Liquid fuel synthesis system and liquid fuel synthesis method

Abstract

To provide an electrochemical cell and a current collector layer material capable of suppressing a decrease in electrical conductivity of a current collector layer.SOLUTION: A liquid fuel synthesis system 100 comprises a liquid fuel synthesis unit 110 and a sweeping gas supply unit 120. The liquid fuel synthesis unit 110 allows a water vapor, which is one of products in a conversion reaction from a raw material gas containing at least hydrogen and carbon dioxide to a liquid fuel, to permeate. The sweeping gas supply unit 120 supplies a sweeping gas for sweeping the water vapor that has permeated the separation membrane 112 to the liquid fuel synthesis unit 110. The sweeping gas contains hydrogen or carbon dioxide as a main component.SELECTED DRAWING: Figure 1

Description

[Technical field]

[0001] The present invention relates to a liquid fuel synthesis system and a liquid fuel synthesis method. [Background technology]

[0002] In recent years, liquid fuel synthesis systems have been developed that can improve the efficiency of the conversion reaction from a feed gas containing hydrogen and carbon dioxide to liquid fuels such as methanol and ethanol (specifically, fuels that are in a liquid state at room temperature and pressure) by separating the by-product water vapor.

[0003] Patent Document 1 discloses a liquid fuel synthesis system including a membrane reactor, a raw material gas supply unit, and a sweep gas supply unit. The membrane reactor includes a catalyst that promotes a conversion reaction from a raw material gas containing hydrogen and carbon dioxide to methanol, and a separation membrane that allows water vapor, a by-product of the conversion reaction, to permeate. The raw material gas supply unit supplies the raw material gas to the non-permeation side of the separation membrane. The sweep gas supply unit supplies the sweep gas to the permeation side of the separation membrane. The water vapor that has permeated the separation membrane is discharged from the membrane reactor together with the sweep gas. [Prior art documents] [Patent documents]

[0004] [Patent Document 1] JP 2018-8940 A Summary of the Invention [Problem to be solved by the invention]

[0005] Here, since the molecular diameters of water and hydrogen are similar, some of the hydrogen contained in the raw material gas tends to pass through the separation membrane and become mixed into the sweep gas. However, if the hydrogen mixed into the sweep gas could be reused, the utilization rate of the raw material gas could be improved.

[0006] However, in the liquid fuel synthesis system described in Patent Document 1, at least one of nitrogen and air is used as the sweep gas, and therefore in order to reuse the hydrogen mixed in the sweep gas, it is necessary to individually separate the hydrogen, which is cumbersome.

[0007] The present invention has been made in consideration of the above circumstances, and an object of the present invention is to provide a liquid fuel synthesis system and a liquid fuel synthesis method that can improve the utilization rate of a raw material gas. [Means for solving the problem]

[0008] A liquid fuel synthesis system according to a first aspect of the present invention includes a liquid fuel synthesis unit and a sweep gas supply unit. The liquid fuel synthesis unit allows a product of a conversion reaction from a feed gas containing at least hydrogen and carbon dioxide to a liquid fuel to permeate. The sweep gas supply unit supplies a sweep gas to the liquid fuel synthesis unit for sweeping the product that has permeated the separation membrane. The sweep gas contains hydrogen or carbon dioxide as a main component.

[0009] A liquid fuel synthesis system according to a second aspect of the present invention is related to the first aspect, wherein the sweep gas contains hydrogen as a main component.

[0010] A liquid fuel synthesis system according to a third aspect of the present invention is related to the second aspect, in which the sweep gas contains carbon dioxide as a minor component.

[0011] A liquid fuel synthesis system according to a fourth aspect of the present invention is related to any one of the first to third aspects, and further includes a moisture removal section that removes moisture from exhaust gas that is discharged from the liquid fuel synthesis section and contains the sweep gas and products.

[0012] A liquid fuel synthesis system according to a fifth aspect of the present invention relates to the above-mentioned fourth aspect, and the moisture removing unit includes a heat exchanger that uses a material gas containing at least hydrogen and carbon dioxide as a refrigerant.

[0013] A liquid fuel synthesis system according to a sixth aspect of the present invention relates to the fifth aspect, and includes a pressure booster section that boosts the mixed gas of the material gas and the sweep gas that has passed through the moisture remover section and supplies the boosted mixed gas to the liquid fuel synthesis section.

[0014] A liquid fuel synthesis method according to a seventh aspect of the present invention includes the steps of supplying a feed gas containing at least hydrogen and carbon dioxide to a non-permeation side of a separation membrane to proceed with a conversion reaction from the feed gas to a liquid fuel, while supplying a sweep gas to the permeation side of the separation membrane to sweep up products produced by the conversion reaction and permeating the separation membrane. The sweep gas contains hydrogen or carbon dioxide as a main component.

[0015] The liquid fuel synthesis method according to an eighth aspect of the present invention is the method according to the seventh aspect, further comprising the step of removing moisture from the sweep gas and the exhaust gas containing the products.

[0016] A liquid fuel synthesis method according to a ninth aspect of the present invention relates to the above-mentioned eighth aspect, wherein in the step of removing moisture from the exhaust gas, a material gas containing at least hydrogen and carbon dioxide is used as a coolant.

[0017] A liquid fuel synthesis method according to a tenth aspect of the present invention relates to the above-mentioned ninth aspect, and further comprises a step of increasing pressure of the mixed gas of the material gas and the sweep gas after being used as a coolant. Effect of the Invention

[0018] According to the present invention, it is possible to provide a liquid fuel synthesis system and a liquid fuel synthesis method capable of improving the utilization rate of a raw material gas. [Brief description of the drawings]

[0019] [Figure 1] FIG. 1 is a schematic diagram showing a configuration of a liquid fuel synthesis system according to an embodiment; [Diagram 2] FIG. 13 is a schematic diagram showing a configuration of a liquid fuel synthesis system according to a second modified example. [Diagram 3] FIG. 13 is a schematic diagram showing a configuration of a liquid fuel synthesis system according to a fifth modified example. [Figure 4] FIG. 13 is a schematic diagram showing a configuration of a liquid fuel synthesis system according to a fifth modified example. [Diagram 5] FIG. 13 is a schematic diagram showing a configuration of a liquid fuel synthesis system according to a fifth modified example. [Figure 6] FIG. 13 is a schematic diagram showing a configuration of a liquid fuel synthesis system according to a fifth modified example. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0020] Next, an embodiment of the present invention will be described with reference to the drawings. However, the drawings are schematic and the ratio of dimensions may differ from the actual ones.

[0021] (Liquid Fuel Synthesis System) 1 is a schematic diagram showing the configuration of a liquid fuel synthesis system 100. The liquid fuel synthesis system 100 includes a liquid fuel synthesis section 110, a sweep gas supply section 120, a raw material gas supply section 130, and a first drain trap 140.

[0022] The liquid fuel synthesis unit 110 is a so-called membrane reactor for converting the raw material gas into liquid fuel. The shape of the liquid fuel synthesis unit 110 is not particularly limited, and may be, for example, a monolith shape, a flat plate shape, a tubular shape, a cylindrical shape, a columnar shape, a polygonal column shape, or the like. The monolith shape means a shape having a plurality of cells penetrating in the longitudinal direction, and is a concept that includes a honeycomb shape.

[0023] The raw material gas is supplied from the raw material gas supply unit 130 to the liquid fuel synthesis unit 110. The raw material gas contains at least hydrogen and carbon dioxide. The raw material gas may contain carbon monoxide. The raw material gas may be a so-called synthetic gas (Syngas). The liquid fuel is a fuel that is in a liquid state at normal temperature and pressure, or a fuel that can be liquefied under normal temperature and pressure. Examples of the fuel that is in a liquid state at normal temperature and pressure include methanol, ethanol, and C n H 2(m-2n)(m is an integer less than 90, and n is an integer less than 30), and mixtures thereof. Examples of fuels that can be liquefied under normal temperature and pressure include propane, butane, and mixtures thereof.

[0024] For example, the reaction formula (1) for synthesizing methanol by catalytic hydrogenation of a raw material gas containing carbon dioxide and hydrogen in the presence of a catalyst is as follows.

[0025] CO2+3H2⇔CH3OH+H2O (1)

[0026] The above reaction is an equilibrium reaction, and in order to increase both the conversion rate and the reaction rate, it is preferable to carry out the reaction under high temperature and pressure (for example, 180°C or higher, 2 MPa or higher). The liquid fuel is in a gaseous state when synthesized, and is maintained in this gaseous state at least until it flows out of the liquid fuel synthesis unit 110. It is preferable that the liquid fuel synthesis unit 110 has heat resistance and pressure resistance suitable for the synthesis conditions of the desired liquid fuel.

[0027] The liquid fuel synthesis section 110 according to this embodiment includes a catalyst layer 111, a separation membrane 112, a non-permeation side space 110A, and a permeation side space 110B.

[0028] The catalyst layer 111 is disposed in the non-permeation side space 110 A. In the catalyst layer 111, a conversion reaction from the raw material gas to liquid fuel proceeds.

[0029] The catalyst layer 111 is a porous body composed of a porous material and a catalyst. The average pore diameter of the catalyst layer 111 can be 5 μm or more and 25 μm or less. The average pore diameter of the catalyst layer 111 can be measured by mercury intrusion porosimetry. The porosity of the catalyst layer 111 can be 25% or more and 50% or less. The average particle diameter of the porous material constituting the catalyst layer 111 can be 1 μm or more and 100 μm or less. In this embodiment, the average particle diameter is the arithmetic mean value of the maximum diameters of 30 measurement target particles (randomly selected) measured by cross-sectional microstructure observation using a SEM (Scanning Electron Microscope).

[0030] As the porous material, ceramic materials, metal materials, resin materials, etc. can be used, and ceramic materials are particularly suitable. Examples of aggregates for ceramic materials include alumina (Al2O3), titania (TiO2), mullite (Al2O3·SiO2), cerium oxide, and cordierite (Mg2Al4Si5O 18 ) can be used, and alumina is preferred in consideration of availability, clay stability, and corrosion resistance. As the inorganic binder for the ceramic material, at least one of titania, mullite, sinterable alumina, silica, glass frit, clay minerals, and sinterable cordierite can be used. However, the ceramic material does not have to contain an inorganic binder.

[0031] The catalyst promotes a conversion reaction from the feed gas to a liquid fuel. The catalyst is disposed in the pores of the porous material. The catalyst may be supported on the inner surface of the pores. Alternatively, a support supporting the catalyst may be attached to the inner surface of the pores.

[0032] The catalyst may be any known catalyst suitable for the conversion reaction to the desired liquid fuel. Specifically, metal catalysts (copper, palladium, etc.), oxide catalysts (zinc oxide, zirconia, gallium oxide, etc.), and catalysts made by combining these (copper-zinc oxide, copper-zinc oxide-alumina, copper-zinc oxide-chromium oxide-alumina, copper-cobalt-titania, and catalysts made by modifying these with palladium, etc.) may be used.

[0033] The separation membrane 112 allows the permeation of water vapor, which is one of the products of the conversion reaction from the raw material gas to liquid fuel, thereby making it possible to shift the reaction equilibrium of the above formula (1) to the product side by utilizing the equilibrium shift effect.

[0034] The molecular diameter of water (0.26 nm) is close to the molecular diameter of hydrogen (0.296 nm). Therefore, in this embodiment, it is assumed that not only the water vapor that is the product of the conversion reaction, but also a part of the hydrogen contained in the raw material gas permeates the separation membrane 112.

[0035] The separation membrane 112 has a molecular weight of 100 nmol / (s·Pa·m 2 The water vapor permeability coefficient can be determined by a known method (see Ind. Eng. Chem. Res., 40, 163-175 (2001)).

[0036] The separation membrane 112 preferably has a separation factor of 100 or more. The larger the separation factor, the easier it is for water vapor to permeate and the harder it is for components other than water vapor (such as hydrogen, carbon dioxide, and liquid fuel) to permeate. The separation factor can be determined by a known method (see FIG. 1 in "Separation and Purification Technology 239 (2020) 116533").

[0037] An inorganic membrane can be used as the separation membrane 112. Inorganic membranes are preferable because they have heat resistance, pressure resistance, and water vapor resistance. Examples of inorganic membranes include zeolite membranes, silica membranes, alumina membranes, and composite membranes of these. For example, an LTA-type zeolite membrane in which the molar ratio (Si / Al) of silicon element (Si) to aluminum element (Al) is 1.0 or more and 3.0 or less is preferable because it has excellent water vapor permeability.

[0038] The separation membrane 112 may be supported by a porous substrate.

[0039] The non-permeation side space 110A is a space on the non-permeation side of the separation membrane 112. A raw material gas is supplied to the non-permeation side space 110A from the raw material gas supply unit 130. The raw material gas flows into the non-permeation side space 110A through the inlet a1. The liquid fuel synthesized in the catalyst layer 111 flows out of the non-permeation side space 110A through the outlet a2. The liquid fuel flowing out from the outlet a2 may contain unreacted residual raw material gas. The residual raw material gas mixed in the liquid fuel is separated from the liquid fuel in the first drain trap 140. The separated residual raw material gas is returned to the raw material gas supply unit 130 (specifically, the second boost pump 133b described later). The residual raw material gas contains at least one of hydrogen and carbon dioxide.

[0040] The permeate side space 110B is a space on the permeate side of the separation membrane 112. Water vapor and hydrogen that have permeated through the separation membrane 112 flow into the permeate side space 110B. A sweep gas is supplied from a sweep gas supply unit 120 to the permeate side space 110B. The sweep gas flows into the permeate side space 110B through an inlet b1. Exhaust gas containing the sweep gas and water vapor flows out of the permeate side space 110B through an outlet b2.

[0041] The sweep gas supply unit 120 is disposed upstream of the permeate side space 110B. The sweep gas supply unit 120 includes a reservoir 121, a flow rate adjustment mechanism 122, and a heater 123.

[0042] The storage section 121 stores the sweep gas. The sweep gas contains hydrogen or carbon dioxide as a main component. In this way, the sweep gas contains hydrogen or carbon dioxide as a main component, so that hydrogen that permeates the separation membrane 112 can be reused as part of the raw material gas without being separated from the sweep gas. As a result, the utilization rate of the raw material gas can be easily improved. Incidentally, containing hydrogen or carbon dioxide as a main component means that the sweep gas contains the highest content of hydrogen or carbon dioxide.

[0043] The sweep gas may contain only one of hydrogen and carbon dioxide, or may contain both hydrogen and carbon dioxide. When the sweep gas contains both hydrogen and carbon dioxide, the specific heat of the sweep gas can be made larger than when the sweep gas contains only one of hydrogen and carbon dioxide, and therefore the efficiency of removing heat generated in the synthesis of the liquid fuel can be improved.

[0044] The sweep gas preferably contains hydrogen as a main component, which reduces the difference in hydrogen partial pressure between the non-permeation side space 110A and the permeation side space 110B, thereby suppressing the amount of hydrogen permeating the separation membrane 112. The hydrogen content in the water sweep gas is not particularly limited, but may be, for example, 60 mol% to 100 mol%.

[0045] The sweep gas preferably contains carbon dioxide as a minor component. This can prevent the ratio of the amount of exhaust gas to the amount of moisture in the exhaust gas from becoming excessively small, thereby preventing the dew point (i.e., humidity) of the exhaust gas from becoming low. As a result, the load on the heat exchanger 132a, which will be described later, can be reduced. The fact that carbon dioxide is contained as a minor component means that the content of carbon dioxide is the second highest after hydrogen (i.e., the second highest) among the gases contained in the sweep gas. The content of carbon dioxide in the sweep gas is not particularly limited, but can be, for example, 5 mol% to 40 mol%.

[0046] The flow rate adjustment mechanism 122 adjusts the flow rate of the sweep gas supplied from the storage portion 121. A pump, a blower, or the like can be used as the flow rate adjustment mechanism 122. However, when the sweep gas is stored in the storage portion 121 in a pressurized state, the flow rate adjustment mechanism 122 can be omitted.

[0047] The heating unit 123 heats the sweep gas to a desired temperature. The heating unit 123 is not particularly limited as long as it can heat the sweep gas. The heating unit 123 may be a unit that heats the sweep gas using a regenerative heat exchanger that utilizes heat exchange with the heat exchanger 132a described later.

[0048] The raw material gas supplying section 130 is disposed downstream of the non-permeation side space 110 A. The raw material gas supplying section 130 includes a material gas source 131, a moisture removing section 132, and a pressure increasing section 133.

[0049] The material gas source 131 stores the material gas. The material gas contains at least hydrogen and carbon dioxide. The material gas may contain carbon monoxide. The material gas may be a so-called synthetic gas. The material gas stored in the material gas source 131 is supplied to the moisture remover 132.

[0050] The moisture removing section 132 removes moisture from the exhaust gas that is discharged from the liquid fuel synthesis section and contains the sweep gas and water vapor. This separates the sweep gas from the exhaust gas. The moisture removing section 132 includes a heat exchanger 132a and a second drain trap 132b.

[0051] The heat exchanger 132a has a first flow path c1 through which the material gas supplied from the material gas source 131 flows, and a second flow path c2 through which the exhaust gas discharged from the liquid fuel synthesis unit 110 flows. The heat exchanger 132a condenses water vapor in the exhaust gas into water by using the material gas as a refrigerant. This allows the material gas to be heated and the exhaust gas to be cooled simultaneously, thereby improving the thermal efficiency of the liquid fuel synthesis system 100.

[0052] The second drain trap 132b is disposed downstream of the heat exchanger 132a. The second drain trap 132b separates water condensed in the heat exchanger 132a from the sweep gas. The sweep gas separated by the second drain trap 132b is mixed with the material gas that has passed through the heat exchanger 132a downstream of the second drain trap 132b. This produces a mixed gas in which the sweep gas and the material gas are mixed.

[0053] The mixed gas is supplied to the pressure boosting section 133. The pressure boosting section 133 is disposed downstream of the second drain trap 132b and upstream of the liquid fuel synthesis section 110. The pressure boosting section 133 boosts the material gas and sweep gas that have passed through the moisture removal section 132, and supplies the boosted gas to the liquid fuel synthesis section 110. The pressure boosting section 133 includes a first boost pump 133a and a second boost pump 133b.

[0054] The first boost pump 133a boosts the mixed gas to a predetermined first pressure. The mixed gas boosted by the first boost pump 133a is mixed with the remaining raw material gas separated from the liquid fuel in the first drain trap 140. As a result, a raw material gas in which the mixed gas and the remaining raw material gas are mixed is generated.

[0055] The second boost pump 133b boosts the raw material gas to a predetermined second pressure. The second pressure is a pressure suitable for a conversion reaction from the raw material gas to liquid fuel, and is higher than the first pressure. The raw material gas pressurized by the second boost pump 133b is supplied to the non-permeation side space 110A of the liquid fuel synthesis section 110.

[0056] (Liquid fuel synthesis method) Next, a liquid fuel synthesis method using the liquid fuel synthesis system 100 will be described.

[0057] The liquid fuel synthesis method includes a step of supplying a raw material gas to the non-permeate side of the separation membrane 112, and supplying a sweep gas containing hydrogen or carbon dioxide as a main component to the permeate side of the separation membrane 112. A conversion reaction from the raw material gas to liquid fuel proceeds on the non-permeate side of the separation membrane 112. On the permeate side of the separation membrane 112, water vapor permeating through the separation membrane 112 is taken up in the sweep gas.

[0058] The liquid fuel synthesis method further includes a step of removing moisture from the sweep gas and the exhaust gas containing water vapor. In this embodiment, the material gas is used as a coolant in this step. This allows the material gas to be heated and the exhaust gas to be cooled simultaneously, thereby improving the thermal efficiency of the liquid fuel synthesis system 100.

[0059] The liquid fuel synthesis method further includes a step of increasing the pressure of a mixed gas of the feed gas and the sweep gas after the coolant is used. In this step, it is preferable to generate the feed gas by mixing the remaining feed gas separated from the liquid fuel with the mixed gas. This can improve the utilization efficiency of the feed gas.

[0060] (Modification of the embodiment) Although one embodiment of the present invention has been described above, the present invention is not limited to the above embodiment, and various modifications are possible without departing from the gist of the invention.

[0061] (Variation 1) In the above embodiment, the catalyst layer 111 is disposed on the separation membrane 112, but this is not limited thereto. For example, the non-permeation side space 110A may be filled with a particulate catalyst. The particle size (diameter) of the particulate catalyst is not particularly limited, but may be, for example, 0.5 mm or more and 10 mm or less.

[0062] (Variation 2) In the above embodiment, the liquid fuel synthesis system 100 includes the liquid fuel synthesis unit 110 which is a membrane reactor, but is not limited to this.

[0063] For example, the liquid fuel synthesis system 100 may include a liquid fuel synthesis section 160 having a catalyst section 161 and a separation section 162 as shown in FIG.

[0064] The raw material gas is supplied to the catalyst section 161 from the raw material gas supply section 130. The catalyst described in the above embodiment is disposed in the catalyst section 161. The catalyst section 161 converts the raw material gas into liquid fuel.

[0065] The separation section 162 includes a separation membrane 112, a non-permeation side space 160A, and a permeation side space 160B.

[0066] Liquid fuel, water vapor, and residual fuel gas flow into the non-permeation side space 160A. Water vapor permeates the separation membrane 112. Also, a portion of the hydrogen contained in the residual fuel gas permeates the separation membrane 112. The liquid fuel flows out of the non-permeation side space 160A without permeating the separation membrane 112.

[0067] Water vapor that has permeated through the separation membrane 112 flows into the permeate side space 160B. A sweep gas supplied from the sweep gas supply unit 120 flows into the permeate side space 160B. Exhaust gas containing the sweep gas, water vapor, and hydrogen flows out of the permeate side space 160B.

[0068] In this modification, the sweep gas contains hydrogen or carbon dioxide as a main component, so that hydrogen permeating through the separation membrane 112 can be reused as part of the source gas without being separated from the sweep gas. As a result, the utilization rate of the source gas can be easily improved.

[0069] (Variation 3) 1 and 2, the source gas and the sweep gas flow in opposite directions (i.e., opposite directions) in the side view of the separation membrane 112, but they may flow in the same direction (i.e., parallel directions).

[0070] (Variation 4) In the above embodiment, the material gas supplied from the material gas source 131 is used as the coolant of the heat exchanger 132a, but this is not limited thereto. Water or the like may be used as the coolant of the heat exchanger 132a. In this case, the material gas may be directly mixed with the sweep gas flowing out from the second drain trap 132b without passing through the heat exchanger 132a.

[0071] (Variation 5) In the above embodiment, the remaining raw material gas separated from the liquid fuel in the first drain trap 140 is entirely returned to the raw material gas supply unit 130, but this is not limiting.

[0072] 3, a part of the remaining raw material gas may be mixed with the sweep gas flowing out from the storage section 121 and supplied to the flow rate adjustment mechanism 122. In this case, a part of the remaining raw material gas is used as a part of the sweep gas. The mixed amount of the remaining raw material gas can be adjusted by the flow rate adjustment mechanism 124.

[0073] 4, the entire remaining raw material gas may be mixed with the sweep gas flowing out from the storage section 121 and supplied to the flow rate adjustment mechanism 122. The remaining raw material gas flows toward the flow rate adjustment mechanism 122 because the flow toward the storage section 121 is restricted by the check valve 125. In this case, the entire remaining raw material gas is used as part of the sweep gas.

[0074] 5, the sweep gas supply unit 120 may not have the storage unit 121, and a part of the remaining raw material gas may be supplied to the flow rate adjustment mechanism 122. In this case, the part of the remaining raw material gas is used as the sweep gas as it is. The supply amount of the sweep gas (remaining raw material gas) can be adjusted by the flow rate adjustment mechanism 122.

[0075] 6, the sweep gas supply unit 120 may not have the storage unit 121, and the remaining raw material gas may be entirely supplied to the flow rate adjustment mechanism 122. In this case, the remaining raw material gas may be entirely used as the sweep gas.

[0076] (Variation 6) In the above embodiment, the separation membrane 112 is designed to allow water vapor, which is one of the products of the conversion reaction from the raw material gas to liquid fuel, to pass therethrough, but this is not limited thereto. The separation membrane 112 may also allow the liquid fuel itself, which is produced by the conversion reaction from the raw material gas to liquid fuel, to pass therethrough. Even in this case, the reaction equilibrium of the above formula (1) can be shifted to the product side.

[0077] In addition, when the separation membrane 112 allows liquid fuel to permeate, even when liquid fuel is produced by a reaction that does not produce water vapor (for example, 2H2+CO⇔CH3OH), the reaction equilibrium can be shifted to the product side. [Explanation of symbols]

[0078] 1. Membrane Reactor 100 Liquid Fuel Synthesis System 110 Liquid Fuel Synthesis Department 111 Catalyst layer 112 Separation membrane 110A Non-transparent side space 110B Transmission side space 120 Sweep gas supply unit 130 Raw material gas supply section

Claims

1. a liquid fuel synthesis section including a non-permeation side space in which a conversion reaction from a feed gas containing at least hydrogen and carbon dioxide to a liquid fuel proceeds, a separation membrane that allows a product of the conversion reaction to permeate, and a permeation side space into which the product that has permeated the separation membrane flows; a sweep gas supply unit that supplies a sweep gas to the permeate side space to sweep the product that has permeated the separation membrane; Equipped with the sweep gas contains hydrogen or carbon dioxide as a main component; At least a portion of the remaining raw material gas discharged from the non-permeation side space is utilized as at least a portion of the sweep gas. Liquid fuel synthesis system.

2. A portion of the remaining raw material gas is utilized as a portion of the raw material gas. The liquid fuel synthesis system of claim 1 .

3. The sweep gas is utilized as part of the source gas. The liquid fuel synthesis system of claim 1 .

4. a step of supplying a feed gas containing at least hydrogen and carbon dioxide to a non-permeation side space of a separation membrane to cause a conversion reaction from the feed gas to a liquid fuel, while supplying a sweep gas to a permeation side space of the separation membrane to sweep products produced by the conversion reaction and permeating the separation membrane, the sweep gas contains hydrogen or carbon dioxide as a main component; At least a portion of the remaining raw material gas discharged from the non-permeation side space is utilized as at least a portion of the sweep gas. Liquid fuel synthesis method.

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