WO2005097317A1 - 水蒸気改質触媒、水蒸気改質方法、水素製造装置および燃料電池システム - Google Patents
水蒸気改質触媒、水蒸気改質方法、水素製造装置および燃料電池システム Download PDFInfo
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- WO2005097317A1 WO2005097317A1 PCT/JP2005/007195 JP2005007195W WO2005097317A1 WO 2005097317 A1 WO2005097317 A1 WO 2005097317A1 JP 2005007195 W JP2005007195 W JP 2005007195W WO 2005097317 A1 WO2005097317 A1 WO 2005097317A1
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- catalyst
- steam reforming
- hydrogen
- carbon monoxide
- fuel cell
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Classifications
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
- H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
-
- 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
- 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
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/63—Platinum group metals with rare earths or actinides
-
- 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
- C01B3/40—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 characterised by the catalyst
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
- H01M8/0668—Removal of carbon monoxide or carbon dioxide
-
- 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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
- B01J37/0207—Pretreatment of the support
-
- 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
- C01B2203/06—Integration with other chemical processes
- C01B2203/066—Integration with other chemical processes with fuel cells
-
- 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
-
- 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
- C01B2203/1082—Composition of support materials
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- 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
- Y02E60/50—Fuel cells
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the present invention relates to a hydrocarbon reforming catalyst for hydrocarbon compounds.
- the present invention relates to a steam reforming catalyst for hydrocarbon compounds that can be advantageously purged with an oxygen-containing gas when the operation of a hydrogen production device is stopped, and a steam reforming method using the catalyst and a hydrogen production device. And a fuel cell system.
- the system may be shut down to respond to power and heat demand conditions and to perform checks.
- the catalyst may deteriorate, restartability may deteriorate, and fuel may leak. Therefore, it is preferable to purge the inside of the system with an appropriate gas at the time of shutdown.
- a gas containing oxygen such as air was used as the purge gas, deterioration of the reforming catalyst due to oxygen could not be ignored.
- An object of the present invention is to provide a hydrogen reforming catalyst and a fuel cell system capable of stably operating for a long period of time by providing a steam reforming catalyst that achieves both a long-term operation life and resistance to purging with an oxygen-containing gas. Aim.
- the present inventors have intensively searched for a steam reforming catalyst having high activity, capable of long-term operation, and having excellent resistance to purging with an oxygen-containing gas. As a result, the present invention has been completed. It is. That is, the present invention provides a steam reforming catalyst for hydrocarbon compounds, which comprises rhodium supported on a carrier comprising (a) alumina, (b) ceria, and (c) a barrier and no or magnesia as constituents. About.
- the present invention also relates to a steam reforming method characterized by producing a mixed gas containing carbon monoxide and hydrogen from a raw material mixture containing hydrocarbon compounds and steam using the steam reforming catalyst.
- the present invention has a reforming section for performing a steam reforming reaction of hydrocarbon compounds, wherein the reforming section uses the steam reforming catalyst, and purges the reforming section with a gas containing oxygen at the time of shutdown.
- the reforming section uses the steam reforming catalyst, and purges the reforming section with a gas containing oxygen at the time of shutdown.
- the present invention relates to a hydrogen production apparatus comprising a step of treating a mixed gas containing carbon monoxide and hydrogen produced by the steam reforming method in a subsequent carbon monoxide removal step.
- the present invention relates to the hydrogen production apparatus, wherein the carbon monoxide removing step comprises a water gas reaction step and a subsequent carbon monoxide selective oxidation step.
- the present invention also relates to a fuel cell system characterized by using hydrogen produced by the hydrogen production device as fuel.
- the present invention will be described in detail.
- the steam reforming reaction in the present invention refers to a reaction in which a hydrocarbon compound is reacted with steam in the presence of a catalyst to convert the compound into a reforming gas containing carbon monoxide and hydrogen.
- the hydrocarbon compounds as the original family are organic compounds having 1 to 40 carbon atoms, preferably 1 to 30 carbon atoms. Specific examples include saturated aliphatic hydrocarbons, unsaturated aliphatic hydrocarbons, aromatic hydrocarbons, and the like. For saturated aliphatic hydrocarbons and unsaturated aliphatic hydrocarbons, linear and cyclic Can be used regardless. Aromatic hydrocarbons can be used regardless of whether they are monocyclic or polycyclic. Such hydrocarbon compounds can contain substituents. As the substituent, any of a chain and a cyclic may be used, and examples thereof include an alkyl group, a cycloalkyl group, an aryl group, an alkylaryl group and an aralkyl group.
- these hydrocarbon compounds include a hydroxy group, an alkoxy group, a hydroxygarbonyl group, an alkoxycarbonyl group, It may be substituted by a substituent containing a hetero atom such as a rumyl group.
- Saturated aliphatic hydrocarbons unsaturated aliphatic hydrocarbons such as ethylene, propylene, butene, pentene and hexene, alicyclic hydrocarbons such as cyclopentane and cyclohexane, and aromatic hydrocarbons such as benzene, toluene, xylene and naphthalene Hydrogen can be mentioned.
- mixtures thereof can also be suitably used, and examples thereof include materials that can be obtained industrially at low cost, such as natural gas, LPG, naphtha, gasoline, kerosene, and gas oil.
- hydrocarbon compounds having a substituent containing a hetero atom include methanol, ethanol, propanol, butanol, dimethyl ether, phenol, anisol monoacetone, acetoaldehyde, and acetic acid.
- a raw material containing hydrogen, water, carbon dioxide, carbon monoxide, or the like as the above raw material can also be used.
- the residual hydrogen used in the reaction can be used without any particular separation.
- the amount of steam introduced into the reaction system is a value defined as a ratio of the number of moles of water molecules to the number of moles of carbon atoms contained in the raw hydrocarbon compounds (steam / carbon ratio). However, it is preferably in the range of 0.3 to 10, more preferably 0.5 to 5, and even more preferably 1 to 3. If this value is smaller than the above range, coke tends to precipitate on the catalyst and the hydrogen fraction cannot be increased.On the other hand, if it is larger, the reforming reaction proceeds but steam generation equipment and steam recovery There is a risk that the equipment will be enlarged.
- the method of addition is not particularly limited, but it may be introduced into the reaction zone at the same time as the starting hydrocarbon compounds, or may be introduced separately from a different position in the reactor zone or by dividing into several portions. May be.
- carbon dioxide can be added to the source gas for the purpose of mainly obtaining carbon monoxide.
- the amount of carbon dioxide added is the ratio of the number of moles of carbon dioxide molecules to the number of moles of carbon atoms (excluding carbon dioxide) contained in the raw material.
- the steam reforming catalyst of the present invention is obtained by supporting rhodium on a carrier containing (a) alumina, (b) ceria, and (c) barrier and Z or magnesium as constituents.
- the method for supporting rhodium is not particularly limited, and a known method such as a usual impregnation method can be employed. Usually, it is dissolved in a solvent such as water, ethanol or acetone as a rhodium salt or complex, and impregnated into a carrier.
- a solvent such as water, ethanol or acetone
- the metal salt or metal complex to be supported chlorides, nitrates, sulfates, acetates, acetate acetates, and the like are preferably used, and specific examples include compounds such as rhodium chloride, rhodium nitrate, and rhodium carbonyl.
- the present invention is not limited to these.
- the content of rhodium in the catalyst is usually from 0.05 to 20% by mass, preferably from 0.1 to 10% by mass, and more preferably from 0.3 to 5% by mass, as a nitrogen atom. . If the content is higher than this range, the agglomeration of the active metal increases, and the proportion of the metal coming out on the surface is extremely reduced, which is not preferable. On the other hand, if the amount is less than the above range, sufficient activity cannot be exhibited, so that a large amount of catalyst is required, and the reactor needs to be made larger than necessary.
- the carrier used in the catalyst of the present invention comprises (a) alumina, (b) ceria, and (c) a barrier and Z or magnesia as constituents.
- the composition ratio of the cerium is in the range of 1 to 50% by mass, preferably 1.5 to 30% by mass, more preferably 2 to 20% by mass based on the alumina. Further, the composition ratio of the barrier and / or magnesia is in the range of 1 to 50% by mass, preferably 1.5 to 30% by mass, and more preferably 2 to 20% by mass based on the alumina. is there. If the ratio is less than the above-mentioned ratio, the effect of suppressing carbon deposition becomes insufficient. On the other hand, if the ratio is higher than the above-mentioned ratio, the surface area is reduced and the activity is lowered, which is not preferable.
- calcium, scandia, italia, titania, zirconia, hafnia, thoria, silica, silica alumina, zeolite, etc. may be appropriately mixed with the carrier, if necessary. Can be used.
- a gas containing oxygen when the operation of the apparatus is stopped. Air is usually used as the oxygen-containing gas, but a gas having a reduced oxygen concentration, such as combustion exhaust gas or air electrode off-gas of a fuel cell, can be more preferably used.
- the temperature of the reforming section at the time of purging is usually from room temperature to 400 ° C, preferably 100 ° (: up to 300 ° C. If the temperature is lower than this, water may condense and the purging effect may not be sufficiently obtained. On the other hand, if it is higher than this, unexpected catalyst deterioration may proceed.
- the form of the reforming catalyst of the present invention there is no particular limitation on the form of the reforming catalyst of the present invention.
- a catalyst which is tablet-formed, pulverized and then sized to an appropriate range, an extruded catalyst, a catalyst extruded by adding an appropriate binder, a powdered catalyst, and the like.
- the metal is formed on a carrier formed by tableting, crushed and sized to an appropriate range, an extruded carrier, powder or a carrier formed into an appropriate shape such as a sphere, ring, tablet, cylinder, flake, etc.
- a supported catalyst or the like can be used.
- a catalyst in which the catalyst itself is formed into a monolithic shape, a honeycomb shape, or the like, or a catalyst obtained by coating a monolithic honeycomb with an appropriate material or the like can be used.
- the thus obtained reforming catalyst of the present invention is activated by hydrogen reduction, if necessary.
- a form of the reactor used for the steam reforming reaction a flow-type fixed bed reactor is preferably used, but a fluidized bed reactor can also be used.
- the shape of the reactor any known shape such as a cylindrical shape and a flat shape depending on the purpose of each process can be adopted.
- the space velocity of the feedstock (feedstock + steam) introduced into the reactor is preferably GHSV, preferably 100 to 100, more preferably 300 to 50, 00Oh— ⁇ 500, more preferably 500 to 30, In the range of 0 00 h 1 , it is set in consideration of each purpose.
- the reaction temperature is not particularly limited, but is preferably in the range of 200 to 1 000 ° (:, more preferably 300 to 900, more preferably 500 to 800 ° C.).
- the reaction pressure is not particularly limited, and is preferably atmospheric pressure to 20M.
- the reaction pressure is not particularly limited, and is preferably atmospheric pressure to 20M.
- FIG. 1 is a schematic diagram showing an example of the fuel cell system of the present invention.
- fuel in a fuel tank 3 flows into a desulfurizer 5 via a fuel pump 4.
- the desulfurizer can be filled with, for example, a copper-zinc based sorbent or a nickel-zinc based sorbent.
- the hydrogen-containing gas from the carbon monoxide selective oxidation reactor 11 can be added.
- the fuel desulfurized in the desulfurizer 5 is mixed with water passed through the water pump 2 from the water tank 1, introduced into the vaporizer 6, vaporized, and sent to the reformer 7.
- the steam Z carbon ratio is set to preferably 1 to 20, more preferably 1.5 to 10, and still more preferably 2 to 5.
- the space velocity of the raw material for distribution is preferably GHSV in terms of the above-mentioned catalyst amount, standard temperature and pressure, and is preferably 100 to: L 0 0, OOO h— 1 , more preferably.
- the reformer reaction tube is heated by a burner 18 using fuel from a fuel tank and anode off-gas as fuel, preferably at 200 to 100 ° C., more preferably at 300 to 900 ° C. ° (:, more preferably in the range of 500 to 80 ° C.
- the reformed gas containing hydrogen and carbon monoxide produced in this manner is passed through a high-temperature shift reactor 9, a low-temperature shift reactor 10, and a carbon monoxide selective oxidation reactor 11 in that order.
- the carbon monoxide concentration is reduced to such an extent that the characteristics of the fuel cell are not affected.
- catalysts used in these reactors include an iron chromium-based catalyst for the high-temperature shift reactor 9, a copper-zinc-based catalyst for the low-temperature shift reactor 10, and a carbon monoxide selective oxidation reactor. Ruthenium-based catalysts and the like can be fisted in 11.
- the polymer electrolyte fuel cell 17 is composed of an anode 12, a power source 13, and a solid polymer electrolyte 14, and the fuel gas containing high-purity hydrogen obtained by the above method is provided on the anode side.
- the air sent from the air blower 18 is introduced to the force sword side after performing appropriate humidification processing if necessary (humidifier is not shown).
- hydrogen gas becomes a proton at the anode, and the reaction of emitting electrons progresses. It is carried out in the range of Pa, more preferably in the range of atmospheric pressure to 5 MPa, still more preferably in the range of atmospheric pressure to 1 MPa, but if necessary, it can be carried out at atmospheric pressure or lower.
- the present invention provides a hydrogen production apparatus, comprising a step of treating a mixed gas containing carbon monoxide and hydrogen obtained by the steam reforming reaction in a subsequent carbon monoxide removal step.
- the mixed gas containing carbon monoxide and hydrogen obtained by the steam reforming reaction of the present invention can be used as it is as a fuel for a fuel cell in the case of a solid oxide fuel cell.
- a carbon monoxide removal step can be used in combination to make it suitable as a source of hydrogen for the fuel cell. Can be used.
- Removal of carbon oxide can be performed, for example, by performing a shift step and a carbon monoxide selective oxidation step.
- the shift process is a process in which carbon monoxide and water are reacted to convert them to hydrogen and carbon dioxide, and contain mixed oxides of iron and chromium, mixed oxides of copper and zinc, platinum, ruthenium, iridium, etc.
- the amount of carbon monoxide is preferably 2% by volume or less, more preferably 1% by volume or less, and still more preferably 0.5% by volume. Decrease to / 0 or less. Normally, the mixed gas in this state can be used as fuel in a phosphoric acid fuel cell.
- the treatment is performed in a carbon monoxide selective oxidation step or the like.
- a catalyst containing iron, cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, platinum, gold, silver, gold, or the like is used.
- 0.1 to 10 times, more preferably 0.7 to 5 times, and more preferably 1 to 3 times by mole of oxygen is added to selectively convert carbon monoxide to carbon dioxide.
- Reduce carbon concentration In this case, the carbon monoxide concentration can be reduced by reacting with the coexisting hydrogen simultaneously with the oxidation of carbon monoxide to produce methane.
- the present invention also provides a fuel cell system using hydrogen produced by the hydrogen production apparatus as a fuel.
- MEA Membrane Electrode Assembly 1 y: a membrane electrode assembly.
- a fuel cell can be assembled by sandwiching the MEA with a separator that has a gas supply function consisting of metal materials, graphite, carbon composite, etc., a collector function, and especially a cathode that has an important drainage function.
- the electric load 15 is electrically connected to the anode and the power source.
- the anode off-gas is burned in the burner 18 and discharged after being used for heating the reforming pipe. Force sword off-gas is exhausted from exhaust port 16.
- the water vapor reforming catalyst which was not difficult conventionally and does not fall in activity even by purging with an oxygen-containing gas at the time of an operation stop, and was excellent in durability in normal operation is provided.
- a fuel cell system using the same is provided.
- Y -alumina with a surface area of 16.5 g / cm 2 is used as the catalyst carrier (1).
- the catalyst (A) is tablet-molded, pulverized, and sized to a size of 250 to 500 ⁇ m.
- the mixture is charged into a fixed-bed flow reactor, and desulfurized kerosene (0.05 mass ppm or less as sulfur atom) ) And steam were used as raw materials to perform a steam reforming reaction.
- kerosene is stopped, the temperature is lowered to 300 ° C in 20 minutes, air is introduced, steam is stopped, and the temperature is lowered to 30 ° C in 20 minutes.
- the above was taken as one DSS cycle, and repeated experiments were performed.
- the reaction conditions were a steam / carbon ratio of 3.0, a catalyst amount of 6 cm 3 , and a desulfurized kerosene flow rate of 0.244 g / min.
- the catalyst (D) is tablet-molded, pulverized, and sized to a range of 250 to 500 ⁇ .
- the resulting mixture is charged into a fixed-bed flow reactor, and desulfurized kerosene (0.05 mass ppm as sulfur atom)
- the steam reforming reaction was carried out continuously at 700 ° C using a mixed gas of Figure 3 shows the change over time in catalyst degradation during continuous operation.
- Figure 3 As can be seen, the catalyst of the present invention was found to be a catalyst having excellent durability.
- FIG. 1 is a schematic diagram showing one example of the fuel cell system of the present invention.
- FIG. 2 is a graph showing the relationship between the kerosene conversion rate and the number of DDS cycles in DDS operation using catalysts A to E.
- FIG. 3 is a diagram showing the relationship between kerosene conversion and elapsed time in a steam reforming reaction using catalyst D.
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Abstract
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JP2004114430A JP2005296755A (ja) | 2004-04-08 | 2004-04-08 | 水蒸気改質触媒、水蒸気改質方法、水素製造装置および燃料電池システム |
JP2004-114430 | 2004-04-08 |
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Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2008153826A2 (en) * | 2007-05-31 | 2008-12-18 | Corning Incorporated | Catalyst for hydrogen production by autothermal reforming, method of making same and use thereof |
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JP5428103B2 (ja) * | 2007-02-21 | 2014-02-26 | 国立大学法人 大分大学 | 低温水素製造用触媒及びその製造方法と水素製造方法 |
WO2009028113A1 (ja) * | 2007-08-29 | 2009-03-05 | National University Corporation Oita University | 低温水素製造用触媒及びその製造方法と水素製造方法 |
JP6198032B2 (ja) * | 2012-11-21 | 2017-09-20 | 日産自動車株式会社 | 水素生成用触媒及び水素生成用触媒を用いたシステム |
JP2015196142A (ja) * | 2014-04-02 | 2015-11-09 | 株式会社豊田中央研究所 | 水蒸気改質触媒、それを用いた水蒸気改質方法、及び水蒸気改質反応装置 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5724639A (en) * | 1980-07-17 | 1982-02-09 | Toyota Central Res & Dev Lab Inc | Catalyst for water vapor reforming and its manufacture |
JP2001158603A (ja) * | 1999-11-30 | 2001-06-12 | Honda Motor Co Ltd | メタノール改質装置の停止方法 |
JP2001190908A (ja) * | 2000-01-07 | 2001-07-17 | Soken Chem & Eng Co Ltd | 濾過装置及び濾過法 |
JP2002336702A (ja) * | 2001-05-11 | 2002-11-26 | Nippon Oil Corp | オートサーマルリフォーミング触媒および燃料電池用燃料ガスの製造方法 |
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2004
- 2004-04-08 JP JP2004114430A patent/JP2005296755A/ja active Pending
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2005
- 2005-04-07 WO PCT/JP2005/007195 patent/WO2005097317A1/ja active Application Filing
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5724639A (en) * | 1980-07-17 | 1982-02-09 | Toyota Central Res & Dev Lab Inc | Catalyst for water vapor reforming and its manufacture |
JP2001158603A (ja) * | 1999-11-30 | 2001-06-12 | Honda Motor Co Ltd | メタノール改質装置の停止方法 |
JP2001190908A (ja) * | 2000-01-07 | 2001-07-17 | Soken Chem & Eng Co Ltd | 濾過装置及び濾過法 |
JP2002336702A (ja) * | 2001-05-11 | 2002-11-26 | Nippon Oil Corp | オートサーマルリフォーミング触媒および燃料電池用燃料ガスの製造方法 |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2008153826A2 (en) * | 2007-05-31 | 2008-12-18 | Corning Incorporated | Catalyst for hydrogen production by autothermal reforming, method of making same and use thereof |
WO2008153826A3 (en) * | 2007-05-31 | 2009-02-12 | Corning Inc | Catalyst for hydrogen production by autothermal reforming, method of making same and use thereof |
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