide-containing gas described in claim 1 to obtain a carbon oxide-reduced product.

3. A method for producing a carbon oxide reduction product, comprising synthesizing hydrocarbons and / or alcohols by an inversion reaction from a carbon oxide-containing gas obtained from the method for producing a carbon oxide-containing gas described in claim 1.

4. The method for producing a carbon oxide reduction product according to claim 3, wherein the alcohol includes ethanol or methanol.

5. The method for producing a carbon oxide-containing gas according to claim 1, wherein the temperature of the reaction field in the gas reforming apparatus is 500°C or lower.

6. The method for producing a carbon oxide-containing gas according to claim 1, wherein the temperature of the cooling section is 0°C or higher and 180°C or lower.

7. The method for producing a carbon oxide-containing gas according to claim 1, wherein the catalyst is a catalyst containing a transition metal.

8. The method for producing a carbon oxide-containing gas according to claim 1, wherein the catalyst is a copper-containing catalyst.

9. A method for producing a first synthesis gas used in a method for producing a carbon oxide reduction product, comprising: a gas production step of producing a first synthesis gas containing carbon oxide by steam reforming and / or oxidation of a carbon-containing raw material; and a gas reforming step of producing a second synthesis gas by reforming a first supply gas containing carbon dioxide and hydrogen, wherein the gas reforming step is carried out using a gas reforming apparatus equipped with a reactor that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas into carbon monoxide and steam by contacting it with a catalyst, the reactor having a high-temperature section for heating the reaction field and a cooling section for condensing at least a portion of the gas in the reactor, and the waste heat from the gas production step is used as the heat source for the high-temperature section, the method comprising a gas production step of producing the first synthesis gas used as at least a portion of the second supply gas by steam reforming and / or oxidation of a carbon-containing raw material.

10. A method for producing a second synthesis gas used in a method for producing a carbon oxide reduction product, comprising: a gas production step of producing a first synthesis gas containing carbon oxide by steam reforming and / or oxidation of a carbon-containing raw material; and a gas reforming step of producing a second synthesis gas by reforming a first supply gas containing carbon dioxide and hydrogen, wherein the gas reforming step is carried out using a gas reforming apparatus equipped with a reactor that converts at least a portion of the carbon dioxide and hydrogen contained in the first supply gas into carbon monoxide and steam by contacting it with a catalyst, the reactor having a high-temperature section for heating the reaction field and a cooling section for condensing at least a portion of the gas in the reactor, and the waste heat from the gas production step is used as the heat source for the high-temperature section, the method comprising a gas reforming step of producing the second synthesis gas used as at least a portion of the second supply gas by reforming a first supply gas containing carbon dioxide and hydrogen.

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