WO2006109949A1 - Hydrogen generating apparatus and hydrogen generating method using the hydrogen generating apparatus - Google Patents
Hydrogen generating apparatus and hydrogen generating method using the hydrogen generating apparatus Download PDFInfo
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- WO2006109949A1 WO2006109949A1 PCT/KR2006/001219 KR2006001219W WO2006109949A1 WO 2006109949 A1 WO2006109949 A1 WO 2006109949A1 KR 2006001219 W KR2006001219 W KR 2006001219W WO 2006109949 A1 WO2006109949 A1 WO 2006109949A1
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- WIPO (PCT)
- Prior art keywords
- reaction device
- plate assembly
- combustion
- unit reaction
- reforming
- Prior art date
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- 239000001257 hydrogen Substances 0.000 title claims abstract description 154
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 154
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 145
- 238000000034 method Methods 0.000 title claims abstract description 31
- 238000006243 chemical reaction Methods 0.000 claims abstract description 318
- 238000002485 combustion reaction Methods 0.000 claims abstract description 231
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 143
- 238000006057 reforming reaction Methods 0.000 claims abstract description 131
- 239000000446 fuel Substances 0.000 claims abstract description 118
- 239000003054 catalyst Substances 0.000 claims abstract description 94
- 238000002407 reforming Methods 0.000 claims abstract description 60
- 238000000429 assembly Methods 0.000 claims abstract description 47
- 230000000712 assembly Effects 0.000 claims abstract description 47
- 239000002994 raw material Substances 0.000 claims abstract description 44
- 239000007789 gas Substances 0.000 claims description 38
- 239000007788 liquid Substances 0.000 claims description 32
- 239000000203 mixture Substances 0.000 claims description 29
- 239000010949 copper Substances 0.000 claims description 20
- 238000007254 oxidation reaction Methods 0.000 claims description 19
- 238000002309 gasification Methods 0.000 claims description 17
- 230000003647 oxidation Effects 0.000 claims description 17
- 239000007800 oxidant agent Substances 0.000 claims description 16
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 12
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 11
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 claims description 11
- 229910001928 zirconium oxide Inorganic materials 0.000 claims description 11
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical group [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 10
- 229910000431 copper oxide Inorganic materials 0.000 claims description 8
- 239000011248 coating agent Substances 0.000 claims description 7
- 238000000576 coating method Methods 0.000 claims description 7
- 229910052802 copper Inorganic materials 0.000 claims description 7
- CETPSERCERDGAM-UHFFFAOYSA-N ceric oxide Chemical compound O=[Ce]=O CETPSERCERDGAM-UHFFFAOYSA-N 0.000 claims description 6
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 claims description 6
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 4
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- 229910000420 cerium oxide Inorganic materials 0.000 claims description 4
- 229910052593 corundum Inorganic materials 0.000 claims description 4
- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 claims description 4
- 229910052697 platinum Inorganic materials 0.000 claims description 4
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 4
- 239000011787 zinc oxide Substances 0.000 claims description 4
- -1 α-aluminum oxide Chemical compound 0.000 claims description 4
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 3
- 238000001354 calcination Methods 0.000 claims description 3
- 238000000975 co-precipitation Methods 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 3
- 229910052725 zinc Inorganic materials 0.000 claims description 3
- 239000011701 zinc Substances 0.000 claims description 3
- 239000005751 Copper oxide Substances 0.000 claims description 2
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 claims description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims description 2
- 229910052737 gold Inorganic materials 0.000 claims description 2
- 239000010931 gold Substances 0.000 claims description 2
- 229910052762 osmium Inorganic materials 0.000 claims description 2
- SYQBFIAQOQZEGI-UHFFFAOYSA-N osmium atom Chemical compound [Os] SYQBFIAQOQZEGI-UHFFFAOYSA-N 0.000 claims description 2
- 229910052763 palladium Inorganic materials 0.000 claims description 2
- 229910052703 rhodium Inorganic materials 0.000 claims description 2
- 239000010948 rhodium Substances 0.000 claims description 2
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 claims description 2
- 229910052707 ruthenium Inorganic materials 0.000 claims description 2
- 229910052709 silver Inorganic materials 0.000 claims description 2
- 239000004332 silver Substances 0.000 claims description 2
- 239000006104 solid solution Substances 0.000 claims description 2
- 229910052741 iridium Inorganic materials 0.000 claims 1
- GKOZUEZYRPOHIO-UHFFFAOYSA-N iridium atom Chemical compound [Ir] GKOZUEZYRPOHIO-UHFFFAOYSA-N 0.000 claims 1
- 150000002431 hydrogen Chemical class 0.000 abstract description 7
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 abstract description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 21
- 229910002091 carbon monoxide Inorganic materials 0.000 description 21
- 239000012071 phase Substances 0.000 description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 10
- 239000001301 oxygen Substances 0.000 description 10
- 229910052760 oxygen Inorganic materials 0.000 description 10
- 238000001651 catalytic steam reforming of methanol Methods 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000011112 process operation Methods 0.000 description 2
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000002542 deteriorative effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000003028 elevating effect Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 229910052738 indium Inorganic materials 0.000 description 1
- APFVFJFRJDLVQX-UHFFFAOYSA-N indium atom Chemical compound [In] APFVFJFRJDLVQX-UHFFFAOYSA-N 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
Classifications
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- A—HUMAN NECESSITIES
- A63—SPORTS; GAMES; AMUSEMENTS
- A63H—TOYS, e.g. TOPS, DOLLS, HOOPS OR BUILDING BLOCKS
- A63H3/00—Dolls
- A63H3/36—Details; Accessories
- A63H3/46—Connections for limbs
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
-
- A—HUMAN NECESSITIES
- A63—SPORTS; GAMES; AMUSEMENTS
- A63H—TOYS, e.g. TOPS, DOLLS, HOOPS OR BUILDING BLOCKS
- A63H3/00—Dolls
- A63H3/04—Dolls with deformable framework
-
- A—HUMAN NECESSITIES
- A63—SPORTS; GAMES; AMUSEMENTS
- A63H—TOYS, e.g. TOPS, DOLLS, HOOPS OR BUILDING BLOCKS
- A63H3/00—Dolls
- A63H3/16—Dolls made of parts that can be put together
-
- A—HUMAN NECESSITIES
- A63—SPORTS; GAMES; AMUSEMENTS
- A63H—TOYS, e.g. TOPS, DOLLS, HOOPS OR BUILDING BLOCKS
- A63H9/00—Special methods or compositions for the manufacture of dolls, toy animals, toy figures, or parts thereof
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
- C01B3/326—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents characterised by the catalyst
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00783—Laminate assemblies, i.e. the reactor comprising a stack of plates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00801—Means to assemble
- B01J2219/00804—Plurality of plates
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00819—Materials of construction
- B01J2219/00822—Metal
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00819—Materials of construction
- B01J2219/00835—Comprising catalytically active material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00851—Additional features
- B01J2219/00858—Aspects relating to the size of the reactor
- B01J2219/0086—Dimensions of the flow channels
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00851—Additional features
- B01J2219/00858—Aspects relating to the size of the reactor
- B01J2219/00862—Dimensions of the reaction cavity itself
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00873—Heat exchange
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00891—Feeding or evacuation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0435—Catalytic purification
- C01B2203/044—Selective oxidation of carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/047—Composition of the impurity the impurity being carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/066—Integration with other chemical processes with fuel cells
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1005—Arrangement or shape of catalyst
- C01B2203/1035—Catalyst coated on equipment surfaces, e.g. reactor walls
-
- 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
- C01B2203/1076—Copper or zinc-based catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1217—Alcohols
- C01B2203/1223—Methanol
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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 hydrogen generating apparatus and a hydrogen generating method. Specifically, the present invention relates to a hydrogen generating apparatus comprising unit reaction devices comprising micro-channels containing coated combustion catalyst and/or coated reforming catalyst, designed for generating hydrogen with high heat efficiency and high conversion ratio to hydrogen, in supplying hydrogen to fuel cell system or the like by using alcohol such as methanol as a raw material, and to a hydrogen generating method using the same.
- Hydrogen is the lightest gas among all gases, and is easy to explode in air, and so its storage and handling are very difficult.
- hydrogen is supplied by using a large scale of storage tank.
- such storage tank for hydrogen cannot solve the above problems completely, and enormous early investment for facilities such as developing a large scale of storage tank and preparing a larger storage space is needed for such supply method of hydrogen.
- the supply of hydrogen had to be a national infra-structure project.
- a gasifier for gasifying a mixture of methanol and water in liquid phase a gasifier for gasifying a combustor for supplying heat to a reforming reactor, and a gasifier for gasifying liquid fuel for combustion are required first, and a preferential oxidation reactor for lowering the content of carbon monoxide contained in hydrogen generated is required separately.
- the methanol-steam reforming reaction is represented by the following reaction scheme 1 :
- the methanol-steam reforming reaction is optimally conducted around 300 °C. If the temperature is higher than this, the direct decomposition of methanol and the reverse reaction of the above reaction (3) are occurred to raise the concentration of carbon monoxide in product. To lower the concentration of carbon monoxide, the above reaction (3), water-gas shift reaction, is required. Accordingly, to lower the concentration of carbon monoxide, the temperature of the reformer should be maintained accurately.
- Korean Patent No. 0314829 describes a methanol reforming apparatus constituted as double tube type to maintain the temperature of reformer constantly.
- honeycomb combustion catalyst is arranged at uniform distances in the inner tube and reforming catalyst is filled in the outer tube, to conduct the reforming reaction.
- local temperature elevation of the reformer is prevented, and the temperature is maintained constantly in the range of 200 to 300 ° C .
- a reactor structured like this is not enough to reduce the size of reformer.
- a small-sized methanol-steam reforming apparatus using methanol as a fuel for combustion and as a raw material for reforming reaction at the same time is disclosed in J. of Power source, 108 (2002) 21 - 27 by the Pacific North National Laboratory.
- this apparatus has drawbacks that its output is as low as about 200 mW, and that the total heat efficiency is as low as 5 to 10 % since the amount of methanol as a fuel fed into combustor to maintain the reaction temperature is large.
- the present invention is to solve the problems of the conventional technologies as described above. Therefore, the object of the present invention is to provide a hydrogen generating apparatus comprising unit reaction devices comprising micro-channels containing coated combustion catalyst and/or coated reforming catalyst, designed for generating hydrogen with high heat efficiency and high conversion ratio to hydrogen, in supplying hydrogen to fuel cell system or the like by using alcohol such as methanol as a raw material, and to a hydrogen generating method using the same.
- the hydrogen generating apparatus comprises at least one first unit reaction device for combustion/ reforming reaction comprising a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst, wherein each of the plate assemblies comprises a pair of micro-channel plates, on the surface of one side of which micro- channels are formed, and which are combined to each other in a manner that the micro- channels are opposed to each other; wherein the plate assembly for combustion contains the combustion catalyst in the micro-channels; and wherein the plate assembly for reforming reaction contains the reforming catalyst in the micro-channels.
- the hydrogen generating apparatus comprises at least one first unit reaction device for combustion/reforming reaction, at least one second unit reaction device for gasification, and at least one third unit reaction device for heat exchange
- the first unit reaction device comprises a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst
- the second unit reaction device comprises a plate assembly for combustion and a plate assembly for heat exchange
- the third unit reaction device comprises plate assemblies for heat exchange; wherein the plate assembly for combustion of the first unit reaction device is connected to one of the plate assemblies for heat exchange of the third unit reaction device; wherein the other of the plate assemblies for heat exchange of the third unit reaction device is connected to the plate assembly for combustion of the first unit reaction device; and wherein the plate assembly for heat exchange of the second unit reaction device is connected to the plate assembly for reforming reaction of the first unit reaction device.
- the hydrogen generating method comprises, (1) a first combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion of the first unit reaction device and burning the fuel in the plate assembly for combustion, and heating the plate assembly for reforming reaction adjacent to the plate assembly for combustion by using the combustion heat; and (2) a reforming step of generating hydrogen by feeding a raw material for reforming reaction comprising a mixture of methanol and water to the heated plate assembly for reforming reaction and reforming the raw material, in generating hydrogen by using a hydrogen generating apparatus comprising at least one first unit reaction device for combustion/reforming reaction comprising a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst, wherein each of the plate assemblies comprises a pair of micro-channel plates, on the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other; wherein the plate assembly for combustion contains the combustion catalyst in the micro-channels; and
- the hydrogen generating method comprises, (1) a first combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion of the first unit reaction device and burning the fuel; (2) a first preheat step of preheating the third unit reaction device to 80 to 100 °C by emitting exhaust gas from the plate assembly for combustion in the first combustion step via one plate assembly for heat exchange of the third unit reaction device; (3) a second combustion step of heating the first unit reaction device to 260 to 320 ° C by feeding and gasifying liquid fuel to the plate assembly for combustion of the first unit reaction device via the other plate assembly for heat exchange of the third unit reaction device, and burning the fuel with feeding oxidizing agent at the same time; (4) a third combustion step of heating the second unit reaction device to 110 to 200 °C by feeding fuel in gas phase to the plate assembly for combustion of the second unit reaction device and burning the fuel together with oxidizing agent; (5) a gasification step of gasifying a mixture of methanol and water as raw material for reforming reaction by passing through the plate assembly for
- Figure 1 is a schematic diagram illustrating the overall constitution of the hydrogen generating apparatus according to the present invention.
- Figure 2 is a diagram illustrating disassembly of the unit reaction device used in the hydrogen generating apparatus of Figure 1.
- Figure 3 is a photograph for disassembly of an embodiment of the hydrogen generating apparatus according to the present invention.
- Figure 4 is a diagram illustrating disassembly of only the plate assemblies constituting the unit reaction device of Figure 2.
- Figure 5 is a plane figure of the micro-channel plate constituting the plate assemblies of Figure 4.
- Figure 6 is a plane figure of the gasket used in the plate assembly constituting the unit reaction device according to the present invention.
- Figure 7 is a side cross-sectional diagram of the plate assembly constituting the unit reaction device of Figure 2.
- the hydrogen generating apparatus is characterized in comprising at least one first unit reaction device (11) for combustion/reforming reaction which is comprised of a plate assembly for combustion containing a coated combustion catalyst and a plate assembly for reforming reaction containing a coated reforming catalyst, wherein each of the plate assemblies comprises a pair of micro-channel plates, on the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other; wherein the plate assembly for combustion contains the combustion catalyst in the micro-channels; and wherein the plate assembly for reforming reaction contains the reforming catalyst in the micro-channels.
- the characteristic of the present invention lies in that the heat for reforming reaction can be obtained from a plate assembly for combustion adjacent to a plate assembly for reforming reaction containing reforming catalyst whereby the reforming reaction can be conducted at optimized temperature to heighten heat efficiency and conversion ratio to hydrogen at the same time.
- the characteristics lie in that the present apparatus can be made smaller while performing the function of combustor in a conventional hydrogen generating apparatus by constituting the plate assembly for combustion to perform the function of combustor in which the combustion reaction is conducted, and having this combustion reaction in the plate assembly for combustion performed in the micro-channel, and that the apparatus can be made smaller while performing the function of reformer in a conventional hydrogen generating apparatus by constituting the plate assembly for reforming reaction to perform the function of reformer in which the reforming reaction is conducted, and having this reforming reaction in the plate assembly for reforming reaction performed in the micro-channel. Further, according to the present invention, as shown in Fig.
- combustion heat is utilized in the reforming reaction at its maximum by constituting the first unit reaction device (11) comprising the plate assembly for combustion (41') and the plate assembly for reforming reaction (41") to make the plate assembly for combustion (41') and the plate assembly for reforming reaction (41") stacked alternately.
- the expression "first" in the first unit reaction device (11) is used to distinguish the unit reaction device comprising both of the combustion catalyst and the reforming catalyst.
- the combustion catalyst may be selected from the group consisting of platinum group elements such as platinum, rhodium, ruthenium, osmium, indium and palladium, gold, silver, copper and mixtures thereof.
- the combustion catalyst may be supported by a catalyst support.
- the supporting of the combustion catalyst consists of coating a catalyst support firstly, then adding an aqueous solution of the combustion catalyst thereto in an amount of 0.1 to 5 wt% to the catalyst support, and then drying and calcining the mixture.
- the catalyst support may be selected from the group consisting of aluminum oxide, ⁇ -aluminum oxide, zirconium oxide (ZrO 2 ), silica (SiO 2 ), ceria (CeO 2 ) and mixtures thereof, and preferably, ⁇ -aluminum oxide may be used.
- the present invention is not limited thereto, and it is natural that other catalysts capable of being used for promoting oxidation of hydrocarbon, alcohol or the like may be also used in the present invention.
- the unit reaction device (41) constituting the first unit reaction device (11) comprises cases (42 and 42') consisting of two metallic blocks, wherein the plate assembly for combustion (41') and the plate assembly for reforming reaction (41") are stacked alternately and fixed between the cases (42 and 42').
- cases (42 and 42') for example, combustor outlet (43') and reformer outlet (44') are formed in the upper case (42), and combustor inlet (43) and reformer inlet (44) are formed in the lower case (42').
- FIG. 3 A photograph for disassembly of an embodiment of the unit reaction device is shown in Fig. 3.
- the thickness of the micro-channel plate (45) is about 0.3 mm, and the micro-channel is formed with a depth of 10 to 150 ⁇ m.
- Channel is formed on metal plate in a parallelogramic form, and holes allowing fluid to flow are formed at each vertex of the metal plate.
- the plate assemblies constituting the unit reaction device (41) comprise a pair of micro-channel plates (45 and 45'), on the surface of one side of which micro-channels (51 and 51') are formed in common, and which are combined to each other in a manner that the micro-channels (51 and 51') are opposed to each other, and the plate assembly for combustion (41') contains the combustion catalyst in the micro- channels (51 and 51'); and the plate assembly for reforming reaction (41") contains the reforming catalyst in the micro-channels (51 and 51'). All of the cases and micro- channels can be molded out of metal, preferably material having good corrosion resistance and heat resistance such as stainless steel or the like.
- a gasket (61) may be inserted between the micro-channel plates (45 and 45'), as shown in Fig. 6.
- the gasket (61) may be made up of copper plate, and consist of openings (62) and perforation holes (63) formed to make a uniform space between the micro-channel plates (45 and 45').
- two or more plate assemblies such as the plate assembly for combustion (41') and the plate assembly for reforming reaction (41") can be stacked with each other. If necessary, i.e. according to the amount of hydrogen desired to be generated or the like, the number of the plate assembly for combustion (41') and the plate assembly for reforming reaction (41") to be stacked may be increased or decreased.
- plural channel forming spaces (71) are formed, and the inner walls function as catalyst coating part (72) wherein catalysts such as the combustion catalyst or the reforming catalyst are coated.
- upper micro-channel plate (45) has an inlet (46), an outlet(47), first connecting aperture (48) and second connecting aperture (49), wherein the inlet and the outlet are located diagonally to each other, and the first connecting aperture and the second connecting aperture are located diagonally to each other, and wherein a groove having certain depth from surface with including the inlet (46) and the outlet (47) is formed between the inlet (46) and the outlet (47), and the wall of the groove functions as a cutoff wall (53) to restrict the flow direction of fuel or raw materials which pass through the micro-channels (51).
- the micro-channels (51) are separated by separating walls (52) and formed in plural.
- micro-channel plates (45 and 45') are formed around the inlet (46) and the outlet (47), convergent depressions (54) and convergent prominences (55) to restrict the flow of fuel or raw materials so as to diffuse the fuel or raw materials from the inlet (46) or the outlet (47) to the micro-channels (51) or to collect the fuel or raw materials to the inlet (46) or the outlet (47).
- lower micro-channel plate (45') is the same as the upper micro-channel plate (45), but has a mirror-image symmetrical structure thereto, and so refers to the same symbols, only distinguished by the symbol (').
- the fuel flowing in the combustor inlet (43) flows into the inside of the plate assembly for combustion (41') through the inlet (46) of the plate assembly for combustion (41'), is burned in passing the micro-channels, then exits through the outlet (47) of the plate assembly for combustion (41'), then passes through the second connecting aperture (49) of the plate assembly for reforming reaction (41") placed in the upper stage, and then flows in the outlet (47) of the plate assembly for combustion (41') placed in the upper stage.
- This is also applied to the flow of raw material to the plate assembly for reforming reaction (41") in the same manner, and so the fuel and the raw material can flow separately from each other.
- Hydrogen can be generated by generating combustion heat by feeding and burning fuel in gas phase, preferably hydrogen, together with oxidizing agent, preferably oxygen or air, from hydrogen source (21) and first oxygen source (22) through the combustor inlet (43) to the plate assembly for combustion (41') of the first unit reaction device (11) in the plate assembly for combustion (41'), supplying the heat to the plate assembly for reforming reaction (41") adjacent thereto, and feeding a mixture of methanol and water as a raw material from the raw material source (27) to the plate assembly for reforming reaction (41"), and converting methanol to hydrogen.
- fuel preferably hydrogen
- oxidizing agent preferably oxygen or air
- the reforming reaction may also be conducted by passing heat flow through the inside of the plate assembly for combustion (41') of the first unit reaction device (11), and it is naturally understandable by a skilled person in the art that where exhaust heat is generated in a large scale, heat flow having such exhaust heat may also be used.
- the plate assembly for combustion (41') may not contain the combustion catalyst therein.
- a third unit reaction device (12) may be further connected to the first unit reaction device (11).
- the third unit reaction device (12) comprises plate assemblies for heat exchange comprising a pair of micro-channel plates, on the surface of one side of which micro-channels are formed and which are combined to each other in a manner that the micro-channels are opposed to each other.
- the plate assemblies for heat exchange have a structure the same as or similar to the plate assembly for combustion (41') or the plate assembly for reforming reaction (41"), only except that the plate assemblies for heat exchange do not contain catalysts such as a combustion catalyst, a reforming catalyst and the like at all, and enable heat exchange between fluids passing the plate assemblies adjacent to each other by allowing the fluids to pass the micro-channels.
- the expression "third” in the third unit reaction device (12) is used to distinguish the unit reaction device comprising neither the combustion catalyst nor the reforming catalyst.
- the third unit reaction device (12) may be connected to the plate assembly for combustion (41') of the first unit reaction device (11), wherein the inlet of one of the plate assemblies for heat exchange of the third unit reaction device (12) may be connected to the outlet of the plate assembly for combustion (41') of the first unit reaction device (11).
- the exhaust gas emitted from the plate assembly for combustion (41') of the first unit reaction device (11) passes through one of the plate assemblies for heat exchange of the third unit reaction device (12), and heats other plate assembly for heat exchange adjacent thereto, whereby a fluid passing inside of the other plate assembly for heat exchange can be heated.
- the first fuel source (24) connects to the other plate assembly for heat exchange and liquid fuel supplied therefrom passes through the other plate assembly for heat exchange, this liquid fuel is gasified, and the gasified fuel is connected again to the plate assembly for combustion (41') of the first unit reaction device (11), and the combustion reaction can continue.
- the reforming reaction can be continued by cutting off the fuel in gas phase and continuing the combustion reaction with using the fuel gasified by the third unit reaction device (12).
- a small-sized hydrogen generating apparatus can use liquid fuel which is more convenient to handle and store, with minimizing the use of fuel in gas phase which is inconvenient to handle and store.
- the liquid fuel methanol may be preferred.
- a second unit reaction device (13) may be connected to the first unit reaction device (11).
- the second unit reaction device (13) comprises a plate assembly for combustion and a plate assembly for heat exchange.
- the second unit reaction device (13) may be connected to the plate assembly for reforming reaction (41") of the first unit reaction device (11), wherein the outlet of the plate assembly for heat exchange of the second unit reaction device may be connected to the inlet of the plate assembly for reforming reaction of the first unit reaction device.
- the plate assembly for combustion of the second unit reaction device (13) has a constitution the same as or similar to the plate assembly for combustion (41') of the first unit reaction device (11).
- the expression "second" in the second unit reaction device (13) is used to distinguish the unit reaction device comprising the combustion catalyst only.
- the second unit reaction device (13) functions to promote the reforming reaction in the first unit reaction device (11) by heating and gasifying a mixture of methanol and water as a fuel supplied to the first unit reaction device (11).
- the fuel in gas phase is supplied and burnt together with oxidizing agent by connecting a hydrogen source (21) and a second oxygen source (25) to the plate assembly for combustion of the second unit reaction device (13); a plate assembly for heat exchange adjacent to the plate assembly for combustion of the second unit reaction device (13) is heated by using the combustion heat; a mixture of methanol and water as a raw material is passed through the inside of the plate assembly for heat exchange and gasified, by connecting a raw material source (27) to the plate assembly for heat exchange; and the gasified raw material is supplied to the plate assembly for reforming reaction (41") of the first unit reaction device (11) to be reformed.
- the second unit reaction device (13) may be maintained, for example, in the range of 110 to 200 °C .
- a fourth unit reaction device (15) may be connected further between the second unit reaction device (13) and the first unit reaction device (11).
- the fourth unit reaction device (15) comprises plate assemblies for heat exchange.
- the expression "fourth" in the fourth unit reaction device (15) is used to distinguish the unit reaction device comprising neither the combustion catalyst nor the reforming catalyst.
- the liquid fuel may be gasified by using the heat of product flow emitted therefrom, and supplied to the plate assembly for combustion of the second unit reaction device (13), to conduct the combustion reaction.
- the combustion reaction can be continued by using the fuel gasified by the fourth unit reaction device (15) while the fuel in gas phase supplied from the hydrogen source (21) is cut off.
- the fuel in gas phase which is inconvenient to handle and store
- the liquid fuel which is more convenient to handle and store
- methanol may be preferred.
- a preferential oxidation reactor (14) may be further connected to the outlet of the plate assembly for reforming reaction (41") of the first unit reaction device (11).
- the preferential oxidation reactor (14) functions to conduct the oxidation of carbon monoxide to remove carbon monoxide which could be included in hydrogen as a product reformed and produced by the first unit reaction device (11), whereby the hydrogen produced from the apparatus of the present invention can be directly connected to fuel cell or the like and used, without additional purification procedure, since carbon monoxide which can affect to the electrode of fuel cell is removed at a maximum.
- the plate assemblies according to the present invention are used.
- Preferential oxidation reactor may have a structure the same as or similar to the plate assembly, only except further comprising a preferential oxidation catalyst, instead of the combustion catalyst or the reforming catalyst as described above.
- a third oxygen source (28) for supplying oxygen or air for oxidation of carbon monoxide is connected to the preferential oxidation reactor (14).
- a filter may be connected between the plate assembly for reforming reaction (41") of the first unit reaction device (11) and the preferential oxidation reactor (14).
- the filter may be a conventional mechanical filter.
- the hydrogen generating apparatus is characterized in comprising at least one first unit reaction device (11) for combustion/reforming reaction, at least one second unit reaction device (13) for gasification, and at least one third unit reaction device (12) for heat exchange
- the first unit reaction device (11) comprises a plate assembly for combustion (41') comprising a combustion catalyst and a plate assembly for reforming reaction (41") comprising a reforming catalyst
- the second unit reaction device (13) comprises a plate assembly for combustion and a plate assembly for heat exchange
- the third unit reaction device (12) comprises a plate assemblies for heat exchange; wherein the plate assembly for combustion (41') of the first unit reaction device (11) is connected to one of the plate assemblies for heat exchange of the third unit reaction device (12); wherein the other of the plate assemblies for heat exchange of the third unit reaction device (12) is connected to the plate assembly for combustion (41') of the first unit reaction device (11); and wherein the plate assembly for heat exchange of the second unit reaction device (13) is connected
- a valve for changing flow direction (23) is connected to the plate assembly for combustion (41') of the first unit reaction device (11). And, to this valve for changing flow direction (23), a hydrogen source (21) is connected.
- the valve for changing flow direction (23) may be a 4-way valve preferably so that hydrogen supplied from the hydrogen source connected thereto can be firstly fed into the plate assembly for combustion (41') of the first unit reaction device (11) for reduction, then into the plate assembly for reforming reaction (41") for reduction, and finally into the plate assembly for combustion of the second unit reaction device (13) in order.
- the temperatures of the first unit reaction device (11) and the third unit reaction device (12) connected thereto are elevated higher than the boiling point of methanol as a fuel by using the hydrogen as a fuel, the fuel is replaced from hydrogen to methanol. And, after elevating the temperature of the first unit reaction device (11) to the reduction temperature (about 300 °C) by the continued combustion reaction of methanol, the reforming catalyst in the plate assembly for reforming reaction (41") can be reduced by hydrogen.
- the present invention provides such advantages that by conducting the combustion reaction in the plate assembly for combustion of the unit reaction device comprising a micro-channel, and stacking and placing the plate assembly for reforming reaction adjacent thereto, thereby enabling the plate assembly for reforming reaction where the reforming reaction is conducted to maintain a stable operation temperature, the conversion ratio of methanol and the composition of hydrogen in the product can be raised, and high heat efficiency and hydrogen productivity can be exhibited by lowering the content of carbon monoxide; and the apparatus can be smaller and attached directly to a fuel cell or the like to supply hydrogen by reducing the content of carbon monoxide. Also, the present invention provides an advantage that fuel cell can be operated without deactivating the electrode of the fuel cell by removing carbon monoxide as much as possible by further comprising preferential oxidation reactor.
- the hydrogen generating method comprises (1) a first combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion (41') of the first unit reaction device (11) and burning the fuel in the plate assembly for combustion (41'), and heating the plate assembly for reforming reaction (41") adjacent to the plate assembly for combustion (41') by using the combustion heat; and (2) a reforming step of generating hydrogen by feeding raw material for reforming reaction comprising a mixture of methanol and water to the heated plate assembly for reforming reaction (41") and reforming the raw material, in generating hydrogen by using a hydrogen generating apparatus comprising at least one first unit reaction device (11) for combustion/reforming reaction comprising a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst, wherein each of the plate assemblies comprises a pair of micro-channel plates, on the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other; where
- the plate assembly for reforming reaction (41") is heated by supplying the combustion heat generated from the first combustion step, and the reforming reaction is conducted by using this heat.
- the characteristic of the present invention lies in that by conducting the combustion reaction in the plate assembly for combustion (41') of the unit reaction device comprising a micro- channel, and stacking and placing the plate assembly for reforming reaction (41") adjacent thereto, thereby enabling the plate assembly for reforming reaction (41") where the reforming reaction is conducted to maintain a stable operation temperature of 260 to 320 ° C , the conversion ratio of methanol and the composition of hydrogen in the product can be raised, and high heat efficiency and hydrogen productivity can be exhibited by lowering the content of carbon monoxide.
- the conversion ratio to hydrogen may decrease since the temperature of the reforming reaction is too low, and to the contrary, if it is higher than 320 ° C , the content of carbon monoxide in product is raised too much, and the concentration of carbon monoxide cannot be sufficiently lowered in spite of subsequent preferential oxidation reaction, and so the hydrogen productivity may decrease. If the concentration of carbon monoxide becomes relatively high, there may be a problem that the hydrogen as a product cannot be incorporated directly as a fuel for fuel cell.
- the hydrogen generating method according to the present invention may further comprise, between the first combustion step (1) and the reforming step (2), a first connection step of connecting a third unit reaction device (12) comprising plate assemblies for heat exchange, each of which comprises a pair of micro-channel plates, on the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other, to the plate assembly for combustion (41') of the first unit reaction device (11), wherein any inlet of the plate assembly for heat exchange of the third unit reaction device (12) is connected to an outlet of the plate assembly for combustion (41') of the first unit reaction device (11); and a first gasification step of connecting exhaust gas emitted from the plate assembly for combustion (41') of the first unit reaction device (11) to one plate assembly for heat exchange of the third unit reaction device (12), and feeding liquid fuel to the other plate assembly for heat exchange to gasify the liquid fuel.
- a third unit reaction device (12) comprising plate assemblies for heat exchange, each of which comprises a
- the characteristic lies in that by the first connection step, the third unit reaction device (12) is connected to the first unit reaction device (11), and the liquid fuel is gasified by using the exhaust gas emitted from the first unit reaction device (11), and by supplying the gasified fuel again to the first unit reaction device (11) to use it as a fuel, if the reaction is started and the third unit reaction device (12) is heated to a given temperature, preferably 80 to 100 °C, further use of the fuel in gas phase is stopped and the liquid fuel is used, whereby it is possible to minimize the use of fuel in gas phase which is inconvenient to handle and store, and to use liquid fuel which is more convenient to handle and store. If the temperature of the third unit reaction device is lower than 80 "C, the liquid fuel cannot be sufficiently gasified, and in real process operation, there is no case that the temperature is higher than 100 ° C .
- the hydrogen generating method according to the present invention may further comprise, between the first combustion step (1) and the reforming step (2), a second connection step of connecting a second unit reaction device (13) comprising a plate assembly for combustion and a plate assembly for heat exchange to the plate assembly for reforming reaction (41") of the first unit reaction device (11), wherein an outlet of the plate assembly for heat exchange of the second unit reaction device (13) is connected to an inlet of the plate assembly for reforming reaction (41") of the first unit reaction device (11); a second combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion of the second unit reaction device (13), burning the fuel in the plate assembly for combustion, and heating the plate assembly for heat exchange adjacent to the plate assembly for combustion by using the combustion heat; a second gasification step of feeding raw material for reforming reaction comprising a mixture of methanol and water to the plate assembly for heat exchange of the second unit reaction device (13) to gasify the raw material; and a first feed step of feeding the gasified raw material for reforming reaction in the second gas
- the second unit reaction device (13) is connected to the first unit reaction device (11), and the reforming reaction can be conducted smoothly by firstly gasifying the raw material which is introduced into the first unit reaction device (11) and reformed, by using the combustion heat from the combustion reaction in the plate assembly for combustion of the second unit reaction device (13), whereby the heat efficiency and the conversion ratio to hydrogen can be raised.
- the hydrogen generating method according to the present invention may further comprise, between the first combustion step (1) and the reforming step (2), a third connection step of connecting a fourth unit reaction device (15) comprising plate assemblies for heat exchange to the plate assembly for combustion of the second unit reaction device (13), wherein any one outlet of the plate assembly for heat exchange of the fourth unit reaction device (15) is connected to an inlet of the plate assembly for combustion of the second unit reaction device (13), and an inlet of the plate assembly for heat exchange is connected to a source of liquid fuel; a fourth connection step of connecting the other inlet of the fourth unit reaction device (15) to an outlet of the plate assembly for reforming reaction of the first unit reaction device (11), and connecting an outlet of the plate assembly for heat exchange to a product collector; and a third gasification step of gasifying the liquid fuel fed to the second unit reaction device (13) by using heat from product flow emitted from the plate assembly for reforming reaction of the first unit reaction device (11).
- the characteristic lies in that until the second unit reaction device (13) is raised to a given temperature, preferably 110 to 200 °C, and the fourth unit reaction device (15) is sufficiently preheated by the product flow emitted from the first unit reaction device (11), the process is operated by using fuel in gas phase, i.e. hydrogen, and after the second unit reaction device (13) is raised to a given temperature, preferably 110 to 200 ° C, the liquid fuel, i.e.
- methanol is supplied to, and gasified in, the fourth unit reaction device (15), and by supplying the gasified fuel to the second unit reaction device (13) to use it as a fuel, it is possible to minimize the use of fuel in gas phase which is inconvenient to handle and store, and use liquid fuel which is more convenient to handle and store. If the temperature of the third unit reaction device is lower than 110 "C, liquid fuel may not be sufficiently gasified, and in real process operation, there is no case that the temperature exceeds 200 ° C .
- the hydrogen generating method is characterized in comprising, (1) a first combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion of the first unit reaction device and burning the fuel; (2) a first preheat step of preheating the third unit reaction device to 80 to 100 ° C by emitting exhaust gas from the plate assembly for combustion in the first combustion step via one plate assembly for heat exchange of the third unit reaction device; (3) a second combustion step of heating the first unit reaction device to 260 to 320 °C by feeding and gasifying liquid fuel to the plate assembly for combustion of the first unit reaction device via the other plate assembly for heat exchange of the third unit reaction device, and burning the fuel with feeding oxidizing agent at the same time; (4) a third combustion step of heating the second unit reaction device to 110 to 200 ° C by feeding fuel in gas phase to the plate assembly for combustion of the second unit reaction device and burning the fuel together with oxidizing agent; (5) a gasification step of gasifying a mixture of methanol and water as raw material for reforming reaction by passing
- the above method may be used as optimized example. That is, to initiate the reforming reaction, first, a gas mixture of hydrogen and air or oxygen is supplied to the first unit reaction device (11) and burnt in the plate assembly for combustion (41'); heat generated at this time is exhausted with exhaust gas via the third unit reaction device (12), and after methanol as liquid fuel is supplied to third unit reaction device (12) and gasified, the gasified methanol is supplied again to the first unit reaction device (11) to continue the combustion reaction.
- the combustion reaction is initiated by methanol, the supply of hydrogen as a fuel in gas phase is stopped, and hydrogen is supplied to the second unit reaction device (13), with air or a gas mixture of oxygen.
- the combustion reaction is continued by adjusting the feeding ratio of methanol until the temperature of the first unit reaction device (11) reaches up to 260 to 320 ° C , and if reached, the combustion reaction is conducted by supplying a mixture of methanol and water as a raw material to the plate assembly for reforming reaction (41") of the first unit reaction device (11), and the hydrogen flow as a product flow is supplied to the fourth unit reaction device (15).
- methanol as a liquid fuel is also gasified and supplied to the second unit reaction device (13).
- the combustion reaction is also conducted, and if the temperature reaches to 110 to 200 0 C , the operation initiation step of the hydrogen generating apparatus according to the present invention is completed, and the combustion reaction is continued in the first unit reaction device (11) and the second unit reaction device (13) by continuously using methanol only as a liquid fuel, and hydrogen is generated continuously by reforming a mixture of methanol and water as a raw material in the plate assembly for reforming reaction (41") of the first unit reaction device (11).
- a plate assembly for reforming reaction was constituted by using a copper/zinc/aluminum oxide synthesized by co-precipitation method in the weight ratio of 4/4/2 as a reforming catalyst, and coating it in the amount of 0.6 g per micro-channel plate of the plate assembly for reforming reaction of the first unit reaction device.
- a plate assembly for combustion was constituted by firstly coating ⁇ -aluminum oxide as a combustion catalyst on a micro-channel plate, and adding an aqueous solution of platinum having the platinum amount of about 3 wt% to the ⁇ -aluminum oxide, and drying and calcining the plate.
- the first unit reaction device was constituted by stacking six plate assemblies for reforming reaction and five plate assemblies for combustion, as constituted above, alternately to each other, and the reforming reaction was conducted by starting the operation with adjusting the temperature of the first unit reaction device to about 300 °C , without attaching a preferential oxidation reactor.
- the mixture ratio of methanol : water as a raw material for reforming reaction was 50 : 50, and the flow rate of the raw material for reforming reaction supplied into the first unit reaction device was adjusted to 3 cc/min, and the flow rate of methanol as a fuel was adjusted to 1.1 cc/min. Under such operation conditions, the first unit reaction device was reached to the above temperature after about 90 minutes.
- ⁇ H c H 2 is total enthalpy of the hydrogen generated
- ⁇ H c total CH 3 OH is total enthalpy of the total methanol participated in the reforming reaction and the combustion reaction.
- the heat efficiency of the hydrogen generating apparatus according to the present invention was 59.5 %. Also, after connecting a preferential oxidation reactor, the content of carbon monoxide in the hydrogen product was lowered to 70 ppm. The heat efficiency at that time was also lowered to 56.7 % since some hydrogen was reacted together during the preferential oxidation reaction.
- the hydrogen generating apparatus comprising unit reaction devices micro-channel comprising the coating of combustion catalyst and/or reforming catalyst, and the hydrogen generating method using the same according to the present invention
- the unit reaction device comprising a plate assembly for combustion comprising a combustion catalyst on micro-channel and a plate assembly for reforming reaction comprising a reforming catalyst on micro-channel, stacking them adjacent to each other, conducting the combustion reaction and the reforming reaction in maintaining the reforming reaction in a constant temperature range, transferring the heat generated from the combustion reaction to the reforming reaction rapidly due to the constitution that where the reforming reaction occurs is close to where the combustion reaction occurs, and conducting the combustion reaction and the reforming reaction in micro-channel in maintaining high reaction temperature, the conversion ratio of methanol of 99 % or more and the high heat efficiency of 59.5 % or more in generating hydrogen can be achieved.
- the present hydrogen generating apparatus and hydrogen generating method using the same designed for generating hydrogen with high heat efficiency and high conversion ratio to hydrogen are effective for supplying hydrogen to a fuel cell system by using alcohol such as methanol as a fuel since all of the combustion reaction and the reforming reaction can be conducted by using micro-channel, and the hydrogen generating apparatus itself can be very smaller by the gasification by heat exchange. Further, the production amount of hydrogen can be controlled optionally only by adjusting the stacking number of these plate assemblies by constituting the plate assemblies for combustion and the plate assemblies for reforming reaction as a unit.
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Abstract
The present invention relates to a hydrogen generating apparatus comprising unit reaction devices comprising micro-channels containing coated combustion catalyst and/or coated reforming catalyst, designed for generating hydrogen with high heat efficiency and high conversion ratio to hydrogen, in supplying hydrogen to fuel cell system or the like by using alcohol like methanol as a raw material, and to a hydrogen generating method using the same. The hydrogen generating apparatus according to the present invention is characterized in comprising at least one first unit reaction device (11) for combustion/reforming reaction comprising a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst, wherein each of the plate assemblies comprises a pair of micro-channel plates, on the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other; wherein the plate assembly for combustion contains the combustion catalyst in the micro-channels; and wherein the plate assembly for reforming reaction contains the reforming catalyst in the micro-channels.
Description
HYDROGEN GENERATING APPARATUS AND
HYDROGEN GENERATING METHOD USING THE HYDROGEN GENERATING APPARATUS
TECHNICAL FIELD
The present invention relates to a hydrogen generating apparatus and a hydrogen generating method. Specifically, the present invention relates to a hydrogen generating apparatus comprising unit reaction devices comprising micro-channels containing coated combustion catalyst and/or coated reforming catalyst, designed for generating hydrogen with high heat efficiency and high conversion ratio to hydrogen, in supplying hydrogen to fuel cell system or the like by using alcohol such as methanol as a raw material, and to a hydrogen generating method using the same.
BACKGROUND ART
Recently, as more and more interest has been paid to the environment, clean fuel using hydrogen as fuel has gained more interest and demand.
Accordingly, continuous and vigorous researches have been conducted for fuel cell as an alternative to conventional gasoline engine and electric power generation using fossil fuel.
To heighten applicability of fuel cell, other conditions for better production and/or supply of hydrogen used as raw material should be accompanied. Hydrogen is the lightest gas among all gases, and is easy to explode in air, and so its storage and handling are very difficult. At the present technology level, hydrogen is supplied by using a large
scale of storage tank. However, such storage tank for hydrogen cannot solve the above problems completely, and enormous early investment for facilities such as developing a large scale of storage tank and preparing a larger storage space is needed for such supply method of hydrogen. Thus, the supply of hydrogen had to be a national infra-structure project.
Therefore, it is very preferable to make a hydrogen generating apparatus smaller and reduce its weight and volume in enabling hydrogen to be used as clean fuel without the above enormous investment for facilities.
To supply hydrogen generated from the smaller hydrogen generating apparatus directly to fuel cell or the like, the content of carbon monoxide (CO) deteriorating the activity of anode in fuel cell should be lowered.
As a method of generating hydrogen from methanol, a methanol-steam reforming method has been already developed and widely used.
To conduct the methanol steam-reforming reaction, a gasifier for gasifying a mixture of methanol and water in liquid phase, a combustor for supplying heat to a reforming reactor, and a gasifier for gasifying liquid fuel for combustion are required first, and a preferential oxidation reactor for lowering the content of carbon monoxide contained in hydrogen generated is required separately.
The methanol-steam reforming reaction is represented by the following reaction scheme 1 :
[Reaction Scheme 1]
CH3OH + H2O → CO2 + 3H2 Δ H = 49.4 kJ/mol (1)
CH3OH → CO + 2H2 Δ H - 90.5 kJ/mol (2) CO + H2O → CO2 + H2 Δ H = -41.1 kJ/mol (3)
The methanol-steam reforming reaction as shown above is conducted as the reaction (1) in the Reaction Scheme 1, and the reaction (2) in the Reaction Scheme 1, direct decomposition of methanol, is also conducted partly at high temperature. The reactions (1) and (2) in the Reaction Scheme 1 are endothermic reactions, and so heat should be continuously supplied from outside to conduct these reactions.
It is known that the methanol-steam reforming reaction is optimally conducted around 300 °C. If the temperature is higher than this, the direct decomposition of methanol and the reverse reaction of the above reaction (3) are occurred to raise the concentration of carbon monoxide in product. To lower the concentration of carbon monoxide, the above reaction (3), water-gas shift reaction, is required. Accordingly, to lower the concentration of carbon monoxide, the temperature of the reformer should be maintained accurately.
Korean Patent No. 0314829 describes a methanol reforming apparatus constituted as double tube type to maintain the temperature of reformer constantly. In this apparatus, honeycomb combustion catalyst is arranged at uniform distances in the inner tube and reforming catalyst is filled in the outer tube, to conduct the reforming reaction. By this structure, local temperature elevation of the reformer is prevented, and the temperature is maintained constantly in the range of 200 to 300 °C . However, to use a reactor structured like this is not enough to reduce the size of reformer.
A small-sized methanol-steam reforming apparatus using methanol as a fuel for combustion and as a raw material for reforming reaction at the same time is disclosed in J. of Power source, 108 (2002) 21 - 27 by the Pacific North National Laboratory. However, this apparatus has drawbacks that its output is as low as about 200 mW, and that the total heat efficiency is as low as 5 to 10 % since the amount of methanol as a fuel fed into
combustor to maintain the reaction temperature is large.
Therefore, there still has been a urgent need to develop a hydrogen generating apparatus whose weight and size are small but has high heat efficiency and conversion ratio to hydrogen, and which is capable of generating a large amount of hydrogen.
DISCLOSURE OFTHE INVENTION
The present invention is to solve the problems of the conventional technologies as described above. Therefore, the object of the present invention is to provide a hydrogen generating apparatus comprising unit reaction devices comprising micro-channels containing coated combustion catalyst and/or coated reforming catalyst, designed for generating hydrogen with high heat efficiency and high conversion ratio to hydrogen, in supplying hydrogen to fuel cell system or the like by using alcohol such as methanol as a raw material, and to a hydrogen generating method using the same.
The hydrogen generating apparatus according to the present invention comprises at least one first unit reaction device for combustion/ reforming reaction comprising a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst, wherein each of the plate assemblies comprises a pair of micro-channel plates, on the surface of one side of which micro- channels are formed, and which are combined to each other in a manner that the micro- channels are opposed to each other; wherein the plate assembly for combustion contains the combustion catalyst in the micro-channels; and wherein the plate assembly for reforming reaction contains the reforming catalyst in the micro-channels. The hydrogen generating apparatus according to the present invention comprises
at least one first unit reaction device for combustion/reforming reaction, at least one second unit reaction device for gasification, and at least one third unit reaction device for heat exchange, wherein the first unit reaction device comprises a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst; wherein the second unit reaction device comprises a plate assembly for combustion and a plate assembly for heat exchange; wherein the third unit reaction device comprises plate assemblies for heat exchange; wherein the plate assembly for combustion of the first unit reaction device is connected to one of the plate assemblies for heat exchange of the third unit reaction device; wherein the other of the plate assemblies for heat exchange of the third unit reaction device is connected to the plate assembly for combustion of the first unit reaction device; and wherein the plate assembly for heat exchange of the second unit reaction device is connected to the plate assembly for reforming reaction of the first unit reaction device.
The hydrogen generating method according to the present invention comprises, (1) a first combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion of the first unit reaction device and burning the fuel in the plate assembly for combustion, and heating the plate assembly for reforming reaction adjacent to the plate assembly for combustion by using the combustion heat; and (2) a reforming step of generating hydrogen by feeding a raw material for reforming reaction comprising a mixture of methanol and water to the heated plate assembly for reforming reaction and reforming the raw material, in generating hydrogen by using a hydrogen generating apparatus comprising at least one first unit reaction device for combustion/reforming reaction comprising a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst, wherein each of the plate assemblies comprises a pair of micro-channel plates, on
the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other; wherein the plate assembly for combustion contains the combustion catalyst in the micro-channels; and wherein the plate assembly for reforming reaction contains the reforming catalyst in the micro-channels.
The hydrogen generating method according to the present invention comprises, (1) a first combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion of the first unit reaction device and burning the fuel; (2) a first preheat step of preheating the third unit reaction device to 80 to 100 °C by emitting exhaust gas from the plate assembly for combustion in the first combustion step via one plate assembly for heat exchange of the third unit reaction device; (3) a second combustion step of heating the first unit reaction device to 260 to 320 °C by feeding and gasifying liquid fuel to the plate assembly for combustion of the first unit reaction device via the other plate assembly for heat exchange of the third unit reaction device, and burning the fuel with feeding oxidizing agent at the same time; (4) a third combustion step of heating the second unit reaction device to 110 to 200 °C by feeding fuel in gas phase to the plate assembly for combustion of the second unit reaction device and burning the fuel together with oxidizing agent; (5) a gasification step of gasifying a mixture of methanol and water as raw material for reforming reaction by passing through the plate assembly for combustion of the second unit reaction device and feeding the mixture to the plate assembly for reforming reaction of the first unit reaction device; and (6) a reforming step of reforming the gasified raw material to hydrogen by passing through the plate assembly for reforming reaction of the first unit reaction device, in generating hydrogen by using a hydrogen generating apparatus comprising at least one first unit reaction device for combustion/reforming reaction, at least one second unit reaction device for gasification,
and at least one third unit reaction device for heat exchange, wherein the first unit reaction device comprises a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst; wherein the second unit reaction device comprises a plate assembly for combustion and a plate assembly for heat exchange; wherein the third unit reaction device comprises a plate assemblies for heat exchange; wherein the plate assembly for combustion of the first unit reaction device is connected to one of the plate assemblies for heat exchange of the third unit reaction device; wherein the other of the plate assemblies for heat exchange of the third unit reaction device is connected to the plate assembly for combustion of the first unit reaction device; and wherein the plate assembly for heat exchange of the second unit reaction device is connected to the plate assembly for reforming reaction of the first unit reaction device.
BRIEF DESCRIPTION OF DRAWINGS
Figure 1 is a schematic diagram illustrating the overall constitution of the hydrogen generating apparatus according to the present invention.
Figure 2 is a diagram illustrating disassembly of the unit reaction device used in the hydrogen generating apparatus of Figure 1.
Figure 3 is a photograph for disassembly of an embodiment of the hydrogen generating apparatus according to the present invention.
Figure 4 is a diagram illustrating disassembly of only the plate assemblies constituting the unit reaction device of Figure 2.
Figure 5 is a plane figure of the micro-channel plate constituting the plate assemblies of Figure 4. Figure 6 is a plane figure of the gasket used in the plate assembly constituting the
unit reaction device according to the present invention.
Figure 7 is a side cross-sectional diagram of the plate assembly constituting the unit reaction device of Figure 2.
* Symbols shown in the Figures
11 : First unit reaction device
12 : Third unit reaction device
13 : Second unit reaction device
14 : Preferential oxidation reactor
15 : Fourth unit reaction device
21 : Hydrogen source
22 : First oxygen source
23: Valve for changing flow direction
24 : First fuel source
25 : Second oxygen source
26 : Second fuel source
27 : Raw material source
28 : Third oxygen source
31 : Filter
41 : Unit reaction device
41' : Plate assembly for combustion
41" : Plate assembly for reforming reaction
42 and 42' : Upper and lower cases
43 : combustor inlet
43' : combustor outlet
44 : reformer inlet
44' : reformer outlet
45 and 45' : Micro-channel plates
46 and 46' : Inlets
47 and 47' : Outlets
48 and 48' : First connecting apertures
49 and 49' : Second connecting apertures
51 and 51' : Micro-channels
52 and 52' : Separating walls
53 and 53' : Cutoff walls
54 and 54' : Convergent depressions
55 and 55' : Convergent prominences
61 : Gasket
62 : Opening
63 : Perforation hole
71 : Channel forming space
72 : Catalyst coating part
BEST MODE FOR CARRYING OUT THE INVENTION
In reference to the accompanying drawings, the present invention is described in more detail below.
As represented in Fig. 1, the hydrogen generating apparatus according to the present invention is characterized in comprising at least one first unit reaction device (11) for combustion/reforming reaction which is comprised of a plate assembly for combustion containing a coated combustion catalyst and a plate assembly for reforming reaction containing a coated reforming catalyst, wherein each of the plate assemblies comprises a pair of micro-channel plates, on the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other; wherein the plate assembly for combustion contains the combustion
catalyst in the micro-channels; and wherein the plate assembly for reforming reaction contains the reforming catalyst in the micro-channels. Accordingly, the characteristic of the present invention lies in that the heat for reforming reaction can be obtained from a plate assembly for combustion adjacent to a plate assembly for reforming reaction containing reforming catalyst whereby the reforming reaction can be conducted at optimized temperature to heighten heat efficiency and conversion ratio to hydrogen at the same time. Also, the characteristics also lie in that the present apparatus can be made smaller while performing the function of combustor in a conventional hydrogen generating apparatus by constituting the plate assembly for combustion to perform the function of combustor in which the combustion reaction is conducted, and having this combustion reaction in the plate assembly for combustion performed in the micro-channel, and that the apparatus can be made smaller while performing the function of reformer in a conventional hydrogen generating apparatus by constituting the plate assembly for reforming reaction to perform the function of reformer in which the reforming reaction is conducted, and having this reforming reaction in the plate assembly for reforming reaction performed in the micro-channel. Further, according to the present invention, as shown in Fig. 2, combustion heat is utilized in the reforming reaction at its maximum by constituting the first unit reaction device (11) comprising the plate assembly for combustion (41') and the plate assembly for reforming reaction (41") to make the plate assembly for combustion (41') and the plate assembly for reforming reaction (41") stacked alternately. Here, the expression "first" in the first unit reaction device (11) is used to distinguish the unit reaction device comprising both of the combustion catalyst and the reforming catalyst. Also, here, the combustion catalyst may be selected from the group consisting of platinum group elements such as platinum, rhodium, ruthenium, osmium, indium and palladium, gold, silver, copper and mixtures thereof. In particular, the combustion catalyst may be
supported by a catalyst support. The supporting of the combustion catalyst consists of coating a catalyst support firstly, then adding an aqueous solution of the combustion catalyst thereto in an amount of 0.1 to 5 wt% to the catalyst support, and then drying and calcining the mixture. Here, the catalyst support may be selected from the group consisting of aluminum oxide, α-aluminum oxide, zirconium oxide (ZrO2), silica (SiO2), ceria (CeO2) and mixtures thereof, and preferably, α-aluminum oxide may be used. However, the present invention is not limited thereto, and it is natural that other catalysts capable of being used for promoting oxidation of hydrocarbon, alcohol or the like may be also used in the present invention. Here, as a reforming catalyst, a synthesized product of copper/cerium oxide/zirconium oxide (Cu/CeO2/ZrO2), a synthesized product of copper/zinc oxide/aluminum oxide (Cu/ZnO2/Al2θ3), a synthesized product of copper/cerium oxide/aluminum oxide (Cu/CeO2/Al2O3), a synthesized product of copper/zirconium oxide/aluminum oxide (Cu/ZrO2/Al2O3), solid-solution copper-zinc-aluminum (CuZnAl) oxides or the like may be used, and preferably a synthesized product by co-precipitation method with a weight ratio of copper : zinc : aluminum oxide of 3 to 5 : 3 to 5 : 1 to 3. However, the present invention is not limited thereto, and it is natural that other catalysts capable of being used for reforming hydrocarbon, alcohol or the like to generate hydrogen may be also used in the present invention. As shown in Fig. 2, the unit reaction device (41) constituting the first unit reaction device (11) comprises cases (42 and 42') consisting of two metallic blocks, wherein the plate assembly for combustion (41') and the plate assembly for reforming reaction (41") are stacked alternately and fixed between the cases (42 and 42'). Among the cases (42 and 42'), for example, combustor outlet (43') and reformer outlet (44') are formed in the upper case (42), and combustor inlet (43) and reformer inlet (44) are formed in the lower
case (42'). However, it is naturally understandable that these quotation marks are just for reference, and the inverse case may function. A photograph for disassembly of an embodiment of the unit reaction device is shown in Fig. 3. In the example of constitution shown in Fig. 3, the thickness of the micro-channel plate (45) is about 0.3 mm, and the micro-channel is formed with a depth of 10 to 150 μm. Channel is formed on metal plate in a parallelogramic form, and holes allowing fluid to flow are formed at each vertex of the metal plate.
As shown in Figs. 2, 4 and 5, the plate assemblies constituting the unit reaction device (41) comprise a pair of micro-channel plates (45 and 45'), on the surface of one side of which micro-channels (51 and 51') are formed in common, and which are combined to each other in a manner that the micro-channels (51 and 51') are opposed to each other, and the plate assembly for combustion (41') contains the combustion catalyst in the micro- channels (51 and 51'); and the plate assembly for reforming reaction (41") contains the reforming catalyst in the micro-channels (51 and 51'). All of the cases and micro- channels can be molded out of metal, preferably material having good corrosion resistance and heat resistance such as stainless steel or the like. A gasket (61) may be inserted between the micro-channel plates (45 and 45'), as shown in Fig. 6. Preferably, the gasket (61) may be made up of copper plate, and consist of openings (62) and perforation holes (63) formed to make a uniform space between the micro-channel plates (45 and 45'). Accordingly, as shown in an example of Fig. 2, two or more plate assemblies such as the plate assembly for combustion (41') and the plate assembly for reforming reaction (41") can be stacked with each other. If necessary, i.e. according to the amount of hydrogen desired to be generated or the like, the number of the plate assembly for combustion (41') and the plate assembly for reforming reaction (41") to be stacked may be increased or decreased. In the inside of each plate assembly, as shown in Fig. 7, plural channel
forming spaces (71) are formed, and the inner walls function as catalyst coating part (72) wherein catalysts such as the combustion catalyst or the reforming catalyst are coated.
Among the micro-channel plates (45 and 45'), as shown in Figs. 4 and 5, upper micro-channel plate (45) has an inlet (46), an outlet(47), first connecting aperture (48) and second connecting aperture (49), wherein the inlet and the outlet are located diagonally to each other, and the first connecting aperture and the second connecting aperture are located diagonally to each other, and wherein a groove having certain depth from surface with including the inlet (46) and the outlet (47) is formed between the inlet (46) and the outlet (47), and the wall of the groove functions as a cutoff wall (53) to restrict the flow direction of fuel or raw materials which pass through the micro-channels (51). In the groove, the micro-channels (51) are separated by separating walls (52) and formed in plural. Around the inlet (46) and the outlet (47), convergent depressions (54) and convergent prominences (55) to restrict the flow of fuel or raw materials so as to diffuse the fuel or raw materials from the inlet (46) or the outlet (47) to the micro-channels (51) or to collect the fuel or raw materials to the inlet (46) or the outlet (47) are formed. Among the micro-channel plates (45 and 45'), lower micro-channel plate (45') is the same as the upper micro-channel plate (45), but has a mirror-image symmetrical structure thereto, and so refers to the same symbols, only distinguished by the symbol (').
Also, according to the present invention, as shown in Fig. 2, even in the case that two or more plate assemblies for combustion (41') and plate assemblies for reforming reaction (41") are stacked alternately to each other, the flow of fuel and the flow of raw material do not cross each other. Referring to Fig. 2, the fuel flowing in the combustor inlet (43) flows into the inside of the plate assembly for combustion (41') through the inlet (46) of the plate assembly for combustion (41'), is burned in passing the micro-channels, then exits through the outlet (47) of the plate assembly for combustion (41'), then passes
through the second connecting aperture (49) of the plate assembly for reforming reaction (41") placed in the upper stage, and then flows in the outlet (47) of the plate assembly for combustion (41') placed in the upper stage. This is also applied to the flow of raw material to the plate assembly for reforming reaction (41") in the same manner, and so the fuel and the raw material can flow separately from each other.
Hydrogen can be generated by generating combustion heat by feeding and burning fuel in gas phase, preferably hydrogen, together with oxidizing agent, preferably oxygen or air, from hydrogen source (21) and first oxygen source (22) through the combustor inlet (43) to the plate assembly for combustion (41') of the first unit reaction device (11) in the plate assembly for combustion (41'), supplying the heat to the plate assembly for reforming reaction (41") adjacent thereto, and feeding a mixture of methanol and water as a raw material from the raw material source (27) to the plate assembly for reforming reaction (41"), and converting methanol to hydrogen. Instead of using the combustion heat, the reforming reaction may also be conducted by passing heat flow through the inside of the plate assembly for combustion (41') of the first unit reaction device (11), and it is naturally understandable by a skilled person in the art that where exhaust heat is generated in a large scale, heat flow having such exhaust heat may also be used. In this case, the plate assembly for combustion (41') may not contain the combustion catalyst therein.
As shown in Fig. 1, a third unit reaction device (12) may be further connected to the first unit reaction device (11). The third unit reaction device (12) comprises plate assemblies for heat exchange comprising a pair of micro-channel plates, on the surface of one side of which micro-channels are formed and which are combined to each other in a manner that the micro-channels are opposed to each other. It can be understood that the plate assemblies for heat exchange have a structure the same as or similar to the plate assembly for combustion (41') or the plate assembly for reforming reaction (41"), only
except that the plate assemblies for heat exchange do not contain catalysts such as a combustion catalyst, a reforming catalyst and the like at all, and enable heat exchange between fluids passing the plate assemblies adjacent to each other by allowing the fluids to pass the micro-channels. Here, the expression "third" in the third unit reaction device (12) is used to distinguish the unit reaction device comprising neither the combustion catalyst nor the reforming catalyst. The third unit reaction device (12) may be connected to the plate assembly for combustion (41') of the first unit reaction device (11), wherein the inlet of one of the plate assemblies for heat exchange of the third unit reaction device (12) may be connected to the outlet of the plate assembly for combustion (41') of the first unit reaction device (11).
Accordingly, the exhaust gas emitted from the plate assembly for combustion (41') of the first unit reaction device (11) passes through one of the plate assemblies for heat exchange of the third unit reaction device (12), and heats other plate assembly for heat exchange adjacent thereto, whereby a fluid passing inside of the other plate assembly for heat exchange can be heated. At this time, if the first fuel source (24) connects to the other plate assembly for heat exchange and liquid fuel supplied therefrom passes through the other plate assembly for heat exchange, this liquid fuel is gasified, and the gasified fuel is connected again to the plate assembly for combustion (41') of the first unit reaction device (11), and the combustion reaction can continue. Therefore, during initial preheating, after preheating the first unit reaction device (11) and the third unit reaction device (12) to a given temperature, for example, 260 to 320 °C for the first unit reaction device (11) and 80 to 100 °C for the third unit reaction device (12), by using the fuel in gas phase, the reforming reaction can be continued by cutting off the fuel in gas phase and continuing the combustion reaction with using the fuel gasified by the third unit reaction device (12). A small-sized hydrogen generating apparatus can use liquid fuel which is
more convenient to handle and store, with minimizing the use of fuel in gas phase which is inconvenient to handle and store. As the liquid fuel, methanol may be preferred. The constitution as shown above enables efficient use of fuel by gasifying liquid fuel with using exhaust heat of exhaust gas emitted from the first unit reaction device (11). A second unit reaction device (13) may be connected to the first unit reaction device (11). The second unit reaction device (13) comprises a plate assembly for combustion and a plate assembly for heat exchange. The second unit reaction device (13) may be connected to the plate assembly for reforming reaction (41") of the first unit reaction device (11), wherein the outlet of the plate assembly for heat exchange of the second unit reaction device may be connected to the inlet of the plate assembly for reforming reaction of the first unit reaction device. It can be understood that the plate assembly for combustion of the second unit reaction device (13) has a constitution the same as or similar to the plate assembly for combustion (41') of the first unit reaction device (11). Here, the expression "second" in the second unit reaction device (13) is used to distinguish the unit reaction device comprising the combustion catalyst only. The second unit reaction device (13) functions to promote the reforming reaction in the first unit reaction device (11) by heating and gasifying a mixture of methanol and water as a fuel supplied to the first unit reaction device (11). That is, the fuel in gas phase is supplied and burnt together with oxidizing agent by connecting a hydrogen source (21) and a second oxygen source (25) to the plate assembly for combustion of the second unit reaction device (13); a plate assembly for heat exchange adjacent to the plate assembly for combustion of the second unit reaction device (13) is heated by using the combustion heat; a mixture of methanol and water as a raw material is passed through the inside of the plate assembly for heat exchange and gasified, by connecting a raw material source (27) to the plate assembly for heat exchange; and the gasified raw material is supplied to the plate
assembly for reforming reaction (41") of the first unit reaction device (11) to be reformed. The second unit reaction device (13) may be maintained, for example, in the range of 110 to 200 °C .
A fourth unit reaction device (15) may be connected further between the second unit reaction device (13) and the first unit reaction device (11). The fourth unit reaction device (15) comprises plate assemblies for heat exchange. Here, the expression "fourth" in the fourth unit reaction device (15) is used to distinguish the unit reaction device comprising neither the combustion catalyst nor the reforming catalyst. That is, by connecting the outlet of any one of the plate assemblies for heat exchange of the fourth unit reaction device (15) to the inlet of the plate assembly for combustion of the second unit reaction device (13), and at the same time, connecting a second fuel source (26) of liquid fuel source to the inlet of the plate assembly, and connecting the inlet of the other plate assembly for heat exchange of the fourth unit reaction device (15) to the outlet of the plate assembly for reforming reaction (41") of the first unit reaction device (11), the liquid fuel may be gasified by using the heat of product flow emitted therefrom, and supplied to the plate assembly for combustion of the second unit reaction device (13), to conduct the combustion reaction. By this, the combustion reaction can be continued by using the fuel gasified by the fourth unit reaction device (15) while the fuel in gas phase supplied from the hydrogen source (21) is cut off. Thus, in operating a small-sized hydrogen generating apparatus, it can be minimized to use the fuel in gas phase which is inconvenient to handle and store, and the liquid fuel which is more convenient to handle and store can be used. As the liquid fuel, methanol may be preferred. The constitution as shown above enables efficient use of fuel by gasifying liquid fuel with using exhaust heat of product flow emitted from the first unit reaction device (11). A preferential oxidation reactor (14) may be further connected to the outlet of the
plate assembly for reforming reaction (41") of the first unit reaction device (11). The preferential oxidation reactor (14) functions to conduct the oxidation of carbon monoxide to remove carbon monoxide which could be included in hydrogen as a product reformed and produced by the first unit reaction device (11), whereby the hydrogen produced from the apparatus of the present invention can be directly connected to fuel cell or the like and used, without additional purification procedure, since carbon monoxide which can affect to the electrode of fuel cell is removed at a maximum. For the preferential oxidation reactor (14), the plate assemblies according to the present invention are used. Preferential oxidation reactor may have a structure the same as or similar to the plate assembly, only except further comprising a preferential oxidation catalyst, instead of the combustion catalyst or the reforming catalyst as described above. To the preferential oxidation reactor (14), a third oxygen source (28) for supplying oxygen or air for oxidation of carbon monoxide is connected.
A filter may be connected between the plate assembly for reforming reaction (41") of the first unit reaction device (11) and the preferential oxidation reactor (14). The filter may be a conventional mechanical filter.
As shown in Figs. 1 to 7, the hydrogen generating apparatus according to the present invention is characterized in comprising at least one first unit reaction device (11) for combustion/reforming reaction, at least one second unit reaction device (13) for gasification, and at least one third unit reaction device (12) for heat exchange, wherein the first unit reaction device (11) comprises a plate assembly for combustion (41') comprising a combustion catalyst and a plate assembly for reforming reaction (41") comprising a reforming catalyst; wherein the second unit reaction device (13) comprises a plate assembly for combustion and a plate assembly for heat exchange; wherein the third unit reaction device (12) comprises a plate assemblies for heat exchange; wherein the plate
assembly for combustion (41') of the first unit reaction device (11) is connected to one of the plate assemblies for heat exchange of the third unit reaction device (12); wherein the other of the plate assemblies for heat exchange of the third unit reaction device (12) is connected to the plate assembly for combustion (41') of the first unit reaction device (11); and wherein the plate assembly for heat exchange of the second unit reaction device (13) is connected to the plate assembly for reforming reaction (41") of the first unit reaction device (11).
To the plate assembly for combustion (41') of the first unit reaction device (11), a valve for changing flow direction (23) is connected. And, to this valve for changing flow direction (23), a hydrogen source (21) is connected. The valve for changing flow direction (23) may be a 4-way valve preferably so that hydrogen supplied from the hydrogen source connected thereto can be firstly fed into the plate assembly for combustion (41') of the first unit reaction device (11) for reduction, then into the plate assembly for reforming reaction (41") for reduction, and finally into the plate assembly for combustion of the second unit reaction device (13) in order. By this, if the temperatures of the first unit reaction device (11) and the third unit reaction device (12) connected thereto are elevated higher than the boiling point of methanol as a fuel by using the hydrogen as a fuel, the fuel is replaced from hydrogen to methanol. And, after elevating the temperature of the first unit reaction device (11) to the reduction temperature (about 300 °C) by the continued combustion reaction of methanol, the reforming catalyst in the plate assembly for reforming reaction (41") can be reduced by hydrogen.
By the constitution as above, the present invention provides such advantages that by conducting the combustion reaction in the plate assembly for combustion of the unit reaction device comprising a micro-channel, and stacking and placing the plate assembly for reforming reaction adjacent thereto, thereby enabling the plate assembly for reforming
reaction where the reforming reaction is conducted to maintain a stable operation temperature, the conversion ratio of methanol and the composition of hydrogen in the product can be raised, and high heat efficiency and hydrogen productivity can be exhibited by lowering the content of carbon monoxide; and the apparatus can be smaller and attached directly to a fuel cell or the like to supply hydrogen by reducing the content of carbon monoxide. Also, the present invention provides an advantage that fuel cell can be operated without deactivating the electrode of the fuel cell by removing carbon monoxide as much as possible by further comprising preferential oxidation reactor.
The hydrogen generating method according to the present invention comprises (1) a first combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion (41') of the first unit reaction device (11) and burning the fuel in the plate assembly for combustion (41'), and heating the plate assembly for reforming reaction (41") adjacent to the plate assembly for combustion (41') by using the combustion heat; and (2) a reforming step of generating hydrogen by feeding raw material for reforming reaction comprising a mixture of methanol and water to the heated plate assembly for reforming reaction (41") and reforming the raw material, in generating hydrogen by using a hydrogen generating apparatus comprising at least one first unit reaction device (11) for combustion/reforming reaction comprising a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst, wherein each of the plate assemblies comprises a pair of micro-channel plates, on the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other; wherein the plate assembly for combustion contains the combustion catalyst in the micro-channels; and wherein the plate assembly for reforming reaction contains the reforming catalyst in the micro-channels. The plate assembly for reforming reaction
(41") is heated by supplying the combustion heat generated from the first combustion step, and the reforming reaction is conducted by using this heat. Accordingly, the characteristic of the present invention lies in that by conducting the combustion reaction in the plate assembly for combustion (41') of the unit reaction device comprising a micro- channel, and stacking and placing the plate assembly for reforming reaction (41") adjacent thereto, thereby enabling the plate assembly for reforming reaction (41") where the reforming reaction is conducted to maintain a stable operation temperature of 260 to 320 °C , the conversion ratio of methanol and the composition of hydrogen in the product can be raised, and high heat efficiency and hydrogen productivity can be exhibited by lowering the content of carbon monoxide. Here, if the temperature of the first unit reaction device (11) is lower than 260 °C, the conversion ratio to hydrogen may decrease since the temperature of the reforming reaction is too low, and to the contrary, if it is higher than 320 °C , the content of carbon monoxide in product is raised too much, and the concentration of carbon monoxide cannot be sufficiently lowered in spite of subsequent preferential oxidation reaction, and so the hydrogen productivity may decrease. If the concentration of carbon monoxide becomes relatively high, there may be a problem that the hydrogen as a product cannot be incorporated directly as a fuel for fuel cell.
The hydrogen generating method according to the present invention may further comprise, between the first combustion step (1) and the reforming step (2), a first connection step of connecting a third unit reaction device (12) comprising plate assemblies for heat exchange, each of which comprises a pair of micro-channel plates, on the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other, to the plate assembly for combustion (41') of the first unit reaction device (11), wherein any inlet of the plate assembly for heat exchange of the third unit reaction device (12) is connected to an outlet
of the plate assembly for combustion (41') of the first unit reaction device (11); and a first gasification step of connecting exhaust gas emitted from the plate assembly for combustion (41') of the first unit reaction device (11) to one plate assembly for heat exchange of the third unit reaction device (12), and feeding liquid fuel to the other plate assembly for heat exchange to gasify the liquid fuel. The characteristic lies in that by the first connection step, the third unit reaction device (12) is connected to the first unit reaction device (11), and the liquid fuel is gasified by using the exhaust gas emitted from the first unit reaction device (11), and by supplying the gasified fuel again to the first unit reaction device (11) to use it as a fuel, if the reaction is started and the third unit reaction device (12) is heated to a given temperature, preferably 80 to 100 °C, further use of the fuel in gas phase is stopped and the liquid fuel is used, whereby it is possible to minimize the use of fuel in gas phase which is inconvenient to handle and store, and to use liquid fuel which is more convenient to handle and store. If the temperature of the third unit reaction device is lower than 80 "C, the liquid fuel cannot be sufficiently gasified, and in real process operation, there is no case that the temperature is higher than 100 °C .
The hydrogen generating method according to the present invention may further comprise, between the first combustion step (1) and the reforming step (2), a second connection step of connecting a second unit reaction device (13) comprising a plate assembly for combustion and a plate assembly for heat exchange to the plate assembly for reforming reaction (41") of the first unit reaction device (11), wherein an outlet of the plate assembly for heat exchange of the second unit reaction device (13) is connected to an inlet of the plate assembly for reforming reaction (41") of the first unit reaction device (11); a second combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion of the second unit reaction device (13), burning the fuel in the plate assembly for combustion, and heating the plate assembly for heat exchange
adjacent to the plate assembly for combustion by using the combustion heat; a second gasification step of feeding raw material for reforming reaction comprising a mixture of methanol and water to the plate assembly for heat exchange of the second unit reaction device (13) to gasify the raw material; and a first feed step of feeding the gasified raw material for reforming reaction in the second gasification step to the plate assembly for reforming reaction (41") of the first unit reaction device (11). By the second connection step, the second unit reaction device (13) is connected to the first unit reaction device (11), and the reforming reaction can be conducted smoothly by firstly gasifying the raw material which is introduced into the first unit reaction device (11) and reformed, by using the combustion heat from the combustion reaction in the plate assembly for combustion of the second unit reaction device (13), whereby the heat efficiency and the conversion ratio to hydrogen can be raised.
The hydrogen generating method according to the present invention may further comprise, between the first combustion step (1) and the reforming step (2), a third connection step of connecting a fourth unit reaction device (15) comprising plate assemblies for heat exchange to the plate assembly for combustion of the second unit reaction device (13), wherein any one outlet of the plate assembly for heat exchange of the fourth unit reaction device (15) is connected to an inlet of the plate assembly for combustion of the second unit reaction device (13), and an inlet of the plate assembly for heat exchange is connected to a source of liquid fuel; a fourth connection step of connecting the other inlet of the fourth unit reaction device (15) to an outlet of the plate assembly for reforming reaction of the first unit reaction device (11), and connecting an outlet of the plate assembly for heat exchange to a product collector; and a third gasification step of gasifying the liquid fuel fed to the second unit reaction device (13) by using heat from product flow emitted from the plate assembly for reforming reaction of the
first unit reaction device (11). Thus, the characteristic lies in that until the second unit reaction device (13) is raised to a given temperature, preferably 110 to 200 °C, and the fourth unit reaction device (15) is sufficiently preheated by the product flow emitted from the first unit reaction device (11), the process is operated by using fuel in gas phase, i.e. hydrogen, and after the second unit reaction device (13) is raised to a given temperature, preferably 110 to 200 °C, the liquid fuel, i.e. methanol, is supplied to, and gasified in, the fourth unit reaction device (15), and by supplying the gasified fuel to the second unit reaction device (13) to use it as a fuel, it is possible to minimize the use of fuel in gas phase which is inconvenient to handle and store, and use liquid fuel which is more convenient to handle and store. If the temperature of the third unit reaction device is lower than 110 "C, liquid fuel may not be sufficiently gasified, and in real process operation, there is no case that the temperature exceeds 200 °C .
The hydrogen generating method according to the present invention is characterized in comprising, (1) a first combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion of the first unit reaction device and burning the fuel; (2) a first preheat step of preheating the third unit reaction device to 80 to 100 °C by emitting exhaust gas from the plate assembly for combustion in the first combustion step via one plate assembly for heat exchange of the third unit reaction device; (3) a second combustion step of heating the first unit reaction device to 260 to 320 °C by feeding and gasifying liquid fuel to the plate assembly for combustion of the first unit reaction device via the other plate assembly for heat exchange of the third unit reaction device, and burning the fuel with feeding oxidizing agent at the same time; (4) a third combustion step of heating the second unit reaction device to 110 to 200 °C by feeding fuel in gas phase to the plate assembly for combustion of the second unit reaction device and burning the fuel together with oxidizing agent; (5) a gasification step of
gasifying a mixture of methanol and water as raw material for reforming reaction by passing through the plate assembly for combustion of the second unit reaction device and feeding the mixture to the plate assembly for reforming reaction of the first unit reaction device; and (6) a reforming step of reforming the gasified raw material to hydrogen by passing through the plate assembly for reforming reaction of the first unit reaction device, in generating hydrogen by using the present hydrogen generating apparatus comprising at least one first unit reaction device for combustion/reforming reaction, at least one second unit reaction device for gasification, and at least one third unit reaction device for heat exchange, wherein the first unit reaction device comprises a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst; wherein the second unit reaction device comprises a plate assembly for combustion and a plate assembly for heat exchange; wherein the third unit reaction device comprises plate assemblies for heat exchange; wherein the plate assembly for combustion of the first unit reaction device is connected to one of the plate assemblies for heat exchange of the third unit reaction device; wherein the other of the plate assemblies for heat exchange of the third unit reaction device is connected to the plate assembly for combustion of the first unit reaction device; and wherein the plate assembly for heat exchange of the second unit reaction device is connected to the plate assembly for reforming reaction of the first unit reaction device. In generating hydrogen by using the hydrogen generating apparatus according to the present invention as shown above, the above method may be used as optimized example. That is, to initiate the reforming reaction, first, a gas mixture of hydrogen and air or oxygen is supplied to the first unit reaction device (11) and burnt in the plate assembly for combustion (41'); heat generated at this time is exhausted with exhaust gas via the third unit reaction device (12), and after methanol as liquid fuel is supplied to third
unit reaction device (12) and gasified, the gasified methanol is supplied again to the first unit reaction device (11) to continue the combustion reaction. Here, if the combustion reaction is initiated by methanol, the supply of hydrogen as a fuel in gas phase is stopped, and hydrogen is supplied to the second unit reaction device (13), with air or a gas mixture of oxygen. On the other hand, the combustion reaction is continued by adjusting the feeding ratio of methanol until the temperature of the first unit reaction device (11) reaches up to 260 to 320 °C , and if reached, the combustion reaction is conducted by supplying a mixture of methanol and water as a raw material to the plate assembly for reforming reaction (41") of the first unit reaction device (11), and the hydrogen flow as a product flow is supplied to the fourth unit reaction device (15). In the fourth unit reaction device (15), methanol as a liquid fuel is also gasified and supplied to the second unit reaction device (13). In the second unit reaction device (13), the combustion reaction is also conducted, and if the temperature reaches to 110 to 200 0C , the operation initiation step of the hydrogen generating apparatus according to the present invention is completed, and the combustion reaction is continued in the first unit reaction device (11) and the second unit reaction device (13) by continuously using methanol only as a liquid fuel, and hydrogen is generated continuously by reforming a mixture of methanol and water as a raw material in the plate assembly for reforming reaction (41") of the first unit reaction device (11).
The present invention can be more specifically explained by the following example. However, it should be understood that the present invention is not limited by the example in any manner.
Example 1
A plate assembly for reforming reaction was constituted by using a
copper/zinc/aluminum oxide synthesized by co-precipitation method in the weight ratio of 4/4/2 as a reforming catalyst, and coating it in the amount of 0.6 g per micro-channel plate of the plate assembly for reforming reaction of the first unit reaction device. A plate assembly for combustion was constituted by firstly coating α-aluminum oxide as a combustion catalyst on a micro-channel plate, and adding an aqueous solution of platinum having the platinum amount of about 3 wt% to the α-aluminum oxide, and drying and calcining the plate. The first unit reaction device was constituted by stacking six plate assemblies for reforming reaction and five plate assemblies for combustion, as constituted above, alternately to each other, and the reforming reaction was conducted by starting the operation with adjusting the temperature of the first unit reaction device to about 300 °C , without attaching a preferential oxidation reactor. At that time, the mixture ratio of methanol : water as a raw material for reforming reaction was 50 : 50, and the flow rate of the raw material for reforming reaction supplied into the first unit reaction device was adjusted to 3 cc/min, and the flow rate of methanol as a fuel was adjusted to 1.1 cc/min. Under such operation conditions, the first unit reaction device was reached to the above temperature after about 90 minutes. When the first unit reaction device was operated at 300 "C , the composition ratio of the product after reforming reaction was analyzed as 74.8 % of hydrogen, 24.4 % of carbon dioxide, and 0.84% of carbon monoxide, based on dry weight which moisture was removed. Based upon the amount of methanol participated in the reforming reaction, the conversion ratio of methanol was 99.5 %. The heat efficiency indicating the operation efficiency was calculated by using the following Equation (1), based on J. of Power source, 108 (2002) 21 - 27 by the Pacific North National Laboratory that describes a small aqueous vapor reforming apparatus of methanol mentioned in the present application as a prior art, for objective comparison:
[Equation (I)]
Operation efficiency = (Δ Hc H2) / (Δ Hc total CH3OH) CH3OH (lquid) + 1.5 O2 = CO2 + 2H2O (lquid) Δ H = -726 kJ/mol H2 + 0.5 O2 = H2O (gas) Δ H = -242 kJ/mol
In the above equation, Δ Hc H2 is total enthalpy of the hydrogen generated, and Δ Hc total CH3OH is total enthalpy of the total methanol participated in the reforming reaction and the combustion reaction. As a result of calculation according to the above equation, the heat efficiency of the hydrogen generating apparatus according to the present invention was 59.5 %. Also, after connecting a preferential oxidation reactor, the content of carbon monoxide in the hydrogen product was lowered to 70 ppm. The heat efficiency at that time was also lowered to 56.7 % since some hydrogen was reacted together during the preferential oxidation reaction.
INDUSTRIAL APPLICABILITY
According to the hydrogen generating apparatus comprising unit reaction devices micro-channel comprising the coating of combustion catalyst and/or reforming catalyst, and the hydrogen generating method using the same according to the present invention, by using the unit reaction device comprising a plate assembly for combustion comprising a combustion catalyst on micro-channel and a plate assembly for reforming reaction comprising a reforming catalyst on micro-channel, stacking them adjacent to each other, conducting the combustion reaction and the reforming reaction in maintaining the
reforming reaction in a constant temperature range, transferring the heat generated from the combustion reaction to the reforming reaction rapidly due to the constitution that where the reforming reaction occurs is close to where the combustion reaction occurs, and conducting the combustion reaction and the reforming reaction in micro-channel in maintaining high reaction temperature, the conversion ratio of methanol of 99 % or more and the high heat efficiency of 59.5 % or more in generating hydrogen can be achieved. Also, the present hydrogen generating apparatus and hydrogen generating method using the same designed for generating hydrogen with high heat efficiency and high conversion ratio to hydrogen are effective for supplying hydrogen to a fuel cell system by using alcohol such as methanol as a fuel since all of the combustion reaction and the reforming reaction can be conducted by using micro-channel, and the hydrogen generating apparatus itself can be very smaller by the gasification by heat exchange. Further, the production amount of hydrogen can be controlled optionally only by adjusting the stacking number of these plate assemblies by constituting the plate assemblies for combustion and the plate assemblies for reforming reaction as a unit.
Claims
1. A hydrogen generating apparatus comprising at least one first unit reaction device for combustion/reforming reaction comprising a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst, wherein each of the plate assemblies comprises a pair of micro-channel plates, on the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other; wherein the plate assembly for combustion contains the combustion catalyst in the micro-channels; and wherein the plate assembly for reforming reaction contains the reforming catalyst in the micro-channels.
2. The hydrogen generating apparatus according to claim 1, wherein the first unit reaction device comprises the plate assembly for combustion and the plate assembly for reforming reaction which are stacked alternately.
3. The hydrogen generating apparatus according to claim 1, wherein the combustion catalyst is selected from the group consisting of platinum group elements such as platinum, rhodium, ruthenium, osmium, iridium, and palladium; gold; silver; copper and mixtures thereof.
4. The hydrogen generating apparatus according to claim 3, wherein the combustion catalyst is formed by coating a catalyst support, adding the combustion catalyst thereto in an amount of 0.1 to 5 wt% to the catalyst support, and drying, calcining, and supporting the combustion catalyst.
5. The hydrogen generating apparatus according to claim 4, wherein the catalyst support is selected from the group consisting of aluminum oxide, α-aluminum oxide, zirconium oxide (ZrO2), silica (SiO2), or mixtures thereof.
6. The hydrogen generating apparatus according to claim 1, wherein the reforming catalyst is selected from the group consisting of a synthesized product of copper/cerium oxide/zirconium oxide (Cu/CeO2/ZrO2), a synthesized product of copper/zinc oxide/aluminum oxide (Cu/ZnO2/Al2O3), a synthesized product of copper/cerium oxide/aluminum oxide (Cu/CeO2/Al2O3), a synthesized product of copper/zirconium oxide/aluminum oxide (CuZZrO2ZAl2Os) and solid-solution copper- zinc-aluminum (CuZnAl) oxides.
7. The hydrogen generating apparatus according to claim 6, wherein the reforming catalyst is a synthesized product by co-precipitation method with a weight ratio of copper : zinc : aluminum oxide of 3 to 5 : 3 to 5 : 1 to 3.
8. The hydrogen generating apparatus according to claim 1, wherein the first unit reaction device comprises a unit reaction device comprising cases consisting of two metallic blocks, and wherein the plate assembly for combustion and the plate assembly for reforming reaction are stacked alternately between the cases.
9. The hydrogen generating apparatus according to claim 8, wherein each of the plate assemblies constituting the unit reaction device comprises a pair of micro-channel plates, on the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other.
10. The hydrogen generating apparatus according to claim 8, further comprising a gasket made of copper plate.
11. The hydrogen generating apparatus according to claim 9, wherein the micro-channel plate has an inlet, an outlet, first connecting aperture, and second connecting aperture, wherein the inlet and the outlet are located diagonally to each other, and the first connecting aperture and the second connecting aperture are located diagonally to each other, and wherein a groove having a certain depth from surface with including the , inlet and the outlet is formed between the inlet and the outlet.
12. The hydrogen generating apparatus according to claim 11, wherein convergent depressions and convergent prominences to restrict the flow of fuel or raw materials so as to diffuse the fuel or raw materials from the inlet or outlet to the micro-channels or to collect the fuel or raw materials to the inlet or outlet are formed around the inlet and the outlet.
13. The hydrogen generating apparatus according to claim 1, wherein a third unit reaction device (12) is connected to the first unit reaction device.
14. The hydrogen generating apparatus according to claim 13, wherein the third unit reaction device comprises a plate assembly for heat exchange comprising a pair of micro-channel plates, on the surface of one side of which micro-channels are formed, and which are combined to each other in a manner that the micro-channels are opposed to each other; wherein the plate assembly for heat exchange does not contain a catalyst such as combustion catalyst or reforming catalyst.
15. The hydrogen generating apparatus according to claim 1, wherein a second unit reaction device is connected to the first unit reaction device.
16. The hydrogen generating apparatus according to claim 15, wherein the second unit reaction device comprises a plate assembly for combustion and a plate assembly for heat exchange.
17. The hydrogen generating apparatus according to claim 15, wherein a fourth unit reaction device is connected between the second unit reaction device and the first unit reaction device.
18. The hydrogen generating apparatus according to claim 17, wherein the fourth unit reaction device comprises plate assemblies for heat exchange.
19. The hydrogen generating apparatus according to claim 1, wherein a preferential oxidation reactor is further connected to the first unit reaction device.
20. The hydrogen generating apparatus according to claim 19, wherein a filter is connected between the first unit reaction device and the preferential oxidation reactor.
21. A hydrogen generating apparatus comprising at least one first unit reaction device for combustion/reforming reaction, at least one second unit reaction device for gasification, and at least one third unit reaction device for heat exchange, wherein the first unit reaction device comprises a plate assembly for combustion comprising a combustion catalyst and a plate assembly for reforming reaction comprising a reforming catalyst; wherein the second unit reaction device comprises a plate assembly for combustion and a plate assembly for heat exchange; wherein the third unit reaction device comprises a plate assemblies for heat exchange; wherein the plate assembly for combustion of the first unit reaction device is connected to one of the plate assemblies for heat exchange of the third unit reaction device; wherein the other of the plate assemblies for heat exchange of the third unit reaction device is connected to the plate assembly for combustion of the first unit reaction device; and wherein the plate assembly for heat exchange of the second unit reaction device is connected to the plate assembly for reforming reaction of the first unit reaction device.
22. A hydrogen generating method using the hydrogen generating apparatus according to claim 1 comprising:
(1) a first combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion of the first unit reaction device, burning the fuel in the plate assembly for combustion, and heating the plate assembly for reforming reaction adjacent to the plate assembly for combustion by using the combustion heat; and
(2) a reforming step of generating hydrogen by feeding raw material for reforming reaction comprising a mixture of methanol and water to the heated plate assembly for reforming reaction and reforming the raw material.
23. The hydrogen generating method according to claim 22, wherein the temperature of the first unit reaction device is constantly maintained in the range of 260 to 320 0C .
24. The hydrogen generating method according to claim 22, further comprising, between the first combustion step (1) and the reforming step (2):
a first connection step of connecting a third unit reaction device comprising plate assemblies for heat exchange, each of which comprises a pair of micro-channel plates, on the surface of one side of which micro-channels are formed and which are combined to each other in a manner that the micro-channels are opposed to each other, to the plate assembly for combustion of the first unit reaction device, wherein any inlet of the plate assembly for heat exchange of the third unit reaction device is connected to an outlet of the plate assembly for combustion of the first unit reaction device; and
a first gasification step of connecting exhaust gas emitted from the plate assembly for combustion of the first unit reaction device to one plate assembly for heat exchange of the third unit reaction device, and feeding liquid fuel to the other plate assembly for heat exchange of the third unit reaction device to gasify the liquid fuel.
25. The hydrogen generating method according to claim 24, wherein the temperature of the third unit reaction device is constantly maintained in the range of 80 to 100 °C .
26. The hydrogen generating method according to claim 22, further comprising, between the first combustion step (1) and the reforming step (2): a second connection step of connecting a second unit reaction device comprising a plate assembly for combustion and a plate assembly for heat exchange to the plate assembly for reforming reaction of the first unit reaction device, wherein an outlet of the plate assembly for heat exchange of the second unit reaction device is connected to an inlet of the plate assembly for reforming reaction of the first unit reaction device;
a second combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion of the second unit reaction device, burning the fuel in the plate assembly for combustion, and heating the plate assembly for heat exchange adjacent to the plate assembly for combustion by using the combustion heat;
a second gasification step of feeding raw material for reforming reaction comprising a mixture of methanol and water to the plate assembly for heat exchange of the second unit reaction device to gasify the raw material; and
a first feed step of feeding the gasified raw material for reforming reaction in the second gasification step to the plate assembly for reforming reaction of the first unit reaction device.
27. The hydrogen generating method according to claim 22, further comprising between the first combustion step (1) and the reforming step (2): a third connection step of connecting a fourth unit reaction device comprising plate assemblies for heat exchange to the plate assembly for combustion of the second unit reaction device, wherein any one outlet of the plate assembly for heat exchange of the fourth unit reaction device is connected to an inlet of the plate assembly for combustion of the second unit reaction device, and an inlet of the plate assembly for heat exchange is connected to a source of liquid fuel;
a fourth connection step of connecting the other inlet of the fourth unit reaction device to an outlet of the plate assembly for reforming reaction of the first unit reaction device, and connecting an outlet of the plate assembly for heat exchange to a product collector; and
a third gasification step of gasifying the liquid fuel fed to the second unit reaction device by using heat from product flow emitted from the plate assembly for reforming reaction of the first unit reaction device.
28. The hydrogen generating method according to claim 27, wherein the temperature of the second unit reaction device is constantly maintained in the range of 110 to 200 °C .
29. A hydrogen generating method using the hydrogen generating apparatus according to claim 21 comprising:
(1) a first combustion step of feeding fuel in gas phase together with oxidizing agent to the plate assembly for combustion of the first unit reaction device and burning the fuel; (2) a first preheat step of preheating the third unit reaction device to 80 to 100 °C by emitting exhaust gas from the plate assembly for combustion in the first combustion step via one plate assembly for heat exchange of the third unit reaction device;
(3) a second combustion step of heating the first unit reaction device to 260 to 320 °C by feeding and gasifying liquid fuel to the plate assembly for combustion of the first unit reaction device via the other plate assembly for heat exchange of the third unit reaction device, and burning the fuel with feeding oxidizing agent at the same time;
(4) a third combustion step of heating the second unit reaction device to 110 to 200 °C by feeding fuel in gas phase to the plate assembly for combustion of the second unit reaction device and burning the fuel together with oxidizing agent;
(5) a gasification step of gasifying a mixture of methanol and water as raw material for reforming reaction by passing the mixture through the plate assembly for combustion of the second unit reaction device, and feeding the mixture to the plate assembly for reforming reaction of the first unit reaction device; and
(6) a reforming step of reforming the gasified raw material to hydrogen by passing it through the plate assembly for reforming reaction of the first unit reaction device.
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| JP2007556092A JP5252927B2 (en) | 2005-04-01 | 2006-04-03 | Hydrogen production apparatus and hydrogen production method using the same |
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| KR10-2005-0027570 | 2005-04-01 | ||
| KR20050027570 | 2005-04-01 |
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| PCT/KR2006/001219 WO2006109949A1 (en) | 2005-04-01 | 2006-04-03 | Hydrogen generating apparatus and hydrogen generating method using the hydrogen generating apparatus |
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| JP (1) | JP5252927B2 (en) |
| KR (1) | KR100733582B1 (en) |
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| WO (1) | WO2006109949A1 (en) |
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- 2006-04-03 JP JP2007556092A patent/JP5252927B2/en active Active
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI404827B (en) * | 2010-08-31 | 2013-08-11 | ||
| JP2013528560A (en) * | 2011-04-15 | 2013-07-11 | コリア インスティテュート オブ エナジー リサーチ | Hydrocarbon reformer using microchannel heater |
| JP2014517804A (en) * | 2011-05-09 | 2014-07-24 | コリア インスティテュート オブ エナジー リサーチ | Laminated hydrocarbon reformer using microchannel heater |
| US9266732B2 (en) | 2011-05-09 | 2016-02-23 | Korea Institute Of Energy Research | Apparatus for a hydrocarbon reforming using a micro-channel heater |
| CN106132532A (en) * | 2013-12-19 | 2016-11-16 | 乔治洛德方法研究和开发液化空气有限公司 | It is combined with the geometry of the catalytic reactor of good mechanical strength and the distribution of good fluid |
| CN106132532B (en) * | 2013-12-19 | 2019-03-29 | 乔治洛德方法研究和开发液化空气有限公司 | It is combined with the geometry of the catalytic reactor of good mechanical strength and the distribution of good fluid |
| CN111302305A (en) * | 2020-03-25 | 2020-06-19 | 哈尔滨工业大学 | Low-carbon monoxide micro hydrogen generation device utilizing methanol steam reforming |
| CN114955994A (en) * | 2022-06-14 | 2022-08-30 | 中南大学 | Hydrogen production device and system by cracking alcohol fuel |
Also Published As
| Publication number | Publication date |
|---|---|
| TW200711989A (en) | 2007-04-01 |
| JP5252927B2 (en) | 2013-07-31 |
| JP2008529953A (en) | 2008-08-07 |
| KR20060106778A (en) | 2006-10-12 |
| KR100733582B1 (en) | 2007-06-28 |
| TWI306081B (en) | 2009-02-11 |
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