Solid-state on-site hydrolysis hydrogen production fuel cell system and water and heat management method thereof

Abstract

The present application relates to the field of fuel cell technology, and in particular to a solid-state on-site hydrolysis hydrogen production fuel cell system and its water and heat management method. The solid-state on-site hydrolysis hydrogen production fuel cell system includes a fuel cell, a hydrogen generator, a first water storage tank, a liquid cooling circulation pipeline, a first heat exchanger, a liquid cooling circulation pump, and a second heat exchanger. During operation, the first heat exchanger can realize refrigeration and cooling of the working medium in the third main pipeline. After the low-temperature working medium in the first sub-pipeline passes through the fuel cell, the fuel cell is cooled. After the second sub-pipeline passes through the second heat exchanger, the water vapor passing through the water vapor recovery pipeline is actively cooled by the second heat exchanger. The solid-state on-site hydrolysis hydrogen production fuel cell system provided in an embodiment of the present invention realizes effective water and heat coupling management. While realizing the cooling of the fuel cell, the water vapor produced by the fuel cell is condensed and recycled to avoid the problem of water loss in the system.

Description

Technical Field

[0001] The present application relates to the field of fuel cell technology, and in particular to a solid-state on-site water splitting hydrogen production fuel cell system and a water heat management method thereof. Background Art

[0002] The increasing global concern for environmental protection and climate change has driven the urgent need for clean energy. Emissions from the combustion of traditional fossil fuels have had a serious impact on the environment and health, so finding alternative energy sources has become a global focus. Hydrogen energy is regarded as an ideal clean energy source because the only byproduct of its combustion is water. However, traditional fuel cell technology relies on the storage and transportation of hydrogen, which increases system complexity and safety risks and limits its widespread application. The solid-state on-site hydrolysis fuel cell system avoids the storage and transportation problems of hydrogen by producing hydrogen in an on-site real-time hydrolysis reaction, while also improving the efficiency and stability of the system. However, extreme environments pose challenges to the hydrothermal management of both solid-state sodium borohydride hydrolysis hydrogen production and proton exchange membrane fuel cell (PEMFC) power generation systems. At the same time, the water vapor or liquid water generated during use needs to be properly managed to reduce the impact on the environment. Therefore, the design of a reasonable and efficient hydrothermal management solution is of great significance to promote the development and application of this new hydrogen energy technology. Summary of the invention

[0003] The present application provides a solid-state on-site water splitting hydrogen production fuel cell system and a water and heat management method thereof to solve the above-mentioned technical problems.

[0004] In a first aspect, the present application provides a solid-state on-site water splitting hydrogen production fuel cell system, the solid-state on-site water splitting hydrogen production fuel cell system comprising:

[0005] A fuel cell comprising an anode, an electrolyte layer and a cathode;

[0006] A hydrogen generator having a hydrogen outlet, a hydrogen recovery inlet and a water inlet, wherein the hydrogen outlet is connected to the anode inlet via a hydrogen supply pipeline, and the anode outlet is connected to the hydrogen recovery inlet via a hydrogen recovery pipeline;

[0007] a first water storage tank, wherein the cathode outlet is connected to the water recovery port of the first water storage tank through a water vapor recovery pipeline, and the water outlet of the first water storage tank is connected to the water inlet through a water supply pipeline;

[0008] a liquid cooling circulation pipeline, comprising a first main pipeline, a second main pipeline, a third main pipeline, a first sub-pipeline and a second sub-pipeline, wherein the first sub-pipeline and the second sub-pipeline are arranged in parallel and are both located between the first main pipeline and the second main pipeline, and the fuel cell is connected in series to the first sub-pipeline;

[0009] A first heat exchanger, wherein a hot end of the first heat exchanger is connected in series to the third main pipe;

[0010] a liquid cooling circulation pump, used for driving the working medium in the liquid cooling circulation pipeline to circulate in the first main pipeline, at least one of the first sub-pipeline and the second sub-pipeline, the second main pipeline, the third main pipeline, and the first main pipeline in sequence;

[0011] A second heat exchanger, wherein a hot end of the second heat exchanger is connected in series to the water vapor recovery pipeline, and a cold end of the second heat exchanger is connected in series to the second sub-pipeline.

[0012] Furthermore, the solid-state on-site hydrolysis hydrogen production fuel cell system also includes a heat pump circulation system, which includes an evaporator, a throttle valve, a condenser and a compressor arranged in series through pipelines, the outlet of the compressor is connected to the inlet of the condenser, the outlet of the condenser is connected to the inlet of the evaporator, the outlet of the evaporator is connected to the inlet of the compressor, the throttle valve is arranged on the pipeline between the evaporator and the condenser, and the cold end of the first heat exchanger is connected in series on the pipeline between the evaporator and the compressor.

[0013] Furthermore, a first control valve is provided on the hydrogen supply pipeline, a tail gas recovery pump is provided on the hydrogen recovery pipeline, and a water supply pump is provided on the water supply pipeline.

[0014] Furthermore, a second control valve is provided on the first sub-pipeline, and a third control valve is provided on the second sub-pipeline.

[0015] Furthermore, the solid-state on-site hydrolysis hydrogen production fuel cell system also includes a second water storage tank, the inlet of the second water storage tank is connected to the outlet of the second main pipeline, and the outlet of the second water storage tank is connected to the inlet of the third main pipeline.

[0016] Furthermore, the solid-state on-site hydrolysis hydrogen production fuel cell system also includes an air input pipeline connected to the inlet of the cathode, and an air supercharger is provided on the air input pipeline.

[0017] Furthermore, the liquid cooling circulation pipeline also includes a third sub-pipeline, the third sub-pipeline is arranged in parallel with the first sub-pipeline and is located between the first main pipeline and the second main pipeline, and the hydrogen generator is connected in series to the third sub-pipeline.

[0018] Furthermore, a fourth control valve is provided on the third sub-pipeline.

[0019] In the second aspect, the present application provides a hydrothermal management method for a solid-state on-site hydrolysis hydrogen production fuel cell system, which is applied to the solid-state on-site hydrolysis hydrogen production fuel cell system provided in the first aspect of the present application. The hydrothermal management method includes a high-temperature working mode hydrothermal management method, and the high-temperature working mode hydrothermal management method includes:

[0020] The first heat exchanger cools down the working medium in the third main pipe;

[0021] The liquid cooling circulation pump drives the working medium to circulate in the liquid cooling circulation pipeline;

[0022] The first sub-pipeline exchanges heat with the fuel cell after being opened;

[0023] After the second sub-pipeline is opened, heat is exchanged between the second heat exchanger and the water vapor recovery pipeline.

[0024] Furthermore, the liquid cooling circulation pipeline also includes a third sub-pipeline, the third sub-pipeline and the first sub-pipeline are arranged in parallel and located between the first main pipeline and the second main pipeline, the hydrogen generator is connected in series to the third sub-pipeline, and sodium borohydride powder is installed inside the hydrogen generator; the high-temperature working mode hydrothermal management method also includes: after the third sub-pipeline is opened, heat is exchanged with the hydrogen generator.

[0025] The above technical solution provided by the embodiment of the present application has the following advantages compared with the prior art: the liquid cooling circulation pipeline is coupled with the first heat exchanger through the liquid cooling circulation pump and the first water storage tank, the inlet of the liquid cooling circulation pump is connected with the third main pipeline, the outlet of the liquid cooling circulation pump is connected with the inlet of the first sub-pipeline and the second sub-pipeline respectively through the first main pipeline, the first sub-pipeline is connected with the second main pipeline after passing through the inside of the fuel cell, and the second sub-pipeline is connected with the second main pipeline after passing through the cold end of the second heat exchanger. The second main pipeline is connected with the third main pipeline, thereby forming the entire liquid cooling circulation system. During operation, the first heat exchanger can realize refrigeration and cooling of the working medium in the third main pipeline, the liquid cooling circulation pump drives the cooled working medium to enter the first sub-pipeline and the second sub-pipeline respectively, the low-temperature working medium in the first sub-pipeline passes through the fuel cell to realize cooling of the fuel cell, and the second sub-pipeline passes through the second heat exchanger, and the water vapor passing through the water vapor recovery pipeline is actively cooled by the second heat exchanger. The solid-state on-site hydrolysis hydrogen production fuel cell system provided in the embodiment of the present invention realizes effective water-heat coupling management. While cooling the fuel cell, the fuel cell product water vapor is condensed and recycled, avoiding the problem of water loss in the system. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the invention and, together with the description, serve to explain the principles of the invention.

[0027] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, for ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative labor.

[0028] One or more embodiments are exemplarily described by pictures in the corresponding drawings, and these exemplified descriptions do not constitute limitations on the embodiments. Elements with the same reference numerals in the drawings represent similar elements, and unless otherwise stated, the figures in the drawings do not constitute proportional limitations.

[0029] Figure 1 A schematic diagram of the structure of a solid-state on-site water splitting hydrogen production fuel cell system provided in an embodiment of the present application.

[0030] In the figure:

[0031] 1. First heat exchanger; 2. Liquid cooling circulation pump; 3. Heat pump circulation system; 301. Evaporator; 302. Throttle valve; 303. Condenser; 304. Compressor; 4. Second control valve; 5. Third control valve; 6. Fourth control valve; 7. First control valve; 8. Fuel cell; 801, anode; 802, electrolyte layer; 803, cathode; 9, pressure sensor; 10, tail gas recovery pump; 11, hydrogen generator; 12, second heat exchanger; 13, air supercharger; 14, preheating device; 15, first water storage tank; 16, water supply pump; 17, second water storage tank; 18, third heat exchanger; 101, liquid cooling circulation pipeline; 101-1, first sub-pipeline; 101-2, second sub-pipeline; 101-3, third sub-pipeline; 101-4, first main pipeline; 101-5, second main pipeline; 101-6, third main pipeline; 102, hydrogen supply pipeline; 103, hydrogen recovery pipeline; 104, water vapor recovery pipeline; 105, water supply pipeline; 106, air input pipeline. DETAILED DESCRIPTION

[0032] In order to make the purpose, technical solution and advantages of the embodiments of the present application clearer, the technical solution in the embodiments of the present application will be clearly and completely described below in conjunction with the drawings in the embodiments of the present application. Obviously, the described embodiments are part of the embodiments of the present application, not all of the embodiments. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of this application.

[0033] The disclosure below provides many different embodiments or examples to implement different structures of the present invention. In order to simplify the disclosure of the present invention, the parts and settings of specific examples are described below. Of course, they are only examples, and the purpose is not to limit the present invention. In addition, the present invention can repeat reference numbers and / or letters in different examples. This repetition is for the purpose of simplification and clarity, and does not itself indicate the relationship between the various embodiments and / or settings discussed.

[0034] like Figure 1 As shown, the main structure of the solid-state on-site hydrolysis hydrogen production fuel cell system disclosed in the embodiment of the present invention includes a fuel cell 8, a hydrogen generator 11, a first water storage tank 15, a liquid cooling circulation pipeline 101, a first heat exchanger 1, a liquid cooling circulation pump 2 and a second heat exchanger 12.

[0035] The fuel cell 8 is selected as a proton exchange membrane fuel cell (PEMFC), which specifically includes an anode 801, an electrolyte layer 802 and a cathode 803 arranged in sequence. The anode 801 of the fuel cell 8 is provided with an inlet for supplying hydrogen and an outlet for discharging hydrogen; the cathode 803 of the fuel cell 8 is provided with an inlet for supplying air and an outlet for discharging water vapor. The hydrogen inlet provided on the anode 801 side of the proton exchange membrane fuel cell (PEMFC) is used to supply hydrogen to the anode 801, and the hydrogen outlet is used to discharge the unreacted hydrogen in the anode 801. The electrolyte layer 802 is located between the anode 801 and the cathode 803, and is used to transfer protons and isolate hydrogen and air. The electrolyte layer 802 is usually composed of a proton exchange membrane (PEM), which has high proton conductivity and good insulation performance. The cathode 803 side of the proton exchange membrane fuel cell (PEMFC) is provided with an air inlet for supplying oxygen or air to the cathode 803, and the outlet on the cathode 803 side is used to discharge the water vapor generated by the cathode 803. During operation of the proton exchange membrane fuel cell (PEMFC), hydrogen is decomposed into protons and electrons at the anode 801, the protons move to the cathode 803 through the electrolyte layer 802, the electrons flow through the external circuit to form an electric current, and the oxygen in the air reacts with the protons and electrons at the cathode 803 to generate water.

[0036] The hydrogen generator 11 has a hydrogen outlet, a hydrogen recovery inlet and a water inlet, wherein the hydrogen outlet is connected to the inlet of the anode 801 via a hydrogen supply pipeline 102, and the outlet of the anode 801 is connected to the hydrogen recovery inlet via a hydrogen recovery pipeline 103. The outlet of the cathode 803 is connected to the water recovery port of the first water storage tank 15 via a water vapor recovery pipeline 104, and the water outlet of the first water storage tank 15 is connected to the water inlet via a water supply pipeline 105. The hydrogen generator 11 is used to generate hydrogen and provide it to the fuel cell 8. The hydrogen outlet of the hydrogen generator 11 is connected to the hydrogen inlet of the anode 801 of the fuel cell 8. The hydrogen recovery inlet of the hydrogen generator 11 is used to receive hydrogen recovery from the anode 801 of the fuel cell 8. The hydrogen recovery pipeline 103 connects the hydrogen outlet of the anode 801 of the fuel cell 8 with the hydrogen recovery inlet of the hydrogen generator 11. The unreacted hydrogen of the anode 801 is recovered to the hydrogen generator 11 through the pipeline for reprocessing or recycling, thereby improving the efficiency of the overall system. The water inlet of the hydrogen generator 11 is used to provide water to the hydrogen generator 11 to generate hydrogen. The hydrogen supply pipeline 102 connects the hydrogen outlet of the hydrogen generator 11 with the hydrogen inlet of the anode 801 of the fuel cell 8 to ensure that hydrogen can smoothly enter the fuel cell 8. The direct connection and recovery system between the hydrogen generator 11 and the fuel cell 8 simplifies the overall system design and reduces the complexity of system components and pipelines.

[0037] The liquid cooling circulation pipeline 101 includes a first main pipeline 101-4, a second main pipeline 101-5, a third main pipeline 101-6, a first sub-pipeline 101-1 and a second sub-pipeline 101-2. The first sub-pipeline 101-1 and the second sub-pipeline 101-2 are arranged in parallel and are both located between the first main pipeline 101-4 and the second main pipeline 101-5. The fuel cell 8 is connected in series to the first sub-pipeline 101-1. The hot end of the first heat exchanger 1 is connected in series to the third main pipeline 101-6. The first heat exchanger 1 can exchange heat with the working medium in the third main pipeline 101-6 to cool the working medium in the third main pipeline 101-6. The liquid cooling circulation pump 2 is used to drive the working medium in the liquid cooling circulation pipeline 101 to circulate in the first main pipeline 101-4, at least one of the first sub-pipeline 101-1 and the second sub-pipeline 101-2, the second main pipeline 101-5, the third main pipeline 101-6, and the first main pipeline 101-4 in sequence. The hot end of the second heat exchanger 12 is connected in series to the water vapor recovery pipeline 104, and the cold end of the second heat exchanger 12 is connected in series to the second sub-pipeline 101-2. The working medium in the second sub-pipeline 101-2 and the fluid in the water vapor recovery pipeline 104 can complete heat exchange through the second heat exchanger 12.

[0038] In the above embodiment, the liquid cooling circulation pipeline 101 is coupled with the first heat exchanger 1 through the liquid cooling circulation pump 2 and the first water storage tank 15, the inlet of the liquid cooling circulation pump 2 is connected with the third main pipeline 101-6, the outlet of the liquid cooling circulation pump 2 is connected with the inlet of the first sub-pipeline 101-1 and the second sub-pipeline 101-2 through the first main pipeline 101-4, the first sub-pipeline 101-1 is connected with the second main pipeline 101-5 after passing through the inside of the fuel cell 8, and the second sub-pipeline 101-2 is connected with the second main pipeline 101-5 after passing through the cold end of the second heat exchanger 12. The second main pipeline 101-5 is connected with the third main pipeline 101-6, thereby forming the entire liquid cooling circulation system. During operation, the first heat exchanger 1 can realize refrigeration and cooling of the working medium in the third main pipeline 101-6, and the liquid cooling circulation pump 2 drives the cooled working medium to enter the first sub-pipeline 101-1 and the second sub-pipeline 101-2 respectively. The low-temperature working medium in the first sub-pipeline 101-1 passes through the fuel cell 8 to cool the fuel cell 8. After the second sub-pipeline 101-2 passes through the second heat exchanger 12, the water vapor passing through the water vapor recovery pipeline 104 is actively cooled by the second heat exchanger 12.

[0039] The solid-state on-site hydrolysis hydrogen production fuel cell system provided in the embodiment of the present invention realizes effective water-heat coupling management. While cooling the fuel cell 8, the product water vapor of the fuel cell 8 is condensed and recycled, avoiding the problem of water loss in the system.

[0040] In some embodiments, the solid-state on-site hydrolysis hydrogen production fuel cell system also includes a heat pump circulation system 3, which includes an evaporator 301, a throttle valve 302, a condenser 303 and a compressor 304 arranged in series through pipelines, the outlet of the compressor 304 is connected to the inlet of the condenser 303, the outlet of the condenser 303 is connected to the inlet of the evaporator 301, the outlet of the evaporator 301 is connected to the inlet of the compressor 304, the throttle valve 302 is arranged on the pipeline between the evaporator 301 and the condenser 303, and the cold end of the first heat exchanger 1 is connected in series on the pipeline between the evaporator 301 and the compressor 304.

[0041] The compressor 304 is used to compress the refrigerant, increase its temperature and pressure, and obtain a high-temperature and high-pressure gaseous refrigerant. The outlet of the compressor 304 is connected to the inlet of the condenser 303. The condenser 303 is used to condense the high-temperature and high-pressure gaseous refrigerant to obtain a high-temperature and high-pressure liquid refrigerant. The outlet of the condenser 303 is connected to the inlet of the evaporator 301. The throttle valve 302 is located on the pipeline between the evaporator 301 and the condenser 303. The throttle valve 302 is used to control the flow rate and pressure of the refrigerant so that it undergoes an appropriate pressure reduction process before entering the evaporator 301 to obtain a low-temperature and low-pressure liquid refrigerant. The evaporator 301 is used to absorb the heat of the surrounding environment to evaporate the low-temperature and low-pressure liquid refrigerant to obtain a low-temperature and low-pressure gaseous refrigerant. The low-temperature and low-pressure gaseous refrigerant completes heat exchange with the first heat exchanger 1 and the working medium in the liquid cooling circulation pipeline 101. On the one hand, it realizes the positive cooling of the working medium in the liquid cooling circulation pipeline 101, enhancing the thermal management effect of the system. On the other hand, it can increase the temperature of the gaseous refrigerant entering the compressor 304. Increasing the suction temperature of the compressor 304 can reduce the power consumption of the compressor 304, making the compressor 304 more efficient in processing gas. The heat pump circulation system 3 works in coordination with the liquid cooling circulation system to optimize thermal management and ensure that the fuel cell 8 operates within the optimal temperature range, thereby improving the energy efficiency of the fuel cell 8 system. The heat pump circulation system 3 can adjust the cooling and heating capacity according to the actual heat load of the system to adapt to different operating conditions, that is, the flexible adjustment capability of the heat pump system can effectively cope with the heat load changes of the fuel cell 8 under different working conditions and improve the operating stability of the system.

[0042] In some embodiments, a first control valve 7 is provided on the hydrogen supply pipeline 102, a tail gas recovery pump 10 is provided on the hydrogen recovery pipeline 103, and a water supply pump 16 is provided on the water supply pipeline 105, so as to further optimize the hydrogen supply, tail gas recovery and water supply control, and ensure the efficient operation of the fuel cell 8 system.

[0043] The hydrogen supply pipeline 102 is used to supply the hydrogen generated by the hydrogen generator 11 to the anode 801 of the fuel cell 8. In order to achieve precise control of the hydrogen supply amount, a first control valve 7 is provided on the hydrogen supply pipeline 102. The first control valve 7 adjusts the flow of hydrogen by monitoring the working state of the fuel cell 8 (such as load, hydrogen demand, etc.), ensuring that a suitable amount of hydrogen is provided under different load conditions, avoiding waste of resources caused by excessive supply or a decrease in battery output power caused by insufficient hydrogen. The first control valve 7 can be connected to the control module of the system. The control module monitors the operating parameters of the fuel cell 8 in real time through sensors, such as voltage, temperature and hydrogen concentration, and adjusts the opening of the first control valve 7 according to the monitoring data to achieve dynamic regulation of hydrogen supply. This precise control can improve the utilization rate of hydrogen and enhance the overall energy efficiency of the system.

[0044] During the operation of the fuel cell 8, part of the hydrogen fails to react completely at the anode 801. In order to improve the utilization rate of hydrogen, the hydrogen recovery pipeline 103 is used to recover these unreacted hydrogen and return them to the hydrogen generator 11 for reprocessing or recycling. To ensure the smooth flow of recovered hydrogen and prevent hydrogen leakage, a tail gas recovery pump 10 is provided on the hydrogen recovery pipeline 103. The tail gas recovery pump 10 can pressurize the recovered unreacted hydrogen to ensure that it can smoothly flow back to the hydrogen generator 11, thereby avoiding the problem of low hydrogen recovery efficiency caused by insufficient air pressure. At the same time, the tail gas recovery pump 10 can also ensure that the recovery process is coordinated with the hydrogen generation and supply process in the system by controlling the recovery flow, further improving the overall efficiency of the system. The tail gas recovery pump 10 can also be connected to the system control module to adjust the operating speed and power of the pump in real time to cope with the hydrogen recovery demand under different working conditions. This automatic adjustment method not only simplifies the operation, but also reduces the energy consumption of the system.

[0045] The hydrogen generator 11 requires water as a reaction raw material, and generates hydrogen through the electrolysis or chemical reaction of water. In order to ensure that the hydrogen generator 11 has sufficient water source, a water supply pump 16 is provided on the water supply pipeline 105. The water supply pump 16 is used to transport the water in the first water storage tank 15 to the hydrogen generator 11, and adjust the water supply according to the operating state of the system. The water supply pump 16 is also connected to the system control module, and the flow rate of the water pump is automatically adjusted by monitoring the water level in the water tank and the hydrogen production of the hydrogen generator 11 to ensure that the hydrogen generator 11 is always in the best water supply state. In order to obtain the pressure of the hydrogen supplied to the anode 801 of the fuel cell 8, a pressure sensor 9 for detecting the pressure at the outlet of the hydrogen generator 11 can be provided on the hydrogen generator 11.

[0046] By providing the first control valve 7 on the hydrogen supply pipeline 102, the tail gas recovery pump 10 on the hydrogen recovery pipeline 103, and the water supply pump 16 on the water supply pipeline 105, the entire fuel cell 8 system realizes the accurate supply and efficient recovery of hydrogen and water. This not only enhances the operating efficiency of the fuel cell 8, but also reduces the waste of hydrogen and water, and prolongs the service life of the system. By means of the above structure, the flow and pressure of various fluids can be accurately controlled, the operation of the system is more stable, the response speed is also faster, and the overall performance and economy of the fuel cell 8 system are further improved.

[0047] In some embodiments, a second control valve 4 is provided on the first sub-pipeline 101-1, and a third control valve 5 is provided on the second sub-pipeline 101-2. The second control valve 4 and the third control valve 5 are provided on the first sub-pipeline 101-1 and the second sub-pipeline 101-2, respectively, for accurately controlling the flow rate of the cooling medium to further improve the thermal management performance of the system.

[0048] The first sub-pipeline 101-1 is responsible for delivering the cooling medium to the fuel cell 8, and ensures that it works within the optimal temperature range by cooling the anode 801 and cathode 803 of the fuel cell 8. In order to accurately adjust the flow of the cooling medium into the fuel cell 8, the second control valve 4 is set on the first sub-pipeline 101-1 in this embodiment. The second control valve 4 can be connected to the system control module, and the control module monitors the operating temperature of the fuel cell 8 in real time through a sensor, and automatically adjusts the opening of the second control valve 4 according to the thermal load of the fuel cell 8, and then dynamically controls the flow of the cooling medium. The second control valve 4 can increase the cooling amount when the fuel cell 8 generates high heat, and reduce the cooling amount under low load conditions, ensuring that the fuel cell 8 maintains a stable operating temperature.

[0049] The second sub-pipeline 101-2 is used to cool the water vapor generated by the cathode 803 of the fuel cell 8, prevent water loss and optimize the recycling of water resources. In order to achieve precise control of water vapor recovery and condensation efficiency under different working conditions, the third control valve 5 is set on the second sub-pipeline 101-2 in this embodiment. The third control valve 5 controls the condensation rate of water vapor by adjusting the flow rate of the cooling medium flowing through the second heat exchanger 12. The third control valve 5 can be connected to the system control module, and the control module can adjust the opening of the third control valve 5 according to the amount of water vapor generated, the condensation demand and the water circulation in the system. If the amount of water vapor generated is large, the third control valve 5 will increase the flow rate of the cooling medium to speed up the condensation process; if the amount of water vapor generated is small, the third control valve 5 will appropriately reduce the flow rate to avoid unnecessary energy consumption.

[0050] The second control valve 4 adjusts the flow rate of the cooling medium through the fuel cell 8 to ensure that the fuel cell 8 can be cooled in time under high load or high heat conditions; under low load conditions, unnecessary cooling is reduced to improve energy efficiency. The third control valve 5 flexibly adjusts the cooling medium flow rate of the second sub-pipeline 101-2 according to the system's water resource demand and water vapor generation, ensuring that the water vapor can be effectively condensed and recycled to the system's first water storage tank 15, reducing water loss and improving the system's water resource management efficiency. The coordinated control of the second control valve 4 and the third control valve 5 can not only reduce the system's cooling energy consumption, but also improve the overall operating efficiency of the system and reduce operating costs by effectively managing water resources.

[0051] In some embodiments, the solid-state on-site hydrolysis hydrogen production fuel cell system further includes a second water storage tank 17, the inlet of the second water storage tank 17 is connected to the outlet of the second main line 101-5, and the outlet of the second water storage tank 17 is connected to the inlet of the third main line 101-6. In this embodiment, in addition to the first water storage tank 15, the solid-state on-site hydrolysis hydrogen production fuel cell system also includes a second water storage tank 17. The main function of the second water storage tank 17 is to serve as a temporary storage unit for the cooling medium, help regulate the flow of the medium and temperature fluctuations in the liquid cooling circulation system, and ensure that the cooling medium maintains an appropriate temperature and flow rate under different operating conditions. Through this setting, the second water storage tank 17 can act as a buffer in the liquid cooling circulation system, and play a regulating and stabilizing role when the cooling load of the system fluctuates.

[0052] The inlet of the second water storage tank 17 is connected to the outlet of the second main line 101-5, so that the cooling medium flowing out of the second main line 101-5 can smoothly enter the second water storage tank 17. This design allows the cooling medium in the liquid cooling circulation system to be temporarily stored and temperature-adjusted through the second water storage tank 17 after passing through the fuel cell 8 and the second heat exchanger 12, ensuring that it is at an appropriate temperature before entering the next circulation stage. The outlet of the second water storage tank 17 is connected to the inlet of the third main line 101-6, which means that the cooling medium stored in the second water storage tank 17 is introduced into the third main line 101-6 at an appropriate time. The third main line 101-6 is mainly responsible for guiding the cooling medium to the first heat exchanger 1 for heat exchange, thereby achieving further cooling of the medium. Therefore, the second water storage tank 17, as an intermediate storage unit connecting the second main line 101-5 and the third main line 101-6, not only plays a buffering role, but also can ensure that the cooling medium flows as required in the liquid cooling cycle, avoiding the influence of flow fluctuations or insufficient cooling on system performance. The second water tank 17 can store the cooling medium flowing out through the second main line 101-5, and supply the cooling medium to the third main line 101-6 according to the system requirements, so as to ensure the stability of the flow of the cooling system. This design is particularly important when the system load changes greatly, and can effectively prevent the sudden drop or overload of the cooling medium flow, so as to ensure the efficient cooling of the fuel cell 8 and each heat exchanger. The second water tank 17 can play the role of regulating the temperature of the cooling medium. The cooling medium may experience temperature fluctuations after passing through the fuel cell 8 and the second heat exchanger 12, and the second water tank 17 can temporarily store the cooling medium so that it reaches a suitable temperature before entering the third main line 101-6, thereby ensuring the cooling efficiency of the system. The setting of the second water tank 17 in the system also helps to reduce the waste of cooling medium. During the liquid cooling cycle, the cooling medium may be lost or leaked due to pressure or temperature fluctuations, and the buffering function of the second water tank 17 can slow down the occurrence of this phenomenon, so as to ensure that the working medium in the system is fully utilized. In addition, the second water tank 17 can also be used to replenish the working medium in the cooling circulation system.

[0053] In some embodiments, the solid-state on-site hydrolysis hydrogen production fuel cell system further includes an air input pipeline 106 connected to the inlet of the cathode 803, and an air booster 13 is provided on the air input pipeline 106. This embodiment optimizes the air supply part of the solid-state on-site hydrolysis hydrogen production fuel cell system, adds an air input pipeline 106 and provides an air booster 13 on the pipeline. By increasing the air pressure and flow supplied to the cathode 803 of the fuel cell 8, it is helpful to improve the reaction efficiency and electrical performance of the fuel cell 8, especially at high power output.

[0054] Specifically in this embodiment, the solid-state on-site hydrolysis hydrogen production fuel cell system is equipped with an air input pipeline 106 connected to the cathode 803 inlet. The pipeline is used to continuously supply air (including oxygen) to the cathode 803 of the fuel cell 8 for the electrochemical reaction inside the battery. The air input pipeline 106 is connected to the external air source of the system and is responsible for introducing fresh air into the cathode 803 of the fuel cell 8. The oxygen in the air reacts with the protons from the anode 801 and the electrons flowing through the external circuit at the cathode 803 to generate water vapor, thereby completing the electrochemical reaction process. In order to improve the air supply efficiency, an air booster 13 is provided on the air input pipeline 106 in this embodiment. The main function of the air booster 13 is to increase the air pressure and flow rate in the air input pipeline 106, thereby enhancing the supply rate of oxygen in the air, making the reaction inside the fuel cell 8 more sufficient, and then increasing the output power of the battery. The air booster 13 can adjust the pressure of the input air according to the system requirements. Under high-load conditions, the air supercharger 13 will increase the air pressure to ensure that sufficient oxygen is supplied to the cathode 803, promoting the efficient redox reaction; and under low-load conditions, the air supercharger 13 can reduce the air pressure and reduce system energy consumption. The air supercharger 13 is preferably connected to the system control module, and can automatically adjust the air flow and pressure according to the load demand of the fuel cell 8, so that the fuel cell 8 can maintain the best operating state under different operating conditions, avoiding the problem of reduced efficiency or insufficient power due to insufficient air supply. In addition, the temperature of the fuel cell 8 will rise rapidly under high-load conditions. By increasing the air flow, the air supercharger 13 not only provides more oxygen, but also takes away part of the heat of the cathode 803, plays a role in auxiliary cooling, and reduces the working pressure of the first sub-pipeline 101-1. That is to say, by setting an air booster 13 on the air input pipeline 106 of the solid-state on-site hydrolysis hydrogen production fuel cell system, the oxygen supply efficiency of the cathode 803 of the fuel cell 8 is effectively improved, thereby improving the power output and overall performance of the fuel cell 8. The air booster 13 not only helps to optimize the electrochemical reaction conditions of the fuel cell 8, but also can enhance the system's dynamic response capability and stability under high load. While ensuring high-efficiency performance, the air booster 13 can achieve reasonable control of energy consumption through dynamic adjustment, thereby ensuring the energy efficiency and stability of the system.

[0055] In some embodiments, the liquid cooling circulation pipeline 101 of the solid-state on-site hydrolysis hydrogen production fuel cell system also includes a third sub-pipeline 101-3, the third sub-pipeline 101-3 and the first sub-pipeline 101-1 are arranged in parallel and are located between the first main pipeline 101-4 and the second main pipeline 101-5, and the hydrogen generator 11 is connected in series to the third sub-pipeline 101-3. In this embodiment, a third sub-pipeline 101-3 is further added to the liquid cooling circulation pipeline 101 of the solid-state on-site hydrolysis hydrogen production fuel cell system, and the hydrogen generator 11 is arranged in series on the pipeline to achieve efficient cooling of the hydrogen generator 11. Through this design, the system can not only ensure the normal operating temperature of the fuel cell 8 and effectively recover water vapor, but also effectively manage the heat of the hydrogen generator 11, thereby improving the working efficiency and stability of the entire system.

[0056] In this embodiment, the liquid cooling circulation pipeline 101 of the solid-state on-site hydrolysis hydrogen production fuel cell system includes three sub-pipelines, namely the first sub-pipeline 101-1, the second sub-pipeline 101-2 and the third sub-pipeline 101-3. The third sub-pipeline 101-3 is specifically used to cool the hydrogen generator 11 to ensure that the temperature is effectively controlled during the hydrogen generation process to avoid affecting the efficiency of hydrogen generation or causing potential damage to the system due to excessive temperature. By setting the third sub-pipeline 101-3, the first sub-pipeline 101-1 and the second sub-pipeline 101-2 in parallel, the cooling capacity of the system is flexibly configured, and the coolant can be distributed between different sub-pipelines according to the actual cooling needs, ensuring that the fuel cell 8 and the hydrogen generator 11 are efficiently cooled at the same time, and taking into account the recovery of water vapor. The hydrogen generator 11 releases a large amount of heat during the process of hydrolysis to produce hydrogen. A rapid temperature rise may affect its working efficiency or even cause damage to the system. By connecting the hydrogen generator 11 in series in the third sub-pipeline 101-3, the coolant exchanges heat with the heat source in the hydrogen generator 11 when passing through the hydrogen generator 11. After absorbing the heat released, the coolant with increased temperature will continue to flow to the second main pipeline 101-5, mix with the coolant in other sub-pipelines and enter the next cycle. The heat generated by the hydrogen generator 11 can be quickly taken away from the system to avoid heat accumulation leading to reduced efficiency or system failure, and keep the hydrogen generator 11 at a suitable working temperature, thereby ensuring the stability and efficiency of the hydrogen generation process.

[0057] Preferably, a fourth control valve 6 is provided on the third sub-pipeline 101-3 to precisely adjust the flow rate of the cooling medium. The fourth control valve 6 can dynamically adjust the flow rate of the coolant according to the working state and temperature change of the hydrogen generator 11 to adapt to the cooling requirements under different loads. When the working intensity of the hydrogen generator 11 is high, the system will increase the flow rate of the cooling medium in the third sub-pipeline 101-3 through the fourth control valve 6 to ensure that sufficient cooling medium passes through the hydrogen generator 11 for heat exchange and maintains it within a suitable temperature range; and when the load of the hydrogen generator 11 is small, the fourth control valve 6 reduces the flow rate to avoid energy waste caused by excessive cooling.

[0058] In some embodiments, the hydrogen generator 11 is filled with an appropriate amount of solid sodium borohydride, and the reaction temperature of the hydrogen generator 11 is controlled at 80 degrees Celsius. The sodium borohydride powder reacts with water, and the number of water molecules in the hydrolysis reaction is equal to the amount of hydrogen produced by the hydrolysis reaction. The generated hydrogen then reaches the anode 801 of the fuel cell 8 to react with oxygen for a hydrogen-oxygen electrochemical reaction, wherein the amount of water molecules generated at the anode 801 is equal to the amount of hydrogen participating in the hydrogen-oxygen electrochemical reaction, so that water and hydrogen form a closed material cycle.

[0059] In this embodiment, the hydrogen generator 11 is filled with an appropriate amount of solid sodium borohydride (NaBH 4 ), the substance undergoes hydrolysis under the action of water to generate hydrogen and by-products. The reaction formula is as follows: NaBH 4 +2H 2 O→NaBO 2 +4H 2 . In order to optimize the hydrolysis reaction of sodium borohydride, the present embodiment sets the operating temperature of the hydrogen generator 11 to 80 degrees Celsius, which can not only ensure the rapid progress of the reaction, but also prevent the excessive generation of by-products, thereby maintaining a stable supply of hydrogen. Sodium borohydride powder reacts with water molecules to generate hydrogen, wherein the number of water molecules required for the reaction is equal to the number of hydrogen molecules generated, ensuring that the hydrogen generator 11 can continuously provide sufficient hydrogen for the fuel cell 8. The generated hydrogen enters the anode 801 of the fuel cell 8 through the hydrogen supply line 102. In the fuel cell 8, the hydrogen undergoes a hydrogen-oxygen electrochemical reaction with oxygen in the air to generate water and electrical energy. The hydrogen undergoes an oxidation reaction at the anode 801 and decomposes into protons (H + ) and electron (e - ). Protons pass through the electrolyte layer 802 to the cathode 803, and combine with oxygen and electrons in the air to generate water molecules. The overall reaction formula is as follows: 2H 2 +O 2 →2H 2O. In the electrochemical reaction, the number of water molecules generated by the anode 801 is equal to the number of hydrogen molecules consumed in the reaction, which means that the water consumed in the hydrolysis reaction is regenerated during the operation of the fuel cell 8. These water molecules flow back to the hydrogen generator 11 through the system's water recovery device for use in the next round of hydrolysis reaction, realizing the circulation of water and avoiding water loss in the system. The hydrogen in the system mainly comes from the hydrolysis reaction of sodium borohydride. After the generated hydrogen is used by the fuel cell 8, part of the unreacted hydrogen flows back to the hydrogen generator 11 through the hydrogen recovery pipeline 103 for reuse. This closed loop not only improves the utilization efficiency of hydrogen, but also reduces the system's dependence on external hydrogen supply. The recycling of water and hydrogen in the system minimizes the consumption of materials, reduces the need for replenishment during the operation of the system, and extends the working time of the equipment. It is particularly suitable for application scenarios with limited water resources or long-term autonomous operation.

[0060] The reaction temperature of the hydrogen generator 11 can be controlled at 80 degrees Celsius by adjusting the fourth control valve 6 on the third sub-pipeline 101-3 in the liquid cooling circulation system, ensuring the stability and efficiency of the reaction, while avoiding local overheating of the system, further improving the stability of the entire system. Specifically, the reaction temperature of the hydrogen generator 11 can be monitored in real time by a temperature sensor, and the fourth control valve 6 can be automatically adjusted in combination with the control module to keep the internal temperature of the hydrogen generator 11 stable at 80 degrees Celsius. The water supply pump 16 provided on the water supply pipeline 105 is used to accurately control the water flow entering the hydrogen generator 11, ensuring that the ratio of water to sodium borohydride is appropriate and maintaining the balance of the reaction rate.

[0061] In some embodiments, the solid-state on-site hydrolysis hydrogen production fuel cell system further includes a third heat exchanger 18, wherein the hot end of the third heat exchanger 18 is connected in series to the third sub-pipeline 101-3 between the hydrogen generator 11 and the second main pipeline 101-5, and the cold end of the third heat exchanger 18 is connected in series to the air input pipeline 106, and the working fluid flowing out of the hydrogen generator 11 in the third sub-pipeline 101-3 and the air in the air input pipeline 106 can complete heat exchange through the third heat exchanger 18. When in an extremely low temperature environment, the fuel cell 8 cannot start the reaction to enter a normal working state. At this time, the exothermic reaction of sodium borohydride hydrolysis to produce hydrogen in the hydrogen generator 11 can be used to heat the working fluid in the third sub-pipeline 101-3, and then the working fluid in the third sub-pipeline 101-3 preheats the cold air in the air input pipeline 106 through the third heat exchanger 18 to ensure that the proton exchange membrane fuel cell obtains air of suitable temperature for warm start.

[0062] The following will explain in detail the mechanism of preheating the air through the third heat exchanger 18 to ensure that the fuel cell 8 can start normally in an extremely low temperature environment. When the solid-state on-site hydrolysis hydrogen production fuel cell system is in an extremely low temperature environment, the proton exchange membrane fuel cell (PEMFC) cannot directly start the reaction at low temperatures. The reason is that the proton conductivity in the fuel cell 8 decreases in the low temperature environment, and the reaction rate of oxygen in the air at the cathode 803 slows down, thereby hindering the normal operation of the fuel cell 8, making it difficult to successfully start the fuel cell 8 in this environment. When the solid sodium borohydride in the hydrogen generator 11 undergoes a hydrolysis reaction with water, heat is released. The hydrolysis reaction of sodium borohydride with water is as follows: NaBH 4 +2H 2 O→NaBO 2 +4H 2 + heat. The heat of the exothermic reaction is used to heat the working fluid in the third sub-pipeline 101-3 flowing through the hydrogen generator 11, so that its temperature rises. The heated working fluid flows into the hot end of the third heat exchanger 18 through the third sub-pipeline 101-3. The third heat exchanger 18 transfers the heat of these working fluids to the air in the air input pipeline 106 at its cold end through heat conduction. When the cold air enters the fuel cell 8 through the air input pipeline 106, it first passes through the cold end of the third heat exchanger 18. The cold air exchanges heat with the heated working fluid, and the air is effectively preheated to ensure that the cathode 803 obtains air with a higher temperature to accelerate the reaction rate of oxygen and protons. The preheated air enables the fuel cell 8 to start smoothly at a lower ambient temperature, that is, to achieve a "warm start" of the fuel cell 8, which is particularly important for application scenarios in cold areas or cold environments. Through the third heat exchanger 18, the heat of the exothermic reaction of the hydrogen generator 11 is effectively utilized, avoiding energy waste and achieving secondary heat recovery. At the same time, the preheated air can make the fuel cell 8 work at a higher efficiency, reducing the impact of low temperature on the battery performance. The addition of the third heat exchanger 18 enables the system to simultaneously complete air preheating and working fluid cooling, which can share the refrigeration pressure of the heat pump system, simplify the system structure, and improve the compactness and integration of the overall design.

[0063] In some embodiments, the solid-state on-site hydrolysis hydrogen production fuel cell system further includes a preheating device 14, which is preferably a lithium battery heating device with good emergency heating performance. It can generate heat under extremely low temperature conditions through the electric energy provided by the lithium battery to preheat the first water storage tank 15. When in the extremely low temperature working mode, the preheating device 14 is in an emergency working state to slowly heat the first water storage tank 15, so that part of the melted water enters the hydrogen generator 11 under the action of the supply water pump 16, and the water enters the hydrogen generator 11 and contacts with the sodium borohydride therein to undergo a violent hydrolysis reaction to generate a large amount of hydrogen, which enters the proton exchange membrane fuel cell through the hydrogen supply pipeline to provide it with the necessary reaction raw materials, and transfers the heat to the air entering the cathode 803 through the third sub-pipeline 101-3 and the third heat exchanger 18. This design ensures the smooth progress of the hydrolysis reaction and the continuous operation of the fuel cell 8 system through the emergency preheating mechanism.

[0064] The preheating device 14 is preferably installed near the first water tank 15 or close to one side of the first water tank 15 to ensure that heat can be directly transferred to the water inside the first water tank 15. Through this close contact installation method, the preheating device 14 can efficiently heat the water in the first water tank 15, thereby improving the heating efficiency.

[0065] In the emergency working mode, the preheating device 14 heats the water in the water tank to gradually melt the partially frozen water. Under the action of the water supply pump 16, the melted water can smoothly enter the hydrogen generator 11 to provide the necessary water source for the subsequent hydrogen generation reaction. When the melted water enters the hydrogen generator 11 through the water supply pump 16, it immediately contacts the solid sodium borohydride inside the hydrogen generator 11, and a violent hydrolysis reaction occurs. This reaction not only produces a large amount of hydrogen, providing the hydrogen required for the reaction of the proton exchange membrane fuel cell (PEMFC), but is also accompanied by heat release, further providing the system with the heat required for preheating the air supplying the anode 801.

[0066] This embodiment further enhances the adaptability and reliability of the solid-state on-site hydrolysis hydrogen production fuel cell system in low temperature environments through the design of the preheating device 14. The preheating device 14 can be started in an extremely low temperature environment to perform emergency heating on the water in the first water storage tank 15 to ensure a stable supply of water and provide the necessary conditions for the hydrolysis reaction of the hydrogen generator 11. Through the hydrolysis reaction of the hydrogen generator 11, the system can not only generate hydrogen, but also preheat the air through heat transfer, thereby solving the problem that the fuel cell 8 cannot be started in a low temperature environment. This design enables the fuel cell 8 system to smoothly achieve warm start in an extremely low temperature environment, ensuring the stable operation of the system.

[0067] Based on the same technical concept, an embodiment of the present application also provides a hydrothermal management method for a solid-state on-site hydrolysis hydrogen production fuel cell system, which is applied to the solid-state on-site hydrolysis hydrogen production fuel cell system provided in the aforementioned embodiment of the present application. The hydrothermal management method includes a high-temperature working mode hydrothermal management method and a low-temperature working mode hydrothermal management method.

[0068] The high-temperature working mode hydrothermal management method includes: the first heat exchanger 1 cools down the working medium in the third main pipeline 101-6; the liquid cooling circulation pump 2 drives the working medium to circulate in the liquid cooling circulation pipeline 101; after the first sub-pipeline 101-1 is opened, heat is exchanged with the fuel cell 8; after the second sub-pipeline 101-2 is opened, heat is exchanged with the water vapor recovery pipeline 104 in the second heat exchanger 12.

[0069] In the high-temperature working mode, the main goal of the water thermal management method is to ensure the normal operation of the system in a high-temperature environment and prevent overheating through effective cooling and heat management. During the operation of the fuel cell 8 system, when the ambient temperature is high, the working medium in the third main circuit 101-6 may accumulate a large amount of heat due to the heat exchange process. At this time, the first heat exchanger 1 is responsible for cooling the working medium flowing through the third main circuit 101-6, and the liquid cooling circulation pump 2 ensures that the heat inside the system is transferred out through the circulation of the working medium, and exchanges heat with the external environment through the heat pump system, and discharges excess heat to the environment to maintain the normal operating temperature of the system, so that the temperature of the working medium is maintained within a reasonable range to prevent the fuel cell 8 from overheating. Specifically, after the first sub-pipeline 101-1 is opened, the working medium exchanges heat with the cooling circuit of the fuel cell 8. By flowing the working medium through the fuel cell 8, the system effectively removes the excess heat generated by the fuel cell 8 during operation, ensuring that the fuel cell 8 maintains an optimal working state in a high-temperature environment and avoids overheating and resulting in a decrease in efficiency; after the second sub-pipeline 101-2 is opened, the working medium exchanges heat with the water vapor recovery pipeline 104 in the second heat exchanger 12. The water vapor accumulated in the water vapor recovery pipeline 104 will be recovered as water through cooling and enter the first water storage tank 15 for the next hydrolysis reaction process. This design ensures that the water resources in the system can be effectively recycled, thereby improving the overall efficiency of the system.

[0070] In some embodiments, the liquid cooling circulation pipeline 101 further includes a third sub-pipeline 101-3, which is arranged in parallel with the first sub-pipeline 101-1 and is located between the first main pipeline 101-4 and the second main pipeline 101-5, for further optimizing the thermal management of the system. The third sub-pipeline 101-3 is specifically used for heat exchange with the hydrogen generator 11 to further improve the water thermal management capability of the system.

[0071] In some embodiments, the liquid cooling circulation pipeline 101 also includes a third sub-pipeline 101-3, which is arranged in parallel with the first sub-pipeline 101-1 and is located between the first main pipeline 101-4 and the second main pipeline 101-5, and the hydrogen generator 11 is connected in series to the third sub-pipeline 101-3, and sodium borohydride powder is filled in the hydrogen generator 11; the high-temperature working mode hydrothermal management method also includes: after the third sub-pipeline 101-3 is turned on, heat is exchanged with the hydrogen generator 11.

[0072] In the high temperature working mode, when the third sub-pipeline 101-3 is turned on, the working medium exchanges heat with the hydrogen generator 11 through the third sub-pipeline 101-3, and transfers the excess heat inside the hydrogen generator 11 to the liquid cooling circulation pipeline 101, so as to prevent the internal temperature of the hydrogen generator 11 from being too high and affecting the hydrolysis efficiency of sodium borohydride. At the same time, the hydrolysis reaction inside the hydrogen generator 11 will release a large amount of heat, which can be transferred to other heat exchange devices in the system through the third sub-pipeline 101-3, further ensuring the stability and efficiency of the system. The high temperature working mode hydrothermal management method in this embodiment ensures the stable operation of the solid-state on-site hydrolysis hydrogen production fuel cell system in a high temperature environment through the reasonable design of the liquid cooling circulation pipeline 101, the first heat exchanger 1, and the three sub-pipelines. The method can not only effectively manage the heat in the system and prevent the system from overheating, but also can efficiently recycle and utilize the water resources in the system, ensuring that the fuel cell 8 system operates continuously and efficiently in a high temperature environment, greatly improving the system's adaptability to extreme high temperatures.

[0073] In some embodiments, the solid-state on-site hydrolysis hydrogen production fuel cell system includes the third heat exchanger 18 and the preheating device 14 in the aforementioned embodiments, and the low-temperature working mode water thermal management method includes: the heat pump system is turned off, the first sub-pipeline 101-1 and the second sub-pipeline 101-2 are both closed, and the third sub-pipeline 101-3 is turned on; after the preheating device 14 is turned on, the water in the first water storage tank 15 is preheated; the water supply pump 16 supplies water to the hydrogen generator 11 loaded with sodium borohydride; the liquid cooling circulation pump 2 drives the working medium to circulate in the liquid cooling circulation pipeline 101; the working fluid flowing out of the hydrogen generator 11 in the third sub-pipeline 101-3 exchanges heat with the cold air in the air input pipeline 106 in the third heat exchanger 18.

[0074] In the low temperature working mode, due to the low external ambient temperature, the heat demand of the system increases. In the startup phase and the initial working period of the fuel cell 8, there is no need to cool the fuel cell 8 and there is no need to recover water vapor by means of heat pump refrigeration. Therefore, the heat pump system is first turned off, and the first sub-pipeline 101-1 and the second sub-pipeline 101-2 are turned off at the same time. When the external temperature is low, the water in the first water storage tank 15 may freeze or the temperature is too low, and it is difficult to supply to the hydrogen generator 11 for hydrolysis reaction. Through the operation of the preheating device 14, the water in the first water storage tank 15 gradually melts and heats to a suitable temperature, ensuring that a stable water source can be provided for the hydrogen generator 11. As the water in the first water storage tank 15 is preheated to a suitable temperature, the water supply pump 16 starts to work and supplies water to the hydrogen generator 11 loaded with sodium borohydride. When the water enters the hydrogen generator 11, it contacts the sodium borohydride therein, and a violent hydrolysis reaction occurs, producing a large amount of hydrogen while releasing a large amount of heat. In order to cope with the low temperature environment, the third sub-pipeline 101-3 is opened, and the third sub-pipeline 101-3 is connected in series with the hydrogen generator 11 to ensure that the heat of the hydrolysis reaction in the hydrogen generator 11 can be transferred to other parts of the system, especially through heat exchange with the third heat exchanger 18, the heat is effectively transferred to the cold air in the air input pipeline 106. In the low temperature environment, the air temperature in the air input pipeline 106 is too low, which is not conducive to the hydrogen-oxygen electrochemical reaction of the fuel cell 8. Through the heat exchange of the third heat exchanger 18, the cold air in the air input pipeline 106 is preheated to a temperature suitable for the reaction of the fuel cell 8, ensuring that the proton exchange membrane fuel cell can be warm-started smoothly.

[0075] The low-temperature working mode hydrothermal management method of this embodiment ensures that the fuel cell 8 system can be started smoothly and work stably in a low-temperature environment through the synergistic effect of the preheating device 14, the third sub-pipeline 101-3 and the third heat exchanger 18, thereby improving the adaptability of the system in different temperature environments.

[0076] The device embodiments described above are merely illustrative, wherein the units described as separate components may or may not be physically separated, and the components shown as units may or may not be physical units, that is, they may be located in one place or distributed on multiple network units. Some or all of the modules may be selected according to actual needs to achieve the purpose of the solution of this embodiment.

[0077] Through the description of the above implementation methods, those skilled in the art can clearly understand that each implementation method can be implemented by means of software plus a general hardware platform, and of course, by hardware. Based on this understanding, the above technical solution, in essence, or the part that contributes to the relevant technology, can be embodied in the form of a software product, which can be stored in a computer-readable storage medium, such as ROM / RAM, a disk, an optical disk, etc., including a number of instructions for a computer device (which can be a personal computer, a server, or a network device, etc.) to execute the methods described in each embodiment or some parts of the embodiment.

[0078] It should be understood that the terms used herein are only for the purpose of describing specific example embodiments and are not intended to be limiting. Unless the context clearly indicates otherwise, the singular forms "one", "an" and "said" as used herein may also be meant to include plural forms. The terms "include", "comprise", "contain", and "have" are inclusive, and therefore specify the existence of stated features, steps, operations, elements and / or parts, but do not exclude the existence or addition of one or more other features, steps, operations, elements, parts, and / or combinations thereof. The method steps, processes, and operations described herein are not interpreted as necessarily requiring them to be performed in the specific order described or illustrated, unless the execution order is clearly indicated. It should also be understood that additional or alternative steps may be used.

[0079] The foregoing is merely a specific embodiment of the present invention, which enables those skilled in the art to understand or implement the present invention. Various modifications to these embodiments will be 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 present invention. Therefore, the present invention will not be limited to the embodiments shown herein, but rather to the widest scope consistent with the principles and novel features claimed herein.

Claims

1. A solid-state on-site hydrolysis hydrogen production fuel cell system, characterized in that: include: A fuel cell (8) comprising an anode (801), an electrolyte layer (802) and a cathode (803); A hydrogen generator (11) having a hydrogen outlet, a hydrogen recovery inlet and a water inlet, wherein the hydrogen outlet is connected to the inlet of the anode (801) via a hydrogen supply pipeline (102), and the outlet of the anode (801) is connected to the hydrogen recovery inlet via a hydrogen recovery pipeline (103); A first water storage tank (15), wherein the outlet of the cathode (803) is connected to the water recovery port of the first water storage tank (15) via a water vapor recovery pipeline (104), and the water outlet of the first water storage tank (15) is connected to the water inlet via a water supply pipeline (105); A liquid cooling circulation pipeline (101), comprising a first main pipeline (101-4), a second main pipeline (101-5), a third main pipeline (101-6), a first sub-pipeline (101-1) and a second sub-pipeline (101-2), wherein the first sub-pipeline (101-1) and the second sub-pipeline (101-2) are arranged in parallel and are both located between the first main pipeline (101-4) and the second main pipeline (101-5), and the fuel cell (8) is connected in series to the first sub-pipeline (101-1); A first heat exchanger (1), wherein a hot end of the first heat exchanger (1) is connected in series to the third main pipeline (101-6); a liquid cooling circulation pump (2) for driving the working fluid in the liquid cooling circulation pipeline (101) to circulate in sequence in the first main pipeline (101-4), at least one of the first sub-pipeline (101-1) and the second sub-pipeline (101-2), the second main pipeline (101-5), the third main pipeline (101-6), and the first main pipeline (101-4); A second heat exchanger (12), wherein a hot end of the second heat exchanger (12) is connected in series to the water vapor recovery pipeline (104), and a cold end of the second heat exchanger (12) is connected in series to the second sub-pipeline (101-2).

2. The solid-state on-site water splitting hydrogen production fuel cell system according to claim 1 is characterized in that: The heat pump circulation system (3) further comprises an evaporator (301), a throttle valve (302), a condenser (303) and a compressor (304) which are arranged in series via pipelines, the outlet of the compressor (304) being connected to the inlet of the condenser (303), the outlet of the condenser (303) being connected to the inlet of the evaporator (301), the outlet of the evaporator (301) being connected to the inlet of the compressor (304), the throttle valve (302) being arranged on the pipeline between the evaporator (301) and the condenser (303), and the cold end of the first heat exchanger (1) being connected in series to the pipeline between the evaporator (301) and the compressor (304).

3. The solid-state on-site water splitting hydrogen production fuel cell system according to claim 1 is characterized in that: The hydrogen supply pipeline (102) is provided with a first control valve (7), the hydrogen recovery pipeline (103) is provided with a tail gas recovery pump (10), and the water supply pipeline (105) is provided with a water supply pump (16).

4. The solid-state on-site water splitting hydrogen production fuel cell system according to claim 1 is characterized in that: The first sub-pipeline (101-1) is provided with a second control valve (4), and the second sub-pipeline (101-2) is provided with a third control valve (5).

5. The solid-state on-site water splitting hydrogen production fuel cell system according to claim 1 is characterized in that: It also comprises a second water storage tank (17), the inlet of the second water storage tank (17) being in communication with the outlet of the second main pipeline (101-5), and the outlet of the second water storage tank (17) being in communication with the inlet of the third main pipeline (101-6).

6. The solid-state on-site water splitting hydrogen production fuel cell system according to claim 1 is characterized in that: It also includes an air input pipeline (106) connected to the inlet of the cathode (803), and an air booster (13) is provided on the air input pipeline (106).

7. The solid-state on-site water splitting hydrogen production fuel cell system according to any one of claims 1 to 6, characterized in that: The liquid cooling circulation pipeline (101) further comprises a third sub-pipeline (101-3), the third sub-pipeline (101-3) being arranged in parallel with the first sub-pipeline (101-1) and being located between the first main pipeline (101-4) and the second main pipeline (101-5), and the hydrogen generator (11) being connected in series to the third sub-pipeline (101-3).

8. The solid-state on-site water splitting hydrogen production fuel cell system according to claim 7 is characterized in that: The third sub-pipeline (101-3) is provided with a fourth control valve (6).

9. A hydrothermal management method for a solid-state on-site hydrolysis hydrogen production fuel cell system, applied to the solid-state on-site hydrolysis hydrogen production fuel cell system as claimed in any one of claims 1 to 8, characterized in that: The hydrothermal management method includes a high-temperature working mode hydrothermal management method, and the high-temperature working mode hydrothermal management method includes: The first heat exchanger (1) cools down the working medium in the third main pipeline (101-6); The liquid cooling circulation pump (2) drives the working medium to circulate in the liquid cooling circulation pipeline (101); After the first sub-pipeline (101-1) is opened, heat is exchanged with the fuel cell (8); After the second sub-pipeline (101-2) is opened, heat is exchanged with the water vapor recovery pipeline (104) in the second heat exchanger (12).

10. The hydrothermal management method for a solid-state on-site hydrolysis hydrogen production fuel cell system according to claim 9, characterized in that: The liquid cooling circulation pipeline (101) further comprises a third sub-pipeline (101-3), the third sub-pipeline (101-3) and the first sub-pipeline (101-1) being arranged in parallel and located between the first main pipeline (101-4) and the second main pipeline (101-5), the hydrogen generator (11) being connected in series to the third sub-pipeline (101-3), the hydrogen generator (11) being filled with sodium borohydride powder; the high temperature working mode hydrothermal management method further comprises: after the third sub-pipeline (101-3) is turned on, heat is exchanged with the hydrogen generator (11).

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