A solid oxide fuel cell stack system, its operation control method and application

Abstract

The application discloses a solid oxide fuel cell stack system and a running control method and application thereof, and belongs to the technical field of fuel cells. The cell stack system comprises a cell stack body, a temperature detection module, a power detection module and a control module; the cell stack body is formed by stacking a plurality of cell bodies in sequence; a reforming porous area is arranged between a reforming synthesis gas flow channel and an oxidation gas flow channel in a connecting body of each cell body; an anode, an electrolyte and a cathode are sequentially arranged on the surface of the connecting body; the power detection module is used for detecting the power required by a total load and feeding back to the control module; the temperature detection module is used for detecting the gas temperature and feeding back to the control module; and the control module is used for receiving signals and outputting relevant control signals. The cell stack system adopts an indirect internal reforming mode, avoids carbon deposition on the anode, causes the cell structure to be damaged and the performance to be degraded, and realizes efficient thermal management of the cell stack by jointly controlling the gas flow based on the power and temperature signals, thereby prolonging the service life of the cell stack system and improving the efficiency.

Description

Technical Field

[0001] The present invention relates to the field of fuel cell technology, and in particular to a solid oxide fuel cell stack system, an operation control method and an application thereof. Background Art

[0002] Solid oxide fuel cells (SOFCs) can use a wide range of fuels. In addition to hydrogen, other hydrocarbon fuels, such as methane, syngas, ethanol, and diesel, can also be used for power generation. When using hydrocarbons as SOFC fuels, the fuel is typically reformed to produce a syngas mixture of CO and H₂, which then enters the porous electrodes for an electrochemical reaction.

[0003] From the perspective of the reforming scenario, fuel reforming can be divided into external reforming and internal reforming. External reforming increases the size and complexity of the system, increasing costs. Although internal reforming can reduce the complexity and cost of external reforming equipment, the internal reforming of the fuel inside the battery is a very fast, highly endothermic chemical reaction that requires the absorption of a large amount of heat, resulting in a large temperature gradient within the battery. The resulting thermal stress can easily damage the battery structure and lead to performance degradation. In addition, hydrocarbon fuels are prone to cracking during reforming inside the high-temperature anode, and the resulting carbon deposits cover the surface of the anode active sites, significantly reducing battery performance.

[0004] Furthermore, the temperature of a solid oxide fuel cell stack plays a crucial role in its performance. Excessively low temperatures result in low power density and power generation efficiency within a single cell, while excessively high temperatures or large temperature gradients can lead to corrosion, deformation, and even cracking and delamination of sealing materials, battery electrodes, electrolytes, and interconnects, significantly reducing stack performance and shortening its service life. Therefore, scientifically and rationally managing the thermal performance of solid oxide fuel cell stacks to maintain operation within the set operating temperature range can improve system reliability.

[0005] Currently, there are two main thermal management methods for overheating during battery stack operation: one is to increase the flow rate of oxidizing gas in the battery cathode flow channel, allowing the excess gas to remove heat; the other is to design specialized cooling gas flow channels to control the battery stack temperature. Both methods use gas to remove heat to control the battery stack temperature, but because this heat is not reused, it reduces the energy efficiency of the entire system. Moreover, allowing excess oxidizing gas to directly contact the battery cathode surface may cause internal heterogeneous interface separation and other structural damage.

[0006] In view of this, the present invention is proposed. Summary of the Invention

[0007] One of the purposes of the present invention is to provide a solid oxide fuel cell stack system, which adopts an indirect internal reforming method to avoid damage to the battery structure and performance degradation caused by anode carbon deposition. By using power and temperature signals to jointly control the gas flow to achieve efficient thermal management of the battery stack, the life and efficiency of the battery stack system can be improved.

[0008] A second object of the present invention is to provide an operation control method for the above-mentioned solid oxide fuel cell stack system.

[0009] A third object of the present invention is to provide an application of the above-mentioned solid oxide fuel cell stack system.

[0010] This application can be implemented as follows:

[0011] In a first aspect, the present invention provides a solid oxide fuel cell stack system, comprising a cell stack body, a temperature detection module, a power detection module, a load, and a control module;

[0012] The battery stack body is formed by stacking a plurality of battery bodies in sequence; each battery body includes a single battery and a connector and a reassembly plate; the connector and the reassembly plate include a connector body, the upper and lower surfaces of the connector body are respectively provided with a battery support porous area and an oxidation flow channel, the lower surface of the battery support porous area is provided with a reforming synthesis flow channel, a reforming porous area for providing a catalytic reaction of the reformed fuel is provided between the reforming synthesis flow channel and the oxidation flow channel, and the reforming porous area is separated from the reforming synthesis flow channel and the oxidation flow channel by a leak-proof wall to achieve self-sealing of the reformed fuel; the single battery includes an anode, an electrolyte and a cathode arranged in sequence, and the anode, the electrolyte and the cathode are arranged in sequence on the side of the battery support porous area away from the reforming synthesis flow channel;

[0013] The power detection module is used to detect the power required by the total load in the circuit and feed it back to the control module;

[0014] The temperature detection module is used to detect the gas temperature at at least part of the flow channel inlet and feed it back to the control module;

[0015] The control module is used to receive the real-time operation signal data of the battery stack body fed back by the temperature detection module and the power detection module. After iterative calculation and processing of the load power and the gas temperature signal data of the gas path monitoring point, it outputs relevant signals including the control of the flow rate of each reaction gas and controls the introduction of each reaction gas.

[0016] In an optional embodiment, the solid oxide fuel cell stack system further includes a DC / AC voltage conversion device, which is simultaneously connected to the cell stack body, the power detection module, and the load.

[0017] In an optional embodiment, the temperature detection module is connected to at least one of the following gas paths in each battery body:

[0018] Gas path 1: air path entering the cathode;

[0019] Gas path 2: The reformed mixed gas entering the reforming porous zone enters the gas path;

[0020] Gas path three: the gas outlet path for the synthesis gas flowing out of the reforming porous zone.

[0021] In an optional embodiment, a gas flow meter is provided on at least part of the gas path, and the gas flow meter is connected to the control module signal so that the gas flow control instruction output by the control module to the gas flow meter controls the introduction of each reaction gas.

[0022] In an optional embodiment, the solid oxide fuel cell stack system further includes a heat exchanger connected to at least one of the gas path 1 and the gas path 2 in each cell body for preheating at least a portion of the initial gas entering the corresponding flow channel;

[0023] The initial raw materials entering gas path 1 include air, and the initial raw materials entering gas path 2 include water vapor, nitrogen and hydrocarbon fuel.

[0024] In an optional embodiment, the solid oxide fuel cell stack system also includes a burner, the inlet of which is connected to the cathode oxidizing gas outlet and the anode reforming synthesis gas outlet in each cell body for recovering the reaction exhaust gas discharged from the cell stack body and performing catalytic reaction combustion.

[0025] In an optional embodiment, the inlet of the burner is further connected to the hydrocarbon fuel outlet of the heat exchanger so as to introduce part of the preheated hydrocarbon fuel gas into the burner for catalytic reaction and combustion.

[0026] In an optional embodiment, the outlet of the burner is also connected to the inlet of the heat exchanger so that the high-temperature gas generated after the catalytic reaction and combustion can be passed into the heat exchanger.

[0027] In a second aspect, the present application provides an operation control method of a solid oxide fuel cell stack system according to any one of the aforementioned embodiments, comprising the following steps:

[0028] The power detection module is used to detect the power required by the total load in the circuit and feed it back to the control module;

[0029] A temperature detection module is used to detect the gas temperature at at least part of the flow channel inlet and feed it back to the control module;

[0030] After receiving the real-time operation signal data of the battery stack body fed back by the temperature detection module and the power detection module, the control module performs iterative calculations on the power and gas temperature signal data, outputs relevant control signals including the flow rate of each reaction gas, and controls the introduction of each reaction gas.

[0031] In a third aspect, the present application provides an application of a solid oxide fuel cell stack system according to any one of the aforementioned embodiments, which can be used, for example, for power supply.

[0032] The beneficial effects of this application include:

[0033] The solid oxide fuel cell stack system provided in this application adopts an indirect internal reforming method to avoid damage to the battery structure and performance degradation caused by anode carbon deposition. By using power and temperature signals to jointly control the gas conditions to achieve efficient thermal management of the battery stack, the life and efficiency of the battery stack system can be improved. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following briefly introduces the drawings required for use in the embodiments. It should be understood that the following drawings only illustrate certain embodiments of the present invention and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other relevant drawings can be obtained based on these drawings without paying any creative work.

[0035] Figure 1 A schematic diagram of the structure of the battery stack provided in this application;

[0036] Figure 2 This is a schematic diagram of the structure of the battery body provided in this application at a first viewing angle;

[0037] Figure 3 This is a schematic structural diagram of the connecting weight adjustment plate in the battery body provided by this application at a second viewing angle;

[0038] Figure 4 Schematic diagram of the operation control method of the solid oxide fuel cell stack system provided in this application.

[0039] Icon: 100 - cell stack body; 1 - cell body; 10 - connecting body reforming plate; 11 - connecting body body; 111 - first side; 112 - second side; 113 - third side; 114 - fourth side; 115 - reforming synthesis gas inlet; 116 - reforming synthesis gas outlet; 117 - oxidizing gas inlet; 118 - oxidizing gas outlet; 119 - reforming fuel inlet; 120 - reforming fuel outlet; 12 - cell support porous area; 13 - reforming synthesis gas flow channel; 14 - reforming porous area; 15 - oxidizing gas flow channel; 20 - single cell; 21 - anode; 22 - electrolyte; 23 - cathode; 30 - temperature detection module; 31 - thermometer; 40 - power detection module; 50 - control module; 60 - DC / AC voltage conversion device; 61 - load; 70 - gas path flow meter; 80 - heat exchanger; 90 - burner. DETAILED DESCRIPTION

[0040] In order to make the purpose, technical solutions and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application will be described clearly and completely below. If specific conditions are not indicated in the embodiments, conventional conditions or the conditions suggested by the manufacturers are adopted. If the reagents or instruments used are not indicated by the manufacturers, they are all conventional products that can be purchased in the market.

[0041] The solid oxide fuel cell stack system provided by the present application and the operation control method and application thereof will be described in detail below.

[0042] Please refer to Figures 1 to 4 , the present application provides a solid oxide fuel cell stack system, which comprises a cell stack body 100, a temperature detection module 30, a power detection module 40, a load 61 and a control module 50.

[0043] In combination Figure 1 , the cell stack body 100 is formed by stacking a plurality of cell bodies 1 in sequence; each cell body 1 comprises a single cell 20 and a connecting body reforming plate 10, and two adjacent cell bodies 1 are sealed by a sealing material (not shown in the figure).

[0044] In combination Figure 2 , the connecting body reforming plate 10 comprises a connecting body body 11, the upper surface and the lower surface of the connecting body body 11 are respectively provided with a cell support porous area 12 and an oxidizing gas flow channel 15, the lower surface of the cell support porous area 12 is provided with a reforming synthesis gas flow channel 13, the reforming synthesis gas flow channel 13 and the oxidizing gas flow channel 15 are provided with a reforming porous area 14 for catalytic reaction of reforming fuel, and the reforming porous area 14 is separated from the reforming synthesis gas flow channel 13 and the oxidizing gas flow channel 15 by a wall surface without leakage to realize the sealing of the reforming fuel.

[0045] In combination Figure 1 and Figure 2The single cell 20 includes an anode 21, an electrolyte 22, and a cathode 23, which are sequentially arranged on the side of the cell-supporting porous region 12 away from the re-integration synthesis channel 13. The anode 21 covers the upper surface of the cell-supporting porous region 12, while the electrolyte 22 covers the entire interconnect body 11 and the upper surface of the anode 21. The projection of the cathode 23 overlaps with the area occupied by the re-integration synthesis channel 13.

[0046] That is, it can be understood that a single battery body 1 includes a cathode 23, an electrolyte 22, an anode 21 and a connecting and reorganizing plate 10 from top to bottom, and the structure of the connecting and reorganizing plate 10 roughly includes a battery support porous area 12, a reforming synthesis airflow channel 13, a reforming porous area 14 and an oxidation airflow channel 15 from top to bottom.

[0047] The above-mentioned single cell body 1 can simultaneously realize indirect reforming of hydrocarbon fuels and self-sealing of the fuel gas path.

[0048] It should be noted that the number of battery bodies 1 contained in the battery stack system provided in this application can be 2, 3 or more, and the specific number depends on the situation.

[0049] Taking the case where the number of battery bodies 1 contained in the battery stack system is two as an example, for the sake of easy distinction and understanding, the two battery bodies 1 are defined as the first battery body and the second battery body respectively, and the oxidation flow channel 15 of the second battery body is arranged (for example, by bonding with sealant) on the cathode 23 of the first battery body.

[0050] In a single battery body 1, the area of ​​the battery supporting porous region 12 is smaller than the area of ​​the upper surface of the connector body 11, and the battery supporting porous region 12 is connected to the re-integrated synthesis flow channel 13 to allow the synthesis gas to diffuse through the pores of the battery supporting porous region 12 to the anode 21 located on the upper surface of the battery supporting porous region 12.

[0051] In the present application, the reforming porous region 14 is a region having a polyhedral lattice unit structure. For example, the polyhedron may be a hexahedron or an octahedron.

[0052] In some embodiments, the number of reforming porous regions 14 may be only one. In other embodiments, the reforming porous region 14 includes at least two porous sub-regions. When the reforming porous region 14 includes at least two porous sub-regions, adjacent porous sub-regions are separated by ribs, and the multiple porous sub-regions are arranged in sequence perpendicular to the flow direction of the reformed fuel.

[0053] In the present application, the porosity of each porous sub-region gradually decreases along the flow direction of the reformed fuel, preferably decreasing in a gradient.

[0054] It should be noted that the fuel reforming that occurs within the battery is a highly endothermic chemical reaction with a very fast rate, requiring the absorption of a large amount of heat. By setting the porosity to decrease in a gradient, this application helps avoid the large temperature gradients within the battery caused by the reforming process, reduces the thermal stress generated, and prevents damage to the battery structure. Furthermore, this approach not only prevents carbon deposits formed by hydrocarbon fuels from covering the surface of the active sites of the anode 21, causing a significant decrease in battery performance, but also prevents separation of the heterogeneous interface within the battery, which can damage the structure.

[0055] For reference, the maximum porosity of the above porosity is no more than 90%, and the minimum porosity is no less than 50%. The diameter of each pore in the reforming porous region 14 can be 50-1000 μm, and the total thickness of the reforming porous region 14 can be 0.5-2.0 mm.

[0056] For ease of understanding, the re-integrated synthesis flow channel 13 may be a groove recessed from top to bottom. Similarly, the oxidation flow channel 15 may be a groove recessed upward from the lower surface of the connector body 11 .

[0057] Preferably, all surfaces in contact with the reforming fuel are provided with a catalyst for the hydrocarbon fuel to undergo a reforming reaction. Alternatively, a portion of the surface in contact with the reforming fuel may be provided with a catalyst for the hydrocarbon fuel to undergo a reforming reaction.

[0058] In this application, combined Figure 3 The connector body 11 is provided with at least one pair of through holes for the flow of at least one of hydrocarbon fuel, reformed synthetic gas (including hydrocarbon fuel, water vapor and liquefied natural gas) and oxidizing gas.

[0059] In some specific embodiments, the arrangement of the connector body 11 and the through hole can refer to the following method: taking the connector body 11 as a whole being a quadrilateral (such as a rectangle) as an example, it has a first side 111, a second side 112, a third side 113 and a fourth side 114 connected end to end, wherein the first side 111 and the third side 113 are arranged opposite to each other, and the second side 112 and the fourth side 114 are arranged opposite to each other.

[0060] The through hole includes a reformed synthetic gas inlet 115 , a reformed synthetic gas outlet 116 , an oxidizing gas inlet 117 , an oxidizing gas outlet 118 , a reformed fuel inlet 119 , and a reformed fuel outlet 120 .

[0061] The reforming syngas inlet 115 is arranged at a position close to the first side face 111 of the connecting body 11 and penetrates the upper surface and the lower surface of the connecting body 11, and the reforming syngas outlet 116 is arranged at a position close to the third side face 113 of the connecting body 11 and penetrates the upper surface and the lower surface of the connecting body 11; the oxidizing gas inlet 117 is arranged at a position close to the third side face 113 of the connecting body 11 and penetrates the upper surface and the lower surface of the connecting body 11, and the oxidizing gas outlet 118 is arranged at a position close to the first side face 111 of the connecting body 11 and penetrates the upper surface and the lower surface of the connecting body 11; the reforming fuel inlet 119 is arranged at a position close to the second side face 112 of the connecting body 11 and penetrates the upper surface and the lower surface of the connecting body 11, and the reforming fuel outlet 120 is arranged at a position close to the fourth side face 114 of the connecting body 11 and penetrates the upper surface and the lower surface of the connecting body 11.

[0062] The two ends of the reforming syngas flow channel 13 are in communication with the reforming syngas inlet 115 and the reforming syngas outlet 116 respectively, the two ends of the oxidizing gas flow channel 15 are in communication with the oxidizing gas inlet 117 and the oxidizing gas outlet 118 respectively, and the two ends of the reforming porous region 14 are in communication with the reforming fuel inlet 119 and the reforming fuel outlet 120 respectively.

[0063] Exemplarily, the reforming syngas flow channel 13 can be formed by a plurality of reforming syngas sub-flow channels arranged at intervals, and the extension direction of each reforming syngas sub-flow channel is the flow direction of the reforming syngas, which specifically extends from the first side face 111 to the third side face 113. Similarly, the oxidizing gas flow channel 15 can also be formed by a plurality of oxidizing gas sub-flow channels arranged at intervals, and the extension direction of each oxidizing gas sub-flow channel is the flow direction of the oxidizing gas, which specifically extends from the third side face 113 to the first side face 111.

[0064] In some embodiments, the number of reforming syngas inlets 115 can be 2, and the number of reforming syngas outlets 116 can be 1, in which case one end of part of the reforming syngas sub-flow channels is in communication with one of the reforming syngas inlets 115, the other end of the remaining reforming syngas sub-flow channels is in communication with the remaining one of the reforming syngas inlets 115, and the other end of all the reforming syngas sub-flow channels is in communication with the reforming syngas outlet 116.

[0065] The connection relationship between the oxidizing gas inlet 117, the oxidizing gas outlet 118, and the oxidizing gas sub-flow channels, and the connection relationship between the reforming fuel inlet 119, the reforming fuel outlet 120, and the porous sub-regions can be set by referring to the connection relationship of the reforming syngas inlet 115, the reforming syngas outlet 116, and the reforming syngas sub-flow channels.

[0066] It should be noted that in other embodiments, the shape of the connector body 11 and the location and number of the through holes can also be adjusted according to actual needs. In addition, other solid fuel cell related contents not described in detail in this application can be referred to the corresponding existing technology and will not be elaborated here.

[0067] In the present application, the power detection module 40 is used to detect the power required by the total load in the circuit and feed back the power to the control module 50 .

[0068] In some optional embodiments, the solid oxide fuel cell stack system further includes a DC / AC voltage conversion device 60 , which is simultaneously connected to the cell stack body 100 , the power detection module 40 and the load 61 .

[0069] That is, the power detection module 40 and the load 61 are connected to the DC / AC voltage conversion device 60 derived from the battery stack, which monitors the power changes of the load 61 in the circuit in real time and feeds back the power-related signals in the circuit to the control module 50.

[0070] In the present application, the temperature detection module 30 is used to detect the gas temperature at least at a portion of the flow channel inlet and feed it back to the control module 50 .

[0071] For reference, the temperature detection module 30 may be connected to at least one of the following gas paths in each battery body 1:

[0072] Gas path 1: air path entering the cathode 23;

[0073] Gas path 2: the reformed mixed gas entering the reforming porous zone 14 enters the gas path;

[0074] Gas path three: the gas outlet path for the synthesis gas flowing out of the reforming porous zone 14 .

[0075] That is, in some embodiments, the temperature detection module 30 is connected to gas circuit one, gas circuit two, or gas circuit three in each battery body 1; in other embodiments, the temperature detection module 30 is connected to gas circuit one and gas circuit two at the same time, or is connected to gas circuit one and gas circuit three at the same time, or is connected to gas circuit two and gas circuit three at the same time; in other embodiments, the temperature detection module 30 is connected to gas circuit one, gas circuit two, and gas circuit three at the same time.

[0076] When the temperature detection module 30 is connected to gas path 1, it can detect the inlet temperature of the power generation air entering the cell stack. When the temperature detection module 30 is connected to gas path 2, it can detect the inlet temperature of the mixed gas to be reformed (including a mixture of hydrocarbon fuel and water vapor) entering the cell stack. When the temperature detection module 30 is connected to gas path 3, it can detect the outlet temperature of the syngas catalytically generated by the mixed gas in the reforming porous zone 14. Based on this, the temperature detection module 30 can feed back the gas temperature at each detection point to the control module 50.

[0077] It should be noted that nitrogen can also be introduced into gas line 2, firstly to purge the stack before startup, and secondly to provide a protective atmosphere for the stack reaction. In addition, the raw materials entering gas line 2 can also include liquefied natural gas.

[0078] In the present application, a gas flow meter 70 is provided on at least part of the gas path, and the gas flow meter 70 is signal-connected to the control module 50 so as to control the introduction of each reaction gas through the gas flow control instruction output by the control module 50 to the gas flow meter 70.

[0079] Preferably, according to the connection conditions between the temperature detection module 30 and each gas path, a corresponding gas path flow meter 70 is provided on each gas path connected to the temperature detection module 30 .

[0080] In this application, the control module 50 is used to receive the real-time operation signal data of the battery stack body 100 fed back by the temperature detection module 30 and the power detection module 40, and after iterative calculation and processing of the load 61 power and the gas temperature signal data of the gas path monitoring point, output relevant control signals including controlling the flow rate of each reaction gas and controlling the introduction of each reaction gas.

[0081] Specifically, the control module 50 can determine the corresponding air, hydrocarbon fuel and water vapor flow rates under normal system operation based on the power data signal of the load 61; the control module 50 can determine the hydrocarbon fuel flow rate entering the following burner 90 based on the temperature data signal to ensure that the heat exchanger 80 has sufficient energy to preheat the air, hydrocarbon fuel, nitrogen and water vapor, or determine the ratio of hydrocarbon fuel and liquefied natural gas entering the cell stack reforming porous area 14, thereby comprehensively realizing efficient thermal management of the operating cell stack.

[0082] It should be noted that the configuration and working principle of the control module 50 can be referred to the relevant existing technologies and will not be elaborated here.

[0083] Furthermore, the solid oxide fuel cell stack system provided in the present application also includes a heat exchanger 80, which is connected to at least one of the gas circuits 1 and 2 in each cell body 1 to preheat at least part of the initial gas entering the corresponding flow channel.

[0084] Preferably, the heat exchanger 80 is connected to both the gas path 1 and the gas path 2 in each cell body 1 to preheat at least part of the initial gas entering the corresponding flow channel (part of the hydrocarbon fuel can be directly introduced into the burner 90 described below without preheating).

[0085] The initial raw materials entering the gas line 1 include air, and the initial raw materials entering the gas line 2 include water vapor, nitrogen and hydrocarbon fuel. In addition, the initial raw materials entering the gas line 2 may also include liquefied natural gas.

[0086] Furthermore, the solid oxide fuel cell stack system provided in the present application may also include a burner 90, the inlet of which is connected to the cathode oxidizing gas outlet and the anode reforming synthesizer outlet in each cell body 1 for recovering the reaction exhaust gas discharged from the cell stack body 100 and performing catalytic reaction combustion.

[0087] Furthermore, the inlet of the burner 90 is also connected to the hydrocarbon fuel outlet of the heat exchanger 80 so as to introduce part of the preheated hydrocarbon fuel gas into the burner 90 for catalytic reaction and combustion.

[0088] Furthermore, the outlet of the burner 90 is also connected to the inlet of the heat exchanger 80 to return the high-temperature gas generated after the catalytic reaction and combustion to the heat exchanger 80.

[0089] In some preferred embodiments, the burner 90 recovers the cell stack reaction exhaust or preheated hydrocarbon fuel gas, and after sufficient catalytic reaction and combustion, the high-temperature gas is passed to the heat exchanger 80. The heat exchanger 80 uses the high-temperature gas provided by the burner 90 as a heat source to preheat the hydrocarbon fuel, water vapor, nitrogen, and air entering the oxidation flow channel 15 to a temperature suitable for cell stack operation, and can also provide sufficient heat for cell stack preheating and startup.

[0090] Accordingly, the present application provides an operation control method of the solid oxide fuel cell stack system, comprising the following steps:

[0091] The power detection module 40 is used to detect the power required by the total load in the circuit and feed it back to the control module 50;

[0092] The temperature detection module 30 is used to detect the gas temperature at least at the inlet of the flow channel and feed it back to the control module 50; this process can be carried out by providing a thermometer 31 or a temperature detector.

[0093] After the control module 50 receives the real-time operation signal data of the battery stack body 100 fed back by the temperature detection module 30 and the power detection module 40, it performs iterative calculations on the power and gas temperature signal data, outputs relevant control signals including the flow rate of each reaction gas, and controls the introduction of each reaction gas.

[0094] When the solid oxide fuel cell stack system further comprises a DC / AC voltage conversion device 60, a gas path flow meter 70, a heat exchanger 80, a load 61 and a combustor 90, the operation control method further comprises:

[0095] The power detection module 40 is connected with the DC / AC voltage conversion device 60 leading out from the cell stack, the change of the power of the load 61 in the circuit is monitored in real time, and the power-related signal in the circuit is fed back to the control module 50. The control module 50 is connected with each control gas path flow meter 70, so that the control module 50 outputs corresponding gas flow control instructions to each flow meter 70, and each gas path flow meter 70 adjusts the corresponding gas flow according to the instructions.

[0096] The combustor 90 is used to recover the tail gas of the cell stack reaction or pass through the preheated hydrocarbon fuel gas, and after sufficient catalytic reaction and combustion, the high-temperature gas is delivered to the heat exchanger 80.

[0097] The heat exchanger 80 uses the high-temperature gas provided by the combustor 90 as a heat source to preheat the hydrocarbon fuel, water vapor, nitrogen and air entering the oxidation gas flow channel 15.

[0098] It should be emphasized that the nitrogen gas flowing in during the heating process of the cell stack can protect the electrode. The principle of the heat management control system includes: initially, only air is passed through the normal cathode, water vapor and hydrocarbon fuel are passed through the reforming area to allow the reforming reaction to occur. If the temperature control system detects that the temperature of the synthesis gas out of the reforming area is higher than the set operating temperature of the cell stack, then the amount of hydrocarbon fuel and water vapor is gradually increased, so that more fuel is reformed to absorb heat and reduce temperature; when the flow of hydrocarbon fuel is increased to the maximum set value, the control system starts to open the liquefied natural gas pipeline valve, and controls the flow ratio of hydrocarbon fuel and liquefied natural gas, thereby realizing the heat management control of the cell stack.

[0099] It should be noted that the above control process or principle which is not specifically expanded can refer to similar technologies, and will not be described in detail here.

[0100] In addition, the application also provides the application of the above-mentioned solid oxide fuel cell stack system, for example, it can be used for power supply, specifically, it can be applied to the solid oxide fuel cell power supply using hydrocarbon fuel as a reducing agent.

[0101] In summary, the solid oxide fuel cell stack system provided by the application adopts an indirect internal reforming method, which avoids the carbon deposition on the anode 21 causing the structural damage and performance degradation of the cell, and the power and temperature signals are used to control the gas together to realize the efficient heat management of the cell stack, which can improve the service life and efficiency of the cell stack system.

[0102] The above are merely preferred embodiments of the present invention and are not intended to limit the present invention. Those skilled in the art will readily appreciate that various modifications and variations of the present invention are possible. Any modifications, equivalent substitutions, or improvements made within the spirit and principles of the present invention shall be included within the scope of protection of the present invention.

Claims

1. A solid oxide fuel cell stack system, characterized in that: Including battery stack body, temperature detection module, power detection module, load and control module; The battery stack body is formed by stacking a plurality of battery bodies in sequence; each of the battery bodies includes a single battery and a connector weight adjustment plate; the connector weight adjustment plate includes a connector body, the upper and lower surfaces of the connector body are respectively provided with a battery support porous area and an oxidation flow channel, the lower surface of the battery support porous area is provided with a reforming synthesis flow channel, a reforming porous area for providing a catalytic reaction for the reformed fuel is provided between the reforming synthesis flow channel and the oxidation flow channel, and the reforming porous area is separated from the reforming synthesis flow channel and the oxidation flow channel by a leak-proof wall to achieve self-sealing of the reformed fuel; the single battery includes an anode, an electrolyte and a cathode arranged in sequence, and the anode, the electrolyte and the cathode are arranged in sequence on the side of the battery support porous area away from the reforming synthesis flow channel; The power detection module is used to detect the power required by the total load in the circuit and feed it back to the control module; The temperature detection module is used to detect the gas temperature at least at the inlet of a part of the flow channel and feed it back to the control module; The control module is used to receive the real-time operation signal data of the battery stack body fed back by the temperature detection module and the power detection module, and output relevant signals including control signals for each reaction gas flow after iteratively processing the load power and gas temperature signal data at the gas path monitoring point, and control the introduction of each reaction gas; The temperature detection module is connected to at least one of the following gas paths in each battery body: Gas path 1: air path entering the cathode; Gas path 2: gas path for the reformed mixed gas entering the reforming porous zone; Gas path three: a gas outlet path for the synthesis gas flowing out of the reforming porous zone; The solid oxide fuel cell stack system further includes a heat exchanger connected to at least one of the gas path 1 and the gas path 2 in each of the cell bodies for preheating at least a portion of the initial gas entering the corresponding flow channel; The initial raw materials entering gas path 1 include air, and the initial raw materials entering gas path 2 include water vapor, nitrogen and hydrocarbon fuel; The solid oxide fuel cell stack system also includes a burner, the inlet of which is connected to the cathode oxidizing gas outlet and the anode reforming synthesis gas outlet in each cell body for collecting the reaction tail gas discharged from the cell stack body and performing catalytic reaction combustion.

2. The solid oxide fuel cell stack system according to claim 1, characterized in that: The solid oxide fuel cell stack system further includes a DC / AC voltage conversion device, which is connected to the cell stack body, the power detection module and the load at the same time.

3. The solid oxide fuel cell stack system according to claim 1, characterized in that: At least part of the gas path is provided with a gas flow meter, which is signal-connected to the control module so that the gas flow control instructions output by the control module to the gas flow meter control the introduction of each reaction gas.

4. The solid oxide fuel cell stack system according to claim 1, characterized in that: The inlet of the burner is also connected to the hydrocarbon fuel outlet of the heat exchanger so as to introduce part of the preheated hydrocarbon fuel gas into the burner for catalytic reaction and combustion.

5. The solid oxide fuel cell stack system according to claim 4, characterized in that: The outlet of the burner is also connected to the inlet of the heat exchanger so that the high-temperature gas generated after the catalytic reaction and combustion can be introduced into the heat exchanger.

6. An operation control method for a solid oxide fuel cell stack system according to any one of claims 1 to 5, characterized in that: The following steps are involved: The power detection module is used to detect the power required by the total load in the circuit and feed it back to the control module; Using a temperature detection module to detect the gas temperature at at least part of the flow channel inlet and feeding it back to the control module; After receiving the real-time operation signal data of the battery stack body fed back by the temperature detection module and the power detection module, the control module performs iterative calculations on the power and gas temperature signal data, outputs relevant control signals including the flow rate of each reaction gas, and controls the introduction of each reaction gas.

7. An application of the solid oxide fuel cell stack system according to any one of claims 1 to 5, characterized in that: The solid oxide fuel cell stack system is used for powering electricity.

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