Hydrocarbon production apparatus and hydrocarbon production method

Abstract

To improve process efficiency during the production of a hydrocarbon compound.SOLUTION: There is provided a hydrocarbon production apparatus which comprises a co-electrolysis unit for co-electrolyzing water and carbon dioxide to produce hydrogen and carbon monoxide, a hydrogen separation unit for separating part of the hydrogen produced by the co-electrolysis unit and a first catalytic reaction unit for producing a hydrocarbon compound by using a catalyst for the remaining hydrogen after separation supplied from the co-electrolysis unit and the carbon monoxide supplied from the co-electrolysis unit.SELECTED DRAWING: Figure 1

Description

[Technical Field]

[0001] The present invention relates to a hydrocarbon production apparatus and a hydrocarbon production method. [Background technology]

[0002] A technique is known for producing hydrocarbon compounds in a catalytic reaction section using hydrogen and carbon monoxide generated by the co-electrolysis of water and carbon dioxide (see, for example, Patent Document 1). In the hydrocarbon production system described in Patent Document 1, hydrocarbon compounds are efficiently produced by using a catalyst in which a metal oxide support bearing ruthenium is used as the catalyst for the catalytic reaction.

[0003] Non-patent document 1 describes the individual processes involved in co-electrolysis and FT (Fischer-Tropsch process) synthesis. The apparatus and materials are described. Non-patent document 1 states that when producing a gas with a hydrogen-to-carbon monoxide molar ratio of 2.0 by co-electrolysis, it is preferable that the molar ratio of the raw materials, water and carbon dioxide, be close to 2.0. On the other hand, when performing co-electrolysis using SOEC (Solid Oxide Electrolysis Cell), the electrolytic reaction rate (actual electrolysis relative to the amount of raw materials supplied) is described. If the ratio of water and carbon dioxide used is increased too much, the upper limit of the thermodynamic carbon deposition temperature rises. Since co-electrolysis is an endothermic reaction, if the upper limit of the thermodynamic carbon deposition temperature rises, carbon deposition will occur near the end of the fuel electrode, which may lead to deterioration of the SOEC's lifespan or failure. Non-patent document 1 states that, as a specific numerical value for the electrolytic reaction rate of co-electrolysis, it is preferable for the electrolytic reaction rate to be 80% when the molar ratio of the raw materials is 2.0.

[0004] Patent Document 2 discloses a technique for producing a first hydrocarbon product and a second synthesis gas from a first synthesis gas using a first FT reactor, and for producing a second hydrocarbon product from a modified synthesis gas obtained by mixing the second synthesis gas with hydrogen using a second FT reactor. [Prior art documents] [Patent Documents]

[0005] [Patent Document 1] Japanese Patent Publication No. 2021-161124 [Patent Document 2] Special Publication No. 2007-517084 [Non-patent literature]

[0006] [Non-Patent Document 1] National Research and Development Agency, New Energy and Industrial Technology Development Organization (NEDO), "Next-Generation Thermal Power Generation Technology Development / Next-Generation Thermal Power Generation Technology Promotion Project / Survey for the Discovery of Development Seeds for Liquid Fuel Production Technology from CO2", FY2019-FY2020 Results Report, Report Management Number 20200000000487 [Overview of the project] [Problems that the invention aims to solve]

[0007] Non-patent document 1 describes the possibility of improving the electrolytic reaction rate while maintaining the upper limit of the thermodynamic carbon deposition temperature by increasing the molar ratio of water to carbon dioxide in the raw materials to more than 2.0. However, it does not disclose specific molar ratios of raw materials or electrolytic reaction rates for improving the electrolytic reaction rate. If the molar ratio of the raw materials in co-electrolysis is greater than 2.0, excess hydrogen will be produced by co-electrolysis in amounts greater than that required for the production of hydrocarbon compounds. Energy is also required for the production of excess hydrogen, in order to heat and pressurize the water and carbon dioxide, which are the raw materials for co-electrolysis. Therefore, even if the electrolytic reaction rate of co-electrolysis increases, the process efficiency of the system for producing hydrocarbon compounds will not improve if the molar ratio of the raw materials in co-electrolysis increases.

[0008] In the FT reaction, hydrocarbon compounds with different numbers of carbon atoms are produced simultaneously, making it difficult to produce only the desired hydrocarbon compound in high yield. The stoichiometric ratio (optimal mixing ratio) of carbon monoxide and hydrogen, which are the raw material gases, differs depending on the hydrocarbon compound to be produced. In co-electrolysis, which produces carbon monoxide and hydrogen, the raw material gases for hydrocarbon compounds, from carbon dioxide and water, it is not possible to produce raw material gases with different mixing ratios simultaneously. In other words, in order to produce different types of hydrocarbon compounds simultaneously, a co-electrolysis apparatus that produces raw material gases with the desired mixing ratio for each hydrocarbon compound to be produced was necessary.

[0009] The present invention has been made to solve at least some of the problems described above, and aims to improve process efficiency in the production of hydrocarbon compounds. [Means for solving the problem]

[0010] The present invention has been made to solve at least some of the above-mentioned problems and can be realized in the following forms. A hydrocarbon production apparatus comprising: a co-electrolytic reaction section that generates hydrogen and carbon monoxide by co-electrolytically reacting water and carbon dioxide; a first gas channel through which the hydrogen and carbon monoxide generated in the co-electrolytic reaction section flow; a hydrogen separation section located in the middle of the first gas channel that separates a portion of the hydrogen generated in the co-electrolytic reaction section; a hydrogen tank for storing the hydrogen separated by the hydrogen separation section; and a catalyst used on the remaining hydrogen after separation supplied from the co-electrolytic reaction section and the carbon monoxide supplied from the co-electrolytic reaction section to produce hydrocarbon compounds. A hydrocarbon production apparatus comprising: a first catalytic reaction section; a second gas flow path arranged in parallel with the first gas flow path, connecting the co-electrolytic reaction section and the first catalytic reaction section, through which hydrogen and carbon monoxide produced by the co-electrolytic reaction section flow; and a control unit that switches the supply flow path for hydrogen and carbon monoxide from the co-electrolytic reaction section between the first gas flow path and the second gas flow path according to the amount of hydrogen stored in the hydrogen tank, wherein the first catalytic reaction section is supplied with residual hydrogen after separation by the hydrogen separation section and carbon monoxide via the first gas flow path. A hydrocarbon production apparatus comprising: a co-electrolytic reaction section that co-electrolyzes water and carbon dioxide to produce hydrogen and carbon monoxide; a hydrogen separation section that separates a portion of the hydrogen produced by the co-electrolytic reaction section; a first catalytic reaction section that produces a hydrocarbon compound by using a catalyst on the remaining hydrogen after separation supplied from the co-electrolytic reaction section and the carbon monoxide supplied from the co-electrolytic reaction section; a second catalytic reaction section that produces a hydrocarbon compound of a different type from the hydrocarbon compound produced in the first catalytic reaction section using at least a portion of a mixed gas containing carbon monoxide and hydrogen supplied from the co-electrolytic reaction section; and a third gas flow path that supplies the mixed gas supplied from the co-electrolytic reaction section to the second catalytic reaction section and the hydrogen separation section, wherein the hydrogen separation section separates a portion of the hydrogen contained in the mixed gas supplied from the co-electrolytic reaction section via the third gas flow path. In addition, the present invention can also be realized in the following forms.

[0011] (1) According to one embodiment of the present invention, a hydrocarbon production apparatus is provided. This hydrocarbon production apparatus comprises a co-electrolytic reaction unit that produces hydrogen and carbon monoxide by co-electrolytically reacting water and carbon dioxide; a hydrogen separation unit that separates a portion of the hydrogen produced by the co-electrolytic reaction unit; and a first catalytic reaction unit that produces a hydrocarbon compound by using a catalyst on the remaining hydrogen after separation supplied from the co-electrolytic reaction unit and the carbon monoxide supplied from the co-electrolytic reaction unit.

[0012] In this configuration, hydrogen and carbon monoxide produced from water and carbon dioxide in the co-electrolytic reaction section are used to produce hydrocarbon compounds in the first catalytic reaction section. The molar ratio (H2 / CO) of hydrogen to carbon monoxide supplied to the first catalytic reaction section during hydrocarbon compound production is preferably around 2.0. Therefore, the molar ratio (H2O / CO2) of water to carbon dioxide used as the raw material for co-electrolysis in the co-electrolytic reaction section is preferably 2.0. However, when using raw materials with a molar ratio of 2.0 for co-electrolysis, the electrolytic reaction rate of the co-electrolysis must be set lower than 100% to suppress damage such as deterioration occurring in the co-electrolytic reaction section. On the other hand, it is known that if the molar ratio of the co-electrolytic raw materials supplied to the co-electrolytic reaction section is set higher than 2.0, the electrolytic reaction rate of the co-electrolysis can be set higher while suppressing damage to the co-electrolytic reaction section. In this configuration, the hydrogen separation section separates a portion of the hydrogen produced by co-electrolysis. Therefore, by increasing the molar ratio of the co-electrolytic raw materials supplied to the co-electrolytic reaction section, the electrolytic reaction rate can be increased, and the excess hydrogen generated by the co-electrolysis can be separated by the hydrogen separation section. Since the separated hydrogen can be used for other purposes, this configuration improves the electrolytic reaction rate of the co-electrolysis, and improves the utilization rate of raw materials and the process efficiency of the apparatus during the production of hydrocarbon compounds without recirculating unused gases. Furthermore, since this configuration does not require separate equipment for the production and supply of hydrogen, the apparatus can be made smaller and simpler.

[0013] (2) The hydrocarbon production apparatus according to the above embodiment may further include an upgrading unit that performs hydrocracking of the hydrocarbon compound produced in the first catalytic reaction unit using the hydrogen separated by the hydrogen separation unit to produce a lighter hydrocarbon compound. In this configuration, the hydrogen separated by the hydrogen separation unit is used to produce even higher quality hydrocarbon compounds as required, using the hydrocarbon compounds manufactured in the first catalytic reaction unit. In other words, by improving the electrolytic reaction rate of the co-electrolysis, the excess hydrogen produced is used to manufacture high-quality hydrocarbon compounds, thus further improving the process efficiency of this configuration.

[0014] (3) In the hydrocarbon production apparatus according to the above embodiment, the apparatus further comprises a first gas channel through which hydrogen and carbon monoxide produced by the co-electrolytic reaction section flow, the hydrogen separation section is located in the middle of the first gas channel, and the first catalytic reaction section is supplied with the remaining hydrogen after separation by the hydrogen separation section and carbon monoxide via the first gas channel. This configuration allows for improved process efficiency of the apparatus with a simple setup that places the hydrogen separation section in the middle of the first gas flow path.

[0015] (4) The hydrocarbon production apparatus according to the above embodiment may further include a hydrogen tank for storing the hydrogen separated by the hydrogen separation unit, a second gas flow path arranged in parallel with the first gas flow path through which hydrogen and carbon monoxide generated by the co-electrolytic reaction unit flow, and a control unit that switches the supply flow path for hydrogen and carbon monoxide from the co-electrolytic reaction unit between the first gas flow path and the second gas flow path according to the amount of hydrogen stored in the hydrogen tank. In this configuration, the supply channel through which hydrogen and carbon monoxide produced by co-electrolysis flow is switched between the first gas channel and the second gas channel, depending on the amount of hydrogen stored in the hydrogen tank. Therefore, when the amount of hydrogen in the hydrogen tank is small, the first gas channel is selected as the supply channel, and the amount of hydrogen in the hydrogen tank can be increased by the hydrogen separation unit located in the middle of the first gas channel. On the other hand, when the amount of hydrogen in the hydrogen tank is large, the supply The second gas flow path is selected as the flow path. In particular, when the amount of hydrogen in the hydrogen tank is large, setting the molar ratio of the co-electrolysis raw materials to the stoichiometric ratio of 2.0 prevents the generation of excess hydrogen. As a result, the amount of hydrogen and carbon monoxide produced by co-electrolysis is controlled according to the amount of hydrogen in the hydrogen tank, further improving the process efficiency of the device.

[0016] (5) In the hydrocarbon production apparatus according to the above aspect, the apparatus further comprises a pressure sensor that detects a pressure in the hydrogen tank, wherein the control unit switches the supply flow path for hydrogen and carbon monoxide from the co-electrolysis reaction unit between the first gas flow path and the second gas flow path according to the detected pressure in the hydrogen tank, and may control the molar ratio of water to carbon dioxide supplied to the co-electrolysis reaction unit. According to this configuration, the amount of hydrogen stored in the hydrogen tank is detected as the pressure in the hydrogen tank, and thus is identified with a simple configuration. The molar ratio of the raw materials for co-electrolysis is controlled according to the internal pressure of the hydrogen tank. Therefore, when the internal pressure of the hydrogen tank is low, increasing the molar ratio of the raw materials for co-electrolysis increases the amount of hydrogen stored in the hydrogen tank, and then improves the electrolytic reaction rate of co-electrolysis. As a result, the process efficiency of the apparatus having this configuration is further improved.

[0017] (6) In the hydrocarbon production apparatus according to the above aspect, when the pressure in the hydrogen tank is equal to or higher than a first threshold, the control unit sets the molar ratio to a first molar ratio, controls the electrolytic reaction rate of co-electrolysis to a first reaction rate, and sets the supply flow path as the second gas flow path; and when the pressure in the hydrogen tank is less than the first threshold, the control unit sets the molar ratio to a second molar ratio higher than the first molar ratio until the pressure in the hydrogen tank exceeds a second threshold higher than the first threshold, controls the electrolytic reaction rate of co-electrolysis to a second reaction rate higher than the first reaction rate, and may set the supply flow path as the first gas flow path. According to this configuration, when the pressure in the hydrogen tank is equal to or higher than the low first threshold, that is, when a certain amount of hydrogen is stored in the hydrogen tank, co-electrolysis is performed at a low first molar ratio of raw materials and a low first electrolytic reaction rate, thereby suppressing the production amount of excess hydrogen from the co-electrolysis. On the other hand, when the pressure in the hydrogen tank is less than the first threshold, that is, when a certain amount of hydrogen is not stored in the hydrogen tank, co-electrolysis is performed at a high second molar ratio of raw materials and a high second electrolytic reaction rate, and the excess hydrogen produced by the co-electrolysis is stored in the hydrogen tank. Hydrogen is stored in the hydrogen tank until the pressure in the hydrogen tank exceeds the second threshold. In the present configuration, since control is switched based on criteria such as thresholds, the amount of hydrogen stored in the hydrogen tank can be maintained at or above a certain level by simple control, while improving process efficiency.

[0018] (7) In the hydrocarbon production apparatus of the above aspect, the apparatus further comprises: a second catalyst reaction section that produces a hydrocarbon compound of a different type from the hydrocarbon compound produced in the first catalyst reaction section using at least a part of a mixed gas containing carbon monoxide and hydrogen supplied from the co-electrolytic reaction section; and a third gas flow path that supplies the mixed gas supplied from the co-electrolytic reaction section to the second catalyst reaction section and the hydrogen separation section, wherein the hydrogen separation section may separate a part of the hydrogen contained in the mixed gas supplied from the co-electrolytic reaction section via the third gas flow path. According to this configuration, the mixed gas containing carbon monoxide and hydrogen generated in the co-electrolytic reaction section is supplied to the first catalyst reaction section and the second catalyst reaction section arranged in parallel. Therefore, different types of hydrocarbon compounds can be produced simultaneously from one co-electrolytic reaction section by the first catalyst reaction section and the second catalyst reaction section. Furthermore, excess hydrogen in the mixed gas supplied to the hydrogen separation section is separated, and the separated hydrogen can be used for other purposes, so that different types of hydrocarbon compounds can be efficiently produced.

[0019] (8) The hydrocarbon production apparatus according to the above embodiment may further include an upgrading unit which hydrocracking of the hydrocarbon compound produced in the first catalytic reaction unit using hydrogen separated by the hydrogen separation unit is performed to produce a hydrocarbon compound that is lighter than the hydrocarbon compound produced in the first catalytic reaction unit. In this configuration, the hydrogen separated by the hydrogen separation unit is used to produce even higher quality hydrocarbon compounds as required, using the hydrocarbon compounds manufactured in the first catalytic reaction unit. In other words, by improving the electrolytic reaction rate of the co-electrolysis, the excess hydrogen produced is used to manufacture high-quality hydrocarbon compounds, thus further improving the process efficiency of this configuration.

[0020] (9) In the hydrocarbon production apparatus according to the above embodiment, the apparatus further comprises a hydrogen tank for storing the hydrogen separated by the hydrogen separation unit, and a fourth gas flow path connecting the hydrogen tank and the third gas flow path, the fourth gas flow path for adding hydrogen to the mixed gas supplied to the second catalytic reaction unit, wherein the third gas flow path may branch downstream of the point where it connects to the fourth gas flow path and connect to the second catalytic reaction unit and the hydrogen separation unit, respectively. In this configuration, the electrolytic reaction rate of the co-electrolytic reaction section is set high, and hydrogen supplied from the hydrogen tank is added to the mixed gas via the fourth gas flow path. By adding hydrogen, the molar ratio of hydrogen to carbon monoxide in the mixed gas can be adjusted to a molar ratio suitable for the first catalytic reaction section and the second catalytic reaction section, respectively, which produce hydrocarbon compounds. As a result, higher quality hydrocarbon compounds can be produced without using additional hydrogen production or hydrogen supply means.

[0021] (10) In the hydrocarbon production apparatus according to the above embodiment, the apparatus may further include a control unit that controls the amount of hydrogen supplied from the hydrogen tank to the fourth gas flow path and the amount of hydrogen separated from the separated gas by the hydrogen separation unit, in accordance with the amount of hydrocarbon compounds produced in the first catalytic reaction unit and the second catalytic reaction unit, respectively. In this configuration, the molar ratio of the mixed gas is adjusted according to the amount of hydrogen in the hydrogen tank, thereby adjusting the amount of hydrocarbon compounds produced in the first catalytic reaction section and the second catalytic reaction section. As a result, the amount of hydrogen and carbon monoxide produced by co-electrolysis is controlled according to the amount of hydrogen in the hydrogen tank, and no excess raw materials are produced, further improving the process efficiency of the apparatus.

[0022] (11) In the hydrocarbon production apparatus according to the above embodiment, the molar ratio of hydrogen to carbon monoxide required for the hydrocarbon compound produced in the first catalytic reaction section may be smaller than the molar ratio of the hydrocarbon compound produced in the second catalytic reaction section. This configuration improves the electrolytic reaction rate of the co-electrolysis in the co-electrolysis reaction section, allowing hydrocarbon compounds that require more hydrogen for production to be manufactured in the second catalytic reaction section. Conversely, hydrocarbon compounds that require less hydrogen for production in the second catalytic reaction section are manufactured in the first catalytic reaction section. This improves the electrolytic reaction rate of the co-electrolysis in the co-electrolysis reaction section, and by supplying the hydrogen that is not needed in the second catalytic reaction section as the hydrogen needed in the first catalytic reaction section, different types of hydrocarbon compounds can be manufactured simultaneously.

[0023] Furthermore, the present invention can be realized in various forms, for example, as a hydrocarbon production apparatus, a hydrocarbon production system, an SOEC system, a hydrocarbon production method, and a system comprising these apparatuses, a computer program for executing these apparatuses, a server device for distributing this computer program, and a non-temporary storage medium storing the computer program. [Brief explanation of the drawing]

[0024] [Figure 1] This is a schematic block diagram of a hydrocarbon manufacturing apparatus as an embodiment of the present invention. [Figure 2] This is a flowchart of the hydrocarbon manufacturing process. [Figure 3] This is a schematic block diagram of a hydrocarbon production apparatus according to the second embodiment. [Figure 4] This is a schematic block diagram of the hydrocarbon production apparatus according to the third embodiment. [Figure 5] This is a schematic block diagram of the third embodiment in which hydrocarbons are produced using only the methane reactor. [Figure 6] This is a schematic block diagram of the third embodiment in which hydrocarbons are produced in the first catalytic reactor instead of the methane reactor. [Figure 7] This is a flowchart of the hydrocarbon production method according to the third embodiment. [Figure 8] This is a flowchart of a modified hydrocarbon manufacturing method. [Modes for carrying out the invention]

[0025] <First Embodiment> 1. Configuration of the hydrocarbon production equipment: Figure 1 is a schematic block diagram of a hydrocarbon production apparatus 100 as one embodiment of the present invention. The hydrocarbon production apparatus 100 uses hydrogen and carbon monoxide generated by co-electrolysis of SOEC (Solid Oxide Electrolysis Cell) 1 to produce hydrocarbon compounds (hereinafter also simply referred to as "hydrocarbons") in a catalytic reactor 2. In this embodiment, the electrolytic reaction rate of the co-electrolysis is improved by making the molar ratio of the co-electrolysis raw materials supplied to SOEC 1 greater than 2.0. A portion of the hydrogen generated in excess of what is used to produce hydrocarbons in SOEC 1 is used to convert the hydrocarbons produced by the catalytic reactor 2 into lighter hydrocarbons. In other words, the hydrocarbon production apparatus 100 of this embodiment improves process efficiency by improving the electrolytic reaction rate of the co-electrolysis and reusing the excess hydrogen generated.

[0026] As shown in Figure 1, the hydrocarbon production apparatus 100 includes an evaporator 11 that converts liquid water into water vapor, a SOEC (synthetic electrolytic reaction unit) 1 that synthesizes water vapor and gaseous carbon dioxide, a catalytic reactor (first catalytic reaction unit) 2 that produces hydrocarbons from hydrogen and carbon monoxide, a first gas flow path FP1 and a second gas flow path FP2 that connect the SOEC 1 and the catalytic reactor 2, a hydrogen separator (hydrogen separation unit) 3 located in the middle of the first gas flow path FP1, a hydrogen tank 4 that stores the hydrogen separated by the hydrogen separator 3, a pressure sensor S1 that detects the pressure inside the hydrogen tank 4, an upgrading reactor (upgrading unit) 5, and a control unit 6 that controls each unit. In Figure 1, the piping through which the gas flows is represented by solid lines. Also, the control unit 6 and the objects controlled by the control unit 6 are represented by dashed lines.

[0027] The hydrocarbon production apparatus 100 further includes flow controllers 7 and 8 that adjust the flow rate of raw materials supplied to SOEC 1, a dewaterer 12, valves VL1 and VL2, check valves CV1 and CV2, a compressor CP, a flow controller 18 that adjusts the flow rate of hydrogen supplied to the upgrading reactor 5, a gas-liquid separator 14, a liquid separator 15, a first hydrocarbon tank 16 and a second hydrocarbon tank 17 for storing specific hydrocarbons, and a flow sensor S2.

[0028] The evaporator 11 converts the supplied liquid water into high-temperature steam by boiling it. The flow controllers 7, 8, and 18 are controlled by the control unit 6 to adjust the flow rate of gas flowing through the piping. In this embodiment, the control unit 6 is a personal computer equipped with a keyboard and mouse as input receiving units. The control unit 6 controls each unit based on user input received from the keyboard and mouse.

[0029] SOEC1 is a cell stack in which multiple electrolytic cells are stacked. Each electrolytic cell comprises a thin film made of YSZ (yttria-stabilized zirconia) or the like, and electrode layers made of NiO-GDC or the like on both sides of the thin film. In SOEC1, a co-electrolytic reaction occurs, represented by equation (3) below, which is a combination of equations (1) and (2) below. As a result, SOEC1 produces hydrogen and carbon monoxide from the raw materials, water vapor and carbon dioxide. From equation (3) below, the stoichiometric ratio of the molar ratio Rf (=H2O / CO2) of water and carbon dioxide as raw materials for co-electrolysis is 2.0. The molar ratio Rf of the co-electrolytic raw materials supplied to SOEC1 is determined by the control unit 6 controlling the flow controllers 7 and 8.

[0030]

number

number

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[0031] The dewaterer 12 separates and recovers unreacted water vapor contained in the mixed gas discharged from SOEC1. The mixed gas contains, in addition to water vapor, hydrogen produced by co-electrolysis, carbon monoxide, and unreacted carbon dioxide, as shown in equation (3) above.

[0032] As shown in Figure 1, the mixed gas from which water vapor has been recovered flows through either the first gas channel FP1 or the second gas channel FP2, controlled by the opening and closing of valves VL1 and VL2 by the control unit 6. In other words, the control unit 6 switches the supply channel through which hydrogen and carbon monoxide from SOEC1 flows between the first gas channel FP1 and the second gas channel FP2, which is arranged in parallel with the first gas channel FP1. Valve VL1 is located upstream of the hydrogen separator 3 in the first gas channel FP1. Also, check valve CV1 is located downstream of the hydrogen separator 3 in the first gas channel FP1. In the second gas channel FP2, valve VL2 and check valve CV2 are located in order from the upstream side. Check valves CV1 and CV2 prevent the mixed gas supplied to the catalytic reactor 2 from flowing back through either the first gas channel FP1 or the second gas channel FP2.

[0033] The hydrogen separator 3 separates a portion of the hydrogen supplied from the SOEC 1 via the first gas flow path FP1. The separated portion of hydrogen is pressurized by the compressor CP and stored in the hydrogen tank 4. The flow rate of hydrogen separated by the hydrogen separator 3 and supplied to the hydrogen tank 4 is determined by the differential pressure between the hydrogen separator 3 and the hydrogen tank 4. The hydrogen stored in the hydrogen tank 4 from the first gas flow path FP1 is supplied to the upgrading reactor 5 as appropriate, under the control of the flow controller 18 of the control unit 6.

[0034] The catalytic reactor 2 produces hydrocarbons using hydrogen and carbon monoxide supplied through the first gas channel FP1 or the second gas channel FP2. When the supply channel through which hydrogen and carbon monoxide from SOEC1 pass is the first gas channel FP1, the hydrogen separated by the hydrogen separator 3, and the remaining hydrogen after separation, is supplied to the catalytic reactor 2.

[0035] Catalytic reactor 2 produces hydrocarbons by carrying out an FT reaction represented by the following formula (4) using Fe and Co compounds as catalysts.

number

[0036] The mixed gas containing hydrocarbons produced by the catalytic reactor 2 is separated into a gas component and a liquid component by the gas-liquid separator 14. In the present embodiment, the gas-liquid separator 14 sends unreacted hydrogen and carbon monoxide separated as the gas component, and low molecular weight hydrocarbons such as methane to the gas recovery line. On the other hand, the gas-liquid separator 14 sends the hydrocarbon molecules containing 5 or more carbon atoms separated as the liquid component (for example, C5H 10 ,C 10 H 20 ,C 11 H 22 ) to the liquid separator 15.

[0037] In the present embodiment, the liquid separator 15 separates the hydrocarbon molecules containing 5 or more carbon atoms into hydrocarbon molecules containing 11 or more carbon atoms (for example, C 11 H 22 ) and hydrocarbon molecules containing less than 11 carbon atoms (for example, C5H 10 ,C 10 H 20 ). The liquid separator 15 stores the classified hydrocarbon molecules containing 11 or more carbon atoms in the first hydrocarbon tank 16, and stores the classified hydrocarbon molecules containing less than 11 carbon atoms in the second hydrocarbon tank 17. The hydrocarbons stored in the second hydrocarbon tank 17 are supplied to a consumption line.

[0038] The upgrading reactor 5 hydrocracking hydrocarbon molecules containing 11 or more carbon atoms stored in the first hydrocarbon tank 16 using hydrogen stored in the hydrogen tank 4 to produce lighter hydrocarbons. The upgrading reactor 5 also produces hydrocarbon molecules containing fewer than 11 carbon atoms as lighter hydrocarbons and stores the produced lighter hydrocarbons in the second hydrocarbon tank 17. The flow sensor S2 detects the flow rate of hydrocarbons supplied from the first hydrocarbon tank 16 to the upgrading reactor 5. The control unit 6 acquires the flow rate detected by the flow sensor S2 and controls the flow controller 18 according to the acquired detected flow rate to control the flow rate of hydrogen supplied to the upgrading reactor 5.

[0039] 2. Control of hydrocarbon manufacturing equipment: In this embodiment, the control unit 6 switches the supply channel from SOEC1 to the catalytic reactor 2 between the first gas channel FP1 and the second gas channel FP2, depending on the amount of hydrogen stored in the hydrogen tank 4. Furthermore, along with switching the supply channel, the control unit 6 controls the molar ratio Rf of water vapor to carbon dioxide supplied to SOEC1. The control unit 6 determines the amount of hydrogen stored in the hydrogen tank 4 by obtaining the internal pressure of the hydrogen tank 4 using the pressure sensor S1.

[0040] When the pressure inside the hydrogen tank 4 is equal to or greater than the first threshold Th1, the control unit 6 sets the molar ratio Rf of water vapor and carbon dioxide supplied to SOEC1 to the first molar ratio Rm1 and controls the electrolytic reaction rate of co-electrolysis in SOEC1 to the first reaction rate Rr1. The electrolytic reaction rate of co-electrolysis in SOEC1 is controlled by the power supplied to the cells of SOEC1. When the pressure inside the hydrogen tank 4 is equal to or greater than the first threshold Th1, the control unit 6 further selects the second gas flow path FP2 as the supply flow path from SOEC1 to the catalytic reactor 2. In this embodiment, the first threshold Th1 is set to 20% of the maximum value of the internal pressure set in the hydrogen tank 4. The first molar ratio Rm1 is 2.0 and the first reaction rate Rr1 is 80%.

[0041] When the pressure inside the hydrogen tank 4 is less than the first threshold Th1, the control unit 6 sets the molar ratio Rf to a second molar ratio Rm2 that is higher than the first molar ratio Rm1 until the internal pressure of the hydrogen tank 4 exceeds a second threshold TH2 that is higher than the first threshold Th1. The control unit 6 also controls the electrolytic reaction rate of the co-electrolysis in SOEC1 to a second reaction rate Rr2 that is higher than the first reaction rate Rr1. Furthermore, the control unit 6 selects the first gas flow path FP1 as the supply flow path from SOEC1 to the catalytic reactor 2. In this embodiment, the second threshold TH2 is set to 80% of the maximum internal pressure set in the hydrogen tank 4. The second molar ratio Rm2 is 2.5, and the second reaction rate Rr2 is 85%.

[0042] The hydrocarbon production apparatus 100 produces lighter hydrocarbons in the upgrading reactor 5, as needed, in addition to the production of hydrogen and carbon monoxide in SOEC1 and the production of hydrocarbons in catalytic reactor 2. Therefore, the amount of hydrogen stored in hydrogen tank 4 decreases in accordance with the reaction in upgrading reactor 5. For this reason, when the amount of hydrogen stored in hydrogen tank 4 falls below the first threshold Th1, the control unit 6 increases the molar ratio Rf of the raw materials supplied to SOEC1 to supply the hydrogen produced in excess by co-electrolysis to hydrogen tank 4.

[0043] Figure 2 is a flowchart of the hydrocarbon production method. In the hydrocarbon production flow shown in Figure 2, first, the control unit 6 supplies water vapor and carbon dioxide to SOEC1, where the molar ratio Rf of the co-electrolysis raw materials is the first molar ratio Rm1 (=2.0) (step S1). The control unit 6 controls the electrolytic reaction rate of the co-electrolysis carried out in SOEC1 so that the first reaction rate Rr1 (80%) is reached (step S2). The control unit 6 closes valve VL1 and opens valve VL2, selecting the second gas flow path FP2 as the supply flow path (step S3). As a result, all of the mixed gas containing hydrogen and carbon monoxide produced by the co-electrolysis of the raw materials in SOEC1 is supplied to the catalytic reactor 2 via the second gas flow path FP2.

[0044] The control unit 6 acquires the internal pressure of the hydrogen tank 4 detected by the pressure sensor S1 (step S4). Thereafter, the control unit 6 continues to acquire the internal pressure of the hydrogen tank 4. The control unit 6 determines whether the acquired internal pressure of the hydrogen tank 4 is less than the first threshold Th1 (20% of the maximum tank pressure) (step S5). The hydrogen stored in the hydrogen tank 4 may decrease due to hydrocracking performed in the upgrading reactor 5, in addition to the co-electrolysis performed in SOEC1. If it is determined that the internal pressure of the hydrogen tank 4 is greater than or equal to the first threshold Th1 (step S5: NO), SOEC1 continues to perform co-electrolysis of the raw materials under the same conditions and waits until the internal pressure of the hydrogen tank 4 changes to less than the first threshold Th1.

[0045] If it is determined that the internal pressure of the hydrogen tank 4 is less than the first threshold Th1 (step S5: YES), the control unit 6 supplies the raw material to SOEC 1 with the molar ratio Rf changed to the second molar ratio Rm2 (=2.5) (step S6). The control unit 6 changes the electrolytic reaction rate of the co-electrolysis performed in SOEC 1 from the first reaction rate Rr1 (80%) to the second reaction rate Rr2 (85%) (step S7). The control unit 6 closes the open valve VL2 and opens the closed valve VL1, switching the supply flow path from the second gas flow path FP2 to the first gas flow path FP1 (step S8). As a result, some of the hydrogen in the mixed gas containing hydrogen and carbon monoxide produced by the co-electrolysis of the raw material in SOEC 1 is separated by the hydrogen separator 3 and sent to the hydrogen tank 4. Of the mixed gas flowing through the first gas flow path FP1, the remaining mixed gas after the separation of hydrogen is supplied to the catalytic reactor 2.

[0046] The control unit 6 determines whether the internal pressure of the hydrogen tank 4 exceeds the second threshold TH2 (80% of the maximum pressure of the tank) (step S9). If it is determined that the internal pressure of the hydrogen tank 4 is less than or equal to the second threshold TH2 (step S9: NO), the control unit 6 waits until the internal pressure of the hydrogen tank 4 exceeds the second threshold TH2. If it is determined that the internal pressure of the hydrogen tank 4 has exceeded the second threshold TH2 (step S9: YES), the control unit 6 performs the processing from step S1 onward. Although not shown in Figure 2, the control unit 6 can terminate the hydrocarbon manufacturing process by accepting predetermined operations from the user, regardless of which process is being performed.

[0047] As described above, the hydrocarbon production apparatus 100 of this embodiment includes a SOEC 1 that co-electrolyzes water vapor and gaseous carbon dioxide as raw materials, a catalytic reactor 2 that produces hydrocarbons from hydrogen and carbon monoxide, and a hydrogen separator 3 that separates a portion of the hydrogen supplied from SOEC 1. Therefore, in this embodiment, hydrogen and carbon monoxide produced from water and carbon dioxide by SOEC 1 are used to produce hydrocarbons in catalytic reactor 2. The molar ratio (H2 / CO) of hydrogen to carbon monoxide supplied to catalytic reactor 2 during hydrocarbon production is preferably around 2.0. Therefore, the molar ratio (H2O / CO2) of water and carbon dioxide as raw materials that undergo co-electrolysis in SOEC 1 is preferably 2.0. However, when co-electrolyzing raw materials with a molar ratio of 2.0, it is necessary to set the electrolytic reaction rate of the co-electrolysis lower than 100% in order to suppress damage such as deterioration that occurs in SOEC 1. On the other hand, it is known that setting the molar ratio of the co-electrolysis raw materials supplied to SOEC1 to a value greater than 2.0 allows for a higher electrolytic reaction rate of the co-electrolysis while suppressing damage to SOEC1. In this embodiment, the hydrogen separator 3 separates a portion of the hydrogen produced by the co-electrolysis. Therefore, the electrolytic reaction rate is increased by increasing the molar ratio of the co-electrolysis raw materials supplied to SOEC1, and any excess hydrogen generated by the co-electrolysis is separated by the hydrogen separator 3. The separated hydrogen is used for other purposes, such as lightening hydrocarbons by the upgrading reactor 5. As a result, the electrolytic reaction rate of the co-electrolysis is improved, and the utilization rate of raw materials and the process efficiency of the apparatus are improved without recirculating unused gases. Furthermore, since the hydrocarbon production apparatus 100 of this embodiment does not require a separate apparatus for hydrogen production and supply, the hydrocarbon production apparatus 100 is miniaturized and simplified.

[0048] Furthermore, the upgrading reactor 5 of this embodiment performs hydrocracking of hydrocarbons stored in the first hydrocarbon tank 16 using hydrogen separated by the hydrogen separator 3 to produce lighter hydrocarbons. Therefore, in this embodiment, the hydrogen separated by the hydrogen separator 3 is used to produce even higher quality hydrocarbons from the hydrocarbons produced in the catalytic reactor 2, as required. In other words, by improving the electrolytic reaction rate of the co-electrolysis in SOEC1, the excess hydrogen produced is used to produce high-quality hydrocarbons, thereby further improving the process efficiency of the hydrocarbon production apparatus 100.

[0049] Furthermore, the first gas flow path FP1 in this embodiment connects the SOEC1 and the catalytic reactor 2. The hydrogen separator 3 is located in the middle of the first gas flow path FP1. Therefore, in this embodiment, the process efficiency of the hydrocarbon production apparatus 100 can be improved with a simple configuration in which the hydrogen separator 3 is located in the middle of the first gas flow path FP1.

[0050] Furthermore, the control unit 6 in this embodiment switches the supply channel through which hydrogen and carbon monoxide from SOEC1 flow between the first gas channel FP1 and the second gas channel FP2, which is arranged in parallel with the first gas channel FP1. Therefore, in this embodiment, when the amount of hydrogen in the hydrogen tank 4 is small, the first gas channel FP1 is selected as the supply channel, and the amount of hydrogen in the hydrogen tank 4 can be increased by the hydrogen separator 3 located in the middle of the first gas channel FP1. On the other hand, when the amount of hydrogen in the hydrogen tank 4 is large, the second gas channel FP2 is selected as the supply channel. In particular, when the amount of hydrogen in the hydrogen tank 4 is large, the molar ratio of the co-electrolysis raw materials is set to the stoichiometric ratio of 2.0, so that no excess hydrogen is generated. As a result, the amount of hydrogen and carbon monoxide produced by co-electrolysis is controlled according to the amount of hydrogen in the hydrogen tank 4, so that the process efficiency of the hydrocarbon production apparatus 100 is further improved.

[0051] Furthermore, the control unit 6 of this embodiment switches the supply channel from SOEC1 to the catalytic reactor 2 between the first gas channel FP1 and the second gas channel FP2, depending on the amount of hydrogen stored in the hydrogen tank 4. In addition, along with switching the supply channel, the control unit 6 controls the molar ratio Rf of water vapor to carbon dioxide supplied to SOEC1. As a result, the amount of hydrogen stored in the hydrogen tank 4 is detected as the pressure inside the hydrogen tank 4 and can be determined with a simple configuration. The molar ratio Rf of the co-electrolysis raw materials is controlled according to the internal pressure of the hydrogen tank 4. Therefore, when the internal pressure of the hydrogen tank 4 is low, the amount of hydrogen stored in the hydrogen tank 4 can be increased by increasing the molar ratio Rf of the co-electrolysis raw materials, and the electrolytic reaction rate of the co-electrolysis can be improved. As a result, the process efficiency of the hydrocarbon production apparatus 100 of this embodiment is further improved.

[0052] Furthermore, in this embodiment, when the pressure inside the hydrogen tank 4 is equal to or greater than the first threshold Th1, the control unit 6 sets the molar ratio Rf of water vapor to carbon dioxide to the first molar ratio Rm1 (2.0) and controls the electrolytic reaction rate of co-electrolysis in SOEC1 to the first reaction rate Rr1 (80%). The control unit 6 also selects the second gas flow path FP2 as the supply flow path from SOEC1 to the catalytic reactor 2. When the pressure inside the hydrogen tank 4 is less than the first threshold Th1, the control unit 6 sets the molar ratio Rf to the second molar ratio Rm2 (2.5), which is higher than the first molar ratio Rm1 (2.0), until the internal pressure of the hydrogen tank 4 exceeds the second threshold TH2, which is higher than the first threshold Th1. The control unit 6 also controls the electrolytic reaction rate of co-electrolysis in SOEC1 to the second reaction rate Rr2 (85%), which is higher than the first reaction rate Rr1 (80%), and selects the first gas flow path FP1 as the supply flow path from SOEC1 to the catalytic reactor 2. In other words, when a certain amount of hydrogen determined by the first threshold Th1 is stored in the hydrogen tank 4, co-electrolysis is performed with a low first molar ratio Rm1 and a low first electrolytic reaction rate Rr1 of the raw materials, thereby suppressing the production of excess hydrogen by co-electrolysis. On the other hand, when a certain amount of hydrogen is not stored in the hydrogen tank 4, co-electrolysis is performed with a high second molar ratio Rm2 and a second electrolytic reaction rate Rr2 of the raw materials, and the excess hydrogen produced by co-electrolysis is stored in the hydrogen tank 4. Hydrogen is stored in the hydrogen tank until the pressure inside the hydrogen tank 4 exceeds the second threshold TH2. Because the hydrocarbon production apparatus 100 of this embodiment switches control based on criteria such as thresholds, it is possible to improve process efficiency while maintaining the amount of hydrogen stored in the hydrogen tank 4 at or above a certain level with simple control.

[0053] When the molar ratio Rf of water vapor to carbon dioxide is 2.0 and the electrolytic reaction rate of co-electrolysis in SOEC1 is 80%, the upper limit of the thermodynamic carbon deposition temperature is 640°C. On the other hand, when the molar ratio Rf of water vapor to carbon dioxide is 2.5 and the electrolytic reaction rate of co-electrolysis in SOEC1 is 85%, the upper limit of the thermodynamic carbon deposition temperature is also 640°C. Therefore, in this embodiment, the molar ratio Rf and the electrolytic reaction rate can be set higher without changing the upper limit of the thermodynamic carbon deposition temperature.

[0054] <Second Embodiment> Figure 3 is a schematic block diagram of the hydrocarbon production apparatus 100a of the second embodiment. As shown in Figure 3, the hydrocarbon production apparatus 100a of the second embodiment does not have a second gas flow path FP2 and a check valve CV2 compared to the hydrocarbon production apparatus 100 of the first embodiment, but it does have a hydrogen valve VL3. In the second embodiment, the configuration and control that differ from the first embodiment will be described, and the description of the configuration and control that are the same as the first embodiment will be omitted.

[0055] As shown in Figure 3, the hydrogen valve VL3 in the second embodiment is positioned between the hydrogen separator 3 and the compressor CP. The hydrogen valve VL3 is controlled by the control unit 6a to adjust the flow rate of hydrogen from the hydrogen separator 3 to the compressor CP. In the second embodiment, when the first gas flow path FP1 is selected as the supply flow path in the first embodiment, the control unit 6a opens the hydrogen valve VL3 to supply hydrogen from the hydrogen separator 3 to the hydrogen tank 4. On the other hand, when the second gas flow path FP2 is selected as the supply flow path in the first embodiment, the control unit 6a closes the hydrogen valve VL3 to limit the supply of hydrogen flowing through the first gas flow path FP1 to the hydrogen tank 4.

[0056] As described above, the hydrocarbon production apparatus 100a of the second embodiment does not necessarily have to include two first gas flow paths FP1 and second gas flow paths FP2 that function as supply channels. Preferably, the flow rate of hydrogen separated by the hydrogen separator 3 is controlled in accordance with the change in the molar ratio Rf of the co-electrolytic raw materials controlled by the control unit 6a.

[0057] <Third Embodiment> Figure 4 is a schematic block diagram of the hydrocarbon production apparatus 100b of the third embodiment. The hydrocarbon production apparatus 100b of the third embodiment differs significantly from the hydrocarbon production apparatus 100a of the second embodiment in that it includes a first catalytic reactor 2b and a methane reactor 19 that function as a second catalytic reactor, each capable of producing different hydrocarbons. By including the first catalytic reactor 2b and the methane reactor 19, the hydrocarbon production apparatus 100b of the third embodiment can produce different types of hydrocarbons simultaneously and with high efficiency from a single SOEC1. In the third embodiment, the differences from the hydrocarbon production apparatus 100a of the second embodiment will be explained, and the explanation of the same configuration as the hydrocarbon production apparatus 100a of the second embodiment will be omitted.

[0058] The hydrocarbon production apparatus 100b of the third embodiment includes an evaporator 11, an SOEC 1, a first catalytic reactor 2b, a methane reactor (second catalytic reactor) 19 for producing methane as a hydrocarbon, a third gas channel FP3 connecting the SOEC 1 and the methane reactor 19, a hydrogen tank 4, a fourth gas channel FP4 connecting the hydrogen tank 4 and the third gas channel FP3, a hydrogen separator 3, a pressure sensor S1, an upgrading reactor 5, and a control unit 6b for controlling each part.

[0059] The hydrocarbon production apparatus 100b further includes flow controllers 7, 8, 18, a dewaterer 12, a compressor CP, a gas-liquid separator 14, a liquid separator 15, a first hydrocarbon tank 16, a second hydrocarbon tank 17, a liquid level sensor S4 for detecting the height of the liquid level in the second hydrocarbon tank 17, a flow sensor S2, a flow controller 25 for controlling the flow rate of the mixed gas GS1 supplied from SOEC 1 to the methane reactor 19, a dewaterer 22 for separating and recovering water vapor contained in the mixed gas GS1 containing hydrocarbons produced in the methane reactor 19, a methane tank 21 for storing the hydrocarbons from which the water vapor has been separated and recovered, a pressure sensor S3 for detecting the pressure inside the methane tank 21, a flow controller 24 for controlling the flow rate of the separated gas supplied from the mixed gas GS1 to the hydrogen separator 3, and a flow controller 23 for controlling the flow rate of hydrogen supplied from the hydrogen tank 4 to the third gas flow path FP3 via the fourth gas flow path FP4.

[0060] The methane reactor 19 produces methane by causing a reaction represented by the following formula (5) using Fe and Co compounds as catalysts.

number

[0061] The methane reactor 19 uses at least a portion of the mixed gas GS1, which contains carbon monoxide and hydrogen, supplied from SOEC1, to produce methane different from the hydrocarbons produced in the first catalytic reactor 2b. In other words, different types of hydrocarbons are produced in the first catalytic reactor 2b than the methane produced in the methane reactor 19, and the hydrocarbons produced in the first catalytic reactor 2b may include the same types of hydrocarbons as the methane produced in the methane reactor 19.

[0062] As shown in equation (5) above, the stoichiometric ratio Rp of hydrogen to carbon monoxide in the raw materials for methane production is 3.0. That is, the stoichiometric ratio (molar ratio of hydrogen to carbon monoxide) Rp (=H2 / CO) required to produce hydrocarbons in the first catalytic reactor 2b is smaller than the stoichiometric ratio of 3.0 required to produce methane in the methane reactor 19. In Figure 4, the gas flow in the piping when both the first catalytic reactor 2b and the methane reactor 19 are producing hydrocarbons is represented by arrows.

[0063] As shown in Figure 4, the third gas channel FP3 connects SOEC1 in parallel to the methane reactor 19 and the hydrogen separator 3, respectively. Therefore, the third gas channel FP3 supplies the mixed gas GS1 supplied from SOEC1 to the methane reactor 19 and the hydrogen separator 3. The hydrogen separator 3 separates a portion of the hydrogen contained in the mixed gas GS1 supplied from SOEC1 via the third gas channel FP3. The separated hydrogen is stored in the hydrogen tank 4.

[0064] The fourth gas channel FP4 connects the hydrogen tank 4 to connection point P1 in the third gas channel FP3, which is downstream of the dewaterer 12 and upstream of the methane reactor 19 and hydrogen separator 3. Therefore, the hydrogen supplied from the hydrogen tank 4 is mixed with carbon monoxide and hydrogen supplied from SOEC1 to form a mixed gas GS1, which is then supplied to the methane reactor 19 and the hydrogen separator 3, respectively. In other words, the fourth gas channel FP4 adds the hydrogen supplied from the hydrogen tank 4 to the mixed gas GS1 supplied to the methane reactor 19. The third gas channel FP3 branches downstream of connection point P1, where it connects to the fourth gas channel FP4, and connects to the methane reactor 19 and the hydrogen separator 3, respectively.

[0065] Flow controllers 23-25 ​​adjust the flow rate of gas flowing through the piping under the control of control unit 6b. Flow controller 25 controls the flow rate of mixed gas GS1 supplied to the methane reactor 19 via the third gas channel FP3. Flow controller 24 controls the flow rate of mixed gas GS1 supplied to the hydrogen separator 3 via the third gas channel FP3. Flow controller 23 controls the flow rate of hydrogen supplied from the hydrogen tank 4 to the third gas channel FP3 via the fourth gas channel FP4.

[0066] The control unit 6b controls the amount of methane produced in the methane reactor 19 according to the pressure in the methane tank 21 detected by the pressure sensor S3. The control unit 6b also controls the amount of light hydrocarbons produced in the upgrading reactor 5 according to the amount stored in the second hydrocarbon tank 17 detected by the liquid level sensor S4.

[0067] In the state shown in Figure 4, the control unit 6b controls the flow controllers 7, 8, 18, 23-25 ​​to simultaneously produce different types of hydrocarbons using the methane reactor 19 and the first catalytic reactor 2b.

[0068] Here, as shown in equation (4) above, in the FT reaction carried out in the first catalytic reactor 2b, the stoichiometric ratio Rp of hydrogen to carbon monoxide is around 2.0. Therefore, in order to improve the process efficiency of the hydrocarbon production apparatus 100b, the molar ratio Rp of the gas supplied to the first catalytic reactor 2b is preferably around 2.0. On the other hand, as shown in equation (5) above, the molar ratio Rp of the reaction carried out in the methane reactor 19 is 3.0, so the molar ratio Rp of the mixed gas GS1 supplied to the methane reactor 19 is preferably 3.0.

[0069] In the third embodiment, the control unit 6b supplies steam and carbon dioxide to the SOEC1 by controlling the flow controllers 7 and 8 to produce hydrogen and carbon monoxide, which are raw materials for hydrocarbons. The control unit 6b controls the amount of hydrogen supplied from the hydrogen tank 4 and the amount of hydrogen separated by the hydrogen separator 3 and stored in the hydrogen tank 4, according to the amount of hydrocarbons produced in the first catalytic reactor 2b and the methane reactor 19, respectively.

[0070] For example, the control unit 6b controls the flow rates of water vapor and carbon dioxide supplied to SOEC1 so that the molar ratio Rp of hydrogen to carbon monoxide produced is (3-X). X is a value greater than zero and less than 1. Therefore, (3-X) is a value greater than 2 and less than 3.

[0071] The hydrocarbon feedstock gas with a molar ratio Rp of (3-X) generated by the co-electrolysis of SOEC1 is separated and recovered from unreacted water vapor by the dewaterer 12. The control unit 6b adds hydrogen from the hydrogen tank 4 to the mixed gas GS1 containing hydrogen and carbon monoxide, which is discharged from the dewaterer 12 and flows through the third gas channel FP3, by controlling the flow controller 23. The control unit 6b adds an amount of hydrogen to the mixed gas GS1 so that its molar ratio Rp changes from (3-X) to 3.0. The control unit 6b supplies a portion of the mixed gas GS1 to the methane reactor 19 and the remaining mixed gas GS1 to the hydrogen separator 3 by controlling the flow controllers 24 and 25. The amount of hydrogen added to the mixed gas GS1 from the hydrogen tank 4 varies according to the flow rate and molar ratio Rp of the mixed gas GS1.

[0072] The control unit 6b controls the flow controllers 24 and 25 according to instructions received from the outside, the liquid level height of the second hydrocarbon tank 17 detected by the liquid level sensor S4, or the pressure in the methane tank 21 detected by the pressure sensor S3.

[0073] The methane reactor 19 produces methane from the supplied mixed gas GS1 with a molar ratio Rp of 3.0. The gas containing the produced methane is separated and recovered from water vapor by the dewaterer 22. The methane from which the water vapor has been removed is stored in the methane tank 21 and supplied to the consumption line.

[0074] The hydrogen separator 3 separates some of the hydrogen from the supplied mixed gas GS1 so that its molar ratio Rp is approximately 2.0, and supplies it to the hydrogen tank 4. The mixed gas GS1, with some of the hydrogen separated and a molar ratio Rp of approximately 2.0, is supplied to the first catalytic reactor 2b. In the first catalytic reactor 2b, several types of hydrocarbons are produced from the mixed gas GS1 by the FT reaction, as in the first embodiment. The mixed gas containing the produced hydrocarbons is supplied to the gas-liquid separator 14. The amount of hydrogen separated by the hydrogen separator 3 and stored in the hydrogen tank 4 varies depending on the amount of mixed gas GS1 supplied to the hydrogen separator 3 and its molar ratio Rp.

[0075] Figure 5 is a schematic block diagram of the third embodiment in which hydrocarbons are produced using only the methane reactor 19. Figure 5 shows a state in which the control unit 6b controls each part to produce methane in the methane reactor 19, and does not produce hydrocarbons by not performing the FT reaction in the first catalytic reactor 2b. In Figure 5, the piping through which the raw materials and produced gases such as methane flow is represented as thicker.

[0076] In the state shown in Figure 5, the control unit 6b controls the flow controllers 7 and 8 so that the molar ratio Rp of hydrogen to carbon monoxide produced in SOEC1 becomes 3.0. The mixed gas GS1, from which water vapor has been separated by the dewaterer 12, is supplied to the methane reactor 19 without hydrogen being added from the hydrogen tank 4. In the methane reactor 19, methane is produced using the mixed gas GS1 with a molar ratio Rp of 3.0. The produced methane is stored in the methane reactor 19.

[0077] Figure 6 is a schematic block diagram of the third embodiment in which hydrocarbons are produced in the first catalytic reactor 2b without producing hydrocarbons in the methane reactor 19. Figure 6 shows a state in which the control unit 6b controls each part to produce hydrocarbons by performing an FT reaction in the first catalytic reactor 2b without producing methane in the methane reactor 19. The hydrocarbon production apparatus 100b shown in Figure 6, which does not produce methane in the reactor 19, is substantially the same as the hydrocarbon production apparatus 100a of the second embodiment. The control unit 6b adds hydrogen to the mixed gas GS1 supplied to the first catalytic reactor 2b by controlling the flow controller 23 so that the molar ratio Rp of the mixed gas GS1 is 2.0 or more. Note that in Figure 6, as in Figure 5, the piping through which the raw materials and the produced hydrocarbon gases flow is represented as thicker.

[0078] In the third embodiment, the control unit 6b controls the hydrocarbons produced in the methane reactor 19 and the first catalytic reactor 2b using instructions to the hydrocarbon production apparatus 100b and the detected values ​​of each sensor S1 to S4. For example, when switching from a state in which no methane is produced in the methane reactor 19 as shown in Figure 6 to a state in which hydrocarbons are produced only in the methane reactor 19 as shown in Figure 5, the control unit 6b controls the flow rate controller 23 to add hydrogen from the hydrogen tank 4 to the mixed gas GS1. This allows for the temporary replenishment of hydrogen from the hydrogen tank 4 when increasing the amount of hydrogen produced in SOEC1 from a state where the molar ratio Rp is small, i.e., the amount of hydrogen produced in SOEC1 is small, corresponding to the first catalytic reactor 2b, and the amount of hydrogen produced in SOEC1 cannot keep up with the state change.

[0079] Figure 7 is a flowchart of the hydrocarbon production method according to the third embodiment. In the hydrocarbon production flow shown in Figure 3, first, the control unit 6b controls the flow controllers 7 and 8 to supply water vapor and carbon dioxide, which are the raw materials for co-electrolysis, to SOEC1 in a predetermined molar ratio Rf (step S21). The control unit 6b sets and controls the electrolytic reaction rate of the co-electrolysis performed in SOEC1 to a predetermined value (step S22). SOEC1 performs a co-electrolytic reaction process to produce hydrogen and carbon monoxide, which are raw materials for hydrocarbons, using the raw materials in a predetermined molar ratio Rf (step S23). The mixed gas GS1 produced by the co-electrolytic reaction process has its water separated by the dewaterer 12 and is supplied to the methane reactor 19 and the hydrogen separator 3. The predetermined molar ratio Rf and predetermined electrolytic reaction rate set in steps S21 and S22 may be preset initial values, or they may be set to values ​​according to the detection values ​​of each sensor S1 to S4.

[0080] Next, the control unit 6b controls the flow rate controller 23 to perform a hydrogen addition process in which hydrogen is added from the hydrogen tank 4 to the mixed gas GS1 flowing through the third gas channel FP3 (step S24). In the third embodiment, the control unit 6b adds hydrogen so that the molar ratio Rp of hydrogen to carbon monoxide in the mixed gas GS1 becomes 3.0. That is, the control unit 6b adds an amount of hydrogen determined according to the flow rate of the mixed gas GS1 generated by SOEC1 from the hydrogen tank 4 to the mixed gas GS1. The control unit 6b controls the flow rates of the mixed gas GS1 supplied to the methane reactor 19 and the hydrogen separator 3, respectively, by controlling the flow rate controllers 24 and 25 (step S25).

[0081] The methane reactor 19 performs a second catalytic reaction step to produce methane using the mixed gas GS1 supplied by the flow controller 25 (step S26). The produced methane is separated from the water vapor by the dewaterer 22 and stored in the methane tank 21. The hydrogen separator 3 performs a hydrogen separation step to separate a portion of the hydrogen contained in the mixed gas GS1 supplied by the flow controller 24 (step S27). In the hydrogen separation step, the amount of hydrogen separated is determined according to the flow rate of the mixed gas GS1 supplied to the hydrogen separator 3 so that the molar ratio Rp of hydrogen to carbon monoxide supplied to the first catalytic reactor 2b is approximately 2.0. The separated hydrogen is supplied to the hydrogen tank 4. The first catalytic reactor 2b performs a first catalytic reaction step to produce hydrocarbons by generating an FT reaction using the mixed gas GS1 supplied with some of the separated hydrogen (step S28).

[0082] The control unit 6b determines whether or not there is an instruction to change the control content (step S29). For example, if the detection values ​​of each sensor S1 to S4 exceed a predetermined threshold, or if an instruction to change the control content is received from the user, the control unit 6b changes the flow rate controllers 7, 8, 18, 23 to 25 and the electrolytic reaction rate of SOEC1. If it is determined that there is no change in the control content (step S29: NO), the control unit 6b monitors for the receipt of an instruction to change the control content without changing it. If the control unit 6b determines that there is an instruction to change the control content (step S29: YES), it controls the flow rate controllers 7, 8, 28, 23 to 25 to change the electrolytic reaction rate of SOEC1 and proceeds with the processing from step S21 onwards. Examples of the changed control state include the states shown in Figures 5 and 6. Although not shown in Figure 7, the control unit 6b can terminate the hydrocarbon manufacturing process regardless of which process is being performed.

[0083] As described above, the hydrocarbon production apparatus 100b of the third embodiment includes a first catalytic reactor 2b and a methane reactor 19, each capable of producing different hydrocarbons. The third gas channel FP3 supplies the mixed gas GS1 supplied from SOEC1 to the methane reactor 19 and the hydrogen separator 3. The hydrogen separator 3 separates a portion of the hydrogen contained in the mixed gas GS1 supplied from SOEC1 via the third gas channel FP3. As a result, the mixed gas GS1, containing carbon monoxide and hydrogen generated in SOEC1, is supplied to the first catalytic reactor 2b and the methane reactor 19, which are arranged in parallel. Consequently, different types of hydrocarbons can be produced simultaneously from a single SOEC1 by the first catalytic reactor 2b and the methane reactor 19. Furthermore, the hydrogen separator 3 separates excess hydrogen from the mixed gas GS1 supplied to the first catalytic reactor 2b, and the separated excess hydrogen can be used for other purposes. Therefore, the hydrocarbon production apparatus 100b can produce different types of hydrocarbon compounds simultaneously and efficiently.

[0084] Furthermore, the hydrogen tank 4 stores the hydrogen contained in the mixed gas GS1 separated by the hydrogen separator 3. The separated hydrogen is stored in the hydrogen tank 4. The fourth gas channel FP4 adds hydrogen supplied from the hydrogen tank 4 to the mixed gas GS1 supplied to the methane reactor 19. The third gas channel FP3 branches downstream of the connection point P1 where it connects to the fourth gas channel FP4, and connects to the methane reactor 19 and the hydrogen separator 3, respectively. In the third embodiment, the electrolytic reaction rate of the co-electrolysis in SOEC1 is set high, and hydrogen supplied from the hydrogen tank 4 is added to the mixed gas GS1 via the fourth gas channel FP4. By adding hydrogen, the molar ratio Rp of hydrogen to carbon monoxide in the mixed gas GS1 can be adjusted to a molar ratio suitable for the first catalytic reactor 2b and the methane reactor 19, respectively, which produce hydrocarbons. As a result, the hydrocarbon production apparatus 100b of the third embodiment can produce higher quality hydrocarbons without using additional hydrogen production or hydrogen supply means.

[0085] Furthermore, the control unit 6b controls the amount of hydrogen supplied from the hydrogen tank 4 and the amount of hydrogen separated by the hydrogen separator 3 and stored in the hydrogen tank 4, according to the amount of hydrocarbons produced in the first catalytic reactor 2b and the methane reactor 19, respectively. In the third embodiment, the molar ratio Rp of the mixed gas GS1 is adjusted according to the amount of hydrogen in the hydrogen tank 4, thereby adjusting the amount of hydrocarbons produced in the first catalytic reactor 2b and the methane reactor 19. As a result, the amount of hydrogen and carbon monoxide produced by the co-electrolysis of SOEC1 is controlled according to the amount of hydrogen in the hydrogen tank 4, and no excess hydrocarbon raw material is generated, further improving the process efficiency of the apparatus.

[0086] Furthermore, the molar ratio Rp of hydrogen to carbon monoxide required to produce hydrocarbons in the first catalytic reactor 2b is smaller than the molar ratio of 3.0 required to produce methane in the methane reactor 19. In the third embodiment, the electrolytic reaction rate of the co-electrolysis in SOEC1 is improved to produce methane in the methane reactor 19, which requires more hydrogen for production. On the other hand, hydrocarbons that require less hydrogen than methane are produced in the first catalytic reactor 2b. This improves the electrolytic reaction rate by co-electrolysis, and by supplying the hydrogen that is not needed in the first catalytic reactor 2b as the hydrogen needed in the methane reactor 19, different types of hydrocarbons can be produced simultaneously.

[0087] <Modification of the above embodiment> The present invention is not limited to the embodiments described above, and can be implemented in various forms without departing from its spirit. For example, the following modifications are possible. In addition, in the above embodiments, some of the configurations implemented by hardware may be replaced with software, and conversely, some of the configurations implemented by software may be replaced with hardware.

[0088] [Example 1] The hydrocarbon production apparatus 100 in the above embodiment is an example and can be modified to include a co-electrolytic reaction section for co-electrolysis, a hydrogen separator 3 for separating a portion of the generated hydrogen, and a catalytic reactor 2 for producing hydrocarbons using the remaining hydrogen and carbon monoxide after separation. The hydrocarbon production apparatus 100, 100a, and 100b do not necessarily have, for example, a hydrogen tank 4 or an upgrading reactor 5. The hydrocarbon production apparatus 100 may also have other configurations that utilize hydrogen, and the excess hydrogen generated by co-electrolysis may be used in those configurations.

[0089] Furthermore, hydrocarbon production apparatuses 100, 100a, and 100b may also include a third hydrocarbon tank and a fourth hydrocarbon tank that are different from either the first hydrocarbon tank 16 or the second hydrocarbon tank 17. In this case, the third and fourth hydrocarbon tanks may store hydrocarbons that have been further hydrocracking and lightened from the hydrocarbons stored in the first hydrocarbon tank 16.

[0090] In the above embodiment, the first threshold Th1 and second threshold TH2 of the internal pressure of the hydrogen tank 4, the first molar ratio Rm1 and second molar ratio Rm2 of the co-electrolysis raw materials, and the first reaction rate Rr1 and second reaction rate Rr2 of the electrolysis reaction rate were given as examples of indicators for the control unit 6 to control the flow controllers 7,8 and SOEC1, but the indicators can be modified. For example, the control unit 6 may control each part according to a preset map or formula. The specific numerical values ​​of the first threshold Th1, etc., can be modified as appropriate. Note that the flow controllers 7,8 and valves VL1,VL2 controlled by the control unit 6 may be considered as part of the control unit 6.

[0091] [Differentiation 2] Figure 8 is a flowchart of a modified hydrocarbon production method. The modified hydrocarbon production flow shown in Figure 8 differs from the hydrocarbon production flow of the embodiment described above (Figure 2) in that, first, the internal pressure of the hydrogen tank 4 is detected, and the molar ratio Rf of the raw material supplied to SOEC1 at the start changes according to the detected internal pressure. In terms of processing, steps S11 and S12 of the modified method are new, while steps S13 to S20 of the modified method are the same as steps S1 to S3 and S5 to S9 of the embodiment, respectively. Therefore, in the modified method, we will describe the processes that differ from the embodiment and omit the description of the processes that are the same.

[0092] As shown in Figure 8, in the modified example, first, the control unit 6 acquires the internal pressure of the hydrogen tank 4 detected by the pressure sensor S1 (step S11). Thereafter, the control unit 6 continues to acquire the internal pressure of the hydrogen tank 4. The control unit 6 determines whether the acquired internal pressure of the hydrogen tank 4 is equal to or greater than the first threshold Th1 (step S12). If it is determined that the internal pressure of the hydrogen tank 4 is equal to or greater than the first threshold Th1 (step S12: YES), the processing from step S13 onwards is performed. On the other hand, if it is determined that the internal pressure of the hydrogen tank 4 is less than the first threshold Th1 (step S12: NO), the processing from step S17 onwards is performed. As described above, the control of SOEC1 according to the internal pressure of the hydrogen tank 4 may be performed at the start of hydrocarbon production as in the modified example, or it may be performed after a predetermined process from the start of production as in the embodiment.

[0093] [Difference 3] The hydrocarbon production apparatus 100b of the third embodiment described above included a methane reactor 19 for producing a different type of hydrocarbon from the hydrocarbon produced in the first catalytic reactor 2b. However, instead of the methane reactor 19, a reactor for producing hydrocarbons other than methane may be included. It is preferable that the stoichiometric molar ratio Rp required for production of the hydrocarbon produced in the reactor replacing the methane reactor 19 is greater than the stoichiometric molar ratio Rp required for production of the hydrocarbon produced in the first catalytic reactor 2b.

[0094] The hydrocarbon production apparatus 100b of the third embodiment does not necessarily have a hydrogen tank 4. The third gas flow path FP3 and the fourth gas flow path FP4 of the hydrocarbon production apparatus 100 shown in Figures 4 to 6 are one structural example for arranging the methane reactor 19 and the first catalytic reactor 2b in parallel, and are modifiable.

[0095] The embodiments of this specification have been described above based on the embodiments and modifications described above. The embodiments described above are for the purpose of facilitating understanding of this specification and do not limit it. This specification may be modified and improved without departing from its spirit and the scope of the claims, and equivalents thereof are included in this specification. Furthermore, any technical features that are not described as essential in this specification may be deleted as appropriate.

[0096] The present invention can also be realized in the following forms. [Application Example 1] A hydrocarbon production apparatus, A co-electrolytic reaction section that generates hydrogen and carbon monoxide by co-electrolytically reacting water and carbon dioxide, A hydrogen separation unit separates a portion of the hydrogen generated by the aforementioned co-electrolytic reaction unit, A 11th catalytic reaction unit produces hydrocarbon compounds by using a catalyst on the residual hydrogen after separation supplied from the co-electrolytic reaction unit and the carbon monoxide supplied from the co-electrolytic reaction unit, A hydrocarbon production apparatus equipped with the following features. [Application Example 2] The hydrocarbon production apparatus described in Application Example 1, further, A hydrocarbon production apparatus comprising an upgrading section that performs hydrocracking of a hydrocarbon compound produced in the first catalytic reaction section using hydrogen separated by the hydrogen separation section to produce a lighter hydrocarbon compound. [Application Example 3] A hydrocarbon production apparatus as described in Application Example 1 or Application Example 2, further, The system includes a first gas channel through which hydrogen and carbon monoxide generated by the aforementioned co-electrolytic reaction section flow. The hydrogen separation unit is located in the middle of the first gas flow path. A hydrocarbon production apparatus wherein the first catalytic reaction section is supplied with the remaining hydrogen after separation by the hydrogen separation section and carbon monoxide via the first gas flow path. [Application Example 4] A hydrocarbon production apparatus described in any one of Application Examples 1 to 3, further, A hydrogen tank for storing the hydrogen separated by the hydrogen separation unit, A second gas channel is arranged in parallel with the first gas channel, through which hydrogen and carbon monoxide generated by the co-electrolytic reaction section flow, A control unit that switches the supply channel for hydrogen and carbon monoxide from the co-electrolytic reaction unit between the first gas channel and the second gas channel, depending on the amount of hydrogen stored in the hydrogen tank, A hydrocarbon production apparatus equipped with the following features. [Application Example 5] A hydrocarbon production apparatus described in any one of Application Examples 1 to 4, further, The hydrogen tank is equipped with a pressure sensor that detects the pressure inside the hydrogen tank, A hydrocarbon production apparatus comprising a control unit that, in accordance with the detected pressure in the hydrogen tank, switches the supply channel for hydrogen and carbon monoxide from the co-electrolytic reaction unit between the first gas channel and the second gas channel, and controls the molar ratio of water and carbon dioxide supplied to the co-electrolytic reaction unit. [Application Example 6] A hydrocarbon production apparatus described in any one of the application examples 1 to 5, The control unit, When the pressure inside the hydrogen tank is above a first threshold, the molar ratio is set to a first molar ratio, the electrolytic reaction rate of the co-electrolysis is controlled to a first reaction rate, and the supply channel is set to the second gas channel. A hydrocarbon production apparatus comprising: when the pressure in the hydrogen tank is less than the first threshold, the molar ratio is set to a second molar ratio higher than the first molar ratio until the pressure in the hydrogen tank exceeds a second threshold higher than the first threshold, thereby controlling the electrolytic reaction rate of co-electrolysis to a second reaction rate higher than the first reaction rate, and the supply channel is the first gas channel. [Application Example 7] A hydrocarbon production apparatus described in any one of the application examples 1 to 6, further comprising: A second catalytic reaction unit, using at least a portion of the mixed gas containing carbon monoxide and hydrogen supplied from the co-electrolytic reaction unit, produces a hydrocarbon compound of a different type from the hydrocarbon compound produced in the first catalytic reaction unit. A third gas channel supplies the mixed gas supplied from the co-electrolytic reaction section to the second catalytic reaction section and the hydrogen separation section, Equipped with, The hydrogen separation unit separates a portion of the hydrogen contained in the mixed gas supplied from the co-electrolytic reaction unit via the third gas flow path, in a hydrocarbon production apparatus. [Application Example 8] A hydrocarbon production apparatus described in any one of Application Examples 1 to 7, further, A hydrocarbon production apparatus comprising an upgrading section that performs hydrocracking of a hydrocarbon compound produced in the first catalytic reaction section using hydrogen separated by the hydrogen separation section, thereby producing a hydrocarbon compound lighter than the hydrocarbon compound produced in the first catalytic reaction section. [Example 9] A hydrocarbon production apparatus described in any one of Application Examples 1 to 8, further comprising: A hydrogen tank for storing the hydrogen separated by the hydrogen separation unit, A fourth gas passage connecting the hydrogen tank and the third gas passage, the fourth gas passage for adding hydrogen to the mixed gas supplied to the second catalytic reaction section, Equipped with, A hydrocarbon production apparatus wherein the third gas flow path branches downstream of the point where it connects to the fourth gas flow path and connects to the second catalytic reaction section and the hydrogen separation section, respectively. [Application Example 10] A hydrocarbon production apparatus described in any one of Application Examples 1 to 9, further comprising: A hydrocarbon production apparatus comprising a control unit that controls the amount of hydrogen supplied from the hydrogen tank to the fourth gas flow path and the amount of hydrogen separated from the separated gas by the hydrogen separation unit, according to the amount of hydrocarbon compounds produced in the first catalytic reaction unit and the second catalytic reaction unit, respectively. [Application Example 11] A hydrocarbon production apparatus described in any one of the application examples 1 to 10, A hydrocarbon production apparatus wherein the molar ratio of hydrogen to carbon monoxide required for the hydrocarbon compound produced in the first catalytic reaction section is smaller than the molar ratio of the hydrocarbon compound produced in the second catalytic reaction section. [Application Example 12] A method for producing hydrocarbons, A co-electrolytic reaction section generates hydrogen and carbon monoxide by co-electrolytically reacting water and carbon dioxide, A hydrogen separation process that separates a portion of the hydrogen produced by co-electrolysis, A first catalytic reaction step for producing a hydrocarbon compound by using a catalyst on the residual hydrogen after separation supplied from the co-electrolytic reaction unit and the carbon monoxide supplied from the co-electrolytic reaction unit, A hydrocarbon production method comprising the following: [Application Example 13] A hydrocarbon production method described in Application Example 12, further, A second catalytic reaction step, using at least a portion of the mixed gas containing carbon monoxide and hydrogen generated in the co-electrolytic reaction step, produces a hydrocarbon compound of a different type from the hydrocarbon compound produced in the first catalytic reaction step. A hydrogen addition step is performed in which an amount of hydrogen determined according to the amount of hydrogen and carbon monoxide produced in the co-electrolytic reaction step is added to the mixed gas from a hydrogen tank that stores the hydrogen separated in the hydrogen separation step, Equipped with, The mixed gas supplied from the co-electrolytic reaction section that carries out the co-electrolytic reaction step is supplied to the second catalytic reaction section where the second catalytic reaction step is carried out and to the hydrogen separation section where the hydrogen separation step is carried out. A hydrocarbon production method comprising the hydrogen separation step of separating an amount of hydrogen determined according to the amount of the mixed gas supplied to the hydrogen separation unit, and supplying the separated hydrogen to the hydrogen tank. [Explanation of Symbols]

[0097] 1…SOEC (Co-electrolytic reaction section) 2…Catalytic reactor (first catalytic reaction section) 2b...First catalytic reactor (first catalytic reaction section) 3…Hydrogen separator (hydrogen separation unit) 4…Hydrogen tank 5…Upgrading reactor (upgrading section) 6, 6a, 6b... Control Units 7, 8, 18, 23~25… Flow controller 11… Evaporator 12,22…Dehydrator 14... Gas-liquid separator 15…Liquid separator 16…1st Hydrocarbon Tank 17…Second hydrocarbon tank 19…Methane reactor (second catalytic reaction section) 21…Methane tank 100,100a...Hydroxide production equipment CP... Compressor CV1, CV2... Check valves FP1…First gas flow path FP2…Second gas flow path FP3…Third gas flow path FP4…Fourth gas channel GS1…Mixed gas Rf... Molar ratio of water to carbon dioxide Rm1...1st molar ratio Rm2...2nd molar ratio Rp... Molar ratio of hydrogen to carbon monoxide Rr1...First response rate Rr2…Second response rate S1, S3... Pressure sensors S2... Flow sensor S4... Liquid level sensor Th1...First threshold TH2…Second threshold VL1, VL2… valve VL3…Hydrogen valve

Claims

1. A hydrocarbon production apparatus, A co-electrolytic reaction section that generates hydrogen and carbon monoxide by co-electrolytically reacting water and carbon dioxide, A first gas channel through which hydrogen and carbon monoxide generated by the aforementioned co-electrolytic reaction section flow, A hydrogen separation unit is positioned in the middle of the first gas flow path and separates a portion of the hydrogen generated by the co-electrolytic reaction unit, A hydrogen tank for storing the hydrogen separated by the hydrogen separation unit, A first catalytic reaction unit produces a hydrocarbon compound by using a catalyst on the residual hydrogen after separation supplied from the co-electrolytic reaction unit and the carbon monoxide supplied from the co-electrolytic reaction unit, A second gas channel is arranged in parallel with the first gas channel, connecting the co-electrolytic reaction section and the first catalytic reaction section, and through which hydrogen and carbon monoxide generated by the co-electrolytic reaction section flow, A control unit that switches the supply channel for hydrogen and carbon monoxide from the co-electrolytic reaction unit between the first gas channel and the second gas channel, depending on the amount of hydrogen stored in the hydrogen tank, Equipped with, A hydrocarbon production apparatus in which the first catalytic reaction section is supplied with the remaining hydrogen after separation by the hydrogen separation section and carbon monoxide via the first gas flow path.

2. A hydrocarbon production apparatus according to claim 1, further, The hydrogen tank is equipped with a pressure sensor that detects the pressure inside the hydrogen tank, A hydrocarbon production apparatus comprising a control unit that, in accordance with the detected pressure in the hydrogen tank, switches the supply channel for hydrogen and carbon monoxide from the co-electrolytic reaction unit between the first gas channel and the second gas channel, and controls the molar ratio of water to carbon dioxide in the water and carbon dioxide supplied to the co-electrolytic reaction unit.

3. A hydrocarbon production apparatus according to claim 2, The control unit, When the pressure inside the hydrogen tank is above a first threshold, the molar ratio is set to a first molar ratio, the electrolytic reaction rate of the co-electrolysis is controlled to a first reaction rate, and the supply channel is set to the second gas channel. A hydrocarbon production apparatus comprising: when the pressure in the hydrogen tank is less than the first threshold, the molar ratio is set to a second molar ratio higher than the first molar ratio until the pressure in the hydrogen tank exceeds a second threshold higher than the first threshold, thereby controlling the electrolytic reaction rate of co-electrolysis to a second reaction rate higher than the first reaction rate, and the supply channel is the first gas channel.

4. A hydrocarbon production apparatus, A co-electrolytic reaction section that generates hydrogen and carbon monoxide by co-electrolytically reacting water and carbon dioxide, A hydrogen separation unit separates a portion of the hydrogen generated by the aforementioned co-electrolytic reaction unit, A first catalytic reaction unit produces a hydrocarbon compound by using a catalyst on the residual hydrogen after separation supplied from the co-electrolytic reaction unit and the carbon monoxide supplied from the co-electrolytic reaction unit, A second catalytic reaction unit, using at least a portion of the mixed gas containing carbon monoxide and hydrogen supplied from the co-electrolytic reaction unit, produces a hydrocarbon compound of a different type from the hydrocarbon compound produced in the first catalytic reaction unit. A third gas channel supplies the mixed gas supplied from the co-electrolytic reaction section to the second catalytic reaction section and the hydrogen separation section, Equipped with, The hydrogen separation unit separates a portion of the hydrogen contained in the mixed gas supplied from the co-electrolytic reaction unit via the third gas flow path, in a hydrocarbon production apparatus.

5. A hydrocarbon production apparatus according to claim 4, further, A hydrogen tank for storing the hydrogen separated by the hydrogen separation unit, A fourth gas channel connecting the hydrogen tank and the third gas channel, the fourth gas channel for adding hydrogen to the mixed gas supplied to the second catalytic reaction section, Equipped with, A hydrocarbon production apparatus wherein the third gas flow path branches downstream of the point where it connects to the fourth gas flow path and connects to the second catalytic reaction section and the hydrogen separation section, respectively.

6. A hydrocarbon production apparatus according to claim 5, further, A hydrocarbon production apparatus comprising a control unit that controls the amount of hydrogen supplied from the hydrogen tank to the fourth gas flow path and the amount of hydrogen separated by the hydrogen separation unit, according to the amount of hydrocarbon compounds produced in the first catalytic reaction unit and the second catalytic reaction unit, respectively.

7. A hydrocarbon production apparatus according to any one of claims 4 to 6, A hydrocarbon production apparatus wherein the molar ratio of hydrogen to carbon monoxide required for the hydrocarbon compound produced in the first catalytic reaction section is smaller than the molar ratio of the hydrocarbon compound produced in the second catalytic reaction section.

8. A hydrocarbon production apparatus according to any one of claims 1 to 6, further, A hydrocarbon production apparatus comprising an upgrading section that performs hydrocracking of a hydrocarbon compound produced in the first catalytic reaction section using hydrogen separated by the hydrogen separation section to produce a lighter hydrocarbon compound.

9. A method for producing hydrocarbons, A co-electrolytic reaction section generates hydrogen and carbon monoxide by co-electrolytically reacting water and carbon dioxide, A hydrogen separation process that separates a portion of the hydrogen produced by co-electrolysis, A first catalytic reaction step for producing a hydrocarbon compound by using a catalyst on the residual hydrogen after separation supplied from the co-electrolytic reaction unit and the carbon monoxide supplied from the co-electrolytic reaction unit, A second catalytic reaction step, using at least a portion of the mixed gas containing carbon monoxide and hydrogen generated in the co-electrolytic reaction step, produces a hydrocarbon compound of a different type from the hydrocarbon compound produced in the first catalytic reaction step. A hydrogen addition step is performed in which an amount of hydrogen determined according to the amount of hydrogen and carbon monoxide produced in the aforementioned co-electrolytic reaction step is added to the mixed gas from a hydrogen tank that stores the hydrogen separated in the aforementioned hydrogen separation step, Equipped with, The mixed gas supplied from the co-electrolytic reaction section that carries out the co-electrolytic reaction step is supplied to the second catalytic reaction section where the second catalytic reaction step is carried out and to the hydrogen separation section where the hydrogen separation step is carried out. A hydrocarbon production method comprising the hydrogen separation step of separating an amount of hydrogen determined according to the amount of the mixed gas supplied to the hydrogen separation unit, and supplying the separated hydrogen to the hydrogen tank.

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