Process and device for green hydrogen energy storage, transportation and purification

Abstract

The application discloses a process method and device for green hydrogen energy storage, transportation and purification, comprising ammonia hydrogen storage and ammonia hydrogen release two parts, wherein 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 delivered by a liquid ammonia delivery device is treated by an ammonia hydrogen release device to obtain purified hydrogen, a nitrogen-hydrogen mixture and an ammonia-containing product. The scheme can produce high-concentration liquid ammonia products, convert helium from gas to liquid, reduce the problems of pressure and large gas volume, solve the problems of storage and transportation difficulties, high cost and the like; all emissions, gas emissions and the like are collected and treated to return to be used as raw material gas, and the single consumption is the lowest; waste water, waste residue and waste gas in the three wastes are collected and treated in a three-in-one mode, which is more environmentally friendly; an investment is more saved and more energy-saving in an optimized raw material gas, reaction gas, steam, circulating cooling water and refrigerated water utilization system.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of chemical process and equipment technology, in particular to a process method and device for green hydrogen energy storage, transportation and purification. BACKGROUND

[0002] Hydrogen energy is an important secondary clean energy to replace fossil energy and solve the problem of insufficient utilization of wind and solar energy. From the perspective of energy storage and transportation, high-pressure gaseous hydrogen storage is the most mature and widely used hydrogen storage technology at present. It compresses hydrogen into a high-pressure container, usually using a steel cylinder as a storage container. However, high-pressure hydrogen storage needs to withstand high pressure, which has certain safety hazards, and the hydrogen storage density is relatively low. Therefore, the main difficulties of hydrogen energy application are high storage and transportation difficulty and high storage and transportation cost. From the application perspective, the traditional process is to synthesize ammonia from hydrogen and nitrogen, and the synthesized ammonia is mainly used for the production of nitrogen fertilizer and compound fertilizer, such as urea, ammonium nitrate, ammonium phosphate, ammonium chloride and various nitrogen-containing compound fertilizers, or for the production of nitric acid, various nitrogen-containing inorganic salts and organic intermediates, sulfonamide drugs, polyurethane, polyamide fiber and nitrile rubber, etc. Hydrogen is mainly used as an intermediate or raw material for chemical products. There is a problem that hydrogen energy cannot be used as a secondary clean energy.

[0003] Therefore, the present application provides a process method and device for green hydrogen energy storage, transportation and purification to at least partially solve the problems of high hydrogen energy transportation difficulty and limited utilization range in the prior art. SUMMARY

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

[0005] In order to achieve the above-mentioned purpose, the embodiments of the present application provide the following technical solutions:

[0006] The present application provides a device for green hydrogen energy storage, transportation and purification, which comprises:

[0007] An ammonia hydrogen storage device, the feed end of the ammonia hydrogen storage device is connected in communication with 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 a pipeline, and liquid ammonia is obtained after treatment of the ammonia hydrogen storage device;

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

[0009] An ammonia hydrogen release device, the other end of the liquid ammonia conveying device is connected with the inlet end of the ammonia hydrogen release device, and the 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.

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

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

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

[0013] A liquid ammonia separation assembly, the outlet side of the synthetic ammonia reaction assembly is connected with 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 circulating gas pressurization assembly, the gaseous ammonia is conveyed to the circulating gas pressurization assembly through a pipeline and mixed into the high-pressure mixed gas after being pressurized by the circulating gas pressurization assembly.

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

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

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

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

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

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

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

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

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

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

[0025] a primary reactor, an inlet of the primary reactor is connected to a high-temperature side port of the first gas-gas heat exchanger through a pipeline;

[0026] a mixing tank, an inlet of the mixing tank is connected to an outlet of the primary reactor;

[0027] a secondary reactor, an inlet of the secondary reactor is connected to an outlet of the mixing tank, and an outlet of the secondary reactor is connected to an inlet of the liquid ammonia separation assembly as an outlet side of the ammonia synthesis reaction assembly.

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

[0029] a first gas-liquid water-cooled heat exchanger, an outlet of the secondary reactor is connected to an inlet of the first gas-liquid water-cooled heat exchanger;

[0030] a first gas-liquid deep water-cooled heat exchanger, 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;

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

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

[0033] In some embodiments, the ammonia hydrogen release device comprises:

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

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

[0036] a hydrogen separation assembly, an inlet side of the hydrogen separation assembly being in communication with the mixed gas outlet of the ammonia decomposition assembly, the reaction mixed gas being cooled by the hydrogen separation assembly to obtain cooled mixed gas;

[0037] a hydrogen purification assembly, an inlet side of the hydrogen purification assembly being in communication with the outlet side of the hydrogen separation assembly, the cooled mixed gas being separated into hydrogen, nitrogen and ammonia-containing product in the hydrogen purification assembly.

[0038] In some embodiments, the liquid ammonia gasification assembly comprises, in sequence and in communication through pipelines, a second liquid ammonia storage tank, a liquid ammonia delivery pump, a liquid ammonia vaporizer and an ammonia gas buffer tank, wherein the inlet of the second liquid ammonia storage tank is in communication with the liquid ammonia delivery device;

[0039] The ammonia decomposition assembly comprises, in communication through pipelines, a second gas-gas heat exchanger and an ammonia decomposition reactor, wherein the low-temperature side pipe opening of the second gas-gas heat exchanger is in communication with the outlet of the ammonia gas buffer tank, and the high-temperature side pipe opening of the second gas-gas heat exchanger is in communication with the inlet of the ammonia decomposition reactor;

[0040] The hydrogen separation assembly comprises, in sequence and in communication through pipelines, a second gas-liquid water-cooled heat exchanger, a second gas-liquid deep water-cooled heat exchanger and an ammonia-nitrogen-hydrogen buffer tank, wherein the inlet of the second gas-liquid water-cooled heat exchanger is in communication with the outlet of the ammonia decomposition reactor;

[0041] The hydrogen purification assembly comprises, in sequence and in communication through pipelines, a hydrogen gas dryer, an ammonia-nitrogen-hydrogen buffer tank, a nitrogen-hydrogen pressurizing device and an adsorption device, wherein the inlet of the hydrogen gas dryer is in communication with the outlet of the ammonia-nitrogen-hydrogen buffer tank, the nitrogen gas outlet of the adsorption device is in communication with a nitrogen gas buffer tank, and the hydrogen gas outlet of the adsorption device is in communication with a hydrogen gas buffer tank.

[0042] The present application also provides a process for green hydrogen energy storage, transportation, purification and use, which comprises the following steps:

[0043] Step (1): using the catalyst and the high-pressure hydrogen and high-pressure nitrogen obtained after pressurization as reaction raw materials to perform a synthesis reaction, and after removing the reaction heat from the product of the synthesis reaction, inputting the product 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, and pressurizing the unreacted gas and mixing it with the reaction raw materials to perform the synthesis reaction again;

[0044] Step (2): inputting the liquid-phase product of the synthesis reaction in step (1) into a liquid ammonia transportation device, and delivering the product to an ammonia hydrogen release device through the liquid ammonia delivery device;

[0045] Step (3): the liquid phase product in step (2) is decomposed in an ammonia decomposition reactor by pressurization and temperature increase, and the product of the decomposition reaction is input into an ammonia-nitrogen-hydrogen buffer tank after the reaction heat is removed and the product is cooled by 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 a copper-based, manganese-based, nickel-based, titanium-based, and magnesium-based catalyst; the pressure of the synthesis reaction is 11-19.5 MPaG; the temperature of the synthesis reaction is 325-575℃; the 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--5℃.

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

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

[0051] 1. High-concentration liquid ammonia products can be produced, hydrogen gas can be converted from gas to liquid, the problems of large pressure and gas volume can be reduced, and the problems of storage and transportation difficulties and high cost can be solved;

[0052] 2. All emissions, such as gas emissions, are collected and treated and then returned for use as raw gas, and the single consumption is minimized;

[0053] 3. Waste water, waste residue, and waste gas in the three wastes are collected and treated, which is more environmentally friendly;

[0054] 4. The utilization system of raw gas, reaction gas, steam, circulating cooling water, and refrigeration water is optimized, investment is saved, and energy is saved;

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

[0056] 6. The device can realize 500,000-4,000,000 tons / year of liquid ammonia product (i.e. 0.89-7.02 tons / year of hydrogen can be stored and transported). BRIEF DESCRIPTION OF DRAWINGS

[0057] In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings needed to be used in the following embodiment or prior art description will be briefly introduced. Obviously, the drawings in the following description are only exemplary, and for those skilled in the art, other drawings can also be obtained according to the provided drawings without creative labor.

[0058] The structures, proportions, sizes, etc. shown in the specification are only used to cooperate with the content disclosed in the specification, to be understood and read by those skilled in the art, and are not used to limit the limiting conditions that the present application can be implemented, so they do not have technical significance. Any modification of the structure, change of the proportion relationship or adjustment of the size, without affecting the effect and purpose that the present application can produce, should still fall within the scope of the technical content disclosed by the present application.

[0059] Figure 1 Structure diagram of the ammonia hydrogen storage device in the device for green hydrogen energy storage, transportation and purification provided by the present application;

[0060] Figure 2 Structure diagram of the ammonia hydrogen release device in the device for green hydrogen energy storage, transportation and purification provided by the present application;

[0061] Explanation of reference signs:

[0062] 1, hydrogen low-pressure buffer tank; 2, hydrogen booster; 3, hydrogen high-pressure buffer tank; 4, nitrogen low-pressure buffer tank; 5, nitrogen booster; 6, nitrogen high-pressure 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, circulating gas booster; 16, circulating 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 gas 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 booster; 31, adsorption device; 32, hydrogen buffer tank; 33, nitrogen buffer tank. DETAILED DESCRIPTION

[0063] The following embodiments of the present application are illustrated by way of specific examples, and other advantages and effects of the present application will be readily appreciated by those skilled in the art upon reading the disclosure. It is obvious that the described embodiments are only a part of the embodiments of the present application, but not all the embodiments. Based on the embodiments of the present application, all other embodiments obtained by those skilled in the art without creative work fall within the scope of the present application.

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

[0065] Based on this, the present application provides a process and device for green hydrogen energy storage, transportation, purification and use. The device is applied to green hydrogen energy storage, transportation and purification. The device comprises an ammonia hydrogen storage device and an ammonia hydrogen release device. The ammonia hydrogen storage device comprises a hydrogen-nitrogen pressurization and mixing unit, a synthetic ammonia reaction unit, a liquid ammonia separation unit and a circulating gas pressurization unit. The ammonia hydrogen release device comprises a liquid ammonia gasification unit, an ammonia decomposition unit, a hydrogen separation unit and a hydrogen purification unit.

[0066] In one specific embodiment, as shown in Figure 1 and Figure 2 The device for green hydrogen energy storage, transportation, purification and use provided by the present application comprises an ammonia hydrogen storage device, a liquid ammonia transportation device and an ammonia hydrogen release device. The feed end of the ammonia hydrogen storage device is connected to a hydrogen source and a nitrogen source in communication. The hydrogen in the hydrogen source and the nitrogen in the nitrogen source enter the ammonia hydrogen storage device through a pipeline and are treated by the ammonia hydrogen storage device to obtain liquid ammonia. One end of the liquid ammonia transportation device is connected to the liquid ammonia outlet of the ammonia hydrogen storage device. The liquid ammonia obtained by reaction in the ammonia hydrogen storage device is transported to 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. The liquid ammonia transported by the liquid ammonia transportation device is treated by the ammonia hydrogen release device to obtain purified hydrogen, a nitrogen-hydrogen mixture and an ammonia-containing product.

[0067] In some embodiments, as shown in Figure 1As shown, the ammonia hydrogen storage device comprises a hydrogen-nitrogen pressurization and mixing assembly, a synthetic ammonia reaction assembly, a liquid ammonia separation assembly, and a circulating gas pressurization assembly; wherein the gas inlet side of the hydrogen-nitrogen pressurization and mixing assembly is connected in communication with a hydrogen source and a nitrogen source, respectively, and the hydrogen in the hydrogen source and the nitrogen in the nitrogen source are pressurized and mixed into high-pressure mixed gas in the hydrogen-nitrogen pressurization and mixing unit; the gas outlet side of the hydrogen-nitrogen pressurization and mixing assembly is connected in communication with the gas inlet side of the synthetic ammonia reaction assembly, and the high-pressure mixed gas completes the synthesis reaction in the synthetic ammonia reaction assembly and obtains gas-liquid mixed ammonia; the outlet side of the synthetic ammonia reaction assembly is connected in communication with the inlet side of the liquid ammonia separation assembly, and the gas-liquid mixed ammonia is separated into liquid ammonia and gaseous ammonia in the liquid ammonia separation assembly; the gaseous ammonia is transported to the circulating gas pressurization assembly through a pipeline and mixed into the high-pressure mixed gas after being pressurized by the circulating gas pressurization assembly.

[0068] Specifically, the hydrogen-nitrogen pressurization and mixing assembly comprises a hydrogen low-pressure buffer tank 1, a hydrogen pressurization device 2, a hydrogen high-pressure buffer tank 3, a nitrogen low-pressure buffer tank 4, a nitrogen pressurization device 5, a nitrogen high-pressure buffer tank 6, and a high-pressure mixed gas buffer tank 7; wherein the inlet of the hydrogen low-pressure buffer tank 1 is connected in communication with the hydrogen source, the outlet of the hydrogen low-pressure buffer tank 1 is connected in communication with the inlet of the hydrogen pressurization device 2 through a pipeline, the outlet of the hydrogen pressurization device 2 is connected in communication with the hydrogen high-pressure buffer tank 3 through a pipeline, the inlet of the nitrogen low-pressure buffer tank 4 is connected in communication with the nitrogen source, the outlet of the nitrogen low-pressure buffer tank 4 is connected in communication with the inlet of the nitrogen pressurization device 5 through a pipeline, the outlet of the nitrogen pressurization device 5 is connected in communication with the nitrogen high-pressure buffer tank 6 through a pipeline, and the outlet of the nitrogen high-pressure buffer tank 6 and the outlet of the hydrogen high-pressure buffer tank 3 are respectively connected in communication with the high-pressure mixed gas buffer tank 7 through pipelines.

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

[0070] Specifically, the synthetic ammonia reaction assembly comprises a first gas-gas heat exchanger 8, a first-stage reactor 9, a mixing tank 10 and a second-stage reactor 11; wherein the outlet of the high-pressure mixed gas buffer tank 7 is connected with the low-temperature side pipe opening of the first gas-gas heat exchanger 8 through a pipeline, and the inlet of the first-stage reactor 9 is connected with the high-temperature side pipe opening of the first gas-gas heat exchanger 8 through a pipeline; the inlet of the mixing tank 10 is connected with the outlet of the first-stage reactor 9, the inlet of the second-stage reactor 11 is connected with the outlet of the mixing tank 10, and the outlet of the second-stage reactor 11 is connected with the inlet of the liquid ammonia separation assembly.

[0071] In this embodiment, the synthetic ammonia reaction unit comprises a first gas-gas heat exchanger 8, a preheating device, a first-stage reactor 9, a second-stage reactor 11, and a mixing tank 10; the first gas-gas heat exchanger 8 is one of a tube-shell 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 first-stage reactor 9 is a fixed bed reactor or other reactor, and the second-stage reactor 11 is a fixed bed reactor or other reactor; the preheating device can be one of a vessel heating device, an electric heater, or a pipe jacket electric heater; the preheating device can be combined with the first-stage reactor 9 and / or the second-stage reactor 11, and the preheating device can be directly arranged outside or inside the first-stage reactor 9 and / or the second-stage reactor 11; when arranged outside, the preheating device can be heated by a flame, an electric heater, a jacketed device (oil bath, water bath, steam bath, or other high-temperature medium), and when arranged inside, the preheating device can be heated by an internally extending electric heating rod or an internally extending pipe (oil, water, steam, or other high-temperature medium); the first-stage reactor 9 and the second-stage reactor 11 are internally provided with a catalyst for the reaction; the mixing tank 10 is a pressure vessel, and the design pressure of the first gas-gas heat exchanger 8, the preheating device, the first-stage reactor 9, the second-stage reactor 11, and the mixing tank 10 is 19.5 MPaG. The high-pressure mixed gas buffer tank 7 is connected to the low-temperature side pipe opening of the first gas-gas heat exchanger 8 through a pipeline, the mixed gas is preheated by the first gas-gas heat exchanger 8, enters the first-stage reactor 9 through a pipeline, and the first-stage reactor 9 is connected to the high-temperature side pipe opening of the first gas-gas heat exchanger 8 through a pipeline; the reacted mixed gas provides heat source for the mixed gas in the high-pressure mixed gas buffer tank 7 by passing through the first gas-gas heat exchanger 8, and part of the cooled product mixed gas enters the second-stage reactor 11 through a pipeline, is further reacted in the second-stage reactor 11, and then enters the first gas-liquid water-cooled heat exchanger 12 through a pipeline.

[0072] Specifically, the liquid ammonia separation assembly comprises a first gas-liquid water-cooled heat exchanger 12, a first gas-liquid deep water-cooled heat exchanger 13, a gas-liquid separator 14, and a first liquid ammonia storage tank 17; the outlet of the second-stage reactor 11 is in communication with the inlet of the first gas-liquid water-cooled heat exchanger 12, and the inlet of the first gas-liquid deep water-cooled heat exchanger 13 is in communication with the outlet of the first gas-liquid water-cooled heat exchanger 12; the inlet of the gas-liquid separator 14 is in communication with the outlet of the first gas-liquid deep water-cooled heat exchanger 13, the gaseous outlet of the gas-liquid separator 14 is in communication with the inlet of the circulating gas pressurizing assembly, the outlet of the circulating gas pressurizing assembly is in communication with the high-pressure mixed gas buffer tank 7, and the tail gas outlet of the gas-liquid separator 14 is in communication with a discharge header; the inlet of the first liquid ammonia storage tank 17 is in communication with the liquid outlet of the gas-liquid separator 14, and the outlet of the first liquid ammonia storage tank 17 is in communication with the liquid ammonia transportation device 18.

[0073] In the embodiment, the first gas-liquid water-cooled heat exchanger 12 is one of a tube-in-shell 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 tube-in-shell 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 pressure of the medium side 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 is 19.5 MPaG; a pressure reducing device is arranged 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 tank transportation vehicle, a filling transportation train or a tubular transportation device. In 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 and is gradually cooled, and then enters the gas-liquid separator 14; the condensed liquid ammonia enters the first liquid ammonia storage tank 17 and the subsequent liquid ammonia transportation device through the pipeline below the gas-liquid separator 14; the gaseous phase mixed gas separated by the gas-liquid separator 14 enters the preceding circulating gas buffer tank 16 through a pipeline.

[0074] Further, the ammonia hydrogen storage device provided by the present application further comprises a circulating gas pressurizing assembly, please continue to refer to Figure 1 The circulating gas pressurizing unit comprises a circulating gas pressurizing device 15 and a circulating gas buffer tank 16; the circulating gas pressurizing device 15 is one of a booster pump, a booster fan or a compressor; the circulating gas buffer tank 16 is a pressure vessel; the design pressure of the circulating gas high-pressure buffer tank is 19.5 MPaG; the circulating gas pressurizing device 15 is connected with the circulating gas buffer tank 16 through a pipeline; the pressurized circulating gas enters the circulating gas buffer tank 16 through a pipeline, and then enters the high-pressure mixed gas buffer tank through a pipeline, and is recycled. The circulating gas buffer tank 16 and the circulating gas pressurizing device 15 are both provided with a pressure protection device (such as a pressure relief valve) and a pressure control device (such as a pressure control valve); the pipeline connected with the high-pressure mixed gas buffer tank 7 is provided with a flow control valve, which is used to control the proportion of the recycled mixed gas, nitrogen and hydrogen return gas.

[0075] In some embodiments, as Figure 2As shown, the ammonia releasing hydrogen device comprises a liquid ammonia gasification assembly, an ammonia decomposition assembly, a hydrogen separation assembly and a hydrogen purification assembly; wherein the other end of the liquid ammonia conveying device is connected to the inlet side of the liquid ammonia gasification assembly, and the liquid ammonia conveyed by the liquid ammonia conveying device is treated by the liquid ammonia gasification assembly to obtain high-pressure ammonia gas; 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 conveyed by the liquid ammonia gasification assembly is subjected to a decomposition reaction in the ammonia decomposition assembly to obtain a reaction mixed gas of ammonia, hydrogen and nitrogen; the inlet side of the hydrogen separation assembly is connected to the mixed gas outlet of the ammonia decomposition assembly, and the reaction mixed gas is cooled by the hydrogen separation assembly to obtain a cooled mixed gas; and the inlet side of the hydrogen purification assembly is connected to the outlet side of the hydrogen separation assembly, and the cooled mixed gas is separated into hydrogen, nitrogen and an ammonia-containing product in the hydrogen purification assembly.

[0076] Specifically, the liquid ammonia gasification assembly comprises a second liquid ammonia storage tank 19, a liquid ammonia conveying pump 20, a liquid ammonia vaporizer 21 and an ammonia gas buffer tank 22 connected in sequence by pipelines, wherein the inlet of the second liquid ammonia storage tank 19 is connected to the liquid ammonia conveying device. In this embodiment, the liquid ammonia gasification unit comprises the second liquid ammonia storage tank 19, the liquid ammonia conveying pump 20, the liquid ammonia vaporizer 21 and the ammonia gas buffer tank 22; the liquid ammonia vaporizer 21 is one of a tube-in-shell heat exchanger, a plate-and-frame heat exchanger, a jacketed heat exchanger, a U-tube heat exchanger or a fixed tube sheet heat exchanger; the second liquid ammonia storage tank 19 and the ammonia gas buffer tank 22 are both pressure vessels; the liquid ammonia conveying pump 20 is one of a centrifugal pump, a reciprocating pump, a metering pump, a gear pump or a rotor positive displacement pump; the design pressure of the second liquid ammonia storage tank 19 and the ammonia gas buffer tank 22 is both 1.2 MPaG; the liquid ammonia in the second liquid ammonia storage tank 19 comes from the liquid ammonia conveying device, and the second liquid ammonia storage tank 19, the liquid ammonia conveying pump 20, the liquid ammonia vaporizer 21 and the ammonia gas buffer tank 22 are connected by pipelines to complete the processes of pressurization and gasification of the liquid ammonia.

[0077] As Figure 2As shown, the ammonia decomposition assembly comprises a second gas-gas heat exchanger 23 and an ammonia decomposition reactor 24 which are connected by pipelines, wherein the low-temperature side pipe opening of the second gas-gas heat exchanger 23 is connected with the outlet of the ammonia gas buffer tank 22, and the high-temperature side pipe opening of the second gas-gas heat exchanger 23 is connected with the inlet of the ammonia decomposition reactor 24. In this embodiment, the second gas-gas heat exchanger 23 is one of a tube-in-shell heat exchanger, a plate-and-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 type of reactor; the ammonia decomposition reactor 24 contains a heating device which can be directly arranged outside or inside the ammonia decomposition reactor 24, and can adopt flame heating, electric heating, jacketed equipment (oil bath, water bath, steam bath or other high-temperature medium) heating when arranged outside, and can adopt an internally extending electric heating rod or an internally extending pipe (oil, water, steam or other high-temperature medium) when arranged inside; the ammonia decomposition reactor 24 is internally provided with a catalyst for reaction; the ammonia decomposition reactor 24 is a pressure vessel with a design pressure of 1.2 MPaG and a design temperature of 850℃. The ammonia gas buffer tank 22 is connected with the low-temperature side pipe opening of the second gas-gas heat exchanger 23 by a pipeline, the ammonia gas is preheated by the second gas-gas heat exchanger 23, enters the ammonia decomposition reactor 24 through a pipeline for reaction, and the ammonia gas after reaction is connected with the high-temperature side pipe opening of the second gas-gas heat exchanger 23 by a pipeline, and provides heat source for the ammonia gas of the ammonia gas buffer tank 22 through the second gas-gas heat exchanger 23, and the partially cooled product mixed gas enters the second gas-liquid water-cooled heat exchanger 25 through a pipeline.

[0078] The hydrogen separation assembly comprises a second gas-liquid water-cooled heat exchanger 25, a second gas-liquid deep cooling heat exchanger 26 and an ammonia-nitrogen-hydrogen buffer tank 27 which are connected by pipelines in sequence, wherein the inlet of the second gas-liquid water-cooled heat exchanger 25 is connected with the outlet of the ammonia decomposition reactor 24; in this embodiment, the second gas-liquid water-cooled heat exchanger 25 is one of a tube-in-shell heat exchanger, a plate-and-frame heat exchanger, a double-pipe heat exchanger, a U-tube heat exchanger or a fixed tube sheet heat exchanger; the gas-liquid deep cooling heat exchanger is one of a tube-in-shell heat exchanger, a plate-and-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 mixed gas enters the ammonia-nitrogen-hydrogen buffer tank 27 after being gradually cooled by the second gas-liquid water-cooled heat exchanger 25 and the second gas-liquid deep cooling heat exchanger 26 through pipelines respectively.

[0079] The hydrogen purification assembly comprises, in sequence through pipelines, a hydrogen dryer 28, a nitrogen-hydrogen buffer tank 29, a nitrogen-hydrogen pressurizing device and an adsorption device 31, wherein the hydrogen dryer 28 is connected with the outlet of the ammonia-nitrogen-hydrogen buffer tank 27, the nitrogen outlet of the adsorption device 31 is connected with the nitrogen buffer tank 33, and the hydrogen outlet of the adsorption device 31 is connected with the hydrogen buffer tank 32. In this embodiment, the hydrogen purification unit comprises the hydrogen dryer 28, the nitrogen-hydrogen buffer tank 29, the nitrogen-hydrogen pressurizing device, the adsorption device 31, the nitrogen buffer tank 33 and the hydrogen buffer tank 32; the hydrogen dryer 28 is a packed tower and belongs to a pressure container; the nitrogen-hydrogen buffer tank 29, the nitrogen buffer tank 33 and the hydrogen buffer tank 32 all are pressure containers; the nitrogen-hydrogen pressurizing device is one of a booster pump, a booster fan and a compressor; and the adsorption device 31 is one of a pressure swing adsorption device, a temperature swing adsorption device and a membrane treatment device. The gas in the ammonia-nitrogen-hydrogen buffer tank 27 is connected with the hydrogen dryer 28 through a pipeline, the hydrogen dryer 28 is connected with the nitrogen-hydrogen buffer tank 29 and the nitrogen-hydrogen pressurizing device through pipelines, and the nitrogen-hydrogen buffer tank 29 and the nitrogen-hydrogen pressurizing device are both provided with pressure protection devices and pressure control devices; the nitrogen-hydrogen pressurizing device is connected with the adsorption device 31 through a pipeline, and the adsorption device 31 is subsequently connected with 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 ammonia hydrogen storage process device, the application further provides a process method for green hydrogen energy storage, transportation and purification, which comprises the following steps:

[0081] Step (1): the catalyst, high-pressure hydrogen and high-pressure nitrogen obtained after pressurization are used as reaction raw materials to perform a synthesis reaction, and the product of the synthesis reaction 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 after removing reaction heat, and the unreacted gas is pressurized and mixed with the reaction raw materials and then subjected to a synthesis reaction again;

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

[0083] Step (3): the liquid-phase product in step (2) is pressurized and heated to enter an ammonia decomposition reactor to perform a decomposition reaction, and the product of the decomposition reaction 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 after removing reaction heat;

[0084] Step (4): the product of the reaction in step (3) is input into a dryer to perform gas-liquid separation, the separated gas is pressurized and purified and separated in an adsorption device to obtain hydrogen.

[0085] In some embodiments, in step (1), the catalyst is one of a copper-based, manganese-based, nickel-based, titanium-based, magnesium-based catalyst; 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,

[0086] 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.

[0087] In some embodiments, in step (3), the catalyst is one of a copper-based, manganese-based, nickel-based, titanium-based, magnesium-based catalyst; 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; and 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 15-30°C.

[0088] In one specific embodiment, the process provided by the present application comprises the following steps:

[0089] Step (1): inputting reaction raw materials containing pressurized hydrogen and nitrogen into a first reactor and a second reactor for a synthesis reaction; after the reaction heat is removed by a first gas-gas heat exchanger, the product of the synthesis reaction is inputted 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 raw materials before being inputted into the reactor A and the reactor B for a synthesis reaction; wherein the reaction raw materials include hydrogen and nitrogen, the catalyst is one of a copper-based, manganese-based, nickel-based, titanium-based, or magnesium-based catalyst; the hydrogen pressurization system and the nitrogen pressurization system pressurize the pressure from 1.0 MPaG to 11-19.5 MPaG, i.e., 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 is 50,000-130,000; due to the heat release of the synthesis reaction, the reaction speed decreases, a first gas-gas heat exchanger is added between the first reactor and the second reactor to remove the heat in the first reactor with the initial reaction gas to reduce the heat in the middle of the reaction and increase the reaction rate of the synthesis reaction in the second 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 before being subjected to gas-liquid separation; the gas obtained by the gas-liquid separation is returned to the first reactor as raw materials for recycling; the storage pressure of liquid ammonia is 0.8-1.5 MPaG, and the storage temperature is -20 to -5°C.

[0090] Step (2): The liquid phase product of the synthesis reaction in step (1) is input into a liquid ammonia transportation device and transported to a desired ammonia hydrogen release device; the storage pressure of the liquid ammonia is 0.8-1.5 MPaG, and the storage temperature is -20 to -5℃.

[0091] Step (3): The liquid phase product in step (2) is input into an ammonia decomposition reactor through pressurization and temperature increase for decomposition reaction, and the product of the decomposition reaction is input into an ammonia-nitrogen-hydrogen buffer tank through a second gas-gas heat exchanger to remove reaction heat, a second gas-liquid water-cooled heat exchanger, and a second gas-liquid deep water-cooled heat exchanger; the catalyst is one of copper-based, manganese-based, nickel-based, titanium-based, or magnesium-based catalysts; the pressure of the pressurization system is increased to 0.8-1.2 MPaG, i.e., the pressure of the decomposition reaction is 0.8-1.2 MPaG; the temperature of the decomposition reaction is 500-850℃; the reaction space velocity is 50,000-130,000; and 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℃.

[0092] 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; the adsorbent in the dryer can absorb water and liquid ammonia; all the adsorbents of the dryer are one of high-temperature regenerable or non-regenerable; when the adsorbent of the dryer is a high-temperature regenerable adsorbent, the removed ammonia gas mixture needs to be absorbed to meet the standard before being discharged, and the absorption tower is one of a water, alkali, or acid absorption tower; the nitrogen-hydrogen mixture after purification and separation can be discharged or recycled to step (1) for recycling.

[0093] In the above process, due to different requirements of the synthesis reaction, the decomposition reaction form, the catalyst, the use of hydrogen, and the product scale, the pressure, temperature, and residence time of each reaction unit are different, but the pressure and temperature range corresponding to the gas phase reaction conditions must be met to prevent liquid hammer, overpressure, and out-of-control phenomena during the reaction; the reaction raw materials, reaction gas, steam, circulating cooling water, and chilled water are optimized through multiple heat exchanger forms such as a gas-gas reactor, a gas-liquid water-cooled exchanger, and a gas-liquid deep-cooled exchanger, which reduces energy consumption, improves the utilization rate of hydrogen, nitrogen, and ammonia, and reduces unit consumption; the purification and separation system can adopt a membrane recovery system, a pressure swing adsorption system, or a temperature swing adsorption system, which can realize the purification of hydrogen and the reverse osmosis recovery of nitrogen, improve the quality and efficiency, reduce unit consumption, and improve the drying efficiency.

[0094] The process method and device provided by the application can produce high-concentration liquid ammonia products, convert hydrogen from gas to liquid, reduce the problems of pressure and large gas volume, solve the problems of storage and transportation difficulties, high cost and the like, all emissions, gas emissions and the like are collected and treated and then returned to be used as raw material gas, the single consumption is the lowest, wastewater, waste residue and the like in the three wastes are collected and treated, the method is more environmentally friendly, the utilization system of raw material gas, reaction gas, steam, circulating cooling water and refrigerated water is optimized, investment is more saved and more energy-saving, the drying and purification separation system can be a dryer, a drying tower, a reverse osmosis membrane system, a pressure swing adsorption system or a temperature swing adsorption system, hydrogen purification and nitrogen-hydrogen separation are carried out, 5-40 million tons / year of liquid ammonia products (that is, 0.89-7.02 million tons / year of hydrogen can be stored and transported) can be realized in a multi-capacity device layout, operation is flexible and convenient, safe and reliable, the degree of automation is high, the product performance is better, and the method is more suitable for the storage, transportation and purification of green hydrogen energy and takes a high-end production route. The application has few moving devices, short device construction period, compact layout, can adopt modular construction and greatly reduces investment cost.

[0095] The above specific embodiments further specifically describe the purposes, technical solutions and beneficial effects of the application, and it should be understood that the above is only a specific embodiment of the application and is not used to limit the protection scope of the application, and any modification, equivalent replacement, improvement and the like made on the basis of the technical solutions of the application should be included in the protection scope of the application.

Claims

1. A device for green hydrogen energy storage, transportation and purification, characterized in that, The device comprises: An ammonia hydrogen storage device, a feed end of the ammonia hydrogen storage device is connected with a hydrogen source and a nitrogen source respectively, hydrogen in the hydrogen source and nitrogen in the nitrogen source enter the ammonia hydrogen storage device through a pipeline, and liquid ammonia is obtained through treatment of the ammonia hydrogen storage device; A liquid ammonia conveying device, one end of the liquid ammonia conveying device is connected with a liquid ammonia outlet of the ammonia hydrogen storage device, liquid ammonia obtained by reaction in the ammonia hydrogen storage device is conveyed to the liquid ammonia conveying device through the liquid ammonia outlet; An ammonia hydrogen release device, the other end of the liquid ammonia conveying device is connected with an inlet end of the ammonia hydrogen release 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; The ammonia hydrogen storage device comprises: A hydrogen-nitrogen pressurization and mixing assembly, a gas inlet side of the hydrogen-nitrogen pressurization and mixing assembly is connected with the hydrogen source and the nitrogen source respectively, hydrogen in the hydrogen source and nitrogen in the nitrogen source are pressurized and mixed into high-pressure mixed gas in the hydrogen-nitrogen pressurization and mixing assembly; A synthetic ammonia reaction assembly, a gas outlet side of the hydrogen-nitrogen pressurization and mixing assembly is connected with a gas inlet side of the synthetic ammonia reaction assembly, the high-pressure mixed gas completes a synthesis reaction in the synthetic ammonia reaction assembly, and gas-liquid mixed ammonia is obtained; A liquid ammonia separation assembly, an outlet side of the synthetic ammonia reaction assembly is connected with an inlet side of the liquid ammonia separation assembly, the gas-liquid mixed ammonia is separated into liquid ammonia and gaseous ammonia in the liquid ammonia separation assembly; A circulating gas pressurization assembly, the gaseous ammonia is conveyed to the circulating gas pressurization assembly through a pipeline, and is mixed into the high-pressure mixed gas after being pressurized by the circulating gas pressurization assembly; The ammonia hydrogen release device comprises: A liquid ammonia gasification assembly, the other end of the liquid ammonia conveying device is connected with an inlet side of the liquid ammonia gasification assembly, liquid ammonia conveyed by the liquid ammonia conveying device is treated by the liquid ammonia gasification assembly to obtain high-pressure ammonia gas; An ammonia decomposition assembly, an inlet side of the ammonia decomposition assembly is connected with an outlet side of the liquid ammonia gasification assembly, high-pressure ammonia gas conveyed by the liquid ammonia gasification assembly is subjected to a decomposition reaction in the ammonia decomposition assembly to obtain a reaction mixture of ammonia, hydrogen and nitrogen; A hydrogen separation assembly, an inlet side of the hydrogen separation assembly is connected with a mixed gas outlet of the ammonia decomposition assembly, the reaction mixture is cooled by the hydrogen separation assembly to obtain cooled mixed gas; A hydrogen purification assembly, an inlet side of the hydrogen purification assembly is connected with an outlet side of the hydrogen separation assembly, the cooled mixed gas is separated into hydrogen, nitrogen and an ammonia-containing product in the hydrogen purification assembly.

2. The device for green hydrogen energy storage, transportation and purification use according to claim 1, characterized in that, The hydrogen-nitrogen pressurization and mixing assembly comprises: A hydrogen low-pressure buffer tank, an inlet of the hydrogen low-pressure buffer tank is connected with the hydrogen source; A hydrogen pressurization device, an outlet of the hydrogen low-pressure buffer tank is connected with an inlet of the hydrogen pressurization device through a pipeline; A hydrogen high-pressure buffer tank, an outlet of the hydrogen pressurization device is connected with the hydrogen high-pressure buffer tank through a pipeline; A nitrogen low-pressure buffer tank, an inlet of the nitrogen low-pressure buffer tank is connected with the nitrogen source; A nitrogen gas pressurizing device, an outlet of the nitrogen low-pressure buffer tank being connected to an inlet of the nitrogen gas pressurizing device through a pipeline; A nitrogen high-pressure buffer tank, an outlet of the nitrogen gas pressurizing device being connected to the nitrogen high-pressure buffer tank through a pipeline; A high-pressure mixed gas buffer tank, an outlet of the nitrogen high-pressure buffer tank and an outlet of the hydrogen high-pressure buffer tank being connected to the high-pressure mixed gas buffer tank through pipelines respectively.

3. The device for green hydrogen energy storage, transportation and purification use according to claim 2, characterized in that, The synthetic ammonia reaction assembly comprises: A first gas-gas heat exchanger, an outlet of the high-pressure mixed gas buffer tank being connected to a low-temperature side pipe opening of the first gas-gas heat exchanger through a pipeline; A first-stage reactor, an inlet of the first-stage reactor being connected to a high-temperature side pipe opening of the first gas-gas heat exchanger through a pipeline; A mixing tank, an inlet of the mixing tank being connected to an outlet of the first-stage reactor; A second-stage reactor, an inlet of the second-stage reactor being connected to an outlet of the mixing tank, and an outlet of the second-stage reactor being connected to an inlet of the liquid ammonia separation assembly as an outlet side of the synthetic ammonia reaction assembly.

4. The device for green hydrogen energy storage, transportation and purification use according to claim 3, characterized in that, The liquid ammonia separation assembly comprises: A first gas-liquid water-cooled heat exchanger, an outlet of the second-stage reactor being connected to an inlet of the first gas-liquid water-cooled heat exchanger; A first gas-liquid deep water-cooled heat exchanger, an inlet of the first gas-liquid deep water-cooled heat exchanger being connected to an outlet of the first gas-liquid water-cooled heat exchanger; A gas-liquid separator, an inlet of the gas-liquid separator being connected to an outlet of the first gas-liquid deep water-cooled heat exchanger, a gaseous outlet of the gas-liquid separator being connected to an inlet of the circulating gas pressurizing assembly, an outlet of the circulating gas pressurizing assembly being connected to the high-pressure mixed gas buffer tank, and a tail gas outlet of the gas-liquid separator being connected to a discharge main pipe; A first liquid ammonia storage tank, an inlet of the first liquid ammonia storage tank being connected to a liquid outlet of the gas-liquid separator, and an outlet of the first liquid ammonia storage tank being connected to the liquid ammonia delivery device.

5. The device for green hydrogen energy storage, transportation and purification use according to claim 4, 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 gas buffer tank connected in sequence through pipelines, wherein an inlet of the second liquid ammonia storage tank is connected to the liquid ammonia delivery device; The ammonia decomposition assembly comprises a second gas-gas heat exchanger and an ammonia decomposition reactor connected through pipelines, wherein a low-temperature side pipe opening of the second gas-gas heat exchanger is connected to an outlet of the ammonia gas buffer tank, and a high-temperature side pipe opening of the second gas-gas heat exchanger is connected to an 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 connected in sequence through pipelines, wherein an inlet of the second gas-liquid water-cooled heat exchanger is connected to an outlet of the ammonia decomposition reactor; The hydrogen purification assembly comprises a hydrogen gas dryer, an ammonia-nitrogen-hydrogen buffer tank, a nitrogen-hydrogen pressurizing device and an adsorption device connected in sequence through pipelines, wherein an inlet of the hydrogen gas dryer is connected to an outlet of the ammonia-nitrogen-hydrogen buffer tank, a nitrogen gas outlet of the adsorption device is connected to a nitrogen gas buffer tank, and a hydrogen gas outlet of the adsorption device is connected to a hydrogen gas buffer tank.

6. A process for green hydrogen energy storage and transportation and purification, characterized in that, The method applied to the device for green hydrogen energy storage, transportation and purification of claim 5, the method comprising the following steps: The method applied to the device for green hydrogen energy storage, transportation and purification of claim 5, the method comprising the following steps: Step (1): the catalyst and the high-pressure hydrogen and high-pressure nitrogen obtained after pressurization are used as reaction raw materials to perform a synthesis reaction, and the product of the synthesis reaction is removed from the reaction heat, and then input into a gas-liquid separator through a first gas-liquid water-cooled heat exchanger and a first gas-liquid deep water-cooled heat exchanger, and the unreacted gas is pressurized and mixed with the reaction raw materials and then used to perform a synthesis reaction again; Step (2): the liquid-phase product of the synthesis reaction in step (1) is input into a liquid ammonia delivery device and delivered to an ammonia hydrogen release device through the liquid ammonia delivery device; Step (3): the liquid-phase product in step (2) is pressurized and heated to enter an ammonia decomposition reactor to perform a decomposition reaction, and the product of the decomposition reaction is removed from the reaction heat, and then 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; Step (4): the product of the reaction in step (3) is input into a dryer to perform gas-liquid separation, the separated gas is pressurized and purified and separated in an adsorption device to obtain hydrogen.

7. The process of claim 6, wherein the process is characterized by, In step (1), the catalyst is one of a copper-based, manganese-based, nickel-based, titanium-based, and magnesium-based catalyst; the pressure of the synthesis reaction is 11-19.5 MPaG; the temperature of the synthesis reaction is 325-575 ℃; and / or, In steps (1) and (2), the storage pressure of the liquid ammonia is 0.8-1.5 MPaG, and the storage temperature is -20--5 ℃.

8. The process of claim 7, wherein, In step (3), the pressure of the decomposition reaction is 0.8-1.2 MPaG; the temperature of the decomposition reaction is 500-850 ℃; and the temperature of the 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 ℃.

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