Method and system for coupling compressed-air energy storage with thermochemical hydrogen production

Abstract

A method and system for coupling compressed-air energy storage with thermochemical hydrogen production. The system for coupling compressed-air energy storage with thermochemical hydrogen production comprises a compressed-air energy storage unit, a thermochemical conversion unit, and a compressed-air energy release unit. The thermochemical conversion unit comprises a methanol storage tank (5), a demineralized-water storage tank (6), a mixing tank (7), a liquid pump (8), a first regenerator (9), a gas-liquid separator (10), a flow splitter (11), a pressure swing adsorption device (12), a hydrogen storage and transportation device (13), a purge gas compressor (14) and a fuel-gas storage device (15).

Description

Compressed air energy storage method coupled with thermo-chemical hydrogen production and system thereof

[0001] The present application claims priority to the Chinese patent application No. 2024113032555, filed on September 18, 2024, and entitled "Compressed air energy storage method coupled with thermo-chemical hydrogen production and system thereof", the content of which is incorporated herein by reference in its entirety. TECHNICAL FIELD

[0002] The present application belongs to the technical field of compressed gas energy storage and thermo-chemical hydrogen production, and specifically relates to a compressed air energy storage method coupled with thermo-chemical hydrogen production and a system thereof. BACKGROUND

[0003] Large-scale deployment of renewable power requires urgent energy storage, and compressed air energy storage technology has the advantages of large scale, long service life, high energy storage density, and low emissions, and is a promising large-scale physical energy storage technology. Utilization of compression heat is one of the key factors affecting the performance of compressed air energy storage, and medium and low temperature thermo-chemical conversion has the technical advantage of upgrading and increasing the efficiency of low-grade heat energy to high-grade chemical energy. Coupling medium and low temperature thermo-chemistry is a new way to improve the operating efficiency of compressed air energy storage systems. There are related studies on compressed air energy storage coupled with methanol decomposition reaction, but the existing technology focuses on the role of thermo-chemical upgrading and increasing efficiency, and does not consider and improve the flexibility of compressed air energy storage. In addition, the introduction of methanol fuel for power generation will reduce the technical and economic efficiency of the system.

[0004] On the other hand, hydrogen energy plays a key role in energy structure transformation, and methanol is a good carrier of hydrogen energy. With the development of green methanol technology, methanol reforming for hydrogen production is gradually becoming a promising distributed hydrogen supply method. However, in existing methanol reforming for hydrogen production technology, there are problems of high carbon emissions due to large fossil fuel consumption and high cost of methanol hydrogen production, and it is urgent to find a clean and cheap heat source to replace the original fossil fuel consumption. SUMMARY

[0005] The present application provides a compressed air energy storage method coupled with thermo-chemical hydrogen production to solve the problem of large fossil fuel consumption in existing methanol reforming for hydrogen production technology.

[0006] The present application provides a compressed air energy storage system coupled with thermo-chemical hydrogen production to solve the problem of poor system energy storage and release adjustment capability and decreased technical and economic efficiency in existing compressed air energy storage technology coupled with thermo-chemical reaction.

[0007] The present application provides a compressed air energy storage system coupled with thermo-chemical hydrogen production, which includes a compressed air energy storage unit, a thermo-chemical conversion unit, and a compressed air energy release unit.

[0008] The compressed air energy storage unit comprises a motor set, an air compressor set, a high-pressure air storage device connected with the air compressor set through a thermochemical reactor, which are connected in sequence.

[0009] The thermochemical conversion unit comprises a methanol storage tank, a desalted water storage tank, a mixing tank communicated with the methanol storage tank and the desalted water storage tank respectively via pipelines, a liquid pump, a first heat exchanger and a thermochemical reactor connected with the mixing tank in sequence, and a gas-liquid separator connected with the first heat exchanger, a flow divider connected with a gas outlet of the gas-liquid separator, a fuel gas storage device communicated with the flow divider, a pressure swing adsorption device communicated with the flow divider, a purge gas compressor connected with a hydrogen outlet of the pressure swing adsorption device, and a hydrogen storage and transportation device communicated with a hydrogen outlet of the pressure swing adsorption device; wherein a liquid outlet of the gas-liquid separator is connected with the mixing tank, the purge gas compressor is communicated with the fuel gas storage device, and the fuel gas storage device is communicated with the combustion chamber.

[0010] The compressed air energy storage unit comprises a motor set, an air compressor set, a high-pressure air storage device connected with the air compressor set through a thermochemical reactor, which are connected in sequence.

[0011] The compressed air energy storage system coupled with thermochemical hydrogen production as described above, wherein the gas inlet of the thermochemical reactor is connected with the gas outlet of the air compressor set, and the gas outlet of the thermochemical reactor is connected with the gas inlet of the high-pressure air storage device.

[0012] The compressed air energy storage system coupled with thermochemical hydrogen production as described above, wherein the first inlet of the first heat exchanger is connected with the outlet of the mixing tank via the liquid pump, and the first outlet of the first heat exchanger is communicated with the feed inlet of the thermochemical reactor.

[0013] The compressed air energy storage system coupled with thermochemical hydrogen production as described above, wherein the second inlet of the first heat exchanger is communicated with the discharge outlet of the thermochemical reactor, and the second outlet of the first heat exchanger is connected with the gas-liquid separator.

[0014] The compressed air energy storage system coupled with thermochemical hydrogen production as described above, wherein the thermochemical reactor comprises a compact reactor, specifically a compressed air pipeline with parallel reaction column pipes, the column pipes being filled with catalysts required for reaction, and the reaction flow direction being opposite to the compressed air flow direction.

[0015] The compressed air energy storage system coupled with thermochemical hydrogen production as described above, wherein the fuel gas storage device is also provided with a fuel gas compressor for pressure compensation to ensure the inlet pressure of the fuel gas into the combustion chamber, and the purge gas compressor can be shared.

[0016] The application also provides a compressed air energy storage method coupled with thermochemical hydrogen production, based on the above-mentioned compressed air energy storage system coupled with thermochemical hydrogen production, and specifically as follows.

[0017] In the energy storage stage, the normal pressure air is compressed to a high pressure state, and the compression heat generated is used as a heat source for thermochemical hydrogen production. The selected thermochemical hydrogen production is a methanol reforming hydrogen production reaction. The obtained partial reforming gas is separated into hydrogen gas by pressure swing adsorption. The separated purge gas is compressed and stored together with the remaining reforming gas.

[0018] In the energy releasing stage, the high pressure air is released to generate electricity by an air turbine unit. The high pressure air after the release of the air turbine unit is burned with the above-mentioned stored purge gas and reforming gas, and then electricity is generated by a gas turbine unit. The power waste heat generated by electricity generation is recovered to preheat the high pressure air entering the air turbine unit.

[0019] The compressed air energy storage method coupled with thermochemical hydrogen production as described above, wherein specifically:

[0020] In the energy storage stage, the air enters an air compressor unit and is compressed, and the obtained high pressure air is stored in a high pressure air storage device. The compression heat generated by adiabatic compression is used to drive a methanol thermochemical reaction in a thermochemical reactor. The methanol and water are mixed in a mixing tank, preheated by heat exchange in a first regenerator by a liquid pump, and then enter the thermochemical reactor for a reforming hydrogen production reaction. The above-mentioned compression heat is used as a heat source. The reaction mixture gas is cooled by heat exchange in the first regenerator, separated into reforming gas and unreacted substances by a gas-liquid separator, and the unreacted substances are transported back to the mixing tank for reuse. The reforming gas is controlled by a flow divider to be divided into two streams, one of which is transported to a fuel gas storage device for the energy releasing stage, and the other is separated into hydrogen gas and purge gas by a pressure swing adsorption device. The hydrogen gas is transported to a hydrogen gas storage and transportation device, and the purge gas is further compressed by a purge gas compressor and then transported to the fuel gas storage device. The specific reforming gas splitting ratio is determined by the electricity demand in the energy releasing stage. The higher the electricity demand in the energy releasing stage, the higher the reforming gas storage ratio, and vice versa.

[0021] In the energy releasing stage, the high pressure air in the high pressure air storage device recovers the power waste heat from the outlet of the gas turbine unit in the second regenerator through a throttle valve. The preheated high pressure air enters the air turbine unit to release energy and generate electricity. Then, the high pressure air enters a combustion chamber and is mixed with the fuel gas in the fuel gas storage device at a certain ratio to burn. The high temperature gas generated by the burning enters the gas turbine unit to release energy and generate electricity.

[0022] The compressed air energy storage method coupled with thermochemical hydrogen production as described above, wherein the temperature of the compression heat generated by adiabatic compression is controlled to be 200-300℃. In this case, part or all of the low temperature compression heat that cannot be absorbed by the thermochemical reaction in the compressed air energy storage process can be used to preheat the normal pressure inlet air.

[0023] The compressed air energy storage method coupled with thermo-chemical hydrogen production as described above, further comprising adjusting the methanol concentration and liquid level of the methanol aqueous solution in the mixing tank by adjusting the opening degree of the methanol feed pump and the desalted water feed pump; and adjusting the effect of the thermo-chemical reaction by controlling the reaction outlet temperature, which is controlled by the opening degree of the liquid pump after the mixing tank.

[0024] The present application replaces fossil fuel with compressed air energy storage stage compression heat to drive methanol reforming to produce hydrogen, thereby reducing the cost and carbon emission of the methanol reforming process; and the present application controls the fuel gas consumption in the compressed air energy release process by adjusting the hydrogen output, thereby realizing wide-range matching of the compressed air energy storage system. BRIEF DESCRIPTION OF DRAWINGS

[0025] The accompanying drawings are included to provide a further understanding of the application, and are incorporated in and constitute a part of this specification, illustrate embodiments of the application, and together with the description serve to explain the principles of the application. In the drawings:

[0026] Fig. 1 is a schematic diagram of the compressed air energy storage system coupled with thermo-chemical hydrogen production of the present application;

[0027] Fig. 2 is a structural diagram of the thermo-chemical reactor of the present application.

[0028] BRIEF DESCRIPTION OF DRAWINGS 1 - motor set, 2 - air compressor set, 3 - high-pressure air storage device, 4 - thermo-chemical reactor, 5 - methanol storage tank, 6 - desalted water storage tank, 7 - mixing tank, 8 - liquid pump, 9 - first heat exchanger, 10 - gas-liquid separator, 11 - flow divider, 12 - pressure swing adsorption device, 13 - hydrogen storage and transportation device, 14 - purge gas compressor, 15 - fuel gas storage device, 16 - throttle valve, 17 - second heat exchanger, 18 - air turbine set, 19 - combustion chamber, 20 - gas turbine set, 21 - generator, 22 - uniform material device, 23 - reaction column, 24 - flow combining device, 25 - compressed air pipeline. DETAILED DESCRIPTION

[0029] To make the skilled in the art better understand the scheme of the present application, the present application is further described in detail as follows. The specific embodiments listed below are only to describe the principles and characteristics of the present application, and the examples are only to explain the present application, but not to limit the scope of the present application. Based on the embodiments of the present application, all other embodiments obtained by the skilled in the art without creative labor fall within the scope of the present application.

[0030] In the description of the present application, unless otherwise explicitly specified and limited, the terms "arrangement", "installation", "connection", "connected" should be understood broadly, for example, can be fixedly connected, can also be detachably connected, can also be integrally connected; can be mechanically connected, can also be electrically connected, can also be communicatively connected (network connection); can be directly connected, can also be indirectly connected through an intermediate medium, or can be internal communication of two elements. For those skilled in the art, the above belongs to the specific meaning in the present application can be understood according to the specific circumstances. In addition, the terms "first", "second" and the like are only for the purpose of description, for example, to distinguish components, so as to make the technical scheme clearer / interpretation, and cannot be understood as indicating or implying the number of indicated technical features or having substantial meaning of the order, etc.

[0031] In one aspect, the present application provides a compressed air energy storage system coupled with thermochemical hydrogen production, comprising a compressed air energy storage unit, a thermochemical conversion unit, a compressed air energy release unit;

[0032] The compressed air energy storage unit comprises a motor set 1, an air compressor set 2 connected in sequence, a high-pressure air storage device 3 connected with the air compressor set 2 through a thermochemical reactor 4;

[0033] The thermochemical conversion unit comprises a methanol storage tank 5, a desalted water storage tank 6, a mixing tank 7 in communication with the methanol storage tank 5 and the desalted water storage tank 6 respectively via pipes, a liquid pump 8, a first regenerator 9 and the thermochemical reactor 4 connected in sequence with the mixing tank 7, a gas-liquid separator 10 connected with the first regenerator 9, a flow divider 11 connected with the gas outlet of the gas-liquid separator 10, a fuel gas storage device 15 in communication with the flow divider 11, a pressure swing adsorption device 12 in communication with the flow divider 11, a purge gas compressor 14 connected with the purge gas outlet of the pressure swing adsorption device 12, and a hydrogen storage and transportation device 13 in communication with the hydrogen outlet of the pressure swing adsorption device 12; wherein the liquid outlet of the gas-liquid separator 10 is connected with the mixing tank 7, the purge gas compressor 14 is in communication with the fuel gas storage device 15, and the fuel gas storage device 15 is in communication with the combustion chamber 20;

[0034] The compressed air energy release unit comprises a throttle valve 16, a second regenerator 17, an air turbine set 18, a combustion chamber 19, a gas turbine set 20 and a generator 21 connected in sequence; wherein the second regenerator 17 is connected with the high-pressure air storage device 3 through the throttle valve 16, and the gas turbine set 20 is in communication with the second regenerator 17. As shown in Figure 1.

[0035] Specifically, the methanol storage tank 5 is connected with the mixing tank 7 through a methanol feed pump, and the desalted water storage tank 6 is connected with the mixing tank 7 through a desalted water feed pump.

[0036] Specifically, the air inlet of the thermo-chemical reactor 4 is connected to the air outlet of the air compressor set 2, and the air outlet of the thermo-chemical reactor 4 is connected to the air inlet of the high-pressure air storage device 3.

[0037] In order to directly drive the methanol reforming reaction by compression heat, the heat exchange loss in the prior art is avoided.

[0038] Specifically, the first inlet of the first regenerator 9 is connected to the outlet of the mixing tank 7 through the liquid pump 8, and the first outlet of the first regenerator 9 is connected to the feed inlet of the thermo-chemical reactor 4.

[0039] Specifically, the second inlet of the first regenerator 9 is connected to the discharge outlet of the thermo-chemical reactor 4, and the second outlet of the first regenerator 9 is connected to the gas-liquid separator 10.

[0040] Specifically, the thermo-chemical reactor 4 comprises a compact reactor, specifically a compressed air pipeline with parallel reaction column pipes, the column pipes are filled with catalysts required for the reaction, and the flow direction of the reaction is opposite to the flow direction of the compressed air.

[0041] The use of the compact reactor can effectively avoid the heat exchange loss caused by the use of heat-conducting oil heat exchange in the prior art methanol reforming technology, and reduce the complexity of the device.

[0042] Specifically, the thermo-chemical reactor 4 mainly comprises a compressed air pipeline 25 and a reaction column pipe 23, and the specific process is that the methanol water vapor enters the uniformizing device 22 from the outlet of the first regenerator 9 through the pipeline, is divided into the reaction column pipe 23 through the uniformizing device 22, and flows out of the thermo-chemical reactor 4 after the reaction is completed through the converging device 24, and the flow direction of the reaction is opposite to the flow direction of the compressed air.

[0043] The structural diagram of the thermo-chemical reactor 4 is shown in FIG. 2.

[0044] Specifically, the fuel gas storage device 15 is also provided with a fuel gas compressor for pressure compensation to ensure the inlet pressure of the fuel gas entering the combustion chamber, and the fuel gas compressor can be shared with the exhaust gas compressor.

[0045] The hydrogen-rich exhaust gas or discharge in the prior art methanol reforming hydrogen production technology, or the combustion heat supply driving 200-300℃ methanol reforming reaction, has a large irreversible loss, and can better utilize its value when used for combustion power generation.

[0046] On the other hand, the application also provides a compressed air energy storage method coupled with thermo-chemical hydrogen production, based on the above-mentioned compressed air energy storage system coupled with thermo-chemical hydrogen production, and the specific process is as follows:

[0047] In the energy storage stage, the normal pressure air is compressed to high pressure state, and the compression heat generated is used as the heat source of the thermo-chemical hydrogen production. The thermo-chemical hydrogen production selected is the methanol reforming hydrogen production reaction. The partial reforming gas obtained is separated into hydrogen by the pressure swing adsorption, and the separated purge gas is compressed and stored together with the remaining reforming gas.

[0048] In the energy release stage, the high pressure air is released to generate electricity by the air turbine set 18. The high pressure air after the release of the air turbine set 18 is combusted with the stored purge gas and reforming gas, and then the high temperature gas is released to generate electricity by the gas turbine set 20. The power waste heat generated by the electricity generation is recovered to preheat the high pressure air entering the air turbine set 18.

[0049] Specifically, in the energy storage stage, the air enters the air compressor set 2 to be compressed, and the high pressure air obtained is stored in the high pressure air storage device 3. The compression heat generated by the adiabatic compression is used to drive the methanol thermo-chemical reaction in the thermo-chemical reactor 4. The methanol and water are mixed in the mixing tank 7, preheated by heat exchange in the first regenerator 9 by the liquid pump 8, and then enter the thermo-chemical reactor 4 to perform the reforming hydrogen production reaction. The above compression heat is used as the heat source. The mixed gas stream is cooled by heat exchange in the first regenerator 9, and the reforming gas and unreacted substances are separated by the gas-liquid separator 10. The unreacted substances are transported back to the mixing tank 7 for reuse, and the reforming gas is controlled by the flow divider 11 to be divided into two streams. One stream is transported to the fuel gas storage device 15 for the energy release stage, and the other stream is separated into hydrogen and purge gas by the pressure swing adsorption device 12. The hydrogen is transported to the hydrogen storage and transportation device 13, and the purge gas is further compressed by the purge gas compressor 14 and then transported to the fuel gas storage device 15. The specific proportion of the reforming gas is determined by the electricity demand in the energy release stage. The higher the electricity demand in the energy release stage, the higher the proportion of the reforming gas storage, and vice versa.

[0050] In the energy release stage, the high pressure air of the high pressure air storage device 3 recovers the power waste heat from the outlet of the gas turbine set 20 in the second regenerator 17 through the throttle valve 16. The preheated high pressure air enters the air turbine set 18 to release energy to generate electricity, and then enters the combustion chamber 19 to be mixed with the fuel gas of the fuel gas storage device at a certain proportion to be combusted. The high temperature gas generated by the combustion enters the gas turbine set 20 to release energy to generate electricity.

[0051] Specifically, the compression heat generated by the adiabatic compression is controlled to have a temperature of 200-300℃. The part or all of the low temperature compression heat that cannot be absorbed by the thermo-chemical reaction in the compression air energy storage process can be used to preheat the normal pressure inlet air.

[0052] The quality of the compression heat is ensured and the utilization rate of the compression heat is improved. The compression heat temperature is set to 200-300℃, which can well match the methanol reforming reaction requirement, and both the reaction effect of the methanol reforming and the problem of energy efficiency decline caused by higher temperature in the compression process are avoided.

[0053] Specifically, the method further comprises adjusting the methanol concentration and liquid level of the methanol aqueous solution in the mixing tank 7, and the adjusting means is adjusting the opening degree of the methanol feed pump and the desalted water feed pump; the effect of the thermochemical reaction is controlled by the reaction outlet temperature, and the reaction outlet temperature is controlled by the opening degree of the liquid pump 8 after the mixing tank 7.

[0054] The compressed air energy storage technology and green methanol have market prospects. The application first proposes the design idea of integrating the compressed air energy storage technology and the methanol reforming hydrogen production technology, that is, using the compression heat of the compressed air energy storage stage for methanol reforming hydrogen production, and using the purge gas produced in the hydrogen production for complementary compressed air energy release, to construct a near-zero-emission efficient hydrogen and electricity cogeneration system. For the methanol reforming hydrogen production process, the fossil fuel consumption is reduced, the process carbon reduction and cost reduction are realized, the high-quality purge gas produced in the hydrogen production process is not used for medium and low temperature heat supply, and irreversible loss is avoided. For the compressed air energy storage process, the original heat storage is replaced by fuel combustion such as purge gas, which can improve the initial temperature of the compressed air energy release, reduce the heat exchange loss in the prior art, and improve the operation efficiency of the existing compressed air energy storage. Coupling the two technologies can improve the energy utilization efficiency of the system, thereby improving the technical and economic efficiency.

[0055] The system adjusts the hydrogen output of the methanol reforming hydrogen production process to control the power generation of the compressed air energy storage system, thereby improving the operation flexibility of the compressed air energy storage system.

Claims

1. A compressed air energy storage system coupled with thermochemical hydrogen generation, wherein, The compressed air energy storage unit, the thermochemical conversion unit, and the compressed air energy release unit; The compressed air energy storage unit comprises a motor set (1), an air compressor set (2), and a high-pressure air storage device (3) connected with the air compressor set (2) through a thermochemical reactor (4) in sequence. The thermochemical conversion unit comprises a methanol storage tank (5), a desalted water storage tank (6), a mixing tank (7) communicated with the methanol storage tank (5) and the desalted water storage tank (6) respectively via pipelines, a liquid pump (8), a first heat exchanger (9), and the thermochemical reactor (4) connected with the mixing tank (7) in sequence, and further comprises a gas-liquid separator (10) connected with the first heat exchanger (9), a flow divider (11) connected with a gas outlet of the gas-liquid separator (10), a fuel gas storage device (15) communicated with the flow divider (11), a pressure swing adsorption device (12) communicated with the flow divider (11), a purge gas compressor (14) connected with a purge gas outlet of the pressure swing adsorption device (12), and a hydrogen storage and transportation device (13) communicated with a hydrogen outlet of the pressure swing adsorption device (12); the liquid outlet of the gas-liquid separator (10) is connected with the mixing tank (7), the purge gas compressor (14) is communicated with the fuel gas storage device (15), and the fuel gas storage device (15) is communicated with a combustion chamber (20). The compressed air energy release unit comprises a throttle valve (16), a second heat exchanger (17), an air turbine set (18), the combustion chamber (19), a gas turbine set (20), and a generator (21) connected in sequence; the second heat exchanger (17) is connected with the high-pressure air storage device (3) through the throttle valve (16), and the gas turbine set (20) is communicated with the second heat exchanger (17).

2. The coupled thermochemical hydrogen generation compressed air energy storage system of claim 1, wherein, The gas inlet of the thermochemical reactor (4) is connected with the gas outlet of the air compressor set (2), and the gas outlet of the thermochemical reactor (4) is connected with the gas inlet of the high-pressure air storage device (3).

3. The coupled thermochemical hydrogen generation compressed air energy storage system of claim 1, wherein, The first inlet of the first heat exchanger (9) is connected with the outlet of the mixing tank (7) through the liquid pump (8), and the first outlet of the first heat exchanger (9) is communicated with the feed inlet of the thermochemical reactor (4).

4. The coupled thermochemical hydrogen generation compressed air energy storage system of claim 1, wherein, The second inlet of the first heat exchanger (9) is communicated with the discharge outlet of the thermochemical reactor (4), and the second outlet of the first heat exchanger (9) is connected with the gas-liquid separator (10).

5. The coupled thermochemical hydrogen generation compressed air energy storage system of claim 1, wherein, The thermochemical reactor (4) comprises a compact reactor, specifically a compressed air pipeline with parallel reaction column tubes, the column tubes are filled with catalysts required for reaction, and the reaction flow direction is opposite to the compressed air flow direction.

6. The coupled thermochemical hydrogen generation compressed air energy storage system of claim 5, wherein, The fuel gas storage device (15) is further provided with a fuel gas compressor for pressure compensation, so as to ensure the inlet pressure of fuel gas into the combustion chamber, and the purge gas compressor can be shared.

7. A compressed air energy storage method coupled with thermochemical hydrogen generation, wherein, The compressed air energy storage system coupled with thermochemical hydrogen production according to any one of the above, specifically as follows: In the energy storage stage, normal-pressure air is compressed to a high-pressure state, and the generated compression heat is used as a heat source for thermochemical hydrogen production; the selected thermochemical hydrogen production is a methanol reforming hydrogen production reaction; a part of the obtained reforming gas is separated into hydrogen by pressure swing adsorption; the separated purge gas is compressed and stored together with the remaining reforming gas; In the energy release stage, the high pressure air is released to generate electricity by air turbine unit (18), the high pressure air after energy release of air turbine unit (18) is combusted with the above-mentioned stored exhaust gas and reforming gas, and then electricity is generated by gas turbine unit (20), and the power waste heat generated by electricity generation is recovered to preheat the high pressure air entering the air turbine unit (18).

8. The coupled thermochemical hydrogen generation compressed air energy storage method of claim 7, wherein, Specifically: In the energy storage stage, air enters the air compressor unit (2) to be compressed, and the obtained high pressure air is stored in the high pressure air storage device (3), the compression heat generated by adiabatic compression is used to drive the methanol thermochemical reaction in the thermochemical reactor (4); methanol and water are mixed in the mixing tank (7), preheated by heat exchange in the first regenerator (9) through the liquid pump (8), and then enter the thermochemical reactor (4) to carry out the reforming reaction to produce hydrogen, the above-mentioned compression heat is used as a heat source, the mixed gas stream after the reaction is cooled by heat exchange in the first regenerator (9), and the reforming gas and unreacted substances are separated by the gas-liquid separator (10), the unreacted substances are transported back to the mixing tank (7) for reuse, and the reforming gas is controlled to be divided into two streams by the flow divider (11), one of which is transported to the fuel gas storage device (15) for use in the energy release stage, and the other is separated into hydrogen and exhaust gas by the pressure swing adsorption device (12), the hydrogen is transported to the hydrogen storage and transportation device (13), and the exhaust gas is further compressed by the exhaust gas compressor (14) and then transported to the fuel gas storage device (15), the specific reforming gas splitting ratio is determined by the power demand in the energy release stage, when the power demand in the energy release stage is higher, the reforming gas storage ratio is higher, and vice versa; In the energy release stage, the high pressure air of the high pressure air storage device (3) recovers the power waste heat from the outlet of the gas turbine unit (20) in the second regenerator (17) through the throttle valve (16), the preheated high pressure air enters the air turbine unit (18) to release energy to generate electricity, and then enters the combustion chamber (19) to be mixed with the fuel gas of the fuel gas storage device at a certain ratio to burn, and the high temperature gas generated by the burning enters the gas turbine unit (20) to release energy to generate electricity.

9. The coupled thermochemical hydrogen generation compressed air energy storage method of claim 8, wherein, The temperature of the compression heat generated by adiabatic compression is controlled to be 200-300℃; part or all of the low-temperature compression heat that cannot be absorbed by the thermochemical reaction in the energy storage process of compressed air can be used to preheat the normal pressure inlet air.

10. The coupled thermochemical hydrogen generation compressed air energy storage method of claim 8, wherein, The method further comprises adjusting the methanol concentration and liquid level of the methanol aqueous solution in the mixing tank (7), and the adjusting means is to adjust the opening degree of the methanol feed pump and the desalted water feed pump; the thermochemical reaction effect is adjusted and controlled by the outlet temperature of the reaction, and the outlet temperature of the reaction is controlled by the opening degree of the liquid pump (8) after the mixing tank (7). The temperature of the compression heat generated by adiabatic compression is controlled to be 200-300℃; part or all of the low-temperature compression heat that cannot be absorbed by the thermochemical reaction in the energy storage process of compressed air can be used to preheat the normal pressure inlet air. The method further comprises adjusting the methanol concentration and liquid level of the methanol aqueous solution in the mixing tank (7), and the adjusting means is to adjust the opening degree of the methanol feed pump and the desalted water feed pump; the thermochemical reaction effect is adjusted and controlled by the outlet temperature of the reaction, and the outlet temperature of the reaction is controlled by the opening degree of the liquid pump (8) after the mixing tank (7).

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