Valuable material production system, valuable material production apparatus, and valuable material production method

Abstract

To provide a valuable material production system and the like that enable production of a valuable material with lowered environmental load and cost.SOLUTION: According to one embodiment of the present invention, a valuable material production system is provided, the production system comprising: a gas generation unit that generates a source gas containing carbon monoxide and carbon dioxide; a gas separation unit that separates a separation gas containing carbon dioxide from the source gas; a gas liquefaction unit that liquefies the carbon dioxide in the separation gas; a valuable material generation unit that generates a valuable material from the source gas having the separation gas separated therefrom; and a post-treatment unit that performs post-treatment of at least the valuable material.SELECTED DRAWING: Figure 1

Description

[Technical Field]

[0001] The present invention relates to a valuable material production system, a valuable material production device, and a valuable material production method. [Background technology]

[0002] In recent years, efforts have been made to produce valuable materials with low environmental impact by using carbon monoxide in synthesis gas generated during waste treatment as a raw material for valuable materials such as organic substances (see, for example, Patent Document 1). [Prior art documents] [Patent documents]

[0003] [Patent Document 1] Japanese Patent Publication No. 2022-159562 Summary of the Invention [Problem to be solved by the invention]

[0004] However, in Patent Document 1, although valuable materials are produced by extracting carbon monoxide from synthesis gas, it is difficult to say that other compounds in the synthesis gas are fully utilized. In other words, the other compounds are exhausted, and there is room for reduction in the environmental load and costs involved in producing valuable materials.

[0005] In view of the above circumstances, the present invention provides a valuable material production system and the like that can produce valuable materials while reducing environmental load and costs. [Means for solving the problem]

[0006] According to one aspect of the present invention, there is provided a system for producing valuable materials, comprising: a gas generator that produces a raw material gas containing carbon monoxide and carbon dioxide; a gas separator that separates a separated gas containing carbon dioxide from the raw material gas; a gas liquefaction unit that liquefies the carbon dioxide in the separated gas; a valuable material generator that produces valuable materials from the raw material gas from which the separated gas has been separated; and a post-processing unit that post-processes at least the valuable materials.

[0007] According to this aspect, valuable materials can be produced while reducing environmental load and costs. [Brief explanation of the drawings]

[0008] [Figure 1] 1 is a schematic diagram showing the configuration of a system for producing an organic substance according to the present invention. [Figure 2] FIG. 2 is a schematic diagram showing an example of the configuration of a PSA device in a pretreatment section. [Figure 3] FIG. 1 is a diagram showing an example of the shape of a porous material used in a PSA device. [Figure 4] FIG. 1 is a schematic diagram showing an example of a cross section of a reactor of a PSA device. [Figure 5] FIG. 1 is a schematic diagram showing an example of a cross section of a reactor of a PSA device. DETAILED DESCRIPTION OF THE INVENTION

[0009] Hereinafter, a system for producing valuable materials, an apparatus for producing valuable materials, and a method for producing valuable materials will be described in detail with reference to the accompanying drawings. Note that the following description will be given assuming that the valuable materials are organic substances as an example. First, an organic substance production system according to one embodiment of the valuable resource production system will be described. Fig. 1 is a schematic diagram showing the configuration of the organic substance production system of the present invention. As will be described in detail below, the organic substance production system is a system capable of producing liquefied carbon dioxide and mainly organic substances from exhaust gas.

[0010] The organic substance manufacturing system 100 (hereinafter also simply referred to as "manufacturing system 100") shown in Figure 1 includes a gasification furnace (gas generation section) 10 and an organic substance manufacturing apparatus 1 (hereinafter also simply referred to as "manufacturing apparatus 1") connected to the gasification furnace 10. In this specification, the upstream side with respect to the flow direction of gas and liquid is also simply referred to as the "upstream side," and the downstream side is also simply referred to as the "downstream side." In this embodiment, the gasifier 10 is not particularly limited, but examples thereof include a fluidized bed furnace, a kiln furnace, a shaft furnace, etc. In addition to the gasifier 10, the gas generating unit may be a CO2 generating unit of at least one facility selected from a combustion furnace (incinerator), a paper mill, a cement factory, a thermal power plant, an oil refinery, an ethylene cracker, a refinery, a chemical plant, a blast furnace in a steel mill, a converter, or an electric furnace (electric furnace). x It may also be an emission source.

[0011] In each furnace, exhaust gas (raw material gas) containing carbon monoxide and carbon dioxide is generated (produced) when the contents are burned, melted, refined, etc. In the case of a combustion furnace or gasification furnace at a waste incineration plant, the contents (waste) include, for example, plastic waste, food waste, municipal solid waste (MSW), industrial waste, discarded tires, biomass waste, household waste (futons, paper), building materials, etc. These wastes may contain one type alone or two or more types. In addition, in the case of a blast furnace, converter, or electric furnace in a steelworks, exhaust gas is generated (or produced) when, for example, iron ore is heated together with coke, limestone, etc. In the case of a chemical plant, exhaust gas is generated (or produced) when, for example, methane is steam reformed.

[0012] The carbon in exhaust gases derived from waste, etc. is different from the carbon in petroleum. 14 C. 13 The abundance ratio of carbon isotopes such as C (e.g., δ 14 C, δ 13The carbon isotope ratios contained in the organic substances and liquefied carbon dioxide produced by the production system 100 using exhaust gas as a raw material are different from those of the organic substances and liquefied carbon dioxide derived from petroleum. Therefore, even if the organic substances or liquefied carbon dioxide produced by the production system 100 are converted into other compounds and used, it is possible to determine (trace) that they are derived from the organic substances or liquefied carbon dioxide produced by the method of the present invention, which has a low environmental impact.

[0013] Exhaust gas typically contains, in addition to carbon dioxide and carbon monoxide, other gas components such as hydrogen, nitrogen, oxygen, water vapor, methane, etc. Exhaust gas may further contain other components such as soot, tar, nitrogen compounds, sulfur compounds, phosphorus-based compounds, aromatic compounds, etc. The exhaust gas may be generated as a gas containing 10% or more by volume of carbon monoxide by subjecting the contents (carbon source) to a heat treatment (commonly known as gasification) that incompletely combusts the contents (carbon source) (i.e., by partially oxidizing the carbon source).

[0014] If valuable materials such as organic substances are produced using exhaust gas, carbon sources such as carbon dioxide that have conventionally been emitted into the atmosphere can be effectively utilized, thereby reducing the burden on the environment. From the viewpoint of carbon circulation, it is preferable to use exhaust gas generated in a combustion furnace or a smelter. The gasifier 10 may have an oxygen generator that generates oxygen necessary for combustion. Examples of oxygen generators include cryogenic separation devices that compress, cool, and liquefy atmospheric air to extract liquefied oxygen, liquefied nitrogen, and the like. The endothermic heat generated when the resulting liquefied nitrogen evaporates can be utilized, particularly, for generating liquefied carbon dioxide in the liquefaction unit 8 (see below). Furthermore, the nitrogen gas obtained by evaporating the liquefied nitrogen can be suitably used as a purge gas for each part of the production system 100.

[0015] The gasifier 10 may also have a reforming area inside or outside thereof for reforming the exhaust gas. The reforming area converts methane, ethane, and other gases, as well as hydrocarbons such as char, tar, and dioxins, contained in the exhaust gas into carbon monoxide and hydrogen by retaining the exhaust gas at high temperatures. At this time, a combustion-supporting gas such as oxygen or air may be supplied to raise the temperature. Furthermore, a portion of the carbon monoxide may be converted to carbon dioxide by reacting with oxygen. The temperature is preferably 1000°C or higher, and more preferably 1100°C or higher and 1400°C or lower.

[0016] In the reforming area, a method may be adopted in which steam is reacted with hydrocarbons such as methane contained in the exhaust gas at high temperatures in the presence of a catalyst to convert them into carbon monoxide and hydrogen. At this time, part of the carbon monoxide may be further converted into carbon dioxide and hydrogen by reacting with steam. The reaction temperature is preferably 500° C. or higher and 1200° C. or lower. Examples of the catalyst include nickel catalysts, nickel oxide catalysts, ruthenium catalysts, rhodium catalysts, palladium catalysts, and platinum catalysts. Here, the stable carbon isotope ratio δ 13 C has δ 13 The value of C tends to be high, and incomplete combustion causes δ 13 Therefore, by providing a reforming area, the exhaust gas will have its own δ 13 Therefore, even if the organic substance or liquefied carbon dioxide produced by the production system 100 is converted into another compound and used, it can be determined (traced) that it originates from the organic substance or liquefied carbon dioxide produced by the method of the present invention, which has a low environmental impact.

[0017] The synthesis gas (hereinafter also referred to as "exhaust gas") generated by the gasifier 10 is at a high temperature. The heat of this high-temperature exhaust gas may be used to generate steam from water. For example, a tank storing water may be provided in the gas line GL1 connected downstream of the gasifier 10, and steam may be generated by heat exchange between the exhaust gas and the water. Alternatively, a heat recovery device suitable for recovering high-temperature heat, such as an economizer, may be provided near the gasifier 10 and the gas line GL1, and steam may be generated by heat exchange with the exhaust gas using the heat recovery device. In this way, by efficiently recovering the heat of the exhaust gas and utilizing it without waste, the environmental impact during the production of organic substances and liquefied carbon dioxide can be further reduced. However, the heat of the exhaust gas may be used for various purposes, without being limited to this purpose. A manufacturing apparatus 1 is connected to the gasification furnace 10. The manufacturing apparatus 1 has a generation section (organic substance generation section) 2, and the gasification furnace 10 and the generation section 2 are connected by a gas line GL1.

[0018] The generation unit 2 generates mainly organic substances (hereinafter also simply referred to as "organic substances") from the supplied exhaust gas (raw material gas). Specifically, molecules in the exhaust gas can be reacted with a catalyst or the like to generate organic substances (carbon valuables). Examples of such organic substances include alcohols such as methanol and ethanol, organic acids such as acetic acid and formic acid, and sustainable aviation fuel (SAF). For example, the catalyst can be used to add hydrogen to carbon monoxide in the exhaust gas to generate the organic substances. Examples of the catalyst used here include lithium (Li), sodium (Na), manganese (Mn), rhenium (Re), ruthenium (Ru), cobalt (Co), rhodium (Rh), nickel (Ni), palladium (Pd), and alloys of these elements that combine elements belonging to different groups in the periodic table. The catalyst is preferably a metal catalyst, but is not particularly limited. The organic substances generated in the generation unit 2 are generated using carbon derived from the exhaust gas, and are therefore different from organic substances derived from petroleum. 14 C. 13 The abundance ratio of carbon isotopes such as C (e.g., δ14 C, δ 13 Therefore, even if this organic substance is converted into other compounds or other products and used, it can be determined (traced) that it originates from the organic substance produced by the method of the present invention, which has a low environmental impact. Furthermore, the valuable resource is not limited to organic substances and may contain, for example, ammonia. When the valuable resource contains ammonia, the generation unit 2 can generate ammonia by, for example, allowing nitrogen and hydrogen in the exhaust gas to act on a catalyst containing iron (Fe), ruthenium (Ru), or the like.

[0019] Instead of or in addition to a reaction using a non-biocatalyst, the production unit 2 may produce the above-mentioned organic substances from molecules in the exhaust gas by the action of a biocatalyst such as a gas-assimilating bacterium. Examples of gas-assimilating bacteria that can be used include Butyribacterium methylotrophicum, Clostridium autoethanogenum, Clostridium carboxidivorans, Clostridium ljungdahlii, Clostridium ragsdalei, Moorella, and Carboxydothermus. When microorganisms such as gas-utilizing bacteria are used as biocatalysts, 14 C. 13 The abundance ratio of carbon isotopes such as C (e.g., δ 14 C, δ 13 Therefore, even if the produced organic substance is converted into another compound and used, it can be more easily identified (traced) as being derived from the organic substance produced by the method of the present invention, which has a low environmental impact.

[0020] Furthermore, multiple types of molecules in the exhaust gas may be reacted with a catalyst to generate multiple types of compounds. Note that the raw materials such as hydrogen supplied to the generation unit 2 may be contained in the exhaust gas, or may be supplied separately from a hydrogen supply source (gas tank).

[0021] A pretreatment section 5 is provided in the middle of the gas line GL1. The exhaust gas generated in the gasification furnace 10 is supplied to the pretreatment section 5. The pretreatment section 5 has a PSA device (gas separation section). FIG. 2 is a diagram showing an example of the configuration of the PSA device in the pretreatment section. FIG. 3 is a diagram showing an example of the shape of a porous material used in the PSA device. FIG. 4 is a schematic diagram showing an example of the cross section of a reactor of a PSA device. FIG. 5 is a schematic diagram showing an example of the cross section of a reactor of a PSA device. A PSA unit is a pressure swing adsorption separator that removes (separates) a separated gas containing carbon dioxide from exhaust gas (feed gas). Separating carbon dioxide from exhaust gas using a PSA unit can significantly increase the separation efficiency. In other words, the carbon dioxide concentration in the separated gas can be made relatively high. Furthermore, compared to using a TSA unit, no thermal energy is required to separate and recover carbon dioxide from the PSA unit after separating it from exhaust gas, making it possible to produce organic substances and liquefied carbon dioxide with a low environmental impact.

[0022] As shown in FIG. 2, the PSA device has reactors 51a and 51b through which exhaust gas passes and from which separated gases are separated. In reactors 51a and 51b, for example, porous materials such as activated carbon, zeolite, silica gel, and molecular sieves, or aqueous solutions such as amine solutions, can be used as adsorbents. Activated carbon or zeolite is preferably used in the PSA device. By selecting the type of porous material and the pore size, it is possible to select the compounds that can be separated. In FIG. 2, the porous material is indicated by a shaded area.

[0023] As shown by the solid black arrows in Figure 2, when exhaust gas is passed through reactor 51a, the exhaust gas comes into contact with the porous material, causing carbon dioxide to be adsorbed by the porous material. At the same time, when a purge gas (nitrogen, hydrogen, argon, helium, etc.) is passed through reactor 51b while the pressure inside is reduced, as shown by the solid white arrows in Figure 2, the carbon dioxide and other gases adsorbed by the porous material are released and can be recovered. The recovered gas containing carbon dioxide is the separated gas. After a certain period of time, the porous material in reactor 51a becomes saturated with carbon dioxide, reducing the carbon dioxide adsorption capacity of the porous material. In this case, as shown by the black dotted arrow in Figure 2, exhaust gas is passed through reactor 51b instead of reactor 51a. As described above, carbon dioxide has already been desorbed from the porous material in reactor 51b. Therefore, the carbon dioxide in the exhaust gas is adsorbed by the porous material in reactor 51b. At the same time, the pressure in reactor 51a is reduced and purge gas is passed through reactor 51a as shown by the white dotted arrow in Figure 2. This causes the carbon dioxide and other substances adsorbed by the porous material to desorb and be recovered. When the gasification furnace 10 has an oxygen generator and liquid nitrogen can be obtained, it is preferable to use nitrogen gas obtained by vaporizing the liquid nitrogen as the purge gas.

[0024] The number of reactors in the PSA device is not limited to two, but is preferably two or more. This allows exhaust gas to pass through one reactor to adsorb carbon dioxide while the other reactor desorbs carbon dioxide. As a result, a porous material from which carbon dioxide has been desorbed is prepared in one of the reactors, and by passing exhaust gas through the reactors while switching between them, separated gases can be continuously produced from the exhaust gas.

[0025] The reactors 51a and 51b of the PSA device are generally filled with granular (spherical or cylindrical) porous materials. Among the granular porous materials, those with a cross section resembling three columnar grains lined up (i.e., a cloverleaf-shaped cross section), as shown in FIG. 3, are preferred. In this case, there are many gaps through which exhaust gas can pass, preventing or suppressing unnecessary increases in the packing density of the porous material. Therefore, exhaust gas can smoothly pass through the reactors 51a and 51b, making it easy to reduce pressure loss. Furthermore, instead of filling the reactors 51a and 51b with granular porous material, the porous material may be formed into a molded body having a large number of mutually partitioned small spaces 53 and then filled, as shown in FIG. The large number of small spaces 53 may be formed so as to partition the internal spaces of the reactors 51a and 51b in a direction perpendicular to the direction in which the exhaust gas passes through the reactors 51a and 51b. In other words, the partition walls 52 that partition each small space 53 of the molded body may have an elongated cylindrical shape extending along the direction in which the exhaust gas passes. This configuration can more effectively prevent turbulence in the flow of the exhaust gas passing through each small space 53, thereby further reducing pressure loss.

[0026] Reducing the pressure loss of the exhaust gas allows the exhaust gas to flow at a relatively low pressure, making it possible to produce organic substances and liquefied carbon dioxide with less power consumption. Furthermore, since the exhaust gas flows at a low flow rate, it is easy to ensure sufficient contact between the exhaust gas and the porous material. In other words, since the porous material can easily adsorb carbon dioxide, it is easy to increase the concentration of carbon dioxide in the separated gas.

[0027] When reactors 51a and 51b are enlarged, they must be designed to withstand the pressure changes (pressure increase and pressure decrease) of the pressure swing adsorption system, so there is a limit to how large they can be in the radial direction. Therefore, when reactors 51a and 51b are enlarged, they are manufactured to have an elongated shape. Therefore, in order to allow the exhaust gas to pass smoothly through reactors 51a and 51b, the exhaust gas must be supplied at a certain level of high pressure and high flow rate. In this case, when a large number of small spaces 53 are formed, the exhaust gas can be preferentially passed through the small spaces 53 compared to when the porous material is filled with granular porous material. Therefore, it is less likely that the high-flow rate exhaust gas will pass between the particles, preventing the porous material from adsorbing carbon dioxide. Furthermore, because the porous material is not arranged so as to block the direction in which the exhaust gas passes, it is possible to prevent unnecessary molecules (impurity molecules) other than carbon dioxide from being forcibly adsorbed (supported) by the porous material due to the high pressure of the exhaust gas. In other words, when a large number of small spaces 53 are formed, the selectivity of the porous material is less likely to decrease when exhaust gas is passed through at a high flow rate, making it easier to increase the size of the reactors 51a and 51b. Furthermore, as described above, when a large number of small spaces 53 are formed, the pressure loss is smaller than when the reactors are filled with a granular porous material, and therefore the exhaust gas can pass through at a relatively low pressure and a low flow rate. Therefore, in this case, even if the reactors 51a and 51b are enlarged, the exhaust gas can pass through at a relatively low pressure and a low flow rate.

[0028] The cross-sectional shape of the partition wall 52 taken along the orthogonal direction may be a circle or an ellipse as shown in Fig. 5, or may be a polygonal shape such as a square, rectangle, parallelogram, trapezoid, triangle, or hexagon as shown in Fig. 4. In particular, when the cross-sectional shape is a polygon, it is easy to arrange a plurality of small spaces 53 closely, which makes it easy to increase the contact area between the exhaust gas and the porous material. It is particularly preferable that the cross-sectional shape of the partition wall 52 along the orthogonal direction is hexagonal. In this case, the cross-sectional shape can be said to be honeycomb-shaped. With such a configuration, a plurality of small spaces 53 can be arranged regularly and densely, thereby further improving the carbon dioxide concentration in the separated gas. Furthermore, since the corners of the partition wall 52 are obtuse angles, sufficient space can be secured even at the corners. This makes it difficult for the exhaust gas to be compressed, and therefore pressure loss can be sufficiently reduced. As a result, the exhaust gas can be made to flow at a lower pressure and a lower flow rate, and an increase in the above-mentioned effects can be expected.

[0029] The PSA unit may further be used to separate and remove nitrogen, BTEX (benzene, toluene, ethylbenzene, xylene), and the like. The nitrogen separated by the PSA unit may be filled into the PSA unit and / or TSA unit (if used), the deoxidizer (if used) and / or deacetylenizer (if used), the piping of the gas analysis equipment, the equipment in the gasification furnace process, etc. for cleaning each part of the system, or may be filled into a cylinder to seal the generated organic substances to prevent oxidation, or may be filled into two or more of the listed units. Note that nitrogen may be filled into only one or two or more of the listed units.

[0030] When separating two or more compounds in a PSA device, multiple separators filled with porous materials of different types or pore sizes may be used, or a single separator filled with porous materials of different types or pore sizes may be used. In this way, by removing carbon dioxide and the like from the exhaust gas, the volume of the exhaust gas to be treated downstream can be reduced, and therefore the generation unit 2 arranged downstream can be made smaller.

[0031] In addition to the PSA unit, the pretreatment unit 5 may include a scrubber, a dehydrator (dehumidifier), a filter, a deoxygenator, a deacetylenizer, a dehydrogenator, a TSA unit, a PTSA unit, a reduction unit, an impurity removal unit, and the like. These units can be used alone or in any combination. The order in which these units are arranged is arbitrary, but if they are installed upstream of the PSA unit, the carbon dioxide concentration in the exhaust gas flowing into the PSA unit increases, thereby increasing the carbon dioxide concentration in the separated gas. The higher the carbon dioxide concentration in the separated gas, the less energy is required to purify the liquefied carbon dioxide, and therefore liquefied carbon dioxide can be produced with a lower environmental impact.

[0032] Scrubbers are used to remove pollutants (e.g., soot), water-soluble substances, and the like contained in exhaust gas. In a scrubber, cleaning is performed by bringing a cleaning liquid into contact with the object to be removed (wet cleaning method). An example of a wet cleaning method is a cleaning method using a water curtain. Examples of cleaning liquids include water, acidic solutions, and alkaline solutions. Among these, water is preferred as the cleaning liquid. The temperature of the cleaning liquid is usually 40°C or less, preferably 30°C or less, more preferably 25°C or less, and even more preferably 15°C or less.

[0033] A dehydrator (dehumidifier) is used to dehydrate exhaust gas whose moisture content has increased due to scrubbing with a scrubber. This dehydrator (dehumidifier) may be, for example, a cooling device that cools the exhaust gas to condense it and remove moisture, or a device that removes moisture by passing the exhaust gas through a membrane separation device such as a membrane dryer, or a mist separator. It may also be a device that adsorbs and removes moisture using a moisture adsorbent such as a porous material, alumina (Al2O3), or silica gel, a moisture absorbent such as calcium chloride, or a moisture absorbing liquid such as monoethylene glycol or diethylene glycol.

[0034] The filter is used to remove particles smaller than the size of soot, and may be, for example, a bag filter. The deoxidizer is used to remove oxygen and can be configured as a reactor filled with metal particles such as copper (Cu), platinum (Pt), nickel (Ni), etc. as an oxygen removal catalyst. The oxygen removal catalyst is preferably heated to, for example, 150°C or higher and 400°C or lower. The deacetyleneizer is used to remove acetylene, and can be configured with a reactor filled with particles of a noble metal such as palladium (Pd) or platinum (Pt) as an acetylene removal catalyst. By removing acetylene prior to deoxidation, there is an advantage that the adverse effect of acetylene on the oxygen removal catalyst can be suitably prevented or reduced.

[0035] The dehydrogenation device is used to remove hydrogen, and can be configured, for example, with a separator containing a cylindrical separation membrane that selectively permeates and separates hydrogen. Examples of materials constituting such separation membranes include metal materials, ceramic materials, and resin materials. Examples of the metal material include Pd-Cu alloy, Pd-Ag alloy, vanadium alloy, and amorphous alloy such as La-Ni-Mg alloy. Examples of ceramic materials include titanium nitride, zeolite, silica (glass), alumina (Al2O3), and composite materials containing one or more of these (for example, alumina carbon-based materials). Examples of the resin material include polyamide, polyimide, and polysulfone.

[0036] The TSA unit is a temperature swing adsorption separator used to remove aromatic compounds other than BTEX, hydrogen cyanide, etc. The PTSA unit is a pressure and temperature swing adsorption type separator, and is used, for example, to collectively remove the components that are removed by the PSA unit and the TSA unit. The types of adsorbents and constituent materials used in the TSA and PTSA devices can be the same as those explained for the PSA device.

[0037] The oxygen removed by the deoxidizer may be configured to be supplied to the gasifier 10 in order to increase the heating temperature in the gasifier 10. This not only reduces the effort required to transport oxygen from another location to supply it to the gasifier 10, but also further reduces the environmental load when producing organic substances and liquefied carbon dioxide.

[0038] The reduction device is configured to produce carbon monoxide from carbon dioxide using hydrogen, for example, through a catalytic reverse water gas shift reaction or a chemical looping reaction. The reduction device is, for example, a reactor filled with a catalyst. When the pretreatment unit 5 includes a dehydrogenation device, the reduction device is preferably configured to produce carbon monoxide from carbon dioxide using hydrogen removed by the dehydrogenation device. This allows organic substances and liquefied carbon dioxide to be produced with a lower environmental impact than when hydrogen is transported from another location. Alternatively, hydrogen obtained by electrolysis of water using green electricity generated by natural energy sources such as wind, hydropower, solar, and geothermal energy may be used. This further reduces the environmental impact of producing organic substances and liquefied carbon dioxide. When producing carbon monoxide from carbon dioxide in the exhaust gas, the oxygen concentration in the reduction device (i.e., in the reduction reaction environment) is preferably 1% by volume or less. This prevents or suppresses inhibition of the reduction reaction by oxygen. By providing a reduction device, the amount of carbon monoxide converted into organic substances can be increased, thereby improving the yield of organic substances.

[0039] The configuration of the reduction device is not limited to the above configuration, and may be configured to reduce carbon dioxide to carbon monoxide using a reducing agent, for example. The reducing agent is not particularly limited as long as it can extract oxygen element from carbon dioxide and reduce the carbon dioxide. Such a reducing agent preferably contains a compound having oxygen ion conductivity (so-called oxygen carrier). As this oxygen carrier, for example, a metal oxide containing at least one metal element selected from the metal elements belonging to groups 3 to 12 can be used. In addition, in the reducing agent, the oxygen carrier may be supported on a carrier such as a carbon material (graphite, graphene, etc.), zeolite, montmorillonite, SiO2, ZrO2, TiO2, VO5, MgO, alumina (Al2O3), or silica.

[0040] In this case, the oxidized reducing agent after reducing carbon dioxide can be reduced using, for example, a reducing gas containing at least one selected from hydrogen, hydrocarbons (e.g., methane, ethane, acetylene, etc.), and ammonia removed in the pretreatment unit 5. In this case, the reduction device preferably has two or more reactors filled with reducing agent. This allows exhaust gas to pass through one reactor to perform the reduction reaction of carbon dioxide, while reducing gas is passed through the other reactor to perform the reduction reaction of the oxidized reducing agent. As a result, an activated reducing agent is prepared in one of the reactors, and by passing exhaust gas through the reactors while switching between them, the reduction reaction of carbon dioxide can be continuously performed by chemical looping. The reduction device may also be configured to reduce carbon dioxide to carbon monoxide through a reduction reaction of carbon dioxide using electrical energy.

[0041] The impurity removal device removes impurities such as sulfur or sulfur compounds, chlorine or chlorine compounds, and cyanide compounds. Among these, it is preferable to remove sulfur compounds, especially hydrogen sulfide, as impurities. Removal of hydrogen sulfide can effectively prevent an extreme decrease in reactivity or deactivation of the catalyst and filler downstream of the impurity removal device. The impurity removal device can be composed of, for example, a reactor filled with a desulfurizing agent.

[0042] The PSA unit in the pretreatment unit 5 is connected to a liquefaction unit (gas liquefaction unit) 8 via a gas line GL2. As a result, the separated gas separated in the PSA unit is supplied to the liquefaction unit 8 and becomes a raw material for liquefied carbon dioxide. The carbon dioxide content in the separated gas is preferably 20% by volume or more and 80% by volume or less, more preferably 30% by volume or more and 75% by volume or less, and even more preferably 35% by volume or more and 70% by volume or less.

[0043] The liquefaction unit 8 includes a high-pressure compressor and the like for liquefying the carbon dioxide in the separated gas. If the production system 100 includes an oxygen generator and liquefied nitrogen is obtained, it is preferable to liquefy the carbon dioxide by lowering the temperature of the carbon dioxide using the heat absorbed when the liquefied nitrogen evaporates. This further reduces the energy consumed when producing liquefied carbon dioxide. Furthermore, if electricity is used in the liquefaction unit 8, it is preferable to use green electricity generated from natural energy sources such as wind, hydropower, solar, and geothermal energy. This further reduces the environmental impact when producing liquefied carbon dioxide and enables efficient production. Furthermore, the average temperature of the separated gas during liquefaction of carbon dioxide is preferably higher than the boiling point of nitrogen. More specifically, the difference between the average temperature of the separated gas during liquefaction and the boiling point of nitrogen is preferably about 20°C or more and 100°C or less. With such a sufficient temperature difference, it is considered that the nitrogen in the separated gas is in a gaseous state or a supercritical state, and the carbon dioxide is in a liquid state or a solid state, regardless of the pressure of the separated gas. Therefore, even if the separated gas contains nitrogen, it is easy to separate nitrogen and carbon dioxide. Therefore, high-purity liquefied carbon dioxide can be easily produced from the separated gas. The average temperature of the separated gas during liquefaction can be appropriately set depending on the pressure of the separated gas during liquefaction.

[0044] The liquefaction unit 8 may further include a PSA device, a filter, a dehumidifier, etc. for increasing the carbon dioxide concentration in the separated gas. The purity of the liquefied carbon dioxide obtained by the liquefaction unit 8 is preferably 95% or more, more preferably 99% or more, and even more preferably 99.99% or more. As mentioned above, the carbon dioxide content in the separated gas is relatively high. Therefore, even if the carbon dioxide is further purified, less energy is required. In addition, it is possible to replace the PSA unit, filter, dehumidifier, etc. used to purify carbon dioxide with simpler units. In other words, the amount of energy required to produce liquefied carbon dioxide can be reduced, and liquefied carbon dioxide can be produced efficiently with a low environmental impact. The liquefied carbon dioxide thus produced may be distributed as is or may be used for cooling during the production of carbon monoxide. Carbon monoxide may also be used as a raw material for producing valuable materials such as various organic substances (e.g., hydrocarbon compounds). For example, valuable materials can be produced by promoting a reaction, such as the direct addition of hydrogen to carbon dioxide using a catalyst. Methods for producing hydrocarbon compounds include the Fischer-Tropsch reaction. Examples of hydrocarbon compounds include methane, ethane, propane, and carbonate-based substances. The hydrogen used in the reaction is not particularly limited, and hydrogen produced using a photocatalyst, for example, can be used. In this case, the environmental impact of producing valuable materials from carbon dioxide can be further reduced.

[0045] Conventionally, liquefied carbon dioxide has been produced using carbon dioxide contained in exhaust gases emitted during petroleum refining. However, in recent years, concerns have been raised about the risk of petroleum becoming depleted, making it difficult to continue producing liquefied carbon dioxide using this method. As an alternative to petroleum, it is possible to use carbon dioxide captured and stored from exhaust gases produced in thermal power plants using coal or biomass fuels as a raw material for liquefied carbon dioxide (e.g., Toshiba Energy Systems & Solutions Corporation, Thermal & Hydropower Division, "Environmentally Friendly CCS Demonstration Project CO2 Separation and Capture," [online], March 5, 2019, Ministry of the Environment, CCUS Early Social Implementation Conference - Demonstration Project Achievements and Future Directions, [Retrieved August 25, 2023], Internet,<https: / / www.env.go.jp / earth / ccs / ccus-kaigi / 2-3_CCUS_capture.pdf> (See "Document A" below).

[0046] However, as described in Document A, when carbon dioxide is separated using chemical absorption, a large amount of thermal energy is required to separate the carbon dioxide from the absorption liquid. Furthermore, the carbon dioxide concentration in the exhaust gas in Document A is about 10%, which means that a large amount of energy is consumed in the purification process when producing liquefied carbon dioxide. Therefore, the environmental load when producing liquefied carbon dioxide is large. On the other hand, the separated gas separated by the PSA unit in the pretreatment unit 5 is derived from exhaust gas, and therefore can be said to be a sustainable raw material for liquefied carbon dioxide. Furthermore, by using the PSA unit in the pretreatment unit 5 to separate carbon dioxide from exhaust gas, the carbon dioxide concentration in the separated gas supplied to the liquefaction unit 8 can be increased as described above. As a result, the environmental load generated when refining carbon dioxide in the liquefaction unit 8 can be reduced. Furthermore, the manufacturing apparatus 1 can generate liquefied carbon dioxide using the carbon dioxide in the separated gas in the liquefaction section 8, while generating organic substances from the exhaust gas from which the separated gas has been separated in the generation section 2. In other words, the manufacturing apparatus 1 can provide liquefied carbon dioxide and organic substances with a low environmental impact.

[0047] The liquefied carbon dioxide produced in the liquefaction unit 8 is produced using carbon derived from the exhaust gas, and therefore is different from liquefied carbon dioxide derived from petroleum. 14 C. 13 The abundance ratio of carbon isotopes such as C (e.g., δ 14 C, δ 13 Therefore, even if this liquefied carbon dioxide is processed and used in products such as dry ice, beverages, and fire extinguishing gas, it can be determined (traced) that it is derived from the liquefied carbon dioxide produced by the method of the present invention, which has a low environmental impact.

[0048] The exhaust gas treated in the pretreatment unit 5 is supplied to the generation unit 2. Since the separated gas containing carbon dioxide is separated in the pretreatment unit 5, the volume of the exhaust gas supplied to the generation unit 2 is reduced. This allows the pressure applied to the exhaust gas to be reduced when it is supplied from the pretreatment unit 5 to the generation unit 2, thereby reducing the energy required to pressurize the exhaust gas. Also, the piping diameter of the gas line supplying the exhaust gas can be reduced, thereby reducing the number and size of the gas line piping itself and related parts such as valves and screws. This reduces the construction cost of the gas line, thereby reducing the production costs of organic substances and liquefied carbon dioxide.

[0049] Furthermore, since the reactor that generates organic substances from exhaust gas in the generation unit 2 can be made smaller, the energy consumed and costs in the generation unit 2 can be reduced. For example, if the reactor is a liquid reaction reactor, the required stirring power can be reduced. Also, for example, if the reactor is a gas reaction reactor, the pressure for supplying exhaust gas into the reactor and the pressure for pushing the product out of the reactor can be reduced. In addition, since the amount of catalyst used inside the reactor can be reduced, the energy and costs required for tasks such as procuring and replacing the catalyst can be reduced.

[0050] In this way, by separating the separated gas in the pretreatment unit 5, the cost and energy consumed in the production unit 2 can be reduced, thereby reducing the cost and environmental load not only during the production of organic substances and liquefied carbon dioxide, but also during the operation of the entire production system 100. Furthermore, when electricity is used for pressurization, heating, stirring, etc. in the generation unit 2, it is advisable to use green electricity generated from natural energy such as wind power, water power, solar power, and geothermal energy. This allows for efficient production while further reducing the environmental impact during organic substance production.

[0051] The concentration of carbon monoxide contained in the exhaust gas supplied to the generation section 2 is preferably 10% by volume or more and 70% by volume or less, more preferably 20% by volume or more and 60% by volume or less, and even more preferably 30% by volume or more and 50% by volume or less. Furthermore, the concentration of hydrogen contained in the exhaust gas supplied to the generation section 2 is preferably 30% by volume or more and 90% by volume or less, more preferably 40% by volume or more and 80% by volume or less, and even more preferably 50% by volume or more and 70% by volume or less. According to the above configuration, hydrogen can be suitably added to carbon monoxide, and therefore organic substances can be efficiently produced in the production unit 2.

[0052] In the generation unit 2, an organic substance-containing liquid containing mainly organic substances is generated from the exhaust gas (raw material gas from which the separated gas has been separated) from which carbon dioxide has been removed by the action of a catalyst or the like. If the organic substance generated in the generation unit 2 is gaseous, the generated organic substance can be cooled to generate an organic substance-containing liquid or the like. If the gasification furnace 10 has an oxygen generation device and liquefied nitrogen is obtained, the endothermic heat generated when the liquefied nitrogen is vaporized can be used to cool the gaseous organic substance. The generator 2 is connected to the gas line GL1 upstream of the pre-treatment unit 5 via a gas line GL3. This allows the generator 2 to return waste materials generated in the generator (organic substance generator) 2 to the pre-treatment unit 5. The waste materials include, for example, carbon monoxide that was not converted into organic substances in the generator 2, carbon dioxide that was not separated in the PSA device of the pre-treatment unit 5, etc. This allows the carbon-containing gas that was not converted into the target organic substance to be reused as a raw material for the organic substance or liquefied carbon dioxide, rather than simply being exhausted, thereby improving the yield of the organic substance or liquefied carbon dioxide.Furthermore, compared to the case of exhausting carbon dioxide, the organic substance or liquefied carbon dioxide can be produced with a lower environmental impact.

[0053] Furthermore, a refining device (organic substance refining section) 6 is connected to the generating section 2 via a liquid line LL1. The refining device 6 is a device that purifies organic substances from the organic substance-containing liquid. Examples of such a purification device 6 include a distillation device, a treatment device including a pervaporation membrane, a zeolite dehydration membrane, a treatment device including an organic membrane, a treatment device for removing low-boiling substances having a boiling point lower than that of organic substances, a treatment device for removing high-boiling substances having a boiling point higher than that of organic substances, a treatment device including an ion exchange membrane, etc. These devices may be used alone or in combination of two or more types.

[0054] When using a distillation apparatus, the temperature inside the distillation apparatus during the distillation of an organic substance (e.g., ethanol) is not particularly limited, but is preferably 100°C or less, and more preferably 70°C to 95°C. Setting the temperature at this level ensures separation of the necessary organic substance from other components, i.e., distillation (purification) of the organic substance. Furthermore, if the gasification furnace 10 includes an oxygen generator and liquefied nitrogen is produced, the endothermic heat generated when the liquefied nitrogen evaporates can be utilized to condense the distilled organic substance. This shortens the time required to produce the organic substance without consuming additional energy, such as electricity. Furthermore, when storing the resulting high-concentration organic substance, the nitrogen gas obtained after evaporating the liquefied nitrogen can be filled into a tank or the like for storing the organic substance. This allows for the effective use of the resulting liquefied nitrogen, preventing deterioration of the organic substance due to oxidation, and also prevents fires and other hazards caused by the inflow of oxygen.

[0055] The pressure inside the distillation apparatus during distillation of the organic substance may be normal pressure, but is preferably lower than atmospheric pressure (reduced pressure distillation), more preferably 60 to 95 kPaA. Setting the pressure at this level can improve the separation efficiency of the organic substance, and ultimately improve the yield of the organic substance. The concentration of organic substances contained in the purified product is preferably 90% by weight or more, more preferably 99% by weight or more, and even more preferably 99.5% by weight or more.

[0056] Examples of organic substances obtained in this manner include monools such as methanol and ethanol, diols such as 2,3-butanediol, organic acids such as acetic acid and lactic acid, isoprene, butadiene, ammonia, and SAF (Sustainable Aviation Fuel). Such organic substances can be used, for example, as raw materials for resin materials, rubber materials, etc., and can also be used as various solvents, disinfectants, or fuel. High-concentration ethanol can be used as fuel ethanol to be mixed with gasoline, etc., and can also be used as a raw material for cosmetics, beverages, chemicals, fuel (jet fuel), etc., and as an additive for foods, etc., making it extremely versatile.

[0057] Furthermore, products such as fusel oil that are fractionated in the refining process may also be used in the production system 100 (production apparatus 1). Furthermore, when exhaust heat is generated during distillation or the like in the refining device 6, the exhaust heat may be recovered and utilized in the manufacturing system 100 (manufacturing device 1).

[0058] The refining device 6 is connected to a waste liquid treatment unit 7 via a liquid line LL2, so that waste liquid generated during the refining of the organic substance is sent to the waste liquid treatment unit 7. The waste liquid treatment unit 7 has, for example, a filter, and removes solid matter such as metal particles and soot from the waste liquid. Furthermore, the wastewater treatment unit 7 performs anaerobic wastewater treatment, converting waste materials in the wastewater into gases such as methane through the action of anaerobic bacteria. If the gasifier 10 has an oxygen generator and produces liquefied nitrogen, it is preferable to use the endothermic heat generated when the liquefied nitrogen is vaporized to remove the heat generated during wastewater treatment. This makes it possible to maintain an optimal temperature for the anaerobic bacteria without consuming additional energy such as electricity. It is also preferable to fill the nitrogen gas obtained by vaporizing the liquefied nitrogen into a culture tank for anaerobic bacteria to maintain an anaerobic environment.

[0059] In the wastewater treatment unit 7, it is only necessary to recover the carbon source in the wastewater, and aerobic wastewater treatment may be performed instead of or in addition to anaerobic wastewater treatment. In aerobic wastewater treatment, waste materials in the wastewater are converted into gases such as carbon dioxide by the action of aerobic bacteria. When performing aerobic wastewater treatment, the wastewater treatment unit 7 has a blower fan that supplies air (oxygen) to the aerobic bacteria culture tank. The wastewater treatment unit 7 may also have a cryogenic separation type oxygen generator. Supplying the generated oxygen to the aerobic bacteria culture tank can improve the efficiency of aerobic wastewater treatment. The endothermic heat generated when the liquefied nitrogen obtained together with the liquefied oxygen by the oxygen generator can be used to cool various parts of the production system 100, such as the generation of liquefied carbon dioxide in the liquefaction unit 8. The nitrogen gas obtained by vaporizing the liquefied nitrogen can also be suitably used as a purge gas for various parts of the production system 100.

[0060] The waste liquid treatment unit 7 is connected to the gas line GL1 upstream of the pretreatment unit 5 via a gas line GL4. This allows the gas obtained by wastewater treatment in the wastewater treatment unit 7, i.e., the waste material generated in the purification device (posttreatment unit) 6, to be returned to the pretreatment unit (gas separation unit) 5. The returned gas (waste material) may contain unused carbon monoxide, carbon dioxide generated by aerobic wastewater treatment, etc., and therefore can be reused as a raw material for liquefied carbon dioxide or organic substances.

[0061] Furthermore, the effluent produced in the production unit 2 may be sent to the effluent treatment unit 7 via a liquid line. For example, when a liquid containing an organic substance that is poorly soluble in water and an effluent that is readily soluble in water are produced in the production unit 2, or when a gaseous organic substance and an effluent are produced, the organic substance and the effluent can be easily separated, and therefore the effluent may be sent to the effluent treatment unit 7. This makes it possible to reduce the energy required for the subsequent purification process of the organic substance, thereby enabling the organic substance to be produced with a lower environmental impact. In this embodiment, the post-treatment section is made up of the refining device 6 and the waste liquid treatment section 7. Therefore, the post-treatment section treats not only the organic substances but also the waste liquid generated during the purification of the organic substances, the waste liquid generated in the generation section 2, etc., i.e., at least the organic substances.

[0062] Furthermore, in the production system 100, a heat exchanger suitable for exchanging lower temperature heat, such as a heat pump, may be installed as appropriate to supply heat from a location requiring cooling to a location requiring heating. This not only makes it possible to maintain a constant temperature in the production system 100, but also eliminates the need to consume extra energy for cooling and heating. This further reduces the environmental impact caused by the production of organic substances and liquefied carbon dioxide. Examples of locations that require cooling include the vicinity of the gas outlet of the TSA device during adsorption in the pretreatment unit 5, the vicinity of the gas outlet of the reduction device during carbon dioxide reduction, the liquefaction unit 8, the reactor (or culture tank) in the production unit 2, the vicinity of the gas outlet of the purification unit 6, and the culture tank (microbial tank) in the wastewater treatment unit 7. Examples of locations that require heating include the vicinity of the gas supply port of the TSA device during desorption in the pretreatment unit 5, the vicinity of the gas supply port of the reduction device, the reactor of the reduction device, the reactor in the production unit 2, the distillation unit in the purification unit 6, the treatment unit for removing low-boiling-point substances, and the treatment unit for removing high-boiling-point substances.

[0063] Next, a method for using the production system 100 (a method for producing an organic substance) will be described. [1] First, exhaust gas containing carbon monoxide, carbon dioxide, and hydrogen is supplied from the gasifier 10. If the manufacturing apparatus 1 has a reduction device, the exhaust gas is mixed with hydrogen in the reduction device. As a result, carbon dioxide in the exhaust gas is reduced to produce carbon monoxide. Furthermore, if the manufacturing apparatus 1 has an impurity removal device, the exhaust gas is supplied to the impurity removal device. This removes hydrogen sulfide and other substances from the exhaust gas, preventing performance degradation and deactivation of downstream catalysts, reducing agents (oxygen carriers), fillers, and the like.

[0064] [2] Next, the exhaust gas is supplied to the pre-treatment section 5. In the pre-treatment section 5, a PSA device separates a separated gas containing carbon dioxide from the exhaust gas (a raw material gas containing carbon monoxide and carbon dioxide) (gas separation step). The PSA device may further remove BTEX, nitrogen, oxygen, etc. from the exhaust gas. The removed oxygen may be supplied to the gasifier 10 to increase the temperature of the gasifier 10. This can reduce the effort required to transport oxygen from another location. Furthermore, when the production apparatus 1 has a reduction device and the pretreatment section 5 removes hydrogen, hydrocarbons (e.g., methane, ethane, acetylene, etc.), or ammonia, at least one of these gases may be supplied to the reduction device. This can reduce the effort required to transport gases used in the reverse water-gas shift reaction or the reduction reaction of a reducing agent (oxygen carrier) from another location.

[0065] [3] The separated gas is supplied to the liquefaction unit 8. In the liquefaction unit 8, the carbon dioxide in the separated gas is liquefied to produce liquefied carbon dioxide (gas liquefaction process). The liquefied carbon dioxide produced here can be used as a raw material for manufacturing chemical products such as shielding gas for welding, dry ice for cooling, carbon dioxide for drinking, carbon dioxide for food processing, fire extinguishing gas, and synthetic fuel. It can also be sent to a plant factory to promote plant growth or used to neutralize basic wastewater in wastewater treatment. In the liquefaction section 8, the carbon dioxide in the separated gas may be further purified.

[0066] [4] The exhaust gas (raw material gas from which the separated gas has been separated) that has passed through the pretreatment unit 5 is supplied to the generation unit 2. In the generation unit 2, an organic substance-containing liquid containing mainly organic substances generated from the exhaust gas is obtained. If the organic substance generated in the generation unit 2 is in a gaseous state, the generated organic substance may be cooled to generate the organic substance-containing liquid. The waste material generated in the production unit 2 is returned to the pretreatment unit 5 via the gas line GL3 and reused as a raw material for organic substances or liquefied carbon dioxide. In addition, the liquid waste material generated in the production unit 2 may be sent to the waste liquid treatment unit 7.

[0067] [5] The organic substance-containing liquid produced in the production unit 2 is supplied to the purification device 6 via the liquid line LL1. In the purification device 6, the organic substances contained in the organic substance-containing liquid are purified, and a purified product containing the organic substances at a high concentration is obtained. [6] The wastewater generated during the purification process in the purification device 6 is sent to the wastewater treatment unit 7 via the liquid line LL2. In the wastewater treatment unit, the wastewater is treated by removing solids from the wastewater using a filter and by anaerobic wastewater treatment and / or aerobic wastewater treatment.

[0068] According to the organic substance production system, organic substance production apparatus, and organic substance production method described above, carbon dioxide separated from exhaust gas during the process of producing an organic substance can be effectively utilized as a raw material for liquefied carbon dioxide. This significantly reduces the amount of carbon dioxide released into the atmosphere during the organic substance production process, while ensuring that the separated gas, which has a relatively high carbon dioxide concentration, can be used as a raw material for liquefied carbon dioxide. In other words, it is possible to provide organic substances with a low environmental impact, while efficiently producing liquefied carbon dioxide with a low environmental impact.

[0069] (Variation) Modifications of the above-described embodiment will be described below. Note that the above-described embodiment and the following descriptions can be combined with each other.

[0070] The pretreatment unit 5 may be equipped with all of the above-mentioned devices, or any of them may be omitted. For example, the pretreatment unit 5 may not be equipped with a reduction unit. In this case, the exhaust gas is directly supplied to the PSA unit. Then, some or all of the carbon dioxide in the exhaust gas is separated by the PSA unit to form separated gas, and at least a part of this is supplied to the liquefaction unit 8.

[0071] Furthermore, at least a portion of the separated gas separated by the PSA unit may be supplied to a location other than the liquefaction unit 8. For example, the production apparatus 1 may further include a second production unit, to which at least a portion of the separated gas is supplied. The second production unit can react carbon dioxide in the separated gas with a catalyst or the like to produce valuable materials such as organic substances. For example, the second production unit generates organic substances such as formic acid by adding hydrogen to carbon dioxide in the separated gas using a metal catalyst. Examples of catalysts used here include iridium (Ir), rhodium (Rh), nickel (Ni), and alloys containing these. Furthermore, instead of or in addition to a reaction using a non-biological catalyst, the second production unit may generate organic substances such as polymers and methane from carbon dioxide in the separated gas through the action of a biocatalyst such as hydrogen-oxidizing bacteria. Examples of hydrogen-oxidizing bacteria that generate polymers include bacteria belonging to the genus Cupriavidus or genetically modified bacteria thereof, and cyanobacteria (cyanobacteria) belonging to the genus Synechocystis or genetically modified bacteria thereof. Examples of hydrogen-oxidizing bacteria that generate methane include archaea belonging to the phylum Crenarchaeota or genetically modified archaea thereof. The manufacturing apparatus 1 may have only one second generation unit or may have multiple second generation units. In the latter case, the same reaction may occur between the multiple second generation units by the same mechanism, or different reactions may occur by different mechanisms.

[0072] It may be provided in the following manner.

[0073] (1) A system for producing valuable materials, comprising: a gas generation unit that generates a raw material gas containing carbon monoxide and carbon dioxide; a gas separation unit that separates a separated gas containing the carbon dioxide from the raw material gas; a gas liquefaction unit that liquefies the carbon dioxide in the separated gas; a valuable material generation unit that generates valuable materials from the raw material gas from which the separated gas has been separated; and a post-treatment unit that post-treats at least the valuable materials.

[0074] (2) The valuable resource production system according to (1) above, wherein the post-treatment section has a valuable resource refining section that refines the valuable resource.

[0075] (3) A valuable resource production system according to (1) or (2) above, wherein the gas separation unit has a pressure swing adsorption separator.

[0076] (4) The system for producing valuable resources according to any one of (1) to (3) above, wherein the carbon dioxide content in the separated gas is 20% by volume or more and 80% by volume or less.

[0077] (5) A valuable resource manufacturing apparatus used in connection with a gas generation unit that generates a raw material gas containing carbon monoxide and carbon dioxide, the valuable resource manufacturing apparatus comprising: a gas separation unit that separates a separated gas containing the carbon dioxide from the raw material gas; a gas liquefaction unit that liquefies the carbon dioxide in the separated gas; a valuable resource generation unit that generates valuable resources from the raw material gas from which the separated gas has been separated; and a post-processing unit that post-processes at least the valuable resources.

[0078] (6) A method for producing valuable materials, comprising: a gas separation process for separating a separated gas containing carbon dioxide from a raw material gas containing carbon monoxide and carbon dioxide; a gas liquefaction process for liquefying the carbon dioxide in the separated gas; a valuable material production process for producing valuable materials from the raw material gas from which the separated gas has been separated; and a post-treatment process for post-treating at least the valuable materials. Of course, this is not the case.

[0079] As described above, various embodiments of the present invention have been described, but these are presented as examples and do not limit the scope of the invention in any way. The novel embodiments can be embodied in various other forms, and various omissions, substitutions, and modifications can be made without departing from the spirit of the invention. Such embodiments and their modifications are intended to be included within the scope and spirit of the invention, as well as within the scope of the inventions and their equivalents as set forth in the claims.

[0080] For example, the organic substance manufacturing system and organic substance manufacturing apparatus of the present invention may each have any other additional configuration compared to the above embodiments, may be replaced with any configuration that performs a similar function, or may have some configurations omitted. Furthermore, the method for producing an organic substance of the present invention may have any other additional steps compared to the above-described embodiment, may be replaced with any step that exhibits a similar function, or may omit some steps. [Explanation of symbols]

[0081] 1: Manufacturing equipment 2: Generation part 5: Preprocessing section 51a: reactor 51b: reactor 52: Bulkhead 53: Small space 6: Purification equipment 7: Drainage treatment section 8: Liquefaction section 10: Gasification furnace 100: Manufacturing Systems GL1: Gas line GL2: Gas line GL3: Gas line GL4: Gas line LL1: Liquid line LL2: Liquid line

Claims

1. A valuable material production system, a gas generating unit that generates a raw material gas containing carbon monoxide and carbon dioxide; a gas separation unit that separates a separated gas containing the carbon dioxide from the raw material gas; a gas liquefaction unit that liquefies the carbon dioxide in the separated gas; a valuable resource generating unit that generates valuable resources from the raw material gas from which the separated gas has been separated; A valuable resource manufacturing system comprising: a post-processing section for post-processing at least the valuable resource.

2. 2. The valuable resource production system according to claim 1, The post-treatment unit includes a valuable material refining unit that refines the valuable material.

3. 2. The valuable resource production system according to claim 1, The gas separation unit has a pressure swing adsorption separator.

4. In the valuable resource production system according to any one of claims 1 to 3, A system for producing valuable materials, wherein the carbon dioxide content in the separated gas is 20% by volume or more and 80% by volume or less.

5. A valuable resource manufacturing device used in connection with a gas generating unit that generates a raw material gas containing carbon monoxide and carbon dioxide, a gas separation unit that separates a separated gas containing the carbon dioxide from the raw material gas; a gas liquefaction unit that liquefies the carbon dioxide in the separated gas; a valuable resource generating unit that generates valuable resources from the raw material gas from which the separated gas has been separated; and a post-processing unit that post-processes at least the valuables. Equipment for producing valuable materials.

6. A method for producing valuable materials, a gas separation step of separating a separated gas containing carbon dioxide from a raw material gas containing carbon monoxide and carbon dioxide; a gas liquefaction step of liquefying the carbon dioxide in the separated gas; a valuable material generating step of generating valuable materials from the raw material gas from which the separated gas has been separated; and a post-treatment step of post-treating the valuable material.

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