Reactor

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

[0001] The present invention relates to a reactor into which a predetermined raw material gas is introduced and into which a predetermined product is produced while an exothermic reaction occurs through the catalytic action of a predetermined catalyst.

[0002] In recent years, regulations on automobile exhaust gases have become increasingly stringent in order to reduce the adverse effects on the global environment. In particular, carbon dioxide contained in exhaust gases from internal combustion engines is said to be one of the causes of global warming, and there is a need to reduce carbon dioxide emissions.

[0003] In order to effectively utilize the carbon dioxide as described above, Patent Document 1 describes a reaction apparatus in which a raw material gas containing hydrogen and carbon dioxide is introduced into a reactor filled with a predetermined catalyst, and hydrocarbons are produced in the reactor.

[0004] In this reactor, a first catalyst section that produces carbon monoxide from the feed 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 reactor, a reverse shift reaction occurs in the upstream first catalyst section, while a Fischer-Tropsch (FT) reaction occurs in the downstream second catalyst section. The FT reaction is an exothermic reaction, and heat generated is concentrated in the upstream portion of the second catalyst section, resulting in significant temperature imbalances in the second catalyst section. To reduce such temperature imbalances, an inert catalyst is mixed in the upstream portion of the second catalyst section. This suppresses temperature differences throughout the second catalyst section, thereby stabilizing the reaction in the second catalyst section.

[0005] Japanese Patent Application Laid-Open No. 2022-102704

[0006] In the above reactor, as the reaction progresses and the product concentration increases, the rate of reaction slows down. In particular, when the reaction reaches equilibrium, the reaction itself stops progressing. As a result, the product recovery efficiency and reaction rate may decrease in the above reactor.

[0007] The present invention has been made to solve the above-mentioned problems, and an object of the present invention is to provide a reactor that can efficiently recover products and improve the reaction rate.

[0008] In order to achieve the above object, the invention according to claim 1 provides a reactor 1 for producing a predetermined product while causing an exothermic reaction by catalytic action of a predetermined catalyst 5 when a predetermined raw material gas is introduced, the reactor 1 comprising: a casing 2 having a raw material gas inlet 12a through which the raw material gas is introduced and a product outlet 13b through which the produced product is discharged, the casing 2 being filled with a catalyst; a first refrigerant flow path (control refrigerant pipe 3) arranged to allow a predetermined first refrigerant (control refrigerant in this embodiment (the same applies hereinafter in this paragraph)) to flow within the casing and for controlling the reaction temperature within the casing; a second refrigerant flow path (condensation refrigerant pipe 4) arranged to allow a predetermined second refrigerant (condensation refrigerant) to flow within the casing and for condensing 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.

[0009] According to this configuration, a 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 a 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 catalytic action of the catalyst, and the predetermined product is produced while controlling the reaction temperature by flowing the first refrigerant through the first refrigerant flow path. In this case, the second refrigerant flows through the second refrigerant flow path, causing the product to condense on the outer peripheral surface of the second refrigerant flow path. That is, the produced 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 via the product guide path to the product discharge port of the casing and discharged to the outside.

[0010] As described above, the gaseous product produced by the reaction in the reactor casing is condensed on the outer circumferential surface of the second refrigerant flow path, thereby changing the state of the product to a liquid, and thereby the product can be efficiently recovered. In addition, by reducing the concentration of the gaseous product in the casing, the progress of the reaction taking place in the casing can be maintained at a high level, thereby improving the reaction rate compared to conventional reactors.

[0011] A second aspect of the present invention is the reactor according to the first aspect, wherein the second refrigerant is set to have a temperature lower than that of the first refrigerant.

[0012] 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. Thus, with the above configuration, it is possible to achieve both promotion of the reaction inside the casing and condensation of the product.

[0013] The invention according to claim 3 is the reactor according to claim 1, characterized in that the casing has a main body portion 11 formed in a cylindrical shape extending in the vertical direction, an upper wall portion 12 closing the upper end of the main body portion and having a raw material gas inlet port, and a lower wall portion 13 closing the lower end of the main body portion and having a product discharge outlet port, the second refrigerant flow path extending in the vertical direction within the main body portion has a plurality of vertical flow path portions (vertical pipe portions 4 a) through which the second refrigerant flows, the first refrigerant flow path has a plurality of catalyst holding portions 3 c configured to surround each of the vertical flow path portions with a predetermined interval between them and the outer circumferential surfaces of the plurality of vertical flow path portions, the first refrigerant flowing around the outer circumferential portions of each catalyst holding portion, and a catalyst is filled between each vertical flow path portion and each catalyst holding portion.

[0014] According to this configuration, the casing has a cylindrical main body portion extending vertically, with the upper and lower ends of the main body portion blocked by upper and lower wall portions, respectively. The second refrigerant flow path extends vertically in the main body portion of the casing and has multiple vertical flow path portions through which the second refrigerant flows. The first refrigerant flow path has multiple catalyst holding portions configured to surround the multiple vertical flow path portions of the second refrigerant flow path, respectively, and is configured so that the first refrigerant flows around the outer periphery of each catalyst holding portion. A catalyst is filled between each vertical flow path portion and each catalyst holding portion. By having the first refrigerant flow around the outer periphery of each catalyst holding portion of the first refrigerant flow path, the reaction temperature of the source gas passing through the catalyst filled between the vertical flow path portion and the catalyst holding portion can be appropriately controlled. Additionally, by having the second refrigerant flow through each vertical flow path portion of the second refrigerant flow path, gaseous products generated in the catalyst holding portion can be easily condensed on the outer periphery of each vertical flow path portion.

[0015] 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 path section cover (vertical pipe section cover 6) which is formed in a cylindrical shape extending along the vertical flow path section and separating the catalyst in the catalyst holding section from the vertical flow path section with a predetermined gap remaining between it and the outer peripheral surface of the vertical flow path section, and which allows gas to pass through and prevents the catalyst from coming into contact with the vertical flow path section.

[0016] According to this configuration, each catalyst holding unit is provided with a cylindrical vertical flow path cover that extends along the vertical flow path unit and separates the catalyst from the vertical flow path unit with a predetermined gap between the vertical flow path cover and the outer peripheral surface of the vertical flow path unit. This vertical flow path cover is configured to allow gas to pass through while preventing the catalyst in the catalyst holding unit from contacting the vertical flow path unit. This allows liquid products that condense on the outer peripheral surface of the vertical flow path unit to fall along the outer peripheral surface of the vertical flow path unit and be efficiently collected without leaking to the catalyst side.

[0017] The invention according to claim 5 is characterized in that, in the reactor according to claim 4, the vertical flow path section cover is made of a punching plate in which a large number of through holes having a predetermined diameter are formed.

[0018] According to this configuration, by forming each through hole of the punching plate to have a diameter that prevents the catalyst from passing through, it is possible to easily obtain a vertical flow path section cover that allows gaseous products generated in the catalyst holding section to move from the catalyst side to the vertical flow path section side.

[0019] The invention of claim 6 is characterized in that, in the reactor described in any one of claims 3 to 5, the casing further has a post-reaction gas discharge port 13a in the lower wall portion for discharging the gas after the reaction, and the product discharge port is shifted radially in the lower wall portion of the casing and provided at a predetermined position different from the post-reaction gas discharge port.

[0020] According to this configuration, the reaction gas discharge port is provided in the lower wall of the casing, so that the reaction gas remaining in the casing is smoothly discharged to the outside through the reaction gas discharge port. Also, the product discharge port is provided in the lower wall of the casing at a predetermined position that is radially shifted and different from the reaction gas discharge port, so that the liquid product is smoothly discharged to the outside through the product discharge port without being mixed with the reaction gas.

[0021]

[0023] Figure 1 is a cross-sectional view showing a reactor according to one embodiment of the present invention, where (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) cut along line bb, line cc, line dd, and line ee, respectively. Figure 2 is a diagram for explaining the reaction operation in the reactor, where (a) is a longitudinal cross-sectional view of the reactor, and (b) and (c) are transverse cross-sectional views of the reactor shown in (a) cut along line bb and line cc, respectively. Figure 3 is a diagram for explaining the gas flow and product condensation in a catalyst holding section within the reactor, where (a) is a longitudinal cross-sectional view of the reactor, (b) is an enlarged view of the vertical tube section and its surroundings surrounded by the dashed dotted line in (a), and (c), (d), and (e) are transverse cross-sectional views of the enlarged view shown in (b) cut along line cc, line dd, and line ee, respectively.

[0022]

[0023] Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the drawings. Fig. 1(a) is a longitudinal sectional view of a reactor according to one embodiment of the present invention, and Fig. 1(b), (c), (d), and (e) are transverse sectional views of the reactor shown in (a) taken along line bb, line cc, line dd, and line ee, respectively.

[0023] This reactor 1 is configured to, for example, supply a predetermined raw material gas (e.g., H ２ (hydrogen) and CO (carbon monoxide) or CO ２ A mixture of gases (carbon dioxide, etc.) is introduced into the reactor, causing an exothermic reaction inside to produce a desired product (for example, useful compounds such as hydrocarbons and alcohols).

[0024] As shown in FIG. 1 , the reactor 1 includes 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 in 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 a product produced by the reaction (hereinafter referred to as the “condensation refrigerant”) flows, and a pellet-shaped catalyst 5 filled in the casing 2.

[0025] The casing 2 has a main body 11 formed in a tubular shape (cylindrical in this embodiment) extending a predetermined length in the vertical direction, an upper wall 12 closing the upper end of the main body 11 and provided with a raw material gas inlet 12a, and a lower wall 13 closing the lower end of the main body 11 and provided with a post-reaction gas outlet 13a and a product discharge outlet 13b.

[0026] The raw material gas inlet 12a and the post-reaction gas outlet 13a are provided in the central portions of the upper wall portion 12 and the lower wall portion 13, respectively. The product discharge port 13b is provided at a predetermined position radially shifted from the center of the lower wall portion 13 and 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 a lower horizontal pipe portion 4b (described later) of the condensation refrigerant pipe 4 and opens upward in order to prevent the condensed liquid product from being discharged.

[0027] The control refrigerant pipe 3 is assembled inside the casing 2, with an inlet 3a for the control refrigerant provided in the lower part of the casing 2 and an outlet 3b provided in the upper part of the casing 2. The upper and lower positions of the inlet 3a and outlet 3b can be reversed depending on the method and conditions of use of the reactor 1, the reaction conditions, etc. The control refrigerant pipe 3 is configured to surround a plurality of (ten in this embodiment) catalyst holding portions 3c, each of which extends a predetermined length in the vertical direction and is made up of a through-hole having a predetermined diameter.

[0028] The condensation refrigerant pipe 4 has a plurality of (ten in this embodiment) vertical pipe sections 4a (vertical flow passage sections) that penetrate the 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 the vertical pipe sections 4a and extends horizontally, and an upper horizontal pipe section 4c that connects the upper ends of the vertical pipe sections 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 upper and lower positions of the inlet 4d and the outlet 4e can be reversed depending on the usage method and conditions of the reactor 1, the reaction conditions, etc.

[0029] Each vertical pipe section 4a of the condensation refrigerant pipe 4 is provided with a vertical pipe section cover 6 extending in the up-down direction so as to cover its outer periphery. This vertical pipe section cover 6 is made of a punched 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 sized to allow gas to pass through but not allow catalyst 5 pellets to pass through.

[0030] 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 producing 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 pipe 3 in the casing 2 of the reactor 1. Specifically, the catalyst 5 is filled between the inner circumferential surface of each catalyst holding portion 3c and the vertical pipe cover 6 that surrounds the vertical pipe portion 4a of the condensation refrigerant pipe 4. As shown in FIG. 1( a), the upper and lower sides of the control refrigerant pipe 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 pipe 3 to effectively control the reaction temperature in each catalyst holding portion 3c and allows the raw material gas introduced through the raw material gas inlet 12a to flow smoothly through each catalyst holding portion 3c.

[0031] Next, an example of a reaction in the reactor 1 configured as described above will be described with reference to FIG. ２ and CO ２ The raw material gas, which is a mixed gas of the above, is introduced into the reactor 1, and the direct FT reaction, which is an exothermic reaction, is caused to occur, thereby producing hydrocarbons.

[0032] As shown in FIG. 2( a), a raw material gas is introduced into the reactor 1 through the upper raw material gas inlet 12a. In this case, the reactor 1 is pressurized, and a control refrigerant at a predetermined temperature (e.g., 200 to 300°C) is flowed through the control refrigerant pipe 3 from the lower inlet 3a to the upper outlet 3b, i.e., 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), producing predetermined hydrocarbons (e.g., octane) and water in a gaseous state. The control refrigerant flowing through the control refrigerant pipe 3 flows out through the outlet 3b, is cooled by a cooling device (not shown), and circulates so as to flow back into the inlet 3a.

[0033] In this case, a condensation refrigerant at a predetermined temperature (200°C or lower) lower than that of the control refrigerant flows through the condensation refrigerant pipe 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 pipe section 4b, the ten vertical pipe sections 4a, and the upper horizontal pipe section 4c of the condensation refrigerant pipe 4 in this order, before flowing out through the outlet 4e. After flowing out through the outlet 4e to the outside, the condensation refrigerant flowing through the condensation refrigerant pipe 4 is cooled by a cooling device (not shown) and circulates so as to flow back into the inlet 4d.

[0034] 3(a) and (b) show the flow of gas and products and the state of condensation of the products during the Direct FT reaction in the catalyst holding section 3c in the reactor 1. As shown in FIG. 3(b), the vertical pipe section covers 6 provided to cover the outer peripheries of the vertical pipe sections 4a have a structure in which no through-holes are formed by punching plates at their upper ends 6a. That is, the upper ends 6a of the vertical pipe section covers 6 have a top plate section 6b through which the corresponding vertical pipe section 4a passes and an upper cylindrical section 6c that is continuous with the periphery of the top plate section 6b and extends downward by a predetermined distance. Furthermore, the vertical pipe section covers 6 have a cylindrical cover main section 6d that is continuous with the lower peripheral edge of the upper cylindrical section 6c and extends relatively long to near the lower end of the control refrigerant pipe 3, and a number of through-holes are formed in the cover main section 6d by punching plates. A condensation space 7 having a circular cross section is defined between the upper end cylindrical portion 6c and cover main body portion 6d of the vertical pipe cover 6 and the vertical pipe portion 4a located inside them.

[0035] As described above, when the raw material gas is introduced into the reactor 1, the raw material gas flows downward while coming into contact with the catalyst 5 packed in the catalyst holding unit 3c, as indicated by the downward arrows in Fig. 3(b). In this case, gaseous hydrocarbons and water produced in the catalyst holding unit 3c pass through the numerous through-holes in the cover body 6d of the vertical pipe cover 6, as indicated by the inclined arrows pointing toward the vertical pipe 4a in Fig. 3(b), and move through the condensation space 7 toward the vertical pipe 4a.

[0036] Furthermore, since no through holes are provided by a punching plate at the upper end 6a of the vertical pipe section cover 6, 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 from flowing into the condensation space 7 without coming into contact with the catalyst 5.

[0037] As the condensation refrigerant flows through the condensation refrigerant pipe 4, the gaseous hydrocarbons and water that have moved to the vertical pipe section 4a side condense and form condensation on the outer circumferential surface of the vertical pipe section 4a. In the following description, unless a distinction is made between the condensed hydrocarbons and water, both will be referred to as products.

[0038] The liquid product condensed on the outer peripheral surface of each vertical pipe section 4a falls down the outer peripheral surface of the vertical pipe section 4a due to 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 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 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.

[0039] The reacted gas remaining inside the casing 2 is discharged to the outside through a reacted gas discharge port 13 a provided in the lower wall portion 13 of the casing 2 .

[0040] 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 the 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 produced. In this case, the condensation refrigerant flows through the condensation refrigerant pipe 4, causing the produced gaseous products to condense, and the liquid products are condensed on the outer peripheral surface of the vertical pipe portion 4a of the condensation refrigerant pipe 4. The condensed products are then guided to the product discharge outlet 13b via the product guide path 13c and discharged to the outside.

[0041] As described above, the gaseous product produced by the Direct FT reaction in the casing 2 of the reactor 1 is condensed on the outer peripheral surface of the vertical pipe section 4a of the condensation refrigerant pipe 4, thereby changing the state of the product to a liquid, and thereby enabling efficient recovery of the product. In addition, by being able to reduce the concentration of the gaseous product in the casing 2, the degree of progress of the Direct FT reaction taking place in the casing 2 can be maintained at a high level, thereby enabling an improvement in the reaction rate compared to conventional reactors.

[0042] Furthermore, in the reactor 1, the control refrigerant is used to promote 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 pipe section 4a of the condensation refrigerant pipe 4. In this way, with the above-described configuration, it is possible to achieve both promotion of the Direct FT reaction inside the casing 2 and condensation of the product.

[0043] Furthermore, in the reactor 1, the vertical pipe section 4a through which each catalyst holding section 3c is inserted is provided with a vertical pipe section cover 6 made of a punching plate so as to cover the outer surface of the vertical pipe section 4a. Therefore, the liquid product that condenses on the outer surface of the vertical pipe section 4a can be allowed to fall along the outer surface of the vertical pipe section 4a without leaking to the catalyst 5 side, and can be efficiently recovered.

[0044] Furthermore, a post-reaction gas discharge port 13a is provided in the center of the lower wall portion 13 of the casing 2, and a product discharge port 13b is provided radially offset from the center at a predetermined position different from the post-reaction gas discharge port 13a. This allows the post-reaction gas remaining in the casing 2 to be smoothly discharged to the outside through the post-reaction gas discharge port 13a, and also allows the liquid product to be smoothly discharged to the outside through the product discharge port 13b without being mixed with the post-reaction gas.

[0045] The present invention is not limited to the above-described embodiment, and can be implemented in various modes. For example, in the embodiment, the reactor 1 ２ and CO ２In the above description, a direct FT reaction is carried out to produce hydrocarbons from a feed gas containing H. However, 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 feed 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, ２ and CO ２ from a source gas containing CH ３ The reactor 1 can also be applied to a methanol synthesis reaction that produces OH (methanol).

[0046] In the embodiment, the reactor 1 is provided with ten catalyst holding portions 3c of the control refrigerant pipe 3 and ten vertical pipe portions 4a of the condensation refrigerant pipe 4, but the number of these is not particularly limited, and it is also possible to provide a number other than one or ten depending on the size, shape, etc. of the reactor.

[0047] Furthermore, the detailed configurations of the casing 2, the control refrigerant pipe 3, the condensation refrigerant pipe 4, the catalyst 5, and the vertical pipe cover 6 of the reactor 1 shown in the embodiment are merely examples, and can be changed as appropriate within the scope of the spirit of the present invention.

[0048] DESCRIPTION OF SYMBOLS 1 Reactor 2 Casing 3 Control refrigerant pipe (first refrigerant flow path) 3a Inlet 3b Outlet 3c Catalyst holding section 4 Condensation refrigerant pipe (second refrigerant flow path) 4a Vertical pipe section (vertical flow path section) 4b Lower horizontal pipe section 4c Upper horizontal pipe section 4d Inlet 4e Outlet 5 Catalyst 6 Vertical pipe section cover (vertical flow path section cover) 6a Upper end of vertical pipe section cover 6b Top plate section 6c Upper cylindrical section 6d Cover main body section 7 Condensation space 11 Main body section of casing 12 Upper wall section of casing 12a Raw material gas inlet 13 Lower wall section of casing 13a Post-reaction gas outlet 13b Product discharge outlet 13c Product guide path

Claims

1. A reactor for producing a predetermined product by introducing a predetermined raw material gas and generating an exothermic reaction through the catalytic action of a predetermined catalyst, A casing having a raw material gas inlet into which the raw material gas is introduced, and a product outlet for discharging the generated product, the casing being filled with the catalyst inside, A first refrigerant flow path is provided within the casing to allow a predetermined first refrigerant to flow, and to control the reaction temperature within the casing. A second refrigerant channel is provided within the casing to allow a predetermined second refrigerant to flow, and to cause condensation of the product on the outer surface. A product guide path is provided within the casing and guides the product condensed on the outer surface of the second refrigerant flow path to the product outlet, Equipped with, The casing comprises a main body formed in a cylindrical shape extending vertically, an upper wall portion that closes the upper end of the main body and is provided with the raw material gas inlet, and a lower wall portion that closes the lower end of the main body and is provided with the product outlet. The second refrigerant flow path extends vertically within the main body and includes a plurality of vertical flow path sections through which the second refrigerant flows, a lower horizontal flow path section that connects the lower ends of each of the vertical flow path sections and extends horizontally, and an upper horizontal flow path section that connects the upper ends of each of the vertical flow path sections and extends horizontally. The first refrigerant flow path has a plurality of catalyst holding portions that surround each of the plurality of vertical flow path portions, with a predetermined distance between each of the outer surfaces of the respective vertical flow path portions, and the first refrigerant is configured to flow around the outer surface of each catalyst holding portion. The catalyst is filled between each of the vertical channel sections and each of the catalyst holding sections. An inlet for the second refrigerant is provided in one of the lower horizontal flow section and the upper horizontal flow section, and an outlet for the second refrigerant is provided in the other of the lower horizontal flow section and the upper horizontal flow section. A reactor characterized in that the inlet and outlet are configured to be interchangeable in their vertical positional relationship.

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

3. The reactor according to claim 1, wherein each catalyst holding portion is provided with a vertical channel cover that extends along the vertical channel portion and maintains a predetermined gap between itself and the outer surface of the vertical channel portion, and is formed in a cylindrical shape to partition the catalyst within the catalyst holding portion from the vertical channel portion, allowing the passage of gas and preventing the catalyst from coming into contact with the vertical channel portion.

4. The reactor according to claim 3, characterized in that the vertical channel cover is made of a punched plate having a number of through holes having a predetermined diameter.

5. The casing further has a post-reaction gas outlet in its lower wall for discharging the gas after the reaction, The reactor according to any one of claims 1 to 4, characterized in that the product outlet is radially offset in the lower wall portion of the casing and is provided at a predetermined position different from the post-reaction gas outlet.