Process method and device for storing, transporting and purifying green hydrogen energy

Abstract

The invention discloses a process method and device for green hydrogen energy storage, transportation and purification, the device comprises an ammonia hydrogen storage part and an ammonia hydrogen release part, hydrogen in a hydrogen source and nitrogen in a nitrogen source enter an ammonia hydrogen storage device through a pipeline, and liquid ammonia is obtained through treatment of the ammonia hydrogen storage device; liquid ammonia conveyed by the liquid ammonia conveying device is treated by the ammonia hydrogen release device to obtain purified hydrogen, a nitrogen-hydrogen mixture and an ammonia-containing product. According to the scheme, a high-concentration liquid ammonia product can be produced, helium is converted into liquid from gas, the problems of pressure and large gas volume are reduced, and the problems of difficult storage and transportation, high cost and the like are solved; all discharged gas, gas discharged gas and the like are collected and treated and then returned to be used as raw material gas, and unit consumption is lowest; waste water and waste residues in three wastes are subjected to three-in-one collection treatment, so that the method is more A raw material gas, reaction gas, steam, circulating cooling water and chilled water utilization system is optimized, and the investment and energy are saved.

Description

Technical Field

[0001] The present invention relates to the technical fields of chemical processes and equipment, and particularly relates to a process method and device for the storage, transportation, purification, and use of green hydrogen energy. Background Art

[0002] Hydrogen energy is an important secondary clean energy source that can replace fossil energy and solve the problem of insufficient utilization of wind energy and solar energy. From the perspective of energy storage and transportation, high-pressure gaseous hydrogen storage is currently the most mature and widely used hydrogen storage technology. It compresses hydrogen into high-pressure-resistant containers, usually using steel cylinders as storage containers. However, high-pressure hydrogen storage needs to withstand high pressures, has certain safety hazards, and has a relatively low hydrogen storage density. Therefore, the main difficulties in the application of hydrogen energy are the high difficulty and high cost of storage and transportation. From the application perspective, the traditional process is to synthesize ammonia from hydrogen and nitrogen, and synthetic ammonia is mainly used to manufacture nitrogen fertilizers and compound fertilizers, such as urea, ammonium nitrate, ammonium phosphate, ammonium chloride, and various nitrogen-containing compound fertilizers, or as raw materials for nitric acid, various nitrogen-containing inorganic salts and organic intermediates, sulfonamides, polyurethanes, polyamide fibers, and nitrile rubber. Hydrogen is mainly used as an intermediate or raw material for chemical products, and there is a problem that hydrogen energy cannot be used as a secondary clean energy source.

[0003] In view of this, the present invention provides a process method and device for the storage, transportation, purification, and use of green hydrogen energy to at least partially solve the problems of high difficulty in hydrogen energy transportation and limited utilization range existing in the prior art. Summary of the Invention

[0004] In view of this, the purpose of the present invention is to provide a process method and device for the storage, transportation, purification, and use of green hydrogen energy to at least partially solve the problems existing in the prior art, improve the efficiency of hydrogen energy storage and transportation, and reduce the difficulty of storage and transportation.

[0005] To achieve the above purpose, the embodiments of the present invention provide the following technical solutions:

[0006] The present invention provides a device for the storage, transportation, purification, and use of green hydrogen energy, and the device includes:

[0007] An ammonia hydrogen storage device, the feed end of the ammonia hydrogen storage device is respectively connected to a hydrogen source and a nitrogen source, hydrogen in the hydrogen source and nitrogen in the nitrogen source enter the ammonia hydrogen storage device through pipelines, and liquid ammonia is obtained after being processed by the ammonia hydrogen storage device;

[0008] A liquid ammonia conveying device, one end of the liquid ammonia conveying device is connected to the liquid ammonia outlet of the ammonia hydrogen storage device, and the liquid ammonia obtained by the reaction in the ammonia hydrogen storage device is transported into the liquid ammonia conveying device through the liquid ammonia outlet;

[0009] Ammonia hydrogen release device, the other end of the liquid ammonia conveying device is connected to the inlet end of the ammonia hydrogen release device, and the liquid ammonia conveyed by the liquid ammonia conveying device is processed by the ammonia hydrogen release device to obtain purified hydrogen, nitrogen-hydrogen mixture and ammonia-containing products.

[0010] In some embodiments, the ammonia hydrogen storage device includes:

[0011] A hydrogen-nitrogen pressurization and mixing assembly, the intake side of the hydrogen-nitrogen pressurization and mixing assembly is respectively connected to a hydrogen source and a nitrogen source, and the hydrogen in the hydrogen source and the nitrogen in the nitrogen source are pressurized and mixed into a high-pressure mixed gas in the hydrogen-nitrogen pressurization and mixing unit;

[0012] A synthetic ammonia reaction assembly, the outlet side of the hydrogen-nitrogen pressurization and mixing assembly is connected to the inlet side of the synthetic ammonia reaction assembly, and the high-pressure mixed gas completes a synthesis reaction in the synthetic ammonia reaction assembly and obtains a gas-liquid mixed ammonia;

[0013] A liquid ammonia separation assembly, the outlet side of the synthetic ammonia reaction assembly is connected to the inlet side of the liquid ammonia separation assembly, and the gas-liquid mixed ammonia is separated in the liquid ammonia separation assembly to generate liquid ammonia and gaseous ammonia;

[0014] A recycle gas pressurization assembly, the gaseous ammonia is transported through a pipeline into the recycle gas pressurization assembly and is pressurized by the recycle gas pressurization assembly and then mixed into the high-pressure mixed gas.

[0015] In some embodiments, the hydrogen-nitrogen pressurization and mixing assembly includes:

[0016] A low-pressure hydrogen buffer tank, the inlet of the low-pressure hydrogen buffer tank is connected to the hydrogen source;

[0017] A hydrogen pressurization device, the outlet of the low-pressure hydrogen buffer tank is connected to the inlet of the hydrogen pressurization device through a pipeline;

[0018] A high-pressure hydrogen buffer tank, the outlet of the hydrogen pressurization device is connected to the high-pressure hydrogen buffer tank through a pipeline;

[0019] A low-pressure nitrogen buffer tank, the inlet of the low-pressure nitrogen buffer tank is connected to the nitrogen source;

[0020] A nitrogen pressurization device, the outlet of the low-pressure nitrogen buffer tank is connected to the inlet of the nitrogen pressurization device through a pipeline;

[0021] A high-pressure nitrogen buffer tank, the outlet of the nitrogen pressurization device is connected to the high-pressure nitrogen buffer tank through a pipeline;

[0022] A high-pressure mixed gas buffer tank, the outlets of the high-pressure nitrogen buffer tank and the high-pressure hydrogen buffer tank are respectively connected to the high-pressure mixed gas buffer tank through pipelines.

[0023] In some embodiments, the ammonia synthesis reaction assembly includes:

[0024] A first gas-gas heat exchanger, the outlet of the high-pressure mixed gas buffer tank is connected to the low-temperature side pipe orifice of the first gas-gas heat exchanger through a pipeline;

[0025] A first-stage reactor, the inlet of the first-stage reactor is connected to the high-temperature side pipe orifice of the first gas-gas heat exchanger through a pipeline;

[0026] A mixing tank, the inlet of the mixing tank is connected to the outlet of the first-stage reactor;

[0027] A second-stage reactor, the inlet of the second-stage reactor is connected to the outlet of the mixing tank, and the outlet of the second-stage reactor serves as the outlet side of the ammonia synthesis reaction assembly and is connected to the inlet side of the liquid ammonia separation assembly.

[0028] In some embodiments, the liquid ammonia separation assembly includes:

[0029] A first gas-liquid water-cooled heat exchanger, the outlet of the second-stage reactor is connected to the inlet of the first gas-liquid water-cooled heat exchanger;

[0030] A first gas-liquid deep water-cooled heat exchanger, the inlet of the first gas-liquid deep water-cooled heat exchanger is connected to the outlet of the first gas-liquid water-cooled heat exchanger;

[0031] A gas-liquid separator, the inlet of the gas-liquid separator is connected to the outlet of the first gas-liquid deep water-cooled heat exchanger, the gaseous outlet of the gas-liquid separator is connected to the inlet of the recycle gas boosting assembly, the outlet of the recycle gas boosting assembly is connected to the high-pressure mixed gas buffer tank, and the tail gas outlet of the gas-liquid separator is connected to the discharge main pipe;

[0032] A first liquid ammonia storage tank, the inlet of the first liquid ammonia storage tank is connected to the liquid outlet of the gas-liquid separator, and the outlet of the first liquid ammonia storage tank is connected to the liquid ammonia transportation device.

[0033] In some embodiments, the ammonia dehydrogenation device includes:

[0034] A liquid ammonia gasification assembly, the other end of the liquid ammonia transportation device is connected to the inlet side of the liquid ammonia gasification assembly, and the liquid ammonia transported by the liquid ammonia transportation device is processed by the liquid ammonia gasification assembly to obtain high-pressure ammonia gas;

[0035] An ammonia decomposition assembly, the inlet side of the ammonia decomposition assembly is connected to the outlet side of the liquid ammonia gasification assembly, and the high-pressure ammonia gas transported by the liquid ammonia gasification assembly undergoes a decomposition reaction in the ammonia decomposition assembly to obtain a reaction mixture of ammonia gas, hydrogen gas, and nitrogen gas;

[0036] A hydrogen separation component, the inlet side of the hydrogen separation component is connected to the mixed gas outlet of the ammonia decomposition component, and the reaction mixed gas is cooled by the hydrogen separation component to obtain a cooled mixed gas;

[0037] A hydrogen purification component, the inlet side of the hydrogen purification component is connected to the outlet side of the hydrogen separation component, and the cooled mixed gas is separated into hydrogen, nitrogen and ammonia-containing products in the hydrogen purification component.

[0038] In some embodiments, the liquid ammonia gasification component includes a second liquid ammonia storage tank, a liquid ammonia transfer pump, a liquid ammonia vaporizer and an ammonia buffer tank that are sequentially connected through pipelines. Among them, the inlet of the second liquid ammonia storage tank is connected to the liquid ammonia transfer device;

[0039] The ammonia decomposition component includes a second gas-gas heat exchanger and an ammonia decomposition reactor connected through pipelines. Among them, the low-temperature side pipe orifice of the second gas-gas heat exchanger is connected to the outlet of the ammonia buffer tank, and the high-temperature side pipe orifice of the second gas-gas heat exchanger is connected to the inlet of the ammonia decomposition reactor;

[0040] The hydrogen separation component includes a second gas-liquid water-cooled heat exchanger, a second gas-liquid deep water-cooled heat exchanger and an ammonia-nitrogen-hydrogen buffer tank that are sequentially connected through pipelines. Among them, the inlet of the second gas-liquid water-cooled heat exchanger is connected to the outlet of the ammonia decomposition reactor;

[0041] The hydrogen purification component includes a hydrogen dryer, a nitrogen-hydrogen buffer tank, a nitrogen-hydrogen pressurization device and an adsorption device that are sequentially connected through pipelines. Among them, the inlet of the hydrogen dryer is connected to the outlet of the ammonia-nitrogen-hydrogen buffer tank, the nitrogen outlet of the adsorption device is connected to the nitrogen buffer tank, and the hydrogen outlet of the adsorption device is connected to the hydrogen buffer tank.

[0042] The present invention also provides a process method for the storage, transportation, purification and use of green hydrogen energy. The method includes the following steps:

[0043] Step (1): Using the catalyst, the high-pressure hydrogen and high-pressure nitrogen obtained after pressurization as reaction raw materials, carrying out a synthesis reaction. After the heat of the product of the synthesis reaction is withdrawn, it is input into a gas-liquid separation tank through a first gas-liquid water-cooled heat exchanger and a first gas-liquid deep water-cooled heat exchanger. The unreacted gas is pressurized and mixed with the reaction raw materials and then the synthesis reaction is carried out again;

[0044] Step (2): Inputting the liquid phase product of the synthesis reaction in step (1) into a liquid ammonia transportation device and transporting it to an ammonia hydrogen release device through the liquid ammonia transfer device;

[0045] Step (3): The liquid-phase product in step (2) enters an ammonia decomposition reactor through pressure increase and temperature increase for decomposition reaction. After the reaction heat of the decomposition reaction product is withdrawn, it is input into an ammonia-nitrogen-hydrogen buffer tank through a second gas-liquid water-cooled heat exchanger and a second gas-liquid deep water-cooled heat exchanger;

[0046] Step (4): The product of the reaction in step (3) is input into a dryer for gas-liquid separation. The separated gas is pressurized and purified and separated in an adsorption device to obtain hydrogen.

[0047] In some embodiments, in step (1), the catalyst is one of copper-based, manganese-based, nickel-based, titanium-based, and magnesium-based catalysts; the pressure of the synthesis reaction is 11-19.5 MPaG; the temperature of the synthesis reaction is 325-575 °C; the reaction space velocity of the synthesis reaction is 50,000-130,000; and / or,

[0048] In steps (1) and (2), the storage pressure of liquid ammonia is 0.8-1.5 MPaG, and the storage temperature is -20 to -5 °C.

[0049] In some embodiments, in step (3), the catalyst is one of copper-based, manganese-based, nickel-based, titanium-based, and magnesium-based catalysts; the pressure of the decomposition reaction is 0.8-1.2 MPaG; the temperature of the decomposition reaction is 500-850 °C; the reaction space velocity is 50,000-130,000; the temperature of the reaction product after condensation through a second gas-liquid water-cooled heat exchanger and a second gas-liquid deep water-cooled heat exchanger is 15-30 °C.

[0050] In one or several specific embodiments, the process method and device for green hydrogen energy storage, transportation, and purification provided by the present invention have the following technical effects:

[0051] 1. High-concentration liquid ammonia products can be produced, converting hydrogen from gas to liquid, reducing problems such as pressure and large gas volume, and solving problems such as difficult storage and transportation and high costs;

[0052] 2. All emissions, such as gas emissions, are collected and treated and then returned as raw material gas, with the lowest unit consumption;

[0053] 3. The wastewater and waste residue in the three wastes are collected and treated in a three-in-one manner, which is more environmentally friendly;

[0054] 4. The utilization systems of raw material gas, reaction gas, steam, circulating cooling water, and chilled water are optimized, resulting in more savings in investment and energy;

[0055] 5. The drying and purification separation system can be a dryer, or a drying tower, or a reverse osmosis membrane system, or a pressure swing adsorption system, or a temperature swing adsorption system for hydrogen purification and nitrogen-hydrogen separation;

[0056] 6. It is possible to achieve a multi-capacity device layout for liquid ammonia products of 50,000 to 400,000 tons / year (i.e., it is possible to store and transport 8,900 to 70,200 tons / year of hydrogen). BRIEF DESCRIPTION OF THE DRAWINGS

[0057] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following will briefly introduce the drawings required for use in the description of the embodiments or the prior art. Obviously, the drawings in the following description are only exemplary, and for those of ordinary skill in the art, without creative efforts, other implementation drawings can also be obtained according to the provided drawings.

[0058] The structures, ratios, sizes, etc. shown in this specification are only used to cooperate with the content disclosed in the specification for those familiar with this technology to understand and read, and are not used to limit the limiting conditions for the implementation of the present invention. Therefore, they do not have technical substance significance. Any modification of the structure, change of the proportional relationship, or adjustment of the size, without affecting the effects that the present invention can produce and the purposes that can be achieved, should still fall within the scope covered by the technical content disclosed in the present invention.

[0059] Figure 1 It is a schematic structural diagram of the ammonia hydrogen storage device in the device for green hydrogen energy storage, transportation, purification and use provided by the present invention;

[0060] Figure 2 It is a schematic structural diagram of the ammonia hydrogen release device in the device for green hydrogen energy storage, transportation, purification and use provided by the present invention;

[0061] Description of the reference numerals:

[0062] 1. Low-pressure hydrogen buffer tank; 2. Hydrogen boosting device; 3. High-pressure hydrogen buffer tank; 4. Low-pressure nitrogen buffer tank; 5. Nitrogen boosting device; 6. High-pressure nitrogen buffer tank; 7. High-pressure mixed gas buffer tank; 8. First gas-gas heat exchanger; 9. First-stage reactor; 10. Mixing tank; 11. Second-stage reactor; 12. First gas-liquid water-cooled heat exchanger; 13. First gas-liquid deep water-cooled heat exchanger; 14. Gas-liquid separator; 15. Circulation gas boosting device; 16. Circulation gas buffer tank; 17. First liquid ammonia storage tank; 18. Liquid ammonia transportation device; 19. Second liquid ammonia storage tank; 20. Liquid ammonia delivery pump; 21. Liquid ammonia vaporizer; 22. Ammonia buffer tank; 23. Second gas-gas heat exchanger; 24. Ammonia decomposition reactor; 25. Second gas-liquid water-cooled heat exchanger; 26. Second gas-liquid deep water-cooled heat exchanger; 27. Ammonia-nitrogen-hydrogen buffer tank; 28. Hydrogen dryer; 29. Nitrogen-hydrogen buffer tank; 30. Nitrogen-hydrogen boosting device; 31. Adsorption device; 32. Hydrogen buffer tank; 33. Nitrogen buffer tank. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0063] The following specific embodiments illustrate the implementation manners of the present invention. Those skilled in this technology can easily understand other advantages and effects of the present invention from the content disclosed in this specification. Obviously, the described embodiments are part of the embodiments of the present invention, rather than all the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts belong to the scope protected by the present invention.

[0064] Ammonia synthesis for hydrogen storage is a technology for efficient storage and transportation by converting hydrogen into ammonia (NH3). In principle, the core of ammonia synthesis for hydrogen storage lies in using ammonia (NH3) as a carrier of hydrogen. An ammonia molecule consists of one nitrogen atom and three hydrogen atoms, and the mass fraction of hydrogen is about 17.6%. Ammonia has advantages such as easy liquefaction, convenient storage and transportation, and high safety. The synthesized ammonia can be liquefied and stored at room temperature and transported over long distances through existing transportation means such as pipelines, tank trucks, or ships. The transportation cost of liquid ammonia is much lower than that of high-pressure hydrogen transportation; at the place where hydrogen is needed, ammonia is decomposed into nitrogen and hydrogen (2NH3 → N2 + 3H2) through a catalyst, and the decomposed hydrogen can be used for fuel cells or industrial purposes after purification.

[0065] Based on this, the present invention provides a process method and device for the storage, transportation, purification, and use of green hydrogen energy, which are applied to the storage, transportation, purification, and use of green hydrogen energy. The device includes an ammonia hydrogen storage device and an ammonia hydrogen release device; among them, the ammonia hydrogen storage device includes a hydrogen-nitrogen pressurization and mixing unit, an ammonia synthesis reaction unit, a liquid ammonia separation unit, and a recycle gas pressurization unit; the ammonia hydrogen release device includes a liquid ammonia gasification unit, an ammonia decomposition unit, a hydrogen separation unit, and a hydrogen purification unit.

[0066] In a specific embodiment, as Figure 1 and Figure 2 shown, the device for the storage, transportation, purification, and use of green hydrogen energy provided by the present invention includes an ammonia hydrogen storage device, a liquid ammonia transportation device, and an ammonia hydrogen release device; among them, the feed end of the ammonia hydrogen storage device is respectively connected to a hydrogen source and a nitrogen source, hydrogen in the hydrogen source and nitrogen in the nitrogen source enter the ammonia hydrogen storage device through pipelines, and liquid ammonia is obtained after being processed by the ammonia hydrogen storage device; one end of the liquid ammonia transportation device is connected to the liquid ammonia outlet of the ammonia hydrogen storage device, and the liquid ammonia obtained by the reaction in the ammonia hydrogen storage device is transported into the liquid ammonia transportation device through the liquid ammonia outlet; the other end of the liquid ammonia transportation device is connected to the inlet end of the ammonia hydrogen release device, and the liquid ammonia transported by the liquid ammonia transportation device is processed by the ammonia hydrogen release device to obtain purified hydrogen, a nitrogen-hydrogen mixture, and an ammonia-containing product.

[0067] In some embodiments, as Figure 1As shown, the ammonia hydrogen storage device includes a hydrogen-nitrogen pressurization and mixing component, a synthetic ammonia reaction component, a liquid ammonia separation component, and a recycle gas pressurization component. Among them, the intake side of the hydrogen-nitrogen pressurization and mixing component is respectively connected to a hydrogen source and a nitrogen source. Hydrogen in the hydrogen source and nitrogen in the nitrogen source are pressurized and mixed into a high-pressure mixed gas in the hydrogen-nitrogen pressurization and mixing unit. The outlet side of the hydrogen-nitrogen pressurization and mixing component is connected to the intake side of the synthetic ammonia reaction component. The high-pressure mixed gas undergoes a synthesis reaction in the synthetic ammonia reaction component to obtain a gas-liquid mixed ammonia. The outlet side of the synthetic ammonia reaction component is connected to the inlet side of the liquid ammonia separation component. The gas-liquid mixed ammonia is separated in the liquid ammonia separation component to generate liquid ammonia and gaseous ammonia. The gaseous ammonia is transported through a pipeline into the recycle gas pressurization component and, after being pressurized by the recycle gas pressurization component, is mixed into the high-pressure mixed gas.

[0068] Specifically, the hydrogen-nitrogen pressurization and mixing component includes a low-pressure hydrogen buffer tank 1, a hydrogen pressurization device 2, a high-pressure hydrogen buffer tank 3, a low-pressure nitrogen buffer tank 4, a nitrogen pressurization device 5, a high-pressure nitrogen buffer tank 6, and a high-pressure mixed gas buffer tank 7. Among them, the inlet of the low-pressure hydrogen buffer tank 1 is connected to the hydrogen source. The outlet of the low-pressure hydrogen buffer tank 1 is connected to the inlet of the hydrogen pressurization device 2 through a pipeline. The outlet of the hydrogen pressurization device 2 is connected to the high-pressure hydrogen buffer tank 3 through a pipeline. The inlet of the low-pressure nitrogen buffer tank 4 is connected to the nitrogen source. The outlet of the low-pressure nitrogen buffer tank 4 is connected to the inlet of the nitrogen pressurization device 5 through a pipeline. The outlet of the nitrogen pressurization device 5 is connected to the high-pressure nitrogen buffer tank 6 through a pipeline. The outlets of the high-pressure nitrogen buffer tank 6 and the high-pressure hydrogen buffer tank 3 are respectively connected to the high-pressure mixed gas buffer tank 7 through pipelines.

[0069] In this embodiment, the low-pressure hydrogen buffer tank 1, the low-pressure nitrogen buffer tank 4, the high-pressure hydrogen buffer tank 3, the high-pressure nitrogen buffer tank 6, and the high-pressure mixed-gas buffer tank 7 are all pressure vessels; the design pressures of the high-pressure hydrogen buffer tank 3, the high-pressure nitrogen buffer tank 6, and the high-pressure mixed-gas buffer tank 7 are 19.5 MPaG. The hydrogen boosting device 2 can be one of a booster pump, a booster fan, or a compressor, and the nitrogen boosting device 5 can be one of a booster pump, a booster fan, or a compressor. The low-pressure hydrogen buffer tank 1 is connected to the hydrogen boosting device 2 through a pipeline, and after boosting, it is connected to the high-pressure hydrogen buffer tank 3 through a pipeline. The low-pressure hydrogen buffer tank 1, the hydrogen boosting device 2, and the high-pressure hydrogen buffer tank 3 are all equipped with a pressure protection device (such as a relief valve) and a pressure control device (such as a pressure regulating valve). The high-pressure hydrogen buffer tank 3 is connected to the high-pressure mixed-gas buffer tank 7 through a pipeline, and a flow control valve is provided on this pipeline to control the ratio of hydrogen to nitrogen and the recycle gas return gas; the low-pressure nitrogen buffer tank 4 is connected to the nitrogen boosting device 5 through a pipeline, and after boosting, it is connected to the high-pressure nitrogen buffer tank 6 through a pipeline. The low-pressure nitrogen buffer tank 4, the nitrogen boosting device 5, and the high-pressure nitrogen buffer tank 6 are all equipped with a pressure protection device (such as a relief valve) and a pressure control device (such as a pressure regulating valve). The high-pressure nitrogen buffer tank 6 is connected to the high-pressure mixed-gas buffer tank 7 through a pipeline, and a flow control valve is provided on this pipeline to control the ratio of nitrogen to hydrogen and the recycle gas return gas.

[0070] Specifically, the ammonia synthesis reaction assembly includes a first gas-gas heat exchanger 8, a primary reactor 9, a mixing tank 10, and a secondary reactor 11; wherein, the outlet of the high-pressure mixed-gas buffer tank 7 is communicated with the low-temperature side pipe orifice of the first gas-gas heat exchanger 8 through a pipeline, and the inlet of the primary reactor 9 is communicated with the high-temperature side pipe orifice of the first gas-gas heat exchanger 8 through a pipeline; the inlet of the mixing tank 10 is connected to the outlet of the primary reactor 9, the inlet of the secondary reactor 11 is connected to the outlet of the mixing tank 10, and the outlet of the secondary reactor 11 serves as the outlet side of the ammonia synthesis reaction assembly and is connected to the inlet side of the liquid ammonia separation assembly.

[0071] In this embodiment, the ammonia synthesis reaction unit includes a first gas-gas heat exchanger 8, a preheating device, a primary reactor 9, a secondary reactor 11, and a mixing tank 10; the first gas-gas heat exchanger 8 is one of a shell-and-tube heat exchanger, a plate-frame heat exchanger, a double-pipe heat exchanger, a U-tube heat exchanger, or a fixed-tube-sheet heat exchanger; the primary reactor 9 is a fixed-bed reactor or other reactor, and the secondary reactor 11 is a fixed-bed reactor or other reactor; the preheating device can be one of a container-type heating device, an electric heater, or an electric heater with an outer sleeve on the pipeline; the preheating device can be combined with the primary reactor 9 and / or the secondary reactor 11, and the preheating device can be directly arranged outside or inside the primary reactor 9 and / or the secondary reactor 11. When arranged outside, it can be heated by flame, electric heating, a jacket device (oil bath, water bath, steam bath, or other high-temperature medium), and when arranged inside, it can be heated by an extended electric heating rod or an extended pipe (oil, water, steam, or other high-temperature medium); the primary reactor 9 and the secondary reactor 11 are filled with a catalyst for the reaction; the mixing tank 10 is a pressure vessel, and the design pressures of the first gas-gas heat exchanger 8, the preheating device, the primary reactor 9, the secondary reactor 11, and the mixing tank 10 are all 19.5 MPaG. The high-pressure mixed gas buffer tank 7 is connected to the low-temperature side pipe orifice of the first gas-gas heat exchanger 8 through a pipeline. The mixed gas is preheated by the first gas-gas heat exchanger 8 and enters the primary reactor 9 for reaction through the pipeline. The primary reactor 9 is connected to the high-temperature side pipe orifice of the first gas-gas heat exchanger 8 through a pipeline. The reacted mixed gas provides heat for the mixed gas coming from the high-pressure mixed gas buffer tank 7 through the first gas-gas heat exchanger 8. Part of the cooled product mixed gas enters the secondary reactor 11 through a pipeline and further reacts in the secondary reactor 11, and then enters the first gas-liquid water-cooled heat exchanger 12 through a pipeline.

[0072] Specifically, the liquid ammonia separation component includes a first gas-liquid water-cooled heat exchanger 12, a first deep gas-liquid water-cooled heat exchanger 13, a gas-liquid separator 14, and a first liquid ammonia storage tank 17; wherein, the outlet of the secondary reactor 11 is communicated with the inlet of the first gas-liquid water-cooled heat exchanger 12, and the inlet of the first deep gas-liquid water-cooled heat exchanger 13 is communicated with the outlet of the first gas-liquid water-cooled heat exchanger 12; the inlet of the gas-liquid separator 14 is communicated with the outlet of the first deep gas-liquid water-cooled heat exchanger 13. The gas outlet of the gas-liquid separator 14 is communicated with the inlet of the recycle gas boosting component, the outlet of the recycle gas boosting component is communicated with the high-pressure mixed gas buffer tank 7, and the tail gas outlet of the gas-liquid separator 14 is communicated with the discharge main pipe; the inlet of the first liquid ammonia storage tank 17 is communicated with the liquid outlet of the gas-liquid separator 14, and the outlet of the first liquid ammonia storage tank 17 is communicated with the liquid ammonia transportation device 18.

[0073] In this embodiment, the first gas-liquid water-cooled heat exchanger 12 is one of a shell-and-tube heat exchanger, a plate-frame heat exchanger, a double-pipe heat exchanger, a U-tube heat exchanger, or a fixed-tube-sheet heat exchanger; the gas-liquid cryogenic heat exchanger is one of a shell-and-tube heat exchanger, a plate-frame heat exchanger, a double-pipe heat exchanger, a U-tube heat exchanger, or a fixed-tube-sheet heat exchanger; the gas-liquid separator 14 and the first liquid ammonia storage tank 17 are pressure vessels; the design pressures of the medium sides of the first gas-liquid water-cooled heat exchanger 12, the first gas-liquid deep water-cooled heat exchanger 13, and the gas-liquid separator 14 are all 19.5 MPaG; a pressure reducing device is provided on the pipeline between the gas-liquid separator 14 and the first liquid ammonia storage tank 17, and the design pressure of the first liquid ammonia storage tank 17 is 1.2 MPaG; the liquid ammonia transportation device 18 is one of a canned transportation vehicle, a filling transportation train, or a tubular transportation device. During the working process, the reaction mixed gas enters the first gas-liquid water-cooled heat exchanger 12 and the first gas-liquid deep water-cooled heat exchanger 13 through pipelines respectively, is gradually cooled, and then enters the gas-liquid separator 14. The liquid ammonia generated by condensation enters the first liquid ammonia storage tank 17 and the subsequent liquid ammonia conveying device through the pipeline below the gas-liquid separator 14; the gas-phase mixed gas separated by the gas-liquid separator 14 enters the previous cycle gas buffer tank 16 through the pipeline.

[0074] Further, the ammonia hydrogen storage device provided by the present invention further includes a cycle gas boosting assembly. Please continue to refer to Figure 1 , the cycle gas boosting unit includes a cycle gas boosting device 15 and a cycle gas buffer tank 16; the cycle gas boosting device 15 is one of a booster pump, a booster fan, or a compressor; the cycle gas buffer tank 16 is a pressure vessel; the design pressure of the cycle gas high-pressure buffer tank is 19.5 MPaG; the cycle gas boosting device 15 is connected to the cycle gas buffer tank 16 through a pipeline. After the boosted cycle gas enters the cycle gas buffer tank 16 through the pipeline, it enters the mixed gas high-pressure buffer tank through the pipeline and is recycled. Both the cycle gas buffer tank 16 and the cycle gas boosting device 15 are provided with a pressure protection device (such as a relief valve) and a pressure control device (such as a pressure control valve). A flow control valve is provided on the pipeline connecting the cycle gas buffer tank 16 to the high-pressure mixed gas buffer tank 7, and this flow control valve is used to control the ratio of the cycle mixed gas to the nitrogen and hydrogen return gas.

[0075] In some embodiments, such as Figure 2As shown, the ammonia hydrogen release device includes a liquid ammonia gasification component, an ammonia decomposition component, a hydrogen separation component, and a hydrogen purification component; wherein, the other end of the liquid ammonia delivery device is connected to the inlet side of the liquid ammonia gasification component, and the liquid ammonia delivered by the liquid ammonia delivery device is processed by the liquid ammonia gasification component to obtain high-pressure ammonia gas; the inlet side of the ammonia decomposition component is connected to the outlet side of the liquid ammonia gasification component, and the high-pressure ammonia gas delivered by the liquid ammonia gasification component undergoes a decomposition reaction in the ammonia decomposition component to obtain a reaction mixture of ammonia gas, hydrogen gas, and nitrogen gas; the inlet side of the hydrogen separation component is connected to the mixed gas outlet of the ammonia decomposition component, and the reaction mixture is cooled by the hydrogen separation component to obtain a cooled mixed gas; the inlet side of the hydrogen purification component is connected to the outlet side of the hydrogen separation component, and the cooled mixed gas is separated into hydrogen gas, nitrogen gas, and ammonia-containing products in the hydrogen purification component.

[0076] Specifically, the liquid ammonia gasification component includes a second liquid ammonia storage tank 19, a liquid ammonia transfer pump 20, a liquid ammonia vaporizer 21, and an ammonia gas buffer tank 22 that are sequentially connected through pipelines, wherein the inlet of the second liquid ammonia storage tank 19 is connected to the liquid ammonia delivery device. In this embodiment, the liquid ammonia gasification unit includes a second liquid ammonia storage tank 19, a liquid ammonia transfer pump 20, a liquid ammonia vaporizer 21, and an ammonia gas buffer tank 22; the liquid ammonia vaporizer 21 is one of a shell-and-tube heat exchanger, a plate-frame heat exchanger, a double-pipe heat exchanger, a U-tube heat exchanger, or a fixed-tube-sheet heat exchanger; both the second liquid ammonia storage tank 19 and the ammonia gas buffer tank 22 are pressure vessels; the liquid ammonia transfer pump 20 is one of a centrifugal pump, a reciprocating pump, a metering pump, a gear pump, or a rotary positive-displacement pump; the design pressures of both the second liquid ammonia storage tank 19 and the ammonia gas buffer tank 22 are 1.2 MPaG; the liquid ammonia in the second liquid ammonia storage tank 19 comes from the liquid ammonia delivery device, and the second liquid ammonia storage tank 19, the liquid ammonia transfer pump 20, the liquid ammonia vaporizer 21, and the ammonia gas buffer tank 22 are connected through pipelines to enable the liquid ammonia to complete the pressurization and gasification processes.

[0077] As Figure 2As shown, the ammonia decomposition component includes a second gas-gas heat exchanger 23 and an ammonia decomposition reactor 24 connected by a pipeline. Among them, the low-temperature side pipe orifice of the second gas-gas heat exchanger 23 is connected to the outlet of the ammonia buffer tank 22, and the high-temperature side pipe orifice of the second gas-gas heat exchanger 23 is connected to the inlet of the ammonia decomposition reactor 24. In this embodiment, the second gas-gas heat exchanger 23 is one of a shell-and-tube heat exchanger, a plate-frame heat exchanger, a double-pipe heat exchanger, a U-tube heat exchanger, or a fixed tube sheet heat exchanger; the ammonia decomposition reactor 24 is a fixed-bed reactor or other types of reactors; the ammonia decomposition reactor 24 is equipped with a heating device, and the heating device can be directly arranged outside or inside the ammonia decomposition reactor 24. When arranged outside, it can use flame heating, electric heating, jacket equipment (oil bath, water bath, steam bath, or other high-temperature media) heating. When arranged inside, it can use internal extended electric heating rods for heating, internal extended tubes (oil, water, steam, or other high-temperature media) for heating; the inside of the ammonia decomposition reactor 24 is filled with a reaction catalyst; the ammonia decomposition reactor 24 is a pressure vessel with a design pressure of 1.2 MPaG and a design temperature of 850 °C. The ammonia buffer tank 22 is connected to the low-temperature side pipe orifice of the second gas-gas heat exchanger 23 through a pipeline. Ammonia is preheated by the second gas-gas heat exchanger 23 and enters the ammonia decomposition reactor 24 through a pipeline for reaction. The ammonia decomposition reactor 24 is connected to the high-temperature side pipe orifice of the second gas-gas heat exchanger 23 through a pipeline. The reacted ammonia provides heat for the ammonia in the ammonia buffer tank 22 through the second gas-gas heat exchanger 23. Part of the cooled product gas mixture enters the second gas-liquid water-cooled heat exchanger 25 through a pipeline.

[0078] The above hydrogen separation component includes a second gas-liquid water-cooled heat exchanger 25, a second gas-liquid deep water-cooled heat exchanger 26, and an ammonia-nitrogen-hydrogen buffer tank 27 connected in sequence through a pipeline. Among them, the inlet of the second gas-liquid water-cooled heat exchanger 25 is connected to the outlet of the ammonia decomposition reactor 24; in this embodiment, the second gas-liquid water-cooled heat exchanger 25 is one of a shell-and-tube heat exchanger, a plate-frame heat exchanger, a double-pipe heat exchanger, a U-tube heat exchanger, or a fixed tube sheet heat exchanger; the gas-liquid deep-cooled heat exchanger is one of a shell-and-tube heat exchanger, a plate-frame heat exchanger, a double-pipe heat exchanger, a U-tube heat exchanger, or a fixed tube sheet heat exchanger; the ammonia-nitrogen-hydrogen buffer tank 27 is a pressure vessel with a design pressure of 1.2 MPaG; the reaction gas mixture enters the second gas-liquid water-cooled heat exchanger 25 and the second gas-liquid deep water-cooled heat exchanger 26 through a pipeline and is gradually cooled and then enters the ammonia-nitrogen-hydrogen buffer tank 27.

[0079] The hydrogen purification component includes a hydrogen dryer 28, a nitrogen-hydrogen buffer tank 29, a nitrogen-hydrogen pressurizing device, and an adsorption device 31 connected in sequence through pipelines. Among them, the inlet of the hydrogen dryer 28 is connected to the outlet of the ammonia-nitrogen-hydrogen buffer tank 27. The nitrogen outlet of the adsorption device 31 is connected to a nitrogen buffer tank 33, and the hydrogen outlet of the adsorption device 31 is connected to a hydrogen buffer tank 32. In this embodiment, the hydrogen purification unit includes a hydrogen dryer 28, a nitrogen-hydrogen buffer tank 29, a nitrogen-hydrogen pressurizing device, an adsorption device 31, a nitrogen buffer tank 33, and a hydrogen buffer tank 32. The hydrogen dryer 28 is a packed tower and belongs to a pressure vessel. The nitrogen-hydrogen buffer tank 29, the nitrogen buffer tank 33, and the hydrogen buffer tank 32 are all pressure vessels. The nitrogen-hydrogen increasing device is one of a booster pump, a booster fan, or a compressor. The adsorption device 31 is one of a pressure swing adsorption, a temperature swing adsorption, or a membrane treatment device. The gas in the ammonia-nitrogen-hydrogen buffer tank 27 is connected to the hydrogen dryer 28 through a pipeline. The hydrogen dryer 28 is connected to the nitrogen-hydrogen buffer tank 29 and the nitrogen-hydrogen pressurizing device through pipelines. The nitrogen-hydrogen buffer tank 29 and the nitrogen-hydrogen pressurizing device are both equipped with a pressure protection device and a pressure control device. The nitrogen-hydrogen pressurizing device is connected to the adsorption device 31 through a pipeline. The adsorption device 31 is subsequently connected to the nitrogen buffer tank 33 and the hydrogen buffer tank 32 through pipelines. The nitrogen in the nitrogen buffer tank 33 can be recycled, and the hydrogen stored in the hydrogen buffer tank 32 is the hydrogen stored and released by the ammonia hydrogen storage device.

[0080] In addition to the above ammonia hydrogen storage process device, the present invention also provides a process method for the storage, transportation, purification, and use of green hydrogen energy. The method includes the following steps:

[0081] Step (1): Using a catalyst, high-pressure hydrogen, and high-pressure nitrogen obtained after pressurization as reaction raw materials, performing a synthesis reaction. After the heat of reaction of the synthesis reaction product is withdrawn, it is input into a gas-liquid separation tank through a first gas-liquid water cooler and a first gas-liquid deep water cooler. The unreacted gas is pressurized and mixed with the reaction raw materials and then undergoes a synthesis reaction again;

[0082] Step (2): Inputting the liquid-phase product of the synthesis reaction in step (1) into a liquid ammonia transportation device and transporting it to an ammonia hydrogen release device through the liquid ammonia transportation device;

[0083] Step (3): Pressurizing and heating the liquid-phase product in step (2) and entering an ammonia decomposition reactor for a decomposition reaction. After the heat of reaction of the decomposition reaction product is withdrawn, it is input into an ammonia-nitrogen-hydrogen buffer tank through a second gas-liquid water cooler and a second gas-liquid deep water cooler;

[0084] Step (4): Inputting the product of the reaction in step (3) into a dryer for gas-liquid separation. The separated gas is pressurized and undergoes purification separation in an adsorption device to obtain hydrogen.

[0085] In some embodiments, in step (1), the catalyst is one of copper-based, manganese-based, nickel-based, titanium-based, and magnesium-based catalysts; the pressure of the synthesis reaction is 11 to 19.5 MPaG; the temperature of the synthesis reaction is 325 to 575 °C; the reaction space velocity of the synthesis reaction is 50,000 to 130,000; and / or,

[0086] In steps (1) and (2), the storage pressure of liquid ammonia is 0.8 to 1.5 MPaG, and the storage temperature is -20 to -5 °C.

[0087] In some embodiments, in step (3), the catalyst is one of copper-based, manganese-based, nickel-based, titanium-based, and magnesium-based catalysts; the pressure of the decomposition reaction is 0.8 to 1.2 MPaG; the temperature of the decomposition reaction is 500 to 850 °C; the reaction space velocity is 50,000 to 130,000; the temperature of the reaction product after condensation by the second gas-liquid water-cooled heat exchanger and the second gas-liquid deep water-cooled heat exchanger is 15 to 30 °C.

[0088] In a specific embodiment, the process method provided by the present invention includes the following steps:

[0089] Step (1): Input the reaction raw materials containing pressurized hydrogen and nitrogen into the first-stage reactor and the second-stage reactor for synthesis reaction. After the heat of the synthesis reaction product is removed by the first gas-gas heat exchanger, it passes through the first gas-liquid water-cooled heat exchanger and the first gas-liquid deep water-cooled heat exchanger and then enters the gas-liquid separation tank. The unreacted gas is pressurized and mixed with the raw materials and then enters reactor A and reactor B for synthesis reaction; wherein, the reaction raw materials include hydrogen and nitrogen, and the catalyst is one of copper-based, manganese-based, nickel-based, titanium-based, or magnesium-based catalysts; the hydrogen pressurization system and the nitrogen pressurization system increase the pressure from 1.0 MPaG to 11 to 19.5 MPaG, that is, the pressure of the synthesis reaction is 11 to 19.5 MPaG; the temperature of the synthesis reaction is 325 to 575 °C; the reaction space velocity is 50,000 to 130,000; in the synthesis reaction, due to the exothermic heat of the synthesis reaction, the reaction rate decreases. A first gas-gas heat exchanger is added between the first-stage reactor and the second-stage reactor to take away the heat in the first-stage reactor with the initial reaction gas to reduce the heat during the reaction and increase the reaction rate of the synthesis reaction in the second-stage reactor; the reaction product is condensed by the first gas-liquid water-cooled heat exchanger and the first gas-liquid deep water-cooled heat exchanger and then undergoes gas-liquid separation, and the gas obtained from the gas-liquid separation returns to the first-stage reactor for recycling as raw materials; the storage pressure of liquid ammonia is 0.8 to 1.5 MPaG, and the storage temperature is -20 to -5 °C.

[0090] Step (2): Feed the liquid-phase product from the synthesis reaction in step (1) into an ammonia transportation device and transport it to the required ammonia dehydrogenation device; the storage pressure of the liquid ammonia is 0.8 - 1.5 MPaG, and the storage temperature is -20 - -5 °C.

[0091] Step (3): Feed the liquid-phase product in step (2) into an ammonia decomposition reactor through pressurization and temperature increase for decomposition reaction. After the reaction heat of the decomposition reaction product is removed by a second gas-gas heat exchanger, it is fed into an ammonia-nitrogen-hydrogen buffer tank through a second gas-liquid water cooler and a second gas-liquid deep water cooler; the catalyst is one of copper-based, manganese-based, nickel-based, titanium-based or magnesium-based catalysts; the pressurization system increases the pressure from to 0.8 - 1.2 MPaG, that is, the pressure of the decomposition reaction is 0.8 - 1.2 MPaG; the temperature of the decomposition reaction is 500 - 850 °C; the reaction space velocity is 50,000 - 130,000; the temperature of the reaction product after condensation by the second gas-liquid water cooler and the second gas-liquid deep water cooler is 15 - 30 °C.

[0092] Step (4): Feed the product from the reaction in step (3) into a dryer for gas-liquid separation. The separated gas is pressurized and then purified and separated in an adsorption device to obtain hydrogen; the adsorbent in the dryer can absorb water and liquid ammonia; all the dryer adsorbents are either high-temperature regenerable or non-regenerable; when the dryer adsorbent is a high-temperature regenerable adsorbent, the ammonia mixture removed needs to be absorbed and discharged up to standard through an absorption tower, and the absorption tower is one of water, alkali, and acid absorption towers; the purified nitrogen-hydrogen mixture after separation can be discharged and recycled to step (1).

[0093] In the above process method, due to different requirements for indicators such as the form of the synthesis reaction, decomposition reaction, catalyst, use of hydrogen, and product scale, the control of pressure, temperature, residence time, etc. in each reaction unit is different, but it must meet the pressure and temperature ranges corresponding to the gas-phase reaction conditions to prevent phenomena such as liquid hammer, overpressure, and runaway during the reaction; after the synthesis reaction and decomposition reaction, through various heat exchanger forms such as gas-gas reactors, gas-liquid water coolers, and gas-liquid deep coolers, the reaction raw materials, reaction gas, steam, circulating cooling water, and chilled water are optimized, which is an economic mode for the whole system, reducing energy consumption, improving the utilization rates of hydrogen, nitrogen, and ammonia, and reducing the unit consumption; the purification and separation system can adopt a membrane recovery system, pressure swing adsorption system, or temperature swing adsorption system, which can realize the purification of hydrogen in the components, as well as the reverse osmosis recovery of nitrogen, improving quality and efficiency, reducing unit consumption, and improving drying efficiency.

[0094] A process method and device for storing, transporting, purifying and using green hydrogen energy provided by the present invention can produce high-concentration liquid ammonia products, convert hydrogen gas into liquid, reduce problems such as high pressure and large gas volume, and solve problems such as difficult storage and transportation and high costs; all emissions, gas emissions, etc. are collected and treated and then returned for use as raw material gas, with the lowest specific consumption; the waste water and waste residue in the three wastes are collected and treated in a three-in-one manner, which is more environmentally friendly; the utilization systems of raw material gas, reaction gas, steam, circulating cooling water and chilled water are optimized, with more savings in investment and more energy conservation; the drying and purification separation system can be a dryer, or a drying tower, or a reverse osmosis membrane system, or a pressure swing adsorption system, or a temperature swing adsorption system, for hydrogen purification and nitrogen-hydrogen separation; it can achieve a multi-production capacity device layout of 50,000 to 400,000 tons / year of liquid ammonia products (that is, 8,900 to 70,200 tons / year of hydrogen can be stored and transported), with flexible and convenient operation, safety and reliability, high automation, better product performance, more suitable for the storage, transportation, purification and use of green hydrogen energy, and taking a high-end production route. The present invention has few moving equipment, a short device construction period, a compact layout, and can adopt modular construction, greatly reducing the investment cost.

[0095] The above specific implementation manners have further detailed the purpose, technical solution and beneficial effects of the present invention. It should be understood that the above are only the specific implementation manners of the present invention and are not used to limit the protection scope of the present invention. Any modifications, equivalent replacements, improvements, etc. made on the basis of the technical solution of the present invention shall be included in the protection scope of the present invention.

Claims

1. A device for storing, transporting and purifying green hydrogen, characterized in that: The device comprises: An ammonia hydrogen storage device, wherein the feed end of the ammonia hydrogen storage device is respectively connected to a hydrogen source and a nitrogen source, the hydrogen in the hydrogen source and the nitrogen in the nitrogen source enter the ammonia hydrogen storage device through pipelines, and are processed by the ammonia hydrogen storage device to obtain liquid ammonia; A liquid ammonia conveying device, one end of which is connected to the liquid ammonia outlet of the ammonia hydrogen storage device, and the liquid ammonia obtained by the reaction in the ammonia hydrogen storage device is conveyed to the liquid ammonia conveying device through the liquid ammonia outlet; The ammonia hydrogen release device, the other end of the liquid ammonia conveying device is connected to the inlet end of the ammonia hydrogen release device, and the liquid ammonia conveyed by the liquid ammonia conveying device is processed by the ammonia hydrogen release device to obtain purified hydrogen, nitrogen-hydrogen mixture and ammonia-containing products.

2. The device for storing, transporting and purifying green hydrogen according to claim 1 is characterized in that: The ammonia hydrogen storage device comprises: A hydrogen-nitrogen pressurized mixing component, wherein the air inlet side of the hydrogen-nitrogen pressurized mixing component is respectively connected to a hydrogen source and a nitrogen source, and the hydrogen in the hydrogen source and the nitrogen in the nitrogen source are pressurized and mixed into a high-pressure mixed gas in the hydrogen-nitrogen pressurized mixing unit; A synthetic ammonia reaction component, wherein the outlet side of the hydrogen-nitrogen pressurized mixing component is connected to the inlet side of the synthetic ammonia reaction component, and the high-pressure mixed gas completes the synthesis reaction in the synthetic ammonia reaction component to obtain gas-liquid mixed ammonia; A liquid ammonia separation component, wherein the outlet side of the synthetic ammonia reaction component is connected to the inlet side of the liquid ammonia separation component, and the gas-liquid mixed ammonia is separated into liquid ammonia and gaseous ammonia in the liquid ammonia separation component; A circulating gas pressurizing component, wherein the gaseous ammonia is transported to the circulating gas pressurizing component through a pipeline, and is mixed into the high-pressure mixed gas after being pressurized by the circulating gas pressurizing component.

3. The device for storing, transporting and purifying green hydrogen according to claim 2 is characterized in that: The hydrogen-nitrogen boosting mixing assembly comprises: A hydrogen low-pressure buffer tank, wherein the inlet of the hydrogen low-pressure buffer tank is connected to the hydrogen source; A hydrogen boosting device, wherein the outlet of the hydrogen low-pressure buffer tank is connected to the inlet of the hydrogen boosting device through a pipeline; A hydrogen high-pressure buffer tank, wherein the outlet of the hydrogen booster device is connected to the hydrogen high-pressure buffer tank through a pipeline; A nitrogen low-pressure buffer tank, wherein the inlet of the nitrogen low-pressure buffer tank is connected to the nitrogen source; A nitrogen booster device, wherein the outlet of the nitrogen low-pressure buffer tank is connected to the inlet of the nitrogen booster device through a pipeline; A nitrogen high-pressure buffer tank, wherein the outlet of the nitrogen booster device is connected to the nitrogen high-pressure buffer tank through a pipeline; A high-pressure mixed gas buffer tank, wherein the outlet of the nitrogen high-pressure buffer tank and the outlet of the hydrogen high-pressure buffer tank are respectively connected to the high-pressure mixed gas buffer tank through pipelines.

4. The device for storing, transporting and purifying green hydrogen according to claim 3 is characterized in that: The synthetic ammonia reaction assembly comprises: A first gas-to-gas heat exchanger, wherein the outlet of the high-pressure mixed gas buffer tank is connected to a low-temperature side pipe outlet of the first gas-to-gas heat exchanger through a pipeline; A primary reactor, the inlet of which is connected to the high-temperature side pipe outlet of the first gas-to-gas heat exchanger through a pipeline; a mixing tank, wherein the inlet of the mixing tank is connected to the outlet of the primary reactor; A secondary reactor, the inlet of the secondary reactor is connected to the outlet of the mixing tank, and the outlet of the secondary reactor serves as the outlet side of the synthetic ammonia reaction component and is connected to the inlet side of the liquid ammonia separation component.

5. The device for storing, transporting and purifying green hydrogen according to claim 4 is characterized in that: The liquid ammonia separation component comprises: a first gas-liquid water-cooled heat exchanger, wherein the outlet of the secondary reactor is connected to the inlet of the first gas-liquid water-cooled heat exchanger; A first gas-liquid deep water-cooled heat exchanger, wherein an inlet of the first gas-liquid deep water-cooled heat exchanger is connected to an outlet of the first gas-liquid water-cooled heat exchanger; A gas-liquid separator, wherein the inlet of the gas-liquid separator is connected to the outlet of the first gas-liquid deep water-cooled heat exchanger, the gaseous outlet of the gas-liquid separator is connected to the inlet of the circulating gas boosting component, the outlet of the circulating gas boosting component is connected to the high-pressure mixed gas buffer tank, and the tail gas outlet of the gas-liquid separator is connected to the exhaust main pipe; A first liquid ammonia storage tank, wherein the inlet of the first liquid ammonia storage tank is connected to the liquid outlet of the gas-liquid separator, and the outlet of the first liquid ammonia storage tank is connected to the liquid ammonia transport device.

6. The device for storing, transporting and purifying green hydrogen according to claim 1, characterized in that: The ammonia hydrogen release device comprises: A liquid ammonia gasification component, wherein the other end of the liquid ammonia conveying device is connected to the inlet side of the liquid ammonia gasification component, and the liquid ammonia conveyed by the liquid ammonia conveying device is processed by the liquid ammonia gasification component to obtain high-pressure ammonia gas; an ammonia decomposition component, wherein the inlet side of the ammonia decomposition component is connected to the outlet side of the liquid ammonia gasification component, and the high-pressure ammonia gas delivered by the liquid ammonia gasification component undergoes a decomposition reaction in the ammonia decomposition component to obtain a reaction mixture of ammonia, hydrogen and nitrogen; A hydrogen separation component, wherein the inlet side of the hydrogen separation component is connected to the mixed gas outlet of the ammonia decomposition component, and the reaction mixed gas is cooled by the hydrogen separation component to obtain a cooled mixed gas; A hydrogen purification component, wherein the inlet side of the hydrogen purification component is connected to the outlet side of the hydrogen separation component, and the cooled mixed gas is separated into hydrogen, nitrogen and ammonia-containing products in the hydrogen purification component.

7. The device for storing, transporting and purifying green hydrogen according to claim 6 is characterized in that: The liquid ammonia gasification assembly comprises a second liquid ammonia storage tank, a liquid ammonia delivery pump, a liquid ammonia vaporizer and an ammonia buffer tank which are sequentially connected through pipelines, wherein the inlet of the second liquid ammonia storage tank is connected to the liquid ammonia delivery device; The ammonia decomposition component comprises a second gas-to-gas heat exchanger and an ammonia decomposition reactor connected by a pipeline, wherein the low-temperature side pipe port of the second gas-to-gas heat exchanger is connected to the outlet of the ammonia buffer tank, and the high-temperature side pipe port of the second gas-to-gas heat exchanger is connected to the inlet of the ammonia decomposition reactor; The hydrogen separation assembly comprises a second gas-liquid water-cooled heat exchanger, a second gas-liquid deep water-cooled heat exchanger and an ammonia nitrogen hydrogen buffer tank which are sequentially connected through pipelines, wherein the inlet of the second gas-liquid water-cooled heat exchanger is connected to the outlet of the ammonia decomposition reactor; The hydrogen purification component includes a hydrogen dryer, a nitrogen-hydrogen buffer tank, a nitrogen-hydrogen booster and an adsorption device in sequence through pipelines, wherein the inlet of the hydrogen dryer is connected to the outlet of the ammonia-nitrogen-hydrogen buffer tank, the nitrogen outlet of the adsorption device is connected to the nitrogen buffer tank, and the hydrogen outlet of the adsorption device is connected to the hydrogen buffer tank.

8. A process for storing, transporting and purifying green hydrogen, characterized in that: The method comprises the following steps: Step (1): using the catalyst and the high-pressure hydrogen and high-pressure nitrogen obtained after pressurization as reaction raw materials to carry out a synthesis reaction; after the reaction heat is removed from the product of the synthesis reaction, it is input into a gas-liquid separation tank through a first gas-liquid water-cooled heat exchanger and a first gas-liquid deep water-cooled heat exchanger; the unreacted gas is pressurized and mixed with the reaction raw materials before carrying out a synthesis reaction; Step (2): the liquid phase product of the synthesis reaction in step (1) is input into a liquid ammonia transport device, and then transported to an ammonia hydrogen release device through the liquid ammonia transport device; Step (3): the liquid phase product in step (2) is fed into the ammonia decomposition reactor by pressurization and temperature increase to undergo a decomposition reaction. After the reaction heat is removed from the decomposition reaction product, it is fed into the ammonia nitrogen hydrogen buffer tank through a second gas-liquid water-cooled heat exchanger and a second gas-liquid deep water-cooled heat exchanger; Step (4): The product of the reaction in step (3) is input into a dryer for gas-liquid separation, and the separated gas is pressurized and purified and separated in an adsorption device to obtain hydrogen.

9. The process for storing, transporting and purifying green hydrogen according to claim 8, characterized in that: In step (1), the catalyst is one of copper, manganese, nickel, titanium and magnesium catalysts; the pressure of the synthesis reaction is 11-19.5 MPaG; the temperature of the synthesis reaction is 325-575° C.; the reaction space velocity of the synthesis reaction is 50000-130000; and / or, In step (1) and step (2), the storage pressure of liquid ammonia is 0.8 to 1.5 MPaG, and the storage temperature is -20 to -5°C.

10. The process for storing, transporting and purifying green hydrogen according to claim 8, characterized in that: In step (3), the catalyst is one of copper, manganese, nickel, titanium and magnesium catalysts; the pressure of the decomposition reaction is 0.8-1.2 MPaG; the temperature of the decomposition reaction is 500-850°C; the reaction space velocity is 50,000-130,000; the temperature of the reaction product after condensation through the second gas-liquid water-cooled heat exchanger and the second gas-liquid deep water-cooled heat exchanger is 15-30°C.

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