• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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    • 专利摘要:
    The invention relates to a fuel cell system (100) with fuel supply unit (8) and fuel cell (1, 2) with cathode (4, 4 ') and anode (3, 3'), wherein the cathode (4, 4 ') has a cathode feed line (40 ) and the anode (3, 3 ') has an anode feed line (30), the anode (3, 3') is flow-connected to the fuel supply unit (8) via the anode feed line (30), in which a reforming device (13) is arranged and an anode exhaust gas line (6) having at least one firing device (22, 23) is provided. According to the invention, a first heat exchanger (16) is provided in the cathode feed line (40), and an evaporation device (12) arranged upstream of the reforming device (13) and a second heat exchanger (29) are provided, with the anode exhaust gas line (6) downstream dividing the firing device (22, 23) into first (6a) and second anode exhaust gas sub-lines (6b) respectively connected to an exhaust gas outlet (21), and wherein the first anode exhaust gas line (6a) is passed over a warm side of the first heat exchanger (16) and second anode exhaust gas partial line (6b) is guided over a warm side of the second heat exchanger (29) and the evaporation device (12) can be heated via the second anode exhaust gas partial line (6b).
    公开号:AT519416A1
    申请号:T51081/2016
    申请日:2016-11-29
    公开日:2018-06-15
    发明作者:Dipl Ing Michael (Fh) Reissig；Bernd Reiter Bsc；Ing Jörg Mathé Dipl；Ing Thomas Krauss Dipl；Planitzer Stefan；Vincent Lawlor Dr；Dipl Ing Rechberger Jürgen；Yanagisawa Masanari；Miyazaki Shinichi；Chikugo Hayato；Mano Tadaki；Yaguchi Tatsuya
    申请人:Avl List Gmbh；Nissan Motor；
    IPC主号:
    专利说明:

    SUMMARY
    The invention relates to a fuel cell system (100) with a fuel supply unit (8) and a fuel cell (1, 2) with a cathode (4, 4j and anode (3, 3 '), the cathode (4, 4 j being a cathode feed line (40) and the Anode (3, 3 ') has an anode feed line (30), the anode (3, 3') via the anode feed line (30), in which a reforming device (13) is arranged, is flow-connected to the fuel supply unit (8) and an anode exhaust gas line (6) with at least one burning device (22, 23) is provided.
    According to the invention, a first heat exchanger (16) is provided in the cathode feed line (40) and an evaporation device (12) arranged upstream of the reforming device (13) and a second heat exchanger (29) are provided in the anode feed line (30), the anode exhaust gas line (6) being located downstream divides the combustion device (22, 23) into first (6a) and second anode exhaust gas sub-lines (6b), each connected to an exhaust gas outlet opening (21), and wherein the first anode exhaust gas sub-line (6a) is led over a warm side of the first heat exchanger (16) and the second anode exhaust gas line (6b) is guided over a warm side of the second heat exchanger (29) and the evaporation device (12) can be heated via the second anode exhaust gas line (6b).
    Fig. 1
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    FUEL CELL SYSTEM
    The invention relates to a fuel cell system, comprising a
    Fuel supply unit, at least one fuel cell with a cathode and an anode, wherein the cathode has a cathode feed line and the anode has an anode feed line and the anode is connected to the flow via the anode feed line and a reforming device is arranged in the anode feed line, and at least one anode exhaust gas line for discharge of anode exhaust from the anode, being in the
    Anode exhaust line is arranged at least one burner.
    A fuel cell system, which is used, for example, as an auxiliary power supply device in motor vehicles or as a “stationary power plant” (APU - “auxiliary power unit”), usually comprises at least one fuel cell for generating electrical current from cathode air and fuel or reformate gas. Such a fuel cell is usually composed of a large number of individual fuel cell elements which are stacked on top of one another and are referred to as fuel cell stacks. A person skilled in the art understands a fuel cell, in particular a high-temperature fuel cell, to be, for example, a molten carbonate fuel cell (English: Molten Carbonate Fuel Cell, MCFC), which operates at operating temperatures of approximately 580 ° C. to 675 ° C. An alkali carbonate mixed melt of lithium and potassium carbonate is usually used as the electrolyte in this type of fuel cell. Solid oxide fuel cells (SOFC) are also known. Solid oxide fuel cells are operated at operating temperatures of around 650 ° C to 1000 ° C.
    The electrolyte of this cell type consists of a solid ceramic material that is able to conduct oxygen ions, but has an insulating effect on electrons. The electrodes, cathode and anode are attached to both sides of the electrolyte layer. They are gas-permeable electrical conductors. The oxygen-ion-conducting electrolyte is designed, for example, as a thin membrane in order to be able to transport the oxygen ions with low energy at the high temperatures mentioned. The outer side of the cathode facing away from the electrolyte is surrounded by air (hereinafter also referred to as cathode gas), the outer anode side by
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    Fuel or reformate gas. Unused air and unused fuel gas as well
    Combustion products are derived, for example, by suction.
    To generate reformate gas, the fuel cell system can be equipped with a reforming device which generates the reformate gas from a fuel, usually a hydrocarbon such as natural gas, diesel or an alcohol, and optionally from reformer air and / or water vapor. The reformate gas then contains, among other things, hydrogen gas and carbon monoxide. The reforming can take place in a separate reformer device or in the fuel cell itself. The fuel cell system can also be equipped with an air supply device, which by means of a
    Air delivery device from an environment of the fuel cell system
    Sucks in ambient air and divides it into reformer air and cathode air, for example. The reformer air can then be supplied to the reformer via a reformer air line, while the cathode air can be supplied via a cathode supply line to a cathode side of the at least one fuel cell.
    A disadvantage of known solutions is, in particular, that much of the energy obtained in the fuel cell escapes into the environment as waste heat via the anode exhaust gas. High, theoretically implementable efficiencies of such fuel cell systems cannot be achieved with this.
    It is therefore an object of the invention to overcome these disadvantages of the prior art and to provide a fuel cell system with high efficiency.
    This object is achieved according to the invention with a fuel cell system mentioned at the outset in that at least one first heat exchanger is arranged in the cathode feed line, at least one evaporation device and a second heat exchanger are arranged in the anode feed line and the evaporation device is arranged upstream of the reforming device, the anode exhaust gas line being located downstream of the Splits the combustion device into a first anode exhaust gas line connected to an exhaust gas outlet opening and a second anode exhaust gas line connected to an exhaust gas outlet opening, the first anode exhaust gas line being led over a warm or hot side of the first heat exchanger and the second anode exhaust gas line over a warm one
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    Side of the second heat exchanger is guided and the evaporation device can be heated via the second anode exhaust gas line.
    In the context of the present disclosure, a heat exchanger is understood in particular to be a device for indirect heat transfer, where material flows of different temperature levels are spatially separated by a heat-permeable wall. The goal is the heat transfer from the warmer to the cooler material flow, with the cold or cool side of the heat exchanger being understood as the area of the cooler material flow, while with the warm or hot side of the heat exchanger the area of the warmer material flow is understood.
    An evaporation device in the sense of the invention designates a special form of a heat exchanger, where the physical state of a medium is changed by heat transfer from a spatially separated material flow, in particular a liquid medium being brought into the vapor phase.
    An advantage achieved with the invention is to be seen in particular in that waste heat of the fuel cell reaction in the anode exhaust gas can be used efficiently by the course and arrangement of the anode exhaust gas line and by division into first and second anode exhaust gas lines with parallel flow. The anode exhaust gas of high temperature flows through both the reforming device and the evaporation device and the two heat exchangers. The heat of the anode exhaust gas can thus be used optimally for an interaction or heat transfer with currents in the anode feed line and cathode feed line. By dividing the anode exhaust gas line into a first and second anode exhaust gas line, each of these elements can be acted upon with a temperature sufficient for heat transfer and the mass flows can be adjusted or regulated depending on the application.
    A medium guided in the cathode supply line, in particular air, flows through a cold side of the first heat exchanger, whereas the anode exhaust gas flows through the first anode exhaust gas partial line, a warm side thereof, whereby the anode exhaust gas emits heat and the medium guided in the cathode supply line absorbs it. The same also takes place in the second anode exhaust gas line, in which the warm anode exhaust gas passes through warm sides of the second
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    Heat exchanger and flows through a warm side of the evaporation device, the anode exhaust gas exchanging heat with the medium, in particular fuel, conducted in the anode feed line.
    Furthermore, the anode exhaust gas also supplies the reforming unit with the thermal energy required for the reforming reaction, particularly in the case of endothermic reforming.
    By dividing the anode exhaust gas line into two anode exhaust gas partial lines through which the flow is essentially parallel, a pressure loss in the fuel cell system is also reduced, which further increases the efficiency.
    The fuel supply unit advantageously has a fuel tank in which the fuel is stored. In principle, the fuel cell system according to the invention can be operated with any fuel, in particular a liquid hydrocarbon such as natural gas, diesel or an alcohol such as ethanol. It is particularly advantageous if the fuel is designed as a mixture of water and ethanol. In particular, this can already be provided mixed in the fuel supply unit, but it can also be advantageous if a separate tank for water and ethanol is provided in each case. If two tanks are provided, it is expedient to provide a mixing device for mixing water and ethanol.
    In principle, the first and second anode exhaust gas sub-lines can each have their own exhaust gas outlet openings at their ends, but in a variant of the invention, the first anode exhaust gas sub-line and second anode exhaust gas sub-line are led to a common exhaust gas outlet opening. The anode exhaust gas is discharged into the environment via the exhaust gas outlet opening, a large part of the heat of the anode exhaust gas having been converted due to the interactions with the various elements and e.g. The temperature resistance of the materials used for the exhaust gas outlet opening is not subject to great demands, which reduces the manufacturing costs.
    Advantageously, a first control valve device is provided in the first anode exhaust gas line, preferably downstream of the warm side of the first heat exchanger, and / or a second one is provided in the second anode exhaust gas line, preferably downstream of the evaporation device
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    Control valve device provided. A flow rate of the anode exhaust gas through the first and second anode exhaust gas line can thereby be influenced or regulated. Furthermore, flow of the anode exhaust gas through one of the two anode exhaust gas lines can also be stopped completely. The
    Heat input into the various elements of the fuel cell system and thus also heat transfer to the media guided in the cathode feed line and anode feed line can be precisely regulated and can be adapted to different applications.
    In addition or as an alternative to the control valve devices, the
    Anode exhaust gas sub-lines with different geometries or cross-sectional areas or diameters are designed to control the mass flow. For example, the first anode exhaust gas partial line can be designed with a larger diameter than the second anode exhaust gas partial line in order to ensure high heat transfer to the material flow supplied to the cathode.
    It is expedient if anode exhaust gas conducted in the second anode exhaust gas line flows through the reforming device in such a way that heat is transferred to the reforming device. In other words, both the material flow guided in the anode feed line and the anode exhaust gas are guided through the reforming device, with a heat-permeable spatial separation being provided between the material flows. The reforming device and in particular the material flow guided therein in the direction of the anode (s) are thus heated in such a way that the temperature level necessary for a correct reforming reaction is reached.
    In a variant of the invention, the second heat exchanger is designed as a superheater in order to heat the fuel to a temperature higher than 350 ° C. or to a temperature level necessary for the reforming reaction. A superheater is therefore to be understood in particular as a heat exchanger which heats a stream of material to a temperature necessary for a reforming reaction.
    Advantageously, the second heat exchanger and the
    Reforming device combined in an overheating reformer element as a common component. As a result, the warm anode exhaust gas carried in the second anode exhaust gas line acts on the second heat exchanger and the
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    Reforming device simultaneously with heat - the material flow supplied is brought to the temperature necessary for the reforming reaction and reformed.
    In a further variant of the invention, the second heat exchanger and the evaporation device are combined in one evaporator superheater element (12a) as a common component. As a result, the warm anode exhaust gas conducted in the second anode exhaust gas line simultaneously applies heat to the second heat exchanger and the evaporation device. The fuel in the anode feed line is thus evaporated and overheated at the same time.
    These combined components bring advantages in particular in applications in which there is little space available for the fuel cell system, as is the case, for example, in vehicles. It also prevents heat loss or possibly condensation of the vaporized fuel in pipes between the vaporization device and the superheater.
    It is particularly expedient if anode exhaust gas can flow through the reforming device upstream of the second heat exchanger in the flow direction after the combustion device, preferably anode exhaust gas can flow through the evaporation device after the second heat exchanger. In this way, the thermal energy of the anode exhaust gas can be used particularly efficiently and brought to the points of the fuel cell system where it is needed. The anode exhaust gas first flows through the reforming device and provides the amount of heat required for the reforming reaction before it continues to flow through the second heat exchanger and the evaporation device. As a result, the entire thermal energy of the anode exhaust gas carried in the second anode exhaust gas line can be optimally used.
    The anode exhaust gas line advantageously divides downstream of the reforming device into the first anode exhaust gas line and the second anode exhaust gas line, the anode exhaust gas flowing through the reforming device after the combustion device.
    The combustion device is advantageously a catalytic burner or a starting burner unit with an ignition device or a combination element with a catalytic burner and starting burner device. The
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    The combustion device is designed as a catalytic burner for burning fuel residues and other by-products from the fuel cell reaction in the anode gas. Depending on the fuel used, the anode exhaust gas consists, for example, of approximately 80 percent water and carbon dioxide and approximately 20 percent hydrogen and carbon monoxide. The catalytic burner also converts the 20 percent hydrogen and carbon monoxide into water and carbon dioxide. In addition, a starting burner or a separate starting burner with such a starting burner can be provided. However, this can also be provided in a line running between the fuel supply and the anode exhaust gas line, which opens into the anode exhaust gas line downstream of the combustion device. It is also possible to combine a catalytic (after) burner and a starting burner with a separate fuel supply as a common element.
    In a variant of the invention, a starting fuel line is provided between the fuel supply unit and the anode exhaust line, in which a starting fuel metering device is preferably arranged. The combustion device and / or a start burner unit can be flow-connected to the fuel supply unit via the start fuel metering device. Fuel can be supplied via this starting fuel line, in particular in a start-up or warm-up phase of the fuel cell system, in order to raise the system - essentially the reforming device and the evaporation device - to a necessary operating temperature.
    In order to regulate a quantity of fuel in the anode feed line, a fuel injection device is advantageously arranged in the anode feed line upstream of the evaporation device. The amount of fuel supplied can thus be regulated depending on the operating phase or demand, and in particular can also be introduced in a form which promotes evaporation in the evaporation device.
    In a variant of the invention, at least one bypass line branches off from the cathode supply line upstream of the first heat exchanger and from the cathode supply line again flows into the cathode supply line downstream of the first heat exchanger, wherein a bypass control valve device is preferably arranged in the bypass line. In this way, the
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    Regulate the temperature of the medium supplied on the cathode side or prevent the air supplied to the cathode from entering the fuel cell at too high a temperature and causing damage due to thermal stresses.
    In a further variant of the invention, at least one purge air line branches off from the cathode feed line upstream of the first heat exchanger and opens into the anode feed line upstream of the reforming device, a purge air control valve device preferably being arranged in the purge air line. On the one hand, the fuel cell system can be flushed via the purge air line after being switched off, for example with air or another medium. This prevents the anodes from oxidizing and / or from the formation of nickel carbonyl in the system endangering the health or the users of the fuel cell system. On the other hand, the starting process or the heating of the fuel cell system can be supported via the purge air line, since the air supplied via the purge air line supports the reforming reaction. In an exemplary operating method, the evaporation device is brought to temperature via the anode exhaust gas warmed up with the aid of a star burner, after which a small amount of fuel is fed to the evaporation device via the anode feed line in order to evaporate it. The now predominantly gaseous fuel is then fed to the reforming device, air also being fed in via the purge air line. There is consequently an exothermic reaction at the reforming device, whereby hot gas can be fed to the anode at an early stage. As a result, the heating-up time of the fuel cell system can be significantly reduced. Furthermore, this exothermic reaction also has a protective function for the anode, since the gas that is produced displaces the oxygen in the anode.
    The invention is described below on the basis of a non-restrictive
    Embodiment explained in more detail, which is shown in the figure. In it shows
    1 is a schematic view of a first variant of a fuel cell system according to the invention,
    2 shows a schematic view of a second variant of a fuel cell system according to the invention, and
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    3 shows a schematic view of a third variant of a fuel cell system according to the invention.
    For reasons of clarity, similar elements are identified in the following figures with the same reference symbols.
    All of the variants shown also show a fuel cell system 100
    Fuel cells in the form of two fuel cell stacks 1, 2, each consisting of several stacked fuel cells. The fuel cells each have anode 3, 3 'and cathode 4, 4', which are supplied with the necessary operating media via a process gas distributor 5. The individual stacks 1, 2 are supplied collectively.
    Accordingly, an anode feed line 30 leading to the anode 3, 3 'for combustion or. Reformate gas and a cathode feed line 40 leading to the cathode 4, 4 'are provided for essentially air or ambient air. An anode exhaust gas line 6 serves to discharge the exhaust gases of the fuel cell, e.g. Air and unused fuel gas and other combustion products, but at least from anode exhaust gas from anode 3, 3 '. The fuel cell stacks 1, 2 are connected to supply or peripheral devices, the “balance of plant” (BOP), via an interface device 7. These include fuel preparation and supply, air supply and electrical components (not discussed further below).
    The system periphery has a fuel supply unit 8, which comprises a fuel tank 9 and a fuel pump 10. In particular, liquid fuel, usually a liquid hydrocarbon such as natural gas, diesel or an alcohol, can be used as fuel. The anode 3, 3 'is connected to the fuel supply unit 8 via the anode feed line 30.
    The fuel is introduced in liquid form via a fuel injection device 11 into an evaporation device 12, in which the fuel is evaporated with the addition of heat. The evaporated fuel is then fed to a reforming device 13, in which hydrogen-rich fuel or reformate gas is generated, which is converted into electrical energy in the fuel cell. In the reforming process, the fuel is either passed over a catalyst surface with the addition of air and / or together with water (steam) and converted into hydrogen, carbon dioxide, carbon monoxide and steam 9
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    Fuel off. The steam reforming as an endothermic process must be supplied with the required heat. The higher the reforming temperature and the higher the proportion of water (steam), the purer the resulting burning or
    Reformate.
    After the reforming device 13, the fuel or reformate gas is supplied to the anodes 3, 3 'of the fuel cell stacks 1, 2 via the anode feed line 30.
    The air necessary for the fuel cell reaction is supplied by means of a
    Air conveying device - for example a blower 14 - via the
    Cathode lead 40 supplied. A cathode air control device 15 in the form of a control valve is provided in the cathode feed line 40, with which the amount of air supplied to the cathode 4, 4 'can be controlled. In order to preheat the air supplied to the cathode 4, 4 ′ - on the one hand to promote the reaction and on the other hand to prevent thermal stresses in the fuel cell stacks 1, 2 due to the high temperatures of the anode - there is a first heat exchanger 16 in the cathode feed line 40 provided that has a hot side and a cold side in a known manner, each different from media
    Temperature levels are flowed through, so that a heat transfer from the hot to the cold side can take place, the heat flows being spatially separated. The medium supplied to the cathode 4, 4 'is guided over the cold side of the first heat exchanger 16 and then flows on to the
    Process gas distributor 5 or to the cathode 4, 4 '.
    In the variants shown, a bypass line 17 branches off from the cathode supply line 40 between the blower 14 and the cathode air control device 15, and opens again into the cathode supply line 40 downstream of the first heat exchanger 16. In the bypass line 17 is one
    Bypass control valve device 18 arranged with which the flow can be controlled. In certain operating states, the cathode air can be guided partially or completely past the first heat exchanger 16 via the bypass line 17, which enables the air supplied to the cathode 4, 4 ′ to be tempered. In this way, thermal stresses in the fuel cell stacks 1, 2, which could occur, for example, due to heating up too quickly, or generally damage to the cathode 4, 4 ′ by excessively hot air can be prevented.
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    Between the blower 14 and the cathode air control device 15, a purge air line 19 branches off from the cathode supply line 40, which opens upstream of the reforming device 13, preferably between the evaporation device 12 and the reforming device 13, into the anode supply line 30. In the purge air line 19, a purge air control valve device 20 is arranged, with which the flow can be regulated as required. Air can be supplied to the vaporized fuel via the purge air line 19 in order to support the reaction in the reforming device 13. This is particularly advantageous in a startup phase of the fuel cell system 100: the air supplied via the purge air line 19 supports the reforming reaction and shortens the heating-up time of the system.
    The exhaust gases from anode 3, 3 'and cathode 4, 4' are collected in the fuel cell stacks 1, 2 and led via the process gas distributor 5 and the anode exhaust gas line 6 to an exhaust gas outlet opening 21, where they e.g. be derived into the environment.
    The exhaust gases leave the fuel cell stacks 1, 2 at high temperatures, which are used according to the invention to increase the overall efficiency.
    A combustion device 22 is arranged downstream of the process gas distributor 5. In the combustion device 22, on the one hand, fuel can be converted into heat when the fuel cell system 1 is started up in order to bring the fuel cells in the fuel cell stacks 1, 2 quickly to operating temperature. On the other hand, fuel residues and other reaction products contained in the exhaust gases (in particular the anode exhaust gases) can be burned to ensure complete conversion.
    In Figs. 1 to 3, the burner 22 is designed as a combination element comprising a catalytic burner (“Oxi-Kat”) and a starting burner. The starting combustion device has an ignition device 24, for example an electrically operated igniter, with which fuel can be burned. A starting fuel line 25 leads from the fuel supply unit 8 to the anode exhaust line 6, where it opens upstream of the combustion device 22. In the exemplary embodiments shown, the starting fuel line 25 branches between the fuel supply unit 8 and the fuel injection device
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    In an exemplary operating method of the invention
    In a starting phase, fuel cell system 100 is supplied with fuel via the starting fuel line 25 and the ignition device 24 is activated. In this way, heat is generated in the combustion device 22 or in the starting combustion device 23, which accelerates the heating of the system, in particular via the heat exchangers described below. As soon as a certain temperature level has been reached, the ignition device 24 or the starting combustion device 23 can be deactivated, the metering of fuel via the starting fuel line 25 is reduced, if necessary, but in any case continued. This is particularly advantageous if the fuel residues and by-products in the exhaust gas from the fuel cell stacks 1, 2 are not yet sufficient to generate sufficient heat in the combustion device 22. As soon as the fuel cell system 100 has reached the optimum operating temperature, the metering of fuel via the starting fuel line 25 can also be set. As a result, the heating-up time of the fuel cell system 100 can be shortened to the operating temperature.
    In order to ensure that the waste heat from the fuel cell stacks 1, 2 is used as completely as possible, the anode exhaust gas line 6 divides downstream of the combustion device 22 into a first anode exhaust gas line 6a and a second anode exhaust gas line 6b, which open into a common exhaust gas outlet opening 21. In variants not shown, each anode exhaust gas line 6a, 6b can also open into its own exhaust outlet opening. To regulate the amount of exhaust gas flowing through the respective anode exhaust gas line 6a, 6b, a first control valve device 27 is provided in the first anode exhaust gas line 6a and in the second anode exhaust gas line 6b
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    Control valve devices 27, 28 are arranged as close as possible to the exhaust gas outlet opening 21, where the exhaust gas flowing through the anode exhaust gas partial lines 6a, 6b is already relatively cool and no high structural or material requirements - in particular with regard to temperature resistance - are placed on the control valve devices 27, 28, so that these can be carried out inexpensively.
    In Fig. 1, the control valve devices 27, 28 are dashed - this means that in a variant of the invention, these two control valve devices 27, 28 can be omitted if the respective amount of exhaust gas by the geometries of the anode exhaust gas lines 6a, 6b, in particular their cross sections or Diameter, can be adjusted. Combinations of these variants, namely that different cross sections as well as one or both control valve devices 27, 28 are provided, are possible.
    The variants shown in the figures differ in particular by the arrangement and course of the components in connection with the exhaust gas.
    1 shows a variant where the first anode exhaust gas partial line 6a is led through the hot side of the first heat exchanger 16 in order to heat or preheat the air supplied to the cathode 4, 4 '. The anode exhaust gas flowing in the first anode exhaust gas line 6a can have a temperature of approx. 720 ° C. when it enters the first heat exchanger 16, whereby the cold side of the first heat exchanger 16 cathode medium, i.e. e.g. Air that is heated up to 540 ° C.
    The second anode exhaust gas line 6b is first passed in the flow direction of the exhaust gas through a component in which a reforming device 13 and a second heat exchanger 29 are combined into a common superheat reformer element 13a, and then through the evaporation device 12. The anode feed line 30 leads downstream of the fuel injection device 11 via the evaporation device 12, where the fuel injected at approximately 30-35 ° C. evaporates and is heated to approximately 120 ° C. before it is passed through the
    Overheating reformer element 13a is performed, where the reformate gas for the fuel cell stacks 1, 2 is generated.
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    In this variant, the approximately 600 ° C hot exhaust gas from the fuel cell stacks 1, 2, which is additionally heated to up to 720 ° C in the combustion device 22 and / or the starting combustion device 23, is first used to overheat and reform the vaporized Fuel used.
    With the overheating in the second heat exchanger 29, the vaporized fuel is brought to the temperature required for the reforming of greater than 350 ° C. The heat provided is also in the case of an endothermic
    Reforming reaction - such as in the case of steam reforming - required in the reforming device 13. By supplying the overheating reformer element 13a with the heat of the exhaust gas, both purposes can be achieved. The exhaust gas is then passed on to the vaporization device 12, where it enters at approximately 500 ° C. and the heat of the exhaust gas is used for the vaporization of the fuel.
    FIG. 2 shows a variant where the anode exhaust line 6 is led downstream of the combustion device 22 through the reforming device 13 before it is divided into first 6a and second anode exhaust sub-lines 6b. This has the advantage in particular in the case of endothermic reforming reactions that a particularly large amount of heat can be supplied from the exhaust gas to the reforming reaction. The heat not required by the reform is still available afterwards. The first anode exhaust gas partial line 6a is then likewise passed through the hot side of the first heat exchanger 16 in order to heat or preheat the air supplied to the cathode 4, 4 ′. The second anode exhaust gas line 6b then flows through a component in which the evaporation device 12 and the second heat exchanger 29 are combined into a common component. This evaporator superheater element 12a thus combines the vaporization of the fuel with the superheating to the temperature required for the reforming. In the anode feed line 30, the fuel first flows into the evaporator superheater element 12a and from there further into the reforming device 13. The reformate or: fuel gas is then fed to the anode 3, 3 ′ of the fuel cell stacks 1, 2.
    FIG. 3 shows a variant in which, on the one hand, as in FIG. 2, the anode exhaust gas line 6 is led downstream of the combustion device 22 through the reforming device 13 before it is divided into the first 6a and second anode exhaust gas line 6b. Here, too, the advantage lies in supporting endothermic
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    Reforming reactions. Again, the first anode exhaust gas line 6a is led through the hot side of the first heat exchanger 16 in order to heat up or preheat the air supplied to the cathode 4, 4 ′. In the second anode exhaust gas line 6b, the hot side of the second heat exchanger 29, which functions as a superheater, is flowed through first, before the exhaust gas flows through the evaporation device 12 and further to the exhaust gas outlet opening 21. The supplied fuel is thus first evaporated in the evaporation device 12, fed to the second heat exchanger 29 at approximately 120 ° C., where it overheats and then into the
    Reforming device 13 is initiated. The order in which the exhaust gas flows through the components mentioned ensures optimal utilization of the thermal energy.
    The solution according to the invention thus allows the implementation of a
    Fuel cell system 100 with particularly good efficiency. The parallel flow through the anode exhaust gas lines 6a, 6b on the one hand results in a lower pressure loss than in conventional systems and on the other hand allows a precise adjustment of the exhaust gas quantities and thus heat transfers to the individual gas flows. Because of the amounts of heat required in each case, it is advantageous if the mass flow through the first anode exhaust gas line 6a is greater than the mass flow through the second anode exhaust gas line 6b.
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    权利要求:
    Claims (14)
    [1]
    1. Fuel cell system (100), comprising a fuel supply unit (8), at least one fuel cell (1, 2) with a cathode (4, 4 j and an anode (3, 3 '), the cathode (4, 4 j being a cathode lead (40) and the anode (3, 3 ') has an anode feed line (30) and the anode (3, 3') is fluidly connected to the fuel supply unit (8) via the anode feed line (30) and one in the anode feed line (30) Reforming device (13) is arranged, and an anode exhaust gas line (6) for discharging at least one anode exhaust gas from the anode (3, 3 '), wherein at least one combustion device (22, 23) is arranged in the anode exhaust gas line (6), characterized in that at least one first heat exchanger (16) is arranged in the cathode feed line (40), at least one evaporation device (12) and a second heat exchanger (29) are arranged in the anode feed line (30) and the evaporation device (12) upstream of the reforming gs device (13), the anode exhaust gas line (6) downstream of the combustion device (22, 23) extending into a first anode exhaust gas line (6a) connected to an exhaust gas outlet opening (21) and a second anode exhaust gas line (6b) connected to an exhaust gas outlet opening (21) divides, and wherein the first anode exhaust gas line (6a) is guided over a warm side of the first heat exchanger (16) and the second anode exhaust gas line (6b) is guided over a warm side of the second heat exchanger (29) and the evaporation device (12) over the second Anode exhaust gas line (6b) can be heated.
    [2]
    2. Fuel cell system (100) according to claim 1, characterized in that the first anode exhaust gas line (6a) and second anode exhaust gas line (6b) are guided to a common exhaust gas outlet opening (21).
    [3]
    3. Fuel cell system (100) according to claim 1 or 2, characterized in that in the first anode exhaust gas line (6a), preferably downstream of the warm side of the first heat exchanger (16), a first control valve device (27) is provided and / or in the second Anode exhaust gas line (6b), preferably downstream of the evaporation device (12), a second control valve device (28) is provided.
    17/26
    PP31473AT
    AVL List GmbH
    [4]
    4. Fuel cell system (100) according to one of claims 1 to 3, characterized in that in the second anode exhaust gas line (6b) anode exhaust gas flows through the reforming device (13) such that heat is transferred to the reforming device.
    [5]
    5. Fuel cell system (100) according to one of claims 1 to 4, characterized in that the second heat exchanger (29) is designed as a superheater.
    [6]
    6. The fuel cell system (100) according to any one of claims 1 to 5, characterized in that the second heat exchanger (29) and the reforming device (13) are combined in a superheat reformer element (13a) as a common component.
    [7]
    7. The fuel cell system (100) according to any one of claims 1 to 5, characterized in that the second heat exchanger (29) and the evaporation device (12) are combined as a common component in an evaporator superheater element (12a).
    [8]
    8. Fuel cell system (100) according to one of claims 1 to 7, characterized in that in the flow direction after the burning device (22, 23), the reforming device (13) before the second heat exchanger (29) can be flowed through with anode exhaust gas, preferably the evaporation device ( 12) after the second heat exchanger (29) through which anode exhaust gas can flow.
    [9]
    9. The fuel cell system (100) according to any one of claims 1 to 8, characterized in that the anode exhaust line (6) downstream of the reforming device (13) in the first anode exhaust line (6a) and the second anode exhaust line (6b), the anode exhaust after the reforming device (13) flows through the burning device (22, 23).
    [10]
    10. The fuel cell system (100) according to one of claims 1 to 9, characterized in that the combustion device (22, 23) is a catalytic burner or a starting burner unit (23) with an ignition device (24) or a combination element with a catalytic burner and Start burning device (24).
    18/26
    PP31473AT
    AVL List GmbH
    [11]
    11. The fuel cell system (100) according to any one of claims 1 to 10, characterized in that a starting fuel line (25) is provided between the fuel supply unit (8) and the anode exhaust line (6), in which a starting fuel metering device (26) is preferably arranged.
    [12]
    12. The fuel cell system (100) according to one of claims 1 to 11, characterized in that a fuel injection device (11) is arranged in the anode feed line (30) upstream of the evaporation device (12).
    [13]
    13. The fuel cell system (100) according to one of claims 1 to 12, characterized in that at least one bypass line (17) branches off from the cathode supply line (40) upstream of the first heat exchanger (16) from the cathode supply line (40), which is downstream of the first heat exchanger (16) again opens into the cathode feed line (40), a bypass control valve device (18) preferably being arranged in the bypass line (17).
    [14]
    14. The fuel cell system (100) according to any one of claims 1 to 13, characterized in that at least one purge air line (19) branches off from the cathode supply line (40) upstream of the first heat exchanger (16), which flows upstream of the reforming device (13) into the anode supply line ( 30) opens, wherein a purge air control valve device (20) is preferably arranged in the purge air line (19).
    19/26
    PP31473AT AVL List GmbH
    20/26
    PP31473AT
    AVL List GmbH
    21/26
    PP31473AT
    AVL Lisi GmbH
    22/26
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    同族专利:
    公开号 | 公开日
    JP2019536243A|2019-12-12|
    US20190379069A1|2019-12-12|
    AT519416B1|2019-01-15|
    US11196059B2|2021-12-07|
    CN110100339A|2019-08-06|
    WO2018099993A1|2018-06-07|
    EP3549191A1|2019-10-09|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    ATA51081/2016A|AT519416B1|2016-11-29|2016-11-29|The fuel cell system|ATA51081/2016A| AT519416B1|2016-11-29|2016-11-29|The fuel cell system|
    PCT/EP2017/080858| WO2018099993A1|2016-11-29|2017-11-29|Fuel cell system|
    US16/464,305| US11196059B2|2016-11-29|2017-11-29|Fuel cell system|
    EP17808422.4A| EP3549191A1|2016-11-29|2017-11-29|Fuel cell system|
    JP2019528532A| JP2019536243A|2016-11-29|2017-11-29|Fuel cell system|
    CN201780072954.5A| CN110100339A|2016-11-29|2017-11-29|Fuel cell system|
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