Reactors or methods for producing hydrogen.

Abstract

To provide an apparatus capable of producing hydrogen stably.SOLUTION: A reactor for producing hydrogen is provided which comprises a reaction vessel that performs a first process of generating alkali metal oxides and hydrogen by reacting alkali metals with alkali metal hydroxides, a second process of generating alkali metal peroxides and alkali metals by heating the alkali metal oxides, and a fourth process of generating alkali metal hydroxides and oxygen by reacting the alkali metal peroxides with water, a condensing vessel that performs a third process of condensing the alkali metals generated in the second process, and a moving part that connects the reaction vessel and the condensing vessel and moves the alkali metals between the reaction vessel and the condensing vessel.SELECTED DRAWING: Figure 3

Description

Technical Field

[0001] The present invention relates to a reactor for hydrogen production or a hydrogen production method.

Background Art

[0002] As a conventional technique, a hydrogen production method by low-temperature thermochemical water splitting that uses heat to produce hydrogen has been proposed (Non-Patent Document 1).

Prior Art Documents

Non-Patent Documents

[0003]

Non-Patent Document 1

Summary of the Invention

Problems to be Solved by the Invention

[0004] In the prior art, the theory of hydrogen production has been clarified. However, neither the apparatus nor the method for stably producing hydrogen using this theory has been clarified.

Means for Solving the Problems

[0005] To solve the aforementioned problems, the present invention provides, in one aspect, a reactor for hydrogen production comprising: a reaction vessel that carries out a first step of reacting an alkali metal with an alkali metal hydroxide to produce an alkali metal oxide and hydrogen; a second step of heating the alkali metal oxide to produce an alkali metal peroxide and alkali metal; and a fourth step of reacting the alkali metal peroxide with water to produce an alkali metal hydroxide and oxygen; a condensing vessel that carries out a third step of condensing the alkali metal generated in the second step; and a transfer unit that connects the reaction vessel and the condensing vessel and moves the alkali metal between the reaction vessel and the condensing vessel. [Effects of the Invention]

[0006] According to the present invention, an apparatus or method for stably producing hydrogen can be provided. [Brief explanation of the drawing]

[0007] [Figure 1] This is a diagram showing the configuration of the power generation system according to the first embodiment. [Figure 2] This figure shows the configuration of the ORC power generation mechanism according to the first embodiment. [Figure 3] This is a diagram showing the configuration of the reactor according to the first embodiment. [Figure 4] This diagram shows the process of reaction 1 in the reactor in the order of (a) to (c). [Figure 5] This diagram shows the processes of reactions 2 and 3 in the reactor in the order of (a) to (c). [Figure 6] This diagram shows the process of reaction 4 in the reactor in the order of (a) to (c). [Figure 7] This diagram shows the process of reaction 4 in the reactor in the order of (a) to (b). [Figure 8] (a) This graph shows the temperature progression in the reactor. Figures (b) and (c) are graphs showing the temperature progression in the second and third reactors (modified versions). [Figure 9]This diagram illustrates the transfer of heat and power generation efficiency in a power generation system, showing the calculation results for cases where the heat supplied from the heat source is (a) 100°C and (b) 150°C. [Figure 10] This is a diagram showing a power generation system according to the second embodiment. [Figure 11] This diagram shows the configuration of a power generation system that uses steam as a low-temperature heating medium, as shown in the modified example. [Figure 12] This diagram shows the configuration of a power generation system that uses air as a low-temperature heating medium, as shown in the modified example. [Modes for carrying out the invention]

[0008] <First Embodiment> Referring to Figures 1 to 9, a power generation system 100, which is one embodiment of the power generation method, will be described below. Figure 1 is a diagram showing an example of the configuration of the power generation system 100.

[0009] In the specification and drawings, the state of a substance—solid, liquid, or gas—is indicated by adding (s), (l), and (g), respectively, after the substance name.

[0010] (overview) As shown in Figure 1, the power generation system 100 comprises a heat source 1, a heat exchanger 2, a reactor 3, a hydrogen (H2) tank 4, a compressor 5, a power generation mechanism 6, an ORC power generation mechanism 7, a fan 8, a pump 9, and supply units 10A, 10B, and 10C.

[0011] Heat source 1 includes waste heat discharged from at least one of a power plant and / or factory. For example, waste heat from a boiler flue or manufacturing equipment. Alternatively, heat source 1 may include a heat source derived from natural energy such as solar heat.

[0012] The temperature of the heat supplied from heat source 1 is between 100°C (100 degrees Celsius) and less than 400°C, and especially when it is waste heat from a factory or power plant, it is between 100°C and 200°C.

[0013] The heat exchanger 2 has a function of heating a medium (low-temperature heating medium) using the heat from the heat source 1. In this embodiment, water is used as the low-temperature heating medium as shown in FIG. 1. In this case, the heat exchanger 2 heats the water to generate steam (100°C or higher and 150°C or lower). In addition, as the low-temperature heating medium that transports heat from the heat source 1, various substances other than water, such as gases like air, can be considered.

[0014] The reactor 3 receives heat supply from the heat exchanger via a low-temperature heating medium and produces hydrogen. The method for producing hydrogen used by the reactor 3 is low-temperature thermochemical water splitting using an alkali metal such as sodium, potassium, or lithium (see Non-Patent Document 1). In this embodiment, sodium is used as the alkali metal, and the details will be described later.

[0015] The hydrogen tank 4 is a tank that stores the hydrogen produced by the reactor 3. The compressor 5 has a function of taking out hydrogen from the hydrogen tank 4, pressurizing it, and supplying it to the power generation mechanism 6.

[0016] The power generation mechanism 6 is a mechanism that generates electricity using hydrogen as fuel. The power generation mechanism 6 includes an engine 61 and a generator 62.

[0017] The engine 61 is a device that generates power using hydrogen as fuel. In this embodiment, a rotary engine is used. The generator 62 obtains power from the engine 61 and generates electricity. The engine 61 generates high-temperature waste heat.

[0018] Note that an engine other than a rotary engine, such as a reciprocating engine or a gas turbine, may be used for the engine 61, or a fuel cell may be used as the power generation mechanism 6. Although any of these devices generates heat, it is preferable to use a rotary engine with a high waste heat temperature as the engine 61. In addition, the rotary engine has a large inertial force of the rotor, which is different from a reciprocating engine, and is suitable for steady operation.

[0019] The ORC power generation mechanism 7 is a mechanism that generates electricity using an organic Rankine cycle (ORC) with an organic medium that vaporizes at temperatures below 100°C. The ORC power generation mechanism 7 comprises an evaporator 71, a turbine 72, a generator 73 driven by the turbine 72, and a condenser 74 (Figure 2).

[0020] The evaporator 71 is a device that heats and evaporates an organic medium. Figure 2 shows an example in which silicone oil is used as the organic medium. The heat source for the evaporator 71 is heated air or steam at approximately 100°C generated in the reactor 3.

[0021] The organic medium evaporated in the evaporator 71 drives the turbine 72, and the generator 73 receives power from the turbine 72 to generate electricity.

[0022] After driving the turbine 72, the organic medium condenses in the condenser 74 and is then supplied back to the evaporator 71 by a pump.

[0023] Fan 8 has the function of supplying outside air to reactor 3 as a cooling medium.

[0024] Pump 9 has the function of supplying water cooled in the evaporator 71 to the heat exchanger 2.

[0025] The supply unit 10A has the function of supplying heat generated by the power generation mechanism 6 to the engine 61. In this embodiment, the supply unit 10A uses the waste heat of the engine 61 to generate steam at a temperature of 500°C to 800°C, and supplies the generated steam to the reactor 3 via piping as a high-temperature heating medium.

[0026] The supply section 10B is a pipe that supplies heat from the heat source 1 to the reactor 3 using a low-temperature heating medium. While water or air can be used as the low-temperature heating medium, water is used in this embodiment.

[0027] The supply section 10C is a pipe that receives air from the fan 8 and supplies it to the reactor 3 as a cooling medium.

[0028] (Details of the reactor) The details of reactor 3 are described below. Reactor 3 is a device that performs low-temperature thermochemical water splitting using a sodium redox cycle. As shown in Figure 3, reactor 3 comprises a heat exchange section 31, a reaction section 32, a condensation section 33, a cooling section 34, piping 35A, 35B, piping 37A, 37B, and 37C, all of which are housed inside the containment vessel 30.

[0029] The containment vessel 30 is the outer shell of the reactor 3 and houses the main components of the reactor 3. The inside of the containment vessel 30 is filled with an inert gas such as nitrogen to prevent fire and damage in the event of a sodium spill.

[0030] The reaction section 32 is a sealable container where hydrogen is generated and produced. Sodium or sodium compounds are stored in the reaction section 32. The reaction section 32 is connected to the condensation section 33 via pipes 35A and 35B. The sodium stored in the reaction section 32 is movable between the reaction section 32 and the condensation section 33 via pipes 35A and 35B. Pipes 37A, 37B, and 37C are connected to the top of the reaction section 32 for the discharge or supply of water, oxygen, and hydrogen.

[0031] The heat exchange unit 31 is a device that heats and cools the reaction unit 32. The heat exchange unit 31 is connected to supply units 10A, 10B, and 10C, from which it receives high-temperature heating medium, low-temperature heating medium, and cooling medium, respectively. Each of the supply units 10A, 10B, and 10C is equipped with a valve near the connection point to the heat exchange unit 31, allowing the piping to be opened and closed.

[0032] The condensing unit 33 is a hollow container and has the function of condensing the sodium vaporized in the reaction unit 32. The condensing unit 33 is connected to the reaction unit 32 via pipes 35A and 35B, and exchanges sodium between the two units.

[0033] Pipes 35A and 35B are each equipped with valves that allow them to be opened and closed. Furthermore, pipes 35A and 35B are heated to prevent phase changes in the sodium passing through them.

[0034] The pipe 35A connects the upper part of the reaction section 32 and the upper part of the condensation section 33, and the pipe 35A has the function of moving vaporized sodium from the reaction section 32 to the condensation section 33.

[0035] The piping 35B connects the lower part of the reaction section 32 and the lower part of the condensation section 33, and has the function of flowing liquid sodium from the condensation section 33 to the reaction section 32. The piping 35B is sloped downward from the condensation section 33 to the reaction section 32, facilitating the flow of sodium.

[0036] The cooling unit 34 is a hollow container mounted around the condensing unit 33 and has the function of cooling the condensing unit 33. The cooling unit 34 is connected to the supply unit 10C and receives air as a cooling medium inside. The cooling unit 34 is also connected to the supply unit 10B and receives steam (low-temperature heating medium). Therefore, the cooling unit 34 can also heat the condensing unit 33.

[0037] Piping 37A, 37B, and 37C are connected to the reaction section 32. Each of the pipes 37A, 37B, and 37C is equipped with a valve that allows the pipe to be opened and closed. Piping 37A has the function of supplying water to the reaction section 32, and pipe 37B has the function of discharging oxygen (g) from the reaction section 32. Piping 37C connects the reaction section 32 to the hydrogen tank 4 and has the function of supplying hydrogen from the reaction section 32 to the hydrogen tank 4.

[0038] (Hydrogen production) Hydrogen production in reactor 3 consists of four processes: Reactions 1 to 4. Briefly, Reaction 1 is the process of reacting an alkali metal (sodium in this embodiment) with an alkali metal hydroxide to produce alkali metal oxide and hydrogen. Reaction 2 is the process of decomposing the alkali metal oxide to produce alkali metal peroxide and alkali metal. Reaction 3 is the process of condensing the alkali metal and is carried out in parallel with Reaction 2. Reaction 4 is the process of reacting alkali metal peroxide with water to produce alkali metal hydroxide and oxygen.

[0039] The details of each reaction will be explained sequentially below using Figures 4 to 8.

[0040] [Response 1] In reaction 1, the low-temperature heating medium and high-temperature heating medium are first supplied to the heat exchange section 31 by the supply sections 10A and 10B, and the reaction section 32 is heated to 350°C (Figure 4(a)). Both pipes 35A and 35B are closed.

[0041] As the reaction section 32 is heated, the liquid sodium and sodium hydroxide (s) stored in the reaction section 32 are heated, and sodium oxide (s) and hydrogen (g) are produced (Figures 4(b), (c)). This is an endothermic reaction. The generated hydrogen (g) is removed from the reaction section 32 via piping 37C and supplied to the hydrogen tank 4.

[0042] [Reaction 2] Next, the reaction section 32 and the sodium oxide(s) inside it are further heated to 400°C using a low-temperature heating medium and a high-temperature heating medium (Figure 5(a)). Meanwhile, a cooling medium is supplied to the cooling section 34 via the supply section 10C, and the condensation section 33 is kept below 100°C.

[0043] Upon heating, sodium oxide (s) decomposes into sodium peroxide (s) and sodium (g) (Figure 5(b)). As sodium (g) is generated, pipe 37A opens, and sodium (g) moves to the condensation section 33.

[0044] Once the movement of the generated sodium (g) is complete, pipe 35A is closed again (Figure 5(c)).

[0045] By transferring all of the sodium (g) in reaction 2 to the condensation section 33, it is prevented that the water and sodium will react explosively in the subsequent reaction 4.

[0046] [Response 3] The sodium (g) that moves to the condensation section 33 is cooled to below 100°C and condenses to become sodium (l, s) (Figure 5(b)). If sodium (s) is present, the condensation section 33 may be heated later by the cooling section 34 to melt the sodium (s).

[0047] [Reaction 4] In reaction 4, a cooling medium is first supplied from the supply unit 10C to the heat exchange unit 31, and the reaction unit 32 is maintained at 110°C (Figure 6(a)). Meanwhile, the condensation unit 33 is kept below 100°C, and sodium (l, s) is retained inside. At the same time, water (l) is injected into the reaction unit 32 from the pipe 37A.

[0048] Inside the reaction section 32, sodium peroxide (s) and water (l) react to produce oxygen (g) and sodium hydroxide (s) (Figure 6(b)). The injection of water (l) continues until all of the sodium peroxide (s) has reacted (Figure 6(c)). The generated oxygen (g) is discharged from the reaction section 32 through piping 37B.

[0049] After all the sodium peroxide (s) has reacted, pipe 35B is opened, and sodium (l) moves from the condensation section 33 to the reaction section 32 (Figure 7(a)). After the movement of sodium (l) is complete, pipe 35B is closed.

[0050] After reaction 4 is complete, the conditions are the same as at the start of reaction 1, as shown in Figure 7(b). Figure 8(a) shows the temperature change of reactor 3 during reactions 1 to 4. As shown in this figure, hydrogen production continues by repeating the cycle (period) of reactions 1 to 4 in reactor 3.

[0051] (Thermal efficiency) The power generation efficiency of the power generation system 100 configured as described above will be explained using Figure 9. In Figure 9, the transfer of heat in the power generation system 100 is shown by arrows, and the amount of heat consumed in each device and mechanism is also calculated.

[0052] The numbers in parentheses in Figure 9 indicate the amount of heat supplied to each device and mechanism, with the amount of heat supplied from heat source 1 to reactor 3 being normalized to 100.

[0053] In Figure 9, it is assumed that 35% of the heat supplied to reactor 3 is used for hydrogen production, and 65% of the heat is discharged.

[0054] In the ORC power generation mechanism 7, 60% of the heat discharged from reactor 3 is utilized, and 19% of that 60% is converted into electricity. In addition, the power generation mechanism 6 uses a rotary engine as the engine 61, and 30% of the heat generated by the combustion of hydrogen is converted into electricity.

[0055] Under these assumptions, the amount of heat used for hydrogen production in reactor 3, the amount of heat discharged, and the power generation efficiency in ORC power generation mechanism 7 and power generation mechanism 6 are calculated as shown in Figure 9.

[0056] More specifically, since the waste heat from the rotary engine, which is the engine 61, is high temperature, steam (high-temperature heating medium) at 500°C to 800°C is generated from the engine's waste heat and added to the 100°C steam (low-temperature heating medium) supplied from the heat source 1, thereby obtaining steam at 400°C or higher. By using steam at 400°C or higher in reactor 3, low-temperature thermochemical hydrolysis, which requires temperatures above 400°C, becomes possible.

[0057] In this case, the amount of heat that should be supplied from the engine 61 is only about 22% of the amount of heat from the heat source 1 (about 75% of the engine waste heat). This is evident from the fact that the specific enthalpy of 400°C superheated steam at 0.1 MPa (1 atmosphere) is about 122% of the specific enthalpy of 100°C superheated steam (2676 kJ / kg).

[0058] The overall power generation efficiency of the power generation system 100 can be derived as 21.8%, since the total power generation of the system is 21.8, calculated by adding the power generated by the power generation mechanism 6 (12.8) and the power generated by the ORC power generation mechanism 7 (9.0). The power generation system 100 achieves such high-efficiency power generation even while using waste heat at 100°C.

[0059] Furthermore, if the heat from heat source 1 is 150°C, the heat supplied to reactor 3 can be set to 450°C, and as shown in Figure 9(b), the power generation efficiency becomes even higher at 22.6%. Thus, the higher the temperature supplied from heat source 1, the higher the power generation efficiency of the system.

[0060] Since the temperature of the heat supplied from heat source 1 is less than 400°C, hydrogen production cannot be carried out by directly using this heat. If hydrogen production is not possible, only ORC power generation can be carried out from the 100°C waste heat, and the overall power generation efficiency of the system can only be expected to be about 11%.

[0061] On the other hand, the power generation system 100 incorporates a power generation mechanism 6 that generates high-temperature waste heat, thereby achieving a temperature of over 400°C and enabling hydrogen production by low-temperature thermochemical hydrolysis. The power generated is then used as fuel to achieve the high-efficiency power generation described above.

[0062] In particular, it is noteworthy that the power generation efficiency of power generation mechanism 6 is 12.8%, which is higher than that of ORC power generation mechanism 7. This suggests that the power generation efficiency is equivalent to or higher than conventional systems using only the heat source 1 - reactor 3 - power generation mechanism 6 system.

[0063] <Second Embodiment> In the first embodiment, steam was used as the low-temperature heating medium, but in the second embodiment, as shown below, air can also be used as the low-temperature heating medium.

[0064] Figure 10 shows a power generation system 101 according to a second embodiment, in which air is used as a low-temperature heating medium. In the power generation system 101, air is used as a low-temperature heating medium heated in the heat exchanger 2. The air heated in the heat exchanger 2 is supplied to the reactor 3 by the supply unit 10B as heated air between 100°C and 150°C.

[0065] Furthermore, in the power generation system 101, a fan 8 supplies air to the heat exchanger 2 instead of the pump 9, thus omitting the pump 9 and resulting in a simpler configuration. The other configurations are the same as those of the power generation system 100 in the first embodiment.

[0066] In the power generation system 101 described above, as in the first embodiment, highly efficient power generation can be performed using hydrogen production by low-temperature thermochemical hydrolysis.

[0067] <Variation> Furthermore, in the first and second embodiments, the power generation systems 100 and 101 were configured to have one reactor 3, but as a modified example, a configuration using multiple reactors 3 may be used, as shown in Figures 11 and 12.

[0068] Figures 11 and 12 show power generation systems 100A and 101A, respectively, which use steam and air as low-temperature heating media. Both systems are equipped with multiple reactors 3 in parallel.

[0069] In power generation systems 100A and 101A, the phases of the cycles of reactions 1 to 4 in the hydrogen production process are shifted among multiple reactors 3. Figures 8(a) to 8(c) show the cycles of hydrogen production by three reactors 3 (referred to as reactors 1 to 3 in the figures). Reaction 1 is carried out sequentially by the three reactors 3, resulting in a state where hydrogen is steadily produced throughout the entire system.

[0070] In power generation systems 100A and 101A, reaction 1 occurs in either reactor 3, and hydrogen is continuously produced and supplied. Since hydrogen is always supplied to the power generation mechanism 6, stable power generation can be performed without reducing power generation efficiency. In addition, high-temperature and low-temperature heating media can be constantly supplied to either reactor 3, reducing the stagnation of heating media and the associated heat loss. Therefore, power generation systems 100A and 101A can achieve highly efficient hydrogen production or highly efficient power generation.

[0071] (Other variations) In each of the embodiments and modifications described above, the ORC power generation mechanism 7 used the waste heat from the reactor 3, but it may also use the waste heat from the power generation mechanism 6. Furthermore, the ORC power generation mechanism 7 may use the waste heat from both the reactor 3 and the power generation mechanism 6. In addition, the ORC power generation mechanism 7 may perform binary power generation instead of organic Rankine cycle power generation.

[0072] In each of the above embodiments and modifications, a compressor for drawing hydrogen from the reactor 3 may be installed between the reactor 3 and the hydrogen tank 4 as needed.

[0073] <Effects> In each of the embodiments and modified examples described above, the reaction section 32 of the reactor 3 (corresponding to the reaction vessel of the present invention) carries out reaction 1, in which an alkali metal reacts with an alkali metal hydroxide to produce an alkali metal oxide and hydrogen; reaction 2, in which an alkali metal oxide is heated to produce an alkali metal peroxide and an alkali metal; and reaction 4, in which an alkali metal peroxide reacts with water to produce an alkali metal hydroxide and oxygen. The condensation section 33 (condensation vessel) carries out reaction 3, in which the alkali metal generated in reaction 2 is condensed. Piping 35A and 35B connect the reaction section 32 and the condensation section 33, and move the alkali metal between the reaction section 32 and the condensation section 33.

[0074] Reactor 3 can continuously produce a constant amount of hydrogen by carrying out reactions 1 to 4 in separate containers. In particular, since alkali metals are separated from the reaction section 32 and condensed in the condensation section 33, contact between the water and oxygen supplied to the reaction section 32 and the alkali metals is prevented, allowing for safe hydrogen production.

[0075] Pipe 35A connects the upper part of the reaction section 32 to the upper part of the condensation section 33, moving the alkali metal gas generated in reaction 2 from the reaction section 32 to the condensation section 33. Pipe 35B connects the lower part of the reaction section 32 to the lower part of the condensation section 33, moving the alkali metal liquid generated in reaction 3 from the reaction section 32 to the condensation section 33.

[0076] In reactor 3, gaseous alkali metals and liquid alkali metals are moved independently through two separate systems, pipes 35A and 35B. This prevents unnecessary heating and cooling of the alkali metals and allows for efficient movement of the alkali metals between the reaction section 32 and the condensation section 33. Pipe 35A connects the upper parts of the reaction section 32 and the condensation section 33, making it suitable for the movement of gaseous alkali metals. Pipe 35B connects the lower parts of the reaction section 32 and the condensation section 33, allowing for efficient flow of liquid alkali metals.

[0077] Reactor 3 includes a containment vessel 30 which houses the reaction section 32, the condensing section 33, and the piping 35A and 35B. The containment vessel 30 is filled with an inert gas.

[0078] The containment vessel 30 isolates the reaction section 32, the condensation section 33, and the piping 35A and 35B from the external environment. As a result, rapid reactions of alkali metals are prevented in the reactor 3, enabling safe hydrogen production.

[0079] The reactor 3 includes a heat exchange section 31 for heating and cooling the reaction section 32, and a cooling section 34 (corresponding to a heat exchange section for condensation) for heating and cooling the condensation section 33. The heat exchange section 31 uses the heat obtained by burning the hydrogen produced in the reaction section 32 as a high-temperature heating medium to heat the reaction section 32.

[0080] By controlling the temperatures of the reaction section 32 and the condensation section 33 using the heat exchange section 31 and the cooling section 34, the reactor 3 can generate reactions 1 to 4 at appropriate timings. In particular, the heat exchange section 31 utilizes the combustion heat of hydrogen generated from the reaction section 32, and can efficiently heat the reaction section 32.

[0081] The reactor 3 includes a pipe 37C for discharging hydrogen from the reaction section 32, a pipe 37B for discharging oxygen, and a pipe 37A for supplying water to the reaction section 32.

[0082] As shown in the above configuration, by installing separate pipes for the movement of hydrogen, oxygen, and water, the risk of substances mixing, the wrong substance being introduced into the reaction section 32, or water being injected into the reaction section 32 at the wrong time is reduced or prevented. In addition, the operations of introducing and discharging substances become easier.

[0083] Alkali metals are sodium, lithium, and potassium.

[0084] By using sodium, lithium, or potassium as the alkali metal, hydrogen can be produced stably and efficiently in reactor 3. However, considering thermodynamic properties, sodium is preferable.

[0085] As shown in the modified example, power generation systems 100A and 101A are equipped with multiple reactors 3. Furthermore, the phase of the hydrogen production process cycle differs among the multiple reactors 3.

[0086] With this configuration, power generation systems 100A and 101A can produce hydrogen on a steady basis. Because hydrogen can be constantly supplied to the power generation mechanism 6, stable power generation becomes possible. In addition, low-temperature and high-temperature heating media can be constantly supplied to either reactor 3, reducing the stagnation of the heating media and the resulting heat loss. Therefore, power generation systems 100A and 101A can achieve highly efficient hydrogen production or highly efficient power generation. [Explanation of Symbols]

[0087] Power generation systems 100, 101, 100A, 101A heat source 1 heat exchanger 2 Reactor 3 Hydrogen tank 4 Compressor 5 Power generation mechanism 6 Engine 61 Generator 62 ORC power generation mechanism 7 Fan 8 Pump 9 Supply section 10A, 10B, 10C

Claims

1. A reaction vessel for carrying out the following steps: a first step of reacting an alkali metal with an alkali metal hydroxide to produce an alkali metal oxide and hydrogen; a second step of heating the alkali metal oxide to produce an alkali metal peroxide and alkali metal; and a fourth step of reacting the alkali metal peroxide with water to produce an alkali metal hydroxide and oxygen. A condensing vessel that carries out a third process in which the alkali metals generated in the second process are condensed, The system includes a moving section that connects the reaction vessel and the condenser, and moves alkali metals between the reaction vessel and the condenser, The aforementioned movable part is A first pipe connects the upper part of the reaction vessel and the upper part of the condenser, and moves the alkali metal gas produced in the second process from the reaction vessel to the condenser. A reactor for hydrogen production, comprising: a second pipe connecting the lower part of the reaction vessel and the lower part of the condensing vessel, for moving the condensed alkali metal liquid from the condensing vessel to the reaction vessel in the third process.

2. The reactor according to claim 1, further comprising a storage container filled with an inert gas for housing the reaction vessel, the condenser, and the moving part.

3. A reaction vessel for carrying out the following steps: a first step of reacting an alkali metal with an alkali metal hydroxide to produce an alkali metal oxide and hydrogen; a second step of heating the alkali metal oxide to produce an alkali metal peroxide and alkali metal; and a fourth step of reacting the alkali metal peroxide with water to produce an alkali metal hydroxide and oxygen. A condensing vessel that carries out a third process in which the alkali metals generated in the second process are condensed, A moving section connects the reaction vessel and the condenser, and moves alkali metals between the reaction vessel and the condenser. A reaction heat exchange unit for heating and cooling the reaction vessel, A reactor for hydrogen production, comprising a condensing heat exchange section for heating and cooling the aforementioned condensing vessel.

4. The reactor according to claim 3, wherein the reaction heat exchange unit heats the reaction vessel using heat obtained by burning hydrogen generated in the reaction vessel.

5. A hydrogen discharge unit for discharging hydrogen from the reaction vessel, An oxygen discharge unit for discharging oxygen from the reaction vessel, The reactor according to any one of claims 1 to 4, further comprising an injection section for injecting water into the reaction vessel.

6. The reactor according to any one of claims 1 to 5, wherein the alkali metal is selected from sodium, lithium, and potassium.

7. A reaction vessel for carrying out the following steps: a first step of reacting an alkali metal with an alkali metal hydroxide to produce an alkali metal oxide and hydrogen; a second step of heating the alkali metal oxide to produce an alkali metal peroxide and alkali metal; and a fourth step of reacting the alkali metal peroxide with water to produce an alkali metal hydroxide and oxygen. A condensing vessel that carries out a third process in which the alkali metals generated in the second process are condensed, The reactor comprises a plurality of reactors, each of which connects the reaction vessel and the condenser, and includes a moving section for moving alkali metals between the reaction vessel and the condenser. A system in which multiple reactors execute the first to fourth processes with their cycles staggered relative to each other.

8. In a reactor comprising a reaction vessel, a condenser, a first pipe connecting the upper part of the reaction vessel and the upper part of the condenser, for moving gaseous alkali metal from the reaction vessel to the condenser, and a second pipe connecting the lower part of the reaction vessel and the lower part of the condenser, for moving liquid alkali metal from the condenser to the reaction vessel, The first step involves reacting an alkali metal with an alkali metal hydroxide in the aforementioned reaction vessel to produce an alkali metal oxide and hydrogen, A second step involves heating an alkali metal oxide in the reaction vessel to produce an alkali metal peroxide and an alkali metal, A third step involves condensing the alkali metal generated in the second step in the condensation vessel, A fourth step is performed in which alkali metal peroxide and water are reacted in the aforementioned reaction vessel to produce alkali metal hydroxide and oxygen. Methods for producing hydrogen.

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