WO2024257435A1 - Reactor - Google Patents

Abstract

Provided is a reactor from which a product can be efficiently collected and with which an improvement in conversion can be attained. A reactor 1 is for yielding a predetermined product from a predetermined feed gas introduced thereinto, through an exothermic reaction caused by the catalysis of a predetermined catalyst 5. The reactor 1 comprises: a casing 2 which has a feed-gas inlet 12a through which the feed gas is introduced and a product discharge opening 13b for discharging the yielded product and has the catalyst 5 packed inside; a refrigerant pipe 3 for regulation placed inside the casing 2 so that a refrigerant for regulation flows therethrough in order to regulate the reaction temperature inside the casing 2; refrigerant pipes 4 for dew condensation arranged inside the casing 2 so that a refrigerant for dew condensation flows therethrough in order to condense the product on the outer peripheral surfaces of vertical pipes 4a; and product guide paths 13c arranged inside the casing 2 to guide the product condensed on the outer peripheral surfaces of the vertical pipes 4a to the product discharge opening 13b.

Description

Reactor

The present invention relates to a reactor into which a specified raw material gas is introduced and into which a specified product is produced while causing an exothermic reaction through the catalytic action of a specified catalyst.

In recent years, regulations on automobile exhaust gases have become more stringent in order to reduce the negative impact on the global environment. In particular, carbon dioxide contained in exhaust gases from internal combustion engines is said to be a cause of global warming, and there is a demand to reduce carbon dioxide emissions.

In order to effectively utilize the carbon dioxide described above, Patent Document 1 describes a reaction device in which a feed gas containing hydrogen and carbon dioxide is introduced into a reactor filled with a specific catalyst, and hydrocarbons are produced in the reactor.

In this reactor, a first catalyst section that produces carbon monoxide from the above-mentioned raw material gas is disposed upstream of the reactor, and a second catalyst section that produces hydrocarbons using the produced carbon monoxide and hydrogen is disposed downstream of the reactor. In the above reactor, a reverse shift reaction occurs in the first catalyst section on the upstream side, while an FT (Fischer-Tropsch) reaction occurs in the second catalyst section on the downstream side. This FT reaction is an exothermic reaction, and in particular, heat generated is concentrated in the upstream portion of the second catalyst section, resulting in a large temperature bias in the second catalyst section. In order to reduce such temperature bias, an inert catalyst is mixed in the upstream portion of the second catalyst section, and as a result, in the above reactor, the temperature difference in the entire second catalyst section is suppressed, thereby stabilizing the reaction in the second catalyst section.

JP 2022-102704 A

In the above reactor, as the reaction progresses and the concentration of the product increases, the rate of reaction progress decreases. In particular, when the reaction reaches equilibrium, the reaction itself stops progressing. As a result, the above reactor may experience a decrease in product recovery efficiency and reaction rate.

The present invention was made to solve the above problems, and aims to provide a reactor that can efficiently recover products and improve the reaction rate.

In order to achieve the above object, the invention according to claim 1 is a reactor 1 for generating a predetermined product while causing an exothermic reaction by catalytic action of a predetermined catalyst 5 when a predetermined raw material gas is introduced, and the reactor 1 is characterized in that it has a raw material gas inlet 12a through which the raw material gas is introduced and a product discharge outlet 13b for discharging the generated product, a casing 2 filled with a catalyst, a first refrigerant flow path (control refrigerant tube 3) arranged so that a predetermined first refrigerant (control refrigerant in this embodiment (hereinafter the same in this paragraph)) flows within the casing and controls the reaction temperature within the casing, a second refrigerant flow path (condensation refrigerant tube 4) arranged so that a predetermined second refrigerant (condensation refrigerant) flows within the casing and condenses the product on the outer peripheral surface, and a product guide path 13c provided within the casing for guiding the product condensed on the outer peripheral surface of the second refrigerant flow path to the product discharge outlet.

According to this configuration, the reactor casing is filled with a predetermined catalyst, and the casing is provided with a first refrigerant flow path for controlling the reaction temperature, a second refrigerant flow path for condensing the product on the outer peripheral surface, and a product guide path for guiding the condensed product to the product discharge port. When a predetermined raw material gas is introduced into the casing through the raw material gas inlet, an exothermic reaction occurs due to the catalytic action of the catalyst, and the first refrigerant flows through the first refrigerant flow path to generate a predetermined product while controlling the reaction temperature. In this case, the second refrigerant flows through the second refrigerant flow path, and the product condenses on the outer peripheral surface of the second refrigerant flow path. That is, the generated gaseous product condenses, and the liquid product adheres to the outer peripheral surface of the second refrigerant flow path. The condensed product is then guided to the product discharge port of the casing through the product guide path and discharged to the outside.

As described above, the gaseous products generated by the reaction inside the reactor casing can be condensed on the outer circumferential surface of the second refrigerant flow path, changing the state to a liquid state, and the products can be efficiently recovered. In addition, by reducing the concentration of the gaseous products inside the casing, the progress of the reaction taking place inside the casing can be maintained at a high level, thereby improving the reaction rate compared to conventional reactors.

The invention according to claim 2 is characterized in that in the reactor described in claim 1, the second refrigerant is set to a lower temperature than the first refrigerant.

With this configuration, the first refrigerant promotes the reaction while controlling the reaction temperature inside the casing, while the second refrigerant, which has a lower temperature than the first refrigerant, condenses the gaseous product and causes it to condense on the outer circumferential surface of the second refrigerant flow path. In this way, with the above configuration, it is possible to achieve both promotion of the reaction inside the casing and condensation of the product.

The invention according to claim 3 is characterized in that, in the reactor according to claim 1, the casing has a main body 11 formed in a cylindrical shape extending in the vertical direction, an upper wall 12 closing the upper end of the main body and having a raw material gas inlet, and a lower wall 13 closing the lower end of the main body and having a product discharge outlet, the second refrigerant flow path extends in the vertical direction within the main body and has a plurality of vertical flow path sections (vertical pipe sections 4a) through which the second refrigerant flows, the first refrigerant flow path has a plurality of catalyst holding sections 3c configured to surround each vertical flow path section with a predetermined interval between each of the outer circumferential surfaces of the plurality of vertical flow path sections, the first refrigerant flows around the outer circumferential section of each catalyst holding section, and a catalyst is filled between each vertical flow path section and each catalyst holding section.

According to this configuration, the casing has a main body portion formed in a cylindrical shape extending in the vertical direction, and the upper end and lower end of the main body portion are blocked by the upper wall portion and the lower wall portion, respectively. In addition, the second refrigerant flow path has a plurality of vertical flow path portions extending in the vertical direction in the main body portion of the casing, through which the second refrigerant flows. Furthermore, the first refrigerant flow path has a plurality of catalyst holding portions configured to surround the plurality of vertical flow path portions of the second refrigerant flow path, respectively, and is configured so that the first refrigerant flows on the outer periphery of each catalyst holding portion. Then, a catalyst is filled between each vertical flow path portion and each catalyst holding portion. By the first refrigerant flowing on the outer periphery of each catalyst holding portion of the first refrigerant flow path, the reaction temperature of the raw material gas passing through the catalyst filled between the vertical flow path portion and the catalyst holding portion can be appropriately controlled. In addition, by the second refrigerant flowing in each vertical flow path portion of the second refrigerant flow path, the gaseous product generated in the catalyst holding portion can be easily condensed on the outer periphery of each vertical flow path portion.

The invention according to claim 4 is characterized in that in the reactor according to claim 3, each catalyst holding section is provided with a vertical flow section cover (vertical pipe section cover 6) that is formed in a cylindrical shape that extends along the vertical flow section and leaves a predetermined gap between itself and the outer peripheral surface of the vertical flow section, separating the catalyst in the catalyst holding section and the vertical flow section, allowing gas to pass through and preventing the catalyst from coming into contact with the vertical flow section.

According to this configuration, each catalyst holding section is provided with a cylindrical vertical flow section cover that extends along the vertical flow section and separates the catalyst from the vertical flow section with a specified gap between the vertical flow section and its outer peripheral surface. This vertical flow section cover is configured to allow gas to pass through while preventing the catalyst in the catalyst holding section from coming into contact with the vertical flow section. This allows liquid products that condense on the outer peripheral surface of the vertical flow section to fall along the outer peripheral surface of the vertical flow section without leaking to the catalyst side, allowing them to be efficiently collected.

The invention according to claim 5 is characterized in that in the reactor described in claim 4, the vertical flow passage cover is composed of a punched plate in which a large number of through holes having a predetermined diameter are formed.

With this configuration, by forming each through hole in the punching plate to have a diameter that the catalyst cannot pass through, it is possible to easily obtain a vertical flow path cover that allows gaseous products generated in the catalyst holding section to move from the catalyst side to the vertical flow path side.

The invention according to claim 6 is characterized in that in the reactor according to any one of claims 3 to 5, the casing further has a post-reaction gas exhaust port 13a in the lower wall portion for discharging the gas after the reaction, and the product discharge port is radially shifted in the lower wall portion of the casing and provided at a predetermined position different from the post-reaction gas exhaust port.

With this configuration, a post-reaction gas exhaust port is provided in the lower wall of the casing, so that the post-reaction gas remaining in the casing is smoothly discharged to the outside through the post-reaction gas exhaust port. In addition, a product discharge port is provided in the lower wall of the casing at a predetermined position that is radially shifted and different from the post-reaction gas exhaust port, so that the liquid product is smoothly discharged to the outside through the product discharge port without being mixed with the post-reaction gas.

FIG. 1 is a cross-sectional view showing a reactor according to one embodiment of the present invention, in which (a) is a longitudinal cross-sectional view of the reactor, and (b), (c), (d) and (e) are transverse cross-sectional views of the reactor shown in (a) taken along the lines bb, cc, dd and ee, respectively. FIG. 1 is a diagram for explaining the reaction operation in a reactor, in which (a) is a longitudinal sectional view of the reactor, and (b) and (c) are transverse sectional views of the reactor shown in (a) taken along lines bb and cc, respectively. FIG. 1 is a diagram for explaining the gas flow and condensation of products in a catalyst holding section in a reactor, in which (a) is a vertical cross-sectional view of the reactor, (b) is an enlarged view of the vertical tube section surrounded by a dashed dotted line in (a) and its surroundings, and (c), (d), and (e) are cross-sectional views of the enlarged view shown in (b) taken along lines c-c, d-d, and ee, respectively.

Below, preferred embodiments of the present invention will be described in detail with reference to the drawings. Figure 1(a) is a vertical cross-sectional view of a reactor according to one embodiment of the present invention, and Figures 1(b), (c), (d) and (e) are cross-sectional views of the reactor shown in (a) taken along lines b-b, c-c, d-d and ee, respectively.

This reactor 1 is configured to, for example, introduce a predetermined raw material gas (e.g., a mixed gas of _H2 (hydrogen) and CO (carbon monoxide) or _CO2 (carbon dioxide)) and generate a predetermined product (e.g., useful compounds such as hydrocarbons and alcohols) while causing an exothermic reaction inside.

As shown in FIG. 1, the reactor 1 is equipped with a casing 2 extending in the vertical direction, a control refrigerant pipe 3 (first refrigerant flow path) through which a refrigerant (first refrigerant) for controlling the reaction temperature inside the casing 2 (hereinafter referred to as the "control refrigerant") flows, a condensation refrigerant pipe 4 (second refrigerant flow path) through which a refrigerant (second refrigerant) for condensing the product produced by the reaction (hereinafter referred to as the "condensation refrigerant") flows, and a pellet-shaped catalyst 5 filled inside the casing 2.

The casing 2 has a main body 11 formed in a tubular shape (cylindrical in this embodiment) that extends a predetermined length in the vertical direction, an upper wall 12 that closes the upper end of the main body 11 and is provided with a raw material gas inlet 12a, and a lower wall 13 that closes the lower end of the main body 11 and is provided with a post-reaction gas outlet 13a and a product discharge outlet 13b.

The raw gas inlet 12a and the post-reaction gas outlet 13a are provided in the center of the upper wall 12 and the lower wall 13, respectively. The product discharge port 13b is radially shifted from the center of the lower wall 13 and is provided at a predetermined position different from the post-reaction gas outlet 13a. The post-reaction gas outlet 13a is configured so that its upper end protrudes to a position higher than the lower horizontal pipe section 4b of the condensation refrigerant pipe 4 (described later) and opens upward in order to prevent the condensed liquid product from being discharged.

The control refrigerant pipe 3 is assembled inside the casing 2, with the inlet 3a for the control refrigerant provided at the bottom of the casing 2 and the outlet 3b provided at the top of the casing 2. The inlet 3a and outlet 3b can be switched in their vertical positions depending on the method and conditions of use of the reactor 1, the reaction conditions, etc. The control refrigerant pipe 3 is also configured to surround multiple catalyst holders 3c (10 in this embodiment), each of which extends a predetermined length in the vertical direction and is made up of a through hole with a predetermined diameter.

The condensation refrigerant pipe 4 has a plurality of (ten in this embodiment) vertical pipe sections 4a (vertical flow passage sections) that penetrate the above-mentioned catalyst holding section 3c of the control refrigerant pipe 3 and are arranged to extend in the vertical direction, a lower horizontal pipe section 4b that connects the lower ends of each vertical pipe section 4a and extends horizontally, and an upper horizontal pipe section 4c that connects the upper ends of each vertical pipe section 4a and extends horizontally. The lower horizontal pipe section 4b is provided with an inlet 4d for the condensation refrigerant, while the upper horizontal pipe section 4c is provided with an outlet 4e for the condensation refrigerant. The inlet 4d and outlet 4e can be swapped in their vertical positions depending on the method and conditions of use of the reactor 1, the reaction conditions, etc.

Furthermore, each vertical pipe section 4a of the condensation refrigerant pipe 4 is provided with a vertical pipe section cover 6 extending in the vertical direction so as to cover its outer periphery. This vertical pipe section cover 6 is made of a punching plate with a large number of through holes of a predetermined diameter formed therein, and is formed in a cylindrical shape with an inner diameter slightly larger than the outer diameter of the vertical pipe section 4a and an outer diameter smaller than the diameter of the catalyst holding section 3c of the control refrigerant pipe 3. Each through hole of the vertical pipe section cover 6 is configured in a size that allows gas to pass through but does not allow catalyst 5 pellets to pass through.

The catalyst 5 is made of a material (e.g., Fe (iron), Zr (zirconium), Ga (gallium) and/or Na (sodium)) that promotes the reaction when generating the product depending on the raw material gas and the product. As described above, the catalyst 5 is formed into pellets of a predetermined size. The catalyst 5 is filled in each catalyst holding portion 3c of the control refrigerant tube 3 in the casing 2 of the reactor 1. Specifically, in each catalyst holding portion 3c, the catalyst 5 is filled between the inner circumferential surface and the vertical tube cover 6 that surrounds the vertical tube portion 4a of the condensation refrigerant tube 4. As shown in FIG. 1(a), the upper and lower sides of the control refrigerant tube 3 in the casing 2 are hollow spaces that are not filled with the catalyst 5. This allows the control refrigerant flowing through the control refrigerant tube 3 to effectively control the reaction temperature in each catalyst holding portion 3c, and allows the raw material gas introduced from the raw material gas inlet 12a to flow smoothly through each catalyst holding portion 3c.

Next, an example of a reaction in the reactor 1 configured as above will be described with reference to Fig. 2. In this reaction example, a raw material gas, which is a mixed gas of _H2 and _CO2, is introduced into the reactor 1, and an exothermic direct FT reaction is caused to occur, thereby producing hydrocarbons.

As shown in FIG. 2(a), the raw gas is introduced into the reactor 1 through the raw gas inlet 12a at the top. In this case, the inside of the reactor 1 is pressurized, and the control refrigerant at a predetermined temperature (e.g., 200 to 300°C) is flowed through the control refrigerant tube 3 from the inlet 3a at the bottom to the outlet 3b at the top, that is, from the bottom to the top of the reactor 1. As a result, a direct FT reaction occurs in the reactor 1 at a predetermined pressure (e.g., 3 MPa) and a predetermined temperature (e.g., 380°C), and a predetermined hydrocarbon (e.g., octane) and water are produced in a gaseous state. The control refrigerant flowing through the control refrigerant tube 3 flows out from the outlet 3b to the outside, is cooled by a cooling device (not shown), and circulates so as to flow back into the inlet 3a.

In this case, the condensation refrigerant at a predetermined temperature (200°C or less) lower than the control refrigerant flows through the condensation refrigerant tube 4 from the lower inlet 4d to the upper outlet 4e. Specifically, the condensation refrigerant that flows into the inlet 4d passes through the lower horizontal tube section 4b, the ten vertical tube sections 4a, and the upper horizontal tube section 4c of the condensation refrigerant tube 4 in that order, before flowing out from the outlet 4e. The condensation refrigerant flowing through the condensation refrigerant tube 4 is cooled by a cooling device (not shown) after flowing out to the outside from the outlet 4e, and circulates to flow back into the inlet 4d.

3(a) and (b) show the flow of gas and products and the state of condensation of products when a direct FT reaction occurs in the catalyst holding section 3c in the reactor 1. As shown in FIG. 3(b), the vertical pipe section cover 6, which is provided to cover the outer periphery of each vertical pipe section 4a, has a structure in which no through holes are formed by a punching plate at its upper end 6a. That is, the upper end 6a of the vertical pipe section cover 6 has a top plate section 6b through which the corresponding vertical pipe section 4a penetrates, and an upper end cylindrical section 6c that is connected to the peripheral section of the top plate section 6b and extends downward for a certain length. In addition, the vertical pipe section cover 6 has a cylindrical cover main body section 6d that is connected to the lower end peripheral section of the upper end cylindrical section 6c and extends relatively long to the vicinity of the lower end of the control refrigerant pipe 3, and a large number of through holes are formed in this cover main body section 6d by a punching plate. A condensation space 7 with a circular cross section is defined between the upper end cylindrical portion 6c and the cover body portion 6d of the vertical pipe cover 6 and the vertical pipe portion 4a located inside them.

As described above, when the raw material gas is introduced into the reactor 1, the raw material gas flows downward while contacting the catalyst 5 packed in the catalyst holding section 3c, as shown by the downward arrow in FIG. 3(b). In this case, the gaseous hydrocarbons and water generated in the catalyst holding section 3c pass through the numerous through holes in the cover body section 6d of the vertical tube section cover 6, as shown by the inclined arrows pointing toward the vertical tube section 4a in FIG. 3(b), and move to the vertical tube section 4a side through the condensation space 7.

In addition, since the upper end 6a of the vertical tube cover 6 does not have a through hole formed by a punching plate, it is possible to prevent the raw material gas flowing into the catalyst holding section 3c from above from flowing directly into the condensation space 7 or flowing into the condensation space 7 with almost no contact with the catalyst 5.

Then, as the condensation refrigerant flows through the condensation refrigerant tube 4, the gaseous hydrocarbons and water that have moved to the vertical tube section 4a condense and condense on the outer circumferential surface of the vertical tube section 4a. In the following description, unless there is a particular distinction between the condensed hydrocarbons and water, both will be referred to as products.

The liquid product that condenses on the outer peripheral surface of each vertical tube section 4a falls down the outer peripheral surface of the vertical tube section 4a under its own weight. Then, as shown by the arrow of the product guide path 13c on the lower wall section 13 in Figure 2 (c), the liquid product is guided to the product discharge outlet 13b and discharged to the outside. Note that the above product guide path 13c is not tubular, but is formed so that the upper surface of the lower wall section 13 is inclined downward toward the front toward the product discharge outlet 13b. Therefore, the liquid product that falls on the upper surface of the lower wall section 13 automatically flows toward the product discharge outlet 13b and is discharged through the product discharge outlet 13b.

The post-reaction gas remaining in the casing 2 is discharged to the outside through the post-reaction gas exhaust port 13a provided in the lower wall portion 13 of the casing 2.

As described above in detail, according to the reactor 1 of this embodiment, when the raw material gas is introduced into the casing 2 through the raw material gas inlet 12a, an exothermic reaction occurs by a direct FT reaction due to the catalytic action of the catalyst 5 and the reaction temperature control by the control refrigerant, and gaseous products (hydrocarbons and water) are generated. In this case, the condensation refrigerant flows through the condensation refrigerant tube 4, causing the generated gaseous products to condense, and the liquid products condense on the outer peripheral surface of the vertical tube section 4a of the condensation refrigerant tube 4. The condensed products are then guided to the product discharge outlet 13b via the product guide path 13c and discharged to the outside.

As described above, the gaseous products generated by the direct FT reaction in the casing 2 of the reactor 1 are condensed on the outer peripheral surface of the vertical tube section 4a of the condensation refrigerant tube 4, changing the state to a liquid state, and the products can be efficiently recovered. In addition, by reducing the concentration of the gaseous products in the casing 2, the progress of the direct FT reaction taking place in the casing 2 can be maintained at a high level, thereby improving the reaction rate compared to conventional reactors.

In addition, in the reactor 1, the control refrigerant promotes the direct FT reaction while controlling the reaction temperature inside the casing 2, while the condensation refrigerant, which has a lower temperature than the control refrigerant, condenses the gaseous product and causes it to condense on the outer circumferential surface of the vertical tube section 4a of the condensation refrigerant tube 4. In this way, with the above configuration, it is possible to promote the direct FT reaction inside the casing 2 and condense the product at the same time.

Furthermore, in the reactor 1, the vertical tube section 4a through which each catalyst holding section 3c is inserted is provided with a vertical tube section cover 6 made of a punching plate so as to cover the outer circumferential surface of the vertical tube section 4a, so that the liquid product that condenses on the outer circumferential surface of the vertical tube section 4a falls along the outer circumferential surface of the vertical tube section 4a without leaking to the catalyst 5 side, and can be efficiently collected.

The lower wall 13 of the casing 2 is provided with a post-reaction gas exhaust port 13a in its center, and a product discharge port 13b is provided radially offset from the center at a predetermined position different from the post-reaction gas exhaust port 13a. This allows the post-reaction gas remaining in the casing 2 to be smoothly discharged to the outside via the post-reaction gas exhaust port 13a, and allows the liquid product to be smoothly discharged to the outside via the product discharge port 13b without being mixed with the post-reaction gas.

The present invention is not limited to the above-described embodiment, and can be implemented in various aspects. For example, in the embodiment, the reactor 1 is used to perform a direct FT reaction to generate hydrocarbons from a raw material gas containing H ₂ and CO ₂ , but the reactor of the present invention is not limited to this, and can be applied to a reaction in which an exothermic reaction occurs in the casing 2 of the reactor 1, the raw material gas does not contain liquid components at room temperature and reaction pressure, and the product contains a large amount of liquid components at room temperature and reaction pressure. For example, the reactor 1 can be applied to a methanol synthesis reaction to generate CH ₃ OH (methanol) from a raw material gas containing H ₂ and CO ₂ .

In the embodiment, the reactor 1 has 10 catalyst holding sections 3c of the control refrigerant tube 3 and 10 vertical tube sections 4a of the condensation refrigerant tube 4, but the number is not particularly limited, and it is possible to have a number other than 1 or 10 depending on the size and shape of the reactor.

Furthermore, the detailed configurations of the casing 2, control refrigerant tube 3, condensation refrigerant tube 4, catalyst 5, and vertical tube cover 6 of the reactor 1 shown in the embodiment are merely examples and can be modified as appropriate within the scope of the spirit of the present invention.

1 Reactor 2 Casing 3 Control refrigerant pipe (first refrigerant flow path)
3a Inlet 3b Outlet 3c Catalyst holding part 4 Refrigerant pipe for dew condensation (second refrigerant flow path)
4a Vertical pipe section (vertical channel section)
4b Lower horizontal pipe part 4c Upper horizontal pipe part 4d Inlet 4e Outlet 5 Catalyst 6 Vertical pipe part cover (vertical channel part cover)
6a Upper end of vertical tube cover 6b Top plate 6c Upper cylindrical portion 6d Cover main body 7 Condensation space 11 Casing main body 12 Casing upper wall 12a Raw material gas inlet 13 Casing lower wall 13a Post-reaction gas outlet 13b Product discharge outlet 13c Product guide path

Claims (6)

A reactor for producing a predetermined product while causing an exothermic reaction by catalytic action of a predetermined catalyst in which a predetermined raw material gas is introduced, the reactor comprising:
a casing having a raw material gas inlet through which the raw material gas is introduced and a product discharge outlet through which the generated product is discharged, the casing being filled with the catalyst;
a first coolant flow passage arranged in the casing so that a predetermined first coolant flows therethrough, for controlling a reaction temperature in the casing;
a second refrigerant flow path arranged within the casing so that a predetermined second refrigerant flows therethrough, and for condensing the product on an outer peripheral surface of the casing;
a product guide path provided in the casing and configured to guide a product condensed on an outer peripheral surface of the second refrigerant flow path to the product discharge port;
A reactor comprising: The reactor described in claim 1, characterized in that the second refrigerant is set to a lower temperature than the first refrigerant. the casing has a main body formed in a cylindrical shape extending in a vertical direction, an upper wall portion closing an upper end of the main body and provided with the raw material gas inlet, and a lower wall portion closing a lower end of the main body and provided with the product discharge outlet,
The second refrigerant flow path extends in a vertical direction within the main body portion and has a plurality of vertical flow path portions through which the second refrigerant flows,
the first refrigerant flow path has a plurality of catalyst holding portions configured to surround each of the vertical flow path portions with a predetermined interval between each of the vertical flow path portions and an outer circumferential surface of each of the vertical flow path portions, and the first refrigerant is configured to flow around the outer circumferential portion of each of the catalyst holding portions;
2. The reactor according to claim 1, wherein the catalyst is filled between each of the vertical flow passage sections and each of the catalyst holding sections. The reactor described in claim 3 is characterized in that each catalyst holding section is provided with a vertical flow section cover that is formed in a cylindrical shape that extends along the vertical flow section and leaves a predetermined gap between the catalyst inside the catalyst holding section and the vertical flow section, and that allows gas to pass through while preventing the catalyst from coming into contact with the vertical flow section. The reactor described in claim 4, characterized in that the vertical flow passage cover is made of a punched plate having a large number of through holes having a predetermined diameter. the casing further has a post-reaction gas exhaust port in the lower wall portion for exhausting a post-reaction gas,
6. The reactor according to claim 3, wherein the product discharge port is radially shifted from the lower wall of the casing and is provided at a predetermined position different from the post-reaction gas discharge port.