Hydrogenation reaction apparatus and control apparatus

Abstract

To provide a hydrogen supply system capable of efficiently initiating a system while suppressing loss of a raw material and generated hydrogen.SOLUTION: In a hydrogen supply system 100 according to this embodiment, a dehydrogenation reaction part 3 obtains a hydrogen-containing gas by subjecting a raw material containing a hydride to a dehydrogenation reaction. The dehydrogenation reaction part 3 performs the dehydrogenation reaction while a catalyst is heated. Here, when the generation of hydrogen-containing gas in the dehydrogenation reaction part 3 is stopped, a control part 50 circulates a non-reactive fluid through a circulation system 40. In this case, the dehydrogenation reaction part 3 can remain in standby mode while maintaining the temperature, by passing the non-reactive fluid instead of the raw material, without performing the dehydrogenation reaction. Since the dehydrogenation reaction part 3 does not perform the dehydrogenation reaction, loss of raw material and hydrogen can be suppressed. Furthermore, by maintaining the temperature of the dehydrogenation reaction while operating in standby mode, the hydrogen supply system 100 can be started promptly.SELECTED DRAWING: Figure 3

Description

[Technical field]

[0001] The present invention relates to a hydrogen supply system that supplies hydrogen. [Background technology]

[0002] Known conventional hydrogen supply systems include, for example, the one disclosed in Patent Document 1. The hydrogen supply system of Patent Document 1 includes a tank for storing a hydride of an aromatic hydrocarbon as a raw material, a dehydrogenation reaction section for obtaining hydrogen by dehydrogenating the raw material supplied from the tank, a gas-liquid separation section for separating the hydrogen obtained in the dehydrogenation reaction section into gas and liquid, and a hydrogen purification section for purifying the hydrogen obtained by gas-liquid separation. [Prior art documents] [Patent documents]

[0003] [Patent Document 1] JP 2006-232607 A Summary of the Invention [Problem to be solved by the invention]

[0004] In the hydrogen supply system described above, when the generation of hydrogen-containing gas in the dehydrogenation reaction section is stopped, a start-up time is required to start the system when the generation of hydrogen-containing gas is resumed next time. It is desired to shorten such a start-up time. Here, for example, in the steam reforming method, in order to start the system early, the reformer may be heated with fuel (no raw material is input) while inert nitrogen gas or product hydrogen gas is input and circulated into the reformer and placed on standby. When starting up and starting hydrogen production, if operation is performed with the minimum load that can maintain heat balance within the system, a standby method of inputting raw material into the reformer is adopted. However, such a method has a problem in that the reaction in the reforming section proceeds, resulting in loss of raw material and generated hydrogen.

[0005] The present invention has been made to solve the above-mentioned problems, and has an object to provide a hydrogen supply system that can efficiently start up the system while suppressing loss of raw materials and generated hydrogen. [Means for solving the problem]

[0006] In order to solve the above problems, the hydrogen supply system of the present invention is a hydrogen supply system that supplies hydrogen, and includes a dehydrogenation reaction section that obtains a hydrogen-containing gas by dehydrogenating a raw material containing a hydride, a circulation system that circulates an inactive fluid to the dehydrogenation reaction section, and a control section that controls the hydrogen supply system, and when the generation of the hydrogen-containing gas in the dehydrogenation reaction section is stopped, the control section circulates the inactive fluid in the circulation system.

[0007] In the hydrogen supply system, the dehydrogenation reaction section obtains hydrogen-containing gas by dehydrogenating a raw material containing a hydride. The dehydrogenation reaction section performs the dehydrogenation reaction while the catalyst is heated. Here, when the control section stops the generation of the hydrogen-containing gas in the dehydrogenation reaction section, it circulates an inactive fluid in the circulation system. In this case, the dehydrogenation reaction section can wait while maintaining the temperature without performing the dehydrogenation reaction by passing an inactive fluid instead of the raw material. Since the dehydrogenation reaction section does not perform the dehydrogenation reaction, loss of raw material and hydrogen can be suppressed. In addition, by keeping the system in standby operation while maintaining the temperature of the dehydrogenation reaction, the hydrogen supply system can be started up quickly. As described above, the system can be started up efficiently while suppressing loss of raw material and generated hydrogen.

[0008] The circulation system may circulate the dehydrogenation product produced by the dehydrogenation reaction. In this case, the fluid produced in the dehydrogenation reaction section can be used as it is as a circulation fluid during standby.

[0009] The circulatory system may circulate a fluid from an external source, in which case an appropriate amount of the fluid may be circulated through the circulatory system. Effect of the Invention

[0010] According to the present invention, it is possible to provide a hydrogen supply system that can efficiently start up the system while suppressing loss of raw materials and generated hydrogen. [Brief description of the drawings]

[0011] [Figure 1] 1 is a block diagram showing a configuration of a hydrogen supply system according to an embodiment of the present invention. [Diagram 2] FIG. 2 is a block diagram showing the operation of the hydrogen supply system in a normal operating state. [Diagram 3] FIG. 4 is a block diagram showing the operation of the hydrogen supply system in a standby state. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0012] DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS A preferred embodiment of the hydrogen supply system according to the present invention will now be described in detail with reference to the drawings. In the following description, the same or corresponding parts are designated by the same reference numerals, and duplicated description will be omitted.

[0013] FIG. 1 is a block diagram showing the configuration of a hydrogen supply system according to an embodiment of the present invention. The hydrogen supply system 100 uses an organic compound (liquid at room temperature) as a raw material. In the process of hydrogen purification, the raw organic compound (liquid at room temperature) is dehydrogenated and a dehydrogenation product (organic compound (liquid at room temperature)) is removed. An example of the organic compound as the raw material is organic hydride. A suitable example of the organic hydride is a hydride obtained by reacting hydrogen, which is produced in large quantities in oil refineries, with aromatic hydrocarbons. In addition, the organic hydride is not limited to aromatic hydrogenated compounds, and there is also a system of 2-propanol (which produces hydrogen and acetone). The organic hydride can be transported to the hydrogen supply system 100 as a liquid fuel by a tanker truck or the like, similar to gasoline. In this embodiment, methylcyclohexane (hereinafter referred to as MCH) is used as the organic hydride. In addition, aromatic hydrocarbon hydrides such as cyclohexane, dimethylcyclohexane, ethylcyclohexane, decalin, methyldecalin, dimethyldecalin, and ethyldecalin can be used as organic hydrides (aromatic compounds are particularly suitable examples with high hydrogen content). The hydrogen supply system 100 can supply hydrogen to fuel cell vehicles (FCVs) and hydrogen engine vehicles. It is also applicable to the production of hydrogen from liquid hydrocarbon raw materials such as natural gas containing methane as the main component, LPG containing propane as the main component, or gasoline, naphtha, kerosene, and diesel.

[0014] As shown in FIG. 1, the hydrogen supply system 100 according to the present embodiment includes a liquid transfer pump 1, a heat exchanger 2, a dehydrogenation reaction unit 3, a heater 4, a gas-liquid separator 6, a compressor 7, and a hydrogen purifier 8. Among these, the liquid transfer pump 1, the heat exchanger 2, and the dehydrogenation reaction unit 3 belong to a hydrogen production unit 10 that produces a hydrogen-containing gas. The gas-liquid separator 6, the compressor 7, and the hydrogen purifier 8 belong to a hydrogen purity adjuster 11 that increases the purity of hydrogen. The hydrogen supply system 100 also includes lines L1 to L12. In this embodiment, MCH is used as a raw material, and the dehydrogenation product removed in the hydrogen purification process is toluene. In reality, not only toluene but also unreacted MCH and small amounts of by-products and impurities are present, but in this embodiment, they are mixed with toluene and behave the same as toluene. Therefore, in the following description, what is referred to as "toluene" includes unreacted MCH and by-products.

[0015] Lines L1 to L12 are flow paths through which MCH, toluene, hydrogen-containing gas, off-gas, high-purity hydrogen, or a heating medium passes. Line L1 is a line for liquid transfer pump 1 to pump MCH from an MCH tank (not shown), and connects liquid transfer pump 1 to the MCH tank. Line L2 connects liquid transfer pump 1 to dehydrogenation reaction section 3. Line L3 connects dehydrogenation reaction section 3 to gas-liquid separation section 6. Line L4 connects gas-liquid separation section 6 to a toluene tank (not shown). Line L5 connects gas-liquid separation section 6 to compression section 7. Line L6 connects compression section 7 to hydrogen purification section 8. Line L7 connects hydrogen purification section 8 to a supply destination of off-gas. Line L8 connects hydrogen purification section 8 to a supply device for purified gas (not shown). Lines L11 and L12 connect heating section 4 to dehydrogenation reaction section 3. The lines L11 and L12 allow the heat transfer medium to flow.

[0016] The liquid transfer pump 1 supplies the raw material MCH to the dehydrogenation reaction section 3. The MCH transported from outside by a tank truck or the like is stored in an MCH tank. The MCH stored in the MCH tank is supplied to the dehydrogenation reaction section 3 by the liquid transfer pump 1 via lines L1 and L2.

[0017] The heat exchanger 2 exchanges heat between the MCH flowing through the line L2 and the hydrogen-containing gas flowing through the line L3. The hydrogen-containing gas coming out of the dehydrogenation reaction section 3 has a higher temperature than the MCH. Therefore, in the heat exchanger 2, the MCH is heated by the heat of the hydrogen-containing gas. As a result, the MCH is supplied to the dehydrogenation reaction section 3 in a state where its temperature has increased. The MCH is supplied to the dehydrogenation reaction section 3 together with the off-gas supplied from the hydrogen purification section 8 via the line L7.

[0018] The dehydrogenation reaction section 3 is a device that obtains hydrogen by dehydrogenating MCH. That is, the dehydrogenation reaction section 3 is a device that extracts hydrogen from MCH by a dehydrogenation reaction using a dehydrogenation catalyst. The dehydrogenation catalyst is not particularly limited, but is selected from, for example, a platinum catalyst, a palladium catalyst, and a nickel catalyst. These catalysts may be supported on a carrier such as alumina, silica, and titania. The reaction of organic hydrides is a reversible reaction, and the direction of the reaction changes depending on the reaction conditions (temperature, pressure) (subject to the constraints of chemical equilibrium). On the other hand, the dehydrogenation reaction is an endothermic reaction that always increases the number of molecules. Therefore, high temperature and low pressure conditions are advantageous. Since the dehydrogenation reaction is an endothermic reaction, heat is supplied to the dehydrogenation reaction section 3 from the heating section 4 via a heat medium circulating through lines L11 and L12. The dehydrogenation reaction section 3 has a mechanism that allows heat exchange between the MCH flowing through the dehydrogenation catalyst and the heat medium from the heating section 4. The hydrogen-containing gas extracted in the dehydrogenation reaction section 3 is supplied to the gas-liquid separation section 6 via a line L3. The hydrogen-containing gas in the line L3 is supplied to the gas-liquid separation section 6 in a state where it contains toluene, which is a liquid, as a mixture.

[0019] The heating section 4 heats the heat medium and supplies the heat medium to the dehydrogenation reaction section 3 via a line L11. The heated heat medium is returned to the heating section 4 via a line L12. The heat medium is not particularly limited, and oil or the like may be used. The heating section 4 may be any type that can heat the dehydrogenation reaction section 3. For example, the heating section 4 may directly heat the dehydrogenation reaction section 3, or may heat the MCH supplied to the dehydrogenation reaction section 3 by heating the line L2. The heating section 4 may heat both the dehydrogenation reaction section 3 and the MCH supplied to the dehydrogenation reaction section 3. For example, a burner or an engine may be used as the heating section 4.

[0020] The gas-liquid separation unit 6 is a tank that separates toluene from the hydrogen-containing gas. The gas-liquid separation unit 6 separates hydrogen, which is a gas, from toluene, which is a liquid, by storing the hydrogen-containing gas containing toluene as a mixture. The hydrogen-containing gas supplied to the gas-liquid separation unit 6 is cooled by the heat exchange unit 2. The gas-liquid separation unit 6 may be cooled by a cooling medium from a cold heat source. In this case, the gas-liquid separation unit 6 has a mechanism capable of exchanging heat between the hydrogen-containing gas in the gas-liquid separation unit 6 and the cooling medium from the cold heat source. The toluene separated by the gas-liquid separation unit 6 is supplied to a toluene tank (not shown) via a line L4. The hydrogen-containing gas separated by the gas-liquid separation unit 6 is supplied to the hydrogen purification unit 8 via lines L5 and L6 by the pressure of the compression unit 7. When the hydrogen-containing gas is cooled, a part of the gas (toluene) is liquefied, and the gas-liquid separation unit 6 can separate the toluene from the non-liquefied gas (hydrogen). The lower the gas temperature, the more efficient the separation becomes, and increasing the pressure further promotes the liquefaction of toluene.

[0021] The hydrogen purification unit 8 removes the dehydrogenation product (toluene in this embodiment) from the hydrogen-containing gas obtained in the dehydrogenation reaction unit 3 and separated into gas and liquid in the gas-liquid separation unit 6. In this way, the hydrogen purification unit 8 purifies the hydrogen-containing gas to obtain high-purity hydrogen (purified gas). The obtained purified gas is supplied to line L8. The off-gas generated in the hydrogen purification unit 8 is supplied to the dehydrogenation reaction unit 3 via line L7.

[0022] The hydrogen purification unit 8 varies depending on the hydrogen purification method employed, but specifically, when membrane separation is used as the hydrogen purification method, it is a hydrogen separation device equipped with a hydrogen separation membrane, and when the PSA (pressure swing adsorption) method or the TSA (temperature swing adsorption) method is used, it is an adsorption removal device equipped with multiple adsorption towers that store adsorbents that adsorb impurities.

[0023] A case where the hydrogen purification unit 8 uses membrane separation will be described. In this method, a hydrogen-containing gas pressurized to a predetermined pressure by a compression unit (not shown) is made to pass through a membrane heated to a predetermined temperature, thereby removing dehydrogenation products and obtaining high-purity hydrogen gas (purified gas). The pressure of the permeated gas that has permeated the membrane is reduced compared to the pressure before permeating the membrane. On the other hand, the pressure of the non-permeated gas that has not permeated the membrane is approximately the same as the predetermined pressure before permeating the membrane. At this time, the non-permeated gas that has not permeated the membrane corresponds to the off-gas of the hydrogen purification unit 8.

[0024] There are no particular limitations on the type of membrane used in hydrogen purification unit 8, and it is possible to use porous membranes (those that separate by molecular flow, those that separate by surface diffusion flow, those that separate by capillary condensation, those that separate by molecular sieving, etc.) or non-porous membranes. As the membrane used in hydrogen purification unit 8, for example, metal membranes (PbAg-based, PdCu-based, Nb-based, etc.), zeolite membranes, inorganic membranes (silica membranes, carbon membranes, etc.), and polymer membranes (polyimide membranes, etc.) can be used.

[0025] A case where the PSA method is adopted as a removal method of the hydrogen purification unit 8 will be described. The adsorbent used in the PSA method has the property of adsorbing toluene contained in the hydrogen-containing gas under high pressure and desorbing the adsorbed toluene under low pressure. The PSA method utilizes such a property of the adsorbent. That is, by increasing the pressure inside the adsorption tower, the toluene contained in the hydrogen-containing gas is adsorbed by the adsorbent and removed, thereby obtaining high-purity hydrogen gas (purified gas). When the adsorption function of the adsorbent in the adsorption tower is reduced by adsorption, the pressure inside the adsorption tower is reduced to desorb the toluene adsorbed on the adsorbent, and at the same time, a part of the removed purified gas is reversed to remove the desorbed toluene from the adsorption tower, thereby regenerating the adsorption function of the adsorbent (at this time, the hydrogen-containing gas containing at least hydrogen and toluene discharged by removing toluene from the adsorption tower corresponds to the off-gas from the hydrogen purification unit 8).

[0026] A case where the TSA method is adopted as the removal method of the hydrogen purification unit 8 will be described. The adsorbent used in the TSA method has the property of adsorbing toluene contained in the hydrogen-containing gas at room temperature and desorbing the adsorbed toluene at high temperature. The TSA method utilizes such a property of the adsorbent. That is, by bringing the temperature inside the adsorption tower to room temperature, the toluene contained in the hydrogen-containing gas is adsorbed by the adsorbent and removed, thereby obtaining high-purity hydrogen gas (high-purity hydrogen). When the adsorption function of the adsorbent in the adsorption tower is reduced by adsorption, the toluene adsorbed by the adsorbent is desorbed by raising the temperature inside the adsorption tower, and the desorbed toluene is removed from the adsorption tower by backflowing a part of the removed high-purity hydrogen, thereby regenerating the adsorption function of the adsorbent (at this time, the hydrogen-containing gas containing at least hydrogen and toluene discharged by removing toluene from the adsorption tower corresponds to the off-gas from the hydrogen purification unit 8).

[0027] Next, characteristic parts of the above-mentioned hydrogen supply system 100 will be described with reference to Fig. 2 and Fig. 3. Fig. 2 is a block diagram showing the operation of the hydrogen supply system 100 in a normal operating state. Fig. 3 is a block diagram showing the operation of the hydrogen supply system 100 in a standby state. As shown in Figs. 2 and 3, the hydrogen supply system 100 includes a circulation system 40 and a control unit 50.

[0028] The circulation system 40 is a system that circulates a reactively inert fluid to the dehydrogenation reaction section 3. The reactively inert fluid is a fluid that, even if supplied to the dehydrogenation reaction section 3, hardly reacts with the dehydrogenation catalyst in the dehydrogenation reaction section 3. The circulation system 40 includes a line L20 that extends from the middle of the line L4 to the middle of the line L1. The upstream side of the line L4 from the connection point with the line L20 is referred to as the first part L4a, and the downstream side of the connection point is referred to as the second part L4b. The upstream side of the line L1 from the connection point with the line L20 is referred to as the first part L1a, and the downstream side of the connection point is referred to as the second part L1b. In this case, the circulation system 40 is composed of the line L20, the second part L1b of the line L1, the line L2, the line L3, and the first part L4a of the line L4.

[0029] A valve 21 is provided in the first portion L1a of the line L2. The valve 21 switches between opening and closing to switch between supplying and stopping the supply of the raw material to the dehydrogenation reaction section 3. A valve 22 is provided in the second portion L4b of the line L4. The valve 22 switches between opening and closing to switch between discharging toluene from the gas-liquid separation section 6 and stopping the discharge. A valve 23 is provided in the line L5. The valve 23 switches between supplying and stopping the supply of hydrogen-containing gas from the gas-liquid separation section 6 to the downstream side. A valve 24 is provided in the line L20. The valve 24 switches between opening and closing to switch between supplying and stopping the supply of the reactively inert fluid to the dehydrogenation reaction section 3.

[0030] The circulation system 40 circulates toluene (dehydrogenation product) produced by the dehydrogenation reaction. That is, the circulation system 40 circulates toluene separated in the gas-liquid separation section 6 after the dehydrogenation reaction in the dehydrogenation reaction section 3 is completed. Since the toluene is produced from the raw material by the dehydrogenation reaction, even if it is supplied again to the dehydrogenation reaction section 3, the dehydrogenation reaction does not occur in the dehydrogenation reaction section 3. Note that if a small amount of raw material remains in the toluene, the raw material will undergo a dehydrogenation reaction, but in this specification, toluene with a small amount of raw material remaining therein is also treated as a fluid that is inactive for reaction.

[0031] When the generation of hydrogen-containing gas in the dehydrogenation reaction section 3 is stopped, the control section 50 controls the circulation system 40 to circulate an inactive fluid. The control section 50 is electrically connected to the valves 21, 22, 23, and 24. The control section 50 controls the flow of the fluid in the hydrogen supply system 100 by transmitting a signal to the valves 21, 22, 23, and 24 to switch between opening and closing.

[0032] Specifically, as shown in FIG. 2, in a normal operating state, the control unit 50 opens the valve 21 of the line L1, opens the valve 22 of the line L4, opens the valve 23 of the line L5, and closes the valve 24 of the line L20. As a result, the raw material flows through the first portion L1a of the line L1, flows through the second portion L1b of the line L1, and is supplied to the dehydrogenation reaction unit 3 through the liquid transfer pump 1 and the line L2 (see F1). In addition, the hydrogen-containing gas generated in the dehydrogenation reaction unit 3 flows through the line L3 and is supplied to the gas-liquid separation unit 6. The toluene separated in the gas-liquid separation unit 6 flows through the line L4 and is discharged (see F2). The hydrogen-containing gas from which the toluene has been separated in the gas-liquid separation unit 6 is supplied to the downstream side through the line L5 (see F3). At this time, since the valve 24 of the line L20 is closed, the toluene does not flow through the line L20 and is not supplied to the dehydrogenation reaction unit 3. As described above, the toluene produced in the dehydrogenation reaction section 3 is discharged from the gas-liquid separation section 6 without being circulated through the circulation system 40.

[0033] When the supply of hydrogen is stopped, the dehydrogenation reaction in the dehydrogenation reaction section 3 is also stopped. In this case, the dehydrogenation reaction in the dehydrogenation reaction section 3 is put into a standby state so that the dehydrogenation reaction in the dehydrogenation reaction section 3 can be quickly resumed when the supply of hydrogen is started again. In the standby state, as shown in FIG. 3, the control section 50 closes the valve 21 in the line L1, closes the valve 22 in the line L4, closes the valve 23 in the line L5, and opens the valve 24 in the line L20. As a result, the passage of the raw material from the first part L1a of the line L1 is restricted by the valve 21. Furthermore, the passage of the toluene separated in the gas-liquid separation section 6 is restricted by the valve 22 in the second part L4b of the line L4, and passes from the first part L4a of the line L4 to the line L20 (see F5). Then, the toluene passes from the line L20 through the second part L1b of the line L1 and is supplied to the dehydrogenation reaction section 3 via the liquid transfer pump 1 and the line L2 (see F6). Toluene is heated by the effect of the heat medium from the heating section 4 (see FIG. 1). The heated toluene does not react in the dehydrogenation reaction section 3, but passes through the dehydrogenation reaction section 3 while suppressing a decrease in the temperature of the dehydrogenation catalyst. The toluene leaving the dehydrogenation reaction section 3 flows through the line L3, the gas-liquid separation section 6, and the first portion L4a of the line L4, and is repeatedly circulated through the circulation system 40.

[0034] Then, when the supply of hydrogen is resumed and the dehydrogenation reaction in the dehydrogenation reaction unit 3 is resumed, the control unit 50 switches the valves 21, 22, 23, and 24 between open and closed states to achieve the state shown in Fig. 2. At this time, since the temperature decrease of the dehydrogenation reaction catalyst in the dehydrogenation reaction unit 3 was suppressed during standby, the dehydrogenation reaction can be resumed promptly.

[0035] Next, the operation and effect of the hydrogen supply system 100 according to this embodiment will be described.

[0036] First, a hydrogen supply system according to a comparative example will be described. In the hydrogen supply system according to the comparative example, even in a standby state, the raw material is supplied to the dehydrogenation reaction section 3 to suppress a decrease in the temperature of the dehydrogenation catalyst. However, the hydrogen supply system according to the comparative example has a problem in that the reaction in the dehydrogenation reaction section 3 proceeds, resulting in a loss of the raw material and the generated hydrogen.

[0037] In contrast, in the hydrogen supply system 100 according to the present embodiment, the dehydrogenation reaction section 3 obtains hydrogen-containing gas by dehydrogenating the raw material containing hydride. The dehydrogenation reaction section 3 performs the dehydrogenation reaction in a state in which the catalyst is heated. Here, when the control section 50 stops the generation of the hydrogen-containing gas in the dehydrogenation reaction section 3, it circulates an inactive fluid in the circulation system 40. In this case, the dehydrogenation reaction section 3 can wait while maintaining the temperature without performing the dehydrogenation reaction by passing an inactive fluid instead of the raw material. Since the dehydrogenation reaction section 3 does not perform the dehydrogenation reaction, the loss of the raw material and hydrogen can be suppressed. In addition, the hydrogen supply system 100 can be quickly started up by keeping the system in standby operation while maintaining the temperature of the dehydrogenation reaction. As described above, the system can be efficiently started up while suppressing the loss of the raw material and the generated hydrogen.

[0038] The circulation system 40 may circulate the dehydrogenation product produced by the dehydrogenation reaction. In this case, the fluid produced in the dehydrogenation reaction section 3 can be used as it is as a circulating fluid during standby.

[0039] The present invention is not limited to the above-described embodiment.

[0040] For example, the circulation system 40 may circulate a fluid from the outside. Specifically, as shown in FIG. 1, a reactively inert fluid may be supplied from the outside through a line L30 connected to the line L1, and the fluid may be circulated through the circulation system 40. In this case, an appropriate amount of fluid can be circulated through the circulation system. That is, when the dehydrogenation product is circulated as in the above embodiment, the amount of the dehydrogenation product present in the line at the time when the dehydrogenation reaction is stopped is circulated, so that it is difficult to control how much fluid can be circulated. On the other hand, when a fluid is supplied from the outside, the amount of circulation can be easily controlled. For example, in the above embodiment, a hydrogen station for an FVC is exemplified as the hydrogen supply system, but the hydrogen supply system may be a hydrogen supply system for a distributed power source such as a household power source or an emergency power source. [Explanation of symbols]

[0041] 3...dehydrogenation reaction section, 40...circulation system, 50...control section, 100...hydrogen supply system.

Claims

1. A hydrogen supply system that supplies hydrogen, a dehydrogenation reaction section for obtaining a hydrogen-containing gas by dehydrogenating a raw material containing a hydride; a circulation system that circulates a reactively inert fluid to the dehydrogenation reaction section; A control unit that controls the hydrogen supply system, The control unit circulates the inert fluid in the circulation system when production of the hydrogen-containing gas in the dehydrogenation reaction unit is stopped.

2. The hydrogen supply system according to claim 1 , wherein the circulation system circulates a dehydrogenation product produced by the dehydrogenation reaction.

3. The hydrogen supply system according to claim 1 , wherein the circulation system circulates a fluid from an outside source.

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