Hydrocarbon production system and hydrocarbon production method

Abstract

A hydrocarbon production system 100 comprises an impurity removal device 140 that removes impurities that include one or both of oxygen and a sulfur component from a mixed gas that includes carbon dioxide and the impurities, a hydrocarbon production device 160 that includes a hydrocarbon synthesis catalyst for accelerating a reaction by which a hydrocarbon is synthesized from hydrogen and carbon dioxide and synthesizes a hydrocarbon from hydrogen and the carbon dioxide included in the mixed gas from which the impurities were removed by the impurity removal device 140, and a heat supply unit 170 that supplies reaction heat produced at the hydrocarbon production device 160 to the impurity removal device 140.

Description

[Technical Field]

[0001] This disclosure relates to a hydrocarbon production system and a hydrocarbon production method. This application claims the benefit of priority to Japanese Patent Application No. 2022-145886, filed on September 14, 2022, the contents of which are incorporated herein by reference. [Background technology]

[0002] Fossil fuels such as coal, heavy oil, and extra-heavy oil are burned in plants such as thermal power plants, steel mills, and boilers. As a result, exhaust gases containing carbon dioxide are emitted from the plants due to the combustion of fossil fuels. Carbon dioxide is considered to be a factor in global warming, so there is a widespread demand for reducing carbon dioxide emissions into the atmosphere.

[0003] Therefore, a technology has been developed in which carbon dioxide is extracted from exhaust gas or the atmosphere and hydrocarbons are synthesized from the extracted carbon dioxide (for example, Patent Document 1). [Prior art documents] [Patent documents]

[0004] [Patent Document 1] Japanese Patent Publication No. 2020-37535 Summary of the Invention [Problem to be solved by the invention]

[0005] In the technology for synthesizing hydrocarbons from carbon dioxide contained in the exhaust gas or the atmosphere, there is a demand for the development of a technology that efficiently utilizes thermal energy.

[0006] Therefore, an object of the present disclosure is to provide a hydrocarbon production system and a hydrocarbon production method that are capable of efficiently utilizing thermal energy. [Means for solving the problem]

[0007] In order to solve the above problems, a hydrocarbon production system according to one embodiment of the present disclosure includes a wet desulfurization device that removes sulfur components from a mixed gas that contains impurities including oxygen and sulfur components and carbon dioxide, an oxygen removal device that includes an oxygen removal catalyst and to which hydrogen is supplied, and a catalytic desulfurization device that includes a desulfurization catalyst, and that removes impurities from the mixed gas that has been treated by the wet desulfurization device, a hydrocarbon production device that includes a hydrocarbon synthesis catalyst that promotes a reaction for synthesizing hydrocarbons from carbon dioxide and hydrogen, and that synthesizes hydrocarbons from the carbon dioxide and hydrogen contained in the mixed gas from which the impurities have been removed by the impurity removal device, and a heat supply unit that has a heat medium that recovers reaction heat generated in the hydrocarbon production device, and that heats the catalytic desulfurization device with the heat medium and then heats the oxygen removal device, a water electrolysis device that electrolyzes water to generate hydrogen and oxygen; and a startup device that supplies the oxygen generated by the water electrolysis device to the oxygen removal device when starting up the hydrocarbon production device; Equipped with The oxygen removal catalyst and the hydrocarbon production unit are supplied with hydrogen generated by the water electrolysis unit. do.

[0009] the above The oxygen removal device includes: Mixed gas treated by wet desulfurization equipment Su Supplied The catalytic desulfurization equipment includes: The mixed gas is supplied after being treated by an oxygen removal device. Re Good too.

[0010] The impurity removal device , sulfur A dry desulfurization device that contains an adsorbent that adsorbs sulfur components and is supplied with mixed gas that has been treated by a wet desulfurization device. Furthermore, , The oxygen removal device includes: Mixed gas treated by dry desulfurization equipment Su Supplied The catalytic desulfurization equipment includes: The mixed gas is supplied after being treated by an oxygen removal device. R, The heat supply section consists of a catalytic desulfurization unit, an oxygen removal unit, and a dry desulfurization unit. Place Reaction heat may be provided.

[0015] The hydrocarbon production system may include a heat exchanger that exchanges heat between the mixed gas treated by the wet desulfurization unit and the mixed gas treated by the impurity removal unit.

[0017] In order to solve the above problems, a hydrocarbon production method according to one embodiment of the present disclosure includes: Electrolyzes water to produce hydrogen and oxygen,In the wet desulfurization device, a sulfur component is removed from a mixed gas containing impurities containing oxygen and sulfur components and carbon dioxide, and the wet desulfurization device includes an oxygen removal catalyst, generated an oxygen removal device to which hydrogen is supplied, and a catalytic desulfurization device including a desulfurization catalyst, for removing impurities from the mixed gas treated by the wet desulfurization device; In a hydrocarbon production plant, a mixed gas from which impurities have been removed; generated reacting with hydrogen, In hydrocarbon production equipment The generated reaction heat is recovered by a heat transfer medium, which then heats the catalytic desulfurization unit and the oxygen removal unit. When starting up the hydrocarbon production plant, the oxygen produced is supplied to the oxygen removal device. do. [Effects of the Invention]

[0018] According to the present disclosure, it is possible to efficiently utilize thermal energy. [Brief explanation of the drawings]

[0019] [Figure 1] FIG. 1 is a diagram illustrating a hydrocarbon production system according to a first embodiment. [Figure 2] FIG. 2 is a flowchart showing the flow of the process of the hydrocarbon production method according to the first embodiment. [Figure 3] FIG. 3 is a diagram illustrating a hydrocarbon production system according to a second embodiment. [Figure 4] FIG. 4 is a diagram illustrating a hydrocarbon production system according to a third embodiment. [Figure 5] FIG. 5 is a diagram illustrating a hydrocarbon production system according to a fourth embodiment. [Figure 6] FIG. 6 is a diagram illustrating a hydrocarbon production system according to a fifth embodiment. [Figure 7] FIG. 7 is a diagram illustrating a hydrocarbon production system according to a sixth embodiment. DETAILED DESCRIPTION OF THE INVENTION

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

[0021] [First embodiment: hydrocarbon production system 100] FIG. 1 is a diagram illustrating a hydrocarbon production system 100 according to a first embodiment. As shown in FIG. 1, the hydrocarbon production system 100 includes a wet desulfurization unit 110, a pressure booster 120, a heat exchanger 130, an impurity removal unit 140, a water electrolysis unit 150, a hydrocarbon production unit 160, a heat supply unit 170, a start-up unit 180, and a central control unit 190. In FIG. 1, solid arrows indicate mixed gas, carbon dioxide (CO), oxygen (O), hydrogen (H), hydrocarbons (CH, CH), and the like. n 1 indicates the flow of gas such as a gas containing oxygen and a gas such as a gas containing nitrogen. In addition, in FIG. 1, the dashed arrows indicate the flow of the heat transfer medium.

[0022] The hydrocarbon production system 100 extracts carbon dioxide from a mixed gas and reacts the extracted carbon dioxide with hydrogen to produce hydrocarbons. In this embodiment, the mixed gas contains a sulfur component, oxygen, and carbon dioxide. The mixed gas is, for example, a gas produced by burning a fossil fuel with oxygen.

[0023] The wet desulfurization unit 110 removes sulfur components from the mixed gas. The wet desulfurization unit 110 is, for example, a spray tower that sprays a liquid containing a basic substance into the mixed gas. The basic substance is, for example, sodium hydroxide or magnesium hydroxide. The wet desulfurization unit 110 reduces the concentration of sulfur components in the mixed gas to, for example, about 10 ppm. The wet desulfurization unit 110 is operated, for example, at a temperature above room temperature and below 60°C. The room temperature is, for example, 25°C.

[0024] The suction side of the pressure booster 120 is connected to the wet desulfurization apparatus 110. The discharge side of the pressure booster 120 is connected to a heat exchanger 130, which will be described later. The pressure booster 120 boosts the pressure of the mixed gas treated by the wet desulfurization apparatus 110 and supplies the mixed gas to the heat exchanger 130. The pressure booster 120 is, for example, a pump or a blower.

[0025] The heat exchanger 130 exchanges heat between the mixed gas treated by the wet desulfurization device 110 and discharged by the pressure booster 120 and the mixed gas treated by the catalytic desulfurization device 146 described below.

[0026] The impurity removal device 140 removes impurities from the mixed gas. In this embodiment, the impurities are sulfur components and oxygen. In this embodiment, the impurity removal device 140 includes a dry desulfurization device 142, an oxygen removal device 144, and a catalytic desulfurization device 146.

[0027] The dry desulfurization unit 142 is supplied with the mixed gas that has passed through the wet desulfurization unit 110, the booster unit 120, and the heat exchanger 130. The dry desulfurization unit 142 further removes sulfur components from the mixed gas that has been treated by the wet desulfurization unit 110. The dry desulfurization unit 142 removes sulfur components from the mixed gas in the gas phase. In this embodiment, the dry desulfurization unit 142 includes an adsorbent that adsorbs the sulfur components. The dry desulfurization unit 142 is operated at a temperature between room temperature and 60°C. The adsorbent is, for example, an alumina-based adsorbent or activated carbon.

[0028] The oxygen remover 144 is supplied with the mixed gas processed by the dry desulfurization apparatus 142 and hydrogen produced by the water electrolysis apparatus 150, which will be described later. The oxygen remover 144 reacts oxygen and hydrogen contained in the mixed gas to produce water. In this way, oxygen is removed from the mixed gas in the oxygen remover 144. The oxygen remover 144 removes oxygen from the mixed gas in the gas phase. In this embodiment, the oxygen remover 144 includes an oxygen removal catalyst. The oxygen remover 144 is operated at a temperature between room temperature and 200°C, for example, between 50°C and 200°C. The reaction between oxygen and hydrogen that proceeds in the oxygen remover 144 is an exothermic reaction.

[0029] In this embodiment, the oxygen removing catalyst is, for example, a platinum (Pt) based catalyst, a palladium (Pd) based catalyst, a nickel (Ni) based catalyst, etc. The oxygen removing catalyst is in the form of, for example, a pellet or a honeycomb.

[0030] The catalytic desulfurization device 146 is supplied with the mixed gas treated by the oxygen remover 144. The catalytic desulfurization device 146 further removes sulfur components from the mixed gas treated by the oxygen remover 144. The catalytic desulfurization device 146 removes sulfur components from the mixed gas in the gas phase. In this embodiment, the catalytic desulfurization device 146 includes a desulfurization catalyst. The catalytic desulfurization device 146 is operated at a temperature of 200°C or higher and 300°C or lower.

[0031] In this embodiment, the desulfurization catalyst contained in the catalytic desulfurization device 146 is a catalyst that desulfurizes under a hydrogen atmosphere, i.e., a reducing atmosphere. The desulfurization catalyst contained in the catalytic desulfurization device 146 is a zinc (Zn)-based catalyst, a nickel-based catalyst, or a cobalt (Co)-based catalyst. The desulfurization catalyst contained in the catalytic desulfurization device 146 is in the form of, for example, a pellet or a honeycomb.

[0032] The water electrolysis device 150 electrolyzes water to produce hydrogen and oxygen. The water electrolysis device 150 electrolyzes water using electricity generated by, for example, renewable energy.

[0033] The hydrogen produced by the water electrolysis apparatus 150 is supplied to the hydrocarbon production apparatus 160 and the oxygen removal apparatus 144 through flow paths 152 and 154. The flow path 152 connects the hydrogen output port of the water electrolysis apparatus 150 to the hydrocarbon production apparatus 160. The flow path 154 connects the hydrogen output port of the water electrolysis apparatus 150 to the oxygen removal apparatus 144.

[0034] The hydrocarbon production apparatus 160 is supplied with the mixed gas treated by the impurity removal apparatus 140 (catalytic desulfurization apparatus 146) and hydrogen produced by the water electrolysis apparatus 150. The hydrocarbon production apparatus 160 synthesizes hydrocarbons from carbon dioxide contained in the mixed gas from which sulfur components and oxygen have been removed by the impurity removal apparatus 140, and the hydrogen produced by the water electrolysis apparatus 150. The hydrocarbon production apparatus 160 reacts carbon dioxide and hydrogen in the gas phase. In this embodiment, the hydrocarbon production apparatus 160 includes a hydrocarbon synthesis catalyst. The hydrocarbon synthesis catalyst is a catalyst that promotes the reaction of synthesizing hydrocarbons from carbon dioxide and hydrogen. The hydrocarbon production apparatus 160 is operated at a temperature of 300°C or higher and 350°C or lower.

[0035] In this embodiment, the hydrocarbon synthesis catalyst is a catalyst that promotes a methanation reaction shown in the following formula (1) or a catalyst that promotes a Fischer-Tropsch (FT) synthesis reaction shown in the following formula (2). The catalyst that promotes a methanation reaction is, for example, a nickel-based catalyst. The catalyst that promotes a FT synthesis reaction is, for example, an iron (Fe)-based catalyst. CO2+ 4H2→ CH4+ 2H2O…Formula (1) nCO2 + 3nH2 → (CH2) n + 2nH2O…Formula (2) In the above formula (2), n is, for example, 2 or more and 4 or less. The methanation reaction and the FT synthesis reaction are exothermic reactions.

[0036] The hydrocarbon synthesis catalyst may be in the form of, for example, pellets or honeycomb.

[0037] The heat supply unit 170 supplies the reaction heat generated in the hydrocarbon production unit 160 to the impurity removal unit 140. In this embodiment, the heat supply unit 170 supplies the reaction heat generated in the hydrocarbon production unit 160 to the catalytic desulfurization unit 146 and the oxygen removal unit 144.

[0038] In this embodiment, the heat supplying unit 170 includes flow paths 172a to 172h, a heat exchanger 174, and delivery devices 176a and 176b. The flow paths 172a to 172e are flow paths through which a first heat medium circulates. The flow paths 172f to 172h are flow paths through which a second heat medium circulates.

[0039] The flow path 172a connects the hydrocarbon production apparatus 160 and the heat exchanger 174. The flow path 172b connects the flow path 172a and the catalytic desulfurization apparatus 146. The first heat medium heated by recovering the heat of reaction generated in the hydrocarbon production apparatus 160 is supplied to the heat exchanger 174 through the flow path 172a and then supplied to the catalytic desulfurization apparatus 146 through the flow paths 172a and 172b.

[0040] A flow path 172c connects the heat exchanger 174 and the suction side of the delivery device 176a. A flow path 172d connects the discharge side of the delivery device 176a and the hydrocarbon production device 160. A flow path 172e connects the catalytic desulfurization device 146 and the flow path 172c.

[0041] The delivery device 176a is, for example, a pump. When the delivery device 176a is operated, the first heat medium circulates through the hydrocarbon production device 160, the catalytic desulfurization device 146, and the heat exchanger 174 through the flow paths 172a to 172e.

[0042] Flow path 172f connects heat exchanger 174 and oxygen remover 144. Flow path 172g connects oxygen remover 144 and the suction side of delivery device 176b. Flow path 172h connects heat exchanger 174 and the discharge side of delivery device 176b.

[0043] The sending device 176b is, for example, a pump. When the sending device 176b is operated, the second heat medium circulates through the heat exchanger 174 and the oxygen removing device 144 via the flow paths 172f to 172f.

[0044] The heat exchanger 174 exchanges heat between the first heat medium and the second heat medium.

[0045] The reaction heat generated in the hydrocarbon production unit 160 is first transferred to a first heat medium. Then, the heat possessed by the first heat medium is supplied to the catalytic desulfurization unit 146. In addition, the heat possessed by the first heat medium is transferred to a second heat medium by a heat exchanger 174, and then supplied to the oxygen removal unit 144.

[0046] Furthermore, flow path 172b is provided with a flow rate adjustment valve RV1. Flow path 172f is provided with a flow rate adjustment valve RV2. The opening degrees of flow rate adjustment valves RV1 and RV2 are adjusted by a thermal control unit 192, which will be described later.

[0047] When starting up the hydrocarbon production apparatus 160, the start-up device 180 supplies oxygen generated by the water electrolysis device 150 to the oxygen remover 144. In this embodiment, the start-up device 180 has a flow path 182 and an on-off valve 184. The flow path 182 connects the oxygen output port of the water electrolysis device 150 to the oxygen remover 144. The on-off valve 184 is provided in the flow path 182. The on-off valve 184 opens and closes the flow path 182. The on-off valve 184 is controlled to open and close by a start-up control unit 194, which will be described later.

[0048] The central control unit 190 is configured by a semiconductor integrated circuit including a CPU (central processing unit). The central control unit 190 reads out programs, parameters, etc. for operating the CPU from the ROM. The central control unit 190 manages and controls the entire hydrocarbon production system 100 in cooperation with RAM as a work area and other electronic circuits.

[0049] In this embodiment, the central control unit 190 also functions as a thermal control unit 192 and a startup control unit 194 .

[0050] The thermal control unit 192 adjusts the aperture of the flow control valve RV1 so that the temperature of the catalytic desulfurization device 146 is maintained at the activation temperature of the desulfurization catalyst. In this embodiment, the thermal control unit 192 adjusts the aperture of the flow control valve RV1 so that the temperature of the catalytic desulfurization device 146 is 200°C or higher and 300°C or lower.

[0051] Furthermore, the heat control unit 192 adjusts the aperture of the flow rate control valve RV2 so that the temperature of the oxygen removing device 144 is maintained at the activation temperature of the oxygen removing catalyst. In this embodiment, the heat control unit 192 adjusts the aperture of the flow rate control valve RV2 so that the temperature of the oxygen removing device 144 is 50°C or higher and 200°C or lower.

[0052] The startup control unit 194 opens the on-off valve 184 when starting up the hydrocarbon production apparatus 160. Furthermore, the startup control unit 194 closes the on-off valve 184 when the temperatures of the oxygen removing unit 144, the catalytic desulfurization unit 146, and the hydrocarbon production apparatus 160 reach the operating temperatures.

[0053] [Hydrocarbon production method] Next, a description will be given of a hydrocarbon production method using the hydrocarbon production system 100. Fig. 2 is a flowchart showing the flow of processing in the hydrocarbon production method according to this embodiment.

[0054] 2, the hydrocarbon production method includes a water electrolysis device operation process S110, an opening process S112, a temperature determination process S114, a closing process S116, a booster device operation process S118, a sending device operation process S120, an adjustment process S122, a stop determination process S124, a water electrolysis device stop process S126, a booster device stop process S128, and a sending device stop process S130. Each process will be described below.

[0055] [Water electrolysis device operation process S110] The start-up control unit 194 starts the operation of the water electrolysis device 150. As a result, water is electrolyzed by the water electrolysis device 150 to produce hydrogen and oxygen. The hydrogen produced by the water electrolysis device 150 is supplied to the oxygen removal device 144 and the hydrocarbon production device 160.

[0056] [Opening process S112] The start-up control unit 194 opens the on-off valve 184. As a result, the oxygen produced by the water electrolysis device 150 is supplied to the oxygen remover 144. Therefore, in the oxygen remover 144, an exothermic reaction between the hydrogen produced by the water electrolysis device 150 and the oxygen proceeds.

[0057] [Temperature determination process S114] The start-up control unit 194 determines whether the temperature of the oxygen removing device 144 has reached the operating temperature. The operating temperature is the activation temperature of the oxygen removing catalyst included in the oxygen removing device 144. As a result, if it is determined that the temperature of the oxygen removing device 144 is below the operating temperature (NO in S114), the start-up control unit 194 repeats the temperature determination process S114. On the other hand, if it is determined that the temperature of the oxygen removing device 144 has reached the operating temperature (YES in S114), the start-up control unit 194 proceeds to the closing process S116.

[0058] [Closing process S116] The start-up control unit 194 closes the on-off valve 184. This stops the supply of oxygen produced by the water electrolysis device 150 to the oxygen remover 144.

[0059] [Boost device operation process S118] The startup control unit 194 starts the operations of the wet desulfurization unit 110 and the booster 120. This causes the mixed gas to be supplied to the wet desulfurization unit 110, where the mixed gas is desulfurized by the wet desulfurization unit 110. The mixed gas desulfurized by the wet desulfurization unit 110 is then supplied to the impurity removal unit 140 (the dry desulfurization unit 142, the oxygen removal unit 144, and the catalytic desulfurization unit 146), where impurities (sulfur components and oxygen) are removed by the impurity removal unit 140. The mixed gas from which the impurities have been removed is then supplied to the hydrocarbon production unit 160. Then, in the hydrocarbon production unit 160, carbon dioxide contained in the mixed gas is reacted with hydrogen supplied from the water electrolysis unit 150 to produce hydrocarbons.

[0060] [Sending device operation process S120] The heat control unit 192 starts the operation of the delivery device 176a. Then, the first heat medium circulates through the hydrocarbon production device 160, the catalytic desulfurization device 146, and the heat exchanger 174. As a result, the reaction heat generated in the hydrocarbon production device 160 is supplied to the catalytic desulfurization device 146 via the first heat medium.

[0061] Furthermore, the heat control unit 192 starts the operation of the delivery device 176b. This causes the second heat medium to circulate through the heat exchanger 174 and the oxygen remover 144. As a result, the reaction heat generated in the hydrocarbon production apparatus 160 is supplied to the oxygen remover 144 via the first heat medium, the heat exchanger 174, and the second heat medium.

[0062] [Adjustment process S122] The heat control unit 192 adjusts the aperture of the flow control valve RV1 so that the temperature of the catalytic desulfurization device 146 is maintained at the activation temperature of the desulfurization catalyst. The heat control unit 192 also adjusts the aperture of the flow control valve RV2 so that the temperature of the oxygen removing device 144 is maintained at the activation temperature of the oxygen removing catalyst.

[0063] While the hydrocarbon production plant 160 is in operation, the adjustment process S122 is continuously performed.

[0064] [Stop determination process S124] The central control unit 190 determines whether an instruction to stop operation has been received from the user. As a result, if it is determined that an instruction to stop operation has not been received (NO in S124), the central control unit 190 proceeds to the adjustment process S122. On the other hand, if it is determined that an instruction to stop operation has been received (YES in S124), the central control unit 190 proceeds to the water electrolysis device shutdown process S126.

[0065] [Water electrolysis equipment stop processing S126] The central control unit 190 stops the operation of the water electrolysis device 150.

[0066] [Boost device stop processing S128] The central control unit 190 stops the operations of the wet desulfurization device 110 and the booster device 120.

[0067] [Sending device stop processing S130] The central control unit 190 stops the operation of the transmission devices 176a and 176b.

[0068] As described above, the hydrocarbon production system 100 according to this embodiment includes the wet desulfurization unit 110, the dry desulfurization unit 142, and the catalytic desulfurization unit 146. As a result, the hydrocarbon production system 100 can extremely reduce the concentration of sulfur components contained in the mixed gas supplied to the hydrocarbon production system 160. Therefore, the hydrocarbon production system 100 can reduce the amount of poisoning of the hydrocarbon synthesis catalyst included in the hydrocarbon production system 160. As a result, the hydrocarbon production system 100 can reduce the amount of hydrocarbon synthesis catalyst in the hydrocarbon production system 160. Furthermore, the hydrocarbon production system 100 can reduce the frequency of replacing the poisoned hydrocarbon synthesis catalyst with a new, unpoisoned hydrocarbon synthesis catalyst in the hydrocarbon production system 160. Therefore, the hydrocarbon production system 100 can reduce the running costs of the hydrocarbon production system 160.

[0069] Furthermore, as described above, the hydrocarbon production system 100 includes the dry desulfurization unit 142 upstream of the oxygen removing unit 144. This makes it possible for the dry desulfurization unit 142 to suppress a decrease in the oxygen removing function even when the oxygen removing catalyst of the oxygen removing unit 144 has low sulfur resistance.

[0070] Furthermore, as described above, the hydrocarbon production system 100 includes the oxygen remover 144. This makes it possible for the oxygen remover 144 to suppress the intrusion of oxygen into the catalytic desulfurization device 146, which performs desulfurization under a reducing atmosphere. Therefore, the oxygen remover 144 can suppress a decrease in the desulfurization function of the catalytic desulfurization device 146.

[0071] Furthermore, the oxygen remover 144 can suppress the mixing of oxygen into the hydrocarbon production unit 160. As a result, the oxygen remover 144 can suppress a decrease in reaction efficiency in the hydrocarbon production unit 160.

[0072] Furthermore, as described above, the hydrocarbon production system 100 and the hydrocarbon production method using the same supply the reaction heat generated in the hydrocarbon production apparatus 160 to the catalytic desulfurization apparatus 146 and the oxygen removal apparatus 144. As a result, the hydrocarbon production system 100 and the hydrocarbon production method using the same can use the reaction heat to provide the thermal energy for maintaining the desulfurization catalyst in the catalytic desulfurization apparatus 146 and the oxygen removal catalyst in the oxygen removal apparatus 144 at their active temperatures. In other words, the hydrocarbon production system 100 can efficiently utilize thermal energy. Therefore, the hydrocarbon production system 100 and the hydrocarbon production method using the same can reduce the cost required for the thermal energy for maintaining the desulfurization catalyst in the catalytic desulfurization apparatus 146 and the oxygen removal catalyst in the oxygen removal apparatus 144 at their active temperatures. Therefore, the hydrocarbon production system 100 and the hydrocarbon production method using the same can reduce the running cost of the impurity removal apparatus 140.

[0073] As described above, the activation temperature of the desulfurization catalyst in the catalytic desulfurization device 146 is higher than the activation temperature of the oxygen removal catalyst in the oxygen removal device 144. The heat supply unit 170 heats the catalytic desulfurization device 146 with the first heat medium, and then heats the oxygen removal device 144 with the first heat medium and the second heat medium. This allows the heat supply unit 170 to efficiently heat both the catalytic desulfurization device 146 and the oxygen removal device 144.

[0074] Furthermore, as described above, the hydrocarbon production system 100 includes the heat exchanger 130. As a result, the heat exchanger 130 can heat the mixed gas before it is supplied to the dry desulfurization unit 142. Therefore, the heat exchanger 130 can prevent condensation from occurring in the dry desulfurization unit 142. Therefore, the heat exchanger 130 can suppress a decrease in the desulfurization function of the dry desulfurization unit 142.

[0075] Furthermore, as described above, the hydrocarbon production system 100 includes the start-up device 180. As a result, the start-up device 180 can promote the exothermic reaction of hydrogen and oxygen in the oxygen remover 144 when starting up the hydrocarbon production apparatus 160. Therefore, when starting up the hydrocarbon production apparatus 160, the start-up device 180 can warm up the oxygen remover 144, the catalytic desulfurization device 146, and the hydrocarbon production apparatus 160 by using the reaction heat generated in the oxygen remover 144. Therefore, the start-up device 180 can reduce the cost required for warm-up.

[0076] [Second embodiment: hydrocarbon production system 200] In the above first embodiment, an example has been given in which the hydrocarbon production system 100 includes the dry desulfurization unit 142. However, if the oxygen removal catalyst has high sulfur resistance, the dry desulfurization unit 142 may be omitted.

[0077] Fig. 3 is a diagram illustrating a hydrocarbon production system 200 according to a second embodiment. As shown in Fig. 3, the hydrocarbon production system 200 includes a wet desulfurization unit 110, a pressure booster 120, a heat exchanger 130, an impurity removal unit 240, a water electrolysis unit 150, a hydrocarbon production unit 160, a heat supplier 170, a start-up unit 180, and a central control unit 190. In Fig. 3, solid arrows indicate the flow of gases such as mixed gas, carbon dioxide, oxygen, hydrogen, and hydrocarbons. In Fig. 3, dashed arrows indicate the flow of a heat medium.

[0078] Note that components that are substantially the same as those in the hydrocarbon production system 100 described above are denoted by the same reference numerals and descriptions thereof will be omitted.

[0079] The impurity removal device 240 includes an oxygen removal device 144 and a catalytic desulfurization device 146. Therefore, in this embodiment, the mixed gas that has passed through the wet desulfurization device 110, the pressure booster 120, and the heat exchanger 130 is supplied to the oxygen removal device 144.

[0080] Furthermore, in this embodiment, the oxygen removing catalyst provided in the oxygen removing device 144 has higher sulfur resistance than the oxygen removing catalyst provided in the oxygen removing device 144 of the hydrocarbon production system 100. The oxygen removing catalyst provided in the oxygen removing device 144 of this embodiment is, for example, a platinum-based catalyst, a palladium-based catalyst, a nickel-based catalyst, or the like. The shape of the oxygen removing catalyst is, for example, a pellet or a honeycomb.

[0081] As described above, the hydrocarbon production system 200 according to this embodiment can omit the dry desulfurization unit 142 compared to the hydrocarbon production system 100. Therefore, the hydrocarbon production system 200 can efficiently utilize thermal energy while reducing the cost required for the dry desulfurization unit 142.

[0082] [Third embodiment: hydrocarbon production system 300] In the above first embodiment, an example has been given in which the hydrocarbon production system 100 includes the catalytic desulfurization unit 146. However, if the hydrocarbon synthesis catalyst has high sulfur tolerance, the catalytic desulfurization unit 146 may be omitted.

[0083] Fig. 4 is a diagram illustrating a hydrocarbon production system 300 according to a third embodiment. As shown in Fig. 4, the hydrocarbon production system 300 includes a wet desulfurization unit 110, a pressure booster 120, a heat exchanger 130, an impurity removal unit 340, a water electrolysis unit 150, a hydrocarbon production unit 160, a heat supplier 370, a start-up unit 180, and a central control unit 390. In Fig. 4, solid arrows indicate the flow of gases such as mixed gas, carbon dioxide, oxygen, hydrogen, and hydrocarbons. In Fig. 4, dashed arrows indicate the flow of a heat medium.

[0084] Note that components that are substantially the same as those in the hydrocarbon production system 100 described above are denoted by the same reference numerals and descriptions thereof will be omitted.

[0085] The impurity removal unit 340 includes a dry desulfurization unit 142 and an oxygen removal unit 144 .

[0086] In this embodiment, the heat exchanger 130 exchanges heat between the mixed gas treated by the wet desulfurization device 110 and discharged by the pressure booster 120 and the mixed gas treated by the oxygen remover 144 .

[0087] In this embodiment, the hydrocarbon production unit 160 is supplied with the mixed gas treated by the oxygen removal unit 144 and hydrogen produced by the water electrolysis unit 150 .

[0088] Furthermore, in this embodiment, the hydrocarbon synthesis catalyst possessed by the hydrocarbon production apparatus 160 has higher sulfur resistance than the hydrocarbon synthesis catalyst possessed by the hydrocarbon production apparatus 160 of the hydrocarbon production system 100. The hydrocarbon synthesis catalyst possessed by the hydrocarbon production apparatus 160 of this embodiment is, for example, a nickel-based catalyst, an iron-based catalyst, or the like. The shape of the hydrocarbon synthesis catalyst is, for example, a pellet or a honeycomb.

[0089] The heat supplying unit 370 supplies the reaction heat generated in the hydrocarbon production unit 160 to the oxygen removing unit 144. In this embodiment, the heat supplying unit 370 includes flow paths 372a to 372c and a sending unit 376.

[0090] The flow path 372a connects the hydrocarbon production apparatus 160 and the oxygen remover 144. The flow path 372b connects the oxygen remover 144 and the suction side of the delivery device 376. The flow path 372c connects the discharge side of the delivery device 376 and the hydrocarbon production apparatus 160.

[0091] The delivery device 376 is, for example, a pump. When the delivery device 376 is operated, the heat medium circulates through the hydrocarbon production device 160 and the oxygen remover 144 via the flow paths 372a to 372c. As a result, the reaction heat generated in the hydrocarbon production device 160 is supplied to the oxygen remover 144.

[0092] The flow path 372a is also provided with a flow rate adjustment valve RV3, the opening of which is adjusted by a heat control unit 392, which will be described later.

[0093] The central control unit 390 is configured by a semiconductor integrated circuit including a CPU (central processing unit). The central control unit 390 reads out programs, parameters, etc. for operating the CPU from the ROM. The central control unit 390 manages and controls the entire hydrocarbon production system 300 in cooperation with RAM as a work area and other electronic circuits.

[0094] In this embodiment, the central control unit 390 also functions as a thermal control unit 392 and a startup control unit 194 .

[0095] The heat control unit 392 adjusts the aperture of the flow rate control valve RV3 so that the temperature of the oxygen removing device 144 is maintained at the activation temperature of the oxygen removing catalyst. In this embodiment, the heat control unit 392 adjusts the aperture of the flow rate control valve RV3 so that the temperature of the oxygen removing device 144 is 50°C or higher and 200°C or lower.

[0096] As described above, the hydrocarbon production system 300 according to this embodiment can omit the catalytic desulfurization unit 146, as compared to the hydrocarbon production system 100. Therefore, the hydrocarbon production system 300 can efficiently utilize thermal energy while reducing the cost required for the catalytic desulfurization unit 146.

[0097] [Fourth embodiment: hydrocarbon production system 400] In the above-described first embodiment, an example has been given in which the hydrocarbon production system 100 includes the dry desulfurization unit 142 and the catalytic desulfurization unit 146. However, if the oxygen removal catalyst and the hydrocarbon synthesis catalyst have high sulfur resistance, the dry desulfurization unit 142 and the catalytic desulfurization unit 146 may be omitted.

[0098] Fig. 5 is a diagram illustrating a hydrocarbon production system 400 according to a fourth embodiment. As shown in Fig. 5, the hydrocarbon production system 400 includes a wet desulfurization unit 110, a pressure booster 120, a heat exchanger 130, an impurity removal unit 440, a water electrolysis unit 150, a hydrocarbon production unit 160, a heat supplier 370, a start-up unit 180, and a central control unit 390. In Fig. 5, solid arrows indicate the flow of gases such as mixed gas, carbon dioxide, oxygen, hydrogen, and hydrocarbons. In Fig. 5, dashed arrows indicate the flow of a heat medium.

[0099] Note that components that are substantially the same as those in the hydrocarbon production system 300 are denoted by the same reference numerals and descriptions thereof will be omitted.

[0100] The impurity remover 440 includes the oxygen remover 144 .

[0101] In this embodiment, the heat exchanger 130 exchanges heat between the mixed gas treated by the wet desulfurization device 110 and discharged by the pressure booster 120 and the mixed gas treated by the oxygen remover 144 .

[0102] In this embodiment, the hydrocarbon production unit 160 is supplied with the mixed gas treated by the oxygen removal unit 144 and hydrogen produced by the water electrolysis unit 150 .

[0103] Furthermore, in this embodiment, the oxygen removing catalyst provided in the oxygen removing device 144 has higher sulfur resistance than the oxygen removing catalyst provided in the oxygen removing device 144 of the hydrocarbon production system 100. The oxygen removing catalyst provided in the oxygen removing device 144 of this embodiment is, for example, a platinum-based catalyst, a palladium-based catalyst, a nickel-based catalyst, or the like. The shape of the oxygen removing catalyst is, for example, a pellet or a honeycomb.

[0104] Furthermore, in this embodiment, the hydrocarbon synthesis catalyst possessed by the hydrocarbon production apparatus 160 has higher sulfur resistance than the hydrocarbon synthesis catalyst possessed by the hydrocarbon production apparatus 160 of the hydrocarbon production system 100. The hydrocarbon synthesis catalyst possessed by the hydrocarbon production apparatus 160 of this embodiment is, for example, a nickel-based catalyst, an iron-based catalyst, or the like. The shape of the hydrocarbon synthesis catalyst is, for example, a pellet or a honeycomb.

[0105] As described above, the hydrocarbon production system 400 according to this embodiment can omit the dry desulfurization unit 142 and the catalytic desulfurization unit 146, as compared to the hydrocarbon production system 100. Therefore, the hydrocarbon production system 400 can efficiently utilize thermal energy while reducing the costs required for the dry desulfurization unit 142 and the catalytic desulfurization unit 146.

[0106] [Fifth Embodiment: Hydrocarbon Production System 500] In the above-described first embodiment, an example has been given in which the hydrocarbon production system 100 extracts carbon dioxide from a mixed gas containing sulfur components, oxygen, and carbon dioxide. However, if the mixed gas contains sulfur components and carbon dioxide and little oxygen, the dry desulfurization unit 142 and the oxygen removal unit 144 may be omitted.

[0107] Fig. 6 is a diagram illustrating a hydrocarbon production system 500 according to a fifth embodiment. As shown in Fig. 6, the hydrocarbon production system 500 includes a wet desulfurization unit 110, a pressure booster 120, a heat exchanger 130, an impurity removal unit 540, a water electrolysis unit 150, a hydrocarbon production unit 160, a heat supplier 570, and a central controller 590. In Fig. 6, solid arrows indicate the flow of gases such as mixed gas, carbon dioxide, hydrogen, and hydrocarbons. In Fig. 6, dashed arrows indicate the flow of a heat medium.

[0108] Note that components that are substantially the same as those in the hydrocarbon production system 100 described above are denoted by the same reference numerals and descriptions thereof will be omitted.

[0109] In this embodiment, the mixed gas contains sulfur components and carbon dioxide, and contains almost no oxygen. The mixed gas is, for example, exhaust gas emitted from a coal-fired power plant.

[0110] The impurity removal unit 540 includes a catalytic desulfurization unit 146 .

[0111] The heat supply unit 570 supplies the reaction heat generated in the hydrocarbon production unit 160 to the catalytic desulfurization unit 146. In this embodiment, the heat supply unit 570 includes flow paths 572a to 572c and a delivery device 576.

[0112] The flow path 572a connects the hydrocarbon production apparatus 160 and the catalytic desulfurization apparatus 146. The flow path 572b connects the catalytic desulfurization apparatus 146 and the suction side of the delivery apparatus 576. The flow path 572c connects the discharge side of the delivery apparatus 576 and the hydrocarbon production apparatus 160.

[0113] The delivery device 576 is, for example, a pump. When the delivery device 576 is operated, the heat medium circulates through the hydrocarbon production device 160 and the catalytic desulfurization device 146 via the flow paths 572a to 572c. As a result, the reaction heat generated in the hydrocarbon production device 160 is supplied to the catalytic desulfurization device 146.

[0114] The flow path 572a is provided with a flow rate adjusting valve RV4, the opening of which is adjusted by a heat control unit 592, which will be described later.

[0115] The central control unit 590 is configured by a semiconductor integrated circuit including a CPU (central processing unit). The central control unit 590 reads out programs, parameters, etc. for operating the CPU from the ROM. The central control unit 590 manages and controls the entire hydrocarbon production system 500 in cooperation with RAM as a work area and other electronic circuits.

[0116] In this embodiment, the central control unit 590 also functions as a thermal control unit 592 and an activation control unit 594 .

[0117] The heat control unit 592 adjusts the aperture of the flow control valve RV4 so that the temperature of the catalytic desulfurization device 146 is maintained at the activation temperature of the desulfurization catalyst. In this embodiment, the heat control unit 592 adjusts the aperture of the flow control valve RV4 so that the temperature of the catalytic desulfurization device 146 is 200°C or higher and 300°C or lower.

[0118] When starting up the hydrocarbon production apparatus 160, the start-up control unit 594 starts the operations of the pressure booster 120, the water electrolysis apparatus 150, and the delivery apparatus 576.

[0119] As described above, the hydrocarbon production system 500 according to this embodiment can omit the dry desulfurization unit 142 and the oxygen remover 144, as compared to the hydrocarbon production system 100. Therefore, the hydrocarbon production system 500 can efficiently utilize thermal energy while reducing the costs required for the dry desulfurization unit 142 and the oxygen remover 144.

[0120] [Sixth embodiment: hydrocarbon production system 600] In the above-described first embodiment, an example has been given in which the hydrocarbon production system 100 extracts carbon dioxide from a mixed gas containing sulfur components, oxygen, and carbon dioxide. However, if the mixed gas contains oxygen and carbon dioxide and contains almost no sulfur components, the wet desulfurization unit 110, the dry desulfurization unit 142, and the catalytic desulfurization unit 146 may be omitted.

[0121] Fig. 7 is a diagram illustrating a hydrocarbon production system 600 according to a sixth embodiment. As shown in Fig. 7, the hydrocarbon production system 600 includes a carbon dioxide recovery unit 610, a pressure booster 120, a heat exchanger 130, an impurity removal unit 440, a water electrolysis unit 150, a hydrocarbon production unit 160, a heat supplier 370, a start-up unit 180, and a central control unit 390. In Fig. 7, solid arrows indicate the flow of gases such as mixed gas, carbon dioxide, oxygen, hydrogen, and hydrocarbons. In Fig. 7, dashed arrows indicate the flow of a heat medium.

[0122] Note that components that are substantially the same as those in the hydrocarbon production systems 300 and 400 are denoted by the same reference numerals and descriptions thereof will be omitted.

[0123] The carbon dioxide capture device 610 captures carbon dioxide from the air and is, for example, a DAC (Direct Air Capture) device. The mixed gas output from the carbon dioxide capture device 610 contains oxygen and carbon dioxide, and contains almost no sulfur components.

[0124] In this embodiment, the intake side of the pressure booster 120 is connected to the carbon dioxide capture device 610. The discharge side of the pressure booster 120 is connected to the oxygen remover 144. Therefore, the mixed gas output from the carbon dioxide capture device 610 is supplied to the oxygen remover 144.

[0125] As described above, the hydrocarbon production system 600 according to this embodiment can omit the wet desulfurization unit 110, the dry desulfurization unit 142, and the catalytic desulfurization unit 146, compared to the hydrocarbon production system 100. Therefore, the hydrocarbon production system 600 can efficiently utilize thermal energy while reducing the costs required for the wet desulfurization unit 110, the dry desulfurization unit 142, and the catalytic desulfurization unit 146.

[0126] Although the embodiments have been described above with reference to the accompanying drawings, it goes without saying that the present disclosure is not limited to the above-described embodiments. It is clear that a person skilled in the art can conceive of various modifications or alterations within the scope of the claims, and it is understood that these also naturally fall within the technical scope of the present disclosure.

[0127] For example, in the above first to sixth embodiments, the heat supply units 170, 370, 570 supply the reaction heat generated in the hydrocarbon production apparatus 160 to either or both of the oxygen remover 144 and the catalytic desulfurization unit 146. However, the heat supply units may supply the reaction heat generated in the hydrocarbon production apparatus 160 to one or more of the dry desulfurization unit 142, the oxygen remover 144, and the catalytic desulfurization unit 146.

[0128] Furthermore, in the above first to sixth embodiments, an example has been given in which hydrogen produced by the water electrolysis system 150 is distributed to the impurity removal systems 140, 240, 340, 440, 550 and the hydrocarbon production system 160. However, all of the hydrogen produced by the water electrolysis system 150 may be supplied to the hydrocarbon production system 160 after passing through the impurity removal systems 140, 240, 340, 440, 550.

[0129] Furthermore, in the above first to sixth embodiments, examples have been given in which the hydrocarbon production systems 100, 200, 300, 400, 500, and 600 include the water electrolysis device 150. However, the hydrocarbon production system may include either or both of a hydrogen production device and a hydrogen cylinder instead of or in addition to the water electrolysis device 150. The hydrogen production device is, for example, a steam reformer.

[0130] In the above first embodiment, an example has been given in which the heat medium that has recovered the heat of reaction generated in the hydrocarbon production apparatus 160 heats the catalytic desulfurization apparatus 146 and then heats the oxygen remover 144. However, the heat medium that has recovered the heat of reaction generated in the hydrocarbon production apparatus 160 may heat the oxygen remover 144 and then heat the catalytic desulfurization apparatus 146. In addition, the heat medium that has recovered the heat of reaction generated in the hydrocarbon production apparatus 160 may heat the oxygen remover 144 and the catalytic desulfurization apparatus 146 in parallel (simultaneously).

[0131] Furthermore, in the above first to fourth and sixth embodiments, examples have been given in which the hydrocarbon production systems 100, 200, 300, 400, and 600 are equipped with the start-up device 180. However, the start-up device 180 is not an essential component.

[0132] Furthermore, in the above first to sixth embodiments, examples have been given in which the hydrocarbon production systems 100, 200, 300, 400, 500, and 600 include the heat exchanger 130. However, the heat exchanger 130 is not an essential component.

[0133] This disclosure can contribute, for example, to Sustainable Development Goals (SDGs) Goal 7: "Ensure access to affordable, reliable, sustainable and modern energy" and Goal 13: "Take urgent action to combat climate change and its impacts." [Explanation of symbols]

[0134] 100: Hydrocarbon production system 110: Wet desulfurization device 130: Heat exchanger 140: Impurity removal device 142: Dry desulfurization device 144: Oxygen removal device 146: Catalytic desulfurization device 150: Water electrolysis device 160: Hydrocarbon production device 170: Heat supply unit 180: Start-up device 200: Hydrocarbon production system 240: Impurity removal device 300: Hydrocarbon production system 340: Impurity removal device 370: Heat supply unit 400: Hydrocarbon production system 440: Impurity removal device 500: Hydrocarbon production system 540: Impurity removal device 570: Heat supply unit 600: Hydrocarbon production system

Claims

1. a wet desulfurization device that removes sulfur components from a mixed gas containing impurities including oxygen and sulfur components and carbon dioxide; an impurity removal device including an oxygen removal catalyst and to which hydrogen is supplied, and a catalytic desulfurization device including a desulfurization catalyst, for removing the impurities from the mixed gas treated by the wet desulfurization device; a hydrocarbon production device that includes a hydrocarbon synthesis catalyst that promotes a reaction for synthesizing hydrocarbons from carbon dioxide and hydrogen, and that synthesizes the hydrocarbons from carbon dioxide and hydrogen contained in the mixed gas from which the impurities have been removed by the impurity removal device; a heat supply unit that has a heat medium that recovers reaction heat generated in the hydrocarbon production apparatus, and heats the catalytic desulfurization unit with the heat medium, and then heats the oxygen removal unit; a water electrolysis device that electrolyzes water to generate hydrogen and oxygen; a startup device that supplies oxygen generated by the water electrolysis device to the oxygen removal device when starting up the hydrocarbon production device; Equipped with The hydrocarbon production system, wherein the oxygen removal catalyst and the hydrocarbon production device are supplied with hydrogen produced by the water electrolysis device.

2. The oxygen removal device is supplied with the mixed gas treated by the wet desulfurization device, The hydrocarbon production system according to claim 1 , wherein the catalytic desulfurization unit is supplied with the mixed gas treated by the oxygen removal unit.

3. the impurity removal device further includes a dry desulfurization device that includes an adsorbent that adsorbs the sulfur components and to which the mixed gas treated by the wet desulfurization device is supplied; The oxygen removal device is supplied with the mixed gas treated by the dry desulfurization device, The catalytic desulfurization device is supplied with the mixed gas treated by the oxygen removal device, The hydrocarbon production system according to claim 1 , wherein the heat supply unit supplies the reaction heat to the catalytic desulfurization unit, the oxygen remover, and the dry desulfurization unit.

4. 4. The hydrocarbon production system according to claim 1, further comprising a heat exchanger that exchanges heat between the mixed gas treated by the wet desulfurization unit and the mixed gas treated by the impurity removal unit.

5. Electrolyzing water to produce hydrogen and oxygen, In a wet desulfurization device, the sulfur component is removed from a mixed gas containing impurities including oxygen and sulfur components and carbon dioxide, an oxygen removal device including an oxygen removal catalyst and to which the generated hydrogen is supplied, and a catalytic desulfurization device including a desulfurization catalyst, for removing the impurities from the mixed gas treated by the wet desulfurization device; In a hydrocarbon production apparatus, the mixed gas from which the impurities have been removed is reacted with the produced hydrogen; Recovering reaction heat generated in the hydrocarbon production apparatus using a heat transfer medium; heating the catalytic desulfurization device with the heat medium and then heating the oxygen removal device; The hydrocarbon production method includes supplying the generated oxygen to the oxygen remover when starting up the hydrocarbon production apparatus.

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