Hydrocarbon Production Systems

Abstract

To provide a system for hydrocarbon production that can improve the production cost of hydrocarbon.SOLUTION: A system for hydrocarbon production comprises a hydrogen compound member, a reactor for accommodating the hydrogen compound member, a heater for heating the interior of the reactor, a gas feeder for feeding a gas comprising carbon dioxide to the interior of the reactor, and a water feeder for feeding water to the interior of the reactor.SELECTED DRAWING: Figure 1

Description

[Technical field]

[0001] The present disclosure relates to hydrocarbon production systems. [Background technology]

[0002] The device described in Patent Document 1 applies mechanical energy to a metal body including stainless steel in the presence of a gas including carbon dioxide and a hydrogen source, resulting in a contact pressure per unit area of ​​30 kPa or more through solid-to-solid contact, thereby adding hydrogen to the carbon dioxide and purifying hydrocarbons. [Prior art documents] [Patent documents]

[0003] [Patent Document 1] JP 2020-62618 A Summary of the Invention [Problem to be solved by the invention]

[0004] However, the device of Patent Document 1 has a problem of high manufacturing costs because electricity is consumed to provide mechanical energy to the metal body. In response to this, the inventors of the present application, taking into consideration that hydrogen compound members that can release hydrogen when heated are publicly known, have discovered that when a hydrogen compound member in a state where hydrogen is stored is heated and carbon dioxide is supplied while releasing hydrogen, hydrocarbons are produced, and they conceived that this could be used to produce hydrocarbons.

[0005] In view of the above, an object of at least one embodiment of the present disclosure is to provide a hydrocarbon production system that can improve the production cost of hydrocarbons. [Means for solving the problem]

[0006] In order to achieve the above object, the hydrocarbon production system according to the present disclosure includes a hydrogen compound member, a reaction vessel that accommodates the hydrogen compound member, a heating device that heats the inside of the reaction vessel, a gas supply device that supplies a carbon dioxide-containing gas that contains carbon dioxide to the inside of the reaction vessel, and a water supply device that supplies water to the inside of the reaction vessel. The hydrogen compound member has a chemical formula X, where X is an element other than hydrogen. m H n The hydrogen compound is represented by the formula: wherein the stoichiometric ratio m:n is 1:1 to 3:4, the element X is boron, and a hydrocarbon is produced from the water and the carbon dioxide in the presence of the hydrogen compound member contained in the reaction vessel. do. Effect of the Invention

[0007] According to the hydrocarbon production system of the present disclosure, when carbon dioxide and hydrogen are heated in the presence of a hydrogen compound member, the two react to produce hydrocarbons. Hydrogen can be stored in the hydrogen compound member by supplying water to the hydrogen compound member, and hydrogen can be released from the hydrogen compound member by heating the hydrogen compound member in a state in which hydrogen has been stored. Therefore, by producing hydrocarbons from water and carbon dioxide in the presence of a hydrogen compound member, the production cost of hydrocarbons can be improved. [Brief description of the drawings]

[0008] [Figure 1] FIG. 1 is a schematic diagram of a hydrocarbon production system according to an embodiment of the present disclosure. [Diagram 2] FIG. 1 is a schematic diagram showing a configuration in which a plant including a heat source and a hydrocarbon production system according to the present disclosure are combined. [Diagram 3] FIG. 1 is a schematic diagram of a GTCC power plant including a heat source and a gas source in combination with a hydrocarbon production system according to the present disclosure. [Figure 4] FIG. 1 is a schematic diagram showing a configuration in which a carbon dioxide recovery unit serving as a heat supply source and a gas supply source is combined with a hydrocarbon production system according to the present disclosure. [Diagram 5] FIG. 1 is a schematic diagram of a configuration in which a methanol synthesis plant including a heat source is combined with a hydrocarbon production system according to the present disclosure. [Figure 6]FIG. 1 is a schematic diagram of a fertilizer plant including a heat source and a gas source combined with a hydrocarbon production system of the present disclosure. [Figure 7] FIG. 1 is a schematic diagram showing a configuration in which a solar light collecting device and a hydrocarbon production system according to the present disclosure are combined. [Figure 8] FIG. 2 is a schematic diagram showing the configuration of an apparatus used in the examples. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0009] Hereinafter, a hydrocarbon production system according to an embodiment of the present disclosure will be described with reference to the drawings. The embodiment described below shows one aspect of the present disclosure, and does not limit the present disclosure. The embodiment can be arbitrarily modified within the scope of the technical idea of ​​the present disclosure.

[0010] <Configuration of Hydrocarbon Production System According to an Embodiment of the Present Disclosure> 1, a hydrocarbon production system 1 according to an embodiment of the present disclosure includes a reaction vessel 2 accommodating a hydrogen compound member 3, a heating device 4 for heating the inside of the reaction vessel 2, a gas supply device 5 for supplying a carbon dioxide-containing gas containing carbon dioxide into the reaction vessel 2, and a water supply device 6 for supplying water into the reaction vessel 2. The reaction vessel 2 is provided with an outlet 8 for discharging a fluid in the reaction vessel 2 to the outside.

[0011] The hydrogen compound member 3 has the chemical formula X, where X is an element other than hydrogen (H). m H n The hydrogen compound member 3 contains a two-dimensional arrangement of hydrogen compounds represented by the formula (1) and the stoichiometric ratio m:n is 1:1 to 3:4 (for example, XH, XH2, XH3, XH4, X2H3, X3H4). Although not limited thereto, the element X is, for example, boron (B). In this embodiment, the hydrogen compound member 3 is described as being borohydride (HB).

[0012] The heating device 4 is for heating the inside of the reaction vessel 2, i.e., the hydrogen compound member 3 housed in the reaction vessel 2. The heating device 4 may be configured so that a heat medium is directly contacted with the hydrogen compound member 3 by supplying the heat medium into the reaction vessel 2, but hereinafter, the heating device 4 will be described as having a configuration in which the heat medium is circulated through a heat medium passage 9 such as a jacket or passage provided so as to cover the outer surface of the reaction vessel 2, and heat is exchanged between the heat medium and the gas in the reaction vessel 2, thereby heating the hydrogen compound member 3 housed in the reaction vessel 2. The heat medium is not particularly limited, but it is preferable to use a liquid such as water or oil.

[0013] The heating device 4 includes a heat medium circulation line 4a, one end of which is connected to the inlet of the heat medium passage 9 and the other end of which is connected to the outlet of the heat medium passage 9, through which the heat medium circulates, and the heat medium circulation line 4a is configured to transfer heat generated in the heat supply source 10 to the heat medium circulating in the heat medium circulation line 4a, for example, by heat exchange. However, the heating device 4 is not limited to this form, and depending on the configuration of the heat supply source 10, a fluid containing heat generated in the heat supply source 10 and directly supplied from the heat supply source 10, or a part of the fluid, may be circulated as the heat medium in the heat medium circulation line 4a. The configuration of the heat supply source 10 will be described later.

[0014] The configuration of the gas supply device 5 is not particularly limited, and may be, for example, a compressor communicating with a gas supply source 11. As the gas supply source 11, a carbon dioxide cylinder for storing carbon dioxide or the like can be used, but gas supply sources 11 with other configurations will be described later. The water supply device 6 is for supplying liquid water or steam, or a fluid containing at least one of water or steam as a main component (hereinafter, simply referred to as "water" to mean any of these) into the reaction vessel 2.

[0015] Operation of the Hydrocarbon Production System According to an Embodiment of the Present Disclosure Next, an operation of the hydrocarbon production system 1 according to an embodiment of the present disclosure will be described. The hydrocarbon production system 1 operates to alternately switch between an operation of driving the water supply device 6 to store hydrogen in the hydrogen compound member 3 (hydrogen storage operation) and an operation of driving the heating device 4 and the gas supply device 5 to produce hydrocarbons (hydrocarbon production operation).

[0016] First, the hydrogen storage operation will be described. When the temperature inside the reaction vessel 2 is less than about 150°C, preferably between about 80°C or higher and less than about 150°C, water is supplied from the water supply device 6 into the reaction vessel 2. Then, as represented by the following reaction formula (1), the water is decomposed into hydrogen and oxygen in the presence of the hydrogen compound member 3, and the hydrogen is stored in the hydrogen compound member 3. HB(C1)+yH2O→HB(C2)+zO2···(1) In addition, in reaction formula (1), "C1" means a state (state 1) in which hydrogen stored in HB is released, and "C2" means a state (state 2) in which hydrogen is stored in HB. This reaction causes the hydrogen compound member 3 to store hydrogen. Although oxygen remains in the reaction vessel 2, oxygen can be recovered by flowing out the oxygen from the reaction vessel 2 through the outflow part 8.

[0017] Next, the hydrocarbon production operation will be described. The hydrogen compound member 3 accommodated in the reaction vessel 2 is in a state of storing hydrogen by the above-mentioned hydrogen storage operation. The heat medium, which is a fluid that absorbs heat generated by the heat supply source 10, is caused to circulate through the heat medium circulation line 4a so that the heat medium flows through the heat medium passage 9. That is, the heating device 4 is driven. Then, the heat medium exchanges heat with the gas in the reaction vessel 2 while flowing through the heat medium passage 9, thereby heating the hydrogen compound member 3 accommodated in the reaction vessel 2. When the temperature of the hydrogen compound member 3 reaches a range of about 150°C to about 300°C, the gas supply device 5 is started to supply a carbon dioxide-containing gas into the reaction vessel 2.

[0018] When the temperature of the hydrogen compound member 3 in a state where hydrogen is stored falls within the above temperature range, hydrogen is released from the hydrogen compound member 3. As a result, hydrogen and carbon dioxide coexist in the reaction vessel 2 in the presence of the hydrogen compound member 3. The present inventors have found that in the presence of the hydrogen compound member 3, hydrogen and carbon dioxide react to produce hydrocarbons. The reaction for producing hydrocarbons is considered to be as follows.

[0019] If the hydrogen compound constituting the hydrogen compound member 3 is borohydride (HB), hydrogen is released from the hydrogen compound member 3 according to the following reaction formula (2). HB(C2) → HB(C1) + xH2 (2) In the presence of the hydrogen compound member 3, the hydrogen released according to reaction formula (2) and the carbon dioxide supplied into the reaction vessel 2 by the gas supply device 5 react as shown in the following reaction formula (3). aCO2+bH2→C a H b +cH2O (3)

[0020] In experiments conducted by the present inventors, it was found that the hydrocarbons produced by reaction formula (2) are not limited to methane when a=1 and b=2 in reaction formula (2), but include ethane or ethylene when a=2, propane or propylene when a=3, and even butane or butene when a=4.

[0021] The hydrocarbons thus produced are discharged from the reaction vessel 2 via the outlet 8 after the heating device 4 and the gas supply device 5 are stopped, and can be recovered or supplied to equipment requiring the hydrocarbons. By discharging the produced hydrocarbons from the outlet 8, the temperature inside the reaction vessel 2 is lowered, and hydrogen storage operation is then possible, and continuous production of hydrocarbons is possible by sequentially repeating the hydrocarbon production operation and the hydrogen storage operation. Note that by circulating a heat medium for cooling through the heat medium passage 9 (forming a cooling device), the inside of the reaction vessel 2 can be actively cooled to a temperature suitable for hydrogen storage operation.

[0022] The results of comparing the above-described hydrocarbon production technology of the present disclosure with conventional carbon dioxide reduction technology are summarized in the following Table 1. In Table 1, the advantages of each technology are marked with "◯", disadvantages with "×", and points that cannot be determined are marked with "△".

[0023] [Table 1]

[0024] According to electrolytic reduction technology and methanation, methane can be produced in the same manner as the technology of the present disclosure, but electrolytic reduction technology requires electric power, and methanation requires hydrogen supply and heat of 400 ° C. In contrast, in the technology of the present disclosure, if an electric heater is not used as the heating device 4, electric power is not required to generate the above reaction formulas (1) and (2), and the reaction temperature is in the range of about 150 ° C to about 300 ° C., so it can be said that the technology of the present disclosure is superior in terms of the production cost of hydrocarbons compared to electrolytic reduction technology and methanation. In addition, although the artificial photosynthesis technology has a different product from the technology of the present disclosure, it has the advantage that it can cause a reaction by irradiating light using water and carbon dioxide as raw materials, but has the disadvantage that it requires a large reaction area, and is considered to have no advantage over the technology of the present disclosure. Therefore, it can be said that the hydrocarbon production technology of the present disclosure is superior in terms of the production cost of hydrocarbons compared to the conventional carbon dioxide reduction technology.

[0025] In this way, when carbon dioxide and hydrogen are heated in the presence of the hydrogen compound member 3, the two react with each other to produce hydrocarbons. Hydrogen can be stored in the hydrogen compound member 3 by supplying water to the hydrogen compound member 3, and hydrogen can be released from the hydrogen compound member 3 by heating the hydrogen compound member 3 in a state in which hydrogen has been stored. Therefore, by producing hydrocarbons from water and carbon dioxide in the presence of the hydrogen compound member 3, the production cost of hydrocarbons can be improved.

[0026] <Configuration of heat supply source 10 and gas supply source 11> Next, several configurations of the heat supply source 10 and the gas supply source 11 will be described, but the heat supply source 10 and the gas supply source 11 are not limited to the configurations described below. FIG. 2 shows a schematic configuration of a combination of a plant 100 such as a factory or a power plant including the heat supply source 10 and a hydrocarbon production system 1. The plant 100 may include a gas supply source 11. Before specifically describing the configurations of the heat supply source 10 and the gas supply source 11, a general configuration for supplying a heat medium and a carbon dioxide-containing gas from the plant 100 to the hydrocarbon production system 1 and supplying the hydrocarbons produced in the hydrocarbon production system 1 to other facilities (including the plant 100) will be described based on FIG. 2.

[0027] A plant 100 such as a factory or a power plant includes a combustion device such as a boiler and a chemical reaction device, and may generate heat or discharge exhaust gas containing carbon dioxide. By supplying a heat medium 101 containing this heat to a reaction vessel 2 of a hydrocarbon production system 1, or supplying an exhaust gas 104 containing carbon dioxide or a gas 105 with an increased carbon dioxide content by a carbon dioxide capture device 102 of any configuration as a carbon dioxide-containing gas into the reaction vessel 2, it becomes possible to heat the reaction vessel 2 and supply a carbon dioxide-containing gas into the reaction vessel 2. The hydrocarbons 103 generated in the hydrocarbon production system 1 can be used as fuel or a raw material for chemical reactions in the plant 100. By the hydrocarbon production system 1 utilizing the exhaust heat generated in the plant 100, it is possible to suppress the energy consumption in the hydrocarbon production system 1. In addition, by the hydrocarbon production system 1 utilizing the carbon dioxide generated in the plant 100, it is possible to improve the power efficiency of the entire facility including the plant 100 and the hydrocarbon production system 1, and to reuse the carbon dioxide that would otherwise be discharged into the atmosphere.

[0028] 3 shows a schematic diagram of a gas turbine combined cycle (GTCC) power plant 100a as an example of a plant 100 including a heat supply source 10 and a gas supply source 11, combined with a hydrocarbon production system 1. The GTCC power plant 100a includes a gas turbine 110, a generator 111 driven by the gas turbine 110, a boiler 113 that generates steam using exhaust gas 112 from the gas turbine 110, a steam turbine 115 driven by steam 114 generated by the boiler 113, and a generator 116 driven by the steam turbine 115.

[0029] In this embodiment, a part of the exhaust gas 112 from the gas turbine 110 can be supplied as a heat medium 118 to the reaction vessel 2 of the hydrocarbon production system 1, and the heat medium 118 that has been heat exchanged with a part of the exhaust gas 112 in a heat exchanger (not shown) can be supplied to the reaction vessel 2. Therefore, in this embodiment, the gas turbine 110 is a heat supply device serving as the heat supply source 10.

[0030] Since the exhaust gas 112 of the gas turbine 110 contains carbon dioxide, in this embodiment, a part of the exhaust gas 112 can be supplied as a carbon dioxide-containing gas 119 into the reaction vessel 2 of the hydrocarbon production system 1, and a gas with an increased carbon dioxide content by the carbon dioxide capture device 102 can be supplied as the carbon dioxide-containing gas 119 into the reaction vessel 2 of the hydrocarbon production system 1. Therefore, in this embodiment, the gas turbine 110 is the gas supply source 11. By the hydrocarbon production system 1 utilizing the exhaust heat of the gas turbine 110, it is possible to suppress energy consumption in the hydrocarbon production system 1. In addition, by the hydrocarbon production system 1 utilizing the carbon dioxide in the exhaust gas of the gas turbine 110, it becomes possible to reuse carbon dioxide that would otherwise be discharged into the atmosphere.

[0031] In this embodiment, the hydrocarbons 117 produced in the hydrocarbon production system 1 can be supplied as fuel or a part thereof to be combusted in the combustor of the gas turbine 110. This can improve the power generation efficiency in the GTCC power plant 100a.

[0032] 4 shows a schematic diagram of a configuration in which a carbon dioxide capture unit 120 provided in any facility as a heat supply source 10 and a gas supply source 11 is combined with a hydrocarbon production system 1. The carbon dioxide capture unit 120 may be provided for any purpose, and may be, for example, the carbon dioxide capture unit 102 provided in the plant 100 in FIG. 2, or may be provided for capturing carbon dioxide contained in the atmosphere, although the carbon dioxide capture efficiency is low.

[0033] In this embodiment, the gas 121 having an increased carbon dioxide content by capturing carbon dioxide in the carbon dioxide capture unit 120 can be supplied as a carbon dioxide-containing gas into the reaction vessel 2 of the hydrocarbon production system 1. Generally, heat is generated in the process of capturing carbon dioxide. Therefore, a fluid 122 containing the heat generated in the carbon dioxide capture unit 120 can be supplied to the reaction vessel 2 as a heat medium. If there is a risk that the amount of heat generated by the carbon dioxide capture unit 120 alone is insufficient, an additional heating device 123 such as an electric heater may be provided. This makes it possible to reuse the carbon dioxide that is originally emitted into the atmosphere but is captured by the carbon dioxide capture unit 120. In addition, the hydrocarbon production system 1 utilizes the heat generated in the process of capturing carbon dioxide in the carbon dioxide capture unit 120, thereby reducing the energy consumption in the hydrocarbon production system 1.

[0034] In this embodiment, the hydrocarbons 124 produced in the hydrocarbon production system 1 can be supplied to any facility. Although the configuration is not limited to this embodiment, a steam cracker 125 can also be provided. The hydrocarbons 124 can be decomposed into ethylene and propylene in the steam cracker 125 and supplied to any chemical plant. This makes it possible to effectively utilize carbon dioxide that would otherwise be emitted into the atmosphere.

[0035] 5 shows a schematic diagram of a methanol synthesis plant 100b as an example of a plant 100 including a heat supply source 10, which is combined with a hydrocarbon production system 1. The methanol synthesis plant 100b includes a reformer 130 that reforms natural gas with steam, a compressor 131 that compresses the reformed gas produced in the reformer 130, a methanol synthesis unit 132 that synthesizes methanol using the reformed gas supplied by the compressor 131, and a distillation column 133 that refines the crude methanol produced in the methanol synthesis unit 132.

[0036] The water supply device 6 of the hydrocarbon production system 1 is configured so as to be able to supply a part of the steam supplied to the reformer 130 into the reaction vessel 2. In this embodiment, the gas supply source 11 may have any configuration. The hydrocarbons 134 produced in the hydrocarbon production system 1 are supplied to the reformer 130 together with the natural gas supplied to the reformer 130, and can be used as a part of the raw material for producing the reformed gas. This makes it possible to reduce the amount of natural gas used as the raw material for methanol production, thereby reducing the cost of producing methanol.

[0037] In this embodiment, since the reforming reaction of natural gas in the reformer 130 is an endothermic reaction, a heat medium for supplying heat to the reformer 130 is supplied to the reformer 130. The heat medium 135 flowing out from the reformer 130 is cooled below the temperature when it is supplied to the reformer 130, but has a sufficient temperature to be used as a heat medium to be supplied to the reaction vessel 2. Therefore, the heat medium 135 flowing out from the reformer 130 can be supplied to the reaction vessel 2. Therefore, in this embodiment, the reformer 130 is a heat supply device serving as the heat supply source 10. The remaining heat for the reforming reaction of natural gas is utilized by the hydrocarbon production system 1, thereby making it possible to suppress energy consumption in the hydrocarbon production system 1.

[0038] 6 illustrates a schematic configuration diagram of a fertilizer plant 100c as an example of a plant 100 including a heat supply source 10 and a gas supply source 11, in combination with a hydrocarbon production system 1. The fertilizer plant 100c is a plant that produces urea as a fertilizer. The fertilizer plant 100c includes a reformer 140 that reforms natural gas with steam, a modifier 141 that modifies carbon monoxide and steam in the reformed gas generated by the reformer 140 into carbon dioxide and hydrogen, a carbon dioxide recovery unit 142 that recovers carbon dioxide in the gas supplied from the modifier 141, a methanation unit 143 that converts the carbon monoxide and carbon dioxide remaining in the gas from which the carbon dioxide has been recovered in the carbon dioxide recovery unit 142 into methane, a compressor 144 that compresses the gas flowing out from the methanation unit 143, an ammonia production unit 145 that produces ammonia by reacting hydrogen and nitrogen in the gas supplied from the compressor 144, and a urea production unit 146 that produces urea by reacting carbon dioxide 147 recovered in the carbon dioxide recovery unit 142 with ammonia 148 produced in the ammonia production unit 145.

[0039] The water supply device 6 of the hydrocarbon production system 1 is configured to be able to supply a part of the steam supplied to the reformer 140 into the reaction vessel 2. In addition, the gas supply device 5 of the hydrocarbon production system 1 is configured to be able to supply a part of the carbon dioxide 147 recovered in the carbon dioxide recovery device 142 into the reaction vessel 2. Furthermore, the hydrocarbons 150 produced in the hydrocarbon production system 1 are supplied to the reformer 140 together with the natural gas supplied to the reformer 140, and can be used as a part of the raw material for producing the reformed gas. This makes it possible to reduce the amount of natural gas used as a raw material for urea production, thereby reducing the production cost of urea.

[0040] In this embodiment, since the reforming reaction of natural gas in the reformer 140 is an endothermic reaction, a heat medium for supplying heat to the reformer 140 is supplied to the reformer 140. The heat medium 149 flowing out from the reformer 140 is cooled below the temperature when it is supplied to the reformer 140, but has a sufficient temperature to be used as a heat medium to be supplied to the reaction vessel 2. Therefore, the heat medium 149 flowing out from the reformer 140 can be supplied to the reaction vessel 2. Therefore, in this embodiment, the reformer 140 is a heat supply device serving as the heat supply source 10. The remaining heat for the reforming reaction of natural gas is utilized by the hydrocarbon production system 1, thereby making it possible to suppress energy consumption in the hydrocarbon production system 1.

[0041] 7 shows a hydrocarbon production system 1 provided with a solar collector 160 for collecting sunlight as the heat supply source 10. The configuration of the solar collector 160 is not particularly limited, and any type of device such as a parabolic trough, a solar power generation tower, or a parabolic dish can be used, but considering the maximum heating temperature, costs, etc., a parabolic trough type device is preferable. The other configuration is the same as that of the hydrocarbon production system 1 shown in FIG.

[0042] However, the specific configuration of the gas supply source 11 and the supply source of water supplied by the water supply device 6 differ depending on the location where the hydrocarbon production system 1 is installed. For example, when the hydrocarbon production system 1 is installed in the plant 100 of Fig. 2, the gas supply source 11 and the supply source of water can be the same as those in the hydrocarbon production systems 1 shown in each of Figs. 3 to 6, depending on the specific configuration of the plant 100.

[0043] However, since the light collecting device 160 is generally installed in a relatively large installation site, it is often the case that the gas supply source 11 and the water supply source installed in the plant 100 of Fig. 2 cannot be used. In such a case, a carbon dioxide separator 11a that separates carbon dioxide from air may be installed as the gas supply source 11. As the carbon dioxide separator 11a, for example, a device configured to absorb carbon dioxide in a liquid absorption liquid such as an amine aqueous solution, or a device configured to adsorb carbon dioxide in a solid absorbent can be used. As the water supply source, a river, lake, or marsh existing near the installation site may be used, or a tank for storing water may be used.

[0044] In this embodiment, the heat medium circulating through the heat medium circulation line 4a is irradiated with sunlight concentrated by the light collector 160, thereby heating the heat medium. Since the inside of the reaction vessel 2 is heated by the heat of sunlight, it is possible to improve the thermal efficiency, and as a result, it is possible to further improve the cost of producing hydrocarbons. In addition, by providing a carbon dioxide separator 11a as the gas supply source 11, it is possible to produce hydrocarbons even if there is no carbon dioxide supply source nearby.

[0045] <Example> Next, it was verified by an example that when a hydrogen compound member in a state where hydrogen is stored is heated and carbon dioxide is supplied while releasing hydrogen, hydrocarbons are generated. FIG. 8 shows the configuration of the device 200 used in this example. The device 200 includes a reactor 202 (volume: 0.3 L) capable of accommodating a hydrogen compound member 201 (HB) therein. The reactor 202 includes a mantle heater 203 for heating the inside of the reactor 202. The reactor 202 is in communication with an argon cylinder 204 and a carbon dioxide cylinder 205. The reactor 202 is in communication with a microsyringe 206 for injecting water into the reactor 202 and a gas syringe 207 for sampling the gas inside the reactor 202.

[0046] Using the device 200, an experiment was carried out in the following procedure. Argon was supplied from an argon cylinder 204 to the reactor 202, and the inside of the reactor 202 was pressurized to 0.1 MPaG. The pressure inside the reactor 202 was reduced and set to 0.01 MPaG or less. The gas in the reactor 202 was sampled using a gas syringe 207, and the sampled gas was analyzed by gas chromatography. Using the microsyringe 206, 0.5 cc of water was injected into the reactor 202. Carbon dioxide was supplied from a carbon dioxide cylinder 205 to the reactor 202, and the inside of the reactor 202 was pressurized to 0.1 MPaG. The mantle heater 203 was started, and the temperature inside the reactor 202 was increased stepwise by 50° C. each time. Immediately after the temperature inside the reactor 202 reached 200° C., the gas inside the reactor 202 was sampled using the gas syringe 207, and the sampled gas was analyzed by gas chromatography. After the temperature in the reactor 202 reached 250° C., the temperature was adjusted to be maintained at that temperature, and the gas in the reactor 202 was sampled periodically and analyzed by gas chromatography.

[0047] Table 2 shows the results of gas chromatography analysis before the start of the experiment, 2 hours after the start of the experiment, and 40 hours after the start of the experiment.

[0048] [Table 2]

[0049] According to Table 2, it can be confirmed that methane and ethane are produced at the reaction temperatures of 200°C and 250°C. In addition, although the specific composition of C3 or C4 equivalent substances was not quantified at the reaction temperature of 250°C, the total estimated value was "5.0 x 10 -4 The analytical result of "mol" is described. From this result, it can be confirmed that a substance equivalent to C3 or C4 is generated. Therefore, from this example, it was confirmed that when a hydrogen compound member in a state where hydrogen is stored is heated and carbon dioxide is supplied while releasing hydrogen, hydrocarbons having a carbon number of 4 or less are generated.

[0050] The contents described in each of the above embodiments can be understood, for example, as follows.

[0051] [1] A hydrocarbon production system according to one embodiment comprises: A hydrogen compound member (3); a reaction vessel (2) for accommodating the hydrogen compound member (3); A heating device (4) for heating the inside of the reaction vessel (2); a gas supply device (5) for supplying a carbon dioxide-containing gas containing carbon dioxide into the reaction vessel (2); a water supply device (6) for supplying water to the inside of the reaction vessel (2); Equipped with.

[0052] According to the hydrocarbon production system of the present disclosure, when carbon dioxide and hydrogen are heated in the presence of a hydrogen compound member, the two react to produce hydrocarbons. Hydrogen can be stored in the hydrogen compound member by supplying water to the hydrogen compound member, and hydrogen can be released from the hydrogen compound member by heating the hydrogen compound member in a state in which hydrogen has been stored. Therefore, by producing hydrocarbons from water and carbon dioxide in the presence of a hydrogen compound member, the production cost of hydrocarbons can be improved.

[0053] [2] A hydrocarbon production system according to another embodiment is the hydrocarbon production system according to [1], The temperature inside the reaction vessel (2), which contains the hydrogen compound member (3) in a state where hydrogen is stored, is kept in the range of 150°C to 300°C by the heating device (4), and the carbon dioxide-containing gas is supplied from the gas supply device (5) to the inside of the reaction vessel (2).

[0054] According to this configuration, hydrogen released from the hydrogen compound component and carbon dioxide supplied to the inside of the reaction vessel react in the presence of the hydrogen compound component to produce hydrocarbons, making it possible to produce hydrocarbons from water and carbon dioxide in the presence of the hydrogen compound component.

[0055] [3] A hydrocarbon production system according to yet another embodiment is the hydrocarbon production system according to [1], When the temperature inside the reaction vessel (2) accommodating the hydrogen compound member (3) is less than 150° C., water is supplied from the water supply device (6) into the reaction vessel (2).

[0056] According to such a configuration, since hydrogen can be stored in the hydrogen compound member after hydrocarbons are produced by releasing hydrogen, the hydrogen compound member can be repeatedly used for producing hydrocarbons.

[0057] [4] A hydrocarbon production system according to yet another embodiment is any one of the hydrocarbon production systems [1] to [3], Further comprising a heat supply device (10), The heating device (4) is configured to heat the inside of the reaction vessel (2) by a heating fluid, The heating fluid is a fluid that has absorbed heat generated in the heat supply device (10).

[0058] According to such a configuration, the inside of the reaction vessel is heated by heat from the heat supply device, so that the thermal efficiency can be improved, and as a result, the production cost of hydrocarbons can be further improved.

[0059] [5] A hydrocarbon production system according to yet another embodiment is the hydrocarbon production system according to [4], a gas source (11) for producing or recovering carbon dioxide; The gas supply device (5) communicates with the gas supply source (11).

[0060] According to such a configuration, the carbon dioxide generated or recovered at the gas source can be used for the production of hydrocarbons, thereby further improving the cost of producing hydrocarbons.

[0061] [6] A hydrocarbon production system according to yet another embodiment is any one of the hydrocarbon production systems [1] to [3], The solar panel further includes a solar collector (160), The heating device (4) is configured to heat the inside of the reaction vessel (2) by a heating fluid, The heated fluid is a fluid that has been heated by irradiation with sunlight concentrated by the light collecting device (160).

[0062] According to such a configuration, the inside of the reaction vessel is heated by the heat of sunlight, so that the thermal efficiency can be improved, and as a result, the production cost of hydrocarbons can be further improved.

[0063] [7] A hydrocarbon production system according to yet another embodiment is the hydrocarbon production system according to [6], A carbon dioxide separator (11a) for separating carbon dioxide from air is further provided, The gas supply device (5) communicates with the carbon dioxide separator (11a).

[0064] According to this configuration, carbon dioxide in the air is used to produce hydrocarbons, so that it is possible to produce hydrocarbons even when there is no carbon dioxide source nearby. [Explanation of symbols]

[0065] 1. Hydrocarbon Production System 2 Reaction vessel 3 Hydrogen compound materials 4 Heating device 5 Gas supply equipment 6 Water supply device 10 Heat supply source (heat supply device) 11 Gas supply source 11a Carbon dioxide separator 160 Light Concentrator

Claims

1. A hydrogen compound member; a reaction vessel for accommodating the hydrogen compound member; A heating device for heating the inside of the reaction vessel; A gas supply device for supplying a carbon dioxide-containing gas containing carbon dioxide into the reaction vessel; a water supply device for supplying water to the inside of the reaction vessel; Equipped with The hydrogen compound member contains a hydrogen compound represented by a chemical formula X m H n , where X is an element other than hydrogen, and the stoichiometric ratio m:n is 1:1 to 3:4, and the element X is boron; A hydrocarbon production system that produces hydrocarbons from the water and the carbon dioxide in the presence of the hydrogen compound member contained in the reaction vessel.

2. 2. The hydrocarbon production system according to claim 1, wherein the carbon dioxide-containing gas is supplied from the gas supply device to the inside of the reaction vessel, which contains the hydrogen compound member in a state where hydrogen is stored, in a state where the temperature inside the reaction vessel is kept in the range of 150°C to 300°C by the heating device.

3. The hydrocarbon production system according to claim 1 , wherein water is supplied from the water supply device to the inside of the reaction vessel accommodating the hydrogen compound member in a state in which the temperature inside the reaction vessel is less than 150° C.

4. Further comprising a heat supply device; The heating device is configured to heat the interior of the reaction vessel with a heating fluid; The hydrocarbon production system according to any one of claims 1 to 3, wherein the heating fluid is a fluid that has absorbed heat generated in the heat supply device.

5. Further comprising a gas source for producing or capturing carbon dioxide; The hydrocarbon production system of claim 4 , wherein the gas supply is in communication with the gas source.

6. Further comprising a light collecting device for collecting sunlight, The heating device is configured to heat the interior of the reaction vessel with a heating fluid; The hydrocarbon production system according to any one of claims 1 to 3, wherein the heated fluid is a fluid heated by irradiation with sunlight concentrated by the light collecting device.

7. A carbon dioxide separator is further provided for separating carbon dioxide from the air, The hydrocarbon production system of claim 6 , wherein the gas supply is in communication with the carbon dioxide separator.

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