Hydrocarbon production facility, hydrocarbon production system, controller for hydrocarbon production device, and method for producing hydrocarbons

Abstract

In the present invention, hydrocarbon production equipment comprises a first reaction device that generates a first intermediate gas by accepting a raw material gas and reacting the raw material gas using a catalyst, a second reaction device that generates a second intermediate gas by reacting the first intermediate gas using a catalyst, a heat supplier with which heat for heating the catalyst can be supplied to a reactor and with which heat for heating the catalyst can be supplied to a reactor, and a controller for controlling the operation of the heat supplier. The controller selectively outputs to the heat supplier a first control signal that causes heat to be supplied to each of the first reaction device and the second reaction device or a second control signal that causes heat to be supplied to only one of the first reaction device and the second reaction device. The controller selects either the first control signal or the second control signal on the basis of the amount of hydrogen contained in the raw material gas.

Description

[Technical field]

[0001] The present disclosure relates to a hydrocarbon production facility, a hydrocarbon production system, a controller for a hydrocarbon production apparatus, and a method for producing hydrocarbons. [Background technology]

[0002] In recent years, the use of renewable energy has been increasing. There is a technology that converts surplus electricity generated by renewable energy into an energy medium other than electricity and stores the energy medium. For example, water electrolysis technology uses surplus electricity to generate hydrogen as an energy medium. By storing hydrogen, it is possible to store surplus electricity. In addition to technology for using stored hydrogen alone, there is also active development of technology for converting hydrogen into a form that is easy to transport or use.

[0003] The energy medium is not limited to hydrogen. For example, hydrocarbons and ammonia can also be used as energy mediums. Technology for producing hydrocarbons and ammonia using hydrogen as a raw material has been attracting attention. Hydrocarbons use hydrogen and carbon dioxide as raw materials. Therefore, it is advantageous in that carbon dioxide is effectively utilized. For example, Patent Document 1 discloses a technology for producing methane using hydrogen and carbon dioxide. The device of Patent Document 1 produces hydrogen using a water electrolysis device that uses renewable energy. The device of Patent Document 1 omits some of the reaction steps when a load fluctuation occurs. As a result, the reaction state in each step is adjusted to be in equilibrium. [Prior art documents] [Patent documents]

[0004] [Patent Document 1] JP 2018-135283 A Summary of the Invention [Problem to be solved by the invention]

[0005] When a raw material gas containing hydrogen is used to generate a gas containing a hydrocarbon, a certain amount of energy is required to cause a reaction. For example, when generating a hydrocarbon using hydrogen and carbon dioxide, a catalyst for causing the reaction must be maintained at a certain temperature. When a sufficient amount of raw material gas is supplied, the temperature of the catalyst can be maintained by the heat generated by the reaction. However, when a sufficient amount of raw material gas is not supplied, energy must be supplied from the outside to maintain the temperature of the catalyst.

[0006] In solar power generation and wind power generation that use renewable energy, the output power is prone to fluctuation. Therefore, water electrolysis devices that operate by receiving power from power generation facilities that use renewable energy are also prone to output fluctuation. As a result, when the amount of hydrogen output by the water electrolysis device is insufficient, it is necessary to supply the energy required for the reaction from an external source, as described above. Therefore, a situation may arise in which it is difficult to improve the overall energy efficiency.

[0007] The present disclosure describes a hydrocarbon production facility, a hydrocarbon production system, a controller for a hydrocarbon production apparatus, and a method for producing hydrocarbons that allows for improved energy efficiency. [Means for solving the problem]

[0008] A hydrocarbon production facility according to one embodiment of the present disclosure includes a first reactor that receives a raw material gas containing hydrogen and carbon and reacts the raw material gas using a first catalyst heated to a predetermined temperature to generate a first intermediate gas containing hydrocarbons, a second reactor that reacts the first intermediate gas using a second catalyst heated to a predetermined temperature to generate a second intermediate gas containing hydrocarbons, a heat supplier that can supply heat to the first reactor for heating the first catalyst and can supply heat to the second reactor for heating the second catalyst, and a controller that controls the operation of the heat supplier. The controller selectively outputs to the heat supplier a first control signal that causes each of the first reactor and the second reactor to supply heat, and a second control signal that causes only one of the first reactor and the second reactor to supply heat. The controller selects either the first control signal or the second control signal based on the amount of hydrogen contained in the raw material gas. Effect of the Invention

[0009] The above-mentioned hydrocarbon production facility, hydrocarbon production system, controller for a hydrocarbon production apparatus, and method for producing hydrocarbons can improve energy efficiency in producing hydrocarbons. [Brief description of the drawings]

[0010] [Figure 1] FIG. 1 is a diagram illustrating a hydrocarbon production system. [Diagram 2] FIG. 2 is a diagram showing the structure of the reactor. [Diagram 3] FIG. 3 is a diagram illustrating a configuration of the controller. [Figure 4] FIG. 4 is a flow diagram showing the operation of the controller. [Diagram 5] FIG. 5 is a diagram showing a hydrocarbon production apparatus according to the embodiment. [Figure 6] FIG. 6 is a diagram showing a reaction device provided in a modified example of a hydrocarbon production apparatus. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0011] A hydrocarbon production facility according to one embodiment of the present disclosure includes a first reactor that receives a raw material gas containing hydrogen and carbon and reacts the raw material gas using a first catalyst heated to a predetermined temperature to generate a first intermediate gas containing hydrocarbons, a second reactor that reacts the first intermediate gas using a second catalyst heated to a predetermined temperature to generate a second intermediate gas containing hydrocarbons, a heat supplier that can supply heat to the first reactor for heating the first catalyst and can supply heat to the second reactor for heating the second catalyst, and a controller that controls the operation of the heat supplier. The controller selectively outputs to the heat supplier a first control signal that causes each of the first reactor and the second reactor to supply heat, and a second control signal that causes only one of the first reactor and the second reactor to supply heat. The controller selects either the first control signal or the second control signal based on the amount of hydrogen contained in the raw material gas.

[0012] When the amount of hydrogen supplied to the hydrocarbon production facility is small, the amount of heat generated by the reaction is also small. As a result, it is necessary to heat the first catalyst and the second catalyst to a temperature required to cause the reaction. The hydrocarbon production facility switches between a mode in which the heat medium is supplied to both the first reactor and the second reactor and a mode in which the heat medium is supplied only to one of the first reactor and the second reactor, based on the amount of hydrogen contained in the raw material gas. As a result, when the amount of hydrogen supplied to the hydrocarbon production facility is small, the amount of heat to be supplied to maintain the reaction can be reduced by switching to a mode in which the heat medium is supplied only to one of the first reactor and the second reactor. Therefore, the hydrocarbon production facility can improve the energy efficiency in the operation of generating a gas containing hydrocarbons from the raw material gas.

[0013] The heat supplier of the above-mentioned hydrocarbon production facility may have a heat medium passage section through which the heat medium supplied to the first reaction device and the second reaction device flows, and a heat control section that performs heat exchange with the heat medium. The heat medium passage section may include a first heat medium passage connected to the first reaction device, a second heat medium passage connecting the first reaction device to the second reaction device, and a third heat medium passage connected to the second reaction device. According to this configuration, the heat medium that has received heat supply in the heat control section is supplied to the first reaction device and the second reaction device. As a result, the amount of heat required for the reaction can be provided to the first catalyst and the second catalyst.

[0014] The heat medium passage section of the above-mentioned hydrocarbon production facility may have a heat medium bypass passage connecting the second heat medium passage to the third heat medium passage, and a heat medium switching section for switching between a mode in which the heat medium is supplied to the second reaction device upon receiving a first control signal and a mode in which the heat medium is supplied to the heat medium bypass passage without being supplied to the second reaction device upon receiving a second control signal. With this configuration, switching between a mode in which the heat medium is supplied to the second reaction device and a mode in which the heat medium is not supplied to the second reaction device can be realized with a simple configuration.

[0015] The above-mentioned hydrocarbon production facility may further include a first gas flow passage connected to the first reactor, a second gas flow passage connecting the first reactor to the second reactor, a third gas flow passage connected to the second reactor, a gas bypass flow passage connecting the second gas flow passage to the third gas flow passage, and a gas switching unit that switches between a mode in which the first intermediate gas is supplied to the second reactor upon receiving a first control signal and a mode in which the first intermediate gas is supplied to the gas bypass flow passage without being supplied to the second reactor upon receiving a second control signal. With this configuration, it is possible to realize a simple configuration to switch between a mode in which the first intermediate gas is supplied to the second reactor and a mode in which the first intermediate gas is not supplied to the second reactor.

[0016] The controller of the above-mentioned hydrocarbon production facility may include a hydrogen amount acquisition unit that acquires data on the amount of hydrogen contained in the raw material gas, a heat amount comparison unit that compares a reaction heat amount including the amount of heat generated by the reaction in the first reactor and the amount of heat generated by the reaction in the second reactor with a required amount of heat required to maintain the reaction in the first reactor and the reaction in the second reactor when the raw material gas containing the amount of hydrogen indicated by the data on the amount of hydrogen is received, and a signal output unit that outputs a second control signal to the heat supplier when the reaction heat amount is smaller than the required amount of heat. This controller makes it easy to determine a state in which heat should be supplied to only one of the first reactor and the second reactor.

[0017] The first reaction device of the above-mentioned hydrocarbon production facility may include at least two reactors connected in parallel to each other. With this configuration, the amount of the first intermediate gas generated can be increased.

[0018] A hydrocarbon production system according to another embodiment of the present disclosure includes a hydrogen supply facility that outputs hydrogen, and a hydrocarbon production facility that receives a raw gas containing hydrogen and carbon and generates a gas containing hydrocarbon. The hydrocarbon production facility includes a first reactor that receives a raw gas containing hydrogen and carbon and generates a first intermediate gas containing hydrocarbon by reacting the raw gas using a first catalyst heated to a predetermined temperature, a second reactor that generates a second intermediate gas containing hydrocarbon by reacting the first intermediate gas using a second catalyst heated to a predetermined temperature, a heat supplier that supplies heat to the first reactor and heat to the second reactor for heating the second catalyst, and a controller that controls the operation of the heat supplier. The controller selectively outputs to the heat supplier a first control signal that causes each of the first reactor and the second reactor to supply heat, and a second control signal that causes only one of the first reactor and the second reactor to supply heat. The controller selects either the first control signal or the second control signal based on the amount of hydrogen contained in the raw gas.

[0019] The hydrocarbon production system includes the above-mentioned hydrocarbon production equipment, and therefore, it is possible to improve the energy efficiency in the operation of generating a gas containing hydrocarbons from a raw material gas.

[0020] A controller for a hydrocarbon production apparatus according to yet another embodiment of the present disclosure includes a first reactor that receives a raw material gas containing hydrogen and carbon and generates a first intermediate gas containing hydrocarbons by reacting the raw material gas using a first catalyst heated to a predetermined temperature, and a second reactor that generates a second intermediate gas containing hydrocarbons by reacting the first intermediate gas using a second catalyst heated to a predetermined temperature. The controller of the hydrocarbon production apparatus has a hydrogen amount acquisition unit that acquires data on the amount of hydrogen contained in the raw material gas, a heat amount comparison unit that compares a reaction heat amount including the amount of heat generated by the reaction in the first reactor and the amount of heat generated by the reaction in the second reactor with a required amount of heat required to maintain the reaction in the first reactor and the reaction in the second reactor when the hydrocarbon production apparatus receives a raw material gas containing hydrogen in an amount indicated by the data on the amount of hydrogen, and a signal output unit that outputs a control signal to a heat supplier that supplies heat to the first reactor for heating the first catalyst and is capable of supplying heat to the second reactor for heating the second catalyst, to only one of the first reactor and the second reactor when the reaction heat amount is smaller than the required amount of heat.

[0021] The controller of the hydrocarbon production apparatus can determine the target to which the heat medium is provided based on the amount of hydrogen contained in the feed gas supplied to the hydrocarbon production apparatus. Therefore, the controller of the hydrocarbon production apparatus can improve the energy efficiency of the operation of generating a gas containing hydrocarbons from the feed gas performed by the hydrocarbon production apparatus.

[0022] A method for producing hydrocarbons using a hydrocarbon production apparatus according to yet another embodiment of the present disclosure includes a first reactor that receives a raw material gas containing hydrogen and carbon and reacts the raw material gas using a first catalyst heated to a predetermined temperature to generate a first intermediate gas containing hydrocarbons, and a second reactor that reacts the first intermediate gas using a second catalyst heated to a predetermined temperature to generate a second intermediate gas containing hydrocarbons. The method for producing hydrocarbons using the hydrocarbon production apparatus includes the steps of: obtaining data on the amount of hydrogen contained in the raw material gas; comparing a reaction heat amount, including the amount of heat generated by the reaction in the first reactor and the amount of heat generated by the reaction in the second reactor, with a required amount of heat required to maintain the reaction in the first reactor and the reaction in the second reactor, when the raw material gas containing hydrogen in an amount indicated by the data on the amount of hydrogen, received by the hydrocarbon production apparatus; and outputting a control signal to a heat supplier that supplies heat to the first reactor for heating the first catalyst and supplies heat to the second reactor for heating the second catalyst, to supply heat to only one of the first reactor and the second reactor, when the reaction heat amount is smaller than the required amount of heat.

[0023] The method for producing hydrocarbons determines a target to which a heat medium is provided based on the amount of hydrogen contained in the raw material gas supplied to the hydrocarbon production apparatus. Therefore, the method for producing hydrocarbons can improve the energy efficiency of the operation of generating a gas containing hydrocarbons from the raw material gas performed by the hydrocarbon production apparatus.

[0024] Hereinafter, the hydrocarbon production facility, the hydrocarbon production system, the controller of the hydrocarbon production apparatus, and the method of producing hydrocarbons of the present disclosure will be described in detail with reference to the drawings. In addition, in the description of the drawings, the same elements and corresponding elements are given the same reference numerals. In addition, duplicated descriptions may be omitted.

[0025] As shown in Fig. 1, a hydrocarbon production facility 1 receives a supply of a raw material gas. The hydrocarbon production facility 1 reacts the raw material gas using a catalyst. As a result, the hydrocarbon production facility 1 produces a product gas.

[0026] The feed gas includes hydrogen gas and carbon dioxide gas. The feed gas may include carbon monoxide gas instead of carbon dioxide gas. The hydrocarbon production facility 1 may have an input 1a for receiving hydrogen gas and an input 1b for receiving carbon dioxide gas. The hydrocarbon production facility 1 may have an input for receiving a feed gas in which hydrogen gas and carbon dioxide gas are mixed.

[0027] The product gas contains hydrocarbons. The hydrocarbon production facility 1 outputs the product gas from an output 1c.

[0028] The hydrocarbon production facility 1 receives a supply of hydrogen gas from, for example, a water electrolysis device 101 (hydrogen supply facility). The water electrolysis device 101 receives electric power. The water electrolysis device 101 generates hydrogen from water. The electric power consumed by the water electrolysis device 101 is purchased, for example, from an electric power company 105. The electric power consumed by the water electrolysis device 101 is supplied from a renewable energy facility 102. An example of the renewable energy facility 102 is a solar power generation facility that uses solar light, which is a renewable energy. An example of the renewable energy facility 102 is a wind power generation facility that uses wind power, which is a renewable energy. A solar power generation facility and a wind power generation facility are examples of the renewable energy facility 102. The power generation facility constituting the renewable energy facility 102 may be a facility that generates electric power using other renewable energy.

[0029] When generating electricity using solar or wind power, the amount of electricity generated varies depending on the weather and the time of day. For example, solar power generation facilities cannot generate electricity at night in the first place. The amount of electricity generated by solar power generation facilities drops significantly during bad weather. Hydrogen is sometimes produced by the water electrolysis apparatus 101 using surplus electricity. For these reasons, the electricity supplied to the water electrolysis apparatus 101 is prone to fluctuation, and as a result, the amount of hydrogen output by the water electrolysis apparatus 101 is also prone to fluctuation. As a result, there are times when a sufficient amount of hydrogen gas cannot be supplied to the hydrocarbon production facility 1.

[0030] An example of the water electrolysis apparatus 101 is an alkaline water electrolysis apparatus. The alkaline water electrolysis apparatus may have a minimum load power determined for operational reasons. The alkaline water electrolysis apparatus needs to be supplied with power required for low-load operation. For example, when power cannot be supplied from the renewable energy facility 102, the alkaline water electrolysis apparatus may be supplied with power from a storage battery. The alkaline water electrolysis apparatus may also be supplied with power purchased from a power company 105.

[0031] The hydrocarbon production facility 1 further receives a supply of hydrogen gas from a hydrogen storage facility 103 (hydrogen supply facility). The hydrogen stored in the hydrogen storage facility 103 may be surplus hydrogen output by the water electrolysis device 101. The hydrogen stored in the hydrogen storage facility 103 may be hydrogen transported from an external source.

[0032] The hydrocarbon production facility 1 is supplied with carbon dioxide gas. The carbon dioxide gas is, for example, supplied from a carbon dioxide capture facility 104. The hydrocarbon production facility 1 receives carbon dioxide gas from an input 1b.

[0033] A configuration including the hydrocarbon production facility 1 and at least one of the water electrolysis device 101 or the hydrogen storage facility 103 is referred to as a hydrocarbon production system 100. The hydrocarbon production system 100 may also include the other of the water electrolysis device 101 or the hydrogen storage facility 103, and a carbon dioxide recovery facility 104. In short, the hydrocarbon production system 100 refers to a system including the hydrocarbon production facility 1 and a facility for supplying raw materials to the hydrocarbon production facility 1.

[0034] The hydrocarbon production facility 1 has a hydrocarbon production apparatus 2 and a controller 3 (controller). The hydrocarbon production apparatus 2 produces a product gas from a raw material gas. The controller 3 controls the hydrocarbon production apparatus 2. The controller 3 may be connected to the hydrocarbon production apparatus 2 so as to be able to transmit a control signal θ to the hydrocarbon production apparatus 2. The control signal θ may be transmitted by wired communication. The control signal θ may be transmitted by wireless communication. The controller 3 may be disposed in the vicinity of the hydrocarbon production apparatus 2. The controller 3 may be disposed away from the hydrocarbon production apparatus 2. Details of the controller 3 will be described later.

[0035] The hydrocarbon production apparatus 2 has a first reactor 21S, a second reactor 22S, a third reactor 23S, and a heat supplier 24. The first reactor 21S includes one reactor 21. Similarly, the second reactor 22S also includes one reactor 22. The third reactor 23S also includes one reactor 23. The reactor of the present disclosure includes one reactor. The number of reactors constituting the reactor is not limited to one. The reactor may be composed of at least two reactors. Modified examples of the reactor will be described later.

[0036] The first reactor 21S, the second reactor 22S, and the third reactor 23S react the raw material gas with a catalyst to generate a gas containing hydrocarbons. The first reactor 21S, the second reactor 22S, and the third reactor 23S are connected to each other by a plurality of gas pipes.

[0037] Schematically, the first reactor 21S, the second reactor 22S, and the third reactor 23S are connected in series in this order. The first reactor 21S receives hydrogen gas from the input 1a and carbon dioxide gas from the input 1b. The first reactor 21S provides the first intermediate gas generated as a result to the second reactor 22S. The second reactor 22S receives the first intermediate gas. The second reactor 22S generates a second intermediate gas from the first intermediate gas. The second intermediate gas has a higher proportion of hydrocarbons than the first intermediate gas. The second reactor 22S provides the second intermediate gas to the third reactor 23S. The third reactor 23S receives the second intermediate gas. The third reactor 23S generates a product gas from the second intermediate gas. The product gas has a higher proportion of hydrocarbons than the second intermediate gas. Finally, the third reactor 23S provides the product gas to the outside from the output 1c.

[0038] The above gas flows are realized by the gas flow passage section 25. The gas flow passage section 25 includes a first gas pipe 251 (first gas flow passage), a second gas pipe 252 (second gas flow passage), a third gas pipe 253 (third gas flow passage), and a fourth gas pipe 254. The first gas pipe 251 connects the input 1a and the input 1b to the first reactor 21S. The second gas pipe 252 connects the first reactor 21S to the second reactor 22S. The third gas pipe 253 connects the second reactor 22S to the third reactor 23S. The fourth gas pipe 254 connects the third reactor 23S to the output 1c.

[0039] The first reactor 21S, the second reactor 22S, and the third reactor 23S have differences in performance such as the capacity of gas that can be received, but basically have the same structure. The first reactor 21S synthesizes hydrocarbons using hydrogen gas and carbon dioxide gas as raw materials. An example of a reaction for synthesizing a hydrocarbon compound from carbon dioxide is methanation shown in formula (1). An example of a reaction for synthesizing a hydrocarbon compound from carbon dioxide is FT synthesis shown in formula (2). CO2+4H2→CH4+2H2O…(1) nCO2+3nH2→-(CH2)-n+2nH2O…(2)

[0040] Methanation and FT synthesis generally use a catalyst and react at high temperatures of 200°C or higher. Since a catalyst that is active at high temperatures is used, it is necessary to preheat the catalyst to a high temperature using a heat transfer medium (HM). Examples of heat transfer mediums (HM) include oil, steam, and molten salt. When the catalyst is heated to the temperature required for the reaction, if heating with a heat transfer medium (HM) is used, it takes several hours to about 24 hours, depending on the capacity of the hydrocarbon reactor. Therefore, after the catalyst is heated to the temperature required for the reaction, it is common to maintain it at a high temperature.

[0041] 2 is an example of the internal structure of the reactor 21 included in the first reaction device 21S. The reactor 21 has a shell 211, a plurality of tubes 212, and a buffer 213. The shell 211 constitutes the outer shell of the reactor 21. The shell 211 has a gas inlet 211a, a gas outlet 211b, a heat medium inlet 211c, and a heat medium outlet 211d.

[0042] The gas inlet 211a is connected to the gas outlet 211b by a plurality of tubes 212. A catalyst CT (first catalyst) is disposed inside the tube 212. When the raw material gas passes through the catalyst CT disposed in the tube 212, a reaction occurs. As a result, a gas containing hydrocarbons is produced. The heat medium inlet 211c is connected to the heat medium outlet 211d via a space surrounded by the shell 211, the tubes 212, and the partition wall 215. The region where the gas flows and the region where the heat medium HM flows are separated by the tubes 212 and the partition wall 215.

[0043] The heat medium HM flows from the heat medium inlet 211c to the heat medium outlet 211d while contacting the outer circumferential surface of the tube 212. In the process of flowing from the heat medium inlet 211c to the heat medium outlet 211d, heat exchange between the heat medium HM and the catalyst CT occurs through the outer circumferential surface of the tube 212. The heat exchange includes a mode in which heat is transferred from the heat medium HM to the catalyst CT. The heat exchange also includes a mode in which heat is transferred from the catalyst CT to the heat medium HM. For example, oil at 300 degrees Celsius to 330 degrees Celsius is supplied from the heat medium inlet 211c. In the mode in which heat is transferred from the heat medium HM to the catalyst CT, the temperature of the oil discharged from the heat medium outlet 211d is lower than the temperature of the oil flowing into the heat medium inlet 211c. In the mode in which heat is transferred from the catalyst CT to the heat medium HM, the temperature of the oil discharged from the heat medium outlet 211d is higher than the temperature of the oil flowing into the heat medium inlet 211c.

[0044] Referring again to FIG. 1, the heat supplier 24 supplies the heat medium HM to each of the first reaction device 21S, the second reaction device 22S, and the third reaction device 23S. The amount of heat generated in the first reaction device 21S, the second reaction device 22S, and the third reaction device 23S increases or decreases depending on the state of the reaction. For example, when the amount of heat generated is small, the heat medium HM supplies heat to each catalyst CT equipped in the first reaction device 21S, the second reaction device 22S, and the third reaction device 23S. For example, when the amount of heat generated is large, the heat medium HM removes heat from each catalyst CT. By circulating the heat medium HM, the catalyst CT equipped in the first reaction device 21S, the second reaction device 22S, and the third reaction device 23S can be maintained at a predetermined temperature.

[0045] The heat supplier 24 has a heat control device 241 (heat control unit) and a heat medium passage unit 242. The heat supplier 24 is allowed to include components other than the heat control device 241 and the heat medium passage unit 242.

[0046] The heat control device 241 has a function of providing heat to the heat medium HM and a function of removing heat from the heat medium HM. The heat control device 241 may include a heater 241a for providing heat to the heat medium HM. The heat control device 241 may include a heat exchanger 241b for removing heat from the heat medium HM. For example, the heat exchanger 241b may be a cooler. The heat control device 241 may include a pump 241c for moving the heat medium HM. For example, as shown in FIG. 1, the heat exchanger 241b, the pump 241c, and the heater 241a may be connected in this order along the direction in which the heat medium HM flows. Both the methanation shown in the above formula (1) and the FT reaction shown in the formula (2) are exothermic reactions. When the reaction starts, the temperature of the catalyst CT rises rapidly. Therefore, it is necessary to control the temperature so that the temperature of the catalyst CT falls within a predetermined range by removing the amount of heat generated. The thermal control device 241 can also be used for thermal control to keep the temperature of the catalyst CT within a predetermined range.

[0047] The heat medium flow passage section 242 has a first heat medium pipe 242a (first heat medium flow passage), a second heat medium pipe 242b (second heat medium flow passage), a third heat medium pipe 242c (third heat medium flow passage), and a fourth heat medium pipe 242d. These pipes allow the heat medium HM to flow through a closed flow passage. The first heat medium pipe 242a connects the first reaction device 21S to the heat control device 241. The second heat medium pipe 242b connects the first reaction device 21S to the second reaction device 22S. The third heat medium pipe 242c connects the second reaction device 22S to the third reaction device 23S. The fourth heat medium pipe 242d connects the heat control device 241 to the third reaction device 23S. The heat medium HM flows in the order of the third reaction device 23S, the second reaction device 22S, and the first reaction device 21S. In other words, the direction in which the heat medium HM flows is opposite to the direction in which the gas flows.

[0048] The hydrocarbon production apparatus 2 basically generates product gas by three reactors. The hydrocarbon production apparatus 2 can also generate product gas by two reactors, if necessary. In the example of FIG. 1, the hydrocarbon production apparatus 2 can generate product gas by the first reactor 21S, the second reactor 22S, and the third reactor 23S. The hydrocarbon production apparatus 2 can also generate product gas by the first reactor 21S and the third reactor 23S. In generating product gas, the hydrocarbon production apparatus 2 can select a state in which the second reactor 22S is used and a state in which the second reactor 22S is not used. The state in which the second reactor 22S is used means, in other words, a state in which the temperature of the catalyst CT (second catalyst) of the second reactor 22S is maintained in a state in which a reaction is possible. The state in which the second reactor 22S is not used means, in other words, a state in which the temperature of the catalyst CT of the second reactor 22S is not maintained in a state in which a reaction is possible.

[0049] The temperature of the catalyst CT of the second reaction device 22S is determined by the amount of heat generated by the reaction and the amount of heat supplied by the heat medium HM. The temperature of the catalyst CT of the second reaction device 22S is determined by the amount of heat generated by the reaction and the amount of heat taken away by the heat medium HM. For example, if the amount of heat generated by the reaction is small and the supply of heat by the heat medium HM is stopped, the temperature of the catalyst CT of the second reaction device 22S cannot be maintained. If the supply of heat by the heat medium HM is stopped, the second reaction device 22S can be put into a state where it is not used. The heat medium passage section 242 has a configuration that switches between supplying and stopping the supply of the heat medium HM to the second reaction device 22S. Specifically, the heat medium passage section 242 has a heat medium bypass piping 242P (heat medium bypass passage) and a heat medium switching device 242S (heat medium switching section).

[0050] The heat medium bypass pipe 242P connects the third heat medium pipe 242c to the second heat medium pipe 242b. Specifically, a first end of the heat medium bypass pipe 242P is connected to the second heat medium pipe 242b. A second end of the heat medium bypass pipe 242P is connected to the third heat medium pipe 242c. A heat medium switch 242S is provided at the second end of the heat medium bypass pipe 242P. The heat medium switch 242S switches between a configuration in which the heat medium HM provided from the third reaction device 23S is supplied to the second reaction device 22S and a configuration in which the heat medium HM is supplied to the heat medium bypass pipe 242P. The switching operation of the heat medium switch 242S follows a control signal θ of the controller 3. The heat medium switch 242S may be composed of two valves, for example, as shown in FIG. 5. When the heat medium HM flows through the heat medium bypass pipe 242P, the heat medium HM is not supplied to the second reaction device 22S.

[0051] The hydrocarbon production apparatus 2 may have a configuration for bypassing the gas in addition to the configuration for bypassing the heat medium HM. The gas flow passage section 25 may have a gas bypass pipe 25P (gas bypass flow passage) and a gas switch 25S (gas switching section).

[0052] The gas bypass pipe 25P connects the second gas pipe 252 to the third gas pipe 253. Specifically, a first end of the gas bypass pipe 25P is connected to the second gas pipe 252. A second end of the gas bypass pipe 25P is connected to the third gas pipe 253. A gas switch 25S is provided at the first end of the gas bypass pipe 25P. The gas switch 25S switches between a configuration in which the first intermediate gas generated in the first reaction device 21S is supplied to the second reaction device 22S and a configuration in which the first intermediate gas is supplied to the gas bypass pipe 25P. The switching operation of the gas switch 25S follows a control signal θ of the controller 3. For example, when the first intermediate gas flows through the gas bypass pipe 25P, the first intermediate gas is not supplied to the second reaction device 22S.

[0053] The controller 3 outputs a control signal θ for switching between a state in which the second reaction device 22S is used and a state in which the second reaction device 22S is not used. The controller 3 outputs a first control signal θ when the second reaction device 22S is used. The controller 3 outputs a first control signal θ when the heat medium HM and gas are supplied to the second reaction device 22S. The controller 3 outputs a second control signal θ when the second reaction device 22S is not used. The controller 3 outputs the second control signal θ when the heat medium HM and gas are not supplied to the second reaction device 22S.

[0054] The controller 3 is realized by a computer having the hardware configuration shown in Fig. 3. The controller 3 includes one or more computers. The computer has a processor 31, a main memory unit 32, an auxiliary memory unit 33, a communication control unit 34, an input device 35, and an output device 36. The controller 3 is configured by one or more computers configured by these hardware units and software such as programs.

[0055] When the controller 3 is composed of multiple computers, these computers may be connected locally. The multiple computers may be connected to each other via a communication network such as the Internet or an intranet. This connection logically constitutes one controller 3.

[0056] The processor 31 executes an operating system and application programs, etc. The main memory 32 is composed of a ROM (Read Only Memory) and a RAM (Random Access Memory). The auxiliary memory 33 is a storage medium composed of a hard disk, a flash memory, etc. The auxiliary memory 33 generally stores a larger amount of data than the main memory 32. The communication control unit 34 is composed of a network card or a wireless communication module. The auxiliary memory 33 generally stores a larger amount of data than the main memory 32. The input device 35 is composed of a keyboard, a mouse, a touch panel, a microphone for voice input, etc. The output device 36 is composed of a display, a printer, etc.

[0057] The auxiliary storage unit 33 stores in advance a program and data necessary for processing. The program causes the computer to execute each functional element of the controller 3. The program causes the computer to execute processing related to, for example, a method for producing hydrocarbons. For example, the program is read by the processor 31 or the main storage unit 32, and causes at least one of the processor 31, the main storage unit 32, the auxiliary storage unit 33, the communication control unit 34, the input device 35, and the output device 36 to operate. For example, the program executes reading and writing of data in the main storage unit 32 and the auxiliary storage unit 33.

[0058] The program may be provided in a form recorded on a tangible storage medium such as a CD-ROM, a DVD-ROM, a semiconductor memory, etc. The program may be provided as a data signal via a communication network.

[0059] Fig. 4 is a flow diagram showing the operation of the controller 3. According to the flow of Fig. 4, it is possible to select whether to output the first control signal θ or the second control signal θ.

[0060] The controller 3 acquires data (variable X) indicating the amount of hydrogen gas contained in the raw material gas (step S101). The amount of hydrogen gas is expressed, for example, as a volumetric flow rate (m3 / s). The configuration in which the controller 3 acquires the flow rate data φ (variable X) is not particularly limited. For example, the controller 3 may acquire the flow rate data φ from the flow sensor 106 (see FIG. 1).

[0061] Next, the controller 3 compares the amounts of heat. The operation of comparing the amounts of heat includes an operation of obtaining the amount of reaction heat (step S102) and an operation of comparing the amount of reaction heat with the required amount of heat (step S103). The controller 3 outputs a control signal θ for switching between a state in which the second reaction device 22S is used and a state in which the second reaction device 22S is not used. The controller 3 selects the control signal θ based on the amount of heat generated by the reaction and the amount of heat (variable Y) required to maintain the reaction.

[0062] For example, when the amount of heat generated by the reaction is not less than the amount of heat (variable Y) required to maintain the reaction, the raw material gas is being supplied sufficiently. Therefore, there is no need to stop the second reaction device 22S. When the amount of heat generated by the reaction is sufficient, the temperature of the hydrocarbon reactor can be maintained by the reaction heat alone. This state is a so-called thermally independent state in which no heat supply is required. When in a thermally independent state, the energy consumed by the hydrocarbon production apparatus 2 is only the operating power, such as the energy for driving the pump 591 (see FIG. 5) that circulates the heat medium HM.

[0063] For example, when the amount of heat generated by the reaction is less than the amount of heat (variable Y) required to maintain the reaction, the raw material gas is not being supplied sufficiently. In such a situation, the reaction may not occur. Or, the amount of reaction may be small. Even in these cases, it is possible to cause the reaction in the second reaction device 22S. In order to maintain the reaction, the temperature of the catalyst CT needs to be maintained. In other words, heat needs to be supplied. The supply of heat is performed, for example, by providing a heat medium HM. By providing the heat medium HM, heat is continuously supplied to obtain a small amount of resultant product (hydrocarbon). Therefore, energy efficiency tends to decrease.

[0064] In particular, the hydrocarbon production apparatus 2 employing the methanation shown in formula (1) and the FT reaction shown in formula (2) often includes multiple reactors. The scale of the hydrocarbon production apparatus 2 including multiple reactors is large. As a result, a huge amount of energy is required for operation to maintain the temperature. Therefore, when the amount of heat generated by the reaction is less than the amount of heat (variable Y) required to maintain the reaction, it is more energy efficient overall to stop the supply of the heat medium HM and gas to the second reactor 22S. Therefore, the controller 3 selects the second control signal θ that stops the supply of the heat medium HM and gas to the second reactor 22S.

[0065] The controller 3 judges whether the amount of heat of reaction is smaller than the required amount of heat. If the amount of heat of reaction is smaller than the required amount of heat, power is consumed to maintain the temperature of the catalyst CT. By using the amount of heat of reaction and the required amount of heat, the timing at which the heat medium HM starts to flow into the heat medium bypass pipe 242P and the timing at which the intermediate gas starts to flow into the gas bypass pipe 25P can be automatically controlled.

[0066] An example of the operation executed by the controller 3 will be described. In this example, it is assumed that methane is produced as the hydrocarbon. The operation of avoiding the supply of the heat transfer medium HM and the supply of the intermediate gas to the second reaction device 22S (output of the second control signal θ) is executed when the following formula (3) is satisfied. (X×a÷b×c) [kW] <Y[kW]…(3) X: Hydrogen production volume of the water electrolysis device 101 [m 3 / s] a: The ratio of the amount of methane produced to the amount of hydrogen supplied (e.g., 0.25) b: Volume per unit mole [m 3 / mol] (e.g. 0.0224) c: Heat generation per unit mole [kJ / mol] (165) Y: Heat release amount during low load operation of hydrocarbon production unit 2 [kW]

[0067] On the left side of formula (3), the value obtained by variables X, a, and b is the amount of methane [mol / s] obtained as a result assuming that all of the received hydrogen gas is converted to methane. The amount of methane is multiplied by the calorific value per unit mole (variable c) to obtain the amount of reaction heat (step S102).

[0068] The amount of hydrogen produced (variable X) can also be said to be the amount of hydrogen received by the hydrocarbon production facility 1. Various methods may be used to derive the amount of hydrogen produced, depending on factors such as the state, capacity, and control system of the hydrocarbon production facility 1. Some specific examples will be given below.

[0069] As a first specific example, the amount of hydrogen produced is obtained as an average value of the amount of hydrogen output by the water electrolysis apparatus 101. It can be said that the first specific example assumes prediction of a local amount of hydrogen produced. When the power required for hydrogen production is obtained from the renewable energy facility 102, a local decrease in the amount of power generated may occur due to the influence of clouds or wind. Therefore, the average value of the amount of hydrogen produced by the water electrolysis apparatus 101 in the most recent minutes to hours may be used based on the timing at which steps S102 and S103 are performed.

[0070] As a second specific example, there is a case where the amount of hydrogen produced is obtained from the remaining amount of hydrogen in the hydrogen storage facility. Assuming that the renewable energy facility 102 is a solar power generation facility, the renewable energy facility 102 cannot supply power at night. As a result, the amount of hydrogen produced drops drastically. In other words, when the hydrocarbon production facility 1 is operated at night, hydrogen is supplied from the hydrogen storage facility 103. Therefore, the remaining amount of hydrogen in the hydrogen storage facility 103 limits the amount of product gas produced.

[0071] As a third specific example, there is an example in which the amount of hydrogen production is obtained from the amount of power generated by the renewable energy facility 102. The amount of power generated by solar power generation for each hour of the day is predicted based on weather forecasts, etc. If the amount of power generation can be predicted, the amount of hydrogen production by the water electrolysis device 101 to which the power is supplied can be predicted. In the third specific example, it is possible to predict the amount of hydrogen production. Therefore, an operation plan for the hydrocarbon production facility 1 can be determined before the start of actual operation.

[0072] The reaction heat generated by the reaction to generate hydrocarbons is exchanged with the heat medium HM inside the first reactor 21S, the second reactor 22S, and the third reactor 23S. In other words, heat is removed. The heat medium HM is heated by the reaction heat. As a result, heat is released from the entire hydrocarbon production facility 1. The amount of heat released from the entire hydrocarbon production facility 1 (variable Y [kW]) can be measured in advance. By using the amount of heat released, it can be determined whether the first reactor 21S, the second reactor 22S, and the third reactor 23S are in a state where they can maintain the temperature or in a state where they cannot maintain the temperature, based on the amount of hydrogen produced by the water electrolysis device 101. The amount of heat released is determined by supplying an inert gas such as nitrogen gas to the three first reactors 21S, the second reactor 22S, and the third reactor 23S, and keeping the temperature of the catalyst constant. In order to maintain the temperature of the catalyst, it is necessary to supply an amount of heat equivalent to the amount of heat lost by heat release from the catalyst to the catalyst CT from the heat medium HM. The amount of heat supplied by the heat medium HM to the catalyst CT can be considered to be equivalent to the amount of heat input that the heat medium HM receives from the heater of the heat control device 241. Therefore, the amount of heat dissipation can be known by measuring the amount of heat provided from the heater to the heat medium HM to keep the temperature of the catalyst constant. The amount of heat dissipation is the amount of heat that must be supplied to maintain the temperature of the catalyst. Therefore, the amount of heat dissipation is the amount of heat required to maintain the reaction.

[0073] The result of step S103 is either that "the amount of heat generated by the reaction is less than the amount of heat (variable Y) required to maintain the reaction" or that "the amount of heat generated by the reaction is not less than the amount of heat (variable Y) required to maintain the reaction."

[0074] The controller 3 outputs the first control signal θ or the second control signal θ to the heat medium switch 242S and the gas switch 25S according to the result of step S103. If the result of step S103 is that the amount of reaction heat is not less than the required amount of heat (variable Y) (step S103: NO), the controller 3 outputs the first control signal θ (step S104). If the result of step S103 is that the amount of reaction heat is less than the required amount of heat (variable Y) (step S103: YES), the controller 3 outputs the second control signal θ (step S105).

[0075] The controller 3 realizes the above operations by a computer executing a program. As shown in Fig. 1, the controller 3 has functional components for realizing the above operations. The controller 3 has a hydrogen amount acquisition unit 3a, a heat amount comparison unit 3b, and a signal output unit 3c. The functions of these elements are realized by a processor 31 executing a program.

[0076] The hydrogen amount acquiring unit 3a acquires flow rate data φ (variable X) relating to the amount of hydrogen that can be accepted by the hydrocarbon production facility 1. The hydrogen amount acquiring unit 3a executes step S101.

[0077] The heat quantity comparison unit 3b outputs either "the amount of heat of reaction is less than the required amount of heat" or "the amount of heat of reaction is not less than the required amount of heat". The heat quantity comparison unit 3b executes steps S102 and S103. Specifically, the heat quantity comparison unit 3b calculates the amount of heat of reaction using data on the amount of hydrogen (variable X) (step S102). The heat quantity comparison unit 3b reads out the required amount of heat stored in advance. Then, the heat quantity comparison unit 3b compares the calculated amount of heat of reaction with the read out required amount of heat (step S103). As a result, the heat quantity comparison unit 3b outputs either "the amount of heat of reaction is less than the required amount of heat" or "the amount of heat of reaction is not less than the required amount of heat".

[0078] Based on the result output by the heat quantity comparing unit 3b, the signal output unit 3c outputs either the first control signal θ or the second control signal θ to the heat medium passage unit 242 and the gas passage unit 25. The signal output unit 3c executes steps S104 and S105.

[0079] <Action and effect> The hydrocarbon production facility 1 includes a first reactor 21S that receives a raw material gas containing hydrogen and carbon and reacts the raw material gas using a catalyst CT heated to a predetermined temperature to generate a first intermediate gas containing hydrocarbons, a second reactor 22S that reacts the first intermediate gas using the catalyst CT heated to a predetermined temperature to generate a second intermediate gas containing hydrocarbons, a heat supplier 24 that can supply heat for heating the catalyst CT to the first reactor 21S and can supply heat for heating the catalyst CT to the second reactor 22S, and a controller 3 that controls the operation of the heat supplier 24. The controller 3 selectively outputs to the heat supplier 24 a first control signal θ that causes the first reactor 21S and the second reactor 22S to supply heat, and a second control signal θ that causes the first reactor 21S to supply heat only to the first reactor 21S. The controller 3 selects either the first control signal θ or the second control signal θ based on the amount of hydrogen contained in the raw material gas.

[0080] When the amount of hydrogen supplied to the hydrocarbon production facility 1 is small, the amount of heat generated by the reaction is also small. As a result, it is necessary to heat the catalyst CT to a temperature required to cause the reaction. The hydrocarbon production facility 1 switches between a mode in which the heat medium HM is supplied to the first reactor 21S, the second reactor 22S, and the third reactor 23S and a mode in which the heat medium HM is supplied to the first reactor 21S and the third reactor 23S based on the amount of hydrogen contained in the raw material gas. As a result, when the amount of hydrogen supplied to the hydrocarbon production facility 1 is small, the mode in which the heat medium HM is supplied to the first reactor 21S and the third reactor 23S is selected. As a result, the amount of heat to be supplied to maintain the reaction in the second reactor 22S can be reduced. Therefore, the hydrocarbon production facility 1 can improve the energy efficiency in the operation of generating a gas containing hydrocarbons from the raw material gas.

[0081] In other words, the hydrocarbon production facility 1 produces hydrocarbons using hydrogen, carbon monoxide or carbon dioxide as a raw material. The hydrocarbon production facility 11 includes a first reactor 21S, a second reactor 22S and a third reactor 23S each having a catalyst for producing hydrocarbons. The first reactor 21S, the second reactor 22S and the third reactor 23S are provided with a heat medium bypass pipe 242P and a gas bypass pipe 25P as bypass lines. The heat medium bypass pipe 242P and the gas bypass pipe 25P selectively prevent the flow of the raw material gas and the heat medium HM. The hydrocarbon production facility 11 can limit the range in which the high-temperature raw material gas, the high-temperature intermediate gas and the heat medium HM flow, thereby reducing the amount of heat consumed.

[0082] With the above-mentioned configuration, the hydrocarbon production facility 1 can operate the hydrocarbon production facility 11 at a low load by using the water electrolysis device 101 that continues to produce hydrogen at a low load during the night and in bad weather. By providing a mechanism for avoiding the supply of gas and the supply of the heat medium HM to the first reactor 21S, the second reactor 22S, and the third reactor 23S, it is possible to reduce the power required to maintain the temperatures of the first reactor 21S, the second reactor 22S, and the third reactor 23S.

[0083] The hydrocarbon production facility 11 circulates the raw material gas and heat transfer medium HM, and automatically or manually switches the number of the first reactor 21S, second reactor 22S, and third reactor 23S that produce hydrocarbons depending on the amount of hydrogen supplied from a hydrogen generation device such as a water electrolysis device 101, the remaining amount of hydrogen stored in the hydrogen storage device, or the amount of electricity actually output by the renewable energy facility 102, or the predicted amount of electricity that the renewable energy facility 102 will output.

[0084] In essence, the above-described hydrocarbon production facility 11 increases energy efficiency in the production of product gases containing hydrocarbons by relating the amount of hydrogen that the hydrocarbon production facility 11 can accept to the amount of hydrocarbons produced.

[0085] The heat supplier 24 of the hydrocarbon production facility 1 has a heat medium passage section 242 through which the heat medium HM that exchanges heat with the first reaction device 21S and the second reaction device 22S flows, and a heat control device 241 that exchanges heat with the heat medium HM. The heat medium passage section 242 includes a first heat medium pipe 242a connected to the first reaction device 21S, a second heat medium pipe 242b that connects the first reaction device 21S to the second reaction device 22S, and a third heat medium pipe 242c connected to the second reaction device 22S. According to this configuration, the heat medium HM that has received heat from the heat control device 241 is supplied to the first reaction device 21S and the second reaction device 22S. As a result, the amount of heat required for the reaction can be provided to the catalyst CT.

[0086] The heat medium passage section 242 of the hydrocarbon production facility 1 includes a heat medium bypass pipe 242P that connects the second heat medium pipe 242b to the third heat medium pipe 242c, and a heat medium switch 242S that switches between a mode in which the heat medium HM is supplied to the second reaction device 22S upon receiving a first control signal θ and a mode in which the heat medium HM is supplied to the heat medium bypass pipe 242P without being supplied to the second reaction device 22S upon receiving a second control signal θ. With this configuration, it is possible to realize, with a simple configuration, switching between a mode in which the heat medium HM is supplied to the second reaction device 22S and a mode in which the heat medium HM is not supplied to the second reaction device 22S.

[0087] The hydrocarbon production facility 1 includes a first gas pipe 251 connected to the first reactor 21S, a second gas pipe 252 connecting the first reactor 21S to the second reactor 22S, a third gas pipe 253 connected to the second reactor 22S, and a gas bypass pipe 25P connecting the second gas pipe 252 to the third gas pipe 253. The hydrocarbon production facility 1 includes a gas switch 25S that switches between a mode in which the first intermediate gas is supplied to the second reactor 22S upon receiving a first control signal θ and a mode in which the first intermediate gas is supplied to the gas bypass pipe 25P without being supplied to the second reactor 22S upon receiving a second control signal θ. With this configuration, it is possible to realize a simple configuration to switch between a mode in which the first intermediate gas is supplied to the second reactor 22S and a mode in which the first intermediate gas is not supplied to the second reactor 22S.

[0088] The controller 3 has a hydrogen amount acquisition unit 3a for acquiring data on the amount of hydrogen contained in the raw material gas, a heat amount comparison unit 3b for comparing a reaction heat amount including the heat amount generated by the reaction in the first reactor 21S and the heat amount generated by the reaction in the second reactor 22S with a required heat amount required to maintain the reaction in the first reactor 21S and the reaction in the second reactor 22S when the raw material gas containing the amount of hydrogen indicated by the data on the amount of hydrogen is received, and a signal output unit 3c for outputting a second control signal θ to the heat supplier 24 when the reaction heat amount is smaller than the required heat amount. The controller 3 can easily determine a state in which heat should be supplied to only one of the first reactor 21S and the second reactor 22S.

[0089] The hydrocarbon production system 100 includes a water electrolysis device 101 that outputs hydrogen, and a hydrocarbon production facility 1 that receives a raw material gas containing hydrogen and carbon and generates a gas containing hydrocarbons. The hydrocarbon production facility 1 includes a first reactor 21S that receives the raw material gas and generates a first intermediate gas containing hydrocarbons by reacting the raw material gas with a catalyst CT heated to a predetermined temperature, a second reactor 22S that generates a second intermediate gas containing hydrocarbons by reacting the first intermediate gas with the catalyst CT heated to a predetermined temperature, a heat supplier 24 that supplies heat to the first reactor 21S for heating the catalyst CT and also supplies heat to the second reactor 22S for heating the catalyst CT, and a controller 3 that controls the operation of the heat supplier 24. The controller 3 selectively outputs a first control signal θ for supplying heat to each of the first reactor 21S and the second reactor 22S, and a second control signal θ for supplying heat to only one of the first reactor 21S and the second reactor 22S, to the heat supplier 24. The controller 3 selects either the first control signal θ or the second control signal θ based on the amount of hydrogen contained in the raw material gas.

[0090] The hydrocarbon production system 100 includes the above-mentioned hydrocarbon production facility 1. Therefore, the hydrocarbon production system 100 can improve the energy efficiency in the operation of generating gas containing hydrocarbons from a feed gas.

[0091] The controller 3 of the hydrocarbon production apparatus 2 includes a hydrogen amount acquisition unit 3a that acquires data on the amount of hydrogen contained in the raw material gas, a heat amount comparison unit 3b that compares a reaction heat amount, including the amount of heat generated by the reaction in the first reactor 21S and the amount of heat generated by the reaction in the second reactor 22S, with a required amount of heat required to maintain the reaction in the first reactor 21S and the reaction in the second reactor 22S, when the hydrocarbon production apparatus 2 receives a raw material gas containing hydrogen in an amount indicated by the data on the amount of hydrogen, and a signal output unit 3c that outputs a control signal θ to the heat supplier 24 that supplies heat to the first reactor 21S for heating the catalyst CT and supplies heat to the second reactor 22S for heating the catalyst CT, when the reaction heat amount is smaller than the required amount of heat, to cause the heat supplier 24 to supply heat to only one of the first reactor 21S and the second reactor 22S.

[0092] The controller 3 of the hydrocarbon production apparatus 2 can determine a target to which the heat medium HM is provided, based on the amount of hydrogen contained in the raw material gas supplied to the hydrocarbon production apparatus 2. Therefore, the controller 3 of the hydrocarbon production apparatus 2 can improve the energy efficiency of the operation of generating gas containing hydrocarbons from the raw material gas, which is performed by the hydrocarbon production apparatus 2.

[0093] The method for producing hydrocarbons includes step S101 of obtaining data on the amount of hydrogen contained in the raw material gas, step S103 of comparing, when the hydrocarbon production apparatus 2 receives the raw material gas containing the amount of hydrogen indicated by the data on the amount of hydrogen, a reaction heat amount including the amount of heat generated by the reaction in the first reactor 21S and the amount of heat generated by the reaction in the second reactor 22S with a required amount of heat required to maintain the reaction in the first reactor 21S and the reaction in the second reactor 22S, and step S105 of outputting a control signal θ to the heat supplier 24 capable of supplying heat for heating the catalyst CT to the first reactor 21S and the second reactor 22S to supply heat only to the first reactor 21S when the reaction heat amount is smaller than the required amount of heat.

[0094] The method for producing hydrocarbons determines a target to which the heat medium HM is provided based on the amount of hydrogen contained in the raw material gas supplied to the hydrocarbon production apparatus 2. Therefore, the method for producing hydrocarbons can improve the energy efficiency of the operation of generating a gas containing hydrocarbons from the raw material gas performed by the hydrocarbon production apparatus 2.

[0095] <Example> 5 is a specific example of a hydrocarbon production apparatus 5. The hydrocarbon production apparatus 5 is equipped with three reactors, a reactor 51, a reactor 52, and a reactor 53. The reactors 51 and 52 are thermally controlled by a heat medium. The reactor 51 is provided with a heat exchanger 541 for preheating the raw material gas. The reactor 52 is provided with a heat exchanger 542. The reactor 53 is thermally controlled by a heater 5H.

[0096] The reactor 51 receives the raw material gas provided from the mass flow controllers 551 and 552 via the heat exchanger 541. A pipe for receiving a heat transfer medium is connected to the reactor 51. The heat transfer medium does not bypass the reactor 51. The reactor 51 outputs the generated intermediate gas to the tank 561 via the heat exchanger 541 and the heat exchanger 571. The intermediate gas contains hydrocarbons such as methane and water as products. The heat exchanger 571 condenses the water by cooling the intermediate gas. The water liquefied by condensation is stored in the tank 561. The tank 561 outputs the intermediate gas from which the water has been removed and which contains hydrocarbons, toward the reactor 52.

[0097] The reactor 52 receives the intermediate gas from the tank 561 via the heat exchanger 542. The reactor 52 outputs the intermediate gas generated via the heat exchanger 572 to the tank 562. The roles of the heat exchanger 572 and the tank 562 are as described above. The piping for introducing the intermediate gas to the reactor 52 includes a path for introducing the intermediate gas to the reactor 52 and a path for introducing the intermediate gas directly to the reactor 53, bypassing the reactor 52. The path through which the intermediate gas flows is controlled by two valves 581 and 582. When the valve 581 is closed and the valve 582 is opened, the intermediate gas is introduced to the reactor 52. On the other hand, when the valve 581 is opened and the valve 582 is closed, the intermediate gas is introduced to the reactor 53, bypassing the reactor 52.

[0098] The reactor 52 is connected to a pipe for receiving a heat medium, similar to the reactor 51. The pipe for the heat medium provided in the reactor 52 includes a path for leading the heat medium to the reactor 52 and a path for leading the heat medium to the reactor 51 without leading the heat medium to the reactor 52. The path through which the heat medium flows is controlled by two valves 583 and 584. When the valve 583 is closed and the valve 584 is opened, the heat medium is led to the reactor 52. On the other hand, when the valve 583 is opened and the valve 584 is closed, the heat medium is led to the reactor 51, bypassing the reactor 52. The opening and closing of the valves 583 and 584 can be controlled by the operations of steps S104 and S105 executed by the controller 3. As a result, it is possible to operate in such a way that the heat medium and the intermediate gas are not flowed to the reactor 52. Therefore, the amount of heat radiation can be reduced.

[0099] The reactor 53 receives the intermediate gas from the reactor 51 or the reactor 52. The reactor 53 outputs the generated intermediate gas to the tank 563 via the heat exchanger 573. The roles of the heat exchanger 573 and the tank 563 are as described above.

[0100] For example, it is assumed that the heat dissipation amount (variable Y) of the hydrocarbon production apparatus 2 shown in Fig. 5 is 9 kW. Under this assumption, if the intermediate gas and heat transfer medium are not supplied to the reactor 52, a reduction in the amount of heat can be expected of about 1 / 3. If the amount of hydrogen production is small, such as at night or during bad weather, and 6 kW of heat generation cannot be expected, an operation is performed in which the intermediate gas and heat transfer medium are not supplied to the reactor 52.

[0101] <Modification> The hydrocarbon production facility, the hydrocarbon production system, the controller for the hydrocarbon production apparatus, and the method for producing hydrocarbons of the present disclosure have been described in detail above. However, the hydrocarbon production facility, the hydrocarbon production system, the controller for the hydrocarbon production apparatus, and the method for producing hydrocarbons of the present disclosure are not limited to the above-mentioned embodiments. The hydrocarbon production facility, the hydrocarbon production system, the controller for the hydrocarbon production apparatus, and the method for producing hydrocarbons of the present disclosure can be modified in various ways without departing from the gist of the present disclosure.

[0102] For example, the hydrocarbon production facility 1 shown in FIG. 1 includes three reactors, a first reactor 21S, a second reactor 22S, and a third reactor 23S. The hydrocarbon production facility 1 may include two or more reactors. For example, the hydrocarbon production facility 1 may include two reactors. The hydrocarbon production facility 1 may include four reactors.

[0103] For example, the hydrocarbon production equipment 1 shown in FIG. 1 has a configuration in which only the second reaction device 22S bypasses the intermediate gas and the heat medium HM. The hydrocarbon production equipment 1 may have a configuration in which only the first reaction device 21S bypasses the intermediate gas and the heat medium HM. The hydrocarbon production equipment 1 may have a configuration in which only the third reaction device 23S bypasses the intermediate gas and the heat medium HM. For example, the hydrocarbon production equipment 1 may have a configuration in which the first reaction device 21S and the second reaction device 22S bypass the intermediate gas and the heat medium HM. The hydrocarbon production equipment 1 may have a configuration in which the first reaction device 21S and the third reaction device 23S bypass the intermediate gas and the heat medium HM. The hydrocarbon production equipment 1 may have a configuration in which the second reaction device 22S and the third reaction device 23S bypass the intermediate gas and the heat medium HM. Furthermore, the hydrocarbon production facility 1 may be configured such that the first reactor 21S, the second reactor 22S, and the third reactor 23S bypass the intermediate gas and the heat transfer medium HM.

[0104] When a plurality of first reactors 21S, second reactors 22S, and third reactors 23S are provided with a configuration for bypassing the intermediate gas and heat medium HM, more precise control can be performed. For example, when the second reactors 22S and third reactors 23S are provided with a configuration for bypassing the intermediate gas and heat medium HM, three operation patterns can be realized: a mode in which the intermediate gas and heat medium HM are supplied to all of the first reactors 21S, second reactors 22S, and third reactors 23S, a mode in which the intermediate gas and heat medium HM are supplied to two first reactors 21S and second reactors 22S, and a mode in which the intermediate gas and heat medium HM are supplied to one first reactor 21S. In step S103, one of the two control signals θ was selected depending on whether the relationship of formula (3) was satisfied, but one of the three operation patterns may be selected using multiple conditional formulas.

[0105] The hydrocarbon production facility 1 shown in FIG. 1 employs a configuration in which a heat medium HM is circulated as the heat supplier 24. As another configuration, the heat supplier 24 may be a heater provided in each of the first reactor 21S, the second reactor 22S, and the third reactor 23S. In this case, the controller 3 outputs, for example, a control signal θ for passing a current to the heater provided in the second reactor 22S, and a control signal θ for stopping the current. When the condition shown in formula (3) is satisfied, the controller 3 can suppress energy consumption by stopping the current passed through the heater.

[0106] The heat supplier 24 may include a heat supply configuration using a heat medium HM and a heat supply configuration using a heater. For example, the first reaction device 21S and the second reaction device 22S may be supplied with heat by the heat medium HM. The third reaction device 23S may be supplied with heat by a heater.

[0107] The first reactor 21S of the hydrocarbon production apparatus 2 shown in FIG. 1 is composed of one reactor 21. For example, as shown in FIG. 6, a modified hydrocarbon production apparatus 2A may be equipped with a first reactor 21K, and the first reactor 21K has a first reactor 21a and a second reactor 21b. In the modified example, an example will be described in which the first-stage reactor that receives the raw material gas is equipped with a plurality of reactors. The second reactor 22S and / or the third reactor 23S may also be composed of a plurality of reactors.

[0108] The first reactor 21K has a gas input 21Ka for receiving hydrogen gas and a gas input 21Kb for receiving carbon dioxide. A first gas pipe 251 is connected to the gas input 21Ka. The first gas pipe 251 is also connected to the gas input 21Kb. The first reactor 21K has a gas output 21Kc for outputting the generated intermediate gas to the second reactor 22S. A second gas pipe 252 is connected to the gas output 21Kc.

[0109] The gas input 21Ka is connected to the first gas internal pipe 21Ha. The first gas internal pipe 21Ha has a branched portion. The first output of the first gas internal pipe 21Ha is connected to the first reactor 21a. The second output of the first gas internal pipe 21Ha is connected to the second reactor 21b. With this connection configuration, the hydrogen gas is distributed to the first reactor 21a and the second reactor 21b, respectively. The gas input 21Kb is connected to the second internal pipe 21Hb. The first output of the second internal pipe 21Hb is connected to the first reactor 21a. The second output of the second internal pipe 21Hb is connected to the second reactor 21b. With this connection configuration, the carbon dioxide gas is distributed to the first reactor 21a and the second reactor 21b, respectively.

[0110] The output of the first reactor 21a is connected to an input end of the third internal pipe 21Hc. The output of the second reactor 21b is connected to another input end of the third internal pipe 21Hc. The third internal pipe 21Hc has a junction. At the junction, the intermediate gas generated by the first reactor 21a and the intermediate gas generated by the second reactor 21b are joined. The joined intermediate gas is sent from the gas output 21Kc to the second reactor 22S.

[0111] The first reactor 21K is configured to supply a heat medium to each of the first reactor 21a and the second reactor 21b. The first reactor 21K has a heat medium input 21Kd and a heat medium output 21Ke. The heat medium input 21Kd receives the heat medium flowing out from the second reactor 22S, or the heat medium that has not passed through the second reactor 22S after flowing out from the third reactor 23S. The first heat medium internal pipe 21Ja is connected to the heat medium input 21Kd. The first heat medium internal pipe 21Ja is connected to the first reactor 21a. The first heat medium internal pipe 21Ja is also connected to the second reactor 21b. With this configuration, the first reactor 21a and the second reactor 21b can each receive a heat medium. The second heat medium internal pipe 21Jb is connected to the first reactor 21a. The second heat medium internal pipe 21Jb is also connected to the second reactor 21b. The second heat medium internal pipe 21Jb is connected to the heat medium output 21Ke. The second heat medium internal pipe 21Jb receives the heat medium flowing out from the first reactor 21a and the second reactor 21b. The second heat medium internal pipe 21Jb leads to the heat medium output 21Ke.

[0112] Such a connection configuration can be said to be a configuration in which the first reactor 21a and the second reactor 21b are connected in parallel to each other. A reaction apparatus constituted by a plurality of reactors can increase the amount of intermediate gas generated. The number of reactors connected in parallel is not limited to two. The number of reactors constituting the reaction apparatus may be appropriately selected according to the amount of intermediate gas required.

[0113] This technology contributes to "Affordable and clean energy" as goal 7 of the United Nations' Sustainable Development Goals (SDGs) as it contributes to the effective use of renewable energy. In addition, as it is a technology for manufacturing products using carbon dioxide as a material, it also contributes to "Take urgent action to combat climate change and its impacts" as goal 13 of the United Nations' Sustainable Development Goals (SDGs) as it helps reduce carbon dioxide emissions.

[0114] [Note] The present disclosure includes the following configurations.

[0115] The hydrocarbon production facility of the present disclosure is [1] "a first reactor that receives a raw material gas containing hydrogen and carbon, and generates a first intermediate gas containing hydrocarbons by reacting the raw material gas using a first catalyst heated to a predetermined temperature, a second reactor that generates a second intermediate gas containing hydrocarbons by reacting the first intermediate gas using a second catalyst heated to a predetermined temperature, a heat supplier that can supply heat for heating the first catalyst to the first reactor and can supply heat for heating the second catalyst to the second reactor, and a controller that controls the operation of the heat supplier, wherein the controller selectively outputs to the heat supplier a first control signal that causes heat to be supplied to each of the first reactor and the second reactor, and a second control signal that causes heat to be supplied only to one of the first reactor and the second reactor, and the controller selects either the first control signal or the second control signal based on the amount of hydrogen contained in the raw material gas."

[0116] The hydrocarbon production facility of the present disclosure is [2] "the hydrocarbon production facility described in the above [1], wherein the heat supplier has a heat medium passage section through which a heat medium supplied to the first reaction device and the second reaction device flows, and a heat control section which performs heat exchange with the heat medium, and the heat medium passage section includes a first heat medium passage connected to the first reaction device, a second heat medium passage connecting the first reaction device to the second reaction device, and a third heat medium passage connected to the second reaction device."

[0117] The hydrocarbon production equipment disclosed herein is [3] "the hydrocarbon production equipment described in the above [2], wherein the heat medium passage section has a heat medium bypass passage connecting the second heat medium passage to the third heat medium passage, and a heat medium switching section which switches between a mode in which the heat medium is supplied to the second reaction apparatus upon receiving the first control signal and a mode in which the heat medium is supplied to the heat medium bypass passage without being supplied to the second reaction apparatus upon receiving the second control signal."

[0118] The hydrocarbon production equipment of the present disclosure is [4] "the hydrocarbon production equipment according to any one of the above [1] to [3], further comprising: a first gas flow passage connected to the first reaction apparatus, a second gas flow passage connecting the first reaction apparatus to the second reaction apparatus, a third gas flow passage connected to the second reaction apparatus, a gas bypass flow passage connecting the second gas flow passage to the third gas flow passage, and a gas switching unit which switches between a mode in which the first intermediate gas is supplied to the second reaction apparatus upon receiving the first control signal and a mode in which the first intermediate gas is supplied to the gas bypass flow passage without being supplied to the second reaction apparatus upon receiving the second control signal."

[0119] The hydrocarbon production equipment of the present disclosure is [5] "the hydrocarbon production equipment according to any one of the above [1] to [4], wherein the controller has: a hydrogen amount acquisition unit that acquires data on the amount of hydrogen contained in the raw material gas; a heat amount comparison unit that compares a reaction heat amount including the heat amount produced by the reaction in the first reactor and the heat amount produced by the reaction in the second reactor, with a required heat amount required to maintain the reaction in the first reactor and the reaction in the second reactor, when the raw material gas containing the amount of hydrogen indicated by the data on the amount of hydrogen is received; and a signal output unit that outputs the second control signal to the heat supplier when the reaction heat amount is smaller than the required heat amount."

[0120] The hydrocarbon production equipment of the present disclosure is [6] "the hydrocarbon production equipment according to any one of the above [1] to [5], wherein the first reaction apparatus includes at least two reactors connected in parallel to each other."

[0121] The hydrocarbon production system of the present disclosure includes, [7] "a hydrogen supply facility that outputs hydrogen, and a hydrocarbon production facility that receives a raw material gas containing hydrogen and carbon and generates a gas containing hydrocarbons, the hydrocarbon production facility including a first reactor that receives a raw material gas containing hydrogen and carbon and generates a first intermediate gas containing hydrocarbons by reacting the raw material gas using a first catalyst heated to a predetermined temperature, a second reactor that generates a second intermediate gas containing hydrocarbons by reacting the first intermediate gas using a second catalyst heated to a predetermined temperature, and a second reactor that generates a second intermediate gas containing hydrocarbons by reacting the first intermediate gas using a second catalyst heated to a predetermined temperature. a heat supplier that supplies heat to the first reactor for heating the second catalyst and supplies heat to the second reactor for heating the second catalyst, and a controller that controls an operation of the heat supplier, wherein the controller selectively outputs to the heat supplier a first control signal that causes heat to be supplied to each of the first reactor and the second reactor, and a second control signal that causes heat to be supplied to only one of the first reactor and the second reactor, and the controller selects either the first control signal or the second control signal based on the amount of hydrogen contained in the raw material gas.

[0122] The controller of the hydrocarbon production apparatus of the present disclosure is [8] "a controller for a hydrocarbon production apparatus including a first reaction device that receives a raw material gas containing hydrogen and carbon and generates a first intermediate gas containing hydrocarbons by reacting the raw material gas using a first catalyst heated to a predetermined temperature, and a second reaction device that generates a second intermediate gas containing hydrocarbons by reacting the first intermediate gas using a second catalyst heated to a predetermined temperature, the controller including a hydrogen amount acquisition unit that acquires data regarding the amount of hydrogen contained in the raw material gas, and a controller that acquires the amount of hydrogen contained in the raw material gas by the data regarding the amount of hydrogen. a heat quantity comparing unit which, when the reaction heat quantity is smaller than the required heat quantity, compares a reaction heat quantity including the heat quantity generated by the reaction in the first reactor and the heat quantity generated by the reaction in the second reactor with a required heat quantity required to maintain the reaction in the first reactor and the reaction in the second reactor, and a signal output unit which, when the reaction heat quantity is smaller than the required heat quantity, outputs a control signal to a heat supplier which supplies heat to the first reactor for heating the first catalyst and is capable of supplying heat to the second reactor for heating the second catalyst, to supply heat only to one of the first reactor and the second reactor."

[0123] The method for producing hydrocarbons of the present disclosure is, [9] "a method for producing hydrocarbons using a hydrocarbon production apparatus including a first reactor that receives a raw material gas containing hydrogen and carbon and generates a first intermediate gas containing hydrocarbons by reacting the raw material gas using a first catalyst heated to a predetermined temperature, and a second reactor that generates a second intermediate gas containing hydrocarbons by reacting the first intermediate gas using a second catalyst heated to a predetermined temperature, the method comprising the steps of: obtaining data on the amount of hydrogen contained in the raw material gas; and reacting the raw material gas containing the amount of hydrogen indicated by the data on the amount of hydrogen to produce the hydrocarbon production apparatus. and when the reaction heat amount is smaller than the required amount of heat, outputting a control signal to a heat supplier that supplies heat to the first reactor for heating the first catalyst and that supplies heat to the second reactor for heating the second catalyst to the first reactor, to cause the heat supplier to supply heat to only one of the first reactor and the second reactor. [Explanation of symbols]

[0124] 1. Hydrocarbon production facilities 2. Hydrocarbon production equipment 3 Controller 5. Hydrocarbon production equipment 21, 22, 23, 51, 52, 53 Reactor 21S First Reactor 22S Second Reactor 23S 3rd Reactor 24 Heat supplier 241 Thermal control device (thermal control section) 25 Gas flow passage 25P Gas bypass piping (gas bypass flow path) 25S Gas Switch (Gas Switching Unit) 100 Hydrocarbon Production System 101 Water electrolysis equipment (hydrogen supply equipment) 102 Renewable energy facilities 103 Hydrogen storage equipment (hydrogen supply equipment) 104 Carbon dioxide capture equipment 106 Flow Sensor 242a First heat transfer medium piping (first heat transfer medium flow path) 242b Second heat transfer medium piping (second heat transfer medium flow path) 242c Third heat transfer medium piping (third heat transfer medium flow path) 242d 4th heat medium pipe 242 Heat transfer medium passage section 242P Heat transfer medium bypass piping (heat transfer medium bypass flow path) 242S Heat medium switching device (heat medium switching section) 251 First gas piping (first gas flow path) 252 Second gas piping (second gas flow path) 253 Third gas piping (third gas flow path) 254 4th Gas Pipe CT catalyst HM heat medium θ Control Signal

Claims

1. a first reactor that receives a raw material gas containing hydrogen and carbon and reacts the raw material gas with a first catalyst heated to a predetermined temperature to generate a first intermediate gas containing hydrocarbons; a second reactor for generating a second intermediate gas containing a hydrocarbon by reacting the first intermediate gas with a second catalyst heated to a predetermined temperature; a heat supplier capable of supplying heat to the first reactor for heating the first catalyst and capable of supplying heat to the second reactor for heating the second catalyst; A controller for controlling the operation of the heat supplier; The controller selectively outputs to the heat supplier a first control signal for supplying heat to each of the first reactor and the second reactor, and a second control signal for supplying heat to only one of the first reactor and the second reactor; The controller selects one of the first control signal and the second control signal based on the amount of hydrogen contained in the raw material gas.

2. The heat supplier comprises: a heat medium flow passage portion through which a heat medium supplied to the first reaction device and the second reaction device flows; A heat control unit that exchanges heat with the heat medium, The heat medium passage portion is a first heat transfer medium flow path connected to the first reaction device; A second heat transfer medium flow passage connecting the first reactor to the second reactor; A third heat transfer medium passage connected to the second reaction device.

3. The heat medium passage portion is a heat medium bypass flow path connecting the second heat medium flow path to the third heat medium flow path; a heat medium switching unit that switches between a mode in which the heat medium is supplied to the second reaction device upon receiving the first control signal and a mode in which the heat medium is supplied to the heat medium bypass passage without being supplied to the second reaction device upon receiving the second control signal.

4. a first gas flow path connected to the first reactor; a second gas flow path connecting the first reactor to the second reactor; a third gas flow path connected to the second reactor; a gas bypass flow path connecting the second gas flow path to the third gas flow path; 2. The hydrocarbon production facility according to claim 1, further comprising a gas switching unit that switches between a mode in which the first intermediate gas is supplied to the second reaction device upon receiving the first control signal and a mode in which the first intermediate gas is supplied to the gas bypass passage without being supplied to the second reaction device upon receiving the second control signal.

5. The controller includes: a hydrogen amount acquiring unit for acquiring data on the amount of hydrogen contained in the raw material gas; a heat quantity comparison unit that compares a reaction heat quantity, including a heat quantity generated by a reaction in the first reactor and a heat quantity generated by a reaction in the second reactor, with a required heat quantity required to maintain the reaction in the first reactor and the reaction in the second reactor, when the raw material gas containing the hydrogen in an amount indicated by the data on the amount of hydrogen is received; 2. The hydrocarbon production facility according to claim 1, further comprising: a signal output unit that outputs the second control signal to the heat supplier when the amount of reaction heat is smaller than the required amount of heat.

6. 2. The hydrocarbon production facility of claim 1, wherein the first reactor comprises at least two reactors connected in parallel to each other.

7. A hydrogen supply facility that outputs hydrogen; a hydrocarbon production facility that receives the feed gas containing hydrogen and carbon and generates a gas containing hydrocarbons, The hydrocarbon production facility comprises: a first reactor that receives a raw material gas containing hydrogen and carbon and reacts the raw material gas with a first catalyst heated to a predetermined temperature to generate a first intermediate gas containing hydrocarbons; a second reactor for generating a second intermediate gas containing a hydrocarbon by reacting the first intermediate gas with a second catalyst heated to a predetermined temperature; a heat supplier that supplies heat to the first reactor for heating the first catalyst and that supplies heat to the second reactor for heating the second catalyst; A controller for controlling the operation of the heat supplier; The controller selectively outputs to the heat supplier a first control signal for supplying heat to each of the first reactor and the second reactor, and a second control signal for supplying heat to only one of the first reactor and the second reactor; The controller selects one of the first control signal and the second control signal based on the amount of hydrogen contained in the feed gas.

8. A controller for a hydrocarbon production apparatus, comprising: a first reactor that receives a raw material gas containing hydrogen and carbon, and generates a first intermediate gas containing hydrocarbons by reacting the raw material gas with a first catalyst heated to a predetermined temperature; and a second reactor that generates a second intermediate gas containing hydrocarbons by reacting the first intermediate gas with a second catalyst heated to a predetermined temperature, a hydrogen amount acquiring unit for acquiring data on the amount of hydrogen contained in the raw material gas; a heat quantity comparison unit that compares a reaction heat quantity, including a heat quantity generated by a reaction in the first reactor and a heat quantity generated by a reaction in the second reactor, with a required heat quantity required to maintain the reaction in the first reactor and the reaction in the second reactor, when the hydrocarbon production apparatus receives the raw material gas containing the hydrogen in an amount indicated by the data on the amount of hydrogen; and a signal output unit that outputs a control signal to a heat supplier that is capable of supplying heat for heating the first catalyst to the first reaction device and supplying heat for heating the second catalyst to the second reaction device, when the amount of reaction heat is smaller than the required amount of heat.

9. A method for producing hydrocarbons using a hydrocarbon production apparatus including: a first reactor that receives a raw material gas containing hydrogen and carbon, and generates a first intermediate gas containing hydrocarbons by reacting the raw material gas using a first catalyst heated to a predetermined temperature; and a second reactor that generates a second intermediate gas containing hydrocarbons by reacting the first intermediate gas using a second catalyst heated to a predetermined temperature, comprising: obtaining data regarding the amount of hydrogen contained in the feed gas; A step of comparing a reaction heat amount including a heat amount generated by the reaction in the first reactor and a heat amount generated by the reaction in the second reactor with a required heat amount required to maintain the reaction in the first reactor and the reaction in the second reactor when the hydrocarbon production apparatus receives the raw material gas containing the hydrogen in an amount indicated by the data on the amount of hydrogen; and when the amount of reaction heat is smaller than the required amount of heat, outputting a control signal to a heat supplier that supplies heat to the first reactor for heating the first catalyst and that supplies heat to the second reactor for heating the second catalyst, to cause the heat supplier to supply heat to only one of the first reactor and the second reactor.

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