Solid-liquid fuel composite hydrogen production and high-low temperature fuel cell coupling intelligent power system

Abstract

The application provides a kind of solid-liquid fuel composite hydrogen production and high-low temperature fuel cell coupling intelligent power system.It includes: aluminum trihydride fuel tank, methanol steam reforming hydrogen production reactor, high temperature proton exchange membrane fuel cell stack and low temperature proton exchange membrane fuel cell stack;The outlet of the aluminum trihydride fuel tank is connected with the inlet of high-pressure hydrogen storage bottle through pipeline;The outlet of the high-pressure hydrogen storage bottle is connected with the anode inlet of the low temperature proton exchange membrane fuel cell stack through pressure reducing valve;The dual hydrogen source synergistic coupling mechanism of the application effectively solves the inherent limitations of single hydrogen source in fuel cell application through complementary reaction characteristics and energy cascade utilization, breaks the traditional single hydrogen source, single type fuel cell system architecture, creatively deeply integrates two hydrogen production methods and two stack technologies, and realizes the comprehensive breakthrough of the system in efficiency, dynamic response, fuel adaptability and reliability.

Description

Technical Field

[0001] This invention relates to the field of fuel cell technology, and more particularly to an intelligent power system for hydrogen production using a combination of solid and liquid fuels and coupling of high and low temperature fuel cells. Background Technology

[0002] A fuel cell is a device that directly converts the chemical energy of fuel into electrical energy through an electrochemical reaction. It boasts advantages such as high energy conversion efficiency, environmental friendliness, and low operating noise, and has broad application prospects in transportation, stationary power generation, and other fields. Based on operating temperature, proton exchange membrane fuel cells can be divided into high-temperature (HT-PEMFC) and low-temperature (LT-PEMFC) types. HT-PEMFCs typically operate between 150°C and 180°C, employing a phosphoric acid-doped polymer electrolyte membrane, exhibiting strong tolerance to carbon monoxide (CO), and can use hydrogen-rich gas produced by methanol reforming as fuel. LT-PEMFCs generally operate between 60°C and 80°C, using high-purity hydrogen as fuel, and feature fast start-up, high power density, and good dynamic response, but have extremely stringent requirements for hydrogen purity. In terms of hydrogen sources, methanol steam reforming for hydrogen production has the advantages of large hydrogen storage capacity and stable hydrogen supply, while aluminum trihydride (AlH3), as a solid hydrogen storage material, has the characteristics of high hydrogen storage density, low hydrogen release temperature and rapid start-up.

[0003] Currently, most common fuel cell systems employ a single hydrogen source and a single type of fuel cell architecture. For example, some systems rely solely on methanol reforming to produce hydrogen for high-temperature proton exchange membrane fuel cells, while others use solid hydrogen storage materials such as aluminum trihydride to supply hydrogen for low-temperature proton exchange membrane fuel cells. Although this single hydrogen source, single stack structure simplifies system design and control, in practical applications it is often limited by the inherent characteristics of the technology and fuel used, making it difficult to simultaneously meet the multiple requirements of high system efficiency, rapid start-up, dynamic response, and long-term continuous operation.

[0004] However, the aforementioned existing technologies have significant shortcomings: methanol reforming for hydrogen production has a slow start-up time (typically several minutes to over ten minutes) and a lagging dynamic response, failing to meet transient load requirements; while aluminum trihydride hydrogen production starts up quickly, its hydrogen storage capacity is limited, making it difficult to support long-term continuous system operation. Furthermore, a single type of fuel cell cannot fully leverage the respective advantages of high-temperature stacks (impurity resistance and high waste heat quality) and low-temperature stacks (high efficiency and fast response). In addition, single hydrogen source systems also have significant limitations in fuel adaptability, system reliability, and overall energy utilization efficiency, failing to achieve complementary advantages and tiered integration between the hydrogen source and the stack, thus restricting the overall performance of fuel cell systems in complex application scenarios. Summary of the Invention

[0005] To address the shortcomings of single-hydrogen-source and single-type fuel cell systems in terms of start-up speed, dynamic response, fuel adaptability, reliability, and energy efficiency, this invention provides an intelligent power system that combines solid-liquid fuel hybrid hydrogen production with high- and low-temperature fuel cell coupling. This invention primarily utilizes a combination of methanol reforming for hydrogen production and aluminum trihydride hydrogen production, coupled with high- and low-temperature proton exchange membrane fuel cells. Through intelligent airflow distribution, graded thermal energy management, and material recycling, it achieves synergistic effects between the two hydrogen sources and tiered energy utilization, thereby improving system efficiency, enhancing dynamic response, expanding fuel adaptability, and increasing reliability.

[0006] The technical means employed in this invention are as follows:

[0007] A smart power system for hydrogen production using solid-liquid fuels coupled with high and low temperature fuel cells includes an aluminum trihydride fuel tank, a methanol steam reforming hydrogen production reactor, a high-temperature proton exchange membrane fuel cell stack, and a low-temperature proton exchange membrane fuel cell stack.

[0008] The outlet of the aluminum trihydride fuel tank is connected to the inlet of the high-pressure hydrogen storage cylinder via a pipeline; the outlet of the high-pressure hydrogen storage cylinder is connected to the anode inlet of the cryogenic proton exchange membrane fuel cell stack via a pressure reducing valve; the cathode inlet of the cryogenic proton exchange membrane fuel cell stack is connected to the cathode gas pump of the cryogenic fuel cell stack via a pipeline; the electrical output terminal of the cryogenic proton exchange membrane fuel cell stack is electrically connected to the reactor bed electric heater of the methanol steam reforming hydrogen production reactor; the electrical output terminal of the cryogenic proton exchange membrane fuel cell stack is electrically connected to the circulating oil electric heater; and the electrical output terminal of the cryogenic proton exchange membrane fuel cell stack is electrically connected to the cryogenic fuel cell stack DC / DC converter.

[0009] The outlet of the methanol-water solution fuel tank is connected to the methanol-water solution inlet of the coupled heat exchanger via a methanol-water solution pump; the methanol-water solution outlet of the coupled heat exchanger is connected to the inlet of the methanol-water vapor reforming hydrogen production reactor; the outlet of the methanol-water vapor reforming hydrogen production reactor is connected to the inlet of the aluminum powder reaction tank; the outlet of the aluminum powder reaction tank is connected to the hydrogen-rich gas inlet of the coupled heat exchanger; the hydrogen-rich gas outlet of the coupled heat exchanger is connected to the anode inlet of the high-temperature proton exchange membrane fuel cell stack; the cathode gas pump of the high-temperature fuel cell stack is connected to the cathode inlet of the high-temperature proton exchange membrane fuel cell stack; and the electrical output terminal of the high-temperature proton exchange membrane fuel cell stack is electrically connected to the DC / DC converter of the high-temperature fuel cell stack.

[0010] Furthermore, the anode outlet of the high-temperature proton exchange membrane fuel cell stack is connected to the anode exhaust gas inlet of the catalytic combustion reactor via a pipeline; the combustion gas pump is connected to the air inlet of the catalytic combustion reactor via a pipeline; the outlet of the catalytic combustion reactor is connected to the inlet of the gas heat exchanger via a combustion exhaust gas three-way valve; the outlet of the gas heat exchanger is connected to the exhaust gas emission pipeline; and the gas heat exchanger is thermally coupled to the aluminum trihydride fuel tank.

[0011] Furthermore, the aluminum powder reaction vessel is a detachable, independent vessel; after hydrogen release is completed, the aluminum trihydride fuel vessel can be structurally used as an aluminum powder reaction vessel.

[0012] Furthermore, a hydrogen flow regulating three-way valve is installed on the outlet pipeline of the pressure reducing valve, and one outlet of the hydrogen flow regulating three-way valve is connected to one inlet of a gas mixing three-way valve through a pipeline; the outlet of the gas mixing three-way valve is connected to the pipeline between the hydrogen-rich gas outlet of the coupling heat exchanger and the anode inlet of the high-temperature proton exchange membrane fuel cell stack through a pipeline.

[0013] Furthermore, the circulating oil heater is connected to the circulating oil radiator, and a cooling fan is provided on the outside of the circulating oil radiator; a stack electric heater is provided on the outside of the low-temperature proton exchange membrane fuel cell stack, and an external fan is provided on the outside of the stack electric heater.

[0014] Furthermore, the hydrogen-rich reformed gas produced by the methanol steam reforming hydrogen production reactor is supplied as fuel to the high-temperature proton exchange membrane fuel cell stack, wherein the volume fraction of hydrogen in the hydrogen-rich gas is >60%, and the high-purity hydrogen produced by the thermal decomposition of the aluminum trihydride fuel tank is supplied as fuel to the low-temperature proton exchange membrane fuel cell stack.

[0015] Furthermore, the operating strategies of the intelligent power system include a pure aluminum trihydride mode for rapid start-up and low load, a mixed hydrogen supply mode for steady state and high load, and a methanol reforming-dominated mode for when aluminum trihydride reserves are insufficient.

[0016] The pure aluminum trihydride mode is as follows: the electric heater installed on the aluminum trihydride fuel tank is controlled to start heating; the hydrogen flow regulating three-way valve is controlled to allow the high-purity hydrogen produced by the thermal decomposition of the aluminum trihydride fuel tank to flow sequentially through the high-pressure hydrogen storage cylinder, the high-pressure hydrogen pressure reducing valve, and the hydrogen flow regulating three-way valve, and finally supply it to the anode of the low-temperature proton exchange membrane fuel cell stack; the low-temperature proton exchange membrane fuel cell stack cathode gas pump is controlled to operate to supply gas to the stack cathode; the electrical energy generated by the low-temperature proton exchange membrane fuel cell stack is distributed to the reactor bed electric heater and the circulating oil electric heater of the methanol steam reforming hydrogen production reactor to provide heat for the subsequent start-up of the system;

[0017] The hybrid hydrogen supply mode is as follows: The methanol steam reforming hydrogen production reactor is maintained in operation. The hydrogen-rich gas produced by the methanol steam reforming hydrogen production reactor flows sequentially through the aluminum powder reactor and the coupled heat exchanger before being supplied to the anode of the high-temperature proton exchange membrane fuel cell stack. The hydrogen flow regulating three-way valve and the gas mixing three-way valve are controlled to supply a portion of the high-purity hydrogen produced by the aluminum trihydride fuel tank to the anode of the low-temperature proton exchange membrane fuel cell stack. Simultaneously, another portion of high-purity hydrogen is incorporated into the hydrogen-rich gas pipeline flowing to the anode of the high-temperature proton exchange membrane fuel cell stack, forming a mixed gas and increasing the hydrogen concentration. The anode exhaust gas of the high-temperature proton exchange membrane fuel cell stack is introduced into the catalytic combustion reactor for combustion. The resulting high-temperature flue gas heats the methanol steam reforming hydrogen production reactor. The high-temperature exhaust gas after combustion then heats the aluminum trihydride fuel tank via the gas heat exchanger.

[0018] The methanol reforming dominant mode is as follows: the hydrogen flow regulating three-way valve is controlled to close the flow path to the low-temperature proton exchange membrane fuel cell stack; the methanol steam reforming hydrogen production reactor is maintained in operation. In this mode, the hydrogen-rich gas generated by the methanol steam reforming hydrogen production reactor serves as the sole hydrogen source. After passing through the aluminum powder reactor and the coupling heat exchanger, it is supplied to the anode of the high-temperature proton exchange membrane fuel cell stack; the tail gas from the anode of the high-temperature proton exchange membrane fuel cell stack is introduced into the catalytic combustion reactor for combustion, and the generated high-temperature flue gas is used to heat the methanol steam reforming hydrogen production reactor.

[0019] Compared with the prior art, the present invention has the following advantages:

[0020] This invention combines methanol reforming for hydrogen production with aluminum trihydride hydrogen production, and simultaneously couples high-temperature (HT-PEMFC) and low-temperature (LT-PEMFC) proton exchange membrane fuel cells to form a powerful composite power system. This dual-hydrogen-source synergistic coupling mechanism effectively solves the inherent limitations of a single hydrogen source in fuel cell applications through complementary reaction characteristics and cascaded energy utilization. It breaks away from the traditional system architecture of a single hydrogen source and a single type of fuel cell, creatively integrating two hydrogen production methods and two fuel cell stack technologies. Through the coordinated management of energy flow, material flow, and information flow, it achieves comprehensive breakthroughs in system efficiency, dynamic response, fuel adaptability, and reliability.

[0021] This invention employs a single system, two hydrogen sources, two types of fuel cell stacks, multiple modes, and intelligent collaboration. Through ingenious system integration and advanced control strategies, it maximizes the advantages of different technical approaches while cleverly avoiding their respective disadvantages. Ultimately, it creates a new generation of hybrid power systems that excels in efficiency, power, response speed, reliability, and fuel flexibility, providing a novel technical solution for the widespread application of fuel cells in transportation, stationary power generation, and other fields. Attached Figure Description

[0022] 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 some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0023] Figure 1 This is a schematic diagram of the overall structure of the present invention.

[0024] Figure 2 This is a schematic diagram of the structure and interface of the gas heat exchanger and aluminum trihydride fuel tank of the present invention.

[0025] Figure 3 This is a schematic diagram of the structure and interface of the coupling heat exchanger, methanol steam reforming hydrogen production reactor, catalytic combustion reactor, and aluminum powder reaction tank of the present invention.

[0026] Figure 4 This is a schematic diagram of the structure and interface of the high-temperature fuel cell stack and the low-temperature fuel cell stack of the present invention.

[0027] In the diagram: 1. High-temperature fuel cell stack; 2. Low-temperature fuel cell stack; 3. Methanol steam reforming hydrogen production reactor; 4. Catalytic combustion reactor; 5. Methanol-water solution fuel tank; 6. Methanol-water solution pump; 7. Aluminum trihydride fuel tank; 8. High-temperature fuel cell stack cathode gas pump; 9. Combustion gas pump; 10. Low-temperature fuel cell stack cathode gas pump; 11. Circulating oil pump; 12. Circulating oil heater; 13. Circulating oil radiator; 14. Circulating oil cooling fan; 15. Coupled heat exchanger; 16. Reactor bed heater. 17. Aluminum powder reactor; 18. Fuel cell stack cooling fan; 19. Fuel cell stack electric heater; 20. Gas heat exchanger; 21. Electric heater; 22. High-pressure hydrogen storage tank; 23. High-pressure hydrogen pressure reducing valve; 24. Hydrogen flow regulating three-way valve; 25. Combustion exhaust gas three-way valve; 26. Gas mixing three-way valve; 27. High-temperature fuel cell stack DC / DC converter; 28. Low-temperature fuel cell stack DC / DC converter; 29. ​​High-temperature fuel cell stack cathode inlet; 30. High-temperature fuel cell stack cathode outlet; 31. High-temperature fuel... 32. High-temperature fuel cell stack anode inlet; 33. High-temperature fuel cell stack circulating oil inlet; 34. High-temperature fuel cell stack circulating oil outlet; 35. Low-temperature fuel cell stack cathode inlet; 36. Low-temperature fuel cell stack cathode outlet; 37. Low-temperature fuel cell stack anode inlet; 38. Low-temperature fuel cell stack anode outlet; 39. Coupled heat exchanger methanol-water solution inlet; 40. Coupled heat exchanger methanol-water solution outlet; 41. Coupled heat exchanger circulating oil inlet; 42. Coupled heat exchanger circulating oil outlet. 43. Oil outlet; 44. Hydrogen-rich gas inlet of coupling heat exchanger; 45. Hydrogen-rich gas outlet of coupling heat exchanger; 46. Inlet of methanol steam reforming hydrogen production reactor; 47. Outlet of methanol steam reforming hydrogen production reactor; 48. Inlet of aluminum powder reactor; 49. Outlet of aluminum powder reactor; 50. Air inlet of catalytic combustion reactor; 51. Anode tail gas inlet of high-temperature fuel cell stack of catalytic combustion reactor; 52. Outlet of catalytic combustion reactor; 53. Inlet of gas heat exchanger; 54. Outlet of aluminum trihydride fuel tank. Detailed Implementation

[0028] It should be noted that, unless otherwise specified, the embodiments and features described in the present invention can be combined with each other. The present invention will now be described in detail with reference to the accompanying drawings and embodiments.

[0029] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, 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. The following description of at least one exemplary embodiment is merely illustrative and is in no way intended to limit the present invention or its application or use. 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.

[0030] It should be noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the scope of exemplary embodiments according to the invention. As used herein, the singular form is intended to include the plural form as well, unless the context clearly indicates otherwise. Furthermore, it should be understood that when the terms "comprising" and / or "including" are used in this specification, they indicate the presence of features, steps, operations, devices, components, and / or combinations thereof.

[0031] Unless otherwise specifically stated, the relative arrangement, numerical expressions, and values ​​of the components and steps described in these embodiments do not limit the scope of the invention. It should also be understood that, for ease of description, the dimensions of the various parts shown in the drawings are not drawn to actual scale. Techniques, methods, and devices known to those skilled in the art may not be discussed in detail, but where appropriate, such techniques, methods, and devices should be considered part of the specification. In all examples shown and discussed herein, any specific values ​​should be interpreted as merely exemplary and not as limitations. Therefore, other examples of exemplary embodiments may have different values. It should be noted that similar reference numerals and letters in the following figures denote similar items; therefore, once an item is defined in one figure, it need not be further discussed in subsequent figures.

[0032] In the description of this invention, it should be understood that the orientation or positional relationship indicated by directional terms such as "front, back, up, down, left, right", "horizontal, vertical, horizontal" and "top, bottom" is generally based on the orientation or positional relationship shown in the accompanying drawings, and is only for the convenience of describing this invention and simplifying the description. Unless otherwise stated, these directional terms 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, and therefore should not be construed as a limitation on the scope of protection of this invention. The directional terms "inner" and "outer" refer to the inner and outer contours relative to the outline of each component itself.

[0033] For ease of description, spatial relative terms such as "above," "over," "on the upper surface of," "above," etc., are used herein to describe the spatial positional relationship of a device or feature as shown in the figures to other devices or features. It should be understood that spatial relative terms are intended to encompass different orientations in use or operation besides the orientation of the device as described in the figures. For example, if the device in the figures is inverted, a device described as "above" or "above" other devices or structures would subsequently be positioned as "below" or "under" other devices or structures. Thus, the exemplary term "above" can include both "above" and "below." The device may also be positioned in other different ways (rotated 90 degrees or in other orientations), and the spatial relative descriptions used herein will be interpreted accordingly.

[0034] Furthermore, it should be noted that the use of terms such as "first" and "second" to define components is merely for the purpose of distinguishing the corresponding components. Unless otherwise stated, the above terms have no special meaning and therefore should not be construed as limiting the scope of protection of this invention.

[0035] This invention employs a dual-hydrogen-source, dual-stall hybrid power topology, integrating a methanol steam reforming hydrogen production subsystem (stable and high-capacity), an aluminum trihydride (AlH3) pyrolysis hydrogen production subsystem (fast and high-purity), an HT-PEMFC subsystem (CO-resistant and with high waste heat quality), and an LT-PEMFC subsystem (rapid start-up and high power density). These four subsystems are organically integrated through optimized airflow and thermal management channels. It offers fuel flexibility, utilizing both widely available and easily transported methanol, as well as aluminum trihydride with extremely high hydrogen storage density. The HT-PEMFC utilizes reformed gas, and the LT-PEMFC utilizes high-purity hydrogen, maximizing resource utilization. This dual-hydrogen-source synergistic coupling mechanism effectively overcomes the inherent limitations of a single hydrogen source in fuel cell applications through complementary reaction characteristics and cascaded energy utilization.

[0036] like Figure 1-4 As shown, the present invention provides an intelligent power system for hydrogen production by solid-liquid fuel composite and high- and low-temperature fuel cell coupling, including an aluminum trihydride fuel tank 7, a methanol steam reforming hydrogen production reactor 3, a high-temperature fuel cell stack 1 and a low-temperature fuel cell stack 2.

[0037] The aluminum trihydride fuel tank outlet 54 is connected to the inlet of the high-pressure hydrogen storage cylinder 22 via a pipeline; the outlet of the high-pressure hydrogen storage cylinder 22 is connected to the anode inlet 37 of the cryogenic fuel cell stack via the high-pressure hydrogen pressure reducing valve 23; the cathode inlet 35 of the cryogenic fuel cell stack is connected to the cathode gas pump 10 of the cryogenic fuel cell stack via a pipeline; the cryogenic fuel cell stack 2 also includes a cathode outlet 36 and an anode outlet 38; the electrical output terminal of the cryogenic fuel cell stack 2 is electrically connected to the reactor bed electric heater 16 of the methanol steam reforming hydrogen production reactor 3; the electrical output terminal of the cryogenic fuel cell stack 2 is electrically connected to the circulating oil electric heater 12; the electrical output terminal of the cryogenic fuel cell stack 2 is electrically connected to the DC / DC converter 28 of the cryogenic fuel cell stack; after the aluminum trihydride fuel tank 7 completes hydrogen release, the aluminum powder generated is used as the filler of the aluminum powder reaction tank 17, replacing the old aluminum powder reaction tank 17, realizing the recycling of aluminum elements and the system's self-hydrogenation. The high-purity hydrogen produced by the thermal decomposition of aluminum trihydride can be stored in a high-pressure hydrogen storage cylinder 22, and then supplied to the fuel cell stack as needed via a high-pressure hydrogen pressure reducing valve 23.

[0038] The outlet of the methanol-water solution fuel tank 5 is connected to the methanol-water solution inlet 39 of the coupling heat exchanger via the methanol-water solution pump 6; the methanol-water solution outlet 40 of the coupling heat exchanger is connected to the inlet 45 of the methanol-water vapor reforming hydrogen production reactor; the coupling heat exchanger 15 also includes a coupling heat exchanger circulating oil inlet 41 and a coupling heat exchanger circulating oil outlet 42; the outlet 46 of the methanol-water vapor reforming hydrogen production reactor is connected to the inlet 47 of the aluminum powder reactor; the outlet 48 of the aluminum powder reactor is connected to the hydrogen-rich gas inlet 43 of the coupling heat exchanger; the hydrogen-rich gas outlet 44 of the coupling heat exchanger is connected to the anode inlet 31 of the high-temperature fuel cell stack; the cathode gas pump 8 of the high-temperature fuel cell stack is connected to the cathode inlet 29 of the high-temperature fuel cell stack; the high-temperature fuel cell stack 1 also includes a cathode outlet 30, a circulating oil inlet 33, and a circulating oil outlet 34 of the high-temperature fuel cell stack; the electrical output terminal of the high-temperature fuel cell stack 1 is electrically connected to the DC / DC converter 27 of the high-temperature fuel cell stack. An aluminum powder reaction vessel 17 is connected in series downstream of the outlet of the methanol steam reforming hydrogen production reactor 3. It utilizes the active aluminum powder after aluminum trihydride decomposition to undergo a hydrolysis reaction with the water vapor in the reformed gas to remove water vapor and produce additional hydrogen, thereby improving the quality of the fuel gas entering the high-temperature fuel cell stack 1.

[0039] The anode outlet 32 ​​of the high-temperature fuel cell stack is connected to the anode exhaust gas inlet 50 of the high-temperature fuel cell stack in the catalytic combustion reactor via a pipeline; the combustion gas pump 9 is connected to the air inlet 49 of the catalytic combustion reactor via a pipeline; the outlet 51 of the catalytic combustion reactor is connected to the inlet 52 of the gas heat exchanger via the combustion exhaust gas three-way valve 25; the outlet 53 of the gas heat exchanger is connected to the exhaust gas emission pipeline; the gas heat exchanger 20 is thermally coupled to the aluminum trihydride fuel tank 7; an electric heater 21 is arranged between the gas heat exchanger 20 and the aluminum trihydride fuel tank 7 for heating the aluminum trihydride fuel tank 7 during the system start-up phase.

[0040] A hydrogen flow regulating three-way valve 24 is installed on the outlet pipeline of the high-pressure hydrogen pressure reducing valve 23. One outlet of the hydrogen flow regulating three-way valve 24 is connected to one inlet of the gas mixing three-way valve 26 via a pipeline. The outlet of the gas mixing three-way valve 26 is connected to the pipeline between the hydrogen-rich gas outlet 44 of the coupling heat exchanger and the anode inlet 31 of the high-temperature fuel cell stack via a pipeline. This is used to preferentially supply high-purity hydrogen generated by the aluminum trihydride fuel tank 7 to the low-temperature fuel cell stack 2, and to supply hydrogen-rich gas generated by the methanol steam reforming hydrogen production reactor 3 to the high-temperature fuel cell stack 1.

[0041] The circulating oil heater 12 is connected to the circulating oil radiator 13, and the circulating oil radiator 13 is equipped with a circulating oil cooling fan 14 on the outside; the low-temperature fuel cell stack 2 is equipped with a stack electric heater 19 on the outside, and the stack electric heater 19 is equipped with a stack cooling fan 18 on the outside.

[0042] The intelligent power system's operating strategies include a pure aluminum trihydride mode for rapid start-up and low load, a mixed hydrogen supply mode for steady state and high load, and a methanol reforming-dominated mode when aluminum trihydride reserves are insufficient. When the high-temperature fuel cell stack 1 or its hydrogen source fails, the system can switch to a working mode dominated by the aluminum trihydride fuel tank 7 and the low-temperature fuel cell stack 2, and vice versa, to ensure uninterrupted system operation.

[0043] The pure aluminum trihydride mode is as follows: the electric heater 21 installed on the aluminum trihydride fuel tank 7 is controlled to start heating; the hydrogen flow regulating three-way valve 24 is controlled to allow the high-purity hydrogen produced by the thermal decomposition of the aluminum trihydride fuel tank 7 to flow sequentially through the high-pressure hydrogen storage cylinder 22, the high-pressure hydrogen pressure reducing valve 23, and the hydrogen flow regulating three-way valve 24, and finally supply it to the anode inlet 37 of the low-temperature fuel cell stack; the low-temperature fuel cell stack cathode gas pump 10 is controlled to operate to supply gas to the stack cathode; the electrical energy generated by the low-temperature fuel cell stack 2 is distributed to the reactor bed electric heater 16 and the circulating oil electric heater 12 of the methanol steam reforming hydrogen production reactor 3 to provide heat for the subsequent start-up of the system;

[0044] The mixed hydrogen supply mode is as follows: The methanol steam reforming hydrogen production reactor 3 is maintained in operation. The hydrogen-rich gas produced by the methanol steam reforming hydrogen production reactor 3 flows sequentially through the aluminum powder reaction tank 17 and the coupling heat exchanger 15, and is then supplied to the anode inlet 31 of the high-temperature fuel cell stack. The hydrogen flow regulating three-way valve 24 and the gas mixing three-way valve 26 are controlled to supply a portion of the high-purity hydrogen produced by the aluminum trihydride fuel tank to the anode inlet 37 of the low-temperature fuel cell stack. At the same time, another portion of the high-purity hydrogen is merged into the hydrogen-rich gas pipeline flowing to the anode inlet 31 of the high-temperature fuel cell stack to form a mixed gas. The anode tail gas of the high-temperature fuel cell stack 1 is introduced into the catalytic combustion reactor 4 for combustion. The high-temperature flue gas produced is used to heat the methanol steam reforming hydrogen production reactor 3. The high-temperature tail gas after combustion is then used to heat the aluminum trihydride fuel tank 7 through the gas heat exchanger 20. The mixed hydrogen supply mode can mix a portion of the high-purity hydrogen into the reformed gas to increase the hydrogen concentration and reduce the carbon monoxide concentration, so that it can adapt to the tolerance range of the high-temperature fuel cell stack 1.

[0045] The methanol reforming main mode is as follows: the hydrogen flow regulating three-way valve 24 is closed to shut off the flow path to the low-temperature fuel cell stack 2; the methanol steam reforming hydrogen production reactor 3 is maintained in operation. In this mode, the hydrogen-rich gas produced by the methanol steam reforming hydrogen production reactor 3 serves as the sole hydrogen source. After passing through the aluminum powder reactor 17 and the coupling heat exchanger 15, it is supplied to the anode inlet 31 of the high-temperature fuel cell stack; the anode tail gas of the high-temperature fuel cell stack 1 is introduced into the catalytic combustion reactor 4 for combustion, and the high-temperature flue gas produced is used to heat the methanol steam reforming hydrogen production reactor 3.

[0046] This invention employs a graded thermal energy management and cascade utilization network, which preheats the methanol solution through a coupling heat exchanger 15 by using the waste heat from the reaction of the high-temperature fuel cell stack 1; the anode tail gas of the high-temperature fuel cell stack 1 is combusted in the catalytic combustion reactor 4 to provide the main heat source for the methanol steam reforming hydrogen production reactor 3; the high-temperature tail gas after heat exchange provides an auxiliary heat source for the thermal decomposition of the aluminum trihydride fuel tank 7 through a gas heat exchanger 20.

[0047] The power system of this invention includes an airflow distribution and quality control subsystem, which is equipped with an intelligent airflow distribution unit that can direct hydrogen to different fuel cell stacks as needed.

[0048] High-purity hydrogen flow path: Pure hydrogen produced by the decomposition of aluminum trihydride fuel tank 7 is preferentially supplied to the CO-sensitive low-temperature fuel cell stack 2.

[0049] Reformed hydrogen flow path: The hydrogen-rich gas (containing 0.52% CO) produced by the methanol steam reforming hydrogen production reactor 3 is specially supplied to the CO-resistant high-temperature fuel cell stack 1. This flow path is connected in series with a tank filled with active aluminum powder, the product of AlH3 decomposition. Hydrogen is produced by the hydrolysis reaction of elemental aluminum and water, which removes water vapor while increasing the amount of hydrogen produced and improving the hydrogen concentration.

[0050] Mixing / Switching Flow Path: Under specific operating conditions, some of the pure hydrogen generated from AlH3 can be mixed into the reformed gas to reduce the CO concentration or to provide a supplementary hydrogen source for the high-temperature fuel cell stack 1.

[0051] The above airflow distribution and quality control design increases the hydrogen concentration in the reformed gas, reduces the carbon monoxide concentration in the reformed gas, weakens the CO poisoning problem of high-temperature fuel cell stack 1, and ensures that both stacks can obtain the most suitable fuel, maximizing their performance and lifespan.

[0052] The power system described in this invention employs a hierarchical thermal energy management and cascade utilization network, and features a unique thermal integration scheme that distributes thermal energy of different grades as needed. Regarding the coordination of reaction conditions, the methanol-water solution evaporation and methanol reforming reaction are endothermic processes requiring a continuous external heat source to maintain the reaction temperature; similarly, aluminum hydride decomposition is also an endothermic process. The system integrates the thermal characteristics of methanol steam reforming (a strongly endothermic reaction), aluminum hydride decomposition (an endothermic reaction), and the power generation process of the high-temperature fuel cell stack 1 (an exothermic reaction), improving the overall energy efficiency of the system and achieving optimal energy cascade utilization and waste heat recovery. Through coupled heat exchanger technology, the reaction heat generated by the fuel cell and the catalytic combustion heat of unreacted exhaust gas are efficiently transferred to the methanol-water solution evaporation chamber, the methanol steam reforming hydrogen production reactor 3, and the decomposition chamber of the aluminum hydride fuel tank 7. The system adopts a layered thermal integration strategy, realizing the cascade utilization of energy of different grades.

[0053] Regarding the complementary characteristics of hydrogen sources, methanol reforming hydrogen production offers high capacity and stable hydrogen production, but its start-up speed is relatively slow (typically requiring several minutes to tens of minutes to reach a stable hydrogen production state) and its dynamic response to load changes is relatively sluggish. To address the system's cold start problem, the patented design incorporates a composite start-up preheating scheme. In the initial startup phase, an independent electric heating element rapidly heats the aluminum trihydride hydrogen storage module, enabling it to generate sufficient hydrogen within a short time (<1 minute), directly supplying the cryogenic fuel cell stack 2 for initial power generation. Once the cryogenic fuel cell stack 2 begins operation, it can provide energy for the entire system's output and overall startup, significantly reducing external energy consumption during system startup. Compared to traditional single methanol reforming systems, this startup strategy shortens system startup time and reduces startup energy consumption. By intelligently coupling these two hydrogen sources, a perfect combination of steady-state hydrogen supply and transient response is achieved.

[0054] The power system described in this invention possesses fault-tolerant and redundant control strategies. For example, when a subsystem (such as the high-temperature fuel cell stack 1) fails or requires maintenance, the system can switch to a mode using AlH3 as the primary hydrogen source while the low-temperature fuel cell stack 2 serves as the main power source, ensuring that the system does not completely fail. Conversely, it switches to the high-temperature fuel cell stack 1. This design greatly improves the reliability and availability of the power system, making it particularly suitable for applications with extremely high reliability requirements, such as communication base stations, emergency power supplies, and special vehicles.

[0055] See Figure 2 As shown, in the power system of the present invention, during the startup phase, the energy storage battery starts the electric heater 21 to heat the aluminum trihydride fuel tank 7. The high-purity hydrogen produced by the thermal decomposition reaction (1) of the aluminum trihydride fuel tank 7 enters the high-pressure hydrogen storage bottle 22 through the pipeline and enters the anode of the low-temperature fuel cell stack 2 through the high-pressure hydrogen pressure reducing valve 23. The cathode of the low-temperature fuel cell stack 2 is fed by the low-temperature fuel cell stack cathode gas pump 10. Hydrogen and oxygen undergo an electrochemical reaction (2) in the low-temperature fuel cell stack 2 to achieve external power supply. When the low-temperature fuel cell stack 2 starts running, it can provide energy for the entire system to output to the outside and start up as a whole, reducing the external energy consumption during the system startup process. The low-temperature fuel cell stack 2 generates electricity to start the reactor bed electric heater 16 and the circulating oil electric heater 12 of the methanol steam reforming hydrogen production reactor 3 for heating, thereby realizing the startup heating of the HT-PEMFC subsystem.

[0056] See Figure 3 As shown, in the power system of the present invention, after the HT-PEMFC subsystem is started and heated, the methanol-water solution in the methanol-water solution fuel tank 5 enters the coupling heat exchanger 15 through the methanol-water solution pump 6. After being heated and evaporated by the circulating oil, it enters the methanol-water vapor reforming hydrogen production reactor 3. The hydrogen-rich gas prepared by the reaction (3) first enters the aluminum powder reaction tank 17. The water vapor in the hydrogen-rich gas undergoes a hydrolysis reaction (4) with the aluminum powder to produce hydrogen. While removing the water vapor, the hydrogen concentration in the hydrogen-rich gas is increased. Subsequently, the hydrogen-rich gas enters the anode of the high-temperature fuel cell stack 1 after being cooled by heat exchange with the circulating oil through the coupling heat exchanger 15. The cathode of the high-temperature fuel cell stack 1 is fed by the high-temperature fuel cell stack cathode gas pump 8. Hydrogen and oxygen undergo an electrochemical reaction in the high-temperature fuel cell stack 1 to achieve external power supply.

[0057] The chemical reaction equations for the above-mentioned aluminum trihydride thermal decomposition hydrogen production method are as follows:

[0058] (1)

[0059] The chemical reaction equations in the above fuel cell stack are as follows:

[0060] 2H2 + O2 → 2H2O (2)

[0061] The chemical reaction equations for the above methanol steam reforming hydrogen production method are as follows:

[0062] CH3OH + H2O → CO2 + 3H2 (3)

[0063] The chemical reaction equations for the above aluminum hydrolysis hydrogen production method are as follows:

[0064] (4)

[0065] See Figure 3 As shown, in the power system of the present invention, the anode tail gas of the high-temperature fuel cell stack 1 contains a certain amount of unreacted hydrogen. This hydrogen is introduced into the catalytic combustion reactor 4 and mixed with the air provided by the combustion gas pump 9. After catalytic combustion, high-temperature tail gas is generated, which heats the methanol steam reforming hydrogen production reactor 3 to maintain its endothermic reforming reaction. The catalytic combustion reactor 4 and the methanol steam reforming hydrogen production reactor 3 are structurally coupled, and the principle is the same as that of the indirect heat exchanger. A reactor bed heater 16 is set in the intermediate heat-conducting wall for heating during the start-up stage. The tail gas, which still has residual heat after heat exchange, enters the gas heat exchanger 20 to heat the aluminum trihydride fuel tank 7 and maintain its endothermic reaction of hydrogen decomposition. As needed, the amount of gas entering the gas heat exchanger 20 can be adjusted by the combustion tail gas three-way valve 25 to control the heat exchange, thereby controlling the thermal decomposition rate of the aluminum trihydride fuel tank 7.

[0066] See Figure 3 As shown, in the power system of the present invention, the product of the thermal decomposition of aluminum trihydride in the aluminum trihydride fuel tank 7 is active aluminum powder, which is the packing material of the aluminum powder reactor 17 connected in series in the above-mentioned HT-PEMFC subsystem to remove water vapor in the reformed hydrogen-rich gas and increase the hydrogen concentration. It can be replaced in stages during operation, that is, after the aluminum trihydride fuel tank 7 is thermally decomposed and hydrogen is released, it becomes a new aluminum powder reactor 17, replacing the previously working aluminum powder reactor 17, so as to realize the cascade utilization of materials.

[0067] See Figure 2 , 3 As shown, in the power system of the present invention, the high-purity hydrogen produced by the thermal decomposition of aluminum trihydride fuel tank 7 enters the high-pressure hydrogen storage cylinder 22 through the pipeline for storage. Through the action of the high-pressure hydrogen pressure reducing valve 23 and the hydrogen flow regulating three-way valve 24, the high-purity hydrogen can be mixed with the hydrogen-rich gas after methanol water vapor reforming and then enter the anode of the high-temperature fuel cell stack 1 at appropriate operating stages of the system, thereby increasing the hydrogen concentration of the hydrogen-rich gas, reducing its carbon monoxide (CO) concentration, and improving the performance and lifespan of the high-temperature fuel cell stack 1.

[0068] See Figure 1As shown, in the power system of this invention, the HT-PEMFC subsystem maintains the stack operating temperature through circulating oil, and dissipates excess heat through the circulating oil radiator 13 and the circulating oil cooling fan 14. The low-temperature fuel cell stack 2 is an air-cooled cathode closed stack, that is, the cathode of the low-temperature fuel cell stack 2 is supplied with air through the low-temperature fuel cell stack cathode air pump 10, and the heat dissipation of the low-temperature fuel cell stack 2 is achieved by the stack cooling fan 18 to dissipate excess heat. This design separates the cathode air supply and the heat dissipation of the low-temperature fuel cell stack 2, avoiding the large volume of air blowing on the membrane electrode of the low-temperature fuel cell stack 2, which helps to improve the specific power and lifespan of the low-temperature fuel cell stack 2.

[0069] See Figure 4 As shown, in the power system of the present invention, the high-temperature fuel cell stack 1 and the low-temperature fuel cell stack 2 are respectively converted by the high-temperature fuel cell stack DC / DC converter 27 and the low-temperature fuel cell stack DC / DC converter 28, and can be connected in series or in parallel according to external needs.

[0070] Example

[0071] The power system described in this invention employs a multi-mode operation strategy to address performance and efficiency optimization requirements in different application scenarios. By monitoring key parameters such as load power demand, hydrogen source availability, and temperature status in real time, the system intelligently switches between the following operating modes:

[0072] Pure Aluminum Hydrogenation Mode: This mode is designed for rapid start-up and low-load operation. During initial system startup or when load demand is less than 30% of rated power, the system prioritizes using high-purity hydrogen produced by the thermal decomposition of aluminum hydride fuel tank 7 as fuel. This strategy fully leverages the advantages of aluminum hydride's rapid hydrogen production response and excellent low-temperature start-up characteristics, avoiding the low efficiency problem of the methanol steam reforming hydrogen production reactor 3 under low-load conditions. Simultaneously, it significantly reduces start-up time through the fast-track "aluminum hydride + low-temperature fuel cell stack," solving the core pain points of slow start-up and sluggish response in traditional reforming fuel cell systems.

[0073] Hybrid Hydrogen Supply Mode: When the system is operating in steady state or requires peak power (i.e., when the load demand rises to more than 30% of the rated power), the system automatically switches to hybrid hydrogen supply mode. In this mode, the methanol-water vapor reforming hydrogen production reactor 3 serves as the basic hydrogen source, providing a stable and continuous hydrogen-rich gas. The hydrogen-rich gas first enters the aluminum powder reaction tank 17, where the water vapor in the hydrogen-rich gas undergoes a hydrolysis reaction with the aluminum powder to produce hydrogen, removing water vapor while increasing the hydrogen concentration in the hydrogen-rich gas. The aluminum trihydride fuel tank 7 can serve as a peak-shaving hydrogen source, quickly responding to fluctuations in load demand. Simultaneously, it utilizes the cascade heat exchange of the high-temperature exhaust gas generated by the catalytic combustion of the high-temperature proton exchange membrane fuel cell subsystem to maintain the endothermic reaction of its thermal decomposition and hydrogen release, avoiding unnecessary parasitic power consumption. The mixing ratio of the two types of hydrogen is adjusted in real time by the hydrogen flow regulating three-way valve 24 to ensure that the CO concentration in the hydrogen entering the high-temperature fuel cell stack 1 is always maintained within the optimal tolerance range of the high-temperature proton exchange membrane fuel cell (0.1~1.5%). This system mode enables high-efficiency output from dual parallel stacks, achieving the highest energy efficiency and significantly enhanced resilience to load fluctuations, thus meeting instantaneous high-power demands. Methanol liquid fuel has high energy density, while aluminum trihydride solid hydrogen storage has high energy density; their combination allows the system to store far more energy than traditional batteries within limited space and weight, resulting in a substantial increase in range.

[0074] Methanol reforming-dominated mode: When the aluminum trihydride fuel tank 7 of the system is insufficient, the system switches to methanol reforming-dominated mode. In this mode, in order to extend the system's range, priority is given to ensuring the operation of the high-temperature proton exchange membrane fuel cell, while the low-temperature proton exchange membrane fuel cell stops working, and hydrogen is supplied only by the methanol steam reforming hydrogen production reactor 3.

[0075] See Figures 1-4As shown, in the power system of this invention, during the startup phase, the electric heater 21 is started by the energy storage battery to heat the aluminum trihydride fuel tank 7 to 120~160°C. The high-purity hydrogen (>99.9%) produced by the thermal decomposition reaction of the aluminum trihydride fuel tank 7 is discharged from the aluminum trihydride fuel tank outlet 54, enters the high-pressure hydrogen storage cylinder 22 through the pipeline for storage, and enters the low-temperature fuel cell stack anode inlet 37 through the high-pressure hydrogen pressure reducing valve 23. The cathode of the low-temperature fuel cell stack 2 is fed by the low-temperature fuel cell stack cathode gas pump 10, with hydrogen and oxygen being supplied. An electrochemical reaction occurs in the low-temperature fuel cell stack 2 to generate electricity. The electricity generated by the low-temperature fuel cell stack 2 starts the reactor bed heater 16 and circulating oil heater 12 of the methanol steam reforming hydrogen production reactor 3 for heating, raising the reactor bed temperature to 300°C and the high-temperature fuel cell stack 1 to its operating temperature of 160°C. After reaching the temperature, the methanol aqueous solution (60 vof%) in the methanol aqueous solution fuel tank 5 enters the coupling heat exchanger 15 through the methanol aqueous solution pump 6. After being heated and evaporated, the circulating oil enters the methanol-water vapor reforming hydrogen production reactor 3 through inlet 45. The hydrogen-rich gas produced by the reaction is discharged from outlet 46 of the methanol-water vapor reforming hydrogen production reactor. The hydrogen-rich gas after the reaction (~65% hydrogen, ~22% carbon dioxide, ~12% water vapor, ~1% carbon monoxide, etc.) enters the aluminum powder reaction tank 17 through inlet 47. The water vapor in the hydrogen-rich gas undergoes a hydrolysis reaction with the aluminum powder to produce hydrogen, removing water vapor while increasing the hydrogen concentration in the hydrogen-rich gas. The hydrogen-rich gas (~75.9% hydrogen, ~23% carbon dioxide, ~1.1% carbon monoxide) after the reaction is discharged from the outlet 48 of the aluminum powder reaction tank. The hydrogen-rich gas (~75.9% hydrogen, ~23% carbon dioxide, ~1.1% carbon monoxide) enters the coupling heat exchanger 15 from the hydrogen-rich gas inlet 43 of the coupling heat exchanger and exchanges heat with the circulating oil to cool down. Then it enters the anode of the high-temperature fuel cell stack 1 from the anode inlet 31 of the high-temperature fuel cell stack. The cathode of the high-temperature fuel cell stack 1 is fed by the high-temperature fuel cell stack cathode gas pump 8. Hydrogen and oxygen undergo an electrochemical reaction in the high-temperature fuel cell stack 1 to generate electricity.

[0076] Because hydrogen-rich gas, rather than pure hydrogen, is introduced into the anode of the high-temperature fuel cell stack 1, hydrogen-rich gas with a metering ratio of 1.15 to 1.4 times is typically used at the anode to ensure the power generation performance of the high-temperature fuel cell stack 1. Unreacted hydrogen is discharged from the anode outlet 32 ​​of the high-temperature fuel cell stack and enters the catalytic combustion reactor 4 from the anode tail gas inlet 50 of the high-temperature fuel cell stack. Under the action of a special catalyst, it undergoes flameless combustion, producing high-temperature flue gas at 400 to 500°C. This flue gas is used to maintain the temperature requirements of the methanol steam reforming hydrogen production reactor 3. After heat exchange, the flue gas temperature drops to 150 to 200°C and is discharged from the catalytic combustion reactor outlet 51. It then enters the gas heat exchanger 20 from the gas heat exchanger inlet 52 and exchanges heat with the aluminum trihydride fuel tank 7 to meet the temperature requirements of the aluminum trihydride thermal decomposition hydrogenation reaction. The amount of gas entering the gas heat exchanger 20 can be adjusted by the combustion tail gas three-way valve 25 to control the heat exchange, thereby controlling the thermal decomposition temperature (120 to 160°C) of the aluminum trihydride fuel tank 7.

[0077] The power system of this invention carries 50 kg of aluminum trihydride (AlH3) and 100 L of methanol aqueous solution (60% volume concentration), maintaining the temperature of the aluminum trihydride fuel tank 7 at 120-160°C and the pressure inside the tank between 0.1-0.4 MPa, maintaining the bed temperature of the methanol steam reforming hydrogen production reactor 3 at 220-300°C, the circulating oil temperature at 150-155°C, the temperature of the low-temperature fuel cell stack 2 at 50-70°C, and the temperature of the high-temperature fuel cell stack 1 at 160-170°C, with both stacks operating at 400 mA / cm². 2 At the operating point, the combined output power can reach 20kW, and it can operate stably and continuously for 8~10 hours.

[0078] This invention discloses an intelligent power system for solid-liquid fuel hybrid hydrogen production and high- and low-temperature fuel cell coupling. It combines methanol reforming for hydrogen production with aluminum trihydride hydrogen production, and simultaneously couples high-temperature and low-temperature proton exchange membrane fuel cells, forming a powerful hybrid power system. This dual-hydrogen source synergistic coupling mechanism effectively solves the inherent limitations of a single hydrogen source in fuel cell applications through complementary reaction characteristics and energy cascade utilization. It breaks the traditional system architecture of a single hydrogen source and a single type of fuel cell, creatively integrating two hydrogen production methods and two fuel cell stack technologies. Through the coordinated management of energy flow, material flow, and information flow, it achieves comprehensive breakthroughs in system efficiency, dynamic response, fuel adaptability, and reliability.

[0079] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A smart power system for solid-liquid fuel hybrid hydrogen production and high / low temperature fuel cell coupling, characterized in that: The system comprises a trihydrogen aluminum fuel tank, a methanol water vapor reforming hydrogen production reactor, a high-temperature proton exchange membrane fuel cell stack and a low-temperature proton exchange membrane fuel cell stack. An outlet of the trihydrogen aluminum fuel tank is connected with an inlet of a high-pressure hydrogen storage bottle through a pipeline; an outlet of the high-pressure hydrogen storage bottle is connected with an anode inlet of the low-temperature proton exchange membrane fuel cell stack through a pressure reducing valve; a cathode inlet of the low-temperature proton exchange membrane fuel cell stack is connected with a low-temperature fuel cell stack cathode gas pump through a pipeline; an electric output end of the low-temperature proton exchange membrane fuel cell stack is electrically connected with a reactor bed layer electric heater of the methanol water vapor reforming hydrogen production reactor; the electric output end of the low-temperature proton exchange membrane fuel cell stack is electrically connected with a circulating oil electric heater; the electric output end of the low-temperature proton exchange membrane fuel cell stack is electrically connected with a low-temperature fuel cell stack DC / DC converter. An outlet of a methanol water solution fuel tank is connected with a methanol water solution inlet of a coupling heat exchanger through a methanol water solution pump; a methanol water solution outlet of the coupling heat exchanger is connected with an inlet of the methanol water vapor reforming hydrogen production reactor; an outlet of the methanol water vapor reforming hydrogen production reactor is connected with an inlet of an aluminum powder reaction tank; an outlet of the aluminum powder reaction tank is connected with a hydrogen-rich gas inlet of the coupling heat exchanger; a hydrogen-rich gas outlet of the coupling heat exchanger is connected with an anode inlet of the high-temperature proton exchange membrane fuel cell stack; a high-temperature fuel cell stack cathode gas pump is connected with a cathode inlet of the high-temperature proton exchange membrane fuel cell stack; an electric output end of the high-temperature proton exchange membrane fuel cell stack is electrically connected with a high-temperature fuel cell stack DC / DC converter. An anode outlet of the high-temperature proton exchange membrane fuel cell stack is connected with an anode tail gas inlet of a catalytic combustion reactor through a pipeline; a combustion gas pump is connected with an air inlet of the catalytic combustion reactor through a pipeline; an outlet of the catalytic combustion reactor is connected with an inlet of a gas heat exchanger through a combustion tail gas three-way valve; an outlet of the gas heat exchanger is connected with a tail gas discharge pipeline; the gas heat exchanger is heat-coupled with the trihydrogen aluminum fuel tank. A hydrogen flow regulating three-way valve is arranged on an outlet pipeline of the pressure reducing valve; one outlet of the hydrogen flow regulating three-way valve is connected with one inlet of a gas mixing three-way valve through a pipeline; an outlet of the gas mixing three-way valve is connected with a pipeline between a hydrogen-rich gas outlet of the coupling heat exchanger and an anode inlet of the high-temperature proton exchange membrane fuel cell stack.

2. The solid-liquid fuel composite hydrogen production and high-low temperature fuel cell coupled intelligent power supply system according to claim 1, characterized in that, The aluminum powder reaction tank is a detachable independent tank; after hydrogen is discharged, the tank of the trihydrogen aluminum fuel tank can be used as the aluminum powder reaction tank in structure.

3. The solid-liquid fuel composite hydrogen production and high-low temperature fuel cell coupled intelligent power supply system according to claim 1, characterized in that, The circulating oil electric heater is connected with a circulating oil radiator, and an external fan is arranged outside the circulating oil radiator; an electric heater is arranged outside the low-temperature proton exchange membrane fuel cell stack, and an external fan is arranged outside the electric heater.

4. The solid-liquid fuel composite hydrogen production and high-low temperature fuel cell coupled intelligent power supply system according to claim 1, characterized in that, The hydrogen-rich reforming gas generated by the methanol steam reforming reactor is supplied to the high-temperature proton exchange membrane fuel cell stack as fuel, and the volume fraction of hydrogen in the hydrogen-rich gas is >60%. The high-purity hydrogen generated by thermal decomposition of the aluminum hydride fuel tank is supplied to the low-temperature proton exchange membrane fuel cell stack as fuel.

5. The solid-liquid fuel composite hydrogen production and high-low temperature fuel cell coupled intelligent power supply system according to claim 1, characterized in that, The operation strategy of the intelligent power supply system includes a pure aluminum hydride mode for quick start and low load, a mixed hydrogen supply mode for steady state and high load, and a methanol reforming dominant mode for insufficient aluminum hydride reserves. In the pure aluminum hydride mode, the electric heater provided on the aluminum hydride fuel tank is controlled to start heating, the hydrogen flow regulating three-way valve is controlled to regulate the flow of high-purity hydrogen generated by thermal decomposition of the aluminum hydride fuel tank, the high-purity hydrogen flows through the high-pressure hydrogen storage bottle, the high-pressure hydrogen reducing valve, and the hydrogen flow regulating three-way valve in sequence, and is finally supplied to the anode of the low-temperature proton exchange membrane fuel cell stack. The cathode gas pump of the low-temperature proton exchange membrane fuel cell stack is controlled to operate to supply gas to the cathode of the stack. The electric energy generated by the low-temperature proton exchange membrane fuel cell stack is distributed to the reactor bed electric heater and the circulating oil electric heater of the methanol steam reforming reactor to provide heat for subsequent start-up of the system. In the mixed hydrogen supply mode, the methanol steam reforming reactor is maintained in operation, the hydrogen-rich gas generated by the methanol steam reforming reactor flows through the aluminum powder reaction tank and the coupled heat exchanger in sequence, and is then supplied to the anode of the high-temperature proton exchange membrane fuel cell stack. The hydrogen flow regulating three-way valve and the gas mixing three-way valve are controlled to supply a part of the high-purity hydrogen generated by the aluminum hydride fuel tank to the anode of the low-temperature proton exchange membrane fuel cell stack, and to mix another part of the high-purity hydrogen with the hydrogen-rich gas flowing to the anode of the high-temperature proton exchange membrane fuel cell stack to form a mixed gas and increase the hydrogen concentration. The anode tail gas of the high-temperature proton exchange membrane fuel cell stack is introduced into the catalytic combustion reactor for combustion, and the high-temperature flue gas generated by the combustion provides heat for the methanol steam reforming reactor. The high-temperature tail gas after combustion is further supplied to the aluminum hydride fuel tank through the gas heat exchanger. In the methanol reforming dominant mode, the hydrogen flow regulating three-way valve is controlled to close the flow path to the low-temperature proton exchange membrane fuel cell stack. The methanol steam reforming reactor is maintained in operation, and in this operation mode, the hydrogen-rich gas generated by the methanol steam reforming reactor is the only hydrogen source, flows through the aluminum powder reaction tank and the coupled heat exchanger, and is then supplied to the anode of the high-temperature proton exchange membrane fuel cell stack. The anode tail gas of the high-temperature proton exchange membrane fuel cell stack is introduced into the catalytic combustion reactor for combustion, and the high-temperature flue gas generated by the combustion provides heat for the methanol steam reforming reactor.

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