Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
  • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
  • F17C11/00—Use of gas-solvents or gas-sorbents in vessels
  • F17C11/005—Use of gas-solvents or gas-sorbents in vessels for hydrogen
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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  • B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
  • B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
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  • B01J15/00—Chemical processes in general for reacting gaseous media with non-particulate solids, e.g. sheet material; Apparatus specially adapted therefor
  • B01J15/005—Chemical processes in general for reacting gaseous media with non-particulate solids, e.g. sheet material; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
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  • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
  • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
  • B01J21/04—Alumina
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  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
  • B01J23/42—Platinum
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  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/34—Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves ; Ionic sputtering; Flame or plasma spraying; Particle radiation
  • B01J37/348—Electrochemical processes, e.g. electrochemical deposition or anodisation
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
  • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
  • B01J8/0403—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
  • B01J8/0407—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds
  • B01J8/0411—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds the beds being concentric
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
  • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
  • B01J8/0496—Heating or cooling the reactor
• • 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; Reversible storage of hydrogen
  • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
  • C01B3/22—Production of hydrogen; Production of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds
  • C01B3/24—Production of hydrogen; Production of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
  • C01B3/26—Production of hydrogen; Production of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using catalysts
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/00106—Controlling the temperature by indirect heat exchange
  • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
  • B01J2208/00123—Fingers
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  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
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  • B01J2208/00017—Controlling the temperature
  • B01J2208/00106—Controlling the temperature by indirect heat exchange
  • B01J2208/00309—Controlling the temperature by indirect heat exchange with two or more reactions in heat exchange with each other, such as an endothermic reaction in heat exchange with an exothermic reaction
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/00504—Controlling the temperature by means of a burner
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00051—Controlling the temperature
  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
  • B01J2219/00078—Fingers
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00051—Controlling the temperature
  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00117—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with two or more reactions in heat exchange with each other, such as an endothermic reaction in heat exchange with an exothermic reaction
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00051—Controlling the temperature
  • B01J2219/00157—Controlling the temperature by means of a burner
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00051—Controlling the temperature
  • B01J2219/00159—Controlling the temperature controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00761—Details of the reactor
  • B01J2219/00763—Baffles
  • B01J2219/00765—Baffles attached to the reactor wall
  • B01J2219/00768—Baffles attached to the reactor wall vertical
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J35/00—Catalysts, in general, characterised by their form or physical properties
  • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
  • B01J35/56—Foraminous structures having flow-through passages or channels, e.g. grids or three-dimensional [3D] monoliths
• • 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
  • C01B2203/02—Processes for making hydrogen or synthesis gas
  • C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
  • C01B2203/0277—Processes for making hydrogen or synthesis gas containing a decomposition step containing a catalytic decomposition step
• • 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
• • 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
  • C01B2203/0822—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel the fuel containing hydrogen
• • 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
  • C01B2203/10—Catalysts for performing the hydrogen forming reactions
  • C01B2203/1005—Arrangement or shape of catalyst
  • C01B2203/1023—Catalysts in the form of a monolith or honeycomb
• • 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
  • C01B2203/10—Catalysts for performing the hydrogen forming reactions
  • C01B2203/1005—Arrangement or shape of catalyst
  • C01B2203/1035—Catalyst coated on equipment surfaces, e.g. reactor walls
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
  • Y02E60/30—Hydrogen technology
  • Y02E60/32—Hydrogen storage
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/10—Process efficiency

Definitions

• the present invention relates to a hydrogen generator that generates hydrogen by a dehydrogenation reaction of an organic hydride, and a hydrogenation reactor that stores hydrogen by synthesizing an organic hydride by an unsaturated hydrocarbon hydrogenation reaction.
• Examples of hydrogen storage methods that are currently in practical use include a method of sealing as a gas in a high-pressure cylinder, a method of storing in a hydrogen storage alloy, and a method of storing as liquid hydrogen.
• benzene and cyclohexane are known as cyclic hydrocarbons having the same carbon number.
• the former benzene is an unsaturated hydrocarbon in which carbon-carbon bonds are partially double bonds, while the latter cyclohexane is saturated without double bonds in carbon-carbon bonds. It is a hydrocarbon.
• decalin is obtained by hydrogenation of naphthalene, and naphthalene is obtained by dehydrogenation of decalin.
• organic compound that can supply hydrogen to the outside by a dehydrogenation reaction, such as a saturated hydrocarbon, is referred to as “organic hydride”.
• organic hydride an organic compound that can supply hydrogen to the outside by a dehydrogenation reaction
• these charcoal By using hydrogenation hydrogenation and dehydrogenation, hydrogen can be stored and supplied.
• Powerful hydrogen storage or supply technology is expected for power and power generation of automobiles (see, for example, Patent Document 1).
• Patent Document 1 JP 2002-187702 (abstract)
• the present invention has been made in view of such problems, and an object thereof is to increase the efficiency of a dehydrogenation reaction or a hydrogenation reaction.
• the present invention provides a hydrogen generator for generating hydrogen by dehydrogenation of an organic hydride in the presence of a catalyst, and a fuel for generating heat necessary for the dehydrogenation reaction And a region having a combustion catalyst used for combustion of the fuel and a region having a dehydrogenation catalyst necessary for the dehydrogenation reaction are provided adjacent to each other in a radial direction with a wall therebetween.
• the hydrogen generator has a multi-tube reactor.
• the dehydration reaction of organic hydride is an extremely endothermic reaction, and it is difficult to supply the energy necessary for the reaction in a normal packed reactor.
• the hydrogen generator of the present invention is adopted, the energy generated by the combustion of the fuel is directly transmitted to the dehydrogenation catalyst in the other region, and the energy utilization efficiency is extremely high, and the hydrogen generation rate is further increased. can do.
• another aspect of the present invention provides a hydrogen generator in which at least one of the combustion catalyst and the dehydrogenation catalyst in the previous invention is supported on the wall surface in the reactor. For this reason, the heat of combustion catalytic power is directly transmitted to the catalyst through the wall surface. Therefore, the hydrogen generation rate can be increased.
• another aspect of the present invention is a hydrogen generator in which the wall surface in the previous invention is a wall surface of a fin, pleat, lattice, or Harcam-shaped member. For this reason, the area per unit volume carrying the catalyst is increased, and the reaction efficiency can be further increased.
• another aspect of the present invention provides a hydrogen generator in which at least one of the combustion catalyst and the dehydrogenation catalyst in each of the preceding inventions is supported on an aluminum compound by anodizing treatment. It is said. For this reason, a catalyst carrier having good thermal conductivity can be obtained. Furthermore, by using aluminum with good thermal conductivity for the wall surface or fin of each region, the heat in the heat generation region can be quickly transferred to the heat absorption region.
• another aspect of the present invention is a hydrogen generation apparatus in which the fuel in each of the above inventions is a product obtained by a dehydrogenation reaction. For this reason, self-sufficient hydrogen generation using reaction products of raw materials can be realized with little or no externally supplied fuel.
• Another invention of the present invention is a hydrogenation reaction force of unsaturated hydrocarbon in the presence of a catalyst, which is a hydrogenation reaction apparatus for storing hydrogen by synthesizing an organic halide, which is generated by a hydrogenation reaction.
• a catalyst which is a hydrogenation reaction apparatus for storing hydrogen by synthesizing an organic halide, which is generated by a hydrogenation reaction.
• a hydrogen addition reaction apparatus having a multi-tube reactor equipped with a region for removing heat and a region having a hydrogenation catalyst necessary for a hydrogenation reaction, adjacent to each other in the radial direction with a wall therebetween.
• the hydrogenation reaction of unsaturated hydrocarbons for hydrogen storage is a large exothermic reaction and an equilibrium reaction, and the reaction rate decreases as the temperature increases.
• the hydrogenation reaction apparatus of the present invention is employed, the increase in reaction temperature is controlled, the efficiency of the hydrogenation reaction is improved, and the hydrogenation reaction rate can be increased.
• Another aspect of the present invention is a hydrogenation reaction apparatus in which the hydrogenation catalyst according to the previous invention is supported on a wall surface in a reactor. For this reason, the heat generated by the hydrogenation reaction is immediately removed through the wall surface. Therefore, the hydrogenation reaction rate can be further increased.
• Another aspect of the present invention is a hydrogenation reaction apparatus in which the wall surface in the previous invention is a wall surface of a fin, pleat, lattice, or Harcam-shaped member. For this reason, the area per unit volume carrying the catalyst is increased, and the reaction efficiency can be further increased.
• Another aspect of the present invention is a hydrogenation reaction apparatus in which the hydrogenation catalyst in each of the preceding inventions is supported on an aluminum compound by anodization. For this reason, a catalyst carrier having high thermal conductivity can be obtained. Furthermore, aluminum with good thermal conductivity is applied to the wall surface of each region. Alternatively, by using the fin, the heat in one region can be quickly transferred to the other region.
• FIG. 1 is a diagram schematically showing a preferred embodiment of a hydrogen generator according to the present invention.
• FIG. 2 is a perspective view schematically showing the reactor shown in FIG. 1.
• FIG. 3 is a view showing a cross section B when the reactor shown in FIG. 2 is cut along the A plane.
• FIG. 4 is a diagram schematically showing a preferred embodiment of a hydrogenation reaction apparatus according to the present invention.
• FIG. 1 is a diagram schematically showing a configuration of a preferred embodiment of a hydrogen generator according to the present invention. This figure shows one form of the hydrogen generator, and is not limited to these.
• a hydrogen generator 1 is a reactor 10 that serves as a field for dehydrogenation of methylcyclohexane (shown as "OHY” in Fig. 1), which is an example of an organic hydride. It is equipped with.
• the reactor 10 has a vertically long cylindrical shape, and has a triple tube structure in which three tubes are stacked in the radial direction.
• the innermost tube of the reactor 10 is a passage 13 for the exhaust gas produced by the combustion of a mixture of fuel (denoted “FU” in FIG. 1;) and air.
• the fuel includes Tokyo Gas, LPG, kerosene and so on.
• the upper and lower sides of the passage 13 are openings, and the exhaust gas flows from the upper side of the passage 13 downward and is discharged from the reactor 10.
• a pipe having a diameter larger than that of the passage 13 is disposed outside the passage 13.
• a region sandwiched between the pipe and the outer wall of the passage 13 is a region where a mixture of fuel and air is introduced and burned (referred to as an “inner region” in this embodiment) 12.
• the inner region 12 is connected to the lower side surface of the reactor 10 and the upper side of the passage 13.
• the lower side of the reactor 10 is provided with one or more ports leading to the inner region 12. In FIG. 1, only two mouths are shown, but one or more than three may be used.
• Fuel and air enter the inner region 12 from the lower side of the reactor 10 and burn there.
• the exhaust gas generated by the combustion enters from above the passage 13 and flows to the outside of the reactor 10.
• a tube that also serves as the outer wall of the reactor 10 is disposed further outside the inner region 12.
• the region sandwiched between the inner wall of this tube and the outer wall of the tube that constitutes the inner region is a region where toluene (shown as “TL” in FIG. 1) and hydrogen are generated by the dehydrogenation reaction of methylcyclohexane (FIG. 1). In this embodiment, it is referred to as an “outer region”. 11)
• the outer region 11 is connected to the lower side surface of the reactor 10 and the upper side of the reactor 10.
• One or more ports connected to the outer region 11 are provided on the lower side surface of the reactor 10. In Figure 1, one or more forces showing only two mouths may be used.
• Methylcyclohexane enters the outer region 11 from the lower side of the reactor 10 where it is dehydrogenated. Toluene and hydrogen generated by the dehydrogenation flow upward in the outer region 11 and the upper force of the reactor 10 is also discharged to the outside. Further details of the structure of the reactor 10 will be described later.
• the thermal energy required for the dehydrogenation reaction in the reactor 10 is obtained by heating the fuel and supplying it to the combustion catalyst.
• the fuel is sent to the flow path switching valve 21, the heat exchange 22, and the heat exchange by the pump 20a, and then heated by an electric heater 24 as an example of a heating means.
• air air for fuel mixing
• AR air
• the thermal energy required for the dehydrogenation reaction in the reactor 10 is obtained by heating the fuel and supplying it to the combustion catalyst.
• the fuel is sent to the flow path switching valve 21, the heat exchange 22, and the heat exchange by the pump 20a, and then heated by an electric heater 24 as an example of a heating means.
• air air for fuel mixing
• AR shown as “AR” in FIG. 1
• the mixer 28 is provided with an electric heater 29 which is an example of a heating means.
• the mixture of fuel and air is sufficiently heated in the mixer 28.
• the mixture of fuel and air mixed in the mixer 28 is guided to the inner region 12 in the reactor 10 from a plurality of ports (fuel inlet ports) provided on the lower side surface of the reactor 10.
• the electric heater mentioned as an example of the heating means here is mainly used at the time of start-up, and it is not always necessary to use it during the steady operation because the heat energy can be self-supplied.
• the heat exchanger 22 is a place where heat is exchanged between the fuel and the mixture of toluene and hydrogen generated by the dehydrogenation reaction of methylcyclohexane in the reactor 10.
• the fuel is preheated by the heat of the mixture of toluene and hydrogen.
• the mixture of toluene and hydrogen is deprived of heat and cooled.
• Heat exchange 23 is a place where heat is exchanged between the exhaust gas generated by the combustion of the fuel and air mixture and the fuel.
• the fuel is preheated by receiving heat from the exhaust gas power.
• the exhaust gas is cooled by the heat deprived of the fuel.
• the heat exchange 26 is a place where heat is exchanged between the exhaust gas generated by the combustion of the fuel / air mixture and the fuel mixing air.
• the air is preheated by receiving heat from the exhaust gas power.
• exhaust gas takes heat away from the air. And cooled.
• the methylcyclohexane to be dehydrogenated in the reactor 10 is sent to the heat exchanger 30 and the heat exchanger by the pump 20b.
• the methylcyclohexane is then heated by an electric heater 32 which is an example of a heating means, and sent to the outer region 11 from a plurality of ports (raw material introduction ports) provided on the lower side surface of the reactor 10.
• Heat exchange is a place where heat is exchanged between exhaust gas and raw material generated by combustion of a mixture of fuel and air.
• the raw material is preheated by receiving heat from the exhaust gas power.
• the exhaust gas is deprived of heat by the raw material and cooled. After that, the exhaust gas is discharged to the outside.
• the heat exchanger 31 is a place where heat is exchanged between the raw material and the mixture of toluene and hydrogen produced by the dehydration reaction of methylcyclohexane in the reactor 10.
• the raw material is preheated by receiving heat from a mixture of toluene and hydrogen.
• the mixture of toluene and hydrogen is cooled by taking heat away from the raw material.
• the mixture of toluene and hydrogen passes through the heat exchanger 31, the heat exchanger 22, and the heat exchanger 33 in this order, and enters the reactant container 35.
• the hydrogen that has entered the reactant container 35 passes through the heat exchanger 34 and is sent to the outside of the reactant container 35.
• the heat exchanger 33 is a place where heat is exchanged between a mixture of toluene and hydrogen and cooling water (indicated as “CW” in FIG. 1).
• CW cooling water
• Heat exchange is a place where heat is exchanged between hydrogen and cooling water.
• the heat is deprived of heat by the cooling water, cooled, and discharged outside the power.
• the fuel supply from the outside to the reactor 10 and the toluene supply to the reactor 10 The changeover valve 21 can be easily switched. Adjust the flow rate ratio between external fuel and toluene using a flow controller that does not completely switch between external fuel supply to reactor 10 and toluene supply to reactor 10. It ’s okay.
• FIG. 2 is a schematic perspective view of the reactor 10.
• FIG. 3 is a view showing a cross section B when the reactor 10 is cut along the A plane shown in FIG.
• the reactor 10 is a concentric arrangement of the largest diameter tube 14 that also serves as the outer wall of the reactor 10, the smaller diameter tube 15 than the tube 14, and the smaller diameter tube 16 than the tube 15. It is a triple-structured container that is stacked on top of each other.
• the region between tubes 14 and 15 is the outer region 11 where toluene and hydrogen are produced by the dehydrogenation reaction of methylcyclohexane.
• the outer region 11 is provided with a plurality of fins 17 arranged in the direction of the force from the tube 14 to the tube 15.
• the region between tubes 15 and 16 is an inner region 12 for introducing a mixture of fuel (including when toluene is used as fuel) and air.
• the inner region 12 is provided with a plurality of fins 18 extending from the tube 15 to the tube 16 in the direction of the force!
• the fin 17 and the fin 18 are a catalyst carrier or a member having a catalyst carrier attached to the outer surface.
• the catalyst carrier is preferably acid aluminum prepared by anodizing treatment of aluminum.
• the fin 17 carries a combustion catalyst necessary for burning a mixture of fuel and air.
• Fin 18 carries a dehydrogenation catalyst necessary for the dehydrogenation reaction of methylcyclohexane.
• platinum is suitable as the dehydrogenation catalyst.
• the catalyst carrier made of aluminum oxide is a catalyst carrier having high heat resistance.
• a catalyst carrier having a form other than the fins 17 may be disposed in the outer region 11.
• a pleat may be formed on the surface of the tube 14 or 15, and a dehydrogenation catalyst may be supported on the pleat.
• a lattice-shaped or Hercam-shaped member may be disposed in the outer region 11 and a dehydrogenation catalyst may be supported on each wall surface thereof.
• a pleat may be formed on the surface of the tube 15 or 16, and a combustion catalyst may be supported on the pleat.
• a lattice-shaped or Hercam-shaped member may be disposed in the inner region 12, and a combustion catalyst may be carried on each of these wall surfaces.
• a catalyst carrier having a form other than the fins 17 may be arranged in the inner region 12.
• the dehydrogenation catalyst in the outer region 11 is immediately heated by the heat generated by the combustion of the fuel, and the efficiency of the dehydrogenation reaction is immediately increased, and the hydrogen generation rate can be increased.
• the combustion catalyst and the dehydrogenation catalyst are supported on the fins 17 and 18 in the reactor 10, heat is directly transmitted to the dehydrogenation catalyst through the wall surfaces of the fins 17 and 18 without gas film resistance. Therefore, it is possible to further increase the hydrogen generation rate at which the energy use efficiency is extremely high.
• Table 1 shows the results of examining the hydrogen generation amount at each supply amount by changing the supply amount of methylcyclohexane.
• FIG. 4 is a diagram schematically showing a configuration of a preferred embodiment of the hydrogenation reaction apparatus according to the present invention.
• the hydrogenation reactor 40 is a reactor that serves as a field for the hydrogenation reaction of toluene (indicated as "TL" in FIG. 4), which is an example of an unsaturated hydrocarbon. 10 is provided.
• the reactor 10 has a vertically long cylindrical shape and has a triple tube structure in which three tubes are stacked in the radial direction.
• the innermost tube of the reactor 10 is a passage 13 for cooling air or cooling water. The heated air or water that is open at both the upper side and the lower side of the passage 13 flows from the upper side to the lower side of the passage 13 and is discharged from the reactor 10.
• the temperature of the hydrogenation catalyst in the reactor 10 is preferably in the range of 70 to 250 ° C. Since the hydrogenation reaction is an exothermic reaction, when the temperature exceeds 250 ° C, the hydrogenation reaction is suppressed and the dehydrogenation reaction becomes dominant. The conversion rate from benzene to methylcyclohexane decreases. Therefore, it is better to maintain the temperature of the hydrogenation catalyst in the range of 70 to 250 ° C. A more preferred temperature is in the range of 80-200 ° C.
• the configuration of the hydrogenation reactor 40 has many common parts with the configuration of the hydrogen generator 1 described above, and is therefore denoted by the same reference numerals and description thereof is omitted.
• the main differences from the hydrogen generator 1 are that toluene is mixed with hydrogen before entering the reactor 10, and what is discharged from the reaction product container 35. It is a point that contains surplus hydrogen with enough power to react.
• the place where toluene and hydrogen are mixed is between the heat exchanger 30 and the heat exchanger 31, but is upstream from the heat exchanger 30 or downstream from the heat exchanger 31. May be.
• a triple-pipe reactor 10 having an inner region 12 and an outer region 11 that has a hydrogenation catalyst necessary for the hydrogenation reaction outside the inner region 12 and a wall is employed.
• the generated heat is immediately removed, the efficiency of the reaction increases, and the hydrogenation reaction rate can be increased.
• the cooling air (or cooling water) and the hydrogenation catalyst are in contact with the fins 17 and 18 in the reactor 10, the heat of the hydrogenation catalyst is immediately heated through the walls of the fins 17 and 18. Removed. Therefore, the hydrogenation reaction rate and the conversion rate can be further increased.
• the cooling area and the area per unit volume carrying the catalyst increase, and the reaction efficiency is further improved. Can be increased.
• the catalyst carrier made of acid aluminum is a catalyst carrier having high heat resistance. Furthermore, since the fins 17 and 18 are made of aluminum having good thermal conductivity, the heat transfer rate between the inner region 12 and the outer region 11 can be increased.
• the catalyst carrier may be a member made of a material such as zirconium oxide or silicon nitride in addition to aluminum oxide.
• the catalyst supported on the catalyst support may be palladium, ruthenium, iridium, rhenium, nickel, molybdenum, tungsten. Ten, niteum, vanadium, osmium, chromium, cobalt, iron, or any combination of these yarns!
• the reactor 10 has a triple tube structure! /, But may have a double tube structure or a multiple tube structure of four or more layers.
• a region where a dehydrogenation reaction or a hydrogenation reaction occurs may be an inner region, and a region adjacent to the inner region with a wall may be an outer region.
• a structure in which a large number of the reactors are combined in parallel may be used.
• the present invention is applicable to industries that use or store hydrogen.

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