Reactor

Abstract

A reactor (1) is equipped with a porous support body (10), a plurality of first cells (11) through which a source gas flows, a plurality of second cells (12) through which a sweep gas flows, a separation membrane (20), and a catalyst (30). The first cell (11) penetrates the porous support body (10) in the longitudinal direction. The second cell (12) extends in the porous support body (10) in the longitudinal direction. The separation membrane (20) is formed on the inner periphery surface of the first cell (11). The catalyst (30) is disposed inside the separation membrane (10). In a cross-section taken along the transverse direction, the average cross-sectional area of the first cell (11) is larger than the average cross-sectional area of the second cell (12).

Description

[Technical field]

[0001] The present invention relates to a reactor. [Background technology]

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

[0003] For example, Patent Document 1 discloses a tubular reactor including a first cell provided on the non-permeation side of a plurality of separation membranes and a second cell provided on the permeation side of each separation membrane. Each separation membrane is supported by a cylindrical porous support. The first cell is filled with a catalyst and is supplied with a raw material gas. The second flow path is supplied with a sweep gas for sweeping the product that has permeated the separation membrane. [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] The present inventors have investigated the above-mentioned conversion reaction in a monolith reactor. The monolith reactor includes a porous support, a plurality of first cells penetrating the porous support and through which a raw material gas flows, a plurality of second cells formed within the porous support and through which a sweep gas flows, a separation membrane formed on the inner circumferential surface of each of the first cells, and a catalyst disposed inside the separation membrane.

[0006] In a monolithic reactor, increasing the diameter of the first cell allows the catalyst packing rate to approach close packing, which increases the amount of catalyst and improves conversion efficiency, but the strength of the porous support decreases. Therefore, in a monolithic reactor, it is not easy to improve conversion efficiency and ensure strength at the same time.

[0007] In addition, in a tube-type reactor, the amount of catalyst can be increased by reducing the number of separation membranes, which improves the conversion efficiency, but the separation membrane is subjected to stress due to the thermal expansion of the catalyst as well as the weight of the increased catalyst, making the porous support that supports the separation membrane prone to damage. Therefore, even in a tube-type reactor, it is not easy to achieve both improved conversion efficiency and sufficient strength.

[0008] An object of the present invention is to provide a reactor that can improve conversion efficiency while ensuring strength. [Means for solving the problem]

[0009] The reactor according to a first aspect of the present invention is a monolithic reactor used for a conversion reaction from a raw material gas containing at least hydrogen and carbon oxides to a liquid fuel. The reactor comprises a porous support, a plurality of first cells through which a raw material gas flows, a plurality of second cells through which a sweep gas flows, a separation membrane, and a catalyst. The plurality of first cells penetrate the porous support in a first direction. The plurality of second cells extend in the first direction within the porous support. The separation membrane is formed on the inner peripheral surface of each of the plurality of first cells and allows the product of the conversion reaction to permeate. The catalyst is disposed inside the separation membrane and promotes the conversion reaction. In a cross section along a second direction perpendicular to the first direction, the average cross-sectional area of ​​the plurality of first cells is larger than the average cross-sectional area of ​​the plurality of second cells.

[0010] A reactor according to a second aspect of the present invention is related to the first aspect, wherein, in the cross-section, each of the plurality of first cells is circular, in the cross-section, each of the plurality of second cells is circular, and in the cross-section, an average diameter of the plurality of first cells is larger than an average diameter of the plurality of second cells.

[0011] A reactor according to a third aspect of the present invention is related to the first aspect, wherein, in the cross-section, each of the plurality of first cells is circular, and in the cross-section, each of the plurality of second cells is polygonal, and in the cross-section, an average diameter of the plurality of first cells is larger than an average diameter of the plurality of second cells.

[0012] A reactor according to a fourth aspect of the present invention is related to any one of the first to third aspects and includes a plurality of first slits through which the sweep gas flows and a plurality of second slits through which the sweep gas flows. In the cross section, the second cells are arranged in a plurality of rows. Each of the first slits penetrates one end of each of the rows, and each of the second slits penetrates the other end of each of the rows.

[0013] A reactor according to a fifth aspect of the present invention is a tubular reactor used for a conversion reaction from a raw material gas containing at least hydrogen and carbon oxides to a liquid fuel. The reactor comprises a plurality of separation membranes, a first cell, a plurality of second cells, and a catalyst. Each of the plurality of separation membranes is supported by a porous support. The first cell is provided on the non-permeation side of each of the plurality of separation membranes, and the raw material gas flows through it. The plurality of second cells are provided on the permeation side of each of the plurality of separation membranes, and a sweep gas flows through it. The catalyst is disposed on the non-permeation side of each of the plurality of separation membranes, and promotes the conversion reaction. The first cell and each of the plurality of second cells extend in a first direction. In a cross section along a second direction perpendicular to the first direction, a value obtained by dividing a cross-sectional area of ​​the first cell by the number of the second cells is greater than an average cross-sectional area of ​​the plurality of second cells. Effect of the Invention

[0014] According to the present invention, it is possible to provide a reactor that can achieve both improved conversion efficiency and sufficient strength. [Brief description of the drawings]

[0015] [Figure 1] FIG. 1 is a perspective view of a monolithic reactor 1 according to an embodiment. [Diagram 2] Cross-sectional view of Fig. 1 along line II-II [Diagram 3] III-III cross section of Figure 1 [Figure 4] IV-IV cross section of Figure 1 [Diagram 5] VV cross section of Figure 2 [Figure 6] Cross-sectional view of a porous support according to Modification 3 [Figure 7] 11 is a cross-sectional view of a tube-type reactor 100 according to a sixth modified example. [Figure 8] 11 is a cross-sectional view of a tube-type reactor 100 according to a sixth modified example. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0016] 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.

[0017] (Reactor 1) Fig. 1 is a perspective view of the reactor 1. Fig. 2 is a cross-sectional view taken along line II-II in Fig. 1. Fig. 3 is a cross-sectional view taken along line III-III in Fig. 1. Fig. 4 is a cross-sectional view taken along line IV-IV in Fig. 1.

[0018] 2 to 4 show a cross section along the short side direction perpendicular to the longitudinal direction of the reactor 1. In the following description, a cross section refers to a cross section along the short side direction. The longitudinal direction is an example of a "first direction" according to the present invention, and the short side direction is an example of a "second direction" according to the present invention.

[0019] The reactor 1 is a so-called membrane reactor used for a conversion reaction from a raw material gas to a liquid fuel. The raw material gas contains at least hydrogen and carbon oxide. At least one of carbon monoxide and carbon dioxide can be used as the carbon oxide. 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.

[0020] For example, the reaction formula (1) when methanol is synthesized by catalytic hydrogenation of a raw material gas containing hydrogen and carbon dioxide in the presence of a catalyst is as follows. CO 2 +3H 2 ⇔ CH 3 OH+H 2 O (1)

[0021] 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.

[0022] 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.

[0023] The reactor 1 has a first end surface S1, a second end surface S2, and a side surface S3. The first end surface S1 is provided on the opposite side of the second end surface S2. The side surface S3 is continuous with the outer edges of the first end surface S1 and the second end surface S2. In this embodiment, the reactor 1 is formed in a cylindrical shape.

[0024] As shown in FIGS. 1 to 4, the reactor 1 includes a porous support 10, a separation membrane 20, a catalyst 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.

[0025] [Porous support 10] The porous support 10 is a columnar body extending in the longitudinal direction of the reactor 1. In this embodiment, the cross-sectional shape of the porous support 10 is circular. In this specification, the concept of a circular shape includes not only a perfect circle, but also a circle having a degree of distortion that is unavoidable during manufacturing.

[0026] The porous support 10 is made of a porous material. As the porous material, a ceramic material, a metal material, a resin material, or the like can be used, and a ceramic material is particularly preferable. As an 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.

[0027] As shown in FIGS. 2 to 4, the porous support 10 has a plurality of first cells 11, a plurality of second cells 12, a plurality of first slits 13, and a plurality of second slits 14.

[0028] The first cells 11 extend in the longitudinal direction of the reactor 1. The first cells 11 penetrate the porous support 10 in the longitudinal direction. The first cells 11 open to a first end face S1 and a second end face S2 of the reactor 1. A raw material gas is allowed to flow through the first cells 11. In this embodiment, the cross-sectional shape of the first cells 11 is circular. This makes it possible to suppress the occurrence of cracks in the separation membrane 20.

[0029] The second cell 12 extends in the longitudinal direction of the reactor 1. The second cell 12 is formed inside the porous support 10. The second cell 12 does not penetrate the porous support 10 in the longitudinal direction. The second cell 12 does not open to the first end face S1 and the second end face S2 of the reactor 1. Specifically, both ends of the second cell 12 are sealed by first and second plugging portions 17, 18 (see FIG. 5). The first and second plugging portions 17, 18 can be made of the above-mentioned porous material. A sweep gas for sweeping the water vapor that has permeated the separation membrane 20 is flowed through the second cell 12. As the sweep gas, an inert gas (e.g., nitrogen) or air can be used. In this embodiment, the cross-sectional shape of the second cell 12 is circular.

[0030] As shown in FIG. 2, the first cells 11 are arranged in six columns L along the short side direction, and the second cells 12 are arranged in three columns M along the short side direction. Each column L includes two or more first cells 11. Each column M includes five or more second cells 12. On both sides of the column M of the second cells 12, there is one column L of the first cells 11. However, the number of columns L, the number of columns M, and their arrangement can be changed as appropriate. Furthermore, the number of first cells 11 included in the column L and the number of second cells 12 included in the column M can be changed as appropriate.

[0031] As shown in FIG. 1, the first slit 13 is formed at one end of the reactor 1. As shown in FIG. 3, the first slit 13 extends in the short direction. The first slit 13 penetrates the porous support 10 and one end of the row M of the second cells 12. Both ends of the first slit 13 open to the side surface S3 of the reactor 1. A sweep gas flows through the first slit 13. In this embodiment, the sweep gas is supplied from both ends of the first slit 13.

[0032] As shown in FIG. 1, the second slit 14 is formed at the other end of the reactor 1. As shown in FIG. 4, the second slit 14 extends in the short direction. The second slit 14 penetrates the porous support 10 and the other end of the row M of the second cells 12. Both ends of the second slit 14 open to the side surface S3 of the reactor 1. A sweep gas flows through the second slit 14. In this embodiment, the sweep gas is discharged from both ends of the second slit 14.

[0033] In this embodiment, the second cells 12 are arranged in three columns M, so that three first and three second slits 13, 14 are provided, but the numbers of the first and second slits 13, 14 can be changed as appropriate depending on the number of columns M of the second cells 12.

[0034] The porous support 10 is produced by firing a molded body in which the first and second cells 11, 12 are formed, and then perforating the first and second slits 13, 14 for each row M of the second slits 14.

[0035] Here, as shown in FIG. 2, the average cross-sectional area of ​​the plurality of first cells 11 is larger than the average cross-sectional area of ​​the plurality of second cells 12.

[0036] In this way, by relatively increasing the average cross-sectional area of ​​the first cells 11, it is possible to increase the volume of the space (non-permeation side space inside the separation membrane 20) in which the catalyst 30 described later is placed. Therefore, the amount of the catalyst 30 that promotes the conversion reaction can be increased, and the conversion efficiency from the raw material gas to the liquid fuel can be improved. In addition, by relatively decreasing the average cross-sectional area of ​​the second cells 12, it is possible to prevent the occupancy rate of the porous support 10 in the cross section from decreasing. Therefore, the volume of the voids in the porous support 10 can be reduced, and the strength of the porous support 10 can be ensured. Therefore, according to the reactor 1 of this embodiment, it is possible to achieve both improved conversion efficiency and ensured strength.

[0037] The average cross-sectional area of ​​the first cells 11 is obtained by taking the arithmetic mean of the cross-sectional areas of each of the first cells 11. The average cross-sectional area of ​​the second cells 12 is obtained by taking the arithmetic mean of the cross-sectional areas of each of the second cells 12.

[0038] In this embodiment, the cross-sectional shape of the first cells 11 is circular, and the cross-sectional shape of the second cells 12 is circular. Therefore, by making the average diameter of the second cells 12 smaller than the average diameter of the first cells 11, the average cross-sectional area of ​​the second cells 12 can be made smaller than the average cross-sectional area of ​​the first cells 11. In addition, the average cross-sectional areas of the first and second cells 11, 12 can be easily adjusted by changing the average diameters of the first and second cells 11, 12.

[0039] The average diameter of the first cells 11 is obtained by arithmetically averaging the equivalent circle diameters of the first cells 11 in the cross section. The average diameter of the second cells 12 is obtained by arithmetically averaging the equivalent circle diameters of the second cells 12 in the cross section. The equivalent circle diameter is the diameter of a circle having the same area as the cell cross section. When the cell cross section is a perfect circle, the equivalent circle diameter is the same as the diameter of the perfect circle.

[0040] The total area ratio of the first cells 11 in the cross section is not particularly limited, but may be, for example, 15% to 40%. In this case, the number of the first cells 11 may be, for example, 20 to 1700.

[0041] The total area ratio of the second cells 12 in the cross section is not particularly limited, but can be, for example, 5% to 15%. In this case, the number of the second cells 12 can be, for example, 40 to 700.

[0042] The total area percentage of the first cells 11 is obtained by dividing the total cross-sectional area of ​​the first cells 11 by the total area of ​​the porous support 10 in cross section (including the cross-sectional areas of the first and second cells 11, 12). The total area percentage of the second cells 12 is obtained by dividing the total cross-sectional area of ​​the second cells 12 by the total area of ​​the porous support 10 in cross section.

[0043] The average cross-sectional area, average diameter, and total area ratio of the first and second cells 11, 12 are calculated in the cross section at the center of the porous support 10 in the longitudinal direction.

[0044] [Separation membrane 20] The separation membrane 20 is supported by the porous support 10. The separation membrane 20 is formed on the inner circumferential surface of the first cell 11. The separation membrane 20 is cylindrical. The separation membrane 20 surrounds the catalyst 30.

[0045] The separation membrane 20 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 shift the reaction equilibrium of the above formula (1) to the product side by utilizing the equilibrium shift effect.

[0046] The separation membrane 20 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)).

[0047] The separation membrane 20 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 oxides, and liquid fuels) to permeate. The separation factor can be determined by a known method (see FIG. 1 in "Separation and Purification Technology 239 (2020) 116533").

[0048] An inorganic membrane can be used as the separation membrane 20. 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.

[0049] [Catalyst 30] The catalyst 30 promotes the conversion reaction shown in the above formula (1). The catalyst 30 is disposed in the non-permeation side space inside the separation membrane 20. The catalyst 30 is preferably filled in the non-permeation side space, but may be disposed on the inner peripheral surface of the separation membrane 20 in the form of layers or islands.

[0050] Any known catalyst suitable for the desired conversion reaction into liquid fuel can be used as the catalyst 30. Examples of the catalyst 30 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 made by modifying these with palladium, etc.).

[0051] [First and second seal portions 40, 50] 1, the first sealing portion 40 covers one end surface of the porous support 10. The first sealing portion 40 prevents the source gas from entering the porous support 10. The first sealing portion 40 is formed so as not to block the openings of the first cells 11. The first sealing portion 40 can be made of glass, metal, rubber, resin, or the like.

[0052] 1, the second seal portion 50 covers the other end face of the porous support body 10. 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 openings of the first cells 11. The second seal portion 50 can be made of glass, metal, rubber, resin, or the like.

[0053] (Method of synthesizing liquid fuel using reactor 1) Next, a liquid fuel synthesis method using the reactor 1 will be described.

[0054] The method for synthesizing a liquid fuel using the reactor 1 includes a step of flowing a raw material gas through the first cell 11 and flowing a sweep gas through the second passage 12.

[0055] The raw material gas flows into the first cell 11 from the inlet e1 of the first cell 11. In the first cell 11, liquid fuel is synthesized from the raw material gas by the action of the catalyst 30, and water vapor is also generated. The synthesized liquid fuel flows out from the outlet e2 of the first cell 11 to the outside. Water vapor, which is one of the products, sequentially permeates the separation membrane 20 and the porous support 10, and moves to the second flow path 12.

[0056] The sweep gas flows into the first slit 13 from the inlet d1 of the first slit 13, and then flows into the second cell 12. The sweep gas that flows into the second cell 12 takes in the water vapor that has permeated the separation membrane 20 and absorbs the reaction heat accompanying the conversion reaction, and then flows out from the outlet d2 of the second slit 14 to the outside.

[0057] In FIG. 5, the direction of the source gas flowing through the first cell 11 is the same as the direction of the sweep gas flowing through the second cell 12, but it may be opposite.

[0058] (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.

[0059] (Variation 1) In the above embodiment, the cross-sectional shape of the porous support 10 is circular, but it may be, for example, elliptical.

[0060] (Variation 2) In the above embodiment, the cross-sectional shape of the first cells 11 is circular, but it may be elliptical. Even if the cross-sectional shape of the first cells 11 is elliptical, the occurrence of cracks in the separation membrane 20 can be suppressed. The elliptical shape also includes an elliptical shape having a degree of distortion that is unavoidable during manufacturing. Even if the cross-sectional shape of the first cells 11 is elliptical, the average diameter of the first cells 11 can be obtained by arithmetically averaging the circle-equivalent diameters of the first cells 11, as described in the above embodiment.

[0061] (Variation 3) In the above embodiment, the cross-sectional shape of the second cells 12 is circular, but it may be, for example, an ellipse, a polygon, or a complex shape other than these. The ellipse and polygon include shapes having a degree of distortion that is unavoidable during manufacturing. The polygon includes not only a polygon with all angles bent, but also a polygon with at least one angle curved. Even if the cross-section of the second cells 12 is an ellipse or a polygon, the average diameter of the second cells 12 can be obtained by arithmetically averaging the circle-equivalent diameters of the second cells 12, as described in the above embodiment.

[0062] (Variation 4) In the above embodiment, an example has been described in which one row L of the first cells 11 is provided on each side of the row M of the second cells 12, but the arrangement of the first and second cells 11, 12 can be changed as appropriate.

[0063] For example, only one row M may be provided, or two or more rows M may be provided. The position of the row M is not particularly limited, and the row M may be provided at a position shifted from the center point of the porous support 10. Furthermore, when two or more rows M are provided, at least two rows M may be perpendicular to or intersect with each other. This can improve the strength of the porous support 10 compared to a case where all rows M are arranged so as not to be perpendicular to or intersect with each other. In this case, the first cells 11 may be arranged in an area where no row M is provided, regardless of whether or not a row L is formed.

[0064] 6, the second cells 12 can be arranged in point symmetry with respect to the center point CP of the porous support 10. In this case, by orthogonally or intersecting at least two rows M, not only is the strength of the porous support 10 improved, but the strength of the porous support 10 can be prevented from becoming anisotropic, thereby further improving the strength of the porous support 10. Point symmetry is a concept that includes not only the case where the cross section of the second cell 12 coincides with the original cross section when rotated 180 degrees around the center point CP, but also the case where the cross section does not partially coincide with the original cross section due to a degree of deviation or distortion that is unavoidable during manufacturing.

[0065] 6, since the second cells 12 are arranged in two rows M, it is sufficient to provide two each of the first and second slits 13, 14 penetrating the rows M. The two first slits 13 intersect (join) each other near the center point CP, and the two second slits 14 intersect each other near the center point CP.

[0066] However, as shown in FIG. 6, when the second cells 12 are arranged point symmetrically, the number of rows M of the second cells 12 is not limited, and may be one or more rows.

[0067] [Variation 5] In the above embodiment, the separation membrane 20 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 20 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.

[0068] In addition, when the separation membrane 20 is permeable to liquid fuel, reactions that do not generate water vapor (e.g., H 2 +CO ⇔ CH 3 Even when producing liquid fuels using ethanol (OH), the reaction equilibrium can be shifted to the product side.

[0069] [Variation 6] In the above embodiment, it has been described that by optimizing the cross-sectional areas of the first and second cells 11, 12 in the monolithic reactor, it is possible to improve the conversion efficiency while ensuring the strength.

[0070] However, the reactor is not limited to a monolith type, and may be a tube type. In the tube type reactor, the cross-sectional areas of the first and second cells are optimized to improve the conversion efficiency and ensure the strength.

[0071] Fig. 7 is a cross-sectional view along the longitudinal direction of the tube-type reactor 100 according to this modification. Fig. 8 is a cross-sectional view along the transverse direction of the tube-type reactor 100 according to this modification. The longitudinal direction is an example of the "first direction" according to the present invention, and the transverse direction is an example of the "second direction" according to the present invention. The transverse direction is perpendicular to the longitudinal direction.

[0072] The reactor 100 is used for conversion reactions of a feed gas containing at least hydrogen and carbon oxides to liquid fuel.

[0073] As shown in FIGS. 7 and 8, the reactor 100 includes a housing 110, a plurality of porous supports 120, a plurality of separation membranes 130, a first cell 140, a plurality of second cells 150, and a catalyst 160.

[0074] The housing 110 is an enclosure of the reactor 100. The housing 110 is formed in a cylindrical shape extending along the longitudinal direction.

[0075] The porous support 120 supports the separation membrane 130. The porous support 120 is formed in a cylindrical shape extending along the longitudinal direction. The outer surface of the porous support 120 is surrounded by the separation membrane 130. The inside of the porous support 120 is hollow. The constituent material of the porous support 120 is the same as that of the porous support 10 according to the above embodiment.

[0076] The separation membrane 130 is supported by the porous support 120. In this modification, the separation membrane 130 is disposed on the outer surface of the porous support 120. The separation membrane 130 is formed in a cylindrical shape extending along the longitudinal direction. The separation membrane 130 is surrounded by a catalyst 160. The separation membrane 130 allows the product (steam or liquid fuel) generated from the raw material gas in the first cell 140 to permeate toward each second cell 150. The characteristics and constituent materials of the separation membrane 130 are similar to those of the separation membrane 20 according to the above embodiment. The separation membrane 130 may be disposed on the inner surface of the porous support 120.

[0077] The first cells 140 are provided on the non-permeation side of each separation membrane 130. The first cells 140 are spaces between the outer surface of each separation membrane 130 and the inner surface of the housing 110. A raw material gas is made to flow through the first cells 140. The first cells 140 extend in the longitudinal direction.

[0078] The second cells 150 are provided inside the porous support 120. The second cells 150 are spaces on the permeate side of each separation membrane 130. A sweep gas is caused to flow through the second cells 150. The second cells 150 extend in the longitudinal direction.

[0079] The catalyst 160 is disposed in the first cell 140. The catalyst 160 promotes a conversion reaction from the raw material gas to liquid fuel. The constituent material of the catalyst 160 is the same as that of the catalyst 30 according to the above embodiment.

[0080] 8, in a cross section along the short side direction, the value obtained by dividing the cross-sectional area of ​​the first cell 140 by the number of the second cells 150 is larger than the average cross-sectional area of ​​the second cells 150. This makes it possible to increase the volume of the first cell 140 allocated to one second cell 150. In other words, when the first cell 140 is regarded as an assembly of a plurality of small cells corresponding to the plurality of second cells 150, the volume of each small cell can be made larger than the volume of each second cell 150. This makes it possible to increase the amount of catalyst 160 disposed in the first cell 140, which is an assembly of a plurality of small cells, and thus improves the efficiency of conversion from the raw material gas to liquid fuel.

[0081] Furthermore, since the number of second cells 150 can be increased while the value obtained by dividing the cross-sectional area of ​​the first cells 140 by the number of second cells 150 is made larger than the average cross-sectional area of ​​the second cells 150, it is possible to reduce the stress applied to each second cell 150 due to the weight of the catalyst 160 and the thermal expansion of the catalyst 160. Therefore, damage to the porous support 120 of each second cell 150 can be suppressed.

[0082] As described above, the tubular reactor 100 according to this modified example can improve the conversion efficiency while ensuring the strength. [Explanation of symbols]

[0083] 1. Monolithic reactor 10 Porous support 11 Cell 1 L 1st cell column 12 Cell 2 M Second cell column 13 First slit 14 Second slit d2 outlet 20 Separation membrane 30 Catalyst 100 Tube type reactor 110 Housing 120 Porous support 130 Separation membrane 140 Cell 1 150 Second Cell 160 Catalyst

Claims

1. A monolithic reactor used for a conversion reaction from a feed gas containing at least hydrogen and carbon oxides to a liquid fuel, comprising: A porous support; a plurality of first cells penetrating the porous support in a first direction and through which the source gas flows; a plurality of second cells extending in the first direction within the porous support and through which a sweep gas flows; a separation membrane formed on an inner circumferential surface of each of the first cells and allowing a product of the conversion reaction to pass therethrough; A catalyst disposed inside the separation membrane to promote the conversion reaction; Equipped with In a cross section along a second direction perpendicular to the first direction, an average cross-sectional area of ​​the first cells is larger than an average cross-sectional area of ​​the second cells. Reactor.

2. In the cross section, each of the plurality of first cells is circular; In the cross section, each of the plurality of second cells is circular; In the cross section, an average diameter of the plurality of first cells is greater than an average diameter of the plurality of second cells.

10. The reactor of claim 1.

3. In the cross section, each of the plurality of first cells is circular; In the cross section, each of the plurality of second cells is a polygon; In the cross section, an average diameter of the plurality of first cells is greater than an average diameter of the plurality of second cells.

10. The reactor of claim 1.

4. a plurality of first slits through which the sweep gas flows; a plurality of second slits through which the sweep gas flows; Equipped with In the cross section, the second cells are arranged in a plurality of rows, Each of the first slits penetrates one end of each of the rows, Each of the second slits penetrates the other end of each of the rows.

10. The reactor of claim 1.

5. A tubular reactor used for a conversion reaction from a feed gas containing at least hydrogen and carbon oxides to a liquid fuel, comprising: A plurality of separation membranes, each of which is supported by a porous support; a first cell provided on a non-permeation side of the plurality of separation membranes and through which the raw material gas flows; A plurality of second cells provided inside the porous support and through which a sweep gas flows; a catalyst disposed within the first cell to promote the conversion reaction; Equipped with The first cell and each of the plurality of second cells extend in a first direction, In a cross section along a second direction perpendicular to the first direction, a value obtained by dividing a cross-sectional area of ​​the first cell by the number of the second cells is greater than an average cross-sectional area of ​​the plurality of second cells. Reactor.

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