• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The invention relates to a method for operating a fuel cell system (100), wherein a first operating fluid and a second operating fluid are introduced into a first combustion chamber (2) of a burner (1), the first operating fluid and the second operating fluid upstream of a chamber inlet (4). the first combustion chamber (2) are mixed together to form an operating fluid mixture, wherein the operating fluid mixture is at least partially catalytically combusted, wherein the partially burned operating fluid mixture is passed into a second combustion chamber (3) of the burner (1) second combustion chamber (3) is disposed immediately downstream of the first combustion chamber (2), and optionally wherein the operating fluid mixture in the second combustion chamber comprising a flame burner (3) is completely burned. Furthermore, the invention relates to a burner (1) for a fuel cell system (100), wherein the burner (1) is designed and arranged as a starting burner and / or afterburner. Furthermore, the invention relates to a use of such a burner (1). Moreover, the invention relates to a fuel cell system (100) with such a burner (1).
    公开号:AT520881A1
    申请号:T50031/2018
    申请日:2018-01-17
    公开日:2019-08-15
    发明作者:Dipl Ing Nikolaus Soukup Bsc；Ing Michael Seidl Dipl；Martin Hauth Dr
    申请人:Avl List Gmbh；
    IPC主号:
    专利说明:

    Summary
    The invention relates to a method for operating a fuel cell system (100), a first operating fluid and a second operating fluid being introduced into a first combustion chamber (2) of a burner (1), the first operating fluid and the second operating fluid upstream of a chamber entrance (4) of the first combustion chamber (2) are mixed with one another to form an operating fluid mixture, the operating fluid mixture being at least partially catalytically burned, the partially burned operating fluid mixture being passed into a second combustion chamber (3) of the burner (1), the second combustion chamber (3) is arranged immediately downstream of the first combustion chamber (2), and where appropriate the operating fluid mixture in the second combustion chamber (3) comprising a flame burner is completely burned.
    The invention further relates to a burner (1) for a fuel cell system (100), the burner (1) being designed and arranged as a starting burner and / or afterburner.
    The invention further relates to the use of such a burner (1). The invention also relates to a fuel cell system (100) with such a burner (1).
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    Method for operating a fuel cell system
    The invention relates to a method for operating a fuel cell system, in particular a stationary fuel cell system.
    The invention further relates to a burner for a fuel cell system, in particular a stationary SOFC system, the burner being designed and arranged as a starting burner and / or afterburner.
    In addition, the invention relates to the use of such a burner.
    Furthermore, the invention relates to a fuel cell system, in particular a stationary SOFC system with such a burner.
    Burners for fuel cell systems are known from the prior art. In the case of stationary SOFC systems in particular, which are operated with gaseous fuel such as natural gas, it is necessary to reform the gaseous fuel in a first step. It is also necessary to heat the fuel cell system to an operating temperature during a cold start, for which purpose a so-called start burner is usually provided. In addition, an afterburner is usually also necessary to completely burn off exhaust gas from an anode section while supplying air from the cathode section. Consequently, a start burner and an afterburner are usually provided in known fuel cell systems.
    The start burner is usually understood to mean a start burner for heating a fuel cell system. The start burner provides energy in the form of heat in order to bring the entire fuel cell system up to operating temperature. The operating temperature is not to be understood as a fixed temperature for the entire system. Rather, each component of the fuel cell system has a specific operating temperature. As soon as the fuel cell system is brought up to operating temperature, reformed fuel or fuel gas can be converted into electricity and heat in the fuel cell stack or in the stack. For physical reasons, it is not possible with this conversion to convert all of the fuel gas, as a result of which part of it is not used.
    In order not to waste the fuel gas and to reduce exhaust gases, it is burned in an afterburner. The heat generated during the conversion of the fuel gas into electricity, which is subsequently used to
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    Keep the fuel cell system at operating temperature. Depending on the selected operating point and the electricity produced, it is possible to switch the start burner off or off.
    In order to bring stationary SOFC systems up to operating temperature, fuel combustion is usually selected according to the prior art. This creates high temperature peaks, which in turn leads to the formation of nitrogen oxides (NOx formation). However, this type of exhaust gas should be avoided as far as possible in accordance with legal requirements. Another known solution is to carry out the combustion catalytically, as a result of which the temperature peaks are reduced and the NOx formation can thus be greatly reduced. However, catalytic burners must first be brought to operating temperature before they can be used, since the catalytic combustion of natural gas is only possible from temperatures of at least 350 ° C or higher.
    In an afterburner of an SOFC system, residues of anode exhaust gas are oxidized with the addition of cathode exhaust gas, on the one hand to reduce emissions and on the other hand to achieve a higher utilization of the fuel. Flammable components of the anode exhaust gas are usually hydrogen and carbon monoxide.
    Suitable catalytic converters for afterburner operation require lower space velocities for the catalytic combustion of natural gas than are necessary for the combustion of H2 and CO. The combustion of CH4 on such catalysts therefore either requires more space or only less can be implemented. Suitable coatings for catalysts in the SOFC area with an operating temperature of 900 ° C are also limited.
    The object of the invention is to provide an improved method for operating a fuel cell system
    Another goal is to increase the efficiency of a burner of the type mentioned at the beginning, by means of which it is simultaneously possible to reduce the number of components in a fuel cell system.
    It is also an aim to indicate the use of such a burner.
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    It is also an aim to provide a fuel cell system with such a burner.
    According to the invention, this object is achieved in that a method of the type mentioned at the outset has the following steps:
    Introducing a first operating fluid and a second operating fluid into a first combustion chamber of a burner, the first operating fluid and the second operating fluid being mixed upstream of a chamber entrance of the first combustion chamber to form an operating fluid mixture;
    - At least partial catalytic combustion of the operating fluid mixture;
    Directing the partially burned operating fluid mixture into a second combustion chamber of the burner, the second combustion chamber being arranged immediately downstream of the first combustion chamber;
    - optionally complete combustion of the operating fluid mixture in the second combustion chamber comprising a flame burner.
    An advantage achieved with the invention is to be seen in particular in the fact that the gradual combustion makes controlled combustion possible, as a result of which an exit temperature of the burned operating fluid mixture from the burner is achieved which is greater than a temperature permitted in the catalytic coating first combustion chamber. For this purpose, the first combustion chamber, which is essentially formed by a catalytic converter, is not designed large enough to achieve complete combustion of an amount of natural gas, which is necessary for a heating process of a fuel cell system. Complete combustion then takes place in the second combustion chamber. This division makes it possible to keep a temperature in the first combustion chamber lower, thereby protecting the catalytic coating thereof. In addition, the method according to the invention makes it possible to use a catalytic afterburner which is necessary anyway in the system as the starting burner. So only one burner is required, which is used as a start burner or afterburner depending on an operating mode. According to the invention, the operating fluid mixture is also gaseous.
    It is advantageous if the burner, in particular the catalytic material of the first combustion chamber, is brought to operating temperature in advance, preferably by an electrical heat source. The operating temperature is within the / 26
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    Invention to understand a temperature from which a complete catalytic combustion of the operating fluid mixture is possible.
    Within the scope of the invention, a gaseous fuel, preferably a natural gas mixture, which mainly consists of methane, is used as the first operating fluid. Subsequently, natural gas is to be understood in particular as a natural gas mixture, although this can also consist exclusively or almost exclusively of methane. Air, in particular ambient air, is generally used as the second operating fluid, the first operating fluid being at least partially burned with the addition or admixture of the second operating fluid. In principle, a liquid fuel can also be used as the first operating fluid, but this must be evaporated before being fed to the burner or to the fuel cell stack. However, it is particularly expedient if the method is carried out with already gaseous operating fluids.
    It is advantageous if a flow rate of the operating fluid mixture in the first combustion chamber is increased to a predetermined value.
    In particular, the flow rate of the first operating fluid is increased to a predetermined value, so that a complete combustion of the first operating fluid in the first combustion chamber is not possible when the burner is used as a starting burner. The heat generated during catalytic combustion can thus be limited. A maximum achievable temperature is therefore always below a calculated adiabatic combustion temperature. As a result, a temperature in the first combustion chamber is always kept below a permissible maximum temperature of the catalytic coating. Suitable catalytic materials are usually limited to an operating temperature of around 900 ° C. The temperature in the first combustion chamber is kept in the range from 700 ° C to 900 ° C, in particular at about 800 ° C, by the method according to the invention. For this purpose, the two operating fluids are advantageously mixed with one another in such a way that the combustion temperature does not exceed the permissible maximum operating temperature of the catalytic material of the first combustion chamber. As soon as the first combustion chamber, more precisely the catalytic material of the first combustion chamber, is fully heated, the amount of the operating fluid mixture which is fed to the burner is further increased in order to achieve a greater thermal output. The mixture is adjusted so that in the / 26
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    AVL List GmbH first combustion chamber there is no complete combustion, which means that when the burner is used as a starting burner, not all of the first operating fluid is burned in the first combustion chamber. A flow rate is achieved which is greater than a local flame rate.
    It is advantageous if the fuel cell system is heated by burning the operating fluid mixture in the burner. According to the invention, an oxidation catalytic converter, which is usually designed for afterburner operation, is simultaneously used at least as part of the burner operating as a starting burner. The above-described gradual combustion of the first operating fluid avoids high temperature peaks on the one hand and on the other hand a very high initial temperature of the process gas is reached. It is expedient if the operating fluid is only partially burned in the first combustion chamber in a first step and completely burned in the second combustion chamber in a second step. For this purpose, the first combustion chamber, which represents a catalytic burner, is not designed large enough so that a space velocity of the operating fluid mixture is too high to achieve complete combustion of the amount of operating fluid mixture required for heating operation of the fuel cell system. The operating fluid is then completely burned in the second chamber. On the one hand, this avoids excessive temperatures in the first, catalytically coated combustion chamber, on the other hand, however, a temperature is reached at the outlet of the second combustion chamber which is significantly above a maximum permissible temperature for the catalytic coating. A residual gas is thus completely burned in the second combustion chamber, which leads to a further increase in the temperature of the gaseous fuel mixture. In addition, the second combustion chamber also makes it possible for components of the operating fluid mixture which cannot be converted in the first combustion chamber to be burned in it. For example, long hydrocarbon chains such as propane in natural gas. Furthermore, such high flow velocities of the operating fluid mixture are achieved in the first combustion chamber that at least largely prevent the flame combustion in the second combustion chamber from burning back into the first combustion chamber. Thus, the catalytic material of the first combustion chamber is also damaged in this way by method / 26 according to the invention
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    AVL List GmbH avoided. The controlled catalytic partial combustion according to the invention with subsequent flame combustion also keeps the peak temperatures in the flame space below approximately 1200 ° C. and thus does not exceed a critical threshold (approximately 1200 ° C. or more) for the formation of thermal nitrogen oxides (NOx), which is lower NOx formation results.
    A completely burned operating fluid mixture - hot process gas - then emerges from the burner.
    Furthermore, it is advantageous if an introduction of a first operating fluid from a first operating fluid source and a second operating fluid from a second operating fluid source is set as soon as the fuel cell system reaches a predetermined operating temperature. The partial lines from the operating fluid sources to the burner are interrupted by valves. The pre-burner function of the burner is therefore switched off since the fuel cell system has already reached the desired temperature necessary for operation. A heat exchanger is arranged downstream of the burner, through the warm side of which the hot operating fluid mixture or process gas flows. Via the cold side of the heat exchanger, the second operating fluid, in particular ambient air, is conducted in a first partial line in the direction of the cathode section of the fuel cell stack, as a result of which the fuel cell stack is heated to a predetermined temperature. Parallel to the heat exchanger, a reformer is also arranged downstream of the burner, by means of which fuel (first operating fluid) is reformed by the hot process gas from the burner before being fed to the anode section. The fuel which is fed to the anode section is passed over a cold side of the reformer, whereas the hot operating fluid from the burner is passed over the warm side of the reformer, thereby heating and reforming the fuel. The line section through which the operating fluid mixture emerges from the burner is consequently divided downstream of the burner and upstream of the heat exchanger or the reformer. Downstream of the heat exchanger or the reformer, the two sub-lines are combined again to form a common line section, through which completely combusted and heat-emitted fuel cell stack exhaust gas is released to the environment. In a regular operation of the fuel cell system, the burner is then / 26
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    Afterburner used, in which anode exhaust gas is completely burned using cathode exhaust gas.
    It is therefore advantageous if fuel cell stack exhaust gas is burned in the burner, the fuel cell stack exhaust gas consisting of cathode exhaust gas and anode exhaust gas being completely burned in the first combustion chamber. The burner is used as an afterburner. Since the first combustion chamber is designed or arranged for afterburner operation, the fuel cell stack exhaust gas is completely or completely burned in the first combustion chamber. It is advantageous if cathode exhaust gas and anode exhaust gas are brought together upstream of the burner and downstream of the fuel cell stack. However, it can also be provided that the cathode exhaust gas and the anode exhaust gas are only mixed with one another directly at a chamber entrance of the first combustion chamber to form the operating fluid mixture. Downstream of the first combustion chamber, the operating fluid mixture is passed directly into the second combustion chamber, which, however, has no further function when the burner is operating as an afterburner, since the operating fluid mixture is already completely burned in the first combustion chamber. Hot process gas is led out of the burner.
    It is expedient if the burned operating fluid mixture downstream of the burner is used to heat up at least one heat exchanger and / or a reformer, the burned operating fluid mixture being supplied as system exhaust gas to a warm side of the at least one heat exchanger and / or the reformer. It is particularly advantageous if at least one heat exchanger and one reformer are heated by the burned operating fluid mixture. The heat exchanger and the reformer are preferably arranged in two line sections aligned parallel to one another. The respective cold sides of the heat exchanger and the reformer are flowed through as described above, whereby the two operating fluids and consequently the entire fuel cell system are warmed up.
    The further aim is achieved if, in the case of a burner of the type mentioned at the outset, the burner comprises two combustion chambers arranged in succession, a first combustion chamber comprising a catalytic material and one immediately downstream of the / 26
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    An advantage achieved in this way can be seen in particular in the fact that this design of the burner means that a catalytic afterburner can also be used for a heating process of a fuel cell system. In known catalytic afterburners, this is not possible since the catalytic material is not designed for the high temperatures of 950 ° C. or more necessary for a heating process. In known catalytic afterburners, temperatures of over 900 ° C are not permissible since excessive temperatures damage the catalytic material and thus the afterburner and consequently destroy its function. Afterburner are consequently designed so that during catalytic combustion of a fuel mixture these permissible temperatures for the catalytic material are not exceeded. By designing the burner with two combustion chambers, it is not necessary to generate such high temperatures in the first combustion chamber. An operating fluid mixture is only partially combustible during a heating process in the first combustion chamber, which is why the temperatures in the first combustion chamber can be kept in a range between approximately 700 ° C. and 900 ° C. A complete combustion of the operating fluid mixture during the heating process then takes place in the second combustion chamber, which comprises a flame burner. Consequently, temperatures of the operating fluid mixture which are above an allowable maximum temperature of the catalytic material of the first combustion chamber, for example in the range from 950 ° C. to 1000 ° C. or more, can be generated at an outlet or downstream of the burner. The burner is designed and arranged in particular as a starting burner and afterburner. This means that a single component functions simultaneously as a start burner and as an afterburner, depending on an operating state of a fuel cell system in which the burner is arranged.
    The burner is in particular designed to at least partially burn gaseous fuel or fuel, for which purpose the first combustion chamber comprises a catalytic material and the second combustion chamber comprises a flame burner.
    It is favorable if at least the first combustion chamber comprises honeycomb elements. It is particularly advantageous if the catalytic material of the first / 26th
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    Combustion chamber is at least partially formed from honeycomb elements with channels running or formed parallel to each other.
    In principle, it can also be provided if the combustion chambers are each hollow cylindrical at least in sections. These preferably have a circular cross section. The cross section of the combustion chambers can, however, also be rectangular, oval or any other form. It is always expedient if the first combustion chamber and the second combustion chamber have the same cross section, it being possible for an inner free diameter of the two combustion chambers to differ. It is advantageous if at least the first combustion chamber comprises at least two cylindrical layers, which are in particular inserted coaxially into one another or arranged with respect to one another. In this case, a first cylindrical layer can close off the first combustion chamber radially to the outside and can be coated on its radial inside with a second cylindrical layer, which is designed as a catalytic material. Within the scope of the invention, all cylindrical layers are to be understood as hollow-cylindrical layers unless clearly described otherwise.
    It is advantageous if the catalytic material of the first combustion chamber is designed as a catalytically coated ceramic or as a catalytically coated metal. The honeycomb-shaped bodies are formed from a ceramic or a metal or a metal alloy, and these are advantageously catalytically coated. It is particularly advantageous if the catalytic material is monolithic.
    However, it can also be provided that the catalytic material of the first combustion chamber is designed as a catalytically coated fabric. The catalytic material or the second cylindrical layer of the first combustion chamber is in particular arranged in a ring within the first cylindrical layer. Basically, the catalytic material formed as a coated fabric can be shaped as desired.
    A burner according to the invention is advantageously used as a starting burner and afterburner in a fuel cell system which is operated with gaseous fuel, in particular in a stationary fuel cell system operated with natural gas.
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    According to a further aspect of the present invention, a fuel cell system with a burner as detailed above is provided. Such a fuel cell system also has a fuel cell stack with an anode section and a cathode section and a reformer and at least one heat exchanger, the burner, the fuel cell stack, the reformer and the heat exchanger being arranged in a hot box.
    A fuel cell system according to the invention thus has the same advantages as have been described in detail with reference to the burner according to the invention. The fuel cell system is preferably a stationary SOFC system. A particular advantage can be seen in the fact that a separate starting burner is not necessary in such a fuel cell system, as a result of which components can be saved. The reformer is preferably designed to reform a fuel, for example natural gas, into another fuel mixture, in this case a fuel mixture rich in hydrogen and carbon dioxide. The reformed hydrogen can be used in a fuel cell stack to generate electricity. The burner is designed to heat the reformer by means of fuel cell exhaust gas from the fuel cell stack. Process gas or burned operating fluid mixture, which emerges from the burner, flows over a warm side of the heat exchanger and heats air, which flows over a cold side of the heat exchanger to a cathode section of the fuel cell stack. The reformer and the heat exchanger are arranged in parallel in two separate fluid lines downstream of the burner. Furthermore, it can be favorable if an additional heat exchanger is arranged downstream of the fuel cell stack and upstream of the reformer or the heat exchanger. This is designed to adapt the inlet temperatures of the operating fluids (fuel and air). The aim is to keep temperature differences between the two operating fluids as low as possible so that thermal stresses in the fuel cell stack are largely avoided.
    According to a first aspect of the present invention, the fuel cell system is a stationary SOFC system (SOFC stands for “solid oxide fuel cell” or solid oxide fuel cell). Such a fuel cell system is operated in particular with gaseous fuel.
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    All functional elements of the fuel cell system are arranged in the hot box. For the most effective heat protection possible for functional elements or auxiliary devices outside the hotbox, the hotbox preferably has an insulation housing for thermal insulation of the components inside the hotbox from the auxiliary devices outside the hotbox. The insulation housing is an at least essentially closed housing. In other words, the hotbox has at least one insulation wall for the thermal insulation of components inside the hotbox from components outside the hotbox. In particular, the hotbox is closed on all sides. According to a preferred embodiment variant of the present invention, the hotbox has a housing section which encloses the fuel cell unit, the reformer and the burner and the heat exchanger in a thermally insulating manner, or at least essentially encloses it. Furthermore, the hot box can optionally also be gas-tight. A hot box in the sense of the invention is a housing within which an elevated temperature is present. The housing is at least partially designed for the thermal insulation of elements within it.
    It is also advantageous if a first operating fluid source is provided to provide a first operating fluid and a second operating fluid source is provided to provide a second operating fluid. The operating fluid sources are each arranged outside the hotbox, the first operating fluid source providing the fuel, in particular natural gas, and the second operating fluid source an oxidizing agent, in particular ambient air, a fluid line emerging from each operating fluid source. According to the invention, it is advantageous if each fluid line comprises at least two sub-lines. A fan is preferably arranged downstream of the second operating fluid source outside the hot box. A first partial line of the second fluid line leads in the direction of the cathode section of the fuel cell stack, the air guided therein upstream of the cathode section being conducted via a cold side of the heat exchanger and from the burned and heated operating fluid mixture which emerges from the burner and via a warm side of the heat exchanger is heated. Upstream of the heat exchanger and downstream of the fan, a second partial line is advantageously branched off from the second fluid line, via which air can be transported in the direction of a burner inlet. This allows / 26
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    AVL List GmbH can be influenced by adding air to a combustion ratio in the burner. A valve for controlling this air supply is advantageously provided in the second partial line of the second fluid line outside the hotbox. It is also favorable if the first fluid line is divided into a first and a second partial line downstream of the fuel source. The first partial line of the first fluid line leads via a valve to the reformer and downstream of the same to the anode section of the fuel cell stack. The second partial line of the first fluid line also leads to the combustion inlet via a valve. As a result, a combustion ratio in the burner can also be influenced by supplying fuel, if necessary.
    The fuel cell system advantageously further comprises an electrical heat source, which is arranged outside the hot box. The electrical heat source is designed and arranged to bring the burner, in particular the catalytic material of the first combustion chamber, to operating temperature.
    Further advantages, features and effects result from the exemplary embodiments shown below. In the drawings, to which reference is made, show:
    1 shows a section through a burner according to the invention.
    FIG. 2 shows a block diagram for illustrating a fuel cell system according to an embodiment of the invention;
    3 shows a block diagram for illustrating a fuel cell system according to a further embodiment according to the invention.
    1 shows a burner 1 according to the invention. This comprises a first combustion chamber 2 and a second combustion chamber 3, the second combustion chamber 3 connecting directly downstream to the first combustion chamber 2. The first combustion chamber 2 comprises a catalytic material 9, which is designed, for example, as a fabric, whereas the second combustion chamber 3 comprises a flame burner, not shown in FIG. 1. The two combustion chambers 2, 3 directly adjoin one another in the direction of flow, a fuel mixture first flowing through the first combustion chamber 2 and then through the second combustion chamber 3. The flow direction is thus indicated from right to left in FIG. 1. The burner 1 is in a / 26 both as a start burner and as an afterburner
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    Fuel cell system 100 can be used. When the burner 1 is used as a starting burner, an operating fluid mixture, in particular a mixture of fuel and air, is completely burned in it, the resulting gas being usable for heating components of the fuel cell system 100 or the fuel cell system 100 itself. If the burner 1 is used as an afterburner, then the fuel cell stack exhaust gas is burned. FIG. 2 shows a fuel cell system 100 according to the invention with such a burner 1. The fuel cell system 100 further comprises a fuel cell stack 110 with an anode section 120 and a cathode section 130 as well as a heat exchanger 7 and a reformer 8, all of these elements being arranged in a hot box 10. The hot box 10 thermally insulates the elements arranged therein from the surroundings. The fuel cell system 100 further comprises a first operating fluid source 5 and a second operating fluid source 6, the first operating fluid source 5 providing a fuel in the form of natural gas and a second operating fluid source 6 an oxidizing agent in the form of ambient air. A blower 11 and a plurality of valves 12 are also provided. All of these elements are arranged outside the hot box 10.
    In addition, a fuel cell system 100 also includes several fluid lines. A first fluid line 13 leads from the first operating fluid source 5 and a second fluid line 14 leads away from the second operating fluid source 6. The first fluid line 13 separates outside the hotbox 10 into a first sub-line 13 a and a second sub-line 13 b of the second fluid line 13. The first sub-line 13 a of the first fluid line 13 leads to the reformer 8 via a valve 12 and downstream to the anode section 120 of the fuel cell stack 110 The second partial line 13b of the first fluid line 13 likewise leads via a valve 12 to the chamber inlet 4 of the burner 1. The second fluid line 14 also separates downstream of the second operating fluid source 6 into a first partial line 14a and second partial line 14b. A fan 11 is arranged downstream of the second operating fluid source 6 outside the hot box 10. The first partial line 14a of the second fluid line 14 leads in the direction of the cathode section 130 of the fuel cell stack 110, the air conducted therein being conducted upstream of the cathode section 130 via a cold side of the heat exchanger 7. Upstream of the heat exchanger 7 and downstream of the blower 11, the second / 26
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    Branch 14b branched, via which air can be transprotected in the direction of the chamber entrance 4 of the burner 1.
    The second partial line 13b of the first fluid line 13 and the second partial line 14b of the second partial line 14 thus lead to the burner 1 in order to heat the fuel cell system 100 when the burner 1 is used as a starting burner. Downstream of the burner 1, the heat of the burned operating fluid mixture or the process gas resulting therefrom is used to heat the heat exchanger 7 and the reformer 8, these being arranged in two parallel lines 15a, 15b. The hot gas is thus fed to a warm side of the heat exchanger 7 and the reformer 8. The operating fluids of the operating fluid sources 5, 6 are thus brought to a predetermined temperature by the banished operating fluid mixture.
    FIG. 3 shows another fuel cell system 100 according to the invention with such a burner 1. All elements which correspond to those (including their function) of the fuel cell system according to FIG. 1 are not described in more detail. In contrast to FIG. 1, this fuel cell system 100 comprises an electrical heat source 17, which is arranged outside the hot box 10. The electrical heat source 17 is designed and arranged to bring the burner 1, in particular the catalytic material of the first combustion chamber 2, to the operating temperature. The electrical heat source 17 can be configured, for example, as a calorific heating device or can have such a caloric heating device. The blower 11 is also designed (in addition to the above-described mode of operation) or can also be used to apply a temperature control fluid to the electrical heat source 17. In the present case, air is used as the temperature control fluid. The supply of air to the electrical heat source 17 can be controlled by a valve 12 or switched on and off.
    In a method according to the invention, the burner 1 is used both as a starting burner and as an afterburner. To warm up the fuel cell system 100, the second operating fluid is electrically heated via the second operating line 14b and subsequently heats the burner 1 to operating temperature. The operating temperature is the temperature above which the complete catalytic combustion of natural gas is possible. As soon as the burner 1 this / 26
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    Has reached operating temperature, the first operating fluid in the form of natural gas is fed via the first sub-line 13b and the second operating fluid in the form of ambient air via the two second sub-lines 14a, 14b into the first combustion chamber 2 of the burner 1, the latter upstream of the chamber inlet 4 first combustion chamber 2 are mixed together to form an operating fluid mixture. In the first combustion chamber 2, the operating fluid mixture is burned catalytically at a temperature of approximately 600 ° C. The operating fluid mixture present as an air-fuel mixture is mixed in such a way that the combustion temperature does not exceed the permissible maximum operating temperature of the catalytic converter. As soon as the catalyst is fully heated, the amount of fuel and air is increased further in order to achieve a higher thermal output. The mixture is adjusted so that there is no complete combustion in the first combustion chamber. Immediately after the first combustion chamber 2, the partially burned operating fluid mixture is passed into the second combustion chamber 3, in which it is completely burned by flame combustion. The burned operating fluid mixture or the process gas is now conducted out of the burner 1, which, depending on a heating strategy, has a temperature of approximately 900 ° C. to approximately 1100 ° C. Downstream of the burner 1, the process gas is divided into the two lines 15a, 15b arranged parallel to one another. A first part of the process gas is led to the warm side of the heat exchanger 7 and a second part to the warm side of the reformer 8. At the same time, natural gas is led from the first operating fluid source 5 via the first partial line 13a to the cold side of the reformer 8, the natural gas now being warmed up or reformed by the hot process gas before it is passed on to the anode section 120. At the same time, air is conducted from the second operating fluid source 6 via the first sub-line 14a with the aid of the blower to the heat exchanger 7, as a result of which the air for the cathode section 130 is heated. As a result, the fuel cell stack 110 and the fuel cell system 100 are brought to a predefined operating temperature. As soon as this is reached, the supply of the first operating fluid to the burner 1 via the first sub-line 13b is stopped by setting the valve 12.
    The fuel cell system 100 is now in normal operation and the burner 1 is used as an afterburner. Exhaust gas from the fuel cell stack 110, which was not completely burned in the latter, is burned in this. For this, / 26
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    Anode exhaust gas and cathode exhaust gas are brought together downstream of the fuel cell stack 110 and upstream of the chamber entrance 4 of the first combustion chamber 2. This is fed into the first combustion chamber 2 and burned completely catalytically in this. The burned gas is then passed through the second combustion chamber 3, which has no further function in this operation. Since the exhaust gas is already completely burned in the first combustion chamber 2, further combustion in the second combustion chamber 3 is not necessary. The hot process gas, which emerges from the burner 1, is in turn passed to the heat exchanger 7 and reformer 8 in order to heat up the process fluids. Downstream of the heat exchanger 7 and the reformer 8, the two lines 15a, 15b are brought together again and the gas which has now cooled is released to the environment or collected in a container 16.
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    权利要求:
    Claims (13)
    [1]
    Claims
    1. A method for operating a fuel cell system (100), in particular a stationary fuel cell system (100), the method comprising the following steps:
    - Introducing a first operating fluid and a second operating fluid into a first combustion chamber (2) of a burner (1), the first operating fluid and the second operating fluid being mixed upstream of a chamber entrance (4) of the first combustion chamber (2) to form an operating fluid mixture ;
    - At least partial catalytic combustion of the operating fluid mixture;
    - guiding the partially burned operating fluid mixture into a second combustion chamber (3) of the burner (1), the second combustion chamber (3) being arranged immediately downstream of the first combustion chamber (2);
    - optionally complete combustion of the operating fluid mixture in the second combustion chamber (3) comprising a flame burner.
    [2]
    2. The method according to claim 1, characterized in that a flow rate of the operating fluid mixture in the first combustion chamber (2) is increased to a predetermined value.
    [3]
    3. The method according to claim 1 or 2, characterized in that the fuel cell system (100) is heated by the combustion of the operating fluid mixture in the burner (1).
    [4]
    4. The method according to claim 3, characterized in that the operating fluid is only partially burned in a first step in the first combustion chamber (2) and completely burned in a second step in the second combustion chamber (3).
    [5]
    5. The method according to claim 4, characterized in that an introduction of a first operating fluid from a first operating fluid source (5) and a second operating fluid from a second operating fluid source (6) is set as soon as the fuel cell system (100) reaches a predetermined operating temperature.
    [6]
    6. The method according to any one of claims 1 to 5, characterized in that in the burner (1) fuel cell stack exhaust gas is burned, which is from
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    Existing fuel cell stack exhaust gas and cathode exhaust gas is completely burned in the first combustion chamber (2).
    [7]
    7. The method according to any one of claims 1 to 6, characterized in that the burned operating fluid mixture downstream of the burner (1) for heating at least one heat exchanger (7) and / or a reformer (8) is used, the burned operating fluid Mixture is supplied as system exhaust gas to a warm side of the at least one heat exchanger (7) and / or the reformer (8).
    [8]
    8. burner (1) for a fuel cell system (100), in particular a stationary SOFC system, the burner (1) being designed and arranged as a starting burner and / or afterburner, characterized in that the burner (1) has two combustion chambers arranged one after the other (2, 3), a first combustion chamber (2) comprising a catalytic material (9) and a second combustion chamber (3) arranged immediately downstream of the first combustion chamber (2) comprising a flame burner.
    [9]
    9. burner (1) according to claim 8, characterized in that at least the first combustion chamber (2) comprises honeycomb elements.
    [10]
    10. Burner (1) according to claim 8 or 9, characterized in that the catalytic material (9) of the first combustion chamber (2) is designed as a catalytically coated ceramic or as a catalytically coated metal.
    [11]
    11. Use of a burner (1) according to one of claims 8 to 10 as a starting burner and / or afterburner in a fuel cell system (100) which is operated with gaseous fuel, in particular in a stationary fuel cell system (100) operated with natural gas.
    [12]
    12. Fuel cell system (100), in particular a stationary SOFC system with a burner (1) according to one of claims 8 to 10, characterized in that the fuel cell system (100) further comprises a fuel cell stack (110) with an anode section (120) and one Cathode section (130) and a reformer (8) and at least one heat exchanger (7), the burner (1), the fuel cell stack (110), the reformer (8) and the heat exchanger (7) arranged in a hot box (10) are.
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    [13]
    13. The fuel cell system (100) according to claim 12, a first operating fluid source (5) for providing a first operating fluid and a second operating fluid source (6) are provided for providing a second operating fluid.
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    1/2
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    2/2
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    Patent office
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    引用文献:
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    WO2003060380A1|2002-01-11|2003-07-24|General Motors Corporation|Quick start large dynamic range combustor configuration|
    EP1465274A2|2003-04-03|2004-10-06|J. Eberspächer GmbH Co. KG|Fuel cell system and a burner arrangement for a fuel cell system|
    WO2007079976A1|2005-12-29|2007-07-19|Süd-Chemie AG|Catalyst based on a hexaaluminate for the combustion of hydrocarbons and fuel cell arrangement with exhaust burner|
    EP1845576A2|2006-04-12|2007-10-17|J. Eberspächer GmbH & Co. KG|Fuel cell system|
    EP2023040A1|2006-05-30|2009-02-11|Nippon Chemical Plant Consultant Co., Ltd.|Combustor|
    WO2017003089A1|2015-06-29|2017-01-05|주식회사 경동나비엔|Solid oxide fuel cell system heated by external heat source|EP3893304A1|2020-04-08|2021-10-13|inhouse engineering GmbH|Fuel cell system for power and heat generation and method for operating the fuel cell system|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    ATA50031/2018A|AT520881B1|2018-01-17|2018-01-17|Method for operating a fuel cell system|ATA50031/2018A| AT520881B1|2018-01-17|2018-01-17|Method for operating a fuel cell system|
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