Hydrocarbon production device

Abstract

The hydrocarbon production device 100 comprises: a reaction device 110 which has an inlet 230a, an outlet 232c, and one or a plurality of supply ports 230b, 230c provided between the inlet 230a and the outlet 232c, and in which a catalyst 220 for promoting an exothermic reaction between hydrogen and carbon dioxide is housed; a first hydrogen supply part 120 for supplying hydrogen into the reaction device 110 through the inlet 230a of the reaction device 110; and a carbon dioxide supply part 130 for supplying carbon dioxide into the reaction device 110 through the inlet 230a and supply ports 230b, 230c of the reaction device 110.

Description

Hydrocarbon Production Equipment

[0001] This application claims the benefit of priority from Japanese Patent Application No. 2023-199655, filed on November 27, 2023, the contents of which are incorporated herein by reference.

[0002] Fossil fuels such as coal, heavy oil, and extra-heavy oil are burned in plants such as thermal power plants, steel mills, and boilers. Consequently, exhaust gases containing either or both of carbon dioxide and carbon monoxide, which are generated by the combustion of fossil fuels, are emitted from the plants into the atmosphere. Because carbon dioxide and carbon monoxide are considered to be factors contributing to global warming, technologies have been developed to capture either or both of carbon dioxide and carbon monoxide from the atmosphere.

[0003] Furthermore, as a technology for effectively utilizing recovered carbon dioxide, for example, Patent Document 1 discloses a technology in which carbon dioxide and hydrogen are supplied to a reactor containing a catalyst that promotes a methanation reaction, and the carbon dioxide and hydrogen are reacted in the reactor to produce methane.

[0004] Japanese Patent Application Laid-Open No. 2021-116294

[0005] However, a synthesis reaction between hydrogen and either or both of carbon dioxide and carbon monoxide, such as a methanation reaction, is an exothermic reaction. Therefore, in a technology such as that disclosed in Patent Document 1 that promotes the synthesis reaction between carbon dioxide and hydrogen using a catalyst, the reaction heat from the synthesis reaction may cause the temperature inside the reactor to rise too high, which may result in catalyst deterioration.

[0006] In view of the above problems, the present disclosure has an object to provide a hydrocarbon production apparatus capable of maintaining an appropriate temperature inside the reactor.

[0007] In order to solve the above problems, a hydrocarbon production apparatus according to one embodiment of the present disclosure includes a reactor having an inlet, an outlet, and one or more supply ports provided between the inlet and the outlet, and containing a catalyst that promotes an exothermic reaction between hydrogen and carbon dioxide; a first hydrogen supply unit that supplies hydrogen into the reactor through the inlet of the reactor; and a carbon dioxide supply unit that supplies carbon dioxide into the reactor through the inlet and the supply port of the reactor.

[0008] The hydrocarbon production apparatus may also include a flow rate control unit that controls the flow rate of the carbon dioxide supplied by the carbon dioxide supply unit.

[0009] The flow rate control unit may also control the flow rate of carbon dioxide based on the temperature of the catalyst housed in the reaction device.

[0010] Furthermore, the distance between the inlet and the supply port that is the shortest distance from the inlet may be shorter than the distance between the outlet and the supply port that is the shortest distance from the outlet.

[0011] The reactor may also have two or more supply ports, and the distance between the inlet and the supply port that is the shortest from the inlet may be shorter than the distance between adjacent supply ports, and the distance between the outlet and the supply port that is the shortest from the outlet may be longer than the distance between adjacent supply ports.

[0012] The reactor may have three or more supply ports, and the distance between adjacent supply ports may increase from the inlet side toward the outlet side.

[0013] Alternatively, the reaction apparatus may include a plurality of reactors connected in series, with the inlet provided in the reactor at the front stage and the outlet provided in the reactor at the last stage.

[0014] The hydrocarbon production apparatus may further include a cooler that cools the gas discharged from the outlet of at least one of the plurality of reactors.

[0015] The hydrocarbon production apparatus may also include a second hydrogen supply unit that supplies hydrogen into the reactor through a supply port of the reactor.

[0016] In order to solve the above problems, another hydrocarbon production apparatus according to one embodiment of the present disclosure includes a reactor having an inlet, an outlet, and one or more supply ports provided between the inlet and the outlet, and containing a catalyst that promotes an exothermic reaction between hydrogen and carbon monoxide; a first hydrogen supply unit that supplies hydrogen into the reactor through the inlet of the reactor; and a carbon monoxide supply unit that supplies carbon monoxide into the reactor through the inlet and the supply port of the reactor.

[0017] In order to solve the above problems, another hydrocarbon production apparatus according to one embodiment of the present disclosure includes a reactor having an inlet, an outlet, and one or more supply ports provided between the inlet and the outlet, and accommodating a catalyst that promotes an exothermic reaction of hydrogen, carbon monoxide, and carbon dioxide; a first hydrogen supply unit that supplies hydrogen into the reactor through the inlet of the reactor; a carbon monoxide supply unit that supplies carbon monoxide into the reactor through the inlet and the supply port of the reactor; and a carbon dioxide supply unit that supplies carbon dioxide into the reactor through the inlet and the supply port of the reactor.

[0018] According to the present disclosure, it is possible to maintain an appropriate temperature inside the reactor.

[0019] FIG. 1 is a diagram illustrating a hydrocarbon production apparatus according to a first embodiment. FIG. 2 is a diagram illustrating a hydrocarbon production apparatus according to a second embodiment. FIG. 3 is a diagram illustrating a hydrocarbon production apparatus according to a modified example. FIG. 4 is a graph showing simulation results of a comparative example. FIG. 5 is a graph showing simulation results of a first reactor in an example. FIG. 6 is a graph showing simulation results of a second reactor in an example.

[0020] Hereinafter, embodiments of the present disclosure will be described in detail with reference to the accompanying drawings. Dimensions, materials, and other specific numerical values ​​shown in the embodiments are merely examples for ease of understanding and do not limit the present disclosure unless otherwise specified. In this specification and drawings, elements having substantially the same functions and configurations are designated by the same reference numerals to avoid redundant explanation. Elements not directly related to the present disclosure are not shown.

[0021] [First embodiment: hydrocarbon production apparatus 100] Fig. 1 is a diagram illustrating a hydrocarbon production apparatus 100 according to a first embodiment. As shown in Fig. 1, the hydrocarbon production apparatus 100 according to the first embodiment includes a reaction device 110, temperature sensors T1, T2, and T3, a hydrogen supply unit 120, a carbon dioxide supply unit 130, a cooler 150, a gas-liquid separator 160, a temperature adjustment unit 170, and a central control unit 180. In Fig. 1, solid arrows indicate the flows of hydrogen (gas), carbon dioxide (gas), hydrocarbons (gas), and water (gas and liquid). Also, in Fig. 1, dashed arrows indicate the flow of a heat transfer medium.

[0022] In the reaction device 110, a synthesis reaction between hydrogen and carbon dioxide takes place to produce hydrocarbons. The synthesis reaction between hydrogen and carbon dioxide is an exothermic reaction. The synthesis reaction between hydrogen and carbon dioxide is, for example, the reaction shown in the following formulas (1) to (4). 4H ２ + CO ２ → CH ４ + 2H ２ O...Formula (1) 6H ２ + 2CO ２ → C ２ H ４ + 4H ２ O...Formula (2) 9H ２ + 3CO ２ → C ３ H ６ + 6H ２ O ... Formula (3) mH ２ + nCO ２ → hydrocarbon + 2nH ２ O ... Equation (4) Methane is produced by the reaction shown in the above formula (1). Ethylene is produced by the reaction shown in the above formula (2). Propylene is produced by the reaction shown in the above formula (3). Hydrocarbons are produced by the Fischer-Tropsch (FT) synthesis reaction shown in the above formula (4). In this embodiment, an example will be given in which the reaction shown in the above formula (1) is carried out in the reaction device 110 to produce methane.

[0023] The reaction device 110 has an inlet 230a for hydrogen and carbon dioxide, an outlet 232c for the gas after the reaction, and one or more carbon dioxide supply ports 230b, 230c provided between the inlet 230a and the outlet 232c. The reaction device 110 also contains a catalyst 220. A layer of the catalyst 220 (catalytic layer) is formed in the reaction device 110. The catalyst 220 is a catalyst that promotes the exothermic reaction between hydrogen and carbon dioxide. The catalyst 220 is, for example, a catalyst that promotes the reaction shown in formula (1). In FIG. 1, the catalyst 220 is indicated by cross-hatching.

[0024] In this embodiment, the reaction device 110 includes, for example, a plurality of reactors 210 connected in series. By configuring the reaction device 110 with a plurality of reactors 210 connected in series, the carbon dioxide supply ports 230b, 230c can be easily formed. The reactor 210 is, for example, a multi-tube heat exchange reactor. The reactor 210 has a heat medium container 212 and a plurality of reaction tubes 214. A heat medium is supplied to the heat medium container 212 by a temperature adjustment unit 170, which will be described later.

[0025] The plurality of reaction tubes 214 are provided in the heat medium container 212. The reaction tubes 214 contain a catalyst 220. A layer of the catalyst 220 (catalyst layer) is formed in the reaction tubes 214. The temperature inside the reaction tubes 214 (the temperature of the catalyst layer) is, for example, 200°C or higher and 550°C or lower due to the heat generated by the heat medium passing through the heat medium container 212 and the exothermic reaction proceeding inside the reaction tubes 214.

[0026] In this embodiment, the reaction apparatus 110 includes, for example, three reactors 210: a first reactor 210a, a second reactor 210b, and a third reactor 210c. The first reactor 210a, the second reactor 210b, and the third reactor 210c are connected in series in this order.

[0027] The first reactor 210a in the front stage is provided with an inlet 230a and an outlet 232a. The inlet 230a is connected to one side of the plurality of reaction tubes 214 of the first reactor 210a. The outlet 232a is connected to the other side of the plurality of reaction tubes 214 of the first reactor 210a. The inlet 230a of the first reactor 210a is connected to a hydrogen supply unit 120 and a carbon dioxide supply unit 130, which will be described later. The outlet 232a of the first reactor 210a is connected to a supply port 230b of the second reactor 210b via a pipe 240a.

[0028] The second reactor 210b is provided with a supply inlet 230b and a discharge outlet 232b. The supply inlet 230b is connected to one side of the plurality of reaction tubes 214 of the second reactor 210b. The discharge outlet 232b is connected to the other side of the plurality of reaction tubes 214 of the second reactor 210b. The discharge outlet 232b of the second reactor 210b is connected to the supply inlet 230c of the third reactor 210c, which is the final stage, via a pipe 240b.

[0029] The third reactor 210c is provided with a supply port 230c and an outlet 232c. The supply port 230c is connected to one side of the plurality of reaction tubes 214 of the third reactor 210c. The outlet 232c is connected to the other side of the plurality of reaction tubes 214 of the third reactor 210c. A pipe 240c is connected to the outlet 232c of the third reactor 210c. The product gas produced in the reaction apparatus 110 and containing 90% or more hydrocarbons is discharged to the outside through the pipe 240c.

[0030] In this embodiment, for example, the length of the reaction tube 214 of the reactor 210 increases from the front stage to the rear stage. For example, the length of the reaction tube 214 may increase in the order of the first reactor 210a, the second reactor 210b, and the third reactor 210c. That is, in the reaction device 110, the distance between the inlet 230a and the supply port 230b, which is the shortest from the inlet 230a, may be shorter than the distance between the supply port 230b and the supply port 230c. Furthermore, in the reaction device 110, the distance between the outlet 232c and the supply port 230c, which is the shortest from the outlet 232c, may be longer than the distance between the supply port 230b and the supply port 230c.

[0031] The temperature sensor T1 detects the temperature of the catalyst 220 (catalyst layer) accommodated in the reaction tube 214 of the first reactor 210a. The temperature sensor T2 detects the temperature of the catalyst 220 (catalyst layer) accommodated in the reaction tube 214 of the second reactor 210b. The temperature sensor T3 detects the temperature of the catalyst 220 (catalyst layer) accommodated in the reaction tube 214 of the third reactor 210c.

[0032] The hydrogen supply unit 120 (first hydrogen supply unit) supplies hydrogen into the first reactor 210 a of the reaction device 110 through the inlet 230 a of the first reactor 210 a.

[0033] The hydrogen supply unit 120 includes, for example, a blower 122 and a raw material gas supply pipe 124. The suction side of the blower 122 is connected to a hydrogen supply source. The discharge side of the blower 122 is connected to the raw material gas supply pipe 124. The raw material gas supply pipe 124 connects the discharge side of the blower 122 to the inlet 230a of the first reactor 210a of the reaction device 110.

[0034] The carbon dioxide supply unit 130 supplies carbon dioxide into the first reactor 210a, the second reactor 210b, and the third reactor 210c through the inlet 230a of the first reactor 210a, the supply port 230b of the second reactor 210b, and the supply port 230b of the third reactor 210c of the reaction device 110.

[0035] The carbon dioxide supply unit 130 includes, for example, a blower 132, a carbon dioxide supply pipe 134, branch pipes 136a, 136b, and 136c, and flow rate adjustment valves 138a, 138b, and 138c. The suction side of the blower 132 is connected to a carbon dioxide supply source. The discharge side of the blower 132 is connected to the carbon dioxide supply pipe 134.

[0036] The branch pipe 136a connects the carbon dioxide supply pipe 134 and the raw material gas supply pipe 124. The carbon dioxide discharged from the blower 132 is supplied to the first reactor 210a through the carbon dioxide supply pipe 134, the branch pipe 136a, the raw material gas supply pipe 124, and the inlet 230a of the first reactor 210a of the reaction apparatus 110.

[0037] The branch pipe 136b connects the carbon dioxide supply pipe 134 and the pipe 240a. The carbon dioxide discharged from the blower 132 is supplied to the second reactor 210b through the carbon dioxide supply pipe 134, the branch pipe 136b, the pipe 240a, and the supply port 230b of the second reactor 210b of the reaction device 110.

[0038] The branch pipe 136c connects the carbon dioxide supply pipe 134 and the pipe 240b. The carbon dioxide discharged from the blower 132 is supplied to the third reactor 210c through the carbon dioxide supply pipe 134, the branch pipe 136c, the pipe 240b, and the supply port 230c of the third reactor 210c of the reaction device 110.

[0039] The flow rate adjustment valve 138a is provided in the branch pipe 136a. The flow rate adjustment valve 138a adjusts the opening degree of the flow path formed in the branch pipe 136a. The flow rate adjustment valve 138b is provided in the branch pipe 136b. The flow rate adjustment valve 138b adjusts the opening degree of the flow path formed in the branch pipe 136b. The flow rate adjustment valve 138c is provided in the branch pipe 136c. The flow rate adjustment valve 138c adjusts the opening degree of the flow path formed in the branch pipe 136c. The opening degrees of the flow rate adjustment valves 138a, 138b, and 138c are adjusted by a flow rate control unit 182, which will be described later. The opening degree adjustment process performed by the flow rate control unit 182 will be described in detail later.

[0040] The cooler 150 cools the gas discharged from the outlets 232 a, 232 b of at least one of the reactors 210. The cooler 150 is, for example, a heat exchanger. In this embodiment, the hydrocarbon production apparatus 100 has, for example, three coolers 150 a, 150 b, and 150 c.

[0041] The cooler 150a is provided on the pipe 240a. The cooler 150a cools the gas discharged from the outlet 232a of the first reactor 210a. The gas discharged from the first reactor 210a includes hydrogen, carbon dioxide, methane, and water (gas). The cooler 150b is provided on the pipe 240b. The cooler 150b cools the gas discharged from the outlet 232b of the second reactor 210b. The gas discharged from the second reactor 210b includes hydrogen, carbon dioxide, methane, and water (gas). The cooler 150c is provided on the pipe 240c. The cooler 150c cools the gas discharged from the outlet 232c of the third reactor 210c. The gas discharged from the third reactor 210c includes hydrogen, carbon dioxide, methane, and water (gas).

[0042] The gas-liquid separator 160 separates the mixture of gas and liquid (liquid water) cooled by the cooler 150 into gas and liquid. In this embodiment, the hydrocarbon production apparatus 100 has, for example, three gas-liquid separators 160a, 160b, and 160c.

[0043] Gas-liquid separator 160a is provided on pipe 240a. Gas-liquid separator 160a separates the mixture of gas cooled by cooler 150a and liquid water into gas and liquid. Gas-liquid separator 160b is provided on pipe 240b. Gas-liquid separator 160b separates the mixture of gas cooled by cooler 150b and liquid water into gas and liquid. Gas-liquid separator 160c is provided on pipe 240c. Gas-liquid separator 160c separates the mixture of gas cooled by cooler 150c and liquid water into gas and liquid.

[0044] The temperature adjustment unit 170 maintains the temperature of the reactor 210 of the reaction device 110 within a predetermined reaction temperature range. The reaction temperature range is a temperature range in which the synthesis reaction of hydrogen and carbon dioxide proceeds efficiently and is a temperature range in which deterioration of the catalyst 220 can be suppressed. The reaction temperature range is, for example, 200°C or higher and 550°C or lower, and preferably 300°C or higher and 500°C or lower.

[0045] The temperature adjustment unit 170 circulates a heat medium at a predetermined temperature through, for example, the heat medium container 212 of the first reactor 210a, the heat medium container 212 of the second reactor 210b, and the heat medium container 212 of the third reactor 210c. The temperature adjustment unit 170 includes, for example, a circulation path 172, a pump 174, and a heating / cooling unit 176. The circulation path 172 is a flow path through which the heat medium circulates. The circulation path 172 is provided with the pump 174, the heating / cooling unit 176, the heat medium container 212 of the first reactor 210a, the heat medium container 212 of the second reactor 210b, and the heat medium container 212 of the third reactor 210c in this order. The suction side of the pump 174 is connected to the heat medium container 212 of the third reactor 210c. The discharge side of the pump 174 is connected to the heating / cooling unit 176. When the pump 174 is operated, the heat medium circulates through the circulation path 172. The heating and cooling unit 176 heats or cools the heat medium.

[0046] The central control unit 180 is configured by a semiconductor integrated circuit including a CPU (central processing unit). The central control unit 180 reads out programs, parameters, etc. for operating the CPU from the ROM. The central control unit 180 manages and controls the entire hydrocarbon production apparatus 100 in cooperation with RAM as a work area and other electronic circuits.

[0047] In this embodiment, the central control unit 180 controls the temperature adjustment unit 170 to circulate the heat medium to the first reactor 210 a, the second reactor 210 b, and the third reactor 210 c. The central control unit 180 also controls the hydrogen supply unit 120 to supply a predetermined amount of hydrogen to the reaction device 110. The central control unit 180 also controls the carbon dioxide supply unit 130 to supply a predetermined amount of carbon dioxide to the reaction device 110.

[0048] Furthermore, the central control unit 180 functions as, for example, a flow rate control unit 182. The flow rate control unit 182 controls the flow rates of carbon dioxide supplied to each of the first reactor 210a, the second reactor 210b, and the third reactor 210c by the carbon dioxide supply unit 130, for example, based on the detection values ​​of the temperature sensors T1, T2, and T3. In this embodiment, the flow rate control unit 182 controls the flow rates of carbon dioxide supplied to each of the first reactor 210a, the second reactor 210b, and the third reactor 210c by adjusting the apertures of the flow rate adjustment valves 138a, 138b, and 138c, respectively.

[0049] In this embodiment, the flow control unit 182 adjusts the aperture of each of the flow control valves 138a, 138b, and 138c so that the detected values ​​of the temperature sensor T1 (the temperature of the first reactor 210a), the temperature sensor T2 (the temperature of the second reactor 210b), and the temperature sensor T3 (the temperature of the third reactor 210c) are all within the above-mentioned reaction temperature range, for example, 200°C or higher and 550°C or lower. For example, if the detected value of the temperature sensor T1 (the temperature of the first reactor 210a) is higher than the reaction temperature range, the flow control unit 182 reduces the aperture of the flow control valve 138a. Furthermore, for example, if the detected value of the temperature sensor T1 (the temperature of the first reactor 210a) is lower than the reaction temperature range, the flow control unit 182 increases the aperture of the flow control valve 138a.

[0050] As described above, the hydrocarbon production apparatus 100 according to this embodiment includes the first reactor 210a, the second reactor 210b, the third reactor 210c, the hydrogen supply unit 120 that supplies hydrogen to the first reactor 210a, and the carbon dioxide supply unit 130 that supplies carbon dioxide to the first reactor 210a, the second reactor 210b, and the third reactor 210c.

[0051] In the prior art, hydrogen and carbon dioxide are supplied only to the first reactor 210a at the front stage, and the exothermic reaction proceeds rapidly in the first reactor 210a, causing the temperature of the first reactor 210a to rise too high. As a result, the prior art has a problem in that the catalyst 220 in the first reactor 210a is deteriorated by the heat.

[0052] In contrast, the hydrocarbon production apparatus 100 according to this embodiment divides and supplies carbon dioxide to each of the multiple reactors 210, thereby making it possible to suppress the rapid progress of the exothermic reaction in the first reactor 210a and to prevent the temperature of the first reactor 210a from rising too high. This allows the hydrocarbon production apparatus 100 to maintain an appropriate temperature inside the reactor 110. Therefore, the hydrocarbon production apparatus 100 can prevent the catalyst 220 in the reactor 110 from being deteriorated by heat.

[0053] It is also possible to use a comparative technology in which carbon dioxide is supplied only to the first reactor 210a in the front stage, and hydrogen is divided and supplied to the first reactor 210a, the second reactor 210b, and the third reactor 210c. However, in the comparative technology, the amount of carbon dioxide supplied to the first reactor 210a is greater than in the hydrocarbon production apparatus 100 according to this embodiment. This poses a problem in that the catalyst 220 in the first reactor 210a is oxidized and deteriorated by the carbon dioxide.

[0054] In contrast, the hydrocarbon production apparatus 100 according to this embodiment supplies hydrogen only to the first reactor 210a in the front stage, and splits and supplies carbon dioxide to the first reactor 210a, the second reactor 210b, and the third reactor 210c, so that the amount of carbon dioxide supplied to the first reactor 210a can be made smaller than that of the comparative art. Furthermore, the hydrocarbon production apparatus 100 according to this embodiment can supply a larger amount of hydrogen to the first reactor 210a than that of the comparative art. This makes it possible for the hydrocarbon production apparatus 100 to avoid a situation in which the catalyst 220 in the first reactor 210a is oxidatively deteriorated.

[0055] Furthermore, as shown in the above formulas (1) to (4), in the synthesis reaction from hydrogen and carbon dioxide to hydrocarbons, the number of moles (flow rate) of hydrogen is greater than that of carbon dioxide at a stoichiometric ratio. Therefore, the hydrocarbon production apparatus 100 according to this embodiment divides the carbon dioxide, which has a relatively small flow rate, and supplies it to each reactor 210. By adjusting the flow rate of carbon dioxide supplied to each reactor 210, it is possible to easily control the temperature of each reactor 210. Furthermore, the hydrocarbon production apparatus 100 according to this embodiment supplies the entire amount of hydrogen, which has a relatively large flow rate, to the first reactor 210a, so that the amount of gas that does not contribute to the reaction in the first reactor 210a can be made larger than in the comparative technology. As a result, the hydrocarbon production apparatus 100 according to this embodiment can suppress the increase in reaction heat caused by gas that does not contribute to the reaction more than in the comparative technology.

[0056] Furthermore, as described above, the flow rate control unit 182 controls the flow rate of carbon dioxide based on the temperature of the catalyst 220 housed in the reaction device 110. This allows the hydrocarbon production apparatus 100 to keep the temperatures of the first reactor 210a, the second reactor 210b, and the third reactor 210c all within the reaction temperature range. Therefore, the hydrocarbon production apparatus 100 can shorten the start-up time, prevent further thermal deterioration of the catalyst 220, and prevent a decrease in hydrocarbon production efficiency.

[0057] Specifically, in the startup process for starting up the hydrocarbon production apparatus 100, for example, the flow rate control unit 182 adjusts the aperture of the flow rate control valve 138a so that the stoichiometric ratio between the hydrogen supplied from the hydrogen supply unit 120 to the first reactor 210a and the carbon dioxide supplied from the carbon dioxide supply unit 130 to the first reactor 210a satisfies the above formula (1). The flow rate control unit 182 also adjusts the aperture of the flow rate control valve 138b so that the stoichiometric ratio between the remaining hydrogen supplied from the first reactor 210a to the second reactor 210b and the carbon dioxide supplied from the carbon dioxide supply unit 130 to the second reactor 210b satisfies the above formula (1). The flow rate control unit 182 also adjusts the aperture of the flow rate control valve 138c so that the stoichiometric ratio between the remaining hydrogen supplied from the second reactor 210b to the third reactor 210c and the carbon dioxide supplied from the carbon dioxide supply unit 130 to the third reactor 210c satisfies the above formula (1).

[0058] In this way, the flow rate control unit 182 supplies carbon dioxide to each of the first reactor 210a, the second reactor 210b, and the third reactor 210c in a stoichiometric ratio during the startup process, thereby allowing the exothermic reaction shown in the above formula (1) to proceed efficiently in the first reactor 210a, the second reactor 210b, and the third reactor 210c. Therefore, the hydrocarbon production apparatus 100 can quickly increase the temperatures of the first reactor 210a, the second reactor 210b, and the third reactor 210c.

[0059] On the other hand, in the conventional technology in which carbon dioxide is supplied only to the first reactor 210a, the exothermic reaction shown in the above formula (1) proceeds less in the second reactor 210b and the third reactor 210c than in the first reactor 210a, and the temperature rise rates in the second reactor 210b and the third reactor 210c are lower than in the first reactor 210a. For this reason, the conventional technology in which carbon dioxide is supplied only to the first reactor 210a has a problem in that the start-up times of the first reactor 210a, the second reactor 210b, and the third reactor 210c are longer.

[0060] In contrast to this, the hydrocarbon production apparatus 100 can quickly increase the temperatures of the first reactor 210a, the second reactor 210b, and the third reactor 210c, and therefore can shorten the start-up time of the first reactor 210a, the second reactor 210b, and the third reactor 210c compared to conventional techniques. Furthermore, the hydrocarbon production apparatus 100 does not require a start-up heating mechanism for heating the second reactor 210b and the third reactor 210c, and can reduce the cost of the entire apparatus.

[0061] Furthermore, in a normal operation process in which the hydrocarbon production apparatus 100 is normally operated, for example, the flow rate control unit 182 adjusts the apertures of the flow rate control valves 138a, 138b, and 138c so that the stoichiometric ratio between the hydrogen supplied from the hydrogen supply unit 120 to the first reactor 210a and the total of the carbon dioxide supplied from the carbon dioxide supply unit 130 to the first reactor 210a, the second reactor 210b, and the third reactor 210c satisfies the above formula (1). Furthermore, for example, the flow rate control unit 182 adjusts the apertures of the flow rate control valves 138a, 138b, and 138c so that the amount of carbon dioxide supplied increases in the order of the first reactor 210a, the second reactor 210b, and the third reactor 210c.

[0062] For example, the flow rate control unit 182 adjusts the apertures of the flow rate control valves 138a and 138b so that the amount of carbon dioxide supplied from the carbon dioxide supply unit 130 to the first reactor 210a is less than the amount of carbon dioxide supplied from the carbon dioxide supply unit 130 to the second reactor 210b. Furthermore, for example, the flow rate control unit 182 adjusts the apertures of the flow rate control valves 138b and 138c so that the amount of carbon dioxide supplied from the carbon dioxide supply unit 130 to the second reactor 210b is less than the amount of carbon dioxide supplied from the carbon dioxide supply unit 130 to the third reactor 210c.

[0063] As a result, less carbon dioxide than the stoichiometric ratio is supplied to the first reactor 210a and the second reactor 210b. Therefore, it is possible to prevent the synthesis reaction represented by the above formula (1) from progressing rapidly in the first reactor 210a and the second reactor 210b. As described above, since the synthesis reaction represented by formula (1) is an exothermic reaction, by preventing the synthesis reaction represented by formula (1) from progressing rapidly, it is possible to avoid a situation in which the temperature in the first reactor 210a and the second reactor 210b rises too much. Therefore, the hydrocarbon production apparatus 100 can avoid a situation in which the catalyst 220 in the first reactor 210a and the second reactor 210b is deteriorated by heat. Furthermore, the hydrocarbon production apparatus 100 does not require a dedicated cooling mechanism for cooling the first reactor 210a and the second reactor 210b, making it possible to reduce the cost of the entire apparatus.

[0064] Furthermore, when the hydrogen supply source is a water electrolysis apparatus that electrolyzes water using renewable energy such as solar power generation, the amount of hydrogen supplied by the hydrogen supply unit 120 may fluctuate. In this case, there is a risk that one or more of the first reactor 210a, the second reactor 210b, and the third reactor 210c may fall below the reaction temperature range. Furthermore, there is a risk that the temperature of the heat medium circulating through the first reactor 210a, the second reactor 210b, and the third reactor 210c may fluctuate suddenly, or that the heat medium may flow unevenly. In this case, there is also a risk that one or more of the first reactor 210a, the second reactor 210b, and the third reactor 210c may fall below the reaction temperature range.

[0065] Therefore, in load fluctuation processing in which the amount of hydrogen supplied fluctuates or the heat transfer medium malfunctions, for example, the flow rate control unit 182 adjusts the apertures of the flow rate adjustment valves 138a, 138b, and 138c so as to increase the amount of carbon dioxide supplied to the reactor 210 in which the temperature of the catalyst 220 has fallen below the reaction temperature range. This allows the hydrocarbon production apparatus 100 to increase the temperature of the reactor 210 in which the temperature of the catalyst 220 has fallen below the reaction temperature range. Therefore, the hydrocarbon production apparatus 100 can prevent a decrease in hydrocarbon production efficiency due to a drop in temperature.

[0066] Furthermore, as described above, in the reaction apparatus 110, the distance between the inlet 230a and the supply port 230b, which is the shortest distance from the inlet 230a, may be shorter than the distance between the supply port 230b and the supply port 230c. That is, in the reaction apparatus 110, the distance between the supply port 230b and the supply port 230c may be longer than the distance between the inlet 230a and the supply port 230b, which is the shortest distance from the inlet 230a. That is, the length of the reaction tube 214 of the second reactor 210b may be longer than that of the first reactor 210a. This allows the residence time of gas in the second reactor 210b to be longer than that of the first reactor 210a. Therefore, it is possible to improve the carbon dioxide conversion rate in the second reactor 210b. The carbon dioxide conversion rate is the rate at which carbon dioxide is converted to hydrocarbons.

[0067] Furthermore, as described above, in the reaction apparatus 110, the distance between the outlet 232c and the supply port 230c, which is the shortest distance from the outlet 232c, may be longer than the distance between the supply port 230b and the supply port 230c. That is, the length of the reaction tube 214 of the third reactor 210c may be longer than that of the second reactor 210b. This allows the residence time of the gas in the third reactor 210c to be longer than that in the second reactor 210b. Therefore, it is possible to improve the carbon dioxide conversion rate in the third reactor 210c.

[0068] Furthermore, as described above, the hydrocarbon production apparatus 100 is equipped with the cooler 150. The synthesis reactions of the above formulas (1) to (4) are exothermic reactions, and therefore the reactions proceed more easily at low temperatures than at high temperatures (the carbon dioxide conversion rate is higher). Therefore, by providing the hydrocarbon production apparatus 100 with the cooler 150, it is possible to further promote the progress of the synthesis reactions of the above formulas (1) to (4) in the second reactor 210b and the third reactor 210c.

[0069] Furthermore, as described above, the hydrocarbon production apparatus 100 is equipped with the gas-liquid separator 160. In the synthesis reactions of the above formulas (1) to (4), water is produced. Therefore, due to the equilibrium relationship, the conversion rate of carbon dioxide can be increased by removing water from the produced gas. Therefore, by providing the hydrocarbon production apparatus 100 with the gas-liquid separator 160, it is possible to further promote the progress of the synthesis reactions of the above formulas (1) to (4) in the second reactor 210b and the third reactor 210c.

[0070] [Second embodiment: hydrocarbon production apparatus 300] Figure 2 is a diagram illustrating a hydrocarbon production apparatus 300 according to a second embodiment. As shown in Figure 2, the hydrocarbon production apparatus 300 according to the second embodiment includes a reaction device 110, a hydrogen supply unit 120, a carbon dioxide supply unit 130, a hydrogen supply unit 340, a cooler 150, a gas-liquid separator 160, a temperature adjustment unit 170, and a central control unit 380. In Figure 2, solid arrows indicate the flows of hydrogen (gas), carbon dioxide (gas), hydrocarbons (gas), and water (gas and liquid). Also, dashed arrows in Figure 2 indicate the flow of a heat transfer medium. Note that components that are substantially the same as those in the hydrocarbon production apparatus 300 described above are assigned the same reference numerals, and description thereof will be omitted.

[0071] The hydrogen supply unit 340 (second hydrogen supply unit) supplies hydrogen into the reaction device 110 through the supply ports 230b and 230c of the reaction device 110. That is, the hydrogen supply unit 340 supplies hydrogen into the second reactor 210b through the supply port 230b of the second reactor 210b, and supplies hydrogen into the third reactor 210c through the supply port 230b of the third reactor 210c.

[0072] The hydrogen supply unit 340 includes, for example, a blower 342, a hydrogen supply pipe 344, branch pipes 346b and 346c, and flow rate control valves 348b and 348c. The intake side of the blower 342 is connected to a hydrogen supply source. The discharge side of the blower 342 is connected to the hydrogen supply pipe 344.

[0073] The branch pipe 346b connects the hydrogen supply pipe 344 and the pipe 240a. The hydrogen discharged from the blower 342 is supplied to the second reactor 210b through the hydrogen supply pipe 344, the branch pipe 346b, the pipe 240a, and the supply port 230b of the second reactor 210b of the reaction device 110.

[0074] The branch pipe 346c connects the hydrogen supply pipe 344 and the pipe 240b. The hydrogen discharged from the blower 342 is supplied to the third reactor 210c through the hydrogen supply pipe 344, the branch pipe 346c, the pipe 240b, and the supply port 230c of the third reactor 210c of the reaction device 110.

[0075] Flow rate adjustment valve 348b is provided in branch pipe 346b. Flow rate adjustment valve 348b adjusts the opening degree of the flow path formed in branch pipe 346b. Flow rate adjustment valve 348c is provided in branch pipe 346c. Flow rate adjustment valve 348c adjusts the opening degree of the flow path formed in branch pipe 346c. The opening degrees of flow rate adjustment valves 348b and 348c are adjusted by a flow rate control unit 382, ​​which will be described later.

[0076] The central control unit 380 is configured by a semiconductor integrated circuit including a CPU (central processing unit). The central control unit 380 reads out programs, parameters, etc. for operating the CPU from the ROM. The central control unit 380 manages and controls the entire hydrocarbon production apparatus 300 in cooperation with RAM as a work area and other electronic circuits.

[0077] In this embodiment, similarly to the first embodiment, the central control unit 380 controls the temperature adjustment unit 170 to circulate the heat medium to the first reactor 210a, the second reactor 210b, and the third reactor 210c. The central control unit 380 also controls the hydrogen supply unit 120 to supply a predetermined amount of hydrogen to the reaction device 110. The central control unit 380 also controls the carbon dioxide supply unit 130 to supply a predetermined amount of carbon dioxide to the reaction device 110.

[0078] Furthermore, the central control unit 380 functions as, for example, a flow rate control unit 382. The flow rate control unit 382 controls the flow rate of carbon dioxide supplied to each of the first reactor 210a, the second reactor 210b, and the third reactor 210c by the carbon dioxide supply unit 130 and the flow rate of hydrogen supplied to each of the first reactor 210a, the second reactor 210b, and the third reactor 210c by the hydrogen supply unit 340, for example, based on the detection values ​​of the temperature sensors T1, T2, and T3. In this embodiment, the flow rate control unit 382 controls the flow rate of carbon dioxide and the flow rate of hydrogen supplied to each of the first reactor 210a, the second reactor 210b, and the third reactor 210c by adjusting the apertures of the flow rate adjustment valves 138a, 138b, 138c, 348b, and 348c, respectively.

[0079] In this embodiment, the flow control unit 382 adjusts the opening degree of each of the flow control valves 138a, 138b, 138c, 348b, and 348c so that the detection value of the temperature sensor T1 (the temperature of the first reactor 210a), the detection value of the temperature sensor T2 (the temperature of the second reactor 210b), and the detection value of the temperature sensor T3 (the temperature of the third reactor 210c) are all within the reaction temperature range.

[0080] As described above, the hydrocarbon production apparatus 300 according to this embodiment includes the hydrogen supply unit 340 in addition to the carbon dioxide supply unit 130, and the flow rate control unit 382 controls the flow rate of carbon dioxide supplied by the carbon dioxide supply unit 130 to each of the first reactor 210 a, the second reactor 210 b, and the third reactor 210 c, and the flow rate of hydrogen supplied by the hydrogen supply unit 340 to each of the first reactor 210 a, the second reactor 210 b, and the third reactor 210 c, based on the detection values ​​of the temperature sensors T1, T2, and T3.

[0081] As a result, the hydrocarbon production apparatus 300 according to this embodiment can control the temperatures of the first reactor 210a, the second reactor 210b, and the third reactor 210c with higher precision.

[0082] [Modification: Hydrocarbon Production Apparatus 400] In the first embodiment described above, an example was given in which the reaction apparatus 110 includes a plurality of reactors 210. However, the reaction apparatus 110 may include only one reactor.

[0083] Fig. 3 is a diagram illustrating a hydrocarbon production apparatus 400 according to a modified example. As shown in Fig. 3, the hydrocarbon production apparatus 400 according to the modified example includes a reaction device 410, a hydrogen supply unit 120, a carbon dioxide supply unit 130, a cooler 150, a gas-liquid separator 160, a temperature adjustment unit 170, and a central control unit 180. In Fig. 3, solid arrows indicate the flows of hydrogen (gas), carbon dioxide (gas), hydrocarbons (gas), and water (gas and liquid). Note that components that are substantially the same as those in the hydrocarbon production apparatus 100 described above are denoted by the same reference numerals, and description thereof will be omitted.

[0084] In this embodiment, the reaction device 410 includes one reactor 420 and temperature sensors T1, T2, and T3.

[0085] The reactor 420 is, for example, an adiabatic reactor. The reactor 420 is provided with an inlet 230a, supply ports 230b, 230b, and an outlet 232c in this order. As in the first embodiment, the reactor 420 also contains a catalyst 220.

[0086] In a variant, temperature sensor T1 senses the temperature of a catalyst bed housed in reactor 420 between inlet 230a and feed inlet 230b. Temperature sensor T2 senses the temperature of a catalyst bed housed in reactor 420 between feed inlet 230b and feed inlet 230c. Temperature sensor T3 senses the temperature of a catalyst bed housed in reactor 420 between feed inlet 230c and outlet 232c.

[0087] In the hydrocarbon production apparatus 400 according to the modified example, carbon dioxide is also supplied in divided portions to the inlet 230a and the supply ports 230b and 230c, respectively, so that it is possible to suppress the rapid progress of the exothermic reaction in the reactor 420 and to prevent the temperature in the reactor 420 from rising too much. This makes it possible for the hydrocarbon production apparatus 400 to maintain an appropriate temperature inside the reactor 410. Therefore, it is possible for the hydrocarbon production apparatus 400 to prevent the catalyst 220 in the reactor 410 from being deteriorated by heat.

[0088] [Example] As an example, the temperature of the catalyst layer and the carbon dioxide conversion rate were simulated when methane was produced using a reaction apparatus 110 including a first reactor 210a and a second reactor 210b. In the example, hydrogen and carbon dioxide were supplied from the inlet 230a of the first reactor 210a, and carbon dioxide was supplied from the supply port 230b of the second reactor 210b. In the example, the ratio of hydrogen (moles) supplied from the inlet 230a to the total (moles) of carbon dioxide supplied from the inlet 230a and the supply port 230b was 4:1. The simulation also covered a case where the ratio of carbon dioxide supplied from the inlet 230a to the carbon dioxide supplied from the supply port 230b was 30:70.

[0089] As a comparative example, the temperature of the catalyst layer and the carbon dioxide conversion rate were simulated when methane was produced using a single reactor equipped only with the inlet 230a and the outlet 232c, without any supply port. In the comparative example, hydrogen and carbon dioxide were supplied from the inlet 230a. The simulation was also performed for a hydrogen (mol):carbon dioxide (mol) ratio of 4:1.

[0090] Fig. 4 is a graph showing the simulation results of a comparative example. Fig. 5 is a graph showing the simulation results of the first reactor 210a in the example. Fig. 6 is a graph showing the simulation results of the second reactor 210b in the example. In Figs. 4 to 6, the left vertical axis indicates temperature [°C], and the right vertical axis indicates the carbon dioxide conversion rate. In Figs. 4 to 6, the solid line indicates the temperature of the catalyst layer, and the dashed line indicates the carbon dioxide conversion rate.

[0091] As shown in Fig. 4, it was confirmed that the temperature of the catalyst layer rose to about 700°C in the comparative example. Therefore, it was found that the catalyst layer in the comparative example was deteriorated by heat.

[0092] On the other hand, as shown in Fig. 5, in the example, it was confirmed that the temperature of the catalyst layer in the first reactor 210a rose only to about 430°C. Also, as shown in Fig. 6, in the example, it was confirmed that the temperature of the catalyst layer in the second reactor 210b rose only to about 480°C. Therefore, it was found that the example could suppress thermal deterioration of the catalyst layer.

[0093] 6, it was confirmed that the conversion rate of carbon dioxide in the second reactor 210b in the example was comparable to that in the comparative example. This demonstrates that the example can efficiently convert carbon dioxide into methane while suppressing thermal deterioration of the catalyst layer.

[0094] Although the embodiments have been described above with reference to the accompanying drawings, it goes without saying that the present disclosure is not limited to the above-described embodiments. It is clear that a person skilled in the art can conceive of various modifications or alterations within the scope of the claims, and it is understood that these also naturally fall within the technical scope of the present disclosure.

[0095] For example, in the above first and second embodiments, an example was given in which the hydrocarbon production apparatus 100, 300 is equipped with temperature sensors T1, T2, T3, and the flow rate control units 182, 382 control the flow rates of carbon dioxide supplied to the first reactor 210a, the second reactor 210b, and the third reactor 210c by the carbon dioxide supply unit 130 based on the detected values ​​of the temperature sensors T1, T2, T3. However, the hydrocarbon production apparatus 100, 300 does not have to be equipped with the temperature sensors T1, T2, T3. In this case, a memory (not shown) of the hydrocarbon production apparatus 100, 300 stores information, which is set in advance by simulation or the like, indicating the relationship between the amount of carbon dioxide supplied to the first reactor 210a and the temperature of the catalytic layer of the first reactor 210a, information indicating the relationship between the amount of carbon dioxide supplied to the second reactor 210b and the temperature of the catalytic layer of the second reactor 210b, and information indicating the relationship between the amount of carbon dioxide supplied to the third reactor 210c and the temperature of the catalytic layer of the third reactor 210c. Then, the flow rate control unit 182, 382 refers to the information, stored in the memory, which indicates the relationship between the amount of carbon dioxide supplied to the first reactor 210a and the temperature of the catalytic layer of the first reactor 210a, and adjusts the aperture of the flow rate control valve 138a so that the temperature of the catalytic layer of the first reactor 210a is within the reaction temperature range. Similarly, the flow rate control units 182, 382 refer to information stored in memory indicating the relationship between the amount of carbon dioxide supplied to the second reactor 210b and the temperature of the catalyst layer of the second reactor 210b, and adjust the aperture of the flow rate control valve 138b so that the catalyst layer of the second reactor 210b is within the reaction temperature range. Also, the flow rate control units 182, 382 refer to information stored in memory indicating the relationship between the amount of carbon dioxide supplied to the third reactor 210c and the temperature of the catalyst layer of the third reactor 210c, and adjust the aperture of the flow rate control valve 138c so that the catalyst layer of the third reactor 210c is within the reaction temperature range.

[0096] Furthermore, the flow rate control units 182, 382 may control the flow rate of carbon dioxide supplied by the carbon dioxide supply unit 130 based on the concentration of hydrocarbons contained in the product gas discharged from the pipe 240c. In other words, the flow rate control units 182, 382 may adjust the apertures of the flow rate adjustment valves 138a, 138b, 138c based on the concentration of hydrocarbons contained in the product gas discharged from the pipe 240c. This allows the inside of the reaction device 110 to be maintained at an appropriate temperature.

[0097] The flow rate control units 182 and 382 may also control the flow rate of carbon dioxide to control the temperature of the catalyst layer housed in the reaction device 110 .

[0098] In the first and second embodiments, the reactor 110 of the hydrocarbon production apparatus 100, 300 has two supply ports 230b, 230c. However, the reactor 110 may have one supply port or three or more supply ports. When the reactor 110 has one supply port, the distance between the inlet and the supply port having the shortest distance from the inlet may be shorter than the distance between the outlet and the supply port having the shortest distance from the outlet. When the reactor 110 has three or more supply ports, the distance between adjacent supply ports may increase from the inlet 230a side toward the outlet 232c side. For example, the length of the reaction tube 214 may be increased toward the later stage. This allows the gas residence time to be increased from the inlet 230a toward the outlet 232c, thereby improving the carbon dioxide conversion rate.

[0099] In the above first and second embodiments, the hydrocarbon production apparatuses 100 and 300 are provided with the coolers 150a, 150b, and 150c. However, it is sufficient for the hydrocarbon production apparatuses 100 and 300 to be provided with at least one of the coolers 150a, 150b, and 150c. Furthermore, the hydrocarbon production apparatuses 100 and 300 do not necessarily have to be provided with the cooler 150.

[0100] Similarly, in the above first and second embodiments, the hydrocarbon production apparatuses 100, 300 are provided with the gas-liquid separators 160a, 160b, 160c as an example. However, it is sufficient that the hydrocarbon production apparatuses 100, 300 are provided with at least one gas-liquid separator 160 among the gas-liquid separators 160a, 160b, 160c. Furthermore, the hydrocarbon production apparatuses 100, 300 do not necessarily have to be provided with the gas-liquid separator 160.

[0101] In the first and second embodiments, the reactor 210 is a multi-tubular heat exchanger reactor. However, the reactor 210 may be an adiabatic reactor. In the modified example, the reactor 420 is an adiabatic reactor. However, the reactor 420 may be a multi-tubular heat exchanger reactor.

[0102] Furthermore, in the first and second embodiments, the gas supplied to the reaction device 110 may be replaced with carbon monoxide instead of carbon dioxide. In a catalytic exothermic reaction, carbon monoxide has a higher reactivity with hydrogen than carbon dioxide, and can quickly increase the temperature of the reaction device 110 during startup. Therefore, by replacing the gas supplied to the reaction device 110 from carbon dioxide to carbon monoxide, the startup time can be further shortened.

[0103] Furthermore, in the first and second embodiments, carbon monoxide may be supplied to the reaction device 110 in addition to hydrogen and carbon dioxide. As described above, carbon monoxide is more reactive with hydrogen than carbon dioxide in a catalytic exothermic reaction, and the temperature of the reaction device 110 can be raised quickly during the startup process. Therefore, by supplying mainly carbon monoxide to the reaction device 110 during the startup process and then supplying carbon dioxide after the temperature of the reaction device 110 has been raised, it becomes possible to react carbon dioxide stably and continuously.

[0104] Furthermore, in addition to hydrogen, gases with different combinations of carbon dioxide and carbon monoxide (carbon dioxide only, carbon monoxide only, mixed gas of carbon dioxide and carbon monoxide) may be supplied to each of the multiple reactors 210. In this case, a desired temperature rise rate can be obtained depending on the temperature rise state of each reactor 210, and efficient operation of the reactors 210 becomes possible.

[0105] When hydrogen and carbon monoxide are supplied to the reactor 110, a synthesis reaction between hydrogen and carbon monoxide takes place in the reactor 110 to produce hydrocarbons. The synthesis reaction between hydrogen and carbon monoxide is an exothermic reaction. The synthesis reaction between hydrogen and carbon monoxide is, for example, the reaction shown in the following formulas (5) to (8). 3H ２ + CO → CH ４ + H ２ O... Formula (5) 4H ２ + 2CO → C ２ H ４ + 2H ２ O...Formula (6) 6H ２ + 3CO → C ３ H ６ + 3H ２ O ... Equation (7) mH ２ + nCO → hydrocarbon + nH ２ O...Formula (8)

[0106] The present disclosure can contribute, for example, to Sustainable Development Goal (SDG) Goal 7: "Ensure access to affordable, reliable, sustainable and modern energy" and Goal 13: "Take urgent action to combat climate change and its impacts."

[0107] 100: Hydrocarbon production apparatus 110: Reactor 120: Hydrogen supply section 130: Carbon dioxide supply section 150: Cooler 150a: Cooler 150b: Cooler 182: Flow rate control section 210: Reactor 210a: First reactor 210b: Second reactor 210c: Third reactor 220: Catalyst 230a: Inlet 230b: Supply port 230c: Supply port 232a: Discharge port 232b: Discharge port 232c: Outlet 300: Hydrocarbon production apparatus 340: Hydrogen supply section 382: Flow rate control section 400: Hydrocarbon production apparatus 410: Reactor 420: Reactor

Claims

1. A hydrocarbon production apparatus comprising: a reactor having an inlet, an outlet, and one or more supply ports provided between the inlet and the outlet, and containing a catalyst that promotes an exothermic reaction between hydrogen and carbon dioxide; a first hydrogen supply unit that supplies the hydrogen into the reactor through the inlet of the reactor; and a carbon dioxide supply unit that supplies the carbon dioxide into the reactor through the inlet and the supply port of the reactor.

2. The hydrocarbon production apparatus according to claim 1, further comprising a flow rate control unit that controls the flow rate of the carbon dioxide supplied by the carbon dioxide supply unit.

3. The hydrocarbon production apparatus according to claim 2, wherein the flow rate control unit controls the flow rate of the carbon dioxide based on the temperature of the catalyst housed in the reaction device.

4. A hydrocarbon production apparatus as described in claim 1 or 2, wherein the distance between the inlet and the supply port that is the shortest distance from the inlet is shorter than the distance between the outlet and the supply port that is the shortest distance from the outlet.

5. The hydrocarbon production apparatus according to claim 4, wherein the reaction apparatus has two or more supply ports, the distance between the inlet and the supply port that is the shortest from the inlet is shorter than the distance between adjacent supply ports, and the distance between the outlet and the supply port that is the shortest from the outlet is longer than the distance between adjacent supply ports.

6. The hydrocarbon production apparatus according to claim 5, wherein the reaction apparatus has three or more of the supply ports, and the distance between adjacent supply ports increases from the inlet side toward the outlet side.

7. The hydrocarbon production apparatus according to claim 1 or 2, wherein the reaction device includes a plurality of reactors connected in series, the inlet is provided in the reactor at the front stage, and the outlet is provided in the reactor at the last stage.

8. The hydrocarbon production apparatus according to claim 7, further comprising a cooler for cooling gas discharged from an outlet of at least any one of the plurality of reactors.

9. The hydrocarbon production apparatus according to claim 1 or 2, further comprising a second hydrogen supply unit that supplies the hydrogen into the reactor through the supply port of the reactor.

10. A hydrocarbon production apparatus comprising: a reactor having an inlet, an outlet, and one or more supply ports provided between the inlet and the outlet, and containing a catalyst that promotes an exothermic reaction between hydrogen and carbon monoxide; a first hydrogen supply unit that supplies the hydrogen into the reactor through the inlet of the reactor; and a carbon monoxide supply unit that supplies the carbon monoxide into the reactor through the inlet and the supply port of the reactor.

11. A hydrocarbon production apparatus comprising: a reactor having an inlet, an outlet, and one or more supply ports provided between the inlet and the outlet, and containing a catalyst that promotes an exothermic reaction of hydrogen, carbon monoxide, and carbon dioxide; a first hydrogen supply unit that supplies the hydrogen into the reactor through the inlet of the reactor; a carbon monoxide supply unit that supplies the carbon monoxide into the reactor through the inlet and the supply port of the reactor; and a carbon dioxide supply unit that supplies the carbon dioxide into the reactor through the inlet and the supply port of the reactor.

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