Hydrogen production system and hydrocarbon production system

Abstract

To provide a hydrogen production system and a hydrocarbon production system reduced in operation cost.SOLUTION: A hydrogen production system includes 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 generated when hydrogen generated by decomposing a part of water into hydrogen and oxygen in the presence of the hydrogen compound member is adsorbed by the hydrogen compound member. The hydrocarbon production system includes a hydrogen compound member, a water supply member that supplies water to the hydrogen compound member, a heat recovery device that recovers heat of adsorption generated when hydrogen generated by decomposition of a portion of the water into hydrogen and oxygen in the presence of the hydrogen compound member is adsorbed by the hydrogen compound member, a heating device that heats the hydrogen compound member 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 member.SELECTED DRAWING: Figure 1

Description

[Technical Field]

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

[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. [Prior art documents] [Patent documents]

[0003] [Patent Document 1] Japanese Patent Publication No. 2023-30975 [Patent Document 2] Japanese Patent Application Publication No. 2023-30964 Summary of the Invention [Problem to be solved by the invention]

[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 the hydrogen production system 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. [Means for solving the problem]

[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. [Effects of the Invention]

[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. [Brief explanation of the drawings]

[0009] [Figure 1] FIG. 1 is a diagram showing a concept common to several specific configurations included in a hydrogen production system according to a first embodiment of the present disclosure. [Figure 2] FIG. 1 is a diagram showing a concept common to specific configurations when a heat recovery device is in the form of a heat exchanger in a hydrogen production system according to a first embodiment of the present disclosure. [Figure 3] 1 is a schematic diagram illustrating an example of a specific configuration of a hydrogen production system according to a first embodiment of the present disclosure. [Figure 4] FIG. 10 is a diagram showing a concept common to several specific configurations included in a hydrogen production system according to a second embodiment of the present disclosure. [Figure 5] FIG. 2 is a diagram showing the configuration of a specific example 1 of a hydrogen production system according to a second embodiment of the present disclosure. [Figure 6] FIG. 2 is a diagram showing the configuration of a specific example 2 of a hydrogen production system according to a second embodiment of the present disclosure. [Figure 7] FIG. 10 is a diagram showing the configuration of a specific example 3 of a hydrogen production system according to the second embodiment of the present disclosure. [Figure 8] FIG. 10 is a diagram showing the configuration of a specific example 4 of a hydrogen production system according to the second embodiment of the present disclosure. [Figure 9] FIG. 10 is a diagram illustrating the concept of a hydrogen production system according to a third embodiment of the present disclosure. [Figure 10] FIG. 10 is a diagram illustrating the concept of a hydrogen production system according to a fourth embodiment of the present disclosure. [Figure 11] 10 is a schematic graph for explaining the effects of the hydrogen production system according to the fourth embodiment of the present disclosure. [Figure 12]10 is a schematic graph for explaining the effects of the hydrogen production system according to the fourth embodiment of the present disclosure. [Figure 13] FIG. 10 is a diagram illustrating the concept of a hydrogen production system according to a fifth embodiment of the present disclosure. [Figure 14] 10 is a schematic graph for explaining the effects of the hydrogen production system according to the fifth embodiment of the present disclosure. [Figure 15] 10 is a schematic graph for explaining the effects of the hydrogen production system according to the fifth embodiment of the present disclosure. [Figure 16] FIG. 10 is a diagram illustrating the concept of a hydrogen production system according to a sixth embodiment of the present disclosure. [Figure 17] FIG. 10 is a diagram illustrating the concept of a hydrogen production system according to a seventh embodiment of the present disclosure. [Figure 18] FIG. 1 is a diagram showing the concept of a hydrocarbon production system according to a first embodiment of the present disclosure. [Figure 19] FIG. 1 is a diagram showing the concept of a hydrocarbon production system according to a second embodiment of the present disclosure. DETAILED DESCRIPTION OF THE INVENTION

[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 hydrogen production system according to embodiment 1 of the present disclosure> The hydrogen production system according to the first embodiment of the present disclosure includes several specific configurations, as will be described later. Figure 1 shows a 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 nThe stoichiometric ratio m:n is 1:1 to 3:4 (e.g., XH, XH2, XH3, XH4, X2H3, X3H4) (m and n are not limited to integers and may be non-integer). The element X is, for example, boron (B), without being limited thereto.

[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 component 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 given fluid (heat recovery fluid). FIG. 2 shows a 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, which is water 7 supplied from the water supply component 3 and has not been decomposed into hydrogen and oxygen or a compound containing oxygen atoms, 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 a housing 8 that accommodates a hydrogen compound member 2 so that the heat recovery fluid 6 can cool the inside of the housing 8. In this form, the temperature inside the housing 8 rises due to heat of adsorption AH generated when hydrogen is adsorbed by the hydrogen compound member 2, and 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, or 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 conductive 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 the first embodiment of the present disclosure> Next, the operation of the hydrogen production system 1 according to the first embodiment of the present disclosure will be described. In the following, a description will be given of a mode in which water is decomposed 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 in which 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 is decomposed 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 temperature of the hydrogen compound member 2 according to the above-mentioned chemical formula X m H n The above temperature is merely an example in which the element X is boron, and 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) and consumed. 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, and the hydrogen can then be consumed in 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 heat of adsorption to embodiment 1. In embodiment 2, the same components as those in embodiment 1 are given the same reference numerals, and detailed descriptions thereof will be omitted.

[0019] <Configuration of hydrogen production system according to embodiment 2 of the present disclosure> The hydrogen production system according to the second embodiment of the present disclosure includes several specific configurations, as will be described later. FIG. 4 shows 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 such 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 absorbing 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 absorbing section 11. In this case, the heat recovery fluid 6 circulates between the heat recovery device 4 and the heat absorbing 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 the second embodiment of the present disclosure> Next, the operation of the hydrogen production system 1 according to the second embodiment 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 the first embodiment. Below, the operation different from the first embodiment 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 heat of adsorption AH in the heat utilization device 10 and by utilizing the waste 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 changes phase 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 form of 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), and therefore heat exchange between the heating fluid 13 and the hydrogen compound member 2 can be performed 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. As such a heating fluid 13, 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. When such a 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. For example, liquid ammonia can be used as this type of 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), and therefore heat exchange between the heat recovery fluid 6 and the hydrogen compound member 2 can be performed with a small temperature difference between them, allowing the heat of adsorption AH to be recovered efficiently 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 therefore heat exchange between the heat recovery fluid 6 and the hydrogen compound member 2 can be performed with a small temperature difference between them, and therefore the heat of adsorption AH can be efficiently recovered from the hydrogen compound member 2.

[0030] <Specific example of hydrogen production system according to embodiment 2 of the present disclosure> (Example 1) 5, the heat utilization device 10 is a gas turbine combined cycle power plant (GTCC) 10a. The GTCC 10a 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 to 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 the hydrogen 2a, and therefore the gas turbine 100 constitutes an oxygen consumer and a hydrogen consumer. Therefore, in this specific example 1, the GTCC 10a, which is the heat utilization device 10, is configured to include an oxygen consumer and a hydrogen consumer.

[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 part 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 part 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 so 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 as cooling medium N into a cooling air cooler that cools air bled from the compressor 101 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 bled 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 bled 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 bled 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 feedwater 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, cooled air cooler 109, cooled air cooler 110, and heat exchanger 303a (low-pressure economizer) in the exhaust heat recovery boiler 301. The cooling medium L, i.e., the feedwater supplied from the condenser 204, flows through the generator cooler 105 and lubricant oil cooler 108 in this order, 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 at two locations, exhaust gas) 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 the 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 unit 12 described above. Furthermore, if the heated fluid 13a (pressurized water) heated in the heat exchanger 303b or the like evaporates and becomes steam, the heated 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] Furthermore, as described above, the cooling medium N, after flowing into the heat recovery device 4 and recovering 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 in each of them while still containing the heat of adsorption AH. When a portion of the cooling medium flowing out of the heat exchanger 303a is configured to flow into the drum 304 that communicates with 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] (Example 2) 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, the liquid ammonia 430, which is the fuel for the gas engine 400, is preheated by heat exchange 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. 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 preheated liquid ammonia 431 may be heated and vaporized by heat exchange between the saturated vapor 450 and the preheated liquid ammonia. The saturated vapor 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 then returned to the heating device 9 as the heating fluid 13a containing the exhaust heat WH, and heats the hydrogen compound material 2 again. 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 then 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 13b 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 component 2. In such a configuration, the preheated liquid ammonia 431 flowing through the vaporizer 403 becomes the heat recovery fluid 6, which corresponds to the fluid that undergoes a phase change (vaporization) when the heat of adsorption AH is recovered from the hydrogen compound component 2 in the heat recovery device 4.

[0044] (Example 3) 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 is equipped with a carbon dioxide recovery unit 500 that recovers carbon dioxide from a gas 520 containing carbon dioxide (for example, the atmosphere or exhaust gas emitted from a combustion device, etc.), a carbon monoxide production unit 501 that produces carbon monoxide from carbon dioxide 521 recovered in the carbon dioxide recovery unit 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 unit 501 as raw materials, and a purification unit 503 that refines the crude hydrocarbons 524 produced in the FT reactor 502 to produce 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 it possible to reuse the absorption liquid for carbon dioxide absorption and also making it possible to utilize the separated carbon dioxide 521. 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 from the heat recovery fluid 6a containing the heat of adsorption AH into the absorption liquid, 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 a 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 the 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 so that the heating fluid 13b is supplied to the cooler 512 after the hydrogen compound component 2 is heated in the heating device 9. In the cooler 512 configured in this way, 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 into 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] (Example 4) In Example 4, as shown in Fig. 8, the heat utilization device 10 is a plant 10d that produces ammonia. The plant 10d includes a nitrogen separator 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 separator 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 absorbing 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 component 2 may be used as the raw material hydrogen 612. In this case, the reactor 601 consumes the hydrogen 612, and therefore serves as a hydrogen consumption device. Since the reaction (ammonia synthesis reaction) for synthesizing ammonia 613 from nitrogen 611 and hydrogen 612 is an exothermic reaction, the reactor 601 is provided with a cooler 603. The cooler 603 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 603 configured in this way, the reaction heat (exhaust heat WH) generated by the ammonia synthesis reaction is recovered by the heating fluid 13b, which becomes the heating fluid 13a and returns to the heating device 9 to heat the hydrogen compound component 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 the second embodiment, 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] For this reason, as shown in FIG. 9 , in a 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. Furthermore, 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 the third embodiment of the present disclosure> The third embodiment differs from the second embodiment 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 those of the second embodiment. Therefore, only the operations different from those of the second embodiment will be described. The heating fluid 13b after heating the hydrogen compound member 2 in the heating device 9 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 Figure 5, in a GTCC 10a, a gas turbine 100 supplies exhaust gas 100a containing exhaust heat after being expanded in a turbine 103 to extract work, 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 of the heat recovery boiler 301 in the following order from upstream to downstream of the flow of the exhaust gas 100a: 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 feedwater (pressurized water) in the above-mentioned order by each heat exchange element. 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, and heats 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 feedwater of the heat recovery boiler 301, evaporating the feedwater 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. On the other hand, as described in specific example 1 of embodiment 2, 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 embodiment 3).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 further exchanges heat 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 temperature of the exhaust gas 100a is higher than that of the hydrogen compound member 2 when hydrogen is released from the hydrogen compound member 2 that has adsorbed hydrogen, and the temperature of the feedwater (cooling media M) is lower than that of 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 costs 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 flow rate of the feedwater is high and a large amount of heat is required for heating. However, even in such a case where a large amount of heat is required for heating 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 material 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 given the same reference numerals, and detailed description thereof will be omitted.

[0062] <Configuration of hydrogen production system according to embodiment 4 of the present disclosure> As shown in FIG. 10 , the hydrogen production system 1 according to the fourth embodiment of the present disclosure includes, in addition to the hydrogen compound material 2, the water supply material 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 material 2 that is recovering the heat of adsorption AH using 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 into 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, the heat of the hydrogen compound material 2, which has a higher temperature than the exhaust heat WH, i.e., the heat of adsorption AH, from the heat recovery fluid 6b recovered from the exhaust heat WH in the first heat exchanger 20 can be recovered, thereby making it possible to effectively utilize the relatively high-temperature heat including the exhaust heat WH.

[0065] In the fourth embodiment, in which the temperature of the hydrogen compound component 2 is higher than that of the heating fluid 13a, the heat of adsorption AH of the heat recovery fluid 6 must be recovered from the hydrogen compound component 2 after heat exchange with the heating fluid 13a in order to obtain the above-described effects. If this order were reversed, as shown in FIG. 11 , the heat recovery fluid 6 would recover the heat of adsorption AH from the hydrogen compound component 2, causing the temperature of the heat recovery fluid 6 to rise from T0°C to T1°C between position P0, where the heat recovery fluid 6 flows into the heat recovery device 4, and position P1, where the heat recovery fluid 6 flows out of the heat recovery device 4. Next, when the heat recovery fluid 6 at T1°C exchanges heat with the heating fluid 13a, which has a lower temperature than the hydrogen compound component 2, in the first heat exchanger 20, the temperatures of both fluids would reach the same temperature, T3°C, at position P2 in the first heat exchanger 20. Therefore, the heat recovery fluid 6 would not be heated between position P2 and position P3, where the heat recovery fluid 6 flows out of the first heat exchanger 20.

[0066] In contrast, when the heat recovery fluid 6 is heated in the order shown in FIG. 10 , as shown in FIG. 12 , from position P0′ where the heat recovery fluid 6 flows into the first heat exchanger 20 to position P1′ where the heat recovery fluid 6 flows out of the first heat exchanger 20, the temperature of the heat recovery fluid 6 rises from temperature T0°C to T4°C due to heat exchange between the heat recovery fluid 6 and the heating fluid 13a. Next, the heat recovery fluid 6 at T4°C flows into the heat recovery unit 4, and the heat of adsorption AH is recovered from the hydrogen compound component 2, which has a higher temperature than the heating fluid 13a. As a result, the temperature of the heat recovery fluid 6 continues to rise until position P2′ where the heat recovery fluid 6 flows out of the heat recovery unit 4. In other words, the heat recovery fluid 6 can continue to absorb the heat of adsorption AH and the waste heat WH from position P0′ to position P2′. Therefore, the amount of heat absorbed by the heat recovery fluid 6 is greater than when the heat recovery fluid 6 exchanges heat with the heating fluid 13a after recovering the heat of adsorption AH from the hydrogen compound component 2.

[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 given the same reference numerals, and detailed description thereof will be omitted.

[0068] <Configuration of hydrogen production system according to embodiment 5 of the present disclosure> 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 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 during the recovery of the heat of adsorption AH by the heat recovery fluid 6b. The other configurations are the same as those of 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 into 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 therefore 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 heat recovery fluid 6 and the heating fluid 13a exchange heat from T0°C to T1°C between the position P0 where the heat recovery fluid 6 flows into the second heat exchanger 30 and the position P1 where the heat recovery fluid 6 flows out of the second heat exchanger 30. Next, when the heat recovery fluid 6 at T1°C recovers the heat of adsorption AH from the hydrogen compound member 2, which has a lower temperature than the heating fluid 13a, in the heat recovery device 4, the temperatures of the heat recovery fluid 6 and the hydrogen compound member 2 reach the same temperature, T3°C, at the position P2 in the heat exchanger 4. Therefore, the heat recovery fluid 6 is not heated between the position P2 and the position P3 where the heat recovery fluid 6 flows out of the heat recovery device 4.

[0072] 13 , as shown in FIG. 15 , the heat recovery fluid 6 recovers the heat of adsorption AH from the hydrogen compound component 2, and the temperature of the heat recovery fluid 6 rises from T0°C to T4°C between position P0′ where the heat recovery fluid 6 flows into the heat recovery unit 4 and position P1′ where the heat recovery fluid 6 flows out of the heat recovery unit 4. Next, the heat recovery fluid 6 at T4°C flows into the second heat exchanger 30 and exchanges heat with the heating fluid 13a, which has a higher temperature than the hydrogen compound component 2. As a result, the temperature of the heat recovery fluid 6 continues to rise until position P2′ where the heat recovery fluid 6 flows out of the second heat exchanger 30. That is, the heat recovery fluid 6 can continue to absorb the heat of adsorption AH and the waste heat WH from position P0′ to position P2′. Therefore, 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 component 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] <Configuration of hydrogen production system according to embodiment 6 of the present disclosure> 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 part 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 on which hydrogen is 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 on which hydrogen is adsorbed.

[0075] The configurations of the hydrogen compound component 2, the water supply component 3, and the heating device 9 can be the same as those of the first to fifth embodiments. The configurations of the oxygen consuming device 41 and the hydrogen consuming device 42 are not particularly limited. For example, the oxygen consuming 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, or a plant using a gasification reaction process. When the oxygen consuming 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 water 7 into hydrogen and oxygen in the presence of the hydrogen compound component 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, etc.). 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 is decomposed 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. In the heating device 9, heat is exchanged between the hydrogen compound member 2 and the heating fluid 13, thereby heating the hydrogen compound member 2 and releasing hydrogen 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 in the oxygen consuming device 41. Note that 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, in the reactor 44, oxygen and methane react by the reaction represented by the following reaction formula (1), and a portion of the methane is decomposed by 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. CH4 + 2O2 → 2H2O + CO2 (1) CH4 + 2H2O → CO2 + 4H2 (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). NH3+(3 / 4)O2→(3 / 2)H2O+(1 / 2)N2...(3) NH3→(3 / 2)H2+(1 / 2)N2···(4)

[0079] When the oxygen consuming device 41 is an ATR device 41a, the oxygen 5b produced by decomposition of a portion of the water 7 in the presence of the hydrogen compound component 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 decomposition of a portion of the water 7 in the presence of the hydrogen compound component 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 a 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 a 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 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 to 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 denoted 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 FIG. 17 , a hydrogen production system 50 according to a seventh 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, 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 using 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 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 the seventh embodiment of the present disclosure> Next, the operation of the hydrogen production system 50 according to the seventh 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 is decomposed 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 collected 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 between the waste heat-containing fluid 58a and the refrigerant occurs, whereby the refrigerant is heated and evaporated, while the waste heat-containing fluid 58a is cooled and returned 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 that has flowed 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-adsorbed hydrogen compound member 2. 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 reacts 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. 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 FIG. 18 , a hydrocarbon production system 60 according to the first 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, 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 member 2 is adsorbed by the hydrogen compound member 2, a heating device 9 that heats the hydrogen compound member 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 member 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. aCO2+bH2→C a H b +cH2O (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, respectively.

[0095] In the hydrocarbon production system 60 according to the first embodiment of the present disclosure, the thermal efficiency is also 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 component 2 is adsorbed by the hydrogen compound component 2, thereby reducing the operating costs of the hydrocarbon production system 60.

[0096] (Embodiment 2) The hydrocarbon production system according to the second embodiment 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 the seventh embodiment, 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 the second embodiment, the same components as those in the hydrogen production system according to the seventh embodiment and the hydrocarbon production system according to the first embodiment 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 the second 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, 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 in specific example 2 of embodiment 2 is an engine that uses ammonia as fuel, but the hydrocarbon consumption device 71 may also be a power generation system including a gas engine that uses hydrocarbons such as methane or ethane as fuel. In this case, a waste heat recovery heat exchanger (corresponding to the waste heat recovery heat exchanger 405 in specific example 2 of embodiment 2) for recovering heat from the exhaust gas discharged from the gas engine corresponds to the waste heat recovery section 73 that recovers the waste 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 between the hydrogen compound material 2 and the heating fluid 13a, while the heating fluid 13a becomes a cooled heating fluid 13b. By the same operation as that of the hydrocarbon production system 60, 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. 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 become the heated fluid 13a (which has absorbed heat H). The operation of heating the heating fluid 13b by the heat pump 51 is the same as that 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 members 2 to release hydrogen from the hydrogen compound members 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 members 2 when hydrogen 2a is released from the hydrogen compound members 2, it is possible to use the low-temperature exhaust heat WH to produce hydrogen using the hydrogen compound members 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 member (2); a water supply member (3) that supplies water (7) to the hydrogen compound member (2); a heat recovery device (4) for recovering heat of adsorption (AH) generated when the hydrogen generated by decomposing a 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); Equipped with.

[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 embodiment is the hydrogen production system according to [1], 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 is not decomposed into hydrogen and oxygen from the water (7) and a heat recovery fluid (6), 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 according to [1] or [2], 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 a waste heat recovery section (12) that recovers waste heat (WH); a heating device (9) for heating 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); Equipped with.

[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 embodiment is the hydrogen production system according to [3], 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 embodiment is the hydrogen production system according to [3], 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 embodiment is the hydrogen production system according to any one of [3] to [5], 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], The heat recovery fluid (6) is 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).

[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 embodiment is the hydrogen production system according to [3], The heat absorption part (11) a first heat absorption portion (11b); a second heat absorbing portion (11c) different from the first heat absorbing portion (11b); Including, The heat of adsorption (AH) recovered in the heat recovery fluid (6) is absorbed in the first heat absorption section (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 in the second heat absorption section (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 embodiment is the hydrogen production system according to [1], 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 a waste heat recovery section (12) that recovers waste heat (WH); a first heat exchanger (20) for exchanging 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); Equipped with The temperature of the heating fluid (13) before heat exchange 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 the heat of adsorption (AH) is recovered.

[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 the hydrogen compound material or the heating fluid, thereby improving the heat utilization efficiency in the heat utilization device.

[0121]

[10] A hydrogen production system according to yet another embodiment is the hydrogen production system according to [1], 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 a waste heat recovery section (12) that recovers waste heat (WH); a second heat exchanger (30) for exchanging 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); Equipped with The temperature of the heating fluid (13) before heat exchange 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 the hydrogen compound material or the heating fluid, thereby improving the heat utilization efficiency in the heat utilization device.

[0123]

[11] A hydrogen production system according to another embodiment includes: A hydrogen compound member (2); a water supply member (3) that supplies water (7) to the hydrogen compound member (2); an oxygen consuming device (41) for consuming the oxygen (5b) produced by decomposing a part of the water (7) into hydrogen and oxygen in the presence of the hydrogen compound member (2); Equipped with.

[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 embodiment is the hydrogen production system according to

[11] , a heating device (9) for heating the hydrogen compound member (2) on 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); a hydrogen consuming device (42) that consumes hydrogen released from the hydrogen compound member (2) to which hydrogen has been adsorbed; Equipped with.

[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 according to

[11] , The oxygen consumer (41) includes a reactor (44) for reacting oxygen (5b) produced by decomposition of a portion of the water (7) in the presence of the hydrogen compound component (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 according to

[12] , The oxygen consuming device is a reactor (44) for reacting oxygen (5b) produced by decomposition of a portion of the water (7) in the presence of the hydrogen compound component (2) with a hydrogen-containing compound (45) containing at least a hydrogen atom; a waste heat recovery section (43) for exchanging heat between an outflow gas (46) flowing out from the reactor (44) and the heating fluid (13) after heat exchange with the hydrogen compound material (2) in the heating device (9); It is equipped with:

[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 member (2); a water supply member (3) that supplies water (7) to the hydrogen compound member (2); a hydrogen consuming device (42) that consumes the hydrogen (2a) produced by decomposing a part of the water (7) into hydrogen and oxygen in the presence of the hydrogen compound member (2); a heating device (9) for heating the hydrogen compound member (2) on which the hydrogen is adsorbed by heat exchange between a heating fluid (13) and the hydrogen compound member (2); a heat pump (51) for heating the heating fluid (13) with exhaust heat (WH) generated in the hydrogen consumption device (42); Equipped with.

[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 member (2); a water supply member (3) that supplies water (7) to the hydrogen compound member (2); a gas supply device (61) for supplying a carbon dioxide-containing gas (62) containing carbon dioxide to the hydrogen compound member (2); a hydrocarbon consuming device (71) that consumes hydrocarbons (72) 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 the carbon dioxide; a heating device (9) for heating the hydrogen compound member (2) on which the hydrogen is adsorbed by heat exchange between a heating fluid (13) and the hydrogen compound member (2); a heat pump (51) for heating the heating fluid (13) by using waste heat (WH) generated in the hydrocarbon consumption device (71); Equipped with.

[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] Another aspect of the hydrocarbon production system includes: A hydrogen compound member (2); a water supply member (3) that supplies water (7) to the hydrogen compound member (2); a heat recovery device (4) for recovering adsorption heat (AH) generated when hydrogen generated by decomposing a part of the water (7) into hydrogen and oxygen in the presence of the hydrogen compound component (2) is adsorbed by the hydrogen compound component (2); a heating device (9) for heating the hydrogen compound member (2) on which the hydrogen is adsorbed; a gas supply device (61) for supplying a carbon dioxide-containing gas (62) containing carbon dioxide to the hydrogen compound member (2); Equipped with.

[0136]

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

[13] , In the reactor (44), the oxygen (5b) is reacted with a portion of the hydrogen-containing compound (45) to generate heat, which is used to decompose at least a portion of the remaining hydrogen-containing compound (45) to produce additional hydrogen.

[0137]

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

[18] , Further comprising a separation device; The separation device is a device for separating substances other than hydrogen from an effluent gas (46) that contains hydrogen produced by decomposing at least a portion of the remaining hydrogen-containing compound (45) and flows 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. [Explanation of symbols]

[0139] 1. Hydrogen production system 2 Hydrogen compound materials 2a Hydrogen 3 Water supply components 4. Heat recovery device 5a water 5b Oxygen 6. Heat recovery fluid 7 water 9 Heating device 10 Heat utilization equipment 11 Heat absorption part 11b First heat absorption part 11c Second heat absorption part 12 Exhaust heat recovery section 13 Heating fluid 20 1st 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 compounds 46 Gas Leak 50 Hydrogen Production System 51 Heat Pump 60 Hydrocarbon Production Systems 61 Gas supply equipment 62 Carbon dioxide-containing gases 70 Hydrocarbon Production Systems 71 Hydrocarbon consumption device 72 Hydrocarbons AH heat of adsorption WH heat dissipation

Claims

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

2. 2. The hydrogen production system according to 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, and a heat exchanger that performs heat exchange between the oxygen and the heat recovery fluid.

3. a heat utilization device including a heat absorption unit that absorbs the heat of adsorption recovered in the heat recovery fluid in the heat recovery device, and a waste heat recovery unit that recovers waste heat; a heating device that heats the hydrogen compound member in 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; The hydrogen production system according to claim 1 or 2, comprising:

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. 4. 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. 4. 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 heat absorption part is A first heat absorption portion; a second heat absorption section different from the first heat absorption section; Including, 4. The hydrogen production system according to claim 3, wherein the heat of adsorption recovered in the heat recovery fluid is absorbed in the first heat absorption section, 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 section.

9. a heat utilization device including a heat absorption unit that absorbs the heat of adsorption recovered in the heat recovery fluid in the heat recovery device, and a waste heat recovery unit that recovers waste heat; a first heat exchanger in which the heat recovery fluid before recovering the heat of adsorption in the heat recovery device exchanges heat with a heating fluid from which the exhaust heat has been recovered in the exhaust heat recovery section; Equipped with 2. The hydrogen production system according to claim 1, wherein the temperature of the heating fluid before heat exchange 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 heat utilization device including a heat absorption unit that absorbs the heat of adsorption recovered in the heat recovery fluid in the heat recovery device, and a waste heat recovery unit that recovers waste heat; a second heat exchanger in which the heat recovery fluid after recovering the heat of adsorption in the heat recovery device exchanges heat with a heating fluid from which the exhaust heat has been recovered in the exhaust heat recovery section; Equipped with The hydrogen production system according to claim 1 , 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 compound member; a water supply member for supplying water to the hydrogen compound member; an oxygen consuming device that consumes the oxygen produced by decomposing a portion of the water into hydrogen and oxygen in the presence of the hydrogen compound member; A hydrogen production system comprising:

12. a heating device that heats the hydrogen compound member on 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; a hydrogen consuming device that consumes hydrogen released from the hydrogen compound member to which hydrogen has been adsorbed; The hydrogen production system according to claim 11 , comprising:

13. 12. 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 oxygen consuming device is a reactor for reacting oxygen generated 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; a waste heat recovery section for exchanging heat between the outflow gas flowing out from the reactor and the heating fluid after heat exchange with the hydrogen compound member in the heating device; The hydrogen production system according to claim 12, comprising:

15. a hydrogen compound member; a water supply member for supplying water to the hydrogen compound member; a hydrogen consuming device that consumes the hydrogen generated by decomposing a portion of the water into hydrogen and oxygen in the presence of the hydrogen compound member; a heating device that heats the hydrogen compound member on which the hydrogen is adsorbed by heat exchange between a heating fluid and the hydrogen compound member; a heat pump that heats the heating fluid using exhaust heat generated in the hydrogen consumption device; A hydrogen production system comprising:

16. a hydrogen compound member; a water supply member for supplying water to the hydrogen compound member; a gas supply device for supplying a carbon dioxide-containing gas containing carbon dioxide to the hydrogen compound member; a hydrocarbon consuming device that consumes hydrocarbons produced by decomposing a portion of the water into hydrogen and oxygen in the presence of the hydrogen compound member and by reacting the hydrogen with the carbon dioxide; a heating device that heats the hydrogen compound member on which the hydrogen is adsorbed by heat exchange between a heating fluid and the hydrogen compound member; a heat pump that heats the heating fluid using exhaust heat generated in the hydrocarbon consumption device; A hydrocarbon production system comprising:

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

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