WO2000078669A1 - Fuel processor for producing hydrogen and apparatus suitable for use in such processor - Google Patents
Fuel processor for producing hydrogen and apparatus suitable for use in such processor Download PDFInfo
- Publication number
- WO2000078669A1 WO2000078669A1 PCT/NL2000/000364 NL0000364W WO0078669A1 WO 2000078669 A1 WO2000078669 A1 WO 2000078669A1 NL 0000364 W NL0000364 W NL 0000364W WO 0078669 A1 WO0078669 A1 WO 0078669A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- gas stream
- mixture
- shift
- fuel processor
- water
- Prior art date
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- 239000000446 fuel Substances 0.000 title claims abstract description 75
- 239000001257 hydrogen Substances 0.000 title claims abstract description 31
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 31
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 239000007789 gas Substances 0.000 claims abstract description 128
- 239000000203 mixture Substances 0.000 claims abstract description 127
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 83
- 229910001868 water Inorganic materials 0.000 claims abstract description 69
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000001301 oxygen Substances 0.000 claims abstract description 17
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 17
- 239000003054 catalyst Substances 0.000 claims description 89
- 229910002830 PrOx Inorganic materials 0.000 claims description 24
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 17
- 230000001105 regulatory effect Effects 0.000 claims description 11
- 238000007084 catalytic combustion reaction Methods 0.000 claims description 8
- 238000013461 design Methods 0.000 claims description 8
- 238000005485 electric heating Methods 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 239000003345 natural gas Substances 0.000 claims description 2
- 239000006096 absorbing agent Substances 0.000 claims 2
- 238000004140 cleaning Methods 0.000 claims 1
- 230000003647 oxidation Effects 0.000 abstract description 9
- 238000007254 oxidation reaction Methods 0.000 abstract description 9
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 7
- 229930195733 hydrocarbon Natural products 0.000 abstract description 7
- 230000003197 catalytic effect Effects 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract 1
- 238000009738 saturating Methods 0.000 abstract 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 38
- 229910002091 carbon monoxide Inorganic materials 0.000 description 38
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 23
- 238000006243 chemical reaction Methods 0.000 description 18
- 238000000034 method Methods 0.000 description 15
- 239000010949 copper Substances 0.000 description 13
- 230000008569 process Effects 0.000 description 11
- 239000000463 material Substances 0.000 description 9
- 230000000694 effects Effects 0.000 description 8
- 229910052751 metal Inorganic materials 0.000 description 8
- 239000002184 metal Substances 0.000 description 8
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 7
- 238000010438 heat treatment Methods 0.000 description 7
- 229910052697 platinum Inorganic materials 0.000 description 7
- 239000010457 zeolite Substances 0.000 description 7
- 229910021536 Zeolite Inorganic materials 0.000 description 6
- 230000004913 activation Effects 0.000 description 6
- 230000002211 methanization Effects 0.000 description 6
- 230000009467 reduction Effects 0.000 description 6
- 229910052802 copper Inorganic materials 0.000 description 5
- 230000007423 decrease Effects 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000011248 coating agent Substances 0.000 description 4
- 238000000576 coating method Methods 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 239000008188 pellet Substances 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 3
- 239000011358 absorbing material Substances 0.000 description 3
- 238000001354 calcination Methods 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000000919 ceramic Substances 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 239000012691 Cu precursor Substances 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- QDOXWKRWXJOMAK-UHFFFAOYSA-N dichromium trioxide Chemical compound O=[Cr]O[Cr]=O QDOXWKRWXJOMAK-UHFFFAOYSA-N 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- SZVJSHCCFOBDDC-UHFFFAOYSA-N ferrosoferric oxide Chemical compound O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 238000005470 impregnation Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- KRKNYBCHXYNGOX-UHFFFAOYSA-K Citrate Chemical compound [O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O KRKNYBCHXYNGOX-UHFFFAOYSA-K 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- -1 Ru and Rh Chemical class 0.000 description 1
- KPAMAAOTLJSEAR-UHFFFAOYSA-N [N].O=C=O Chemical compound [N].O=C=O KPAMAAOTLJSEAR-UHFFFAOYSA-N 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 239000012876 carrier material Substances 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 238000000975 co-precipitation Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24D—DOMESTIC- OR SPACE-HEATING SYSTEMS, e.g. CENTRAL HEATING SYSTEMS; DOMESTIC HOT-WATER SUPPLY SYSTEMS; ELEMENTS OR COMPONENTS THEREFOR
- F24D12/00—Other central heating systems
- F24D12/02—Other central heating systems having more than one heat source
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01B—BOILING; BOILING APPARATUS ; EVAPORATION; EVAPORATION APPARATUS
- B01B1/00—Boiling; Boiling apparatus for physical or chemical purposes ; Evaporation in general
- B01B1/005—Evaporation for physical or chemical purposes; Evaporation apparatus therefor, e.g. evaporation of liquids for gas phase reactions
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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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/80—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with zinc, cadmium or mercury
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- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
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- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/082—X-type faujasite
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- B01J8/0492—Feeding reactive fluids
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- B01J8/0496—Heating or cooling the reactor
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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
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
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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
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- C—CHEMISTRY; METALLURGY
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
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- C—CHEMISTRY; METALLURGY
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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
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- 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
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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
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- 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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- 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
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- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
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- 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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
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- F24D18/00—Small-scale combined heat and power [CHP] generation systems specially adapted for domestic heating, space heating or domestic hot-water supply
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F24D2101/00—Electric generators of small-scale CHP systems
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
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- F24D2200/00—Heat sources or energy sources
- F24D2200/02—Photovoltaic energy
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24H—FLUID HEATERS, e.g. WATER OR AIR HEATERS, HAVING HEAT-GENERATING MEANS, e.g. HEAT PUMPS, IN GENERAL
- F24H2240/00—Fluid heaters having electrical generators
- F24H2240/10—Fluid heaters having electrical generators with fuel cells
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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
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
- H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
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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
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- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B10/00—Integration of renewable energy sources in buildings
- Y02B10/70—Hybrid systems, e.g. uninterruptible or back-up power supplies integrating renewable energies
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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
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- 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
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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
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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
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- 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 invention relates to a fuel processor for producing a gas stream which comprises hydrogen through catalytic combustion of a mixture which: comprises at least one gaseous hydrocarbon compound, water vapor and oxygen, the fuel processor comprising a gas stream path along which the mixture is passed and a CPO catalyst included in the gas stream path, to which the mixture is supplied for the catalytic combustion.
- CPO is understood herein to mean Catalyst Partial Oxidation.
- the invention also relates to an apparatus for generating from a first and second gas stream a third and fourth gas stream.
- a fuel processor of the type described in the opening paragraph is known per se.
- the hydrogen generated is often used to be supplied to a fuel cell which burns the hydrogen for generating electric energy and/or heat.
- the hydrogen generated by the fuel processor comprises as less carbon monoxide as possible, because this is detrimental to the proper operation of the fuel cell.
- the invention has, inter alia, for its object to provide a fuel processor which generates a gas stream with hydrogen which comprises less carbon monoxide than the known fuel processor.
- the fuel processor according to the invention is characterized in that in the gas stream path downstream of the CPO catalyst a plurality of series connected HT shifts are included through which, in use, the mixture leaving the CPO catalyst respectively flows. Because a plurality of series connected HT shifts are included, it has become possible to regulate per HT shift the temperature of the mixture flowing through the HT shifts. Thus the above amount of CO can be minimized.
- HT shift is understood herein to mean high-temperature shift catalyst.
- each HT shift is provided with two opposite sides which form respectively an inlet and an outlet of the HT shift, the HT shifts being arranged with respect to each other in a direction coinciding with the normal of the above sides of the HT shifts, an outlet of a first HT shift being located opposite an inlet of a second HT shift, and the second HT shift being included in a box-shaped chamber having a bottom and upright side walls, the bottom being located between the inlet of the second HT shift and the outlet of the first HT shift, and the gas stream path from the first HT shift to the second HT shift extending respectively along an outer side of the bottom of the box-shaped chamber, between the heat exchanger and an outer side of the upright side wall of the box-shaped chamber, between the second HT shift and an inner side of the upright side wall of the box-shaped chamber to a space located between the inner side of the bottom of the box-shaped chamber and the side of the second HT shift which comprises the inlet.
- the fuel processor may thus be of very compact design.
- each HT shift is included in a box-shaped chamber.
- each HT shift is of tubular design with two opposite open ends which form respectively the inlet and the outlet of the HT shift, axial axes of the HT shifts coinciding at least substantially with an axial axis of the tubular inner wall of the heat exchanger.
- the heat exchanger is further provided with a tubular insulating outer wall which has a heat insulating function.
- an LT shift located downstream of the HT shifts is included in the gas stream path, the fuel processor further being provided with an inlet for, in use, adding water to the mixture supplied to the LT shift for cooling the mixture.
- LT shift is understood herein to mean low-temperature shift catalyst.
- the processor may further be provided with means for adding water in the form of steam.
- the inlet comprises atomizing means for adding the water in atomized condition. This has a very favorable effect on the efficiency.
- the LT shift comprises a tubular insulating outer wall and a tubular insulating inner wall which are arranged concentrically with respect to each other, the mixture, in use, flowing through the space formed between the tubular insulating inner wall and the tubular insulating outer wall, and the HT shifts and the CPO catalyst being included in a space enclosed by the tubular insulating inner wall.
- the fuel processor is of very compact design. In that case the heat flows are particularly directed in a radial direction from the inside to the outside, while the flow of the mixture is directed at least substantially in axial direction.
- the tubular insulating outer wall of the heat exchanger coincides with the tubular insulating inner wall of the LT shift.
- the processor is further provided with a PrOx located in the gas stream path downstream of the LT shift as well as an inlet for adding oxygen to the mixture that has left the LT shift and flows to the PrOx.
- the processor is further provided with a vessel which is filled with water and/or through which water flows, to which vessel, furthermore, the gaseous hydrocarbon compound and oxygen are supplied to be passed through and/or along the water to generate the above mixture supplied to the CPO catalyst, and means for regulating the temperature of the water to adjust the concentration of the water vapor in the mixture supplied to the CPO catalyst. Because water has been supplied to the mixture, more hydrogen is formed per mole of the gaseous hydrocarbon compound in the mixture than when the mixture would comprise only gaseous hydrocarbon and oxygen (air).
- the processor may further be provided with a heat exchanger for exchanging heat between the mixture which has flown through the PrOx and the water contained in the vessel so that the temperature of the mixture forming the gas stream comprising hydrogen falls.
- a heat exchanger is included to further cool the mixture.
- the invention also relates to a fuel processor of the type described in the opening paragraph, which is characterized in that the processor is further provided with a vessel which is filled with water, to which vessel the gaseous hydrocarbon compound and oxygen are supplied to be passed through and/or along the water to generate the above mixture and means for regulating the temperature of the water to adjust the concentration of the water vapor in the mixture.
- the apparatus for the apparatus for generating from a first and second gas stream the third and fourth gas stream it holds according to the mvention that the third gas stream comprises a mixture of the first and second gas stream
- the apparatus being provided with a chamber enclosing a space in which a ventilator is included, the chamber being provided with a first and second inflow opening for, in use, supplying the first and second gas stream to respectively the first and second inflow opening and a first and second outflow opening, the first and second gas stream, in use, being sucked in by the ventilator and being supplied, separated from each other in the chamber, to respectively a first and second outflow opening, the first outflow opening discharging directly into a first outlet, and the second outflow opening discharging into the first outlet and a second outlet via a bifurcation, a controllable valve being included in the first and/or second outlet to adjust the ratio of the amount of gas originating from the first and second gas stream in the third gas stream from the first outlet, the fourth gas stream comprising a part
- Such an apparatus has the advantage that by means of one ventilator two gas streams can be pressurized. Moreover, the size of the two gas streams is regulated (modulated) in a similar ratio through a corresponding regulation (modulation) of the rotational speed of the ventilator.
- the chamber comprises a cylindrical outer wall which encloses a cylindrical space, the ventilator being designed as a wheel, of which an axis of rotation coincides with an axial axis of the chamber, the wheel on both sides being provided near its circumferential edge with blades, and the first gas stream extending on a first side of the wheel where the blades are, the second gas stream extending on a second side of the wheel where the blades are.
- first and second inflow opening are provided in the cylindrical outer wall of the chamber in axial direction of the chamber in a staggered position, the first inflow opening and the first outflow opening being arranged at least substantially in a similar plane directed perpendicularly to the axial axis of the chamber, and the second inflow opening and the second outflow opening being arranged at least substantially in a similar plane directed perpendicularly to the axial axis of the chamber.
- the chamber is provided with two opposite side walls directed perpendicularly to the axial axis of the chamber, the first side wall comprising a first circular groove extending around the axial axis, in which the first inflow and outflow opening is included, and the second side wall comprising a second circular groove extending around the axial axis, in which the second inflow and outflow opening is included, and the blades of the wheel extending respectively along the first and second groove.
- the first gas stream consists of a mixture of air and a gaseous hydrocarbon compound and the second gas stream consists of air
- the third gas consists of a mixture of the first and second gas stream
- the fourth gas stream consists of a fraction of the second gas stream, the third gas stream being supplied to the gas stream path and the fourth gas stream being added to the mixture supplied to the PrOx.
- Fig. 1 shows a possible embodiment of a fuel processor according to the invention
- Fig. 2 shows the temperature curve along the gas stream path through the CPO catalyst, the HT shifts, the LT shift, and the PrOx of the fuel processor of Fig. 1;
- Fig 3 shows the temperature curve along the line of Fig. 1;
- Fig. 4 shows a part of the apparatus of Fig. 1
- Fig. 5A shows a first cross-section of an apparatus according to the invention which can advantageously form part of the fuel processor of Fig. 1;
- Fig. 5B shows a second cross-section of the apparatus of Fig. 5A.
- Fig. 6 shows an alternative embodiment of the vessel 6 of Fig. 1.
- reference numeral 1 denotes a fuel processor for producing a gas stream comprising hydrogen.
- the fuel processor is of a type which generates hydrogen through catalytic treatment of a mixture which comprises at least one gaseous hydrocarbon compound, water vapor and oxygen.
- the mixture is passed along a gas stream path for the combustion of the relevant mixture.
- the apparatus is provided with a vessel 2 filled with water (H 2 O).
- the vessel 2 is provided with an inlet 4, to which the gaseous hydrocarbon, in this example CH , and oxygen, in this example air, is supplied.
- the gaseous hydrocarbon and oxygen are thus injected at the bottom of the vessel 2 and will bubble up through the water 6 contained in the vessel.
- the fuel processor is provided with means 10 for regulating the temperature of the water 6.
- the temperature of the water 6 also determines the temperature of the mixture 8.
- the temperature of the mixture 8 directly determines the amount of water vapor which is included in the mixture 8. The higher the temperature, the higher the degree of saturation of the mixture with water.
- the resulting mixture 8 is passed from an outlet 9 of the vessel 2 along a gas stream path for the catalytic combustion.
- this gas stream path contains, inter alia, a known per se CPO catalyst 11.
- This CPO catalyst is a catalyst, as also used for automobiles.
- a plurality of series connected HT shifts 16.1-16.3. This example relates to three series connected HT shifts. In use, the mixture leaving the CPO catalyst flows through these HT shifts.
- the mixture 8 supplied to the CPO catalyst causes the following reactions in the CPO catalyst: CH 4 + x 0 2 ⁇ C0 2 + s H 2 0 + Q (400 ⁇ 900°C) (1) CH 4 + -X H 2 0 ⁇ X CO + 3/2 H 2 - Q (900 ⁇ 700°C) (2) k CH 4 + % CO 2 ⁇ -> X CO + H 2 - Q (3)
- the vessel is provided with a water outlet 12 diagrammatically shown in Fig. 1 for supplying the water 6 from the vessel to an electric heating element 10.
- the resulting heated water is supplied via a line 14 to the vessel again.
- the heating element 10 the temperature of the water 6 in the vessel 2 can therefore be regulated.
- HT shifts 16.1-16.3 are included in the gas stream path downstream of the CPO catalyst 11 .
- This example relates to three series connected, known per se HT shifts.
- These HT shifts, too, consist of a known per se catalyst of the type also used for automobiles.
- the mixture leaving the CPO catalyst comprises, as discussed, an amount of carbon monoxide (see formula 2 and formula 3).
- this mixture is supplied to the first HT shift 16.1, the following reaction occurs in the HT shift 16.1:
- the advantage of the HT shift is therefore that the amount of CO in the mixture is reduced, while as by-product the CO 2 harmless to a fuel cell is generated.
- the reaction equilibrium of the reaction of formula 4 comes to lie such that the amount of CO is very low, respectively in the gas stream path between the CPO catalyst 11 and a nearest HT shift 16.1 located downstream of the CPO catalyst and between the mutual HT shifts (16.1-16.2; 16.2-16.3) heat exchangers are included, which exchange heat between, on the one hand, the mixture supplied to the CPO catalyst 11 and, on the other hand, the mixture which flows through the series connected HT shifts downstream of the CPO catalyst.
- the heat exchangers comprise a tubular inner wall 18, which encloses a space 20 in which the HT shifts are included.
- Each HT shift 16.1-16.3 is provided with two opposite sides which form respectively their inlet 22 and an outlet 24 of the HT shift.
- the HT shifts are arranged with respect to each other in a direction 26 coinciding with the normal of the above sides of the inlet and outlet 22, 24.
- An outlet 24 of a first HT shift 16.1 is located opposite an inlet 22 of a second HT shift 16.2. It further holds that the second HT shift 16.2 is included in a box-shaped chamber 28 having a bottom 30 and upright side walls 32.
- the bottom 30 is included between the inlet 22 of the second HT shift 16.2 and the outlet 24 of the first HT shift 16.1.
- the gas stream path from the first HT shift 16.1 to the second HT shift 16.2 extends respectively along an outer side of the bottom 30 of the box-shaped chamber 28, between the heat exchanger, i.e. the tubular inner wall 18 and an outer side of the upright side wall 32 of the box-shaped chamber 28, between the HT shift 16.2 and an inner side of the upright side wall 30 of the box-shaped chamber 28, to a space 34 located between the inner side of the bottom 30 of the box-shaped chamber 28 and the side of the second HT shift 16.2 which comprises the inlet 22.
- the first HT shift 16.1 and the third HT shift 16.3 are also provided with a box-shaped chamber 28.
- the gas stream path from the CPO catalyst to the inlet of the first HT shift 16.1 and the gas stream path from the outlet of the second HT shift 16.2 to the inlet of the third HT shift 16.3 is therefore quite analogous as discussed " in relation to the gas stream path from the outlet of the first HT shift 16.1 to the inlet of the second HT shift 16.2.
- each HT shift is of tubular design with two opposite open ends 22, 24, which form respectively the inlet and the outlet of the relevant HT shift.
- Axial axes of the HT shifts coincide at least substantially with an axial axis of the tubular inner wall 18 of the above heat exchanger.
- the relevant heat exchanger is further provided with a tubular insulating outer wall 36 which encloses the tubular inner wall 28 completely but with an interspace.
- the operation of the apparatus described thus far is as follows.
- the mixture 8 flowing into the vessel 2 will have a temperature of about
- Fig. 2 shows the temperature curve of the mixture flowing through respectively the CPO catalyst and HT shifts 16.1, 16.2 and 16.3. Plotted on the horizontal axis is the curve of the gas stream path 2 through the CPO catalyst and the HT shifts.
- the mixture Before the mixture flows into the CPO catalyst, the mixture will have a temperature of about 350-500°C (Fig. 2: 400°C).In the CPO catalyst the reactions of formula 1, 2, 3 and 4 occur. See curve A of Fig. 2. The mixture leaving the CPO catalyst will then have a temperature of about 685°C.
- the mixture flows from the CPO catalyst along the inner side of the inner wall 18 of the heat exchanger and has the result that it heats the mixture flowing on the outer side of the inner wall 18 from the vessel.
- the mixture flowing from the CPO catalyst to the inlet of the first HT shift 16.1 will correspondingly be cooled to, for instance, 575°C (see curve B).
- the mixture will therefore have a temperature which is lower than the temperature of the mixture at the outlet of the CPO catalyst.
- the temperature thereof will increase, as indicated by curve C in Fig. 2.
- the temperature rises again to, for instance, 580°C.
- a plurality of HT shifts are used, in which, for instance, the mixture leaving the first HT shift 16.1 is cooled by flowing along the inner side of the tubular inner wall 18 of the heat exchanger, which has the result that the mixture supplied to the inlet 22 of the second HT shift 16.2 has a lowered temperature of, for instance, 450° C.
- the temperature of the mixture will slowly rise again, as indicated by the curve 16.2 in Fig. 3.
- the mixture leaving the second HT shift 16.2 will be cooled again by flowing along the inner wall 18 of the heat exchanger, which has the result that the mixture supplied to the third HT shift 16.3 has a temperature of, for instance, 370°C.
- the mixture leaving the third HT shift 16.3 has a lower temperature (for instance 355°C), as indicated in Fig. 2 by the point P 2 ).
- the result is that in respect of the mixture leaving the third HT shift 16.3 the reaction equilibrium of the reaction of formula 4 has shifted such that the amount of CO is much less than would have been the case m the point Pi of Fig. 2.
- the processor further comprises measures, to be discussed below m more detail, for further shifting the reaction equilibrium, such that even less CO is contained in the mixture.
- the fuel processor is further provided with an LT shift 38 located downstream of the HT shifts
- the fuel processor is provided with an inlet 40 for, in use, adding water to the mixture supplied to the LT shift for cooling the mixture.
- the mixture leaving the HT shift 16.3 has, for instance, a temperature of 355°C. By supplying water vapor to the mixture via the inlet 40, this will be cooled.
- the following favorable shifting of the thermodynamic equilibrium position occurs:
- the processor may further be provided with means for adding the water via the inlet 40 in the form of steam.
- These means may, for instance, consist of a steam generator 42 comprising an electric heating unit, a hydrogen burner, or a natural gas burner and a heat exchanger.
- the inlet 40 comprises atomizing means for adding the water in atomized condition.
- the water in atomized condition may then have a temperature corresponding to room temperature. It is not necessary to heat water to steam. Instead thereof, the water may be supplied to the mixture after atomization without heating, i.e. without supplying extra energy, for cooling the mixture.
- cooling the mixture to, for instance, 180°C is indicated in Fig. 2 by curve E.
- the cooled mixture is thus supplied to the LT shift 38.
- the LT shift comprises a known per se catalyst material.
- the LT shift comprises a tubular (heat) insulating outer wall 44, and a tubular inner wall 36 which, in this example, coincides with the tubular (heat) insulating outer wall of the heat exchanger.
- the tubular outer wall and the tubular inner wall of the LT shift are arranged concentrically with respect to each other, the mixture, in use, flowing through the space formed between the tubular inner wall 36 and the tubular outer wall 44.
- cooling water 45 Located outside the outer wall 44 is cooling water 45 having a temperature of, for instance, 20-100°C. By heating up this cooling water will be partially converted into steam 47 which is supplied via a line 49 to the mixture 8 flowing through the outlet 9.
- the processor further comprises a known per se PrOx 46 located in the gas stream path downstream of the LT shift, as well as an inlet 48 for adding oxygen to the mixture which has left the LT shift and flows to the PrOx.
- the amount of CO will therefore further decrease in the PrOx.
- the temperature rises from about 100 to 110°C, as shown in Fig. 2 by the curve H.
- the mixture leaves the PrOx via the line 50.
- the final product of the fuel processor therefore flows, which final product consists of a gas stream comprising hydrogen, nitrogen carbon dioxide, and water vapor.
- the apparatus may further be provided with a fuel cell to which the hydrogen can be supplied via the line 50.
- the hydrogen is burned to generate electric energy and/or heat.
- a part of the hydrogen in line 50 is supplied via line 50' to the apparatus 42 when this " is designed as a hydrogen burner for obtaining steam supplied to the inlet 40.
- electric energy E from the fuel cell 52 to the means 42 when these comprise an electric heating unit for generating steam.
- the electric heating elements 10 for heating the water 6 of the vessel 2 is fed by electric energy from the fuel cell 52.
- the electric heating elements 10 may also be replaced by a hydrogen burner 10 for heating the water 6, which hydrogen burner 10 is fed with a part of the hydrogen flowing through the line 50.
- the product may further be provided with a heat exchanger 54 for exchanging heat between the mixture that has flown through the PrOx 46 and the water 6 contained in the vessel, so that the temperature of the mixture falls.
- the fuel processor When the fuel processor is provided with the fuel cell 52, it is further possible that the heated water formed in the fuel cell 52 when burning hydrogen is supplied to the inlet 40 in the form of steam. In that case the fuel cell 52 also forms part of the means for forming steam.
- the apparatus may further be provided with a heat exchanger 53 included between the LTS and the PrOx in the gas stream path, with an inlet 53A for water of, for instance, 20-70°C, and an outlet 53B for water of, for instance, 100°C.
- the mixture then cools in the heat exchanger, for instance, from 200°C to 110°C. (See curve G of Fig. 2.)
- the outlet 53B may, for instance, communicate with the inlet 40.
- the heat exchanger 53 may then replace the steam generator 42.
- the temperature of the mixture rises, as shown in curve H of Fig. 2. Downstream of the PrOx 46 the temperature then falls as a result of the water layer 51, as shown in curve I of
- Figs. 5A and 5B show an apparatus for generating from a first and second gas stream at least a third and fourth gas stream, which third gas stream comprises a mixture of the first and second gas stream.
- the apparatus is provided with a chamber 60 which encloses a space 62 in which a ventilator 64 is included.
- the chamber is provided with first and second inflow opening 66, 68, for supplying, in use, the first and second gas stream to respectively the first and second inflow opening 66, 68.
- the first and second gas stream are sucked in by the ventilator.
- the chamber further comprises first and second outflow opening 70, 72, the first and second gas stream, in use, being sucked in by the ventilator and being supplied to a first and second outflow opening separated from each other in the chamber.
- the first outflow opening discharges into a first outlet 76 having a relatively large cross-section.
- the second outflow opening 72 discharges via a bifurcation into the first outlet 76 and the second outlet 78 having a relatively small cross-section when compared to the cross-section of the first outlet 76. This has the result that the flow resistance of the first outlet 76 is lower than the flow resistance of the second outlet 78.
- a controllable valve 79 is included to adjust the ratio of the amount of gas originating from the first and second gas stream in the third gas stream flowing from the first outlet 76. From the second outlet 78 flows the fourth gas stream which comprises a part of the second gas stream.
- the third gas stream in the outlet 76 therefore comprises a combination of the first gas stream and the second gas stream which are supplied to respectively the first and second inflow opening 66, 68.
- the fourth gas stream of the outlet 78 only comprises a part of the second gas stream which is supplied to the second inflow opening 68. This is caused by the above difference in flow resistances.
- the chamber comp ⁇ ses a cylindrical outer wall which encloses a cylindrical space.
- the ventilator 64 is designed as a wheel, of which an axis of rotation 74 coincides with the axial axis of the chamber. Near its circumferential edge 73 the wheel is provided on both sides 75A, 75B.w ⁇ th blades 77.
- the first gas stream extends to a first side 75A of the wheel, and the second gas stream extends to a second side 75B of the wheel.
- the first and second inflow opening 66, 68 are provided in the cylindrical outer wall in a staggered position.
- the first inflow opening and the first outflow opening are arranged at least substantially in a similar plane which is directed perpendicularly to the axial axis of the chamber It also holds that the second inflow opening and the second outflow opening are arranged at least substantially m a similar plane which is directed perpendicularly to the axial axis 74 of the chamber.
- the first outlet 76 of the apparatus of Figs 5A and 5B is connected with the inlet 4 of the vessel 2 of Fig. 1.
- the second outlet 78 can be connected with the inlet 48 as shown in Fig. 1
- the apparatus of Figs. 5A and 5B is further provided with a known per se gas block 82 having an air inlet 84 and a gas inlet 86 for supplying a mixture of CH 4 and air via a line 87 to the inflow opening 66.
- the chamber is provided with two opposite side walls which are directed perpendicularly to the axial axis of the chamber, the first side wall 90A comprising a first circular groove 92A extending around the axial axis, in which the first inflow and outflow opening are provided, and the second side wall 90B comprising a second circular groove 92B extending around the axial axis, in which the second inflow and outflow opening are provided,
- the blades 77 of the wheel extend respectively along the first and second groove.
- the invention is in no way limited to the above-described embodiments.
- the vessel 6, as shown in Fig. 1, may, for instance, be replaced by an apparatus as shown in Fig. 6.
- the inlet 4 and the outlet 9 shown herein correspond with the inlet 4 and the outlet 9 of Fig. 1.
- the alternative apparatus is provided with a vessel 6', in which a layer 96 of a material in the form of, for instance, balls, salzur etc. is provided.
- the inlet 4 discharges below the layer 96.
- the outlet 9 is located above the layer 96.
- Also located above the layer 96 is a spray nozzle 98, via which water is deposited by means of a pump 100 from a vessel 102 onto the upper side of the layer 96.
- This water flows through the layer in the material 96 to the bottom 104 of the vessel 6'.
- the vessel 6' In a position located right above the bottom 104 the vessel 6' is in fluid communication with the vessel 102 by means of a line 108.
- the vessel 102 is further provided with means for heating the water located in the vessel. These means may consist of electric heating means, a burner, water originating from the above-mentioned fuel cell and/or originating from one of the heat exchangers mentioned before.
- the pump 100 the water is pumped round from the bottom 104 via the line 108 to the vessel 102 and from the vessel 102 to the spray nozzle 98, after which the water flows via the inert material 96 to the bottom 104.
- the gaseous hydrocarbon in this example CH 4 and oxygen, is again supplied to the inlet 4.
- This gas flows via the inert material 96 to the outlet 9.
- the temperature of the water that can be supplied via the spray nozzle 98 to the inert material 96 is of variable design and can be, for instance, about 70°C.
- the mixture is more or less saturated with water vapor.
- the water temperature is therefore a variable, by means of which the amount of water vapor in the mixture 8 can be regulated.
- the fuel processor according to the invention is preeminently suitable for use in microthermal power units in the domestic environment. This imposes special conditions.
- the processor must be transportable as a whole, from the factory to the user location, and may not contain fire or explosion dangerous materials during transport. After placement at the user location the thermal power plant, and therefore also the processor, must be able to be operational within about one hour. In the case of maintenance or failures when air enters the processor, no explosion or fire dangerous situations may arise.
- the processor must be designed so as to be as compact as possible.
- the above conditions impose stringent requirements on the catalysts in the processor.
- the catalysts may not be pyrophoric, that is to say when air enters, no such temperature rise may occur, as a result of oxidation of the catalyst, that the catalyst or the possible combustible content of the processor catches fire.
- the catalysts must have such a chemical composition that activation, if required, can take place within ca. 1 hour and can take place with process gas.
- the catalytic activity must be so high that at a high space throughput speed (Nm 3 process gas/m 3 catalyst/hour), and therefore with small amounts of catalyst, a nearly complete conversion of, successively, methane and carbon monoxide is reached.
- the CPO and PrOx catalysts may, for instance, consist of noble metals, on a carrier material applied as coating onto a ceramic monolith. These types of catalysts are described in the open literature. Suitable active metal is, inter alia, platinum. The above catalysts nearly completely convert methane or carbon monoxide at throughput speeds up to at least 20,000 Nm 3 /m 3 /h.
- the shift catalysts are characterized by a low volume, rapid activation in product gas and a non-pyrophoric character.
- HTS catalysts that mav be used, for instance
- Platinum applied onto a ⁇ -Al2 ⁇ 3 carrier Pt content on the basis of the platinum plus carrier weight: 0.1-20 wt.%, preferably 1-10 wt.%.
- Other metals, such as Ru and Rh, are also useful (Ru as shift and methanization catalyst is described in the open literature).
- Alternative carriers are, inter alia, silica-alumina, zirconia.
- the supported catalyst is applied onto a ceramic monolith by means of coating. Load of the coating: 50-400 g per liter of monolith, preferably 50-300 g/1.
- Platinum has no activation time and is not pyrophoric.
- the CO shift activity is high, i.e. little catalyst material is required. It is a disadvantage that Pt converts a part of the CO in the process gas with H2 to CH 4 (loss of efficiency, power reduction of the fuel cell).
- the degree of methanization is a matter of the kinetics of the methanization with respect to that of the CO shift. ⁇ .ccording as the temperature increases, the methanization relatively increases with respect to the CO shift.
- the problem may, for instance, be solved by using 2 instead of 3 HTS monoliths.
- the monolith directly behind the CPO catalyst has the highest temperature and produces the largest amount.
- Standard commercial Fe 2 ⁇ 3/Cr2 ⁇ 3 high temperature shift catalysts may be used
- the typical composition is 57-59 wt % Fe, on metal basis, 5-7 wt % Cr, on metal basis, and ca 1 wt % Cu, on metal basis, as promoter
- the catalysts are coated onto ceramic monoliths by known techniques
- the load and monolith characteristics are the same as for the Pt monoliths
- the activation of the monoliths occurs in process gas and is completed within 1 hour.
- Fe2 ⁇ 3 is reduced to Fe 3 O 4 .
- Fe 3 O is slightly pyrophoric.
- the catalyst in pellet form can develop such heat that fire dangerous situations arise.
- the standard commercial LTS catalyst is CuO with ZnO (coprecipitation). This is, for instance, contained in the processor as a packed bed of catalyst pellets with a total volume of no less than 20 liters.
- the active form in the shift is Cu metal.
- CuO can be very easily activated in process gas through reduction. However, the heat development is then such that upon a first startup the catalyst could become too hot and sinter.
- Typical loads are 5-30 wt.% Cu, preferably 10-20 wt.%.
- the copper is applied by methods known in the technique, such as impregnation of a Cu precursor, drying and calcining.
- CuO that is finely divided and sintering- resistant when located on a carrier is hard to reduce/activate at process temperatures of ca. 200°C.
- This can, for instance, be solved by addition of 0.1 to 1 wt.% of a metal, for instance Pt, which absorbs H 2 in the process gas and converts it into hydrogen atoms very active for reduction, which reduce CuO at lowered temperatures.
- the amount of platinum and the process temperature are such that no losses of efficiency through methanization occur.
- zeolites molecular sieves
- A4, A5, 13X zeolites
- the catalyst/zeolite weight ratio may vary from 10:1 to 1:10, preferably 1:1 to 1:10.
- the pyrophoric character of the zeolite systems is strongly reduced, because upon contact with the air the oxidation heat provides evaporation of the water in the zeolite. Per liter of zeolite, 50 to 100 liters can thus be released, which displaces-the air and prevents the temperatures in the catalyst bed from getting out of hand, which leads to catalyst deactivation and fire dangerous situations. When coated on a monolith, the locally strong heat development is further inhibited by the rapid heat discharge from the monolith.
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Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
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AU52549/00A AU5254900A (en) | 1999-05-27 | 2000-05-26 | Fuel processor for producing hydrogen and apparatus suitable for use in such processor |
Applications Claiming Priority (4)
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NL1012162 | 1999-05-27 | ||
NL1012162 | 1999-05-27 | ||
NL1013478 | 1999-11-03 | ||
NL1013478A NL1013478C2 (en) | 1999-05-27 | 1999-11-03 | Fuel processor for producing hydrogen and apparatus suitable for use in such a processor for generating a third and fourth gas stream from a first and second gas stream. |
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WO2000078669A1 true WO2000078669A1 (en) | 2000-12-28 |
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PCT/NL2000/000364 WO2000078669A1 (en) | 1999-05-27 | 2000-05-26 | Fuel processor for producing hydrogen and apparatus suitable for use in such processor |
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AU (1) | AU5254900A (en) |
NL (1) | NL1013478C2 (en) |
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EP1270509A2 (en) * | 2001-06-22 | 2003-01-02 | Ballard Generation Systems Inc. | Apparatus, systems and methods for controlling the steam-carbon ratio for a hydrocarbon reformer |
EP1381453A1 (en) * | 2001-04-26 | 2004-01-21 | Texaco Development Corporation | Single chamber compact fuel processor |
WO2004054681A1 (en) * | 2002-12-17 | 2004-07-01 | Hydrogensource Llc | Evaporator |
DE10209832B4 (en) * | 2001-03-08 | 2006-12-21 | Honda Giken Kogyo K.K. | Reforming device and rinsing method for it |
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NL1016848C2 (en) * | 2000-12-11 | 2002-06-13 | Continental Engineering B V | Method and device for the preparation of ammonia. |
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DE10209832B4 (en) * | 2001-03-08 | 2006-12-21 | Honda Giken Kogyo K.K. | Reforming device and rinsing method for it |
EP1381453A1 (en) * | 2001-04-26 | 2004-01-21 | Texaco Development Corporation | Single chamber compact fuel processor |
EP1381453A4 (en) * | 2001-04-26 | 2008-02-13 | Texaco Development Corp | Single chamber compact fuel processor |
AU2002305234B2 (en) * | 2001-04-26 | 2008-07-03 | Texaco Development Corporation | Single chamber compact fuel processor |
US7442216B2 (en) | 2001-04-26 | 2008-10-28 | Texaco Inc. | Compact fuel processor |
EP1270509A2 (en) * | 2001-06-22 | 2003-01-02 | Ballard Generation Systems Inc. | Apparatus, systems and methods for controlling the steam-carbon ratio for a hydrocarbon reformer |
EP1270509A3 (en) * | 2001-06-22 | 2004-06-09 | Ballard Generation Systems Inc. | Apparatus, systems and methods for controlling the steam-carbon ratio for a hydrocarbon reformer |
WO2004054681A1 (en) * | 2002-12-17 | 2004-07-01 | Hydrogensource Llc | Evaporator |
Also Published As
Publication number | Publication date |
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NL1013478C2 (en) | 2000-11-28 |
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