WO2007043571A1 - Catalyseur pour oxydation partielle d’hydrocarbures - Google Patents

Catalyseur pour oxydation partielle d’hydrocarbures Download PDF

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Publication number
WO2007043571A1
WO2007043571A1 PCT/JP2006/320300 JP2006320300W WO2007043571A1 WO 2007043571 A1 WO2007043571 A1 WO 2007043571A1 JP 2006320300 W JP2006320300 W JP 2006320300W WO 2007043571 A1 WO2007043571 A1 WO 2007043571A1
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catalyst
platinum group
group element
coating layer
gas
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PCT/JP2006/320300
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English (en)
Japanese (ja)
Inventor
Akiyoshi Nakajima
Masaaki Okuno
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Nippon Shokubai Co., Ltd.
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Publication of WO2007043571A1 publication Critical patent/WO2007043571A1/fr

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    • 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
    • C01B3/386—Catalytic partial combustion
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/864—Removing carbon monoxide or hydrocarbons
    • 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
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/42—Platinum
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/46—Ruthenium, rhodium, osmium or iridium
    • B01J23/464—Rhodium
    • 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
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    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
    • B01J35/56—Foraminous structures having flow-through passages or channels, e.g. grids or three-dimensional monoliths
    • 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
    • B01J37/0215—Coating
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/10—Noble metals or compounds thereof
    • B01D2255/102—Platinum group metals
    • B01D2255/1021—Platinum
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
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    • B01D2255/1023—Palladium
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/10—Noble metals or compounds thereof
    • B01D2255/102—Platinum group metals
    • B01D2255/1025—Rhodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/10—Noble metals or compounds thereof
    • B01D2255/102—Platinum group metals
    • B01D2255/1026—Ruthenium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/10—Noble metals or compounds thereof
    • B01D2255/102—Platinum group metals
    • B01D2255/1028—Iridium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/90—Physical characteristics of catalysts
    • B01D2255/902—Multilayered catalyst
    • B01D2255/9022—Two layers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/90—Physical characteristics of catalysts
    • B01D2255/92—Dimensions
    • B01D2255/9202—Linear dimensions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/16—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • B01D2257/7022—Aliphatic hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
    • 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
    • C01B2203/1064—Platinum group metal catalysts
    • C01B2203/107—Platinum 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
    • 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 catalyst used when producing a hydrogen-containing gas from a hydrocarbon and a method for producing a hydrogen-containing gas using the catalyst. More specifically, the present invention relates to a catalyst for partial oxidation of hydrocarbon for producing a hydrogen-containing gas from a mixed gas containing a hydrocarbon-containing gas and an oxygen-containing gas, and a hydrocarbon power hydrogen using the catalyst. The present invention relates to a method for producing contained gas.
  • a hydrogen-containing gas mainly composed of hydrogen and carbon monoxide is widely used not only for producing hydrogen gas, but also as a reducing gas and a raw material for various chemical products. Recently, practical research has been promoted for fuel cells.
  • Such a hydrogen-containing gas is mainly obtained by reforming a hydrocarbon compound, and as a reforming method, for example, there is a hydrocarbon partial oxidation method represented by the following chemical formula.
  • the partial oxidation method of hydrocarbons is a method in which a hydrogen-containing gas is produced by partially oxidizing a hydrocarbon with an oxygen-containing gas such as air in the presence of a catalyst. This is a partial oxidation reaction formula when the hydrocarbon is methane.
  • a catalyst for partial oxidation of hydrocarbons a catalyst using a platinum group element as a catalytic active component and a catalyst using a base metal element such as Ni or Co have been proposed.
  • base metal catalysts are difficult to be practically used because they are easily poisoned by sulfur in hydrocarbon fuels and carbon is likely to be deposited again.
  • platinum group element-based catalyst for example, the following catalysts have been proposed.
  • Japanese Unexamined Patent Publication No. 7-187605 discloses a method for reforming a lower hydrocarbon fuel, in which a mixed gas obtained by adding oxygen (or air) and, if necessary, water vapor to a lower hydrocarbon fuel is subjected to partial oxidation reaction Has been proposed.
  • This publication discloses a catalyst in which a Hercam support is coated with alumina having a thickness of about 100 ⁇ m and a platinum group element is supported thereon. However, it is said that it is necessary to carry 5 to 20 g of platinum group element per 1 liter of the hard cam support.
  • JP-A-2004-322001 discloses that a platinum group element is supported at a high concentration on a refractory inorganic oxide such as activated alumina, and further, cerium oxide or cerium-zirconium composite oxide is added.
  • a catalyst in which a catalyst component containing the catalyst component is supported on a monolithic carrier has been proposed! According to the example of this publication, even when the platinum group element loading amount per liter of the hard cam carrier is 1.8 g, high durability can be obtained.
  • the present invention has been made in view of such circumstances, and an object of the present invention is an inexpensive catalyst having a low platinum group element content, high activity, and long-term durability. It is an object to provide a catalyst for partial oxidation of hydrogen and a method for producing a hydrocarbon-powered hydrogen-containing gas using the catalyst.
  • the inventors of the present invention have studied in detail the partial oxidation reaction of hydrocarbons by a platinum group catalyst, and as a result, a layer in which a catalyst component containing a platinum group element and a refractory inorganic oxide is coated on a molded carrier. And the outer layer portion of the coating layer (the central force of the coating layer thickness up to the catalyst surface) is the inner layer portion of the coating layer (the central force of the thickness of the coating layer).
  • the content of the platinum group element is substantially less than the portion up to the support surface)
  • the catalyst has a much higher durability and longer catalyst life than the catalyst with the same platinum group element content and even distribution of the platinum group element in the thickness direction of the coating layer.
  • the present invention has been completed.
  • the present invention has a layer in which a molding component is coated with a catalyst component containing a platinum group element and a refractory inorganic oxide, and an outer layer portion of the coating layer (the thickness of the coating layer).
  • the content of the platinum group element is substantially higher than the inner layer portion of the coating layer (the portion of the coating layer thickness up to the central force carrier surface).
  • the present invention provides a catalyst for partial oxidation of hydrocarbons.
  • the thickness of the coating layer is 10 m or more, 70% by mass or more of the platinum group element has a surface force of 5 m. Exist in the territory until! /, I prefer to be! /.
  • the shaped carrier is preferably a monolithic carrier, and the refractory inorganic oxide is acid cerium and Z or cerium-zyl. It is preferable to contain a compost complex acid.
  • the present invention also provides a hydrogen-containing gas obtained by bringing a mixed gas containing a hydrocarbon-containing gas and an oxygen-containing gas into contact with the hydrocarbon partial oxidation catalyst as described above to partially oxidize the hydrocarbon.
  • a method for producing a hydrogen-containing gas is provided.
  • the mixed gas preferably further contains water vapor.
  • the partial oxidation catalyst of the present invention even if the catalyst has a lower platinum group element content than the conventional catalyst, stable performance with a long catalyst life can be maintained for a long period of time. Can be reduced.
  • the catalyst for partial oxidation of the present invention is suitable for incorporation into a fuel cell that requires long-term stable use, for example, a solid oxide fuel cell or a solid polymer fuel cell. It is also suitable as a synthetic gas production catalyst in a GTL (Gas to Liquid) process.
  • GTL Gas to Liquid
  • FIG. 1 shows an EPMA cross-sectional analysis graph of platinum and rhodium for the catalyst of Catalyst Preparation Example 4.
  • the catalyst for partial oxidation of hydrocarbons is a catalyst for partial oxidation for reforming hydrocarbons, and comprises a shaped carrier having a layer coated with a catalyst component, the catalyst component comprising a platinum group element and fire resistance.
  • the outer layer portion of the coating layer (the central force of the thickness of the coating layer up to the catalyst surface) is the inner layer portion of the coating layer (the center of the thickness of the coating layer).
  • the content of the platinum group element is substantially higher than the portion from the portion to the support.
  • the catalyst of the present invention has a dramatically improved durability and a longer catalyst life than a catalyst having the same platinum group element content and in which the catalyst component is uniformly distributed in the thickness direction of the coating layer. Can be extended. In other words, an equivalent catalyst life can be obtained with a small amount of platinum group element used, and the catalyst cost can be greatly reduced.
  • the present invention will be described in detail.
  • the durability improving effect should be confirmed more than the catalyst uniformly distributed in the thickness direction. More preferably, 80% by mass or more, more preferably 90% by mass or more of a platinum group element is contained in the outer layer portion of the coating layer, whereby the durability can be further improved.
  • the surface force of the coating layer is usually 50 ⁇ m, preferably 25 ⁇ m, more preferably 5 ⁇ m.
  • platinum group elements having a total content of preferably 70% by mass or more, more preferably 80% by mass or more, and even more preferably 90% by mass or more can be present.
  • the supported amount of platinum group elements is catalyst 1 """""liter". The same applies below. ) Is preferably 5 g or less, more preferably 0.1 to 4. Og, and still more preferably 0.3 to 1.5 g. If the supported amount of platinum group element exceeds 5. Og, the catalyst life will not change significantly. The potential may be lost. On the other hand, if the supported amount of platinum group element is less than 0.1 lg, the catalyst life may deteriorate.
  • the platinum group element used in the catalyst of the present invention is preferably at least one selected from the group consisting of platinum, rhodium, palladium, ruthenium and iridium, more preferably platinum, rhodium and Group power consisting of iridium is at least one selected, most preferably rhodium.
  • platinum, rhodium itself is more expensive than other platinum group elements, it is often used in combination with other platinum group elements.
  • the mass ratio of platinum to rhodium is preferably 5: 100 to 100: 10, more preferably 5: 100 to 100: 50, and even more preferably 5: 100 to 100: 100.
  • platinum group element source for producing the catalyst of the present invention various compounds used for producing ordinary catalysts and the like can be used. Specific examples include various complexes such as nitrates, halides, ammonium salts, and ammine complexes. Examples of platinum compounds include PtCl, H PtCl, [Pt (NH) CI], (NH) PtCl, H PtBr, NH [Pt (C
  • ruthenium compounds include RuCl, Ru (NO), Ru (OH) CI ⁇ 7 ⁇
  • iridium compounds include (NH) IrCl, IrCl, H Ir
  • Base metals include, for example, Periodic Tables I, II, ⁇ , IV, V, VIB, VIIB, and VIII, Na, K, Cs, Ni, Co, Fe, Cr, Cu, V, Pr, Mg , Mo, W, Mn, Zn, Ga, Y, Ti, Ba, Examples include base metals such as Re, Bi, Nb, Ta, La, Ag, and Au.
  • base metals may be contained in the catalyst component by any method.
  • the thickness of the coating layer is not particularly limited, but when a monolithic carrier is used as a molded carrier, it is preferably 10 to 400 ⁇ m, more preferably 10 to 300 ⁇ m, and even more preferably 20 to 250. m. When the thickness of the coating layer is less than 10 m, uneven coating of the catalyst component may occur and the surface of the shaped carrier may be exposed, and the catalytic activity and durability may be reduced. Conversely, if the coating layer thickness exceeds 400 m, it may cause clogging and increased pressure loss.
  • the amount of the refractory inorganic oxide supported is preferably 400 g or less, more preferably 100 to 350 g, and still more preferably 150 to 300 g per liter of the catalyst. If the supported amount of the refractory inorganic oxide is less than 5 Og, uneven coating of the catalyst component may occur and the surface of the shaped carrier may be exposed, and the catalytic activity and durability may be reduced. On the other hand, if the amount of the refractory inorganic oxide supported exceeds 400 g, the coating layer becomes thick and peeling is likely to occur. In addition, there is a possibility of clogging of the cell in the case of the carrier carrier.
  • refractory inorganic oxide used in the catalyst of the present invention for example, refractory inorganic oxides used in ordinary catalysts such as alumina, silica, titania, and zircoure can be used. Any inorganic oxide can be used as long as it has the property that shape stability and performance do not deteriorate at high temperatures (for example, 500 to 1000 ° C.). Specific examples include activated alumina, zirconium oxide, cerium oxide, titanium oxide, silica, spinel, mullite, alumina silica, tita-ar silica, and the like.
  • refractory inorganic oxides at least one selected from the group force consisting of activated alumina, acid cerium and acid zirconium is preferable.
  • These refractory inorganic oxides are excellent in high temperature heat resistance. Is also preferable because of its excellent carrying ability of platinum group elements.
  • Activated alumina is desirable because the contact area with the reaction gas having a large specific surface area becomes large, so that the partial acid efficiency can be improved and the high temperature heat resistance is excellent.
  • the active alumina include a-anoremina, y-anoremina, ⁇ -anoremina, ⁇ -anoremina, 7? Alumina, and the like.
  • the properties of the activated alumina are not particularly limited, but activated alumina having a specific surface area of 25 to 250 m 2 / g is preferable.
  • the refractory inorganic oxide may be present by adding or combining other elements.
  • other elements include alkali metals, alkaline earth metals, rare earth elements, manganese, nickel, iron, and cobalt. By adding these elements, the heat resistance of the refractory inorganic oxide, the catalytic activity of the platinum group element, and the durability can be expected.
  • a combination with a refractory inorganic oxide for example, activated alumina containing cerium oxide, cerium-zirconium Those contained as complex oxides are preferred.
  • the addition or combination of other elements to the refractory inorganic oxide can be changed as appropriate according to the conditions of use of the catalyst.
  • the shape of the shaped carrier used for the catalyst of the present invention may be any shape, but is preferably spherical, granular, pellet-shaped, or Hermka-shaped.
  • shaped carriers when a monolithic carrier is used, it is excellent in low pressure loss resistance and dust resistance as compared with other shaped shaped carriers, and in particular, handling such as filling into a reformer becomes easy.
  • a material excellent in heat resistance, dust resistance and the like as the material of the support. Examples of such materials include cordierite, mullite, a alumina, zirconium oxide, titanium, alumina silicate, magnesium silicate, oxides, silicates, stainless steel, Fe-Cr, etc.
  • Heat resistant alloys such as A1 alloy.
  • One or more of these materials can be combined to form a monolith support.
  • the monolithic carrier used for the catalyst of the present invention can be produced by a conventionally known method such as squeeze molding, press molding, extrusion molding, and sheet processing using the above materials. Further, the method for producing the carrier is not particularly limited as long as it is appropriately changed in accordance with the constituent material, pore diameter, pore shape, and the like.
  • the monolithic carrier is formed with a number of holes (cells) penetrating in the parallel direction.
  • the shape of the hole may be any shape such as a circle or a polygon such as a triangle, square, or hexagon.
  • the size of the hole is not particularly limited.
  • the cell density of the carrier is not particularly limited, but is preferably 150 to 600 cells Z square inch, more preferably 250 to 600 cells, in order to increase the contact efficiency with the reaction gas.
  • the partial oxidation catalyst of the present invention can be produced by, for example, the following method, but can be appropriately changed depending on the material, composition, and the like. Therefore, unless otherwise specified, the following production method can be modified as appropriate.
  • a solution containing a platinum group element is supplied to a pulverizer such as a ball mill, and a slurry is prepared by wet pulverization.
  • a pulverizer such as a ball mill
  • a slurry is prepared by wet pulverization.
  • the monolith support is brought into contact with a slurry having a low platinum group element content, and then dried and fired.
  • the catalyst after calcination has a higher platinum group element content. After contacting the slurry, the catalyst is dried and calcined. [0045] (4) When there are three or more types of slurries, the operation of (3) is repeated in the order of slurries having the platinum group element content from the slurries having the least platinum group element content.
  • acids such as hydrochloric acid, sulfuric acid, nitric acid, acetic acid, and oxalic acid, ammonia, and hydroxyammonium hydroxide are used to adjust the viscosity of the slurry and improve the stability of the slurry.
  • acids such as hydrochloric acid, sulfuric acid, nitric acid, acetic acid, and oxalic acid, ammonia, and hydroxyammonium hydroxide are used to adjust the viscosity of the slurry and improve the stability of the slurry.
  • polymer compounds such as polyacrylic acid and polyvinyl alcohol, and the like may be added as necessary.
  • the contacting method is not particularly limited, but it is preferable to immerse the carrier in the slurry because the active component can be uniformly supported. After immersion, it is recommended that excess slurry (for example, slurry remaining in the cell) adhering to the carrier is removed by a method such as air blowing and then subjected to a drying step.
  • the drying method is not particularly limited, and the water content of the slurry supported may be removed by any method.
  • the conditions during drying may be either room temperature or high temperature. Further, firing after drying is desirable because the catalytically active component can be firmly fixed on the carrier.
  • the firing method is not particularly limited, and may be fired at 400 to 800 ° C., for example, in air or in a reducing atmosphere.
  • a powder in which a platinum group element is supported on a refractory inorganic oxide and a refractory inorganic oxide that does not support a platinum group element are supplied to a pulverizer such as a ball mill and wet. Prepare slurry by grinding. Slurries with different platinum group element contents can be prepared depending on the amount of the latter refractory inorganic oxide.
  • the platinum group element on the heat-resistant inorganic oxide it can be preferably prepared by the following method. Basically, a heat-resistant inorganic oxide is added to the solution containing the platinum group element source. After contact, dry by any method and force baked.
  • a desired amount of platinum group element supported Activated alumina is brought into contact with a solution to which an appropriate amount of a platinum group element source is added so that a surface layer of the active alumina is directly supported on the surface of the active alumina, and then dried by any method to remove moisture. And then firing.
  • an inorganic acid such as hydrochloric acid, sulfuric acid or nitric acid, or an organic acid such as acetic acid or oxalic acid may be added to the solution according to the purpose of improving solubility or adjusting pH.
  • the supporting method at this time is not particularly limited, but the impregnation method is preferred.
  • the conditions at the time of contact can also be changed suitably.
  • the contact operation can be performed under normal pressure or reduced pressure.
  • the temperature at the time of contact is not particularly limited, and it may be heated as necessary. Preferably, the temperature may be within the range of room temperature to 90 ° C.
  • a solution containing a platinum group element source may be separately prepared, and the solution may be sequentially contacted with a heat-resistant inorganic oxide.
  • the firing conditions are not particularly limited, for example, firing may be performed in air or in a reducing atmosphere, for example, by firing for about 2 to 6 hours in the range of 300 to 600 ° C.
  • a refractory inorganic oxide carrying a platinum group element is obtained.
  • the platinum group element may be supported on all or part of the refractory inorganic oxide.
  • the platinum group element is supported on all or part of the activated alumina.
  • the obtained activated alumina carrying the platinum group element is mixed with the remaining activated alumina in a pulverizer such as a ball mill. It is preferable to prepare the slurry by feeding and wet grinding.
  • a fire-resistant inorganic oxide is supplied to a pulverizer such as a ball mill, and a slurry is prepared by wet pulverization.
  • a monolith carrier is brought into contact with the slurry obtained in (1), and then dried and fired.
  • a platinum group element is formed on the surface of the monolithic carrier coated with a refractory inorganic acid. After supporting by chemical adsorption, it is dried and fired.
  • the platinum group element can be present in the surface layer of the coating layer by a chemical adsorption method.
  • the distribution position of the platinum group element in the coating layer can be adjusted by adjusting the pH of the solution during chemical adsorption.
  • the method for coating the surface of the monolithic carrier with the refractory inorganic oxide may be performed in the same manner as in Method 1.
  • Platinum is concentrated and firmly applied to the surface of the refractory inorganic oxide coating layer by supporting the platinum group element by chemical adsorption on the surface of the monolith support coated with the refractory inorganic oxide.
  • Group elements can be supported.
  • Method 3 is more preferable than Method 1 or Method 2 because the catalyst production method is simple and platinum group elements can be intensively supported in the region of several / zm from the surface of the coating layer. It is a manufacturing method.
  • chemisorption As a specific means of chemisorption, when a monolith support coated with a refractory inorganic oxide is impregnated in a heated state containing a solution containing a platinum group element, chemisorption is efficiently performed.
  • the platinum group element is unevenly distributed and supported on the surface of the refractory inorganic oxide coating layer. Specifically, it is preferable to heat a solution containing a platinum group element to 40 ° C or higher.
  • the temperature at which the solution containing the platinum group element is heated is more preferably 50 ° C or higher, more preferably 60 ° C or higher, more preferably 70 ° C or higher, further preferably 80 ° C or higher, and more preferably 90 ° C. That's it. If the temperature of the solution containing the platinum group element is too low, the platinum group element may not be unevenly distributed in the outer layer of the coating layer where chemisorption hardly occurs.
  • the distribution of platinum group elements in the coating layer can be confirmed by performing cross-sectional line analysis of the platinum group elements using EPMA (Electron Probe Micro Analyzer) (Electron Probe Micro Analyzer). .
  • a mixed gas containing a hydrocarbon-containing gas and an oxygen-containing gas is brought into contact with the catalyst of the present invention as a reaction gas, and the hydrocarbon is partially oxidized to produce hydrogen. It is characterized by producing a contained gas.
  • the reaction gas used in the production method of the present invention is a mixed gas containing a hydrocarbon-containing gas and an oxygen-containing gas.
  • the hydrocarbon-containing gas is not particularly limited, but light hydrocarbons such as methane, propane, butane, pentane and hexane; petroleum hydrocarbons such as gasoline, kerosene and naphtha; Etc. can be used.
  • natural gas or liquefied natural gas mainly composed of methane city gas mainly composed of this liquid natural gas
  • LPG liquid petroleum gas
  • propane and butane It is preferable because of its abundant resources and easy availability.
  • various synthetic liquid fuels such as methanol or dimethyl ether starting from natural gas, and biogas mainly composed of methane are also favored for effective use of resources.
  • the catalyst of the present invention When the catalyst of the present invention is used, it is not always necessary to remove sulfur even if the hydrocarbon-containing gas contains sulfur. Since the catalyst of the present invention has excellent durability against a catalyst poison component such as sulfur, the performance of the catalyst is hardly deteriorated by the catalyst poison component even if it is used for a long time. Therefore, when the catalyst of the present invention is used, it is desirable to have a viewpoint of cost and maintenance that does not require a device for removing a catalyst poison component, for example, a desulfurization device. However, since cheap natural gas can be used as the hydrocarbon-containing gas as it is, the manufacturing cost can be reduced.
  • the oxygen-containing gas used in the production method of the present invention is not particularly limited as long as it contains oxygen, and oxygen gas, air, or a gas obtained by diluting oxygen with another gas can be used. . From an economical viewpoint, it is preferable to use air.
  • the mixed gas can contain other gases.
  • the other gas include water vapor.
  • a continuous flow method (a method in which a reaction gas is continuously brought into contact with a catalyst) is preferable as a reaction method.
  • hydrocarbon-containing gas and oxygen The mixed gas with the contained gas (or oxygen gas) is brought into contact with the catalyst, but the mixed gas mixture ratio (oxygen molecule Z carbon atom ratio) is preferably 0.45 to 0.8, more preferably 0.48. Adjusted within the range of ⁇ 0.65. If the mixing ratio force of the mixed gas is within this range, an efficient partial acid-acid reaction can be performed.
  • the water molecule Z carbon atom ratio is preferably 0.1 to 5.0, more preferably 0. It is in the range of 5 to 3.0. If the water molecule Z-carbon atom ratio is less than 0.1, the effect of adding water vapor may not appear. On the other hand, if the water molecule Z carbon atom ratio exceeds 5.0, the self-sustaining self-supporting reaction may not be performed.
  • the pressure during the partial oxidation reaction is preferably in the range of normal pressure to 5 MPa'G, more preferably normal pressure to 3MPa'G.
  • the SV (gas space velocity) during the partial acid-acid reaction can be arbitrarily selected. More preferably ⁇ 10, 000-300, in the range of OOOHr _ 1.
  • the maximum temperature of the catalyst layer is preferably 600 to: L 100 ° C, more preferably 700 to 1000 ° C, and further preferably. It is desirable to appropriately adjust the reaction conditions so that the temperature is in the range of 700 to 950 ° C.
  • oxygen-containing gas or oxygen gas
  • water vapor may be added to the hydrocarbon-containing gas and then introduced into the catalyst layer, or may be introduced separately from the hydrocarbon-containing gas into the catalyst layer. A little.
  • the preheating temperature varies depending on the type of hydrocarbon, the composition of the reaction gas, the reaction conditions, etc. Generally, it is heated to 200 to 700 ° C, preferably 300 to 600 ° C. Just do it. After the reaction starts in the catalyst layer, the temperature of the catalyst layer rises due to the heat of reaction, and the reaction becomes self-supporting, so the reaction gas need not be preheated. Of course, preheating of the reaction gas may be continued as necessary in consideration of the thermal tolerance of the entire reaction system.
  • the catalyst layer is generally heated to 200 to 700 ° C, preferably 300 to 600 ° C, prior to the introduction of the reaction gas. Stop heating.
  • Carrier Cordierite knives-cam carrier (manufactured by NGK) having 400 cells per square inch in cross-sectional area was cut into an outer diameter of 25.4 mm and a length of 77 mm (carrier volume: 39. OmL) to obtain a carrier.
  • Activated alumina supporting platinum group element (for inner layer of coating layer): Mixing nitric acid aqueous solution of dinitrodiammine platinum containing 1.20 g of platinum and rhodium nitrate aqueous solution containing 0.24 g of rhodium. The resulting solution was impregnated with activated alumina (150 g) having a specific surface area of 105 m 2 / g, and then dried at 150 ° C. for 15 hours to remove moisture. After drying, the obtained powder was calcined in air at 400 ° C for 2 hours.
  • Activated alumina carrying platinum group element (for outer layer part of coating layer): Solution of nitric acid solution of dinitrodiammine platinum containing 1.80g of platinum and nitric acid solution of nitric acid containing 0.36g of rhodium Further, after impregnating and mixing activated alumina (150 g) having a specific surface area of 105 m 2 Zg, it was dried at 150 ° C. for 15 hours to remove moisture. After drying, the obtained powder was calcined in air at 400 ° C for 2 hours.
  • activated alumina carrying a platinum group element (for the outer layer portion of the coating layer) was made into an aqueous slurry by the same method, and the same operation was repeated using this slurry to obtain the catalyst of Catalyst Preparation Example 1.
  • the obtained catalyst was coated with 253 g of catalyst component per liter of support, and the platinum group element content was 3. Og (platinum: 2.5 g, rhodium: 0.5 g) per liter of support. there were.
  • the mass ratio of the platinum group element content in the outer layer portion and the inner layer portion of the coating layer was 60:40.
  • Activated alumina supporting platinum group element for inner layer of coating layer: A solution of dinitrodiammine platinum aqueous solution containing 0.6 g of platinum and rhodium nitrate aqueous solution containing 0.12 g of rhodium. Activated alumina (150 g) having a specific surface area of 105 m 2 / g was impregnated and mixed, and then dried at 150 ° C. for 15 hours to remove moisture. After drying, the obtained powder was calcined in air at 400 ° C for 2 hours.
  • Activated alumina carrying platinum group element (for outer layer part of coating layer): Solution of nitric acid solution of dinitrodiammine platinum containing 2.40g of platinum and nitric acid solution of nitric acid containing 0.48g of rhodium Further, after impregnating and mixing activated alumina (150 g) having a specific surface area of 105 m 2 Zg, it was dried at 150 ° C. for 15 hours to remove moisture. After drying, the obtained powder was calcined in air at 400 ° C for 2 hours.
  • the obtained catalyst was coated with 253 g of catalyst component per liter of support, and the platinum group element content was 3. Og (platinum: 2.5 g, rhodium: 0.5 g) per liter of support. there were. Ma The mass ratio of the platinum group element content in the outer layer portion and the inner layer portion of the coating layer was 80:20.
  • Activated alumina carrying platinum group elements Activated alumina with a specific surface area of 105 m 2 / g in a mixture of nitric acid aqueous solution of dinitrodiammine platinum containing 1.50 g of platinum and rhodium nitrate aqueous solution containing 0.30 g of rhodium (150 g) was impregnated and mixed, and then dried at 150 ° C. for 15 hours to remove moisture. After drying, the obtained powder was fired in air at 400 ° C for 2 hours.
  • the obtained catalyst was coated with 253 g of catalyst component per liter of support, and the platinum group element content was 3. Og (platinum: 2.5 g, rhodium: 0.5 g) per liter of support. there were.
  • the platinum group element was uniformly distributed in the coating layer, and the mass ratio of the platinum group element content in the outer layer portion and the inner layer portion of the coating layer was 50:50.
  • Coating of refractory inorganic oxide on monolith support 100 g of active alumina having a specific surface area of 105 m 2 Zg, pure water and acetic acid were supplied to a ball mill, and wet pulverized to prepare an aqueous slurry. After the carrier used in Catalyst Preparation Example 1 was immersed in this slurry and adhered to the slurry, the slurry was taken out, and then compressed air was blown onto this carrier to remove excess slurry remaining in the cell. After drying with C to attach the catalyst component to the support, the catalyst component was firmly coated on the support by baking in air (500 ° C.) for 1 hour. The carrier coated with the refractory inorganic oxide was further immersed in the slurry, and the same operation was repeated. When the mass was measured, 250 g of refractory inorganic oxide per liter of support was coated on the monolith support.
  • the obtained catalyst was coated with 253 g of catalyst component per liter of support, and the platinum group element content was 3. Og (platinum: 2.5 g, rhodium: 0.5 g) per liter of support. there were.
  • the mass ratio of the platinum group element content in the outer layer portion and the inner layer portion of the coating layer was 90:10.
  • the platinum group element was 70% by mass of the total content in the region from the surface of the coating layer to 5 ⁇ m.
  • Catalyst Preparation Example 3 the catalyst of Catalyst Preparation Example 4 was obtained in the same manner as Catalyst Preparation Example 3, except that the temperature of the aqueous solution containing the platinum group element was maintained at 90 ° C.
  • the obtained catalyst was coated with 253 g of catalyst component per liter of support, and the platinum group element content was 3. Og (platinum: 2.5 g, rhodium: 0.5 g) per liter of support. there were.
  • the mass ratio of the platinum group element content in the outer layer portion and the inner layer portion of the coating layer was 99: 1.
  • Fig. 1 shows an EPMA cross-sectional analysis graph of platinum and rhodium.
  • the platinum group element was present in a total content of 88 mass o / o in the region from the surface of the coating layer to 5 ⁇ m.
  • Coating of monolithic carrier with refractory inorganic oxides active alumina with specific surface area of 105 m 2 Zg 80.12 g of alumina, cerium oxide with specific surface area of 70 m 2 Zg 19. 88 g of pure water and acetic acid are fed to the ball mill, An aqueous slurry was prepared by wet grinding. A monolithic support was coated with a refractory inorganic acid oxide containing activated alumina and cerium oxide in the same manner as in Catalyst Preparation Example 3 except that this slurry was used. When the mass was measured, 250 g of refractory inorganic oxide per 1 L of the carrier was coated on the monolithic carrier.
  • the obtained catalyst was coated with 251.5 g of catalyst component per liter of support, and the content of platinum group element was 1.5 g (platinum: 1.25 g, rhodium: 0. 25g). Further, the mass ratio of activated alumina to cerium oxide in the catalyst component was 100: 25. As a result of EPMA cross-sectional analysis of platinum and rhodium, the mass ratio of the platinum group element content in the outer layer portion and the inner layer portion of the coating layer was 99: 1. In addition, the platinum group element was present in an area of 91% by mass of the total content from the surface of the coating layer to 5 ⁇ m.
  • cerium-zirconium composite oxide Cerium carbonate powder was calcined at 400 ° C for 2 hours and then pulverized to obtain cerium oxide powder. To this cerium oxide powder, an aqueous solution of zirconium oxynitrate was added so as to have a mass ratio of cerium oxide: zirconium oxide of 100: 20 and mixed uniformly. The obtained mixed slurry was dried at 120 ° C. to remove water, and then baked in air at 500 ° C. for 1 hour to prepare a cerium-zirconium composite oxide.
  • a catalyst of Catalyst Preparation Example 6 was obtained in the same manner as in Catalyst Preparation Example 5 except that the monolith support coated with the above refractory inorganic oxide was used. [0102] The obtained catalyst was coated with 251.5 g of catalyst component per liter of support, and the content of platinum group element was 1.5 g (platinum: 1.25 g, rhodium: 0. 25g). Further, the mass ratio of activated alumina to cerium oxide in the catalyst component was 100: 25. The mass ratio of cerium oxide to zirconium oxide in the catalyst component was 100: 20.
  • the mass ratio of the platinum group element content in the outer layer portion and the inner layer portion of the coating layer was 99: 1.
  • 92% by mass of the platinum group element was present in the region up to 5 m from the surface of the catalyst component coating layer.
  • Each catalyst was cut into a size of 7 mm in length, 7 mm in width, and 10 mm in length, and filled in an Inconel reaction tube kept warm with a refractory.
  • a chromel-alumel (K) metal sheath thermocouple (outer diameter 1 mm) was inserted into the catalyst layer, and the temperature of the catalyst layer was measured.
  • Tosu Gas 13A was used as a hydrocarbon-containing gas without being desulfurized.
  • air was used as the oxygen-containing gas, and a mixed gas prepared so that the oxygen molecule Z carbon atom ratio was 0.52Z1 was used as the reaction gas.
  • the preheating temperature of the reaction gas was set to 250 ° C, and it was supplied to the catalyst layer at a space velocity (STP) of 370, OOOHr- 1 , to carry out a partial oxidation reaction.
  • STP space velocity
  • the generated gas was analyzed using gas chromatography (Gas Chromatography GC—8A, manufactured by Shimadzu Corporation), and the conversion rate of the raw material at the beginning of the reaction (after 3 hours from the start of the reaction) and after 100 hours had elapsed I asked for it. The results are shown in Table 1.
  • the catalyst of Comparative Catalyst Preparation Example 1 is a catalyst in which platinum group elements are uniformly distributed in the coating layer.
  • the catalyst of Catalyst Preparation Example 14 is a catalyst in which the outer layer portion of the coating layer has a substantially higher platinum group element content than the inner layer portion of the coating layer.
  • the catalysts of Catalyst Preparation Examples 1 to 4 are less deteriorated in the conversion rate of the raw material after 100 hours than the catalyst of Comparative Catalyst Preparation Example 1 and are durable. It turns out that it is excellent in property.
  • the higher the platinum group element content in the outer layer portion of the coating layer the higher the initial raw material conversion rate and the higher the raw material conversion rate after 100 hours. It can be seen that the decrease is decreasing and the durability is further improved. Furthermore, the maximum temperature of the catalyst layer is also reduced as the platinum group element content in the outer layer portion of the coating layer is higher. This is a heat that reduces the thermal load of the catalysts in Catalyst Preparation Examples 1 to 4. Suggests that the sintering of the catalyst is significantly suppressed
  • the catalysts of catalyst preparation examples 3 and 4 in which platinum group elements are concentrated unevenly on the surface of the coating layer by chemisorption are platinum present in the region up to 5 m from the surface of the coating layer.
  • the group element content is 70% by mass or more and has particularly excellent durability.
  • Each catalyst was cut into a size of 7 mm in length, 7 mm in width, and 10 mm in length, and filled in an Inconel reaction tube kept warm with a refractory.
  • a chromel-alumel (K) metal sheath thermocouple (outer diameter 1 mm) was inserted into the catalyst layer, and the temperature of the catalyst layer was measured.
  • Tosu Gas 13A was used as a hydrocarbon-containing gas without being desulfurized.
  • air was used as the oxygen-containing gas, and a mixed gas prepared so that the oxygen molecule Z carbon atom ratio was 0.52Z1 was used as the reaction gas.
  • the preheating temperature of the reaction gas was set to 250 ° C, and it was supplied to the catalyst layer at a space velocity (STP) of 370, OOOHr- 1 , to conduct a partial oxidation reaction.
  • STP space velocity
  • the raw material conversion rate at the beginning of the reaction (after 3 hours from the start of the reaction) was analyzed in the same manner as in Example 1. After that, the supply amount of city gas 13A is kept constant, the air supply amount is increased, and the oxygen molecule Z carbon source is increased.
  • the reaction gas prepared so that the child ratio was 0.70Z1 was set to a preheating temperature of 250 ° C and supplied to the catalyst. After 200 hours, the oxygen molecule Z carbon atom ratio was returned to 0.52Z1, and the raw material conversion after 3 hours was analyzed. The results are shown in Table 2.
  • the catalyst of Catalyst Preparation Example 5 is a catalyst containing cerium oxide in addition to activated alumina as a refractory inorganic oxide, but the catalyst of Preparation Example 4 in which the refractory inorganic oxide is only activated alumina.
  • the total platinum group element content is half that of the catalyst, as shown in Table 2, the decrease in the raw material conversion rate is small, and the maximum temperature of the catalyst layer is also low. It turns out that it has sex. Further, it can be seen that the durability of the catalyst of Catalyst Preparation Example 6 containing cerium oxide as cerium-zirconium composite oxide is further improved.
  • the catalyst of Catalyst Preparation Example 6 (outer diameter 25.4 mm x length 77 mm) was filled into a reactor with a material tube of S Inconel with a refractory for heat insulation, and an evaluation test of partial oxidation reaction was conducted. I went. City gas 13A was used as the hydrocarbon-containing gas, and a mixed gas prepared using air as the oxygen-containing gas so that the oxygen molecule Z carbon atom ratio was 0.54Z1 was used as the reaction gas.
  • the reaction gas was supplied to the reactor, and when the temperature of the reaction gas reached 250 ° C, the start of the reaction in the catalyst layer was confirmed, so heating of the reaction gas was stopped.
  • the temperature of the catalyst layer during the reaction was stable at about 855 ° C.
  • the components of the resulting product gas were analyzed in the same manner as in Example 1 using gas chromatography. The raw material conversion was 88% and the hydrogen selectivity was 91%.
  • the catalyst of the present invention is a catalyst for partial acid with little deterioration in performance over a long period of time even when the content of the platinum group element, which is a catalytically active component, is reduced, and is the main catalyst obtained by the production method of the present invention.
  • hydrogen and a hydrogen-containing gas having carbon monoxide can be used as fuel for fuel cells and as raw materials for the chemical industry.
  • molten carbonate type fuel cells and solid oxide type fuel cells which are classified into high-temperature operation types, can use carbon monoxide and hydrocarbons as fuel in addition to hydrogen. It is also desirable to use the hydrogen-containing gas obtained by the catalyst of the present invention or the production method of the present invention for these fuel cells.
  • a high-temperature operation type fuel cell is capable of performing a partial acid-oxidation reaction of hydrocarbons in the cell (internal reforming) by the catalytic action of an electrode.
  • problems such as carbon deposition occur depending on the type of hydrocarbon and the impurities contained in the hydrocarbon, so the entire amount of hydrocarbon may not be internally reformed. Therefore, it is necessary to pre-treat the hydrocarbon before introducing the hydrocarbon into the fuel cell, but pre-reforming can also be suitably performed using the catalyst of the present invention.
  • the catalyst of the present invention can easily start the partial acid-acid reaction by preheating the reaction gas or heating the catalyst layer. It is also suitable as a start-up catalyst for supplying a reducing gas.
  • the hydrogen-containing gas obtained by the partial oxidation reaction using the catalyst of the present invention can be reduced in the carbon monoxide concentration by the Saraco CO modification reaction, the cryogenic separation method, PSA method, hydrogen storage alloy
  • high purity hydrogen gas can be obtained by removing impurities by a palladium membrane diffusion method or the like.
  • reducing the carbon monoxide contained in hydrogen-containing gas water vapor is added to the hydrogen-containing gas obtained by the partial oxidation reaction (or without addition), and the CO modification reaction is carried out in a monoxide-carbon denaturer to convert monoxide-carbon into carbon dioxide gas. Convert to.
  • the catalyst used in the CO modification reaction for example, a known catalyst mainly composed of copper or iron may be used.
  • carbon monoxide concentration is reduced by CO modification reaction.
  • carbon monoxide poisons the electrocatalytic action used in low-temperature, solid polymer fuel cells. Therefore, in order to avoid such poisoning of the catalyst, it is desirable to set the carbon monoxide concentration to 10 ppm or less. In order to reduce the carbon monoxide concentration to 10 ppm or less, for example, a small amount of oxygen may be added to the gas after the CO modification reaction to selectively remove carbon monoxide and carbon.

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Abstract

L’invention concerne un catalyseur d'oxydation partielle destiné à la modification d’hydrocarbures, ledit catalyseur comportant une couche d’un composant catalytique contenant un élément du groupe du platine et un oxyde inorganique résistant au feu, ladite couche étant enduite sur un support moulé. Le catalyseur d’oxydation partielle est caractérisé en ce que la teneur en élément du groupe du platine est substantiellement plus élevée dans la partie externe de la couche de revêtement que dans la partie interne de la couche de revêtement. L’invention concerne également un procédé de fabrication d’un gaz contenant de l’hydrogène à partir d’un hydrocarbure en utilisant un tel catalyseur. Le catalyseur présente une activité importante et une durabilité à long terme élevée, même avec une faible teneur en élément du groupe du platine.
PCT/JP2006/320300 2005-10-12 2006-10-11 Catalyseur pour oxydation partielle d’hydrocarbures WO2007043571A1 (fr)

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JP2011088778A (ja) * 2009-10-22 2011-05-06 Jx Nippon Oil & Energy Corp 水素製造装置および燃料電池システム
JP5788348B2 (ja) * 2011-03-22 2015-09-30 Ｊｘ日鉱日石エネルギー株式会社 水素製造用改質触媒、該触媒を用いた水素製造装置及び燃料電池システム
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BR102017021428B1 (pt) * 2017-10-05 2022-04-19 Petróleo Brasileiro S.A. - Petrobras Processo para preparação de um catalisador de pré-reforma
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JP2003326166A (ja) * 2002-05-09 2003-11-18 Boc Group Inc:The 金属触媒及びその調製方法と使用方法
JP2004230312A (ja) * 2003-01-31 2004-08-19 Idemitsu Kosan Co Ltd 炭化水素の改質用触媒
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