Reactor and liquid fuel synthesis method

Abstract

A reactor 1 is provided with a separation membrane (30), a first flow path (11), and a second flow path (12). The first flow path (11) is provided on a non-permeable side of the separation membrane (30), and the second flow path (12) is provided on a permeable side of the separation membrane (30). The material gas flows through the first flow path (11), and a sweep gas flows through the second flow path (12). In a lateral view of the separation membrane (30), the direction in which the sweep gas flows through the second flow path (12) is opposite to the direction in which the material gas flows through the first flow path (11).

Description

[Technical field]

[0001] The present invention relates to a reactor and a method for synthesizing liquid fuels. [Background technology]

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

[0003] For example, Patent Document 1 discloses a reactor including a separation membrane, a first flow path provided on the non-permeation side of the separation membrane, and a second flow path provided on the permeation side of the separation membrane. A raw material gas is supplied to the first flow path. A sweep gas for sweeping water vapor that has permeated the separation membrane is supplied to the second flow path. The sweep gas flowing through the second flow path can absorb reaction heat while taking in water vapor, and therefore the conversion efficiency can be improved by an equilibrium shift effect. [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, in the reactor described in Patent Document 1, the direction of the sweep gas flowing through the second flow path is the same as the direction of the raw material gas flowing through the first flow path, so the amount of water vapor contained in the sweep gas increases in the downstream area of ​​the second flow path.

[0006] Therefore, the water vapor cannot be smoothly transferred from the downstream area of ​​the first flow passage to the downstream area of ​​the second flow passage, and the water vapor is likely to be mixed into the liquid fuel.

[0007] The present invention has been made in consideration of the above-mentioned circumstances, and has an object to provide a reactor and a reactor device capable of suppressing water vapor from being mixed into liquid fuel. [Means for solving the problem]

[0008] The reactor according to the present invention includes a separation membrane, a first flow path, a second flow path, and a catalyst. The separation membrane allows the product of a conversion reaction from a raw material gas containing at least hydrogen and carbon dioxide to liquid fuel to permeate. The first flow path is provided on the non-permeation side of the separation membrane. A raw material gas flows through the first flow path. The second flow path is provided on the permeation side of the separation membrane. A sweep gas for sweeping water vapor that has permeated the separation membrane flows through the second flow path. The catalyst is disposed in the first flow path and advances the conversion reaction from the raw material gas to liquid fuel. In a side view of the separation membrane, the direction of the sweep gas flowing through the second flow path is opposite to the direction of the raw material gas flowing through the first flow path. Effect of the Invention

[0009] According to the present invention, it is possible to provide a reactor and a liquid fuel synthesis method capable of suppressing the mixing of water vapor into liquid fuel. [Brief description of the drawings]

[0010] [Figure 1] FIG. 1 is a perspective view of a reactor 1 according to an embodiment. [Diagram 2] Cross section AA of Figure 1 [Diagram 3] Cross section B-B of Figure 1 [Figure 4] Cross section of Figure 2 [Diagram 5] FIG. 1 is a perspective view of a reactor 1a according to an embodiment. [Figure 6] Cross-sectional view of reactor 1a [Figure 7] Schematic diagram of a reactor device according to an embodiment. [Figure 8] Schematic diagram of a reactor device according to an embodiment. [Figure 9] FIG. 1 is a schematic diagram showing a configuration of a reactor according to a first modified example. [Figure 10]FIG. 1 is a schematic diagram showing a configuration of a reactor according to a first modified example. [Figure 11] FIG. 1 is a cross-sectional view of a first housing according to an embodiment. [Figure 12] FIG. 1 is a cross-sectional view of a first housing according to an embodiment. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0011] 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.

[0012] (Reactor 1) Fig. 1 is a perspective view of the reactor 1. Fig. 2 is a cross-sectional view taken along line AA in Fig. 1. Fig. 3 is a cross-sectional view taken along line BB in Fig. 1. Fig. 4 is a cross-sectional view taken along line CC in Fig. 2.

[0013] The reactor 1 is a so-called membrane reactor for converting a raw material gas into a liquid fuel. 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 pressure at room temperature include propane, butane, and mixtures thereof.

[0014] 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.

[0015] CO 2 +3H 2 ⇔ CH 3 OH+H 2 O (1) The above reaction is an equilibrium reaction, and is preferably carried out under high temperature and pressure (e.g., 180°C or higher, 2 MPa or higher) in order to increase both the conversion efficiency and the reaction rate. The liquid fuel is in a gaseous state when synthesized, and is maintained in this state at least until it flows out of the reactor 1. The reactor 1 preferably has heat resistance and pressure resistance suitable for the synthesis conditions of the desired liquid fuel.

[0016] As shown in FIG. 1, the reactor 1 is formed in a monolithic shape. The term "monolith" refers to a shape having a plurality of holes penetrating in the longitudinal direction, and is a concept that includes honeycomb. The reactor 1 has a first end face S1, a second end face S2, and a side face S3. The first end face S1 is provided on the opposite side of the second end face S2. The side face S3 is continuous with the outer edges of the first end face S1 and the second end face S2. In this embodiment, the reactor 1 is formed in a cylindrical shape, but the outer shape of the reactor 1 is not particularly limited.

[0017] As shown in FIGS. 1 to 4, the reactor 1 includes a porous support 10, a catalyst 20, a separation membrane 30, a first seal portion 40, and a second seal portion 50. The first seal portion 40 and the second seal portion 50 are arranged in a porous support 10.

[0018] The porous support 10 is a columnar body extending in the longitudinal direction of the reactor 1. The porous support 10 is made of a porous material.

[0019] As the porous material, a ceramic material, a metal material, a resin material, etc. can be used, and a ceramic material is particularly preferable. As the aggregate of the ceramic material, for example, alumina (Al 2 O 3 ), titania (TiO 2 ), Mullite (Al 2 O 3 SiO 2 ), cerberine and cordierite (Mg 2 Al 4 S 5 O 18) can be used. As the inorganic binder for the ceramic material, for example, at least one of titania, mullite, sinterable alumina, silica, glass frit, clay mineral, and sinterable cordierite can be used. However, the ceramic material does not have to contain an inorganic binder.

[0020] As shown in FIGS. 2 and 3, the porous support 10 has a large number of first flow paths 11 and a plurality of second flow paths 12.

[0021] As shown in FIG. 4, each of the first flow paths 11 is formed along the longitudinal direction of the reactor 1. Each of the first flow paths 11 is a through hole. Each of the first flow paths 11 opens to a first end face S1 and a second end face S2 of the reactor 1. Each of the first flow paths 11 has an inlet e1 formed in the first end face S1 and an outlet e2 formed in the second end face S2. Each of the first flow paths 11 is provided on the non-permeation side of the separation membrane 30. A raw material gas is passed through each of the first flow paths 11. A catalyst 20 is disposed in each of the first flow paths 11. The number, position, shape, and the like of the first flow paths 11 can be changed as appropriate.

[0022] Each second flow path 12 is provided on the permeation side of the separation membrane 30. A sweep gas for sweeping water vapor that has permeated the separation membrane 30 flows through each second flow path 12. As the sweep gas, an inert gas (e.g., nitrogen) or air can be used. The number, position, shape, etc. of the second flow paths 12 can be changed as appropriate.

[0023] Here, each of the second flow paths 12 is composed of a plurality of cells 13, an inlet slit 14, and an outlet slit 15, as shown in FIGS.

[0024] The multiple cells 13 are arranged in a row along the short side direction (direction perpendicular to the longitudinal direction) of the reactor 1. As shown in Fig. 4, each cell 13 is formed along the longitudinal direction of the reactor 1. Both ends of each cell 13 are plugged by first and second plugging portions 17, 18. The first and second plugging portions 17, 18 can be made of the porous material described above.

[0025] The inflow slit 14 is formed at one end of the reactor 1 in the longitudinal direction, as shown in FIG. 1. The one end of the reactor 1 is a portion from one end of the liquid fuel outlet side to 2 / 5 when the reactor 1 is divided into 5 equal parts in the longitudinal direction. The inflow slit 14 is formed along the short side of the reactor 1. The inflow slit 14 penetrates a plurality of cells 13, as shown in FIG. 2. Both ends of the inflow slit 14 open to the side surface S3. The inflow slit 14 has a pair of inlets d1 formed in the side surface S3. The pair of inlets d1 is one end of the second flow passage 12 in the longitudinal direction.

[0026] The outflow slit 15 is formed at the other end of the reactor 1 in the longitudinal direction, as shown in FIG. 1. The other end of the reactor 1 is a portion from the other end of the inlet side of the raw material gas to 2 / 5 of the total length when the reactor 1 is divided into 5 equal parts in the longitudinal direction. The outflow slit 15 is formed along the short side of the reactor 1. The outflow slit 15 penetrates the multiple cells 13, as shown in FIG. 3. Both ends of the outflow slit 15 open to the side surface S3. The outflow slit 15 has a pair of exhaust ports d2 formed in the side surface S3. The pair of exhaust ports d2 are the other ends of the second flow path 12 in the longitudinal direction.

[0027] The catalyst 20 is disposed in each of the first flow paths 11. The catalyst 20 is preferably filled in each of the first flow paths 11, but may be disposed in the form of a layer on the surface of the separation membrane 30. The catalyst 20 promotes the conversion reaction from the raw material gas to liquid fuel, as shown in the above formula (1).

[0028] Any known catalyst suitable for the desired conversion reaction into liquid fuel can be used as the catalyst 20. Examples of the catalyst 20 include 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 obtained by modifying these with palladium, etc.).

[0029] The separation membrane 30 is supported by the porous support 10. The separation membrane 30 surrounds the first flow path 11. The separation membrane 30 is disposed between the first flow path 11 and the second flow path 12.

[0030] The separation membrane 30 allows the permeation of water vapor, which is one of the products of the conversion reaction from the feed gas to liquid fuel, thereby making it possible to utilize the equilibrium shift effect to shift the reaction equilibrium of the above formula (1) to the product side.

[0031] The separation membrane 30 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)).

[0032] The separation membrane 30 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").

[0033] An inorganic membrane can be used as the separation membrane 30. 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. In particular, 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.

[0034] The first sealing portion 40 covers one end surface of the porous support 10, as shown in Fig. 1. The first sealing portion 40 suppresses the intrusion of the raw material gas into the porous support 10. The first sealing portion 40 is formed so as not to block the inlet e1 of the first flow path 11, as shown in Fig. 4. The first sealing portion 40 covers the first plugging portion 17. The first sealing portion 40 can be made of glass, metal, rubber, resin, etc.

[0035] The second seal portion 50 covers the other end face of the porous support body 10, as shown in Fig. 1. The second seal portion 50 prevents liquid fuel from entering the porous support body 10. The second seal portion 50 is formed so as not to block the outlet e2 of the first flow path 11, as shown in Fig. 4. The second seal portion 50 covers the second plugging portion 18. The second seal portion 50 can be made of glass, metal, rubber, resin, etc.

[0036] (Method of synthesizing liquid fuel using reactor 1) A method for synthesizing a liquid fuel using the reactor 1 will be described with reference to FIG.

[0037] The liquid fuel synthesis method using the reactor 1 includes a step of flowing a raw material gas through a first flow path 11 provided on the non-permeation side of the separation membrane 30, while flowing a sweep gas through a second flow path 12 provided on the permeation side of the separation membrane 30.

[0038] The raw material gas flows into the first flow passage 11 from the inlet e1 of the first flow passage 11. In the first flow passage 11, water vapor is generated together with the liquid fuel according to the above formula (1). The synthesized liquid fuel flows out from the outlet e2 of the first flow passage 11. The synthesized liquid fuel may be mixed with residual raw material gas that was not used in the conversion reaction. The product water vapor sequentially permeates the separation membrane 30 and the porous support 10, and moves to the second flow passage 12.

[0039] The sweep gas flows in through the inlet d1 of the inlet slit 14, and then flows from the inlet slit 14 into the cell 13. Next, the sweep gas that flows into the cell 13 from the inlet slit 14 takes in the water vapor that has permeated the separation membrane 30, and flows inside the cell 13 toward the outlet slit 15 while absorbing the reaction heat generated by the conversion reaction. The sweep gas that reaches the outlet slit 15 is discharged from the outlet d2 of the outlet slit 15.

[0040] 4, in a side view of the separation membrane 30, the direction of the sweep gas flowing through the second flow path 12 is opposite to the direction of the raw material gas flowing through the first flow path 11. In other words, the sweep gas flowing through the second flow path 12 flows in a direction opposite to the raw material gas flowing through the first flow path 11.

[0041] Therefore, since the amount of water vapor contained in the sweep gas flowing through the upstream region of the second flow path 12 (specifically, the flow region on the inlet d1 side of the longitudinal center of the cell 13) is small, water vapor can be smoothly moved from the downstream region of the first flow path 11 (specifically, the flow region on the outlet e2 side of the longitudinal center of the first flow path 11) to the upstream region of the second flow path.

[0042] As a result, water vapor can be efficiently removed from the liquid fuel flowing out from the first flow passage 11, so that the liquid fuel can be prevented from being mixed with water vapor, thereby making it possible to obtain high-quality liquid fuel.

[0043] The flow direction of the source gas in the first flow path 11 refers to the direction from upstream to downstream when the side of the first flow path 11 closer to the source gas source is defined as the upstream side and the side farther from the source gas source is defined as the downstream side. The flow direction of the sweep gas in the second flow path 12 refers to the direction from upstream to downstream when the side of the second flow path 12 closer to the sweep gas source is defined as the upstream side and the side farther from the sweep gas source is defined as the downstream side.

[0044] (Reactor device using Reactor 1) The above-mentioned reactor 1 can be used alone, but can also be connected to a reactor 1a described later to form reactor apparatuses 100 and 200. The reactor 1a, reactor apparatus 100, and reactor apparatus 200 will be described below in order.

[0045] [Reactor 1a] The configuration of the reactor 1a is the same as that of the reactor 1a described above. The reactor 1a differs from the reactor 1 in that the sweep gas and the source gas flow in the same direction. This difference will be mainly described below.

[0046] Fig. 5 is a perspective view of the reactor 1a, and Fig. 6 is a cross-sectional view taken along the longitudinal direction of the reactor 1a.

[0047] As shown in FIG. 6, the porous support 10 has a third flow path 11a and a fourth flow path 12a.

[0048] As shown in FIG. 6, the third flow path 11a is formed along the longitudinal direction of the reactor 1a. The third flow path 11a is a through hole. The third flow path 11a opens to each of the first end face S1 and the second end face S2 of the reactor 1a. The third flow path 11a has an inlet e3 formed in the first end face S1 and an outlet e4 formed in the second end face S2. The third flow path 11a is provided on the non-permeation side of the separation membrane 30a. A raw material gas is passed through the third flow path 11a. A catalyst 20 is disposed in the third flow path 11a.

[0049] The fourth flow passage 12a is provided on the permeation side of the separation membrane 30a. A sweep gas for sweeping the water vapor that has permeated the separation membrane 30a flows through the fourth flow passage 12a.

[0050] Here, as shown in FIG. 6, the fourth flow path 12a is composed of a cell 13, an outlet slit 14a, and an inlet slit 15a.

[0051] As shown in FIG. 1, the outflow slit 14a is formed at one end of the reactor 1a in the longitudinal direction. The one end of the reactor 1a is a portion from one end of the liquid fuel outflow side to 2 / 5 when the reactor 1a is divided into 5 equal parts in the longitudinal direction. The outflow slit 14a is formed along the short direction of the reactor 1a. The outflow slit 14a penetrates the cell 13. Both ends of the outflow slit 14a open to the side surface S3. The outflow slit 14a has a pair of exhaust ports d4 formed in the side surface S3. The pair of exhaust ports d4 is one end of the fourth flow path 12a in the longitudinal direction.

[0052] As shown in FIG. 1, the inlet slit 15a is formed at the other end of the reactor 1a in the longitudinal direction. The other end of the reactor 1a is a portion from the other end of the inlet side of the raw material gas to 2 / 5 of the total length when the reactor 1a is divided into 5 equal parts in the longitudinal direction. The inlet slit 15a is formed along the short side of the reactor 1a. The inlet slit 15a penetrates the cell 13. Both ends of the inlet slit 15a open to the side surface S3. The inlet slit 15a has a pair of inlets d3 formed in the side surface S3. The pair of inlets d3 are the other ends of the fourth flow path 12a in the longitudinal direction.

[0053] As described above, in reactor 1a, the positions of the inlet slit and the outlet slit are reversed from those in reactor 1.

[0054] [Method of synthesizing liquid fuel using reactor 1a] A method for synthesizing a liquid fuel using the reactor 1a will be described with reference to FIG.

[0055] The liquid fuel synthesis method using the reactor 1a includes a step of flowing a raw material gas through a third flow path 11a provided on the non-permeation side of a separation membrane 30a (an example of a second separation membrane) while flowing a sweep gas through a fourth flow path 12a provided on the permeation side of the separation membrane 30a.

[0056] The raw material gas flows into the third flow passage 11a from the inlet e3 of the third flow passage 11a. In the third flow passage 11a, water vapor is generated together with the liquid fuel from the raw material gas according to the above formula (1). The synthesized liquid fuel flows out from the outlet e4 of the third flow passage 11a. The synthesized liquid fuel may be mixed with the remaining raw material gas that was not used in the conversion reaction. Water vapor, which is one of the products, sequentially permeates the separation membrane 30a and the porous support 10, and moves to the fourth flow passage 12a.

[0057] The sweep gas flows in through the inlet d3 of the inlet slit 15a, and then flows from the inlet slit 15a into the cell 13. Next, the sweep gas that has flowed into the cell 13 takes in the water vapor that has permeated the separation membrane 30a, and flows through the cell 13 toward the outlet slit 14a while absorbing the reaction heat generated by the conversion reaction. The sweep gas that has reached the outlet slit 14a is discharged from the outlet d4 of the outlet slit 14a.

[0058] 6, in a side view of the separation membrane 30a, the direction of the sweep gas flowing through the fourth flow path 12a is the same as the direction of the source gas flowing through the third flow path 11a. That is, the sweep gas flowing through the fourth flow path 12a flows in a direction parallel to the source gas flowing through the third flow path 11a.

[0059] Therefore, the reaction heat can be efficiently absorbed from the upstream area of ​​the third flow passage 11a (specifically, the flow area on the inlet d3 side from the center in the longitudinal direction of the third flow passage 11a) where the reaction heat is likely to be generated due to the high concentration of the raw material gas. As a result, the deterioration of the catalyst 20 and the separation membrane 30 can be suppressed, and the life of the reactor 1a can be extended.

[0060] [Reactor Apparatus 100] 7 is a schematic diagram of a reactor apparatus 100. The reactor apparatus 100 is one example of the use of the reactor 1.

[0061] The reactor apparatus 100 includes a reactor 1 (an example of a first reactor), a reactor 1a (an example of a second reactor), a first housing H1, and a second housing H2.

[0062] The reactor 1 is accommodated in a first housing H1. A raw material gas and a first sweep gas are separately supplied to the first housing H1. The space in the first housing H1 is partitioned so that the first sweep gas does not mix with the raw material gas and the liquid fuel. The liquid fuel synthesized in the reactor 1 flows out of the first housing H1 together with the remaining raw material gas.

[0063] The reactor 1a is disposed downstream (i.e., at the rear stage) of the reactor 1. The reactor 1a is accommodated in a second housing H2. A liquid fuel containing the remaining raw material gas and a second sweep gas are separately supplied to the second housing H2. The space in the second housing H2 is partitioned so that the second sweep gas does not mix with the remaining raw material gas and the liquid fuel. The liquid fuel synthesized in the reactor 1a flows out of the second housing H2.

[0064] In the reactor 1, as shown in FIG. 4, in a side view of the separation membrane 30 (an example of a first separation membrane), the direction of the first sweep gas flowing through the second flow passage 12 is the same as the direction of the raw material gas flowing through the first flow passage 11. reverse Therefore, it is possible to suppress the mixing of water vapor into the liquid fuel and obtain high-quality liquid fuel.

[0065] 6, in the reactor 1a, the direction of the second sweep gas flowing through the fourth passage 12a is the same as the direction of the raw material gas flowing through the third passage 11a in a side view of the separation membrane 30a (an example of the second separation membrane), so that the reaction heat can be efficiently absorbed and the life of the reactor 1a can be extended.

[0066] In this way, by combining the reactor 1 and the reactor 1a, it is possible to improve the quality of the liquid fuel and extend its life.

[0067] 7, the sweep gas supply port T1 and the sweep gas exhaust port T2 formed in the first housing H1 are arranged on a straight line intersecting the axis of the reactor 1 in a cross-sectional view. This makes it possible to equalize the flow path lengths of the sweep gas flowing from the sweep gas supply port T1 to the sweep gas exhaust port T2 through each second flow path 12, thereby preventing the flow of the sweep gas from being biased. However, the positional relationship between the sweep gas supply port T1 and the sweep gas exhaust port T2 can be changed as appropriate.

[0068] 7, the sweep gas supply port T3 and the sweep gas exhaust port T4 formed in the second housing H2 are arranged on a straight line intersecting the axis of the reactor 1a in a cross-sectional view. This makes it possible to make the flow path lengths of the sweep gas flowing from the sweep gas supply port T3 to the sweep gas exhaust port T4 through each of the fourth flow paths 12a equal, thereby preventing the flow of the sweep gas from being biased. However, the positional relationship between the sweep gas supply port T3 and the sweep gas exhaust port T4 can be changed as appropriate.

[0069] [Reactor Apparatus 200] 8 is a schematic diagram of a reactor apparatus 200. The reactor apparatus 200 is one example of the use of the reactor 1.

[0070] The reactor apparatus 200 includes a reactor 1 (an example of a first reactor), a reactor 1a (an example of a second reactor), a first housing H1', ​​and a second housing H2'.

[0071] The reactor 1a is disposed upstream (i.e., in the front stage) of the reactor 1. The reactor 1a is accommodated in a first housing H1'. A raw material gas and a second sweep gas are separately supplied to the first housing H1'. The space in the first housing H1' is partitioned so that the second sweep gas does not mix with the raw material gas and the liquid fuel. The liquid fuel synthesized in the reactor 1 flows out of the reactor 1a together with the remaining raw material gas.

[0072] The reactor 1 is accommodated in a second housing H2'. A liquid fuel containing the remaining raw material gas and a first sweep gas are separately supplied to the second housing H2'. The space in the second housing H2' is partitioned so that the first sweep gas does not mix with the remaining raw material gas and the liquid fuel. The liquid fuel synthesized in the reactor 1 flows out from the second housing H2'.

[0073] 6, in the reactor 1a, the direction of the second sweep gas flowing through the fourth passage 12a is the same as the direction of the raw material gas flowing through the third passage 11a in a side view of the separation membrane 30a (an example of the second separation membrane), so that the reaction heat can be efficiently absorbed and the life can be extended.

[0074] In the reactor 1, as shown in FIG. 4, in a side view of the separation membrane 30 (an example of a first separation membrane), the direction of the first sweep gas flowing through the second flow passage 12 is the same as the direction of the remaining raw material gas flowing through the first flow passage 11. reverse Therefore, it is possible to suppress the mixing of water vapor into the liquid fuel and obtain high-quality liquid fuel.

[0075] In this way, by combining the reactor 1 and the reactor 1a, it is possible to improve the quality of the liquid fuel and extend its life.

[0076] 8, the sweep gas supply port U1 and the sweep gas exhaust port U2 formed in the first housing H1' are arranged on a straight line intersecting the axis of the reactor 1a in a cross-sectional view. This makes it possible to make the flow path lengths of the sweep gas flowing from the sweep gas supply port U1 to the sweep gas exhaust port U2 through each of the fourth flow paths 12a equal, thereby preventing the flow of the sweep gas from being biased. However, the positional relationship between the sweep gas supply port U1 and the sweep gas exhaust port U2 can be changed as appropriate.

[0077] 8, the sweep gas supply port U3 and the sweep gas exhaust port U4 formed in the second housing H2' are arranged on a straight line intersecting the axis of the reactor 1 in a cross-sectional view. This makes it possible to equalize the flow path lengths of the sweep gas flowing from the sweep gas supply port U3 to the sweep gas exhaust port U4 through each second flow path 12, thereby preventing bias in the flow of the sweep gas. However, the positional relationship between the sweep gas supply port U3 and the sweep gas exhaust port U4 can be changed as appropriate.

[0078] (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.

[0079] (Variation 1) In the above embodiment, the monolithic reactor 1 has been described as an example of the reactor according to the present invention, but the reactor is not limited to this form. The reactor according to the present invention may be, for example, a cylindrical reactor.

[0080] 9 is a cross-sectional view taken along the longitudinal direction of a cylindrical reactor 1b. The reactor 1b includes a cylindrical separation membrane 101, a first flow path 102 provided inside the separation membrane 101 (non-permeation side) through which a raw material gas flows, a second flow path 103 provided outside the separation membrane 101 (permeation side) through which a sweep gas flows, and a catalyst 102a disposed in the first flow path 102.

[0081] The separation membrane 101 is supported by a cylindrical porous support 106. The porous support 106 is disposed inside a dense hollow column 110. The space between the porous support 106 and the hollow column 110 is the second flow path 103. The hollow column 110 is formed with an inlet 111 and an outlet 112 for supplying and discharging a sweep gas.

[0082] In a side view of the separation membrane 101, the direction of the sweep gas flowing through the second flow path 103 is opposite to the direction of the raw material gas flowing through the first flow path 102. Even in such a cylindrical reactor 1b, by flowing the sweep gas in the opposite direction to the raw material gas, it is possible to suppress the mixing of water vapor into the liquid fuel and obtain high-quality liquid fuel.

[0083] The separation membrane 101 may be disposed on either the inner circumferential surface or the outer circumferential surface of the porous support 106, but when there is a difference between the total pressure of the source gas and the total pressure of the sweep gas, it is preferable to dispose the separation membrane 101 on the inner circumferential surface of the porous support 106 as shown in Fig. 9. This can prevent the separation membrane 101 from cracking.

[0084] 10 is a cross-sectional view along the longitudinal direction of a cylindrical reactor 1c. The reactor 1c includes a cylindrical separation membrane 201, a first flow path 202 provided on the outside (non-permeation side) of the separation membrane 201 and through which a raw material gas flows, a second flow path 203 provided on the inside (permeation side) of the separation membrane 201 and through which a sweep gas flows, and a catalyst 202a disposed in the first flow path 202.

[0085] The separation membrane 201 is supported by a cylindrical porous support 206. The separation membrane 201 is surrounded by a dense cylindrical body 210. The space between the separation membrane 201 and the cylindrical body 210 is a first flow path 202. Both ends of the separation membrane 201 and the porous support 206 are blocked by a pair of dense sealing members 211, 212. The space between the pair of dense sealing members 211, 212 is a second flow path 203. The reactor 1c has an inlet 213 and an outlet 214 for supplying and discharging a sweep gas. The inlet slit 213 and the outlet slit 214 are connected to the inside of the porous support 206 and the outside of the cylindrical body 210, respectively.

[0086] In a side view of the separation membrane 201, the direction of the sweep gas flowing through the second flow path 203 is opposite to the direction of the raw material gas flowing through the first flow path 202. Even in such a cylindrical reactor 1c, by flowing the sweep gas in the opposite direction to the raw material gas, it is possible to suppress the mixing of water vapor into the liquid fuel and obtain high-quality liquid fuel.

[0087] The separation membrane 201 may be disposed on either the inner or outer circumferential surface of the porous support 206, but when there is a difference between the total pressure of the source gas and the total pressure of the sweep gas, it is preferable to dispose the separation membrane 201 on the outer circumferential surface of the porous support 206 as shown in Fig. 10. This can prevent the separation membrane 201 from cracking.

[0088] Incidentally, a cylindrical reactor may be used as the reactor 1a.

[0089] (Variation 2) In the above embodiment, the monolithic reactor 1 has been described as an example of the reactor according to the present invention, but the configuration of the reactor 1 can be appropriately changed. For example, the second flow path 12 has a pair of inlets d1 and a pair of outlets d2, but the number and positions of these can be appropriately changed.

[0090] (Variation 3) In the above embodiment, the inflow slit 14 is formed at one end of the reactor 1 (a portion from one end of the liquid fuel outlet side to 2 / 5), but at least a part of the inflow slit 14 may be formed at one end of the reactor 1. Similarly, the outflow slit 15 is formed at the other end of the reactor 1 (a portion from the other end of the raw material gas inflow side to 2 / 5), but at least a part of the outflow slit 15 may be formed at the other end of the reactor 1. However, it is preferable that at least a part of one or both of the inflow slit 14 and the outflow slit 15 is formed at 1 / 5 from the end of the reactor 1. This can widen the flow range of the sweep gas, so that the water vapor can be smoothly moved from the downstream area of ​​the first flow path 11 to the upstream area of ​​the second flow path 12 over a wider range.

[0091] (Variation 4) Fig. 11 is a cross-sectional view of the first housing H1 shown in Fig. 7. In Fig. 11, a cross section perpendicular to the axis of the reactor 1 is shown.

[0092] 11, the first extension direction in which the outflow slit 15 extends inside the reactor 1 is preferably inclined or perpendicular to the discharge direction of the sweep gas discharged to the outside from the sweep gas discharge port formed in the first housing H1. Specifically, the angle θ1 of the first extension direction with respect to the discharge direction is preferably 45 degrees or more and 135 degrees or less. This makes it possible to suppress deviation in the gas flow from the openings on both sides of the outflow slit 15 to the sweep gas discharge port, thereby suppressing deviation in the sweep gas flow.

[0093] Fig. 12 is a cross-sectional view of the first housing H1 shown in Fig. 7. In Fig. 11, a cross section perpendicular to the axis of the reactor 1 is shown.

[0094] 11, the second extension direction in which the inlet slit 14 extends inside the reactor 1 is preferably inclined or perpendicular to the supply direction of the sweep gas supplied from the sweep gas supply port formed in the first housing H1. Specifically, the angle θ2 of the second extension direction with respect to the supply direction is preferably 45 degrees or more and 135 degrees or less. This makes it possible to suppress bias in the gas flow from the sweep gas supply port to the openings on both sides of the inlet slit 14, thereby suppressing bias in the sweep gas.

[0095] It is preferable that the flow of the sweep gas shown in FIGS. 11 and 12 is also applied to the second housing H2 shown in FIG. 7 and the first housing H1' and second housing H2' shown in FIG.

[0096] (Variation 5) In the above embodiment, the separation membrane 30 is permeable to water vapor, which is one of the products of the conversion reaction from the raw material gas to liquid fuel, but this is not limited to this. The separation membrane 30 may also be permeable to the liquid fuel itself, which is produced by the conversion reaction from the raw material gas to liquid fuel. In this case as well, the reaction equilibrium of the above formula (1) can be shifted to the product side.

[0097] In addition, when the separation membrane 30 is permeable to liquid fuel, reactions that do not generate water vapor (e.g., 2H 2 +CO ⇔ CH3 Even when producing liquid fuels using ethanol (OH), the reaction equilibrium can be shifted to the product side. Similarly, the separation membrane 30a 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 may also allow the liquid fuel itself produced by the conversion reaction to pass therethrough. [Explanation of symbols]

[0098] 1. Reactor 10,106,206 Porous support 11,102,202 First flow path e1,111,213 Inlet e2,112,214 Outlet 12 Second flow path 13 Cell 14 Inlet slit d1 Inlet 15 Outlet slit d2 outlet 20,102a,202a Catalyst 30,101,201 Separation membrane 40 First seal part 50 Second seal part

Claims

1. A porous support, a separation membrane that allows permeation of a product of a conversion reaction from a feed gas containing at least hydrogen and carbon dioxide to a liquid fuel; a first flow path provided on a non-permeation side of the separation membrane within the porous support, through which the raw material gas flows; a second flow path provided in the porous support on the permeation side of the separation membrane, through which a sweep gas flows for sweeping a product that has permeated the separation membrane; A catalyst disposed in the first flow path to promote the conversion reaction; Equipped with When viewed from the side of the separation membrane, a direction of the sweep gas flowing through the second flow path is opposite to a direction of the source gas flowing through the first flow path. A monolithic reactor.

2. A method for synthesizing liquid fuel using the monolithic reactor according to claim 1, flowing a sweep gas through the second flow path while flowing the source gas through the first flow path; When viewed from the side of the separation membrane, a direction of the sweep gas flowing through the second flow path is opposite to a direction of the source gas flowing through the first flow path. Liquid fuel synthesis method.

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