CA2202984A1 - Fuel-cell system and method for operating a fuel-cell system - Google Patents
Fuel-cell system and method for operating a fuel-cell systemInfo
- Publication number
- CA2202984A1 CA2202984A1 CA002202984A CA2202984A CA2202984A1 CA 2202984 A1 CA2202984 A1 CA 2202984A1 CA 002202984 A CA002202984 A CA 002202984A CA 2202984 A CA2202984 A CA 2202984A CA 2202984 A1 CA2202984 A1 CA 2202984A1
- Authority
- CA
- Canada
- Prior art keywords
- fuel
- cathode
- offgas
- cell system
- air
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 238000000034 method Methods 0.000 title claims description 15
- 238000010438 heat treatment Methods 0.000 claims abstract 3
- 239000007789 gas Substances 0.000 claims description 29
- 238000002485 combustion reaction Methods 0.000 claims description 17
- 239000000203 mixture Substances 0.000 claims description 13
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 12
- 239000003546 flue gas Substances 0.000 claims description 12
- 238000011144 upstream manufacturing Methods 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims 1
- 239000000446 fuel Substances 0.000 abstract description 26
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 abstract 1
- 239000007784 solid electrolyte Substances 0.000 abstract 1
- 238000007792 addition Methods 0.000 description 14
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 239000002737 fuel gas Substances 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000003792 electrolyte Substances 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241000518994 Conta Species 0.000 description 1
- 102100026933 Myelin-associated neurite-outgrowth inhibitor Human genes 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- SIWVEOZUMHYXCS-UHFFFAOYSA-N oxo(oxoyttriooxy)yttrium Chemical compound O=[Y]O[Y]=O SIWVEOZUMHYXCS-UHFFFAOYSA-N 0.000 description 1
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 1
- 229920005597 polymer membrane Polymers 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 229910001928 zirconium oxide Inorganic materials 0.000 description 1
Classifications
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
- H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
- H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
- H01M8/04097—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with recycling of the reactants
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/10—Fuel cells with solid electrolytes
- H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
- H01M2008/1293—Fuel cells with solid oxide electrolytes
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/14—Fuel cells with fused electrolytes
- H01M2008/147—Fuel cells with molten carbonates
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M2300/00—Electrolytes
- H01M2300/0017—Non-aqueous electrolytes
- H01M2300/0048—Molten electrolytes used at high temperature
- H01M2300/0051—Carbonates
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M2300/00—Electrolytes
- H01M2300/0017—Non-aqueous electrolytes
- H01M2300/0065—Solid electrolytes
- H01M2300/0068—Solid electrolytes inorganic
- H01M2300/0071—Oxides
- H01M2300/0074—Ion conductive at high temperature
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
- H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
- H01M8/04022—Heating by combustion
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
- H01M8/04067—Heat exchange or temperature measuring elements, thermal insulation, e.g. heat pipes, heat pumps, fins
- H01M8/04074—Heat exchange unit structures specially adapted for fuel cell
-
- 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
Abstract
It is current pratice in a high-temperature fuel cell plants to divide the cathode exhaust gas in particular into two partial streams, one of which is recirculated into the cathodes and the other used for heating, in which branching takes place by relatively sophisticated technical means directly a the gas outlets at about the operating temperature of the fuel cells. In order to simplify these means, all the cathode exhaust gas is to be taken via a heat exchanger to a branch with two partial lines, in which the first partial line opens into the cathodes via an air-mixing position and the heat exchanger and the second opens into means for raising the temperature. Thus the branching of the hot cathode exhaust gas is avoided and the heat of all the cathode exhaust gas is used to heat the partial cathode exhaust gas flow taken back into the cathodes. The invention is applicable especially and preferably to fuel cells with an operating temperature of over 600 ~C. Such fuel cells are carbonate melt and solid electrolyte types.
Description
GR 94 P 3632 P ~L~, P~ T~3~ R~ ;;~L-R~ hTlfi~
Description ., Fuel-cell syste~ and method for operating a fuel-cell system The invention relates to a fuel-cell ~ystem, in particular a hi~h-temperature fuel-cell system!
comprising at least one fuel-cell block having an anode section and a cathode section, and also to a method for operating such a fuel-cell system.
A fuel cell contain an anode and a cathode which are separated by an ;mme~;ately adjacent, ion-conducting electrolyte. Said eLectrolyte may be composed of an ion-conducting liguid or of a polymer membrane or, a~ in the case of a high-temperature fuel cell, of a solid body, ~uch as, for example" of zirconium oxide contA;n;ng small additions of yttrium oxide. The electrolyte of a high-temperature fuel cell is oxygen-ion-conducting at operating temperatures of the high-temperature fuel cell of about 1000~C. The fuel, generally hydrogen, is fed to the anode and the oxygen or the combustion air to the cathode by suitable duct systems and the water produced in the reaction of h~drogen and oxyye~l is discharged from the fuel cell with the anode offgas or the cathode offgas, dep~n~;ng on the type of fuel cell. A fuel cell can convert the fuel into electrical energy with a higher efficiency and lower environmental pollution than conventional internal-combustion engines hitherto known, whose efficiency i8 limited by the so-called Carnot proces~, are capable of doing this.
In the case of development project~ currently rllnn; ng, attempts are additionally also being made to utilize the heat produced during the operation of fuel cells, in particular during the operation of high-temperature fuel cells. Thus, the development of a high-temperature fuel-ce:Ll power station proceeds as a rule from the combination of high-temperature fuel cells with a gas turbine and, optionally, a ~team turbine connected downstream of the ga~ turbine, the high-temperature fuel cell t~k;~ over the function of the combustion chamber of the gas turbine.
In particular, in the devices disclosed in the p a p e r b y D r . E . E r d l e e n t i t l e d "Hochtemperaturbrenn~toffzelle SOFC-Stand der Forschung fur eine neue Technik zur Stromerzeugung" ("High-temperature SOFC fuel cell - state of research aimed at a new technology for current generation" in VDI Berichte No. 1029, 1993 and in German Offenlegungsschrift DE 40 21 097 A1 for operating a high-temperature fuel cell, a bifurcation is provided in each case for the cathode offgas produced on the cathode side, at which bifurcation a portion of the cathode offgas is fed to a combustion ch~m~er and at which bifurcation a ~econd portion of the cathode offgas is conveyed via a recuperative heat exchanger to the temperature-lowering system and then mixed with an inflow of cooler air. The inflow of cooler air is fed back into the cathode gas spaces together with the cooled subflow of the cathode offgas via a compressor and the same recuperative heat ~ch~nger. The non-recirculated portion of the cathode offgas is combusted in a burner with the anode offgaA. The flue gas of this combustion process is normally fed to a gas turbine.
This arrangement is ~uite sensible thermodynamically, but has the disadvantage that the cathode offgas at about 1000~C has to be bifurcated. Consequently, a high expenditure is necessary in regard to the pipe system and the connecting and weld~ng procedure.
A further disadvantage of this arrangement is that the amount of recirculated cathode offgas must not exceed a certain proportion because the ~uantity of heat might otherwise no longer be ade~uate to preheat the cathode gaA to be fed to the fuel cell.
GR 94 P 3632 P - 2a -The object of the invention i~ therefore to provide a fuel-cell system and a method for operating it, in which, in a particularly ~imple manner, the problem of removing the cathcde offgas and of heat utilization of the cathode offgas is solved.
In regard to the fuel-cell sys~-em, thi ob~ect i8 achieved according to the invention in that, proceeding from the cathode sect:ion, an offgas pipe i8 provided for the entire cathode offgas, which offgas pipe runs via a heat ~ch~nger to a bifurcation comprising two branch pipes, the first branch pipe opening into the cathode section via an air addition point and the heat ~ch~nger, and a second branch pipe opening preferably into heat utilization means, in particular via temperature-increasing means in the heat utilization means.
In regard to the method, this object is achieved according to the invention in that the entire cathode offgas originating from the cathode section is cooled and divided up into at least two cathode offgas subflows, a first cathode offgas subflow being supplemented with air, heated and fed into the cathode ~ection of the fuel-cell block and the heat of the second cathode offgas subflow preferably being utilized.
In this way it is pos ible to avoid a bifurcation of the hot cathode offgas from the cathode gas spaces.
At the same time, the heat removed from the cathode offgas in the heat ~ch~nger is fed back again to the gas mixture flowing into the cathode gas spaces, a reduction in temperature, which has a beneficial effect on the specification of a compressor, being achieved by feeding in fresh air and an increase in the oxygen content of the gas mixture entering the cathode gas spaces. To explain what is meant by feeding via a heat exchanger to a bifurcation, it may be noted that a splitting-up of the cathode offgas into at least two subflows can al~o already be provided in or at the heat ~ch~nger in the case of a suitably low cathode offgas temperature.
This arrangement fur~her~ore ensures that the quantity of heat available in the heat ~chAnger for preheating the cathode ga5 to be fed into the fuel cell is adequate for all the cathode offgas divisions.
An advantageous embodiment may provide that a compressor is disposed between the heat ~rh~n~er and the air addition point. The temperature of the cathode offga~ subflow is reduced because of the addition of air, with the result that an inexpensive air compressor of particularly simple design, in particular an induced draught fan, can be used. Alternatively, provision can also be made, proceeding from the bifurcation in the first branch pipe in the said sequence, to dispose a first further heat ~ch~nger and a compressor upstream of the air addition point, the air being feedable via the first further heat e~chAnger to the addition point. In this case, the temperature of the cathode offgas subflow is reduced by the first further heat ~ch~nger, 80 that a compressor mentioned above can again be provided. The air fed to the addition point is heated by the heat removed from the cathode offgas subflow and can be fed to the cathode offgas subflow upstream of the heat exchanger.
In a particularly advantageous implementation of the invention, the temperature-increasing means may be a second further heat e~ch~nger, the ~econd branch pipe being routed further from the second further heat ~ch~nger into the i~let of a turbine and a flue gas pipe being provided which opens into the outlet of the turbine via the second further heat exch~nger. In this way, it is pos~ible to deliver heat supplied via the flue gas pipe to the second cathode offgas subflow. In this way, a gas mixture is injected into the turbine inlet at a relatively high flowrate and relatively high temperature, with the result that, when the hot gas mixture, which is still under pres~ure at the cathode outlet, i~ expanded, particularly high power efficiency is achieved in the gas turbine.
In an equally advan'ageou~ manner, the temperature-increasing means may alternatively be a combustion chamber to which there is connected on the inlet side, in addition to the second branch pipe, a feed pipe for a gas mixture originating from the anode section of the fuel-cell block and an air feed pipe, and, on the outlet side, a pip,e connected to the inlet of the turbine. In this way, the second cathode offgas subflow is heated by means of the combustion of a suitable gas mixture, in this case the offgas and air originating from the anode section, which mani~ests itsel~ in a relatively high inlet temperature at the turbine. A gas mixture originating from the anode section of the fuel-cell block is understood as me~n;ng~ inter alia, the anode offgas itself, but also an anode offgas additionally reduced by fuel (hydrogen) or even an anode offgas, a so-called anode residual gas, additionally reduced by fuel and carbon dioxide.
In addition, it is conceivable to combust a combustible gas mixture, which may additionally be available, together with the anode offgas. Such a gaR
mixture may be produced, for example, in the case of fuel reforming or coal ga~ification.
Further advantageous implementations of the invention are to be found in the r~m~;n;ng ~ubclaims.
Exemplary e~bodiments of the invention are explained in greater detail by reference to a drawing.
In the drawing:
FIG. 1 shows the process flow chart of a high-temperature fuel-cell system with downstream gas turbine;
FIG. 2 shows the process flow chart of a fuel-cell sy~tem modified with respect to Figure 1; and FIG. 3 shows the proce~s flow chart of a further high-temperature fuel-cell ~ystem slightly modified with re~pect to Fi~lre 2.
In Figures 1 to 3, identical parts have identical reference symbols.
The process flow chart shown in Figure 1 of a high-temperature fuel-cell system 2 shows in a diagrammatic representation a high-temperature fuel-cell block 4 which is divided up into an anode section 6 having anode gas spaces, not shown further, and a cathode section 8, having cathode gas spaces, not shown further.
In the exemplary embodiment, the high-temperature fuel-cell block 4 is made up of a multiplicity of planarly constructed high-te~perature fuel cells, not shown further, and has an electrical power of 40 megawatts.
Connected to the fuel-cell block 4 is a power inverter 10 which converts the direct current generated by the fuel-cell block 4 into alternating current for a power network, not shown further here.
A steam-cont~;n;ng~ hydrogen-cont~;n;ng and/or carbon-mono~;de-cont~;n;ng fuel gas 14, which i~ heated beforehand to about 900~C in an anode-side recuperative heat ~h~nger 16, is fed to the anode side 6 via a fuel feed pipe 12. A hydrogen-depleted and/or carbon-mo~ox;de-depleted anode offgas 20 at a temperature of about 1000~C is discharged from the anode section 6 via an anode offgas pipe 18. The anode offgas 20 flows via the recuperative heat PYch~nger 16 and gives up most of its heat therein to the fuel gas 14 flowing into the anode section 6. The anode offgas 20 is fed directly in the exemplary embodiment to a co~mbustion chamber 22, in which the residual hydrogen contained in the anode offgas 20 is combusted with air supplied via a compressor 24, which is disposed in an air feed pipe 25.
The flue gas 26 prod~ced in the combustion chamber 22 is fed via a flue gas pipe 28 to a first further heat exchanger 30, in which heat i~ removed from the flue gas 26. Downstream of the first further heat ~h~nger 30, the flue gas pipe 28 opens into a turbine outlet pipe 32 connected to the turbine outlet 31. On entering the turbine outlet pipe 32, the flue gas 28 is therefore at about the temperature of the gas leaving the turbine 34.
Connected to the cathode section 8 on the outlet side i8 a cathode offgas pipe 3 6, via which a cathode offgas 38 at about 1000~C i~ fed via a cathode-side recuperative heat P~ch~nger 40 to a bifurcation 42.
Proceeding from said bifurcation 42 is a first and a second cathode offgas branch pipe 44 and 46, respectively, for a first and a second cathode offgas sub~low 48 and 50, respectively. The first cathode offgas branch pipe 44 i8 fed from the bifurcation via an air addition point 52, a circulating fan 54 and the heat ~chAnger 40 into the cathode gas spaces, not shown further, of the cathode section 8. Comparatively cool air is fed to the air addition point 52 via an air feed pipe 56 and a compressor 58 disposed therein. This results in a temperature reduction in the air-enriched first cathode offgas subflow 48. The circulating fan 54 can therefore be operated at operating temperatures below 600~C, which affects the cost and the design of the circulating fan 54 advantageously. The first cathode offgas subflow 48 forms about 50 to 90%, preferably about 60 to 80%, of the cathode offgas 38 supplied to the bifurcation 42. In the heat exchanger 40, the first cathode offgas subflow 48 is heated by means of the heat given up by the cathode offgas 38 to about 850 to 900~C.
The portion of the cathode offgas 38 left over at the bifurcation 42 is fed as second cathode offgas subflow 50 to the inlet 60 of the turbine 34 via the heat exchanger 30. The second cathode offgas subflow 50 is heated by meanR of the heat given up by the flue gas 26 in the heat ~ nger 30 to a particularly high tur~ine inlet te~perature in order to achieve as high an output as possible during the expansion of the second cathode o~fgas subflow 50 in the turbine 34. The gas mixture di~charging ~rom the turbine 34 can e~cape into the open air via a throttle valve 62 if the valve 62 is in the open position or, alternatively, if the valve poRition is completely closed or slightly throttled, can be fed into a steam generator 64 and from there into the open air. The steam generator 64, which is supplied with water 66, supplies process steam 68, which can be utilized in a steam turbine, not shown further here.
Some of the proce~s steam 68 may also be in~ected into the fuel gas 14, where it serves to reform a carbon-cont~;n;n~ fuel gas. Given a steam excess in the fuel gas,~~soot ~ormation, which normally occurs in the reforming of natural gas to form hydrogen and methane, can largely be avoided.
It should be repeated yet again that the process flow chart explained above is notable for four particular advantages. Fir~tly, the hot cathode offgas 38 discharging from the cathode section 8 is first bifurcated in the cathode-~ide heat e~ch~nger 40 after it has been cooled. Secondly, the air addition point 52 i8 disposed upstream of the circulating fan 54 in the flow direction of the first cathode offgas subflow 48, with the re~ult that the temperature of the first cathode offgas subflow 48 flowing into the circulating fan 54 i5 substantially reduced by the addition of the comparatively cool, compressed air. Thirdly, the temperature of the ~econd cathode offgas subflow 50 is raised considerably in the first further heat exchanger 30 as a result of the utilization of the heat content of the flue gas 26, which corresponds at the ~ame time to a higher gas inlet temperature at the inlet 60 of the turbine 34. Fourthly, an adequate preheating o~ the cathode offgas subflow 48 i~ always ensured, regardles~
of the division of the cathode offgas 38 at the ~ GR 94 P 3632 P - 8a -bifurcation 42.
The drive pipe [~ic] generated by means of the turbine 34 is utilized in the exemplary embodiment to drive the air compre~sor 58, a generator 70 and the air compre~sor 24. The abovementioned components are disposed on a common shaft 72. In this connection, the generator can advantageously also be operated as a motor for starting up the turbine 34.
Figure 2 shows a fuel-cell system 74 which is slightly modified compared with Figure 1. Said fuel-cell sygtem 74 differs from the system shown in Figure 1 ~olely in a modification of the fresh-air feed to the addition point 52 in the first cathode offgas subflow 48.
In the flow direction of the fir~t cathode offgas subflow 48 after the bifurcation 42, there is now disposed, firstly, a second further heat exchanger 76, then the circulating fan 54 and the addition point 52 subsequent thereto. The air supplied by means of the air compressor 5~3 is now heated in the second further heat exchanger 76, which results in the intended and advantageou~
temperature reduction of the first cathode offgas subflow 48. In this exemplary embodiment, too, the circulating fan 54 therefore has to pump the first cathode offgas subflow 48, which is at a comparatively low temperature.
The air then fed to the addition point 52 and already heated flows from that point together with the first cathode offgas subflow 48 to the cathode-side heat exchanger 40.
Figure 3 shows a fuel-cell system 78 which is modified with respect to Figure 2. The modifications relate here to the ~econd cathode offgas subflow 50 and also to the feed of the anode offgas 20. Proceeding from the bifurcation 42, the second branch pipe 46 for the second cathode offgas subflow 50 ig now fed via a combustion chamber 80 to the inlet 60 of the turbine 34.
The anode offgas pipe 18 is now fed via an anode offgas compressor 82 into the combustion chamber 80. In addition, there br~nch.os off from the air feed pipe 56 a branch CA 02202984 l997-04-l7 ~ GR 94 P 3632 P - lO -pipe 84, which also opens into the combustion ch~mher 80.
In the exemplary emhodiment, the combustion chamber 80 serves as tamper~tur~-increa~ing means. The heat liberated during the combustion of the anode offgas 20 with the air and the second cathode offgas subflow 50 results in the second cathode offgas subflow 50, which flows into the inlet 60 of the turbine 34, having a comparatively high inlet temperature and a co~paratively hi~h mass flow, which has an advantageous effect on the output achievable with the turbine 34. At the same time, the offgas mass flow, and consequently also the offgaR
lo~ses, can be reduced with respect to the arrangement according to Figure 2. The compressor 82, which brings the anode offgas 20 to the pressure o~ the cathode offgas :Elow 38, is driven in the exemplary embodiment by means of the Rhaft 72 of the turbine 34.
~~ In an alternative not shown further here, the anode offgas 20 can be additionally subjected to a gas ~eparation upstream of the compression in the compressor 82. In said gas separation, inert constituents in the anode offgas 20, in particular carbon dioxide, can be removed. Although this results, on the one hand, in the reduction in the ma~s flow of the anode offgas 20, it results, on the other hand, in an increase in the temperature in the combustion chamber 80 because inert gas constituents, su.ch as, for example, carbon dioxide, no longer have to be heated in the combustion chamber 80.
Description ., Fuel-cell syste~ and method for operating a fuel-cell system The invention relates to a fuel-cell ~ystem, in particular a hi~h-temperature fuel-cell system!
comprising at least one fuel-cell block having an anode section and a cathode section, and also to a method for operating such a fuel-cell system.
A fuel cell contain an anode and a cathode which are separated by an ;mme~;ately adjacent, ion-conducting electrolyte. Said eLectrolyte may be composed of an ion-conducting liguid or of a polymer membrane or, a~ in the case of a high-temperature fuel cell, of a solid body, ~uch as, for example" of zirconium oxide contA;n;ng small additions of yttrium oxide. The electrolyte of a high-temperature fuel cell is oxygen-ion-conducting at operating temperatures of the high-temperature fuel cell of about 1000~C. The fuel, generally hydrogen, is fed to the anode and the oxygen or the combustion air to the cathode by suitable duct systems and the water produced in the reaction of h~drogen and oxyye~l is discharged from the fuel cell with the anode offgas or the cathode offgas, dep~n~;ng on the type of fuel cell. A fuel cell can convert the fuel into electrical energy with a higher efficiency and lower environmental pollution than conventional internal-combustion engines hitherto known, whose efficiency i8 limited by the so-called Carnot proces~, are capable of doing this.
In the case of development project~ currently rllnn; ng, attempts are additionally also being made to utilize the heat produced during the operation of fuel cells, in particular during the operation of high-temperature fuel cells. Thus, the development of a high-temperature fuel-ce:Ll power station proceeds as a rule from the combination of high-temperature fuel cells with a gas turbine and, optionally, a ~team turbine connected downstream of the ga~ turbine, the high-temperature fuel cell t~k;~ over the function of the combustion chamber of the gas turbine.
In particular, in the devices disclosed in the p a p e r b y D r . E . E r d l e e n t i t l e d "Hochtemperaturbrenn~toffzelle SOFC-Stand der Forschung fur eine neue Technik zur Stromerzeugung" ("High-temperature SOFC fuel cell - state of research aimed at a new technology for current generation" in VDI Berichte No. 1029, 1993 and in German Offenlegungsschrift DE 40 21 097 A1 for operating a high-temperature fuel cell, a bifurcation is provided in each case for the cathode offgas produced on the cathode side, at which bifurcation a portion of the cathode offgas is fed to a combustion ch~m~er and at which bifurcation a ~econd portion of the cathode offgas is conveyed via a recuperative heat exchanger to the temperature-lowering system and then mixed with an inflow of cooler air. The inflow of cooler air is fed back into the cathode gas spaces together with the cooled subflow of the cathode offgas via a compressor and the same recuperative heat ~ch~nger. The non-recirculated portion of the cathode offgas is combusted in a burner with the anode offgaA. The flue gas of this combustion process is normally fed to a gas turbine.
This arrangement is ~uite sensible thermodynamically, but has the disadvantage that the cathode offgas at about 1000~C has to be bifurcated. Consequently, a high expenditure is necessary in regard to the pipe system and the connecting and weld~ng procedure.
A further disadvantage of this arrangement is that the amount of recirculated cathode offgas must not exceed a certain proportion because the ~uantity of heat might otherwise no longer be ade~uate to preheat the cathode gaA to be fed to the fuel cell.
GR 94 P 3632 P - 2a -The object of the invention i~ therefore to provide a fuel-cell system and a method for operating it, in which, in a particularly ~imple manner, the problem of removing the cathcde offgas and of heat utilization of the cathode offgas is solved.
In regard to the fuel-cell sys~-em, thi ob~ect i8 achieved according to the invention in that, proceeding from the cathode sect:ion, an offgas pipe i8 provided for the entire cathode offgas, which offgas pipe runs via a heat ~ch~nger to a bifurcation comprising two branch pipes, the first branch pipe opening into the cathode section via an air addition point and the heat ~ch~nger, and a second branch pipe opening preferably into heat utilization means, in particular via temperature-increasing means in the heat utilization means.
In regard to the method, this object is achieved according to the invention in that the entire cathode offgas originating from the cathode section is cooled and divided up into at least two cathode offgas subflows, a first cathode offgas subflow being supplemented with air, heated and fed into the cathode ~ection of the fuel-cell block and the heat of the second cathode offgas subflow preferably being utilized.
In this way it is pos ible to avoid a bifurcation of the hot cathode offgas from the cathode gas spaces.
At the same time, the heat removed from the cathode offgas in the heat ~ch~nger is fed back again to the gas mixture flowing into the cathode gas spaces, a reduction in temperature, which has a beneficial effect on the specification of a compressor, being achieved by feeding in fresh air and an increase in the oxygen content of the gas mixture entering the cathode gas spaces. To explain what is meant by feeding via a heat exchanger to a bifurcation, it may be noted that a splitting-up of the cathode offgas into at least two subflows can al~o already be provided in or at the heat ~ch~nger in the case of a suitably low cathode offgas temperature.
This arrangement fur~her~ore ensures that the quantity of heat available in the heat ~chAnger for preheating the cathode ga5 to be fed into the fuel cell is adequate for all the cathode offgas divisions.
An advantageous embodiment may provide that a compressor is disposed between the heat ~rh~n~er and the air addition point. The temperature of the cathode offga~ subflow is reduced because of the addition of air, with the result that an inexpensive air compressor of particularly simple design, in particular an induced draught fan, can be used. Alternatively, provision can also be made, proceeding from the bifurcation in the first branch pipe in the said sequence, to dispose a first further heat ~ch~nger and a compressor upstream of the air addition point, the air being feedable via the first further heat e~chAnger to the addition point. In this case, the temperature of the cathode offgas subflow is reduced by the first further heat ~ch~nger, 80 that a compressor mentioned above can again be provided. The air fed to the addition point is heated by the heat removed from the cathode offgas subflow and can be fed to the cathode offgas subflow upstream of the heat exchanger.
In a particularly advantageous implementation of the invention, the temperature-increasing means may be a second further heat e~ch~nger, the ~econd branch pipe being routed further from the second further heat ~ch~nger into the i~let of a turbine and a flue gas pipe being provided which opens into the outlet of the turbine via the second further heat exch~nger. In this way, it is pos~ible to deliver heat supplied via the flue gas pipe to the second cathode offgas subflow. In this way, a gas mixture is injected into the turbine inlet at a relatively high flowrate and relatively high temperature, with the result that, when the hot gas mixture, which is still under pres~ure at the cathode outlet, i~ expanded, particularly high power efficiency is achieved in the gas turbine.
In an equally advan'ageou~ manner, the temperature-increasing means may alternatively be a combustion chamber to which there is connected on the inlet side, in addition to the second branch pipe, a feed pipe for a gas mixture originating from the anode section of the fuel-cell block and an air feed pipe, and, on the outlet side, a pip,e connected to the inlet of the turbine. In this way, the second cathode offgas subflow is heated by means of the combustion of a suitable gas mixture, in this case the offgas and air originating from the anode section, which mani~ests itsel~ in a relatively high inlet temperature at the turbine. A gas mixture originating from the anode section of the fuel-cell block is understood as me~n;ng~ inter alia, the anode offgas itself, but also an anode offgas additionally reduced by fuel (hydrogen) or even an anode offgas, a so-called anode residual gas, additionally reduced by fuel and carbon dioxide.
In addition, it is conceivable to combust a combustible gas mixture, which may additionally be available, together with the anode offgas. Such a gaR
mixture may be produced, for example, in the case of fuel reforming or coal ga~ification.
Further advantageous implementations of the invention are to be found in the r~m~;n;ng ~ubclaims.
Exemplary e~bodiments of the invention are explained in greater detail by reference to a drawing.
In the drawing:
FIG. 1 shows the process flow chart of a high-temperature fuel-cell system with downstream gas turbine;
FIG. 2 shows the process flow chart of a fuel-cell sy~tem modified with respect to Figure 1; and FIG. 3 shows the proce~s flow chart of a further high-temperature fuel-cell ~ystem slightly modified with re~pect to Fi~lre 2.
In Figures 1 to 3, identical parts have identical reference symbols.
The process flow chart shown in Figure 1 of a high-temperature fuel-cell system 2 shows in a diagrammatic representation a high-temperature fuel-cell block 4 which is divided up into an anode section 6 having anode gas spaces, not shown further, and a cathode section 8, having cathode gas spaces, not shown further.
In the exemplary embodiment, the high-temperature fuel-cell block 4 is made up of a multiplicity of planarly constructed high-te~perature fuel cells, not shown further, and has an electrical power of 40 megawatts.
Connected to the fuel-cell block 4 is a power inverter 10 which converts the direct current generated by the fuel-cell block 4 into alternating current for a power network, not shown further here.
A steam-cont~;n;ng~ hydrogen-cont~;n;ng and/or carbon-mono~;de-cont~;n;ng fuel gas 14, which i~ heated beforehand to about 900~C in an anode-side recuperative heat ~h~nger 16, is fed to the anode side 6 via a fuel feed pipe 12. A hydrogen-depleted and/or carbon-mo~ox;de-depleted anode offgas 20 at a temperature of about 1000~C is discharged from the anode section 6 via an anode offgas pipe 18. The anode offgas 20 flows via the recuperative heat PYch~nger 16 and gives up most of its heat therein to the fuel gas 14 flowing into the anode section 6. The anode offgas 20 is fed directly in the exemplary embodiment to a co~mbustion chamber 22, in which the residual hydrogen contained in the anode offgas 20 is combusted with air supplied via a compressor 24, which is disposed in an air feed pipe 25.
The flue gas 26 prod~ced in the combustion chamber 22 is fed via a flue gas pipe 28 to a first further heat exchanger 30, in which heat i~ removed from the flue gas 26. Downstream of the first further heat ~h~nger 30, the flue gas pipe 28 opens into a turbine outlet pipe 32 connected to the turbine outlet 31. On entering the turbine outlet pipe 32, the flue gas 28 is therefore at about the temperature of the gas leaving the turbine 34.
Connected to the cathode section 8 on the outlet side i8 a cathode offgas pipe 3 6, via which a cathode offgas 38 at about 1000~C i~ fed via a cathode-side recuperative heat P~ch~nger 40 to a bifurcation 42.
Proceeding from said bifurcation 42 is a first and a second cathode offgas branch pipe 44 and 46, respectively, for a first and a second cathode offgas sub~low 48 and 50, respectively. The first cathode offgas branch pipe 44 i8 fed from the bifurcation via an air addition point 52, a circulating fan 54 and the heat ~chAnger 40 into the cathode gas spaces, not shown further, of the cathode section 8. Comparatively cool air is fed to the air addition point 52 via an air feed pipe 56 and a compressor 58 disposed therein. This results in a temperature reduction in the air-enriched first cathode offgas subflow 48. The circulating fan 54 can therefore be operated at operating temperatures below 600~C, which affects the cost and the design of the circulating fan 54 advantageously. The first cathode offgas subflow 48 forms about 50 to 90%, preferably about 60 to 80%, of the cathode offgas 38 supplied to the bifurcation 42. In the heat exchanger 40, the first cathode offgas subflow 48 is heated by means of the heat given up by the cathode offgas 38 to about 850 to 900~C.
The portion of the cathode offgas 38 left over at the bifurcation 42 is fed as second cathode offgas subflow 50 to the inlet 60 of the turbine 34 via the heat exchanger 30. The second cathode offgas subflow 50 is heated by meanR of the heat given up by the flue gas 26 in the heat ~ nger 30 to a particularly high tur~ine inlet te~perature in order to achieve as high an output as possible during the expansion of the second cathode o~fgas subflow 50 in the turbine 34. The gas mixture di~charging ~rom the turbine 34 can e~cape into the open air via a throttle valve 62 if the valve 62 is in the open position or, alternatively, if the valve poRition is completely closed or slightly throttled, can be fed into a steam generator 64 and from there into the open air. The steam generator 64, which is supplied with water 66, supplies process steam 68, which can be utilized in a steam turbine, not shown further here.
Some of the proce~s steam 68 may also be in~ected into the fuel gas 14, where it serves to reform a carbon-cont~;n;n~ fuel gas. Given a steam excess in the fuel gas,~~soot ~ormation, which normally occurs in the reforming of natural gas to form hydrogen and methane, can largely be avoided.
It should be repeated yet again that the process flow chart explained above is notable for four particular advantages. Fir~tly, the hot cathode offgas 38 discharging from the cathode section 8 is first bifurcated in the cathode-~ide heat e~ch~nger 40 after it has been cooled. Secondly, the air addition point 52 i8 disposed upstream of the circulating fan 54 in the flow direction of the first cathode offgas subflow 48, with the re~ult that the temperature of the first cathode offgas subflow 48 flowing into the circulating fan 54 i5 substantially reduced by the addition of the comparatively cool, compressed air. Thirdly, the temperature of the ~econd cathode offgas subflow 50 is raised considerably in the first further heat exchanger 30 as a result of the utilization of the heat content of the flue gas 26, which corresponds at the ~ame time to a higher gas inlet temperature at the inlet 60 of the turbine 34. Fourthly, an adequate preheating o~ the cathode offgas subflow 48 i~ always ensured, regardles~
of the division of the cathode offgas 38 at the ~ GR 94 P 3632 P - 8a -bifurcation 42.
The drive pipe [~ic] generated by means of the turbine 34 is utilized in the exemplary embodiment to drive the air compre~sor 58, a generator 70 and the air compre~sor 24. The abovementioned components are disposed on a common shaft 72. In this connection, the generator can advantageously also be operated as a motor for starting up the turbine 34.
Figure 2 shows a fuel-cell system 74 which is slightly modified compared with Figure 1. Said fuel-cell sygtem 74 differs from the system shown in Figure 1 ~olely in a modification of the fresh-air feed to the addition point 52 in the first cathode offgas subflow 48.
In the flow direction of the fir~t cathode offgas subflow 48 after the bifurcation 42, there is now disposed, firstly, a second further heat exchanger 76, then the circulating fan 54 and the addition point 52 subsequent thereto. The air supplied by means of the air compressor 5~3 is now heated in the second further heat exchanger 76, which results in the intended and advantageou~
temperature reduction of the first cathode offgas subflow 48. In this exemplary embodiment, too, the circulating fan 54 therefore has to pump the first cathode offgas subflow 48, which is at a comparatively low temperature.
The air then fed to the addition point 52 and already heated flows from that point together with the first cathode offgas subflow 48 to the cathode-side heat exchanger 40.
Figure 3 shows a fuel-cell system 78 which is modified with respect to Figure 2. The modifications relate here to the ~econd cathode offgas subflow 50 and also to the feed of the anode offgas 20. Proceeding from the bifurcation 42, the second branch pipe 46 for the second cathode offgas subflow 50 ig now fed via a combustion chamber 80 to the inlet 60 of the turbine 34.
The anode offgas pipe 18 is now fed via an anode offgas compressor 82 into the combustion chamber 80. In addition, there br~nch.os off from the air feed pipe 56 a branch CA 02202984 l997-04-l7 ~ GR 94 P 3632 P - lO -pipe 84, which also opens into the combustion ch~mher 80.
In the exemplary emhodiment, the combustion chamber 80 serves as tamper~tur~-increa~ing means. The heat liberated during the combustion of the anode offgas 20 with the air and the second cathode offgas subflow 50 results in the second cathode offgas subflow 50, which flows into the inlet 60 of the turbine 34, having a comparatively high inlet temperature and a co~paratively hi~h mass flow, which has an advantageous effect on the output achievable with the turbine 34. At the same time, the offgas mass flow, and consequently also the offgaR
lo~ses, can be reduced with respect to the arrangement according to Figure 2. The compressor 82, which brings the anode offgas 20 to the pressure o~ the cathode offgas :Elow 38, is driven in the exemplary embodiment by means of the Rhaft 72 of the turbine 34.
~~ In an alternative not shown further here, the anode offgas 20 can be additionally subjected to a gas ~eparation upstream of the compression in the compressor 82. In said gas separation, inert constituents in the anode offgas 20, in particular carbon dioxide, can be removed. Although this results, on the one hand, in the reduction in the ma~s flow of the anode offgas 20, it results, on the other hand, in an increase in the temperature in the combustion chamber 80 because inert gas constituents, su.ch as, for example, carbon dioxide, no longer have to be heated in the combustion chamber 80.
Claims (13)
1. A fuel-cell system (2, 74, 78), in particular a high-temperature fuel-cell system, comprising at least.
one fuel-cell block (4) having an anode section (6) and a cathode section (8), characterized in that, proceeding from the cathode section (8), an offgas pipe (36) is provided for the entire cathode offgas (38), which offgas pipe (36) runs via a heat exchanger (40) to a bifurcation (42) comprising two branch pipes (44, 46), the first branch pipe (44) opening into the cathode section (8) via an air addition point (52) and the heat exchanger (40) and the second branch pipe (46) opening preferably into heat utilization means (34), in particular via temperature-increasing means (30, 80) in the heat utilization means (34).
one fuel-cell block (4) having an anode section (6) and a cathode section (8), characterized in that, proceeding from the cathode section (8), an offgas pipe (36) is provided for the entire cathode offgas (38), which offgas pipe (36) runs via a heat exchanger (40) to a bifurcation (42) comprising two branch pipes (44, 46), the first branch pipe (44) opening into the cathode section (8) via an air addition point (52) and the heat exchanger (40) and the second branch pipe (46) opening preferably into heat utilization means (34), in particular via temperature-increasing means (30, 80) in the heat utilization means (34).
2. The fuel-cell system (2) as claimed in claim 1, characterized in that a circulating fan (54) is disposed in the first branch pipe (44) between the heat exchanger (40) and the air addition point (52).
3. The fuel-cell system (74, 78) as claimed in claim 1, characterized in that, proceeding from the bifurcation (42), there are disposed upstream of the air addition point (52) in the first branch pipe (44) a first further heat exchanger (76) and a circulating fan (54) in the order stated, the air being feedable to the addition point (52) via the first further heat exchanger (76).
4. The fuel-cell system (2, 74) as claimed in any one of claims 1 to 3, characterized in that a temperature-increasing means is a second further heat exchanger (30), the second branch pipe (46) being routed further from the second further heat exchanger (30) into the inlet (60) of a turbine (34) and a flue gas pipe (28) being provided which opens into the outlet of the turbine (34) via the second further heat exchanger (30).
5. The fuel-cell system (2, 74) as claimed in claim 4, characterized in that the flue gas pipe (28) proceeds from a combustion chamber (22) to which there are connected on the inlet side a feed pipe (18) for a gas mixture (20) originating from the anode section (6) of the fuel-cell block (4) and an air feed pipe (25).
6. The fuel-cell system (78) as claimed in any one of claims 1 to 3, characterized in that a temperature-increasing means is a combustion chamber (80) to which there are connected on the inlet side, in addition to the second branch pipe (46), a feed pipe (18) for a gas mixture (20) originating from the anode section (6) of the fuel-cell block (4) and an air feed pipe (84), and, on the outlet side, a pipe (46) connected to the inlet (60) of a turbine (34).
7. The fuel-cell system (2, 74, 78) as claimed in any one of claims 4 to 6, characterized in that a compressor (24, 58) for the air feed is connected to the turbine (34) by means of a shaft (72).
8. The fuel-cell system as claimed in claim 7, characterized in that a generator (70) is connected to the turbine (34) by means of the shaft (72).
9. The fuel-cell system as claimed in claim 7 or 8, characterized in that a compressor (82) for the gas mixture (20) originating from the anode section (6) of the fuel-cell block (4) is connected to the turbine (34) via the shaft (72).
10. A method for operating a fuel-cell system (2, 74, 78) comprising at least one fuel-cell block (4) having an anode section (6) and a cathode section (8), in particular as claimed in any one of claims 1 to 9, characterized in that the entire cathode offgas (38) originating from the cathode section (8) is cooled and divided up into at least two cathode offgas subflows (48, 50), a first cathode offgas subflow (48) being supplemented with air, heated and fed into the cathode section (8) of the fuel-cell block (4) and the heat of the second cathode offgas subflow (50) preferably being utilized.
11. The method as claimed in claim 10, characterized in that the first cathode offgas subflow (50) is compressed prior to the heating.
12. The method as claimed in claim 10, characterized in that the first cathode offgas subflow (48) is cooled and compressed prior to being supplemented with air, the heat energy extracted during the cooling being utilized for the purpose of air preheating.
13. The method as claimed in any one of claims 10 to 12, characterized in that the second cathode offgas subflow (50) is expanded, preferably after heating, in a turbine (34).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE4437413 | 1994-10-19 | ||
| DEP4437413.5 | 1994-10-19 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2202984A1 true CA2202984A1 (en) | 1996-05-09 |
Family
ID=6531207
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002202984A Abandoned CA2202984A1 (en) | 1994-10-19 | 1995-10-06 | Fuel-cell system and method for operating a fuel-cell system |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0787367B1 (en) |
| JP (1) | JPH10507867A (en) |
| AT (1) | ATE165478T1 (en) |
| AU (1) | AU683776B2 (en) |
| CA (1) | CA2202984A1 (en) |
| DE (1) | DE59502015D1 (en) |
| DK (1) | DK0787367T3 (en) |
| ES (1) | ES2116770T3 (en) |
| WO (1) | WO1996013871A2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19807878C2 (en) * | 1998-02-25 | 2001-10-31 | Xcellsis Gmbh | Fuel cell system |
| ATE325433T1 (en) * | 1998-09-14 | 2006-06-15 | Questair Technologies Inc | POWER GENERATION SYSTEM |
| DE10042314B4 (en) * | 2000-08-29 | 2010-06-17 | Alstom Technology Ltd. | Gas turbine arrangement with a fuel cell |
| US6989209B2 (en) * | 2002-12-27 | 2006-01-24 | General Electric Company | Power generation method |
| DE102004002337A1 (en) * | 2004-01-16 | 2005-08-11 | Bayerische Motoren Werke Ag | An energy conversion device and method of operating the energy conversion device |
| DE102004004914B4 (en) * | 2004-01-31 | 2006-11-23 | Forschungszentrum Jülich GmbH | Method for generating electricity and heat |
| EP1804322B1 (en) * | 2004-10-19 | 2011-12-14 | Central Research Institute of Electric Power Industry | Combined power generation equipment |
| DE102006003740B4 (en) * | 2006-01-20 | 2011-06-30 | Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V., 80686 | Method and system for operating a high temperature fuel cell |
| AT502009B1 (en) * | 2006-05-09 | 2007-09-15 | Avl List Gmbh | Fuel cell system, comprises recirculation device on cathode side, and separately adjustable respective recirculation line is provided for every component |
| AT501963B1 (en) * | 2006-05-09 | 2007-09-15 | Avl List Gmbh | Process to fabricate decorative glass panel by bonding granite beads to horizontal surface followed by heating to glass melting point |
| GB201012775D0 (en) * | 2010-07-30 | 2010-09-15 | Rolls Royce Fuel Cell Systems Ltd | A solid ovide fuel cell system |
| DE102010035727A1 (en) * | 2010-08-28 | 2012-03-01 | Daimler Ag | Charging device for fuel cell device of motor vehicle, has recirculation device arranged downstream to compressor and upstream to another compressor at inlet point and recirculating exhaust gas of fuel cell |
| DE102017205704A1 (en) * | 2017-04-04 | 2018-10-04 | Robert Bosch Gmbh | Turbocompressor, in particular for a fuel cell system |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3976506A (en) * | 1975-02-12 | 1976-08-24 | United Technologies Corporation | Pressurized fuel cell power plant with air bypass |
| JPS61176075A (en) * | 1985-01-30 | 1986-08-07 | Hitachi Ltd | Fuel battery cooling system |
| JPS63152878A (en) * | 1986-12-17 | 1988-06-25 | Mitsubishi Heavy Ind Ltd | Solid electrolyte fuel cell power generating system |
| JPS63279576A (en) * | 1987-05-11 | 1988-11-16 | Ishikawajima Harima Heavy Ind Co Ltd | Cathode recycle device for fused carbonate fuel cell |
| JPS63289774A (en) * | 1987-05-22 | 1988-11-28 | Ishikawajima Harima Heavy Ind Co Ltd | Fused carbonate type fuel cell power generator |
| JP2942999B2 (en) * | 1990-05-01 | 1999-08-30 | 石川島播磨重工業株式会社 | Molten carbonate fuel cell power generator |
| DE4021097A1 (en) * | 1990-07-02 | 1992-01-09 | Siemens Ag | FUEL CELL POWER PLANT |
-
1995
- 1995-10-06 JP JP8514225A patent/JPH10507867A/en active Pending
- 1995-10-06 ES ES95934047T patent/ES2116770T3/en not_active Expired - Lifetime
- 1995-10-06 AU AU36497/95A patent/AU683776B2/en not_active Ceased
- 1995-10-06 CA CA002202984A patent/CA2202984A1/en not_active Abandoned
- 1995-10-06 DK DK95934047T patent/DK0787367T3/en active
- 1995-10-06 EP EP95934047A patent/EP0787367B1/en not_active Expired - Lifetime
- 1995-10-06 AT AT95934047T patent/ATE165478T1/en not_active IP Right Cessation
- 1995-10-06 WO PCT/DE1995/001388 patent/WO1996013871A2/en active IP Right Grant
- 1995-10-06 DE DE59502015T patent/DE59502015D1/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| WO1996013871A3 (en) | 1996-06-13 |
| EP0787367B1 (en) | 1998-04-22 |
| JPH10507867A (en) | 1998-07-28 |
| ES2116770T3 (en) | 1998-07-16 |
| AU683776B2 (en) | 1997-11-20 |
| AU3649795A (en) | 1996-05-23 |
| WO1996013871A2 (en) | 1996-05-09 |
| EP0787367A2 (en) | 1997-08-06 |
| ATE165478T1 (en) | 1998-05-15 |
| DE59502015D1 (en) | 1998-05-28 |
| DK0787367T3 (en) | 1999-01-18 |
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