A green hydrogen storage and transportation system based on benzene-cyclohexane cycle

Abstract

The utility model provides a kind of green hydrogen storage and transportation system based on benzene-cyclohexane circulation, including benzene transportation unit, hydrogenation reaction unit, cyclohexane transportation unit and dehydrogenation reaction unit.The hydrogenation reaction unit of the utility model can react green hydrogen of benzene transportation unit transported benzene with first green hydrogen delivery pipeline to generate cyclohexane.Cyclohexane can be safely stored and transported at normal temperature and pressure, compatible with existing fuel infrastructure, can be quickly replenished through ordinary pipelines, tank cars, etc., suitable for long-distance transportation.Subsequently, cyclohexane is sent to the hydrogen site by cyclohexane transportation unit, enters dehydrogenation reaction unit for dehydrogenation, and the process has no tail gas and other pollutant emissions.

Description

Technical Field

[0001] This utility model relates to the field of green hydrogen storage and transportation technology, specifically to a green hydrogen storage and transportation system based on the benzene-cyclohexane cycle. Background Technology

[0002] Since renewable resources such as wind and solar energy are mainly concentrated in the Northwest region, green hydrogen produced through green electricity generation is also primarily distributed in this area. However, China's hydrogen consumption center is located in the Southeast, resulting in a spatial misalignment between green hydrogen and the hydrogen consumption center. How to safely and efficiently store and transport hydrogen is currently the main problem for the practical application of hydrogen energy. In recent years, technologies related to the economics of hydrogen production and the safety of hydrogen utilization have developed rapidly, but the storage and long-distance transportation of hydrogen have become the biggest bottlenecks restricting the utilization of green hydrogen energy.

[0003] Currently, green hydrogen storage and transportation in China mainly employs high-pressure gaseous (20-70 MPa) or low-temperature liquid (-253℃) methods. However, these methods suffer from high equipment costs, difficulties in storage and transportation, and significant safety hazards. Therefore, there is an urgent need to develop a system capable of efficient storage, transportation, and dehydrogenation of green hydrogen. Utility Model Content

[0004] This invention addresses the problems of low efficiency and high energy consumption in existing hydrogen storage and dehydrogenation reactions by providing a green hydrogen storage and transportation system based on a benzene-cyclohexane cycle.

[0005] The technical method of this utility model is as follows:

[0006] A green hydrogen storage and transportation system based on a benzene-cyclohexane cycle includes a benzene transportation unit, a hydrogenation reaction unit, a cyclohexane transportation unit, and a dehydrogenation reaction unit. The input end of the hydrogenation reaction unit is connected to the liquid output end of the benzene transportation unit, and the input end of the hydrogenation reaction unit is connected to a first green hydrogen delivery pipeline. The liquid output end of the hydrogenation reaction unit is connected to the liquid input end of the cyclohexane transportation unit. The liquid output end of the dehydrogenation reaction unit is connected to the liquid input end of the benzene transportation unit, and the gas output end of the dehydrogenation reaction unit is connected to a second green hydrogen delivery pipeline.

[0007] Preferably, the gas output end of the hydrogenation reaction unit is connected to the input end of the residual green hydrogen output pipe, and the input end of the residual green hydrogen output pipe is connected to the first green hydrogen delivery pipe.

[0008] Preferably, the hydrogenation reaction unit includes a hydrogenation heater, a pre-hydrogenation reactor, a hydrogenation reactor, a hydrogenation reaction product cooler, and a hydrogenation product gas-liquid separator; the input end of the hydrogenation heater is connected to the liquid output end of the benzene transport unit and the first green hydrogen transport pipeline; the output end of the hydrogenation heater is sequentially connected to the pre-hydrogenation reactor, the hydrogenation reactor, the hydrogenation reaction product cooler, and the hydrogenation product gas-liquid separator; the liquid output end of the hydrogenation product gas-liquid separator is connected to the liquid input end of the cyclohexane transport unit, and the gas output end of the hydrogenation product gas-liquid separator is connected to the remaining green hydrogen output pipeline.

[0009] Preferably, the system further includes a circulating hydrogen compressor disposed in the remaining green hydrogen output pipeline.

[0010] Preferably, the cyclohexane transport unit includes a cyclohexane product pump and a cyclohexane transport vehicle; the liquid output end of the hydrogenation product gas-liquid separator is connected to a stabilizing tower, the liquid output end of the stabilizing tower is connected to the liquid input end of the cyclohexane product pump; the liquid output end of the cyclohexane product pump is connected to the liquid input end of the cyclohexane transport vehicle.

[0011] Preferably, the cyclohexane transport unit further includes a cyclohexane feed buffer tank and a cyclohexane feed pump; the liquid output end of the cyclohexane transport vehicle is connected to the liquid input end of the cyclohexane feed buffer tank; the liquid output end of the cyclohexane feed buffer tank is connected to the liquid input end of the cyclohexane feed pump; and the liquid output end of the cyclohexane feed pump is connected to the liquid input end of the dehydrogenation reaction unit.

[0012] Preferably, the dehydrogenation reaction unit includes a dehydrogenation heating furnace, a dehydrogenation reactor, a dehydrogenation product cooler, and a dehydrogenation product gas-liquid separator; the liquid input end of the dehydrogenation heating furnace is connected to the liquid output end of the cyclohexane feed pump; the liquid output end of the dehydrogenation heating furnace is sequentially connected to the dehydrogenation reactor, the dehydrogenation product cooler, and the dehydrogenation product gas-liquid separator; the liquid output end of the dehydrogenation product gas-liquid separator is connected to the liquid input end of the benzene transport unit, and the gas output end of the dehydrogenation product gas-liquid separator is connected to a second green hydrogen transport pipeline; a third green hydrogen transport pipeline connects the second green hydrogen transport pipeline to the dehydrogenation heating furnace.

[0013] Preferably, the liquid output end of the dehydrogenation product gas-liquid separator is connected to a distillation column, and the liquid output end of the distillation column is connected to the liquid input end of the benzene transport unit.

[0014] Preferably, the system further includes a hydrogen purification component connected to the gas output end of the dehydrogenation product gas-liquid separator and a hydrogen compressor connected to the hydrogen purification component, the hydrogen compressor being connected to the second green hydrogen delivery pipeline.

[0015] The beneficial effects of this utility model are:

[0016] This invention designs a hydrogenation reaction unit and a dehydrogenation reaction unit. The hydrogenation reaction unit reacts benzene transported by the benzene transport unit with green hydrogen transported by the first green hydrogen transport pipeline to produce cyclohexane. Cyclohexane can be safely stored and transported at ambient temperature and pressure, is compatible with existing fuel infrastructure, and can be quickly replenished via ordinary pipelines, tank trucks, and other equipment, making it suitable for long-distance transportation. Subsequently, the cyclohexane is transported to the hydrogen-using site via the cyclohexane transport unit and enters the dehydrogenation reaction unit for dehydrogenation; this dehydrogenation process produces no exhaust gas or other pollutants. Furthermore, cyclohexane hydrogen storage is in a liquid state at ambient temperature and pressure, avoiding the safety hazards associated with high-pressure hydrogen storage and significantly reducing the risk of explosion or leakage during storage and transportation. Although the storage and transportation of any flammable substance carries certain safety risks, compared to other hydrogen storage methods, cyclohexane's operation and storage are closer to the operating mode of common liquid fuels, resulting in superior safety. Attached Figure Description

[0017] Figure 1 This is a schematic diagram of a green hydrogen storage and transportation system based on the benzene-cyclohexane cycle. Attached image description:

[0019] 1-Benzene transport unit, 101-Raw benzene buffer tank, 102-Benzene feed pump, 103-Benzene transport vehicle, 104-Benzene product pump, 2-Hydrogenation reaction unit, 201-Hydrogenation heater, 202-Pre-hydrogenation reactor, 203-Hydrogenation reactor, 204-Hydrogenation reaction product cooler, 205-Hydrogenation product gas-liquid separator, 3-Cyclohexane transport unit, 301-Cyclohexane product pump, 302-Cyclohexane transport vehicle, 303-Cyclohexane feed Buffer tank, 304-cyclohexane feed pump, 4-dehydrogenation reaction unit, 401-dehydrogenation heater, 402-dehydrogenation reactor, 403-dehydrogenation product cooler, 404-dehydrogenation product gas-liquid separator, 5-first green hydrogen delivery pipeline, 6-residual green hydrogen output pipeline, 7-circulating hydrogen compressor, 8-second green hydrogen delivery pipeline, 9-hydrogen purification component, 10-hydrogen compressor, 11-distillation column, 12-stabilization column, 13-third green hydrogen delivery pipeline. Detailed Implementation

[0020] The technical solution of this utility model will be clearly and completely described below. Obviously, the described embodiments are only some embodiments of this utility model, not all embodiments. Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are within the protection scope of this utility model.

[0021] The terms "first," "second," and "third" in this utility model are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Therefore, a feature defined as "first," "second," or "third" may explicitly or implicitly include at least one of that feature. In the description of this utility model, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified. All directional indications (such as up, down, left, right, front, back, etc.) in the embodiments of this utility model are only used to explain the relative positional relationships and movement of the components in a specific posture (as shown in the accompanying drawings). If the specific posture changes, the directional indications will also change accordingly. Furthermore, the terms "comprising" and "having," and any variations thereof, are intended to cover non-exclusive inclusion.

[0022] Example 1

[0023] refer to Figure 1 This embodiment provides a green hydrogen storage and transportation system based on the benzene-cyclohexane cycle, including a benzene transportation unit 1, a hydrogenation reaction unit 2, a cyclohexane transportation unit 3, and a dehydrogenation reaction unit 4.

[0024] Specifically, the input end of the hydrogenation reaction unit 2 is connected to the liquid output end of the benzene transport unit 1, and the input end of the hydrogenation reaction unit 2 is connected to the first green hydrogen transport pipeline 5. The liquid output end of the hydrogenation reaction unit 2 is connected to the liquid input end of the cyclohexane transport unit 3. The input end of the dehydrogenation reaction unit 4 is connected to the liquid output end of the cyclohexane transport unit 3, and the liquid output end of the dehydrogenation reaction unit 4 is connected to the liquid input end of the benzene transport unit 1. The gas output end of the dehydrogenation reaction unit 4 is connected to the second green hydrogen transport pipeline 8.

[0025] In this embodiment, the benzene transport unit 1 includes a raw benzene buffer tank 101, a benzene feed pump 102, a benzene transport vehicle 103, and a benzene product pump 104. The liquid inlet of the raw benzene buffer tank 101 is connected to the liquid outlet of the benzene transport vehicle 103, and the liquid outlet of the raw benzene buffer tank 101 is connected to the liquid inlet of the benzene feed pump 102. The liquid outlet of the benzene feed pump 102 is connected to the inlet of the hydrogenation reaction unit 2. The liquid inlet of the benzene product pump 104 is connected to the liquid outlet of the dehydrogenation reaction unit 4, and the liquid outlet of the benzene product pump 104 is connected to the liquid inlet of the benzene transport vehicle 103. Specifically, raw benzene from the tank farm or the benzene transport vehicle 103 enters the raw benzene buffer tank 101 through a pipeline, then the benzene enters the benzene feed pump 102 through a pipeline for pressurization, and the pressurized benzene enters the hydrogenation reaction unit 2 through a pipeline.

[0026] In this embodiment, the hydrogenation reaction unit 2 includes a hydrogenation heater 201, a pre-hydrogenation reactor 202, a hydrogenation reactor 203, a hydrogenation reaction product cooler 204, and a hydrogenation product gas-liquid separator 205. The input end of the hydrogenation heater 201 is connected to the liquid output end of the benzene transport unit 1 and the first green hydrogen transport pipeline 5, respectively. The output end of the hydrogenation heater 201 is sequentially connected to the pre-hydrogenation reactor 202, the hydrogenation reactor 203, the hydrogenation reaction product cooler 204, and the hydrogenation product gas-liquid separator 205. The liquid output end of the hydrogenation product gas-liquid separator 205 is connected to the liquid input end of the cyclohexane transport unit 3, and the gas output end of the hydrogenation product gas-liquid separator 205 is connected to the remaining green hydrogen output pipeline 6.

[0027] In this embodiment, the hydrogenation reactor 203 is a tubular reactor, with a nickel catalyst supported on alumina packed within the tubes. For example, the nickel catalyst supported on alumina can be an NCH3-type nickel-based / Al2O3 hydrogenation catalyst, model REZEL-H3. Specifically, the NCH3-type nickel-based hydrogenation catalyst uses nickel as the main active component, alumina as the main support, and trace amounts of rare earth elements as structural aids. The catalyst appears as black or gray cylindrical particles; catalyst size: φ5×4-5mm; catalyst bulk density: 0.9-1.1kg / L; catalyst radial crushing strength: ≥150N / cm. This catalyst can reduce the reaction temperature by 40℃ while maintaining a conversion rate of over 99.8%. Here, the benzene hydrogenation reaction can store a large amount of hydrogen, with a hydrogen storage density comparable to, or even better than, high-pressure gaseous hydrogen storage systems under certain conditions. The reversible hydrogen storage density of this reaction is approximately 5.8 wt%, significantly higher than that of traditional alloy hydrogen storage and high-pressure hydrogen storage. Moreover, its storage and transportation costs are 65% lower than those of high-pressure hydrogen storage. The feedstocks for the hydrogenation reaction are green hydrogen (purity ≥99.9%) produced by water electrolysis and industrial benzene (purity ≥98.5%).

[0028] In this embodiment, the gas output end of the hydrogenation reaction unit 2 is connected to the input end of the residual green hydrogen output pipeline 6, and the input end of the residual green hydrogen output pipeline 6 is connected to the first green hydrogen conveying pipeline 5. The liquid output end of the hydrogenation product gas-liquid separator 205 is connected to the liquid input end of the cyclohexane transport unit 3, and the gas output end of the hydrogenation product gas-liquid separator 205 is connected to the gas input end of the residual green hydrogen output pipeline 6, and the gas output end of the residual green hydrogen output pipeline 6 is connected to the first green hydrogen conveying pipeline 5. The system also includes a circulating hydrogen compressor 7 installed in the residual green hydrogen output pipeline 6.

[0029] In this embodiment, the cyclohexane transport unit 3 includes a cyclohexane product pump 301 and a cyclohexane transport vehicle 302; the liquid output end of the hydrogenation product gas-liquid separator 205 is connected to the stabilizer 12, and the liquid output end of the stabilizer 12 is connected to the liquid input end of the cyclohexane product pump 301; the liquid output end of the cyclohexane product pump 301 is connected to the liquid input end of the cyclohexane transport vehicle 302.

[0030] Specifically, pressurized benzene enters the hydrogenation heater 201 via pipeline for heating. Before entering the hydrogenation heater 201, the benzene is mixed with green hydrogen (also known as hydrogen gas). The green hydrogen mixed with the benzene is a mixture of fresh green hydrogen from the first green hydrogen delivery pipeline 5 and recycled hydrogen from the remaining green hydrogen output pipeline 6. The temperature of the benzene-hydrogen mixture is controlled by the hydrogenation heater 201, heating the benzene-hydrogen mixture to 140-230°C. Then, it enters the pre-hydrogenation reactor 202 from the top via pipeline for hydrogenation reaction. The stream flowing out of the pre-hydrogenation reactor 202 enters the top of the hydrogenation reactor 203 for reaction, completely converting benzene into cyclohexane. The heat of reaction is removed by using hot water on the shell side through by-product steam, maintaining the reaction temperature to a maximum of 230°C. The control scheme for the pre-hydrogenation reactor 202 is the same as that for the hydrogenation reactor 203. The output from the bottom of the hydrogenation reactor 203 enters the hydrogenation product gas-liquid separator 205 via pipeline. After condensation (e.g., using circulating water), the gas is mainly composed of unreacted hydrogen. This hydrogen then enters the inlet of the circulating hydrogen compressor 7 via a pipeline. After being pressurized by the circulating hydrogen compressor 7, it is mixed with fresh green hydrogen and recycled as a reaction feedstock. In this embodiment, a heat recovery heat exchanger can be added after the hydrogenation product gas-liquid separator 205. The liquid phase entering the hydrogenation product cooler 204 is product cyclohexane. After being heated by the hydrogenation product gas-liquid separator 205 and the heat recovery heat exchanger, the cyclohexane enters the stabilizer 12 to remove non-condensable gases dissolved in the cyclohexane. The stabilizer 12 operates under a slight positive pressure. The non-condensable gases at the top of the tower are cooled by cooling water and then discharged into the flare system. The cyclohexane at the bottom of the tower is cooled and then pumped by a cyclohexane pump into a cyclohexane transport vehicle 302 for shipment. The raw material cyclohexane from the cyclohexane transport vehicle 302 or the storage tank enters the raw material cyclohexane feed buffer tank 303 through a pipeline, and then enters the cyclohexane feed pump 304 for pressurization. Some unreacted green hydrogen also appears in the hydrogenation product cooler 204, and the green hydrogen enters the residual green hydrogen output pipeline 6. In the hydrogenation reaction, the reaction temperature is 140-230℃; the operating pressure is 0.3-1.0 MPa; the hydrogen / benzene molar ratio is 3.5-10; and the mass hourly space velocity (HHSV) is 0.2-1.0 h⁻¹. -1 Aromatic hydrocarbon conversion rate ≥99wt%. Purity of cyclohexane ≥99.7wt%, yield ≥99.8wt%. Cyclohexane is transported to hydrogen-using sites via tank trucks (at ambient temperature and pressure), improving storage and transportation safety by more than 90% compared to high-pressure hydrogen tanks.

[0031] In this embodiment, the cyclohexane transport unit 3 further includes a cyclohexane feed buffer tank 303 and a cyclohexane feed pump 304; the liquid output end of the cyclohexane transport vehicle 302 is connected to the liquid input end of the cyclohexane feed buffer tank 303; the liquid output end of the cyclohexane feed buffer tank 303 is connected to the liquid input end of the cyclohexane feed pump 304; and the liquid output end of the cyclohexane feed pump 304 is connected to the liquid input end of the dehydrogenation reaction unit 4.

[0032] In this embodiment, the dehydrogenation reaction unit 4 includes a dehydrogenation heater 401, a dehydrogenation reactor 402, a dehydrogenation product cooler 403, and a dehydrogenation product gas-liquid separator 404; the liquid input end of the dehydrogenation heater 401 is connected to the liquid output end of the cyclohexane feed pump 304; the liquid output end of the dehydrogenation heater 401 is sequentially connected to the dehydrogenation reactor 402, the dehydrogenation product cooler 403, and the dehydrogenation product gas-liquid separator 404; the liquid output end of the dehydrogenation product gas-liquid separator 404 is connected to the liquid input end of the benzene transport unit 1, and the gas output end of the dehydrogenation product gas-liquid separator 404 is connected to the second green hydrogen transport pipeline 8; a third green hydrogen transport pipeline 13 connects the second green hydrogen transport pipeline 8 and the dehydrogenation heater 401.

[0033] Specifically, dehydrogenation reactor 402 is a fixed-bed reactor, which is loaded with a CDH-type platinum-based dehydrogenation catalyst. For example, the CDH-type platinum-based catalyst can be a CDH-type platinum-based catalyst / ZSM-5 molecular sieve catalyst, model REZEL-CDH-1. Specifically, this catalyst is prepared by supporting a CDH-type platinum-based active component on a ZSM-5 molecular sieve. The catalyst appears as gray strips; the catalyst bulk density is 0.5-0.6 t / m³. 3 Catalyst crush resistance: ≥35 N / cm; Specific surface area: >180 m² 2 / g; Pore volume: >0.5ml / g; Platinum content: 0.50±0.02wt%. The CDH-type platinum-based dehydrogenation catalyst has 2-3 times higher activity than traditional catalysts. The dehydrogenation reaction unit 4 uses a CDH-type platinum-based dehydrogenation catalyst, which makes the hydrogen obtained from cyclohexane dehydrogenation high in purity (>99.99%), which can meet the hydrogen quality requirements of fuel cell systems, and the dehydrogenation process has no exhaust gas or other pollutant emissions.

[0034] In this embodiment, the liquid output end of the dehydrogenation product gas-liquid separator 404 is connected to a distillation column 11, and the liquid output end of the distillation column 11 is connected to the liquid input end of the benzene transport unit 1. The system also includes a hydrogen purification component 9 connected to the gas output end of the dehydrogenation product gas-liquid separator 404, and a hydrogen compressor 10 connected to the hydrogen purification component 9. The hydrogen compressor 10 is connected to the second green hydrogen transport pipeline 8. The system also includes a gas input end of a third green hydrogen transport pipeline 13 connected to the gas output end of the second green hydrogen transport pipeline 8, and the gas output end of the third green hydrogen transport pipeline 13 is connected to the input end of the dehydrogenation heater 401.

[0035] Specifically, pressurized cyclohexane is piped into a dehydrogenation heater 401 and heated to 420-480°C. Before entering the dehydrogenation heater 401, the cyclohexane is mixed with a small amount of supplementary hydrogen. After the temperature of the mixture is controlled by the dehydrogenation heater 401, it is piped from the top into the dehydrogenation reactor 402. The mixture then undergoes an oxidative dehydrogenation reaction at a pressure of 0.5-0.8 MPa and a temperature of 420-480°C, producing reaction products containing a large amount of benzene and small amounts of cyclohexene and water. The reaction products are piped into a dehydrogenation product cooler 403, where they condense to 40-43°C and then piped into a dehydrogenation product gas-liquid separator 404. Gas-liquid separation occurs at a pressure of 0.10-0.15 MPa, resulting in a two-phase gas-liquid mixture. The gas phase exiting from the top of the dehydrogenation product gas-liquid separator 404 is piped into the hydrogen purification system for further purification. The purified hydrogen has a purity ≥99.9%. The high-purity hydrogen is pressurized by the hydrogen compressor 10, and a small amount of hydrogen is mixed with the raw material cyclohexane as supplementary hydrogen before entering the dehydrogenation heater 401 for recycling. The majority of the remaining hydrogen is sent out as green hydrogen to users. The liquid phase at the bottom of the dehydrogenation product gas-liquid separator 404 is heated and then piped into the product distillation column 11 for product fractionation. The top pressure of the product distillation column 11 is 0.05-0.07 MPa, the top temperature is 90-95℃, and it has 50 theoretical plates with a reflux ratio of 2-4. Light components are obtained at the top of the column through fractional distillation, and benzene product with a purity ≥98.5% wt is obtained at the bottom. The benzene product is pumped by the benzene product pump 104 to the benzene transport vehicle 103 or storage tank. The benzene is then transported back to the hydrogenation reaction unit 2 by the transport vehicle to react with the green hydrogen. The safe and stable transportation of green hydrogen is achieved through a hydrogenation-dehydrogenation cycle reaction of benzene-cyclohexane.

[0036] This invention establishes a benzene-cyclohexane closed-loop recycling system, increasing the raw material utilization rate to over 99.5%.

[0037] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and variations can be made to these embodiments without departing from the principles and spirit of the present invention, the scope of which is defined by the appended claims and their equivalents.

Claims

1. A green hydrogen storage and transportation system based on the benzene-cyclohexane cycle, characterized in that, It includes a benzene transport unit (1), a hydrogenation reaction unit (2), a cyclohexane transport unit (3), and a dehydrogenation reaction unit (4); The input end of the hydrogenation reaction unit (2) is connected to the liquid output end of the benzene transport unit (1), the input end of the hydrogenation reaction unit (2) is connected to the first green hydrogen transport pipeline (5), and the liquid output end of the hydrogenation reaction unit (2) is connected to the liquid input end of the cyclohexane transport unit (3). The input end of the dehydrogenation reaction unit (4) is connected to the liquid output end of the cyclohexane transport unit (3), the liquid output end of the dehydrogenation reaction unit (4) is connected to the liquid input end of the benzene transport unit (1), and the gas output end of the dehydrogenation reaction unit (4) is connected to the second green hydrogen transport pipeline (8).

2. The green hydrogen storage and transportation system based on the benzene-cyclohexane cycle according to claim 1, characterized in that, The gas output end of the hydrogenation reaction unit (2) is connected to the input end of the residual green hydrogen output pipe (6), and the input end of the residual green hydrogen output pipe (6) is connected to the first green hydrogen delivery pipe (5).

3. The green hydrogen storage and transportation system based on the benzene-cyclohexane cycle according to claim 2, characterized in that, The hydrogenation reaction unit (2) includes a hydrogenation heater (201), a pre-hydrogenation reactor (202), a hydrogenation reactor (203), a hydrogenation reaction product cooler (204), and a hydrogenation product gas-liquid separator (205); The input end of the hydrogenation heating furnace (201) is connected to the liquid output end of the benzene transport unit (1) and the first green hydrogen transport pipeline (5); The output end of the hydrogenation heating furnace (201) is sequentially connected to the pre-hydrogenation reactor (202), the hydrogenation reactor (203), the hydrogenation reaction product cooler (204), and the hydrogenation product gas-liquid separator (205); The liquid output end of the hydrogenation product gas-liquid separator (205) is connected to the liquid input end of the cyclohexane transport unit (3), and the gas output end of the hydrogenation product gas-liquid separator (205) is connected to the residual green hydrogen output pipe (6).

4. The green hydrogen storage and transportation system based on the benzene-cyclohexane cycle according to claim 3, characterized in that, The system also includes a circulating hydrogen compressor (7) located in the remaining green hydrogen output pipeline (6).

5. The green hydrogen storage and transportation system based on the benzene-cyclohexane cycle according to claim 3, characterized in that, The cyclohexane transport unit (3) includes a cyclohexane product pump (301) and a cyclohexane transport vehicle (302); The liquid output end of the hydrogenation product gas-liquid separator (205) is connected to the stabilizer (12), and the liquid output end of the stabilizer (12) is connected to the liquid input end of the cyclohexane product pump (301). The liquid output end of the cyclohexane product pump (301) is connected to the liquid input end of the cyclohexane transport vehicle (302).

6. The green hydrogen storage and transportation system based on the benzene-cyclohexane cycle according to claim 5, characterized in that, The cyclohexane transport unit (3) also includes a cyclohexane feed buffer tank (303) and a cyclohexane feed pump (304); The liquid output end of the cyclohexane transport vehicle (302) is connected to the liquid input end of the cyclohexane feed buffer tank (303); The liquid output end of the cyclohexane feed buffer tank (303) is connected to the liquid input end of the cyclohexane feed pump (304); The liquid output end of the cyclohexane feed pump (304) is connected to the liquid input end of the dehydrogenation reaction unit (4).

7. The green hydrogen storage and transportation system based on the benzene-cyclohexane cycle according to claim 6, characterized in that, The dehydrogenation reaction unit (4) includes a dehydrogenation heating furnace (401), a dehydrogenation reactor (402), a dehydrogenation product cooler (403), and a dehydrogenation product gas-liquid separator (404); The liquid inlet of the dehydrogenation heater (401) is connected to the liquid outlet of the cyclohexane feed pump (304); The liquid output end of the dehydrogenation heating furnace (401) is sequentially connected to the dehydrogenation reactor (402), the dehydrogenation product cooler (403), and the dehydrogenation product gas-liquid separator (404). The liquid output end of the dehydrogenation product gas-liquid separator (404) is connected to the liquid input end of the benzene transport unit (1), and the gas output end of the dehydrogenation product gas-liquid separator (404) is connected to the second green hydrogen transport pipeline (8). A third green hydrogen transport pipeline connects the second green hydrogen transport pipeline (8) to the dehydrogenation heating furnace (401).

8. The green hydrogen storage and transportation system based on the benzene-cyclohexane cycle according to claim 7, characterized in that, The liquid output end of the dehydrogenation product gas-liquid separator (404) is connected to a distillation column (11), and the liquid output end of the distillation column (11) is connected to the liquid input end of the benzene transport unit (1).

9. The green hydrogen storage and transportation system based on the benzene-cyclohexane cycle according to claim 7, characterized in that, The system also includes a hydrogen purification component (9) connected to the gas output end of the dehydrogenation product gas-liquid separator (404) and a hydrogen compressor (10) connected to the hydrogen purification component (9), the hydrogen compressor (10) being connected to the second green hydrogen delivery pipeline (8).

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