A dual-pressure liquid hydrogen hydrogenation station system coupled with an organic rankine cycle

Abstract

This invention provides a dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle (ORC), comprising a liquid hydrogen supply unit, an ORC power generation unit, a dual-pressure refueling unit, and a pre-cooling unit. The liquid hydrogen pipeline is coupled to the ORC via a coupling heat exchanger. Supercritical hydrogen discharged from a cryogenic liquid hydrogen pump serves as a cold source, flowing through the coupling heat exchanger to condense the ORC organic working fluid. The working fluid generates electricity through pumping, evaporation, and expansion. The hydrogen, after absorbing heat, is completely vaporized into room-temperature, high-pressure gas by a vaporizer and enters different pressure-level delivery channels. One channel stores the gas in a first buffer tank and then directly delivers it to a 35 MPa refueling terminal. The other channel undergoes secondary pressurization by a high-pressure compressor and is stored in a second buffer tank before being delivered to a 70 MPa refueling terminal. Both channels are coupled to a liquid hydrogen pre-cooling unit, utilizing a cryogenic liquid hydrogen branch to deeply cool the hydrogen to be refueled.

Description

Technical Field

[0001] This invention belongs to the technical field of liquid hydrogen refueling stations and relates to a dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle. Background Technology

[0002] With the commercialization of hydrogen fuel cell vehicles, hydrogen refueling stations are rapidly developing as a key infrastructure. Compared to gaseous hydrogen refueling stations, liquid hydrogen refueling stations have become an important direction for industry development due to their significant advantages such as high storage and transportation density, small footprint, and suitability for large-scale storage and transportation.

[0003] In liquid hydrogen refueling stations, liquid hydrogen is stored at low pressure and low temperature (approximately -253°C), while on-board hydrogen storage cylinders are mainly in a high-pressure gaseous state of 35MPa or 70MPa. To achieve the conversion from storage to refueling, the industry has attempted a "vaporization followed by compression" technical approach. However, due to issues such as high compression energy consumption, high equipment maintenance costs, and the need for multi-stage cooling, this method has been gradually replaced by the "cryogenic liquid hydrogen pump pressurization and vaporization" method. This method directly pressurizes liquid hydrogen to the target pressure using a liquid hydrogen pump before vaporization, reducing system energy consumption and complexity, and is currently the mainstream method for producing high-pressure gaseous hydrogen.

[0004] To address the issues of cold energy utilization and efficiency in the operation of liquid hydrogen refueling stations, existing technologies have been explored to some extent. For example, a system and method for cold energy recovery and utilization in liquid hydrogen refueling stations (CN113531388A) recovers and utilizes the cold energy during the liquid hydrogen vaporization process through a circulating cooling process, reducing dependence on external refrigeration units; a gas-liquid mixed refueling station system for cold energy recovery and cascade utilization (CN121206373A) attempts to use flash evaporation cold energy in a cascade manner to cool high-pressure hydrogen and the compression process; a BOG recovery and utilization system and method for liquid hydrogen refueling stations (CN119468042A) focuses on BOG recovery, utilizing cold energy to liquefy nitrogen and combining it with metal hydride separation technology to achieve zero emissions; and an operation method and system for a liquid-gas dual-mode liquid hydrogen refueling station (CN121429935A) proposes a dynamic scheduling scheme with dual-pump series pressurization and liquid-gas dual-mode operation.

[0005] Meanwhile, most existing hydrogen refueling stations are designed for a single pressure level, making it difficult to meet the refueling needs of both 35MPa and 70MPa on-board hydrogen storage cylinders, which are the two mainstream pressure types. To achieve dual-pressure refueling, two independent power supply and refueling systems are often required, doubling equipment investment and increasing floor space. Furthermore, liquid hydrogen, after being pressurized by a high-pressure pump, is at an extremely low temperature. Directly entering the vaporizer can easily cause rapid icing on the vaporizer surface, exacerbating the vaporizer's heat load, reducing vaporization efficiency, and even shortening its lifespan, thus affecting system operational stability.

[0006] However, existing liquid hydrogen refueling stations have the following main problems in actual operation: 1. Significant waste of cold energy: Liquid hydrogen is typically stored at an ultra-low temperature of -253°C in tanks. Before refueling, it needs to be converted into ambient temperature gaseous hydrogen by absorbing heat through an ambient temperature vaporizer. During this process, the enormous amount of high-grade cold energy contained in the liquid hydrogen is usually released directly into the environment, resulting in not only a huge waste of energy but also a high risk of severe icing and fogging on the vaporizer surface, affecting the heat transfer efficiency and operational stability of the equipment.

[0007] 2. High system energy consumption: According to the SAE J2601 refueling protocol, in order to ensure the safety of the on-board hydrogen storage tank and the refueling speed, the hydrogen added to the car needs to be pre-cooled to -40℃ (T40 level) before refueling. Traditional hydrogen refueling stations are usually equipped with high-power compression refrigeration units (chilled water units) to provide cooling, which results in extremely high power consumption and high operating costs for hydrogen refueling stations.

[0008] 3. Insufficient pressure adaptability: Some existing hydrogen refueling station systems have a relatively simple design, making it difficult to efficiently handle the flexible switching between two pressure levels of 35 MPa and 70 MPa, or there is a problem of excessive secondary compression energy consumption during the switching process.

[0009] Therefore, how to efficiently recover and utilize the cold energy in the liquid hydrogen vaporization process and organically combine it with the precooling and power system of the hydrogen refueling station to develop an energy-saving, efficient liquid hydrogen refueling station system with multi-pressure level refueling capabilities is a technical problem that urgently needs to be solved. Summary of the Invention

[0010] To overcome the shortcomings of existing liquid hydrogen refueling stations, such as wasted cold energy, high system energy consumption, and poor pressure adaptability, the present invention aims to provide a dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle. By recovering the cold energy from liquid hydrogen vaporization and constructing a multi-pressure integrated refueling system, the system achieves energy cascade utilization, reduces operating energy consumption, and meets the mixed refueling needs of 35 MPa commercial vehicles and 70 MPa passenger vehicles.

[0011] The present invention is achieved by at least one of the following technical solutions.

[0012] A dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle includes: a liquid hydrogen supply and vaporization unit, an organic Rankine cycle power generation unit, a dual-pressure refueling unit, and a precooling unit; The liquid hydrogen supply and vaporization unit includes a liquid hydrogen tanker truck, a liquid hydrogen storage tank, a cryogenic liquid hydrogen pump, a coupling heat exchanger, and a vaporizer; the liquid hydrogen storage tank, the cryogenic liquid hydrogen pump, the coupling heat exchanger, and the vaporizer are connected in sequence. The organic Rankine cycle power generation unit is connected to the coupling heat exchanger to form a closed-loop circuit that generates electricity using liquid hydrogen cold energy. The dual-pressure filling unit is connected to the outlet end of the vaporizer; The precooling unit is coupled to the end of the dual-pressure refueling unit and uses liquid hydrogen drawn from a cryogenic liquid hydrogen pump to cool the hydrogen gas before refueling. The supercritical hydrogen discharged by the cryogenic liquid hydrogen pump serves as a cold source, flowing through the coupling heat exchanger to condense the organic working fluid in the organic Rankine cycle power generation unit; the hydrogen gas, after absorbing heat, is vaporized into room temperature gas by the vaporizer and then diverted.

[0013] Furthermore, the Organic Rankine Cycle (ORC) power generation unit includes an ORC circulating pump, an ORC heat exchanger, an ORC evaporator, and an ORC expander, wherein the ORC circulating pump, ORC heat exchanger, ORC evaporator, ORC expander, and coupling heat exchanger are sequentially connected to form a closed-loop circulation circuit.

[0014] Furthermore, the outlet of the ORC expander is connected to the coupling heat exchanger through the hot side channel of the ORC heat exchanger; the outlet of the ORC circulating pump is connected to the ORC evaporator through the cold side channel of the ORC heat exchanger, using the waste heat of the expanded exhaust gas to preheat the liquid working fluid before entering the evaporator.

[0015] Furthermore, the ORC expander is connected to a generator, which uses the expansion of the organic working fluid to generate electricity.

[0016] Furthermore, the dual-pressure filling unit includes a first filling channel and a second filling channel arranged in parallel; The first refueling channel includes a first buffer tank connected to the vaporizer, a first heat exchanger connected to the outlet of the first buffer tank, and a hydrogen dispenser connected to the outlet of the first heat exchanger; the second refueling channel includes a high-pressure compressor and a condenser connected to the vaporizer, a second buffer tank connected to the outlet of the condenser, a second heat exchanger connected to the outlet of the second buffer tank, and a hydrogen dispenser connected to the outlet of the second heat exchanger.

[0017] Furthermore, the precooling unit is a refrigerant outlet branch led out from the pipeline between the cryogenic liquid hydrogen pump and the coupled heat exchanger. The refrigerant outlet branch is connected to the refrigerant inlets of the first heat exchanger and the second heat exchanger respectively, and is configured to use cryogenic liquid hydrogen to exchange heat with hydrogen in the channel.

[0018] Furthermore, the outlet of the cryogenic liquid hydrogen pump is divided into a main path and a reflux bypass. The reflux bypass is equipped with a first valve to regulate the flow rate of the liquid hydrogen branch. The main path is equipped with a second valve, the rear end of which is connected to the liquid hydrogen side inlet of the coupling heat exchanger. The liquid hydrogen side outlet of the coupling heat exchanger is connected to the vaporizer to completely vaporize the reheated liquid hydrogen into room temperature high-pressure gas.

[0019] Furthermore, a refrigerant diversion node is provided on the main pipeline between the outlet of the cryogenic liquid hydrogen pump and the second valve; the refrigerant diversion node leads out two parallel precooling branches: a third valve is provided on the first precooling branch, the outlet of the third valve is connected to the refrigerant inlet of the first heat exchanger, and the flow rate of liquid hydrogen entering the first heat exchanger is controlled by adjusting the opening of the third valve, so as to regulate the hydrogen temperature before the hydrogen dispenser; a fifth valve is provided on the second precooling branch, the outlet of the fifth valve is connected to the refrigerant inlet of the second heat exchanger, and the flow rate of liquid hydrogen entering the second heat exchanger is controlled by adjusting the opening of the fifth valve, so as to regulate the hydrogen temperature before the hydrogen dispenser.

[0020] Furthermore, a first temperature transmitter and a second temperature transmitter are installed on the hydrogen refueling machine inlet pipeline to detect the temperature of hydrogen before refueling.

[0021] Furthermore, a pressure transmitter is installed on the outlet pipeline of the cryogenic liquid hydrogen pump to detect the pump outlet pressure.

[0022] Compared with the prior art, the beneficial effects of the present invention are: 1) This invention transfers high-grade cold energy from the liquid hydrogen vaporization process to the ORC power generation unit through a coupling heat exchanger, and drives the ORC expander to generate electricity. This not only increases the energy utilization pathways of the hydrogen refueling station and realizes the resource recovery of cold energy, but also feeds back the generated electricity to the station's electricity consumption, reducing the hydrogen refueling station's dependence on the external power grid and indirectly improving operational efficiency.

[0023] 2) Based on the process of pre-cooling to a specified temperature before hydrogen refueling, the cryogenic liquid hydrogen output by the system's own cryogenic liquid hydrogen pump is used as the pre-cooling refrigerant to directly and accurately pre-cool the terminal hydrogen in the two refueling channels of 35MPa and 70MPa. This eliminates the need for additional expensive independent refrigeration units, reduces the power consumption and initial equipment investment cost of the hydrogen refueling station, and simplifies the system structure.

[0024] 3) This invention adopts a dual-module architecture of "direct pump supply" and "pump + compressor combined supply". It designs two independent refueling channels for hydrogen refueling vehicles with different pressure levels, realizing flexible switching between 35MPa and 70MPa refueling modes. It can accurately match the optimal energy supply mode according to the vehicle's needs, ensuring refueling efficiency while taking into account the system energy efficiency under different operating conditions, thus improving the adaptability and operational flexibility of hydrogen refueling stations. Attached Figure Description

[0025] Figure 1 This is a schematic diagram of a dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle, as disclosed in an embodiment of the present invention.

[0026] Figure 2 This is a schematic diagram of the organic Rankine cycle principle in an embodiment of the present invention.

[0027] Figure 3 This is a schematic diagram of the system operation unit of the present invention.

[0028] In the diagram, 1. Liquid hydrogen tanker truck, 2. Liquid hydrogen storage tank, 3. Cryogenic liquid hydrogen pump, 4. First valve, 5. Second valve, 7. Vaporizer, 8. First buffer tank, 9. First heat exchanger, 10. Third valve, 11. Fourth valve, 12. High-pressure compressor, 13. Condenser, 14. Second buffer tank, 15. Second heat exchanger, 16. Fifth valve, 17. Sixth valve, 18. 35MPa hydrogen dispenser, 19. 70MPa hydrogen dispenser, 61. Coupled heat exchanger, 62. ORC circulating pump, 63. ORC heat exchanger, 64. ORC evaporator, 65. ORC expander, 101. Pressure transmitter, 102. First temperature transmitter, 103. Second temperature transmitter. Detailed Implementation

[0029] The following specific examples illustrate the implementation of the present invention. Those skilled in the art can easily understand other advantages and effects of the present invention from the content disclosed in this specification. The present invention can also be implemented or applied through other different specific embodiments, and various details in this specification can also be modified or changed based on different viewpoints and applications without departing from the spirit of the present invention.

[0030] It should be noted that the process equipment or apparatus not specifically mentioned in the following embodiments are all conventional equipment or apparatus in the art.

[0031] It should be noted that the terms "comprising" and "having," and any variations thereof, are intended to cover non-exclusive inclusion. For example, a process, method, system, product, or apparatus that includes a series of steps or units is not necessarily limited to those steps or units explicitly listed, but may include other steps or units not explicitly listed or inherent to these processes, methods, products, or apparatuses. Furthermore, unless otherwise stated, the numbering of each method step is merely a convenient tool for identifying each method step, and not intended to limit the order of the method steps or define the scope of the invention. Changes or adjustments to their relative relationships, without substantially altering the technical content, should also be considered within the scope of the invention.

[0032] Furthermore, it should be noted that the terms "first," "second," etc., used in this invention are used to distinguish similar objects and are not necessarily used to describe a specific order or sequence. It should be understood that such data can be interchanged where appropriate so that the embodiments of the invention described herein can be implemented in orders other than those illustrated or described herein. Moreover, unless otherwise expressly specified and limited, the terms "installed," "connected," and "linked" should be interpreted broadly, for example, referring to a fixed connection or a detachable connection; a direct connection or an indirect connection via an intermediate medium; or a connection within two components.

[0033] like Figures 1-3 As shown, the present invention provides a dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle, the system comprising a liquid hydrogen supply and vaporization unit, an organic Rankine cycle (ORC) power generation unit 6, a dual-pressure refueling unit, and a pre-cooling unit.

[0034] In one embodiment, the liquid hydrogen supply and vaporization unit includes a system equipped with a liquid hydrogen tanker 1, a liquid hydrogen storage tank 2, and a cryogenic liquid hydrogen pump 3. The outlet of the liquid hydrogen storage tank 2 is connected to the cryogenic liquid hydrogen pump 3 via a cryogenic pipeline. The outlet of the cryogenic liquid hydrogen pump 3 is divided into a main line and a return bypass line. The return bypass line is equipped with a first valve 4 for regulating the flow rate of the liquid hydrogen branch line. The main line is equipped with a pressure transmitter 101 and a second valve 5. The cryogenic liquid hydrogen pump 3 is connected to the liquid hydrogen side inlet of the coupling heat exchanger 61 through the second valve 5. The pressure transmitter 101 is located on the outlet pipeline of the cryogenic liquid hydrogen pump 3 for detecting the pump outlet pressure. The liquid hydrogen side outlet of the coupling heat exchanger 61 is connected to a vaporizer 7 for completely vaporizing the reheated liquid hydrogen into a room temperature high-pressure gas.

[0035] The Organic Rankine Cycle (ORC) power generation unit 6 is thermally coupled to the liquid hydrogen pipeline via a coupling heat exchanger 61. This forms a closed-loop circuit, including an ORC circulating pump 62, an ORC heat exchanger 63, an ORC evaporator 64, and an ORC expander 65 connected in sequence via pipelines. The coupling heat exchanger 61 serves as the condenser end of this cycle, with its working fluid inlet connected to the hot-side outlet of the ORC heat exchanger 63, and its working fluid outlet connected to the inlet of the ORC circulating pump 62. The outlet of the ORC expander 65 is connected to the coupling heat exchanger 61 via the hot-side channel of the ORC heat exchanger 63, and the outlet of the ORC circulating pump 62 is connected to the ORC evaporator 64 via the cold-side channel of the ORC heat exchanger 63. This regenerative structure utilizes the waste heat from the expanded exhaust gas to preheat the liquid working fluid before it enters the evaporator, thereby improving the cycle's thermal efficiency.

[0036] The ORC expander 65 is connected to a generator and is configured to generate electricity by expanding the organic working fluid. The electrical energy output by the ORC expander 65 can supply power to the hydrogen refueling station. This structure uses supercritical liquid hydrogen discharged from the cryogenic liquid hydrogen pump 3 as a cold source to condense the organic working fluid, and uses ambient heat or waste heat to evaporate the working fluid in the ORC evaporator 64, thereby generating electricity through the expansion.

[0037] In one embodiment, the dual-pressure refueling unit includes a first refueling channel and a second refueling channel arranged in parallel. The outlet end of the vaporizer 7 flows into the first refueling channel and the second refueling channel through a pipeline. The first refueling channel (35MPa level) includes a first buffer tank 8, a first heat exchanger 9, a fourth valve 11, a first temperature transmitter 102, and a 35MPa hydrogen dispenser 18 connected in sequence. The second refueling channel (70MPa level) includes a high-pressure compressor 12, a condenser 13, a second buffer tank 14, a second heat exchanger 15, a sixth valve 17, a second temperature transmitter 103, and a 70MPa hydrogen dispenser 19 connected in sequence. The high-pressure compressor 12 and the condenser 13 form a compressor unit used to further pressurize and cool the vaporized hydrogen; the condenser 13 cools the hydrogen discharged from the high-pressure compressor 12. A first temperature transmitter 102 is installed on the inlet pipeline of the 35 MPa hydrogen refueling machine 18, and a second temperature transmitter 103 is installed on the inlet pipeline of the 70 MPa hydrogen refueling machine 19, for detecting the temperature of hydrogen before refueling.

[0038] In terms of system operation logic, the supercritical hydrogen gas discharged from the cryogenic liquid hydrogen pump 3 flows through the coupled heat exchanger 61 as a cold source, absorbing heat and condensing the organic working fluid in the organic Rankine cycle power generation unit. After absorbing and reheating, the hydrogen gas then enters the vaporizer 7 and is completely vaporized into room temperature gas. The vaporized hydrogen gas is split: one path enters the first refueling channel, is stored and regulated by the first buffer tank 8, and is then transported to the 35MPa refueling terminal; the other path enters the second refueling channel, is pressurized again by the high-pressure compressor 12, is stored and regulated by the second buffer tank 14, and is then transported to the 70MPa refueling terminal.

[0039] To achieve precise pre-cooling during refueling, a refrigerant diversion node is installed on the main pipeline between the outlet of the cryogenic liquid hydrogen pump 3 and the second valve 5. Two parallel pre-cooling branches are branched off from this node as pre-cooling units: the first pre-cooling branch has a third valve 10, whose outlet is connected to the refrigerant inlet of the first heat exchanger 9. Adjusting the opening of the third valve 10 controls the flow rate of liquid hydrogen entering the first heat exchanger 9, thereby regulating the hydrogen temperature before the 35MPa hydrogen dispenser 18. The second pre-cooling branch has a fifth valve 16, whose outlet is connected to the refrigerant inlet of the second heat exchanger 15. Adjusting the opening of the fifth valve 16 controls the flow rate of liquid hydrogen entering the second heat exchanger 15, thereby regulating the hydrogen temperature before the 70MPa hydrogen dispenser 19. This system, by independently adjusting the third valve 10 and the fifth valve 16, enables independent and precise control of the refueling temperature of the two refueling branches.

[0040] The system's operation mainly includes the following five steps: Step 1: Unload liquid hydrogen from liquid hydrogen tanker 1 into liquid hydrogen storage tank 2. Start cryogenic liquid hydrogen pump 3 to extract liquid hydrogen from storage tank 2 and pressurize it to 45 MPa. Adjust the opening of the first valve 4 according to the pressure detection value of pressure transmitter 101 to perform backflow bypass, so that the pump outlet pressure is stabilized at 45 MPa. Open the second valve 5 on the main line, and cryogenic high-pressure liquid hydrogen enters the coupling heat exchanger 61. At this time, liquid hydrogen acts as a high-grade cold source and exchanges heat with the organic working fluid on the other side of the coupling heat exchanger.

[0041] Step 2: The Organic Rankine Cycle (ORC) power generation unit operates. In the coupled heat exchanger 61, liquid hydrogen absorbs heat and its temperature rises, while the gaseous organic working fluid releases latent heat and is condensed into a liquid state. The liquid working fluid is drawn in and pressurized by the ORC circulation pump 62, and sent to the ORC heat exchanger 63 for preheating. It then enters the ORC evaporator 64 to absorb ambient heat and evaporate into high-temperature, high-pressure steam. The steam enters the ORC expander 65 to expand and do work, driving the generator to generate electricity. The expanded exhaust gas is reheated by the ORC heat exchanger 63 and returns to the coupled heat exchanger 61 for condensation, completing the closed-loop cycle.

[0042] Step 3: Hydrogen vaporization and distribution. The reheated liquid hydrogen flowing out from the coupling heat exchanger 61 enters the vaporizer 7, absorbs heat from the ambient air, and completely transforms into a room-temperature, high-pressure gas. The vaporized hydrogen is then diverted at the vaporizer outlet according to the refueling command: if a 35 MPa refueling is required, the hydrogen flows to the first refueling channel; if a 70 MPa refueling is required, the hydrogen flows to the second refueling channel.

[0043] Step 4: 35 MPa vehicle refueling and independent temperature control. Hydrogen gas, after being pressurized by the first buffer tank 8, enters the first heat exchanger 9. The first temperature transmitter 102 detects the hydrogen temperature before refueling. If the temperature exceeds the requirements of the refueling agreement... At 40 ℃, the third valve 10 is opened, allowing cryogenic liquid hydrogen to be diverted from the pump and flow into the refrigerant side of the first heat exchanger 9, where it exchanges heat with the hydrogen side to cool down. Once the hydrogen temperature reaches the refueling requirement, the fourth valve 11 is opened, and the vehicle is refueled through the 35 MPa hydrogen refueling machine 18.

[0044] Step 5: 70 MPa Vehicle Refueling and Independent Temperature Control. Hydrogen enters the high-pressure compressor 12 for secondary pressurization, for example, to 90 MPa. The pressurized high-temperature gas is cooled to room temperature by the condenser 13 and then stored in the second buffer tank 14. During refueling, the high-pressure hydrogen enters the second heat exchanger 15, and the hydrogen temperature before refueling is detected by the second temperature transmitter 103. When cooling is required, the fifth valve 16 is opened, allowing cryogenic liquid hydrogen to be diverted from the pump and flow into the refrigerant side of the second heat exchanger 15 for pre-cooling. Once the hydrogen temperature reaches the refueling requirement, the sixth valve 17 is opened, and the vehicle is refueled through the 70 MPa hydrogen dispenser 19.

[0045] Through the above steps, this invention enables the cascaded utilization of liquid hydrogen cold energy and flexible switching between two pressure levels, thereby reducing the operating energy consumption of hydrogen refueling stations.

[0046] The preferred embodiments of the present invention disclosed above are merely illustrative of the invention. These preferred embodiments do not exhaustively describe all details, nor do they limit the invention to the specific implementations described. Clearly, many modifications and variations can be made based on the content of this specification. This specification selects and specifically describes these embodiments to better explain the principles and practical applications of the invention, enabling those skilled in the art to better understand and utilize the invention.

Claims

1. A dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle, characterized in that, include: Liquid hydrogen supply and vaporization unit, organic Rankine cycle power generation unit, dual-pressure refueling unit and precooling unit; The liquid hydrogen supply and vaporization unit includes a liquid hydrogen tanker (1), a liquid hydrogen storage tank (2), a cryogenic liquid hydrogen pump (3), a coupling heat exchanger (61), and a vaporizer (7); the liquid hydrogen storage tank (2), the cryogenic liquid hydrogen pump (3), the coupling heat exchanger (61), and the vaporizer (7) are connected in sequence. The organic Rankine cycle power generation unit is connected to the coupling heat exchanger (61) to form a closed loop that generates electricity using liquid hydrogen cold energy. The dual-pressure filling unit is connected to the outlet end of the vaporizer (7); The precooling unit is coupled to the end of the dual-pressure refueling unit and uses the liquid hydrogen drawn out by the cryogenic liquid hydrogen pump (3) to cool the hydrogen before refueling; The supercritical hydrogen discharged by the cryogenic liquid hydrogen pump (3) flows through the coupling heat exchanger (61) as a cold source, causing the organic working fluid in the organic Rankine cycle power generation unit to condense; the hydrogen gas after absorbing heat is vaporized into room temperature gas by the vaporizer (7) and then diverted.

2. The dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle according to claim 1, characterized in that, The organic Rankine cycle power generation unit includes an ORC circulating pump (62), an ORC heat exchanger (63), an ORC evaporator (64), and an ORC expander (65), wherein the ORC circulating pump (62), ORC heat exchanger (63), ORC evaporator (64), ORC expander (65), and coupling heat exchanger (61) are connected in sequence to form a closed loop.

3. The dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle according to claim 2, characterized in that, The outlet of the ORC expander (65) is connected to the coupling heat exchanger (61) through the hot side channel of the ORC heat exchanger (63); the outlet of the ORC circulating pump (62) is connected to the ORC evaporator (64) through the cold side channel of the ORC heat exchanger (63), and the liquid working fluid before entering the evaporator is preheated by the waste heat of the expanded exhaust gas.

4. The dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle according to claim 1, characterized in that, The ORC expander (65) is connected to a generator and generates electricity by expanding the organic working fluid.

5. A dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle according to claim 1, characterized in that, The dual-pressure filling unit includes a first filling channel and a second filling channel arranged in parallel; The first refueling channel includes a first buffer tank (8) connected to the vaporizer (7), a first heat exchanger (9) connected to the outlet of the first buffer tank (8), and a hydrogen dispenser (18) connected to the outlet of the first heat exchanger (9); the second refueling channel includes a high-pressure compressor (12) and a condenser (13) connected to the vaporizer (7), a second buffer tank (14) connected to the outlet of the condenser (13), a second heat exchanger (15) connected to the outlet of the second buffer tank (14), and a hydrogen dispenser (19) connected to the outlet of the second heat exchanger (15).

6. A dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle according to claim 5, characterized in that, The precooling unit is a refrigerant outlet branch led out from the pipeline between the cryogenic liquid hydrogen pump (3) and the coupling heat exchanger (61). The refrigerant outlet branch is connected to the refrigerant inlet of the first heat exchanger (9) and the second heat exchanger (15) respectively, and is configured to use cryogenic liquid hydrogen to exchange heat with hydrogen in the channel.

7. A dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle according to claim 1, characterized in that, The outlet of the cryogenic liquid hydrogen pump (3) is divided into a main path and a reflux bypass. The reflux bypass is equipped with a first valve (4) to regulate the flow rate of the liquid hydrogen branch. The main path is equipped with a second valve (5). The rear end of the second valve (5) is connected to the liquid hydrogen side inlet of the coupling heat exchanger (61). The liquid hydrogen side outlet of the coupling heat exchanger (61) is connected to the vaporizer (7) to completely vaporize the reheated liquid hydrogen into room temperature high pressure gas.

8. A dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle according to claim 7, characterized in that, A refrigerant diversion node is provided on the main pipeline between the outlet of the cryogenic liquid hydrogen pump (3) and the second valve (5); the refrigerant diversion node leads out two parallel precooling branches: a third valve (10) is provided on the first precooling branch, the outlet of the third valve (10) is connected to the refrigerant inlet of the first heat exchanger (9), and the flow rate of liquid hydrogen entering the first heat exchanger (9) is controlled by adjusting the opening degree of the third valve (10) to adjust the hydrogen temperature before the hydrogen dispenser (18); a fifth valve (16) is provided on the second precooling branch, the outlet of the fifth valve (16) is connected to the refrigerant inlet of the second heat exchanger (15), and the flow rate of liquid hydrogen entering the second heat exchanger (15) is controlled by adjusting the opening degree of the fifth valve (16) to adjust the hydrogen temperature before the hydrogen dispenser (19).

9. A dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle according to claim 8, characterized in that, A first temperature transmitter (102) is installed on the inlet pipeline of the hydrogen dispenser (18), and a second temperature transmitter (103) is installed on the inlet pipeline of the hydrogen dispenser (19) to detect the temperature of hydrogen before dispensing.

10. A dual-pressure liquid hydrogen refueling station system coupled with an organic Rankine cycle according to claim 8, characterized in that, The outlet pipeline of the cryogenic liquid hydrogen pump (3) is equipped with a pressure transmitter (101) for detecting the pump outlet pressure.

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