System for producing liquid hydrogen and liquid oxygen by using metal hydrogen storage material

Abstract

This application relates to the field of development and application technology of metal hydrogen storage materials, and provides a system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials, including a hydrogen absorption / desorption cycle unit, a helium circulation unit, and a liquid hydrogen / liquid oxygen preparation unit. The system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials provided in this application utilizes the low temperature generated during the hydrogen absorption / desorption cycle of the metal hydrogen storage material to achieve air separation and hydrogen liquefaction. It fully utilizes natural energy, including solar energy, and the chemical energy of hydrogen absorption / desorption by the metal hydrogen storage material. It effectively utilizes the heat generated by hydrogen absorption and the cold energy generated by hydrogen desorption, achieving efficient utilization of hydrogen energy.

Description

Technical Field

[0001] This application belongs to the field of development and application technology of metal hydrogen storage materials, and in particular relates to a system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials. Background Technology

[0002] Energy shortages, environmental pollution, and global climate change have made the development of clean, efficient, safe, and sustainable energy sources an urgent priority, with hydrogen energy receiving increasing attention from various countries. Hydrogen energy is an ideal clean fuel. As environmental protection measures become increasingly stringent worldwide, hydrogen power generation equipment, due to its energy-saving and low-emission characteristics, has become a focus of research and development and has begun commercialization. Traditional hydrogen energy utilization equipment is relatively inefficient, necessitating the development of more efficient hydrogen energy utilization devices. Summary of the Invention

[0003] In view of this, embodiments of this application provide a system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials, in order to solve the problem of low hydrogen energy utilization efficiency at present.

[0004] This application provides a system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials, comprising: a hydrogen absorption and desorption circulation unit, characterized in that the circulating hydrogen released by the hydrogen absorption and desorption circulation unit is divided into two paths, the first path of circulating hydrogen returns to the hydrogen absorption and desorption circulation unit after passing through the tube side of a single-stage hydrogen expander and a comprehensive heat exchanger; the second path of circulating hydrogen enters a multi-stage hydrogen expander for expansion after passing through a hydrogen heat exchanger and a second air heat exchanger, and then returns to the hydrogen absorption and desorption circulation unit. The first-stage outlet of the helium-2 compressor passes through a hydrogen heat exchanger and a third air heat exchanger before entering the second-stage inlet of the helium-2 compressor. The second-stage outlet of the helium-2 compressor then splits into three streams after passing through an air-helium heat exchanger. The first stream of helium from the air-helium heat exchanger passes through the shell side of the third helium regenerator, the helium single-stage expander, the hydrogen-helium heat exchanger, and the tube side of the third helium regenerator before entering the first-stage inlet of the helium-2 compressor. The second stream of helium from the air-helium heat exchanger passes through the shell side of the second helium regenerator, the second helium multi-stage expander, the hydrogen liquefaction heat exchange center, and the tube side of the second helium regenerator before entering the first-stage inlet of the helium-2 compressor. The third stream of helium from the air-helium heat exchanger passes through the shell side of the first helium regenerator, the second tube side of the evaporator in the fractionation column, the first helium multi-stage expander, the air liquefaction heat exchange center, and the tube side of the first helium regenerator before entering the first-stage inlet of the helium-2 compressor. Ambient temperature air enters the feed inlet of the fractionating tower through a combined heat exchanger, the first tube side of the evaporator in the fractionating tower, and the fifth tube side of the air liquefaction heat exchange center. Nitrogen, oxygen, and argon are output from different outlets of the fractionating tower, respectively. Nitrogen output from the fractionating tower is converted into liquid nitrogen after passing through the sixth tube side of the air liquefaction heat exchange center; oxygen output from the fractionating tower is converted into liquid oxygen after passing through the seventh tube side of the air liquefaction heat exchange center; and argon output from the fractionating tower is converted into liquid argon after passing through the eighth tube side of the air liquefaction heat exchange center. Ambient temperature hydrogen is converted into liquid hydrogen after passing through a combined heat exchanger, the third tube side of the evaporator in the fractionating tower, the shell side of the hydrogen-helium heat exchanger, and the hydrogen liquefaction heat exchange center. A hydrogen multi-stage expander, a helium two-stage compressor, a first helium multi-stage expander, a second helium multi-stage expander, and a helium single-stage expander are coaxially connected.

[0005] Specifically, the hydrogen absorption and desorption cycle unit includes an AB metal hydride reaction bed module, a BA metal hydride reaction bed module, a first air heat exchanger, and a central heat exchanger. The AB metal hydride reaction bed module has a cylindrical structure, symmetrically arranged; the left half is a -2.8℃ metal hydride reaction zone, and the right half is a -50℃ metal hydride reaction zone; a ring plate separates the two parts; within the AB metal hydride reaction bed module, alternating ring-shaped first and second metal hydride material layers are arranged, with copper plates between each metal hydride material layer; in the -2.8℃ metal hydride reaction zone, the heat released during hydrogen absorption by metal hydride B is supplied to metal hydride A for hydrogen release; in the -50℃ metal hydride reaction zone, metal hydride A... The heat released during hydrogen absorption is used to supply hydrogen release from metal hydride B. The outer shell of the AB metal hydride reaction bed module is made of copper, with an insulation layer between the outer shell and the outermost layer of metal hydride material. The first and second metal hydride material layers are respectively filled with metal hydrogen storage material B and metal hydrogen storage material A, and each layer of metal hydrogen storage material is wrapped with a carbon fiber film. The top of the AB metal hydride reaction bed module is equipped with a rotating fork, which can move the metal hydrogen storage material wrapped with carbon fiber film back and forth between the left and right parts of the AB metal hydride reaction bed module. Each carbon fiber membrane is equipped with vents that connect to a gas collecting plate at the top, allowing hydrogen to enter and exit during the absorption and release of hydrogen by the metal hydrogen storage material. A bed rotation drive structure is located at the bottom of the AB metal hydride reactor module. This structure drives the outer shell and various copper plates to rotate between the left and right sides of the module. When the rotating fork rotates the layers of metal hydrogen storage material wrapped in carbon fiber membranes, or when the bed rotation drive structure rotates the outer shell and copper plates, the gas collecting plate lifts, and the vents on the carbon fiber membranes automatically close, allowing for smooth rotation. When the rotation reaches its final position... When the gas collecting plate is pressed down, it opens the vent holes on the carbon fiber membrane to complete the gas path connection, allowing hydrogen to enter and exit. The vent holes of the carbon fiber membrane are equipped with bed plate springs and bed plate steel balls. The gas collecting port of the gas collecting plate is equipped with a gas collecting plate spring and a gas collecting plate steel ball. When the gas collecting plate is pressed down, the gas collecting plate springs and gas collecting plate steel balls squeeze the bed plate steel balls and bed plate springs, thereby completing the gas path connection between the carbon fiber membrane and the gas collecting plate. The BA metal hydride reactor module is equipped with A4' metal hydride, B1' metal hydride, A1' metal hydride, A2' metal hydride, A3' metal hydride and A4' metal hydride for recycling.In the AB metal hydride reactor module, hydrogen A gas is released from the hydrogen outlet of the -2.8℃ metal hydride reaction zone. The hydrogen A gas is divided into two paths. One path is output from the hydrogen absorption and desorption circulation unit and then splits into the first and second circulating hydrogen paths. The other path passes through the first, second, and third shell sides of the central heat exchanger and connects to the hydrogen absorption pipelines corresponding to the B1' metal hydride in the two B1'A1' metal hydride reactors. In the BA metal hydride reactor module, the hydrogen release pipeline corresponding to metal hydride B1' connects to the hydrogen absorption pipeline corresponding to metal hydride A2' after passing through the second tube of the second air heat exchanger; the hydrogen release pipeline corresponding to metal hydride A1' then connects to the hydrogen absorption pipeline corresponding to metal hydride B in the -2.8℃ metal hydride reaction zone of the AB metal hydride reactor module after passing through the second tube of the central heat exchanger and the fifth tube of the second air heat exchanger; the hydrogen release pipeline corresponding to metal hydride A2' connects to the hydrogen absorption pipeline corresponding to metal hydride B in the -2.8℃ metal hydride reaction zone of the AB metal hydride reactor module after passing through the first tube of the central heat exchanger and the fifth tube of the second air heat exchanger; and the hydrogen release pipeline corresponding to metal hydride A3' connects to the hydrogen absorption pipeline corresponding to metal hydride B in the -2.8℃ metal hydride reaction zone of the AB metal hydride reactor module after passing through the fifth tube of the second air heat exchanger. The hydrogen release line corresponding to the A4' metal hydride is connected to the expansion inlet of the turbocharger after passing through the fourth tube side of the second air heat exchanger and the fourth shell side of the central heat exchanger. The expansion outlet of the turbocharger is connected to the hydrogen intake line corresponding to the A1' metal hydride after passing through the first tube side of the second air heat exchanger. In the AB metal hydride reactor module, hydrogen B gas is released from the hydrogen outlet of the -50℃ metal hydride reaction zone. The hydrogen B gas is divided into four parts. The first part is connected to the hydrogen absorption pipe corresponding to metal hydride A in the -50℃ metal hydride reaction zone. The second part is connected to the hydrogen absorption pipe corresponding to metal hydride A2' in the BA metal hydride reactor module after passing through the second tube of the second air heat exchanger. The third part is connected to the hydrogen absorption pipe corresponding to metal hydride A3' in the BA metal hydride reactor module after passing through the third tube of the second air heat exchanger. The fourth part is connected to the compression inlet of the turbocharger. The compression outlet of the turbocharger is connected to the hydrogen absorption pipe corresponding to metal hydride B in the -2.8℃ metal hydride reactor in the AB metal hydride reactor module after passing through the third and fourth tubes of the central heat exchanger and the fifth tube of the second air heat exchanger.

[0006] Specifically, the type of metal hydrogen storage material is selected based on the actual heat exchange requirements between the various metal hydride reaction beds. For the -2.8℃ and -50℃ metal hydride reaction zones in the AB metal hydride reaction bed module, and the BA metal hydride reaction bed module, the type of metal hydride to be filled is selected according to the heat exchange requirements.

[0007] Specifically, metal hydrides A, A1', A2', A3', and A4' are temperature-negative metal hydrogen storage materials; a temperature-negative metal hydrogen storage material is defined as absorbing low-pressure hydrogen at low temperatures and releasing heat, and releasing high-pressure hydrogen at high temperatures and releasing cold energy. Metal hydrides B and B1' are temperature-positive metal hydrogen storage materials; a temperature-positive metal hydrogen storage material is defined as absorbing high-pressure hydrogen at high temperatures and releasing high-temperature heat, and releasing low-pressure hydrogen at low temperatures and releasing low-temperature cold energy.

[0008] Specifically, the hydrogen absorption and desorption cycle unit also includes a pressure hydrogen replacement center; a pressure hydrogen replacement center is set between each metal hydride in the BA metal hydride reaction bed module, and a pressure hydrogen replacement center is set between the -2.8℃ metal hydride reaction area and the -50℃ metal hydride reaction area in the AB metal hydride reaction bed module; the pressure hydrogen replacement center is equipped with multiple gas storage chambers as needed, which store hydrogen at different pressures and temperatures; the two ends of each gas storage chamber of the pressure hydrogen replacement center are connected to the hydrogen absorption and desorption pipelines of the two adjacent metal hydride reaction beds; each gas storage chamber of the pressure hydrogen replacement center is equipped with a pressure stabilizing device.

[0009] This application also provides a system for producing helium and neon, comprising, in sequence, a hydrogen removal furnace, a water separator, a gas storage tank, a first helium-neon compressor, a first air cooler, a dryer, a first helium-neon heat exchanger, a nitrogen removal separator, an activated alumina adsorber, a second helium-neon heat exchanger, a helium coil heat exchanger, a neon separator, a throttling expansion valve, and a distillation column. The gas outlet at the top of the neon separator is sequentially connected to the third tube side of the second helium-neon heat exchanger, the activated carbon adsorber, and the fourth tube side of the first helium-neon heat exchanger. The gas outlet at the top of the distillation column is sequentially connected to the second tube side of the second helium-neon heat exchanger, the second tube side of the first helium-neon heat exchanger, the second helium-neon compressor, the second air cooler, and the liquid nitrogen cooler connected to the activated alumina adsorber. Both the nitrogen removal separator and the liquid nitrogen cooler have corresponding tube sides, into which liquid nitrogen is introduced. The nitrogen discharged from the tube sides of the nitrogen removal separator and the liquid nitrogen cooler can be discharged externally or stored as a byproduct.

[0010] The system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials provided in this application utilizes the low temperature generated by the hydrogen absorption and desorption cycle of the metal hydrogen storage materials to achieve air separation and hydrogen liquefaction. It makes full use of the chemical energy of hydrogen absorption and desorption by the metal hydrogen storage materials, and effectively utilizes the heat generated by hydrogen absorption and desorption and the cold energy generated by hydrogen desorption and desorption, thus achieving efficient utilization of hydrogen energy. Attached Figure Description

[0011] To more clearly illustrate the technical solutions in the embodiments of this application, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0012] Figure 1 This is a schematic diagram of the first part of the system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials, as provided in Embodiment 1 of this application. Figure 2 This is a schematic diagram of the AB metal hydride reaction bed module in Example 1; Figure 3 This is another structural schematic diagram of the AB metal hydride reaction bed module in Example 1; Figure 4 for Figure 2 Schematic diagram of the structure of part A in the middle; Figure 5 This is a schematic diagram of the BA metal hydride reaction bed module in Example 1; Figure 6 This is a schematic diagram of the second part of the system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials, provided in one embodiment of this application. Figure 7 This is a schematic diagram of the third part of the system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials provided in Embodiment 1 of this application; Figure 8 This is a schematic diagram of the structure for producing helium and neon provided in Embodiment 2 of this application; Figure 9 The temperature-pressure curves for hydrogen absorption and desorption of metal hydride A are shown. Figure 10 Temperature and pressure curves for hydrogen absorption and desorption of metal hydride B; Figure 11 Temperature and pressure curves for hydrogen absorption and desorption of Al' metal hydride; Figure 12 Temperature and pressure curves for hydrogen absorption and desorption of A2' metal hydride; Figure 13 Temperature and pressure curves for hydrogen absorption and desorption of A3' metal hydride; Figure 14 Temperature and pressure curves for hydrogen absorption and desorption of A4' metal hydride; Figure 15 Temperature and pressure curves for hydrogen absorption and desorption of B1' metal hydride; Figure 16 This is a schematic diagram of the operating status of producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials, provided in Embodiment 1 of this application; Figure 17This is a schematic diagram of the working principle of the AB metal hydride reaction bed module; Figure 18 This is a schematic diagram of the working principle of the BA metal hydride reaction bed module.

[0013] Wherein, 1—hydrogen expander, 2—integrated heat exchanger, 2-1—first tube side of integrated heat exchanger, 2-2—second tube side of integrated heat exchanger, 2-3—third tube side of integrated heat exchanger, 3—hydrogen heat exchanger, 3-1—first tube side of hydrogen heat exchanger, 3-2—second tube side of hydrogen heat exchanger, 3-3—third tube side of hydrogen heat exchanger, 3-4—fourth tube side of hydrogen heat exchanger, 3-5—fifth tube side of hydrogen heat exchanger, 3-6—sixth tube side of hydrogen heat exchanger, 4—second air heat exchanger, 5—hydrogen multi-stage expander, 6—circulating heat exchanger, 8—helium two-stage compressor, 10—third air heat exchanger, 11—air-helium heat exchanger, 12—third helium regenerator, 1 3—Helium single-stage expander; 14—Helium-hydrogen heat exchanger; 15—Second helium regenerator; 16—Second helium multi-stage expander; 17—Helium liquefaction heat exchange center; 171—First tube side of hydrogen liquefaction heat exchange center; 172—Second tube side of hydrogen liquefaction heat exchange center; 173—Third tube side of hydrogen liquefaction heat exchange center; 174—Fourth tube side of hydrogen liquefaction heat exchange center; 18—First helium regenerator; 19—Fracturing column; 191—First tube side of fractionating column evaporator; 192—Second tube side of fractionating column evaporator; 193—Third tube side of fractionating column evaporator; 20—First helium multi-stage expander; 21—Air liquefaction heat exchange center; 211—First tube side of air liquefaction heat exchange center. 212—Second tube pass of the air liquefaction heat exchange center; 213—Third tube pass of the air liquefaction heat exchange center; 2141—One parallel tube pass forming the fourth tube pass of the air liquefaction heat exchange center; 2142—Another parallel tube pass forming the fourth tube pass of the air liquefaction heat exchange center; 2143—Another parallel tube pass forming the fourth tube pass of the air liquefaction heat exchange center; 215—Fifth shell pass of the air liquefaction heat exchange center; 215'—Gas outlet of the fifth shell pass of the air liquefaction heat exchange center; 216—Sixth shell pass of the air liquefaction heat exchange center; 217—Seventh shell pass of the air liquefaction heat exchange center; 218—Eighth shell pass of the air liquefaction heat exchange center; 22—First metal hydride material layer; 23— Second metal hydride material layer, 24—copper wall, 25—outer shell, 26—insulation layer, 27—carbon fiber film, 28—rotary fork, 29—bed rotation drive structure, 30—ring plate partition, 31—gas collecting plate, 33—bed plate spring, 34—bed plate steel ball, 35—gas collecting plate spring, 36—gas collecting plate steel ball, 37—pressure hydrogen replacement center, 45—second air heat exchanger, 451—first tube side of the second air heat exchanger, 452—second tube side of the second air heat exchanger, 453—third tube side of the second air heat exchanger, 454—fourth tube side of the second air heat exchanger, 455—fifth tube side of the second air heat exchanger, 46—turbocharger, 47—hydrogen removal furnace.48—Water separator, 49—Gas storage tank, 50—First helium-neon compressor, 51—First air cooler, 52—Dryer, 53—First helium-neon heat exchanger, 531—First tube side of the first helium-neon heat exchanger, 532—Second tube side of the first helium-neon heat exchanger, 533—Third tube side of the first helium-neon heat exchanger, 534—Fourth tube side of the first helium-neon heat exchanger, 54—Nitrogen separator, 55—Activated alumina adsorber, 56—Second helium-neon heat exchanger, 561—Second tube side of the first helium-neon heat exchanger, 562—Second tube side of the second helium-neon heat exchanger, 563—Third tube side of the second helium-neon heat exchanger, 57—Helium coil heat exchanger, 58—Neon separator, 59 —Throttling expansion valve, 60—Distillation column, 61—Activated carbon adsorber, 62—Second helium-neon compressor, 63—Second air cooler, 64—Liquid nitrogen cooler, 65—Vacuum pump, 69—Central heat exchanger, 691—First shell side of the central heat exchanger, 691'—First tube side of the central heat exchanger, 692—Second shell side of the central heat exchanger, 692'—Second tube side of the central heat exchanger, 693—Third shell side of the central heat exchanger, 693'—Third tube side of the central heat exchanger, 694—Fourth shell side of the central heat exchanger, 694'—Fourth tube side of the central heat exchanger, 80—AB metal hydride reactor module, 81—BA metal hydride reactor module. Detailed Implementation

[0014] In the following description, specific details such as particular system architectures and techniques are set forth for illustrative purposes and not for limitation, in order to provide a thorough understanding of the embodiments of this application. However, those skilled in the art will understand that this application may also be implemented in other embodiments without these specific details. In other instances, detailed descriptions of well-known systems, apparatuses, and methods have been omitted so as not to obscure the description of this application with unnecessary detail.

[0015] To illustrate the technical solution described in this application, specific embodiments are provided below. Example 1

[0016] Figures 1 to 7 A schematic diagram of a system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials, as provided in an embodiment of this application, is shown. The system includes a hydrogen absorption / desorption cycle unit and a refrigeration unit, such as... Figure 1 As shown, the hydrogen absorption and desorption cycle unit includes an AB metal hydride reaction bed module 80, a BA metal hydride reaction bed module 81, a first air heat exchanger 45, and a central heat exchanger 69.

[0017] The AB metal hydride reactor module 80 is used to generate 2.5 MPa high-pressure hydrogen. The generated high-pressure hydrogen is divided into two parts: one part is supplied to the refrigeration unit; the other part is supplied to the BA metal hydride reactor module 81. The BA metal hydride reactor module 81 uses part of the 2.5 MPa high-pressure hydrogen and 0.15 MPa low-pressure hydrogen generated by the AB metal hydride reactor module 80 to produce an equivalent amount of 0.76 MPa medium-pressure hydrogen, supplementing the hydrogen absorption and desorption cycle required by the AB metal hydride reactor module 80.

[0018] Figure 2 and Figure 3The structure of the AB metal hydride reaction bed module 80 is shown. The AB metal hydride reaction bed module 80 has a cylindrical structure and is symmetrical from left to right. The left half is a -2.8℃ metal hydride reaction zone, and the right half is a -50℃ metal hydride reaction zone. A ring-shaped partition 30 separates the two parts. Within the AB metal hydride reaction bed module 80, alternating ring-shaped first metal hydride material layers 22 and second metal hydride material layers 23 are arranged, with copper walls 24 between each metal hydride material layer. In the -2.8℃ metal hydride reaction zone, the heat released when metal hydride B absorbs hydrogen is used to supply the heat released when metal hydride A releases hydrogen. In the -50℃ metal hydride reaction zone, the heat released when metal hydride A absorbs hydrogen is used to supply the heat released when metal hydride B releases hydrogen. The outer shell 25 of the AB metal hydride reaction bed module 80 is made of copper, and an insulating layer 26 is provided between the outer shell 25 and the outermost metal hydride material layer. The first metal hydride material layer 22 and the second metal hydride material layer 23 are respectively filled with metal hydrogen storage material B and metal hydrogen storage material A, and each layer of metal hydrogen storage material is wrapped with a carbon fiber film 27. Materials with good thermal conductivity and high strength, such as copper, aluminum, or aluminum alloys, can be used instead of carbon fiber. Alternatively, the AB metal hydride reactor module 80 can be entirely made of carbon fiber. A rotating fork 28 is provided at the top of the AB metal hydride reactor module 80, which can push the metal hydrogen storage material wrapped with the carbon fiber film 27 back and forth between the left and right parts of the AB metal hydride reactor module 80. Each carbon fiber film 27 is also provided with ventilation holes that connect to the gas collecting plate 31 located at the top, allowing hydrogen to enter and exit when the metal hydrogen storage material absorbs and releases hydrogen. A bed rotation drive structure 29 is provided at the bottom of the AB metal hydride reactor module 80. The bed rotation drive structure 29 can drive the outer shell 25 and each layer of copper walls 24 to rotate between the left and right parts of the AB metal hydride reactor module 80. Normally, a rotating fork 28 is used to push the metal hydrogen storage material wrapped in carbon fiber film 27 to switch the metal hydrogen storage material between the left and right parts of the AB metal hydride reaction bed module 80. The bed rotation drive structure 29 does not move, and the outer shell 25 and each copper wall 24 remain stationary. In special cases, the metal hydrogen storage material wrapped in carbon fiber film 27 remains stationary, while the bed rotation drive structure 29 drives the outer shell 25 and each copper wall 24 to rotate between the left and right parts of the AB metal hydride reaction bed module 80.

[0019] When the rotating fork 28 drives the metal hydrogen storage materials wrapped by the carbon fiber film 27 to rotate, or when the bed rotation drive structure 29 drives the outer shell 25 and the copper walls 24 to rotate, the gas collecting plate 31 is lifted, and the vent holes on the carbon fiber film 27 are automatically closed, thus allowing the rotation to proceed smoothly. When the rotation is in place, the gas collecting plate 31 is pressed down, opening the vent holes on the carbon fiber film 27 to complete the gas passage connection, allowing hydrogen to enter and exit. Figure 4 A schematic diagram of the assembly of the gas collecting plate 31 and the carbon fiber membrane 27 is shown. A bed spring 33 and a bed steel ball 34 are installed in the vent holes of the carbon fiber membrane 27. A gas collecting plate spring 35 and a gas collecting plate steel ball 36 are installed in the gas collecting port of the gas collecting plate 31. When the gas collecting plate 31 is pressed down, the gas collecting plate spring 35 and the gas collecting plate steel ball 36 compress the bed steel ball 34 and the bed spring 33, thereby establishing air passage between the carbon fiber membrane 27 and the gas collecting plate 31.

[0020] The BA metal hydride reaction bed module 81 is equipped with circulating A4' metal hydride, B1' metal hydride, A1' metal hydride, A2' metal hydride, and A3' metal hydride. The heat of reaction released when A4' metal hydride absorbs hydrogen is used to supply B1' metal hydride when it releases hydrogen; the heat of reaction released when B1' metal hydride absorbs hydrogen is used to supply A1' metal hydride when it releases hydrogen; the heat of reaction released when A1' metal hydride absorbs hydrogen is used to supply A2' metal hydride when it releases hydrogen; the heat of reaction released when A2' metal hydride absorbs hydrogen is used to supply A3' metal hydride when it releases hydrogen; and the heat of reaction released when A3' metal hydride absorbs hydrogen is used to supply A4' metal hydride when it releases hydrogen.

[0021] In the AB metal hydride reaction bed module 80, the hydrogen release outlet of the -2.8℃ metal hydride reaction zone releases 2.5MPa high-pressure hydrogen gas. This 2.5MPa high-pressure hydrogen gas is divided into two paths, one of which is sent to the refrigeration unit (the hydrogen flow path within the refrigeration unit is shown in...). Figure 6 As shown), another path passes through the first shell side 691, the second shell side 692 and the third shell side 693 of the central heat exchanger 69, and then connects to the hydrogen absorption line corresponding to the B1' metal hydride in the BA metal hydride reaction bed module 81.

[0022] In the BA metal hydride reaction bed module 81, the hydrogen release pipeline corresponding to metal hydride B1' connects to the hydrogen absorption pipeline corresponding to metal hydride A2' after passing through the second tube pass 452 of the second air heat exchanger 45. The hydrogen release pipeline corresponding to metal hydride A1' connects to the hydrogen absorption pipeline corresponding to metal hydride B in the -2.8℃ metal hydride reaction zone of the AB metal hydride reaction bed module 80 after passing through the second tube pass 692' of the central heat exchanger 69 and the fifth tube pass 455 of the second air heat exchanger 45. The hydrogen release pipeline corresponding to metal hydride A2' connects to the hydrogen absorption pipeline corresponding to metal hydride B in the -2.8℃ metal hydride reaction zone of the AB metal hydride reaction bed module 80 after passing through the first tube pass 691' of the central heat exchanger 69 and the fifth tube pass 455 of the second air heat exchanger 45. The hydrogen release line corresponding to metal hydride A3' connects to the hydrogen absorption line corresponding to metal hydride B in the -2.8℃ metal hydride reaction zone of the AB metal hydride reaction bed module 80 via the fifth tube 455 of the second air heat exchanger 45. The hydrogen release line corresponding to metal hydride A4' connects to the expansion inlet of turbocharger 46 via the fourth tube 454 of the second air heat exchanger 45 and the fourth shell side 694 of the central heat exchanger 69. The expansion outlet of turbocharger 46 connects to the hydrogen absorption line corresponding to metal hydride A1' via the first tube 451 of the second air heat exchanger 45.

[0023] In the AB metal hydride reaction bed module 80, the hydrogen release outlet of the -50℃ metal hydride reaction zone releases 0.15MPa low-pressure hydrogen gas, which is divided into four parts. The first part is connected to the hydrogen absorption pipeline corresponding to metal hydride A in the -50℃ metal hydride reaction zone, and is used for hydrogen absorption by metal hydride A in the AB metal hydride reaction bed module 80. The remaining three parts are used in the BA metal hydride reactor module 81, namely: the second part is connected to the hydrogen absorption pipe corresponding to metal hydride A2' in the BA metal hydride reactor module 81 after passing through the second tube 452 of the second air heat exchanger 45; the third part is connected to the hydrogen absorption pipe corresponding to metal hydride A3' in the BA metal hydride reactor module 81 after passing through the third tube 453 of the second air heat exchanger 45; the fourth part is connected to the compression inlet of the turbocharger 46, and the compression outlet of the turbocharger 46 is connected to the hydrogen absorption pipe corresponding to metal hydride B in the -2.8℃ metal hydride reactor in the AB metal hydride reactor module 80 after passing through the third tube 693' and fourth tube 694' of the central heat exchanger 69 and the fifth tube 455 of the second air heat exchanger 45.

[0024] Figure 5 The structure of the BA metal hydride reaction bed module 81 is shown. (Example) Figure 5As shown, the BA metal hydride reaction bed module 81 includes zones 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, and 11. Zones 1 and 2 are rotatable and arranged in pairs; zones 3 and 4 are rotatable and arranged in pairs; zones 5 and 6 are rotatable and arranged in pairs; zones 7 and 8 are rotatable and arranged in pairs; and zones 9 and 10 are rotatable and arranged in pairs.

[0025] Zone 1 is the B1'A1' heat exchange zone, used for the hydrogen absorption and heat release of B1' metal hydride and the hydrogen release and heat absorption of A1' metal hydride, while simultaneously completing heat exchange between the two. Zone 2 is the B1'A4' heat exchange zone, used for the hydrogen release and heat absorption of B1' metal hydride and the hydrogen absorption and heat release of A4' metal hydride, while simultaneously completing heat exchange between the two. Zones 3 and 4 are the A1' metal hydride transposition transition zones. Zones 5 and 6 are the A4' metal hydride transposition transition zones. Zone 7 is the A1'A2' heat exchange zone, used for the hydrogen absorption and heat release of A1' metal hydride and the hydrogen release and heat absorption of A2' metal hydride, while simultaneously completing heat exchange between the two. Zone 8 is the A2'A3' heat exchange zone, used for the hydrogen absorption and heat release of A2' metal hydride and the hydrogen release and heat absorption of A3' metal hydride, while simultaneously completing heat exchange between the two. Regions 9 and 10 are the A3' metal hydride transposition transition regions. Region 11 is the A3'A4' heat exchange region, used for the A3' metal hydride to absorb hydrogen and release heat and the A4' metal hydride to release hydrogen and absorb heat, while simultaneously completing the heat exchange between the two.

[0026] The B1' metal hydride in zones 1 and 2 can be directly rotated for switching. The A1' metal hydride in zones 1 and 7 can be transferred to zones 3 and 4 by rotational inversion to complete the position switch. The A2' metal hydride in zones 7 and 8 can be directly rotated for switching. The A3' metal hydride in zones 8 and 11 can be transferred to zones 9 and 10 by rotational inversion to complete the position switch. The A4' metal hydride in zones 2 and 11 can be transferred to zones 5 and 6 by rotational inversion to complete the position switch.

[0027] In addition, A1' metal hydride can move up and down between regions 1 and 7 via region 4; A4' metal hydride can move up and down between regions 2 and 5; and A3' metal hydride can move up and down between regions 8 and 9.

[0028] The working process of BA metal hydride reaction bed module 81 is as follows: Beat 1: In zone 1, metal hydride B1' absorbs hydrogen and releases heat, while metal hydride A1' absorbs hydrogen and releases heat; in zone 7, metal hydride A2' absorbs hydrogen and releases heat, while metal hydride A1' absorbs hydrogen and releases heat; in zone 8, metal hydride A3' absorbs hydrogen and releases heat, while metal hydride A2' absorbs hydrogen and releases heat; in zone 11, metal hydride A4' absorbs hydrogen and releases heat, while metal hydride A3' absorbs hydrogen and releases heat; in zone 2, metal hydride B1' absorbs hydrogen and releases heat, while metal hydride A4' absorbs hydrogen and releases heat.

[0029] Beat 2: The pairs of metal hydrides are transposed. Specifically, (a) the A1' metal hydride in zone 1 first moves down to zone 4 and rotates to zone 3 to wait; then the A1' metal hydride in zone 7 moves up to zone 4 and then continues to rise to zone 1; finally, the A1' metal hydride in zone 3 rotates and transposes back to zone 4 and moves down to zone 7. (b) the A3' metal hydride in zone 8 first moves up to zone 9 and rotates to zone 10 to wait; then the A3' metal hydride in zone 11 moves down to zone 9 and then continues to move down to zone 8; finally, the A3' metal hydride in zone 10 rotates and transposes back to zone 9 and moves up to zone 11. (iii) The A4' metal hydride in zone 2 first moves down to zone 5 and rotates to zone 6 to wait; then the A4' metal hydride in zone 11 moves up to zone 5 and then continues to rise to zone 2; finally, the A4' metal hydride in zone 6 rotates and swaps its position back to zone 5 and moves down to zone 11. (iv) While performing steps (i) to (iii), the B1' metal hydride in zones 1 and 2 directly rotates and swaps its position; the A2' metal hydride in zones 7 and 8 directly rotates and swaps its position.

[0030] Beat 3: Same as beat 1.

[0031] Repeat beats 1 through 3 above.

[0032] The first metal hydride material layer 22 and the second metal hydride material layer 23 of the AB metal hydride reactor module 80 are respectively filled with metal hydrides (also known as metal hydrogen storage materials). The BA metal hydride reactor module 81 is filled with metal hydrides (also known as metal hydrogen storage materials). The type and filling thickness of the metal hydride can be selected according to the actual needs of heat exchange between the various metal hydride reactors. Figure 1In the hydrogen absorption and desorption cycle unit shown, the hydrogen absorption conditions of metal hydride A, filled in the -2.8℃ and -50℃ metal hydride reaction regions of the AB metal hydride reaction bed module 80, are -49℃ and 0.15MPa, and the hydrogen desorption conditions are -2.8℃ and 2.5MPa, with a packing thickness of 0.7mm. The hydrogen absorption conditions of metal hydride B, filled in the -2.8℃ and -50℃ metal hydride reaction regions of the AB metal hydride reaction bed module 80, are -1.8℃ and 0.76MPa, and the hydrogen desorption conditions are -50℃ and 0.15MPa, with a packing thickness of 0.83mm. The hydrogen absorption conditions of metal hydride A1', filled in the BA metal hydride reaction bed module 81, are 11.2℃ and 0.15MPa, and the hydrogen desorption conditions are 49℃ and 0.76MPa. The hydrogen absorption conditions for A2' metal hydride filled in BA metal hydride reactor module 81 are -19.5℃ and 0.15MPa, and the hydrogen release conditions are 10.2℃ and 0.76MPa. The hydrogen absorption conditions for A3' metal hydride filled in BA metal hydride reactor module 81 are -44.4℃ and 0.15MPa, and the hydrogen release conditions are -20.5℃ and 0.76MPa. The hydrogen absorption conditions for A4' metal hydride filled in BA metal hydride reactor module 81 are -49℃ and 0.15MPa, and the hydrogen release conditions are -45.4℃ and 0.2MPa. The hydrogen absorption conditions for B1' metal hydride filled in BA metal hydride reactor module 81 are 50℃ and 2.5MPa, and the hydrogen release conditions are -50℃ and 0.15MPa. The temperature and pressure curves for hydrogen absorption and desorption of each metal hydride are shown below. Figures 9 to 15 As shown. Depending on their specific operating conditions, the aforementioned metal hydrides sometimes absorb hydrogen and sometimes release hydrogen.

[0033] Metal hydrides A, A1', A2', A3', and A4' are temperature-negative metal hydrogen storage materials. Metal hydride B and B1' are temperature-positive metal hydrogen storage materials. A temperature-negatively-dependent metal hydrogen storage material is defined as absorbing low-pressure hydrogen at low temperatures and releasing heat, and releasing high-pressure hydrogen at high temperatures and releasing cold energy. A temperature-positively-dependent metal hydrogen storage material is defined as absorbing high-pressure hydrogen at high temperatures and releasing high-temperature heat, and releasing low-pressure hydrogen at low temperatures and releasing low-temperature cold energy. In this application, metal hydrogen storage material A is a rare-earth-based metal hydrogen storage material, and metal hydrogen storage material B is an iron-titanium-based metal hydrogen storage material. Metal hydrogen storage material A experiences significant pressure changes with temperature, while metal hydrogen storage material B experiences smaller pressure changes with temperature.

[0034] Figure 1 The working process of the hydrogen absorption and desorption cycle unit shown (see...) Figure 16 The schematic diagram of the operating status is shown below: In the AB metal hydride reaction bed module 80, hydrogen gas at 12 g / s, 0.76 MPa, and -1.8°C is supplied to metal hydride B (in a hydrogen-absorbing state) packed in the -2.8°C metal hydride reaction zone. This process causes metal hydride A (in a hydrogen-releasing state) packed in the -2.8°C metal hydride reaction zone to release hydrogen gas at 8.62 g / s, -2.8°C, and 2.5 MPa. The first portion of circulating hydrogen gas at 5.97 g / s, -2.8°C, and 2.5 MPa is output from the hydrogen absorption / desorption cycle unit.

[0035] The second part of the hydrogen gas, at 2.65 g / s, -2.8℃, and 2.5 MPa, is heated to 45.5℃ after passing through the first shell side 691, the second shell side 692, and the third shell side 693 of the central heat exchanger 69. It then enters the hydrogen absorption pipeline corresponding to the B1' metal hydride (in a hydrogen absorption state) in the BA metal hydride reaction bed module 81, allowing the B1' metal hydride to absorb hydrogen and release heat at 50℃ and 2.5 MPa. This heat is used to cause the A1' metal hydride (in a hydrogen release state) in the BA metal hydride reaction bed module 81 to release hydrogen gas at 1.9 g / s, 49℃, and 0.76 MPa. Hydrogen gas at 1.9 g / s, 49°C, and 0.76 MPa passes through the second tube 692' of the central heat exchanger 69 and the fifth tube 455 of the second air heat exchanger 45. After its temperature drops to -1.8°C, it connects to the hydrogen absorption pipeline corresponding to the B metal hydride (in a hydrogen absorption state) packed in the -2.8°C metal hydride reaction zone of the AB metal hydride reaction bed module 80.

[0036] Hydrogen gas at 1.9 g / s, 11.2°C, and 0.15 MPa is supplied to the A1' metal hydride (in a hydrogen-absorbing state) packed in the BA metal hydride reaction bed module 81, causing it to absorb hydrogen and release heat at 11.2°C and 0.15 MPa. This heat is used to cause the A2' metal hydride (in a hydrogen-releasing state) packed in the BA metal hydride reaction bed module 81 to release hydrogen gas at 1.9 g / s, 10.2°C, and 0.76 MPa. The 1.9 g / s, 10.2°C, and 0.76 MPa hydrogen gas passes through the first tube 691' of the central heat exchanger 69 and the fifth tube 455 of the second air heat exchanger 45, and its temperature becomes -1.8°C. Then, it is connected to the hydrogen absorption pipeline corresponding to the B metal hydride (in a hydrogen-absorbing state) packed in the -2.8°C metal hydride reaction zone in the AB metal hydride reaction bed module 80.

[0037] Hydrogen gas at 1.9 g / s, -19.5°C, and 0.15 MPa is supplied to the A2' metal hydride (in a hydrogen-absorbing state) packed in the BA metal hydride reaction bed module 81, causing it to absorb hydrogen and release heat at -19.5°C and 0.15 MPa. This heat is used to cause the A3' metal hydride (in a hydrogen-releasing state) packed in the BA metal hydride reaction bed module 81 to release hydrogen gas at 1.9 g / s, -20.5°C, and 0.76 MPa. The 1.9 g / s, -20.5°C, and 0.76 MPa hydrogen gas is heated to -1.8°C via the fifth tube 455 of the second air heat exchanger 45 and connected to the hydrogen absorption pipeline corresponding to the B metal hydride (in a hydrogen-absorbing state) packed in the metal hydride reaction zone at -2.8°C in the AB metal hydride reaction bed module 80.

[0038] Hydrogen gas at 1.9 g / s, -44.4℃, and 0.15 MPa is supplied to the A3' metal hydride (in a hydrogen absorption state) packed in the BA metal hydride reaction bed module 81, so that it absorbs hydrogen and releases heat at -44.4℃ and 0.15 MPa. This heat is used to cause the A4' metal hydride (in a hydrogen release state) packed in the BA metal hydride reaction bed module 81 to release hydrogen gas at 1.9 g / s, -45.4℃, and 0.2 MPa. Hydrogen gas at 1.9 g / s, -45.4℃, and 0.2 MPa is heated to 20℃ after passing through the fourth tube side 454 of the second air heat exchanger 45 and the fourth shell side 694 of the central heat exchanger 69. It then enters the expansion inlet of the turbocharger 46, expands to 0.15 MPa, and then passes through the inlet of the first tube side 451 of the second air heat exchanger 45, where it is heated to 11.2℃. It is then connected to the hydrogen absorption pipeline corresponding to the Al' metal hydride (in a hydrogen absorption state) in the BA metal hydride reaction bed module 81.

[0039] Hydrogen gas at 1.9 g / s, -49°C, and 0.15 MPa is supplied to the A4' metal hydride (in a hydrogen-absorbing state) packed in the BA metal hydride reactor module 81, causing it to absorb hydrogen and release heat at -49°C and 0.15 MPa. The B1' metal hydride (in a hydrogen-releasing state) packed in the BA metal hydride reactor module 81 absorbs this heat and releases hydrogen gas at 2.65 g / s, -50°C, and 0.15 MPa. The 1.9 g / s, -50°C, and 0.15 MPa hydrogen gas is connected to the hydrogen absorption pipeline corresponding to the A4' metal hydride (in a hydrogen-absorbing state) in the BA metal hydride reactor module 81. The remaining -50℃, 0.15MPa hydrogen gas is heat-exchanged through the second tube 452 of the second air heat exchanger 45 and then connected to the hydrogen absorption pipeline corresponding to the A2' metal hydride (in a hydrogen absorption state) in the BA metal hydride reaction bed module 81.

[0040] Hydrogen gas at 8.62 g / s, 0.15 MPa, and -50°C is supplied to metal hydride A (in a hydrogen-absorbing state) packed in the -50°C metal hydride reaction zone of the AB metal hydride reaction bed module 80. At -49°C and 0.15 MPa, metal hydride A absorbs hydrogen and releases heat. This heat is used to cause metal hydride B (in a hydrogen-releasing state) packed in the -50°C metal hydride reaction zone of the AB metal hydride reaction bed module 80 to release hydrogen gas at 12 g / s, -50°C, and 0.15 MPa. This 12 g / s, -50°C, and 0.15 MPa hydrogen gas is divided into four parts. The first part, 8.62 g / s, 0.15 MPa, and -50°C hydrogen gas, is connected to the hydrogen absorption pipeline corresponding to metal hydride A (in a hydrogen-absorbing state) packed in the -50°C metal hydride reaction zone of the AB metal hydride reaction bed module 80. The second part, hydrogen gas at 1.15 g / s, 0.15 MPa, and -50°C, is connected via the second tube 452 of the second air heat exchanger 45 to the hydrogen absorption line corresponding to metal hydride A2' (in a hydrogen absorption state) in the BA metal hydride reactor module 81. The third part, hydrogen gas at 1.9 g / s, 0.15 MPa, and -50°C, is connected via the third tube 453 of the second air heat exchanger 45 to the hydrogen absorption line corresponding to metal hydride A3' (in a hydrogen absorption state) in the BA metal hydride reactor module 81. The fourth part, 0.33 g / s, 0.15 MPa, -50 °C hydrogen gas, is connected to the compression inlet of turbocharger 46. After being compressed to 0.76 MPa, it passes through the third tube 693' and fourth tube 694' of central heat exchanger 69 and the fifth tube 455 of second air heat exchanger 45 in sequence, and then connects to the hydrogen absorption pipeline corresponding to the B metal hydride (in a hydrogen absorption state) filled in the -2.8 °C metal hydride reaction zone in AB metal hydride reaction bed module 80.

[0041] The hydrogen absorption / desorption cycle unit provided in this application conforms to the following Coleridge's law: 1. Coleridge's First Law It is always possible to find at least two metal hydrides, including temperature-positive and / or temperature-negative metal hydrides, to form at least one cycle, which utilizes ambient energy or system energy, including system heat dissipation, to obtain pressurized hydrogen under a certain state to do work and generate corresponding forms of energy, thus becoming part of the cycle described above; while the cycle consumption within the cycle system is relatively small and comes from a portion of the work it does.

[0042] 2. Coleridge's Second Law For a given high-pressure hydrogen and a given low-pressure hydrogen, there can always be a cycle consisting of at least two metal hydrides to produce medium-pressure hydrogen at the corresponding pressure, while the cycle consumption is relatively small; the mass of medium-pressure hydrogen is the sum of the mass of the high-pressure hydrogen and the low-pressure hydrogen, and the required mass ratio of high-pressure hydrogen to low-pressure hydrogen is related to the following two factors: one is the expansion ratio between high-pressure hydrogen and medium-pressure hydrogen; the other is the compression ratio between low-pressure hydrogen and medium-pressure hydrogen.

[0043] 3. Coleridge's Third Law For a metal hydride undergoing hydrogen absorption / desorption cycles at two different plateau pressures, the hydride inevitably experiences sensible heat loss during each cycle as it switches between high and low temperatures (corresponding to high and low plateau pressures). This loss constitutes a major expense in completing the hydrogen absorption / desorption cycle. To reduce this expense, it is necessary to optimize the heat exchange between the high-temperature and low-temperature metal hydrides during the high / low temperature switching. One effective heat exchange optimization measure is to utilize the sensible heat of the high-temperature metal hydride for hydrogen desorption, gradually releasing hydrogen gas at different pressures (from high to low). This hydrogen gas at different pressures (from low to high) is then supplied to the low-temperature metal hydride for hydrogen absorption, releasing heat and gradually raising its temperature.

[0044] In Embodiment 1 of this application, the hydrogen absorption and desorption cycles of the metal hydrogen storage materials in each hydrogen reaction bed are kept consistent. When the hydrogen absorption cycle of the metal hydrogen storage material located in the hydrogen absorption and exothermic zone ends, a rotating device is used to transfer this portion of the metal hydrogen storage material to the hydrogen desorption and endothermic zone for a hydrogen desorption cycle; conversely, when the hydrogen desorption cycle of the metal hydrogen storage material located in the hydrogen desorption and endothermic zone ends, a rotating device is used to transfer this portion of the metal hydrogen storage material to the hydrogen absorption and exothermic zone for a hydrogen absorption cycle. The two portions of metal hydrogen storage materials in each hydrogen reaction bed thus repeatedly perform hydrogen absorption / desorption operations. For temperature-negatively correlated metal hydrogen storage materials (defined as materials that absorb low-pressure hydrogen and release heat at low temperatures, and absorb heat and release high-pressure hydrogen at high temperatures): The portion of the metal hydrogen storage material that has just been transferred to the hydrogen absorption and heat release zone is at a low temperature. At this time, hydrogen from each storage chamber of the pressure hydrogen replacement center 37 is introduced sequentially from low pressure to high pressure to absorb hydrogen and release heat, causing the metal hydrogen storage material to gradually heat up to near the hydrogen release temperature. Meanwhile, the portion of the metal hydrogen storage material that has just been transferred to the hydrogen absorption and heat release zone is at a high temperature. The sensible heat of the metal hydrogen storage material is used to release hydrogen, causing the metal hydrogen storage material to gradually cool down to near the hydrogen absorption temperature. At the same time, hydrogen at different pressures is released sequentially from high pressure to low pressure and sent to each storage chamber of the pressure hydrogen replacement center 37 for storage. For temperature-dependent metal hydrogen storage materials (defined as those that absorb high-pressure hydrogen at high temperatures and release high-temperature heat, and release low-pressure hydrogen at low temperatures to provide low-temperature cooling), the process is reversed: the portion of the metal hydrogen storage material just transferred to the hydrogen-absorbing heat release zone is at a high temperature. Hydrogen is released using the sensible heat of this portion of the metal hydrogen storage material, causing it to gradually cool down to near the hydrogen release temperature. Simultaneously, hydrogen at different pressures is released sequentially from high pressure to low pressure and sent to the respective storage chambers of the pressure hydrogen replacement center 37 for storage. Conversely, the portion of the metal hydrogen storage material just transferred to the hydrogen-absorbing heat release zone is at a low temperature. Hydrogen is then sequentially introduced into the storage chambers of the pressure hydrogen replacement center 37 in order from low pressure to high pressure to absorb hydrogen and release heat, causing this portion of the metal hydrogen storage material to gradually heat up to near the hydrogen absorption temperature. The amount of hydrogen at different pressures consumed by the metal hydrogen storage material during heating from the pressure hydrogen replacement center 37 is equal to the amount of hydrogen at different pressures sent to the pressure hydrogen replacement center during cooling. The following describes the operation of the pressure hydrogen replacement center 37, which is paired with the AB metal hydride reaction bed module 80: The pressure hydrogen replacement center is divided into 15 storage chambers, which store hydrogen at pressures of 2.56 MPa, 2.18 MPa, 1.85 MPa, 1.56 MPa, 1.31 MPa, 1.1 MPa, 0.92 MPa, 0.76 MPa, 0.63 MPa, 0.52 MPa, 0.43 MPa, 0.35 MPa, 0.28 MPa, 0.23 MPa, and 0.18 MPa, respectively, in order from high pressure to low pressure. At the end of the hydrogen absorption cycle, the metal hydrogen storage material located in the hydrogen absorption and exothermic zone has a temperature of -49℃. It is then transferred to the hydrogen exothermic and exothermic zone using a rotating device. Next, 5.2g of hydrogen gas is introduced into the 0.18MPa storage chamber of the pressure hydrogen replacement center. After absorbing hydrogen, the metal hydrogen storage material releases the heat of reaction, causing its temperature to rise to -46.3℃. Then, 5.2g of hydrogen gas is introduced into the 0.23MPa storage chamber of the pressure hydrogen replacement center. After absorbing hydrogen, the metal hydrogen storage material releases the heat of reaction, causing its temperature to rise to -43℃. 4℃; and so on, following the order from low pressure to high pressure, 5.2g of hydrogen gas was sequentially introduced into the hydrogen replacement center at pressures of 0.28MPa, 0.35MPa, 0.43MPa, 0.52MPa, 0.63MPa, 0.76MPa, 0.92MPa, 1.1MPa, 1.31MPa, 1.56MPa, 1.85MPa, 2.18MPa, and 2.56MPa. The temperature of this part of the metal hydrogen storage material gradually rose to -5.7℃.

[0045] Figure 6 and Figure 7 The diagram shows that the circulating hydrogen released from the hydrogen absorption and desorption cycle unit is divided into two paths after passing through the tube side of the circulating heat exchanger 6. The first path of circulating hydrogen passes through the tube side of the hydrogen expander 1, the integrated heat exchanger 2, and the shell side of the circulating heat exchanger 6 before returning to the hydrogen absorption and desorption cycle unit. The second path of circulating hydrogen passes through the hydrogen heat exchanger 3 and the second air heat exchanger 4 before entering the hydrogen multi-stage expander 5 for expansion, and then returns to the hydrogen absorption and desorption cycle unit through the shell side of the circulating heat exchanger 6.

[0046] The first-stage outlet of the helium-two compressor 8 enters the second-stage inlet of the helium-two compressor 8 after passing through the hydrogen heat exchanger 3 and the third air heat exchanger 10. The second-stage outlet of the helium-two compressor 8 is divided into three paths after passing through the air-helium heat exchanger 11. The first path of helium output from the air-helium heat exchanger 11 passes through the shell side of the third helium regenerator 12, the helium single-stage expander 13, the hydrogen-helium heat exchanger 14, and the tube side of the third helium regenerator 12 before entering the first-stage inlet of the helium-two compressor 8. The second path of helium output from the air-helium heat exchanger 11... Helium gas passes through the shell side of the second helium regenerator 15, the second helium multistage expander 16, the hydrogen liquefaction heat exchange center 17, and the tube side of the second helium regenerator 15 before entering the first stage inlet of the helium-two compressor 8. The third stream of helium gas output from the air-helium heat exchanger 11 passes through the shell side of the first helium regenerator 18, the second tube side 192 of the evaporator in the fractionation tower 19, the first helium multistage expander 20, the air liquefaction heat exchange center 21, and the tube side of the first helium regenerator 18 before entering the first stage inlet of the helium-two compressor 8.

[0047] After pretreatment (for dust removal, water removal, and CO2 removal), ambient temperature air is pre-cooled in the first tube side 191 of the evaporator in the integrated heat exchanger 2 and the fractionation tower 19. Then, it is liquefied in the fifth shell side 215 of the air liquefaction heat exchange center 21. The liquefied air is sent to the feed inlet of the fractionation tower 19, and nitrogen, oxygen, and argon are output from different outlets of the fractionation tower 19. The nitrogen output from the fractionation tower 19 is converted into liquid nitrogen after passing through the sixth shell side 216 of the air liquefaction heat exchange center 21. The oxygen output from the fractionation tower 19 is converted into liquid oxygen after passing through the seventh shell side 217 of the air liquefaction heat exchange center 21. The argon output from the fractionation tower 19 is converted into liquid argon after passing through the eighth shell side 218 of the air liquefaction heat exchange center 21.

[0048] Room temperature hydrogen is converted into liquid hydrogen after passing through the integrated heat exchanger 2, the third tube side 193 of the evaporator in the fractionation tower 19, the shell side of the hydrogen-helium heat exchanger 14, and the fourth tube side 174 of the hydrogen liquefaction heat exchange center 17.

[0049] The hydrogen multistage expander 5, the helium two-stage compressor 8, the first helium multistage expander 20, the second helium multistage expander 16, and the helium single-stage expander 13 are coaxially connected.

[0050] Figure 6 and Figure 7 The working process of the liquid hydrogen and liquid oxygen preparation equipment shown is as follows: The first stream of circulating hydrogen at 0.44 g / s, 15°C, and 2.5 MPa passes through the third tube side 2-3 of the hydrogen expander 1 and the shell side of the integrated heat exchanger 2 and the circulating heat exchanger 6 before returning to the -50°C metal hydride reaction bed 7 of the hydrogen absorption and desorption circulation unit. The second stream of circulating hydrogen gas, at 5.53 g / s, 15°C, and 2.5 MPa, is heated to 400°C in the first tube pass 3-1 of hydrogen heat exchanger 3 before entering the first stage of hydrogen multi-stage expander 5. Circulating hydrogen gas at 345°C and 1.85 MPa is discharged from the first stage expansion outlet of hydrogen multi-stage expander 5. This 345°C, 1.85 MPa circulating hydrogen gas then passes through the second tube pass 3-2 of hydrogen heat exchanger 3, is heated to 400°C, and enters the second stage of hydrogen multi-stage expander 5. Circulating hydrogen gas at 346.5°C and 1.38 MPa is discharged from the second stage expansion outlet of hydrogen multi-stage expander 5. This 346.5°C, 1.38 MPa circulating hydrogen gas then passes through hydrogen heat exchanger 3... After the third tube pass 3-3, the temperature is raised to 400℃. Circulating hydrogen at 400℃ and 1.38MPa enters the third stage of the hydrogen multistage expander 5. Circulating hydrogen at 344.8℃ and 1.02MPa is discharged from the expansion outlet of the third stage of the hydrogen multistage expander 5. This 344.8℃ and 1.02MPa circulating hydrogen is cooled to 43.5℃ via the shell side of the second air heat exchanger 4 before entering the fourth stage of the hydrogen multistage expander 5. Circulating hydrogen at 18℃ and 0.76MPa is discharged from the expansion outlet of the fourth stage of the hydrogen multistage expander 5. This 18℃ and 0.76MPa circulating hydrogen returns to the -2.8℃ metal hydride reaction zone in the AB metal hydride reaction bed module 80 via the shell side of the circulating heat exchanger 6. The first-stage outlet of the helium-two compressor 8 discharges circulating helium gas at 463°C and 1 MPa. This circulating helium gas at 463°C and 1 MPa enters the fourth tube pass (3-4), fifth tube pass (3-5), and sixth tube pass (3-6) of the hydrogen heat exchanger 3 simultaneously via three separate streams. After exiting the shell-side outlet of the hydrogen heat exchanger 3, the circulating helium gas enters the third air heat exchanger 10 to be cooled to 30°C. The 30°C, 1 MPa circulating helium gas is then compressed in the second stage of the helium-two compressor 8 and cooled in the air-helium heat exchanger 11, converting it into 30°C, 10 MPa circulating helium gas.

[0051] The circulating helium gas discharged from the air-helium heat exchanger 11 at 30℃ and 10MPa is divided into three streams. The first stream of circulating helium gas at 30℃ and 10MPa is cooled to -183℃ via the shell side of the third helium regenerator 12. The -183℃ and 10MPa circulating helium gas is then expanded by the helium single-stage expander 13 and converted into -258.9℃ and 0.1MPa circulating helium gas. The -258.9℃ and 0.1MPa circulating helium gas is heated to -190℃ via the tube side of the hydrogen-helium heat exchanger 14. The -190℃ and 0.1MPa circulating helium gas is heated to 20℃ via the tube side of the third helium regenerator 12, and the 20℃ and 0.1MPa circulating helium gas enters the first stage inlet of the helium-two compressor 8.

[0052] The second stream of circulating helium gas at 30°C and 10MPa is cooled to -242°C via the shell side of the second helium regenerator 15. The -242°C, 10MPa circulating helium gas then enters the first stage of the second helium multistage expander 16, and the first stage expansion outlet of the second helium multistage expander 16 outputs circulating helium gas at -253°C and 3.16MPa. -253℃, 3.16MPa circulating helium gas is expanded to -260.3℃, 1MPa in the second stage of the second helium multistage expander 16, and then enters the first tube 171 of the hydrogen liquefaction heat exchange center 17 to be heated to -253℃. Then it is expanded to -260.5℃, 0.316MPa in the third stage of the second helium multistage expander 16, and then enters the second tube 172 of the hydrogen liquefaction heat exchange center 17 to be heated to -253℃. Then it is expanded to -260.5℃, 0.1MPa in the fourth stage of the second helium multistage expander 16, and then enters the third tube 173 of the hydrogen liquefaction heat exchange center 17 to be heated. The third tube 173 of the hydrogen liquefaction heat exchange center 17 discharges -253℃, 0.1MPa circulating helium gas. -253℃, 0.1MPa circulating helium gas is heated to 20℃ through the tube side of the second helium regenerator 15, and the 20℃, 0.1MPa circulating helium gas enters the first stage inlet of the second helium compressor 8.

[0053] The third stream of circulating helium gas at 30℃ and 10MPa is cooled to -182.84℃ in the shell side of the first helium regenerator 18 and then enters the second tube side 192 of the evaporator in the fractionation tower 19, where it is further cooled to -196℃. This -196℃, 10MPa circulating helium gas then enters the first stage of the first helium multi-stage expander 20. The first stage of the first helium multi-stage expander 20 outputs circulating helium gas at -224.5℃ and 3.16MPa. This -224.5℃, 3.16MPa circulating helium gas is then heated to -196℃ in the first tube side 211 of the air liquefaction heat exchange center 21 and then enters the second stage of the first helium multi-stage expander 20. The second stage of the first helium multi-stage expander 20 outputs circulating helium gas at -224.5℃ and 1MPa. Circulating helium gas at -224.5℃ and 1MPa is heated to -196℃ via the second tube 212 of the air liquefaction heat exchange center 21 and then enters the third stage of the first helium multi-stage expander 20. The third stage expansion outlet of the first helium multi-stage expander 20 outputs circulating helium gas at -224.5℃ and 0.316MPa. This circulating helium gas at -224.5℃ and 0.316MPa is then heated to -196℃ via the third tube 213 of the air liquefaction heat exchange center 21 and then enters the fourth stage of the first helium multi-stage expander 20. The fourth stage expansion outlet of the first helium multi-stage expander 20 outputs circulating helium gas at -224.5℃ and 0.1MPa. -224.5℃, 0.1MPa circulating helium gas is sequentially heated to 20℃ after passing through the fourth tube pass of the air liquefaction heat exchange center 21 and the tube pass of the first helium regenerator 18. The 20℃, 0.1MPa circulating helium gas then enters the first stage inlet of the helium-two compressor 8. The fourth tube pass of the air liquefaction heat exchange center 21 consists of three parallel tube passes 2141, 2142, and 2143.

[0054] 4.326 g / s, 20°C ambient air is pretreated (including dust removal, water removal, and CO2 removal) and then cooled to -65°C in the first tube side 2-1 of the integrated heat exchanger 2. It is then further cooled to -183°C in the first tube side 191 of the evaporator in the fractionation tower 19. It then enters the fifth shell side 215 of the air liquefaction heat exchange center 21 to be cooled and liquefied. Non-condensable gas (i.e., helium-neon raw material gas) is discharged from the corresponding gas outlet 215'. The liquefied air is sent to the feed inlet of the fractionation tower 19, where it is evaporated and fractionated. Finally, nitrogen, oxygen, and argon are output from different outlets of the fractionation tower 19. The nitrogen gas output from fractionation column 19 enters the sixth shell 216 of air liquefaction heat exchange center 21 and is cooled and liquefied into liquid nitrogen at -196℃; the oxygen gas output from fractionation column 19 enters the seventh shell 217 of air liquefaction heat exchange center 21 and is cooled and liquefied into liquid oxygen at -184℃; the argon gas output from fractionation column 19 enters the eighth shell 218 of air liquefaction heat exchange center 21 and is cooled and liquefied into liquid argon at -186℃.

[0055] Hydrogen gas at room temperature of 20°C is cooled to -183°C after passing through the second tube side 2-2 of the integrated heat exchanger 2 and the third tube side 193 of the evaporator in the fractionation tower 19. The hydrogen gas at -183°C is cooled to -252°C after passing through the shell side of the hydrogen-helium heat exchanger 14. The hydrogen gas at -252°C is converted into liquid hydrogen at -253°C after passing through the indirect heat exchange of the fourth tube side 174 of the hydrogen liquefaction heat exchange center 17. Example 2

[0056] Figure 8 A schematic diagram of the system for producing helium and neon gas according to Embodiment 2 of this application is shown. Figure 8 As shown, the system for producing helium and neon includes, in sequence, a hydrogen removal furnace 47, a water separator 48, a gas storage tank 49, a first helium-neon compressor 50, a first air cooler 51, a dryer 52, a first helium-neon heat exchanger 53, a nitrogen separator 54, an activated alumina adsorber 55, a second helium-neon heat exchanger 56, a helium coil heat exchanger 57, a neon separator 58, a throttling expansion valve 59, and a distillation column 60. The non-condensable gas outlet at the top of the neon separator 58 is sequentially connected to the third tube side 563 of the second helium-neon heat exchanger, the activated carbon adsorber 61, and the fourth tube side 534 of the first helium-neon heat exchanger. The non-condensable gas outlet at the top of the distillation column 60 is sequentially connected to the second tube side 562 of the second helium-neon heat exchanger, the second tube side 532 of the first helium-neon heat exchanger, the second helium-neon compressor 62, the second air cooler 63, and the liquid nitrogen cooler 64, and is connected to the activated alumina adsorber 55. Both the nitrogen separator 54 and the liquid nitrogen cooler 64 have corresponding tubes, into which liquid nitrogen is introduced. The nitrogen discharged from the tubes of the nitrogen separator 54 and the liquid nitrogen cooler 64 can be discharged externally or stored as a by-product.

[0057] Figure 8 The working process of the system shown for producing helium and neon is as follows: The feed gas and oxygen are conveyed to the hydrogen removal furnace 47 from their respective gas inlets. The feed gas is from Example 1. Figure 7The non-condensable gas discharged from the air liquefaction heat exchange center 21 consists of 49% N2, 35% Ne, 11% He, and 5% H2. A platinum catalyst is added to the hydrogen removal furnace 47. In the hydrogen removal furnace 47, the H2 in the feed gas is oxidized by oxygen at 300°C to produce water vapor. After exiting the hydrogen removal furnace 47, the crude neon-helium gas and water vapor enter the water separator 48. Cooling gas flows through the tubes of the water separator 48, and the water vapor is liquefied after being cooled by the cooling gas and discharged from the liquid outlet of the water separator 48. Crude neon-helium gas (49.6% N2, 38.1% Ne, 12.3% He, H2 < 1 ppm) exits separator 48 and enters the first helium-neon compressor 50 via storage tank 49. After being pressurized to 3.3 MPa by the first helium-neon compressor 50, it enters the shell-side inlet of the first air cooler 51. The 3.3 MPa raw gas exits from the shell-side outlet of the first air cooler 51, passes through dryer 52 to remove moisture, and then enters the first tube side 531 of the first helium-neon heat exchanger 53 for cooling. After exiting the first tube side 531 of the first helium-neon heat exchanger, it enters the denitrification separator 54. In the denitrification separator 54, the 3.3 MPa crude neon-helium gas is further cooled by a liquid nitrogen bath under negative pressure, controlling the vacuum degree to 0.01~0.02 MPa and the temperature to approximately -207℃. Most of the oxygen and nitrogen in the crude neon-helium gas are condensed and discharged from the liquid outlet at the bottom of the denitrification separator 54. Liquid nitrogen flows through the tube side of the denitrification separator 54. After evaporation, the liquid nitrogen is either discharged via vacuum pump 65 or stored as a byproduct. The 3.3 MPa purified neon-helium gas exiting the shell side of the denitrification separator 54 passes through an activated alumina adsorber 55 to remove residual oxygen and nitrogen before entering the shell side of the second helium-neon heat exchanger 56 and being cooled to 30 K. It then passes through the shell side of the helium coil heat exchanger 57, where most of the neon gas is condensed, before entering the neon separator 58 to separate neon and helium. The tube side of the helium coil heat exchanger 57 is the same as in Example 1. Figure 7 The second helium multistage expander 16 is connected. Liquid neon is discharged from the liquid outlet at the bottom of the neon separator 58, and then enters the distillation column 60 after passing through the throttling expansion valve 59. Liquid pure neon is discharged from the liquid outlet at the bottom of the distillation column 60. After heat exchange in the second tube pass 561 and the third tube pass 533 of the first helium-neon heat exchanger, the liquid pure neon can be used as a product.

[0058] The gas outlet at the top of the neon separator 58 discharges uncondensed helium-rich gas (84% He, 16% Ne). This helium-rich gas then passes through the third tube 563 of the second helium-neon heat exchanger and enters the activated carbon adsorber 61. The activated carbon adsorber 61 absorbs all the neon from the uncondensed gas, discharging pure helium. This pure helium then passes through the fourth tube 534 of the first helium-neon heat exchanger and is ready as a product.

[0059] The gas outlet at the top of distillation column 60 discharges non-condensable gas containing 10.6% He and 89.4% Ne. This non-condensable gas, containing 10.6% He and 89.4% Ne, passes through the second tube side 562 of the second helium-neon heat exchanger and the second tube side 532 of the first helium-neon heat exchanger before entering the second helium-neon compressor 62. The second helium-neon compressor 62 pressurizes the gas to 3.3 MPa, and then passes through the shell side of the second air cooler 63 and the shell side of the liquid nitrogen cooler 64 before entering the activated alumina adsorber 55.

[0060] The above-described embodiments are only used to illustrate the technical solutions of this application, and are not intended to limit them. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of this application, and should all be included within the protection scope of this application.

Claims

1. A system for producing liquid hydrogen and liquid oxygen using metallic hydrogen storage materials, comprising a hydrogen absorption and desorption cycle unit, characterized in that, The circulating hydrogen released by the hydrogen absorption and desorption cycle unit is divided into two paths. The first path of circulating hydrogen returns to the hydrogen absorption and desorption cycle unit after passing through the tube side of the hydrogen expander (1) and the integrated heat exchanger (2). The second circulating hydrogen enters the hydrogen multi-stage expander (5) through the hydrogen heat exchanger (3) and the second air heat exchanger (4), and then returns to the hydrogen absorption and desorption cycle unit after expansion. The first-stage outlet of the helium-2 compressor (8) enters the second-stage inlet of the helium-2 compressor (8) after passing through the hydrogen heat exchanger (3) and the third air heat exchanger (10). The second-stage outlet of the helium-2 compressor (8) is divided into three paths after passing through the air-helium heat exchanger (11). The first path of helium output from the air-helium heat exchanger (11) enters the first-stage inlet of the helium-2 compressor (8) after passing through the shell side of the third helium regenerator (12), the helium single-stage expander (13), the hydrogen-helium heat exchanger (14), and the tube side of the third helium regenerator (12). The second path of helium output from the air-helium heat exchanger (11) enters the first-stage inlet of the helium-2 compressor (8). The second stream of helium gas passes through the shell side of the second helium regenerator (15), the second helium multistage expander (16), the hydrogen liquefaction heat exchange center (17), and the tube side of the second helium regenerator (15) before entering the first stage inlet of the helium-two compressor (8); the third stream of helium gas output from the air-helium heat exchanger (11) passes through the shell side of the first helium regenerator (18), the second tube side of the evaporator in the fractionation tower (19), the first helium multistage expander (20), the air liquefaction heat exchange center (21), and the tube side of the first helium regenerator (18) before entering the first stage inlet of the helium-two compressor (8); Ambient air enters the feed inlet of the fractionating tower (19) through the first tube of the evaporator in the integrated heat exchanger (2) and the fifth tube of the air liquefaction heat exchange center (21). Nitrogen, oxygen and argon are output from different outlets of the fractionating tower (19). The nitrogen output from the fractionating tower (19) is converted into liquid nitrogen after passing through the sixth tube of the air liquefaction heat exchange center (21). The oxygen output from the fractionating tower (19) is converted into liquid oxygen after passing through the seventh tube of the air liquefaction heat exchange center (21). The argon output from the fractionating tower (19) is converted into liquid argon after passing through the eighth tube of the air liquefaction heat exchange center (21). Ambient hydrogen is converted into liquid hydrogen after passing through the integrated heat exchanger (2), the third tube side of the evaporator in the fractionation tower (19), the shell side of the hydrogen-helium heat exchanger (14), and the hydrogen liquefaction heat exchange center (17). The hydrogen multistage expander (5), the helium two-stage compressor (8), the first helium multistage expander (20), the second helium multistage expander (16), and the helium single-stage expander (13) are coaxially connected.

2. The system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials as described in claim 1, characterized in that, The hydrogen absorption and desorption cycle unit includes an AB metal hydride reaction bed module (80), a BA metal hydride reaction bed module (81), a first air heat exchanger (45), and a central heat exchanger (69). The AB metal hydride reaction bed module (80) has a cylindrical structure and is symmetrical from left to right. The left half is a metal hydride reaction zone at -2.8℃, and the right half is a metal hydride reaction zone at -50℃. A ring plate partition (30) is provided between the two parts. Inside the AB metal hydride reaction bed module (80), there are alternating ring-shaped first metal hydride material layers (22) and second metal hydride material layers (23), and copper plates (24) are provided between each metal hydride material layer. In the -2.8℃ metal hydride reaction zone, the reaction heat released when metal hydride B absorbs hydrogen is used to supply metal hydride A when it releases hydrogen. In the -50℃ metal hydride reaction zone, the reaction heat released when metal hydride A absorbs hydrogen is used to supply metal hydride B when it releases hydrogen. The outer shell (25) of the AB metal hydride reaction bed module (80) is made of copper, and an insulation layer (26) is provided between the outer shell (25) and the outermost metal hydride material layer. The first metal hydride material layer (22) and the second metal hydride material layer (23) are respectively filled with metal hydrogen storage material B and metal hydrogen storage material A. Each layer of metal hydrogen storage material is wrapped with carbon fiber film (27). The top of the AB metal hydride reaction bed module is provided with a rotating fork (28). The rotating fork (28) can push the metal hydrogen storage material wrapped with carbon fiber film (27) back and forth between the left and right parts of the AB metal hydride reaction bed module (80). Each carbon fiber film (27) is also provided with a vent hole that is connected to the gas collection plate (31) set at the top, so as to supply hydrogen gas in and out when the metal hydrogen storage material absorbs and releases hydrogen. The bottom of the AB metal hydride reaction bed module (80) is provided with a bed rotation drive structure (29). The bed rotation drive structure (29) can drive the outer shell (25) and each copper plate (24) to rotate between the left and right parts of the AB metal hydride reaction bed module (80). When the rotating fork (28) drives the metal hydrogen storage material wrapped by the carbon fiber film (27) to rotate, or when the bed rotation drive structure (29) drives the outer shell (25) and each copper plate (24) to rotate, the gas collecting plate (31) is lifted, and the vent on the carbon fiber film (27) is automatically closed, so that the rotation proceeds smoothly; when the rotation is in place, the gas collecting plate (31) is pressed down, squeezing open the vent on the carbon fiber film (27) to complete the gas path connection, so that hydrogen can enter and exit; the vent of the carbon fiber film (27) is provided with a bed plate spring (33) and a bed plate steel ball (34); the gas collecting port of the gas collecting plate (31) is provided with a gas collecting plate spring (35) and a gas collecting plate steel ball (36); when the gas collecting plate (31) is pressed down, the gas collecting plate spring (35) and the gas collecting plate steel ball (36) squeeze the bed plate steel ball (34) and the bed plate spring (33), so that the carbon fiber film (27) and the gas collecting plate (31) complete the gas path connection; The BA metal hydride reaction bed module (81) is filled with reusable A4' metal hydride, B1' metal hydride, A1' metal hydride, A2' metal hydride and A3' metal hydride; the heat of reaction released when A4' metal hydride absorbs hydrogen is used when B1' metal hydride releases hydrogen; the heat of reaction released when B1' metal hydride absorbs hydrogen is used when A1' metal hydride releases hydrogen; the heat of reaction released when A1' metal hydride absorbs hydrogen is used when A2' metal hydride releases hydrogen; the heat of reaction released when A2' metal hydride absorbs hydrogen is used when A3' metal hydride releases hydrogen; the heat of reaction released when A3' metal hydride absorbs hydrogen is used when A4' metal hydride releases hydrogen. In the AB metal hydride reaction bed module (80), hydrogen A gas is released from the hydrogen outlet of the -2.8℃ metal hydride reaction area. The hydrogen A gas is divided into two paths. One path is output from the hydrogen absorption and desorption circulation unit and then divided into the first circulation hydrogen gas and the second circulation hydrogen gas. The other path passes through the first shell side (691), the second shell side (692) and the third shell side (693) of the central heat exchanger (69) and is connected to the hydrogen absorption pipeline corresponding to the B1' metal hydride in the two B1'A1' metal hydride reaction beds (32). In the BA metal hydride reaction bed module (81), the hydrogen release pipeline corresponding to B1' metal hydride is connected to the hydrogen absorption pipeline corresponding to A2' metal hydride after passing through the second tube (452) of the second air heat exchanger (45); the hydrogen release pipeline corresponding to A1' metal hydride is connected to the hydrogen absorption pipeline corresponding to B metal hydride in the -2.8℃ metal hydride reaction zone in the AB metal hydride reaction bed module (80) after passing through the second tube (692') of the central heat exchanger (69) and the fifth tube (455) of the second air heat exchanger (45); the hydrogen release pipeline corresponding to A2' metal hydride is connected to the hydrogen absorption pipeline corresponding to B metal hydride in the -2.8℃ metal hydride reaction zone in the AB metal hydride reaction bed module (80) after passing through the first tube (691') of the central heat exchanger (69) and the fifth tube (455) of the second air heat exchanger (45). The hydrogen release pipeline corresponding to metal hydride A3' passes through the fifth tube (455) of the second air heat exchanger (45) and is connected to the hydrogen absorption pipeline corresponding to metal hydride B in the -2.8℃ metal hydride reaction zone of the AB metal hydride reaction bed module (80). The hydrogen release pipeline corresponding to the A4' metal hydride passes through the fourth tube side (454) of the second air heat exchanger (45) and the fourth shell side (694) of the central heat exchanger (69) in sequence, and then connects to the expansion inlet of the turbocharger (46). The expansion outlet of the turbocharger (46) passes through the first tube side (451) of the second air heat exchanger (45) and then connects to the hydrogen absorption pipeline corresponding to the A1' metal hydride. In the AB metal hydride reaction bed module (80), hydrogen B gas is released from the hydrogen outlet of the -50℃ metal hydride reaction zone. The hydrogen B gas is divided into four parts. The first part is connected to the hydrogen absorption pipe corresponding to metal A in the -50℃ metal hydride reaction zone; the second part is connected to the hydrogen absorption pipe corresponding to metal A2' in the BA metal hydride reaction bed module (81) after passing through the second tube side (452) of the second air heat exchanger (45); the third part is connected to the hydrogen absorption pipe corresponding to metal A2' in the BA metal hydride reaction bed module (81) after passing through the third tube side (453) of the second air heat exchanger (45). The hydrogen absorption pipe corresponding to metal hydride A3' in the BA metal hydride reactor module (81) is connected; the fourth part is connected to the compression inlet of the turbocharger (46), and the compression outlet of the turbocharger (46) is connected to the hydrogen absorption pipe corresponding to metal hydride B in the -2.8℃ metal hydride reactor (6) in the AB metal hydride reactor module (80) after passing through the third tube (693') and the fourth tube (694') of the central heat exchanger (69) and the fifth tube (455) of the second air heat exchanger (45).

3. The system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials as described in claim 2, characterized in that, For the -2.8℃ metal hydride reaction zone and the -50℃ metal hydride reaction zone in the AB metal hydride reaction bed module (80), and for the AB metal hydride reaction bed module (80), the type of metal hydrogen storage material to be filled is selected according to the actual needs of heat exchange between the various metal hydride reaction beds.

4. The system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials as described in claim 3, characterized in that, A-metal hydride, A1' metal hydride, A2' metal hydride, A3' metal hydride, and A4' metal hydride are temperature-negative metal hydrogen storage materials. Temperature-negative metal hydrogen storage materials are defined as those that absorb low-pressure hydrogen at low temperatures and release heat, and release high-pressure hydrogen at high temperatures and release cold energy. B metal hydride and B1' metal hydride are temperature-dependent metal hydrogen storage materials; temperature-dependent metal hydrogen storage materials are defined as those that absorb high-pressure hydrogen at high temperatures and release high-temperature heat, and release low-pressure hydrogen at low temperatures and release low-temperature cold energy.

5. The system for producing liquid hydrogen and liquid oxygen using metal hydrogen storage materials as described in claim 4, characterized in that, The hydrogen absorption and desorption cycle unit also includes a pressure hydrogen replacement center (37); a pressure hydrogen replacement center (37) is set between each metal hydride in the AB metal hydride reaction bed module (80), and a pressure hydrogen replacement center (37) is set between the -2.8℃ metal hydride reaction area and the -50℃ metal hydride reaction area in the AB metal hydride reaction bed module (80). The pressure hydrogen replacement center (37) is equipped with multiple gas storage chambers as needed to store hydrogen at different pressures and temperatures. The two ends of each gas storage chamber in the pressure hydrogen replacement center (37) are connected to the hydrogen absorption and desorption pipelines of two adjacent metal hydride reaction beds. Each gas storage chamber in the pressure hydrogen replacement center (37) is equipped with a pressure stabilizing device.

6. A system for producing helium and neon, characterized in that, It includes a hydrogen removal furnace (47), a water separator (48), a gas storage tank (49), a first helium-neon compressor (50), a first air cooler (51), a dryer (52), a first helium-neon heat exchanger (53), a nitrogen removal separator (54), an activated alumina adsorber (55), a second helium-neon heat exchanger (56), a helium coil heat exchanger (57), a neon separator (58), a throttling expansion valve (59), and a distillation column (60) connected in sequence. The gas outlet at the top of the neon separator (58) is connected in sequence to the third tube (563) of the second helium-neon heat exchanger, the activated carbon adsorber (61), and the fourth tube (534) of the first helium-neon heat exchanger. The gas outlet at the top of the distillation column (60) is connected in sequence to the second tube side (562) of the second helium-neon heat exchanger, the second tube side (532) of the first helium-neon heat exchanger, the second helium-neon compressor (62), the second air cooler (63), the liquid nitrogen cooler (64), and the activated alumina adsorber (55). Both the nitrogen separator (54) and the liquid nitrogen cooler (64) are equipped with corresponding tubes, and liquid nitrogen is introduced into the tubes of the nitrogen separator (54) and the liquid nitrogen cooler (64) respectively. The nitrogen discharged from the tubes of the nitrogen separator (54) and the liquid nitrogen cooler (64) can be discharged externally or stored as a by-product.

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