Hydrocarbon manufacturing equipment

Abstract

To efficiently produce hydrocarbons. [Solution] The hydrocarbon production apparatus 100 comprises a first reactor 110 to which hydrogen and carbon dioxide are supplied, and which contains a first catalyst 220 that promotes the reaction of hydrogen and carbon dioxide to produce hydrocarbons; a second reactor 120 to which product gas discharged from the first reactor 110 is supplied, and which contains a second catalyst 240 that has a different activation temperature than the first catalyst 220 and promotes the reaction of hydrogen and carbon dioxide to produce hydrocarbons; and a temperature control unit 140 that makes the temperature of the first reactor 110 and the temperature of the second reactor 120 different.

Description

Technical Field

[0001] This disclosure relates to a hydrocarbon production apparatus.

Background Art

[0002] In plants such as thermal power plants, steel mills, and boilers, fossil fuels such as coal, heavy oil, and ultra-heavy oil are being burned. Therefore, exhaust gas containing carbon dioxide generated by the combustion of fossil fuels is discharged from the plant into the atmosphere. Since carbon dioxide is considered a factor in global warming, technologies for recovering carbon dioxide from the atmosphere have been developed.

[0003] Further, as a technology for effectively using the recovered carbon dioxide, for example, in Patent Document 1, carbon dioxide and hydrogen are supplied to a reaction apparatus containing a catalyst that promotes the methanation reaction, and carbon dioxide and hydrogen are reacted in the reaction apparatus to produce methane. A technology for manufacturing is disclosed.

Prior Art Documents

Patent Documents

[0004]

Patent Document 1

Summary of the Invention

Problems to be Solved by the Invention

[0005] In the technology of reacting carbon dioxide and hydrogen to produce hydrocarbons such as methane as in Patent Document 1 above, development of a technology for efficiently producing hydrocarbons is desired.

[0006] In view of such problems, an object of the present disclosure is to provide a hydrocarbon production apparatus capable of efficiently producing hydrocarbons.

Means for Solving the Problems

[0007] To solve the above problems, a hydrocarbon production apparatus according to one aspect of the present disclosure comprises: a first reactor containing a first catalyst that promotes the reaction of hydrogen and carbon dioxide to produce hydrocarbons, and to which hydrogen and carbon dioxide are supplied; a second reactor containing a second catalyst having a different activation temperature from the first catalyst that promotes the reaction of hydrogen and carbon dioxide to produce hydrocarbons, and to which the product gas discharged from the first reactor is supplied; and a temperature control unit that makes the temperature of the first reactor and the temperature of the second reactor different.

[0008] The activation temperature of the first catalyst may be higher than that of the second catalyst, and the temperature control unit may set the temperature of the first reactor higher than that of the second reactor.

[0009] The temperature control unit may set the temperature difference between the first reactor and the second reactor to 100°C or more and 150°C or less.

[0010] The hydrocarbon production apparatus described above may include a cooling unit for cooling the product gas discharged from the first reactor, and a gas-liquid separator for separating water from the product gas cooled by the cooling unit, with the product gas from which water has been removed by the gas-liquid separator being supplied to the second reactor. [Effects of the Invention]

[0011] According to this disclosure, it becomes possible to efficiently produce hydrocarbons. [Brief explanation of the drawing]

[0012] [Figure 1] Figure 1 is a schematic diagram of a hydrocarbon manufacturing apparatus according to an embodiment of this disclosure. [Figure 2] Figure 2 is a schematic diagram showing an example of the first and second reactors according to the same embodiment. [Figure 3] Figure 3 illustrates the effects of including the first cooling unit and the first gas-liquid separator. [Modes for carrying out the invention]

[0013] Embodiments of this disclosure will be described in detail below with reference to the attached drawings. The dimensions, materials, and other specific numerical values ​​shown in the embodiments are merely examples for the purpose of facilitating understanding and do not limit this disclosure unless otherwise specified. In this specification and in the drawings, elements having substantially the same function or configuration are denoted by the same reference numerals to avoid redundant explanations. Elements not directly related to this disclosure are omitted from the illustrations.

[0014] [1. Overview of the hydrocarbon production equipment] First, an overview of the hydrocarbon production apparatus 100 according to the embodiment of this disclosure will be described with reference to Figure 1. Figure 1 is a schematic diagram of the hydrocarbon production apparatus 100 according to the embodiment of this disclosure.

[0015] As shown in Figure 1, the hydrocarbon production apparatus 100 according to this embodiment comprises a first reactor 110, a second reactor 120, a raw material gas supply unit 130, and a temperature control unit 140. In Figure 1, solid arrows indicate the flow of hydrogen (gas), carbon dioxide (gas), hydrocarbons (gas), and water (gas and liquid). Also in Figure 1, dashed arrows indicate the flow of the heat transfer medium.

[0016] The first reactor 110 and the second reactor 120 react hydrogen with carbon dioxide to produce hydrocarbons. In the first reactor 110 and the second reactor 120, the synthesis reaction of hydrogen and carbon dioxide takes place, producing hydrocarbons. The synthesis reaction of hydrogen and carbon dioxide is an exothermic reaction. The synthesis reaction of hydrogen and carbon dioxide is, for example, the reaction shown in at least one of the following equations (1) to (4). 4H2+ CO2→ CH4+ 2H2O…Formula (1) 6H2+ 2CO2→ C2H4+ 4H2O…Formula (2) 9H2+ 3CO2→ C3H6+ 6H2O…Formula (3) mH2 + nCO2 → Hydrocarbon + 2nH2O …Equation (4) Methane is produced by the reaction shown in the above formula (1). Ethylene (olefin) is produced by the reaction shown in the above formula (2). Propylene (olefin) is produced by the reaction shown in the above formula (3). Hydrocarbons are produced by the Fischer-Tropsch (FT) synthesis reaction shown in the above formula (4). In the present embodiment, a case where the reaction shown in the above formula (1) is carried out in the first reactor 110 and the second reactor 120 to produce methane is taken as an example.

[0017] The first reactor 110 houses a first catalyst 220 that promotes the reaction of generating hydrocarbons from hydrogen and carbon dioxide. Hydrogen and carbon dioxide are supplied to the first reactor 110, for example, by a raw material gas supply unit 130 described later.

[0018] The second reactor 120 houses a second catalyst 240 having an activation temperature different from that of the first catalyst 220, which promotes the reaction of generating hydrocarbons from hydrogen and carbon dioxide. The heat-resistant temperature of the second catalyst 240 is, for example, lower than the heat-resistant temperature of the first catalyst 220. The generated gas discharged from the first reactor 110 is supplied to the second reactor 120.

[0019] FIG. 2 is a schematic diagram showing an example of the first reactor 110 and the second reactor 120 according to the present embodiment. In FIG. 2, for ease of understanding, the description of the heat exchanger 180, the first cooling unit 172, and the first gas-liquid separator 174 is omitted.

[0020] As shown in FIG. 2, the first reactor 110 and the second reactor 120 are, for example, multi-tubular heat exchange type reactors. The first reactor 110 has a heat medium container 210 and a plurality of reaction tubes 212. A heat medium is supplied to the heat medium container 210 by a temperature adjustment unit 140 described later.

[0021] <> The plurality of reaction tubes 212 are provided in the heat medium container 210. The first catalyst 220 is accommodated in the reaction tubes 212. The first catalyst 220 contains, for example, NiO (nickel oxide) and SiO2 (silica). <>

[0022] The temperature inside the reaction tube 212 (the temperature of the catalyst) is adjusted, for example, to 300°C or higher and 350°C or lower by the heat transfer medium supplied to the heat transfer medium container 210 by the temperature adjustment unit 140, and preferably to 320°C or higher and 350°C or lower.

[0023] The second reactor 120 is connected to the first reactor 110, for example, by a first discharge pipe 170. In other words, the first reactor 110 and the second reactor 120 are connected in series by the first discharge pipe 170. The first product gas generated in the first reactor 110 is supplied to the second reactor 120 through the first discharge pipe 170. The first product gas contains at least methane, a reaction product, as well as unreacted hydrogen and carbon dioxide.

[0024] The second reactor 120, like the first reactor 110, has a heat transfer medium container 230 and a plurality of reaction tubes 232. The heat transfer medium is supplied to the heat transfer medium container 230 by a temperature control unit 140.

[0025] Multiple reaction tubes 232 are provided within a heat transfer vessel 230. The reaction tubes 232 contain a second catalyst 240. The activation temperature of the second catalyst 240 is different from that of the first catalyst 220. For example, the activation temperature of the second catalyst 240 is lower than that of the first catalyst 220. In other words, the activation temperature of the first catalyst 220 is higher than that of the second catalyst 240. The second catalyst 240 contains at least one of Ni (nickel), Pt (platinum), and Ru (ruthenium) as the active metal. The second catalyst 240 also contains at least one of Al2O3 (alumina), SiO2 (silica), MgO (magnesium oxide), and TiO2 (titania) as a support.

[0026] The temperature inside the reaction tube 232 (the temperature of the catalyst) is adjusted, for example, to between 200°C and 300°C, preferably between 200°C and 275°C, by the heat transfer medium supplied to the heat transfer medium container 230 by the temperature adjustment unit 140.

[0027] Returning to Figure 1, the raw material gas supply unit 130 supplies hydrogen and carbon dioxide to the first reactor 110. The raw material gas supply unit 130 includes, for example, a first raw material gas supply source 130a, a first supply unit 132, a second raw material gas supply source 130b, and a second supply unit 134.

[0028] The first supply unit 132 supplies a first raw material gas to the first reactor 110. The first raw material gas contains at least hydrogen. The first raw material gas consists of, for example, hydrogen and unavoidable impurities. The first supply unit 132 includes, for example, a first supply pipe 132a and a flow rate adjustment mechanism 132b. The first supply pipe 132a is a pipe connecting the supply source 130a of the first raw material gas to the reaction pipe 212 of the first reactor 110. The flow rate adjustment mechanism 132b is provided in the first supply pipe 132a. The flow rate adjustment mechanism 132b adjusts the flow rate of the first raw material gas flowing through the first supply pipe 132a. The flow rate adjustment mechanism 132b is composed of, for example, a mass flow controller.

[0029] The second supply unit 134 supplies a second raw material gas to the first reactor 110. The second raw material gas contains at least carbon dioxide. The second raw material gas consists, for example, carbon dioxide and unavoidable impurities. The second supply unit 134 includes, for example, a second supply pipe 134a and a flow rate adjustment mechanism 134b. The second supply pipe 134a is a pipe connecting the supply source 130b of the second raw material gas to the first supply pipe 132a. In this embodiment, the second supply unit 134 supplies the second raw material gas to the first reactor 110 through the second supply pipe 134a and the first supply pipe 132a. Specifically, the second supply pipe 134a connects the supply source 130b of the second raw material gas to the flow rate adjustment mechanism 132b in the first supply pipe 132a and the heat exchanger 180, which will be described later. The flow rate adjustment mechanism 134b is provided in the second supply pipe 134a. The flow rate adjustment mechanism 134b adjusts the flow rate of the second raw material gas flowing through the second supply pipe 134a. The flow rate adjustment mechanism 134b is composed of, for example, a mass flow controller.

[0030] Furthermore, a heat exchanger 180 may be provided in the first supply pipe 132a. The heat exchanger 180 is provided between the flow rate adjustment mechanism 132b and the first reactor 110. The heat exchanger 180 exchanges heat between the mixed gas consisting of a first raw material gas and a second raw material gas flowing through the first supply pipe 132a and the first product gas flowing through the first discharge pipe 170. As described above, the first product gas is the gas produced in the first reactor 110 and includes hydrogen, carbon dioxide, methane, and water vapor. In this embodiment, the heat exchanger 180 transfers the heat contained in the first product gas to the mixed gas.

[0031] Furthermore, the first discharge pipe 170 may be equipped with a heat exchanger 180, a first cooling section 172, and a first gas-liquid separator 174 in this order.

[0032] The first cooling unit 172 cools the first product gas discharged from the first reactor 110, thereby condensing the water vapor contained in the first product gas. The first cooling unit 172 is, for example, a condenser. The first gas-liquid separator 174 separates water (liquid) from the first product gas cooled by the first cooling unit 172.

[0033] The reaction tube 232 of the second reactor 120 is supplied with the first product gas, from which water has been removed by the first gas-liquid separator 174, through the first discharge pipe 170.

[0034] The second discharge pipe 190 is a pipe that connects the second reactor 120 and the supply destination 102. When the hydrocarbon production apparatus 100 produces methane as hydrocarbons, the supply destination 102 is, for example, a vehicle that runs on methane as fuel, a combustion device that uses methane as fuel, a boiler that includes a combustion device that uses methane as fuel, or a power generation device that includes a combustion device that uses methane as fuel. The second discharge pipe 190 is provided with a second cooling section 192, a second gas-liquid separator 194, and a back pressure valve 196 in that order.

[0035] The second cooling unit 192 cools the second product gas discharged from the second reactor 120, thereby condensing the water vapor contained in the second product gas. The second product gas is the gas produced in the second reactor 120 and contains at least methane and water vapor. The second cooling unit 192 is, for example, a condenser. The second gas-liquid separator 194 separates water (liquid) from the second product gas cooled by the second cooling unit 192. The second product gas from which water has been removed by the second gas-liquid separator 194 is supplied to the destination 102 through the second discharge pipe 190. The back pressure valve 196 maintains the pressure in the second reactor 120 at a predetermined pressure.

[0036] The temperature control unit 140 makes the temperature of the first reactor 110 and the temperature of the second reactor 120 different. As described above, the activation temperature of the first catalyst 220 housed in the first reactor 110 is higher than the activation temperature of the second catalyst 240 housed in the second reactor 120. For this reason, it is preferable for the temperature control unit 140 to make the temperature of the first reactor 110 higher than the temperature of the second reactor 120. Also, the difference between the activation temperature of the first catalyst 220 and the activation temperature of the second catalyst 240 is between 100°C and 150°C. For this reason, it is preferable for the temperature control unit 140 to make the temperature difference between the first reactor 110 and the second reactor 120 between 100°C and 150°C.

[0037] In this embodiment, the temperature control unit 140 adjusts the temperature of the first reactor 110 and the temperature of the second reactor 120 by, for example, circulating a heat transfer medium to the heat transfer medium container 210 of the first reactor 110 and the heat transfer medium container 230 of the second reactor 120.

[0038] The temperature control unit 140 includes, for example, a first temperature control unit 142 and a second temperature control unit 144.

[0039] The first temperature control unit 142 includes a circulation path 142a, a pump 142b, a flow rate adjustment mechanism 142c, and a heating / cooling unit 142d.

[0040] The circulation path 142a is a flow path through which the heat transfer medium circulates. The circulation path 142a is provided with a pump 142b, a flow rate adjustment mechanism 142c, the heat transfer medium container 210 of the first reactor 110, and a heating / cooling section 142d in that order. The suction side of the pump 142b is connected to the heating / cooling section 142d. The discharge side of the pump 142b is connected to the flow rate adjustment mechanism 142c. When the pump 142b is operated, the heat transfer medium circulates through the circulation path 142a. The flow rate adjustment mechanism 142c adjusts the flow rate of the heat transfer medium flowing through the circulation path 142a. The heating / cooling section 142d heats or cools the heat transfer medium.

[0041] The second temperature control unit 144 includes a circulation path 144a, a pump 144b, a flow rate adjustment mechanism 144c, and a heating / cooling unit 144d.

[0042] The circulation path 144a is a flow path through which the heat transfer medium circulates. The circulation path 144a is provided with a pump 144b, a flow rate adjustment mechanism 144c, the heat transfer medium container 230 of the second reactor 120, and a heating / cooling section 144d in that order. The suction side of the pump 144b is connected to the heating / cooling section 144d. The discharge side of the pump 144b is connected to the flow rate adjustment mechanism 144c. When the pump 144b is operated, the heat transfer medium circulates through the circulation path 144a. The flow rate adjustment mechanism 144c adjusts the flow rate of the heat transfer medium flowing through the circulation path 144a. The heating / cooling section 144d heats or cools the heat transfer medium.

[0043] [2. Summary] As described above, the hydrocarbon production apparatus 100 according to this embodiment comprises: a first reactor 110 containing a first catalyst 220 that promotes the reaction of hydrogen and carbon dioxide to produce hydrocarbons, and to which hydrogen and carbon dioxide are supplied; a second reactor 120 containing a second catalyst 240 having a different activation temperature than the first catalyst 220 that promotes the reaction of hydrogen and carbon dioxide to produce hydrocarbons, and to which the product gas discharged from the first reactor 110 is supplied; and a temperature control unit 140 that makes the temperature of the first reactor 110 and the temperature of the second reactor 120 different.

[0044] The activation temperature of the first catalyst 220 may be higher than that of the second catalyst 240, and the temperature control unit 140 may raise the temperature of the first reactor 110 higher than that of the second reactor 120.

[0045] As described above, the synthesis reaction that produces hydrocarbons from hydrogen and carbon dioxide is an exothermic reaction. Therefore, when hydrogen and carbon dioxide are supplied to the first reactor 110, the temperature of the first reactor 110 rises. Similarly, when hydrogen and carbon dioxide are supplied to the second reactor 120, the temperature of the second reactor 120 rises. Hydrogen and carbon dioxide are supplied to the first reactor 110 from the raw material gas supply unit 130, while unreacted hydrogen and carbon dioxide from the first reactor 110, as well as methane produced in the first reactor 110, are supplied to the second reactor 120. Therefore, the amount of hydrogen and carbon dioxide supplied to the second reactor 120 is less than the amount supplied to the first reactor 110. In other words, the amount of hydrogen and carbon dioxide contributing to the synthesis reaction is greater in the first reactor 110 than in the second reactor 120. Therefore, the reaction rate in the first reactor 110 is higher than that of the second reactor 120, and the temperature in the first reactor 110 is higher than that of the second reactor 120. Also, when the temperature of the reaction field is above the reaction start temperature, the conversion rate of the synthesis reaction that produces hydrocarbons from hydrogen and carbon dioxide is higher at lower temperatures and decreases as the temperature increases, due to the equilibrium of the exothermic reaction. Therefore, as described above, by housing the first catalyst 220, which has a higher heat resistance temperature than the second catalyst 240, in the first reactor 110, which is relatively hotter, the hydrocarbon production apparatus 100 according to this embodiment can improve the conversion rate per unit time by improving the reaction rate with the first catalyst 220, and suppress catalyst degradation at high temperatures. As a result, the hydrocarbon production apparatus 100 according to this embodiment can prevent a decrease in the conversion rate of the synthesis reaction in the first reactor 110. Furthermore, since a decrease in the conversion rate can be prevented in the first reactor 110, the hydrocarbon production apparatus 100 according to this embodiment can avoid a situation in which the amount of unreacted hydrogen and carbon dioxide supplied to the second reactor 120 increases. Therefore, in the hydrocarbon production apparatus 100 according to this embodiment, the temperature rise of the second reactor 120 due to the progress of the synthesis reaction can be suppressed, and the conversion rate in the second reactor 120 can be improved. As a result, the hydrocarbon production apparatus 100 according to this embodiment can efficiently produce hydrocarbons.

[0046] Furthermore, the hydrocarbon production apparatus 100 according to this embodiment can improve the conversion rate in the second reactor 120, making it possible to increase the concentration of hydrocarbons in the second product gas discharged from the second reactor 120. For this reason, the hydrocarbon production apparatus 100 according to this embodiment can simplify or omit the purification apparatus for removing impurities (hydrogen, carbon dioxide, and water, etc.) from the second product gas.

[0047] The temperature control unit 140 may also set the temperature difference between the first reactor 110 and the second reactor 120 to 100°C or more and 150°C or less.

[0048] When the temperature difference between the first reactor 110 and the second reactor 120 is 100°C or more, the conversion rate can be improved in both the first reactor 110 and the second reactor 120 compared to when the temperature difference is less than 100°C. Also, when the temperature difference between the first reactor 110 and the second reactor 120 is less than 150°C, the conversion rate can be improved in both the first reactor 110 and the second reactor 120 compared to when the temperature difference is 150°C or more. The temperature control unit 140 according to this embodiment can achieve an even more favorable conversion rate in both the first reactor 110 and the second reactor 120 by setting the temperature difference between the first reactor 110 and the second reactor 120 to 100°C or more and 150°C or less. Therefore, the hydrocarbon production apparatus 100 according to this embodiment can produce hydrocarbons even more efficiently.

[0049] The hydrocarbon production apparatus 100 according to this embodiment includes a cooling unit (first cooling unit 172) for cooling the product gas discharged from the first reactor 110, and a gas-liquid separator (first gas-liquid separator 174) for separating water from the product gas cooled by the cooling unit (first cooling unit 172). The second reactor 120 may be supplied with the product gas from which water has been removed by the gas-liquid separator (first gas-liquid separator 174).

[0050] The concentration of methane in the second product gas was simulated under two conditions: when a first cooling unit 172 and a first gas-liquid separator 174 are provided in the first discharge pipe 170 connecting the first reactor 110 and the second reactor 120, and when the first cooling unit 172 and the first gas-liquid separator 174 are not provided. Figure 3 illustrates the effect of providing the first cooling unit 172 and the first gas-liquid separator 174. In Figure 3, the vertical axis shows the concentration of methane in the second product gas, and the horizontal axis shows the temperature [°C] of the second reactor 120. Note that in Figure 3, the methane concentration is shown as a normalized value. Also, in Figure 3, the solid line shows the change in methane concentration when the first cooling unit 172 and the first gas-liquid separator 174 are provided. In Figure 3, the dashed line shows the change in methane concentration when the first cooling unit 172 and the first gas-liquid separator 174 are not provided.

[0051] As shown in Figure 3, it was confirmed that, regardless of the temperature of the second reactor 120, when the first cooling unit 172 and the first gas-liquid separator 174 are provided, the concentration of methane in the second product gas is higher than when the first cooling unit 172 and the first gas-liquid separator 174 are not provided. In other words, when the first product gas from which water has been removed is supplied to the second reactor 120, it was confirmed that, regardless of the temperature of the second reactor 120, the concentration of methane in the second product gas is higher than when the first product gas from which water has not been removed is supplied to the second reactor 120.

[0052] The hydrocarbon production apparatus 100 according to this embodiment is equipped with a first cooling unit 172 and a first gas-liquid separator 174, which allows for an increase in the conversion rate in the second reactor 120. Therefore, the hydrocarbon production apparatus 100 according to this embodiment can produce hydrocarbons even more efficiently.

[0053] While embodiments have been described above with reference to the attached drawings, it goes without saying that this disclosure is not limited to the embodiments described above. It will be obvious to those skilled in the art that various modifications or alterations can be conceived within the scope of the claims, and these will naturally also fall within the technical scope of this disclosure.

[0054] For example, in the above embodiment, we have given an example in which the hydrocarbon production apparatus 100 comprises a first reactor 110 and a second reactor 120. However, the hydrocarbon production apparatus 100 may also include one or more reactors before the first reactor 110, after the second reactor 120, or between the first reactor 110 and the second reactor 120. In any case, the second reactor 120 only needs to be supplied with the product gas discharged from the first reactor 110.

[0055] Furthermore, in the above embodiment, the case in which the second reactor 120 is a multi-tube, heat-exchange type reactor was given as an example. However, the second reactor 120 may also be an adiabatic reactor. This can reduce the cost of the second reactor 120.

[0056] Furthermore, in the above embodiment, an example was given in which the raw material gas supply unit 130 supplies hydrogen and carbon dioxide only to the first reactor 110. However, the raw material gas supply unit 130 may supply one or both of hydrogen and carbon dioxide to the second reactor 120 in addition to the first reactor 110. For example, the raw material gas supply unit 130 may supply one or both of hydrogen and carbon dioxide to the first reactor 110 and the second reactor 120 such that the temperature of the first reactor 110 is below the degradation temperature of the first catalyst 220, and the temperature of the second reactor 120 is below the degradation temperature of the second catalyst 240. Alternatively, the raw material gas supply unit 130 may supply one or both of hydrogen and carbon dioxide to the first reactor 110 and the second reactor 120 such that the length of the reaction tube 212 of the first reactor 110 is shortened, and the length of the reaction tube 232 of the second reactor 120 is shortened.

[0057] Furthermore, in the above embodiment, an example was given in which the activation temperature of the first catalyst 220 is higher than that of the second catalyst 240. However, it is sufficient that the activation temperatures of the first catalyst 220 and the second catalyst 240 are different. For example, the activation temperature of the first catalyst 220 may be lower than that of the second catalyst 240. In this case, in addition to the first product gas, hydrogen and carbon dioxide may be newly supplied to the second reactor 120.

[0058] This disclosure can contribute, for example, to Sustainable Development Goal (SDG) 7, "Ensure access to affordable, reliable, sustainable and modern energy," and Goal 13, "Take urgent action to combat climate change and its impacts." [Explanation of Symbols]

[0059] 100 Hydrocarbon Production Equipment 110 Reactor No. 1 120 Reactor No. 2 140 Temperature adjustment section 172 1st cooling section (cooling section) 174 1st gas-liquid separator (gas-liquid separator) 220 First Catalyst 240 Second Catalyst

Claims

1. A first reactor is provided, which contains a first catalyst that promotes the reaction of hydrogen and carbon dioxide to produce hydrocarbons, and to which hydrogen and carbon dioxide are supplied. A second reactor is provided, which contains a second catalyst having a different activation temperature than the first catalyst, which promotes the reaction of hydrogen and carbon dioxide to produce hydrocarbons, and to which the product gas discharged from the first reactor is supplied. A temperature control unit that makes the temperature of the first reactor and the temperature of the second reactor different, A hydrocarbon production apparatus equipped with the following features.

2. The activation temperature of the first catalyst is higher than that of the second catalyst. The hydrocarbon production apparatus according to claim 1, wherein the temperature control unit raises the temperature of the first reactor to a higher temperature than the temperature of the second reactor.

3. The hydrocarbon production apparatus according to claim 2, wherein the temperature control unit sets the temperature difference between the first reactor and the second reactor to 100°C or more and 150°C or less.

4. A cooling unit for cooling the generated gas discharged from the first reactor, A gas-liquid separator for separating water from the generated gas cooled by the cooling unit, Equipped with, The hydrocarbon production apparatus according to claim 1 or 2, wherein the second reactor is supplied with a product gas from which the water has been removed by the gas-liquid separator.

Images