Power generation system

Abstract

This power generation system comprises: a dehydrogenation reaction device that generates hydrogen by a dehydrogenation reaction; a fuel cell that generates power using the hydrogen; a first supply line that supplies exhaust gas discharged from the fuel cell to the dehydrogenation reaction device; and an air supply unit that supplies air from the outside to the first supply line.

Description

Power generation system

[0001] The present invention relates to a power generation system.

[0002] As a conventional power generation system using hydrogen, for example, there is disclosed a system that generates hydrogen from an organic hydride through a dehydrogenation reaction in the presence of a dehydrogenation catalyst, and generates power by using energy of fuel gas generated by combusting the hydrogen as fuel (see, for example, Patent Document 1). This system includes a heat exchanger that performs heat exchange between exhaust gas discharged from a power generation unit and a heat medium, and the temperature of the dehydrogenation reactor is appropriately controlled by introducing the heat medium heated by the heat exchanger into the dehydrogenation reactor.

[0003] Japanese Unexamined Patent Publication No. 2015-187049

[0004] In a power generation system as described in Patent Document 1, in which the heat amount of exhaust gas discharged from a power generation unit is introduced into a dehydrogenation reactor via a heat medium (for example, heat transfer oil such as hot oil), there has been concern that the structure of the dehydrogenation reactor becomes complicated.

[0005] In view of such conventional problems, the present inventors have found a power generation system that enables efficient and low-cost power generation by supplying the heat amount of exhaust gas from a fuel cell to various devices.

[0006] One aspect of the present invention as a means for solving the above problems is a power generation system including: a dehydrogenation reactor that generates hydrogen through a dehydrogenation reaction; a fuel cell that generates power using the hydrogen; a first supply line that supplies exhaust gas discharged from the fuel cell to the dehydrogenation reactor; and an air supply unit that supplies external air to the first supply line.

[0007] According to one aspect of the present invention, a power generation system that enables efficient and low-cost power generation can be provided by supplying the heat amount of exhaust gas from a fuel cell to various devices.

[0008] It is a schematic diagram showing an example of the power generation system according to the first embodiment. It is a simplified diagram of FIG. 1A. It is a schematic diagram showing an example of the power generation system according to the second embodiment. It is a simplified diagram of FIG. 2A. It is a schematic diagram showing an example of the power generation system according to the third embodiment. It is a simplified diagram of FIG. 3A. It is a schematic diagram showing an example of the power generation system according to the fourth embodiment. It is a simplified diagram of FIG. 4A. It is a block diagram showing an example of the overall configuration of the power generation system according to the first embodiment. It is a block diagram showing an example of the hardware configuration of a computer. It is a block diagram showing an example of the functional configuration of a control device. It is a block diagram showing an example of a control flow of the power generation system according to the present embodiment. It is a graph showing an example of flow rate ex control of temperature adjustment air. It is a graph showing an example of temperature control of an exhaust gas combustor. It is a block diagram showing another example of a control flow of the power generation system according to the present embodiment.

[0009] Hereinafter, modes for carrying out the present invention will be described.

[0010] A power generation system according to an embodiment of the present invention (hereinafter may be referred to as "the present embodiment") has been found based on the problems in conventional power generation systems. That is, the power generation system according to the present embodiment does not require auxiliary equipment or the like related to the supply of a heat medium, so the system can be simplified and the cost related to the heat medium can be reduced. In addition, it can reduce heat dissipation loss that occurs during heat exchange between exhaust gas from a fuel cell and a heat medium, and can supply the heat quantity of the exhaust gas to various devices without any remainder, thereby improving the efficiency of the system. Furthermore, it facilitates the adjustment of the temperature and pressure of the dehydrogenation reaction device, and allows the output adjustment of the system to be performed promptly.

[0011] Details of the present embodiment will be described below.

[0012] (Power Generation System) The power generation system according to the present embodiment includes: a dehydrogenation reaction device that generates hydrogen through a dehydrogenation reaction; a fuel cell that generates power using the hydrogen; a first supply line that supplies exhaust gas discharged from the fuel cell to the dehydrogenation reaction device; and an air supply unit that supplies air from the outside to the first supply line, and may optionally include other components.

[0013] The power generation system according to this embodiment, with this configuration, enables efficient and low-cost power generation.

[0014] Here, the power generation system according to this embodiment will be described with reference to the drawings. This embodiment is illustrative and not limiting to the invention, and all features and combinations thereof described in this embodiment are not necessarily essential to the invention. The same or similar components, members, and processes shown in each drawing are denoted by the same reference numerals, and redundant explanations are omitted as appropriate. Furthermore, the scale and shape of each part shown in each drawing are set for convenience to facilitate explanation and are not to be interpreted restrictively unless otherwise specified. Also, when terms such as "first," "second," etc. are used in this specification or claims, these terms do not indicate any order or importance, but are used to distinguish one configuration from another. In addition, some components that are not important for explaining this embodiment are omitted in each drawing.

[0015] [First Embodiment] Figure 1A is a schematic diagram showing an example of a power generation system according to the first embodiment. Figure 1B is a simplified diagram of Figure 1A.

[0016] As shown in Figures 1A to 1B, the power generation system 100 mainly comprises a dehydrogenation reactor 1 that generates hydrogen by a dehydrogenation reaction, a fuel cell 6 that generates electricity using hydrogen, first supply lines SL1 to SL6 that supply exhaust gas emitted by the fuel cell 6 to the dehydrogenation reactor 1, and an air supply unit 11 that supplies air from the outside to the first supply lines SL1 to SL6.

[0017] <Dehydrogenation Reactor> The dehydrogenation reactor 1 is not particularly limited as long as it can produce hydrogen by a dehydrogenation reaction, and can be appropriately selected according to the purpose. Examples include means for producing hydrogen by electrolysis of water, and means utilizing the organic chemical hydride method (organic hydride method). Among these, means utilizing the organic hydride method are preferred from the viewpoint of being able to produce a large amount of hydrogen. In other words, the dehydrogenation reactor 1 is preferably means for producing hydrogen from an organic hydride by a dehydrogenation reaction. In this specification, the dehydrogenation reactor 1 is means utilizing the organic hydride method, and the organic hydride is methylcyclohexane (MCH;C ７ H １４ The present invention will be explained using the case of 1a as an example, but it is not limited thereto.

[0018] A feed line FL1 is connected to the dehydrogenation reactor 1, and MCH1a and associated hydrogen 1b are supplied from the outside via the feed line FL1. In the presence of a dehydrogenation catalyst, the dehydrogenation reactor 1 dehydrogenates the organic hydride to produce hydrogen and a hydrogenated substance (dehydrogenation product). For example, when MCH is used as the organic hydride, a dehydrogenation reaction occurs in the dehydrogenation reactor 1 in the presence of a dehydrogenation catalyst to produce hydrogen and toluene (C). ７ H ８ ) is produced. The dehydrogenation reaction in this case is an endothermic reaction.

[0019] -Organic Hydrides- Organic hydrides are hydrogen carriers obtained by reacting hydrogen with a hydride. The hydride and organic hydride are not particularly limited as long as they are organic compounds that can add / remove hydrogen by reversibly undergoing hydrogenation / dehydrogenation reactions. They can be appropriately selected according to the purpose, for example, acetone-isopropanol compounds, benzoquinone-hydroquinone compounds, and aromatic hydrocarbon compounds. Among these, aromatic hydrocarbon compounds are preferred from the viewpoint of transportability during energy transport.

[0020] Aromatic hydrocarbon compounds are compounds containing at least one aromatic ring, and examples include benzene, alkylbenzene, naphthalene, alkylnaphthalene, anthracene, and phenylethane. These may be used individually or in combination of two or more.

[0021] Alkylbenzenes include, for example, compounds in which the 1st to 4th hydrogen atoms of an aromatic ring are substituted with a linear alkyl group having 1 to 6 carbon atoms or a branched alkyl group. Specific examples include toluene, xylene, mesitylene, ethylbenzene, and diethylbenzene. These may be used individually or in combination of two or more.

[0022] Alkylnaphthalenes include compounds in which the 1st to 4th hydrogen atoms of an aromatic ring are substituted with a linear alkyl group having 1 to 6 carbon atoms or a branched alkyl group. A specific example is methylnaphthalene. These may be used individually or in combination of two or more.

[0023] The hydrogenate is preferably at least one of toluene and benzene. Nitrogen-containing heterocyclic aromatic compounds such as pyridine, pyrimidine, pyrazine, quinoline, isoquinoline, N-alkylpyrrole, N-alkylindole, and N-alkyldibenzopyrrole can also be used as hydrogenates.

[0024] Organic hydrides are obtained by hydrogenating the above-mentioned hydrogenated substances, and examples include cyclohexane, MCH, dimethylcyclohexane, and piperidine.

[0025] - Dehydrogenation Catalysts - There are no particular restrictions on the dehydrogenation catalysts, and they can be appropriately selected according to the purpose. Examples include those on which at least one active metal selected from nickel (Ni), platinum (Pt), palladium (Pd), rhodium (Rh), iridium (Ir), and ruthenium (Ru) is supported on a support selected from alumina, silica-alumina, and silica.

[0026] There are no particular limitations on the means used to produce hydrogen from an organic hydride by a dehydrogenation reaction, and can be appropriately selected depending on the purpose. For example, the reactor may have a fixed-bed multitube reactor structure in which multiple reaction tubes filled with a dehydrogenation catalyst are housed in a shell. In such a fixed-bed multitube reactor, hydrogen can be produced by inducing a dehydrogenation reaction by flowing an organic hydride such as MCH in contact with a fixed dehydrogenation catalyst.

[0027] Associated hydrogen 1b can be used in the startup process described later as a reducing gas to prevent oxidation of the dehydrogenation catalyst in the dehydrogenation reactor 1, a reducing gas to prevent oxidation of the anode catalyst in the fuel cell 6, and a fuel to generate combustion heat in the exhaust gas combustor 7. Therefore, it is preferable that the associated hydrogen 1b be supplied to the dehydrogenation reactor 1 during the period from when the power generation system 100 starts operating until its behavior stabilizes. As will be described in detail later, (combustion) exhaust gas is supplied to the dehydrogenation reactor 1 via the first supply line, and the temperature of the dehydrogenation reactor 1 reaches a threshold (T ＤＨ Once the level reaches TH or higher, the supply of associated hydrogen 1b may be stopped.

[0028] The dehydrogenation reactor 1 may be equipped with measuring instruments M1 such as a thermometer, gas sensor, pressure gauge, and flow meter. The data measured by the measuring instruments M1 is output to the control device 200 as a data signal. The supply unit that supplies MCH 1a and associated hydrogen 1b to the dehydrogenation reactor 1 may be equipped with measuring instruments M1a and M1b, respectively, such as a thermometer, gas sensor, pressure gauge, and flow meter, and the data measured by these measuring instruments is output to the control device 200 as a data signal.

[0029] The dehydrogenation reactor 1 is connected to the gas-liquid separation unit 2 by a feed line FL2. The product from the dehydrogenation reactor 1 is sent to the gas-liquid separation unit 2 via the feed line FL2. Since the product from the dehydrogenation reactor 1 may contain dehydrogenation reaction products (toluene) and unreacted organic hydrides, it is preferable to purify the hydrogen in the gas-liquid separation unit 2 and the hydrogen purification unit 4.

[0030] <Gas-Liquid Separation Unit> The gas-liquid separation unit 2 separates the liquid component L and the gas component G0 from the product of the dehydrogenation reactor 1. This configuration can reduce the content of dehydrogenation reaction products (toluene) and organic hydrides, etc., in the gas component (first gas component G1) supplied to the fuel cell 6, and can suppress the generation of coking caused by the dehydrogenation reaction products (toluene), etc. Therefore, the deterioration of the fuel cell 6 can be suppressed.

[0031] Liquid component L contains a large amount of liquid dehydrogenation reaction products (toluene) and liquid organic hydrides. Liquid component L may contain trace amounts of hydrogen gas, but it is preferable that it does not contain hydrogen gas. Gas component G0 contains a large amount of hydrogen gas. Gas component G0 may contain trace amounts of liquid dehydrogenation reaction products (toluene) and liquid organic hydrides, but it is preferable that it does not contain liquid dehydrogenation reaction products (toluene) and liquid organic hydrides.

[0032] The structure of the gas-liquid separation unit 2 is not particularly limited as long as it can separate the liquid component L and the gas component G0 from the product of the dehydrogenation reactor 1, and can be appropriately selected according to the purpose. For example, it may have a structure with a cooler and a knockout drum. The product of the dehydrogenation reactor 1 is cooled by the cooler through heat exchange with cooling water (e.g., 5°C to 50°C) (e.g., 5°C to 50°C). As a result, the dehydrogenation reaction product (toluene) and organic hydride contained in the product of the dehydrogenation reactor 1 become liquid. The product cooled by the cooler is sent to the knockout drum and separated into liquid component L (toluene) and gas component G0. The separated liquid component L (toluene) is discharged out of the system. The liquid component L may be reused in an organic hydride production apparatus.

[0033] A known heat exchanger can be used as the cooler. A known knockout drum can be used.

[0034] The gas-liquid separation unit 2 may be omitted, for example, depending on the required hydrogen purity for the fuel cell 6, and the performance of the hydrogen separation membrane and adsorbent used in the hydrogen purification unit 4, which will be described later.

[0035] The gas-liquid separation unit 2 is connected to the compressor 3 by a feed line FL3. The separated gas component G0 is sent to the compressor 3 via the feed line FL3.

[0036] <Compressor> Compressor 3 increases the pressure of gas component G0 to promote gas separation in the hydrogen purification unit 4, which will be described later. A known compressor can be used as compressor 3.

[0037] The compressor 3 may be omitted, for example, depending on the required hydrogen purity for the fuel cell 6, and the performance of the hydrogen separation membrane and adsorbent in the hydrogen purification unit 4, which will be described later.

[0038] The compressor 3 is connected to the hydrogen purification unit 4 by a feed line FL4. The pressurized gas component G0 is sent to the hydrogen purification unit 4 via the feed line FL4.

[0039] <Hydrogen Purification Section> The hydrogen purification section 4 separates the first gas component G1 and the second gas component G2 from the gas component G0. This configuration can reduce the content of dehydrogenation reaction products (toluene) and organic hydrides, etc., in the gas component (first gas component G1) supplied to the fuel cell 6, and can suppress the generation of coking caused by the dehydrogenation reaction products (toluene), etc. Therefore, the deterioration of the fuel cell 6 can be suppressed.

[0040] The first gas component G1 contains a large amount of hydrogen. The first gas component G1 may contain trace amounts of gaseous dehydrogenation reaction products (toluene) and gaseous organic hydrides, but it is preferable that it does not contain gaseous dehydrogenation reaction products (toluene) and gaseous organic hydrides. The second gas component G2 contains a large amount of gaseous dehydrogenation reaction products (toluene) and gaseous organic hydrides. The second gas component G2 may contain trace amounts of hydrogen, but it is preferable that it does not contain hydrogen.

[0041] The hydrogen purification section 4 is not particularly limited as long as it can separate the first gas component G1 and the second gas component G2 from the gas component G0, and can be appropriately selected according to the purpose. Examples include a hydrogen separation membrane, a TSA (Thermal Swing Adsorption) separation section, a PSA (Pressure Swing Adsorption) separation section, a distillation section, and a cryogenic separation section.

[0042] As hydrogen separation membranes, for example, known silica membranes, zeolite membranes, polymer membranes, carbon membranes, and palladium membranes can be used.

[0043] The TSA separation unit separates a first gas component G1 and a second gas component G2 from a gas component G0 using the temperature swing adsorption method (TSA method). Examples of TSA separation units include those equipped with an adsorbent that adsorbs dehydrogenation reaction products and organic hydrides contained in gas component G0 at room temperature, and desorbs the adsorbed dehydrogenation reaction products and organic hydrides at high temperatures.

[0044] The hydrogen purification unit 4 may employ an adsorption separation unit that utilizes an adsorption principle other than that of the TSA separation unit and the PSA separation unit. Such an adsorption separation unit may include a separation unit that performs only adsorption without regenerating the adsorbent.

[0045] Multiple hydrogen purification units 4 may be provided, and they may be arranged in series or in parallel with each other.

[0046] The hydrogen purification unit 4 may be equipped with measuring instruments M4 such as a thermometer, gas sensor, pressure gauge, and flow meter. The data measured by the measuring instruments M4 is output as a data signal to the control device 200.

[0047] The hydrogen purification unit 4 is connected to the dehydrogenation reaction apparatus 1 via a recycle line RL. The second gas component G2 separated by the hydrogen purification unit 4 is supplied to the dehydrogenation reaction apparatus 1 via the recycle line RL. By supplying the second gas component G2 to the dehydrogenation reaction apparatus 1 via the recycle line RL, unreacted organic hydride contained in the second gas component G2 is reused in the dehydrogenation reaction, so the utilization rate of the organic hydride can be improved. Therefore, the system efficiency of the power generation system 100 can be improved. The system efficiency of the power generation system 100 can be calculated based on the following formula (1). Although details will be described later, the system efficiency may be calculated by the calculation unit 214. System efficiency of power generation system = MCH conversion rate × {power generation amount in fuel cell / (3 × ΔH° ２９８ (H ２ O; g) - endothermic amount in dehydrogenation reaction apparatus)} ... (1)

[0048] In the above formula (1), the MCH conversion rate is a value obtained by dividing the amount of hydrogen introduced into the dehydrogenation reaction apparatus 1 by the amount of hydrogen extracted from MCH in the dehydrogenation reaction apparatus 1 (amount of hydrogen extracted from MCH in the dehydrogenation reaction apparatus 1 / amount of hydrogen introduced into the dehydrogenation reaction apparatus 1). In the above formula (1), "ΔH° ２９８ (H ２ O; g)" is the standard enthalpy change of formation for the hydrogen oxidation reaction, which is, for example, -241.8 kJ / mol. In consideration of losses when converting electricity obtained from power generation from DC (Direct Current) to AC (Alternating Current) and losses for auxiliary device power, etc., a value obtained by multiplying the system efficiency of the power generation system obtained by the above formula (1) by a conversion efficiency including auxiliary device losses may be used as the system efficiency of the power generation system.

[0049] The hydrogen purification unit 4 is connected to the steam reformer 5 via a feed line FL5. The first gas component G1 separated by the hydrogen purification unit 4 is sent to the steam reformer 5 via the feed line FL5.

[0050] <Steam Reformer> The steam reformer 5 hydrocracking or steam reforming at least one of the dehydrogenation reaction product (toluene) and unreacted organic hydride contained in the first gas component G1. The steam reformer 5 may perform both hydrocracking and steam reforming. As a result, the dehydrogenation reaction product (toluene) and organic hydride are converted into methane and hydrogen, etc. This configuration can reduce the amount of dehydrogenation reaction product (toluene) and organic hydride, etc. contained in the gas component (first gas component G1) supplied to the fuel cell 6, and can suppress the generation of coking caused by the dehydrogenation reaction product (toluene), etc. Therefore, the deterioration of the fuel cell 6 can be suppressed.

[0051] When the steam reformer 5 hydrocrackings the dehydrogenation reaction products, a known hydrocracking apparatus can be used as the steam reformer 5. The hydrogen required for hydrocracking can be supplied by the hydrogen contained in the first gas component G1.

[0052] When the steam reformer 5 steam reforms dehydrogenated products, etc., a known reformer can be used as the steam reformer 5. The steam reformer 5 may be integrally provided with the fuel cell 6. For example, the power generation system 100 according to the first embodiment may include a fuel cell 6 with an integrated reformer filled with a reforming catalyst.

[0053] The steam reformer 5 may perform hydrocracking or steam reforming by being equipped with a heating mechanism, or it may perform hydrocracking or steam reforming by utilizing the heat energy of the exhaust gas from the fuel cell 6 (described later) or the heat energy of the combustion exhaust gas burned by the exhaust gas combustor 7.

[0054] In the steam reformer 5, the water (preferably steam) necessary for steam reforming may be supplied from an external source, for example. The power generation system 100 according to the first embodiment may include an evaporator 9, and the steam generated by the evaporator 9 may be supplied to the steam reformer 5. In this case, a feed line FL6 is connected to the evaporator 9, and water (H) may be supplied from an external source via the feed line FL6. ２O) is supplied. The evaporator 9 is connected to the steam reformer 5 by the feed line FL7. The steam generated by the evaporator 9 is supplied to the steam reformer 5 via the feed line FL7.

[0055] The evaporator 9 may be equipped with a heating mechanism to heat water supplied from an external source to generate steam, or it may be equipped with a heating mechanism to heat water to generate steam using the heat energy of the exhaust gas from the fuel cell 6 (described later) or the heat energy of the combustion exhaust gas burned by the exhaust gas combustor 7.

[0056] The evaporator 9 may be equipped with measuring instruments M9 such as a thermometer, gas sensor, pressure gauge, and flow meter. The data measured by the measuring instruments M9 is output as a data signal to the control device 200.

[0057] The steam reformer 5 may be equipped with measuring instruments M5 such as a thermometer, gas sensor, pressure gauge, and flow meter. The data measured by the measuring instruments M5 is output as a data signal to the control device 200.

[0058] In the first embodiment, the power generation system 100 may include an additive section that adds water to the first gas component G1 upstream of the fuel cell 6, instead of the steam reformer 5. As an example, the additive section adds water (preferably steam) supplied from an external source to the first gas component G1. By adding water to the first gas component G1, the steam reforming reaction, such as the dehydrogenation reaction product by the anode catalyst, can proceed at the anode electrode 6a of the fuel cell 6. In other words, the fuel cell 6 can also function as a steam reformer 5 by including the additive section.

[0059] The steam reformer 5 may be omitted if necessary, for example, when the performance of the preceding hydrogen purification unit 4 is sufficiently high, that is, when the hydrogen purification accuracy in the hydrogen purification unit 4 is high and the content of dehydrogenation reaction products (toluene) and organic hydrides in the first gas component G1 is low.

[0060] The steam reformer 5 is connected to the fuel cell 6 by a feed line FL8. The first gas component G1 reformed in the steam reformer 5 is supplied to the fuel cell 6 via the feed line FL8.

[0061] <Fuel Cell> The fuel cell 6 generates electricity using hydrogen. There are no particular restrictions on the fuel cell, and it can be appropriately selected according to the purpose. Examples include solid oxide fuel cells (SOFCs).

[0062] The structure of the fuel cell 6 is not particularly limited as long as it can generate electricity using hydrogen contained in the first gas component G1, and can be appropriately selected according to the purpose. For example, it may have a structure having an anode electrode 6a, a cathode electrode 6b, and an electrolyte membrane 6c separating the anode electrode 6a and the cathode electrode 6b. At the cathode electrode 6b, oxygen reacts with electrons to produce oxygen ions. The oxygen ions move to the anode electrode 6a through the electrolyte membrane 6c. At the anode electrode 6a, hydrogen reacts with oxygen ions to produce water and electrons.

[0063] A feed line FL8 is connected to the inlet of the anode electrode 6a, and a first gas component G1 containing hydrogen is supplied to it.

[0064] A feed line FL10 is connected to the inlet of the cathode electrode 6b, and an oxygen-containing cathode gas is supplied from the outside. Air or other materials can be used as the cathode gas.

[0065] The power generation system 100 according to the first embodiment may include an air preheater 8, and the cathode gas heated by the air preheater 8 may be supplied to the cathode electrode 6b. A feed line FL9 is connected to the air preheater 8, and air is supplied from the outside via the feed line FL9. The air preheater 8 is connected to the inlet of the cathode electrode 6b by a feed line FL10. The air heated by the air preheater 8 is supplied to the inlet of the cathode electrode 6b via the feed line FL10. With this configuration, the temperature difference between the air supplied to the fuel cell 6 and the first gas component G1 is reduced, and the thermal stress generated between the anode electrode 6a and the cathode electrode 6b is alleviated, thereby improving the durability of the fuel cell 6. In addition, the temperature distribution inside the fuel cell 6 is made uniform, so the power generation efficiency of the fuel cell 6 is improved. The power generation efficiency of the fuel cell 6 can be calculated based on the following formula (2). As will be described in detail later, the power generation efficiency may be calculated by the calculation unit 214. Fuel cell power generation efficiency = Amount of power generated by the fuel cell / (3 × ΔH°) ２９８ (H ２ O; g) - Endothermic heat in the dehydrogenation reactor) ... (2)

[0066] Furthermore, considering the losses incurred when converting the electricity generated from DC (Direct Current) to AC (Alternating Current), as well as the losses due to auxiliary equipment power, the power generation efficiency of the fuel cell obtained by formula (2) above may be multiplied by the conversion efficiency including auxiliary equipment losses to obtain the power generation efficiency of the fuel cell.

[0067] The air preheater 8 may heat air supplied from the outside by having a heating mechanism, or it may heat air by utilizing the heat energy of the exhaust gas from the fuel cell 6 (described later) or the heat energy of the combustion exhaust gas burned by the exhaust gas combustor 7.

[0068] The air preheater 8 may be equipped with measuring instruments M8 such as a thermometer, gas sensor, pressure gauge, and flow meter. The data measured by the measuring instruments M8 is output to the control device 200 as a data signal.

[0069] The fuel cell 6 preferably includes an inverter that converts the electricity generated by the fuel cell 6 into usable electricity.

[0070] The outlet of the anode electrode 6a is connected to the exhaust gas combustor 7 by supply line SL1, which is one of the first supply lines. As will be described in detail later, the first supply line in the first embodiment is a series of supply lines from supply line SL1 to supply line SL6. The exhaust gas that has passed through the anode electrode 6a without being used for power generation in the fuel cell 6 (also called anode off-gas) is supplied to the exhaust gas combustor 7 via supply line SL1.

[0071] The outlet of the cathode electrode 6b is connected to the exhaust gas combustor 7 by supply line SL2, which is one of the first supply lines. Exhaust gas that has passed through the cathode electrode 6b and is not used for power generation in the fuel cell 6 (also called cathode-off gas) is supplied to the exhaust gas combustor 7 via supply line SL2.

[0072] <Exhaust Gas Combustor> The exhaust gas combustor 7 burns the exhaust gas emitted from the fuel cell 6. More specifically, it burns the hydrogen contained in the exhaust gas to raise the temperature of the exhaust gas. With this configuration, the heat from the exhaust gas emitted from the fuel cell 6 can be supplied to the various devices arranged in the first supply line without waste, thereby improving the efficiency of the system.

[0073] As for the exhaust gas combustor 7, there are no particular restrictions as long as it can burn the exhaust gas emitted from the fuel cell 6 to raise the temperature of the exhaust gas, and it can be appropriately selected according to the purpose. For example, known combustors and catalytic combustors can be used.

[0074] There are no particular restrictions on the temperature of the exhaust gas combustor 7, and it can be appropriately selected according to the purpose. However, from the viewpoint of supplying the heat of the combustion exhaust gas to various devices and improving system efficiency, it is preferable that the temperature at the outlet of the exhaust gas combustor 7 be between 200°C and 1200°C.

[0075] The exhaust gas combustor 7 may be equipped with measuring instruments M7 such as a thermometer, gas sensor, pressure gauge, and flow meter. The data measured by the measuring instruments M7 is output as a data signal to the control device 200.

[0076] The exhaust gas combustor 7 is connected to the air preheater 8 by supply line SL3, which is one of the first supply lines. The combustion exhaust gas, which has been burned in the exhaust gas combustor 7 and whose temperature has been increased, is supplied to the air preheater 8 via supply line SL3.

[0077] The air preheater 8 may heat the air supplied to the cathode electrode 6b by utilizing the heat of the combustion exhaust gas supplied via the supply line SL3. More specifically, by performing heat exchange between the air supplied to the air preheater 8 via the feed line FL9 and the combustion exhaust gas supplied via the supply line SL3, the temperature of the air supplied to the cathode electrode 6b can be adjusted to a temperature suitable for the fuel cell 6. More specifically, it is preferable that the temperature at the outlet of the air preheater 8 in the direction of the feed line FL10 is between 300°C and 700°C.

[0078] The air preheater 8 may be equipped with measuring instruments M8 such as a thermometer, gas sensor, pressure gauge, and flow meter. The data measured by the measuring instruments M8 is output to the control device 200 as a data signal.

[0079] In the power generation system 100 according to the first embodiment, the exhaust gas combustor 7 is located upstream of the air preheater 8 in the first supply line, so that the temperature of the air preheater 8 can be selectively increased. Such a configuration is effective, for example, when it is desired to further increase the temperature of the air supplied to the cathode electrode 6b.

[0080] In the power generation system 100 according to the first embodiment, the temperature of the combustion exhaust gas may be adjusted by adjusting the amount of air supplied to the air preheater 8. For example, reducing the amount of air supplied to the air preheater 8 reduces the amount of air that exchanges heat with the combustion exhaust gas, thereby increasing the temperature of the combustion exhaust gas. Conversely, for example, increasing the amount of air supplied to the air preheater 8 increases the amount of air that exchanges heat with the combustion exhaust gas, thereby lowering the temperature of the combustion exhaust gas.

[0081] The air preheater 8 is connected to the steam reformer 5 by supply line SL4, which is one of the first supply lines. The combustion exhaust gas that has undergone heat exchange in the air preheater 8 is supplied to the steam reformer 5 via supply line SL4.

[0082] The steam reformer 5 may be heated to a temperature suitable for hydrocracking or steam reforming by utilizing the heat of the combustion exhaust gas supplied via the supply line SL4. More specifically, it is preferable that the temperature at the outlet of the steam reformer 5 in the direction of the feed line FL8 is between 400°C and 800°C.

[0083] In the power generation system 100 according to the first embodiment, the temperature of the combustion exhaust gas may be adjusted by adjusting the amount of water supplied to the steam reformer 5. For example, reducing the amount of water supplied to the steam reformer 5 reduces the amount of water that exchanges heat with the combustion exhaust gas, thus increasing the temperature of the combustion exhaust gas. Alternatively, increasing the amount of water supplied to the steam reformer 5 increases the amount of water that exchanges heat with the combustion exhaust gas, thus lowering the temperature of the combustion exhaust gas.

[0084] The steam reformer 5 is connected to the mixer 10 by supply line SL5, which is one of the first supply lines. The combustion exhaust gas that has undergone heat exchange in the steam reformer 5 is supplied to the mixer 10 via supply line SL5.

[0085] <Mixer> The mixer 10 mixes the combustion exhaust gas supplied from the supply line SL5 with air supplied from the outside by the air supply unit 11 (sometimes referred to as "temperature-adjusting air") to adjust the temperature of the combustion exhaust gas to a temperature suitable for the dehydrogenation reaction in the dehydrogenation reactor 1. If high-temperature combustion exhaust gas is supplied to the dehydrogenation reactor 1, coking (deposition of solid carbon on the catalyst) caused by dehydrogenation reaction products and organic hydrides may occur, or the dehydrogenation reaction products and organic hydrides may decompose. According to the power generation system 100 of the first embodiment, the temperature of the combustion exhaust gas can be adjusted to a temperature suitable for the dehydrogenation reaction by mixing the combustion exhaust gas with air supplied from the outside by the air supply unit 11. With this configuration, the deterioration and decomposition of the catalyst due to sintering and coking can be suppressed. Therefore, the deterioration of the dehydrogenation reactor 1 can be suppressed, and the decrease in the utilization rate of organic hydrides can be suppressed, thereby improving the system efficiency of the power generation system 100.

[0086] The air supply unit 11 is connected to the mixer 10 by a feed line FL1. Air from the outside is supplied to the mixer 10 via the feed line FL1.

[0087] The structure of the air supply unit 11 is not particularly limited as long as it can supply air from the outside to the mixer 10, and can be appropriately selected according to the purpose. For example, an air supply unit equipped with a mass flow meter can be used. This air supply unit equipped with a mass flow meter can constantly monitor the flow rate of air supplied to the mixer 10 and supply a specified flow rate of air using a diaphragm pump or the like while performing feedback control.

[0088] The air supply unit 11 may have measuring instruments M11 such as a thermometer, gas sensor, pressure gauge, and flow meter, and the data measured by these measuring instruments is output as a data signal to the control device 200.

[0089] In this specification, the "temperature suitable for the dehydrogenation reaction" is preferably 300°C to 350°C, although this depends on the type of organic hydride, dehydrogenation catalyst, and dehydrogenation reactor used to carry out the dehydrogenation reaction.

[0090] If the temperature of the combustion exhaust gas in supply line SL5 is suitable for the dehydrogenation reaction, the dehydrogenation reactor 1 may be directly heated with the combustion exhaust gas without using the mixer 10. In this case, the structure of the power generation system 100 can be simplified.

[0091] The structure of the mixer 10 is not particularly limited as long as it can mix combustion exhaust gas and air, and can be appropriately selected according to the purpose, and known types can be used as appropriate.

[0092] The mixer 10 may have measuring instruments M10 such as a thermometer, gas sensor, pressure gauge, and flow meter, and the data measured by these measuring instruments is output as a data signal to the control device 200.

[0093] Mixer 10 is connected to dehydrogenation reactor 1 by supply line SL6, which is one of the first supply lines. Combustion exhaust gas, which is mixed with air and temperature-controlled in mixer 10, is supplied to dehydrogenation reactor 1 via supply line SL6.

[0094] As described above, the dehydrogenation reactor 1 is heated to a temperature suitable for the dehydrogenation reaction by utilizing the heat of the combustion exhaust gas supplied via the supply line SL6. More specifically, it is preferable that the temperature at the outlet of the dehydrogenation reactor 1 in the direction of the feed line FL2 is between 250°C and 400°C.

[0095] In the power generation system 100 according to the first embodiment, the temperature of the combustion exhaust gas may be adjusted by adjusting the amount of organic hydride (MCH) supplied to the dehydrogenation reactor 1. For example, by reducing the amount of MCH 1a supplied to the dehydrogenation reactor 1, the amount of hydrogen contained in the gas supplied to the fuel cell 6 and the exhaust gas combustor 7 can be reduced, and the temperature of the exhaust gas can be lowered. Alternatively, for example, by increasing the amount of MCH 1a supplied to the dehydrogenation reactor 1, the amount of hydrogen contained in the gas supplied to the fuel cell 6 and the exhaust gas combustor 7 can be increased, and the temperature of the exhaust gas can be raised.

[0096] The power generation system 100 according to the first embodiment may include a second supply line that supplies the exhaust gas supplied to the dehydrogenation reactor 1 to the hydrogen purification unit 4. As will be described in detail later, the second supply line in the first embodiment is a series of supply lines from supply line SL7 to supply line SL8.

[0097] The dehydrogenation reactor 1 is connected to the evaporator 9 by supply line SL7, which is one of the second supply lines. The combustion exhaust gas that has undergone heat exchange in the dehydrogenation reactor 1 is supplied to the evaporator 9 via supply line SL7.

[0098] The evaporator 9 may generate steam by utilizing the heat energy of the combustion exhaust gas supplied via the supply line SL7. More specifically, it is preferable that the temperature at the outlet of the evaporator 9 in the direction of the supply line SL8, which will be described later, be 100°C or higher.

[0099] The evaporator 9 is connected to the hydrogen purification unit 4 by supply line SL8, which is one of the second supply lines. The combustion exhaust gas that has undergone heat exchange in the evaporator 9 is supplied to the hydrogen purification unit 4 via supply line SL8.

[0100] The hydrogen purification unit 4 may separate the first gas component G1 and the second gas component G2 from the gas component G0 by utilizing the heat energy of the combustion exhaust gas supplied via the supply line SL8. There are no particular restrictions on the temperature of the hydrogen purification unit 4, and it can be appropriately selected according to the purpose and according to the method of separating the gas components.

[0101] If the amount of heat obtained from the fuel cell 6 and the exhaust gas combustor 7 is still insufficient for the dehydrogenation reaction even after supplying it to the dehydrogenation reactor 1, the heat may be supplied from a device other than the power generation system 100.

[0102] The power generation system 100 may have a power source as needed.

[0103] As described above, the power generation system 100 according to the first embodiment can supply the heat energy of the exhaust gas to various devices without waste, thereby improving the efficiency of the system.

[0104] Conventional power generation systems use heat transfer fluids that have low thermal stability and high heat capacity, making temperature and pressure adjustment of the dehydrogenation reactor complex and sometimes requiring time to adjust the system's thermal balance during startup and load fluctuations. Furthermore, heat transfer fluids themselves are expensive and can incur maintenance costs. As described above, the power generation system 100 according to the first embodiment does not require auxiliary equipment related to the supply of heat transfer fluid, thus simplifying the system and reducing the cost of heat transfer fluid. In addition, temperature and pressure adjustment of the dehydrogenation reactor becomes easier, and system output can be adjusted quickly.

[0105] [Second Embodiment] Figure 2A is a schematic diagram showing an example of a power generation system according to the second embodiment. Figure 2B is a simplified diagram of Figure 2A. Note that in the power generation system 101 according to the second embodiment, the same configuration as in the power generation system 100 according to the first embodiment is omitted from the description.

[0106] As shown in Figures 2A to 2B, the power generation system 101 mainly comprises a dehydrogenation reactor 1 that generates hydrogen by a dehydrogenation reaction, a fuel cell 6 that generates electricity using hydrogen, first supply lines SL1 to SL6 that supply exhaust gas emitted by the fuel cell 6 to the dehydrogenation reactor 1, and an air supply unit 11 that supplies air from the outside to the first supply lines SL1 to SL6.

[0107] The outlet of the cathode electrode 6b is connected to the air preheater 8 by supply line SL31, which is one of the first supply lines. The exhaust gas that has passed through the cathode electrode 6b and is not used for power generation in the fuel cell 6 is supplied to the air preheater 8 via supply line SL31. The air preheater 8 may use the heat from the exhaust gas supplied via supply line SL31 to heat the air supplied to the cathode electrode 6b.

[0108] The air preheater 8 is connected to the exhaust gas combustor 7 by supply line SL41, which is one of the first supply lines. The exhaust gas that has undergone heat exchange in the air preheater 8 is supplied to the exhaust gas combustor 7 via supply line SL41.

[0109] The exhaust gas combustor 7 burns the exhaust gas supplied from the air preheater 8. More specifically, it burns the hydrogen contained in the exhaust gas supplied from the air preheater 8 to raise the temperature of the exhaust gas. With this configuration, the heat from the exhaust gas discharged from the fuel cell can be supplied without waste to the various devices located downstream of the exhaust gas combustor 7 in the supply line, thereby improving the efficiency of the system.

[0110] The exhaust gas combustor 7 is connected to the steam reformer 5 by supply line SL42, which is one of the first supply lines. Combustion exhaust gas is supplied to the steam reformer 5 via supply line SL42.

[0111] In the power generation system 101 according to the second embodiment, the exhaust gas combustor 7 is located upstream of the steam reformer 5 in the first supply line, so that the temperature of the steam reformer 5 can be selectively raised. Such a configuration is effective, for example, when the temperature required for hydrocracking or steam reforming performed in the steam reformer 5 is high.

[0112] [Third Embodiment] Figure 3A is a schematic diagram showing an example of a power generation system according to the third embodiment. Figure 3B is a simplified diagram of Figure 3A. Note that in the power generation system 102 according to the third embodiment, the same configuration as the power generation system 100 according to the first embodiment is omitted from the description.

[0113] As shown in Figures 3A to 3B, the power generation system 102 mainly comprises a dehydrogenation reactor 1 that generates hydrogen by a dehydrogenation reaction, a fuel cell 6 that generates electricity using hydrogen, first supply lines SL1 to SL6 that supply exhaust gas emitted by the fuel cell 6 to the dehydrogenation reactor 1, and an air supply unit 11 that supplies air from the outside to the first supply lines SL1 to SL6.

[0114] The outlet of the cathode electrode 6b is connected to the air preheater 8 by supply line SL31, which is one of the first supply lines. The exhaust gas that has passed through the cathode electrode 6b and is not used for power generation in the fuel cell 6 is supplied to the air preheater 8 via supply line SL31. The air preheater 8 may use the heat from the exhaust gas supplied via supply line SL31 to heat the air supplied to the cathode electrode 6b.

[0115] The steam reformer 5 is connected to the exhaust gas combustor 7 by supply line SL51, which is one of the first supply lines. The exhaust gas that has undergone heat exchange in the steam reformer 5 is supplied to the exhaust gas combustor 7 via supply line SL51.

[0116] The exhaust gas combustor 7 burns the exhaust gas supplied from the air preheater 8. More specifically, it burns the hydrogen contained in the exhaust gas supplied from the steam reformer 5 to raise the exhaust gas temperature. With this configuration, the heat from the exhaust gas discharged from the fuel cell 6 can be supplied without waste to the various devices located downstream of the exhaust gas combustor 7 in the supply line, thereby improving the efficiency of the system.

[0117] In the power generation system 102 according to the third embodiment, the exhaust gas combustor 7 is located upstream of the dehydrogenation reactor 1 in the first supply line, so that the temperature of the dehydrogenation reactor 1 can be selectively increased. Such a configuration is effective, for example, when the temperature required for the dehydrogenation reaction carried out in the dehydrogenation reactor 1 is high.

[0118] The power generation system 102 according to the third embodiment may include a mixer-integrated exhaust gas combustor that functions as a mixer, or it may include an exhaust gas combustor and a mixer separately, as in the other embodiments. The mixer-integrated exhaust gas combustor has the function of mixing the air supplied from the air supply unit 11 with the exhaust gas discharged from the fuel cell 6.

[0119] [Fourth Embodiment] Figure 4A is a schematic diagram showing an example of a power generation system according to the fourth embodiment. Figure 4B is a simplified diagram of Figure 4A. Note that in the power generation system 103 according to the fourth embodiment, the same configuration as in the power generation system 100 according to the first embodiment is omitted from the description.

[0120] As shown in Figures 4A to 4B, the power generation system 103 mainly comprises a dehydrogenation reactor 1 that generates hydrogen by a dehydrogenation reaction, a fuel cell 6 that generates electricity using hydrogen, first supply lines SL1 to SL6 that supply exhaust gas emitted by the fuel cell 6 to the dehydrogenation reactor 1, and an air supply unit 11 that supplies air from the outside to the first supply lines SL1 to SL6.

[0121] The outlet of the cathode electrode 6b is connected to the air preheater 8 by supply line SL31, which is one of the first supply lines. The exhaust gas that has passed through the cathode electrode 6b and is not used for power generation in the fuel cell 6 is supplied to the air preheater 8 via supply line SL31. The air preheater 8 may use the heat from the exhaust gas supplied via supply line SL31 to heat the air supplied to the cathode electrode 6b.

[0122] The dehydrogenation reactor 1 is connected to the exhaust gas combustor 7 by supply line SL71, which is one of the second supply lines. The exhaust gas that has undergone heat exchange in the dehydrogenation reactor 1 is supplied to the exhaust gas combustor 7 via supply line SL71.

[0123] The exhaust gas combustor 7 burns the exhaust gas supplied from the dehydrogenation reactor 1. More specifically, it burns the hydrogen contained in the exhaust gas supplied from the dehydrogenation reactor 1 to increase the exhaust gas temperature. With this configuration, the heat contained in the exhaust gas discharged from the fuel cell can be supplied without waste to the various devices located downstream of the exhaust gas combustor 7 in the supply line, thereby improving the efficiency of the system.

[0124] The exhaust gas combustor 7 is connected to the evaporator 9 by supply line SL72, which is one of the second supply lines. Combustion exhaust gas is supplied to the evaporator 9 via supply line SL72.

[0125] In the power generation system 103 according to the fourth embodiment, the exhaust gas combustor 7 is located upstream of the evaporator 9 in the second supply line, so that the temperature of the evaporator 9 can be selectively raised. Such a configuration is effective, for example, when the temperature required for steam generation in the evaporator 9 is high.

[0126] Here, the overall configuration of the power generation system according to this embodiment will be described with reference to Figure 5. Note that, from this point onward, the power generation system 100 according to the first embodiment will be described as an example, but the present invention is not limited thereto.

[0127] Figure 5 is a block diagram showing an example of the overall configuration of the power generation system according to this embodiment. As shown in Figure 5, the power generation system 100 includes a control device 200 and a terminal device 300.

[0128] The control device 200 and the terminal device 300 may be connected to each other via a communication network N such as a LAN (Local Area Network) or the Internet, enabling data communication.

[0129] The control device 200 is an information processing device such as a personal computer, workstation, or server that controls the amount of electricity obtained from the power generation system 100. The control device 200 is electrically connected to the various devices that make up the power generation system 100, such as the dehydrogenation reactor 1, gas-liquid separation unit 2, compressor 3, hydrogen purification unit 4, steam reformer 5, fuel cell 6, exhaust gas combustor 7, air preheater 8, evaporator 9, mixer 10, air supply unit 11, and various measuring instruments (M1, M1a, M1b, M4, M5, M7, M8, M9, M10, M11), and controls the operation of the power generation system 100.

[0130] The control device 200 acquires information related to power generation and controls the power generation system 100 based on the acquired information.

[0131] The terminal device 300 is an information processing terminal, such as a personal computer, smartphone, or tablet, operated by the user of the power generation system 100. The terminal device 300 receives information related to power generation from the control device 200 and presents that information to the user.

[0132] The overall configuration of the power generation system 100 shown in Figure 5 is just one example, and various system configurations are possible depending on the application and purpose. For example, one or more control devices 200 and terminal devices 300 may be included in multiple units of the power generation system 100. For example, the control device 200 may be implemented by multiple information processing devices (computers), or it may be implemented as a cloud computing service. For example, the control device 200 may be implemented by distributing it across multiple computers according to its function. For example, the power generation system 100 may be implemented by a standalone computer. The classification of devices such as the control device 200 and terminal device 300 shown in Figure 5 is just one example.

[0133] -Hardware Configuration- The control device 200 is implemented, for example, by a computer. Figure 6 is a block diagram showing an example of the computer's hardware configuration. As shown in Figure 6, the control device 200 physically includes a processor 201 which is the arithmetic processing unit, memory 202, auxiliary storage device 203, an input device 204 which is the input device, an output device 205 which is the output device, a communication interface 206, and an external interface 207.

[0134] The processor 201 and memory 202 form a so-called computer. Each piece of computer hardware is interconnected via a bus line 208. The input device 204 and output device 205 may also be used by connecting them to an external I / F 207.

[0135] The processor 201 is an arithmetic unit that realizes the control and functions of the entire computer by reading programs or data from a storage device such as memory 202 or auxiliary storage device 203 into the RAM (Random Access Memory) of memory 202 and executing processing. For example, the processor 201 may be a CPU (Central Processing Unit) or a GPU (Graphics Processing Unit). The processor 201 may also have both a CPU and a GPU.

[0136] Memory 202 includes ROM (Read Only Memory) and RAM, which are main memory devices, and may store management programs. ROM is an example of a non-volatile semiconductor memory (storage device) that can retain programs and data even when the power is turned off. ROM functions as main memory, storing various programs and data necessary for the processor 201 to execute the various programs installed in the auxiliary storage device 203. Specifically, ROM stores boot programs such as BIOS (Basic Input / Output System) and EFI (Extensible Firmware Interface) that are executed when the computer starts up, as well as OS (Operating System) settings and network settings.

[0137] RAM is an example of volatile semiconductor memory (storage device) in which programs or data are erased when the power is turned off. RAM can be, for example, DRAM (Dynamic Random Access Memory) or SRAM (Static Random Access Memory). RAM provides a workspace that is expanded when various programs installed in the auxiliary storage device 203 are executed by the processor 201.

[0138] The auxiliary storage device 203 is a non-volatile storage device that stores programs and data. The programs and data stored in the auxiliary storage device 203 include the OS, which is the basic software that controls the entire computer, and applications that provide various functions on the OS. The auxiliary storage device 203 may be an HDD (Hard Disk Drive) or a storage device that uses flash memory as a storage medium, such as an SSD (Solid State Drive).

[0139] The input device 204 is a touch panel, operation keys, buttons, keyboard, mouse, or microphone used by the user to input various signals, and is used to input sound data such as voice.

[0140] The output device 205 consists of a display such as a liquid crystal or organic EL (Electro-Luminescence) that displays an image, and a speaker that outputs sound data such as voice.

[0141] Communication I / F 206 is an interface for connecting to a communication network and for a computer to perform data communication.

[0142] External I / F 207 is an interface to external devices. Examples of external devices include drive device 209-1.

[0143] The drive device 209-1 is a device for setting the recording medium 209-2. The recording medium 209-2 includes media that record information optically, electrically, or magnetically, such as CD-ROMs, flexible disks, and magneto-optical disks. The recording medium 209-2 may also include semiconductor memory that records information electrically, such as ROM or flash memory. This allows the computer to read and / or write to the recording medium 209-2 via the external I / F 207.

[0144] The various programs to be installed on the auxiliary storage device 203 are installed, for example, when the distributed recording medium 209-2 is set in a drive device 209-1 connected to an external I / F 207, and the various programs recorded on the recording medium 209-2 are read by the drive device 209-1. Alternatively, the various programs to be installed on the auxiliary storage device 203 may be installed by downloading them via the communication I / F 206 from a network other than the communication network.

[0145] The functional configuration of the control device 200 will be explained with reference to Figure 7. Figure 7 is a block diagram showing an example of the functional configuration of the control device 200. As shown in Figure 7, the control device 200 includes an information acquisition unit 211 and a control unit 210.

[0146] The information acquisition unit 211 and the control unit 210 are realized, for example, by a process in which a program loaded from the auxiliary storage device 203 shown in Figure 6 onto a memory 202 such as RAM is executed by the processor 201.

[0147] <Information Acquisition Unit> The information acquisition unit 211 acquires information related to power generation. The information related to power generation includes information output from various devices of the power generation system 100. For example, this includes the temperature of the dehydrogenation reactor 1 measured by measuring instrument M1, the flow rate of MCH 1a measured by measuring instrument M1a, the flow rate of associated hydrogen 1b measured by measuring instrument M1b, the temperature of the hydrogen purification unit 4 measured by measuring instrument M4, the temperature of the steam reformer 5 measured by measuring instrument M5, the flow rate of water introduced into the steam reformer 5 measured by measuring instrument M5, the temperature of the exhaust gas combustor 7 measured by measuring instrument M7, the temperature of the air preheater 8 measured by measuring instrument M8, the flow rate of air introduced into the air preheater 8 measured by measuring instrument M8, the temperature of the evaporator 9 measured by measuring instrument M9, the temperature of the mixer 10 measured by measuring instrument M10, the flow rate of air supplied from the air supply unit 11 measured by measuring instrument M11, and the temperature of exhaust gas at various locations measured by various measuring instruments.

[0148] <Control Unit> The control unit 210 includes an operation control unit 212, a calculation unit 214, a determination unit 215, and an information transmission unit 216.

[0149] The operation control unit 212 controls the operation of the power generation system 100 based on the power generation information acquired by the information acquisition unit 211. That is, the operation control unit 212 controls each device or component that constitutes the power generation system 100 based on the power generation information.

[0150] In the power generation system 100 according to this embodiment, the operation control unit 212 (control unit 210) controls the exhaust gas discharged from the fuel cell 6 that is supplied to the dehydrogenation reactor 1 so that it reaches a predetermined temperature. More specifically, it is preferable that the operation control unit 212 (control unit 210) controls the amount of air supplied to the first supply line so that the temperature of the exhaust gas supplied to the dehydrogenation reactor 1 reaches a predetermined temperature. The predetermined temperature of the exhaust gas supplied to the dehydrogenation reactor 1 is, as described above, a temperature suitable for the dehydrogenation reaction, and can be appropriately set according to the type of organic hydride, dehydrogenation catalyst, and dehydrogenation reactor that performs the dehydrogenation reaction. With this configuration, the deterioration and decomposition of the catalyst due to sintering and coking can be suppressed, thereby suppressing the deterioration of the dehydrogenation reactor 1 and enabling long-term durable operation. In addition, since auxiliary equipment related to the supply of the heat transfer medium is not required, the system can be simplified and the cost related to the heat transfer medium can be reduced.

[0151] The operation control unit 212 (control unit 210) may control the amount of air supplied to the first supply line based on the temperature of the dehydrogenation reactor 1 or the exhaust gas. Temperature information of the dehydrogenation reactor 1 or the exhaust gas is measured by a measuring instrument M1 or the like and acquired by the information acquisition unit 211. With this configuration, temperature information of the dehydrogenation reactor 1 or the exhaust gas can be fed back to the control unit 210, allowing for more accurate adjustment of the exhaust gas temperature.

[0152] The operation control unit 212 (control unit 210) may control the amount of air supplied to the first supply line based on at least one selected from the group consisting of the temperature of the dehydrogenation reactor 1, the temperature of the mixer 10, and the temperature of the exhaust gas. Temperature information for the dehydrogenation reactor 1, the mixer 10, and the exhaust gas is measured by measuring instruments M1 and M10, etc., and acquired by the information acquisition unit 211. With this configuration, temperature information for the dehydrogenation reactor 1, the mixer 10, and the exhaust gas can be fed back to the control unit 210, allowing for more accurate adjustment of the exhaust gas temperature.

[0153] The operation control unit 212 (control unit 210) may control the amount of air supplied to the first supply line based on the temperature of the exhaust gas combustor 7 or the temperature of the exhaust gas heated by the exhaust gas combustor 7. Temperature information of the exhaust gas combustor 7 and the exhaust gas heated by the exhaust gas combustor 7 is measured by a measuring instrument M7 or the like and acquired by the information acquisition unit 211. With this configuration, temperature information of the exhaust gas combustor 7 and the combustion exhaust gas can be fed back to the control unit 210, allowing for more accurate adjustment of the exhaust gas temperature.

[0154] The power generation system 100 according to this embodiment may include a heat exchanger for cooling exhaust gas. The term "heat exchanger" in this specification is not particularly limited as long as it has the function of cooling exhaust gas by heat exchange, and can be appropriately selected according to the purpose, but it is preferable to include a steam reformer 5 and an air preheater 8. When the power generation system 100 according to this embodiment includes a heat exchanger, the amount of heat exchanged can be appropriately set according to the performance of the heat exchanger. The heat exchanger may have measuring instruments such as a thermometer, a gas sensor, a pressure gauge, and a flow meter, and the data measured by these measuring instruments is output to the control device 200 as a data signal.

[0155] If the power generation system according to this embodiment includes a heat exchanger, the operation control unit 212 (control unit 210) may control the amount of air supplied to the first supply line according to the amount of heat exchange in the heat exchanger. Information on the amount of heat exchange in the heat exchanger is measured by measuring instruments etc. in the heat exchanger and acquired by the information acquisition unit 211. With this configuration, the amount of temperature adjustment required for the air supplied from the air supply unit 11 can be reduced.

[0156] The operation control unit 212 (control unit 210) may control the amount of external air supplied to the cathode electrode 6b of the fuel cell 6. This configuration allows for adjustment of the temperature of the exhaust gas discharged from the fuel cell 6.

[0157] The operation control unit 212 (control unit 210) may control the amount of water supplied to the steam reformer 5. This configuration allows for adjustment of the temperature of the exhaust gas discharged from the fuel cell 6.

[0158] The operation control unit 212 (control unit 210) may control the amount of organic hydride (MCH1a) supplied to the dehydrogenation reactor 1. With this configuration, the temperature of the exhaust gas discharged from the fuel cell 6 can be adjusted.

[0159] -Control Flow- Here, an example of the control flow of the power generation system 100 according to this embodiment will be explained with reference to Figure 8.

[0160] --Startup Process-- The operation control unit 212 (control unit 210) controls the startup process to start up the power generation system 100 as Step 11 (S11). In other words, the operation control unit 212 (control unit 210) controls the temperature rise of the various devices in the power generation system 100 until the dehydrogenation reactor 1 reaches a temperature at which it can perform the dehydrogenation reaction.

[0161] In Step 11 (S11), the exhaust gas combustor 7 is turned ON. Also in Step 11 (S11), the flow rate of air supplied from the feed line FL9 is defined as "a", and the flow rate of associated hydrogen 1b is defined as "b0". The flow rate of air supplied from the feed line FL9, a, is sometimes simply referred to as "flow rate a", and the flow rate of associated hydrogen 1b, b0, is sometimes simply referred to as "flow rate b0".

[0162] There are no particular restrictions on the flow rate a, and it can be appropriately selected according to the purpose, but it is preferable that it be at least twice the flow rate b0. It is preferable to gradually increase the flow rate a to the rated flow rate by the time Step 21 (S21) of the operation process described later is reached.

[0163] As described above, the associated hydrogen 1b can be used as a reducing gas to prevent oxidation of the catalysts in the dehydrogenation reactor 1 and fuel cell 6 during the startup process, and as fuel for the exhaust gas combustor 7. There are no particular restrictions on the flow rate b0, and it can be adjusted as appropriate within the range in which it can be used as a reducing gas and fuel.

[0164] The startup process includes a temperature determination step as Step 12 (S12) and Step 13 (S13).

[0165] In Step 12 (S12), the temperature of the dehydrogenation reactor 1 reaches a threshold (T ＤＨ 1) Determine whether or not it exceeds the threshold. Note that the determination in Step 12 (S12) is made when the temperature of the fluid at the outlet of the dehydrogenation reactor 1 is the threshold (T ＤＨ 1) The determination may be made by whether or not it exceeds the threshold. These determinations may be made by the determination unit 215. ＤＨ 1) If it exceeds the threshold, the flow proceeds to Step 13 (S13) (YES direction), and the temperature of the dehydrogenation reactor 1 reaches the threshold (T ＤＨ 1) If the following conditions are met, the flow proceeds to Step 11 (S11) (NO direction).

[0166] Threshold T ＤＨ 1 is a temperature higher than the temperature at which the dehydrogenation reaction begins. Threshold T ＤＨ As for option 1, it can be appropriately set according to the temperature suitable for the dehydrogenation reaction, for example, it can be set to 250°C.

[0167] In Step 13 (S13), the temperature of the hydrogen purification unit 4 reaches a threshold (T ＳＭ 1) Determine whether or not it exceeds the threshold. Note that the determination in Step 13 (S13) is made when the temperature of the fluid at the outlet of the hydrogen purification unit 4 is the threshold (T ＳＭ 1) The determination may be made by whether or not it exceeds the threshold. These determinations may be made by the determination unit 215. ＳＭ 1) If it exceeds the threshold, the flow proceeds to Step 21 (S21) (YES direction), and the temperature of the hydrogen purification unit 4 reaches the threshold (T ＳＭ 1) If the following conditions are met, the flow proceeds to Step 11 (S11) (NO direction).

[0168] The temperature of the hydrogen purification unit 4 reaches a threshold (T ＳＭ 1) By exceeding this threshold (T), the temperature of the hydrogen purification unit 4 can be sufficiently raised, preventing toluene from condensing when the power generation system 100 is in operation. ＳＭ1) There are no particular restrictions, and it can be selected as appropriate depending on the purpose; for example, it can be set to 100°C.

[0169] The startup process may include other temperature determination steps besides Step 12 (S12) and Step 13 (S13).

[0170] Other temperature determination steps include, for example, when the temperature of the steam reformer 5 reaches a threshold (T ＳＲ 1) It may be determined whether or not it exceeds the threshold (T). This determination is made by determining whether the fluid temperature at the outlet of the steam reformer 5 exceeds the threshold (T). ＳＲ 1) The determination may be made by whether or not it exceeds the threshold. These determinations may be made by the determination unit 215. ＳＲ 1) If it exceeds the threshold, the flow proceeds to Step 21 (S21) (YES direction), and the temperature of the steam reformer 5 reaches the threshold (T ＳＲ 1) If the following conditions are met, the flow proceeds to Step 11 (S11) (NO direction).

[0171] The temperature of the steam reformer 5 reaches a threshold (T ＳＲ 1) By exceeding this threshold (T), the temperature of the steam reformer 5 can be sufficiently raised, promoting the decomposition of toluene and suppressing the deterioration of the fuel cell 6. ＳＲ 1) There are no particular restrictions, and the temperature can be appropriately selected according to the purpose; for example, it can be set to 400°C.

[0172] Other temperature determination steps include determining when the temperature of the evaporator 9 reaches a threshold (T ＥＶＰ 1) It may also be determined whether or not the temperature exceeds the threshold (T). This determination is made by checking whether the temperature of the fluid at the outlet of the evaporator 9 exceeds the threshold (T). ＥＶＰ 1) The determination may be made by whether or not it exceeds the threshold. These determinations may also be made by the determination unit 215. ＥＶＰ 1) If it exceeds the threshold, the flow proceeds to Step 21 (S21) (YES direction), and the temperature of the evaporator 9 reaches the threshold (T ＥＶＰ 1) If the following conditions are met, the flow proceeds to Step 11 (S11) (NO direction).

[0173] The temperature of the evaporator 9 reaches the threshold (TＥＶＰ 1) If it exceeds this value, the temperature of the evaporator 9 can be sufficiently raised, which is preferable because it promotes the vaporization of water. Threshold (T ＥＶＰ 1) There are no particular restrictions, and it can be appropriately selected according to the purpose; for example, it can be set to 120°C.

[0174] --Operation Process-- Following the startup process, the operation control unit 212 (control unit 210) controls the operation process to operate the power generation system 100 as Step 21 (S21) to Step 42 (S42). In other words, the operation control unit 212 (control unit 210) controls the operation of various devices in the power generation system 100 so that the temperature of the dehydrogenation reactor 1 is maintained at a temperature suitable for the dehydrogenation reaction.

[0175] The operation process includes a dehydrogenation reaction initiation step as Step 21 (S21) and Step 22 (S22), an associated hydrogen supply cessation step as Step 3 (S3), and a dehydrogenation reactor temperature adjustment step as Step 41 (S41) and Step 42 (S42).

[0176] ---Dehydrogenation Reaction Initiation Process--- The dehydrogenation reaction initiation process is the process of initiating the dehydrogenation reaction in the dehydrogenation reactor 1. In Step 21 (S21), the flow rate of associated hydrogen 1b is defined as "bx", the flow rate of water supplied from feed lines FL6 and FL7 is defined as "cx", and the flow rate of MCH1a supplied from feed line FL1 is defined as "dx". The flow rate of associated hydrogen 1b, bx, may be simply referred to as "flow rate bx", the flow rate of water supplied from feed lines FL6 and FL7, cx, may be simply referred to as "flow rate cx", and the flow rate of MCH1a supplied from feed line FL1, dx, may be simply referred to as "flow rate dx".

[0177] The flow rate bx is preferably adjusted according to the flow rate dx of MCH1a so that the fluid composition at the inlet of the dehydrogenation reactor 1 satisfies the following equation (3): Fluid composition at the inlet of the dehydrogenation reactor = {(flow rate bx + hydrogen flow rate from recycling line RL) / (flow rate dx + toluene flow rate from recycling line RL + MCH flow rate from recycling line RL)} ≥ 0.55 (mol / mol) ... Equation (3)

[0178] By adjusting the flow rate bx to satisfy the above formula (3), carbon deposition caused by the decomposition of MCH and toluene on the dehydrogenation catalyst of the dehydrogenation reactor 1 can be suppressed, thereby suppressing the deterioration of the dehydrogenation reactor 1 and enabling long-term durable operation. These calculations may be performed by the calculation unit 214.

[0179] There are no particular restrictions on the flow rate cx, and it can be appropriately selected according to the purpose. However, when the amount of carbon flowing into the steam reformer 5 is C and the steam flow rate flowing into the steam reformer 5 is S, it is preferable to adjust it so that the following equation (4) is satisfied: S / C ≥ 2.5 ... (4)

[0180] By adjusting the flow rate cx to satisfy the above equation (4), toluene (C) can be produced by steam reforming. ７ H ８ ) can be sufficiently decomposed. That is, if the amount of toluene flowing into the steam reformer 5 is n (mol / h), it is preferable to set the steam flow rate S (mol / h) to be 2.5 × 7 × n or more. These calculations may be performed by the calculation unit 214.

[0181] There are no particular restrictions on the flow rate dx, and it can be appropriately selected according to the purpose. It is preferable to gradually increase it from 0 up to the rated flow rate.

[0182] The operation process includes a temperature determination step as Step 22 (S22). In Step 22 (S22), the temperature of the dehydrogenation reactor 1 is determined to be a threshold (T ＤＨ Determine whether the temperature is above the threshold (T). In Step 22 (S22), the determination is made based on whether the temperature of the fluid at the outlet of the dehydrogenation reactor 1 is above the threshold (T). ＤＨThe determination may also be made by determining whether the temperature is above the threshold (T). These determinations may also be made by the determination unit 215. ＤＨ If the temperature is above TH, the flow proceeds to Step 3 (S3) (YES direction), and the temperature of the dehydrogenation reactor 1 reaches the threshold (T ＤＨ If it is less than TH, the flow proceeds to Step 21 (S21) (NO direction).

[0183] Threshold (T ＤＨ TH) is the threshold (T ＤＨ 1) This temperature is higher than the threshold temperature, and more specifically, it is the temperature at which the dehydrogenation reaction occurs stably. Threshold T ＤＨ As for TH, there are no particular restrictions as long as the dehydrogenation reaction proceeds stably, and it can be appropriately selected according to the purpose. For example, it can be 300°C to 350°C.

[0184] In Step 22 (S22), the temperature of the dehydrogenation reactor 1 reaches a threshold (T ＤＨ In addition to determining whether the temperature is above the threshold (TH), it may also be determined whether the flow rate a and flow rate dx have reached the rated flow rate. These determinations may be made by the determination unit 215. Note that the temperature of the dehydrogenation reactor 1 is above the threshold (T ＤＨ If the flow rate is TH or higher, and the flow rates a and dx have reached the rated flow rate, it is preferable to proceed to Step 3 (S3).

[0185] ---Associated Hydrogen Supply Stoppage Process--- The associated hydrogen supply stoppage process is the process of stopping the supply of associated hydrogen 1b. In Step 3 (S3), the supply of associated hydrogen 1b is stopped. Since the second gas component G2 separated in the hydrogen purification unit 4 is supplied to the dehydrogenation reactor 1 via the recycling line RL, the dehydrogenation reactor 1 can continue to operate even if the supply of associated hydrogen 1b is stopped. When the supply of associated hydrogen 1b is stopped, the flow proceeds to Step 41 (S41).

[0186] ---Dehydrogenation Reactor Temperature Adjustment Process--- The dehydrogenation reactor temperature adjustment process is a process for adjusting the temperature of the dehydrogenation reactor 1. The temperature of the dehydrogenation reactor 1 is adjusted by mixing the exhaust gas discharged by the fuel cell 6 with external air (temperature adjustment air) supplied from the air supply unit 11.

[0187] In Step 41 (S41), the flow rate of the temperature-regulating air supplied by the air supply unit 11 is defined as "ex". The flow rate of the temperature-regulating air supplied by the air supply unit 11, ex, is sometimes simply referred to as "flow rate ex".

[0188] Here, an example of flow rate ex control will be explained with reference to Figure 9. Figure 9 is a graph showing an example of flow rate ex control for temperature-regulating air. Note that there are no particular restrictions on the unit of time shown on the horizontal axis of the graph in Figure 9; it may be seconds, minutes, or hours.

[0189] The flow rate ex is as shown in Figure 9, when the temperature of the dehydrogenation reactor 1 is the lower limit temperature (T) of the dehydrogenation reactor 1. ＤＨ Low) or higher, and the upper limit temperature (T) of the dehydrogenation reactor 1. ＤＨ It is preferable to adjust the temperature to be below High. The temperature information of the dehydrogenation reactor 1 and the flow rate ex information of the temperature-adjusting air are measured by measuring instruments M1 and M11, etc., and acquired by the information acquisition unit 211. For example, when the temperature of the dehydrogenation reactor 1 decreases, the lower limit temperature (T) of the dehydrogenation reactor 1 is lowered. ＤＨ When the temperature approaches Low, the flow rate ex can be reduced to raise the temperature of the dehydrogenation reactor 1. Also, for example, when the temperature of the dehydrogenation reactor 1 rises, the upper limit temperature (T) of the dehydrogenation reactor 1 can be reduced. ＤＨ When the temperature approaches High, the flow rate ex can be increased to lower the temperature of the dehydrogenation reactor 1. By controlling it in this way, the temperature of the dehydrogenation reactor 1 can be maintained at an appropriate temperature, and the dehydrogenation reactor 1 can be operated stably. In addition, deterioration and decomposition of the catalyst due to sintering and coking can be suppressed, thereby suppressing the deterioration of the dehydrogenation reactor 1 and enabling long-term durable operation.

[0190] Lower limit temperature (T) of dehydrogenation reactor 1 ＤＨ Low) may be determined based on the temperature of the fluid flowing into or out of the dehydrogenation reactor 1. More specifically, it is preferable that the temperature of the fluid (MCH1a) at the inlet of the dehydrogenation reactor 1 is 250°C or higher and 300°C or lower, and the temperature of the fluid (MCH1a) at the outlet of the dehydrogenation reactor 1 is 300°C or higher and 350°C or lower.

[0191] The upper limit temperature (T) of the dehydrogenation reactor 1 ＤＨ High) may be determined based on the temperature of the fluid flowing into or out of the dehydrogenation reactor 1. More specifically, it is preferable that the temperature of the fluid (MCH1a) at the inlet of the dehydrogenation reactor 1 is 300°C or higher and 350°C or lower, and the temperature of the fluid (MCH1a) at the outlet of the dehydrogenation reactor 1 is 350°C or higher and 400°C or lower.

[0192] From the viewpoint of avoiding a decrease in system efficiency due to an increase in power consumption on the air supply unit 11, it is preferable that the flow rate ex be less than the flow rate a.

[0193] In Step 41 (S41), the temperature of the dehydrogenation reactor 1 may be adjusted by controlling the temperature of the exhaust gas mixed with external air. Here, an example of temperature control of the exhaust gas combustor will be explained with reference to Figure 10. Figure 10 is a graph showing an example of temperature control of the exhaust gas combustor. Note that there are no particular restrictions on the unit of time shown on the horizontal axis of the graph in Figure 10; it may be seconds, minutes, or hours.

[0194] As shown in Figure 10, it is preferable to switch the operation (ON / OFF) of the exhaust gas combustor 7 to maintain a predetermined temperature of the dehydrogenation reactor 1 or the exhaust gas. In other words, it is preferable for the operation control unit 212 (control unit 210) to switch the operation (ON / OFF) of the exhaust gas combustor 7 to maintain a predetermined temperature of the dehydrogenation reactor 1 or the exhaust gas. For example, if the temperature of the dehydrogenation reactor 1 or the exhaust gas is below the predetermined temperature, the exhaust gas combustor 7 can be turned ON to raise the temperature of the exhaust gas, i.e., to raise the temperature of the dehydrogenation reactor 1. Also, for example, if the temperature of the dehydrogenation reactor 1 or the exhaust gas is above the predetermined temperature, the operation of the exhaust gas combustor 7 can be stopped (OFF) to lower the temperature of the exhaust gas, i.e., to lower the temperature of the dehydrogenation reactor 1. If the exhaust gas does not rise despite the exhaust gas combustor 7 being in operation, a stop command is issued as a misfire determination. The predetermined temperatures for the dehydrogenation reactor 1 and the exhaust gas can be set appropriately according to the flow rate ex, etc. By controlling in this way, the temperature of the dehydrogenation reactor 1 can be maintained at an appropriate temperature, and the dehydrogenation reactor 1 can be operated stably.

[0195] The dehydrogenation reactor temperature adjustment process will be explained again with reference to Figure 8. In Step 42 (S42), whether or not a stop command has been received, the temperature of the dehydrogenation reactor 1 is set to the upper limit temperature (T) of the dehydrogenation reactor 1. ＤＨ Whether the temperature is higher than High, or whether the temperature of the dehydrogenation reactor 1 is higher than the lower limit temperature (T) of the dehydrogenation reactor 1. ＤＨ Determine whether it is lower than Low. These determinations may also be made by the determination unit 215. If a stop command is received, the temperature of the dehydrogenation reactor 1 is set to the upper limit temperature (T) of the dehydrogenation reactor 1. ＤＨ If the temperature is higher than High, or if the temperature of the dehydrogenation reactor 1 is higher than the lower limit temperature (T) of the dehydrogenation reactor 1, ＤＨ If the temperature is lower than Low, the flow proceeds to Step 5 (S5) (YES direction). If a stop command has not been received, the temperature of the dehydrogenation reactor 1 will be lowered to the upper limit temperature of the dehydrogenation reactor 1 (T ＤＨIf the temperature is below High, and the temperature of the dehydrogenation reactor 1 is below the lower limit temperature (T) of the dehydrogenation reactor 1 ＤＨ If the value is Low or higher, the flow proceeds to Step 41 (S41) (No direction).

[0196] --Shutdown Process-- Following the operation process, the operation control unit 212 (control unit 210) controls a shutdown process to stop the power generation system 100 as Step 5 (S5). In the shutdown process, the supply of various fluids is stopped, and the operation of the exhaust gas combustor 7 is also stopped.

[0197] The operation process may include a dehydrogenation reaction initiation step, an associated hydrogen supply cessation step, and a dehydrogenation reactor temperature adjustment step, as well as a dehydrogenation reactor reheating step. Here, the dehydrogenation reactor reheating step will be explained with reference to Figure 11.

[0198] The operation control unit 212 (control unit 210) may, following the dehydrogenation reaction temperature adjustment step, control the dehydrogenation reactor reheating step as Step 43 (S43) to Step 46 (S46). The dehydrogenation reactor reheating step is a step in which, when the temperature of the dehydrogenation reactor 1 falls below a predetermined temperature, the operation of the exhaust gas combustor 7 is stopped and the heater provided in the mixer 10 is activated.

[0199] In Step 43 (S43), the temperature of the dehydrogenation reactor 1 reaches a threshold (T ＤＨ Determine whether the temperature is less than the threshold (T). In Step 43 (S43), the determination is made based on whether the temperature of the fluid at the outlet of the dehydrogenation reactor 1 is less than the threshold (T). ＤＨ The determination may also be made by determining whether or not the temperature is less than the threshold (T). These determinations may also be made by the determination unit 215. ＤＨ If the temperature is less than the threshold (T), the flow proceeds to Step 44 (S44) (YES direction), and the temperature of the dehydrogenation reactor 1 reaches the threshold (T). ＤＨ If the value is TH or higher, the flow proceeds to Step 41 (S41) (NO direction).

[0200] The threshold value (T) of the dehydrogenation reactor 1 in Step 43 (S43) ＤＨ TH) is the threshold (T) in Step 22 (S42). ＤＨThe same as TH can be adopted.

[0201] In Step 44 (S44), the operation of the exhaust gas combustor 7 is stopped, and the heater of the mixer 10 (hereinafter sometimes referred to as the "mixer heater") is turned ON. There are no particular restrictions on the mixer heater, and any known type can be used. At this time, it is preferable to also stop the temperature control of the dehydrogenation reactor 1 by flow rate ex control. By operating the mixer heater, the exhaust gas can be burned in the mixer 10 located upstream of the dehydrogenation reactor 1, and the dehydrogenation reactor 1 can be selectively heated.

[0202] In Step 45 (S45), the temperature of the dehydrogenation reactor 1 is set to a threshold (T) in the same manner as in Step 43 (S43). ＤＨ The temperature of the dehydrogenation reactor 1 is determined again to be less than the threshold (T). ＤＨ If the temperature is less than the threshold (T), the flow proceeds to Step 46 (S46) (YES direction), and the temperature of the dehydrogenation reactor 1 reaches the threshold (T). ＤＨ If the value is TH or higher, the flow proceeds to Step 41 (S41) (NO direction).

[0203] In Step 46 (S46), it is determined whether or not a stop command has been received, and the temperature of the dehydrogenation reactor 1 is the upper limit temperature (T) of the dehydrogenation reactor 1. ＤＨ Whether the temperature is higher than High, or whether the temperature of the dehydrogenation reactor 1 is higher than the lower limit temperature (T) of the dehydrogenation reactor 1. ＤＨ It is determined whether the temperature is lower than the upper limit temperature (T) of the dehydrogenation reactor 1, and whether the operating time of the dehydrogenation reactor 1 has elapsed for a predetermined time. These determinations may also be made by the determination unit 215. If a stop command is received, the temperature of the dehydrogenation reactor 1 is lowered to the upper limit temperature (T) of the dehydrogenation reactor 1. ＤＨ If it is higher than High, the temperature of the dehydrogenation reactor 1 will be lower than the lower limit temperature (T) of the dehydrogenation reactor 1. ＤＨ If the temperature is lower than Low, or if the operating time of the dehydrogenation reactor 1 has elapsed for a predetermined time, the flow proceeds to Step 5 (S5) (YES direction). If a stop command has not been received, the temperature of the dehydrogenation reactor 1 is lower than the upper limit temperature (T) of the dehydrogenation reactor 1. ＤＨIf the temperature is below High, the temperature of the dehydrogenation reactor 1 will be lower than the lower limit temperature (T) of the dehydrogenation reactor 1. ＤＨ If the value is Low or higher, and if the operating time of the dehydrogenation reactor 1 has not elapsed for a predetermined time, the flow proceeds to Step 44 (S44) (NO direction).

[0204] The upper limit temperature (T) of the dehydrogenation reactor 1 ＤＨ High), and the lower limit temperature (T) of the dehydrogenation reactor 1. ＤＨ Low) can be the same as Step 42 (S42) in Figure 8. There are no particular restrictions on the predetermined operating time of the dehydrogenation reactor 1, and it can be set appropriately considering the durability of various devices in the power generation system.

[0205] The operation control unit 212 (control unit 210) may, in the operation process of the power generation system 102 according to the third embodiment, supply anode off-gas discharged from the anode side of the fuel cell 6 to the exhaust gas combustor when the temperature of the dehydrogenation reactor 1 falls below a predetermined temperature, thereby controlling the exhaust gas to rise in temperature. With this configuration, when the temperature of the dehydrogenation reactor 1 decreases, the exhaust gas combustor 7 located upstream of the dehydrogenation reactor 1 increases the exhaust gas temperature, selectively raising the temperature of the dehydrogenation reactor 1.

[0206] In the power generation system 101 according to the second embodiment, the operation control unit 212 (control unit 210) may control the operation of the exhaust gas combustor 7 when the temperature of the steam reformer 5 is lower than a predetermined temperature. With this configuration, when the temperature of the steam reformer 5 decreases, the exhaust gas combustor 7, which is located upstream of the steam reformer 5, increases the exhaust gas temperature, thereby selectively raising the temperature of the steam reformer 5.

[0207] The information transmission unit 216 transmits the information acquired by the information acquisition unit 211, the operation control unit 212, the calculation unit 214, and the determination unit 215 to the power generation system 100 and the like.

[0208] As described above, embodiments of the present invention have been explained, but these embodiments are presented as examples only, and the present invention is not limited by these embodiments. The above embodiments can be implemented in various other forms, and various combinations, omissions, substitutions, or modifications are possible without departing from the spirit of the invention. The above embodiments and their variations are included in the scope or spirit of the invention, as well as in the scope of the invention and its equivalents as described in the claims.

[0209] The embodiments of the present invention disclosed above are further specified by, for example, the following embodiments: [1] A power generation system comprising: a dehydrogenation reactor (1) that generates hydrogen by a dehydrogenation reaction; a fuel cell (6) that generates electricity using the hydrogen; a first supply line that supplies exhaust gas discharged by the fuel cell (6) to the dehydrogenation reactor (1); and an air supply unit (11) that supplies air from the outside to the first supply line. [2] The power generation system according to [1], wherein the air supply unit (11) adjusts the temperature of the exhaust gas by supplying the air to the first supply line. [3] The power generation system according to [2], further comprising a mixer (10) arranged in the first supply line that mixes the exhaust gas and the air, wherein the air supply unit (11) supplies the air to the mixer (10). [4] The power generation system according to [3], comprising a steam reformer (5) arranged in the first supply line and connected to the anode side of the fuel cell (6), wherein the mixer (10) is arranged in the first supply line between the steam reformer (5) and the dehydrogenation reactor (1). [5] The power generation system according to [4], comprising an exhaust gas combustor (7) for burning the exhaust gas, wherein the exhaust gas combustor (7) is arranged in the first supply line between the steam reformer (5) and the dehydrogenation reactor (1). [6] The power generation system according to [5], wherein the exhaust gas combustor (7) is connected to the anode side of the fuel cell (6). [7] The power generation system according to any one of [4] to [6], wherein the temperature of the exhaust gas is adjusted by adjusting the amount of water supplied to the steam reformer (5). [8] The power generation system according to any one of [3] to [7], comprising an air preheater (8) arranged in the first supply line and connected to the cathode side of the fuel cell (6), wherein the mixer (10) is arranged in the first supply line between the air preheater (8) and the dehydrogenation reactor (1). [9] The power generation system according to [8], comprising an exhaust gas combustor (7) for burning the exhaust gas, wherein the exhaust gas combustor (7) is arranged in the first supply line between the air preheater (8) and the dehydrogenation reactor (1).

[10] The power generation system according to [9], wherein the exhaust gas combustor (7) is connected to the anode side of the fuel cell (6).

[11] The power generation system according to any one of [8] to

[10] , wherein the temperature of the exhaust gas is adjusted by adjusting the amount of air supplied to the air preheater (8).

[12] The power generation system according to [3], comprising an exhaust gas combustor (7) for burning the exhaust gas, a hydrogen purification unit (4) for producing hydrogen, and a second supply line for supplying the exhaust gas supplied to the dehydrogenation reactor (1) to the hydrogen purification unit (4), wherein the exhaust gas combustor (7) is located in the second supply line between the dehydrogenation reactor (1) and the hydrogen purification unit (4).

[13] The power generation system according to

[12] , comprising an evaporator (9) located in the second supply line for heating water supplied from an external source to produce steam, wherein the exhaust gas combustor (7) is located in the second supply line between the dehydrogenation reactor (1) and the evaporator (9).

[14] The power generation system according to [3], comprising: a steam reformer (5) arranged in the first supply line and connected to the anode side of the fuel cell (6); an air preheater (8) arranged in the first supply line and connected to the cathode side of the fuel cell (6); and an exhaust gas combustor (7) for burning the exhaust gas, wherein the exhaust gas combustor (7) is arranged in the first supply line between the air preheater (8) and the steam reformer (5).

[15] The power generation system according to any one of [1] to

[14] , wherein the temperature of the exhaust gas is adjusted by adjusting the amount of organic hydride supplied to the dehydrogenation reactor (1).

[0210] This application claims priority based on Japanese Patent Application No. 2025-45540, filed with the Japan Patent Office on 19 March 2025, and incorporates all the contents of the said application.

[0211] 1 Dehydrogenation Reactor 1a MCH 1b Associated Hydrogen 2 Gas-Liquid Separation Unit 3 Compressor 4 Hydrogen Purification Unit 5 Steam Reformer 6 Fuel Cell 6a Anode Electrode 6b Cathode Electrode 6c Electrolyte Membrane 7 Exhaust Gas Combustor 8 Air Preheater 9 Evaporator 100, 101, 102, 103 Power Generation System 200 Control Device 210 Control Unit 211 Information Acquisition Unit 212 Operation Control Unit 214 Calculation Unit 215 Judgment Unit 216 Information Transmission Unit 300 Terminal Device SL1-6 First Supply Line SL7-8 Second Supply Line FL1-11 Feed Line RL Recycling Line M1-M11 Measuring Instruments

Claims

1. A power generation system comprising: a dehydrogenation reactor that generates hydrogen by a dehydrogenation reaction; a fuel cell that generates electricity using the hydrogen; a first supply line that supplies exhaust gas discharged by the fuel cell to the dehydrogenation reactor; and an air supply unit that supplies air from the outside to the first supply line.

2. The power generation system according to claim 1, wherein the air supply unit adjusts the temperature of the exhaust gas by supplying the air to the first supply line.

3. The power generation system according to claim 2, comprising a mixer arranged in the first supply line for mixing the exhaust gas and the air, wherein the air supply unit supplies the air to the mixer.

4. The power generation system according to claim 3, comprising a steam reformer arranged in the first supply line and connected to the anode side of the fuel cell, wherein the mixer is arranged in the first supply line between the steam reformer and the dehydrogenation reactor.

5. The power generation system according to claim 4, comprising an exhaust gas combustor for burning the exhaust gas, wherein the exhaust gas combustor is located in the first supply line between the steam reformer and the dehydrogenation reactor.

6. The power generation system according to claim 5, wherein the exhaust gas combustor is connected to the anode side of the fuel cell.

7. The power generation system according to any one of claims 4 to 6, wherein the temperature of the exhaust gas is adjusted by adjusting the amount of water supplied to the steam reformer.

8. The power generation system according to claim 3, comprising an air preheater arranged in the first supply line and connected to the cathode side of the fuel cell, wherein the mixer is arranged in the first supply line between the air preheater and the dehydrogenation reactor.

9. The power generation system according to claim 8, comprising an exhaust gas combustor for burning the exhaust gas, wherein the exhaust gas combustor is located in the first supply line between the air preheater and the dehydrogenation reactor.

10. The power generation system according to claim 9, wherein the exhaust gas combustor is connected to the anode side of the fuel cell.

11. The power generation system according to any one of claims 8 to 10, wherein the temperature of the exhaust gas is adjusted by adjusting the amount of air supplied to the air preheater.

12. The power generation system according to claim 3, comprising: an exhaust gas combustor for burning the exhaust gas; a hydrogen purification unit for producing hydrogen; and a second supply line for supplying the exhaust gas supplied to the dehydrogenation reactor to the hydrogen purification unit, wherein the exhaust gas combustor is located in the second supply line between the dehydrogenation reactor and the hydrogen purification unit.

13. The power generation system according to claim 12, comprising an evaporator located in the second supply line and heating water supplied from an external source to generate steam, wherein the exhaust gas combustor is located in the second supply line between the dehydrogenation reactor and the evaporator.

14. The power generation system according to claim 3, comprising: a steam reformer disposed in the first supply line and connected to the anode side of the fuel cell; an air preheater disposed in the first supply line and connected to the cathode side of the fuel cell; and an exhaust gas combustor for burning the exhaust gas, wherein the exhaust gas combustor is disposed in the first supply line between the air preheater and the steam reformer.

15. The power generation system according to any one of claims 1 to 6, wherein the temperature of the exhaust gas is adjusted by adjusting the amount of organic hydride supplied to the dehydrogenation reactor.

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