A thermal mass cycle fuel cell power generation system and a control method thereof

Abstract

The application discloses a thermal mass cycle fuel cell power generation system and a control method thereof. The system comprises a methanol supply assembly, an air supply assembly, a pure water supply assembly, a catalytic combustor, a methanol steam reformer, an adjusting assembly, a fuel distributor a, a fuel distributor b, a heat exchanger a, a heat exchanger b, a heat exchanger c, a heat exchanger d, a mixing valve a, a mixing valve b and a fuel cell. Through the realization of the internal thermal mass cycle of the system, the internal cycle of the system is constructed, which comprises methanol catalytic exothermic, methanol steam reforming dehydrogenation, hydrogen reaction power supply and hydrogen catalytic exothermic. The heat generated by the catalytic combustor and the heat after the hydrogen reaction of the fuel cell are used as the heat source for starting together, the starting speed of the system is improved, the system is continuously optimized through the continuous correction of the thermal mass cycle process of the system, the low-power self-sustaining point of the system is found, the net efficiency of the system is improved, and the excessive hydrogen at the anode outlet of the fuel cell is reused for catalytic combustion, the methanol hydrogen dual-fuel combustion is realized, and the heat transfer amount is improved.

Description

Technical Field

[0001] This invention relates to a fuel cell power generation system and its control method, and in particular to a thermo-mass cycle fuel cell power generation system and its control method, belonging to the field of fuel cell technology. Background Technology

[0002] With profound changes in the energy structure—traditional high-carbon and multi-carbon fossil fuels have been gradually reduced, and new low-carbon or even carbon-free fuels have quietly emerged. Against this backdrop, fuel cells, as an emerging power generation technology, have made significant progress in recent years. However, the secondary energy source they use—hydrogen—faces problems in storage, transportation, and utilization, which limit the further development of fuel cells.

[0003] Methanol steam reforming hydrogen production technology is an ideal mobile hydrogen source due to its advantages of low cost, wide availability, mild conditions, and high hydrogen production capacity, and has been widely used in industry. Therefore, integrating methanol steam reforming hydrogen production technology with high-temperature proton exchange membrane fuel cell power generation systems is one of the important future directions.

[0004] Both methanol vapor reforming for hydrogen production and high-temperature proton exchange membrane fuel cells require significant heat during startup. Current technologies use heating rods to provide this heat, but the peak power of these heating rods can reach 4-5 times the system output power, leading to substantial energy loss and hindering rapid startup. If methanol catalytic combustion heating is used, only methanol catalytic combustion provides heating, resulting in a slow heating rate. Furthermore, the anode exhaust gas of the fuel cell is not reused, leading to energy consumption. The lack of multi-stage utilization of catalytic combustion exhaust gas results in insufficient system thermal efficiency, further extending startup time.

[0005] When the system is in standby mode, its standby state determines its external output capacity. For methanol vapor reforming fuel cell power generation system, its standby self-sustaining condition is about 60-80% of the rated condition. Therefore, the system net efficiency is less than 20%, and the system's external output capacity is low.

[0006] Furthermore, existing fuel power generation systems have low material and heat utilization rates, resulting in low net system efficiency. In addition, due to the low material utilization rate, more material is required for the same output, leading to higher power consumption of auxiliary components. Therefore, in order to balance the power consumption within the system, the fuel cell needs to output more power to maintain the internal power consumption of the system, which requires more hydrogen or air. As a result, the power consumption of auxiliary components will still increase. Moreover, since the power required by the fuel cell to maintain the internal operation of the system has increased, the ability to output power externally has weakened. However, thanks to the high calorific value of hydrogen, the power consumption of the system will not increase indefinitely. Instead, there is a balance point between the hydrogen consumed by the fuel cell and the power consumption of auxiliary components. This balance point is the power self-sufficiency point of the system. However, a higher self-sufficiency point requires a longer time for the system's heat and material to meet the usage requirements, resulting in a slow start-up time and high power consumption. Summary of the Invention

[0007] Purpose of the invention: To address the shortcomings of existing technologies, this invention provides a thermo-mass cycle fuel cell power generation system and its control method. By using a thermo-mass cycle, this invention improves the net efficiency of the fuel cell power generation system and achieves the goals of low-energy standby mode and rapid start-up.

[0008] Technical solution: A thermo-mass cycle fuel cell power generation system, comprising a methanol supply component, an air supply component, a pure water supply component, a catalytic burner, a methanol vapor reformer, a regulating component, a fuel distributor a, a fuel distributor b, a heat exchanger a, a heat exchanger b, a heat exchanger c, a heat exchanger d, a mixing valve a, a mixing valve b, and a fuel cell.

[0009] The methanol supply component and air supply component respectively deliver methanol and air to heat exchanger a and heat exchanger b through fuel distributor a and fuel distributor b for preheating, and then deliver them to catalytic combustor for catalytic combustion reaction. The generated high-temperature gas enters heat exchanger a, heat exchanger b and heat exchanger c in sequence, and the remaining gas is discharged from the system.

[0010] The methanol supply component delivers methanol through fuel distributor a, and delivers methanol and pure water delivered by pure water supply component to mixing valve b for mixing. After passing through heat exchanger c, it enters methanol vapor reformer for methanol vapor reforming reaction. The generated hydrogen enters regulating component through heat exchanger d. Regulating component is connected to fuel cell anode inlet, and fuel cell anode outlet is connected to mixing valve a.

[0011] The air supply component transports air to the fuel cell cathode inlet via the fuel distributor b, and after the reaction, it is returned to the air supply component from the fuel cell cathode outlet.

[0012] This invention combines fuel distributor a and fuel distributor b with a regulating component to achieve the recycling of heat and matter between the catalytic burner, methanol steam reformer and fuel cell. It designs heat exchangers a, b, c and d for multi-stage heat energy utilization, enabling the system to have higher net efficiency, low power consumption operation mode, and rapid start-up. It can also reuse exhaust gas and improve exhaust gas utilization rate.

[0013] In a preferred embodiment, to improve the system's net efficiency, the regulating component includes a gas pump, a check valve, a gas storage tank, and an electrically controlled needle valve connected in sequence. The gas pump is connected to heat exchanger d, and the electrically controlled needle valve is connected to the anode inlet of the fuel cell. The regulating component cools the high-temperature reformed gas generated by the methanol reformer via heat exchanger d, then sequentially passes it through the gas pump and check valve to the condensate storage tank. Here, condensation removes methanol and H2O, products detrimental to fuel cell operation. The condensed dry gas is connected to the fuel cell anode via the electromagnetic needle valve. Excess fuel generated after power generation enters mixing valve a and then into the catalytic burner to provide heat to the system. A pressure difference is created through the coordinated action of the gas pump and the electrically controlled needle valve to achieve hydrogen storage. The gas pump flow rate should be less than the hydrogen production rate to avoid excessively low back pressure leading to a low single-pass conversion rate in the reformer. A check valve is also provided to prevent gas backflow. The regulating component converts heat loss due to operating condition adjustments in the thermo-mass cycle into mass stored in the gas storage tank, improving the effectiveness of the thermo-mass cycle and the system's net efficiency.

[0014] In a preferred embodiment, for supplying methanol and controlling the amount of methanol, the methanol supply assembly includes a methanol tank, a methanol pump, and a methanol flow meter connected in sequence.

[0015] In a preferred embodiment, the air supply assembly includes an air supply box and an air compressor connected in sequence to provide air.

[0016] In a preferred embodiment, in order to provide pure water and control the amount of pure water, the pure water supply assembly includes a pure water tank, a pure water pump, and a pure water flow meter connected in sequence.

[0017] A control method for a thermo-mass cycle fuel cell power generation system includes the following steps:

[0018] S1: The system operates in standby mode and fast start mode. The system is in standby mode if there is no external load or if the power of the external load is constant. If there is no external load or the power of the external load is constant, the system is in standby mode and proceeds to S2. If the system is in a stopped state, it proceeds to fast start mode and proceeds to S3.

[0019] S2: By controlling the thermo-mass cycle of the system, the system power consumption in standby mode is minimized;

[0020] S21: Determine the temperature T of the methanol vapor reformer 重整 and fuel cell temperature T 电池 Is it within the normal operating temperature range? If it is within the normal operating temperature range, proceed to S22; otherwise, proceed to S23.

[0021] S22: Determine whether the hydrogen in the gas storage tank is full based on the pressure in the gas storage tank. If it is full, the system is determined to have excess mass; if it is not full, the system is determined to have a mass deficit. After correction and adjustment, proceed to S23.

[0022] S23: Determine the temperature value T of the methanol steam reformer 重整 Or the fuel cell temperature value T 电池 If the temperature is below the normal operating temperature range, the system is determined to have a heat loss. After correction and adjustment, return to S21; otherwise, proceed to S24.

[0023] S24: Determine the temperature value T of the methanol steam reformer 重整 Or the fuel cell temperature value T 电池 If the temperature exceeds the normal operating temperature range, the system is deemed to have excessive heat. After adjustment, the system returns to S21; otherwise, the system returns to S22.

[0024] S3: Control system quick start:

[0025] S31: Select the corresponding rapid heating method based on whether the pressure value in the gas storage tank has reached the pressure value that can be started. If the pressure value for starting has not been reached, select to activate the first rapid heating method. If the pressure value for starting has been reached, select to activate the second rapid heating method and proceed to S32.

[0026] S32: Determine the temperature T of the methanol vapor reformer 重整 and fuel cell temperature T 电池 Is it within the normal operating temperature range? If yes, proceed to S33; otherwise, proceed to S34.

[0027] S33: Fuel distributors a and b distribute the proportion of methanol and the proportion of pure water according to the corresponding fast start method selected in S31, and ensure that the pure water pump and the electronically controlled needle valve are always open. The output power of the fuel cell is greater than or equal to the internal power consumption of the system, which means that the system has started successfully.

[0028] S34: Determine the fuel cell temperature T 电池 Does it precede the methanol vapor reformer temperature T? 重整 If the normal operating temperature range is reached, the air supply to the cathode of the fuel cell is increased through fuel cell b to control the temperature of the fuel cell before returning to S32; otherwise, it proceeds to S35.

[0029] S35: Determining the temperature T of the methanol vapor reformer重整 Does it precede the fuel cell temperature T? 电池 If the normal operating temperature range is reached, the proportion of methanol used for methanol vapor reforming is increased through fuel distributor a, and the pure water pump and electronic needle valve are turned on. Excess heat is absorbed through methanol vapor reforming, and excess hydrogen is stored in the gas storage tank. At the same time, a small amount of hydrogen is introduced into the anode of the fuel cell to accelerate the start-up time of the fuel cell, and then the process returns to S32; otherwise, the process returns to S31.

[0030] This invention aims to ensure that the methanol steam reformer and catalytic burner remain within their normal operating temperature range and output power. By adjusting the power consumption of each auxiliary component, the minimum power consumption is continuously sought. To ensure a sufficiently large minimum power consumption optimization range, the hydrogen in the storage tank can be adjusted to minimize material loss during the optimization process. That is, regardless of whether the system is currently in a state of heat surplus or deficit, or mass excess or deficit, heat and mass can be regulated through the coupling of the catalytic combustion reaction and the reforming reaction. The result of the regulation is the change in the amount of reforming product hydrogen. In standby mode, the amount of hydrogen required by the fuel cell under the current load power is constant. Therefore, the storage tank also plays a role in collecting and releasing hydrogen, which can buffer and utilize the heat and mass losses caused by the system during the heat and mass cycle regulation process. In the fast start-up mode, the hydrogen stored in the gas tank can be used for catalytic combustion and heat release during the start-up process. When the fuel cell has not reached its operating temperature, the hydrogen does not react or reacts very weakly when passing through the anode of the fuel cell. Therefore, the hydrogen in the gas tank flows through the fuel cell with almost no loss and is sent to the catalytic burner. At the same time, methanol also participates in the catalytic combustion. Due to the high calorific value and fast reaction kinetics of hydrogen, the reaction rate is accelerated and the heat transfer rate is also faster. Therefore, the start-up time of the system is greatly shortened.

[0031] Preferably, to ensure the quality cycle of the system, the specific steps for correcting and adjusting the quality cycle of the system in S22 are as follows: ensuring the methanol reformer temperature value T. 重整 and fuel cell temperature T 电池 Within the normal operating temperature range, while meeting the fuel requirements of the fuel cell at the anode and cathode, the system is corrected and adjusted to address any excess or deficiency of mass in the system.

[0032] When the hydrogen storage tank is full, the system experiences a methanol excess. The methanol pump reduces the methanol supply, and fuel distributor a reduces the proportion of methanol used for methanol vapor reforming. To maintain the methanol-to-water ratio, the pure water pump reduces the pure water supply. Therefore, the methanol pump power consumption P... MEOH Reduce the power consumption P of the pure water pump H2O Reduce air pump power consumption P AIRThe power demand of the fuel cell decreases as the system's energy consumption decreases. When the hydrogen storage tank is not full, the system experiences a quality deficit. The methanol supply is increased by the methanol pump, and the proportion of methanol used for methanol steam reforming is increased by controlling the fuel distributor a. To ensure the methanol-water ratio, the pure water supply is increased by the pure water pump. When the amount of hydrogen in the storage tank is in dynamic equilibrium, that is, when the hydrogen pressure in the storage tank remains constant, the system reaches its minimum power consumption when in standby mode, and the output power W of the fuel cell still meets the total output power of the system in real time.

[0033] Preferably, to ensure the thermal cycle of the system, the specific steps for correcting and adjusting the system thermal cycle in S23 and S24 are as follows: ensuring the methanol reformer temperature value T. 重整 and fuel cell temperature T 电池 Within the normal operating temperature range, adjustments are made to correct for heat loss or heat excess in the system.

[0034] When the temperature of the methanol vapor reformer is T 重整 Or the fuel cell temperature value T 电池 When the temperature is below the normal operating temperature range, the system is in heat loss. The methanol supply to the system is increased by the methanol pump, the proportion of methanol used for catalytic combustion is increased by controlling the fuel distributor a, and hydrogen is released from the storage tank through the electronically controlled needle valve to increase the amount of fuel cell anode exhaust gas used for catalytic combustion and quickly replenish the heat.

[0035] When the temperature of the methanol vapor reformer is T 重整 Or the fuel cell temperature value T 电池 When the temperature exceeds the normal operating temperature range, the system experiences thermal interference. The fuel distributor A is controlled to reduce the proportion of methanol used for catalytic combustion and increase the proportion of methanol used for methanol steam reforming. At the same time, excess hydrogen is stored in the storage tank through the electronically controlled needle valve, and the hydrogen and air supply to the fuel cell are reduced.

[0036] In a preferred embodiment, in order to adopt different heating methods for different amounts of hydrogen in the gas storage tank, the first rapid heating method in S31 is to mainly use the heat released by the catalytic combustion of methanol for heating. Fuel distributor a does not supply methanol to the methanol reformer, and all methanol is used for catalytic combustion. At the same time, the pure water pump does not work, and fuel distributor b does not supply air to the fuel cell. All air is used for catalytic combustion. That is, the proportion of methanol and air used for catalytic combustion is adjusted to 1 by controlling fuel distributor a and fuel distributor b. The heat generated by the catalytic burner is sequentially vaporized by heat exchanger a, heated by heat exchanger b, vaporized by methanol water by heat exchanger c, and then discharged from the system. In this process, heat convection and heat conduction work together to raise the temperature of other components.

[0037] The second rapid heating method involves heating primarily through the exothermic combustion of methanol and the exothermic combustion of fuel cell exhaust gas. Hydrogen gas in the storage tank is depressurized to the anode inlet of the fuel cell via an electronically controlled needle valve. All exhaust gas discharged after passing through the anode outlet of the fuel cell is used for catalytic combustion exothermic combustion. Specifically, the fuel distributor a is controlled to adjust the proportion of methanol used for catalytic combustion to 1. At this time, the pure water pump is not working, and the electronically controlled needle valve is opened.

[0038] Preferably, in order to perform low-power system calculations, the calculation method for the correction and adjustment of the thermo-mass cycle is as follows:

[0039] To calculate the internal power consumption of the system, the output power of the fuel cell stack should meet the following requirements:

[0040] W = (P MEOH +P H2O +P AIR +P PCB ) / τ;

[0041] Among them, P MEOH For methanol pump power, P H2O For pure water pump power, P AIR For air pump power, P PCB Let τ be the system power consumption and τ be the DC-DC conversion efficiency.

[0042] To determine the initial fuel cell output power, the feed requirements are calculated based on the stack power demand:

[0043] Hydrogen consumption per hour V H2 :

[0044]

[0045] Where P is the stack output power, t is time, U0 is the single cell design voltage, e is the number of electrons, and ρ is the total output power. H2 Let λ be the density of hydrogen gas. H2 The excess coefficient of hydrogen;

[0046] Methanol consumption per hour V MEOH :

[0047]

[0048] Where P is the stack output power, t is time, U0 is the single cell design voltage, e is the number of electrons, and M is the total output power. H2 λ is the molar mass of hydrogen. H2 λ is the excess hydrogen coefficient. stio The stoichiometric ratio of 1 mole of methanol to water to produce x moles of hydrogen, where η is the methanol conversion rate, and M is the stoichiometric ratio. MEOH ρ is the molar mass of methanol. MEOHWhere is the density of methanol, and μ is the proportion of methanol used for steam reforming;

[0049] Pure water consumption per hour V H2O :

[0050]

[0051] Where P is the stack output power, t is time, U0 is the single cell design voltage, e is the number of electrons, and M is the total output power. H2 λ is the molar mass of hydrogen. H2 λ is the excess hydrogen coefficient. stio η is the stoichiometric ratio of 1 mole of methanol to x moles of hydrogen produced from 1 mole of methanol-water, μ is the methanol conversion rate, μ is the proportion of methanol used for steam reforming, and γ is the water-to-methanol ratio.

[0052] Air consumption per hour V AIR :

[0053]

[0054] Where P is the stack output power, t is time, U0 is the single cell design voltage, e is the number of electrons, and ρ is the total output power. O2 M is the density of oxygen. O2 λ represents the mass fraction of oxygen. O2 For the excess oxygen stoichiometry of a fuel cell, V MEOH ρ is the hourly methanol consumption, μ is the proportion of methanol used for steam reforming, and ρ is the methanol consumption per hour. MEOH M is the density of methanol. MEOH V is the molar mass of methanol. H2 λ represents the hourly consumption of hydrogen. H2 ρ is the excess coefficient of hydrogen. H2 M is the density of hydrogen gas. H2 This refers to the molar mass of hydrogen gas.

[0055] The power consumption is adjusted and corrected based on the feed demand. By determining the relationship between feed demand and power consumption, the system can calculate the current internal energy consumption in real time during the thermo-mass cycle adjustment process.

[0056] Methanol pump power P MEOH :

[0057]

[0058] Among them, V MEOH k represents the hourly consumption of methanol. p I is the coefficient relating fuel pump flow rate to voltage. MEOH This refers to the methanol pump current.

[0059] pure water pump power P H2O :

[0060]

[0061] Among them, V H2O k is the hourly consumption of pure water. p I is the coefficient relating fuel pump flow rate to voltage. H2O This refers to the current of the pure water pump.

[0062] Air pump power P AIR :

[0063]

[0064] Among them, V AIR k is the amount of air consumed per hour. a I is the coefficient relating air pump flow rate to voltage. AIR This refers to the air pump current.

[0065] Control system power consumption P PCB :

[0066] P PCB =I PCB *U PCB

[0067] Among them, I PCB For controller current, U PCB This is the controller voltage.

[0068] Beneficial effects: This invention achieves the recycling of heat and mass within the power generation system, constructing an internal system cycle of methanol catalytic exothermic reaction – methanol steam reforming dehydrogenation – hydrogen reaction power generation – hydrogen catalytic exothermic reaction. The heat generated by the catalytic burner and the heat from the hydrogen reaction in the fuel cell are used together as the start-up heat source, improving the system's start-up speed. Furthermore, through continuous modification of the system's thermo-mass cycle process, the system continuously optimizes itself, finding a low-power self-sustaining point and improving net efficiency. Simultaneously, the heat from the exhaust gas from the catalytic burner is utilized in multiple stages, and excess hydrogen from the fuel cell anode outlet is reused for catalytic combustion, achieving methanol-hydrogen dual-fuel combustion and improving heat transfer. Attached Figure Description

[0069] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on the provided drawings without creative effort.

[0070] Figure 1 This is a schematic diagram of the structure of the present invention;

[0071] Figure 2 This is the overall flowchart of the present invention;

[0072] Figure 3 This is a flowchart of the standby mode low power consumption control of the present invention;

[0073] Figure 4 This is a flowchart of the fast start mode control of the present invention;

[0074] Figure 5 This is a flowchart illustrating the specific control process for low power consumption in standby mode according to the present invention.

[0075] Figure 6 This is a flowchart illustrating the specific control process of the fast startup mode of the present invention. Detailed Implementation

[0076] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0077] In the description of this invention, it should be understood that the terms "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0078] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can include direct contact between the first and second features, or contact between the first and second features through another feature between them. Furthermore, "above," "over," and "on top" of the second feature includes the first feature directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature includes the first feature directly below or diagonally below the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature.

[0079] like Figure 1As shown, a thermo-mass cycle fuel cell power generation system includes a methanol supply component 1, an air supply component 2, a pure water supply component 3, a catalytic combustor 4, a methanol vapor reformer 5, a regulating component 6, a fuel distributor a7, a fuel distributor b8, a heat exchanger a9, a heat exchanger b10, a heat exchanger c11, a heat exchanger d12, a mixing valve a13, a mixing valve b14, and a fuel cell 15.

[0080] The methanol supply component 1 and the air supply component 2 respectively deliver methanol and air to heat exchangers a9 and b10 for preheating via fuel distributors a7 and b8, and then deliver them to catalytic combustor 4 for catalytic combustion reaction. The generated high-temperature gas enters heat exchangers a9, b10 and c11 in sequence, and the remaining gas is discharged from the system.

[0081] The methanol supply component 1 delivers methanol through the fuel distributor a7, and delivers methanol and pure water delivered by the pure water supply component 3 to the mixing valve b14 for mixing. After passing through the heat exchanger c11, it enters the methanol vapor reformer 5 for methanol vapor reforming reaction. The generated hydrogen enters the regulating component 6 through the heat exchanger d12. The regulating component 6 is connected to the anode inlet of the fuel cell 15, and the anode outlet of the fuel cell 15 is connected to the mixing valve a13.

[0082] The air supply component 2 transports air to the cathode inlet of the fuel cell 15 via the fuel distributor b8, and after the reaction, it is returned to the air supply component 2 from the cathode outlet of the fuel cell 15.

[0083] By combining fuel distributor a and fuel distributor b with regulating components, the heat and material recycling between the catalytic burner, methanol steam reformer and fuel cell is realized. Heat exchangers a, b, c and d with multi-stage thermal energy utilization are designed to enable the system to have higher net efficiency, low power consumption operation mode, and can achieve rapid start-up. It can also reuse exhaust gas and improve exhaust gas utilization rate.

[0084] To improve the net efficiency of the system, the regulating component 6 includes an air pump 61, a check valve 62, an air storage tank 63, and an electrically controlled needle valve 64 connected in sequence. The air pump 61 is connected to the heat exchanger d12, and the electrically controlled needle valve 64 is connected to the anode inlet of the fuel cell 15. The regulating component 6 cools the high-temperature reformed gas generated by the methanol vapor reformer 5 through the heat exchanger d12, and then passes it sequentially through the gas pump 61 and check valve 62 to reach the condensate storage tank 63. Here, condensation is carried out to remove methanol, H2O, and other byproducts that are detrimental to the operation of the fuel cell 15. The condensed dry gas is connected to the anode of the fuel cell 15 through the electronically controlled needle valve 64. Excess fuel generated after power generation enters the mixing valve a13 and then enters the catalytic burner 4 to provide heat to the system. The gas pump 61 and the electronically controlled needle valve 64 work together to create a pressure difference to achieve hydrogen storage. The flow rate of the gas pump 61 should be less than the hydrogen production rate to avoid low back pressure that would result in a low single-pass conversion rate of the methanol vapor reformer 5. A check valve 62 is also provided to prevent gas backflow. The regulating component 6 converts the heat loss caused by the adjustment of operating conditions in the thermo-mass cycle into physical mass stored in the storage tank 63, thereby improving the function of the thermo-mass cycle and the net efficiency of the system.

[0085] In order to provide methanol and control the amount of methanol, the methanol supply assembly 1 includes a methanol tank 11, a methanol pump 12 and a methanol flow meter 13 connected in sequence.

[0086] To provide air, the air supply assembly 2 includes an air supply box 21 and an air compressor 22 connected in sequence.

[0087] In order to provide pure water and control the amount of pure water, the pure water supply component 3 includes a pure water tank 31, a pure water pump 32, and a pure water flow meter 33 connected in sequence.

[0088] The methanol tank 11 is connected to the methanol pump 12, and the methanol supply is monitored by the methanol flow meter 13. The methanol is distributed according to the ratio at the fuel distributor a7. One path is heated by the heat exchanger a9 and sent to the mixing valve a13. The other path is mixed with pure water supplied by the pure water pump 32 at the mixing valve b14 to form a methanol-water solution. The methanol-water solution is heated and vaporized by the heat exchangers c11 and d12 respectively and then enters the methanol vapor reformer 5. The ratio of the methanol-water solution is controlled by the pure water pump 31 and the methanol pump 12. The air compressor 22 distributes the air entering the fuel distributor b8 according to the ratio. One path is used as cathode fuel for the fuel cell 15. The other path is mixed with methanol for catalytic combustion at the mixing valve a13 after passing through the heat exchanger b10 and then enters the catalytic combustor 4. The fuel cell 15 is a phosphoric acid-doped high-temperature proton exchange membrane fuel cell. Its cathode exhaust gas is condensed and connected to the air compressor 22 to reduce power consumption.

[0089] like Figures 2-6As shown, a control method for a thermo-mass cycle fuel cell power generation system includes the following steps:

[0090] S1: The system operates in standby mode and fast start mode. The system is in standby mode if there is no external load or if the power of the external load is constant. If there is no external load or the power of the external load is constant, the system is in standby mode and proceeds to S2. If the system is in a stopped state, it proceeds to fast start mode and proceeds to S3.

[0091] S2: By controlling the thermo-mass cycle of the system, the system power consumption in standby mode is minimized;

[0092] S21: Determine the temperature T of methanol steam reformer 5 重整 and fuel cell 15 temperature T 电池 Whether it is within the normal operating temperature range; in this embodiment, the temperature T of the methanol vapor reformer 重整 The normal operating temperature range is 220℃ <T 重整 <260℃, fuel cell temperature T 电池 The normal operating temperature range is 120℃ <T 电池 <180℃; if all are within the normal operating temperature range, proceed to S22; otherwise, proceed to S23.

[0093] S22: Determine whether the hydrogen in the gas storage tank 63 is full based on the pressure in the gas storage tank 63. If it is full, the system is determined to have excess mass; if it is not full, the system is determined to have a mass deficit. After correction and adjustment, proceed to S23.

[0094] S23: Determine the temperature value T of methanol steam reformer 5 重整 Or the fuel cell temperature value T15 电池 If the temperature is below the normal operating temperature range, the system is determined to have a heat loss. After correction and adjustment, return to S21; otherwise, proceed to S24.

[0095] That is, determining the temperature T of methanol steam reformer 5. 重整 Is it less than 220℃ or the fuel cell temperature 15T? 电池 Is it less than 120℃? If T 重整 <220℃ or T 电池 If the temperature is less than 120℃, the system is considered to have a heat deficit. After correction and adjustment, the system returns to S21; otherwise, it proceeds to S24.

[0096] S24: Determine the temperature value T of methanol steam reformer 5 重整 Or the fuel cell temperature value T15 电池 If the temperature exceeds the normal operating temperature range, the system is deemed to have excessive heat. After adjustment, the system returns to S21; otherwise, the system returns to S22.

[0097] That is, to determine the temperature T of methanol steam reformer 5. 重整 Is it greater than 260℃ or the fuel cell temperature 15T? 电池 Is it greater than 180℃? If T 重整 >260℃ or T 电池 If the temperature is >180℃, the system is considered to have excessive heat, and after correction and adjustment, it returns to S21; otherwise, it returns to S22.

[0098] S3: Control system quick start:

[0099] S31: Select the corresponding rapid heating method based on whether the pressure value in the gas storage tank 63 has reached the pressure value that can be started. If the pressure value for starting has not been reached, select to start the first rapid heating method. If the pressure value for starting has been reached, select to start the second rapid heating method and proceed to S32.

[0100] S32: Determine the temperature T of methanol steam reformer 5 重整 and fuel cell 15 temperature T 电池 Is it within the normal operating temperature range? If yes, proceed to S33; otherwise, proceed to S34.

[0101] S33: Fuel distributors a7 and b distribute the proportion of methanol and the proportion of pure water according to the corresponding fast start method selected in S31, and ensure that the pure water pump 32 and the electronically controlled needle valve 64 are normally open. The output power of fuel cell 15 is greater than or equal to the internal power consumption of the system, which means that the system has started successfully.

[0102] S34: Determine the temperature T of fuel cell 15 电池 Does it occur before the methanol steam reformer at temperature T5? 重整 If the normal operating temperature range is reached, the air supply to the cathode of fuel cell 15 is increased through fuel cell 15b to control the temperature of fuel cell 15 before returning to S32; otherwise, it enters S35.

[0103] That is, determining the temperature T of methanol steam reformer 5. 重整 Is it less than 220℃ and the fuel cell temperature is 15T? 电池 Is it within the normal operating temperature range? If T 重整 <220℃ and 220℃ <T 电池 If the temperature is less than 260°C, the amount of air supplied to the cathode of fuel cell 15 is increased through fuel cell 15b to control the temperature of fuel cell 15 before returning to S32; otherwise, it enters S35.

[0104] S35: Determine the temperature T of methanol steam reformer 5 重整 Does it occur before the fuel cell reaches a temperature of 15°C? 电池If the normal operating temperature range is reached, the proportion of methanol used for methanol vapor reforming is increased through fuel distributor a7, and pure water pump 32 and electronic needle valve 64 are turned on. Excess heat is absorbed through methanol vapor reforming, and excess hydrogen is stored in gas storage tank 63. At the same time, a small amount of hydrogen is introduced into the anode of fuel cell 15 to accelerate the start-up time of fuel cell 15, and then the process returns to S32; otherwise, the process returns to S31.

[0105] That is, determining the temperature T of methanol steam reformer 5. 重整 Is it within the normal operating temperature range and the fuel cell temperature is 15T? 电池 Is it less than 120℃? If it is 220℃ <T 重整 <260℃ and T 电池 If the temperature is below 120°C, the proportion of methanol used for methanol vapor reforming is increased through fuel distributor a7, and pure water pump 32 and electronic needle valve 64 are turned on. Excess heat is absorbed through methanol vapor reforming, and excess hydrogen is stored in gas storage tank 63. At the same time, a small amount of hydrogen is introduced into the anode of fuel cell 15 to accelerate the start-up time of fuel cell 15, and then the process returns to S32; otherwise, the process returns to S31.

[0106] By ensuring that the methanol steam reformer and catalytic burner remain within their normal operating temperature range and output power, the minimum power consumption is continuously sought by adjusting the power consumption of each auxiliary component. To ensure a sufficiently large minimum power consumption optimization range, the hydrogen in the storage tank can be adjusted to minimize material loss during the optimization process. That is, regardless of whether the system is currently in a state of heat surplus or deficit, or mass excess or deficit, heat and mass can be regulated through the coupling of the catalytic combustion reaction and the reforming reaction. The result of the regulation is the change in the amount of reforming product hydrogen. In standby mode, the amount of hydrogen required by the fuel cell under the current load power is constant. Therefore, the storage tank also plays a role in collecting and releasing hydrogen, which can buffer and utilize the heat and mass losses caused by the system during the heat and mass cycle regulation process. In the fast start-up mode, the hydrogen stored in the gas tank can be used for catalytic combustion and heat release during the start-up process. When the fuel cell has not reached its operating temperature, the hydrogen does not react or reacts very weakly when passing through the anode of the fuel cell. Therefore, the hydrogen in the gas tank flows through the fuel cell with almost no loss and is sent to the catalytic burner. At the same time, methanol also participates in the catalytic combustion. Due to the high calorific value and fast reaction kinetics of hydrogen, the reaction rate is accelerated and the heat transfer rate is also faster. Therefore, the start-up time of the system is greatly shortened.

[0107] To ensure the quality cycle of the system, the specific steps for correcting and adjusting the system quality cycle in S22 are as follows: ensuring the methanol reformer temperature value T. 重整 and fuel cell 15 temperature T 电池Within the normal operating temperature range, while meeting the fuel requirements of fuel cell 15 at the anode and cathode, the system is corrected and adjusted to address any excess or deficiency of mass in the system.

[0108] When the hydrogen storage tank 63 is full, the system experiences a hydrogen surplus. The methanol supply is reduced by the methanol pump 12, and the fuel distributor a7 is controlled to reduce the proportion of methanol used for methanol vapor reforming. To maintain the methanol-water ratio, the pure water supply is reduced by the pure water pump 32. Therefore, the power consumption P of the methanol pump 12... MEOH Reduce the power consumption of the pure water pump (32 P). H2O Reduced power consumption of air pump 61 P AIR The power demand of fuel cell 15 decreases as the system's power consumption decreases. When the hydrogen storage tank 63 is not full, the system is in a state of quality loss. The methanol pump 12 increases the methanol supply to the system, and the fuel distributor a7 increases the proportion of methanol used for methanol steam reforming. To ensure the methanol-water ratio, the pure water pump 32 increases the pure water supply. When the hydrogen in the storage tank 63 is in dynamic equilibrium, that is, when the hydrogen pressure in the storage tank 63 remains constant, the system reaches its minimum power consumption when in standby mode, and the output power W of fuel cell 15 still meets the total output power of the system in real time.

[0109] To ensure the system's thermal cycle, the specific steps for correcting and adjusting the system's thermal cycle in S23 and S24 are as follows: ensuring the methanol reformer temperature value T. 重整 and fuel cell 15 temperature T 电池 Within the normal operating temperature range, correct and adjust for heat loss or heat excess in the system;

[0110] When the temperature value T of methanol steam reformer 5 重整 Or the fuel cell temperature value T15 电池 When the temperature is below the normal operating temperature range, the system is in heat loss. The methanol supply is increased by the methanol pump 12, the fuel distributor a7 is controlled to increase the proportion of methanol used for catalytic combustion, and hydrogen is released from the gas storage tank 63 through the electronically controlled needle valve 64 to increase the amount of anode tail gas of the fuel cell 15 used for catalytic combustion and quickly replenish the heat.

[0111] When the temperature value T of methanol steam reformer 5 重整 Or the fuel cell temperature value T15 电池 When the temperature exceeds the normal operating temperature range, the system experiences thermal interference. The fuel distributor a7 is controlled to reduce the proportion of methanol used for catalytic combustion and increase the proportion of methanol used for methanol steam reforming. At the same time, the excess hydrogen is stored in the storage tank 63 through the electronically controlled needle valve 64, and the hydrogen supply and air supply of the fuel cell 15 are reduced.

[0112] In order to adopt different heating methods for different amounts of hydrogen in the gas storage tank, the first rapid heating method in S31 is to mainly use the heat released by the catalytic combustion of methanol for heating. The fuel distributor a7 does not supply methanol to the methanol reformer, and all methanol is used for catalytic combustion. At the same time, the pure water pump 32 does not work, and the fuel distributor b8 does not supply air to the fuel cell 15. All air is used for catalytic combustion. That is, the fuel distributor a7 and the fuel distributor b8 are controlled to adjust the proportion of methanol and air used for catalytic combustion to 1. The heat generated by the catalytic burner 4 passes through heat exchanger a9 to vaporize methanol, through heat exchanger b10 to heat air, and through heat exchanger c11 to vaporize methanol water before being discharged from the system. In this process, heat convection and heat conduction work together to raise the temperature of other components.

[0113] The second rapid heating method involves heating primarily through the exothermic combustion of methanol and the exothermic combustion of the exhaust gas from the fuel cell 15. Hydrogen gas in the gas storage tank 63 is depressurized to the anode inlet of the fuel cell 15 via the electronically controlled needle valve 64. All the exhaust gas discharged after passing through the anode outlet of the fuel cell 15 is used for catalytic combustion exothermic combustion. In other words, the fuel distributor a7 is controlled to adjust the proportion of methanol used for catalytic combustion to 1. At this time, the pure water pump 32 is not working, and the electronically controlled needle valve 64 is opened.

[0114] To perform low-power system calculations, the calculation method for the correction and adjustment of the thermo-mass cycle is as follows:

[0115] To calculate the internal power consumption of the system, the output power of the fuel cell stack 15 should meet the following requirements:

[0116] W = (P MEOH +P H2O +P AIR +PP CB ) / τ;

[0117] Among them, P MEOH For methanol pump 12 power, P H2O For pure water pump 32 power, P AIR For air pump 61 power, P PCB Let τ be the system power consumption and τ be the DC-DC conversion efficiency.

[0118] To determine the initial output power of fuel cell 15, the feed requirements are calculated based on the stack power demand:

[0119] Hydrogen consumption per hour V H2 :

[0120]

[0121] Where P is the stack output power, t is time, U0 is the single cell design voltage, e is the number of electrons, and ρ is the total output power. H2 Let λ be the density of hydrogen gas.H2 The excess coefficient of hydrogen;

[0122] Methanol consumption per hour V MEOH :

[0123]

[0124] Where P is the stack output power, t is time, U0 is the single cell design voltage, e is the number of electrons, and M is the total number of electrons. H2 λ is the molar mass of hydrogen. H2 λ is the excess hydrogen coefficient. stio The stoichiometric ratio of 1 mole of methanol to x moles of hydrogen is given by M, where η is the methanol conversion rate. MEOH ρ is the molar mass of methanol. MEOH Where is the density of methanol, and μ is the proportion of methanol used for steam reforming;

[0125] Pure water consumption per hour V H2O :

[0126]

[0127] Where P is the stack output power, t is time, U0 is the single cell design voltage, e is the number of electrons, and M is the total number of electrons. H2 λ is the molar mass of hydrogen. H2 λ is the excess hydrogen coefficient. stio η is the stoichiometric ratio of 1 mole of methanol to x moles of hydrogen produced from 1 mole of methanol-water, μ is the methanol conversion rate, μ is the proportion of methanol used for steam reforming, and γ is the water-to-methanol ratio.

[0128] Air consumption per hour V AIR :

[0129]

[0130] Where P is the stack output power, t is time, U0 is the single cell design voltage, e is the number of electrons, and ρ is the total output power. O2 M is the density of oxygen. O2 λ represents the mass fraction of oxygen. O2 For fuel cell 15, oxygen excess stoichiometry, V MEOH ρ is the hourly methanol consumption, μ is the proportion of methanol used for steam reforming, and ρ is the methanol consumption. MEOH M is the density of methanol. MEOH V is the molar mass of methanol. H2 λ represents the hourly consumption of hydrogen. H2 ρ is the excess coefficient of hydrogen. H2 M is the density of hydrogen gas. H2 This refers to the molar mass of hydrogen gas.

[0131] The power consumption is adjusted and corrected based on the feed demand. By determining the relationship between feed demand and power consumption, the system can calculate the current internal energy consumption in real time during the thermo-mass cycle adjustment process.

[0132] Methanol pump 12 power P MEOH :

[0133]

[0134] Among them, V MEOH k represents the hourly consumption of methanol. p I is the coefficient relating fuel pump flow rate to voltage. MEOH The current for methanol pump 12;

[0135] Pure water pump 32P H2O :

[0136]

[0137] Among them, V H2O k is the hourly consumption of pure water. p I is the coefficient relating fuel pump flow rate to voltage. H2O The current is 32 for a pure water pump;

[0138] Air pump 61 power P AIR :

[0139]

[0140] Among them, V AIR k is the hourly air consumption. a I is the coefficient relating the flow rate of air pump 61 to voltage. AIR The current is 61 for the air pump;

[0141] Control system power consumption P PCB :

[0142] P PCB =I PCB *U PCB

[0143] Among them, I PCB For controller current, U PCB This refers to the controller voltage.

[0144] The various embodiments in this specification are described in a progressive manner, with each embodiment focusing on its differences from other embodiments. Similar or identical parts between embodiments can be referred to interchangeably. For the apparatus disclosed in the embodiments, since they correspond to the methods disclosed in the embodiments, the description is relatively simple; relevant parts can be referred to the method section.

[0145] The above description of the disclosed embodiments enables those skilled in the art to make or use the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the invention. Therefore, the invention is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A thermo-mass cycle fuel cell power generation system, characterized in that: It includes a methanol supply assembly, an air supply assembly, a pure water supply assembly, a catalytic burner, a methanol vapor reformer, a regulating assembly, a fuel distributor a, a fuel distributor b, a heat exchanger a, a heat exchanger b, a heat exchanger c, a heat exchanger d, a mixing valve a, a mixing valve b, and a fuel cell. The methanol supply component and air supply component respectively deliver methanol and air to heat exchanger a and heat exchanger b through fuel distributor a and fuel distributor b for preheating, and then deliver them to catalytic combustor for catalytic combustion reaction. The generated high-temperature gas enters heat exchanger a, heat exchanger b and heat exchanger c in sequence, and the remaining gas is discharged from the system. The methanol supply component delivers methanol through fuel distributor a, and delivers methanol and pure water delivered by pure water supply component to mixing valve b for mixing. After passing through heat exchanger c, it enters methanol vapor reformer for methanol vapor reforming reaction. The generated hydrogen enters regulating component through heat exchanger d. Regulating component is connected to fuel cell anode inlet, and fuel cell anode outlet is connected to mixing valve a. The air supply component transports air to the fuel cell cathode inlet via the fuel distributor b, and after the reaction, it is returned to the air supply component from the fuel cell cathode outlet. The regulating assembly includes an air pump, a check valve, an air tank, and an electrically controlled needle valve connected in sequence. The air pump is connected to the heat exchanger d, and the electrically controlled needle valve is connected to the anode inlet of the fuel cell. The pure water supply assembly includes a pure water tank, a pure water pump, and a pure water flow meter connected in sequence. It also includes a control method for a thermo-mass cycle fuel cell power generation system, comprising the following steps: S1: The system operates in standby mode and fast start mode. The system is in standby mode if there is no external load or if the power of the external load is constant. If there is no external load or the power of the external load is constant, the system is in standby mode and proceeds to S2. If the system is in a stopped state, it proceeds to fast start mode and then to S3. S2: By controlling the thermo-mass cycle of the system, the system power consumption in standby mode is minimized; S21: Determine the temperature T of the methanol vapor reformer 重整 and fuel cell temperature T 电池 Is it within the normal operating temperature range? If it is within the normal operating temperature range, proceed to S22; otherwise, proceed to S23. S22: Determine whether the hydrogen in the gas storage tank is full based on the pressure in the gas storage tank. If it is full, the system is determined to have excess mass. If it is not full, the system is determined to have a mass deficit. After correction and adjustment, proceed to S23. S23: Determine the temperature value T of the methanol steam reformer. 重整 Or the fuel cell temperature value T 电池 If the temperature is below the normal operating temperature range, the system is determined to have a heat loss. After correction and adjustment, return to S21; otherwise, proceed to S24. S24: Determine the temperature value T of the methanol steam reformer. 重整 Or the fuel cell temperature value T 电池 If the temperature exceeds the normal operating temperature range, the system is deemed to have excessive heat. After adjustment, the system returns to S21; otherwise, the system returns to S22. S3: Control system quick start: S31: Select the corresponding rapid heating method based on whether the pressure value in the gas storage tank has reached the pressure value that can be started. If the pressure value for starting has not been reached, select to activate the first rapid heating method. If the pressure value for starting has been reached, select to activate the second rapid heating method and proceed to S32. S32: Determine the temperature T of the methanol vapor reformer 重整 and fuel cell temperature T 电池 Is it within the normal operating temperature range? If yes, proceed to S33; otherwise, proceed to S34. S33: Fuel distributors a and b distribute the proportion of methanol and the proportion of pure water according to the corresponding fast start method selected in S31, and ensure that the pure water pump and the electronically controlled needle valve are always open. The output power of the fuel cell is greater than or equal to the internal power consumption of the system, which means that the system has started successfully. S34: Determine the fuel cell temperature T 电池 Does it precede the methanol vapor reformer temperature T? 重整 If the normal operating temperature range is reached, the air supply to the cathode of the fuel cell is increased through fuel cell b to control the temperature of the fuel cell before returning to S32; otherwise, it proceeds to S35. S35: Determining the temperature T of the methanol vapor reformer 重整 Does it precede the fuel cell temperature T? 电池 If the normal operating temperature range is reached, the proportion of methanol used for methanol vapor reforming is increased through fuel distributor a, and the pure water pump and electronic needle valve are turned on. Excess heat is absorbed through methanol vapor reforming, and excess hydrogen is stored in the gas storage tank. At the same time, a small amount of hydrogen is introduced into the anode of the fuel cell to accelerate the start-up time of the fuel cell, and then the process returns to S32; otherwise, the process returns to S31.

2. The thermo-mass cycle fuel cell power generation system according to claim 1, characterized in that: The methanol supply assembly includes a methanol tank, a methanol pump, and a methanol flow meter connected in sequence.

3. The thermo-mass cycle fuel cell power generation system according to claim 2, characterized in that: The air supply assembly includes an air supply box and an air compressor connected in sequence.

4. The thermo-mass cycle fuel cell power generation system according to claim 3, characterized in that: The specific steps for correcting and adjusting the system mass circulation as described in S22 are as follows: ensuring the methanol reformer temperature value T. 重整 and fuel cell temperature T 电池 Within the normal operating temperature range, while meeting the fuel requirements of the fuel cell at the anode and cathode, the system is corrected and adjusted to address any excess or deficiency of mass in the system. When the hydrogen storage tank is full, the system experiences a hydrogen surplus. The methanol pump reduces the methanol supply, and fuel distributor A reduces the proportion of methanol used for methanol vapor reforming. To maintain the methanol-to-water ratio, the pure water pump reduces the pure water supply. Therefore, the methanol pump power consumption... Reduce the power consumption of the pure water pump Reduce air pump power consumption The power demand of the fuel cell decreases as the system's energy consumption decreases. When the hydrogen storage tank is not full, the system experiences a quality deficit. The methanol supply is increased by the methanol pump, and the proportion of methanol used for methanol steam reforming is increased by controlling the fuel distributor a. To ensure the methanol-water ratio, the pure water supply is increased by the pure water pump. When the amount of hydrogen in the storage tank is in dynamic equilibrium, that is, when the hydrogen pressure in the storage tank remains constant, the system reaches its minimum power consumption when in standby mode, and the output power W of the fuel cell still meets the total output power of the system in real time.

5. The thermo-mass cycle fuel cell power generation system according to claim 3, characterized in that: The specific steps for correcting and adjusting the system thermal cycle described in S23 and S24 are as follows: ensuring the methanol reformer temperature value T. 重整 and fuel cell temperature T 电池 Within the normal operating temperature range, adjustments are made to correct for heat loss or heat excess in the system. When the temperature of the methanol vapor reformer is T 重整 Or the fuel cell temperature value T 电池 When the temperature is below the normal operating temperature range, the system is in heat loss. The methanol supply to the system is increased by the methanol pump, the proportion of methanol used for catalytic combustion is increased by controlling the fuel distributor a, and hydrogen is released from the storage tank through the electronically controlled needle valve to increase the amount of fuel cell anode exhaust gas used for catalytic combustion and quickly replenish the heat. When the temperature of the methanol vapor reformer is T 重整 Or the fuel cell temperature value T 电池 When the temperature exceeds the normal operating temperature range, the system experiences thermal interference. The fuel distributor A is controlled to reduce the proportion of methanol used for catalytic combustion and increase the proportion of methanol used for methanol steam reforming. At the same time, excess hydrogen is stored in the storage tank through the electronically controlled needle valve, and the hydrogen and air supply to the fuel cell are reduced.

6. The thermo-mass cycle fuel cell power generation system according to claim 3, characterized in that: The first rapid heating method described in S31 is as follows: heating is mainly carried out by the heat released from the catalytic combustion of methanol. Fuel distributor a does not supply methanol to the methanol reformer, and all methanol is used for catalytic combustion. At the same time, the pure water pump does not work, and fuel distributor b does not supply air to the fuel cell. All air is used for catalytic combustion. That is, the proportion of methanol and air used for catalytic combustion is adjusted to 1 by controlling fuel distributor a and fuel distributor b. The heat generated by the catalytic burner is sequentially vaporized by heat exchanger a, heated by heat exchanger b, vaporized by methanol water by heat exchanger c, and then discharged from the system. In this process, heat convection and heat conduction work together to raise the temperature of other components. The second rapid heating method involves heating primarily through the exothermic combustion of methanol and the exothermic combustion of fuel cell exhaust gas. Hydrogen gas in the storage tank is depressurized to the anode inlet of the fuel cell via an electronically controlled needle valve. All exhaust gas discharged after passing through the anode outlet of the fuel cell is used for catalytic combustion exothermic combustion. Specifically, the fuel distributor a is controlled to adjust the proportion of methanol used for catalytic combustion to 1. At this time, the pure water pump is not working, and the electronically controlled needle valve is opened.

7. The thermo-mass cycle fuel cell power generation system according to claim 4 or 5, characterized in that: The calculation method for the correction adjustment of the heat mass cycle is as follows: To calculate the internal power consumption of the system, the output power of the fuel cell stack should meet the following requirements: ； in, , , , , ; To determine the initial fuel cell output power, the feed requirements are calculated based on the stack power demand: Hydrogen consumption per hour : ； in, The output power of the fuel cell stack is t, where t is time. Design voltage for a single cell, For the number of electrons, The density of hydrogen gas, The excess coefficient of hydrogen; Methanol consumption per hour : ； in, The output power of the fuel cell stack is t, where t is time. Design voltage for a single cell, For the number of electrons, The molar mass of hydrogen gas is... The excess hydrogen coefficient, To produce 1 unit mole of methanol-water Stoichiometry of hydrogen per mole For methanol conversion rate, The molar mass of methanol is... The density of methanol, The proportion of methanol used for steam reforming; Pure water consumption per hour : ； in, The output power of the fuel cell stack is t, where t is time. Design voltage for a single cell, For the number of electrons, The molar mass of hydrogen gas is... The excess hydrogen coefficient, To produce 1 unit mole of methanol-water Stoichiometry of hydrogen per mole For methanol conversion rate, The proportion of methanol used for steam reforming. The water-to-alcohol ratio; Air consumption per hour : ； in, The output power of the fuel cell stack is t, where t is time. Design voltage for a single cell, For the number of electrons, Oxygen density, This represents the mass fraction of oxygen. For the excess oxygen stoichiometry of fuel cells, This represents the hourly consumption of methanol. The proportion of methanol used for steam reforming. The density of methanol, The molar mass of methanol is... This represents the hourly consumption of hydrogen. The excess coefficient of hydrogen is denoted as . The density of hydrogen gas, This refers to the molar mass of hydrogen gas. The power consumption is adjusted and corrected based on the feed demand. By determining the relationship between feed demand and power consumption, the system can calculate the current internal energy consumption in real time during the thermo-mass cycle adjustment process. Methanol pump power : ； in, This represents the hourly consumption of methanol. This is the coefficient relating fuel pump flow rate to voltage. This refers to the methanol pump current. Pure water pump function : ； in, This represents the hourly consumption of pure water. This is the coefficient relating fuel pump flow rate to voltage. This refers to the current of the pure water pump. air pump function : ； in, This refers to the hourly air consumption. This is the coefficient relating air pump velocity to voltage. This refers to the air pump current. Control system power consumption : ； in, For controller current, This refers to the controller voltage.

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