JP2024006035A - Production system for organic substance, production device for organic substance and production method for organic substance - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a production system or the like for organic substance which can efficiently produce organic substance without wastefully discarding heat.

SOLUTION: A production system for an organic substance is provided. The production system comprises: a gas generation portion which generates gaseous starting material including carbon monoxide and carbon dioxide; an organic substance generation portion which supplies the gaseous starting material, and generates organic substance from the gaseous starting material; and a reduction portion which is provided between the gas generation portion and the organic substance generation portion and has a reductant which reduces carbon dioxide by using carbon dioxide and hydrogen to generate carbon monoxide. When temperature at which the organic substance is generated in the organic substance generation portion is denoted as X[°C], temperature at which the carbon monoxide is generated in the reduction portion is denoted as Y[°C], the production system for the organic substance satisfies a relationship of Y≤15X.

SELECTED DRAWING: Figure 1

COPYRIGHT: (C)2024,JPO&INPIT

Description

The present invention relates to an organic substance production system, an organic substance production apparatus, and an organic substance production method.

In recent years, environmental problems on a global scale have arisen, such as concerns about the depletion of fossil fuel resources and an increase in carbon dioxide in the atmosphere due to the mass consumption of oils, alcohols, and the like produced using petroleum as raw materials. In order to address these problems, methods for producing organic substances using raw materials other than petroleum, such as methods for producing bioethanol from edible raw materials such as corn by sugar fermentation, are attracting attention.

Sugar fermentation methods using such edible raw materials use limited farmland area for production other than food, which may lead to a rise in food prices. Therefore, methods are being considered for producing organic substances, which were conventionally produced from petroleum, using inedible raw materials that would otherwise have been discarded.
For example, Patent Document 1 discloses a method of converting a raw material gas containing carbon dioxide, carbon monoxide, and hydrogen into ethanol using gas-assimilating bacteria.

Japanese Patent Application Publication No. 2018-070465

However, according to studies conducted by the present inventors, the raw material gas generated in the gas generation section and the pretreated raw material gas are at high temperatures and need to be cooled to a temperature suitable for producing organic substances. There are many cases. In this case, the waste heat is wasted.
In view of the above-mentioned circumstances, the present invention provides an organic substance production system that can efficiently produce organic substances without wasting heat.

According to one aspect of the present invention, a system for producing organic substances is provided. This manufacturing system includes a gas generation section that generates a raw material gas containing carbon monoxide and carbon dioxide, an organic substance generation section that supplies the raw material gas and generates an organic substance from the raw material gas, and a gas generation section and an organic A reducing part is provided between the substance producing part and has a reducing body that reduces carbon dioxide to produce carbon monoxide using carbon dioxide and hydrogen. When the temperature at which an organic substance is generated in the organic substance generation section is X [° C.], and the temperature at which carbon monoxide is generated at the reduction section is Y [° C.], the relationship Y≦15X is satisfied.

According to this aspect, organic substances can be produced with high production efficiency without wasting heat.

1 is a schematic diagram showing the configuration of a first embodiment of an organic substance manufacturing system of the present invention. FIG. 2 is a schematic diagram showing the configuration of a reducing section in the organic substance manufacturing system of the first embodiment. FIG. 2 is a schematic diagram showing the structure of a reducing section and its vicinity in an organic substance production system according to a second embodiment. FIG. 2 is a schematic diagram showing the configuration of a reduction section having an irradiation device that irradiates microwaves. FIG. 7 is a schematic diagram showing the configuration of a reducing section in an organic substance manufacturing system according to a third embodiment.

Hereinafter, an organic substance production system, an organic substance production apparatus, and an organic substance production method will be described in detail based on preferred embodiments shown in the accompanying drawings.
<First embodiment>
First, a first embodiment of the organic substance manufacturing system of the present invention will be described.
FIG. 1 is a schematic diagram showing the configuration of a first embodiment of the organic substance manufacturing system of the present invention. FIG. 2 is a schematic diagram showing the configuration of the reducing section in the organic substance manufacturing system of the first embodiment.

The organic substance manufacturing system 100 (hereinafter also simply referred to as the “manufacturing system 100”) shown in FIG. (hereinafter also simply referred to as "manufacturing apparatus 1").
In addition, in this specification, the upstream side with respect to the flow direction of gas and liquid is also simply described as "upstream side," and the downstream side is also simply described as "downstream side."
In this embodiment, examples of the gasification furnace 10 include a combustion furnace, a blast furnace, a converter furnace, an electric furnace, a shaft furnace, and the like. In addition to the gasification furnace 10, the gas generation section is a CO _x emission source of at least one business facility selected from a paper mill, a cement factory, a thermal power plant, an oil refinery, an ethylene cracker, an oil refinery, and a chemical factory. You can.

In each furnace, exhaust gas (raw material gas) containing carbon dioxide and carbon monoxide is generated during combustion, melting, refining, etc. of the contents.
In the case of a combustion furnace (incinerator) in a garbage incinerator, the contents (waste) include, for example, plastic waste, food waste, municipal waste (MSW), industrial waste, waste tires, biomass waste, household waste, etc. Examples include trash (futons, papers), construction materials, etc. Note that these wastes may contain one type alone or two or more types.

In addition to carbon dioxide and carbon monoxide, exhaust gas typically may contain other gas components such as hydrogen, nitrogen, oxygen, water vapor, methane, and the like. The exhaust gas may further contain soot, tar, nitrogen compounds, sulfur compounds, phosphorus compounds, aromatic compounds, etc. as other components.
Exhaust gas is generated as a gas containing 10% by volume or more of carbon monoxide by performing heat treatment (commonly known as gasification) to incompletely burn the contents (carbon source) (that is, partially oxidizing the carbon source). You can.
By using exhaust gas, 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 generated in a combustion furnace or a smelter is preferable.

A manufacturing apparatus 1 is connected to such a gasification furnace 10. This manufacturing device 1 includes a culture tank (organic substance generation section) 2, a purification device 6, a gas line GL1 that connects the gasifier 10 and the culture tank 2, and a gas line GL1 that connects the culture tank 2 and the purification device 6. It has a liquid line LL.
In the culture tank 2, an organic substance-containing liquid containing organic substances is produced from the supplied exhaust gas (raw material gas) by the action of gas-assimilating bacteria (microbial fermentation).
Gas-utilizing bacteria include both eubacteria and archaea.

Examples of true bacteria include Clostridium bacteria, Moorella bacteria, Acetobacterium bacteria, Carboxydocella bacteria, Rhodopseudomonas bacteria, and Eubacterium. Examples include bacteria of the genus Eubacterium, bacteria of the genus Butyribacterium, bacteria of the genus Oligotropha, bacteria of the genus Bradyrhizobium, and bacteria of the genus Ralsotonia, which are aerobic hydrogen-oxidizing bacteria.

On the other hand, examples of archaea include bacteria of the genus Methanobacterium, bacteria of the genus Methanobrevibacter, bacteria of the genus Methanocalculus, bacteria of the genus Methanococcus, bacteria of the genus Methanococcus, and bacteria of the genus Methanococcus. sarcina) genus Bacteria, bacteria of the genus Methanosphaera, bacteria of the genus Methanothermobacter, bacteria of the genus Methanothrix, bacteria of the genus Methanoculeus, bacteria of the genus Methanofollis, bacteria of the genus Methanofollis, Bacteria of the genus Methanogenium, Methanospirylium Examples include bacteria of the genus Methanospirillium, bacteria of the genus Methanosaeta, bacteria of the genus Thermococcus, bacteria of the genus Thermofilum, bacteria of the genus Arcaheoglobus, and the like.

Among the gas-assimilating bacteria mentioned above, bacteria with a high ability to produce the desired organic substance are selected and used. For example, gas-assimilating bacteria with high ethanol-producing ability include Clostridium autoethanogenum, Clostridium ljungdahlii, Clostridium aceticum, and Clostridium aceticum. Clostridium carboxydivorans , Moorella thermoacetica, Acetobacterium woodii, and the like.

The medium (culture solution) used for culturing gas-assimilating bacteria is not particularly limited as long as it has an appropriate composition depending on the type. For example, when using Clostridium bacteria as gas-assimilating bacteria, for the culture medium, refer to paragraph 0091 of International Publication No. 2017/117309, paragraphs 0097 to 0098 of U.S. Patent Application Publication No. 2017/260552, etc. It can be done.
The culture tank 2 includes, for example, a culture reactor of the type that stirs the culture solution with a stirring plate, a culture reactor of the type that stirs the culture solution by circulating the culture solution itself, and a culture reactor of the type that stirs the culture solution by circulating the culture solution itself. A type of culture reactor that stirs the culture solution with accompanying water flow can be used.

In the middle of the gas line GL1 (that is, between the gasifier 10 and the culture tank 2), in order from the gasifier 10 side (upstream side), a reformer 3 and a reduction section 4 (reduction reactor 4a) are installed. and a preprocessing section 5 are provided.
In the reforming furnace 3, for example, in the presence of a catalyst, methane contained in the exhaust gas is reacted with steam at high temperature to convert it into carbon monoxide and hydrogen. At this time, a part of carbon monoxide may be converted into carbon dioxide and hydrogen by further reacting with water vapor.
The reaction temperature is preferably 500°C or higher and 1100°C or lower. Further, examples of the catalyst include a nickel catalyst, a nickel oxide catalyst, a ruthenium catalyst, a rhodium catalyst, a palladium catalyst, and a platinum catalyst.

The reforming furnace 3 may employ a method of converting gases such as methane and ethane contained in the exhaust gas and hydrocarbons such as tar and dioxins into carbon monoxide and hydrogen by retaining the gases at a high temperature. At this time, a combustion supporting gas such as oxygen or air may be supplied to raise the temperature.
Additionally, some of the carbon monoxide may be converted to carbon dioxide by reacting with oxygen. The temperature is preferably 1000°C or higher, more preferably 1100°C or higher and 1300°C or lower.

The exhaust gas that has passed through the reforming furnace 3 is mixed with hydrogen separated by a dehydrogenation device, which will be described later, and is supplied to the reduction reactor 4a (reduction section 4). In the reduction reactor 4a of the first embodiment, carbon monoxide can be generated from carbon dioxide (carbon dioxide can be converted into carbon monoxide) by using the hydrogen by a reverse water gas shift reaction caused by the action of a catalyst. .
As shown in FIG. 2, the reduction reactor 4a is a multi-tubular type that includes a plurality of tubes 41 each filled with (accommodates) a catalyst 4R, and a housing 42 in which the plurality of tubes 41 are housed in an internal space 43. It consists of a reactor (fixed bed type reactor). According to such a multi-tubular reactor, a sufficient opportunity for contact between the catalyst 4R and the gas can be ensured. As a result, the conversion efficiency of carbon dioxide into carbon monoxide can be increased.

Note that the reduction reactor 4a may be configured as a reactor (ie, a simple reactor) in which the pipe body 41 is omitted and the internal space 43 of the housing 42 is filled with the catalyst 4R.
The catalyst 4R of this embodiment is preferably in the form of particles (granules), scales, pellets, etc., for example. If the reducing agent 4R has such a shape, the filling efficiency into the pipe body 41 can be increased, and the contact area with the exhaust gas supplied into the pipe body 41 can be further increased.

When the catalyst 4R is in the form of particles, its volume average particle diameter is not particularly limited, but is preferably 1 mm or more and 50 mm or less, more preferably 1 mm or more and 30 mm or less. In this case, the contact area between the catalyst 4R and the gases (carbon dioxide and hydrogen) can be further increased, and the conversion efficiency of carbon dioxide into carbon monoxide can be further improved.
The particulate catalyst 4R is preferably a molded body manufactured by rolling granulation, since the sphericity is further increased.

Further, the catalyst 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 or reaction conditions, such as carbon materials (graphite, graphene, carbon black, carbon nanotubes, activated carbon, etc.), carbides such as Mo ₂ C, Examples include oxides such as zeolite, montmorillonite, 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 catalyst 4R and has an excellent ability to support the catalyst 4R. Here, the carrier does not participate in the reaction of the catalyst 4R and simply supports (holds) the catalyst 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 catalyst 4R.

Catalyst 4R contains a transition metal. Transition metals are not particularly limited as long as they can reduce carbon dioxide, but include Fe, Sc, Ti, V, Cr, Mn, Co, Ni, Cu, Zn, Y, Zr, Nb, Mo, Tc, Ru, Rh, Pd, Ag, Cd, La, Ce, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, Hf, Ta, W, Re, Os, Ir, Examples include Pt, Au, and Hg.
The catalyst 4R is preferably an alloy formed by adding at least one metal selected from the group consisting of Al, Ga, In, Cu, Ag, Au, Pd, and Mn to Fe, and is an Fe-Pd alloy. It is more preferable that there be. These catalysts 4R are useful because they have particularly good efficiency in converting carbon dioxide into carbon monoxide.

Further, in the reduction reactor 4a, the tube body (cylindrical molded body) 41 may be made of the catalyst 4R itself. Furthermore, a block-shaped, lattice-shaped (for example, net-shaped, honeycomb-shaped) molded body may be produced using the catalyst 4R, and the molded body may be placed in the housing 42. In these cases, the catalyst 4R as a filler may be omitted or may be used in combination.
Among these, a configuration in which a net-like body is made of the catalyst 4R and placed inside the housing 42 is preferable. In the case of such a configuration, it is possible to prevent the passage resistance of the exhaust gas from increasing within the reduction reactor 4a, and to ensure a sufficient opportunity for the catalyst 4R to come into contact with the exhaust gas.

The pretreatment section 5 includes a dehydrogenation device and a PSA device.
The dehydrogenation device is located downstream of the reduction reactor 4a (reduction section 4) and is used to remove (separate) hydrogen from the raw material gas. This dehydrogenation device can be configured with a separator containing a cylindrical separation membrane that selectively permeates and separates hydrogen.
Examples of constituent materials of such a separation membrane include metal materials, ceramic materials, resin materials, and the like.
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 the ceramic material include titanium nitride, zeolite, silica (glass), alumina, and composite materials containing one or more of these (eg, alumina-carbon material).
Examples of the resin material include polyamide, polyimide, polysulfone, 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, hydrogen can be separated 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 hydrogen permeability 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.
The average pore diameter of the separation membrane is preferably 500 pm or less, more preferably 300 pm or more and 400 pm or less. Thereby, hydrogen separation efficiency can be further improved.
The dehydrogenation device is connected to the upstream side of the reduction reactor 4a of the gas line GL1 via the gas line GL2. With this configuration, the reformed exhaust gas and hydrogen are mixed and supplied to the reduction reactor 4a.

A removing section 7 is provided in the middle of the gas line GL2. This removal section 7 removes impurities that are contained in the hydrogen-based gas converted from the dehydrogenation device (the gas before being supplied to the reduction reactor 4a) and reduce the reactivity of the catalyst (reductant) 4R. do.
Such impurities include, but are not particularly limited to, sulfur or sulfur compounds, chlorine or chlorine compounds, cyanide compounds, and the like. Among these, it is preferable to remove sulfur compounds, particularly hydrogen sulfide, as impurities. By removing hydrogen sulfide, it is possible to suitably prevent the reactivity of the catalyst 4R from extremely decreasing or deactivating it.

The removal section 7 can be configured, for example, by a reactor filled with a desulfurizing agent. Examples of the desulfurization agent include iron oxide desulfurization agents, activated carbon desulfurization agents, copper-zinc desulfurization agents, copper-zinc-aluminum desulfurization agents, lime desulfurization agents, and the like.
Note that if an iron oxide desulfurization agent is used, iron sulfide produced by reaction with hydrogen sulfide can react with oxygen, so oxygen can also be removed from the gas passing through the gas line GL2.

A PSA device is a pressure swing adsorption type separator, and is used, for example, to remove BTEX, carbon dioxide, nitrogen, and the like.
For example, porous materials such as activated carbon, zeolite, silica gel, and molecular sieves, and aqueous solutions such as amine solutions can be used as adsorbents in the PSA device. Activated carbon or zeolite is preferably used in the PSA device. Separable compounds can be selected by setting the type of porous material and the size of the pores.
When separating two or more compounds in a PSA device, multiple separators each filled with porous materials of different types and pore sizes may be used; A single packed separator may also be used.

The carbon dioxide separated by the PSA device may be mixed with exhaust gas and supplied to the reduction reactor 4a.
Further, the nitrogen separated by the PSA device may be filled into the culture tank 2 when culturing gas-utilizing bacteria, or may be filled for cleaning the reduction reactor 4a, and the nitrogen separated by the PSA device and/or the TSA May be filled for cleaning of equipment (if used). Note that nitrogen may be filled into only one of the above devices, or may be filled into two or more of the devices.
By removing nitrogen from the exhaust gas in this manner, the volume of the exhaust gas to be treated on the downstream side can be reduced, so that the pretreatment section 5 disposed on the downstream side can be downsized.

In addition to the dehydrogenation device and the PSA device, the pretreatment section 5 may include a washing and dehumidifying tower, a filter, a deoxidation device, a deacetylene device, a TSA device, a PTSA device, and the like. Note that these can be used alone or in any combination, and their arrangement order is also arbitrary.
The cleaning and dehumidifying tower is a so-called scrubber, and is used to remove pollutants (for example, soot), water-soluble substances, and the like contained in exhaust gas. In the cleaning and dehumidifying tower, cleaning is carried out 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. Furthermore, examples of the cleaning liquid include water, acidic solutions, alkaline solutions, and the like. Among these, water is preferred as the cleaning liquid. Further, the temperature of the cleaning liquid is usually 40°C or lower, preferably 30°C or lower, more preferably 25°C or lower, and even more preferably 15°C or lower.

Filters are used to remove particulates with a size smaller than the size of soot. This filter can be composed of, for example, a bag filter.
The deoxidizer is used to remove oxygen and is composed of a reactor filled with metal particles such as copper (Cu), platinum (Pt), and nickel (Ni) as an oxygen removal catalyst. Can be done. The oxygen removal catalyst is preferably heated to, for example, 150°C or more and 400°C or less.
The deacetylenization device is used to remove acetylene, and can be configured with a reactor filled with noble metal particles such as palladium (Pd) and platinum (Pt) as an acetylene removal catalyst.
Note that, by removing acetylene prior to deoxygenation, there is an advantage that the adverse effect of acetylene on the oxygen removal catalyst can be suitably prevented or reduced.

The TSA device is a temperature swing adsorption type separator, and is used, for example, to remove aromatic compounds other than BTEX.
The PTSA device is a pressure and temperature swing adsorption type separator, and is used, for example, to collectively remove the components to be removed by the PSA device and TSA device.
Note that the type of adsorbent, constituent materials, etc. used in the TSA device and the PTSA device can be the same as those described for the PSA device.

The exhaust gas treated in the pretreatment section 5 is supplied to the culture tank 2.
The concentration of carbon dioxide contained in the exhaust gas supplied to the culture tank 2 is preferably 0.1 volume% or more and 30 volume% or less, more preferably 0.3 volume% or more and 25 volume% or less, It is more preferably 0.5 volume % or more and 20 volume % or less, particularly preferably 0.8 volume % or more and 15 volume % or less, and most preferably 1 volume % or more and 10 volume % or less.

The concentration of carbon monoxide contained in the exhaust gas supplied to the culture tank 2 is preferably 10 volume% or more and 80 volume% or less, more preferably 15 volume% or more and 50 volume% or less, and 20 volume%. More preferably, the content is 45% by volume or less.
Further, the concentration of hydrogen contained in the exhaust gas supplied to the culture tank 2 is preferably 1 volume% or more and 45 volume% or less, more preferably 5 volume% or more and 35 volume% or less, and 10 volume% or less. More preferably, the content is 30% by volume or less.

Furthermore, the concentration of nitrogen contained in the exhaust gas supplied to the culture tank 2 is preferably 30 volume% or less, more preferably 1 volume% or more and 25 volume% or less, and 5 volume% or more and 20 volume% or less. % or less is more preferable.
According to the above configuration, since exhaust gas having a low concentration of hydrogen is supplied to the culture tank 2, hydrogen is unlikely to reduce the activity of gas-assimilating bacteria. Moreover, since the exhaust gas has an increased concentration of carbon monoxide by passing through the reduction reactor 4a, organic substances can be efficiently produced in the culture tank 2.

In the culture tank 2, an organic substance-containing liquid containing organic substances is generated from the exhaust gas by the action of gas-assimilating bacteria.
A purification device 6 is connected to the culture tank 2 via a liquid line LL. This purification device 6 is a device that purifies organic substances from an organic substance-containing liquid.
Examples of the 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 that removes low-boiling substances that have a boiling point lower than organic substances, and a treatment device that removes low-boiling substances that have a boiling point lower than that of organic substances. Examples include processing equipment that removes high-boiling substances, processing equipment that includes an ion exchange membrane, and the like. These devices may be used alone or in combination of two or more.

When using a distillation apparatus, the temperature inside the distillation apparatus during distillation of organic substances (especially ethanol) is not particularly limited, but is preferably 100°C or less, more preferably 70°C or more and 95°C or less. preferable. By setting the temperature to such a temperature, separation of necessary organic substances from other components, that is, distillation (purification) of the organic substances can be performed more reliably.
The pressure within the distillation apparatus during distillation of the organic substance may be normal pressure, but is preferably less than atmospheric pressure (vacuum distillation), and more preferably 60 to 95 kPaA. By setting the pressure to such a pressure, it is possible to improve the separation efficiency of organic substances and, by extension, the yield of organic substances.
The yield of organic substances (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.

Examples of the organic substances obtained in this way include monools such as methanol and ethanol, diols such as 2,3-butanediol, acetic acid, lactic acid, isoprene, and butadiene, and have a carbon number of 1 to 1. The monools or diols of No. 4 are preferable, and ethanol is more preferable.
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 fuels. In addition, high-concentration ethanol can be used as fuel ethanol to be mixed with gasoline, etc., and can also be used, for example, as a raw material for cosmetics, beverages, chemicals, fuel (jet fuel), etc., and as an additive for foods. , extremely versatile.

Next, a method of using the manufacturing system 100 of the first embodiment (a method of manufacturing an organic substance) will be described.
[1A] First, exhaust gas (raw material gas containing carbon monoxide, carbon dioxide, and other gas components) discharged from the gasifier 10 is supplied to the reformer 3. At this time, methane contained in the exhaust gas is converted into carbon monoxide and hydrogen.
[2A] Next, the exhaust gas that has passed through the reforming furnace 3 is mixed with hydrogen separated by the dehydrogenator.
[3A] Thereafter, the exhaust gas mixed with hydrogen is supplied to the reduction reactor 4a. In the reduction reactor 4a, carbon dioxide is reduced using carbon dioxide and hydrogen to generate carbon monoxide (reduction step). Specifically, in the reduction reactor 4a, by the action of the catalyst 4R, carbon dioxide and hydrogen are reacted and converted into carbon monoxide and water. This increases the concentration of carbon monoxide and water vapor contained in the exhaust gas.

[4A] Next, the exhaust gas that has passed through the reduction reactor 4a is supplied to the pretreatment section 5. In the pretreatment section 5, hydrogen is removed (separated) from the exhaust gas by a dehydrogenation device.
Furthermore, the PSA device removes (separates) BTEX, carbon dioxide, nitrogen, etc. from the exhaust gas. The separated carbon dioxide can be combined into the gas line GL2, for example.
Further, in the pretreatment section 5, for example, water-soluble substances, soot, fine particles smaller than the size of soot, oxygen, acetylene, aromatic compounds other than BTEX, etc. may be removed from the exhaust gas.

[5A] Next, the hydrogen separated in the pretreatment section 5 flows to the upstream side of the reduction reactor 4a of the gas line GL1 via the gas line GL2.
At this time, the gas mainly consisting of hydrogen flowing through the gas line GL2 passes through the removal section 7 to remove sulfur compounds (especially hydrogen sulfide), so the activity of the catalyst 4R of the reduction reactor 4a is reduced. The decline can be prevented or suppressed.

[6A] Next, the exhaust gas that has passed through the pretreatment section 5 is supplied to the culture tank 2. In the culture tank 2, an organic substance-containing liquid containing organic substances is generated from the exhaust gas by the action of gas-assimilating bacteria (cultivation process: organic substance generation process).
Here, the temperature at which the organic substance-containing liquid is generated in the culture tank (organic substance generation section) 2 is defined as X [°C], and the temperature at which carbon monoxide is generated at the reduction reactor 4a (reduction section 4) is defined as When Y [° C.], it is preferable to satisfy the relationship Y≦15X, more preferably to satisfy the relationship Y≦12.5X, and even more preferably to satisfy the relationship Y≦10X. If X and Y satisfy the above relationship, the temperature at which carbon monoxide is produced in the reduction reactor 4a can be set relatively low. No need for high cooling. Therefore, less heat can be discarded and is less likely to be wasted.

Further, it is preferable that the relationship 3X≦Y is satisfied, it is more preferable that the relationship 4X≦Y is satisfied, and it is even more preferable that the relationship 5X≦Y is satisfied. If X and Y satisfy the above relationship, the temperature when producing carbon monoxide in the reduction reactor 4a can be prevented from becoming extremely low, and sufficient conversion efficiency from carbon dioxide to carbon monoxide can be achieved. can be maintained.
The specific value of X is preferably 25°C or more and 50°C or less, more preferably 30°C or more and 45°C or less, and even more preferably 35°C or more and 40°C or less. The specific value of Y is preferably 125°C or more and 500°C or less, more preferably 150°C or more and 450°C or less, and even more preferably 175°C or more and 400°C or less.

When producing the organic substance-containing liquid in the culture tank 2, the culture tank 2 may be filled with nitrogen removed (separated) by the PSA device. In this case, the concentration of oxygen contained in the space within the culture tank 2 can be relatively reduced, and the adverse effect of oxygen on gas-assimilating bacteria can be prevented or reduced.
[7A] Finally, the organic substance-containing liquid produced in the culture tank 2 is supplied to the purification device 6 via the liquid line LL. In the purification device 6, the organic substance contained in the organic substance-containing liquid is purified, and a purified product containing the organic substance at a high concentration is obtained.

<Second embodiment>
Next, a second embodiment of the organic substance manufacturing system of the present invention will be described.
The organic substance manufacturing system of the second embodiment will be described below, focusing on the differences from the organic substance manufacturing system of the first embodiment, and will omit descriptions of similar matters.
FIG. 3 is a schematic diagram showing the structure of the reduction section and its vicinity in the organic substance production system of the second embodiment.

The manufacturing system 100 of the second embodiment differs in the configuration of the reducing unit 4 and its vicinity, and is otherwise the same as the manufacturing system 100 of the first embodiment.
The manufacturing system 100 shown in FIG. 3 includes a carbon dioxide removal device (separation unit) 8 that separates carbon dioxide from exhaust gas between the reforming furnace 3 and the pretreatment unit 5 of the gas line GL1. In addition to the above-mentioned PSA device or TSA device, this decarbonization device 8 includes, for example, a PTSA device (a pressure and temperature swing adsorption type separator), a low temperature separation type (deep cooling type) separator, and a membrane separation type separator. It can be composed of a separator, an amine absorption type separator, an amine adsorption type separator, etc.

The reduction unit 4 of the second embodiment includes a gas switching unit 44 and two reduction reactors 4b1 and 4b2.
The carbon dioxide removal device 8 is connected to the gas switching unit 44 via the gas line GL11, and the dehydrogenation device is connected to the gas switching unit 44 via the gas line GL2.
The gas switching unit 44 is connected to the inlet ports of the reduction reactors 4b1 and 4b2 via two gas lines GL31 and GL32, respectively.
The gas switching unit 44 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.

With this configuration, carbon dioxide is separated from the exhaust gas by the carbon dioxide removal device 8 when the exhaust gas passes through the gas line GL1. The separated gas mainly composed of carbon dioxide (hereinafter also referred to as "oxidizing gas") passes through the gas line GL11, the gas switching section 44, and the gas lines GL31 and GL32, and is then supplied to each of the reduction reactors 4b1 and 4b2. Supplied.
On the other hand, the gas mainly composed of hydrogen (hereinafter also referred to as "reducing gas") from the dehydrogenation device passes through the gas line GL2, the gas switching section 44, and the gas lines GL31 and GL32, and then passes through each reduction reactor. It is supplied to 4b1 and 4b2.

The reduction reactors 4b1 and 4b2 have the same configuration as the reduction reactor 4a shown in FIG. 2, and a reducing agent 4R is housed (filled) in the tube body 41 instead of the catalyst 4R. The reducing agent 4R can have the same shape, size, configuration, etc. as the catalyst 4R, except that the material of the active part is different.
The reducing agent 4R contains at least one of a metal and its oxide (oxygen carrier with oxygen ion conductivity). At least one of the metal and its oxide is not particularly limited as long as it can reduce carbon dioxide.

At least one of the metal and its oxide preferably contains at least one metal element selected from the metal elements belonging to Groups 3 to 13, and preferably selected from the metal elements belonging to Groups 3 to 12. It is more preferable to contain at least one of lanthanum, titanium, vanadium, iron, copper, zinc, nickel, manganese, chromium, cerium, etc. Particularly preferred are metal oxides or composite metal oxides containing. These metal oxides are useful because they have particularly good efficiency in converting carbon dioxide to carbon monoxide.

The volumes of the two reduction reactors 4b1 and 4b2 are set to be approximately equal to each other, and are set appropriately depending on the amount of gas to be supplied. Further, the volumes of the two reduction reactors 4b1 and 4b2 may be varied depending on the composition of the gas, the performance of the reducing agent 4R, and the like.
According to the configuration described above, by switching the gas line (flow path) in the gas switching unit 44, for example, the oxidation reactor 4b1 containing the reducing agent 4R before oxidation is supplied to the reduction reactor 4b1 via the gas line GL31. Reducing gas can be supplied to the reducing reactor 4b2 containing the oxidized reducing agent 4R via the gas line GL32.

At this time, the reaction of the following formula 1 proceeds in the reduction reactor 4b1, and the reaction of the following formula 2 proceeds in the reduction reactor 4b2. 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 in the gas switching unit 44, the reaction of the above formula 2 can proceed in the reduction reactor 4b1, and the reaction of the above formula 1 can proceed in the reduction reactor 4b2.
That is, the oxidizing gas and the reducing gas are switched and supplied to the reduction reactor 4b1 and the reduction reactor 4b2.

Note that the reactions shown in Formulas 1 and 2 above are both endothermic reactions. For this reason, the manufacturing system 100 performs reducing agent heating that heats the reducing agent 4R when bringing the oxidizing gas and reducing gas into contact with the reducing agent 4R (that is, when the oxidizing gas and reducing gas react with the reducing agent 4R). It is preferable to further include a section (not shown in FIG. 3).
By providing such a reducing agent heating section, the temperature in the reaction between the oxidizing gas and reducing gas and the reducing agent 4R can be easily maintained at a predetermined temperature, and a decrease in the conversion efficiency of carbon dioxide into carbon monoxide can be suitably prevented or In addition to suppressing this, it is possible to further promote the regeneration of the reducing agent 4R by the reducing gas.

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 system 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 oxidizing gas and the reducing gas and the reducing agent 4R, thereby increasing the conversion efficiency of carbon dioxide into carbon monoxide. It is possible to suitably prevent or suppress a decrease in , and further promote the regeneration of the reducing agent 4R by the reducing gas.
That is, it is preferable that the manufacturing system 100 is 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 reduction reactors 4b1 and 4b2 is preferably 70% or more, more preferably 85% or more, and even more preferably 95% or more. . The upper limit of the conversion rate of carbon dioxide to carbon monoxide is usually about 98%.
Such conversion rate depends on the type of reducing agent 4R used, the concentration of carbon dioxide contained in the oxidizing gas, the concentration of hydrogen contained in the reducing gas, the temperature of the reduction reactors 4b1 and 4b2, and the reduction of the oxidizing gas and reducing gas. It can be set by adjusting the flow rate (flow rate) to the reactors 4b1 and 4b2, the timing of switching the oxidizing gas and reducing gas to the reducing reactors 4b1 and 4b2, and the like.

Gas lines GL41 and GL42 are connected to the outlet ports of the reduction reactors 4b1 and 4b2, respectively, and these join together at a gas merging section J to form a gas line GL4. Furthermore, valves (not shown) are provided in the middle of the gas lines GL41 and GL42, as necessary.
For example, by adjusting the opening degree of the valve, the passing rate of the oxidizing gas and reducing gas passing through the reduction reactors 4b1 and 4b2 (i.e., the processing rate of the oxidizing gas by the reducing agent 4R and the processing rate of the reducing agent 4R by the reducing gas) speed) can be set.

The gas line GL4 joins the gas line GL1 between the carbon dioxide removal device 8 and the pretreatment section 5. Thereby, the carbon monoxide generated in the reduction reactors 4b1 and 4b2 can be combined with the exhaust gas and supplied to the culture tank 2.
Therefore, the concentration of carbon monoxide in the exhaust gas supplied to the culture tank 2 via the pretreatment section 5 can be sufficiently increased. As a result, the production efficiency of organic substances in the culture tank 2 can be further improved.

Next, a method of using the manufacturing system 100 of the second embodiment (a method of manufacturing an organic substance) will be described.
[0B] First, by switching the gas lines (flow paths) in the gas switching unit 44, the gas line GL11 and the reduction reactor 4b1 are communicated, and the gas line GL2 and the reduction reactor 4b2 are communicated.
[1B] Next, the exhaust gas discharged from the gasifier 10 is supplied to the reformer 3.
[2B] Thereafter, when the exhaust gas that has passed through the reforming furnace 3 passes through the carbon dioxide removal device 8, carbon dioxide is removed (separated).

[3B-1] Next, the gas mainly composed of carbon dioxide (oxidizing gas) separated by the carbon dioxide removal device 8 is supplied to the reduction reactor 4b1 via the gas line GL11. In the reduction reactor 4b1, the reducing agent 4R reduces carbon dioxide through contact with carbon dioxide and converts it into carbon monoxide. At this time, the reducing agent 4R is brought into an oxidized state by contact with carbon dioxide.
Here, the temperature of the reduction reactor 4b1 (exhaust gas, reducing agent 4R) is preferably 125°C or more and 500°C or less, more preferably 150°C or more and 450°C or less, and 175°C or more and 400°C or less. It is even more preferable that there be.
Note that the heat source here may be obtained by reusing exhaust heat from a process (for example, a reducing gas boiler, etc.).

Further, the pressure of the reduction reactor 4b1 (exhaust gas, reducing agent 4R) is preferably less than 1 MPaG, more preferably 0.9 MPaG or less, and even more preferably 0.2 MPaG or more and 0.8 MPaG or less. .
If the reaction conditions are set within the above range, for example, the reduction reaction of carbon dioxide in the reduction reactor 4b1 can proceed more smoothly.

[3B-2] On the other hand, a gas mainly consisting of hydrogen (reducing gas) is supplied from the dehydrogenation device to the reduction reactor 4b2 via the gas line GL2. In the reduction reactor 4b2, the reducing agent 4R in an oxidized state is reduced (regenerated) by contact with hydrogen. At this time, water is produced.
Here, the temperature of the reduction reactor 4b2 (reducing gas, reducing agent 4R) is preferably 125°C or more and 500°C or less, more preferably 150°C or more and 450°C or less, and 175°C or more and 400°C or less. It is more preferable that
Similar to the above, the heat source here may also be obtained by recycling waste heat from the process (eg, reducing gas boiler, etc.).

Further, the pressure of the reduction reactor 4b2 (reducing gas, reducing agent 4R) is preferably less than 1 MPaG, more preferably 0.9 MPaG or less, and even more preferably 0.2 MPaG or more and 0.8 MPaG or less. preferable.
If the reaction conditions are set within the above range, for example, the reduction reaction of the reducing agent 4R in the reduction reactor 4b2 can proceed more smoothly.

By performing the above step [3B-1] and the above step [3B-2] interchangeably for the reduction reactors 4b1 and 4b2, the conversion of carbon dioxide into carbon monoxide by the reducing agent 4R and the oxidation state Reduction (regeneration) of the reducing agent 4R with hydrogen can be performed alternately.
While replacing step [3B-1] and step [3B-2], the nitrogen separated by the PSA device may be supplied (filled) to the reduction reactors 4b1 and 4b2. That is, the reduction reactors 4b1 and 4b2 may be purged with nitrogen.

[4B] Next, the gas that has passed through the reduction reactors 4b1 and 4b2 is mixed with the exhaust gas that passes through the gas line GL1 via GL41, GL42, and GL4, and then is supplied to the pretreatment section 5.
[5B] Next, the exhaust gas that has passed through the pretreatment section 5 is supplied to the culture tank 2.
[6B] Finally, the organic substance-containing liquid produced in the culture tank 2 is supplied to the purification device 6.

According to the manufacturing system 100 of the second embodiment, the same operations and effects as those of the manufacturing system 100 of the first embodiment can be obtained.
In particular, in the second embodiment, in the two reduction reactors 4b1 and 4b2, at least a part of the oxygen element released from carbon dioxide is converted into the reducing agent 4R by the reduction reaction of carbon dioxide by the reducing agent (reductant) 4R. Since it is incorporated, it can be separated within the reduction reaction system. Then, the oxidizing gas and the reducing gas are switched and supplied to the two reduction reactors 4b1 and 4b2. Therefore, it becomes difficult for carbon monoxide and water, which are reaction products, to coexist in one reduction reactor 4b1, 4b2 (reduction reaction system). Therefore, a decrease in the conversion efficiency of carbon dioxide to carbon monoxide due to chemical equilibrium constraints can be prevented or suppressed.

Note that in the second embodiment, the number of reduction reactors installed may be one, or three or more.
When one reduction reactor is installed, for example, oxidizing gas and reducing gas can be switched and alternately supplied to the reduction reactor.
Further, when three or more reduction reactors are installed, for example, when supplying oxidizing gas to one reduction reactor, reducing gas can be supplied to the remaining reduction reactors continuously or in parallel.

In addition, although we have explained using a gas mainly composed of hydrogen to reduce (regenerate) the reducing agent 4R in an oxidized state, instead of or in addition to hydrogen, hydrocarbons (e.g., methane, ethane, acetylene, etc.) ) and ammonia can also be used.
For example, when a deacetylenization device is used, acetylene separated by the deacetylenization device may be mixed into the gas line GL2 and supplied to the reduction reactors 4b1 and 4b2.

Furthermore, the reduction unit 4 may include an irradiation device 49 that irradiates microwaves.
FIG. 4 is a schematic diagram showing the configuration of a reducing section having an irradiation device that irradiates microwaves.
The reduction section 4 shown in FIG. 4 includes reduction reactors 4a, 4b1, and 4b2 and an irradiation device 49.
By providing such an irradiation device 49, only the vicinity of the surface of the reducing body (catalyst or reducing agent 4R) can be locally (preferentially) activated by microwaves. Therefore, carbon dioxide can be easily converted into carbon monoxide even at relatively low temperatures.

Microwave refers to electromagnetic waves with a frequency of 300 MHz to 300 GHz, including ultrahigh frequency (UHF) with a frequency of 300 to 3000 MHz, centimeter wave (SHF) with a frequency of 3 to 30 GHz, millimeter wave (EHF) with a frequency of 30 to 300 GHz, and It is classified as submillimeter wave (SHF) of ~3000GHz. Among these, ultrahigh frequency (UHF) is preferable as the microwave. By using ultrahigh frequency (UHF), the reductant can be heated to the desired temperature in a shorter time.
Note that when performing microwave irradiation, measures against leakage of radio waves in accordance with the Radio Law are appropriately taken.

Microwave irradiation may be performed continuously or intermittently (pulsed).
Note that the irradiation device 49 may be placed outside or inside the reduction reactors 4a, 4b1, and 4b2, as shown in FIG.
Further, by keeping the gas composition of the exhaust gas away from the explosive range, it is possible to suitably prevent the exhaust gas from becoming an ignition source, regardless of the microwave irradiation conditions.

<Third embodiment>
Next, a third embodiment of the organic substance manufacturing system of the present invention will be described.
The organic substance manufacturing system according to the third embodiment will be described below, focusing on the differences from the organic substance manufacturing systems according to the first and second embodiments, and will omit descriptions of similar matters. do.
FIG. 5 is a schematic diagram showing the configuration of the reducing section in the organic substance manufacturing system of the third embodiment.

The manufacturing system 100 of the third embodiment differs in the configuration of the reducing unit 4, and is otherwise the same as the manufacturing system 100 of the first embodiment.
The reduction unit 4 of the third embodiment is a reduction reactor 4c (also called a reaction cell, an electrolytic cell, or an electrochemical cell) that converts hydrogen into carbon monoxide through an electrochemical reduction reaction of carbon dioxide. ).
The reduction reactor 4c shown in FIG. 5 includes a housing 42 and a bipolar membrane 47 that partitions the space inside the housing 42 into left and right sides.

The bipolar membrane 47 is composed of a joined body in which a cation exchange layer 471 and an anion exchange layer 472 are joined.
A right space 421 and a left space 422 within the housing 42, which are partitioned by the bipolar membrane 47, store liquids (eg, electrolyte) 421w and 422w, respectively.
The cathode 45 is immersed in the liquid 421w, and the anode 46 is immersed in the liquid 422w. The cathode 45 and the anode 46 can each be composed of a catalyst, for example, a surface of copper oxide nanowires coated with tin dioxide.

Further, a power source 48 is electrically connected to the cathode 45 and the anode 46 . 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 organic substances can be further improved.
In the reduction reactor 4c, when exhaust gas (carbon dioxide) is supplied to the liquid 491, carbon monoxide is generated by a reduction reaction of carbon dioxide due to the action of electrons supplied from the power supply 48 and the catalyst.
On the other hand, in the liquid 422w, hydroxide ions are converted into oxygen by having their electrons taken away by the anode 46.

Further, it is preferable that the pH of the liquid 421w is set to around neutrality, and the pH of the liquid 422w is set to be alkaline (about 13).
In this embodiment, the cathode 45 constitutes a reductant that donates electrons and converts carbon dioxide into carbon monoxide. Note that the cathode 45 can also be configured by supporting the above-mentioned catalyst on a current collector, and in this case, the catalyst itself constitutes a reductant.
Further, when a metal complex is used as a catalyst, the metal complex may be dissolved in the liquid 421w.

According to the organic substance production system, organic substance production apparatus, and organic substance production method as described above, the reaction temperature in the reduction reactor (reduction section) and the reaction temperature in the culture tank (organic substance production section) can be adjusted. Since the settings are made so that they do not deviate too much, it is possible to efficiently produce organic substances without wasting discarded heat.
Further, in the present invention, the generation of organic substances from the raw material gas may be performed using a reactor (organic substance generation section) containing a catalyst.
Examples of such catalysts include ruthenium, rhodium, manganese, germanium, tantalum, zirconium, niobium, hafnium, lanthanum, cerium, aluminum, magnesium, copper, zinc, silicon, and oxides thereof. One type can be used alone or two or more types can be used in combination.

Also in this case, the reaction temperature in the organic substance generation section and the reaction temperature in the reduction section are set so as to satisfy the above-mentioned relationship. Thereby, it is possible to suitably prevent or suppress wastage of wasted heat.
The specific temperature at which an organic substance is generated from a raw material gas using a catalyst is preferably 30°C or more and 40°C or less, more preferably 35°C or more and 38°C or less.
Furthermore, each aspect described below may be provided.

(1) A system for producing an organic substance, including a gas generation unit that generates a raw material gas containing carbon monoxide and carbon dioxide, and an organic material that supplies the raw material gas and generates an organic substance from the raw material gas. a reducing body that is provided between the gas generating unit and the organic substance generating unit and that uses the carbon dioxide and hydrogen to reduce the carbon dioxide and generate carbon monoxide; and when the temperature at which the organic substance is produced in the organic substance generation section is X [°C], and the temperature at which the carbon monoxide is produced in the reduction section is Y [°C]. , Y≦15X.

(2) The organic substance manufacturing system according to (1) above, which satisfies the relationship 3X≦Y.

(3) The system for producing an organic substance according to (1) or (2) above, wherein the reducing unit further includes an irradiation device that irradiates the reductant with microwaves.

(4) The system for producing an organic substance according to any one of (1) to (3) above, further comprising a separation section that separates the carbon dioxide supplied to the reduction section from the source gas, The carbon dioxide separated in the separation section is supplied to the reduction section, and the carbon monoxide generated in the reduction section is combined with the raw material gas and supplied to the organic substance generation section. A manufacturing system for organic substances.

(5) In the system for producing an organic substance according to any one of (1) to (4) above, the organic substance generating section converts the raw material gas into the organic substance-containing liquid by the action of gas-assimilating bacteria. An organic substance production system that is a culture tank that produces .

(6) In the system for producing an organic substance according to any one of (1) to (5) above, the reducing unit includes oxygen released from the carbon dioxide by the reduction reaction of the carbon dioxide by the reductant. A system for producing an organic substance, comprising at least one reactor capable of separating at least a portion of an element within the reduction reaction system.

(7) In the system for producing an organic substance according to (6) above, the reductant is brought into an oxidized state when reducing the carbon dioxide and converting it into the carbon monoxide, and the reductant in the oxidized state is A system for producing an organic substance that is reduced by contact with the hydrogen.

(8) In the system for producing an organic substance according to (7) above, the reducing section includes a plurality of the reactors, and each of the reactors is supplied with the carbon dioxide and the hydrogen in a switched manner. A production system for organic substances.

(9) An organic substance production device used by being connected to a gas generation unit that generates a raw material gas containing carbon monoxide and carbon dioxide, which supplies the raw material gas and generates an organic substance from the raw material gas. an organic substance generating section, and a reductant that is provided between the gas generating section and the organic substance generating section, and that reduces the carbon dioxide and generates carbon monoxide using the carbon dioxide and hydrogen. a reducing part having a temperature of X [°C] when the organic substance is produced in the organic substance generating part, and a temperature of Y [°C] when the carbon monoxide is produced in the reducing part. ], an apparatus for producing an organic substance that satisfies the relationship Y≦15X.

(10) A method for producing an organic substance, comprising an organic substance generation step of supplying a raw material gas containing carbon monoxide and carbon dioxide and generating an organic substance from the raw material gas, and prior to the organic substance generation step. , a reduction step of reducing the carbon dioxide with a reductant to generate carbon monoxide using the carbon dioxide and hydrogen, and a temperature at which the organic substance is generated in the organic substance generation step. is X [° C.], and the temperature at which the carbon monoxide is produced in the reduction step is Y [° C.], the method for producing an organic substance satisfies the relationship Y≦15X.
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 organic substance production system and organic substance production apparatus of the present invention may each have any other additional configuration with respect to the above embodiment, or any configuration that exhibits a similar function. may be replaced with , or a part of the structure may be omitted.
In addition, the method for producing an organic substance of the present invention may include any other additional steps than the above embodiments, and may be replaced with any other step that exhibits the same function. Some steps may be omitted.

Furthermore, in the present invention, the dehydrogenation device (hydrogen separation section) that separates hydrogen from exhaust gas (raw material gas) may be omitted.
In this case, for example, hydrogen produced by a hydrogen generator that uses water electrolysis, a device that electrolyzes an aqueous sodium chloride solution, a device that steam reformes petroleum, or a device that produces ammonia can be used as a by-product. Hydrogen produced by a generating device or hydrogen contained in coke oven gas discharged from a coke oven can be used.

100: Organic substance production system 10: Gasification furnace 1: Organic substance production apparatus 2: Culture tank 3: Reforming furnace 4: Reduction section 4a: Reduction reactor 4b1: Reduction reactor 4b2: Reduction reactor 4c: Reduction Reactor 41: Tube 42: Housing 421: Space 421w: Liquid 422: Space 422w: Liquid 43: Internal space 44: Gas switching section 45: Cathode 46: Anode 47: Bipolar membrane 471: Cation exchange layer 472: Anion exchange layer 48: Power source 49: Irradiation device 4R: Catalyst, reducing agent 5: Pretreatment section 6: Purification device 7: Removal section 8: Carbon dioxide removal device GL1: Gas line GL11: Gas line GL2: Gas line GL31: Gas line GL32: Gas line GL4: Gas line GL41: Gas line GL42: Gas line LL: Liquid line J: Gas confluence section

Claims (10)

A production system for organic substances,
a gas generation unit that generates a raw material gas containing carbon monoxide and carbon dioxide;
an organic substance generation unit that supplies the raw material gas and generates an organic substance from the raw material gas;
a reducing section provided between the gas generating section and the organic substance generating section, the reducing section having a reducing body that reduces the carbon dioxide to generate carbon monoxide using the carbon dioxide and hydrogen; Prepare,
When the temperature at which the organic substance is produced in the organic substance generation section is X [°C], and the temperature at which the carbon monoxide is produced at the reduction section is Y [°C], the relationship Y≦15X. A manufacturing system for organic substances that satisfies the following. The organic substance production system according to claim 1,
An organic material manufacturing system that satisfies the relationship 3X≦Y. The organic substance production system according to claim 1,
The reduction unit further includes an irradiation device that irradiates the reductant with microwaves. The organic substance production system according to claim 1,
further comprising a separation unit that separates the carbon dioxide supplied to the reduction unit from the source gas;
The carbon dioxide separated in the separation section is supplied to the reduction section, and the carbon monoxide generated in the reduction section is combined with the raw material gas and supplied to the organic substance generation section. A manufacturing system for organic substances. The organic substance production system according to claim 1,
The organic substance production system is an organic substance production system, wherein the organic substance generation unit is a culture tank that generates the organic substance-containing liquid from the raw material gas by the action of gas-assimilating bacteria. The organic substance production system according to claim 1,
The reduction unit includes at least one reactor capable of separating at least a part of the oxygen element released from the carbon dioxide by the reduction reaction of the carbon dioxide by the reductant in the reduction reaction system. manufacturing system. The organic substance production system according to claim 6,
The reductant is brought into an oxidized state when the carbon dioxide is reduced and converted into the carbon monoxide, and the reductant in the oxidized state is reduced by contact with the hydrogen. The organic substance production system according to claim 7,
The reduction section includes a plurality of the reactors,
A system for producing an organic substance, wherein the carbon dioxide and the hydrogen are selectively supplied to each of the reactors. An organic substance production device used in connection with a gas generation unit that generates a raw material gas containing carbon monoxide and carbon dioxide,
an organic substance generation unit that supplies the raw material gas and generates an organic substance from the raw material gas;
a reducing section provided between the gas generating section and the organic substance generating section, the reducing section having a reducing body that reduces the carbon dioxide to generate carbon monoxide using the carbon dioxide and hydrogen; Prepare,
When the temperature at which the organic substance is produced in the organic substance generation section is X [°C], and the temperature at which the carbon monoxide is produced at the reduction section is Y [°C], the relationship Y≦15X. Organic substance manufacturing equipment that satisfies the following. A method for producing an organic substance, the method comprising:
an organic substance generation step of supplying a raw material gas containing carbon monoxide and carbon dioxide and generating an organic substance from the raw material gas;
Prior to the organic substance generation step, a reduction step of reducing the carbon dioxide with a reductant to generate carbon monoxide using the carbon dioxide and hydrogen,
When the temperature at which the organic substance is generated in the organic substance generation step is X [°C], and the temperature at which the carbon monoxide is generated in the reduction step is Y [°C], the relationship Y≦15X. A method for producing organic substances that satisfies the following.