WO2006100908A1 - 燃料改質装置 - Google Patents
燃料改質装置 Download PDFInfo
- Publication number
- WO2006100908A1 WO2006100908A1 PCT/JP2006/304408 JP2006304408W WO2006100908A1 WO 2006100908 A1 WO2006100908 A1 WO 2006100908A1 JP 2006304408 W JP2006304408 W JP 2006304408W WO 2006100908 A1 WO2006100908 A1 WO 2006100908A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- fuel
- reformer
- reforming
- superheater
- fuel reformer
- Prior art date
Links
- 239000000446 fuel Substances 0.000 title claims abstract description 160
- 230000004048 modification Effects 0.000 title abstract 4
- 238000012986 modification Methods 0.000 title abstract 4
- 239000012530 fluid Substances 0.000 claims abstract description 28
- 238000010438 heat treatment Methods 0.000 claims abstract description 17
- 238000001704 evaporation Methods 0.000 claims abstract description 5
- 238000002407 reforming Methods 0.000 claims description 58
- 239000003054 catalyst Substances 0.000 claims description 48
- 239000007789 gas Substances 0.000 claims description 36
- 238000002485 combustion reaction Methods 0.000 claims description 25
- 239000001257 hydrogen Substances 0.000 claims description 13
- 229910052739 hydrogen Inorganic materials 0.000 claims description 13
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 11
- 239000002737 fuel gas Substances 0.000 claims description 8
- 238000006057 reforming reaction Methods 0.000 claims description 5
- 230000001629 suppression Effects 0.000 claims description 5
- 230000001737 promoting effect Effects 0.000 claims description 3
- 230000003028 elevating effect Effects 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 20
- 239000000567 combustion gas Substances 0.000 description 15
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 12
- 238000005192 partition Methods 0.000 description 8
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- 238000013021 overheating Methods 0.000 description 5
- 230000017525 heat dissipation Effects 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000005452 bending Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 230000002093 peripheral effect Effects 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000003570 air Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 239000011865 Pt-based catalyst Substances 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000005219 brazing Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01B—BOILING; BOILING APPARATUS ; EVAPORATION; EVAPORATION APPARATUS
- B01B1/00—Boiling; Boiling apparatus for physical or chemical purposes ; Evaporation in general
- B01B1/005—Evaporation for physical or chemical purposes; Evaporation apparatus therefor, e.g. evaporation of liquids for gas phase reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
- B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00309—Controlling the temperature by indirect heat exchange with two or more reactions in heat exchange with each other, such as an endothermic reaction in heat exchange with an exothermic reaction
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
-
- 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
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift 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
- C01B2203/08—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
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0833—Heating by indirect heat exchange with hot fluids, other than combustion gases, product gases or non-combustive exothermic reaction product gases
Definitions
- the present invention relates to a fuel reformer that generates hydrogen-rich fuel gas by reforming a reforming fuel.
- a gas mainly containing hydrogen (hereinafter, also referred to as a hydrogen-containing gas) is supplied as a fuel gas.
- a hydrogen-containing gas generally, a reforming raw material gas obtained from hydrocarbon fuel such as fossil fuel such as methanol and LNG is obtained, and steam reforming, partial oxidation reforming, autothermal, etc. Reformed gas generated by reforming is used.
- the evaporator 1 is provided with an evaporative heat exchanger 4 having a heat exchanger that evaporates the water passing through the combustion exhaust gas, which is a heat exchange gas, to generate water vapor.
- the evaporative heat exchanger 4 includes a plurality of pipes 5 arranged in parallel to each other, and an inlet manifold 6 and an outlet manifold 7 in which the upstream end and the downstream end of the pipe 5 are opened.
- the inlet mould 6 is provided with a fibrous protrusion preventing member 8.
- the evaporator 1, the heat exchanger 2 and the reformer 3 are arranged in the flow direction of steam (arrow X direction).
- the heat exchanger 2 and the reformer 3 are connected by piping, although not shown. Therefore, since a plurality of pipes are used, the entire reformer becomes large. In addition, heat dissipation from the piping is likely to occur, resulting in a heat dissipation loss and a decrease in thermal efficiency.
- the evaporator 1 pure water flows along the plurality of pipes 5 in the arrow X direction, while the combustion exhaust gas is supplied in the arrow Y direction orthogonal to the arrow X direction. At that time, in order to reliably evaporate the pure water passing through the pipe 5 and generate water vapor, the pure water is burned and discharged. The gas power also needs to give a predetermined amount of heat. Therefore, in order to secure a heat exchange time between the pure water and the combustion exhaust gas, the pipe 5 must be considerably elongated in the direction of the arrow X. As a result, the evaporator 1 is considerably increased in size in the direction of arrow X, and the entire reformer cannot be reduced in size.
- the present invention solves this type of problem, and it is possible to reduce the number of pipes as much as possible, to improve the thermal efficiency, and to make a fuel reforming device simple and compact.
- the purpose is to provide.
- Another object of the present invention is to provide a fuel reformer that can efficiently and efficiently exchange heat between a reforming fuel and a heating fluid and that can be configured simply and compactly.
- the present invention is a fuel reformer that generates hydrogen-rich fuel gas by reforming a reforming fuel, and the fuel reformer uses the reforming fuel as a heating fluid.
- An evaporator that evaporates by heat exchange, an overheater that raises the temperature of the evaporated reforming fuel to a temperature required for the reforming reaction, and reforming the reformed fuel that has been raised in temperature
- a reformer that generates gas.
- An evaporator is disposed surrounding the superheater, and the superheater and the reformer are connected in series with each other.
- the superheater, the evaporator, and the reformer do not need to be connected by piping, and the piping can be favorably reduced (or shortened).
- the heat radiation from the piping is reduced, the thermal efficiency is improved, and the entire fuel reformer can be configured simply and compactly.
- FIG. 1 is a schematic perspective explanatory view of a fuel reformer according to a first embodiment of the present invention.
- FIG. 2 is a cross-sectional view showing a flow state in the fuel reformer.
- FIG. 3 is an exploded perspective view of an evaporator constituting the fuel reformer.
- FIG. 5 is a partial cross-sectional explanatory view of the evaporator.
- FIG. 6 is a cross-sectional view of the evaporator.
- FIG. 7 is an exploded perspective view of a superheater constituting the fuel reformer.
- FIG. 8 is an exploded perspective view of a reformer constituting the fuel reformer.
- FIG. 9 is a cross-sectional view showing a flow state in the fuel reformer according to the second embodiment of the present invention.
- FIG. 10 is a partial cross-sectional explanatory view of an evaporator constituting the fuel reformer.
- FIG. 11 is a partially omitted perspective view of the evaporator.
- FIG. 12 is a cross-sectional view of an evaporator that constitutes a fuel reformer according to a third embodiment of the present invention.
- FIG. 13 is a cross-sectional explanatory view of an evaporator constituting a fuel reformer according to a fourth embodiment of the present invention.
- FIG. 14 is a schematic explanatory diagram of a conventional reforming apparatus.
- FIG. 1 is a schematic perspective explanatory view of a fuel reformer 10 according to a first embodiment of the present invention
- FIG. 2 is a cross-sectional view showing a flow state in the fuel reformer 10. .
- the fuel reformer 10 generates a hydrogen-rich fuel gas by reforming a reforming fuel containing a hydrocarbon such as methane, alcohol, or the like, for example, and the fuel gas, for example, Supply to a fuel cell (not shown).
- a reforming fuel containing a hydrocarbon such as methane, alcohol, or the like
- the fuel gas for example, Supply to a fuel cell (not shown).
- the fuel reformer 10 includes an evaporator 12 that evaporates the reforming fuel, a superheater 14 that raises the temperature of the evaporated reforming fuel to a temperature required for the reforming reaction, and a temperature rise
- a reformer 16 for reforming the reforming fuel to generate a reformed gas, and a preheater 18 for preheating a heating fluid for evaporating the reforming fuel in the evaporator 12 are provided.
- the evaporator 12 surrounds the superheater 14 and is arranged concentrically, and the superheater 14 and the reformer 16 are connected to each other coaxially and in series.
- the preheater 18 is coaxially and serially connected to the superheater 14 on the side opposite to the reformer 16.
- the evaporator 12 includes a bending tube member 20 and an inner cylinder member disposed on both sides of the bending tube member 20 and concentrically with the bending tube member 20. (Evaporator inner cylinder) 22 and outer cylinder member 24.
- the curved tube member 20 is configured as a fixed end that fixes one end (lower end) in the axial direction (arrow A direction) to the first separator 26 and has an open cross section that has the other end (upper end) in the axial direction as a free end.
- a plurality of arcuate tubes 28a, 28b are provided. [0015] As shown in Figs.
- a plurality of, for example, four arcuate tubes 28a are provided on the same circumference, spaced apart at equal angular intervals, and the four arcuate shapes in the first row are arranged.
- a plurality of, for example, four arcuate tubes 28b are provided concentrically and spaced apart at equal angular intervals on the same circumference.
- the first row of arcuate tubes 28a and the second row of arcuate tubes 28b are provided with phases shifted from each other.
- a first passage 30 is formed in each arcuate tube 28a, 28b to allow the combustion gas, which is a heated fluid, to flow therethrough, and between the inner cylinder member 22, the outer cylinder member 24, and each arcuate tube 28a, 28b.
- the second passage 32 through which the raw fuel that is the reforming fuel is circulated is formed.
- a curved combustion catalyst 34 is disposed in the curved tube member 20.
- the curved combustion catalyst 34 has a circular arc shape in cross section, one end in the axial direction is a fixed end fixed to the second separator 36, and a plurality and two rows of catalyst outer cylinders in which the other end in the axial direction is a free end. 38a and 38b are provided.
- the catalyst outer cylinder 38a in the first row is arranged one by one in the arcuate tube 28a in the first row, and the catalyst outer cylinder 38b in the second row is placed in the arcuate tube 28b in the second row. It is continuously arranged.
- the catalyst outer cylinders 38a are spaced apart at equal angular intervals, and the catalyst outer cylinders 38b are similarly spaced apart at predetermined angular intervals.
- the catalyst outer cylinders 38a and 38b accommodate flat metal cams 40a and 40b carrying a combustion catalyst.
- the first separator 26 is fixed to the lower end portion of the outer cylinder member 24, and the second separator 36 is disposed outside the outer cylinder member 24.
- the first and second separators 26 and 36 are separated by a predetermined distance, and an off-gas fluid path 44 is formed.
- the off-gas fluid path 44 communicates with the passages 46a and 46b formed between the first separator 26 and the catalyst outer cylinders 38a and 38b, and passes between the casing 42 and the outer cylinder member 24.
- the exhaust port 48 formed in the upper end edge of the casing 42 communicates with the outside.
- the upper end portion of the outer cylinder member 24 is fixed to the upper end portion of the casing 42, and the lid member 50 is attached to the upper end portions of the arcuate tubes 28a and 28b.
- a chamber 52 is formed between the upper ends of the arcuate tubes 28a and 28b and the upper ends of the catalyst outer cylinders 38a and 38b. The heated fluid is folded back in the chamber 52 and sent to the first passage 30.
- a ring member 54 is attached to the upper end portion of the casing 42.
- a reforming fuel supply pipe 56 such as methane and an air supply pipe 58 are attached to the ring member 54.
- a water supply pipe 60 is disposed in the ring member 54, and an end 60a of the water supply pipe 60 penetrates the ring member 54 and is exposed to the outside.
- the water supply pipe 60 is formed in a ring shape, and water can be supplied in a shower shape by providing a plurality of holes (not shown) on the lower side.
- a donut-shaped lid 62 is fixed to the upper part of the ring member 54. When methane and air are mixed in advance and supplied from the fuel supply pipe 56, the air supply pipe 58 can be dispensed with.
- the superheater 14 includes an outer cylinder (superheater outer cylinder) 64, and the outer cylinder 64 is fixed to the inner cylinder member 22 of the evaporator 12.
- the outer cylinder 64 is configured to be longer in the direction of the arrow A than the inner cylinder member 22, and a plurality of lower end edges that are located below the lower portion of the inner cylinder member 22 and communicate with the second passage 32.
- Raw fuel inlets 66 are formed at, for example, four locations.
- the raw fuel inlet 66 has a slit shape or a porous shape extending in the circumferential direction.
- a third separator 68 is fixed to the lower end portion of the outer cylinder 64.
- the substantially disc-shaped third separator 68 is formed with a plurality of holes 70, and one end of a pipe 72 is welded or brazed to the holes 70. Fixed.
- a plurality of partition plates 74 are fixed to the pipe body 72 at predetermined height positions by press-fitting, brazing, or the like.
- the partition plate 74 is formed with a plurality of holes 76 for inserting the respective pipes 72, and is also formed with notches 78 at different positions.
- an overheating passage 82 is formed which is meandered by the outer peripheral portions of the plurality of pipe bodies 72 and the cutout portions 78 of the plurality of partition plates 74 (see FIG. 2).
- a passage 84 is formed for flowing the reformed gas (hydrogen-rich gas) heated after reforming from above to below.
- a fourth separator 88 is fixed to the upper side of the pipe body 72 via a distribution plate 86.
- the distribution plate 86 is formed with a hole 90 through which the pipe 72 is inserted, and a distribution opening (reforming fuel outlet) 92 is provided at the center.
- the fourth separator 88 is formed with a hole 94 through which the tubular body 72 is inserted.
- the reformer 16 includes an outer cylinder 96 and an inner cylinder 98, and the outer cylinder 96 and the inner cylinder 98 communicate with an opening 92.
- a raw fuel passage 100 is formed. Outside
- a closed chamber 102 is formed in the upper part of the cylinder 96, and a plurality of raw fuels introduced into the chamber 102 from the raw fuel passage 100 are disposed in the inner cylinder 98 from the reforming fuel introduction part 105. Is supplied to the rectifier plate 104.
- a cover member 111 is disposed so as to surround the outer cylinder 96, and a heat insulating layer 11 la is formed in the cover member 111.
- Each rectifying plate 104 is formed with a plurality of holes 106 and has a rectifying function for raw fuel. Below the rectifying plate 104, a hard cam-shaped catalyst portion 108 carrying a reforming catalyst such as Pd, Pt, Rh or the like is disposed. A fourth separator 88 is fixed to the catalyst portion 108, and a chamber 110 communicating with the passage 84 of each pipe 72 is formed in the fourth separator 88.
- the preheater 18 is connected to the lower end portion of the evaporator 12 via a connecting member 112.
- the connecting member 112 forms a substantially ring-shaped chamber 114, and a ring-shaped plate member 116 is disposed on the upper side of the chamber 114, and a plurality of holes 118 are formed in the plate member 116. Is done.
- the plate member 116 is opposed to the second separator 36 of the evaporator 12 and forms a chamber 120 between the plate member 116 and the second separator 36.
- the chamber 114 is connected to the catalyst outer cylinder 38a via the hole 118 and the chamber 120. , Communicate with 38b.
- the connecting member 112 is provided with a passage 122 that communicates with the chamber 114, and the passage 122 communicates with the outer cylinder member 124 that constitutes the preheater 18. Similar to the superheater 14, a plurality of tubes 126 and a plurality of partition plates 128 are disposed in the outer cylinder member 124.
- the pipe body 126 extends in the direction of the arrow A, and a partition plate 128 provided with alternating cutout portions 130 is fixed to the pipe body 126 at a predetermined height position.
- a passage 1 32 is provided for allowing the reformed gas that has passed through the superheater 14 to flow vertically downward, while heating is performed via the outer peripheral surface of the pipe body 126 and the partition plates 128.
- a preheating passage 134 is provided to guide the fluid in a vertically upward direction in a meandering manner.
- a supply port 136 for supplying a heating fluid is provided at the outer peripheral lower end edge of the outer cylinder member 124.
- a fin member 142 is inserted as a heat transfer suppression medium (heat transfer suppression structure).
- a heat insulating space layer may be formed.
- the heat transfer promoting fin member 140 is inserted.
- the fin member 140 is formed in a wave shape, but is preferably configured to be shorter than the length of the arcuate tubes 28a and 28b in the direction of arrow A, which may be linear.
- a CO transformer (not shown) may be interposed.
- a selective oxidation removal device (PROX) for removing carbon monoxide remaining in the hydrogen-rich gas may be provided downstream of the preheater 18!
- an off-gas force from which a fuel cell force (not shown) is discharged is supplied to the preheater 18 from the supply port 136 of the preheater 18 as a heated fluid.
- the heating fluid meanders through a preheating passage 134 formed between the notch 130 of each partition plate 128 and the outer periphery of the plurality of tubes 126. While moving vertically upward.
- the passage 126 of the pipe 126 passes through the hydrogen-rich reformed gas force superheater 14 generated by reforming as described later, and is supplied after being cooled to about 300 ° C., for example. Yes.
- the heated fluid is heated by exchanging heat with the reformed gas, and then introduced into the chamber 114 from the passage 122 of the connecting member 112.
- a plate member 116 is disposed above the chamber 114, and the preheated heated fluid is introduced into the chamber 120 through a plurality of holes 118 formed in the plate member 116,
- the catalyst outer cylinders 38a and 38b communicating with the chamber 120 move vertically upward along the methalno and the two cams 40a and 40b. Accordingly, the heated fluid is burned through the combustion catalyst carried on the metal hammer cams 40a and 40b, and combustion gas is obtained.
- the combustion gas is produced by the upper ends of the catalyst outer cylinders 38a, 38b and the arc-shaped pipe 28a,
- reforming fuel containing methane or the like is supplied to the fuel supply pipe 56, and air is supplied to the air supply pipe 58. Further, water is supplied to the water supply pipe 60 and mixed in the reforming fuel air and the water queuing member 54 to obtain raw fuel.
- the raw fuel flows vertically downward along the second passage 32 formed between the inner cylinder member 22, the outer cylinder member 24, and the arcuate tubes 28a and 28b, and passes through the first passage 30. With flowing combustion gas Heat exchange takes place between them. As a result, the raw fuel is introduced into the outer cylinder 64 from the raw fuel inlet 66 formed in the lower part of the outer cylinder 64 constituting the superheater 14 after being vaporized.
- the vaporized raw fuel passes through the notch portions 78 provided in the plurality of partition plates 74 and the overheating passage 82 formed between the plurality of pipe bodies 72. Move vertically up through.
- the reformed gas at a high temperature around 650 ° C.
- the vaporized raw fuel that moves in the overheating passage 82 is heated by the reformed gas that moves along the passage 84, and is heated to, for example, around 550 ° C. Supplied from 92 to reformer 16.
- the vaporized and heated raw fuel is introduced into the chamber 102 through the raw fuel passage 100, and then directed downward from the reforming fuel introduction unit 105. Move.
- the reformer 16 has a plurality of rectifying plates 104 arranged in multiple stages, and the raw fuel rectified by the rectifying plates 104 is reformed by the catalyst unit 108 to obtain a reformed gas.
- a reformed gas containing carbon and hydrogen is generated, and this reformed gas is supplied from the chamber 110 to the passages 84 of the plurality of pipe bodies 72.
- the high-temperature (around 650 ° C) reformed gas supplied to the passage 84 heats the raw fuel moving along the superheating passage 82 while moving vertically downward, and then the preheater. 18 is supplied to a passage 132 in a pipe body 126 constituting 18. This reformed gas is supplied to an unillustrated fuel cell or the like after preheating the heated fluid moving along the preheating passage 134 by moving the passage 132 vertically downward.
- an evaporator 12 that evaporates the raw fuel (reforming fuel), and a superheater 14 that raises the temperature of the evaporated raw fuel to a temperature required for the reforming reaction.
- the evaporator 12 is disposed concentrically around the superheater 14. Specifically, as shown in FIG. 2, an inner cylinder member 22 constituting the evaporator 12 and an outer cylinder 64 constituting the superheater 14 are fixed, and the lower end edge of the outer cylinder 64 is Second passage of the evaporator 12 A raw fuel inlet 66 is formed to communicate 32 and the superheating passage 82 in the superheater 14.
- the superheater 14 and the evaporator 12 can favorably reduce the number of pipes that do not need to be connected by pipes. As a result, no heat is radiated from the piping, so that the thermal efficiency can be improved and a simple and compact configuration can be achieved.
- a heat transfer suppression structure (fin member 142 or heat insulating space layer) is provided between the inner cylinder member 22 of the evaporator 12 and the outer cylinder 64 of the superheater 14. ing. For this reason, heat transfer from the superheater 14 to the evaporator 12 is suppressed, and the heat exchange efficiency can be easily improved.
- the first and second passages 30 and 32 extending in the axial direction (arrow A direction) are formed in the evaporator 12, and the combustion gas and raw fuel flow in the arrow A direction. Heat exchange is taking place. Therefore, the outer periphery of the superheater 14 is covered with the first and second passages 30 and 32, and heat dissipation from the outer periphery of the superheater 14 to the outside can be satisfactorily prevented, and the heat exchange efficiency is further improved. To do.
- a superheater 14 that raises the temperature of the raw fuel (reforming fuel) evaporated by the evaporator 12, and a reformer 16 that reforms the heated raw fuel are connected to each other in the same axis and in series (see Fig. 2).
- the distribution plate 86 constituting the superheater 14 has an opening 92 as an outlet for reforming fuel gas for supplying raw fuel, which is a reformed fuel whose temperature has been raised, to the reformer 16.
- the opening 92 is directly connected to the raw fuel passage 100 provided in the reformer 16.
- the raw fuel derived from the superheater 14 is supplied directly from the opening 92 to the raw fuel passage 100 and then supplied from the reforming fuel introduction unit 105 to the rectifying plate 104.
- piping for connecting the superheater 14 and the reformer 16 is not required, the piping can be reduced favorably, heat is not generated from the piping, and thermal efficiency is improved. It becomes possible to construct a simple and compact.
- a chamber 110 is formed on the reformed gas outlet side of the reformer 16 via a fourth separator 88, and a plurality of pipe bodies constituting the superheater 14 are formed in the chamber 110. 72 is fixed. Therefore, the reformed gas generated by the reformer 16 passes through the passage 84 in the pipe body 72. As a result, heat is exchanged immediately with the raw fuel flowing in the superheating passage 82. As a result, the high-temperature reformed gas can be used as an overheating source for overheating the raw fuel, and the thermal efficiency can be easily improved.
- a cover member 111 is disposed so as to cover the outer cylinder 96, and a heat insulating layer 11 la is formed in the cover member 111. For this reason, the raw fuel flowing in the raw fuel passage 100 formed between the outer cylinder 96 and the inner cylinder 98 can effectively prevent the temperature decrease, and the reforming process by the reformer 16 can be prevented. Performed efficiently and reliably.
- the evaporator 12 includes a plurality of arcuate tubes 28a and 28b each having an arcuate cross section of an opening that is arranged in two rows on concentric circles.
- the catalyst outer cylinders 38a and 38b each having an arcuate cross-section with an opening cross section that accommodates the metal nozzle-cams 40a and 40b are disposed in the 8a and 28b.
- a first passage 30 that extends around the catalyst outer cylinders 38a and 38b and extends in the direction of the arrow A is formed in each of the arcuate tubes 28a and 28b, and the inner cylinder member 22 and the outer cylinder member 24
- a second path 32 extending in the direction of arrow A is formed between the arcuate tubes 28a and 28b.
- the raw fuel mixed with reforming fuel, air, and water moves vertically downward along the second passage 32, and heat exchange is performed between the combustion gas and the raw fuel! /
- the combustion gas which is the heating fluid
- the raw fuel exchange heat while moving in the same direction, so that efficient heat exchange is performed and the dimension in the direction of arrow A is effectively set. It becomes possible to shorten the length.
- the evaporator 12 has the effect of improving the heat exchange efficiency and enabling a simple and compact configuration.
- the curved tube member 20 has a plurality of arcuate tubes 28a, 28b arranged in two rows on a concentric circle, and the arcuate tubes 28a, 28b each have a catalyst composing the curved combustion catalyst 34.
- Outer cylinders 38a and 38b are provided. Therefore, a large number (that is, long) first and second passages 30 and 32 can be provided between the outer cylinder member 24 and the inner cylinder member 22, and the heat of the raw fuel and the combustion gas can be provided. There is an advantage that the exchange efficiency is effectively improved.
- the curved combustion catalyst 34 includes flat-type metal nozzle-cams 40a and 40b. to this As a result, the in-plane temperature distribution in the metal nozzle-cams 40a and 40b can be made uniform, the performance of the catalyst can be maintained, and the temperature control of the catalyst can be easily performed. Furthermore, a fin member 140 for promoting heat transfer is disposed between the arcuate tubes 28a and 28b, and the heat exchange efficiency between the raw fuel and the combustion gas is further improved.
- the arcuate tubes 28a and 28b constitute a fixed end fixed to the first separator 26 whose one axial end is open, and the other axial end constitutes a free end.
- the arcuate tubes 28a and 28b are not restricted from extending or contracting in the axial direction, so that thermal stress in the flow direction (axial direction) due to the temperature difference between the operation and the stop is generated. I can stop. Therefore, the arcuate tubes 28a and 28b are improved in durability and can be easily reduced in thickness, and the entire evaporator 12 can be reduced in weight and size.
- the superheater 14 and the reformer 16 are coaxially connected to each other in series, and the preheater 18 is connected to the superheater 14 and the reformer 16. Coaxially and in series on the opposite side.
- the piping connecting the reformer 16, the superheater 14, and the preheater 18 can be reduced at a stroke, and the entire fuel reformer 10 can be reduced in size, and heat dissipation from the piping can be suppressed to reduce thermal efficiency. Can be improved. With less starting energy, the fuel reformer 10 can be started well and energy saving can be ensured.
- FIG. 9 is a cross-sectional view showing a flow state of the fuel reformer 150 according to the second embodiment of the present invention.
- the same components as those of the fuel reformer 10 according to the first embodiment are denoted by the same reference numerals, and detailed description thereof is omitted. Similarly, detailed descriptions of the third and fourth embodiments described below are omitted.
- the cylindrical tube member 154 constituting the evaporator 152 includes an outer cylindrical tube 156 and an inner cylindrical tube 158 that have an opening cross-sectional ring shape and are arranged in two rows on a concentric circle.
- the outer cylindrical tube 156 is configured by fixing the upper ends of the two cylindrical plates 156a and 156b
- the inner cylindrical tube 158 is configured by fixing the upper ends of the two cylindrical plates 158a and 158b.
- the outer cylindrical tube 156 and the inner cylindrical tube 158 are each provided with a chamber 52 in the upper part thereof.
- the lower end portion of the cylindrical plate 156a constituting the outer cylindrical tube 156 is fixed to the outer cylinder member 24, and constitutes the cylindrical plate 156b constituting the outer cylindrical tube 156 and the inner cylindrical tube 158.
- the lower end portions of the cylindrical plate 158a are fixed.
- a lower end portion of the cylindrical plate 158b constituting the inner cylindrical tube 158 is fixed to a lower end portion of the outer cylinder 64 constituting the superheater 14 so as to be located below the raw fuel inlet 66.
- water mainly consists of the outer cylindrical tube 156 and the inner side. It falls vertically downward along the second passage 32 formed between the cylindrical tube 158 and the outer cylindrical member 24 (see FIGS. 10 and 11). At that time, in the curved combustion catalyst 34, the heated fluid is burned to generate combustion gas, and this fuel gas moves vertically downward along the first passage 30.
- the raw fuel and the combustion gas can flow along the axial direction of the cylindrical tube member 154, and the raw fuel flows back and forth in the passage 32.
- the heat exchange can be performed dramatically more efficiently, and the effect than the first embodiment can be obtained.
- FIG. 12 is a cross-sectional view of an evaporator 170 constituting the fuel reformer according to the third embodiment of the present invention.
- the evaporator 170 includes a curved tube member 172, and the curved tube member 172 includes a plurality of circular tubes 174a, 174b, and 174c each having an arcuate cross section.
- the arcuate tubes 174a to 174c are arranged out of phase with each other, whereby a second passage 32 is formed in each arcuate tube 174a to 174c so as to meander.
- catalyst outer cylinders 178a to 178c constituting the curved combustion catalyst 176 are accommodated. Catalyst outer cylinder 1 to 78a to 178c.
- FIG. 13 is an explanatory diagram of a schematic configuration of an evaporator 190 that constitutes the fuel reformer according to the fourth embodiment of the present invention.
- the curved combustion catalyst 192 constituting the evaporator 190 accommodates the first combustion catalyst layer 194a and the second combustion catalyst layer 194b in the catalyst outer cylinders 38a, 38b along the flow direction of the heating fluid.
- a hard cam carrying a Pt-based catalyst having excellent low temperature ignitability is disposed, while on the upper parts of the catalyst outer cylinders 38a and 38b, In particular, a nozzle-cam carrying a PdZPt alloy with excellent methane purification performance is installed.
- the low-temperature ignitability is improved by the first combustion catalyst layer 194a provided on the upstream side of the curved combustion catalyst 192. Even if the CH in the heated fluid flows without being burned by the second combustion catalyst layer 194b arranged on the downstream side,
- CH is purified by the second combustion catalyst layer 194b. As a result, CH is mixed in the combustion gas.
- the evaporators 152, 170, and 190 are disposed concentrically with the superheater 14 so as to surround the superheater 14. For this reason, the effects similar to those of the first embodiment described above, such as reducing the number of pipes favorably, preventing heat radiation from the pipes, improving the heat exchange efficiency, and being simple and compact, can be achieved. Is obtained.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Fuel Cell (AREA)
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN2006800070544A CN101132985B (zh) | 2005-03-18 | 2006-03-07 | 燃料重整装置 |
KR1020077023889A KR100933017B1 (ko) | 2005-03-18 | 2006-03-07 | 연료 개질 장치 |
EP06728727A EP1860064B8 (en) | 2005-03-18 | 2006-03-07 | Fuel modification apparatus |
US11/886,599 US8034135B2 (en) | 2005-03-18 | 2006-03-07 | Fuel modification apparatus having an evaporator arranged around a superheater |
CA002601322A CA2601322A1 (en) | 2005-03-18 | 2006-03-07 | Fuel modification apparatus |
DE602006010035T DE602006010035D1 (de) | 2005-03-18 | 2006-03-07 | Vorrichtung zum modifizieren von brennstoff |
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2005079372A JP4450755B2 (ja) | 2005-03-18 | 2005-03-18 | 燃料改質装置 |
JP2005-080544 | 2005-03-18 | ||
JP2005079186A JP4450754B2 (ja) | 2005-03-18 | 2005-03-18 | 燃料改質装置 |
JP2005080544A JP4450756B2 (ja) | 2005-03-18 | 2005-03-18 | 燃料改質装置 |
JP2005-079186 | 2005-03-18 | ||
JP2005-079372 | 2005-03-18 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2006100908A1 true WO2006100908A1 (ja) | 2006-09-28 |
Family
ID=37023582
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2006/304408 WO2006100908A1 (ja) | 2005-03-18 | 2006-03-07 | 燃料改質装置 |
Country Status (6)
Country | Link |
---|---|
US (1) | US8034135B2 (ja) |
EP (1) | EP1860064B8 (ja) |
KR (1) | KR100933017B1 (ja) |
CA (1) | CA2601322A1 (ja) |
DE (1) | DE602006010035D1 (ja) |
WO (1) | WO2006100908A1 (ja) |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR100981521B1 (ko) * | 2008-09-05 | 2010-09-10 | 삼성에스디아이 주식회사 | 증발기 및 이를 구비한 연료개질기 |
US8568495B2 (en) | 2008-09-05 | 2013-10-29 | Samsung Sdi Co., Ltd. | Evaporator and fuel reformer having the same |
KR101422630B1 (ko) * | 2011-12-30 | 2014-07-23 | 두산중공업 주식회사 | 열교환형 선개질기 |
US10465902B2 (en) | 2015-11-18 | 2019-11-05 | Bosal Emission Control Systems Nv | Combined evaporator and mixer |
US11725835B2 (en) * | 2021-01-02 | 2023-08-15 | Vempati Venkata Sundereswar Rao | Energy efficient and refrigerant-free air cooler |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0375201A (ja) * | 1989-08-17 | 1991-03-29 | Mitsubishi Heavy Ind Ltd | メタノールリフォーマ |
JP2002053306A (ja) * | 2000-08-09 | 2002-02-19 | Babcock Hitachi Kk | 水素製造装置と該水素製造装置を用いる燃料電池システム |
JP2003192304A (ja) | 2001-12-20 | 2003-07-09 | Aisin Seiki Co Ltd | 改質装置用蒸発器 |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0642940B2 (ja) * | 1987-03-31 | 1994-06-08 | 東洋エンジニアリング株式会社 | 気体吸熱反応用装置 |
GB9225188D0 (en) | 1992-12-02 | 1993-01-20 | Rolls Royce & Ass | Combined reformer and shift reactor |
US20020007595A1 (en) * | 1997-06-24 | 2002-01-24 | Uli Maier-Roeltgen | Method for reforming hydrocarbons autothermally |
CA2357960C (en) * | 2000-10-10 | 2007-01-30 | Tokyo Gas Co., Ltd. | Single-pipe cylinder type reformer |
US6984372B2 (en) | 2002-09-06 | 2006-01-10 | Unitel Technologies, Inc. | Dynamic sulfur tolerant process and system with inline acid gas-selective removal for generating hydrogen for fuel cells |
JP2004149402A (ja) * | 2002-10-10 | 2004-05-27 | Matsushita Electric Ind Co Ltd | 水素生成器とそれを備える燃料電池システム |
CA2415536A1 (en) * | 2002-12-31 | 2004-06-30 | Long Manufacturing Ltd. | Reformer for converting fuel to hydrogen |
DE602004028555D1 (de) | 2003-07-29 | 2010-09-23 | Panasonic Corp | Wasserstoffgenerator und Brennstoffzellenstromversorgungssystem |
WO2005056468A1 (ja) * | 2003-12-09 | 2005-06-23 | Matsushita Electric Industrial Co., Ltd. | 水素生成装置 |
-
2006
- 2006-03-07 KR KR1020077023889A patent/KR100933017B1/ko not_active IP Right Cessation
- 2006-03-07 WO PCT/JP2006/304408 patent/WO2006100908A1/ja active Application Filing
- 2006-03-07 CA CA002601322A patent/CA2601322A1/en not_active Abandoned
- 2006-03-07 US US11/886,599 patent/US8034135B2/en not_active Expired - Fee Related
- 2006-03-07 EP EP06728727A patent/EP1860064B8/en not_active Expired - Fee Related
- 2006-03-07 DE DE602006010035T patent/DE602006010035D1/de active Active
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0375201A (ja) * | 1989-08-17 | 1991-03-29 | Mitsubishi Heavy Ind Ltd | メタノールリフォーマ |
JP2002053306A (ja) * | 2000-08-09 | 2002-02-19 | Babcock Hitachi Kk | 水素製造装置と該水素製造装置を用いる燃料電池システム |
JP2003192304A (ja) | 2001-12-20 | 2003-07-09 | Aisin Seiki Co Ltd | 改質装置用蒸発器 |
Also Published As
Publication number | Publication date |
---|---|
EP1860064B1 (en) | 2009-10-28 |
KR20070112418A (ko) | 2007-11-23 |
CA2601322A1 (en) | 2006-09-28 |
KR100933017B1 (ko) | 2009-12-21 |
US8034135B2 (en) | 2011-10-11 |
EP1860064A4 (en) | 2008-06-18 |
DE602006010035D1 (de) | 2009-12-10 |
EP1860064A1 (en) | 2007-11-28 |
EP1860064B8 (en) | 2010-02-03 |
US20090155141A1 (en) | 2009-06-18 |
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