Hydrogen production system and hydrocarbon production system

Abstract

This hydrogen production system comprises: a hydrogen compound member; a water supply member for supplying water to the hydrogen compound member; and a heat recovery device for recovering adsorption heat that is generated when hydrogen, which is generated by decomposing some of water into hydrogen and oxygen in the presence of the hydrogen compound member, is adsorbed to the hydrogen compound member. This hydrocarbon production system comprises: a hydrogen compound member; a water supply member for supplying water to the hydrogen compound member; a heat recovery device for recovering adsorption heat that is generated when hydrogen, which is generated by decomposing some of water into hydrogen and oxygen in the presence of the hydrogen compound member, is adsorbed to the hydrogen compound member; a heating device for heating the hydrogen compound member to which hydrogen is adsorbed; and a gas supply device for supplying a carbon dioxide-containing gas that contains carbon dioxide to the hydrogen compound member.

Description

Hydrogen production system and hydrocarbon production system

[0001] This application claims priority to Japanese Patent Application No. 2024-116683, filed on July 22, 2024, with the Japan Patent Office, the contents of which are incorporated herein by reference.

[0002] Patent Document 1 discloses a hydrogen production system that utilizes the following phenomenon: when water is supplied to a hydrogen compound (e.g., borohydride having a two-dimensional arrangement) at a temperature of about 80°C or higher and lower than about 150°C, hydrogen is adsorbed onto the hydrogen compound and oxygen or a compound containing an oxygen atom (e.g., hydroxide, hydrogen peroxide, etc.) is generated; and when the hydrogen-adsorbed hydrogen compound is heated to a temperature range of about 150°C to about 300°C, hydrogen is released from the hydrogen compound. Patent Document 1 also describes the use of hydrogen released from the hydrogen compound in an ammonia production system, a power generation system, a fuel cell system, a steelmaking system, etc. Patent Document 2 describes a hydrocarbon production system that produces hydrocarbons by reacting hydrogen released from the hydrogen compound with carbon dioxide in the presence of the hydrogen compound.

[0003] JP 2023-30975 A JP 2023-30964 A

[0004] Heat of adsorption is generated when hydrogen is adsorbed onto hydrogen compounds, but the hydrogen production system of Patent Document 1 does not anticipate utilizing this heat of adsorption, and therefore presents a problem of increased operating costs for the hydrogen production system from the perspective of thermal efficiency. Furthermore, while Patent Document 1 describes utilizing hydrogen released from hydrogen compounds, it does not describe utilizing oxygen generated when hydrogen is adsorbed onto hydrogen compounds, and therefore, depending on how the oxygen is utilized, it may be possible to reduce the operating costs of the hydrogen production system.

[0005] In view of the above, an object of at least one embodiment of the present disclosure is to provide a hydrogen production system and a hydrocarbon production system with reduced operating costs.

[0006] In order to achieve the above-mentioned object, the hydrogen production system according to the present disclosure comprises a hydrogen compound element, a water supply element that supplies water to the hydrogen compound element, and a heat recovery device that recovers the heat of adsorption generated when the hydrogen produced by decomposing a portion of the water into hydrogen and oxygen in the presence of the hydrogen compound element is adsorbed by the hydrogen compound element.

[0007] The hydrocarbon production system according to the present disclosure also includes a hydrogen compound element, a water supply element that supplies water to the hydrogen compound element, a heat recovery device that recovers heat of adsorption generated when hydrogen produced by decomposing a portion of the water into hydrogen and oxygen in the presence of the hydrogen compound element is adsorbed by the hydrogen compound element, a heating device that heats the hydrogen compound element to which the hydrogen has been adsorbed, and a gas supply device that supplies a carbon dioxide-containing gas containing carbon dioxide to the hydrogen compound element.

[0008] According to the hydrogen production system and hydrocarbon production system of the present disclosure, the thermal efficiency is improved by recovering and utilizing the heat of adsorption that is generated when hydrogen, which is produced by decomposing a portion of water into hydrogen and oxygen in the presence of a hydrogen compound component, is adsorbed onto the hydrogen compound component, thereby reducing the operating costs of the hydrogen production system and the hydrocarbon production system.

[0009] FIG. 1 is a diagram showing a concept common to several specific configurations included in the hydrogen production system according to embodiment 1 of the present disclosure. FIG. 2 is a diagram showing a concept common to specific configurations in the hydrogen production system according to embodiment 1 of the present disclosure when the heat recovery device is in the form of a heat exchanger. FIG. 3 is a schematic diagram showing an example of a specific configuration of the hydrogen production system according to embodiment 1 of the present disclosure. FIG. 4 is a diagram showing a concept common to several specific configurations included in the hydrogen production system according to embodiment 2 of the present disclosure. FIG. 5 is a diagram showing a configuration of specific example 1 of the hydrogen production system according to embodiment 2 of the present disclosure. FIG. 6 is a diagram showing a configuration of specific example 2 of the hydrogen production system according to embodiment 2 of the present disclosure. FIG. 7 is a diagram showing a configuration of specific example 3 of the hydrogen production system according to embodiment 2 of the present disclosure. FIG. 8 is a diagram showing a configuration of specific example 4 of the hydrogen production system according to embodiment 2 of the present disclosure. FIG. 9 is a diagram showing the concept of the hydrogen production system according to embodiment 3 of the present disclosure. FIG. 10 is a diagram showing the concept of the hydrogen production system according to embodiment 4 of the present disclosure. FIG. 11 is a schematic graph for explaining the functions and effects of the hydrogen production system according to embodiment 4 of the present disclosure. FIG. 12 is a diagram showing the concept of the hydrogen production system according to embodiment 5 of the present disclosure. FIG. 13 is a schematic graph for explaining the functions and effects of the hydrogen production system according to embodiment 5 of the present disclosure. Fig. 1 is a diagram showing the concept of a hydrogen production system according to embodiment 6 of the present disclosure. Fig. 2 is a diagram showing the concept of a hydrogen production system according to embodiment 7 of the present disclosure. Fig. 3 is a diagram showing the concept of a hydrocarbon production system according to embodiment 1 of the present disclosure. Fig. 4 is a diagram showing the concept of a hydrocarbon production system according to embodiment 2 of the present disclosure.

[0010] Hereinafter, a hydrogen production system and a hydrocarbon production system according to embodiments of the present disclosure will be described with reference to the drawings. The embodiments described below represent one aspect of the present disclosure, and are not intended to limit the present disclosure. Any modification can be made within the scope of the technical concept of the present disclosure.

[0011] [Hydrogen Production System of the Present Disclosure] (Embodiment 1) <Configuration of the Hydrogen Production System According to Embodiment 1 of the Present Disclosure> The hydrogen production system according to Embodiment 1 of the present disclosure includes several specific configurations, as will be described later. Figure 1 shows the concept common to these specific configurations. The hydrogen production system 1 includes a hydrogen compound member 2, a water supply member 3 that supplies water 7 to the hydrogen compound member 2, and a heat recovery device 4. The hydrogen compound member 2 is a hydrogen compound represented by the chemical formula X ｍ H ｎ The stoichiometric ratio m:n is 1:1 to 3:4 (for example, XH, XH ２ , X.H. ３ , X.H. ４ , X ２ H ３ , X ３ H ４ ) (m and n are not limited to integers and may be non-integer numbers.) The element X is, but is not limited to, boron (B), for example.

[0012] The heat recovery device 4 recovers the heat of adsorption AH generated when hydrogen generated in the operation described below is adsorbed by the hydrogen compound member 2, and its configuration is not particularly limited. The heat recovery device 4 may be, for example, a heat storage medium capable of storing the heat of adsorption AH, or a heat exchanger for absorbing the heat of adsorption AH into a fluid (heat recovery fluid). FIG. 2 illustrates the conceptual configuration of the hydrogen production system 1 including the heat recovery device 4 in the form of a heat exchanger. The heat exchanger may be a heat exchanger for exchanging heat between a fluid 5 that may contain the heat of adsorption AH and the heat recovery fluid 6, such as a heat exchanger 4a for exchanging heat between the heat recovery fluid 6 and water 5a (water 7 supplied from the water supply member 3 that has not decomposed into hydrogen and oxygen or a compound containing oxygen atoms) and the heat recovery fluid 6, or a heat exchanger 4b for exchanging heat between the generated oxygen 5b and the heat recovery fluid 6, or may be a configuration including both of these heat exchangers 4a and 4b.

[0013] 3, an example of the heat recovery device 4 in the form of a heat exchanger may be a flow path 4c provided in the housing 8 accommodating the hydrogen compound member 2 so that the heat recovery fluid 6 can cool the interior of the housing 8. In this form, the temperature inside the housing 8 rises due to the heat of adsorption AH generated when hydrogen is adsorbed by the hydrogen compound member 2, but the heat of adsorption AH can be recovered into the heat recovery fluid 6 by heat exchange between the heat recovery fluid 6 flowing through the flow path 4c and the gas inside the housing 8. The flow path 4c may be, for example, a space defined between the outer circumferential surface of the housing 8 and a jacket provided at a distance from the outer circumferential surface, a narrow space provided inside the wall of the housing 8, or a pipe provided to pass through the inside of the housing 8. Furthermore, the flow path 4c may receive heat from the hydrogen compound member 2 by radiation, or the flow path 4c and the hydrogen compound member 2 may be connected by a heat-conducting member (not shown) made of a material with high thermal conductivity such as copper, and the flow path 4c (see FIG. 3) may receive heat from the hydrogen compound member 2 by thermal conduction. As described above, the heat recovery device 4 may receive heat from the hydrogen compound member 2 by any of various methods, such as a circulating heat recovery fluid, conduction, radiation, or a combination thereof.

[0014] <Operation of the hydrogen production system according to embodiment 1 of the present disclosure> Next, the operation of the hydrogen production system 1 according to embodiment 1 of the present disclosure will be described. In the following, the description will be given in the form of decomposing water into hydrogen and oxygen in the presence of the hydrogen compound member 2. As shown in FIG. 1 , when the water supply member 3 supplies water 7 to the hydrogen compound member 2 in a state where the temperature of the hydrogen compound member 2 is less than about 150°C, preferably between about 30°C and about 150°C, the water 7 decomposes into hydrogen and oxygen in the presence of the hydrogen compound member 2, and the hydrogen is adsorbed to the hydrogen compound member 2. The generated oxygen may be recovered and stored in a tank or the like, or may be transported to an oxygen consuming device (not shown) and consumed. The above-mentioned temperature of the hydrogen compound member 2 is determined by the above-mentioned chemical formula X ｍ H ｎ This is merely an example in which the element X is boron, and the above-mentioned temperature can be appropriately changed depending on the composition of the hydrogen compound member 2.

[0015] As described above, heat of adsorption is generated when hydrogen is adsorbed onto the hydrogen compound member 2, and the generated heat of adsorption AH is recovered by the heat recovery device 4. As shown in Fig. 2, when the heat recovery device 4 includes a heat exchanger 4a, the heat of adsorption AH is contained in water 5a that is not decomposed into hydrogen and oxygen out of the water 7 supplied to the hydrogen compound member 2. Therefore, the heat of adsorption AH contained in the water 5a is recovered into the heat recovery fluid 6 by heat exchange between the water 5a and the heat recovery fluid 6 in the heat exchanger 4a. When the heat recovery device 4 includes a heat exchanger 4b, the heat of adsorption AH is contained in the generated oxygen 5b. Therefore, the heat of adsorption AH contained in the oxygen 5b is recovered into the heat recovery fluid 6 by heat exchange between the oxygen 5b and the heat recovery fluid 6 in the heat exchanger 4b. The heat recovery fluid 6 from which the heat of adsorption AH has been recovered can be supplied to a heat utilization device (not shown) to utilize the heat of adsorption AH in the heat utilization device.

[0016] When the temperature of the hydrogen compound member 2 that has adsorbed hydrogen is set to a range of approximately 150°C to approximately 300°C, hydrogen can be released from the hydrogen compound member 2. Although FIGS. 1 to 3 do not depict a configuration in which a heating device for heating the hydrogen compound member 2 is provided, by providing such a heating device in the hydrogen production system 1, hydrogen can be released by heating the hydrogen compound member 2 after hydrogen has been adsorbed onto the hydrogen compound member 2. The released hydrogen can be stored in a tank or the like, or transported to a hydrogen consumption device (not shown) for consumption. Furthermore, when the hydrogen production system 1 does not include such a heating device, the hydrogen compound member 2 that has adsorbed hydrogen can be transported to a hydrogen consumption device or a tank at a temperature below approximately 150°C and heated to an appropriate temperature to release the hydrogen, which can then be consumed by the hydrogen consumption device or stored in a tank.

[0017] In this way, by recovering and utilizing the heat of adsorption AH generated when hydrogen produced by the decomposition of part of the water 7 into hydrogen and oxygen in the presence of the hydrogen compound material 2 is adsorbed by the hydrogen compound material 2, thermal efficiency is improved, thereby reducing the operating costs of the hydrogen production system 1.

[0018] (Embodiment 2) Next, a hydrogen production system according to embodiment 2 will be described. The hydrogen production system according to embodiment 2 is configured by adding a heat utilization device that utilizes the heat of adsorption to embodiment 1. In embodiment 2, the same components as those in embodiment 1 are designated by the same reference numerals, and detailed description thereof will be omitted.

[0019] <Configuration of Hydrogen Production System According to Embodiment 2 of the Present Disclosure> The hydrogen production system according to Embodiment 2 of the present disclosure includes several specific configurations, as described below. FIG. 4 illustrates a concept common to these specific configurations. In addition to the hydrogen compound member 2, the water supply member 3, and the heat recovery device 4, the hydrogen production system 1 further includes a heating device 9 that heats the hydrogen compound member 2 that has adsorbed hydrogen, and a heat utilization device 10 that utilizes the heat of adsorption AH recovered by the heat recovery device 4. The configuration of the heating device 9 is not particularly limited, and the heating device 9 may, for example, have a configuration in which a heating fluid 13 for heating the hydrogen compound member 2 flows through a flow path 4c (see FIG. 3 ) that is the heat recovery device 4. The heating device 9 may circulate a heat transport medium (e.g., pressurized water) between the heating device 9 and the hydrogen compound member 2, and transfer heat from the heating fluid 13 to the hydrogen compound member 2 via the heat transport medium. Furthermore, heat may be transferred by radiation from the flow path 4c (see FIG. 3) to the hydrogen compound member 2, or the flow path 4c and the hydrogen compound member 2 may be connected by a heat-conducting member (not shown) made of a material with high thermal conductivity such as copper, and heat may be transferred by thermal conduction from the flow path 4c (see FIG. 3) to the hydrogen compound member 2. As described above, the heating device 9 may transfer heat to the hydrogen compound member 2 by any of various methods, such as a circulating heat transport medium, conduction, radiation, or a combination thereof.

[0020] The configuration of the heat utilization device 10 is not particularly limited, and the heat utilization device 10 may be of any form as long as it is configured to include at least a heat absorption section 11 that absorbs the heat of adsorption AH recovered in the heat recovery fluid 6 and an exhaust heat recovery section 12 that recovers the exhaust heat WH discharged within the heat utilization device 10. Examples of such a heat utilization device 10 include a power generation system including a prime mover such as a gas engine or a boiler, a chemical plant that manufactures various chemical substances, a hot spring bathing facility, a heat storage system including a solar heater, etc.

[0021] The hydrogen production system 1 of the second embodiment is configured so that a heat recovery fluid 6a from which the heat of adsorption AH has been recovered (i.e., heated) in the heat recovery device 4 is supplied to the heat absorption section 11, and a heat recovery fluid 6b not containing the heat of adsorption AH is supplied to the heat recovery device 4. The heat recovery fluid 6b may be the heat recovery fluid 6a from which the heat of adsorption AH has been absorbed (i.e., cooled) in the heat absorption section 11. In this case, the heat recovery fluid 6 circulates between the heat recovery device 4 and the heat absorption section 11. A heating fluid 13 for heating the hydrogen compound member 2 is circulated between the exhaust heat recovery section 12 and the heating device 9. Specifically, the heating fluid 13a from which the exhaust heat WH has been recovered (i.e., heated) in the exhaust heat recovery section 12 is supplied to the heating device 9, and the heating fluid 13b after heating the hydrogen compound member 2 in the heating device 9 (i.e., cooled) returns to the exhaust heat recovery section 12.

[0022] <Operation of the hydrogen production system according to embodiment 2 of the present disclosure> Next, the operation of the hydrogen production system 1 according to embodiment 2 of the present disclosure will be described. The operation of supplying water 7 from the water supply member 3 to the hydrogen compound member 2 to cause hydrogen to be adsorbed by the hydrogen compound member 2 and recovering the heat of adsorption AH generated when hydrogen is adsorbed by the hydrogen compound member 2 using the heat recovery device 4 is the same as in embodiment 1. Below, the operation different from embodiment 1 will be described.

[0023] In the heat recovery unit 4, the heat of adsorption AH is recovered into the heat recovery fluid 6. The heat recovery fluid 6a from which the heat of adsorption AH has been recovered is supplied to the heat absorption section 11, where the heat of adsorption AH is absorbed from the heat recovery fluid 6a by the heat absorption section 11, and the heat of adsorption AH is utilized in the heat utilization unit 10. Meanwhile, the heat recovery fluid 6b that does not contain the heat of adsorption AH is supplied to the heat recovery unit 4, where the heat of adsorption AH is recovered from the heat recovery fluid 6b and becomes the heat recovery fluid 6a. This operation continues while hydrogen is being adsorbed into the hydrogen compound member 2.

[0024] Next, the operation of releasing hydrogen from the hydrogen compound member 2 that has adsorbed hydrogen will be described. The heating fluid 13a from which the exhaust heat WH has been recovered in the exhaust heat recovery section 12 is supplied to the heating device 9. In the heating device 9, the exhaust heat WH moves from the heating fluid 13a to the hydrogen compound member 2, heating the hydrogen compound member 2. When the temperature of the hydrogen compound member 2 reaches a range of approximately 150°C to approximately 300°C, hydrogen is released from the hydrogen compound member 2. The released hydrogen may be recovered and stored in a tank or the like, or transported to a hydrogen consumption device (not shown) for consumption. Note that, as will be described later, the heat utilization device 10 may also include a hydrogen consumption device and an oxygen consumption device. After heating the hydrogen compound member 2 in the heating device 9, the heating fluid 13b returns to the exhaust heat recovery section 12, where the exhaust heat WH is again recovered and becomes the heating fluid 13a. This operation continues while hydrogen is being released from the hydrogen compound member 2.

[0025] In this way, by utilizing the adsorption heat AH in the heat utilization device 10 and using the exhaust heat WH emitted by the heat utilization device 10 to heat the hydrogen compound material 2 to which hydrogen has been adsorbed, the thermal efficiency is further improved, and the operating costs of the hydrogen production system 1 can be further improved.

[0026] <Modification of the hydrogen production system according to the second embodiment of the present disclosure> The heating fluid 13 may be a fluid that undergoes a phase change when it exchanges heat with the hydrogen compound member 2 in the heating device 9. For example, steam can be used as such a heating fluid 13. When such a heating fluid 13 is used, the hydrogen compound member 2 can be heated by utilizing the latent heat (heat of condensation) generated when the heating fluid 13 changes phase (condenses). This allows heat exchange between the heating fluid 13 and the hydrogen compound member 2 with a small temperature difference between them, and therefore the hydrogen compound member 2 can be heated efficiently.

[0027] The heating fluid 13 may be a fluid that heats the hydrogen compound member 2 while causing an exothermic reaction inside the heating fluid 13 in the heating device 9. For example, a reaction gas (a mixed gas of hydrogen and carbon monoxide) supplied from a plant that produces hydrocarbons by the Fischer-Tropsch (FT) reaction can be used as this heating fluid 13. When this type of heating fluid 13 is used, the hydrogen compound member 2 can be heated using reaction heat from the exothermic reaction that occurs inside the heating fluid 13, and heat exchange between the heating fluid 13 and the hydrogen compound member 2 can be performed with a small temperature difference between them, so that the hydrogen compound member 2 can be heated efficiently.

[0028] The heat recovery fluid 6 may be a fluid that undergoes a phase change when the heat of adsorption AH is recovered from the hydrogen compound member 2 in the heat recovery device 4. Liquid ammonia, for example, can be used as this heat recovery fluid 6. When this type of heat recovery fluid 6 is used, the heat of adsorption AH can be recovered from the hydrogen compound member 2 by utilizing the latent heat (heat of vaporization) generated when the heat recovery fluid 6 changes phase (vaporizes). This allows heat exchange between the heat recovery fluid 6 and the hydrogen compound member 2 with a small temperature difference between them, and therefore the heat of adsorption AH can be efficiently recovered from the hydrogen compound member 2.

[0029] The heat recovery fluid 6 may be a fluid that recovers the heat of adsorption AH from the hydrogen compound member 2 while causing an endothermic reaction inside the heat recovery fluid 6 in the heat recovery device 4. As such a heat recovery fluid 6, for example, a reaction gas (a mixed gas of hydrogen and carbon dioxide) supplied from a plant that produces carbon monoxide by electrolysis or a reverse shift reaction of carbon dioxide can be used. When such a form of heat recovery fluid 6 is used, the heat of adsorption AH can be recovered from the hydrogen compound member 2 by utilizing the endothermic reaction that occurs inside the heat recovery fluid 6, and heat exchange between the heat recovery fluid 6 and the hydrogen compound member 2 can be performed with a small temperature difference between them, so that the heat of adsorption AH can be efficiently recovered from the hydrogen compound member 2.

[0030] 5 , the heat utilization device 10 is a gas turbine combined cycle power plant (GTCC) 10 a. The GTCC 10 a includes a gas turbine 100, a steam turbine system 200, and a steam generator 300 for generating steam used in the steam turbine system 200.

[0031] The gas turbine 100 includes a compressor 101 that compresses air, a combustor 102 that combusts fuel 120 using compressed air 131 generated by the compressor 101, and a turbine 103 that is driven by combustion gas 121 generated by the combustor 102. The steam turbine system 200 includes a high-pressure steam turbine 201, an intermediate-pressure steam turbine 202, a low-pressure steam turbine 203, and a condenser 204 that cools steam 210 discharged from the low-pressure steam turbine 203 and converts it back into water. The compressor 101, the turbine 103, the generator 104, the high-pressure steam turbine 201, the intermediate-pressure steam turbine 202, and the low-pressure steam turbine 203 are arranged on the same axis, and their rotors are fixed to the same shaft 106 so that they rotate integrally. The steam generating device 300 includes a heat recovery boiler 301 to which exhaust gas 100a from the gas turbine 100 is supplied. The heat recovery boiler 301 includes a plurality of heat exchangers 303 provided in an exhaust gas flow path 302 through which exhaust gas from the gas turbine 100 flows.

[0032] The oxygen 5b produced when hydrogen is adsorbed into the hydrogen compound material 2 may be mixed with the intake air 130 drawn into the compressor 101, or may be supplied to the compressor 101 instead of the intake air 130. Also, the hydrogen 2a released from the hydrogen compound material 2 may be mixed with the fuel 120 supplied to the combustor 102. In this case, the gas turbine 100 consumes the oxygen 5b and hydrogen 2a, and therefore the gas turbine 100 constitutes an oxygen consumption device and a hydrogen consumption device. Therefore, in this specific example 1, the GTCC 10a, which is the heat utilization device 10, is configured to include an oxygen consumption device and a hydrogen consumption device.

[0033] The generator 104 is provided with a generator cooler 105 for cooling the generator 104. A generator cooling medium such as hydrogen, water, or air is sealed inside the generator 104, and the generator cooling medium circulates between the high-temperature portion of the generator 104 and the generator cooler 105 provided inside the generator 104. The generator cooling medium increases in temperature by cooling the high-temperature portion of the generator 104, and is then cooled by the generator cooler 105. Lubricating oil is supplied to the bearing 107 of the shaft 106 to lubricate and cool the bearing 107. The lubricating oil circulates between the bearing 107 and the lubricating oil cooler 108, and the lubricating oil, which has increased in temperature by recovering frictional heat in the bearing 107, is cooled by the lubricating oil cooler 108. The generator cooler 105 is configured such that feedwater supplied from the condenser 204 flows in as a cooling medium L to cool the generator cooling medium circulating within the generator 104, then flows into the lubricant oil cooler 108 to further cool the lubricant, and then flows out of the lubricant oil cooler 108 as a cooling medium M. The cooling medium M flows into the heat recovery device 4 as a heat recovery fluid 6b that does not contain the heat of adsorption AH, and in the heat recovery device 4, the heat of adsorption AH is recovered from the hydrogen compound member 2 to become a heat recovery fluid 6a.

[0034] The heat recovery fluid 6a from which the heat of adsorption AH has been recovered is sent to the GTCC 10a, where it flows into a cooling air cooler 109 that cools air extracted from the compressor 101 as cooling medium N to prepare cooling air for cooling the low-pressure stage of the turbine 103. In the cooling air cooler 109, the cooling medium N is heated by heat exchange with the air extracted from the compressor 101 and flows out of the cooling air cooler 109 as cooling medium O. The cooling medium O flows into a cooling air cooler 110 that cools air extracted from the compressor 101 to prepare cooling air for cooling the combustor 102. In the cooling air cooler 110, the cooling medium O is heated by heat exchange with the air extracted from the compressor 101 and flows out of the cooling air cooler 110 as cooling medium P. The cooling medium P is further heated in one heat exchanger 303a of the plurality of heat exchangers 303 in the heat recovery boiler 301, and flows out of the heat exchanger 303a as heating media Q and S.

[0035] The heating media S and Q containing the heat of adsorption AH flow into a heat exchanger 111 for heating the intake air 130 drawn into the compressor 101 and a heat exchanger 112 for heating the fuel 120 supplied to the combustor 102, respectively, and exchange heat with the intake air 130 and the fuel 120, thereby heating the intake air 130 and the fuel 120. In this way, the heat of adsorption AH is used as part of the heat source for heating the intake air 130 and the fuel 120, and the heat exchangers 111 and 112 are specific examples of the heat absorption unit 11 that absorbs the heat of adsorption AH.

[0036] As described above, the cooling medium L, i.e., the feed water supplied from the condenser 204, flows in the order of L, M, N, O, and P, that is, through the generator cooler 105, lubricant oil cooler 108, heat recovery device 4, cooling air cooler 109, cooling air cooler 110, and heat exchanger 303a (low-pressure economizer) in the exhaust heat recovery boiler 301. The cooling medium L, i.e., the feed water supplied from the condenser 204, flows in the order of the generator cooler 105 and lubricant oil cooler 108, exchanging heat with the cooled media (generator cooling medium, lubricant oil) of each cooler to recover exhaust heat, and then flows into the heat recovery device 4 to recover the heat of adsorption AH through heat exchange between the hydrogen compound member 2 and the cooling medium M. The cooling medium L then flows through the cooling air cooler 109, the cooling air cooler 110, and the heat exchanger 303a in that order, exchanging heat with the cooled medium of each cooler (the two cooling airs and the exhaust gas) to recover the exhaust heat. Here, it is preferable that the temperature of the cooled medium (generator cooling medium, lubricating oil) flowing into the coolers (generator cooler 105, lubricating oil cooler 108) installed upstream of the heat recovery device 4 in terms of the flow of the cooling medium L is lower than the temperature of the hydrogen compound member 2 when hydrogen is adsorbed, because this allows for effective recovery of low-temperature exhaust heat in areas where the cooling medium temperature is low and high-temperature exhaust heat in areas where the cooling medium temperature is high. Furthermore, it is preferable that the temperature of the cooled medium (cooled air and exhaust gas at two locations) flowing into the coolers (cooled air cooler 109, cooled air cooler 110, heat exchanger 303a) installed downstream of the heat recovery device 4 in terms of the flow of the cooling medium L is higher than the temperature of the hydrogen compound member 2 when adsorbing hydrogen, since this allows for effective recovery of low-temperature exhaust heat in locations where the cooling medium temperature is low and high-temperature exhaust heat in locations where the cooling medium temperature is high. Note that the above coolers and cooled mediums are all examples and are not limited to those exemplified here. Furthermore, a cooler may be provided either upstream or downstream of the heat recovery device 4. Furthermore, the number of these coolers and cooled mediums is arbitrary.

[0037] On the other hand, the heating fluid 13b (here, pressurized water) after heating the hydrogen compound material 2 in the heating device 9 is heated by heat exchange with a medium containing exhaust heat WH generated in the GTCC 10a in one heat exchanger 303b of the multiple heat exchangers 303 in the heat recovery boiler 301 and in several heat exchangers (hereinafter referred to as "heat exchanger 303b, etc.") provided upstream and downstream of the heat exchanger 303b, and returns to the heating device 9 as heating fluid 13a from which the exhaust heat WH has been recovered, and again heats the hydrogen compound material 2. In the heat exchanger 303b, etc., the heating fluid 13b recovers the exhaust heat WH generated in the GTCC 10a, and the heat exchanger 303b, etc. are specific examples of the exhaust heat recovery section 12 described above. Furthermore, if the heating fluid 13a (pressurized water) heated in the heat exchanger 303b or the like evaporates and becomes steam, the heating fluid 13a corresponds to a fluid that undergoes a phase change (condensation) when exchanging heat with the hydrogen compound material 2 in the heating device 9.

[0038] As described above, the cooling medium N, which has flowed into the heat recovery device 4 and recovered the heat of adsorption AH through heat exchange between the hydrogen compound member 2 and the cooling medium M, further flows through the cooling air cooler 109, the cooling air cooler 110, and the heat exchanger 303a in that order, recovering exhaust heat while still containing the heat of adsorption AH. In a configuration in which a portion of the cooling medium flowing out of the heat exchanger 303a flows into the drum 304 that is connected to the heat exchanger 303c (low-pressure evaporator) in the exhaust heat recovery boiler 301, the cooling medium flowing from the drum 304 into the heat exchanger 303c (low-pressure evaporator) while still containing the heat of adsorption AH absorbs the heat recovered from the exhaust gas 100a and becomes steam, and then flows from the drum 304 into the heat exchanger 303d (low-pressure superheater) in the exhaust heat recovery boiler 301 and subsequently into the low-pressure steam turbine 203. In the low-pressure steam turbine 203, the steam containing the heat of adsorption AH expands and the heat containing the heat of adsorption AH is converted into power. Therefore, the low-pressure steam turbine 203 can also constitute the heat absorption unit 11.

[0039] 6 , the heat utilization device 10 is a power generation system 10b including a gas engine 400 fueled by ammonia and a generator 401 driven by the gas engine 400. The power generation system 10b includes a preheater 402 that preheats liquid ammonia, a vaporizer 403 that vaporizes the preheated ammonia, a cooler 404 that prepares cooling water for cooling the gas engine 400, and a waste heat recovery heat exchanger 405 that recovers waste heat from exhaust gas 460 and the like discharged from the gas engine 400. The gas engine 400 includes a cooling mechanism 406 (for example, a cooling water flow path provided in a casing of the gas engine 400) that cools the gas engine 400 with the cooling water prepared by the cooler 404.

[0040] In the preheater 402, heat exchange occurs between the cooling water 440, which has been used to cool the gas engine 400 in the cooling mechanism 406, and the liquid ammonia 430, which is the fuel for the gas engine 400, thereby preheating the liquid ammonia 430. The preheated liquid ammonia 431 is further heated in the vaporizer 403 to become ammonia gas 432, which is supplied to the gas engine 400. The ammonia gas 432 may be configured to be mixed with hydrogen 420 released from the hydrogen compound member 2. In this case, the gas engine 400 consumes the hydrogen 420, and therefore the gas engine 400 constitutes a hydrogen consumption device.

[0041] In the vaporizer 403, the saturated steam 450 may be heat exchanged with the preheated liquid ammonia 431 to heat and vaporize the preheated liquid ammonia. The saturated steam 450 may be generated, for example, in the evaporator 408 by utilizing the heat of the exhaust gas 460 discharged from the gas engine 400. Furthermore, in the vaporizer 403, the preheated liquid ammonia 431 may be heated by heat exchange between the heat recovery fluid 6a, from which the heat of adsorption AH has been recovered in the heat recovery device 4, and the preheated liquid ammonia 431. By adopting at least the latter form of heat exchange, the heat of adsorption AH contained in the heat recovery fluid 6a is absorbed by the preheated liquid ammonia 431 in the vaporizer 403, and therefore the vaporizer 403 is a specific example of the heat absorption unit 11 described above.

[0042] The heating fluid 13b after heating the hydrogen compound material 2 in the heating device 9 is heated in the exhaust heat recovery heat exchanger 405 by heat exchange with the exhaust gas 460 from the gas engine 400, which contains the exhaust heat WH generated by the gas engine 400, and is returned to the heating device 9 as the heating fluid 13a containing the exhaust heat WH, thereby again heating the hydrogen compound material 2. In the exhaust heat recovery heat exchanger 405, the heating fluid 13b recovers the exhaust heat WH generated by the gas engine 400, so the exhaust heat recovery heat exchanger 405 is a specific example of the above-mentioned exhaust heat recovery unit 12. In addition, a portion of the cooling water after cooling the gas engine 400 in the cooling mechanism 406 is depressurized by a pressure reducing valve 407, and the resulting steam 412 is flashed in a flash tank 410. The resulting steam 412 is pressurized by a compressor 411 and sent to the exhaust heat recovery heat exchanger 405. A portion of the heating fluid 13b is heated using the heat generated when the steam 412 condenses in the exhaust heat recovery heat exchanger 405. The vapor 412 is pressurized by the compressor 411 and condenses at a high temperature, so that a heating fluid 13 b having a temperature sufficient to heat the hydrogen compound member 2 can be obtained.

[0043] The vaporizer 403 may be configured in the form of a pipe through which preheated liquid ammonia 431 flows, and the heat recovery device 4 may be configured so that the preheated liquid ammonia 431 flowing through the vaporizer 403 having such a pipe shape exchanges heat with the hydrogen compound member 2. In such a configuration, the preheated liquid ammonia 431 flowing through the vaporizer 403 becomes the heat recovery fluid 6, and corresponds to the fluid that undergoes a phase change (vaporization) when the heat of adsorption AH is recovered from the hydrogen compound member 2 in the heat recovery device 4.

[0044] 7 , the heat utilization device 10 is a plant 10c that produces hydrocarbons by the FT reaction using carbon dioxide and hydrogen as raw materials. The plant 10c includes a carbon dioxide capture device 500 that captures carbon dioxide from a carbon dioxide-containing gas 520 (for example, the atmosphere or an exhaust gas emitted from a combustion device, etc.), a carbon monoxide production device 501 that produces carbon monoxide from the carbon dioxide 521 captured in the carbon dioxide capture device 500, an FT reactor 502 that produces crude hydrocarbons 524 by the FT reaction using carbon monoxide 522 and hydrogen 523 produced in the carbon monoxide production device 501 as raw materials, and a purification device 503 that refines the crude hydrocarbons 524 produced in the FT reactor 502 into refined hydrocarbons 525.

[0045] The configuration of the carbon dioxide capture device 500 is not particularly limited, and may be, for example, a device that captures carbon dioxide using an amine method. The carbon dioxide capture device 500 is provided with a heater 510 for heating the absorption liquid. By heating the absorption liquid that has absorbed carbon dioxide with the heater 510, carbon dioxide 521 is separated from the absorption liquid, making the absorption liquid available for reuse in absorbing carbon dioxide and allowing the separated carbon dioxide 521 to be utilized. The heater 510 may be configured to supply the heat recovery fluid 6a from which the heat of adsorption AH has been recovered in the heat recovery device 4. In the heater 510, the heat of adsorption AH is absorbed by the absorption liquid from the heat recovery fluid 6a containing the heat of adsorption AH, and the heat of adsorption AH is used to capture carbon dioxide. In this way, the heat of adsorption AH contained in the heat recovery fluid 6a is absorbed by the absorption liquid in the carbon dioxide capture device 500 in the heater 510, and therefore the heater 510 is a specific example of the heat absorption unit 11 described above.

[0046] The configuration of the carbon monoxide production apparatus 501 is not particularly limited, and may be, for example, an apparatus that produces carbon monoxide by electrolysis or a reverse shift reaction of carbon dioxide recovered in the carbon dioxide recovery apparatus 500. Because the electrolysis and reverse shift reaction of carbon dioxide are endothermic reactions, the carbon monoxide production apparatus 501 is provided with a heater 511. The heater 511 may be configured to be supplied with a heat recovery fluid 6a from which the heat of adsorption AH has been recovered in the heat recovery unit 4. In the heater 511 configured in this way, as in the heater 510, the heat of adsorption AH contained in the heat recovery fluid 6a is absorbed by carbon dioxide, which is the raw material for producing carbon monoxide, and therefore the heater 511 is a specific example of the heat absorption unit 11 described above.

[0047] In addition, when the carbon monoxide production apparatus 501 is an apparatus that produces carbon monoxide by a reverse shift reaction, the carbon monoxide production apparatus 501 configured in a piping shape without being provided with a heater 511 can also be used as the heat recovery apparatus 4. In such a configuration, the mixed gas of hydrogen and carbon dioxide flowing through the carbon monoxide production apparatus 501 configured in a piping shape becomes the heat recovery fluid 6, which corresponds to the fluid that recovers the heat of adsorption AH from the hydrogen compound member 2 while causing an endothermic reaction inside the heat recovery fluid 6 in the heat recovery apparatus 4.

[0048] In the FT reactor 502, hydrocarbons are produced by the FT reaction using carbon monoxide 522 produced in the carbon monoxide production apparatus 501 and hydrogen 523 as raw materials. Hydrogen released from the hydrogen compound component 2 may be used as the raw material hydrogen 523. In this case, the FT reactor 502 consumes the hydrogen 523 and therefore constitutes a hydrogen consumption device. Because the FT reaction is an exothermic reaction, the FT reactor 502 is provided with a cooler 512. The cooler 512 may be configured to be supplied with the heating fluid 13b obtained after the hydrogen compound component 2 is heated in the heating device 9. In the cooler 512 configured in this manner, the heating fluid 13b recovers the reaction heat (exhaust heat WH) generated by the FT reaction and becomes the heating fluid 13a, which returns to the heating device 9 to heat the hydrogen compound component 2 again. In the cooler 512, the heating fluid 13b recovers the reaction heat generated by the FT reaction, and therefore the cooler 512 is a specific example of the exhaust heat recovery unit 12 described above.

[0049] The FT reactor 502 configured in a piping shape without providing the cooler 512 can also be used as the heating device 9. In such a configuration, the mixed gas of hydrogen and carbon monoxide flowing through the FT reactor 502 configured in a piping shape becomes the heating fluid 13, which corresponds to the fluid that heats the hydrogen compound member 2 while causing an exothermic reaction inside the heating fluid 13 in the heating device 9.

[0050] The configuration of the purification device 503 is not particularly limited, and may be, for example, a distillation column. The purification device 503, which is a distillation column, is provided with a reboiler 513. The reboiler 513 may be configured so that a heat recovery fluid 6a obtained by recovering the heat of adsorption AH in the heat recovery device 4 is supplied to the purification device 503. In the purification device 503 equipped with such a reboiler 513, the heat of adsorption AH contained in the heat recovery fluid 6a is absorbed by the crude hydrocarbons 524, and the crude hydrocarbons 524 are refined. Therefore, the reboiler 513 is a specific example of the heat absorption section 11 described above.

[0051] 8, the heat-utilization device 10 is a plant 10d that produces ammonia. The plant 10d includes a nitrogen separation device 600 that separates nitrogen from the atmosphere 610, and a reactor 601 that synthesizes ammonia 613 by the Haber-Bosch process using nitrogen 611 and hydrogen 612 obtained in the nitrogen separation device 600 as raw materials.

[0052] The configuration of the nitrogen separation apparatus 600 is not particularly limited, and may be, for example, a pressure swing adsorption (PSA) type apparatus or a temperature swing adsorption (TSA) type apparatus. When the nitrogen separation apparatus 600 is a TSA type apparatus, nitrogen is generated from the adsorbent by heating the adsorbent that selectively adsorbs nitrogen. Therefore, the nitrogen separation apparatus 600 is provided with a heater 602. The heater 602 may be configured to be supplied with a heat recovery fluid 6a from which the heat of adsorption AH has been recovered in the heat recovery unit 4. In the heater 602, the heat of adsorption AH is absorbed by the absorption liquid from the heat recovery fluid 6a containing the heat of adsorption AH, and the heat of adsorption AH is used to heat the adsorbent. In this way, the heat of adsorption AH contained in the heat recovery fluid 6a is absorbed by the adsorbent in the heater 602, and therefore the heater 602 is a specific example of the heat absorption unit 11 described above.

[0053] In the reactor 601, ammonia 613 is synthesized by the Haber-Bosch process using nitrogen 611 and hydrogen 612 obtained in the nitrogen separation device 600 as raw materials. Hydrogen released from the hydrogen compound material 2 may be used as the raw material hydrogen 612. In this case, the reactor 601 consumes the hydrogen 612, and therefore constitutes a hydrogen consumption device. Because the reaction (ammonia synthesis reaction) for synthesizing ammonia 613 from the nitrogen 611 and hydrogen 612 is an exothermic reaction, the reactor 601 is provided with a cooler 603. The cooler 603 may be configured so that the heating fluid 13b obtained after heating the hydrogen compound material 2 in the heating device 9 is supplied to the cooler 603. In the cooler 603 configured in this way, the reaction heat (exhaust heat WH) generated by the ammonia synthesis reaction is recovered by the heating fluid 13b and becomes the heating fluid 13a, which returns to the heating device 9 and heats the hydrogen compound material 2 again. In the cooler 603, the reaction heat generated by the ammonia synthesis reaction is recovered by the heating fluid 13b, and therefore the cooler 603 is a specific example of the exhaust heat recovery unit 12 described above.

[0054] The reactor 601 configured in a piping shape without providing the cooler 603 can also be used as the heating device 9. In such a configuration, the mixed gas of hydrogen and nitrogen flowing through the reactor 601 configured in a piping shape becomes the heating fluid 13, which corresponds to the fluid that heats the hydrogen compound member 2 while causing an exothermic reaction inside the heating fluid 13 in the heating device 9.

[0055] (Embodiment 3) Next, a hydrogen production system according to embodiment 3 will be described. The hydrogen production system according to embodiment 3 is different from embodiment 2 in that the configuration of the heat absorption unit 11 is changed. In embodiment 3, the same components as those in embodiment 2 are denoted by the same reference numerals, and detailed description thereof will be omitted.

[0056] <Configuration of hydrogen production system according to embodiment 3 of the present disclosure> In embodiment 2, the heat of adsorption AH is used in the heat utilization device 10, and the heating fluid 13b after heating the hydrogen compound member 2 in the heating device 9 recovers the exhaust heat WH in the heat utilization device 10 and then heats the hydrogen compound member 2 again. However, while the temperature of the heat recovery fluid 6a containing the heat of adsorption AH is 120°C or lower, the temperature of the heating fluid 13b after heating the hydrogen compound member 2 is 160°C or higher. Therefore, the heat still contained in the heating fluid 13b can also be utilized in the heat utilization device 10.

[0057] 9, in the hydrogen production system 1 according to the third embodiment of the present disclosure, the heat absorption unit 11 of the heat utilization device 10 includes two heat recovery units, namely, a first heat absorption unit 11b and a second heat absorption unit 11c. In the heat utilization device 10, the first heat absorption unit 11b and the second heat absorption unit 11c are different. The heat recovery fluid 6 from which the heat of adsorption AH has been recovered in the heat recovery device 4 is supplied to the first heat absorption unit 11b, and the heat of adsorption AH is absorbed by the first heat absorption unit 11b. In addition, the heating fluid 13b after heating the hydrogen compound material 2 in the heating device 9 is supplied to the second heat absorption unit 11c, and the heat still contained in the heating fluid 13b after heating the hydrogen compound material 2 is absorbed by the second heat absorption unit 11c. The other configurations are the same as those of the second embodiment.

[0058] <Operation of the hydrogen production system according to embodiment 3 of the present disclosure> Embodiment 3 differs from embodiment 2 only in the operation in which the heating fluid 13b after heating the hydrogen compound member 2 becomes the heating fluid 13a from which the exhaust heat WH has been recovered in the heat utilization device 10, and the other operations are the same as embodiment 2. Therefore, only the operations that differ from the operation of embodiment 2 will be described. After heating the hydrogen compound member 2 in the heating device 9, the heating fluid 13b absorbs the heat contained in the heating fluid 13b in the second heat absorption section 11c, and the absorbed heat is utilized in the heat utilization device 10. The heating fluid 13b flowing out from the second heat absorption section 11c recovers the exhaust heat WH in the exhaust heat recovery section 12 and becomes the heating fluid 13a.

[0059] More specifically, as shown in specific example 1 of FIG. 5 , in a GTCC 10 a, a gas turbine 100 expands a turbine 103 to extract work, and then supplies exhaust gas 100 a containing exhaust heat to a heat recovery boiler 301, which is a steam generating device 300. The configuration of the heat exchange elements installed in the heat recovery boiler 301 can be selected in various ways and is not limited to this embodiment, but in this embodiment, the heat exchange elements are installed in the exhaust gas flow path 302 in the heat recovery boiler 301, from upstream to downstream of the flow of the exhaust gas 100a, in the following order: second reheater (RH2), second high-pressure superheater (SH2-HP), first reheater (RH1), first high-pressure superheater (SH1-HP), high-pressure evaporator (EVA-HP), second high-pressure economizer (ECO-HP2), heat exchanger 303b, first high-pressure economizer (ECO-HP1), low-pressure superheater (SH-LP), low-pressure evaporator (EVA-LP), and low-pressure economizer (ECO-LP). The exhaust gas 100a flows through the exhaust gas flow path 302 in the heat recovery boiler 301 while heating steam and feed water (pressurized water) in each heat exchange element in the above order. The heat exchanger 303b in the heat recovery boiler 301 exchanges heat between the exhaust gas 100a and a heating fluid 13b (pressurized water) to heat the pressurized water, and the pressurized water is supplied to the heating device 9 as the heating fluid 13a from which the exhaust heat WH has been recovered, thereby heating the hydrogen compound member 2. The exhaust gas 100a, whose temperature has been reduced by heating the hydrogen compound member 2 in the above manner, is sent to the SH-LP, EVA-LP, and ECO-LP provided downstream of the heat exchanger 303b in the exhaust gas flow path in the heat recovery boiler 301, where it exchanges heat with the feed water of the heat recovery boiler 301, evaporating the feed water and generating low-pressure steam (901a, 901b, 901c). The generated low-pressure steam (901c) is sent to the low-pressure steam turbine 203 and expanded to generate power. Meanwhile, the heat of adsorption AH of the heat recovery fluid 6a recovered in the heat recovery device 4 is absorbed in the heat exchangers 111 and 112 (corresponding to the first heat absorption section 11b in the third embodiment) as described in the specific example 1 of the second embodiment.In the third embodiment, the heat exchangers 111 and 112, which are the first heat absorption unit 11b, and the low-pressure economizer (ECO-LP), which is the second heat absorption unit 11c, are connected by a line through which the cooling media flow in the order of N, N, O, and P. The feedwater (cooling media N, O, and P) that has absorbed the heat of adsorption AH in the heat exchangers 111 and 112 is further heat-exchanged with the exhaust gas 100a in the low-pressure economizer (ECO-LP), thereby heating the feedwater (cooling media N, O, and P) and recovering the exhaust heat contained in the exhaust gas 100a. Here, the exhaust gas 100a has a higher temperature than the hydrogen compound member 2 when hydrogen is released from the hydrogen compound member 2 that has adsorbed hydrogen, and the feedwater (cooling media M) has a lower temperature than the hydrogen compound member 2 when the generated hydrogen is adsorbed by the hydrogen compound member 2. The heat exchanger 303b can also constitute the heating device 9. In this case, the gas turbine 100 serves as an exhaust heat recovery unit, the exhaust gas 100a serves as a heating fluid, and the SH-LP, EVA-LP, and ECO-LP serve as a second heat absorption unit.

[0060] In this way, by absorbing the heat of adsorption AH in the first heat absorption unit 11b and absorbing the heat still contained in the heating fluid after heating the hydrogen compound member 2 in the heating device 9 in the second heat absorption unit 11c, thermal efficiency is further improved, thereby further reducing the operating cost of the hydrogen production system 1. In addition, by using the heat of the exhaust gas 100a, which has a temperature high enough to heat the hydrogen compound member 2, to heat the hydrogen compound member 2 and recovering the heat of the exhaust gas 100a after using it to heat the hydrogen compound member 2 to the lower temperature feedwater (cooling media N, O, P), hydrogen can be produced using the heat of the high temperature exhaust gas 100a, which can be used more effectively than directly heating the low temperature feedwater (cooling media N, O, P). In this way, by recovering the heat of the high temperature exhaust gas 100a and the heat of adsorption AH in high temperature locations and low temperature locations according to their respective temperatures, the efficiency of heat utilization can be improved. Furthermore, in the GTCC 10a, the feedwater has a high flow rate and requires a large amount of heat for heating. However, even in such a case where a large amount of heat is required to heat the cooling medium, a sufficient amount of heat can be supplied by using both the heat of adsorption AH and the heat of the exhaust gas 100a after being used to heat the hydrogen compound member 2.

[0061] (Embodiment 4) Next, a hydrogen production system according to embodiment 4 will be described. The hydrogen production system according to embodiment 4 is different from embodiment 1 in that the recovery mode of the heat of adsorption AH is changed. In embodiment 4, the same components as those in embodiment 1 are denoted by the same reference numerals, and detailed description thereof will be omitted.

[0062] 10 , the hydrogen production system 1 according to the fourth embodiment of the present disclosure further includes, in addition to the hydrogen compound member 2, the water supply member 3, and the heat recovery device 4, a heat utilization device 10 that utilizes the heat of adsorption AH recovered by the heat recovery device 4, and a first heat exchanger 20 that exchanges heat between a heat recovery fluid 6b before recovering the heat of adsorption AH in the heat recovery device 4 and a heating fluid 13a that recovers the waste heat WH discharged within the heat utilization device 10. Similar to the heat utilization device 10 according to the second embodiment, the heat utilization device 10 according to the fourth embodiment includes a heat absorption section 11 that absorbs the heat of adsorption AH recovered in the heat recovery fluid 6, and an exhaust heat recovery section 12 that recovers the waste heat WH discharged within the heat utilization device 10. The temperature of the heating fluid 13a from which the waste heat WH has been recovered in the exhaust heat recovery section 12 is lower than the temperature of the hydrogen compound member 2 during the recovery of the heat of adsorption AH by the heat recovery fluid 6b, and higher than the temperature of the heat recovery fluid 6b. The other configurations are the same as those of the first embodiment.

[0063] <Operation of the hydrogen production system according to the fourth embodiment of the present disclosure> Next, an operation of adsorbing hydrogen to the hydrogen compound member 2 in the hydrogen production system 1 according to the fourth embodiment of the present disclosure will be described. First, the heat recovery fluid 6b and the heating fluid 13a exchange heat in the first heat exchanger 20, causing the heat recovery fluid 6b to absorb the waste heat WH contained in the heating fluid 13a. The heat recovery fluid 6b further recovers the heat of adsorption AH in the heat recovery device 4 and flows out of the heat recovery device 4 as the heat recovery fluid 6a. In the heat absorption section 11, the waste heat WH and the heat of adsorption AH are absorbed from the heat recovery fluid 6a.

[0064] In the configuration of the fourth embodiment, the temperature of the heat recovery fluid 6 supplied to the heat utilization device 10 is higher than when the heat recovery fluid 6 exchanges heat with either the hydrogen compound material 2 or the heating fluid 13a, thereby improving the heat utilization efficiency of the heat utilization device 10. Even when the temperature of the exhaust heat WH is relatively low, by recovering the heat of the hydrogen compound material 2, which has a higher temperature than the exhaust heat WH, into the heat recovery fluid 6b recovered from the exhaust heat WH in the first heat exchanger 20, i.e., the heat of adsorption AH, the heat including the exhaust heat WH can be effectively utilized as relatively high-temperature heat.

[0065] In this fourth embodiment, in which the temperature of the hydrogen compound material 2 is higher than that of the heating fluid 13a, in order to obtain the above-described effects, it is essential that the heat recovery fluid 6 exchanges heat with the heating fluid 13a and then recovers the heat of adsorption AH from the hydrogen compound material 2. If this order is reversed, as shown in FIG. ０ The position P from which the heat recovery fluid 6 flows out of the heat recovery device 4 １ During this period, the heat recovery fluid 6 recovers the heat of adsorption AH from the hydrogen compound member 2, and the temperature of the heat recovery fluid 6 is T ０ °C to T １ Then, T １ When the heat recovery fluid 6 at ° C. exchanges heat with the heating fluid 13a at a temperature lower than that of the hydrogen compound member 2 in the first heat exchanger 20, the position P ２ The temperatures of both fluids are the same at T ３ °C, so position P ２ and the position P at which the heat recovery fluid 6 flows out of the first heat exchanger 20 ３ During this time, the temperature of the heat recovery fluid 6 is not increased.

[0066] In contrast, when the heat recovery fluid 6 is heated in the order of the configuration of FIG. 10, as shown in FIG. 12, the position P ０ The position P ′ from which the heat recovery fluid 6 flows out of the first heat exchanger 20 １ During this time, the temperature of the heat recovery fluid 6 is increased to the temperature T ０ °C to T ４ Then, T４ ° C. The heat recovery fluid 6 flows into the heat recovery device 4, and the heat of adsorption AH is recovered from the hydrogen compound member 2, which has a temperature higher than that of the heating fluid 13a. ２ The temperature of the heat recovery fluid 6 continues to rise until the position P ０ ' to position P ２ Since the heat recovery fluid 6 can continue to absorb the heat of adsorption AH and the exhaust heat WH until the time t1, the amount of heat absorbed by the heat recovery fluid 6 is greater than when the heat recovery fluid 6 recovers the heat of adsorption AH from the hydrogen compound material 2 and then exchanges heat with the heating fluid 13a.

[0067] (Embodiment 5) Next, a hydrogen production system according to embodiment 5 will be described. The hydrogen production system according to embodiment 5 is different from embodiment 4 in that the recovery mode of the heat of adsorption AH is changed. In embodiment 5, the same components as those in embodiment 4 are denoted by the same reference numerals, and detailed description thereof will be omitted.

[0068] 13 , a hydrogen production system 1 according to a fifth embodiment of the present disclosure includes, instead of the first heat exchanger 20 (see FIG. 10 ) in the fourth embodiment, a second heat exchanger 30 that exchanges heat between a heat recovery fluid 6a obtained after recovering the heat of adsorption AH in the heat recovery device 4 and a heating fluid 13a containing exhaust heat WH. The temperature of the heating fluid 13a before heat exchange with the heat recovery fluid 6a is higher than the temperature of the hydrogen compound member 2 that is recovering the heat of adsorption AH using the heat recovery fluid 6b. The other configurations are the same as those in the fourth embodiment.

[0069] <Operation of the hydrogen production system according to the fifth embodiment of the present disclosure> Next, an operation of adsorbing hydrogen to the hydrogen compound member 2 in the hydrogen production system 1 according to the fifth embodiment of the present disclosure will be described. First, in the heat recovery unit 4, the heat recovery fluid 6b recovers the heat of adsorption AH from the hydrogen compound member 2 and flows out of the heat recovery unit 4 as the heat recovery fluid 6a. The heat recovery fluid 6a from which the heat of adsorption AH has been recovered further exchanges heat with the heating fluid 13a in the second heat exchanger 30, thereby absorbing the waste heat WH contained in the heating fluid 13a. In the heat absorption unit 11, the waste heat WH and the heat of adsorption AH are absorbed from the heat recovery fluid 6a.

[0070] In the configuration of the fifth embodiment, the temperature of the heat recovery fluid 6 supplied to the heat utilization device 10 is higher than when the heat recovery fluid 6 exchanges heat with either the hydrogen compound material 2 or the heating fluid 13a, thereby improving the heat utilization efficiency of the heat utilization device 10. The heat of the hydrogen compound material 2, i.e., the heat recovery fluid 6a after recovering the heat of adsorption AH, recovers the relatively high-temperature exhaust heat WH, and the heat of the hydrogen compound material 2 can also be effectively utilized as relatively high-temperature heat.

[0071] In this fifth embodiment, in which the temperature of the hydrogen compound member 2 is lower than that of the heating fluid 13a, in order to obtain the above-described effects, the heat recovery fluid 6 must be subjected to heat exchange with the heating fluid 13a after recovering the heat of adsorption AH from the hydrogen compound member 2. If this order is reversed, as shown in FIG. 14, the position P at which the heat recovery fluid 6 flows into the second heat exchanger 30 will be ０ The position P from which the heat recovery fluid 6 flows out of the second heat exchanger 30 １ During this time, the heat recovery fluid 6 and the heating fluid 13a exchange heat, and the temperature of the heat recovery fluid 6 is T ０ °C to T １ Then, T １ When the heat recovery fluid 6 at ° C. recovers the heat of adsorption AH from the hydrogen compound member 2 at a temperature lower than that of the heating fluid 13a in the heat recovery device 4, ２ The temperatures of the heat recovery fluid 6 and the hydrogen compound member 2 are the same at T ３ °C, so position P ２ and the position P at which the heat recovery fluid 6 flows out of the heat recovery device 4. ３ During this time, the temperature of the heat recovery fluid 6 is not increased.

[0072] On the other hand, when the heat recovery fluid 6 is heated in the order of the configuration of FIG. 13, as shown in FIG. 15, the position P ０ The heat recovery fluid 6 flows out of the heat recovery device 4 from the position P １ During the period from the time T 1 to the time T 2 , the heat recovery fluid 6 recovers the heat of adsorption AH from the hydrogen compound member 2, and the temperature of the heat recovery fluid 6 reaches the temperature T ０ °C to T ４Then, T ４ ° C. The heat recovery fluid 6 flows into the second heat exchanger 30 and exchanges heat with the heating fluid 13a, which has a temperature higher than that of the hydrogen compound member 2. As a result, the heat recovery fluid 6 flows out of the second heat exchanger 30 at a position P ２ The temperature of the heat recovery fluid 6 continues to rise until the position P ０ ' to position P ２ Since the heat recovery fluid 6 can continue to absorb the heat of adsorption AH and the waste heat WH until the time t1, the amount of heat absorbed by the heat recovery fluid 6 is greater than when the heat recovery fluid exchanges heat with the heating fluid 13a after recovering the heat of adsorption AH from the hydrogen compound material 2.

[0073] (Embodiment 6) Next, a hydrogen production system according to embodiment 6 will be described. The hydrogen production system according to embodiment 6 is a system including an oxygen consumption device that consumes oxygen generated when hydrogen is adsorbed onto a hydrogen compound material, and a hydrogen consumption device that consumes hydrogen released from the hydrogen compound material. In embodiment 6, the same components as those in embodiments 1 to 5 are designated by the same reference numerals, and detailed descriptions thereof will be omitted.

[0074] 16 , a hydrogen production system 40 according to a sixth embodiment of the present disclosure includes a hydrogen compound member 2, a water supply member 3 that supplies water 7 to the hydrogen compound member 2, and an oxygen consumption device 41 that consumes oxygen 5b produced by decomposition of a portion of the water 7 into hydrogen and oxygen in the presence of the hydrogen compound member 2. The hydrogen production system 40 may further include a heating device 9 that heats the hydrogen compound member 2 to which hydrogen has been adsorbed by heat exchange between the hydrogen compound member 2 and a heating fluid 13 that includes exhaust heat generated in the oxygen consumption device 41, and the hydrogen compound member 2, and a hydrogen consumption device 42 that consumes hydrogen 2a released from the hydrogen compound member 2 to which hydrogen has been adsorbed.

[0075] The configurations of the hydrogen compound member 2, the water supply member 3, and the heating device 9 can be the same as those of the first to fifth embodiments. The configurations of the oxygen consumption device 41 and the hydrogen consumption device 42 are not particularly limited. For example, the oxygen consumption device 41 may be an autothermal reforming (ATR) device, or may be a production plant using an oxidation reaction process, a production plant using an oxygen enrichment process, an ultra-high purity oxygen production plant, a space oxygen concentration control device, a fuel cell, a plant using a gasification reaction process, or the like. When the oxygen consumption device 41 is an ATR device 41a, the ATR device 41a may include a reactor 44. The reactor 44 may be configured to supply oxygen 5b generated by decomposing a portion of the water 7 into hydrogen and oxygen in the presence of the hydrogen compound member 2, and a hydrogen-containing compound 45 containing at least a hydrogen atom (e.g., a hydrocarbon such as methane, an alcohol, an ether such as dimethyl ether, ammonia, a biomass fuel, or the like). The ATR device 41a may include an exhaust heat recovery unit 43 in addition to the reactor 44. The exhaust heat recovery unit 43 may be a heat exchanger that exchanges heat between the outflow gas 46 flowing out from the reactor 44 and the heating fluid 13b that has exchanged heat with the hydrogen compound member 2 in the heating device 9. The hydrogen consumption device 42 may be, for example, a gas turbine, an engine, a hydrogen station, a hydrogenation reaction facility, or the like.

[0076] <Operation of the hydrogen production system according to the sixth embodiment of the present disclosure> Next, the operation of the hydrogen production system 40 according to the sixth embodiment of the present disclosure will be described. First, the operation of adsorbing hydrogen to the hydrogen compound member 2 is similar to the operation of the hydrogen production system 1 according to the first to fifth embodiments. When the water supply member 3 supplies water 7 to the hydrogen compound member 2, the water 7 decomposes into hydrogen and oxygen in the presence of the hydrogen compound member 2, and the hydrogen is adsorbed to the hydrogen compound member 2. The generated oxygen 5b is transported to the oxygen consuming device 41 and consumed.

[0077] Next, the operation of releasing hydrogen from the hydrogen compound member 2 to which hydrogen has been adsorbed will be described. Heat exchange between the hydrogen compound member 2 and the heating fluid 13 in the heating device 9 heats the hydrogen compound member 2, causing hydrogen to be released from the hydrogen compound member 2. When the oxygen consuming device 41 is equipped with an exhaust heat recovery unit 43, the heating fluid 13 can be configured to circulate between the heating device 9 and the exhaust heat recovery unit 43, which recovers the exhaust heat WH discharged within the oxygen consuming device 41. The operation of the heating fluid 13 recovering the exhaust heat WH in the exhaust heat recovery unit 43 will be described using an example in which the oxygen consuming device 41 is an ATR device 41a. Taking the example in which the hydrogen-containing compound 45 is methane, oxygen and methane react in the reactor 44 according to the reaction represented by the following reaction formula (1), and a portion of the methane is decomposed according to the reaction represented by the following reaction formula (2), producing hydrogen. The reaction of reaction formula (1) is an exothermic reaction of 890 kJ / mol-methane, and the reaction of reaction formula (2) is an endothermic reaction of 165 kJ / mol-methane. Therefore, the reaction of reaction formula (2) proceeds by utilizing the heat generated by the reaction of reaction formula (1). The effluent gas 46 flowing out from the reactor 44 contains the waste heat WH discharged from the reactor 44. By flowing into the waste heat recovery section 43 and exchanging heat with the heating fluid 13b, the heating fluid 13b recovers the waste heat WH from the effluent gas 46 and becomes the heating fluid 13a. This operation continues while hydrogen is being released from the hydrogen compound member 2. If the hydrogen consumption device 42 is provided, the effluent gas 46 contains hydrogen, so the effluent gas 46 flowing out from the waste heat recovery section 43 is mixed with hydrogen 2a and supplied to the hydrogen consumption device 42 for consumption. CH ４ +20 ２ →2H ２ O+CO ２ ... (1) CH ４ +2H ２ O → CO ２ +4H ２ ...(2)

[0078] When the hydrogen-containing compound 45 is ammonia, the reactions represented by the following reaction formulas (3) and (4) occur in the reactor 44. The reaction of reaction formula (3) is an exothermic reaction of 383 kJ / mol-ammonia, and the reaction of reaction formula (4) is an endothermic reaction of 46 kJ / mol-ammonia, so the reaction of reaction formula (4) proceeds by utilizing the heat generated in the reaction of reaction formula (3). NH ３ +(3 / 4)O ２ → (3 / 2) H ２ O+(1 / 2)N ２ ... (3) NH ３ → (3 / 2) H ２ +(1 / 2)N ２ ...(4)

[0079] When the oxygen consuming device 41 is an ATR device 41a, the oxygen 5b produced by the decomposition of a portion of the water 7 in the presence of the hydrogen compound material 2 reacts with the hydrogen-containing compound 45 to generate heat, which causes a portion of the hydrogen-containing compound 45 to decompose and generate hydrogen, thereby increasing the amount of hydrogen produced. Furthermore, when the ATR device 41a further includes a heat recovery section 43, the exhaust heat WH from the oxygen consuming device 41 contained in the outflow gas 46 is used to heat the heating fluid 13, thereby increasing the amount of hydrogen produced by the decomposition of a portion of the water 7 in the presence of the hydrogen compound material 2 and reducing the operating costs of the hydrogen production system 40.

[0080] If the hydrogen-containing compound 45 is methane, a separation device such as a pressure swing adsorption (PSA) device, a temperature swing adsorption (TSA) device, or an amine carbon dioxide recovery device may be used at any location between the reactor 44 and the hydrogen consumption device 42 to separate some or all of the carbon dioxide and water, thereby increasing the hydrogen concentration in the effluent gas 46. Although not shown, the heat of adsorption generated during adsorption on the hydrogen compound member 2 may be recovered and used to regenerate the absorbent in the temperature swing adsorption (TSA) device or the amine carbon dioxide recovery device. If the hydrogen-containing compound 45 is ammonia, a separation device such as a pressure swing adsorption (PSA) device or a temperature swing adsorption (TSA) device may be used at any location between the reactor 44 and the hydrogen consumption device 42 to separate some or all of the nitrogen and water, thereby increasing the hydrogen concentration in the effluent gas 46. Using such a method, the relatively low-temperature heat of adsorption generated when hydrogen is adsorbed on the hydrogen compound member 2 can be effectively utilized to increase the hydrogen concentration in the effluent gas 46.

[0081] According to the hydrogen production system 40 of the sixth embodiment, hydrogen and oxygen generated by decomposition of part of the water 7 into hydrogen and oxygen in the presence of the hydrogen compound member 2 are consumed in the hydrogen consumption device 42 and the oxygen consumption device 41, respectively, thereby improving the efficiency of the hydrogen production system 40 and reducing the operating cost. Note that, in the sixth embodiment, as in the first to fifth embodiments, a heat recovery device 4 (see FIG. 4) may be provided to recover the heat of adsorption AH generated when hydrogen is adsorbed by the hydrogen compound member 2, and the recovered heat of adsorption AH may be used in the oxygen consumption device 41.

[0082] (Embodiment 7) Next, a hydrogen production system according to embodiment 7 will be described. The hydrogen production system according to embodiment 7 is a system that uses a heat pump to heat a heating fluid that heats a hydrogen compound member. In embodiment 7, the same components as those in embodiments 1 to 6 are designated by the same reference numerals, and detailed descriptions thereof will be omitted.

[0083] <Configuration of hydrogen production system according to embodiment 7 of the present disclosure> As shown in Figure 17, a hydrogen production system 50 according to embodiment 7 of the present disclosure includes a hydrogen compound member 2, a water supply member 3 that supplies water 7 to the hydrogen compound member 2, a hydrogen consumption device 42 that consumes hydrogen produced by decomposition of part of the water 7 into hydrogen and oxygen in the presence of the hydrogen compound member 2, a heating device 9 that heats the hydrogen compound member 2 to which hydrogen has been adsorbed by heat exchange between the heating fluid 13 and the hydrogen compound member 2, and a heat pump 51 that heats the heating fluid 13 with exhaust heat WH generated in the hydrogen consumption device 42.

[0084] In the seventh embodiment, as long as there is no contradiction in the configuration, the hydrogen consumption device may be any of the hydrogen consumption devices exemplified in the first to fifth embodiments. For example, if the power generation system 10b (see FIG. 6) of the specific example 2 of the second embodiment is used as the hydrogen consumption device 42, the exhaust heat recovery heat exchanger 405 of the power generation system 10b corresponds to the exhaust heat recovery section 57 (see FIG. 6).

[0085] The heat pump 51 has a configuration in which an evaporator 53, a compressor 54, a condenser 55, and a pressure reducer 56 such as an expansion valve or a screw expander are provided in a refrigerant circulation line 52 through which the refrigerant circulates. The evaporator 53 is a heat exchanger that exchanges heat between the refrigerant and an exhaust heat-containing fluid 58 from which exhaust heat WH has been recovered in an exhaust heat recovery section 57 of the hydrogen consumption device 42. The condenser 55 is a heat exchanger that exchanges heat between the heating fluid 13 and the refrigerant.

[0086] <Operation of the Hydrogen Production System According to Embodiment 7 of the Present Disclosure> Next, the operation of the hydrogen production system 50 according to Embodiment 7 of the present disclosure will be described. First, the operation of adsorbing hydrogen to the hydrogen compound member 2 is similar to the operation of the hydrogen production system 1 according to Embodiments 1 to 5. When the water supply member 3 supplies water 7 to the hydrogen compound member 2, the water 7 decomposes into hydrogen and oxygen in the presence of the hydrogen compound member 2, and the hydrogen is adsorbed to the hydrogen compound member 2. The generated oxygen 5b may be recovered and stored in a tank or the like, or may be transported to an oxygen consuming device (not shown) and consumed.

[0087] Next, the operation of releasing hydrogen from the hydrogen compound member 2 to which hydrogen has been adsorbed will be described. The heat pump 51 is started to circulate the refrigerant through the refrigerant circulation line 52. The waste heat-containing fluid 58a, from which the waste heat WH has been recovered in the waste heat recovery section 57 of the hydrogen consumption device 42, is supplied to the evaporator 53. Heat exchange occurs between the waste heat-containing fluid 58a and the refrigerant, causing the refrigerant to heat and evaporate, while the waste heat-containing fluid 58a is cooled and returns to the waste heat recovery section 57 as the waste heat-containing fluid 58b, thereby recovering the waste heat WH again. The gaseous refrigerant evaporated in the evaporator 53 is compressed by the compressor 54 and flows into the condenser 55 in an elevated temperature state. In the condenser 55, heat exchange occurs between the heating fluid 13b, which has heated the hydrogen compound member 2 in the heating device 9, and the gaseous refrigerant flowing into the condenser 55. As a result, the heating fluid 13b is heated to become the heated fluid 13a (which has absorbed heat H), while the gaseous refrigerant is cooled and condensed. The condensed refrigerant flows out of the condenser 55, and then is decompressed by the pressure reducer 56 to lower its temperature. The refrigerant that flows out of the pressure reducer 56 flows into the evaporator 53 again.

[0088] The heated heating fluid 13a is supplied to the heating device 9 and heats the hydrogen compound member 2. Hydrogen 2a is released from the heated hydrogen compound member 2. The released hydrogen 2a is transported to the hydrogen consumption device 42 and consumed. The heating fluid 13a that heated the hydrogen compound member 2 in the heating device 9 becomes cooled heating fluid 13b and returns to the condenser 55, where it is heated again by heat exchange with the refrigerant and becomes heated heating fluid 13a. This operation continues while the hydrogen 2a is being released from the hydrogen compound member 2.

[0089] According to the hydrogen production system 50 of the seventh embodiment, the heat pump 51 uses the exhaust heat WH generated by consuming the hydrogen 2a released from the hydrogen compound member 2 as a heat source to heat the heating fluid 13 for heating the hydrogen compound member 2 to release the hydrogen 2a from the hydrogen compound member 2 to which hydrogen has been adsorbed. Therefore, even if the temperature of the exhaust heat WH is low and the temperature of the exhaust heat-containing fluid 58a is lower than the temperature of the hydrogen compound member 2 when the hydrogen 2a is released from the hydrogen compound member 2, it is possible to utilize the low-temperature exhaust heat WH to produce hydrogen using the hydrogen compound member 2. Therefore, the efficiency of the hydrogen production system 50 can be improved and the operating costs can be reduced.

[0090] [Hydrocarbon Production System of the Present Disclosure] (Embodiment 1) The hydrocarbon production system according to Embodiment 1 of the present disclosure is a system in which a gas supply device that supplies a carbon dioxide-containing gas containing carbon dioxide to the hydrogen compound member 2 is added to any of the hydrogen production systems according to Embodiments 1 to 6, and the hydrogen released from the hydrogen compound member 2 is reacted with the carbon dioxide to produce hydrocarbons. In the following explanation, the hydrocarbon production system according to Embodiment 1 will be described as having a configuration in which a gas supply device is added to the hydrogen production system according to Embodiment 1, but the hydrocarbon production system according to Embodiment 1 can also be configured as having a configuration in which a gas supply device is added to any of the hydrogen production systems according to Embodiments 2 to 6. Note that in the hydrocarbon production system according to Embodiment 1, the same components as those in the hydrogen production systems according to Embodiments 1 to 6 are denoted by the same reference numerals, and detailed explanations thereof will be omitted.

[0091] <Configuration of hydrocarbon production system according to embodiment 1 of the present disclosure> As shown in Figure 18, the hydrocarbon production system 60 according to embodiment 1 of the present disclosure includes a hydrogen compound element 2, a water supply element 3 that supplies water 7 to the hydrogen compound element 2, a heat recovery device 4 that recovers adsorption heat AH generated when hydrogen produced by decomposing a portion of the water 7 into hydrogen and oxygen in the presence of the hydrogen compound element 2 is adsorbed by the hydrogen compound element 2, a heating device 9 that heats the hydrogen compound element 2 to which hydrogen has been adsorbed, and a gas supply device 61 that supplies a carbon dioxide-containing gas 62 containing carbon dioxide to the hydrogen compound element 2.

[0092] <Operation of the hydrocarbon production system according to the first embodiment of the present disclosure> Next, the operation of the hydrocarbon production system 60 according to the first embodiment of the present disclosure will be described. The operation of the water supply member 3 supplying water 7 to the hydrogen compound member 2, causing hydrogen to be adsorbed by the hydrogen compound member 2, and recovering the heat of adsorption AH generated at this time by the heat recovery device 4 is the same as the operation of the hydrogen production system according to the first embodiment.

[0093] After hydrogen is adsorbed to the hydrogen compound member 2, the hydrogen compound member 2 is heated by the heating device 9 (heat H is applied to the hydrogen compound member 2 in the heating device 9), thereby releasing hydrogen from the hydrogen compound member 2. Simultaneously with the hydrogen release operation, a carbon dioxide-containing gas 62 is supplied from the gas supply device 61 to the hydrogen compound member 2. This results in a state in which hydrogen and carbon dioxide coexist in the presence of the hydrogen compound member 2. Then, as described in detail in Patent Document 2, the hydrogen released from the hydrogen compound member 2 reacts with the carbon dioxide in the carbon dioxide-containing gas 62 supplied from the gas supply device 61 according to the following reaction formula (5), thereby producing hydrocarbons: aCO ２ +bH ２ →C ａ H ｂ +cH ２ O... (5)

[0094] The oxygen produced when hydrogen is adsorbed onto the hydrogen compound member 2 and the hydrocarbons produced by the above principle may be recovered and stored in a tank or the like, or may be transported to an oxygen consumption device and a hydrocarbon consumption device (not shown) and consumed.

[0095] In the hydrocarbon production system 60 according to the first embodiment of the present disclosure, the thermal efficiency is improved by recovering and utilizing the heat of adsorption AH generated when hydrogen produced by decomposing a portion of the water 7 into hydrogen and oxygen in the presence of the hydrogen compound member 2 is adsorbed by the hydrogen compound member 2, thereby reducing the operating costs of the hydrocarbon production system 60.

[0096] (Embodiment 2) A hydrocarbon production system according to Embodiment 2 of the present disclosure is a system in which a gas supply device that supplies a carbon dioxide-containing gas containing carbon dioxide to the hydrogen compound member 2 is added to the hydrogen production system 50 according to Embodiment 7, and hydrocarbons are produced by reacting the hydrogen released from the hydrogen compound member 2 with the carbon dioxide. Note that in the hydrocarbon production system according to Embodiment 2, the same components as those in the hydrogen production system according to Embodiment 7 and the hydrocarbon production system according to Embodiment 1 are denoted by the same reference numerals, and detailed descriptions thereof will be omitted.

[0097] <Configuration of hydrocarbon production system according to embodiment 2 of the present disclosure> As shown in FIG. 19 , a hydrocarbon production system 70 according to embodiment 2 of the present disclosure includes a hydrogen compound member 2, a water supply member 3 that supplies water 7 to the hydrogen compound member 2, a heating device 9 that heats the hydrogen compound member 2 by heat exchange between a heating fluid 13 and the hydrogen compound member 2, a gas supply device 61 that supplies a carbon dioxide-containing gas 62 containing carbon dioxide to the hydrogen compound member 2, a hydrocarbon consumption device 71 that consumes hydrocarbons produced by decomposing a portion of the water 7 into hydrogen and oxygen in the presence of the hydrogen compound member 2 and reacting the hydrogen with carbon dioxide, and a heat pump 51 that heats the heating fluid 13 with exhaust heat WH generated in the hydrocarbon consumption device 71.

[0098] There are no particular limitations on the configuration of the hydrocarbon consumption device 71. For example, the gas engine 400 of specific example 2 of embodiment 2 is an engine that uses ammonia as fuel, but a power generation system including a gas engine that uses hydrocarbons such as methane or ethane as fuel may also be used as the hydrocarbon consumption device 71. In this case, an exhaust heat recovery heat exchanger (corresponding to the exhaust heat recovery heat exchanger 405 in specific example 2 of embodiment 2) for recovering heat from exhaust gas discharged from the gas engine corresponds to the exhaust heat recovery unit 73 that recovers the exhaust heat WH.

[0099] <Operation of the hydrocarbon production system according to the second embodiment of the present disclosure> Next, the operation of the hydrocarbon production system 70 according to the second embodiment of the present disclosure will be described. The operation of the hydrocarbon production system 70 differs from the operation of the hydrocarbon production system 60 only in the operation of heating the heating fluid 13. Therefore, the operation of heating the heating fluid 13 will be described below.

[0100] In the heating device 9, the hydrogen compound material 2 is heated by heat exchange with the heating fluid 13a, while the heating fluid 13a becomes a cooled heating fluid 13b. Hydrogen released by heating the hydrogen compound material 2 reacts with carbon dioxide in the carbon dioxide-containing gas 62 supplied by the gas supply device 61 to produce hydrocarbons through the same operation as in the hydrocarbon production system 60. The hydrocarbons produced in this manner are transported to the hydrocarbon consumption device 71 and consumed. The exhaust heat WH generated by the consumption of hydrocarbons in the hydrocarbon consumption device 71 is recovered by the exhaust heat-containing fluid 58 in the exhaust heat recovery section 73. The heating fluid 13b is heated by the heat pump 51, which uses the exhaust heat WH recovered by the exhaust heat-containing fluid 58 as a heat source, to produce the heated heating fluid 13a (which has absorbed heat H). The operation of heating the heating fluid 13b by the heat pump 51 is the same as the operation in the hydrogen production system according to the seventh embodiment.

[0101] According to the hydrocarbon production system 70 of the second embodiment, the heat pump 51 uses as a heat source the exhaust heat WH generated by consuming the hydrocarbons produced by the hydrocarbon production system 70 to heat the heating fluid 13 for heating the hydrogen compound member 2 in order to release hydrogen from the hydrogen compound member 2 to which hydrogen has been adsorbed. Therefore, even if the temperature of the exhaust heat WH is low and the temperature of the exhaust heat-containing fluid 58a is lower than the temperature of the hydrogen compound member 2 when hydrogen 2a is released from the hydrogen compound member 2, it is possible to utilize the low-temperature exhaust heat WH to produce hydrogen using the hydrogen compound member 2. Therefore, the operating costs of the hydrocarbon production system 70 can be reduced.

[0102] The contents described in each of the above embodiments can be understood, for example, as follows.

[0103] [1] A hydrogen production system according to one embodiment includes a hydrogen compound element (2), a water supply element (3) that supplies water (7) to the hydrogen compound element (2), and a heat recovery device (4) that recovers heat of adsorption (AH) generated when the hydrogen, generated by decomposing a portion of the water (7) into hydrogen and oxygen in the presence of the hydrogen compound element (2), is adsorbed by the hydrogen compound element (2).

[0104] According to the hydrogen production system of the present disclosure, the thermal efficiency is improved by recovering and utilizing the heat of adsorption generated when hydrogen produced by the decomposition of part of water into hydrogen and oxygen in the presence of a hydrogen compound component is adsorbed by the hydrogen compound component, thereby reducing the operating costs of the hydrogen production system.

[0105] [2] A hydrogen production system according to another aspect is the hydrogen production system of [1], wherein the heat recovery device (4) includes at least one of a heat exchanger (4a) for exchanging heat between a heat recovery fluid (6) and water (5a) that has not decomposed into the hydrogen and the oxygen from the water (7), or a heat exchanger (4b) for exchanging heat between the oxygen (5b) and the heat recovery fluid (6).

[0106] With this configuration, the thermal efficiency is improved by recovering and utilizing at least one of the heat of adsorption contained in the water that has not decomposed into hydrogen and oxygen, or the heat of adsorption contained in the oxygen produced, in the heat recovery fluid, thereby reducing the operating costs of the hydrogen production system.

[0107] [3] A hydrogen production system according to yet another embodiment is the hydrogen production system of [1] or [2], comprising: a heat utilization device (10) including a heat absorption section (11) that absorbs the heat of adsorption (AH) recovered in the heat recovery fluid (6) in the heat recovery device (4), and an exhaust heat recovery section (12) that recovers exhaust heat (WH); and a heating device (9) that heats the hydrogen compound member (2) to which the hydrogen is adsorbed by heat exchange between the hydrogen compound member (2) and a heating fluid (13) from which the exhaust heat (WH) has been recovered in the exhaust heat recovery section (12).

[0108] With this configuration, the heat of adsorption is utilized in the heat utilization device, and the exhaust heat emitted by the heat utilization device is utilized to heat the hydrogen compound component on which hydrogen has been adsorbed, thereby further improving thermal efficiency and further reducing the operating costs of the hydrogen production system.

[0109] [4] A hydrogen production system according to yet another aspect is the hydrogen production system of [3], wherein the heating fluid (13) is a fluid that undergoes a phase change when the hydrogen compound member (2) is heated in the heating device (9).

[0110] With this configuration, the hydrogen compound material can be heated by utilizing the latent heat generated when the heating fluid changes phase, and heat exchange between the heating fluid and the hydrogen compound material can be carried out with a small temperature difference between the two, allowing the hydrogen compound material to be heated efficiently.

[0111] [5] A hydrogen production system according to yet another aspect is the hydrogen production system of [3], wherein the heating fluid (13) is a fluid that heats the hydrogen compound member (2) while causing an exothermic reaction inside the heating fluid (13) in the heating device (9).

[0112] With this configuration, the hydrogen compound material can be heated using the reaction heat generated by the exothermic reaction inside the heating fluid, and heat exchange between the heating fluid and the hydrogen compound material can be carried out with a small temperature difference between the two, allowing the hydrogen compound material to be heated efficiently.

[0113] [6] A hydrogen production system according to yet another aspect is the hydrogen production system according to any one of [3] to [5], wherein the heat recovery fluid (6) is a fluid that undergoes a phase change when the heat of adsorption (AH) is recovered from the hydrogen compound material (2) in the heat recovery device (4).

[0114] With this configuration, the heat of adsorption can be recovered from the hydrogen compound material by utilizing the latent heat generated when the heat recovery fluid changes phase, and heat exchange between the heat recovery fluid and the hydrogen compound material can be carried out with a small temperature difference between the two, so the heat of adsorption can be recovered efficiently from the hydrogen compound material.

[0115] [7] A hydrogen production system according to yet another embodiment is the hydrogen production system according to any one of [3] to [5], wherein the heat recovery fluid (6) is a fluid that recovers the heat of adsorption (AH) from the hydrogen compound material (2) while causing an endothermic reaction inside the heat recovery fluid (6) in the heat recovery device (4).

[0116] With this configuration, the heat of adsorption can be recovered from the hydrogen compound material by utilizing the endothermic reaction that occurs inside the heat recovery fluid, and heat exchange between the heat recovery fluid and the hydrogen compound material can be carried out with a small temperature difference between the two, so the heat of adsorption can be recovered efficiently from the hydrogen compound material.

[0117] [8] A hydrogen production system according to yet another aspect is the hydrogen production system of [3], wherein the heat absorption unit (11) includes a first heat absorption unit (11b) and a second heat absorption unit (11c) different from the first heat absorption unit (11b), and the heat of adsorption (AH) recovered in the heat recovery fluid (6) is absorbed by the first heat absorption unit (11b), and the heat still contained in the heating fluid (13) after heating the hydrogen compound member (2) in the heating device (9) is absorbed by the second heat absorption unit (11c).

[0118] With this configuration, the heat of adsorption is absorbed in the first heat absorption section, and the heat still contained in the heating fluid after heating the hydrogen compound material in the heating device is absorbed in the second heat absorption section and utilized in the heat utilization device, thereby further improving thermal efficiency and further reducing the operating costs of the hydrogen production system.

[0119] [9] A hydrogen production system according to yet another aspect is the hydrogen production system of [1], comprising: a heat utilization device (10) including a heat absorption section (11) that absorbs the heat of adsorption (AH) recovered in the heat recovery fluid (6) in the heat recovery device (4) and an exhaust heat recovery section (12) that recovers exhaust heat (WH); and a first heat exchanger (20) that exchanges heat between the heat recovery fluid (6) before recovering the heat of adsorption (AH) in the heat recovery device (4) and a heating fluid (13) from which the exhaust heat (WH) has been recovered in the exhaust heat recovery section (12), wherein the temperature of the heating fluid (13) before exchanging heat with the heat recovery fluid (6) is lower than the temperature of the hydrogen compound member (2) and higher than the temperature of the heat recovery fluid (6) before recovering the heat of adsorption (AH).

[0120] With this configuration, the temperature of the heat recovery fluid supplied to the heat utilization device is higher than when the heat recovery fluid exchanges heat with either a hydrogen compound material or a heating fluid, thereby improving the heat utilization efficiency of the heat utilization device.

[0121]

[10] A hydrogen production system according to yet another aspect is the hydrogen production system of [1], comprising: a heat utilization device (10) including a heat absorption section (11) that absorbs the heat of adsorption (AH) recovered in the heat recovery fluid (6) in the heat recovery device (4), and an exhaust heat recovery section (12) that recovers exhaust heat (WH); and a second heat exchanger (30) that exchanges heat between the heat recovery fluid (6) after recovering the heat of adsorption (AH) in the heat recovery device (4) and a heating fluid (13) from which the exhaust heat (WH) has been recovered in the exhaust heat recovery section (12), and the temperature of the heating fluid (13) before exchanging heat with the heat recovery fluid (6) is higher than the temperature of the hydrogen compound member (2).

[0122] With this configuration, the temperature of the heat recovery fluid supplied to the heat utilization device is higher than when the heat recovery fluid exchanges heat with either a hydrogen compound material or a heating fluid, thereby improving the heat utilization efficiency of the heat utilization device.

[0123]

[11] A hydrogen production system according to another aspect includes a hydrogen compound element (2), a water supply element (3) that supplies water (7) to the hydrogen compound element (2), and an oxygen consumption device (41) that consumes the oxygen (5b) produced by decomposition of a portion of the water (7) into hydrogen and oxygen in the presence of the hydrogen compound element (2).

[0124] According to another aspect of the hydrogen production system of the present disclosure, the oxygen produced by the decomposition of a portion of water into hydrogen and oxygen in the presence of a hydrogen compound component is consumed by an oxygen consuming device, thereby reducing the operating costs of the hydrogen production system.

[0125]

[12] A hydrogen production system according to yet another aspect is the hydrogen production system of

[11] , and includes: a heating device (9) that heats the hydrogen compound member (2) to which hydrogen is adsorbed by heat exchange between the hydrogen compound member (2) and a heating fluid (13) containing exhaust heat (WH) generated in the oxygen consumption device (41); and a hydrogen consumption device (42) that consumes hydrogen released from the hydrogen compound member (2) to which hydrogen is adsorbed.

[0126] With this configuration, the hydrogen and oxygen produced by the decomposition of part of the water into hydrogen and oxygen in the presence of the hydrogen compound component are consumed by the hydrogen consumption device and the oxygen consumption device, respectively, thereby reducing the operating costs of the hydrogen production system.

[0127]

[13] A hydrogen production system according to yet another embodiment is the hydrogen production system of

[11] , wherein the oxygen consumption device (41) includes a reactor (44) that reacts oxygen (5b) produced by decomposition of a portion of the water (7) in the presence of the hydrogen compound member (2) with a hydrogen-containing compound (45) containing at least hydrogen atoms.

[0128] According to this configuration, the amount of hydrogen produced can be increased because the heat generated by the reaction between the hydrogen-containing compound and the oxygen produced by the decomposition of part of the water in the presence of the hydrogen compound component causes the hydrogen-containing compound to decompose and produce hydrogen.

[0129]

[14] A hydrogen production system according to yet another embodiment is the hydrogen production system of

[12] , wherein the oxygen consumption device comprises: a reactor (44) that reacts oxygen (5b) produced by decomposition of a portion of the water (7) in the presence of the hydrogen compound member (2) with a hydrogen-containing compound (45) containing at least hydrogen atoms; and an exhaust heat recovery section (43) that exchanges heat between an effluent gas (46) flowing out from the reactor (44) and the heating fluid (13) after heat exchange with the hydrogen compound member (2) in the heating device (9).

[0130] According to this configuration, the waste heat from the oxygen consuming device contained in the outflow gas is used to heat the heating fluid, thereby reducing the operating costs of the hydrogen production system.

[0131]

[15] A hydrogen production system according to yet another embodiment includes a hydrogen compound element (2), a water supply element (3) that supplies water (7) to the hydrogen compound element (2), a hydrogen consumption device (42) that consumes the hydrogen (2a) produced by decomposition of a portion of the water (7) into hydrogen and oxygen in the presence of the hydrogen compound element (2), a heating device (9) that heats the hydrogen compound element (2) to which the hydrogen is adsorbed by heat exchange between a heating fluid (13) and the hydrogen compound element (2), and a heat pump (51) that heats the heating fluid (13) by waste heat (WH) generated in the hydrogen consumption device (42).

[0132] In a hydrogen production system according to yet another aspect of the present disclosure, a heat pump that uses exhaust heat generated by consuming hydrogen released from a hydrogen compound material as a heat source heats a heating fluid that heats the hydrogen compound material to release hydrogen from the hydrogen compound material to which hydrogen has been adsorbed, thereby reducing the operating costs of the hydrogen production system.

[0133]

[16] A hydrocarbon production system according to one embodiment includes: a hydrogen compound element (2); a water supply element (3) that supplies water (7) to the hydrogen compound element (2); a gas supply device (61) that supplies a carbon dioxide-containing gas (62) containing carbon dioxide to the hydrogen compound element (2); a hydrocarbon consumption device (71) that consumes hydrocarbons (72) produced by decomposing a part of the water (7) into hydrogen and oxygen in the presence of the hydrogen compound element (2) and reacting the hydrogen with the carbon dioxide; a heating device (9) that heats the hydrogen compound element (2) to which the hydrogen is adsorbed by heat exchange between a heating fluid (13) and the hydrogen compound element (2); and a heat pump (51) that heats the heating fluid (13) by waste heat (WH) generated in the hydrocarbon consumption device (71).

[0134] According to the hydrocarbon production system of the present disclosure, a heat pump that uses exhaust heat generated by consuming the hydrocarbons produced by the hydrocarbon production system as a heat source heats a heating fluid that heats the hydrogen compound member to release hydrogen from the hydrogen compound member to which hydrogen has been adsorbed, thereby reducing the operating costs of the hydrocarbon production system.

[0135]

[17] A hydrocarbon production system according to another embodiment includes a hydrogen compound element (2), a water supply element (3) that supplies water (7) to the hydrogen compound element (2), a heat recovery device (4) that recovers heat of adsorption (AH) generated when hydrogen, generated by decomposition of a portion of the water (7) into hydrogen and oxygen in the presence of the hydrogen compound element (2), is adsorbed by the hydrogen compound element (2), a heating device (9) that heats the hydrogen compound element (2) to which the hydrogen has been adsorbed, and a gas supply device (61) that supplies a carbon dioxide-containing gas (62) containing carbon dioxide to the hydrogen compound element (2).

[0136]

[18] A hydrogen production system according to yet another embodiment is the hydrogen production system according to

[13] , wherein in the reactor (44), heat generated by reacting oxygen (5b) with a portion of the hydrogen-containing compound (45) is used to decompose at least a portion of the remaining hydrogen-containing compound (45) to further produce hydrogen.

[0137]

[19] A hydrogen production system according to yet another embodiment is the hydrogen production system of

[18] , further comprising a separation device, which separates substances other than hydrogen from an effluent gas (46) containing hydrogen produced by decomposing at least a portion of the remaining hydrogen-containing compound (45) and flowing out of the reactor (44).

[0138] According to the hydrocarbon production system of the present disclosure, the thermal efficiency is improved by recovering and utilizing the heat of adsorption generated when hydrogen, which is produced by decomposing a portion of water into hydrogen and oxygen in the presence of a hydrogen compound component, is adsorbed onto the hydrogen compound component, thereby reducing the operating costs of the hydrogen production system.

[0139] DESCRIPTION OF SYMBOLS 1 Hydrogen production system 2 Hydrogen compound member 2a Hydrogen 3 Water supply member 4 Heat recovery device 5a Water 5b Oxygen 6 Heat recovery fluid 7 Water 9 Heating device 10 Heat utilization device 11 Heat absorption section 11b First heat absorption section 11c Second heat absorption section 12 Exhaust heat recovery section 13 Heating fluid 20 First heat exchanger 30 Second heat exchanger 40 Hydrogen production system 41 Oxygen consumption device 42 Hydrogen consumption device 43 Exhaust heat recovery section 44 Reactor 45 Hydrogen-containing compound 46 Outlet gas 50 Hydrogen production system 51 Heat pump 60 Hydrocarbon production system 61 Gas supply device 62 Carbon dioxide-containing gas 70 Hydrocarbon production system 71 Hydrocarbon consumption device 72 Hydrocarbon AH Heat of adsorption WH Exhaust heat

Claims

1. A hydrogen production system comprising: a hydrogen compound element; a water supply element that supplies water to the hydrogen compound element; and a heat recovery device that recovers heat of adsorption generated when the hydrogen produced by decomposing a portion of the water into hydrogen and oxygen in the presence of the hydrogen compound element is adsorbed by the hydrogen compound element.

2. The hydrogen production system described in claim 1, wherein the heat recovery device includes at least one of a heat exchanger that performs heat exchange between the water that has not been decomposed into the hydrogen and the oxygen and a heat recovery fluid, or a heat exchanger that performs heat exchange between the oxygen and a heat recovery fluid.

3. A hydrogen production system as described in claim 1 or 2, comprising: a heat utilization device including a heat absorption section that absorbs the heat of adsorption recovered in the heat recovery fluid in the heat recovery device, and an exhaust heat recovery section that recovers exhaust heat; and a heating device that heats the hydrogen compound member to which the hydrogen is adsorbed by heat exchange between the heating fluid from which the exhaust heat is recovered in the exhaust heat recovery section and the hydrogen compound member.

4. The hydrogen production system according to claim 3, wherein the heating fluid is a fluid that undergoes a phase change when the hydrogen compound member is heated in the heating device.

5. The hydrogen production system according to claim 3, wherein the heating fluid is a fluid that heats the hydrogen compound member while causing an exothermic reaction inside the heating fluid in the heating device.

6. The hydrogen production system according to claim 3, wherein the heat recovery fluid is a fluid that undergoes a phase change when the heat of adsorption is recovered from the hydrogen compound member in the heat recovery device.

7. The hydrogen production system according to claim 3, wherein the heat recovery fluid is a fluid that recovers the heat of adsorption from the hydrogen compound member while causing an endothermic reaction inside the heat recovery fluid in the heat recovery device.

8. The hydrogen production system described in claim 3, wherein the heat absorption unit includes a first heat absorption unit and a second heat absorption unit different from the first heat absorption unit, and the heat of adsorption recovered in the heat recovery fluid is absorbed in the first heat absorption unit, and the heat still contained in the heating fluid after heating the hydrogen compound member in the heating device is absorbed in the second heat absorption unit.

9. A hydrogen production system as described in claim 1, comprising: a heat utilization device including a heat absorption section that absorbs the heat of adsorption recovered by the heat recovery fluid in the heat recovery device, and a waste heat recovery section that recovers waste heat; and a first heat exchanger that exchanges heat between the heat recovery fluid before recovering the heat of adsorption in the heat recovery device and a heating fluid from which the waste heat has been recovered in the waste heat recovery section, wherein the temperature of the heating fluid before exchanging heat with the heat recovery fluid is lower than the temperature of the hydrogen compound member and higher than the temperature of the heat recovery fluid before recovering the heat of adsorption.

10. A hydrogen production system as described in claim 1, comprising: a heat utilization device including a heat absorption section that absorbs the heat of adsorption recovered in the heat recovery fluid in the heat recovery device, and a waste heat recovery section that recovers waste heat; and a second heat exchanger that exchanges heat between the heat recovery fluid after the heat of adsorption has been recovered in the heat recovery device and a heating fluid from which the waste heat has been recovered in the waste heat recovery section, wherein the temperature of the heating fluid before heat exchange with the heat recovery fluid is higher than the temperature of the hydrogen compound member.

11. A hydrogen production system comprising: a hydrogen compound element; a water supply element that supplies water to the hydrogen compound element; and an oxygen consumption device that consumes the oxygen produced by decomposition of a portion of the water into hydrogen and oxygen in the presence of the hydrogen compound element.

12. A hydrogen production system as described in claim 11, comprising: a heating device that heats the hydrogen compound member to which hydrogen is adsorbed by heat exchange between the hydrogen compound member and a heating fluid containing exhaust heat generated in the oxygen consumption device; and a hydrogen consumption device that consumes hydrogen released from the hydrogen compound member to which hydrogen is adsorbed.

13. The hydrogen production system according to claim 11, wherein the oxygen consuming device comprises a reactor that reacts oxygen produced by decomposition of a portion of the water in the presence of the hydrogen compound component with a hydrogen-containing compound containing at least hydrogen atoms.

14. The hydrogen production system described in claim 12, wherein the oxygen consumption device comprises: a reactor that reacts oxygen produced by decomposition of a portion of the water in the presence of the hydrogen compound member with a hydrogen-containing compound containing at least hydrogen atoms; and an exhaust heat recovery unit that exchanges heat between the effluent gas flowing out from the reactor and the heating fluid after heat exchange with the hydrogen compound member in the heating device.

15. A hydrogen production system comprising: a hydrogen compound element; a water supply element that supplies water to the hydrogen compound element; a hydrogen consumption device that consumes the hydrogen produced by decomposition of part of the water into hydrogen and oxygen in the presence of the hydrogen compound element; a heating device that heats the hydrogen compound element to which the hydrogen is adsorbed by heat exchange between a heating fluid and the hydrogen compound element; and a heat pump that heats the heating fluid using exhaust heat generated in the hydrogen consumption device.

16. A hydrocarbon production system comprising: a hydrogen compound element; a water supply element that supplies water to the hydrogen compound element; a gas supply device that supplies a carbon dioxide-containing gas containing carbon dioxide to the hydrogen compound element; a hydrocarbon consumption device that consumes hydrocarbons produced by the reaction of the hydrogen with the carbon dioxide while part of the water is decomposed into hydrogen and oxygen in the presence of the hydrogen compound element; a heating device that heats the hydrogen compound element to which the hydrogen is adsorbed by heat exchange between a heating fluid and the hydrogen compound element; and a heat pump that heats the heating fluid with exhaust heat generated in the hydrocarbon consumption device.

17. A hydrocarbon production system comprising: a hydrogen compound element; a water supply element that supplies water to the hydrogen compound element; a heat recovery device that recovers heat of adsorption generated when hydrogen produced by decomposing a portion of the water into hydrogen and oxygen in the presence of the hydrogen compound element is adsorbed by the hydrogen compound element; a heating device that heats the hydrogen compound element to which the hydrogen has been adsorbed; and a gas supply device that supplies a carbon dioxide-containing gas containing carbon dioxide to the hydrogen compound element.

Images