JP2023141390A - Manufacturing apparatus of carbon valuable, manufacturing method of carbon valuable, manufacturing system of carbon valuable and manufacturing system of polymer - Google Patents

Abstract

To provide a manufacturing apparatus of carbon valuables capable of efficiently manufacturing the carbon valuables from carbon dioxide, a manufacturing method of the carbon valuables and a manufacturing system of the carbon valuables, as well as a manufacturing system of a polymer using the manufacturing apparatus of the carbon valuables.SOLUTION: According to one aspect of the present invention, an apparatus for manufacturing carbon valuables is provided. This apparatus includes a first reaction section that converts COx (1.5≤x≤2) into COx (1≤x<1.5) using a first gas component that can accept oxygen element, a second reaction section that converts COx (1≤x<1.5) into carbon valuables, a gas line that connects the first reaction section and the second reaction section and supplies gas generated in the first reaction section to the second reaction section, and a gas component removal section that is arranged in the middle of the gas line and removes a second gas component having a boiling point higher than the boiling point of CO from an exhaust gas.SELECTED DRAWING: Figure 1

Description

The present invention relates to an apparatus for producing carbon valuables, a method for producing carbon valuables, a system for producing carbon valuables, and a system for producing polymers.

In recent years, the concentration of carbon dioxide (CO ₂ ), a type of greenhouse gas, in the atmosphere has continued to rise. Rising concentrations of carbon dioxide in the atmosphere contribute to global warming. Therefore, it is important to recover carbon dioxide released into the atmosphere, and if the recovered carbon dioxide can be converted into valuable carbon materials and reused, a carbon recycling society can be realized.
In addition, as a global measure, as stated in the Kyoto Protocol of the United Nations Framework Convention on Climate Change, the reduction rate of carbon dioxide, which is the cause of global warming, in developed countries is set for each country based on 1990. It is stipulated that the reduction targets will be jointly achieved within the commitment period.

In order to achieve this reduction target, exhaust gases containing carbon dioxide generated from steel mills, smelters, and thermal power plants are also targeted, and various technological improvements have been made to reduce carbon dioxide emissions in these industries. ing. An example of such technology is CO ₂ capture and storage (CCS). However, this technology has the physical limit of storage and is not a fundamental solution.
For example, Patent Document 1 discloses a production apparatus for producing carbon monoxide from carbon dioxide using cerium oxide containing zirconium.

Patent No. 5858926

Patent Document 1 discloses an invention that specifies a metal oxide that efficiently converts carbon dioxide into carbon monoxide. However, according to the studies of the present inventors, Patent Document 1 discloses conceptual or general information regarding the manufacturing conditions and manufacturing equipment for carbon monoxide, as can be seen by referring to the figures. Only. For this reason, it has been found that further technological improvements are required to industrially produce carbon valuables such as carbon monoxide.
Further, at present, there is no known production device that can efficiently produce carbon valuables from carbon dioxide.

In view of the above circumstances, the present invention uses a carbon valuables manufacturing apparatus, a carbon valuables manufacturing method, a carbon valuables manufacturing system, and a carbon valuables manufacturing apparatus capable of efficiently manufacturing carbon valuables from carbon dioxide. We decided to provide a production system for polymers that

According to one aspect of the present invention, an apparatus for producing carbon valuables is provided. This device performs a first reaction that converts CO _x (1.5≦x≦2) into CO _x (1≦x<1.5) using a first gas component that can accept oxygen element. a second reaction part that converts CO _x (1≦x<1.5) into carbon valuables; the first reaction part and the second reaction part are connected; A gas line that supplies the generated exhaust gas to a second reaction section, and a gas component removal section that is disposed in the middle of the gas line and removes a second gas component having a boiling point higher than the boiling point of CO from the exhaust gas. Be prepared.

According to this embodiment, carbon valuables and even polymers can be efficiently produced from carbon dioxide.

1 is a schematic diagram showing the configuration of a first embodiment of a system for producing carbon valuables according to the present invention. FIG. 2 is a schematic diagram showing the configuration of a first reactor in the first embodiment. It is a schematic diagram showing the composition of a 2nd embodiment of the production system of carbon valuables of the present invention. FIG. 2 is a schematic diagram showing the configuration of a third embodiment of a system for producing carbon valuables according to the present invention. It is a schematic diagram showing the composition of the 1st reaction part in a 4th embodiment. It is a schematic diagram which shows the structure of the 1st reaction part in 5th Embodiment.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, an apparatus for producing carbon valuables, a method for producing carbon valuables, a system for producing carbon valuables, and a system for producing a polymer according to the present invention will be described in detail based on preferred embodiments shown in the accompanying drawings.
<Carbon valuables production system>
<<First embodiment>>
First, a first embodiment of a system for producing carbon valuables according to the present invention will be described.
FIG. 1 is a schematic diagram showing the configuration of a first embodiment of a system for producing carbon valuables according to the present invention. FIG. 2 is a schematic diagram showing the configuration of the first reactor in the first embodiment.
The carbon valuables manufacturing system 10 shown in FIG. It includes an exhaust gas supply section (gas generation section) 1 that supplies exhaust gas and a reducing gas supply section 2 that supplies reducing gas.
Note that, in this specification, the upstream side with respect to the gas flow direction is also simply referred to as "upstream side," and the downstream side is also simply referred to as "downstream side."

The exhaust gas supply section 1 is not particularly limited, but for example, at least one business facility selected from a paper mill, a cement factory, a steel mill, a smelter, a thermal power plant, an oil refinery, an ethylene cracker, an oil refinery, and a chemical factory. Examples include CO _x emission sources. Among these, as the exhaust gas supply section 1, a furnace (for example, a combustion furnace, a blast furnace, a converter) attached to a steel mill, a smelter, or a thermal power plant is preferable. In a furnace, gas containing CO _x (1.5≦x≦2) is generated (emitted) during combustion, melting, refining, etc. of the contents. That is, exhaust gas rich in carbon dioxide is generated.
In the case of a combustion furnace (incinerator) at a garbage incinerator, the contents (waste) include, for example, plastic waste, food garbage, municipal waste (MSW), waste tires, biomass waste, household garbage (bedding), etc. , paper), construction materials, etc. Note that these wastes may contain one type alone or two or more types.

In addition to carbon dioxide, exhaust gas typically contains other gas components such as nitrogen, oxygen, carbon monoxide, water vapor, and methane. The concentration of carbon dioxide contained in the exhaust gas is not particularly limited, but in consideration of the production cost of produced gas (conversion efficiency to carbon monoxide), it is preferably 1% by volume or more, more preferably 5% by volume or more.
In the case of exhaust gas from a combustion furnace at a garbage incinerator, carbon dioxide is 5% to 15% by volume, nitrogen is 60% to 70% by volume, oxygen is 5% to 10% by volume, and water vapor is 15% by volume. It is contained in an amount of not less than 25% by volume.

Exhaust gas from a blast furnace (blast furnace gas) is a gas generated when producing pig iron in a blast furnace, and contains carbon dioxide of 10% to 15% by volume, nitrogen of 55% to 60% by volume, and carbon monoxide. is contained in an amount of 25 vol.% or more and 30 vol.% or less, and hydrogen is contained in an amount of 1 vol.% or more and 5 vol.% or less.
In addition, exhaust gas from a converter (converter gas) is a gas generated when manufacturing steel in a converter, and contains carbon dioxide of 15% to 20% by volume and carbon monoxide of 50% to 60% by volume. Nitrogen is contained in an amount of 15% to 25% by volume, and hydrogen is contained in an amount of 1% to 5% by volume.

When using blast furnace gas and converter gas, carbon monoxide is separated and removed to prepare carbon dioxide-rich exhaust gas (gas containing CO _x (1.5≦x≦2)). Ru.
Methods for separating carbon monoxide from blast furnace gas and converter gas include, for example, low-temperature separation type (deep cooling type) separators, pressure swing adsorption (PSA) type separators, membrane separation type separators, temperature Swing adsorption (TSA) type separators, amine absorption type separators, amine adsorption type separators, etc. can be used, and one type of these can be used alone or two or more types can be used in combination.
Note that a pure gas containing 100% by volume of carbon dioxide may be used as the gas containing CO _x (1.5≦x≦2).

However, if exhaust gas is used, the carbon dioxide that was conventionally emitted into the atmosphere can be effectively used, and the burden on the environment can be reduced. Among these, from the viewpoint of carbon circulation, exhaust gas containing carbon dioxide generated at a steel mill or a refinery is preferable.
Note that untreated blast furnace gas and converter gas have the gas compositions described above, but the treated gas after removing carbon monoxide has a gas composition similar to that shown in the exhaust gas from the combustion furnace. composition. In this specification, all of the above gases (gases before being supplied to the manufacturing apparatus 100) are referred to as exhaust gas.

The reducing gas supply unit 2 is configured with, for example, a hydrogen generator that generates hydrogen by electrolyzing water. A tank storing water is connected to this hydrogen generator.
According to the hydrogen generator, a large amount of hydrogen can be generated relatively inexpensively and easily. Another advantage is that condensed water generated within the manufacturing apparatus 100 can be reused. Note that since the hydrogen generator consumes a large amount of electrical energy, it is effective to use electricity as renewable energy.
As renewable energy, electrical energy using at least one selected from solar power generation, wind power generation, hydropower generation, wave power generation, tidal power generation, biomass power generation, geothermal power generation, solar heat, and geothermal heat is used. It is possible.

Note that a device that generates by-product hydrogen can also be used as the hydrogen generator. Examples of devices that generate by-product hydrogen include devices that electrolyze an aqueous sodium chloride solution, devices that steam-reform petroleum, and devices that produce ammonia.
Further, the reducing gas supply section 2 can also be a coke oven. In this case, exhaust gas from the coke oven may be used as the reducing gas. This is because the exhaust gas from the coke oven has hydrogen and methane as its main components, and contains hydrogen in an amount of 50% by volume or more and 60% by volume or less.

The production apparatus 100 of this embodiment is an apparatus for producing carbon valuables, and mainly includes a gas switching section 3, two first reactors 4a and 4b (first reaction section 4), and one reactor. A second reactor (second reaction section) 5 is provided.
The exhaust gas supply section 1 is connected to the gas switching section 3 via a gas line GL1, and the reducing gas supply section 2 is connected to the gas switching section 3 via a gas line GL2.
In the middle of each gas line GL1, GL2, at least one of a temperature control section that adjusts the temperature of the gas passing through it, a pressurization section that pressurizes the gas, an impurity removal section that removes impurities from the gas, etc. is arranged. You may also do so.
The gas switching unit 3 can be configured to include, for example, a branch gas line and a passage opening/closing mechanism such as a valve provided in the middle of the branch gas line.

The gas switching unit 3 is connected to the inlet ports of the first reactors 4a, 4b via two gas lines GL3a, GL3b, respectively.
With this configuration, the exhaust gas (oxidizing gas containing CO _x (1.5≦x≦2)) supplied from the exhaust gas supply section 1 passes through the gas line GL1, the gas switching section 3, and the gas lines GL3a and GL3b. , are supplied to each first reactor 4a, 4b.
On the other hand, the reducing gas containing hydrogen (the first gas component capable of accepting oxygen element) supplied from the reducing gas supply section 2 passes through the gas line GL2, the gas switching section 3, and the gas lines GL3a and GL3b, It is supplied to each first reactor 4a, 4b.

The first reactors 4a and 4b convert CO _x (1.5≦x≦2) into CO _x (1≦x<1.5) using a first gas component that can accept oxygen element. It is convertible. COx (1.5≦x≦2) is a gas rich in carbon dioxide, and _COx (1≦x<1.5) is a gas rich in carbon monoxide. As shown in FIG. 2, each of the first reactors 4a and 4b includes a plurality of tube bodies 41 each filled with (housed in) a reducing agent 4R, and a housing 42 in which the plurality of tube bodies 41 are housed in an internal space 43. It consists of a multitubular reactor (fixed bed reactor) equipped with According to such a multi-tubular reactor, a sufficient opportunity for contact between the reducing agent 4R and the exhaust gas and the reducing gas can be ensured. As a result, the production efficiency of generated gas containing carbon valuables can be improved.
The reducing agent 4R of this embodiment is preferably in the form of particles, scales, pellets, etc., for example. If the reducing agent 4R has such a shape, it is possible to increase the filling efficiency into the pipe body 41 and further increase the contact area with the gas supplied into the pipe body 41.

When the reducing agent 4R is in the form of particles, its volume average particle diameter is not particularly limited, but is preferably 1 to 50 mm, more preferably 1 to 30 mm. In this case, the contact area between the reducing agent 4R and the exhaust gas (carbon dioxide) can be further increased, and the conversion efficiency of carbon dioxide into carbon monoxide can be further improved. Similarly, regeneration (reduction) of the reducing agent 4R using a reducing gas containing a reducing substance can be performed more efficiently.
The particulate reducing agent 4R is preferably a molded body manufactured by rolling granulation because the sphericity is further increased.

Further, the reducing agent 4R may be supported on a carrier.
The constituent material of the carrier may be any material that is difficult to modify due to contact with exhaust gas (oxidizing gas) or reaction conditions, such as carbon materials (graphite, graphene, etc.), carbides such as Mo ₂ C, zeolite, montmorillonite, Examples include oxides such as ZrO ₂ , TiO ₂ , V ₂ O ₅ , MgO, CeO ₂ , Al ₂ O ₃ , and SiO ₂ and composite oxides containing these.

Among these, zeolite, montmorillonite, ZrO ₂ , TiO ₂ , V ₂ O ₅ , MgO, Al ₂ O ₃ , SiO ₂ and composite oxides containing these are preferable as constituent materials of the carrier. A carrier made of such a material is preferable because it does not adversely affect the reaction of the reducing agent 4R and has an excellent ability to support the reducing agent 4R. Here, the carrier does not participate in the reaction of the reducing agent 4R and simply supports (holds) the reducing agent 4R.
An example of such a configuration is a configuration in which at least a portion of the surface of the carrier is coated with the reducing agent 4R.

The reducing agent 4R contains at least one of an elemental metal and a metal oxide (oxygen carrier with oxygen ion conductivity). At least one of the simple metal and the metal oxide is not particularly limited as long as it can reduce carbon dioxide, but it is preferable that it contains at least one metal element selected from metal elements belonging to Groups 3 to 13. It is more preferable to contain at least one metal element selected from metal elements belonging to Groups 3 to 12, including lanthanum, titanium, vanadium, iron, indium, cobalt, zirconium, copper, zinc, nickel, manganese, chromium and It is more preferable to contain at least one of cerium and the like, and particularly preferable is a metal oxide or composite metal oxide containing at least one of lanthanum, zirconium, iron, nickel, copper, chromium, and manganese. These metal oxides are useful because they have particularly good efficiency in converting carbon dioxide to carbon monoxide.

Further, in each of the first reactors 4a, 4b, the tube (cylindrical molded body) 41 may be made of the reducing agent 4R (at least one of a simple metal and a metal oxide) itself. Furthermore, a block-shaped, lattice-shaped (for example, net-shaped, honeycomb-shaped) molded body may be produced using the reducing agent 4R, and the molded body may be placed in the housing 42. In these cases, the reducing agent 4R as a filler may be omitted or may be used in combination.

Among these, a configuration in which a net-like body is produced using the reducing agent 4R and placed inside the housing 42 is preferable. In the case of such a configuration, sufficient opportunity for contact between the reducing agent 4R and the exhaust gas and reducing gas is ensured while preventing the passage resistance of the exhaust gas and reducing gas from increasing in each of the first reactors 4a and 4b. You can also do it.
The volumes of the two first reactors 4a and 4b are set approximately equal to each other, and are appropriately set depending on the amount of exhaust gas to be treated (the size of the exhaust gas supply section 1 and the size of the manufacturing apparatus 100). Further, the volumes of the two first reactors 4a and 4b may be varied depending on the types of exhaust gas and reducing gas, the performance of the reducing agent 4R, and the like.

According to the above configuration, by switching the gas line (flow path) in the gas switching unit 3, for example, the reducing agent 4R before oxidation is connected to the first reactor 4a containing the reducing agent 4R via the gas line GL3a. is supplied with exhaust gas (CO _x (1.5≦x≦2)), and the reducing gas (first gas components). At this time, a reaction expressed by the following formula 1 proceeds in the first reactor 4a, and a reaction expressed by the following formula 2 proceeds in the first reactor 4b.

Note that in the following formulas 1 and 2, the case where the reducing agent 4R contains iron oxide (FeO _x-1 ) is shown as an example.
Formula 1: CO ₂ + FeO _x−1 → CO + FeO _x
Formula 2: H ₂ + FeO _x → H ₂ O + FeO _x-1
Thereafter, by switching the gas line in the opposite direction to the above in the gas switching unit 3, the reaction of the above formula 2 is allowed to proceed in the first reactor 4a, and the reaction of the above formula 1 is allowed to proceed in the first reactor 4b. I can do it.
That is, exhaust gas and reducing gas can be supplied alternately.

Note that the reactions shown in Formulas 1 and 2 above are both endothermic reactions. For this reason, the manufacturing apparatus 100 includes a reducing agent heating unit ( (not shown in FIG. 1).
By providing such a reducing agent heating section, the temperature during the reaction between the exhaust gas or reducing gas and the reducing agent 4R is maintained at a high temperature, and a decrease in the conversion efficiency of carbon dioxide to carbon monoxide is suitably prevented or suppressed. , the regeneration of the reducing agent 4R by the reducing gas can be further promoted.

However, depending on the type of reducing agent 4R, the reactions shown in Formulas 1 and 2 above may become exothermic reactions. In this case, it is preferable that the manufacturing apparatus 100 has a reducing agent cooling section that cools the reducing agent 4R instead of the reducing agent heating section. By providing such a reducing agent cooling section, deterioration of the reducing agent 4R is suitably prevented during the reaction between the exhaust gas or reducing gas and the reducing agent 4R, and the conversion efficiency of carbon dioxide into carbon monoxide is improved. It is possible to suitably prevent or suppress the decrease, and further promote the regeneration of the reducing agent 4R by the reducing gas.
That is, the manufacturing apparatus 100 is preferably provided with a reducing agent temperature control section that adjusts the temperature of the reducing agent 4R depending on the type of reducing agent 4R (exothermic reaction or endothermic reaction).

Here, the conversion rate of carbon dioxide to carbon monoxide in the first reactors 4a, 4b is preferably 90% or more, more preferably 92.5% or more, and 95% or more. It is even more preferable. The upper limit of the conversion rate of carbon dioxide to carbon monoxide is usually about 98%.
Such a conversion rate depends on the type of reducing agent 4R used, the concentration of carbon dioxide contained in the exhaust gas, the type of reducing substance, the concentration of reducing substance contained in the reducing gas, the temperature of the first reactors 4a and 4b, It can be set by adjusting the flow rate (flow rate) of exhaust gas and reducing gas to the first reactors 4a, 4b, the timing of switching between exhaust gas and reducing gas, etc.

Gas lines GL4a and GL4b are connected to the outlet ports of the first reactors 4a and 4b, respectively, and these meet at a gas merging section J to form a gas line GL4. Additionally, valves (not shown) are provided in the middle of the gas lines GL4a and GL4b, as necessary.
For example, by adjusting the opening degree of the valve, the passing rate of the exhaust gas and reducing gas passing through the first reactors 4a and 4b (i.e., the processing rate of the exhaust gas by the reducing agent 4R and the processing rate of the reducing agent 4R by the reducing gas) can be adjusted. speed) can be set.

Gas line GL4 is connected to the inlet port of second reactor 5. That is, the second reactor (second reaction section) 5 is connected to the first reactors 4a, 4b (first reaction section) via gas lines GL4a, GL4b and gas line GL4. . Thereby, the exhaust gas generated in the first reactors 4a, 4b can be supplied to the second reactor 5 as a mixed gas.
The second reactor 5 is capable of converting CO _x (1≦x<1.5) into carbon values. Specifically, in the second reactor 5, an olefin compound, which is a type of carbon valuable substance, is produced from carbon monoxide and hydrogen contained in the mixed gas. That is, in the second reactor 5, a so-called Fischer-Tropsch reaction is performed.
As the second reactor 5, a reactor similar to that described for the first reactors 4a, 4b can be used. In this case, the tube body 41 is filled with a catalyst containing at least one of iron, cobalt, ruthenium, nickel, molybdenum, aluminum, and silicon, for example.

Here, examples of the olefin compound include ethylene, propylene, butene, butadiene, etc., and one or more of these may be used. Among these, it is preferable that the olefin compound contains ethylene. This is because olefin compounds containing ethylene are useful as raw materials for various industrial products.
Note that by changing the type of catalyst, the second reactor 5 can generate other carbon valuables other than olefin compounds from the carbon monoxide and hydrogen contained in the mixed gas. Examples of other carbon valuables include oxygen-containing compounds, aromatic compounds, and the like.

Examples of the oxygen-containing compound include methanol, ethanol, acetaldehyde, acetone, and butanol, and one or more of these may be used. Among these, the oxygen-containing compound preferably contains methanol. This is because oxygen-containing compounds containing methanol are useful as raw materials for various industrial products.
In this case, usable catalysts include, for example, catalysts containing at least one of titanium, copper, silver, zinc, rhodium, manganese, nickel, aluminum, and silicon.

On the other hand, examples of the aromatic compound include benzene, toluene, xylene, etc., and one or more of these may be used. Among them, it is preferable that the aromatic compound contains toluene. This is because aromatic compounds containing toluene are useful as raw materials for various industrial products.
In this case, examples of catalysts that can be used include catalysts containing at least one of molybdenum, tungsten, rhenium, nickel, aluminum, and silicon.
Note that the catalyst may be a supported catalyst, a composite oxide such as zeolite, or a composite oxide supporting a metal.

Alternatively, a continuous method may be adopted in which the exhaust gas and reducing gas discharged from the first reactors 4a and 4b are continuously supplied to the second reactor 5 at the same timing without being combined. It is also possible to adopt a batch method in which only the exhaust gas is supplied (sealed) with the outlet port of the second reactor 5 closed, then the reducing gas is supplied, and then the outlet port of the second reactor 5 is opened. . It is also possible to adopt a method in which two second reactors 5 are provided and exhaust gas and reducing gas are alternately supplied to each of them.

The first reaction temperature in the first reactors 4a, 4b (first reaction section 4) is preferably higher than the second reaction temperature in the second reactor (second reaction section) 5. In this case, the reaction heat in the first reactors 4a, 4b can be effectively used in the second reactor 5.
Specifically, the difference between the first reaction temperature and the second reaction temperature is preferably 100°C or more, more preferably 150°C or more and 500°C or less, and 200°C or more and 400°C or less. It is even more preferable that there be. Thereby, while improving the reaction efficiency in the first reactors 4a, 4b and the second reactor 5, it is also possible to improve the heat utilization efficiency.
The reaction temperature of the second reactor 5 is preferably 100°C or more and 400°C or less, more preferably 150°C or more and 350°C or less, and even more preferably 200°C or more and 300°C or less. .

The first reaction pressure in the first reactors 4a, 4b (first reaction section 4) is preferably lower than the second reaction pressure in the second reactor (second reaction section) 5. In this case, gas (exhaust gas, reducing gas, and mixed gas) can be supplied to the second reactor 5 from the front stage of the first reactors 4a and 4b without repeating pressure increase and decrease. That is, since the pressure of the gas can be increased stepwise (efficiently), energy utilization efficiency can be increased.
The second reaction pressure is preferably more than 1 MPa, more preferably 1.5 MPa or more and 5 MPa or less, and even more preferably 2 MPa or more and 4 MPa or less. Thereby, the reaction efficiency in the second reactor 5 can be further improved.

A gas component removing section 8 is arranged in the middle of the gas line GL4. This gas component removing section 8 removes a second gas component having a boiling point higher than the boiling point of CO from the exhaust gas from the first reactors 4a, 4b. By removing this second gas component (impurity gas component), the amount of components that inhibit the reaction in the second reactor 5 is reduced, and the efficiency can be further improved.
In this embodiment, examples of the second gas component include H ₂ O, CO ₂ , methane, ethane, methanol, ethanol, ethylene oxide, propylene oxide, and the like.

The gas component removal unit 8 may be configured with a cooler that cools the exhaust gas (mixed gas) from the first reactors 4a and 4b, and a second cooler that boosts the pressure of the exhaust gas and has a boiling point higher than the boiling point of CO. It may be composed of a condenser that liquefies the gas components of the second reactor 5, a separation membrane that allows the passage of molecules to be reacted in the second reactor 5, and blocks the passage of other molecules, or a second reactor. It may be composed of a separation membrane that blocks the passage of the molecules to be reacted in step 5 and allows the passage of other molecules, or it may be composed of any or all combinations of a cooler, a condenser, and a separation membrane. Good too.
As the cooler, a cooler having the same configuration as that described in the gas purification section described later can be used.
On the other hand, the condenser may include a compressor for increasing the pressure and a gas-liquid separator.
On the other hand, the separation membrane can be made of a metal, an inorganic oxide, or a metal organic framework (Metal Organic FRAM (registered trademark) eworks: MOF).

Here, examples of the metal include titanium, aluminum, copper, nickel, chromium, cobalt, and alloys containing these. When using metal, the separation membrane is preferably a porous body with a porosity of 80% or more.
Examples of the inorganic oxide include silica and zeolite.
Further, examples of the metal-organic structure include a structure of zinc nitrate hydrate and terephthalate dianion, a structure of copper nitrate hydrate and trimesate trianion, and the like.

It is preferable that the separation membrane is composed of a porous body having continuous pores (pores penetrating the cylindrical wall) in which adjacent pores communicate with each other. With a separation membrane having such a configuration, the permeability of H ₂ O or CO can be increased, and the separation between H ₂ O and H ₂ and/or the separation between CO and CO ₂ can be performed more smoothly and reliably. .
The porosity of the separation membrane is not particularly limited, but is preferably 10% or more and 90% or less, more preferably 20% or more and 60% or less. This makes it possible to maintain a sufficiently high permeability of H ₂ O or CO while preventing the mechanical strength of the separation membrane from decreasing excessively.
Note that the shape of the separation membrane is not particularly limited, and examples thereof include a cylindrical shape, a quadrangular shape, a rectangular tube shape such as a hexagonal shape, and the like.

From the viewpoint of further increasing the conversion efficiency of carbon dioxide into carbon monoxide, it is effective to increase the reduction (regeneration) efficiency of the reducing agent 4R in an oxidized state.
In this case, the average pore diameter of the separation membrane is preferably 600 pm or less, more preferably 400 to 500 pm. Thereby, the separation efficiency between H ₂ O and H ₂ can be further improved.
Note that the separation membrane is normally used while being housed in a housing. In this case, the pressure in the space outside the separation membrane within the housing may be reduced or a carrier gas (sweep gas) may be allowed to pass therethrough. Examples of the carrier gas include helium, inert gas such as argon, and the like.

Further, the separation membrane is preferably hydrophilic. If the separation membrane has hydrophilicity, the affinity of water for the separation membrane will increase, and H ₂ O will more easily permeate through the separation membrane.
Methods of imparting hydrophilicity to a separation membrane include methods of improving the polarity of the separation membrane by changing the ratio of metal elements in the inorganic oxide (for example, increasing the Al/Si ratio); Examples include a method of coating the separation membrane with a polymer, a method of treating the separation membrane with a coupling agent having a hydrophilic group (polar group), and a method of subjecting the separation membrane to plasma treatment, corona discharge treatment, etc.
Furthermore, the affinity for water may be controlled by adjusting the surface potential of the separation membrane.

On the other hand, when separating CO and CO ₂ with priority in a separation membrane, or when separating both H ₂ O and H ₂ and separating CO and CO ₂ at the same time, the configuration of the separation membrane is The material, porosity, average pore diameter, degree of hydrophilicity or hydrophobicity, surface potential, etc. may be appropriately combined and set.
It is also possible to configure the tube bodies 41 of the first reactors 4a, 4b with such separation membranes, but in this case, the separation membranes deteriorate due to heat, so the temperature of the first reactors 4a, 4b (reaction temperature ) cannot be set to a high temperature.
On the other hand, by arranging the separation membrane outside the first reactors 4a, 4b, the temperature of the first reactors 4a, 4b can be set to a relatively high temperature, and therefore, the temperature of the first reactors 4a, 4b can be set to a relatively high temperature. The conversion efficiency to carbon oxide and the regeneration (reduction) efficiency of the reducing agent 4R by the reducing gas can be further improved.

The mixed gas (exhaust gas) of exhaust gas and reducing gas that has passed through the gas component removal section 8 is supplied to the second reactor 5 . That is, unreacted hydrogen (reducing substance) with the reducing agent 4R (at least one of an elemental metal and a metal oxide) in the first reactors 4a and 4b is converted into an olefin-based carbon monoxide in the second reactor 5. Configured for use in conversion to chemical compounds.
In this way, by reusing unreacted hydrogen (reducing substance), waste of raw materials can be reduced.

A gas line GL5 is connected to the outlet port of the second reactor 5.
A produced gas discharge section 6 that discharges produced gas to the outside of the manufacturing apparatus 100 is connected to the end of the gas line GL5 on the opposite side of the second reactor 5.
Note that a gas purification section may be provided in the middle of the gas line GL5.
In the gas purification section, olefin compounds are purified from the mixed gas and a generated gas containing a high concentration of olefin compounds is recovered. Note that if the content of olefin compounds in the mixed gas is sufficiently high, the gas purification section is omitted.

Such a gas purification section can be configured with at least one type of processor selected from a cooler, a gas-liquid separator, a gas separator, a separation membrane, and a scrubber (absorption tower), for example.
Examples of gas separators include low-temperature separation type (deep cooling type) separators, pressure swing adsorption (PSA) type separators, membrane separation type separators, temperature swing adsorption (TSA) type separators, and metal ion separators. A separator using a porous coordination polymer (PCP) that is a composite of (e.g., copper ions) and an organic ligand (e.g., 5-azidoisophthalic acid), separation using amine absorption It can be configured using one or more types of vessels.

Next, a method of using the system 10 for producing carbon valuables (method for producing carbon valuables) will be described.
[1] First, by switching the gas line (flow path) in the gas switching unit 3, the exhaust gas supply unit 1 and the first reactor 4a are connected, and the reducing gas supply unit 2 and the first reactor 4b are connected. communicate.
[2] Next, in this state, exhaust gas is supplied from the exhaust gas supply section 1 to the first reactor 4a via the gas line GL1. In the first reactor 4a, carbon dioxide in the exhaust gas is reduced to carbon monoxide by the reducing agent 4R, thereby converting CO _x (1.5≦x≦2) into CO _x (1≦x<1.5 ) is converted to At this time, the reducing agent 4R is brought into an oxidized state by contact with carbon dioxide.

The temperature (first reaction temperature) of the first reactor 4a (exhaust gas, reducing agent 4R) in the above step [2] is preferably 600°C or higher, more preferably 650°C or higher and 1100°C or lower. The temperature is preferably 700°C or more and 1000°C or less.
Further, the pressure (first reaction pressure) of the first reactor 4a (exhaust gas, reducing agent 4R) is preferably 1 MPaG or less, more preferably 0 MPaG or more and 0.5 MPaG or less, and 0.01 MPaG More preferably, it is 0.5 MPaG or less.
If the reaction conditions are set within the above range, for example, it is possible to prevent or suppress a rapid temperature drop in the reducing agent 4R due to an endothermic reaction when converting carbon dioxide to carbon monoxide. The reduction reaction of carbon dioxide can proceed more smoothly.

[3] In parallel with the above steps [1] and [2], water (reducing gas raw material) is supplied from the tank to the hydrogen generator (reducing gas supply unit 2) to generate hydrogen from water.
[4] Next, a reducing gas containing hydrogen is supplied from the hydrogen generator to the first reactor 4b via the gas line GL2. In the first reactor 4b, the reducing agent 4R in an oxidized state is reduced (regenerated) by contact with reducing gas (hydrogen). At this time, water is produced.

The temperature (reaction temperature) of the first reactor 4b (reducing gas, reducing agent 4R) in the above step [4] is preferably 600°C or higher, more preferably 650-1100°C, and 700-1100°C. More preferably, the temperature is 1000°C.
Further, the pressure (first reaction pressure) of the first reactor 4b (reducing gas, reducing agent 4R) is preferably 1 MPaG or less, more preferably 0 MPaG or more and 0.5 MPaG or less, and 0. More preferably, it is 01 MPaG or more and 0.5 MPaG or less.
If the reaction conditions are set within the above range, for example, it is possible to prevent or suppress a rapid temperature drop of the reducing agent 4R due to an endothermic reaction when reducing (regenerating) the reducing agent 4R in an oxidized state. The reduction reaction of the reducing agent 4R in the reactor 4b can proceed more smoothly.
In the embodiment, the above steps [2] to [4] utilize hydrogen (the first gas component capable of accepting oxygen element) to convert CO _x (1.5≦x≦2) into CO _x (1≦ x<1.5).

[5] Next, the gases that have passed through the first reactors 4a and 4b are combined to generate a mixed gas. At this point, the temperature of the gas mixture is typically 600-650°C. If the temperature of the mixed gas at this point is within the above range, it means that the temperature in the first reactors 4a, 4b is maintained at a sufficiently high temperature, and carbon monoxide due to the reducing agent 4R It can be determined that the conversion to 4R and the reduction of the reducing agent 4R by the reducing gas are progressing efficiently.

[6] Next, the mixed gas is passed through the gas component removing section 8 via the gas line GL4. At this time, a second gas component having a boiling point higher than the boiling point of CO is removed from the exhaust gas from the first reactors 4a, 4b.
In this embodiment, this step [6] constitutes a removal step of removing a second gas component having a boiling point higher than the boiling point of CO from the exhaust gas generated in the conversion step.
[7] Next, the mixed gas that has passed through the gas component removal section 8 is supplied to the second reactor 5. In the second reactor 5, carbon monoxide is converted into olefinic compounds.
In this embodiment, this step [7] constitutes the second conversion step of converting CO _x (1≦x<1.5) in the exhaust gas into carbon valuables.

The produced gas (mixed gas) containing the olefin compound is then discharged from the produced gas discharge section 6 to the outside of the manufacturing apparatus 100 via the gas line GL5, and is subjected to the next process.
In this embodiment, the number of installed second reactors 5 is one, and the number of installed first reactors 4a, 4b is two. That is, the number of installed second reactors 5 is less than the number of installed first reactors 4a, 4b. By installing such a number, the absolute amount of carbon monoxide that can be supplied to the second reactor 5 can be increased, and the amount of olefin compounds produced can be increased.

<<Second embodiment>>
Next, a second embodiment of the carbon valuables production system of the present invention will be described.
FIG. 3 is a schematic diagram showing the configuration of a second embodiment of the carbon valuables production system of the present invention.
The carbon valuables manufacturing system 10 of the second embodiment will be described below, focusing on the differences from the carbon valuables manufacturing system 10 of the first embodiment, and the explanation will be omitted for similar matters. Omitted.
The carbon valuables production system 10 of the second embodiment is provided with two second reactors 5a and 5b.

The gas line GL4a connected to the outlet port of the first reactor 4a is connected to the inlet port of the second reactor 5a, and the gas line GL4b connected to the outlet port of the first reactor 4b is connected to the inlet port of the second reactor 5a. It is connected to the inlet port of No. 2 reactor 5b.
Gas lines GL6a and GL6b branch from the middle of gas lines GL4a and GL4b, and merge at a gas merging portion J1 to form gas line GL6.
Further, gas lines GL5a and GL5b are connected to the outlet ports of the second reactors 5a and 5b, and are merged at a gas junction J2 to form a gas line GL5.

A switching valve is provided at the branch portion between the gas lines GL4a, GL4b and the gas lines GL6a, GL6b.
The exhaust gas discharged from the first reactors 4a, 4b passes through gas lines GL4a, GL4b and is supplied to the second reactors 5a, 5b. Further, gas component removal units 8a and 8b are arranged in the middle of the gas lines GL4a and GL4b, respectively.
The reducing gas discharged from the first reactors 4a, 4b passes through the gas lines GL6a, GL6b, GL6, and is returned to the reducing gas supply unit 2 after, for example, water is removed.

In this embodiment, the number of installed second reactors 5a, 5b is two, and the number of installed first reactors 4a, 4b is also two. That is, the number of installed second reactors 5a, 5b is the same as the number of installed first reactors 4a, 4b. With this configuration, when hydrogen or water is not required for converting carbon monoxide into an olefin compound in the second reactors 5a and 5b, the conversion reaction is prevented from being inhibited. I can do it.
Note that the number of second reactors installed may be greater than the number of first reactors installed. In this case, a second reactor can be provided that does not allow exhaust gas to pass through. Therefore, other operations such as maintenance can be performed on the second reactor that is not used for normal operation while continuing normal operation for producing product gas (olefin compound).

<<Third embodiment>>
Next, a third embodiment of the carbon valuables production system of the present invention will be described.
FIG. 4 is a schematic diagram showing the configuration of a third embodiment of the system for producing carbon valuables of the present invention.
The carbon valuables manufacturing system 10 of the third embodiment will be described below, focusing on the differences from the carbon valuables manufacturing system 10 of the first or second embodiment, and regarding similar matters, The explanation will be omitted.
The carbon valuables production system 10 of the second embodiment is provided with three second reactors 5a to 5c.

The gas line GL4 branches at the gas switching section 7 and is connected to the inlet port of each of the second reactors 5a to 5c. Further, a gas component removing section 8 is arranged in the middle of the gas line GL4.
Further, gas lines GL5a to GL5c are connected to the outlet ports of the second reactors 5a to 5c, and the ends of the gas lines GL5a to GL5c opposite to the second reactors 5a to 5c are connected to the generated gas The discharge parts 6a to 6c are connected.
In this embodiment, the second reactors 5a to 5c are configured to be able to convert carbon monoxide into different olefin compounds A to C.

According to this configuration, a plurality of types (in this embodiment, three types) of olefin compounds A to C can be produced by one carbon valuables production system 10, and the system is highly versatile.
Further, in this embodiment, the number of second reactors 5a to 5c installed is three, and the number of first reactors 4a and 4b installed is two. That is, the number of installed second reactors 5a to 5c exceeds the number of installed first reactors 4a and 4b.
In the first to third embodiments described above, an example has been described in which at least one of the simple metal and the metal oxide functions as a reducing agent for reducing carbon dioxide. It can also function as a catalyst that promotes the reaction between carbon dioxide and reducing substances. In this case, a reverse water gas shift reaction is performed by accommodating a catalyst in a first reactor and simultaneously supplying exhaust gas and reducing gas to this first reactor.

<<Fourth embodiment>>
The first reaction section 4 can also have the following configuration.
FIG. 5 is a schematic diagram showing the configuration of the first reaction section of the fourth embodiment.
The first reaction section 4 of the fourth embodiment will be described below, focusing on the differences from the first reaction section 4 of the first embodiment, and omitting the explanation of similar matters. .

The first reaction section 4 of the fourth embodiment has four (plural) first reactors 4a1, 4a2, 4b1, and 4b2.
The gas switching unit 3 is connected to the inlet ports of the first reactors 4a1 and 4b1 via gas lines GL3a and GL3b, respectively.
Gas lines GL4a and GL4b are connected to the outlet ports of the first reactors 4a2 and 4b2, respectively, and join together at a gas junction J4 to form a gas line GL4.
In this embodiment, the first reactor 4a1 and the first reactor 4a2 are connected in series by the gas line GL5a, and the first reactor 4b1 and the first reactor 4b2 are connected by the gas line GL5b. connected in series.

According to this configuration, the conversion efficiency (conversion rate) from CO _x (1.5≦x≦2) to an olefin compound (carbon valuables) can be further improved.
The volumes of the four first reactors 4a1, 4a2, 4b1, and 4b2 are set approximately equal to each other, and can be adjusted as appropriate depending on the amount of exhaust gas to be treated (the size of the exhaust gas supply unit 1 and the size of the manufacturing apparatus 100). Set. Further, the volume of at least one of the four first reactors 4a1, 4a2, 4b1, and 4b2 may be varied depending on the types of exhaust gas and reducing gas, the performance of the reducing agent 4R, and the like.
Further, the reducing agent 4R used in the first reactors 4a1 and 4b1 and the reducing agent 4R used in the first reactors 4a2 and 4b2 may have the same composition and structure (shape), or may have different It may be composition or structure (shape).

<<Fifth embodiment>>
Next, a fifth embodiment of the carbon valuables production system of the present invention will be described.
FIG. 6 is a schematic diagram showing the configuration of the first reactor in the fifth embodiment.
The carbon valuables manufacturing system 10 of the fifth embodiment will be described below, focusing on the differences from the carbon valuables manufacturing system 10 of the first to fourth embodiments, and regarding similar matters, The explanation will be omitted.

The first reaction section 4 shown in FIG. 6 is composed of a reactor (also called a reaction cell, an electrolytic cell, or an electrochemical cell) that electrochemically performs a reduction reaction of carbon dioxide.
The first reaction section 4 includes a housing 42, a cathode 45, an anode 46, and a solid electrolyte layer 47 provided within the housing 42, and a power source 48 electrically connected to the cathode 45 and anode 46. There is.
In this configuration, the space within the housing 42 is divided into left and right sections by a laminate of a cathode (reductant) 45, an anode 46, and a solid electrolyte layer 47.

The housing 42 includes a cathode inlet port 421a, a cathode outlet port 421b, an anode inlet port 422a, and an anode outlet port 422b. The cathode side inlet port 421a and the cathode side outlet port 421b communicate with the cathode chamber in the left side space in the housing 42, and the anode side inlet port 422a and the anode side outlet port 422b communicate with the anode chamber in the right side space in the housing 42. are doing.

The cathode 45 and the anode 46 each include a conductive carrier and a catalyst supported on the carrier.
The carrier can be made of a carbon material such as carbon fiber fabric (carbon cloth, carbon felt, etc.) or carbon paper.
Examples of catalysts include platinum group metals such as platinum, ruthenium, rhodium, palladium, osmium, and iridium, transition metals such as gold, alloys of these metals, and alloys of these metals with other metals. can be mentioned.

The solid electrolyte layer 47 can be composed of, for example, a fluorine-based polymer membrane having sulfonic acid groups (Nafion (registered trademark), etc.), a sulfo-based ion exchange resin membrane, or the like.
As the power source 48, it is preferable to use a power source that generates electricity as renewable energy. Thereby, the energy efficiency in producing generated gas containing carbon valuables can be further improved.

In the first reactor 4, when exhaust gas (carbon dioxide and water) is supplied from the cathode side inlet port 421a, a reduction reaction of carbon dioxide and water occurs due to the action of the electrons supplied from the power supply 48 and the catalyst. Carbon monoxide and hydrogen are produced, as well as oxygen ions.
Carbon monoxide and hydrogen are discharged from the cathode side exit port 421b to the gas line (gas line GL4), and oxygen ions diffuse within the solid electrolyte layer 47 toward the anode 46. The oxygen ions that have reached the anode 46 are converted into oxygen by depriving them of electrons, and are discharged from the anode side exit port 422b.

In this configuration, carbon monoxide and hydrogen discharged from the cathode side outlet port 421b are supplied to the second reactor 5 (5a to 5c). Therefore, it is suitable for reactions that require hydrogen, such as conversion reactions from carbon monoxide to olefin compounds.

In the above description, hydrogen was used as a representative first gas component capable of accepting the oxygen element, but other gas components can also be used. Other first gas components include compounds having at least one structure selected from epoxy groups, hydroxyl groups, carboxyl groups and carbonyl groups, which are converted into CO ₂ or NO ₂ by accepting the oxygen element. Examples include gas components.
Examples of the first gas component include methane, ethane, propane, acetylene, ethylene, propylene, butene, methanol, ethanol, acetaldehyde, propionaldehyde, carbon monoxide, ammonia, and the like.
Note that depending on the configuration of the second reaction section 5, the first gas component that has received the oxygen element can also be used for converting CO _x (1≦x<1.5) into carbon valuables. In this case, the carbon valuables produced include, for example, paraffin, aromatic compounds (benzene, toluene, xylene, styrene, phenol, etc.), oxygenated compounds (ethanol, propanol, butanol, acetaldehyde, propionaldehyde, benzaldehyde, Examples include ethylene glycol, acetone, acrylic acid, etc.), nitrogen-containing compounds (urea, etc.), and the like.

Further, the second reaction section 5 may be supplied with a third gas component that can be used to convert CO _x (1≦x<1.5) into carbon valuables. Examples of the third gas component include the same gas component as the first gas component that has received the oxygen element, a gas component that functions as a catalyst in the reaction in the second reaction section 5, hydrogen chloride, hydrogen cyanide, and bromide. Examples include hydrogen.
Furthermore, by configuring the second reaction section 5 with a plurality of second reactors and alternately switching two types of gas to be supplied, it is also possible to generate (manufacture) carbon valuables by a chemical looping method. .

<Polymer manufacturing system>
The polymer production system of the present invention includes the above-described production apparatus 100 and a polymer production section that polymerizes carbon valuables as monomers to produce polymers.
The polymer generation section is connected to the produced gas discharge section 6 of the manufacturing apparatus 100.
Examples of the polymer produced in the polymer production section include polystyrene, phenol resin, styrene butadiene rubber (SBR), polyethylene terephthalate (PET), polyethylene (PE), polypropylene (PP), acrylic resin, and polycarbonate.
The type of polymer produced depends on the composition of the exhaust gas supplied to the second reaction section 5, the composition of the catalyst used in the second reaction section 5, and the reaction conditions (second reaction temperature, second reaction temperature, (pressure, etc.), the composition of the third gas component, etc.

According to the carbon valuables manufacturing apparatus and manufacturing system and polymer manufacturing system described above, the conversion of CO _x (1.5≦x≦2) into carbon valuables is performed through two steps. Therefore, compared to a single step, the equilibrium state of the reaction can be tilted toward the side where carbon valuables are produced.
In particular, since the second gas component with a boiling point higher than the boiling point of CO is removed between the two reactions, the second-stage reaction is less likely to be inhibited, and the conversion efficiency (conversion rate) to carbon valuables is sufficiently increased. can be increased to
Further, by selecting and combining the types of the first-stage reaction and the second-stage reaction, the desired carbon valuables can be produced.

Furthermore, each aspect described below may be provided.
In the apparatus for producing carbon valuables, the first reaction section includes a reactor containing an oxygen carrier having oxygen ion conductivity, and the first reaction section has a reactor containing an oxygen carrier having oxygen ion conductivity, and the CO _x (1.5≦x≦2) and the first and gas components are alternately supplied to the reactor.
The apparatus for producing carbon valuables, wherein the first reaction section includes a plurality of the reactors connected in series.
In the apparatus for producing carbon valuables, the first gas component accepts the oxygen element to form a compound having at least one structure selected from epoxy groups, hydroxyl groups, carboxyl groups, and carbonyl groups, H An apparatus for producing carbon valuables, which is converted into ₂ O, CO ₂ or NO ₂ .
The apparatus for producing carbon valuables, wherein the first reaction temperature in the first reaction section is higher than the second reaction temperature in the second reaction section.
The apparatus for producing carbon valuables, wherein the difference between the first reaction temperature and the second reaction temperature is 100°C or more.
The apparatus for producing carbon valuables, wherein the first reaction pressure in the first reaction section is lower than the second reaction pressure in the second reaction section.
The apparatus for producing carbon valuables, wherein the first reaction pressure is 1 MPaG or less.
In the apparatus for producing carbon valuables, in the second reaction section, the first gas component that has received the oxygen element converts the CO _x (1≦x<1.5) into the carbon valuables. Carbon valuables production equipment used for.
A method for producing carbon valuables, wherein CO _x (1.5≦x≦2) is converted into CO _x (1≦x<1.5) by using a first gas component that can accept oxygen element. a first conversion step of converting the CO _x (1 ≦x<1.5) into the carbon valuables.
A system for manufacturing carbon valuables, the system comprising the carbon valuables manufacturing device and a gas generation section that generates the gas containing the CO _x (1.5≦x≦2). system.
1. A system for producing a polymer, comprising: a production device for the carbon valuables; and a polymer generation section for producing the polymer by polymerizing the carbon valuables as a monomer.
Of course, this is not the case.

As mentioned above, various embodiments according to 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 new embodiment can be implemented in various other forms, and various omissions, substitutions, and changes can be made without departing from the gist of the invention. The embodiment and its modifications are included within the scope and gist of the invention, and are included within the scope of the invention described in the claims and its equivalents.

For example, the carbon valuables manufacturing device and the carbon valuables manufacturing system may each have any other additional configuration with respect to the above embodiment, or any configuration that exhibits a similar function. They may be replaced, or some components may be omitted.
Further, the method for producing carbon valuables of the present invention may include any other additional steps in addition to the above embodiments, and may be replaced with any other step that exhibits a similar function. , some steps may be omitted.
Furthermore, any configurations of the first to fifth embodiments may be combined.

10 : Carbon valuables manufacturing system 100 : Carbon valuables manufacturing apparatus 1 : Exhaust gas supply part 2 : Reducing gas supply part 3 : Gas switching part 4 : First reaction part 4R : Reducing agent 4a : First reactor 4a1: First reactor 4a2: First reactor 4b: First reactor 4b1: First reactor 4b2: First reactor 41: Pipe body 42: Housing 43: Internal space 421a: Cathode side Inlet port 421b: Cathode side outlet port 422a: Anode side inlet port 422b: Anode side outlet port 45: Cathode 46: Anode 47: Solid electrolyte layer 48: Power supply 5: Second reaction section 5a: Second reactor 5b: Second reactor 5c: Second reactor 6: Product gas discharge section 6a: Product gas discharge section 6b: Product gas discharge section 6c: Product gas discharge section 7: Gas switching section 8: Gas component removal section 8a: Gas Component removing section 8b: Gas component removing section GL1: Gas line GL2: Gas line GL3a: Gas line GL3b: Gas line GL4: Gas line GL4a: Gas line GL4b: Gas line GL5: Gas line GL5a: Gas line GL5b: Gas line GL5c :Gas line GL6 :Gas line GL6a :Gas line GL6b :Gas line J :Gas merging part J1 :Gas merging part J2 :Gas merging part J4 :Gas merging part

Claims (12)

An apparatus for producing carbon valuables,
a first reaction section that converts CO _x (1.5≦x≦2) into CO _x (1≦x<1.5) using a first gas component capable of accepting oxygen element;
a second reaction section that converts the CO _x (1≦x<1.5) into the carbon valuables;
a gas line connecting the first reaction section and the second reaction section and supplying exhaust gas generated in the first reaction section to the second reaction section;
An apparatus for producing carbon valuables, comprising: a gas component removal section that is disposed in the middle of the gas line and removes a second gas component having a boiling point higher than the boiling point of CO from the exhaust gas. The apparatus for producing carbon valuables according to claim 1,
The first reaction section has a reactor containing an oxygen carrier having oxygen ion conductivity,
An apparatus for producing carbon valuables, wherein the CO _x (1.5≦x≦2) and the first gas component are alternately supplied to the reactor. The apparatus for producing carbon valuables according to claim 2,
The first reaction section is an apparatus for producing carbon valuables, wherein the first reaction section includes a plurality of the reactors connected in series. In the apparatus for producing carbon valuables according to any one of claims 1 to 3,
By accepting the oxygen element, the first gas component converts into a compound having at least one structure selected from an epoxy group, a hydroxyl group, a carboxyl group, and a carbonyl group, _H2O , CO2 _, or _NO2 . Equipment for producing carbon valuables. In the apparatus for producing carbon valuables according to any one of claims 1 to 4,
The first reaction temperature in the first reaction section is higher than the second reaction temperature in the second reaction section. The apparatus for producing carbon valuables according to claim 5,
The apparatus for producing carbon valuables, wherein the difference between the first reaction temperature and the second reaction temperature is 100° C. or more. In the apparatus for producing carbon valuables according to any one of claims 1 to 6,
The first reaction pressure in the first reaction section is lower than the second reaction pressure in the second reaction section. The apparatus for producing carbon valuables according to claim 7,
The apparatus for producing carbon valuables, wherein the first reaction pressure is 1 MPaG or less. In the apparatus for producing carbon valuables according to any one of claims 1 to 8,
In the second reaction section, the first gas component that has received the oxygen element is used to convert the CO _x (1≦x<1.5) into the carbon valuables. Manufacturing equipment. A method for producing carbon valuables, the method comprising:
a first conversion step of converting CO _x (1.5≦x≦2) to CO _x (1≦x<1.5) using a first gas component capable of accepting oxygen element;
a removal step of removing a second gas component having a boiling point higher than the boiling point of CO from the exhaust gas generated in the conversion step;
a second conversion step of converting the CO _x (1≦x<1.5) in the exhaust gas into the carbon valuables. A system for producing carbon valuables,
The apparatus for producing carbon valuables according to any one of claims 1 to 9,
A system for producing carbon valuables, comprising: a gas generation section that generates a gas containing the CO _x (1.5≦x≦2). A system for producing a polymer, the system comprising:
The apparatus for producing carbon valuables according to any one of claims 1 to 9,
A polymer production system comprising: a polymer production section that polymerizes the carbon valuables as a monomer to produce the polymer.