Hydrogen production equipment, power generation systems, and steelmaking systems

Abstract

This hydrogen production device comprises: a storage tank 110; a heating unit 120 provided within the storage tank 110; a first air diffuser 130 provided below the heating unit 120 within the storage tank 110; a second air diffuser 140 provided below the first air diffuser 130 within the storage tank 110; a catalyst supply unit 150 for supplying a catalyst containing one or more of iron, nickel, copper, and aluminum from a supply port 116a formed above the heating unit 120 within the storage tank 110; a catalyst discharge unit 160 for discharging the catalyst from a discharge port 114a formed below the second air diffuser 140 within the storage tank 110; and a raw material gas supply unit 170 for supplying a raw material gas containing at least a hydrocarbon to the first air diffuser 130 and the second air diffuser 140.

Description

[Technical Field]

[0001] This disclosure relates to a hydrogen production device, a power generation system, and a steelmaking system. This application claims the benefit of priority from Japanese Patent Application No. 2022-073628 filed on April 27, 2022, the contents of which are incorporated herein by reference. [Background technology]

[0002] One known technology for producing hydrogen is steam reforming of hydrocarbons such as methane. However, steam reforming of hydrocarbons produces carbon dioxide during the hydrogen production process. Therefore, it is conceivable to produce hydrogen without emitting carbon dioxide by thermally decomposing hydrocarbons to produce solid carbon.

[0003] As a technology for thermally decomposing hydrocarbons, an apparatus including a reactor, a raw material gas supply source, and a heating unit provided outside the reactor has been disclosed (for example, Patent Document 1). The reactor contains a catalyst. The raw material gas supply source supplies hydrocarbons to the reactor. The heating unit is provided around the reactor and heats the interior of the reactor. [Prior art documents] [Patent documents]

[0004] [Patent Document 1] Patent No. 5862559 Summary of the Invention [Problem to be solved by the invention]

[0005] The thermal decomposition reaction of hydrocarbons proceeds efficiently at temperatures above 800°C by using a catalyst. However, because the thermal decomposition reaction of hydrocarbons is an endothermic reaction, heat must be supplied from an external source. Therefore, in the technology of externally heating a reactor, such as that described in Patent Document 1, in order to heat the interior of the reactor to 800°C or higher, the reactor walls must be heated to a temperature above the internal temperature (e.g., above 1000°C). This necessitates the reactor being constructed using materials such as expensive heat-resistant alloys that have heat resistance above 1000°C and good heat conductivity, resulting in high costs for the heating device and reactor. Furthermore, in the technology of externally heating a reactor, the catalyst inside is heated from the wall surface, and as the catalyst volume increases, a temperature difference occurs between the vicinity of the wall surface and the center. This makes it difficult to decompose hydrocarbons uniformly and efficiently inside the reactor, making it difficult to increase the size of the reactor.

[0006] In view of the above, an object of the present disclosure is to provide a hydrogen production device, a power generation system, and a steelmaking system that are capable of thermally decomposing hydrocarbons at low cost. [Means for solving the problem]

[0007] In order to solve the above problems, a hydrogen production apparatus according to one embodiment of the present disclosure includes a storage tank, a heating unit provided within the storage tank, a first diffuser pipe provided below the heating unit within the storage tank, a second diffuser pipe provided below the first diffuser pipe within the storage tank, a catalyst supply unit that supplies a catalyst containing one or more of iron, nickel, copper, and aluminum from a supply port formed above the heating unit in the storage tank, a catalyst discharge unit that discharges the catalyst from a discharge port formed below the second diffuser pipe in the storage tank, and a raw material gas supply unit that supplies a raw material gas containing at least hydrocarbons to the first diffuser pipe and the second diffuser pipe.

[0008] Furthermore, the flow rate of the raw material gas supplied to the first diffuser pipe by the raw material gas supply unit may be greater than the flow rate of the raw material gas supplied to the second diffuser pipe.

[0009] The superficial velocity ratio U0 / Umf of the total of the raw material gas diffused from the first diffuser pipe and the raw material gas diffused from the second diffuser pipe may be 1.1 or more and 2.0 or less.

[0010] Furthermore, in the storage tank, a fluidized bed of the catalyst may be formed above the first air diffuser pipe, and a moving bed of the catalyst may be formed below the first air diffuser pipe.

[0011] The storage tank may have a cylindrical upper portion and a lower portion provided below the upper portion, the horizontal cross-sectional area of the internal space of which gradually decreases from top to bottom, the heating portion being provided within the upper portion, and the second aeration pipe being provided within the lower portion.

[0012] The holding vessel may also have one upper portion and multiple lower portions.

[0013] In order to solve the above problems, a power generation system according to one embodiment of the present disclosure includes a storage tank, a heating unit provided within the storage tank, a first diffuser pipe provided below the heating unit, a second diffuser pipe provided within the storage tank below the first diffuser pipe, a catalyst supply unit that supplies a catalyst containing one or more of iron, nickel, copper, and aluminum from a supply port formed above the heating unit in the storage tank, a catalyst discharge unit that discharges the catalyst from a discharge port formed below the second diffuser pipe in the storage tank, and a raw material gas supply unit that supplies a raw material gas containing at least a hydrocarbon to the first diffuser pipe and the second diffuser pipe, and a power generation system that generates power using hydrogen produced by the hydrogen production device.

[0014] In order to solve the above problems, one embodiment of the present disclosure provides an iron-making system comprising: a storage tank; a heating unit provided within the storage tank; a first diffuser pipe provided below the heating unit within the storage tank; a second diffuser pipe provided below the first diffuser pipe within the storage tank; a catalyst supply unit that supplies a catalyst containing one or more of iron, nickel, copper, and aluminum from a supply port formed above the heating unit in the storage tank; a catalyst discharge unit that discharges the catalyst from a discharge port formed below the second diffuser pipe in the storage tank; and a raw material gas supply unit that supplies a raw material gas containing at least hydrocarbons to the first diffuser pipe and the second diffuser pipe; and an iron-making system that produces iron using hydrogen produced by the hydrogen production unit. [Effects of the Invention]

[0015] According to the present disclosure, it is possible to thermally crack hydrocarbons at low cost. [Brief explanation of the drawings]

[0016] [Figure 1] FIG. 1 is a diagram illustrating an outline of a hydrogen production device according to an embodiment. [Figure 2] FIG. 2 is a diagram illustrating a hydrogen production device according to a modified example. [Figure 3] FIG. 3 is a diagram illustrating a power generation system according to an embodiment. [Figure 4] FIG. 4 is a diagram illustrating another power generation system according to an embodiment. [Figure 5] FIG. 5 is a diagram illustrating another power generation system according to an embodiment. [Figure 6] FIG. 6 is a diagram illustrating the iron-making system according to the embodiment. [Figure 7] FIG. 7 is a diagram illustrating another iron-making system according to an embodiment. [Figure 8] FIG. 8 is a diagram illustrating another example of the installation mode of the first air diffusing pipe. [Figure 9] FIG. 9 is a first diagram illustrating another example of the shape of the container. [Figure 10]FIG. 10 is a second diagram illustrating another example of the shape of the storage tank. DETAILED DESCRIPTION OF THE INVENTION

[0017] Hereinafter, embodiments of the present disclosure will be described in detail with reference to the accompanying drawings. Dimensions, materials, and other specific numerical values shown in the embodiments are merely examples for ease of understanding and do not limit the present disclosure unless otherwise specified. In this specification and drawings, elements having substantially the same functions and configurations are designated by the same reference numerals to avoid redundant explanation, and elements not directly related to the present disclosure are not shown.

[0018] [Hydrogen production device 100] FIG. 1 is a diagram illustrating an outline of a hydrogen production apparatus 100 according to this embodiment. In FIG. 1, solid arrows indicate the flow of raw material gas and generated gas. In FIG. 1, dashed arrows indicate the flow of catalyst and solid carbon. In addition, in FIG. 1, a heating unit 120 is indicated by hatching.

[0019] As shown in FIG. 1, the hydrogen production device 100 includes a storage vessel 110, a heating unit 120, a first air diffuser pipe 130, a second air diffuser pipe 140, a catalyst supply unit 150, a catalyst discharge unit 160, and a raw material gas supply unit 170.

[0020] The storage tank 110 is a container (hopper) that temporarily stores the catalyst. The storage tank 110 is cylindrical and is installed so that its central axis is oriented vertically. In this embodiment, the storage tank 110 has an upper portion 112, a lower portion 114, and a lid portion 116.

[0021] The upper portion 112 is a cylindrical portion having a cylindrical shape such as a cylindrical, elliptical, or rectangular shape. The horizontal cross-sectional area of the internal space of the upper portion 112 is, for example, approximately constant from top to bottom.

[0022] The lower portion 114 is a portion provided below the upper portion 112. The horizontal cross-sectional area of the internal space of the lower portion 114 gradually decreases from top to bottom. For example, the lower portion 114 is a conical cylinder whose inner diameter gradually decreases from top to bottom. The inclination angle θ of the lower portion 114 is, for example, 60 degrees.

[0023] The lid 116 is a portion provided above the upper portion 112. The horizontal cross-sectional area of the internal space of the lid 116 gradually increases from top to bottom. For example, the lid 116 is a conical cylinder whose inner diameter gradually increases from top to bottom.

[0024] The catalyst contained in the container 110 is a catalyst that promotes the thermal decomposition reaction shown in the following formula (1). CH4→C + 2H2…Formula (1)

[0025] The catalyst contains one or more of iron, nickel, copper, and aluminum. In this embodiment, the catalyst is a natural mineral, for example, iron ore. Note that the catalyst does not have to be a natural mineral as long as it contains one or more of iron, nickel, copper, and aluminum. The particle size of the catalyst is, for example, 50 μm or more and 1000 μm or less, and preferably 100 μm or more and 300 μm or less.

[0026] The heating unit 120 is provided within the upper portion 112 that constitutes the storage tank 110. The heating unit 120 heats the catalyst to a temperature that efficiently promotes the thermal decomposition reaction represented by the above formula (1). The heating unit 120 heats the catalyst so that the temperature of the catalyst is, for example, 800°C or higher and 900°C or lower. In this embodiment, the heating unit 120 includes a plurality of heating elements 122. The heating elements 122 are, for example, cylindrical or cylindrical. The plurality of heating elements 122 are installed within the upper portion 112 so that their central axes are horizontal. The plurality of heating elements 122 are substantially uniformly arranged within the upper portion 112. In this embodiment, the plurality of heating elements 122 are arranged in parallel in the horizontal direction. Furthermore, in this embodiment, the plurality of heating elements 122 are arranged in two stages at different vertical positions.

[0027] The heating unit 120 is configured, for example, by an electric heater or a heat transfer tube. When the heating unit 120 is configured by an electric heater, it includes, for example, a cylindrical heat transfer body (ceramic) and a heating element built into the heat transfer body. The electric heater may be supplied with either or both of electricity generated by renewable energy and electricity generated by nuclear power generation. When the heating unit 120 is configured by a heat transfer tube, the heat medium passing through the heat transfer tube is, for example, combustion exhaust gas.

[0028] The first aeration pipe 130 is provided below the heating unit 120 in the storage tank 110. In this embodiment, the first aeration pipe 130 is provided in the upper portion 112. A plurality of first aeration pipes 130 are provided. The plurality of first aeration pipes 130 are provided in the upper portion 112 so that the central axis direction is horizontal. In this embodiment, the plurality of first aeration pipes 130 are provided in parallel in the horizontal direction. A plurality of holes are formed in the first aeration pipe 130.

[0029] The second aeration pipe 140 is provided below the first aeration pipe 130 within the storage tub 110. In this embodiment, the second aeration pipe 140 is provided within the lower portion 114 that constitutes the storage tub 110. In this embodiment, a plurality of second aeration pipes 140 are provided. The plurality of second aeration pipes 140 are provided within the lower portion 114 so that their central axes are horizontal. In this embodiment, the plurality of second aeration pipes 140 are provided in parallel in the horizontal direction. The second aeration pipe 140 has a plurality of holes formed therein.

[0030] The catalyst supply unit 150 supplies the catalyst from a supply port 116 a formed in the lid unit 116 .

[0031] The catalyst discharge part 160 discharges the catalyst from a discharge port 114 a formed in the bottom surface of the lower part 114 .

[0032] The raw material gas supply unit 170 supplies raw material gas to the first diffuser pipe 130 and the second diffuser pipe 140. The raw material gas is a gas containing at least hydrocarbons (e.g., methane). The raw material gas is, for example, natural gas obtained by vaporizing liquefied natural gas (LNG).

[0033] In this embodiment, the raw material gas supply unit 170 includes a first supply pipe 172, a flow rate adjustment valve 174, a first blower 176, a second supply pipe 182, a flow rate adjustment valve 184, a second blower 186, and flow meters 190, 192, and 194.

[0034] The first supply pipe 172 is a pipe that connects the raw material gas supply source S and the first air diffuser pipe 130. A flow rate adjustment valve 174 and a first blower 176 are provided on the first supply pipe 172.

[0035] The flow rate adjustment valve 174 adjusts the opening degree of the flow path formed in the first supply pipe 172. The flow rate adjustment valve 174 is, for example, a butterfly valve.

[0036] The first blower 176 is provided in the first supply pipe 172 between the flow rate adjustment valve 174 and the first air diffuser pipe 130. The suction side of the first blower 176 is connected to the flow rate adjustment valve 174. The discharge side of the first blower 176 is connected to the first air diffuser pipe 130. The first blower 176 increases the pressure of the raw material gas.

[0037] The second supply pipe 182 is a pipe that branches off from the first supply pipe 172 between the first blower 176 and the first air diffuser pipe 130 and is connected to the second air diffuser pipe 140. A flow rate adjustment valve 184 and a second blower 186 are provided in the second supply pipe 182.

[0038] The flow rate adjustment valve 184 adjusts the opening degree of the flow path formed in the second supply pipe 182. The flow rate adjustment valve 184 is, for example, a butterfly valve.

[0039] The second blower 186 is provided in the second supply pipe 182 between the flow rate adjustment valve 184 and the second air diffuser pipe 140. The suction side of the second blower 186 is connected to the flow rate adjustment valve 184. The discharge side of the second blower 186 is connected to the second air diffuser pipe 140. The second blower 186 further increases the pressure of the raw material gas that has been increased in pressure by the first blower 176.

[0040] The flow meter 190 detects the flow rate QT of the raw material gas discharged from the first blower 176. The flow meter 192 detects the flow rate Q1 of the raw material gas supplied to the first air diffuser 130. The flow meter 194 detects the flow rate Q2 of the raw material gas supplied to the second air diffuser 140. Note that the flow rate QT = flow rate Q1 + flow rate Q2.

[0041] The aperture of the flow rate control valve 174 and the discharge pressures of the first blower 176 and the second blower 186 are set so that the superficial velocity ratio U0 / Umf of the total of the raw material gas diffused from the first diffuser pipe 130 and the raw material gas diffused from the second diffuser pipe 140 is 1.1 or more and 2.0 or less, preferably 1.1 or more and 1.5 or less. U0 is the velocity at which the raw material gas moves through the fluidized bed FB. Umf is the initiation velocity of fluidization (minimum fluidization velocity).

[0042] The opening of the flow rate adjustment valve 184 is set so that the flow rate Q1 of the raw material gas supplied to the first air diffuser pipe 130 is greater than the flow rate Q2 of the raw material gas supplied to the second air diffuser pipe 140. In this embodiment, the opening of the flow rate adjustment valve 184 is set so that the ratio of the flow rates Q1 and Q2 is Q1:Q2=7:3.

[0043] [Catalyst and raw gas flow] Next, a description will be given of the flow of the catalyst and raw material gas in the hydrogen production device 100. As described above, in the hydrogen production device 100, the catalyst supply unit 150 supplies the catalyst to the storage tank 110, and the catalyst discharge unit 160 discharges the catalyst from the storage tank 110. Therefore, the catalyst moves from top to bottom within the storage tank 110 under its own weight. As a result, a moving layer of the catalyst is formed within the storage tank 110.

[0044] The hydrogen production apparatus 100 also includes a first diffuser pipe 130, a second diffuser pipe 140, and a raw material gas supply unit 170. The raw material gas supply unit 170 supplies the raw material gas to the first diffuser pipe 130 and the second diffuser pipe 140 so that the superficial velocity ratio U0 / Umf of the total of the raw material gas diffused from the first diffuser pipe 130 and the raw material gas diffused from the second diffuser pipe 140 is 1.1 or more and 2.0 or less. As a result, the hydrogen production apparatus 100 can form a fluidized bed FB of the catalyst above the first diffuser pipe 130 and a moving bed MB of the catalyst below the first diffuser pipe 130 in the storage tank 110. Therefore, the catalyst supplied from the catalyst supply unit 150 forms a fluidized bed FB, then a moving bed MB, and is discharged by the catalyst discharge unit 160.

[0045] The catalyst supply unit 150 and the catalyst discharge unit 160 supply and discharge the catalyst so that the upper surface of the fluidized bed FB is maintained at a predetermined position above the heating unit 120. The residence time of the catalyst in the storage tank 110 can be controlled by controlling the supply flow rate of the catalyst by the catalyst supply unit 150 and the discharge flow rate of the catalyst by the catalyst discharge unit 160.

[0046] The heating unit 120 is provided above the first air diffuser pipe 130. Therefore, the heating unit 120 is disposed within the fluidized bed FB of the catalyst. Therefore, the fluidized bed FB of the catalyst is heated by the heating unit 120.

[0047] As a result, the raw material gas diffused from the first diffuser pipe 130 and the second diffuser pipe 140 is heated by the catalyst (convective heat transfer) as it passes through the catalyst fluidized bed FB. This causes the thermal decomposition reaction shown in formula (1) above to proceed, producing hydrogen and solid carbon from the hydrocarbons contained in the raw material gas. In other words, the main thermal decomposition reaction proceeds in the fluidized bed FB.

[0048] The hydrogen thus produced and the unreacted raw material gas are sent to the downstream gas processing equipment T through an exhaust port 116b formed in the lid portion 116.

[0049] Meanwhile, solid carbon produced by the pyrolysis reaction adheres to the surface of the catalyst. Therefore, the solid carbon moves from the fluidized bed FB to the moving bed MB together with the catalyst under its own weight. Then, the solid carbon forms the moving bed MB together with the catalyst, and is finally discharged to the outside by the catalyst discharge unit 160. The catalyst with the solid carbon attached thereto that has been discharged to the outside may be supplied again to the storage tank 110 by the catalyst supply unit 150. Furthermore, the catalyst with the solid carbon attached thereto may be separated into the catalyst and the solid carbon. The separated catalyst may be supplied again to the storage tank 110 by the catalyst supply unit 150.

[0050] The second air diffuser pipe 140 is provided below the first air diffuser pipe 130. Therefore, the second air diffuser pipe 140 is disposed within the moving bed MB of the catalyst. Therefore, the raw material gas diffused from the second air diffuser pipe 140 exchanges heat with the catalyst constituting the moving bed MB. As a result, the raw material gas is heated and the catalyst is cooled.

[0051] As described above, the hydrogen production device 100 according to this embodiment forms a catalyst fluidized bed FB above the first air diffuser pipe 130 and a catalyst moving bed MB below the second air diffuser pipe 140 in the storage tank 110. As a result, the hydrogen production device 100 can continuously bring the catalyst into contact with the raw material gas in the fluidized bed FB to continuously perform the thermal decomposition reaction of the raw material gas, while continuously moving the catalyst after the reaction from the fluidized bed FB to the moving bed MB. In other words, the hydrogen production device 100 according to this embodiment can continuously replace the catalyst in the fluidized bed FB while continuously performing the thermal decomposition reaction of the raw material gas. Therefore, new catalyst is constantly in contact with the raw material gas in the fluidized bed FB, allowing the thermal decomposition reaction to proceed efficiently.

[0052] Furthermore, in the hydrogen production apparatus 100 according to this embodiment, the heating units 120 are uniformly provided within the fluidized bed FB, so that the catalyst in the fluidized bed FB is heated substantially uniformly by the heating units 120. Therefore, the hydrogen production apparatus 100 does not need to heat the storage vessel 110 from the outside. This eliminates the need for the hydrogen production apparatus 100 to construct the furnace wall of the storage vessel 110 using high-quality materials, such as heat-resistant alloys, that have heat resistance of 1000°C or higher and high heat conductivity. Therefore, the hydrogen production apparatus 100 can employ a furnace structure using carbon steel plates lined with a refractory material, thereby reducing the manufacturing cost of the storage vessel 110. This enables the hydrogen production apparatus 100 to thermally decompose hydrocarbons at low cost. In other words, the hydrogen production apparatus 100 can produce hydrogen at low cost.

[0053] Furthermore, in the conventional technology of heating the inside of the storage tank from the outside, it is difficult to uniformize the internal temperature (catalyst temperature) of the storage tank, making it difficult to increase the size of the storage tank. In contrast, the hydrogen production device 100 has the heating unit 120 uniformly provided inside the fluidized bed FB, which makes it possible to uniformize the temperature of the fluidized bed FB inside the storage tank 110 compared to the conventional technology of heating the inside of the storage tank from the outside. This makes it possible for the hydrogen production device 100 to avoid a situation in which the temperature of the catalyst in the fluidized bed FB drops locally. Therefore, the hydrogen production device 100 can efficiently thermally decompose hydrocarbons. Furthermore, since the hydrogen production device 100 can uniformize the temperature of the fluidized bed FB, it is also possible to increase the size of the storage tank 110. This allows the hydrogen production device 100 to inexpensively produce large amounts of hydrogen.

[0054] As described above, the hydrogen production device 100 thermally decomposes the raw material gas to produce hydrogen and solid carbon. Therefore, the hydrogen production device 100 can produce hydrogen without emitting carbon dioxide derived from the raw material gas.

[0055] Furthermore, as described above, the superficial velocity ratio U0 / Umf of the total of the raw material gas diffused from the first diffuser pipe 130 and the raw material gas diffused from the second diffuser pipe 140 is 1.1 or more and 2.0 or less. This makes it possible to suppress abrasion of the heating unit 120 caused by the catalyst. Therefore, it is possible to improve the durability of the heating unit 120.

[0056] As described above, the second air diffuser pipe 140 is provided within the catalyst moving bed MB. This allows heat exchange between the raw material gas diffused from the second air diffuser pipe 140 and the catalyst constituting the moving bed MB. This makes it possible to preheat the raw material gas (by convective heat transfer) using the heat of the catalyst constituting the moving bed MB. This reduces the energy required to heat the catalyst by the heating unit 120. Furthermore, the catalyst constituting the moving bed MB is heated to approximately 200°C to 300°C by the raw material gas. This makes it possible to suppress deterioration of the catalyst discharge unit 160 due to the heat of the catalyst.

[0057] Furthermore, the first and second diffusing pipes 130 and 140 are provided within the moving bed MB, which makes it possible to reduce wear of the first and second diffusing pipes 130 and 140 caused by the catalyst.

[0058] As described above, the flow rate of the raw material gas supplied by the raw material gas supply unit 170 to the first air diffuser pipe 130 is greater than the flow rate of the raw material gas supplied to the second air diffuser pipe 140. The pressure loss of the first blower 176 increases as the catalyst bed height located above the first air diffuser pipe 130 increases. Similarly, the pressure loss of the second blower 186 increases as the catalyst bed height located above the second air diffuser pipe 140 increases. Therefore, by making the flow rate of the raw material gas supplied to the first air diffuser pipe 130, which has a relatively low catalyst bed height above it, greater than the flow rate of the raw material gas supplied to the second air diffuser pipe 140, which has a relatively high catalyst bed height above it, it is possible to reduce the power consumption of the second blower 186.

[0059] As described above, the horizontal cross-sectional area of the internal space of the lower portion 114 of the storage tank 110 gradually decreases from top to bottom. This allows the catalyst to move smoothly in the lower portion 114. Therefore, it is possible to reduce the number of areas in the lower portion 114 where the catalyst may stagnate.

[0060] [Variations] Fig. 2 is a diagram illustrating a hydrogen production device 200 according to a modified example. As shown in Fig. 2, the hydrogen production device 200 includes a storage tank 210, a heating unit 120, a first aeration pipe 130, a second aeration pipe 140, a catalyst supply unit 150, a catalyst discharge unit 160, and a raw material gas supply unit 170. The hydrogen production device 200 according to the modified example differs from the storage tank 110 of the hydrogen production device 100 in the shape of the storage tank 210, but other configurations are substantially the same as those of the hydrogen production device 100. Therefore, components that are substantially the same as those of the hydrogen production device 100 are denoted by the same reference numerals, and descriptions thereof will be omitted.

[0061] The storage tank 210 of this modified example has one upper portion 112, multiple lower portions 114, and one lid portion 116. In this modified example, multiple supply ports 116a are formed in the lid portion 116. The number of supply ports 116a may be equal to the number of lower portions 114.

[0062] When the storage tank 110 has only one lower portion 114, as in the hydrogen production device 100 described above, if an attempt is made to eliminate the horizontally extending bottom surface and increase the horizontal size of the upper portion 112 while maintaining the inclination angle of the lower portion 114 in order to reduce the number of areas where the catalyst stagnates within the upper portion 112, the overall height of the storage tank 110 increases. Therefore, the storage tank 210 of the hydrogen production device 200 according to a modified example has multiple lower portions 114. This allows the height of the storage tank 210 to be reduced even if the horizontally extending bottom surface is eliminated and the inclination angle of the lower portion 114 is maintained, thereby increasing the horizontal size of the upper portion 112. Therefore, it is possible to reduce the height of the storage tank 210 while increasing the size of the catalyst fluidized bed FB, i.e., the reaction field for the pyrolysis reaction.

[0063] The hydrogen production device 200 according to the modified example can increase the amount of raw material gas processed (amount of pyrolysis) per unit time by enlarging the reaction field for the pyrolysis reaction. Therefore, the hydrogen production device 200 according to the modified example can increase the amount of hydrogen produced per unit time.

[0064] Furthermore, the hydrogen production device 200 according to the modified example can reduce the height of the storage tank 210. As a result, the hydrogen production device 200 according to the modified example can reduce the construction cost of the storage tank 210.

[0065] [Power generation system 500] Fig. 3 is a diagram illustrating a power generation system 500 according to this embodiment. As shown in Fig. 3, the power generation system 500 includes the hydrogen production device 100 and a power generation device 510. The power generation device 510 is, for example, a thermal power generation facility. The power generation device 510 includes a boiler 512, a steam turbine 514, and a generator 516.

[0066] The boiler 512 is supplied with hydrogen produced by the hydrogen production apparatus 100 and air. The boiler 512 burns the hydrogen to generate steam. In addition to hydrogen, fuel may be supplied to the boiler 512. The fuel is, for example, coal.

[0067] The steam turbine 514 is supplied with the steam generated by the boiler 512. The steam turbine 514 converts the energy of the steam into rotational energy.

[0068] Generator 516 converts the rotational energy transferred from steam turbine 514 into electrical power.

[0069] As described above, the power generation system 500 according to this embodiment generates power using hydrogen produced by the hydrogen production device 100. This allows the power generation system 500 to generate power at low cost.

[0070] The power generation system 510 may include a gas turbine instead of or in addition to the boiler 512. In this case, the gas turbine burns the hydrogen produced by the hydrogen production system 100 to generate rotational energy. The rotational energy generated by the gas turbine is then transmitted to the steam turbine 514. In addition to hydrogen, fuel may be supplied to the gas turbine. The fuel is, for example, natural gas obtained by vaporizing liquefied natural gas.

[0071] [Power Generation System 550] Fig. 4 is a diagram illustrating another power generation system 550 according to this embodiment. As shown in Fig. 4, the power generation system 550 includes the hydrogen production device 100 and a power generation device 560. The power generation device 560 is, for example, a thermal power generation facility. The power generation device 560 includes an ammonia production device 562, a boiler 512, a steam turbine 514, and a generator 516. Note that components that are substantially the same as those in the power generation system 500 are denoted by the same reference numerals, and description thereof will be omitted.

[0072] The ammonia production unit 562 is supplied with hydrogen produced by the hydrogen production unit 100 and air. The ammonia production unit 562 produces ammonia from hydrogen and nitrogen contained in the air. The ammonia produced by the ammonia production unit 562 is supplied to the boiler 512.

[0073] The boiler 512 of the power generation device 560 burns ammonia to generate steam. Note that, in addition to ammonia, fuel may be supplied to the boiler 512 of the power generation device 560. The fuel is, for example, coal.

[0074] As described above, the power generation system 550 according to this embodiment generates power using hydrogen produced by the hydrogen production device 100. This allows the power generation system 550 to generate power at low cost.

[0075] Like the power generation system 510, the power generation system 560 may include a gas turbine instead of or in addition to the boiler 512. In this case, the gas turbine generates rotational energy by combusting the ammonia produced by the ammonia production system 562. The rotational energy generated by the gas turbine is then transmitted to the steam turbine 514. In addition to the ammonia, fuel may be supplied to the gas turbine. The fuel is, for example, natural gas obtained by vaporizing liquefied natural gas.

[0076] [Power Generation System 600] 5 is a diagram illustrating another power generation system 600 according to this embodiment. As shown in FIG. 5, the power generation system 600 includes the hydrogen production device 100 and a power generation device 610.

[0077] The power generation device 610 of the power generation system 600 includes a fuel cell 612. The fuel cell 612 includes an anode, an cathode, and an electrolyte disposed between the anode and the cathode. The anode of the fuel cell 612 is supplied with hydrogen produced by the hydrogen production device 100. The cathode of the fuel cell 612 is supplied with air. The fuel cell 612 generates electricity by reacting hydrogen with oxygen contained in the air.

[0078] As described above, the power generation system 600 according to this embodiment generates power using hydrogen produced by the hydrogen production device 100. This allows the power generation system 600 to generate power at low cost.

[0079] [Steel Manufacturing System 700] Fig. 6 is a diagram illustrating an iron-making system 700 according to this embodiment. As shown in Fig. 6, the iron-making system 700 includes a hydrogen production apparatus 100 and an iron-making apparatus 710. In this embodiment, the hydrogen production apparatus 100 uses iron ore as a catalyst.

[0080] The iron making facility 710 includes a direct reduction furnace 712 and an electric furnace 714 .

[0081] The direct reduction reactor 712 is supplied with iron ore and hydrogen produced by the hydrogen production device 100. The direct reduction reactor 712 reduces the iron ore in its solid state using hydrogen.

[0082] The electric furnace 714 melts and refines the iron ore reduced by the direct reduction furnace 712. In this way, iron (e.g., steel) is produced.

[0083] As described above, the iron-making system 700 according to this embodiment produces iron using hydrogen produced by the hydrogen production device 100. As a result, the iron-making system 700 can produce iron while reducing carbon dioxide (CO2) emissions.

[0084] [Steel Manufacturing System 750] Fig. 7 is a diagram illustrating another iron-making system 750 according to this embodiment. As shown in Fig. 7, the iron-making system 750 according to this embodiment includes a hydrogen production apparatus 100 and an iron-making apparatus 760. In this embodiment, the hydrogen production apparatus 100 uses iron ore as a catalyst.

[0085] The iron-making equipment 760 of the iron-making system 750 includes a blast furnace 762 and a converter 764. The blast furnace 762 is supplied with hydrogen produced by the hydrogen production apparatus 100, iron ore, and coke. The blast furnace 762 melts and reduces the iron ore to produce pig iron. The converter 764 converts the pig iron into steel. In this manner, iron (e.g., steel) is produced.

[0086] As described above, the iron-making system 750 according to this embodiment produces iron using hydrogen produced by the hydrogen production device 100. This allows the iron-making system 750 to produce iron while reducing carbon dioxide emissions.

[0087] Although the embodiments have been described above with reference to the accompanying drawings, it goes without saying that the present disclosure is not limited to the above-described embodiments. It is clear that a person skilled in the art can conceive of various modifications or alterations within the scope of the claims, and it is understood that these also naturally fall within the technical scope of the present disclosure.

[0088] For example, in the above-described embodiment and modified examples, the heating unit 120 is provided in the upper portion 112. However, the installation position of the heating unit 120 is not limited as long as it is provided above the first air diffuser pipe 130 in the storage tank 110, 210.

[0089] Similarly, in the above-described embodiment and modified examples, the case where the first air diffuser pipe 130 is provided inside the upper portion 112 has been taken as an example. However, the installation position of the first air diffuser pipe 130 is not limited as long as it is provided between the heating unit 120 and the second air diffuser pipe 140 inside the storage tank 110, 210.

[0090] Similarly, in the above-described embodiment and modified examples, the case where the second air diffuser pipe 140 is provided in the lower portion 114 has been taken as an example. However, the installation position of the second air diffuser pipe 140 is not limited as long as it is provided below the first air diffuser pipe 130 in the storage tank 110, 210.

[0091] Similarly, in the above-described embodiment and modified examples, the supply port 116a is formed in the lid 116. However, the supply port 116a may be formed above the heating unit 120 in the containing tank 110.

[0092] Similarly, in the above embodiment and modified examples, the case where the discharge port 114a is formed in the lower portion 114 has been taken as an example. However, the discharge port 114a may be formed below the second air diffuser pipe 140 in the storage tank 110.

[0093] In any case, it is sufficient that the supply port 116a, the heating unit 120, the first air diffuser pipe 130, the second air diffuser pipe 140, and the discharge port 114a are provided in this order from top to bottom.

[0094] Furthermore, in the above-described embodiment and modified examples, a configuration in which a plurality of first aeration pipes 130 are arranged in parallel in the horizontal direction has been exemplified. However, there are no limitations on the manner in which the plurality of first aeration pipes 130 are installed. FIG. 8 is a diagram illustrating another example of the manner in which the first aeration pipes 130 are installed. As shown in FIG. 8, for example, the hydrogen production device 100, 200 may include a first first aeration pipe 130A arranged in parallel in the horizontal direction, and a second first aeration pipe 130B arranged in parallel in the horizontal direction, with its central axis direction intersecting (e.g., perpendicular to) the first first aeration pipe 130A.

[0095] Similarly, in the above embodiment and modified examples, a configuration in which multiple second diffuser pipes 140 are arranged in parallel in the horizontal direction has been exemplified. However, there are no limitations on the manner in which the multiple second diffuser pipes 140 are arranged in parallel in the horizontal direction. For example, the hydrogen production device 100, 200 may include a first second diffuser pipe 140 arranged in parallel in the horizontal direction, and a second second diffuser pipe 140 arranged in parallel in the horizontal direction with its central axis direction intersecting (e.g., perpendicular to) the first second diffuser pipe 140.

[0096] Similarly, in the above embodiment and modified examples, a configuration has been given in which the multiple heating members 122 constituting the heating unit 120 are arranged in parallel in the horizontal direction. However, there are no limitations on the manner in which the multiple heating members 122 are arranged. For example, the heating unit 120 may include a first heating member 122 arranged in parallel in the horizontal direction, and a second heating member 122 arranged in parallel in the horizontal direction with its central axis direction intersecting (e.g., perpendicular to) the first heating member 122.

[0097] Furthermore, in the above embodiment and modified examples, the case has been exemplified where the flow rate of the raw material gas supplied to the first air diffuser pipe 130 by the raw material gas supply unit 170 is greater than the flow rate of the raw material gas supplied to the second air diffuser pipe 140. However, the flow rate of the raw material gas supplied to the first air diffuser pipe 130 may be equal to or smaller than the flow rate of the raw material gas supplied to the second air diffuser pipe 140.

[0098] Furthermore, in the above-described embodiment and modified examples, the case has been exemplified where the superficial velocity ratio U0 / Umf of the total of the raw material gas diffused from the first diffuser pipe 130 and the raw material gas diffused from the second diffuser pipe 140 is 1.1 or more and 2.0 or less. However, the superficial velocity ratio U0 / Umf of the total of the raw material gas diffused from the first diffuser pipe 130 and the raw material gas diffused from the second diffuser pipe 140 may be 1.0 or more, and may be more than 2.0.

[0099] In the above embodiment and modified examples, the storage tanks 110 and 210 have the upper portion 112 and the lower portion 114. However, the shape of the storage tanks 110 and 210 is not limited.

[0100] In the above embodiment and modified example, the case where the plurality of heating elements 122 are provided in two stages at different vertical positions has been exemplified. However, the plurality of heating elements 122 may be provided in one stage, or in three or more stages at different vertical positions. The number of stages of the plurality of heating elements 122 may be determined according to the bed height of the fluidized bed FB.

[0101] In the above embodiment and modified examples, the horizontal cross-sectional area of the internal space of the upper portion 112 of the storage tank 110 is approximately constant from top to bottom. However, the shape of the internal space of the storage tank 110 is not limited.

[0102] FIG. 9 is a first diagram illustrating another example of the shape of the storage tank 310. As shown in FIG. 9, the upper portion 312 of the storage tank 310 includes a small diameter portion 312a, a large diameter portion 312b, and an expanded diameter portion 312c. The small diameter portion 312a is continuous with the upper end of the lower portion 114. The horizontal cross-sectional area of the internal space of the small diameter portion 312a is approximately constant from top to bottom. The heating portion 120 and the first air diffuser pipe 130 are provided within the small diameter portion 312a. Therefore, a fluidized bed FB is formed in the small diameter portion 312a.

[0103] The large diameter portion 312b is located above the small diameter portion 312a. The upper end of the large diameter portion 312b is continuous with the lid portion 116. The horizontal cross-sectional area of the internal space of the large diameter portion 312b is approximately constant from top to bottom. The horizontal cross-sectional area of the internal space of the large diameter portion 312b is larger than that of the small diameter portion 312a. The expanded diameter portion 312c is continuous with the upper end of the small diameter portion 312a and the lower end of the large diameter portion 312b. The horizontal cross-sectional area of the internal space of the expanded diameter portion 312c gradually increases from bottom to top. Since the upper portion 312 includes the small diameter portion 312a, the large diameter portion 312b, and the expanded diameter portion 312c, the flow velocity of the ascending air current toward the exhaust port 116b can be reduced, making it possible to suppress catalyst scattering.

[0104] FIG. 10 is a second diagram illustrating another example of the shape of the storage tank 410. As shown in FIG. 10, the upper portion 412 of the storage tank 410 includes a large diameter portion 412a, a small diameter portion 412b, a large diameter portion 412c, a reduced diameter portion 412d, and an expanded diameter portion 412e. The large diameter portion 412a is continuous with the upper end of the lower portion 114. The horizontal cross-sectional area of the internal space of the large diameter portion 412a is approximately constant from top to bottom. The heating portion 120 and the first air diffuser pipe 130 are provided within the large diameter portion 412a. Therefore, a fluidized bed FB is formed in the large diameter portion 412a.

[0105] Small diameter portion 412b is provided above large diameter portion 412a. The horizontal cross-sectional area of the internal space of small diameter portion 412b is smaller than that of large diameter portion 412a. Reduced diameter portion 412d is continuous with the upper end of large diameter portion 412a and the lower end of small diameter portion 412b. The horizontal cross-sectional area of the internal space of reduced diameter portion 412d gradually decreases from bottom to top.

[0106] Large diameter portion 412c is provided above small diameter portion 412b. The upper end of large diameter portion 412c is continuous with lid portion 116. The horizontal cross-sectional area of the internal space of large diameter portion 412c is larger than that of small diameter portion 412b. Expanded diameter portion 412e is continuous with the upper end of small diameter portion 412b and the lower end of large diameter portion 412c. The horizontal cross-sectional area of the internal space of expanded diameter portion 412e gradually increases from bottom to top. Because upper portion 412 includes large diameter portion 412a, small diameter portion 412b, large diameter portion 412c, contracted diameter portion 412d, and expanded diameter portion 412e, it is possible to differentiate the aeration flow rate in the horizontal direction. For example, by reducing the aeration flow rate in the central portion and increasing the aeration flow rate in the peripheral portion of the central portion, the catalyst can be concentrated in the center.

[0107] The power generation systems 500, 550, and 600 may include a hydrogen production device 200 instead of the hydrogen production device 100. Similarly, the iron-making systems 700 and 750 may include a hydrogen production device 200 instead of the hydrogen production device 100.

[0108] The hydrogen produced by the hydrogen production devices 100 and 200 may also be supplied to a gas pipeline.

[0109] This disclosure can, for example, contribute to Sustainable Development Goal (SDG) 7: "Ensure access to affordable, reliable, sustainable and modern energy." [Explanation of symbols]

[0110] FB: Fluidized bed MB: Moving bed 100: Hydrogen production apparatus 110: Storage tank 112: Upper part 114: Lower part 114a: Discharge port 116a: Supply port 120: Heating section 130: First aeration pipe 140: Second aeration pipe 150: Catalyst supply section 160: Catalyst discharge section 170: Raw material gas supply section 200: Hydrogen production apparatus 210: Storage tank 310: Storage tank 312: Upper part 410: Storage tank 412: Upper part 500: Power generation system 510: Power generation apparatus 550: Power generation system 560: Power generation apparatus 600: Power generation system 610: Power generation apparatus 700: Iron making system 710: Iron making apparatus 750: Iron making system 760: Iron making apparatus

Claims

1. A storage tank; a heating unit provided in the storage tank; a first air diffuser pipe provided below the heating unit in the storage tank; a second air diffuser pipe provided below the first air diffuser pipe in the storage tank; a catalyst supply unit that supplies a catalyst containing one or more of iron, nickel, copper, and aluminum from a supply port formed in the storage tank above the heating unit; a catalyst discharge section that discharges the catalyst from a discharge port formed in the storage tank below the second air diffuser pipe; a raw material gas supply unit that supplies a raw material gas containing at least a hydrocarbon to the first diffuser pipe and the second diffuser pipe; A hydrogen production device comprising:

2. 2. The hydrogen production device according to claim 1, wherein a flow rate of the raw material gas supplied to the first diffuser tube by the raw material gas supply unit is greater than a flow rate of the raw material gas supplied to the second diffuser tube.

3. 2. The hydrogen production device according to claim 1, wherein a superficial velocity ratio U0 / Umf of a total of the raw material gas diffused from the first diffuser pipe and the raw material gas diffused from the second diffuser pipe is 1.1 or more and 2.0 or less.

4. In the storage tank, a fluidized bed of the catalyst is formed above the first diffuser pipe, The hydrogen production device according to claim 1 , wherein a moving layer of the catalyst is formed below the first diffuser pipe.

5. The storage tank is A cylindrical upper portion, a lower portion provided below the upper portion, the horizontal cross-sectional area of the internal space of which gradually decreases from the top to the bottom; and The heating unit is provided in the upper portion, The hydrogen production device according to claim 1 , wherein the second diffuser pipe is provided within the lower portion.

6. The hydrogen production device according to claim 5 , wherein the container vessel has one upper portion and a plurality of lower portions.

7. a hydrogen production device comprising: a storage tank; a heating unit provided within the storage tank; a first diffuser pipe provided below the heating unit within the storage tank; a second diffuser pipe provided below the first diffuser pipe within the storage tank; a catalyst supply unit that supplies a catalyst containing one or more of iron, nickel, copper, and aluminum from a supply port formed above the heating unit in the storage tank; a catalyst discharge unit that discharges the catalyst from a discharge port formed below the second diffuser pipe in the storage tank; and a raw material gas supply unit that supplies a raw material gas containing at least a hydrocarbon to the first diffuser pipe and the second diffuser pipe; a power generation device that generates electricity using hydrogen produced by the hydrogen production device; A power generation system comprising:

8. a hydrogen production device comprising: a storage tank; a heating unit provided within the storage tank; a first diffuser pipe provided below the heating unit within the storage tank; a second diffuser pipe provided below the first diffuser pipe within the storage tank; a catalyst supply unit that supplies a catalyst containing one or more of iron, nickel, copper, and aluminum from a supply port formed above the heating unit in the storage tank; a catalyst discharge unit that discharges the catalyst from a discharge port formed below the second diffuser pipe in the storage tank; and a raw material gas supply unit that supplies a raw material gas containing at least a hydrocarbon to the first diffuser pipe and the second diffuser pipe; an iron-making apparatus for producing iron using hydrogen produced by the hydrogen production apparatus; A steelmaking system comprising:

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