WO2000061491A1 - Appareil d'oxydation sélective de monoxyde de carbone - Google Patents
Appareil d'oxydation sélective de monoxyde de carbone Download PDFInfo
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- WO2000061491A1 WO2000061491A1 PCT/JP2000/002419 JP0002419W WO0061491A1 WO 2000061491 A1 WO2000061491 A1 WO 2000061491A1 JP 0002419 W JP0002419 W JP 0002419W WO 0061491 A1 WO0061491 A1 WO 0061491A1
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- WIPO (PCT)
- Prior art keywords
- hydrogen
- oxygen
- reaction tank
- flow
- carbon monoxide
- Prior art date
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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
- H01M8/0625—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 in a modular combined reactor/fuel cell structure
- H01M8/0631—Reactor construction specially adapted for combination reactor/fuel cell
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- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/248—Reactors comprising multiple separated flow channels
- B01J19/2485—Monolithic reactors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0403—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
- B01J8/0423—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more otherwise shaped beds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0492—Feeding reactive fluids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
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- 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
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
- C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
- C01B3/583—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction the reaction being the selective oxidation of carbon monoxide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
- C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
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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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
- B01J2219/00081—Tubes
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- 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
- C01B2203/0435—Catalytic purification
- C01B2203/044—Selective oxidation of carbon monoxide
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- 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
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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
Definitions
- the present invention relates to a carbon monoxide selective oxidizing apparatus, and more particularly, to a carbon monoxide selective oxidizing apparatus having a reaction tank filled with a catalyst for oxidizing carbon monoxide in hydrogen rich gas in preference to hydrogen in the presence of oxygen. It relates to an oxidation device. Background art
- this type of carbon monoxide selective oxidizer has been used to prioritize hydrogen in the presence of oxygen such as ruthenium and rhodium in hydrogen rich gas obtained by steam reforming hydrocarbon fuels.
- a catalyst that oxidizes carbon monoxide with a catalyst that oxidizes carbon monoxide has been proposed (for example, Japanese Patent Application Laid-Open No. 5-210702).
- the catalyst is housed in an elongated steel tube vessel, and the hydrogen rich gas is introduced into the reaction vessel along the longitudinal direction thereof together with air, while the hydrogen rich gas passes through the reaction vessel. Oxidizes carbon monoxide in hydrogen rich gas.
- the carbon monoxide selective oxidizing apparatus of the present invention further improves the carbon monoxide selective oxidizing apparatus proposed by the present applicant, and one of its objects is to reduce the concentration of carbon monoxide in hydrogen rich gas. . Another object of the present invention is to maintain a high concentration of hydrogen in a hydrogen-rich gas.
- the carbon monoxide selective oxidation apparatus of the present invention employs the following means in order to achieve at least a part of the above object.
- the first carbon monoxide selective oxidation device of the present invention is a first carbon monoxide selective oxidation device of the present invention.
- a carbon monoxide selective oxidizer having a reaction tank filled with a catalyst for oxidizing carbon monoxide in hydrogen rich gas in preference to hydrogen in the presence of oxygen,
- An oxygen-containing gas supply unit that supplies an oxygen-containing gas containing oxygen from a plurality of locations along the flow of the hydrogen rich gas to the reaction tank;
- the reaction tank is formed such that a gas flow path cross section increases toward the downstream side with respect to the flow of the hydrogen rich gas.
- the oxygen-containing gas feeder is provided in a reaction tank formed such that the gas flow path cross section increases toward the downstream side with respect to the flow of the hydrogen rich gas.
- An oxygen-containing gas containing oxygen is supplied from a plurality of locations along the flow of the hydrogen rich gas. Since the reaction tank is formed so that the gas flow path cross section becomes larger toward the downstream side with respect to the flow of the hydrogen rich gas, the amount of gas flowing into the reaction tank increases on the way due to the supply of the oxygen-containing gas.
- the reaction vessel may include a case formed such that the cross-sectional area increases toward the downstream side with respect to the flow of the hydrogen rich gas. it can.
- the reaction vessel is configured such that the catalyst is carried on a monolithic carrier having a smaller number of cells in a downstream side with respect to the flow of the hydrogen rich gas. You can also.
- the reaction vessel can be formed so that the gas flow path cross section becomes larger toward the downstream side with respect to the flow of the hydrogen rich gas, and the catalyst phase filled toward the downstream side with respect to the flow of the hydrogen rich gas.
- the catalyst can be filled so that the gas flow path resistance in the step becomes small.
- the “monolithic carrier” is a carrier composed of a plurality of cells that divide a gas flow path into a plurality of cells, and corresponds to, for example, a honeycomb tube.
- the oxygen-containing gas supply device is arranged such that the downstream of the flow of the hydrogen rich gas in the reaction tank, the smaller the amount of oxygen to the reaction tank.
- the oxygen-containing gas may be supplied, or the oxygen-containing gas may be supplied through a pipe having a smaller flow path cross section toward the downstream side of the flow of the hydrogen-rich gas in the reaction vessel. Since the concentration of carbon monoxide in the hydrogen rich gas is higher on the upstream side with respect to the flow of the hydrogen rich gas in the reactor, the oxidation reaction of carbon monoxide occurs more frequently.
- the oxygen-containing gas supply device may be configured such that the number of pipes is increased toward the downstream side of the flow of the hydrogen-rich gas in the reaction tank so that the oxygen is increased.
- a gas containing gas can also be supplied. In this case, diffusion and mixing of the oxygen-containing gas into the hydrogen-rich gas are performed quickly, so that carbon monoxide can be oxidized efficiently.
- the reaction vessel is cooled such that a cooling effect on the reaction vessel becomes lower toward the downstream side of the flow of the hydrogen-rich gas in the reaction vessel.
- a cooling device may be provided.
- the upstream of the flow of hydrogen rich gas in the reaction vessel the more carbon monoxide Since many oxidation reactions occur, the more upstream the heat is, the higher the temperature tends to be. Therefore, by cooling the reaction tank so that the cooling effect becomes lower toward the downstream side, the temperature of the entire reaction tank can be made more uniform at an appropriate temperature.
- the cooling device may be configured such that the cooling medium is flowed through a flow path having a smaller contact area toward the downstream side of the flow of the hydrogen-rich gas in the reaction vessel.
- the cooling medium may be circulated to the reaction vessel, or the cooling medium may be circulated to the reaction vessel by decreasing the number of flow paths toward the downstream side of the flow of the hydrogen-rich gas in the reaction vessel.
- the reaction tank can be configured such that the gas flow path cross section increases toward the downstream side.
- the second carbon monoxide selective oxidation device of the present invention comprises:
- a carbon monoxide selective oxidizer having a reaction tank filled with a catalyst for oxidizing carbon monoxide in hydrogen rich gas in preference to hydrogen in the presence of oxygen,
- An oxygen-containing gas supply device that supplies an oxygen-containing gas containing oxygen from a plurality of locations along the flow of the hydrogen-rich gas to the reaction tank,
- the reaction tank is filled with a catalyst such that the flow path resistance of the gas in the filled catalyst phase decreases toward the downstream side with respect to the flow of the hydrogen rich gas.
- the oxygen-containing gas feeder is configured so that the flow path resistance of the gas in the catalyst phase filled toward the downstream side with respect to the flow of the hydrogen-rich gas is reduced.
- An oxygen-containing gas containing oxygen is supplied from a plurality of locations along the flow of the hydrogen rich gas to a reaction vessel filled with the hydrogen. Since the reaction tank is filled with a catalyst so that the flow path resistance of the gas in the filled catalyst phase decreases toward the downstream side with respect to the flow of the hydrogen rich gas, it flows into the reaction tank by supplying the oxygen-containing gas.
- the reaction tank has a plurality of filling portions filled with the catalyst so that gas flow resistance in a catalyst phase is different. It can also be done.
- the reaction vessel is configured such that the catalyst is carried on a monolithic carrier having a smaller number of cells toward the downstream side with respect to the flow of the hydrogen rich gas.
- the reaction tank can be formed so that the gas flow path cross section becomes larger toward the downstream side with respect to the flow of the hydrogen rich gas, and the catalyst filled toward the downstream side with respect to the flow of the hydrogen rich gas.
- the catalyst can be packed so that the flow resistance of the gas in the phase is reduced ⁇
- the oxygen-containing gas supply device may be arranged such that the downstream of the flow of the hydrogen rich gas in the reaction tank, the smaller the amount of oxygen to the reaction tank.
- the oxygen-containing gas may be supplied, or the oxygen-containing gas may be supplied through a pipe having a smaller flow path cross section toward the downstream side of the flow of the hydrogen-rich gas in the reaction vessel. Since the concentration of carbon monoxide in the hydrogen rich gas is higher on the upstream side with respect to the flow of the hydrogen rich gas in the reactor, the oxidation reaction of carbon monoxide occurs more frequently.
- the oxygen-containing gas supply device may be configured such that the number of pipes is increased toward the downstream side of the flow of the hydrogen-rich gas in the reaction tank, and A gas containing gas can also be supplied. In this case, diffusion and mixing of the oxygen-containing gas into the hydrogen-rich gas are performed quickly, so that carbon monoxide can be oxidized efficiently.
- a cooling device for cooling the reaction vessel such that a cooling effect on the reaction vessel becomes lower toward the downstream of the flow of the hydrogen rich gas in the reaction vessel May be provided.
- a cooling device for cooling the reaction vessel such that a cooling effect on the reaction vessel becomes lower toward the downstream of the flow of the hydrogen rich gas in the reaction vessel.
- the cooling device may be configured to circulate a cooling medium to the reaction tank through a flow path having a smaller contact area toward the downstream side with respect to the flow of the hydrogen rich gas in the reaction tank.
- the cooling medium may be circulated through the reaction vessel by reducing the number of flow paths toward the downstream side of the flow of the hydrogen rich gas in the reaction vessel.
- the reaction vessel can be configured such that the gas flow path cross section increases toward the downstream side.
- FIG. 1 is a configuration diagram schematically showing the configuration of a reformer 20 including a CO selective oxidation device 30 according to an embodiment of the present invention.
- FIG. 2 is a cross-sectional view schematically illustrating the configuration of the CO selective oxidation device 30 of the embodiment.
- FIG. 3 is a cross-sectional view illustrating the A-A cross section of the CO selective oxidation device 30 of the embodiment of FIG.
- FIG. 4 is a cross-sectional view schematically illustrating the configuration of a CO selective oxidation device 130 according to a modification
- FIG. 5 is a cross-sectional view illustrating a cross-section of a honeycomb tube as an example of a monolith carrier.
- FIG. 1 is a configuration diagram schematically showing the configuration of a reformer 20 including a CO selective oxidation device 30 according to one embodiment of the present invention.
- the reformer 20 is a device that obtains a hydrogen-rich gas supplied to a hydrogen consuming organization having a low allowable concentration of carbon monoxide, for example, a polymer electrolyte fuel cell or the like, from a hydrocarbon-based fuel by steam reforming.
- a reforming section 24 for reforming to a hydrogen-rich gas by the reaction of the formula (3) a heat exchange section 26 for cooling the hydrogen rich gas obtained by the reforming, and a gas contained in the cooled hydrogen rich gas.
- a CO selective oxidation device 30 for oxidizing carbon monoxide with priority over hydrogen as a by-product is provided.
- the reforming reaction in the reforming section 24 is efficient at about 600 ° C to 800 ° C, and the selective oxidation reaction in the CO selective oxidizing device 30 is 140 ° C to 170 ° C. The degree is done efficiently Therefore, cooling of the hydrogen-rich gas is performed in the heat exchange section 26. Therefore, in the embodiment, the CO selective oxidation device 30 is configured to oxidize carbon monoxide in the hydrogen rich gas obtained by the reforming reaction of the reforming section 24.
- FIG. 3 is a cross-sectional view illustrating a C 0 schematic configuration of the selective oxidation apparatus 30 of the embodiment
- the CO selective oxidation device 30 of the embodiment includes a case 32 that forms the outer wall of the CO selective oxidation device 30 and a catalyst that preferentially oxidizes carbon monoxide in hydrogen-rich gas over hydrogen in the presence of oxygen. Filled with catalyst, air introduction pipes 54 to 58 for introducing air as oxygen-containing gas containing oxygen into the hydrogen rich gas, and a cooling medium for cooling the catalyst filled parts 44 to 48 And a cooling water passage 64 to 68 as a cooling water passage.
- catalyst arrangement portions 34 to 38 are formed in which the gas flow path cross-sectional area increases in three stages from the upstream side along the flow of the hydrogen-rich gas.
- the catalyst-filled portion 44 is filled with a carrier having a small particle size carrying a catalyst, and the catalyst-filled portion 48 is loaded with a catalyst on a carrier having a larger particle size than the carrier filled in the catalyst filled portion 44. It is filled with what is carried.
- the catalyst filling section 46 is filled with a carrier having a larger particle size than the carrier filled in the catalyst filling section 44 and having a smaller particle size than the carrier filled in the catalyst filling section 48 carrying the catalyst.
- the gas flow path cross section becomes larger toward the downstream side, and the gas flow path resistance becomes smaller.
- the air introduction pipes 54 to 58 are located at the center upstream of the catalyst placement sections 34 to 38 in Case 32. The section is disposed so as to be orthogonal to the flow of the hydrogen rich gas. Air inlet pipe
- each of the air introduction pipes 54 to 58 has a plurality of air supply holes 54a to 58a formed upstream of the hydrogen-rich gas, and air is introduced into the hydrogen rich gas. It has become so.
- the cooling water passages 64 to 68 are formed as flat, widened passages orthogonal to the flow of the hydrogen-rich gas. They are arranged so as to be stacked. Each of the cooling water passages 64 to 68 has the same shape, but is arranged so that the number of the cooling water passages becomes smaller toward the downstream side along the flow of the hydrogen rich gas. Therefore, the cross section of the cooling water becomes smaller toward the downstream side, and the cooling effect becomes smaller.
- the CO selective oxidizing apparatus 30 of the embodiment configured as described above has a larger gas flow path cross-sectional area, a smaller gas flow path resistance, and a smaller air flow toward the downstream side along the flow of the hydrogen rich gas.
- the volume is small, the number of air supply pipes introduced is large, and the cooling effect is reduced. Therefore, even if the gas flow rate is increased by the introduction of air, the gas can be flowed without stagnation and the increase in the discharge pressure of the hydrogen rich gas at the outlet of the CO selective oxidizer 30 can be prevented. it can.
- a hydrogen rich gas having a high hydrogen content can be obtained. Furthermore, since the catalyst filling sections 44 to 48 are cooled in accordance with the progress of the oxidation reaction of carbon monoxide, the temperature of the entire CO selective oxidation device 30 can be adjusted to a temperature suitable for the oxidation reaction of carbon monoxide. . As a result, the oxidation reaction of carbon monoxide And the concentration of carbon monoxide in the hydrogen rich gas can be further reduced.
- the reformer 20 of the embodiment has the case 32 formed so that the cross-sectional area increases in three steps along the flow of the hydrogen rich gas, but the cross-sectional area is constant along the flow of the hydrogen rich gas. May be provided.
- FIG. 4 schematically shows the configuration of a modified CO selective oxidation apparatus 130.
- the configuration corresponding to the configuration of the CO selective oxidizing device 30 of the embodiment is denoted by the numeral with 100 added.
- the case 132 of the CO selective oxidation device 130 of the modification has a constant cross section with respect to the flow of the hydrogen-rich gas.
- a catalyst carrier is placed in a catalyst filling section 144-148 in which a catalyst is supported on a monolithic carrier (for example, a honeycomb tube illustrated in FIG. 5) divided into a plurality of flow paths.
- the CO selective oxidizing device 130 of this modified example has the same effect as that of the CO selective oxidizing device 30 of the above-described embodiment, and also uses the case 1 32 that does not change the cross-sectional area. Therefore, there is also an effect that the installation of the CO selective oxidation device 130 can be facilitated.
- the gas flow path cross-sectional area increases toward the downstream side along the flow of the hydrogen-rich gas, and the gas flow resistance decreases.
- a small amount of air is introduced, a large number of air supply pipes are introduced, and the cooling effect is reduced.However, it is not necessary to provide all of these elements. May not be provided.
- a configuration in which only elements that increase the gas flow path cross-sectional area toward the downstream side along the flow of hydrogen rich gas from all the above-mentioned elements, or a configuration in which only elements that reduce the gas flow path resistance are removed The configuration that removes only the elements that reduce the amount of air introduced, A configuration in which only the element that increases the number of air supply pipes to be removed may be removed, or a configuration in which only the element that reduces the cooling effect is removed, or a configuration in which two or more such elements are combined and removed may be used.
- the CO selective oxidation device 30 of the embodiment and the CO selective oxidation device 130 of the modified example are described as selectively oxidizing carbon monoxide in a reformed gas obtained by steam reforming a hydrocarbon-based fuel.
- any device that oxidizes carbon monoxide in hydrogen rich gas in preference to hydrogen in the presence of oxygen can be applied to any hydrogen-rich gas. Therefore, the CO selective oxidizing device 30 of the embodiment and the CO selective oxidizing device 130 of the modified example have been described as a part of the reforming device 20, but have no other configuration of the reforming device 20. Needless to say, it is not necessary to be a part of the reformer 20.
- one of hydrogen rich gas supplied to a hydrogen consuming engine having a low allowable concentration of carbon monoxide such as a polymer electrolyte fuel cell, is used.
- carbon oxide is selectively oxidized
- carbon monoxide in hydrogen rich gas supplied to any hydrogen consuming organization may be selectively oxidized.
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP00917307A EP1184336A4 (en) | 1999-04-14 | 2000-04-13 | DEVICE FOR SELECTIVE OXIDATION OF CARBON MONOXIDE |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP11/106230 | 1999-04-14 | ||
JP11106230A JP2000302407A (ja) | 1999-04-14 | 1999-04-14 | 一酸化炭素選択酸化装置 |
Publications (1)
Publication Number | Publication Date |
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WO2000061491A1 true WO2000061491A1 (fr) | 2000-10-19 |
Family
ID=14428334
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/JP2000/002419 WO2000061491A1 (fr) | 1999-04-14 | 2000-04-13 | Appareil d'oxydation sélective de monoxyde de carbone |
Country Status (3)
Country | Link |
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EP (1) | EP1184336A4 (ja) |
JP (1) | JP2000302407A (ja) |
WO (1) | WO2000061491A1 (ja) |
Cited By (1)
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EP2380848A1 (en) * | 2001-03-28 | 2011-10-26 | Osaka Gas Co., Ltd. | Carbon monoxide removal reactor, fuel reforming system, filter and method of removing carbon monoxide |
Families Citing this family (8)
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KR100422804B1 (ko) * | 2001-09-05 | 2004-03-16 | 현대자동차주식회사 | 연료 전지용 co 제거장치 |
JP2005231965A (ja) * | 2004-02-20 | 2005-09-02 | Matsushita Electric Ind Co Ltd | 一酸化炭素除去装置、および燃料電池発電装置 |
KR100570697B1 (ko) | 2004-09-24 | 2006-04-12 | 삼성에스디아이 주식회사 | 연료 전지 시스템 및 이에 사용되는 개질기 |
KR100646985B1 (ko) | 2005-06-24 | 2006-11-23 | 삼성에스디아이 주식회사 | 평판형 연료개질 시스템 및 이를 구비한 연료전지 시스템 |
US8221693B2 (en) | 2005-08-01 | 2012-07-17 | Basf Corporation | Use of a radial zone coating to facilitate a two-stage prox system with single air injection |
KR100814887B1 (ko) | 2007-04-13 | 2008-03-20 | 삼성에스디아이 주식회사 | 연료 전지용 일산화탄소 처리장치 |
KR101113440B1 (ko) * | 2009-11-17 | 2012-02-29 | 삼성에스디아이 주식회사 | 선택적산화 반응장치 |
ES2431491B1 (es) * | 2013-08-07 | 2014-09-29 | Abengoa Hidrógeno, S.A. | Reactor de oxidación preferencial de monóxido de carbono |
Citations (4)
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JPH07185303A (ja) * | 1993-12-28 | 1995-07-25 | Aqueous Res:Kk | 一酸化炭素除去装置 |
JPH0834601A (ja) * | 1994-05-17 | 1996-02-06 | Idemitsu Kosan Co Ltd | 燃料電池用水素含有ガスの製造方法 |
JPH0847621A (ja) * | 1994-08-05 | 1996-02-20 | Toyota Motor Corp | 一酸化炭素の除去装置 |
EP0968958A1 (en) * | 1998-06-29 | 2000-01-05 | Ngk Insulators, Ltd. | Reformer |
Family Cites Families (4)
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JP3096302B2 (ja) * | 1989-12-11 | 2000-10-10 | ゲブリユーダー ズルツアー アクチエンゲゼルシヤフト | 不均一反応型の反応器及び反応器用触媒 |
DE4334983A1 (de) * | 1993-10-14 | 1995-04-20 | Daimler Benz Ag | Verfahren zur katalytischen Entfernung von CO in H¶2¶-reichem Gas |
DE19544895C1 (de) * | 1995-12-01 | 1997-02-27 | Daimler Benz Ag | Verfahren und Vorrichtung zur selektiven katalytischen Oxidation von Kohlenmonoxid |
DE19719997A1 (de) * | 1997-05-13 | 1998-05-28 | Daimler Benz Ag | Reformierungsreaktoranlage und Betriebsverfahren hierfür |
-
1999
- 1999-04-14 JP JP11106230A patent/JP2000302407A/ja active Pending
-
2000
- 2000-04-13 WO PCT/JP2000/002419 patent/WO2000061491A1/ja not_active Application Discontinuation
- 2000-04-13 EP EP00917307A patent/EP1184336A4/en not_active Withdrawn
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
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JPH07185303A (ja) * | 1993-12-28 | 1995-07-25 | Aqueous Res:Kk | 一酸化炭素除去装置 |
JPH0834601A (ja) * | 1994-05-17 | 1996-02-06 | Idemitsu Kosan Co Ltd | 燃料電池用水素含有ガスの製造方法 |
JPH0847621A (ja) * | 1994-08-05 | 1996-02-20 | Toyota Motor Corp | 一酸化炭素の除去装置 |
EP0968958A1 (en) * | 1998-06-29 | 2000-01-05 | Ngk Insulators, Ltd. | Reformer |
Non-Patent Citations (1)
Title |
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See also references of EP1184336A4 * |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2380848A1 (en) * | 2001-03-28 | 2011-10-26 | Osaka Gas Co., Ltd. | Carbon monoxide removal reactor, fuel reforming system, filter and method of removing carbon monoxide |
US8357341B2 (en) | 2001-03-28 | 2013-01-22 | Osaka Gas Co., Ltd. | Carbon monoxide removal method, operating method for fuel reforming system, carbon monoxide remover, fuel removal system having the carbon monoxide remover, and filter |
US8591850B2 (en) | 2001-03-28 | 2013-11-26 | Osaka Gas Co., Ltd. | Carbon monoxide removal method, operating method for fuel reforming system, carbon monoxide remover, fuel reforming system having the carbon monoxide remover, and filter |
Also Published As
Publication number | Publication date |
---|---|
EP1184336A1 (en) | 2002-03-06 |
JP2000302407A (ja) | 2000-10-31 |
EP1184336A4 (en) | 2003-06-25 |
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