WO2021186924A1 - 水素製造装置 - Google Patents
水素製造装置 Download PDFInfo
- Publication number
- WO2021186924A1 WO2021186924A1 PCT/JP2021/003762 JP2021003762W WO2021186924A1 WO 2021186924 A1 WO2021186924 A1 WO 2021186924A1 JP 2021003762 W JP2021003762 W JP 2021003762W WO 2021186924 A1 WO2021186924 A1 WO 2021186924A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- storage tank
- hydrogen
- unit
- heating furnace
- hydrogen production
- Prior art date
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
- C01B3/26—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/05—Preparation or purification of carbon not covered by groups C01B32/15, C01B32/20, C01B32/25, C01B32/30
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
- H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
- C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/046—Purification by cryogenic separation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/049—Composition of the impurity the impurity being carbon
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
- C01B2203/0827—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel at least part of the fuel being a recycle stream
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/14—Details of the flowsheet
- C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
- C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus
Definitions
- an apparatus including a reactor, a raw material gas supply source, and a heating unit is disclosed (for example, Patent Document 1), and the reactor houses a catalyst.
- the raw material gas supply source supplies hydrocarbons to the reactor.
- the heating unit is provided around the reactor and heats the inside of the reactor.
- the thermal decomposition reaction of hydrocarbons proceeds efficiently at 800 ° C. or higher by using a catalyst.
- the thermal decomposition reaction of hydrocarbons is an endothermic reaction, it is necessary to supply heat from the outside. Therefore, in the technique of heating the reactor from the outside as in Patent Document 1, it is necessary to heat the furnace wall of the reactor to 1000 ° C or higher in order to raise the temperature of the inside of the reactor to 800 ° C or higher. .. Then, the reactor must be constructed of a material having a heat resistance of 1000 ° C. or higher, and there is a problem that the cost required for the reactor increases.
- the present disclosure aims to provide a hydrogen production apparatus capable of thermally decomposing hydrocarbons at low cost.
- the hydrogen production apparatus is connected to a heating furnace that burns the fuel supplied by the fuel supply unit to heat the catalyst particles and a downstream side of the heating furnace.
- a cyclone that separates the catalyst particles and the combustion exhaust gas
- a storage tank that houses the catalyst particles separated by the cyclone
- a raw material gas introduction unit that introduces a raw material gas containing at least hydrocarbons from the lower part of the storage tank. It is equipped with a thermal decomposition furnace having the above.
- a hydrogen separation unit that separates hydrogen from the mixed gas sent from the storage tank may be provided, and the fuel supply unit may supply the hydrogen separated by the hydrogen separation unit to the heating furnace as fuel.
- a hydrogen separation unit for separating hydrogen from the mixed gas sent from the storage tank may be provided, and the fuel supply unit may supply the mixed gas after the hydrogen is separated by the hydrogen separation unit to the heating furnace as fuel. ..
- a carbon recovery unit for removing solid carbon from the mixed gas sent from the storage tank may be provided, and the fuel supply unit may supply the mixed gas from which the solid carbon has been removed to the heating furnace as fuel.
- the storage tank is located between the particle introduction port where the catalyst particles separated by the cyclone are guided, the first outlet where the mixed gas generated in the storage tank is sent out, and the particle introduction port and the first outlet.
- the fuel supply unit has a second outlet for sending out the mixed gas generated in the storage tank, and the fuel supply unit uses the mixed gas sent out from the storage tank as fuel through the heating furnace. May be supplied to.
- a partition plate for partitioning the inside of the storage tank may be provided in the first room provided in the storage tank and provided with the first outlet and the second room provided with the second outlet.
- a first heat exchange unit that heat-exchanges the combustion exhaust gas separated by the cyclone and the oxidant, and an oxidant supply unit that supplies the oxidant that has been heat-exchanged by the first heat exchange unit to the heating furnace are provided. You may prepare.
- a second heat exchange unit for heat exchange between the mixed gas sent from the storage tank and the raw material gas is provided, and the raw material gas introduction unit introduces the raw material gas heat exchanged by the second heat exchange unit into the storage tank. You may.
- hydrocarbons can be thermally decomposed at low cost.
- FIG. 1 is a diagram illustrating a hydrogen production apparatus according to the first embodiment.
- FIG. 2 is a diagram illustrating a purification apparatus according to the first embodiment.
- FIG. 3 is a diagram illustrating a fuel supply unit according to the first modification.
- FIG. 4 is a diagram illustrating a fuel supply unit according to the second modification.
- FIG. 5 is a diagram illustrating a heating furnace, a cyclone, and a pyrolysis furnace according to a third modification.
- FIG. 6 is a diagram illustrating a hydrogen production apparatus according to a second embodiment.
- FIG. 7 is a diagram illustrating a purification apparatus according to the second embodiment.
- FIG. 8 is a diagram illustrating the relationship between the reaction time in which methane, which is a raw material gas, is aerated through the catalyst particles and the amount of gas produced in the storage tank.
- FIG. 1 is a diagram illustrating a hydrogen production apparatus 100 according to the first embodiment.
- the hydrogen production apparatus 100 includes a heating furnace 110, a first pipe 112, a second pipe 114, a cyclone 120, a communication pipe 122, a pyrolysis furnace 130, and a first delivery pipe 134.
- a purification device 150, a dust removing device 160, a third pipe 162, an oxidizing agent supply unit 170, a first heat exchange unit 180, and a fuel supply unit 190 are included.
- the solid arrow indicates the gas flow.
- the dashed arrow indicates the flow of the catalyst particle CAT.
- the heating furnace 110 has a tubular shape.
- the first pipe 112 connects the lower part of the heating furnace 110 to the pyrolysis furnace 130 (side surface of the storage tank 132) described later.
- the first pipe 112 is provided with a loop seal (not shown).
- the catalyst particle CAT is introduced into the heating furnace 110 from the pyrolysis furnace 130 through the first pipe 112 and the loop seal.
- the catalyst particle CAT is a catalyst that promotes the thermal decomposition reaction represented by the following formula (1). CH 4 ⁇ C + 2H 2 ... Equation (1)
- the catalyst particle CAT is, for example, an iron-based catalyst (iron, iron ore).
- the particle size of the catalyst particle CAT is, for example, 50 ⁇ m or more and 1000 ⁇ m or less, preferably 100 ⁇ m or more and 300 ⁇ m or less.
- the heating furnace 110 heats the catalyst particle CAT to about 900 ° C. by burning the fuel FG supplied by the fuel supply unit 190, which will be described later, with air.
- the second pipe 114 connects the upper part of the heating furnace 110 to the cyclone 120, which will be described later.
- the catalyst particle CAT and the combustion exhaust gas EX heated in the heating furnace 110 are sent to the cyclone 120 through the second pipe 114.
- the cyclone 120 is provided above the pyrolysis furnace 130.
- the cyclone 120 is connected to the downstream side of the heating furnace 110 via the second pipe 114.
- the cyclone 120 solid-gas separates the mixture of the catalyst particle CAT and the combustion exhaust gas EX introduced from the heating furnace 110 through the second pipe 114.
- the communication pipe 122 connects the bottom of the cyclone 120 and the pyrolysis furnace 130 (accommodation tank 132). Further, the communication pipe 122 is provided with a loop seal (not shown). The high-temperature catalyst particle CAT separated by the cyclone 120 passes through the communication pipe 122 and the loop seal and is introduced into the pyrolysis furnace 130.
- the pyrolysis furnace 130 is, for example, a bubble fluidized bed (bubbling fluidized bed) furnace.
- the pyrolysis furnace 130 fluidizes the high-temperature catalyst particle CAT introduced from the cyclone 120 by the raw material gas GG.
- the raw material gas GG contains at least hydrocarbons (eg, methane).
- the raw material gas GG is, for example, liquefied natural gas (LNG).
- LNG liquefied natural gas
- the pyrolysis furnace 130 includes a storage tank 132 and a raw material gas introduction unit 140.
- the storage tank 132 is a container for containing the high-temperature catalyst particle CAT separated by the cyclone 120.
- a particle introduction port 132a and a first delivery port 132b are provided on the upper surface of the storage tank 132.
- the first outlet 132b is provided on the downstream side of the particle introduction port 132a in the flow direction of the catalyst particle CAT.
- a communication pipe 122 is connected to the particle introduction port 132a.
- the first delivery pipe 134 is connected to the first delivery port 132b.
- a particle discharge port 132c is provided on the side surface of the storage tank 132.
- the first pipe 112 is connected to the particle discharge port 132c.
- the bottom surface of the storage tank 132 is composed of a breathable dispersion plate 142a.
- the raw material gas introduction unit 140 introduces the raw material gas GG from the lower part of the storage tank 132.
- the raw material gas introduction unit 140 includes a wind box 142 and a blower 144.
- the wind box 142 is provided below the storage tank 132.
- the upper part of the wind box 142 is composed of the dispersion plate 142a.
- the dispersion plate 142a partitions the storage tank 132 and the air box 142.
- the blower 144 supplies the raw material gas GG to the air box 142.
- the suction side of the blower 144 is connected to the supply source of the raw material gas GG through the raw material supply pipe 146.
- the discharge side of the blower 144 is connected to the air box 142 through the raw material delivery pipe 148.
- the raw material gas GG supplied to the air box 142 by the blower 144 is introduced into the storage tank 132 from the bottom surface (dispersion plate 142a) of the storage tank 132.
- the high-temperature catalyst particle CAT introduced from the cyclone 120 through the particle introduction port 132a is fluidized by the raw material gas GG, and a fluidized bed R (bubble fluidized bed) is formed in the accommodating tank 132. Further, the thermal decomposition furnace 130 thermally decomposes the raw material gas GG with the heat of the fluidized bed R (catalyst particle CAT). That is, the thermal decomposition reaction represented by the above formula (1) proceeds in the storage tank 132.
- the mixed gas MG containing hydrogen (H 2 ), unreacted methane (CH 4 ), carbon monoxide (CO), carbon dioxide (CO 2 ), and solid carbon (SC) is produced. Will be generated.
- the mixed gas MG generated in the pyrolysis furnace 130 is introduced into the purification apparatus 150 through the first delivery port 132b and the first delivery pipe 134.
- the purification device 150 separates hydrogen from the mixed gas MG.
- the purification apparatus 150 will be described in detail later.
- the catalyst particle CAT fluidized in the pyrolysis furnace 130 is returned to the heating furnace 110 through the particle discharge port 132c and the first pipe 112.
- the catalyst particle CAT includes the heating furnace 110, the second pipe 114, the cyclone 120, the communication pipe 122, the pyrolysis furnace 130 (containment tank 132), and the first pipe 112. Are moved in this order and introduced into the heating furnace 110 again to circulate them.
- the dust remover 160 is connected to the upper part of the cyclone 120 through the third pipe 162.
- the dust remover 160 removes the combustion exhaust gas EX.
- the dust remover 160 is, for example, a bug filter.
- the combustion exhaust gas EX dust removed by the dust remover 160 is released to the atmosphere.
- the oxidant supply unit 170 supplies air to the heating furnace 110.
- the oxidant supply unit 170 includes a blower 172 and an oxidant supply pipe 174.
- the suction side of the blower 172 is opened to the atmosphere.
- the discharge side of the blower 172 is connected to the oxidant supply pipe 174.
- the oxidant supply pipe 174 connects the blower 172 to the bottom of the heating furnace 110.
- the first heat exchange unit 180 exchanges heat between the combustion exhaust gas EX (combustion exhaust gas EX passing through the third pipe 162) separated by the cyclone 120 and the air passing through the oxidant supply pipe 174. As a result, heat is removed (cooled) from the combustion exhaust gas EX, and the air is heated. In this way, the cooled combustion exhaust gas EX is guided to the dust removing device 160. Further, the heated air is guided to the heating furnace 110 by the oxidant supply unit 170.
- the fuel supply unit 190 supplies the fuel FG to the heating furnace 110.
- the fuel supply unit 190 will be described in detail later.
- FIG. 2 is a diagram illustrating the purification apparatus 150 according to the first embodiment.
- the refining apparatus 150 includes a cyclone 210, a fourth pipe 212, a carbon recovery unit 220, a fifth pipe 222, a compressor 230, a sixth pipe 232, a hydrogen separation unit 240, and the like.
- the seventh pipe 242, the eighth pipe 244, and the second heat exchange unit 250 are included.
- the cyclone 210 is connected to the first delivery port 132b of the storage tank 132 via the first delivery pipe 134.
- the cyclone 210 firmly separates the mixed gas MG delivered from the storage tank 132 through the first delivery pipe 134.
- the solid matter (catalyst particle CAT and solid carbon SC) separated by the cyclone 210 is used as a nanocarbon material or mixed with a structural material such as asphalt or concrete.
- the fourth pipe 212 connects the upper part of the cyclone 210 and the carbon recovery unit 220.
- the mixed gas MG after the solid matter is separated by the cyclone 210 is guided to the carbon recovery unit 220 through the fourth pipe 212.
- the carbon recovery unit 220 removes the solid carbon SC from the mixed gas MG.
- the carbon capture unit 220 is, for example, a bag filter or a cyclone.
- the solid carbon SC removed by the carbon recovery unit 220 is transported to the solid carbon utilization facility in the subsequent stage.
- the fifth pipe 222 connects the carbon recovery unit 220 and the suction side of the compressor 230.
- the compressor 230 boosts the mixed gas MG from which the solid carbon SC has been removed by the carbon recovery unit 220 and sends it to the hydrogen separation unit 240.
- the compressor 230 also functions as a fuel supply unit 190.
- the sixth pipe 232 connects the discharge side of the compressor 230 and the hydrogen separation unit 240.
- the hydrogen separation unit 240 separates hydrogen from the mixed gas MG.
- the hydrogen separation unit 240 is, for example, an apparatus using Pressure Swing Adsorption (PSA) or a deep cold separation apparatus.
- PSA Pressure Swing Adsorption
- the seventh pipe 242 connects the hydrogen separation unit 240 and the hydrogen utilization equipment in the subsequent stage.
- the hydrogen separated by the hydrogen separation unit 240 (for example, with a purity of 99% or more) is sent to the hydrogen utilization facility.
- the eighth pipe 244 connects the hydrogen separation unit 240 and the raw material supply pipe 146.
- the mixed gas MG after hydrogen is separated by the hydrogen separation unit 240 is mixed with the raw material gas GG derived from the raw material gas supply source and supplied to the storage tank 132. That is, the mixed gas MG after hydrogen is separated by the hydrogen separation unit 240 is guided to the storage tank 132 as the raw material gas GG.
- the mixed gas MG after hydrogen has been separated by the hydrogen separator 240 contains at least unreacted methane and hydrogen.
- the fuel supply unit 190 includes a compressor 230 and a fuel supply pipe 192.
- the fuel supply pipe 192 connects the seventh pipe 242 and the heating furnace 110 (see FIG. 1). Therefore, in the present embodiment, the fuel supply unit 190 supplies the hydrogen separated by the hydrogen separation unit 240 to the heating furnace 110 as the fuel FG.
- the second heat exchange unit 250 exchanges heat between the mixed gas MG solidly separated by the cyclone 210 and the raw material gas GG.
- the second heat exchange unit 250 exchanges heat between the mixed gas MG passing through the fourth pipe 212 and the raw material gas GG passing through the raw material delivery pipe 148.
- heat is removed (cooled) from the mixed gas MG, and the raw material gas GG is heated.
- the cooled mixed gas MG is guided to the carbon recovery unit 220.
- the heated raw material gas GG is guided to the pyrolysis furnace 130 (accommodation tank 132) by the raw material gas introduction unit 140.
- the hydrogen production apparatus 100 includes a heating furnace 110 and a pyrolysis furnace 130. Therefore, the hydrogen production apparatus 100 can thermally decompose methane (hydrocarbon) by the heat of the catalyst particle CAT heated by the heating furnace 110.
- the heated catalyst particle CAT is introduced into the pyrolysis furnace 130 (inside the storage tank 132). Therefore, the inside of the storage tank 132 is heated substantially uniformly by the catalyst particle CAT. Therefore, the hydrogen production apparatus 100 does not need to heat the pyrolysis furnace 130 from the outside. As a result, the hydrogen production apparatus 100 does not need to form the furnace wall of the pyrolysis furnace 130 with a material having heat resistance of 1000 ° C. or higher, and the production cost of the pyrolysis furnace 130 can be reduced. Therefore, the hydrogen production apparatus 100 can thermally decompose methane (hydrocarbon) at low cost. In other words, the hydrogen production apparatus 100 can produce hydrogen at low cost.
- the hydrogen production apparatus 100 can make the temperature inside the storage tank 132 uniform as compared with the conventional technique of heating the inside of the pyrolysis furnace from the outside. This makes it possible for the hydrogen production apparatus 100 to avoid a situation in which the temperature of the catalyst particle CAT is locally lowered in the storage tank 132. Therefore, the hydrogen production apparatus 100 can efficiently thermally decompose methane (hydrocarbon). Further, since the hydrogen production apparatus 100 can make the temperature inside the storage tank 132 uniform, it is possible to increase the size of the storage tank 132. As a result, the hydrogen production apparatus 100 can produce a large amount of hydrogen at low cost.
- the raw material gas introduction unit 140 forms the fluidized bed R of the catalyst particle CAT in the storage tank 132.
- the pyrolysis furnace 130 can slide the catalyst particle CATs in the accommodation tank 132. Therefore, the pyrolysis furnace 130 can desorb the solid carbon SC grown on the surface of the catalyst particle CAT. Therefore, the hydrogen production apparatus 100 can omit a dedicated apparatus (for example, a chemical cleaning apparatus) for separating the solid carbon SC from the catalyst particle CAT.
- the hydrogen production apparatus 100 includes a hydrogen separation unit 240 and a fuel supply unit 190.
- the hydrogen production apparatus 100 can burn the hydrogen as the fuel FG to heat the catalyst particle CAT. Therefore, the hydrogen production apparatus 100 can prevent the generation of carbon dioxide in the heating of the catalyst particle CAT. Therefore, the hydrogen production apparatus 100 can produce carbon dioxide-free hydrogen.
- the hydrogen production apparatus 100 includes the first heat exchange unit 180, and the oxidant supply unit 170 supplies the air heated by the first heat exchange unit 180 to the heating furnace 110. That is, the hydrogen production apparatus 100 can preheat the air supplied to the heating furnace 110. Therefore, the hydrogen production apparatus 100 can reduce the amount of fuel FG required to heat the catalyst particle CAT to a desired temperature (for example, 900 ° C.). Therefore, the hydrogen production apparatus 100 can heat the catalyst particle CAT at low cost. Further, the first heat exchange unit 180 can cool the combustion exhaust gas EX before supplying it to the dust removing device 160. Therefore, the hydrogen production device 100 can prevent the dust removing device 160 from being damaged.
- the first heat exchange unit 180 can cool the combustion exhaust gas EX before supplying it to the dust removing device 160. Therefore, the hydrogen production device 100 can prevent the dust removing device 160 from being damaged.
- the hydrogen production apparatus 100 includes the second heat exchange unit 250, and the raw material gas introduction unit 140 heats the raw material gas GG heated by the second heat exchange unit 250 into the pyrolysis furnace 130 (accommodation tank). It is introduced in 132). That is, the hydrogen production apparatus 100 can preheat the raw material gas GG supplied to the pyrolysis furnace 130. Therefore, the hydrogen production apparatus 100 can suppress a decrease in the temperature of the pyrolysis furnace 130. Therefore, the hydrogen production apparatus 100 can reduce the heating amount (fuel FG amount) of the catalyst particle CAT in the heating furnace 110. Further, the hydrogen production apparatus 100 can suppress the non-uniformity of the temperature in the pyrolysis furnace 130.
- the hydrogen production apparatus 100 can efficiently thermally decompose methane (hydrocarbon). Further, the second heat exchange unit 250 can cool the mixed gas MG before supplying it to the carbon recovery unit 220. Therefore, the hydrogen production apparatus 100 can prevent the carbon recovery unit 220 from being damaged.
- the configuration in which the fuel supply unit 190 supplies the hydrogen separated by the hydrogen separation unit 240 as the fuel FG to the heating furnace 110 is given as an example.
- the fuel supply unit may supply another gas as a fuel FG to the heating furnace 110.
- FIG. 3 is a diagram for explaining the fuel supply unit 310 according to the first modification.
- the fuel supply unit 310 according to the first modification includes a compressor 230 and a fuel supply pipe 312.
- the fuel supply pipe 312 connects the raw material delivery pipe 148 and the heating furnace 110 (see FIG. 1). Therefore, in the first modification, the fuel supply unit 310 supplies the mixed gas MG after the hydrogen is removed by the hydrogen separation unit 240 to the heating furnace 110 as the fuel FG.
- the mixed gas MG after hydrogen has been removed by the hydrogen separator 240 contains unreacted methane and hydrogen.
- the fuel supply unit 310 supplies the mixed gas MG to the heating furnace 110 instead of hydrogen. That is, unlike the first embodiment, the fuel supply unit 310 does not use the hydrogen produced by the hydrogen separation unit 240 for combustion of the heating furnace 110. Therefore, the fuel supply unit 310 can increase the amount of hydrogen produced per unit amount of raw material gas GG as compared with the first embodiment. Therefore, the hydrogen production apparatus 100 provided with the fuel supply unit 310 can produce hydrogen at low cost.
- the fuel supply units 190 and 310 supply the hydrogen or mixed gas MG separated by the hydrogen separation unit 240 as the fuel FG to the heating furnace 110.
- the fuel supply unit may supply another gas as a fuel FG to the heating furnace 110.
- FIG. 4 is a diagram for explaining the fuel supply unit 320 according to the second modification.
- the fuel supply unit 320 according to the second modification includes a compressor 230 and a fuel supply pipe 322.
- the fuel supply pipe 322 connects the sixth pipe 232 and the heating furnace 110 (see FIG. 1). Therefore, in the second modification, the fuel supply unit 320 supplies the mixed gas MG from which the solid carbon has been removed by the carbon recovery unit 220 to the heating furnace 110 as fuel.
- the mixed gas MG from which solid carbon has been removed by the carbon recovery unit 220 contains unreacted methane and hydrogen.
- the fuel supply unit 320 can reduce the amount of the mixed gas MG guided to the hydrogen separation unit 240 as compared with the first embodiment. This makes it possible to reduce the hydrogen separation power of the hydrogen separation unit 240. Further, the main component of the mixed gas MG guided to the hydrogen separation unit 240 is hydrogen. Therefore, when the fuel supply unit 320 uses the mixed gas MG as the fuel FG, the amount of carbon dioxide generated can be reduced as compared with the case where the hydrocarbon is used as the fuel FG.
- the configuration in which the loop seal is provided in the first pipe 112 and the communication pipe 122 is given as an example.
- the loop seal can be omitted.
- FIG. 5 is a diagram illustrating a heating furnace 110, a cyclone 120, and a pyrolysis furnace 130 according to a third modification.
- the broken line indicates the upper surface of the fluidized bed R of the catalyst particle CAT.
- the communication pipe 122 penetrates the upper surface of the storage tank 132 and extends to the inside of the storage tank 132.
- the lower opening 122a of the communication pipe 122 is located in the fluidized bed R formed in the storage tank 132.
- the side surface of the storage tank 132 and the side surface of the heating furnace 110 communicate with each other through the opening 110a.
- a first partition plate 350 and a second partition plate 352 are provided in the storage tank 132.
- the first partition plate 350 is a plate extending vertically (standing) from the dispersion plate 142a to the upper end 350a and extending over both side surfaces.
- the upper end 350a (tip) of the first partition plate 350 is separated from the upper surface of the storage tank 132.
- the first delivery pipe 134 is connected between the communication pipe 122 and the first partition plate 350 on the upper surface of the storage tank 132.
- the second partition plate 352 is provided between the first partition plate 350 and the opening 110a.
- the second partition plate 352 is a plate extending vertically from the upper surface of the storage tank 132 to the lower end 352a and extending over both side surfaces.
- the lower end 352a (tip) of the second partition plate 352 is separated from the dispersion plate 142a.
- the upper end 350a of the first partition plate 350 is located above the lower end 352a of the second partition plate 352.
- the lower end 352a of the second partition plate 352 is located below the lower end 110b of the opening 110a.
- the lower end 110b of the opening 110a is located below the upper end 350a of the first partition plate 350.
- a third partition plate 142b is provided in the wind box 142 of the third modification.
- the third partition plate 142b is provided at a position corresponding to the first partition plate 350 in the air box 142.
- the third partition plate 142b partitions the inside of the air box 142 so that the raw material gas GG cannot be distributed or is difficult to distribute.
- the raw material delivery pipe 148 is connected between the communication pipe 122 and the first partition plate 350 in the air box 142, and between the first partition plate 350 and the opening 110a.
- the communication pipe 122 according to the third modification penetrates the upper surface of the storage tank 132 and extends to the inside of the storage tank 132.
- the communication pipe 122 of the third modification can omit the loop seal.
- the heating furnace 110 and the pyrolysis furnace 130 according to the third modification include an opening 110a, a first partition plate 350, and a second partition plate 352.
- the heating furnace 110 and the pyrolysis furnace 130 can omit the first pipe 112 and the loop seal.
- the loop seal and the device attached to the loop seal can be omitted. Therefore, in the third modification, the hydrogen production apparatus 100 as a whole can be made compact, and the hydrogen production apparatus 100 can be reduced in cost.
- FIG. 6 is a diagram for explaining the hydrogen production apparatus 400 according to the second embodiment.
- FIG. 7 is a diagram illustrating the purification apparatus 450 according to the second embodiment.
- the hydrogen production apparatus 400 includes a heating furnace 110, a first pipe 112, a second pipe 114, a cyclone 120, a communication pipe 122, a heat decomposition furnace 430, and a first delivery pipe 134.
- a second delivery pipe 136, a purification device 450, a dust removing device 160, a third pipe 162, an oxidant supply unit 170, a first heat exchange unit 180, and a fuel supply unit 490 are included. Further, as shown in FIG.
- the purification apparatus 450 includes a cyclone 210, a fourth pipe 212, a carbon recovery unit 220, a fifth pipe 222, a compressor 230, a sixth pipe 232, and a hydrogen separation unit 240.
- the seventh pipe 242, the eighth pipe 244, the second heat exchange unit 250, the cyclone 460, and the second heat exchange unit 470 are included.
- FIGS. 6 and 7 indicate the gas flow.
- the dashed arrow indicates the flow of the catalyst particle CAT.
- the components substantially the same as those of the hydrogen production apparatus 100 are designated by the same reference numerals and the description thereof will be omitted.
- the pyrolysis furnace 430 includes a storage tank 132, a partition plate 434, and a raw material gas introduction unit 140.
- a particle introduction port 132a, a first delivery port 132b, and a second delivery port 432a are provided on the upper surface of the storage tank 132.
- the second outlet 432a is provided between the particle introduction port 132a and the first outlet 132b. That is, the second outlet 432a is provided on the downstream side in the flow direction of the catalyst particle CAT with respect to the particle introduction port 132a. Further, the second outlet 432a is provided on the upstream side of the first outlet 132b in the flow direction of the catalyst particle CAT.
- a second delivery pipe 136 is connected to the second delivery port 432a.
- the partition plate 434 is provided in the storage tank 132.
- the partition plate 434 is a plate extending vertically from the upper surface to the lower end of the accommodating tank 132 and extending over both side surfaces.
- the lower end (tip) of the partition plate 434 is separated from the dispersion plate 142a (bottom).
- the partition plate 434 divides the inside of the storage tank 132 into a first chamber 432A provided with the first outlet 132b and a second chamber 432B provided with the particle introduction port 132a and the second outlet 432a.
- the lower end of the partition plate 434 is located in the fluidized bed R formed of the catalyst particles CAT. That is, the partition plate 434 divides the freeboard area formed in the storage tank 132 into two.
- FIG. 8 is a diagram for explaining the relationship between the reaction time in which methane, which is the raw material gas GG, is aerated through the catalyst particle CAT, and the amount of gas produced in the storage tank 132.
- the horizontal axis shows the passage of reaction time for methane decomposition.
- the vertical axis indicates the amount of gas produced in the storage tank 132.
- white circles indicate methane.
- white squares indicate hydrogen.
- black squares indicate carbon monoxide.
- black circles indicate carbon dioxide.
- methane decreases with the progress of the thermal decomposition reaction until the residence time of the catalyst particle CAT reaches the time Ta.
- methane gradually increases when the residence time of the catalyst particle CAT exceeds the time Ta.
- the amount of hydrogen produced increases with the progress of the thermal decomposition reaction of methane until the residence time of the catalyst particle CAT reaches the time Ta. In addition, the amount of hydrogen produced gradually decreases beyond the time Ta.
- the amount of carbon monoxide produced increases until the residence time of the catalyst particle CAT reaches Tb, which is shorter than the time Ta, and gradually decreases when the time Tb is exceeded. Further, when the time Ta is exceeded, the amount of carbon monoxide produced becomes about 0.
- the amount of carbon dioxide produced is slightly generated before the residence time of the catalyst particle CAT reaches the time Tb, but when the time Ta is exceeded, the amount of carbon dioxide produced becomes about 0. That is, as shown in FIG. 8, it can be seen that carbon monoxide and carbon dioxide are produced by the time the residence time of the catalyst particle CAT reaches the time Ta.
- the heating furnace 110 At least a part of the catalyst particle CAT is oxidized by oxygen contained in the air used for burning the fuel FG, and the oxidized catalyst particle CAT is guided to the pyrolysis furnace 130. Then, the catalyst particle CAT oxidized in the pyrolysis furnace 130 is reduced by methane to produce carbon monoxide and carbon dioxide.
- the catalyst particle CAT is guided into the storage tank 132 through the particle introduction port 132a and discharged from the storage tank 132 through the particle discharge port 132c. That is, the catalyst particle CAT moves in the storage tank 132 from the right side to the left side in FIG. Therefore, the partition plate 434 is installed at a position in the storage tank 132 where the residence time of the catalyst particle CAT corresponds to a predetermined time of time Ta or more.
- the partition plate 434 restricts the movement of the mixed gas MGb containing carbon monoxide and carbon dioxide produced by the reduction of the catalyst particles CAT to the first chamber 432A in the second chamber 432B. Can be done.
- the reduced catalyst particle CAT passes below the partition plate 434 and moves to the first chamber 432A. Therefore, the pyrolysis furnace 430 can generate a mixed gas MGa containing hydrogen and methane in the first chamber 432A.
- the mixed gas MGb containing methane, hydrogen, carbon monoxide, and carbon dioxide produced in the second chamber 432B is sent to the cyclone 460 through the second delivery port 432a and the second delivery pipe 136.
- the mixed gas MGa containing methane and hydrogen produced in the first chamber 432A is sent to the cyclone 210 through the first delivery port 132b and the first delivery pipe 134.
- the cyclone 460 is connected to the second delivery port 432a of the storage tank 132 via the second delivery pipe 136.
- the cyclone 460 solid-gas separates the mixed gas MGb delivered from the storage tank 132 through the second delivery pipe 136.
- the solid matter (catalyst particle CAT and solid carbon SC) separated by the cyclone 460 is used as a nanocarbon material or mixed with a structural material such as asphalt or concrete.
- the fuel supply unit 490 includes a ninth pipe 492, a carbon recovery unit 494, a tenth pipe 496, a blower 498, and a fuel supply pipe 500.
- the ninth pipe 492 connects the upper part of the cyclone 460 and the carbon capture unit 494.
- the mixed gas MGb after the solid matter is separated by the cyclone 460 is guided to the carbon recovery unit 494 through the ninth pipe 492.
- the carbon recovery unit 494 removes the solid carbon SC from the mixed gas MGb.
- the carbon capture unit 494 is, for example, a bag filter or a cyclone.
- the solid carbon SC removed by the carbon recovery unit 494 is transported to the solid carbon utilization facility in the subsequent stage.
- the tenth pipe 496 connects the carbon recovery unit 494 and the suction side of the blower 498.
- the blower 498 boosts the mixed gas MGb from which the solid carbon SC has been removed by the carbon recovery unit 494 and sends it to the heating furnace 110.
- the fuel supply pipe 500 connects the discharge side of the blower 498 and the heating furnace 110.
- the fuel supply unit 490 supplies the mixed gas MGb separated by the cyclone 460 to the heating furnace 110 as the fuel FG.
- the second heat exchange unit 470 exchanges heat between the mixed gas MGb passing through the ninth pipe 492 and the raw material gas GG passing through the raw material delivery pipe 148. Then, the second heat exchange unit 250 exchanges heat between the raw material gas GG heated by the second heat exchange unit 470 and the mixed gas MGa passing through the fourth pipe 212.
- the hydrogen production apparatus 400 includes a partition plate 434 and a second delivery pipe 136.
- the hydrogen production apparatus 400 can separate carbon monoxide and carbon dioxide generated by the reduction of the catalyst particle CAT from the mixed gas MGa. Therefore, the hydrogen production apparatus 400 can increase the hydrogen concentration in the mixed gas MGa guided to the hydrogen separation unit 240. Therefore, the hydrogen production apparatus 400 can reduce the size of the hydrogen separation unit 240. As a result, the hydrogen production apparatus 400 can reduce the cost of the hydrogen separation unit 240. Therefore, the hydrogen production apparatus 400 can produce hydrogen at low cost.
- the configuration in which the fuel supply unit 190 supplies only hydrogen as the fuel FG to the heating furnace 110 is given as an example.
- the fuel supply unit 190 may supply hydrocarbons as fuel FG to the heating furnace 110 in addition to hydrogen.
- the configuration in which the oxidant supply unit 170 supplies air to the heating furnace 110 is given as an example. ..
- the oxidant supply unit 170 may supply the oxidant to the heating furnace 110.
- the oxidant supply unit 170 may supply the oxygen-enriched gas to the heating furnace 110, for example.
- the hydrogen production apparatus 100 and 400 include the first heat exchange unit 180 as an example. rice field. However, the first heat exchange unit 180 is not an indispensable configuration. Similarly, in the first embodiment, the first modification, the second modification, and the second embodiment, the hydrogen production apparatus 100 and 400 include the second heat exchange unit 250 as an example. Listed in. However, the second heat exchange unit 250 is not an indispensable configuration. Further, in the second embodiment, the configuration in which the hydrogen production apparatus 400 includes the second heat exchange unit 470 is given as an example. However, the second heat exchange unit 470 is not an indispensable configuration.
- the partition plate 434 is not an essential configuration.
- the case where the inside of one storage tank 132 is divided into two by the partition plate 434 is taken as an example.
- it may be provided with two storage tanks 132.
- the first delivery pipe 134 and the first pipe 112 are connected to the first storage tank 132.
- the communication pipe 122 and the second delivery pipe 136 are connected to the second storage tank 132.
- a pipe and a loop seal connecting the side surface of the first storage tank 132 and the side surface of the second storage tank 132 are provided. That is, the first storage tank 132 functions as the first chamber 432A, and the second storage tank 132 functions as the second chamber 432B.
- the configuration in which the second heat exchange unit 250 exchanges heat with the raw material gas GG after the heat exchange by the second heat exchange unit 470 is given as an example.
- the second heat exchange unit 470 may exchange heat with the raw material gas GG after the heat exchange by the second heat exchange unit 250.
- the fuel supply unit includes hydrogen separated by the hydrogen separation unit 240, a mixed gas after hydrogen is separated by the hydrogen separation unit 240, a mixed gas from which solid carbon has been removed by the carbon recovery unit 220, and a second fuel supply unit. Two or more kinds of mixed gases sent out from the accommodating tank 132 through the delivery port 432a may be supplied to the heating furnace 110 as fuel.
- the hydrogen production devices 100 and 400 may be provided with a soot blower or a device for supplying a gas jet in the accommodating tank 132.
- the solid carbon SC can be efficiently desorbed from the catalyst particle CAT.
- the catalyst particle CAT is appropriately added to the hydrogen production apparatus 100. It is preferable that the catalyst particle CAT is added to the accommodating tank 132 through the heating furnace 110, the first pipe 112, the second pipe 114, the cyclone 120, and the communication pipe 122. As a result, the new catalyst particle CAT can be efficiently heated. Therefore, it is possible to avoid a situation in which new catalyst particle CAT at about room temperature is supplied to the storage tank 132. Therefore, it is possible to avoid suppressing the thermal decomposition reaction by the new catalyst particle CAT at about room temperature.
- Hydrogen production equipment 110 Heating furnace 120: Cyclone 130: Thermal decomposition furnace 132: Containment tank 132a: Particle introduction port 132b: First outlet 140: Raw material gas introduction part 170: Oxidating agent supply part 180: First heat exchange Part 190: Fuel supply part 220: Carbon recovery part 240: Hydrogen separation part 250: Second heat exchange part 310: Fuel supply part 320: Fuel supply part 400: Hydrogen production equipment 430: Thermal decomposition furnace 432A: First room 432B: Room 2 432a: 2nd outlet 434: Partition plate 490: Fuel supply unit
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Health & Medical Sciences (AREA)
- Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
Description
図1は、第1の実施形態に係る水素製造装置100を説明する図である。図1に示すように、水素製造装置100は、加熱炉110と、第1配管112と、第2配管114と、サイクロン120と、連通管122と、熱分解炉130と、第1送出管134と、精製装置150と、除塵装置160と、第3配管162と、酸化剤供給部170と、第1熱交換部180と、燃料供給部190とを含む。なお、図1中、実線の矢印は、ガスの流れを示す。図1中、破線の矢印は、触媒粒子CATの流れを示す。
CH4 →C + 2H2 …式(1)
触媒粒子CATは、例えば、鉄系の触媒(鉄、鉄鉱石)である。触媒粒子CATの粒径は、例えば、50μm以上1000μm以下であり、好ましくは、100μm以上300μm以下である。
図2は、第1の実施形態に係る精製装置150を説明する図である。図2に示すように、精製装置150は、サイクロン210と、第4配管212と、炭素回収部220と、第5配管222と、コンプレッサ230と、第6配管232と、水素分離部240と、第7配管242と、第8配管244と、第2熱交換部250とを含む。
上記第1の実施形態では、燃料供給部190が、水素分離部240によって分離された水素を燃料FGとして、加熱炉110に供給する構成を例に挙げた。しかし、燃料供給部は、他のガスを燃料FGとして、加熱炉110に供給してもよい。
上記第1の実施形態および第1の変形例では、燃料供給部190、310が、水素分離部240によって分離された、水素または混合ガスMGを燃料FGとして、加熱炉110に供給する構成を例に挙げた。しかし、燃料供給部は、他のガスを燃料FGとして、加熱炉110に供給してもよい。
上記第1の実施形態では、第1配管112および連通管122にループシールが設けられる構成を例に挙げた。しかし、ループシールを省略することもできる。
図6は、第2の実施形態に係る水素製造装置400を説明する図である。図7は、第2の実施形態に係る精製装置450を説明する図である。図6に示すように、水素製造装置400は、加熱炉110と、第1配管112と、第2配管114と、サイクロン120と、連通管122と、熱分解炉430と、第1送出管134と、第2送出管136と、精製装置450と、除塵装置160と、第3配管162と、酸化剤供給部170と、第1熱交換部180と、燃料供給部490とを含む。また、図7に示すように、精製装置450は、サイクロン210と、第4配管212と、炭素回収部220と、第5配管222と、コンプレッサ230と、第6配管232と、水素分離部240と、第7配管242と、第8配管244と、第2熱交換部250と、サイクロン460と、第2熱交換部470とを含む。
Claims (8)
- 燃料供給部によって供給される燃料を燃焼させて、触媒粒子を加熱する加熱炉と、
前記加熱炉の下流側に接続され、前記触媒粒子と、燃焼排ガスとを分離するサイクロンと、
前記サイクロンによって分離された前記触媒粒子を収容する収容槽と、前記収容槽の下部から、少なくとも炭化水素を含む原料ガスを導入する原料ガス導入部と、を有する熱分解炉と、
を備える水素製造装置。 - 前記収容槽から送出された混合ガスから水素を分離する水素分離部を備え、
前記燃料供給部は、前記水素分離部によって分離された前記水素を前記燃料として前記加熱炉に供給する請求項1に記載の水素製造装置。 - 前記収容槽から送出された混合ガスから水素を分離する水素分離部を備え、
前記燃料供給部は、前記水素分離部によって水素が分離された後の前記混合ガスを前記燃料として前記加熱炉に供給する請求項1または2に記載の水素製造装置。 - 前記収容槽から送出された混合ガスから固体炭素を除去する炭素回収部を備え、
前記燃料供給部は、前記固体炭素が除去された前記混合ガスを前記燃料として前記加熱炉に供給する請求項1から3のいずれか1項に記載の水素製造装置。 - 前記収容槽は、
前記サイクロンによって分離された前記触媒粒子が導かれる粒子導入口と、
前記収容槽において生成された混合ガスが送出される第1送出口と、
前記粒子導入口と前記第1送出口との間に設けられ、前記収容槽において生成された混合ガスが送出される第2送出口と、を有し、
前記燃料供給部は、前記第2送出口を通じて、前記収容槽から送出された前記混合ガスを前記燃料として前記加熱炉に供給する請求項1から4のいずれか1項に記載の水素製造装置。 - 前記収容槽内に設けられ、前記第1送出口が設けられる第1室と、前記第2送出口が設けられる第2室とに前記収容槽内を区画する仕切板を備える請求項5に記載の水素製造装置。
- 前記サイクロンによって分離された前記燃焼排ガスと、酸化剤とを熱交換する第1熱交換部と、
前記第1熱交換部によって熱交換された前記酸化剤を前記加熱炉に供給する酸化剤供給部と、
を備える請求項1から6のいずれか1項に記載の水素製造装置。 - 前記収容槽から送出された混合ガスと、前記原料ガスとを熱交換する第2熱交換部を備え、
前記原料ガス導入部は、前記第2熱交換部によって熱交換された前記原料ガスを前記収容槽に導入する請求項1から7のいずれか1項に記載の水素製造装置。
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2022508114A JP7315092B2 (ja) | 2020-03-19 | 2021-02-02 | 水素製造装置 |
AU2021239327A AU2021239327B2 (en) | 2020-03-19 | 2021-02-02 | Hydrogen production apparatus |
CA3162599A CA3162599A1 (en) | 2020-03-19 | 2021-02-02 | Hydrogen production apparatus via heated catalyst particles |
US17/843,100 US20220324705A1 (en) | 2020-03-19 | 2022-06-17 | Hydrogen production apparatus |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2020-049291 | 2020-03-19 | ||
JP2020049291 | 2020-03-19 |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US17/843,100 Continuation US20220324705A1 (en) | 2020-03-19 | 2022-06-17 | Hydrogen production apparatus |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2021186924A1 true WO2021186924A1 (ja) | 2021-09-23 |
Family
ID=77772031
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2021/003762 WO2021186924A1 (ja) | 2020-03-19 | 2021-02-02 | 水素製造装置 |
Country Status (5)
Country | Link |
---|---|
US (1) | US20220324705A1 (ja) |
JP (1) | JP7315092B2 (ja) |
AU (1) | AU2021239327B2 (ja) |
CA (1) | CA3162599A1 (ja) |
WO (1) | WO2021186924A1 (ja) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN114534418B (zh) * | 2022-02-18 | 2023-11-28 | 阳光氢能科技有限公司 | 气液分离器和制氢系统 |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2001354405A (ja) * | 2000-06-13 | 2001-12-25 | Kawasaki Heavy Ind Ltd | 触媒直接加熱式流動層による水素製造方法及び装置 |
JP2003103235A (ja) * | 2001-09-28 | 2003-04-08 | Asao Tada | バイオマス利用の二酸化炭素除去方法及び装置 |
JP2003238973A (ja) * | 2001-09-28 | 2003-08-27 | Ebara Corp | 可燃ガス改質方法、可燃ガス改質装置及びガス化装置 |
JP2004019018A (ja) * | 2002-06-13 | 2004-01-22 | Mitsubishi Chemical Engineering Corp | 炭素質微細繊維状体の製造方法 |
JP2004256336A (ja) * | 2003-02-25 | 2004-09-16 | Nippon Oil Corp | 水素製造装置及び水素製造方法 |
JP2009221057A (ja) * | 2008-03-17 | 2009-10-01 | Japan Energy Corp | 水素製造システム |
CN108328573A (zh) * | 2018-03-26 | 2018-07-27 | 中国矿业大学 | 一种甲烷催化裂解自热生产高纯氢气的装置及方法 |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP7110885B2 (ja) * | 2018-10-02 | 2022-08-02 | 株式会社Ihi | ガス化ガス製造装置、および、ガス化ガスの製造方法 |
JP7135686B2 (ja) * | 2018-10-02 | 2022-09-13 | 株式会社Ihi | ガス化ガス製造装置、および、ガス化ガスの製造方法 |
-
2021
- 2021-02-02 WO PCT/JP2021/003762 patent/WO2021186924A1/ja active Application Filing
- 2021-02-02 AU AU2021239327A patent/AU2021239327B2/en active Active
- 2021-02-02 CA CA3162599A patent/CA3162599A1/en active Pending
- 2021-02-02 JP JP2022508114A patent/JP7315092B2/ja active Active
-
2022
- 2022-06-17 US US17/843,100 patent/US20220324705A1/en active Pending
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2001354405A (ja) * | 2000-06-13 | 2001-12-25 | Kawasaki Heavy Ind Ltd | 触媒直接加熱式流動層による水素製造方法及び装置 |
JP2003103235A (ja) * | 2001-09-28 | 2003-04-08 | Asao Tada | バイオマス利用の二酸化炭素除去方法及び装置 |
JP2003238973A (ja) * | 2001-09-28 | 2003-08-27 | Ebara Corp | 可燃ガス改質方法、可燃ガス改質装置及びガス化装置 |
JP2004019018A (ja) * | 2002-06-13 | 2004-01-22 | Mitsubishi Chemical Engineering Corp | 炭素質微細繊維状体の製造方法 |
JP2004256336A (ja) * | 2003-02-25 | 2004-09-16 | Nippon Oil Corp | 水素製造装置及び水素製造方法 |
JP2009221057A (ja) * | 2008-03-17 | 2009-10-01 | Japan Energy Corp | 水素製造システム |
CN108328573A (zh) * | 2018-03-26 | 2018-07-27 | 中国矿业大学 | 一种甲烷催化裂解自热生产高纯氢气的装置及方法 |
Also Published As
Publication number | Publication date |
---|---|
JPWO2021186924A1 (ja) | 2021-09-23 |
AU2021239327B2 (en) | 2023-08-24 |
US20220324705A1 (en) | 2022-10-13 |
CA3162599A1 (en) | 2021-09-23 |
JP7315092B2 (ja) | 2023-07-26 |
AU2021239327A1 (en) | 2022-06-30 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
JP5919393B2 (ja) | 二酸化炭素の一酸化炭素への変換方法及び装置 | |
JP3791363B2 (ja) | 重質油の軽質化方法 | |
CA2913725C (en) | Blast furnace and process for operating a blast furnace | |
TW201529859A (zh) | 用於處理金屬礦石的方法以及用於金屬生產的高爐 | |
US10316376B2 (en) | Methods and systems for increasing the carbon content of sponge iron in a reduction furnace | |
BR112016014361B1 (pt) | método de funcionamento de uma instalação de alto-forno de reciclagem de gás do bocal | |
TW201039911A (en) | Method and apparatus for sequestering carbon dioxide from a spent gas | |
WO2021186924A1 (ja) | 水素製造装置 | |
WO2009116274A1 (ja) | ガス化設備のガス化炉構造 | |
RU2726175C1 (ru) | Способы и системы для повышения содержания углерода в губчатом железе в восстановительной печи | |
JP2003226884A (ja) | 液体燃料合成システム | |
ES2704666T3 (es) | Método y equipo para producir coque durante la gasificación calentada indirectamente | |
JP2004137149A (ja) | 燃料の蒸気改質用装置ならびにシステム、および燃料を改質する方法 | |
US11642640B2 (en) | Method of recycling carbon to a feedstock gas reactor | |
US10508314B2 (en) | Methods and systems for increasing the carbon content of sponge iron in a reduction furnace | |
US20230405541A1 (en) | Hydrogen production apparatus | |
KR20150109413A (ko) | 사용후가스로부터 이산화탄소를 격리하는 방법 및 그 장치 | |
TW201617563A (zh) | 化學迴路燃燒系統及其方法 | |
AU2014204520C1 (en) | A Reaction Method and Reactor | |
CN104449861B (zh) | 一种含碳物料分级转化装置及方法 | |
CN103553041A (zh) | 一氧化碳气体发生炉及其制备一氧化碳的方法 | |
KR102640529B1 (ko) | 합성가스 개질을 위한 연속식 폐활성탄 재생 장치 및 방법 | |
JPS60131907A (ja) | 熱エネルギーの回収に適当なガスを同時に発生しながら酸化物質を還元する方法およびプラント | |
JP2004231459A (ja) | 水素製造方法及び装置 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 21770427 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 2022508114 Country of ref document: JP Kind code of ref document: A |
|
ENP | Entry into the national phase |
Ref document number: 3162599 Country of ref document: CA |
|
ENP | Entry into the national phase |
Ref document number: 2021239327 Country of ref document: AU Date of ref document: 20210202 Kind code of ref document: A |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 21770427 Country of ref document: EP Kind code of ref document: A1 |