US20050013754A1 - Apparatus for producing hydrogen - Google Patents

Apparatus for producing hydrogen Download PDF

Info

Publication number
US20050013754A1
US20050013754A1 US10/914,101 US91410104A US2005013754A1 US 20050013754 A1 US20050013754 A1 US 20050013754A1 US 91410104 A US91410104 A US 91410104A US 2005013754 A1 US2005013754 A1 US 2005013754A1
Authority
US
United States
Prior art keywords
hydrogen
cooling
high purity
catalyst
reformer
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US10/914,101
Inventor
Kazuto Kobayashi
Yoshimasa Fujimoto
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mitsubishi Heavy Industries Ltd
Original Assignee
Mitsubishi Heavy Industries Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Mitsubishi Heavy Industries Ltd filed Critical Mitsubishi Heavy Industries Ltd
Priority to US10/914,101 priority Critical patent/US20050013754A1/en
Publication of US20050013754A1 publication Critical patent/US20050013754A1/en
Abandoned legal-status Critical Current

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
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
    • 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
    • C01B3/0005—Reversible uptake of hydrogen by an appropriate medium, i.e. based on physical or chemical sorption phenomena or on reversible chemical reactions, e.g. for hydrogen storage purposes ; Reversible gettering of hydrogen; Reversible uptake of hydrogen by electrodes
    • 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
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
    • 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
    • C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
    • 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
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0405—Purification by membrane separation
    • C01B2203/041—In-situ membrane purification during hydrogen production
    • 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
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • 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
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • 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
    • C01B2203/0816—Heating by flames
    • 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
    • C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
    • C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
    • 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
    • C01B2203/0866—Methods of heating the process for making hydrogen or synthesis gas by combination of different heating methods
    • 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
    • C01B2203/0872—Methods of cooling
    • C01B2203/0883—Methods of cooling by indirect heat exchange
    • 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
    • C01B2203/1011—Packed bed of catalytic structures, e.g. particles, packing elements
    • 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
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1052—Nickel or cobalt catalysts
    • 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
    • C01B2203/1217—Alcohols
    • C01B2203/1223—Methanol
    • 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
    • C01B2203/1241—Natural gas or methane
    • 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
    • C01B2203/16—Controlling the process
    • C01B2203/1628—Controlling the pressure
    • C01B2203/1633—Measuring the pressure
    • 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
    • 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
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry

Definitions

  • the present invention relates to an apparatus for producing hydrogen by a steam reforming reaction using a hydrocarbon or an oxygen-containing hydrocarbon as a raw material.
  • a conventional apparatus for producing hydrogen with the use of a hydrogen separation type reformer is proposed, for example, in Japanese Unexamined Patent Publication No. 4-325402. Disclosed in this proposal is an apparatus for producing hydrogen for a fuel cell with the use of a hydrogen separation type reformer from which hydrogen is withdrawn by a pressure reducing means. The concept of constitution of this apparatus is illustrated in FIG. 9 .
  • a hydrogen separation membrane 02 and a catalyst 08 are provided in a hydrogen separation type reformer 01 .
  • a gas as a raw material (hereinafter referred to as a raw material gas) 06 and steam 07 are fed to the hydrogen separation type reformer 01 , where a reforming reaction takes place. Hydrogen formed by the reforming reaction is separated by the separation membrane 02 .
  • a pressure reducing device 04 is provided to recover high purity hydrogen 05 .
  • the raw material gas 06 comprising a hydrocarbon or an oxygen-containing hydrocarbon such as methane or methanol is introduced, and reformed on the catalyst 08 by a steam reforming reaction and a CO shift reaction to form hydrogen and carbon dioxide mainly.
  • the hydrogen is selectively separated, for recovery, by the hydrogen separation membrane 02 built into the catalyst 08 .
  • the hydrogen separation membrane 02 a non-porous thin film with a thickness as small as about several to 50 ⁇ m, which comprises a hydrogen-permeable metal film of Pd or Pd alloy, is used, as shown in Japanese Unexamined Patent Publication No. 6-321503.
  • a catalyst containing a group VIII metal Fe, Co, Ni, Ru, Rh, Pd or Pt
  • a catalyst bearing Ni, Ru or Rh or an NiO-containing catalyst is particularly preferred.
  • FIG. 7 A perspective sectional view of the structure of a typical hydrogen separation type reformer is shown in FIG. 7 , and a cross sectional view of the structure is shown in FIG. 8 .
  • a hydrogen separation type reformer 10 has an outer tube 14 with a closed bottom 12 , and an intermediate tube 16 and an inner tube 18 disposed in this order inwardly of the outer tube 14 .
  • the outer tube 14 , the intermediate tube 16 , and the inner tube 18 are each in the form of an upright cylinder.
  • a preliminary reforming portion 25 is provided at an upper part of a second annular space portion 26 between the intermediate tube 16 and the inner tube 18 .
  • a preliminary reforming portion 25 is provided at an upper part of a second annular space portion 26 between the intermediate tube 16 and the inner tube 18 .
  • a preliminary reforming portion 25 is provided below the preliminary reforming portion 25 .
  • a plurality of hydrogen permeable cylindrical tubes 34 having a metal film selectively permeable to hydrogen are disposed concentrically with the second annular space
  • a burner 46 burns a fuel gas, which has been introduced through a fuel gas pipe 48 , with air taken in through an air intake pipe 50 to supply thermal energy necessary for a steam reforming reaction to the second annular space portion 26 filled with are forming catalyst A, thereby keeping the catalyst at a predetermined temperature.
  • the fuel gas passes through an inner tube hollow portion 22 , a space between the bottom 12 of the outer tube 14 and an annular bottom portion 24 , and a first annular space portion 20 , and goes outside through a combustion gas outlet 52 . During this motion, the fuel gas heats a layer of the catalyst filled into the second annular space portion 26 .
  • a process feed gas comprising a gas mixture of steam and a raw material gas composed of a hydrocarbon or an oxygen-containing hydrocarbon, such as methane or methanol, is introduced through a feed gas inlet 54 provided at an upper part of the second annular space portion 26 .
  • the process feed gas is partially converted into hydrogen at the preliminary reforming portion 25 , and flowed into the layer of the catalyst filled into the second annular space portion 26 , whereby the process feed gas is converted into hydrogen at a high temperature.
  • the resulting hydrogen is selectively separated and collected by the hydrogen permeable cylindrical tubes 34 , passed through a third space portion 33 , and flowed out through a hydrogen outlet 56 provided above the third space portion 33 .
  • the resulting hydrogen is withdrawn from the hydrogen separation type reformer 10 by a pressure reducing device.
  • a hydrogen separation membrane gives a necessary amount of hydrogen with high efficiency, accordingly, with a small membrane area, if the pressure of the hydrogen permeation side is minimized.
  • a vacuum pump or the like is conceivable as a pressure reducing device.
  • such a rotary device has difficulty in efficiently delivering a light gas, such as hydrogen, thus requiring a high power.
  • the aforementioned Japanese Unexamined Patent Publication No. 4-325402 does not propose a concrete apparatus layout including a pressure reducing device, and cannot actualize a feasible apparatus.
  • the present invention has been accomplished in light of these circumstances. It is an object of this invention to actualize such a concrete and feasible apparatus layout involving a pressure reducing device and provide an apparatus for producing hydrogen with the use a hydrogen separation type reformer, the apparatus having a minimal area required, and having improved durability while using a pressure reducing device.
  • a first aspect of the present invention as a means of attaining the above object, is an apparatus for producing hydrogen by a steam reforming reaction, on a catalyst, of a hydrocarbon or an oxygen-containing hydrocarbon as a raw material, the apparatus comprising a hydrogen separation type reformer which has a means for heating the catalyst and which has a hydrogen separation membrane built into a layer of the catalyst for selectively separating hydrogen, a cooling means for cooling high temperature high purity hydrogen obtained from the reformer, and a hydrogen storage/delivery means disposed downstream from the cooling means and composed of a hydrogen occluding material.
  • the high temperature high purity hydrogen that has been separated from the reformer is once cooled by the cooler, the indirect heat exchanger, to a temperature at which hydrogen is easily occluded in the hydrogen occluding material. Then, the cooled hydrogen is fed to the hydrogen occluding material.
  • the hydrogen occlusion rate and the amount of hydrogen occlusion are increased, and hydrogen can be withdrawn from the reformer at a lower pressure than the atmospheric pressure.
  • the membrane area of the hydrogen separation membrane can be decreased.
  • a required power can be decreased markedly in comparison with the power required for the use of a vacuum pump.
  • the temperature of the hydrogen occluding material is set at an appropriate level, whereby high pressure hydrogen can be obtained.
  • a hydrogen compression power necessary when a compressor is used can be cut down markedly.
  • a second aspect of the invention is the apparatus for producing hydrogen as the first aspect of the invention, wherein the cooling means for cooling the high temperature high purity hydrogen comprises an indirect heat exchanger.
  • the sensible heat of the high temperature high purity hydrogen can be utilized for heating of the raw material gas and steam.
  • the energy efficiency of the apparatus can be increased.
  • a third aspect of the invention is the apparatus for producing hydrogen as the first or second aspect of the invention, wherein a fluid for cooling the high temperature high purity hydrogen via the indirect heat exchanger is one or both of a raw material gas and combustion air to be fed to the hydrogen separation type reformer.
  • a raw material gas a mixture of a hydrocarbon or an oxygen-containing hydrocarbon can be named.
  • the third aspect of the invention it becomes unnecessary to use cooling water, separately, for heat exchange. Also, preheating increases the reforming efficiency, and can improve the thermal efficiency of the entire apparatus.
  • a fourth aspect of the invention is the apparatus for producing hydrogen as any one of the first to third aspects of the invention, wherein a fluid for cooling the high temperature high purity hydrogen via the indirect heat exchanger is one or both of air or cooling water.
  • the sensible heat of the high temperature high purity hydrogen can be recovered and utilized.
  • a fifth aspect of the invention is the apparatus for producing hydrogen as any one of the first to fourth aspects of the invention, wherein the hydrogen storage/delivery means composed of the hydrogen occluding material comprises at least two members of a hydrogen storing alloy incorporating a heating/cooling means.
  • efficient occlusion of hydrogen can be performed.
  • a sixth aspect of the invention is the apparatus for producing hydrogen as the fifth aspect of the invention, wherein a fluid for cooling the high temperature high purity hydrogen via the indirect heat exchanger is cooling water, and hot water heated by heat exchange performed by the heat exchanger is used for heating of a hydrogen delivery means in the hydrogen storage/delivery means composed of the hydrogen occluding material.
  • cooling water used to cool high temperature high purity hydrogen is utilized for heating the hydrogen occluding material.
  • effective use of heat can be achieved.
  • a seventh aspect of the invention is the apparatus for producing hydrogen as any one of the first to sixth aspects of the invention, wherein a pressure regulating means is interposed between the cooling means for cooling the high temperature high purity hydrogen and the hydrogen storage/delivery means disposed downstream from the cooling means and composed of the hydrogen occluding material, to regulate the pressure of the high purity hydrogen to be fed to the hydrogen storage/delivery means.
  • the pressure regulator is installed between the hydrogen occluding material and the cooling means. This prevents a rapid decrease in pressure on the hydrogen permeation side of the hydrogen separation membrane, thus improving the durability of the hydrogen separation membrane. Moreover, a rapid rise in the temperature of the hydrogen occluding material associated with its hydrogen occlusion can also be prevented. Thermal shock to the hydrogen occluding material can be lessened. Furthermore, changes over time in the amount of hydrogen production from the apparatus for producing hydrogen can be minimized and leveled off.
  • FIG. 1 is a schematic view of a first embodiment of the present invention
  • FIG. 2 is a schematic view of a second embodiment of the invention.
  • FIG. 3 is a schematic view of a third embodiment of the invention.
  • FIG. 4 is a schematic view of a fourth embodiment of the invention.
  • FIG. 5 is a schematic view of a fifth embodiment of the invention.
  • FIG. 6 is a graph of changes in the pressure of low temperature high purity hydrogen during hydrogen occlusion
  • FIG. 7 is a perspective sectional view of an apparatus for producing hydrogen
  • FIG. 8 is a schematic cross sectional view of the apparatus for producing hydrogen shown in FIG. 7 ;
  • FIG. 9 is a schematic view of a conventional apparatus for producing hydrogen.
  • FIG. 1 is a schematic view of an apparatus layout for implementing the present invention.
  • an apparatus for producing hydrogen according to the present embodiment is an apparatus for producing hydrogen by a steam reforming reaction, on a catalyst, of a hydrocarbon or an oxygen-containing hydrocarbon as a raw material, the apparatus comprising a hydrogen separation type reformer 100 which has a means for heating the catalyst and which has a hydrogen separation membrane built into a layer of the catalyst for selectively separating hydrogen, a cooler 106 for cooling high temperature high purity hydrogen obtained from the reformer 100 , and a hydrogen storage/delivery means 108 disposed downstream from the cooler 106 and composed of a hydrogen occluding material.
  • a hydrogen separation type reformer 100 which has a means for heating the catalyst and which has a hydrogen separation membrane built into a layer of the catalyst for selectively separating hydrogen
  • a cooler 106 for cooling high temperature high purity hydrogen obtained from the reformer 100
  • a hydrogen storage/delivery means 108 disposed downstream from the cooler 106 and composed of a hydrogen o
  • the hydrogen separation type reformer (hereinafter referred to as “reformer”) 100 may be, but not restricted to, one having a structure as shown in FIGS. 7 and 8 .
  • the same reference numerals as used in the apparatus shown in FIGS. 7 and 8 will be used, and overlapping explanations of the constitution of the apparatus will be omitted.
  • the reformer 100 is supplied with a raw material gas 101 , which comprises a hydrocarbon or an oxygen-containing hydrocarbon such as methane or methanol, and steam 102 . These materials are reformed mainly by a steam reforming reaction to form a mixed gas mainly composed of hydrogen, carbon monoxide and carbon dioxide. Hydrogen in this gas is selectively separated, and withdrawn from the reformer 100 as high temperature (400 to 550° C.) high purity hydrogen 103 . The residual gas after separation of hydrogen is taken out of the reformer 100 as an off-gas 104 .
  • the off-gas 104 is fed to a combustion side of the reformer 100 , mixed with combustion air 105 in a burner of the reformer 100 (the burner 46 of the reformer shown in FIG. 7 ), and then subjected to combustion.
  • the off-gas 104 may be mixed with a portion 101 a of the raw material gas 101 supplied, and then may be used as fuel.
  • the high temperature high purity hydrogen 103 separated from the reformer 100 is cooled by the cooler 106 to become low temperature (30 to 200° C.) high purity hydrogen 107 .
  • This hydrogen 107 is stored in the hydrogen storage/delivery means 108 composed of a hydrogen occluding material, and delivered from the hydrogen storage/delivery means 108 as high pressure hydrogen (2 atm or higher) 109 .
  • the low temperature high purity hydrogen 107 contains trace amounts of impurities such as carbon dioxide and carbon monoxide. Therefore, the low temperature high purity hydrogen 107 during storage or delivery is intermittently sent to the reformer 100 as purge hydrogen 110 a for use as part of fuel. When the low temperature high purity hydrogen 107 is not sent to the reformer 100 , it is discharged out of the system as low purity hydrogen 110 b.
  • a gas mixture 111 of the raw material gas 101 and steam 102 is heat exchanged with the high temperature high purity hydrogen 103 indirectly, and thereby preheated.
  • the preheated gas mixture 111 is supplied to the reformer 100 .
  • the hydrogen occluding material of the hydrogen storage/delivery means 108 for carrying out the invention may be any material, without being restricted to the one disclosed in the embodiment, as long as it selectively occludes hydrogen from the mixed gas containing hydrogen, and releases the occluded hydrogen upon heating.
  • a hydrogen storing alloy is known. Its examples are rare earth metal-Ni alloys such as LaNi 5 , misch metal alloys, titanium-zirconium alloys such as TiFe, Mg alloys such as Mg 2 Ni, V alloys, and calcium alloys such as CaNi 5 .
  • the hydrogen occluding material is not restricted to these alloys. Occluding materials which occlude hydrogen, such as those composed of a carbon nanotube, are also usable.
  • an ordinary shell & tube type heat exchanger or an ordinary plate type heat exchanger can be used as the indirect type heat exchanger for the cooler 106 .
  • Any type of heat exchanger, which can perform cooling without direct contact with the high temperature high purity hydrogen 103 can be used without its embodiment being restricted.
  • the high temperature (400 to 550° C.) high purity hydrogen 103 that has been separated from the reformer 100 is once cooled by the cooler 106 , the indirect heat exchanger, to a temperature of about 30 to 200° C. at which hydrogen is easily occluded in the hydrogen occluding material. Then, the cooled hydrogen is fed to the hydrogen storage/delivery means 108 , the hydrogen occluding material.
  • the hydrogen occlusion rate and the amount of hydrogen occlusion can be increased.
  • hydrogen can be withdrawn from the reformer 100 at a lower pressure than the atmospheric pressure.
  • the membrane area of the hydrogen separation membrane of the reformer 100 can be decreased.
  • a required power for the withdrawal of hydrogen can be decreased markedly in comparison with the power required when a vacuum pump is used.
  • the temperature of the hydrogen storage/delivery means 108 , the hydrogen occluding material is set at an appropriate level (e.g., about 80° C.), whereby hydrogen released at a high-pressure can be obtained.
  • an appropriate level e.g., about 80° C.
  • the sensible heat of the high temperature high purity hydrogen 103 reformed by the reformer 100 can be utilized for heating of the raw material gas and steam in the cooler 106 .
  • the energy efficiency of the entire apparatus can be increased.
  • FIG. 2 is a schematic view of an apparatus layout for a second embodiment of the present invention.
  • the gas mixture 111 of the raw material gas 101 and steam 102 is fed to the cooler 106 for heat exchange, in order to utilize the sensible heat of the high temperature high purity hydrogen 103 .
  • combustion air 105 is supplied as shown in FIG. 2 .
  • an indirect type heat exchanger for example, can be used.
  • heat exchange between the combustion air 105 and high temperature high purity hydrogen 103 takes place to cool the hydrogen, making it low temperature high purity hydrogen 107 .
  • Heated combustion air 105 a after heating by heat exchange is fed to a burner of a reformer 100 (the burner 46 of the reformer illustrated in FIG. 7 ).
  • the combustion air 105 is indirectly heat exchanged with the high temperature high purity hydrogen 103 , and thereby preheated.
  • the preheated combustion air is fed to the reformer 100 , whereby the energy efficiency of the entire apparatus can be increased.
  • FIG. 3 shows a third embodiment of the invention.
  • air or cooling water is fed to a cooler 106 as a low temperature fluid 120 a , which is heat exchanged with high temperature high purity hydrogen 103 to obtain low temperature high purity hydrogen 107 .
  • a low temperature fluid 120 b after heat exchange is discharged out of the system, and utilized as other heat source.
  • FIG. 4 shows a fourth embodiment of the invention.
  • a hydrogen storage/delivery means is composed of two members, a hydrogen occluding material 108 A and a hydrogen occluding material 108 B.
  • the hydrogen occluding material 108 A is defined as a hydrogen occlusion side
  • a hydrogen occluding material 108 B is defined as a hydrogen delivery side.
  • low temperature high purity hydrogen 107 is flowed, and cooling water 121 a is supplied to cool the entire hydrogen occluding material 108 A.
  • cooling water 121 a is supplied to cool the entire hydrogen occluding material 108 A.
  • low purity hydrogen 110 b is intermittently discharged, or sent to a reformer 100 as purge hydrogen 110 a.
  • the low temperature hydrogen 107 is not flowed.
  • separately fed high temperature water (50 to 100° C.) 122 a heats the entire alloy to release hydrogen stored in the hydrogen storing alloy, and the hydrogen is delivered out of the system as high pressure hydrogen 109 .
  • the supply of the low temperature high purity hydrogen 107 and the supply of the cooling water 121 a are stopped. Instead, high temperature water 122 b is flowed to liberate high-pressure hydrogen 109 .
  • high-pressure hydrogen 109 is delivered.
  • low purity hydrogen 110 c present in the hydrogen occluding material 108 B on the hydrogen delivery side can be discharged intermittently.
  • the waste heat of the cooling water 123 used for cooling of the high temperature high purity hydrogen 103 is utilized for heating of the hydrogen occluding material 108 B on the hydrogen delivery side, whereby effective use of heat can be achieved.
  • FIG. 5 shows a fifth embodiment of the invention.
  • a pressure regulator 130 for low temperature high purity hydrogen 107 is installed between a cooler 106 and a hydrogen storage/delivery means 108 .
  • the pressure regulator 130 an ordinary valve can be used, and a valve involving a decreased loss in pressure is preferred.
  • High purity hydrogen 131 after pressure regulation is fed to the hydrogen storage/delivery means 108 .
  • the pressure regulator 130 is installed between the hydrogen storage/delivery means 108 and the cooler 106 .
  • a buffer zone is formed for preventing a rapid pressure drop on the hydrogen permeation side of a hydrogen separation membrane inside are former 100 . Consequently, the durability of the hydrogen separation membrane can be improved.
  • a rapid rise in the temperature of the hydrogen storage/delivery means 108 associated with its hydrogen occlusion can also be prevented.
  • Thermal shock to the hydrogen storage/delivery means 108 can be cushioned.
  • changes over time in the amount of hydrogen production from the apparatus for producing hydrogen can be minimized and leveled off. After all, well balanced hydrogen production can be performed.
  • a hydrogen separation type reformer 100 had the structure shown in FIGS. 7 and 8 , as with the preceding Embodiments.
  • a heat exchanger, a cooler 106 was of a plate fin type, and used cooling water as a low temperature fluid 120 a to cool high temperature high purity hydrogen 103 .
  • a hydrogen occluding material of a hydrogen storage/delivery means 108 was composed of two members of a hydrogen storing alloy of LaNi 5 .
  • Hydrogen was produced under the following concrete conditions in accordance with the flow shown in FIG. 3 .
  • the catalyst of the reformer 100 was an NiO catalyst in particle form, and the hydrogen separation membrane was made of a Pd alloy.
  • the membrane area was 0.68 cm 2 .
  • the reaction temperature of the reformer was 550° C., and the reaction pressure was 6 atm. Methane was used as the raw material gas.
  • the reformer was run, with the flow rate of the raw material gas being 1.5 m 3 N/h and the steam-carbon ratio being 3.
  • the heat exchanger, the cooler 106 was of a plate fin type, and used cooling water as a cooling medium.
  • the inlet temperature of cooling water was 25° C.
  • the outlet temperature of cooling water was 80° C.
  • the inlet temperature of the high temperature high purity hydrogen 103 fed to the cooler 106 was 450° C.
  • the outlet temperature of low temperature high purity hydrogen 107 after heat exchange was 40° C.
  • the hydrogen occluding material, the hydrogen storage/delivery means 108 was composed of two members of an LaNi 5 alloy.
  • the inlet temperature of cooling water during occlusion by the hydrogen storing alloy was 30° C., while the inlet temperature of cooling water during release of hydrogen was 80° C.
  • the occluding capacity of the hydrogen storing alloy was 4 m 3 N/member.
  • the amount of hydrogen production through the use of the hydrogen storing alloy as in the present Example was 3.0 m 3 N/h. Whereas the amount of hydrogen production without the use of the hydrogen storing alloy in the present Example was about a half, i.e., 1.5 m 3 N/h.
  • the power required for supply of 3.0 m 3 N/h of hydrogen at 6 atm by the hydrogen storing alloy was about 0.05 kW.
  • the power required for compression of 3.0 m 3 N/h of hydrogen from 1 atm to 6 atm by a compressor was about 0.9 kW.
  • Example 2 The same constitution and operating conditions as in Example 1 were adopted, except that the outlet temperature of low temperature high purity hydrogen 107 in the cooler 106 was 80° C.
  • Example 1 The same constitution and operating conditions as in Example 1 were adopted.
  • a third example of the invention will be explained based on the apparatus layout shown in FIG. 5 .
  • a hydrogen separation type reformer 100 , a cooler 106 , and a hydrogen storage/delivery means 108 had the same constitutions as in Example 1.
  • a pressure regulator 130 comprises a pressure regulating valve, and mitigates a rapid pressure fall at the start of hydrogen occlusion by the hydrogen storage/delivery means 108 .
  • the pressure regulator 130 curbs a rapid pressure change of low temperature high purity hydrogen 107 flowing out of the cooler 106 .
  • the constitutions and operating conditions of the hydrogen separation type reformer 100 , cooler 106 , and hydrogen storage/delivery means 108 were the same as in Example 1.
  • FIG. 6 shows changes in the pressure of low temperature high purity hydrogen during hydrogen occlusion. Regulation of the pressure results in the mitigation of a rapid pressure drop occurring at the start of occlusion.
  • the amount of hydrogen production was 3.5 m 3 N/h when the pressure regulator 130 was installed. Whereas the amount of hydrogen production was 3.0 m 3 N/h when the pressure regulator was not used.

Abstract

An apparatus for producing hydrogen by a steam reforming reaction, on a catalyst, of a hydrocarbon or an oxygen-containing hydrocarbon as a raw material is disclosed. The apparatus comprises a hydrogen separation type reformer which has a means for heating the catalyst and which has a hydrogen separation membrane built into a layer of the catalyst for selectively separating hydrogen; a cooling means for cooling high temperature high purity hydrogen obtained from the reformer; and a hydrogen storage/delivery means disposed downstream from the cooling means and composed of a hydrogen occluding material.

Description

    BACKGROUND OF THE INVENTION
  • 1. Field of the Invention
  • The present invention relates to an apparatus for producing hydrogen by a steam reforming reaction using a hydrocarbon or an oxygen-containing hydrocarbon as a raw material.
  • 2. Description of the Related Art
  • A conventional apparatus for producing hydrogen with the use of a hydrogen separation type reformer is proposed, for example, in Japanese Unexamined Patent Publication No. 4-325402. Disclosed in this proposal is an apparatus for producing hydrogen for a fuel cell with the use of a hydrogen separation type reformer from which hydrogen is withdrawn by a pressure reducing means. The concept of constitution of this apparatus is illustrated in FIG. 9.
  • As shown in FIG. 9, a hydrogen separation membrane 02 and a catalyst 08 are provided in a hydrogen separation type reformer 01. A gas as a raw material (hereinafter referred to as a raw material gas) 06 and steam 07 are fed to the hydrogen separation type reformer 01, where a reforming reaction takes place. Hydrogen formed by the reforming reaction is separated by the separation membrane 02. On a hydrogen permeation side 03 where the separated hydrogen permeates, a pressure reducing device 04 is provided to recover high purity hydrogen 05.
  • With the hydrogen separation type reformer 01, the raw material gas 06 comprising a hydrocarbon or an oxygen-containing hydrocarbon such as methane or methanol is introduced, and reformed on the catalyst 08 by a steam reforming reaction and a CO shift reaction to form hydrogen and carbon dioxide mainly. The hydrogen is selectively separated, for recovery, by the hydrogen separation membrane 02 built into the catalyst 08. As the hydrogen separation membrane 02, a non-porous thin film with a thickness as small as about several to 50 μm, which comprises a hydrogen-permeable metal film of Pd or Pd alloy, is used, as shown in Japanese Unexamined Patent Publication No. 6-321503. As the catalyst 08, a catalyst containing a group VIII metal (Fe, Co, Ni, Ru, Rh, Pd or Pt) is preferred, and a catalyst bearing Ni, Ru or Rh or an NiO-containing catalyst is particularly preferred.
  • A perspective sectional view of the structure of a typical hydrogen separation type reformer is shown in FIG. 7, and a cross sectional view of the structure is shown in FIG. 8. As shown in these drawings, a hydrogen separation type reformer 10 has an outer tube 14 with a closed bottom 12, and an intermediate tube 16 and an inner tube 18 disposed in this order inwardly of the outer tube 14. The outer tube 14, the intermediate tube 16, and the inner tube 18 are each in the form of an upright cylinder. At an upper part of a second annular space portion 26 between the intermediate tube 16 and the inner tube 18, a preliminary reforming portion 25 is provided. Below the preliminary reforming portion 25, a plurality of hydrogen permeable cylindrical tubes 34 having a metal film selectively permeable to hydrogen are disposed concentrically with the second annular space portion 26.
  • A burner 46 burns a fuel gas, which has been introduced through a fuel gas pipe 48, with air taken in through an air intake pipe 50 to supply thermal energy necessary for a steam reforming reaction to the second annular space portion 26 filled with are forming catalyst A, thereby keeping the catalyst at a predetermined temperature. The fuel gas passes through an inner tube hollow portion 22, a space between the bottom 12 of the outer tube 14 and an annular bottom portion 24, and a first annular space portion 20, and goes outside through a combustion gas outlet 52. During this motion, the fuel gas heats a layer of the catalyst filled into the second annular space portion 26.
  • A process feed gas comprising a gas mixture of steam and a raw material gas composed of a hydrocarbon or an oxygen-containing hydrocarbon, such as methane or methanol, is introduced through a feed gas inlet 54 provided at an upper part of the second annular space portion 26. The process feed gas is partially converted into hydrogen at the preliminary reforming portion 25, and flowed into the layer of the catalyst filled into the second annular space portion 26, whereby the process feed gas is converted into hydrogen at a high temperature. The resulting hydrogen is selectively separated and collected by the hydrogen permeable cylindrical tubes 34, passed through a third space portion 33, and flowed out through a hydrogen outlet 56 provided above the third space portion 33. The unreacted raw material gas and the resulting CO and CO2 gases, which have passed through the catalyst layer, flow through an off-gas pipe 60 having an opening at a lower part of the second annular space portion 26, and flow out of the system through an off-gas outlet 62.
  • With the foregoing conventional apparatus, the resulting hydrogen is withdrawn from the hydrogen separation type reformer 10 by a pressure reducing device. As is well known, a hydrogen separation membrane gives a necessary amount of hydrogen with high efficiency, accordingly, with a small membrane area, if the pressure of the hydrogen permeation side is minimized. Thus, a highly efficient pressure reducing device has been demanded. A vacuum pump or the like is conceivable as a pressure reducing device. However, such a rotary device has difficulty in efficiently delivering a light gas, such as hydrogen, thus requiring a high power. Furthermore, the aforementioned Japanese Unexamined Patent Publication No. 4-325402 does not propose a concrete apparatus layout including a pressure reducing device, and cannot actualize a feasible apparatus.
    • SUMMARY OF THE INVENTION
  • The present invention has been accomplished in light of these circumstances. It is an object of this invention to actualize such a concrete and feasible apparatus layout involving a pressure reducing device and provide an apparatus for producing hydrogen with the use a hydrogen separation type reformer, the apparatus having a minimal area required, and having improved durability while using a pressure reducing device.
  • A first aspect of the present invention, as a means of attaining the above object, is an apparatus for producing hydrogen by a steam reforming reaction, on a catalyst, of a hydrocarbon or an oxygen-containing hydrocarbon as a raw material, the apparatus comprising a hydrogen separation type reformer which has a means for heating the catalyst and which has a hydrogen separation membrane built into a layer of the catalyst for selectively separating hydrogen, a cooling means for cooling high temperature high purity hydrogen obtained from the reformer, and a hydrogen storage/delivery means disposed downstream from the cooling means and composed of a hydrogen occluding material.
  • According to the first aspect of the invention, the following actions and effects are exhibited:
  • The high temperature high purity hydrogen that has been separated from the reformer is once cooled by the cooler, the indirect heat exchanger, to a temperature at which hydrogen is easily occluded in the hydrogen occluding material. Then, the cooled hydrogen is fed to the hydrogen occluding material. As a result, the hydrogen occlusion rate and the amount of hydrogen occlusion are increased, and hydrogen can be withdrawn from the reformer at a lower pressure than the atmospheric pressure. Thus, the membrane area of the hydrogen separation membrane can be decreased. Moreover, a required power can be decreased markedly in comparison with the power required for the use of a vacuum pump.
  • When hydrogen stored in the hydrogen occluding material is to be delivered, the temperature of the hydrogen occluding material is set at an appropriate level, whereby high pressure hydrogen can be obtained. Thus, a hydrogen compression power necessary when a compressor is used can be cut down markedly.
  • A second aspect of the invention is the apparatus for producing hydrogen as the first aspect of the invention, wherein the cooling means for cooling the high temperature high purity hydrogen comprises an indirect heat exchanger.
  • According to the second aspect of the invention, the sensible heat of the high temperature high purity hydrogen can be utilized for heating of the raw material gas and steam. Thus, the energy efficiency of the apparatus can be increased.
  • A third aspect of the invention is the apparatus for producing hydrogen as the first or second aspect of the invention, wherein a fluid for cooling the high temperature high purity hydrogen via the indirect heat exchanger is one or both of a raw material gas and combustion air to be fed to the hydrogen separation type reformer. As the raw material gas, a mixture of a hydrocarbon or an oxygen-containing hydrocarbon can be named.
  • According to the third aspect of the invention, it becomes unnecessary to use cooling water, separately, for heat exchange. Also, preheating increases the reforming efficiency, and can improve the thermal efficiency of the entire apparatus.
  • A fourth aspect of the invention is the apparatus for producing hydrogen as any one of the first to third aspects of the invention, wherein a fluid for cooling the high temperature high purity hydrogen via the indirect heat exchanger is one or both of air or cooling water.
  • According to the fourth aspect of the invention, the sensible heat of the high temperature high purity hydrogen can be recovered and utilized.
  • A fifth aspect of the invention is the apparatus for producing hydrogen as any one of the first to fourth aspects of the invention, wherein the hydrogen storage/delivery means composed of the hydrogen occluding material comprises at least two members of a hydrogen storing alloy incorporating a heating/cooling means.
  • According to the fifth aspect of the invention, efficient occlusion of hydrogen can be performed.
  • A sixth aspect of the invention is the apparatus for producing hydrogen as the fifth aspect of the invention, wherein a fluid for cooling the high temperature high purity hydrogen via the indirect heat exchanger is cooling water, and hot water heated by heat exchange performed by the heat exchanger is used for heating of a hydrogen delivery means in the hydrogen storage/delivery means composed of the hydrogen occluding material.
  • According to the sixth aspect of the invention, cooling water used to cool high temperature high purity hydrogen is utilized for heating the hydrogen occluding material. Thus, effective use of heat can be achieved.
  • A seventh aspect of the invention is the apparatus for producing hydrogen as any one of the first to sixth aspects of the invention, wherein a pressure regulating means is interposed between the cooling means for cooling the high temperature high purity hydrogen and the hydrogen storage/delivery means disposed downstream from the cooling means and composed of the hydrogen occluding material, to regulate the pressure of the high purity hydrogen to be fed to the hydrogen storage/delivery means.
  • According to the seventh aspect of the invention, the pressure regulator is installed between the hydrogen occluding material and the cooling means. This prevents a rapid decrease in pressure on the hydrogen permeation side of the hydrogen separation membrane, thus improving the durability of the hydrogen separation membrane. Moreover, a rapid rise in the temperature of the hydrogen occluding material associated with its hydrogen occlusion can also be prevented. Thermal shock to the hydrogen occluding material can be lessened. Furthermore, changes over time in the amount of hydrogen production from the apparatus for producing hydrogen can be minimized and leveled off.
    • BRIEF DESCRIPTION OF THE DRAWINGS
  • The above and other objects, features and advantages of the present invention will become more apparent from the following description taken in connection with the accompanying drawings, in which:
  • FIG. 1 is a schematic view of a first embodiment of the present invention;
  • FIG. 2 is a schematic view of a second embodiment of the invention;
  • FIG. 3 is a schematic view of a third embodiment of the invention;
  • FIG. 4 is a schematic view of a fourth embodiment of the invention;
  • FIG. 5 is a schematic view of a fifth embodiment of the invention;
  • FIG. 6 is a graph of changes in the pressure of low temperature high purity hydrogen during hydrogen occlusion;
  • FIG. 7 is a perspective sectional view of an apparatus for producing hydrogen;
  • FIG. 8 is a schematic cross sectional view of the apparatus for producing hydrogen shown in FIG. 7; and
  • FIG. 9 is a schematic view of a conventional apparatus for producing hydrogen.
    • DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
  • Embodiments of the present invention will now be described in detail with reference to the accompanying drawings, which in no way limit the invention.
  • [First Embodiment]
  • FIG. 1 is a schematic view of an apparatus layout for implementing the present invention. As shown in FIG. 1, an apparatus for producing hydrogen according to the present embodiment is an apparatus for producing hydrogen by a steam reforming reaction, on a catalyst, of a hydrocarbon or an oxygen-containing hydrocarbon as a raw material, the apparatus comprising a hydrogen separation type reformer 100 which has a means for heating the catalyst and which has a hydrogen separation membrane built into a layer of the catalyst for selectively separating hydrogen, a cooler 106 for cooling high temperature high purity hydrogen obtained from the reformer 100, and a hydrogen storage/delivery means 108 disposed downstream from the cooler 106 and composed of a hydrogen occluding material.
  • The hydrogen separation type reformer (hereinafter referred to as “reformer”) 100 may be, but not restricted to, one having a structure as shown in FIGS. 7 and 8. In the following description, the same reference numerals as used in the apparatus shown in FIGS. 7 and 8 will be used, and overlapping explanations of the constitution of the apparatus will be omitted.
  • The reformer 100 is supplied with a raw material gas 101, which comprises a hydrocarbon or an oxygen-containing hydrocarbon such as methane or methanol, and steam 102. These materials are reformed mainly by a steam reforming reaction to form a mixed gas mainly composed of hydrogen, carbon monoxide and carbon dioxide. Hydrogen in this gas is selectively separated, and withdrawn from the reformer 100 as high temperature (400 to 550° C.) high purity hydrogen 103. The residual gas after separation of hydrogen is taken out of the reformer 100 as an off-gas 104. The off-gas 104 is fed to a combustion side of the reformer 100, mixed with combustion air 105 in a burner of the reformer 100 (the burner 46 of the reformer shown in FIG. 7), and then subjected to combustion. Alternatively, the off-gas 104 may be mixed with a portion 101 a of the raw material gas 101 supplied, and then may be used as fuel.
  • The high temperature high purity hydrogen 103 separated from the reformer 100 is cooled by the cooler 106 to become low temperature (30 to 200° C.) high purity hydrogen 107. This hydrogen 107 is stored in the hydrogen storage/delivery means 108 composed of a hydrogen occluding material, and delivered from the hydrogen storage/delivery means 108 as high pressure hydrogen (2 atm or higher) 109. The low temperature high purity hydrogen 107 contains trace amounts of impurities such as carbon dioxide and carbon monoxide. Therefore, the low temperature high purity hydrogen 107 during storage or delivery is intermittently sent to the reformer 100 as purge hydrogen 110 a for use as part of fuel. When the low temperature high purity hydrogen 107 is not sent to the reformer 100, it is discharged out of the system as low purity hydrogen 110 b.
  • In the cooler 106 of the present First Embodiment, a gas mixture 111 of the raw material gas 101 and steam 102 is heat exchanged with the high temperature high purity hydrogen 103 indirectly, and thereby preheated. The preheated gas mixture 111 is supplied to the reformer 100.
  • The hydrogen occluding material of the hydrogen storage/delivery means 108 for carrying out the invention may be any material, without being restricted to the one disclosed in the embodiment, as long as it selectively occludes hydrogen from the mixed gas containing hydrogen, and releases the occluded hydrogen upon heating. As a practical hydrogen occluding material, a hydrogen storing alloy is known. Its examples are rare earth metal-Ni alloys such as LaNi5, misch metal alloys, titanium-zirconium alloys such as TiFe, Mg alloys such as Mg2Ni, V alloys, and calcium alloys such as CaNi5. In the invention, the hydrogen occluding material is not restricted to these alloys. Occluding materials which occlude hydrogen, such as those composed of a carbon nanotube, are also usable.
  • As the indirect type heat exchanger for the cooler 106, an ordinary shell & tube type heat exchanger or an ordinary plate type heat exchanger can be used. Any type of heat exchanger, which can perform cooling without direct contact with the high temperature high purity hydrogen 103, can be used without its embodiment being restricted.
  • According to the present embodiment, the high temperature (400 to 550° C.) high purity hydrogen 103 that has been separated from the reformer 100 is once cooled by the cooler 106, the indirect heat exchanger, to a temperature of about 30 to 200° C. at which hydrogen is easily occluded in the hydrogen occluding material. Then, the cooled hydrogen is fed to the hydrogen storage/delivery means 108, the hydrogen occluding material. As a result, the hydrogen occlusion rate and the amount of hydrogen occlusion can be increased. Also, hydrogen can be withdrawn from the reformer 100 at a lower pressure than the atmospheric pressure. Thus, the membrane area of the hydrogen separation membrane of the reformer 100 can be decreased. Moreover, a required power for the withdrawal of hydrogen can be decreased markedly in comparison with the power required when a vacuum pump is used.
  • When hydrogen stored in the hydrogen occluding material is to be delivered, the temperature of the hydrogen storage/delivery means 108, the hydrogen occluding material, is set at an appropriate level (e.g., about 80° C.), whereby hydrogen released at a high-pressure can be obtained. Thus, a hydrogen compression power necessary when a compressor is used can be cut down markedly.
  • Besides, the sensible heat of the high temperature high purity hydrogen 103 reformed by the reformer 100 can be utilized for heating of the raw material gas and steam in the cooler 106. Thus, the energy efficiency of the entire apparatus can be increased.
  • [Second Embodiment]
  • FIG. 2 is a schematic view of an apparatus layout for a second embodiment of the present invention.
  • According to the First Embodiment, the gas mixture 111 of the raw material gas 101 and steam 102 is fed to the cooler 106 for heat exchange, in order to utilize the sensible heat of the high temperature high purity hydrogen 103. In the present embodiment, on the other hand, combustion air 105 is supplied as shown in FIG. 2.
  • As the aforementioned cooler 106, an indirect type heat exchanger, for example, can be used. In the case of FIG. 2, heat exchange between the combustion air 105 and high temperature high purity hydrogen 103 takes place to cool the hydrogen, making it low temperature high purity hydrogen 107. Heated combustion air 105 a after heating by heat exchange, on the other hand, is fed to a burner of a reformer 100 (the burner 46 of the reformer illustrated in FIG. 7).
  • In the embodiment shown in FIG. 2, as indicated above, the combustion air 105 is indirectly heat exchanged with the high temperature high purity hydrogen 103, and thereby preheated. The preheated combustion air is fed to the reformer 100, whereby the energy efficiency of the entire apparatus can be increased.
  • [Third Embodiment]
  • FIG. 3 shows a third embodiment of the invention. According to this embodiment, air or cooling water is fed to a cooler 106 as a low temperature fluid 120 a, which is heat exchanged with high temperature high purity hydrogen 103 to obtain low temperature high purity hydrogen 107. A low temperature fluid 120 b after heat exchange is discharged out of the system, and utilized as other heat source.
  • [Fourth Embodiment]
  • FIG. 4 shows a fourth embodiment of the invention. According to this embodiment, a hydrogen storage/delivery means is composed of two members, a hydrogen occluding material 108A and a hydrogen occluding material 108B. In FIG. 4, the hydrogen occluding material 108A is defined as a hydrogen occlusion side, while a hydrogen occluding material 108B is defined as a hydrogen delivery side.
  • In the hydrogen occluding material 108A on the hydrogen occlusion side, low temperature high purity hydrogen 107 is flowed, and cooling water 121 a is supplied to cool the entire hydrogen occluding material 108A. By this measure, hydrogen is efficiently occluded and stored. Also, low purity hydrogen 110 b is intermittently discharged, or sent to a reformer 100 as purge hydrogen 110 a.
  • In the hydrogen occluding material 108B on the hydrogen delivery side, on the other hand, the low temperature hydrogen 107 is not flowed. However, separately fed high temperature water (50 to 100° C.) 122 a heats the entire alloy to release hydrogen stored in the hydrogen storing alloy, and the hydrogen is delivered out of the system as high pressure hydrogen 109.
  • In the hydrogen occluding material 108A on the hydrogen supply side, at a time when hydrogen has been occluded up to a set value for the amount of occlusion in the hydrogen occluding material, the supply of the low temperature high purity hydrogen 107 and the supply of the cooling water 121 a are stopped. Instead, high temperature water 122 b is flowed to liberate high-pressure hydrogen 109.
  • At the same time, in the hydrogen occluding material 108B on the hydrogen release side, the supply of the high temperature water 122 a and the release of the high-pressure hydrogen 109 are stopped. With cooling water 121 b being flowed, low temperature high purity hydrogen 107 is supplied to have hydrogen occluded.
  • By repeating the above procedures alternately, high-pressure hydrogen 109 is delivered. On this occasion, low purity hydrogen 110 c present in the hydrogen occluding material 108B on the hydrogen delivery side can be discharged intermittently.
  • As the high temperature water 122 a, 122 b fed for hydrogen release, it is permissible to use waste heat of cooling water 123 that has been fed to a cooler 106 for cooling high temperature high purity hydrogen 103, in order to utilize the thermal energy within the apparatus efficiently.
  • According to the present embodiment, the waste heat of the cooling water 123 used for cooling of the high temperature high purity hydrogen 103 is utilized for heating of the hydrogen occluding material 108B on the hydrogen delivery side, whereby effective use of heat can be achieved.
  • [Fifth Embodiment]
  • FIG. 5 shows a fifth embodiment of the invention. According to this embodiment, a pressure regulator 130 for low temperature high purity hydrogen 107 is installed between a cooler 106 and a hydrogen storage/delivery means 108. As the pressure regulator 130, an ordinary valve can be used, and a valve involving a decreased loss in pressure is preferred. High purity hydrogen 131 after pressure regulation is fed to the hydrogen storage/delivery means 108.
  • According to the present embodiment, the pressure regulator 130 is installed between the hydrogen storage/delivery means 108 and the cooler 106. As a result, a buffer zone is formed for preventing a rapid pressure drop on the hydrogen permeation side of a hydrogen separation membrane inside are former 100. Consequently, the durability of the hydrogen separation membrane can be improved. Moreover, a rapid rise in the temperature of the hydrogen storage/delivery means 108 associated with its hydrogen occlusion can also be prevented. Thermal shock to the hydrogen storage/delivery means 108 can be cushioned. Furthermore, changes over time in the amount of hydrogen production from the apparatus for producing hydrogen can be minimized and leveled off. After all, well balanced hydrogen production can be performed.
    • EXAMPLES
  • The present invention will be described in further detail with reference to Examples, which are not limitative of the invention.
    • Example 1
  • A first example of the invention will be explained based on the apparatus layout shown in FIG. 3. A hydrogen separation type reformer 100 had the structure shown in FIGS. 7 and 8, as with the preceding Embodiments. A heat exchanger, a cooler 106, was of a plate fin type, and used cooling water as a low temperature fluid 120 a to cool high temperature high purity hydrogen 103. A hydrogen occluding material of a hydrogen storage/delivery means 108 was composed of two members of a hydrogen storing alloy of LaNi5.
  • Hydrogen was produced under the following concrete conditions in accordance with the flow shown in FIG. 3.
  • (1) Hydrogen Separation Type Reformer (100)
  • Main Constitution
  • The catalyst of the reformer 100 was an NiO catalyst in particle form, and the hydrogen separation membrane was made of a Pd alloy. The membrane area was 0.68 cm2.
  • Operating Conditions
  • The reaction temperature of the reformer was 550° C., and the reaction pressure was 6 atm. Methane was used as the raw material gas. The reformer was run, with the flow rate of the raw material gas being 1.5 m3 N/h and the steam-carbon ratio being 3.
  • (2) Cooler (106)
  • The heat exchanger, the cooler 106, was of a plate fin type, and used cooling water as a cooling medium. The inlet temperature of cooling water was 25° C., and the outlet temperature of cooling water was 80° C. The inlet temperature of the high temperature high purity hydrogen 103 fed to the cooler 106 was 450° C., and the outlet temperature of low temperature high purity hydrogen 107 after heat exchange was 40° C.
  • (3) Hydrogen Storage/Delivery Means (108)
  • The hydrogen occluding material, the hydrogen storage/delivery means 108, was composed of two members of an LaNi5 alloy. The inlet temperature of cooling water during occlusion by the hydrogen storing alloy was 30° C., while the inlet temperature of cooling water during release of hydrogen was 80° C. The occluding capacity of the hydrogen storing alloy was 4 m3 N/member.
  • (4) Amount of Hydrogen Production
  • The amount of hydrogen production through the use of the hydrogen storing alloy as in the present Example was 3.0 m3 N/h. Whereas the amount of hydrogen production without the use of the hydrogen storing alloy in the present Example was about a half, i.e., 1.5 m3 N/h.
  • (5) Power for Hydrogen Supply
  • In the present Example, the power required for supply of 3.0 m3N/h of hydrogen at 6 atm by the hydrogen storing alloy was about 0.05 kW. Whereas the power required for compression of 3.0 m3 N/h of hydrogen from 1 atm to 6 atm by a compressor was about 0.9 kW.
    • Example 2
  • A second example of the invention will be explained based on the apparatus layout shown in FIG. 3.
  • (1) Hydrogen Separation Type Reformer (100)
  • The constitution and operating conditions were the same as in Example 1.
  • (2) Cooler (106)
  • The same constitution and operating conditions as in Example 1 were adopted, except that the outlet temperature of low temperature high purity hydrogen 107 in the cooler 106 was 80° C.
  • (3) Hydrogen Storing Alloy
  • The same constitution and operating conditions as in Example 1 were adopted.
  • (4) Amount of Hydrogen Production
  • When the high purity hydrogen outlet temperature was 40° C. as in Example 1, the amount of hydrogen production was 3.0 m3 N/h. When the high purity hydrogen outlet temperature was 80° C., on the other hand, the amount of hydrogen production was 2.0 m3 N/h.
    • Example 3
  • A third example of the invention will be explained based on the apparatus layout shown in FIG. 5.
  • A hydrogen separation type reformer 100, a cooler 106, and a hydrogen storage/delivery means 108 had the same constitutions as in Example 1. A pressure regulator 130 comprises a pressure regulating valve, and mitigates a rapid pressure fall at the start of hydrogen occlusion by the hydrogen storage/delivery means 108. Thus, the pressure regulator 130 curbs a rapid pressure change of low temperature high purity hydrogen 107 flowing out of the cooler 106.
  • Hydrogen was produced under the following concrete conditions:
  • The constitutions and operating conditions of the hydrogen separation type reformer 100, cooler 106, and hydrogen storage/delivery means 108 were the same as in Example 1.
  • FIG. 6 shows changes in the pressure of low temperature high purity hydrogen during hydrogen occlusion. Regulation of the pressure results in the mitigation of a rapid pressure drop occurring at the start of occlusion.
  • The amount of hydrogen production was 3.5 m3 N/h when the pressure regulator 130 was installed. Whereas the amount of hydrogen production was 3.0 m3 N/h when the pressure regulator was not used.
  • The entire disclosure of Japanese Patent Application No.11-162416 filed on Jun. 9, 1999, including specification, claims, drawings and summary, is incorporated herein by reference in its entirety.

Claims (5)

1.-17. (canceled)
18. An apparatus for producing hydrogen by a steam reforming reaction, on a catalyst, of a hydrocarbon or an oxygen-containing hydrocarbon as a raw material, comprising:
a hydrogen separation type reformer which has a means for heating the catalyst and which has a hydrogen separation membrane built into a layer of the catalyst for selectively separating hydrogen;
a cooling means for cooling high temperature high purity hydrogen obtained from the reformer,
wherein:
the cooling means for cooling the high temperature high purity hydrogen comprises an indirect heat exchanger;
wherein:
a fluid for cooling the high temperature high purity hydrogen via the indirect heat exchanger is one or both of a raw material gas and combustion air to be fed to the hydrogen separation type reformer; and
a hydrogen charge/discharge means disposed downstream from the cooling means and composed of a hydrogen storage material,
wherein:
the hydrogen charge/discharge means composed of the hydrogen storage material comprises at least two members of a hydrogen storing alloy incorporating a heating/cooling means.
19. An apparatus for producing hydrogen by a steam reforming reaction, on a catalyst, of a hydrocarbon or an oxygen-containing hydrocarbon as a raw material, comprising:
a hydrogen separation type reformer which has a means for heating the catalyst and which has a hydrogen separation membrane built into a layer of the catalyst for selectively separating hydrogen;
a cooling means for cooling high temperature high purity hydrogen obtained from the reformer;
wherein:
the cooling means for cooling the high temperature high purity hydrogen comprises an indirect heat exchanger;
wherein:
a fluid for cooling the high temperature high purity hydrogen via the indirect heat exchanger is one or both of air or cooling water; and
a hydrogen charge/discharge means disposed downstream from the cooling means and composed of a hydrogen storage material;
wherein:
the hydrogen charge/discharge means composed of the hydrogen storage material comprises at least two members of a hydrogen storing alloy incorporating a heating/cooling means.
20. The apparatus for producing hydrogen as claimed in claim 18, wherein:
a pressure regulating means is interposed between the cooling means for cooling the high temperature high purity hydrogen and the hydrogen charge/discharge means disposed downstream from the cooling means and composed of the hydrogen storage material, to regulate the pressure of the high purity hydrogen to be fed to the hydrogen charge/discharge means.
21. The apparatus for producing hydrogen as claimed in claim 19, wherein:
a pressure regulating means is interposed between the cooling means for cooling the high temperature high purity hydrogen and the hydrogen charge/discharge means disposed downstream from the cooling means and composed of the hydrogen storage material, to regulate the pressure of the high purity hydrogen to be fed to the hydrogen charge/discharge means.
US10/914,101 1999-06-09 2004-08-10 Apparatus for producing hydrogen Abandoned US20050013754A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US10/914,101 US20050013754A1 (en) 1999-06-09 2004-08-10 Apparatus for producing hydrogen

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
JP11162416A JP2000351607A (en) 1999-06-09 1999-06-09 Hydrogen-producing apparatus
JP11-162416 1999-06-09
US09/588,903 US6802876B1 (en) 1999-06-09 2000-06-09 Apparatus for producing hydrogen
US10/914,101 US20050013754A1 (en) 1999-06-09 2004-08-10 Apparatus for producing hydrogen

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
US09/588,903 Division US6802876B1 (en) 1999-06-09 2000-06-09 Apparatus for producing hydrogen

Publications (1)

Publication Number Publication Date
US20050013754A1 true US20050013754A1 (en) 2005-01-20

Family

ID=15754193

Family Applications (2)

Application Number Title Priority Date Filing Date
US09/588,903 Expired - Lifetime US6802876B1 (en) 1999-06-09 2000-06-09 Apparatus for producing hydrogen
US10/914,101 Abandoned US20050013754A1 (en) 1999-06-09 2004-08-10 Apparatus for producing hydrogen

Family Applications Before (1)

Application Number Title Priority Date Filing Date
US09/588,903 Expired - Lifetime US6802876B1 (en) 1999-06-09 2000-06-09 Apparatus for producing hydrogen

Country Status (6)

Country Link
US (2) US6802876B1 (en)
EP (1) EP1061039B1 (en)
JP (1) JP2000351607A (en)
CA (1) CA2310928C (en)
DE (1) DE60009210T2 (en)
DK (1) DK1061039T3 (en)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020114984A1 (en) * 2001-02-21 2002-08-22 Edlund David J. Fuel cell system with stored hydrogen
US20030192251A1 (en) * 2002-04-12 2003-10-16 Edlund David J. Steam reforming fuel processor
US20080244973A1 (en) * 2004-01-30 2008-10-09 Idemitsu Kosan Co., Ltd. Reformer
US20110175032A1 (en) * 2007-08-16 2011-07-21 Dge Dr.-Ing Günther Engineering Gmbh Method and plant for the production of synthesis gas from biogas
WO2012030350A1 (en) * 2010-09-03 2012-03-08 Azur Anergy Llc Reformation and hydrogen purification system

Families Citing this family (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NO317382B1 (en) 2001-02-16 2004-10-18 Norsk Hydro As Method for carrying out a catalytic or non-catalytic process
US7922781B2 (en) 2001-03-02 2011-04-12 Chellappa Anand S Hydrogen generation apparatus and method for using same
US7867300B2 (en) 2001-03-02 2011-01-11 Intelligent Energy, Inc. Ammonia-based hydrogen generation apparatus and method for using same
KR100868392B1 (en) 2001-03-02 2008-11-11 메소퓨얼 인코포레이티드 Ammonia-based hydrogen generation apparatus and method for using same
JP2002338204A (en) * 2001-05-22 2002-11-27 Mitsubishi Gas Chem Co Inc High purity hydrogen producing equipment
US6890672B2 (en) 2001-06-26 2005-05-10 Idatech, Llc Fuel processor feedstock delivery system
US20030223926A1 (en) 2002-04-14 2003-12-04 Edlund David J. Steam reforming fuel processor, burner assembly, and methods of operating the same
US8172913B2 (en) 2002-04-23 2012-05-08 Vencill Thomas R Array of planar membrane modules for producing hydrogen
US7115148B2 (en) 2002-05-14 2006-10-03 Her Majesty The Queen In Right Of Canada, As Respresented By The Minister Of Defence Of Her Majesty's Canadian Government Compact methanol steam reformer with integrated hydrogen separation
US7416583B2 (en) * 2003-10-17 2008-08-26 General Electric Company Appliance having a container including a nanostructured material for hydrogen storage
KR100560488B1 (en) * 2004-01-28 2006-03-13 삼성에스디아이 주식회사 Fuel cell system
JP4899294B2 (en) * 2004-06-10 2012-03-21 株式会社日立製作所 Hydrogen fuel production system, hydrogen fuel production method, and hydrogen fuel production program
EP1669323B1 (en) * 2004-12-08 2017-07-05 Karlsruher Institut für Technologie Reactor and method for the production of hydrogen
US7637971B2 (en) * 2005-06-29 2009-12-29 Hsu Yang Wang Hydrogen fuel supply system
US7569511B2 (en) * 2006-05-05 2009-08-04 Basf Catalysts Llc Catalyst composition for alcohol steam reforming

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4865624A (en) * 1987-06-29 1989-09-12 Nippon Sanso Kabushiki Kaisha Method for steam reforming methanol and a system therefor
US5149600A (en) * 1989-12-27 1992-09-22 Petroleum Energy Center And Showa Shell Sekiyu Kabushiki Kaisha Fuel cell electricity generation process
US5458857A (en) * 1992-12-02 1995-10-17 Rolls-Royce, Plc Combined reformer and shift reactor
US5527632A (en) * 1992-07-01 1996-06-18 Rolls-Royce And Associates Limited Hydrocarbon fuelled fuel cell power system
US5769909A (en) * 1996-05-31 1998-06-23 International Fuel Cells Corp. Method and apparatus for desulfurizing fuel gas
US5938800A (en) * 1997-11-13 1999-08-17 Mcdermott Technology, Inc. Compact multi-fuel steam reformer
US6011073A (en) * 1997-10-10 2000-01-04 Syntroleum Corporation System and method for converting light hydrocarbons to heavier hydrocarbons with separation of water into oxygen and hydrogen
US6306354B1 (en) * 1996-05-17 2001-10-23 International Fuel Cells, Llc Shift converter
US6348278B1 (en) * 1998-06-09 2002-02-19 Mobil Oil Corporation Method and system for supplying hydrogen for use in fuel cells

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1572796A (en) * 1975-12-31 1980-08-06 Johnson Matthey Co Ltd Storage of hydrogen gas
JPS62279264A (en) * 1986-05-27 1987-12-04 Mazda Motor Corp Reformed fuel feeding device for engine
JPH03179672A (en) * 1989-09-01 1991-08-05 Fuji Electric Co Ltd Fuel gas supply unit for fuel cell
JPH04325402A (en) 1991-04-25 1992-11-13 Mitsubishi Heavy Ind Ltd Method and equipment for producing gaseous hydrogen for fuel cell and supply method therefor
CA2118956C (en) * 1993-03-16 1998-08-25 Yoshinori Shirasaki Hydrogen producing apparatus
JP3197108B2 (en) 1993-05-18 2001-08-13 東京瓦斯株式会社 Hydrogen production equipment
US5895519A (en) * 1996-03-28 1999-04-20 Saes Pure Gas, Inc. Method and apparatus for purifying hydrogen gas
JP4000608B2 (en) * 1996-11-07 2007-10-31 トヨタ自動車株式会社 Hydrogen production filling device and electric vehicle

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4865624A (en) * 1987-06-29 1989-09-12 Nippon Sanso Kabushiki Kaisha Method for steam reforming methanol and a system therefor
US5149600A (en) * 1989-12-27 1992-09-22 Petroleum Energy Center And Showa Shell Sekiyu Kabushiki Kaisha Fuel cell electricity generation process
US5527632A (en) * 1992-07-01 1996-06-18 Rolls-Royce And Associates Limited Hydrocarbon fuelled fuel cell power system
US5458857A (en) * 1992-12-02 1995-10-17 Rolls-Royce, Plc Combined reformer and shift reactor
US6306354B1 (en) * 1996-05-17 2001-10-23 International Fuel Cells, Llc Shift converter
US5769909A (en) * 1996-05-31 1998-06-23 International Fuel Cells Corp. Method and apparatus for desulfurizing fuel gas
US6011073A (en) * 1997-10-10 2000-01-04 Syntroleum Corporation System and method for converting light hydrocarbons to heavier hydrocarbons with separation of water into oxygen and hydrogen
US6277338B1 (en) * 1997-10-10 2001-08-21 Syntroleum Corporation System for converting light hydrocarbons to heavier hydrocarbons with separation of water into oxygen and hydrogen
US5938800A (en) * 1997-11-13 1999-08-17 Mcdermott Technology, Inc. Compact multi-fuel steam reformer
US6348278B1 (en) * 1998-06-09 2002-02-19 Mobil Oil Corporation Method and system for supplying hydrogen for use in fuel cells

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020114984A1 (en) * 2001-02-21 2002-08-22 Edlund David J. Fuel cell system with stored hydrogen
US20030192251A1 (en) * 2002-04-12 2003-10-16 Edlund David J. Steam reforming fuel processor
US20080244973A1 (en) * 2004-01-30 2008-10-09 Idemitsu Kosan Co., Ltd. Reformer
US8038960B2 (en) * 2004-01-30 2011-10-18 Idemitsu Kosan Co., Ltd. Reformer
US20110175032A1 (en) * 2007-08-16 2011-07-21 Dge Dr.-Ing Günther Engineering Gmbh Method and plant for the production of synthesis gas from biogas
US8187568B2 (en) * 2007-08-16 2012-05-29 DGE Dr. Ing. Guenther Engineering GmbH Method and plant for the production of synthesis gas from biogas
WO2012030350A1 (en) * 2010-09-03 2012-03-08 Azur Anergy Llc Reformation and hydrogen purification system

Also Published As

Publication number Publication date
CA2310928A1 (en) 2000-12-09
DE60009210T2 (en) 2005-05-25
EP1061039A1 (en) 2000-12-20
DK1061039T3 (en) 2004-08-02
US6802876B1 (en) 2004-10-12
DE60009210D1 (en) 2004-04-29
JP2000351607A (en) 2000-12-19
EP1061039B1 (en) 2004-03-24
CA2310928C (en) 2005-11-29

Similar Documents

Publication Publication Date Title
US6802876B1 (en) Apparatus for producing hydrogen
CA2345966C (en) Fuel processing system
CA2307971C (en) Method for driving a fuel cell vehicle and fuel cell vehicle
US5741474A (en) Process for production of high-purity hydrogen
US20060183009A1 (en) Fuel cell fuel processor with hydrogen buffering
US20040241505A1 (en) Solid oxide fuel cell systems having temperature swing reforming
EP0867404A1 (en) Hydrogen manufacturing apparatus
US8945784B2 (en) Hydrogen production apparatus and fuel cell system using the same
JPS5964501A (en) Manufacture of ammonia synthetic gas
US20020064487A1 (en) Compact Multiple tube steam reformer
US11814288B2 (en) Oxy-fuel heated hydrogen production process
JP2003187849A (en) Solid polymer fuel cell power generator
JP2020079173A (en) Hydrogen production apparatus
JP4663839B2 (en) Hydrogen recovery / storage container
JP2000327306A (en) High-purity hydrogen production apparatus and fuel cell system
JP2000340242A (en) Heat pump type hydrogen purification device using waste heat of fuel cell
KR100415235B1 (en) Fuel processing system
AU745858B2 (en) Fuel processing system
JPH1171101A (en) High-pressure reformer
JP2001338661A (en) High purity hydrogen driven fuel cell system
JP2001313049A (en) Hydrogen supply device for fuel cell
CA2413994C (en) Fuel processing system
JP2003503294A (en) Compact fuel gas reformer with combustor wall temperature control
CN117326526A (en) Catalytic combustion-based methanol reforming hydrogen production system and method
JP2002037605A (en) Device for manufacturing of hydrogen

Legal Events

Date Code Title Description
STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION