US20020068205A1 - Fuel cell system having two reformation reactors and method for operating same - Google Patents
Fuel cell system having two reformation reactors and method for operating same Download PDFInfo
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- US20020068205A1 US20020068205A1 US09/999,069 US99906901A US2002068205A1 US 20020068205 A1 US20020068205 A1 US 20020068205A1 US 99906901 A US99906901 A US 99906901A US 2002068205 A1 US2002068205 A1 US 2002068205A1
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- C01B3/48—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 followed by reaction of water vapour with carbon monoxide
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- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
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- C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
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Definitions
- the present invention relates to a fuel cell system and to a method for operating the fuel cell system.
- DE 196 24 435 C1 (U.S. Pat. No. 5,928,614) discloses a reforming reactor that is used for the steam reforming of methanol.
- a heating device is provided for a middle step, while the steps at the inlet side and the outlet side are constructed as heat exchanges.
- carbon dioxide is formed, which must be removed from the reformate.
- the methanol reforming system is very simple and therefore inexpensive.
- heat exchangers are not required and, instead, adiabatic reactors can be used.
- the efficiency is good, especially in low-pressure systems.
- the system can, however, also be operated in the high-pressure range.
- a portion of the fuel may contain impurities, since these are broken down in the high-temperature adiabatic reactor. This leads to a savings in costs, since fuels of a lesser purity can be used.
- FIG. 1 shows a diagrammatic representation of a device with two reforming reactors according to one embodiment of the present invention
- FIG. 2 shows a diagrammatic representation of a section from a fuel cell system according to the present invention.
- FIG. 3 shows a detail of the reactor arrangement for a cold starting case.
- the present invention is suitable particularly for fuel cell systems that are used in mobile systems.
- FIG. 2 a diagrammatic representation of an arrangement in a fuel cell system according to the present invention is shown.
- the fuel cell system has a fuel cell unit 1 and a gas generating system 2 .
- hydrogen for operating the fuel cell system, is obtained from a fuel, preferably an alcohol such as methanol or an ether, an ester, a hydrocarbon or the like.
- a fuel preferably an alcohol such as methanol or an ether, an ester, a hydrocarbon or the like.
- at least one reforming unit is provided for attaining a hydrogen-rich reformate and the reformate can be supplied at least partly to the anode side of the fuel cell unit.
- the reformate is purified in a gas purifying system to remove undesirable constituents, such as carbon monoxide.
- the fuel cell system has a first reforming reactor 4 for generating a first reformate R 1 and a second reforming reactor 7 for generating a second reformate R 2 .
- a first fuel preferably a mixture of methanol and water as well as reaction air, is supplied to the inlet 3 of the first reforming reactor 4 .
- the mixture is heated with the help of a heat exchanger 11 to a first inlet temperature T 1, in .
- this first inlet temperature is between 200° and 300° C.
- the catalyst-containing reforming reactor 4 may be an auto-thermal reactor with a catalyst, which preferably is not selective.
- the constituents supplied undergo reactions, which take place in accordance with thermodynamic equilibrium, in this reactor.
- the first reforming reactor 4 advisably has a catalyst that permits such reactions, preferably, a noble metal catalyst, such as platinum or a mixed catalyst, such as platinum/ruthenium.
- a reformate R 1 is formed which is in thermodynamic equilibrium.
- the temperature of the first reformate R 1 is appreciably above the first inlet temperature T 1, in .
- the first outlet temperature T 1, out at the outlet 5 of the first reforming reactor 4 of 600° to 900° C. is high.
- An auto-thermal reactor is understood to be a reactor, which is operated adiabatically and in which steam reforming of the fuel takes place simultaneously with a partial oxidation at least of the fuel in the same reactor.
- the fuel, which is supplied to the first reforming reactor 4 may also contain appreciable amounts of impurities, since the materials are decomposed reliably at the high temperature level, which is present.
- the first reformate R 1 is supplied to a second reforming reactor 7 for generating a second reformate R 2 .
- the first reformate R 1 is cooled to a lower temperature in an element 9 , preferably a mixing element, which is between the outlet 5 of the first reforming reactor 4 and an inlet 6 of the second reforming reactor 7 .
- This lower temperature corresponds to the second inlet temperature T 2, in in the second reforming reactor 7 .
- the second inlet temperature T 2 in in preferably is below the first outlet temperature T 1, out .
- a second fuel preferably water and methanol, having a lower temperature T MeOH , such as ambient temperature, is admixed in the mixing element 9 .
- the second inlet temperature T 2 in preferably is between 200° and 500° C.
- the temperature can be adjusted by the amount of fuel, namely MeOH+H 2 O, admixed with the first reformate R 1 .
- the second reforming reactor 7 is an adiabatic reactor. Such an adiabatic reactor is not cooled or heated externally, that is, additional heat is neither supplied from or discharged to the outside, with the exception of heat that is supplied to or discharged from the reforming reactor 7 by the media themselves, which are to be reacted, or of heat that is generated or consumed in the reactor by the reactions of the media, which are to be reacted.
- the second reforming reactor 7 has a catalyst that works selectively. In the second, adiabatic reforming reactor 7 , two reactions take place, namely a steam reforming of the methanol and, simultaneously, a shift reaction, with which the carbon monoxide content in the medium is reduced.
- a copper-containing catalyst, such as Cu—Zn is a preferred catalyst for the second reforming reactor 7 .
- the reformate R 2 leaving at the outlet 8 of the second reforming reactor 7 , has a second outlet temperature T 2, out , which is below the first outlet temperature T 1, out .
- this temperature is between 150° and 250° C.
- the second reformate R 2 can be supplied to a gas purification system 10 and the reformate, purified there, can be supplied to the anode side of the fuel cell unit 1 .
- the first inlet temperature T 1, in is adjusted over the first heat exchanger 11 , which is disposed upstream from the first reforming reactor 4 , in that the medium is tempered there with waste gas from the fuel cell.
- first and second reforming reactors 4 , 7 are considered together, the different temperature levels are practically invisible from the outside.
- the exchange of the necessary reaction temperatures takes place within the reforming region.
- the reforming reactors 4 , 7 are not cooled directly and, instead, are operated adiabatically or auto-thermally.
- the first fuel enters the reforming region 4 , 7 with a first inlet temperature T 1, in of, for example, 250° C. and a reformate R 2 leaves the reforming region 4 , 7 as an end product with an, at most, only slightly lower outlet temperature T 2, out of, for example, 200° C.
- the arrangement enables the reactor to be constructed very simply.
- the reforming reactors 4 , 7 can be constructed, for example, as tubular reactors, which are filled with a catalyst.
- FIG. 2 a diagrammatic representation of a fuel cell system according to the present invention is shown. Comparable components have been given the reference numbers of FIG. 1.
- the gas-purification system 10 Adjoining the reforming region with the reforming reactors 4 , 7 , there is a gas purification system 10 , in which the reformate R 2 is purified by the removal of undesirable residues of carbon monoxide.
- the gas-purification system 10 can be constructed as a one-step system and cooled with the waste gas from the anode and/or of the cathode of the fuel cell unit 1 .
- the gas purification system 10 can, however, also be constructed as a two-step system, the first step 12 preferably being cooled with waste gas from the cathode and the second step 13 being cooled preferably with waste gas from the anode of the fuel cell unit 1 . This is indicated by broken lines in FIG. 2.
- selective oxidation of carbon monoxide takes place in the purification step.
- the gas purification system 10 , an afterburner 15 , and downstream from the afterburner, the first heat exchanger 11 are disposed one after the other in the direction of flow in the waste gas from the fuel cell unit 1 .
- the system can be operated at a low pressure, such as 1 to 2 bar, or also at higher operating pressures.
- a low pressure such as 1 to 2 bar
- the expander 16 may be disposed between the after-burner 15 and the first heat exchanger 11 .
- the temperature load on the expander 16 is high at this place. If a lower temperature load is desired, the expander can also be disposed downstream from the first heat exchanger 11 .
- the expander 16 may be coupled with a compressor 17 in an air supply 20 to the fuel cell unit 1 .
- a reformate cooling device 19 which can be cooled preferably by a cooling medium (not shown) of the fuel cell unit 1 , may be disposed in the flowing reformate 18 downstream from the gas purification system 10 .
- the first reformate R 1 reaches the first reforming reactor 4 in the second reforming reactor 7 .
- a portion of the reformate R 2 which is formed there, is passed from a branch part into part 7 . 1 and oxidized there.
- the waste gas 7 . 1 can be supplied, preferably downstream from the branch part, to the second reformate R 2 .
Abstract
Description
- This applications claims the priority of German patent document 100 59 674.6 filed Dec. 1, 2000, the disclosure of which is expressly incorporated by reference herein.
- The present invention relates to a fuel cell system and to a method for operating the fuel cell system.
- DE 196 24 435 C1 (U.S. Pat. No. 5,928,614) discloses a reforming reactor that is used for the steam reforming of methanol. To stabilize the temperature of the different reactor steps, a heating device is provided for a middle step, while the steps at the inlet side and the outlet side are constructed as heat exchanges. During the methanol reforming reaction, carbon dioxide is formed, which must be removed from the reformate. In general, it is difficult to remove the waste heat developed during a customary, subsequent hydrogen gas shift reaction from the system in order to ensure a balance, thermal equilibrium that has sufficient dynamics.
- Pursuant to the present invention, it is possible to work largely without heat exchange during the reforming and the subsequent gas purification. The reforming reactors can be constructed simply and compactly. The manufacturing costs of the reactors can thus be reduced. The system has fewer components and the pressure loss in the gas generating system is reduced.
- It is advantageous that the methanol reforming system is very simple and therefore inexpensive. In the reforming region, heat exchangers are not required and, instead, adiabatic reactors can be used. The efficiency is good, especially in low-pressure systems. The system can, however, also be operated in the high-pressure range. A portion of the fuel may contain impurities, since these are broken down in the high-temperature adiabatic reactor. This leads to a savings in costs, since fuels of a lesser purity can be used.
- It is to be understood that the aforementioned distinguishing features and those, which are still to be explained below, can be used not only in the combination given, but also in other combinations or by themselves, without leaving the scope of the present invention.
- Other objects, advantages and novel features of the present invention will become apparent from the following detailed description of the present invention when considered in conjunction with the accompanying drawings.
- FIG. 1 shows a diagrammatic representation of a device with two reforming reactors according to one embodiment of the present invention;
- FIG. 2 shows a diagrammatic representation of a section from a fuel cell system according to the present invention; and
- FIG. 3 shows a detail of the reactor arrangement for a cold starting case.
- The present invention is suitable particularly for fuel cell systems that are used in mobile systems.
- In FIG. 2, a diagrammatic representation of an arrangement in a fuel cell system according to the present invention is shown. The fuel cell system has a
fuel cell unit 1 and agas generating system 2. In thegas generating system 2, hydrogen, for operating the fuel cell system, is obtained from a fuel, preferably an alcohol such as methanol or an ether, an ester, a hydrocarbon or the like. In a conventional gas generating system, at least one reforming unit is provided for attaining a hydrogen-rich reformate and the reformate can be supplied at least partly to the anode side of the fuel cell unit. Usually, the reformate is purified in a gas purifying system to remove undesirable constituents, such as carbon monoxide. - As shown in FIG. 1, the fuel cell system has a first reforming
reactor 4 for generating a first reformate R1 and a second reformingreactor 7 for generating a second reformate R2. A first fuel, preferably a mixture of methanol and water as well as reaction air, is supplied to theinlet 3 of the first reformingreactor 4. Previously, the mixture is heated with the help of aheat exchanger 11 to a first inlet temperature T1, in. Preferably, this first inlet temperature is between 200° and 300° C. - The catalyst-containing reforming
reactor 4 may be an auto-thermal reactor with a catalyst, which preferably is not selective. The constituents supplied undergo reactions, which take place in accordance with thermodynamic equilibrium, in this reactor. In addition, the first reformingreactor 4 advisably has a catalyst that permits such reactions, preferably, a noble metal catalyst, such as platinum or a mixed catalyst, such as platinum/ruthenium. A reformate R1 is formed which is in thermodynamic equilibrium. The temperature of the first reformate R1 is appreciably above the first inlet temperature T1, in. The first outlet temperature T1, out at theoutlet 5 of the first reformingreactor 4 of 600° to 900° C. is high. An auto-thermal reactor is understood to be a reactor, which is operated adiabatically and in which steam reforming of the fuel takes place simultaneously with a partial oxidation at least of the fuel in the same reactor. - The fuel, which is supplied to the first reforming
reactor 4, may also contain appreciable amounts of impurities, since the materials are decomposed reliably at the high temperature level, which is present. - The first reformate R1 is supplied to a second reforming
reactor 7 for generating a second reformate R2. For this purpose, the first reformate R1 is cooled to a lower temperature in an element 9, preferably a mixing element, which is between theoutlet 5 of the first reformingreactor 4 and aninlet 6 of the second reformingreactor 7. This lower temperature corresponds to the second inlet temperature T2, in in the second reformingreactor 7. The second inlet temperature T2, in in preferably is below the first outlet temperature T1, out. For this purpose, a second fuel, preferably water and methanol, having a lower temperature TMeOH, such as ambient temperature, is admixed in the mixing element 9. In so doing, the fuel or the mixture of fuels MeOH+H2O is evaporated and the reformate R2 is cooled. The second inlet temperature T2, in preferably is between 200° and 500° C. The temperature can be adjusted by the amount of fuel, namely MeOH+H2O, admixed with the first reformate R1. - Pursuant to the present invention, the second reforming
reactor 7 is an adiabatic reactor. Such an adiabatic reactor is not cooled or heated externally, that is, additional heat is neither supplied from or discharged to the outside, with the exception of heat that is supplied to or discharged from the reformingreactor 7 by the media themselves, which are to be reacted, or of heat that is generated or consumed in the reactor by the reactions of the media, which are to be reacted. The second reformingreactor 7 has a catalyst that works selectively. In the second,adiabatic reforming reactor 7, two reactions take place, namely a steam reforming of the methanol and, simultaneously, a shift reaction, with which the carbon monoxide content in the medium is reduced. A copper-containing catalyst, such as Cu—Zn, is a preferred catalyst for the second reformingreactor 7. - The reformate R2, leaving at the
outlet 8 of the second reformingreactor 7, has a second outlet temperature T2, out, which is below the first outlet temperature T1, out. Preferably, this temperature is between 150° and 250° C. - Subsequently, the second reformate R2 can be supplied to a
gas purification system 10 and the reformate, purified there, can be supplied to the anode side of thefuel cell unit 1. - Preferably, the first inlet temperature T1, in is adjusted over the
first heat exchanger 11, which is disposed upstream from the first reformingreactor 4, in that the medium is tempered there with waste gas from the fuel cell. - If the first and second reforming
reactors reactors region region reactors - In FIG. 2, a diagrammatic representation of a fuel cell system according to the present invention is shown. Comparable components have been given the reference numbers of FIG. 1.
- Adjoining the reforming region with the reforming
reactors gas purification system 10, in which the reformate R2 is purified by the removal of undesirable residues of carbon monoxide. The gas-purification system 10 can be constructed as a one-step system and cooled with the waste gas from the anode and/or of the cathode of thefuel cell unit 1. Thegas purification system 10 can, however, also be constructed as a two-step system, thefirst step 12 preferably being cooled with waste gas from the cathode and thesecond step 13 being cooled preferably with waste gas from the anode of thefuel cell unit 1. This is indicated by broken lines in FIG. 2. Preferably, selective oxidation of carbon monoxide takes place in the purification step. - The
gas purification system 10, anafterburner 15, and downstream from the afterburner, thefirst heat exchanger 11 are disposed one after the other in the direction of flow in the waste gas from thefuel cell unit 1. - The system can be operated at a low pressure, such as 1 to 2 bar, or also at higher operating pressures. For high-pressure operation, it is advantageous to provide an
expander 16 in the waste gas downstream from the afterburner. In a preferred arrangement, theexpander 16 may be disposed between the after-burner 15 and thefirst heat exchanger 11. However, the temperature load on theexpander 16 is high at this place. If a lower temperature load is desired, the expander can also be disposed downstream from thefirst heat exchanger 11. - The
expander 16 may be coupled with acompressor 17 in anair supply 20 to thefuel cell unit 1. - A
reformate cooling device 19, which can be cooled preferably by a cooling medium (not shown) of thefuel cell unit 1, may be disposed in the flowingreformate 18 downstream from thegas purification system 10. - In the case of a cold start, it may be advantageous to supply additional air to the second reforming
reactor 7. This is of benefit when the catalyst material in the second reformingreactor 7 is appropriately robust. It is also possible, in the case of a cold start, to pass waste gas from the second reformingreactor 7 in a region of thereactor 7, which is constructed as an internal heat exchanger 7.1 and in which this waste gas generates heat for heating thereactor 7 by the selective catalytic oxidation of hydrogen. This is shown in FIG. 3. Moreover, air is added only in this region 7.1 (not shown). The heat flux dQ/dt from the integrated, heat-generating starting step 7.1 into the actual reactor part of the reformingreactor 7 is indicated by an arrow. The first reformate R1 reaches the first reformingreactor 4 in the second reformingreactor 7. A portion of the reformate R2, which is formed there, is passed from a branch part into part 7.1 and oxidized there. The waste gas 7.1 can be supplied, preferably downstream from the branch part, to the second reformate R2. - Although particular embodiments of the present invention have been illustrated and described, it will be apparent to those skilled in the art that various changes and modifications can be made without departing from the spirit of the present invention. It is therefore intended to encompass within the appended claims all such changes and modifications that fall within the scope of the present invention.
Claims (25)
Priority Applications (1)
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US11/143,617 US7341610B2 (en) | 2000-12-01 | 2005-06-03 | Fuel cell system having two reformation reactors and method for operating same |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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DE10059674A DE10059674A1 (en) | 2000-12-01 | 2000-12-01 | The fuel cell system |
DE10059674.6 | 2000-12-01 |
Related Child Applications (2)
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US11/143,617 Division US7341610B2 (en) | 2000-12-01 | 2005-06-03 | Fuel cell system having two reformation reactors and method for operating same |
US11/143,617 Continuation US7341610B2 (en) | 2000-12-01 | 2005-06-03 | Fuel cell system having two reformation reactors and method for operating same |
Publications (1)
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US20020068205A1 true US20020068205A1 (en) | 2002-06-06 |
Family
ID=7665378
Family Applications (2)
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US09/999,069 Abandoned US20020068205A1 (en) | 2000-12-01 | 2001-12-03 | Fuel cell system having two reformation reactors and method for operating same |
US11/143,617 Expired - Fee Related US7341610B2 (en) | 2000-12-01 | 2005-06-03 | Fuel cell system having two reformation reactors and method for operating same |
Family Applications After (1)
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US11/143,617 Expired - Fee Related US7341610B2 (en) | 2000-12-01 | 2005-06-03 | Fuel cell system having two reformation reactors and method for operating same |
Country Status (3)
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US (2) | US20020068205A1 (en) |
EP (1) | EP1213779B1 (en) |
DE (2) | DE10059674A1 (en) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20070000176A1 (en) * | 2005-06-30 | 2007-01-04 | General Electric Company | System and method for hydrogen production |
US20120020873A1 (en) * | 2009-01-07 | 2012-01-26 | Aquarden Technologies Aps | Method and apparatus for production of hydrogen from methanol |
WO2017173525A1 (en) * | 2016-04-08 | 2017-10-12 | Future Power Ltd. | Electric power generation using associated petroleum gas |
WO2022193545A1 (en) * | 2021-03-15 | 2022-09-22 | 华能国际电力股份有限公司 | Fuel cell system directly utilizing methanol reformed gas and operating method of fuel cell system |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10253930A1 (en) * | 2002-11-19 | 2004-06-09 | Umicore Ag & Co.Kg | Process for producing a hydrogen-containing fuel gas for fuel cells and device therefor |
AU2004226236A1 (en) | 2003-04-01 | 2004-10-14 | Haldor Topsoe A/S | Process for the preparation of a hydrogen-rich stream |
DE102007001382B4 (en) * | 2007-01-09 | 2009-01-15 | Enerday Gmbh | Reforming system, method of operating a reforming system and use of a reforming system |
DE102007017501A1 (en) * | 2007-04-13 | 2008-10-16 | Enerday Gmbh | Method of checking a reformer and electric control unit |
DE102008021083A1 (en) * | 2008-04-28 | 2009-10-29 | Viessmann Werke Gmbh & Co Kg | Process for the preparation of a hydrogen-containing gas mixture |
DE102013214705A1 (en) | 2013-07-29 | 2015-01-29 | Robert Bosch Gmbh | Component cooling with cathode exhaust gas |
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US5928614A (en) * | 1996-06-19 | 1999-07-27 | Daimler Benz Ag | Reforming reactor, particularly for the water vapor reforming of methanol |
US5948221A (en) * | 1994-08-08 | 1999-09-07 | Ztek Corporation | Pressurized, integrated electrochemical converter energy system |
US6123913A (en) * | 1996-08-26 | 2000-09-26 | Arthur D. Little, Inc. | Method for converting hydrocarbon fuel into hydrogen gas and carbon dioxide |
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US3469944A (en) * | 1968-05-13 | 1969-09-30 | Joseph P Bocard | Process and apparatus for the manufacture of hydrogen for fuel cells |
US5800798A (en) * | 1992-04-06 | 1998-09-01 | Nippon Oil Co., Ltd | Process for producing fuel gas for fuel cell |
JP3257604B2 (en) | 1992-09-18 | 2002-02-18 | 石川島播磨重工業株式会社 | Fuel cell generator |
DE19755116C1 (en) * | 1997-12-11 | 1999-03-04 | Dbb Fuel Cell Engines Gmbh | Method of operating a Proton Exchange Membrane fuel cell system |
JPH11273701A (en) | 1998-03-23 | 1999-10-08 | Ishikawajima Harima Heavy Ind Co Ltd | Fuel cell power generating apparatus |
EP1181241B1 (en) * | 1999-05-03 | 2005-08-24 | Nuvera Fuel Cells | Autothermal reforming system with integrated shift beds, preferential oxidationreactor, auxiliary reactor, and system controls |
-
2000
- 2000-12-01 DE DE10059674A patent/DE10059674A1/en not_active Withdrawn
-
2001
- 2001-11-16 DE DE50114447T patent/DE50114447D1/en not_active Expired - Fee Related
- 2001-11-16 EP EP01127173A patent/EP1213779B1/en not_active Expired - Lifetime
- 2001-12-03 US US09/999,069 patent/US20020068205A1/en not_active Abandoned
-
2005
- 2005-06-03 US US11/143,617 patent/US7341610B2/en not_active Expired - Fee Related
Patent Citations (3)
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US5948221A (en) * | 1994-08-08 | 1999-09-07 | Ztek Corporation | Pressurized, integrated electrochemical converter energy system |
US5928614A (en) * | 1996-06-19 | 1999-07-27 | Daimler Benz Ag | Reforming reactor, particularly for the water vapor reforming of methanol |
US6123913A (en) * | 1996-08-26 | 2000-09-26 | Arthur D. Little, Inc. | Method for converting hydrocarbon fuel into hydrogen gas and carbon dioxide |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
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US20070000176A1 (en) * | 2005-06-30 | 2007-01-04 | General Electric Company | System and method for hydrogen production |
US8216323B2 (en) * | 2005-06-30 | 2012-07-10 | General Electric Company | System and method for hydrogen production |
US20120020873A1 (en) * | 2009-01-07 | 2012-01-26 | Aquarden Technologies Aps | Method and apparatus for production of hydrogen from methanol |
US8586003B2 (en) * | 2009-01-07 | 2013-11-19 | Aquarden Technologies Aps | Method and apparatus for production of hydrogen from methanol |
WO2017173525A1 (en) * | 2016-04-08 | 2017-10-12 | Future Power Ltd. | Electric power generation using associated petroleum gas |
WO2022193545A1 (en) * | 2021-03-15 | 2022-09-22 | 华能国际电力股份有限公司 | Fuel cell system directly utilizing methanol reformed gas and operating method of fuel cell system |
Also Published As
Publication number | Publication date |
---|---|
DE10059674A1 (en) | 2002-06-20 |
EP1213779B1 (en) | 2008-10-29 |
EP1213779A2 (en) | 2002-06-12 |
US7341610B2 (en) | 2008-03-11 |
EP1213779A3 (en) | 2004-09-08 |
US20050252082A1 (en) | 2005-11-17 |
DE50114447D1 (en) | 2008-12-11 |
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