Integrated system and method for co-production of ammonium bicarbonate and methanol from air energy storage

Abstract

The present application relates to an integrated system and method for co-production of ammonium bicarbonate and methanol by air energy storage. The integrated system couples an air energy storage subsystem, an ammonia synthesis subsystem, a methanol synthesis subsystem and an ammonium bicarbonate synthesis subsystem. During the process of energy storage and power generation by the air energy storage subsystem, the co-production of ammonia, methanol and ammonium bicarbonate is realized, which helps to achieve large-scale energy storage, consumption and recycling of various by-products of each subsystem, and multi-directional assistance in achieving the dual-carbon goal. The ammonia synthesis subsystem and the methanol synthesis subsystem are connected to the air energy storage subsystem through at least one set of combined heat recovery loop, so that the reaction heat of each subsystem is recovered and utilized for heating compressed air, increasing the inlet temperature of the expansion work of the air energy storage subsystem, and thus improving the power generation efficiency of the air energy storage system.

Description

Technical Field

[0001] This invention relates to the field of energy storage technology, and in particular to an integrated system and method for co-producing ammonium bicarbonate and methanol from air energy storage. Background Technology

[0002] The intermittent, fluctuating, and unstable nature of renewable energy generation such as wind and solar power makes large-scale, long-duration energy storage technology a key technology for the future development of power systems. Air energy storage technology, represented by compressed air and liquid air energy storage, has outstanding advantages such as being clean, low-carbon, safe, and having a long lifespan, making it one of the most promising and competitive long-duration energy storage technologies.

[0003] Compared to a single air energy storage system, an integrated system of air energy storage and other products is more conducive to improving system efficiency, increasing the scale / duration of energy storage, and effectively utilizing cold energy and clean air resources. However, the integrated systems of air energy storage and other products involved in the existing technology have the following problems: (1) It is difficult to achieve large-scale storage and large-scale consumption of the co-produced products. For example, the coupling system of air energy storage and hydrogen co-production faces the problem of large-scale storage and consumption of hydrogen energy. Another coupling scheme of air energy storage and methane co-production points out that air, captured carbon dioxide and co-produced methane should be stored underground. Large-scale storage requires special geographical environment; (2) The existing technology cannot achieve reasonable and efficient comprehensive utilization of reaction heat. The power generation efficiency of air energy storage system still needs to be further improved.

[0004] In summary, existing integrated systems and methods for cogeneration of other products using air energy storage still suffer from problems such as the difficulty of long-term storage of cogeneration products and the low efficiency of air energy storage systems. Summary of the Invention

[0005] This invention provides an integrated system and method for co-producing ammonium bicarbonate and methanol using air energy storage, which solves the problems of long-term storage difficulty of co-produced products and low efficiency of air energy storage systems in the prior art.

[0006] This invention provides an integrated system for co-producing ammonium bicarbonate and methanol using air energy storage, comprising: an air energy storage subsystem adapted to be connected to a power grid, wherein the air energy storage subsystem generates compressed air during the energy storage phase and transmits power to the power grid by expanding the compressed air during the energy release phase; an ammonia synthesis subsystem connected to the air energy storage subsystem, wherein the ammonia synthesis subsystem can produce ammonia by reacting hydrogen and nitrogen generated from compressed air; a methanol synthesis subsystem connected to the ammonia synthesis subsystem, wherein the methanol synthesis subsystem can synthesize methanol by reacting carbon dioxide with hydrogen and can separate and extract water from methanol; and an ammonium bicarbonate synthesis subsystem connected to both the ammonia synthesis subsystem and the methanol synthesis subsystem, wherein the ammonium bicarbonate synthesis subsystem can produce ammonium bicarbonate by reacting water, carbon dioxide, and ammonia; wherein the ammonia synthesis subsystem and the methanol synthesis subsystem are respectively connected to the air energy storage subsystem through at least one set of synthesis heat recovery loops.

[0007] According to the present invention, an integrated system for co-producing ammonium bicarbonate and methanol using air energy storage includes an air storage subsystem comprising an air compressor, a compressor-stage aftercooler, a compressed air storage tank, a first heat exchanger, and an expander. The air compressor, the compressor-stage aftercooler, the compressed air storage tank, the heat absorption side of the first heat exchanger, and the expander are connected sequentially. The air compressor is connected to an air source, and the expander is connected to the power grid via a generator. The compressed air storage tank is connected to the ammonia synthesis subsystem via a nitrogen production subsystem. The compressor-stage aftercooler is connected to the heat release side of the first heat exchanger via at least one set of synthesis heat recovery loops.

[0008] According to the present invention, an integrated system for co-producing ammonium bicarbonate and methanol using air energy storage is provided. The ammonia synthesis subsystem includes an ammonia synthesis tower, a second heat exchanger, an ammonia compressor, an ammonia cooler, and an ammonia storage tank, which are sequentially connected. A nitrogen preparation subsystem is connected to a hydrogen preparation subsystem, and both the nitrogen preparation subsystem and the hydrogen preparation subsystem are connected to the ammonia synthesis tower. The ammonia storage tank is connected to the ammonium bicarbonate synthesis subsystem. The second heat exchanger is connected to the heat release side of the first heat exchanger through at least one set of synthesis heat recovery loops.

[0009] According to the present invention, an integrated system for co-producing ammonium bicarbonate and methanol from air energy storage is provided. The hydrogen production subsystem includes an electrolyzer and a hydrogen storage tank. The input end of the electrolyzer is connected to a water source, the output end of the electrolyzer is connected to the hydrogen storage tank, and the hydrogen storage tank is connected to the ammonia synthesis tower.

[0010] According to the present invention, an integrated system for co-producing ammonium bicarbonate and methanol using air storage is provided. The nitrogen production subsystem includes an air separation device, a nitrogen storage tank, and a buffer tank. The compressed air storage tank is connected to the nitrogen storage tank via the air separation device, which is used to separate nitrogen from a portion of the compressed air in the compressed air storage tank. The input end of the buffer tank is connected to the nitrogen storage tank and the hydrogen production subsystem, and the output end of the buffer tank is connected to the ammonia synthesis tower. The buffer tank is used to mix and preheat hydrogen and nitrogen.

[0011] According to the present invention, an integrated system for co-producing ammonium bicarbonate and methanol from air energy storage is provided. The ammonia synthesis subsystem further includes an ammonia separator, and the ammonia cooler is connected to the ammonia storage tank through the ammonia separator. The separation output end of the ammonia separator is connected to the nitrogen preparation subsystem and the methanol synthesis subsystem. The ammonia separator is used to separate and extract unreacted hydrogen from ammonia.

[0012] According to the present invention, an integrated system for co-producing ammonium bicarbonate and methanol using air energy storage is provided. The methanol synthesis subsystem includes a methanol synthesis reactor, a third heat exchanger, a methanol separator, a methanol distillation column, and a methanol storage tank, which are sequentially connected. The methanol synthesis reactor is connected to a carbon dioxide capture subsystem. The separation output of the methanol separator is connected to the methanol synthesis reactor and the hydrogen production subsystem, and the methanol separator is used to separate and extract unreacted hydrogen from methanol. The distillation output of the methanol distillation column is connected to both the hydrogen production subsystem and the ammonium bicarbonate synthesis subsystem, and the methanol distillation column is used to distill water from methanol. The third heat exchanger is connected to the heat release side of the first heat exchanger through at least one set of synthesis heat recovery loops.

[0013] According to the present invention, an integrated system for co-producing ammonium bicarbonate and methanol using air energy storage is provided. The ammonium bicarbonate synthesis subsystem includes an ammonium bicarbonate reactor, a crystallizer, a three-in-one filtration device, and an ammonium bicarbonate storage tank, which are sequentially connected. The input end of the ammonium bicarbonate reactor is connected to the methanol distillation column, the carbon dioxide capture subsystem, and the ammonia storage tank, respectively.

[0014] According to the present invention, an integrated system for co-producing ammonium bicarbonate and methanol using air energy storage is provided. The synthesis heat recovery loop includes a high-temperature heat storage medium tank and a low-temperature heat storage medium tank. The output end of the high-temperature heat storage medium tank is connected to the input end of the low-temperature heat storage medium tank through the heat release side of the first heat exchanger. The output end of the low-temperature heat storage medium tank is connected to the input end of the high-temperature heat storage medium tank through the heat absorption side of each subsystem heat exchanger. Each subsystem heat exchanger includes at least one of the compressor-stage aftercooler, the second heat exchanger of the ammonia synthesis subsystem, and the third heat exchanger of the methanol synthesis subsystem.

[0015] This invention provides an integrated method for co-producing ammonium bicarbonate and methanol using air energy storage, which is executed using the aforementioned integrated system for co-producing ammonium bicarbonate and methanol using air energy storage. The integrated method for co-producing ammonium bicarbonate and methanol using air energy storage includes an air energy storage power transmission step, an ammonia synthesis step, a methanol synthesis step, an ammonium bicarbonate synthesis step, and a synthesis heat recovery step.

[0016] The air energy storage and power transmission process includes an energy storage stage and an energy release stage. The energy storage stage uses an air energy storage subsystem to generate compressed air, and the energy release stage heats the compressed air and expands it to generate electricity.

[0017] In the ammonia synthesis step, nitrogen is prepared using compressed air generated in the air energy storage and power transmission step, and ammonia is synthesized by reacting nitrogen and hydrogen using the ammonia synthesis subsystem.

[0018] The methanol synthesis step involves using the methanol synthesis subsystem to react carbon dioxide and hydrogen to synthesize methanol, and then separating and extracting water from the methanol.

[0019] The ammonium bicarbonate synthesis step involves reacting carbon dioxide, water extracted from the methanol synthesis step, and ammonia prepared from the ammonia synthesis step using a subsystem for synthesizing ammonium bicarbonate.

[0020] The synthesis heat recovery step recovers the heat generated in the energy storage stage of the air energy storage and power transmission step, the ammonia synthesis step, and the methanol synthesis step, and introduces the recovered heat into the energy release stage of the air energy storage and power transmission step to heat the compressed air.

[0021] This invention provides an integrated system for co-producing ammonium bicarbonate and methanol using air energy storage, comprising an air energy storage subsystem, an ammonia synthesis subsystem, a methanol synthesis subsystem, and an ammonium bicarbonate synthesis subsystem. The air energy storage subsystem is suitable for connection to the power grid, generating compressed air during the energy storage phase and using the expansion of the compressed air to transmit power to the grid during the energy release phase. The ammonia synthesis subsystem is connected to the air energy storage subsystem, and can produce ammonia by reacting hydrogen and nitrogen generated from compressed air. The methanol synthesis subsystem is connected to the ammonia synthesis subsystem, and can synthesize methanol by reacting carbon dioxide with hydrogen, and can separate and extract water from the methanol. The ammonium bicarbonate synthesis subsystem is connected to both the ammonia synthesis subsystem and the methanol synthesis subsystem, and can produce ammonium bicarbonate by reacting water, carbon dioxide, and ammonia. This integrated system couples together an air energy storage subsystem, ammonia synthesis subsystem, methanol synthesis subsystem, and ammonium bicarbonate synthesis subsystem. During the process of storing energy and generating electricity using the air energy storage subsystem, it achieves the co-production of ammonia, methanol, and ammonium bicarbonate. It also helps to realize the large-scale energy storage and consumption of each subsystem, as well as the recycling of various by-products, thus contributing to the achievement of dual-carbon goals in multiple ways.

[0022] Furthermore, in this integrated air-to-energy storage system for the co-production of ammonium bicarbonate and methanol, the ammonia synthesis subsystem and the methanol synthesis subsystem are each connected to the air-to-energy storage subsystem via at least one set of synthesis heat recovery loops. This configuration allows the reaction heat of the aforementioned subsystems to be recovered and utilized in the heating process of the compressed air by the air-to-energy storage subsystem; that is, by recovering the heat energy from the high-temperature gas exiting the ammonia synthesis reaction and the high-temperature gas exiting the methanol synthesis reaction, the air-to-energy storage subsystem is supplemented with heat during the energy release phase, which helps to increase the inlet temperature of the air-to-energy storage subsystem for expansion work, thereby improving the power generation efficiency of the air-to-energy storage system.

[0023] Moreover, in this integrated system of air energy storage co-producing ammonium bicarbonate and methanol, the co-products of the air energy storage subsystem are ammonium bicarbonate and methanol. Ammonium bicarbonate is a solid product at room temperature and pressure, while methanol is a liquid product at room temperature and pressure. Compared with existing air energy storage co-producing other gaseous products, the non-gaseous co-products are easier to store and transport, making the key links of the entire industrial chain in which this integrated system is located have advantages such as high efficiency, energy saving and environmental protection.

[0024] This invention also provides an integrated method for co-producing ammonium bicarbonate and methanol using air energy storage, which is executed using the aforementioned integrated system. The method includes air energy storage power transmission steps, ammonia synthesis steps, methanol synthesis steps, ammonium bicarbonate synthesis steps, and synthesis heat recovery steps, all corresponding to the integrated system. By setting each step corresponding to the aforementioned integrated system and associating these steps, this integrated method possesses all the advantages of the aforementioned integrated system, the details of which will not be elaborated here. Attached Figure Description

[0025] To more clearly illustrate the technical solutions in this invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0026] Figure 1 This is a schematic diagram of the integrated system for co-producing ammonium bicarbonate and methanol using air energy storage provided by the present invention.

[0027] Figure label:

[0028] 1. Air compressor; 2. Compressor-stage aftercooler; 3. Compressed air storage tank; 4. First heat exchanger; 5. Expander; 6. First high-temperature heat storage medium storage tank; 7. First low-temperature heat storage medium storage tank; 8. Air separator; 9. Nitrogen storage tank; 10. Electrolyzer; 11. Hydrogen storage tank; 12. Oxygen storage tank; 13. Buffer tank; 14. Ammonia synthesis tower; 15. Second heat exchanger; 16. Ammonia compressor; 17. Ammonia cooler; 18. Ammonia separator; 19. Ammonia storage tank; 2 0. Carbon dioxide capture device; 21. Carbon dioxide storage tank; 22. Ammonium bicarbonate reactor; 23. Crystallizer; 24. Three-in-one filter device; 25. Ammonium bicarbonate storage tank; 26. Methanol synthesis reactor; 27. Third heat exchanger; 28. Methanol separator; 29. ​​Methanol distillation column; 30. Methanol storage tank; 31. Second low-temperature heat storage medium storage tank; 32. Second high-temperature heat storage medium storage tank; 33. Third low-temperature heat storage medium storage tank; 34. Third high-temperature heat storage medium storage tank. Detailed Implementation

[0029] To make the objectives, technical solutions, and advantages of this invention clearer, the technical solutions of this invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of this invention. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without creative effort are within the scope of protection of this invention.

[0030] The following is combined Figure 1 This invention describes an integrated system and method for co-producing ammonium bicarbonate and methanol using air energy storage. The integrated system for co-producing ammonium bicarbonate and methanol using air energy storage described in this invention can be simply referred to as the "integrated system" or "system". The integrated method for co-producing ammonium bicarbonate and methanol using air energy storage described in this invention can be simply referred to as the "integrated method" or "method".

[0031] Figure 1This is a schematic diagram of the integrated system provided by the present invention. (See diagram below.) Figure 1 As shown, the integrated system described in this embodiment of the invention includes an air energy storage subsystem and multiple co-production subsystems of the air energy storage subsystem. Specifically, the multiple co-production subsystems of the air energy storage subsystem include an ammonia synthesis subsystem, a methanol synthesis subsystem, and an ammonium bicarbonate synthesis subsystem.

[0032] The air energy storage subsystem is suitable for grid connection. It consists of an energy storage phase and an energy release phase. During the energy storage phase, the subsystem generates compressed air; during the energy release phase, it utilizes the expansion of this compressed air to perform work and transmit electricity to the grid. The ammonia synthesis subsystem is connected to the air energy storage subsystem. This subsystem produces ammonia through a reaction between hydrogen and nitrogen generated from compressed air. The methanol synthesis subsystem is connected to the ammonia synthesis subsystem. This subsystem synthesizes methanol by reacting carbon dioxide with hydrogen and can separate and extract water from the methanol. The ammonium bicarbonate synthesis subsystem is connected to both the ammonia synthesis and methanol synthesis subsystems. This subsystem produces ammonium bicarbonate through a reaction between water, carbon dioxide, and ammonia. This integrated system couples together an air energy storage subsystem, ammonia synthesis subsystem, methanol synthesis subsystem, and ammonium bicarbonate synthesis subsystem. During the process of storing energy and generating electricity using the air energy storage subsystem, it achieves the co-production of ammonia, methanol, and ammonium bicarbonate. It also helps to realize the large-scale energy storage and consumption of each subsystem, as well as the recycling of various by-products, thus contributing to the achievement of dual-carbon goals in multiple ways.

[0033] It should be noted that the hydrogen mentioned in the embodiments of the present invention can be hydrogen introduced from an external hydrogen source, or hydrogen separated and recovered during the ammonia synthesis and post-processing reaction in the ammonia synthesis subsystem for reuse, or hydrogen separated and extracted from co-products after synthesis through relevant reactions in other co-production subsystems for recycling.

[0034] It should be noted that the carbon dioxide described in this embodiment of the invention can be captured and stored from a carbon dioxide source outside the system through the carbon dioxide capture device 20 of the carbon dioxide capture subsystem. The carbon dioxide source is preferably a carbon dioxide-rich exhaust gas, such as chemical plant tail gas or biomass combustion tail gas.

[0035] It should be noted that the water participating in the reaction in the embodiments of the present invention can be obtained from an external water source or it can be a byproduct of related subsystems produced in the system. For example, the water generated during the distillation of the methanol produced in the methanol synthesis subsystem after the synthesis reaction can be recycled and reused. It can be introduced into the hydrogen preparation subsystem to produce hydrogen, or it can be directly introduced into the ammonium bicarbonate synthesis subsystem to participate in the synthesis reaction to produce ammonium bicarbonate.

[0036] As can be seen, the above setup, through the interconnected coupling of various subsystems, enables the reliable recovery, recycling, and rational disposal of byproducts and energy generated during the relevant reactions and operations of these subsystems, thereby avoiding energy waste and contributing to the achievement of dual-carbon goals in multiple ways.

[0037] It should be noted that in this integrated system, the co-products produced by the co-production subsystems of the air energy storage subsystem are in liquid or solid state at room temperature and pressure. For example, the methanol synthesis subsystem ultimately produces methanol, which is liquid at room temperature and pressure; similarly, the ammonium bicarbonate synthesis subsystem ultimately produces ammonium bicarbonate, which is solid at room temperature and pressure. Therefore, compared to previously proposed schemes that co-produce other products (hydrogen, methane, etc., which are gaseous at room temperature and pressure) from air energy storage, this invention provides co-products that are liquid / solid at room temperature and pressure, making them easier to store and transport, and thus having greater potential for widespread application.

[0038] Furthermore, in this integrated system, the ammonia synthesis subsystem and the methanol synthesis subsystem are each connected to the air energy storage subsystem via at least one set of synthesis heat recovery loops. This configuration allows the reaction heat of the aforementioned subsystems to be recovered and utilized in the heating process of the compressed air by the air energy storage subsystem; that is, by recovering the heat energy of the high-temperature gas exiting the ammonia synthesis reaction and the methanol synthesis reaction, the air energy storage subsystem is supplemented with heat during the energy release phase, which helps to increase the inlet temperature of the air energy storage subsystem for expansion work, thereby improving the power generation efficiency of the air energy storage system. The recovery and utilization of reaction heat improves system efficiency, giving this integrated system advantages such as high efficiency, energy saving, and environmental friendliness.

[0039] In some embodiments, such as Figure 1 As shown, the air energy storage subsystem includes an air compressor 1, a compressor-stage aftercooler 2, a compressed air tank 3, a first heat exchanger 4, and an expander 5. The air compressor 1, compressor-stage aftercooler 2, compressed air tank 3, the heat absorption side of the first heat exchanger 4, and expander 5 are connected in sequence. The air compressor 1 is connected to an air source, and the expander 5 is connected to the power grid through a generator. Thus, the air energy storage subsystem connects the air source and the power grid, enabling the system to store energy using compressed air and generate electricity.

[0040] In some specific embodiments, the compressed air storage tank 3 is connected to the ammonia synthesis subsystem via a nitrogen preparation subsystem. The nitrogen preparation subsystem can extract a portion of the compressed air stored in the compressed air storage tank 3 and prepare nitrogen using air separation technology. This nitrogen can then be reliably stored and introduced into the ammonia synthesis subsystem to participate in the reaction, thereby achieving co-production and coupling between the air energy storage subsystem and the ammonia synthesis subsystem. In other words, the nitrogen produced from the compressed air, an intermediate product of the air energy storage subsystem, can serve as a raw material for the ammonia synthesis reaction, achieving coupling and reliable co-production between the subsystems.

[0041] In some specific embodiments, the compressor-stage aftercooler 2 is connected to the heat release side of the first heat exchanger 4 through at least one set of synthetic heat recovery loops. That is, the air energy storage subsystem recovers and utilizes the outlet airflow temperature of the air compressor 1 in the energy storage stage through the compressor-stage aftercooler 2 to heat the inlet airflow at the input end of the expander 5 in the energy release stage. This achieves energy supplementation and heat recovery within the same subsystem, helping to increase the inlet temperature for expansion work in the air energy storage subsystem, thereby significantly improving the power generation efficiency of the air energy storage system. The specific structure and working principle of the synthetic heat recovery loops in the air energy storage subsystem will be described in detail later and will not be repeated here.

[0042] In some embodiments, such as Figure 1 As shown, the ammonia synthesis subsystem includes an ammonia synthesis tower 14, a second heat exchanger 15, an ammonia compressor 16, an ammonia cooler 17, and an ammonia storage tank 19. The ammonia synthesis tower 14, the second heat exchanger 15, the ammonia compressor 16, the ammonia cooler 17, and the ammonia storage tank 19 are connected sequentially to form a reaction flow for ammonia production. A nitrogen production subsystem is connected to a hydrogen production subsystem. Both the nitrogen and hydrogen production subsystems are connected to the ammonia synthesis tower 14. This allows the nitrogen production subsystem to introduce compressed air from the air energy storage subsystem to produce nitrogen, and the hydrogen production subsystem to produce hydrogen. The resulting nitrogen and hydrogen are then fed into the ammonia synthesis tower 14 to participate in the synthesis reaction and produce ammonia. This achieves coupling and linkage between the ammonia synthesis subsystem and the air energy storage subsystem through the nitrogen production subsystem, and the combined action of the nitrogen and hydrogen production subsystems enables efficient co-production between the ammonia synthesis subsystem and the air energy storage subsystem. In this process, nitrogen produced from compressed air, an intermediate product of the air energy storage subsystem, can be used as a raw material for the ammonia synthesis reaction in the ammonia synthesis subsystem. Ammonia storage tank 19 is connected to the ammonium bicarbonate synthesis subsystem, thus coupling the ammonia synthesis subsystem with the ammonium bicarbonate synthesis subsystem, and using ammonia, the final product of the ammonia synthesis subsystem, as a raw material for the ammonium bicarbonate synthesis reaction. Therefore, the above setup can significantly improve the efficiency of co-product utilization between the systems.

[0043] It should be noted that the ammonia synthesis subsystem employs a high-temperature, high-pressure synthesis method. The main reactions occurring in the ammonia synthesis tower are: The temperature of the ammonia synthesis reactor is preferably controlled between 400 and 500 degrees Celsius.

[0044] In some specific embodiments, such as Figure 1As shown, the second heat exchanger 15 is connected to the heat release side of the first heat exchanger 4 through at least one set of synthesis heat recovery loops. That is, the ammonia synthesis subsystem recovers and utilizes the high temperature after the ammonia synthesis reaction in the air energy storage subsystem during the energy release phase of the expander 5 inlet gas heating process. This achieves energy supplementation and heat recovery between different subsystems in the co-production process, helping to increase the inlet temperature of the air energy storage subsystem during expansion work, thereby significantly improving the power generation efficiency of the air energy storage system. The specific structure and working principle of the synthesis heat recovery loops connected to the ammonia synthesis subsystem will be described in detail later and will not be repeated here.

[0045] In some specific embodiments, such as Figure 1 As shown, the hydrogen production subsystem includes an electrolyzer 10 and a hydrogen storage tank 11. The input end of the electrolyzer 10 is connected to a water source, and the output end of the electrolyzer 10 is connected to the hydrogen storage tank 11, which is connected to an ammonia synthesis tower 14. The electrolyzer 10 introduces clean water from an external water source, and then ionizes the water in the electrolyzer 10 to produce hydrogen and oxygen. The hydrogen is stored in the hydrogen storage tank 11, and the oxygen is stored in the oxygen storage tank 12. Since large-scale storage of gaseous co-products is difficult, and hydrogen is a flammable gas, large-scale storage can easily lead to danger. Therefore, by passing the hydrogen in the hydrogen storage tank 11 into the ammonia synthesis tower 14 for rapid digestion, the dangers of large-scale hydrogen storage can be reduced, and the safety of system operation can be improved.

[0046] In some specific embodiments, such as Figure 1 As shown, the nitrogen preparation subsystem includes an air separation device 8, a nitrogen storage tank 9, and a buffer tank 13. The compressed air storage tank 3 is connected to the nitrogen storage tank 9 via the air separation device 8, which is used to separate nitrogen from a portion of the compressed air in the compressed air storage tank 3. The input end of the buffer tank 13 is connected to the nitrogen storage tank 9 and the hydrogen preparation subsystem. Preferably, the input end of the buffer tank 13 is connected to both the nitrogen storage tank 9 and the hydrogen storage tank 11. The output end of the buffer tank 13 is connected to the ammonia synthesis tower 14. The buffer tank 13 is used to mix and preheat hydrogen and nitrogen to improve the synthesis reaction efficiency and sufficiency within the ammonia synthesis tower 14.

[0047] In some specific embodiments, such as Figure 1As shown, the ammonia synthesis subsystem also includes an ammonia separator 18. An ammonia cooler 17 is connected to an ammonia storage tank 19 via the ammonia separator 18. The ammonia separator 18 has an input end, an output end, and a separation output end. The input end of the ammonia separator 18 is connected to the ammonia cooler 17. The output end of the ammonia separator 18 is connected to the ammonia storage tank 19. The separation output end of the ammonia separator 18 is connected to both the nitrogen preparation subsystem and the methanol synthesis subsystem. The ammonia separator 18 is used to separate and extract unreacted hydrogen from ammonia. Preferably, the separation output end of the ammonia separator 18 is connected to the input end of a buffer tank 13 so that unreacted hydrogen in the prepared ammonia is separated and introduced, recycled, and fed back into the buffer tank 13 for thorough mixing and preheating with nitrogen, achieving energy recovery and utilization within the same subsystem. Preferably, the separation output end of the ammonia separator 18 is connected to the input end of the methanol synthesis reactor 26 of the methanol synthesis subsystem, so as to separate the unreacted hydrogen in the prepared ammonia gas and pass it into the methanol synthesis reactor 26 as a raw material for the methanol synthesis subsystem to participate in the methanol synthesis reaction, thereby realizing the coupling connection between the ammonia synthesis subsystem and the methanol synthesis subsystem, and thus realizing reliable and efficient co-production between the two subsystems.

[0048] In some embodiments, such as Figure 1 As shown, the methanol synthesis subsystem includes a methanol synthesis reactor 26, a third heat exchanger 27, a methanol separator 28, a methanol distillation column 29, and a methanol storage tank 30. The methanol synthesis reactor 26, the third heat exchanger 27, the methanol separator 28, the methanol distillation column 29, and the methanol storage tank 30 are connected sequentially to form a reaction flow for methanol production. The methanol synthesis reactor 26 is connected to a carbon dioxide capture subsystem to reliably capture carbon dioxide, which is then used as a raw material for methanol production. The input terminals of the methanol synthesis reactor 26 are connected to a hydrogen storage tank 11 and a carbon dioxide storage tank 21 of the carbon dioxide capture subsystem. Hydrogen and carbon dioxide are introduced into the methanol synthesis reactor 26, respectively, causing the hydrogen and carbon dioxide within the reactor 26 to react and produce methanol. The prepared methanol is cooled by the second heat exchanger 15 and then enters the methanol separator 28. The methanol separator 28 separates the unreacted water in the prepared methanol, thereby increasing the methanol concentration. The separated methanol and water are fed into the methanol distillation column 29 and distilled to obtain methanol with a higher concentration. The methanol is finally stored in the methanol storage tank 30 in a safer liquid form.

[0049] It should be noted that the methanol synthesis subsystem uses a one-step process involving carbon dioxide and hydrogen to synthesize methanol. The main reactions occurring in the methanol synthesis reactor are: The temperature of the preferred methanol synthesis reactor 26 is controlled between 200 and 300 degrees Celsius.

[0050] In some specific embodiments, the methanol separator 28 has an input end, an output end, and a separation output end. The input end of the methanol separator 28 is connected to the third heat exchanger 27. The output end of the methanol separator 28 is connected to the methanol distillation column 29. The separation output end of the methanol separator 28 is connected to the methanol synthesis reactor 26 and the hydrogen production subsystem. The methanol separator 28 is used to separate and extract unreacted hydrogen from methanol. Preferably, the separation output end of the methanol separator 28 is connected to the methanol synthesis reactor 26 so that the recovered hydrogen can be reintroduced into the methanol reactor to participate in the reaction to synthesize methanol, realizing energy recovery and utilization within the same subsystem. Preferably, the separation output end of the methanol separator 28 is connected to the input end of the buffer tank 13 of the hydrogen production subsystem so that unreacted hydrogen in the prepared ammonia can be separated and introduced, recovered, and reintroduced into the buffer tank 13 to be fully mixed and preheated with nitrogen, realizing the coupling connection between the methanol synthesis subsystem and the hydrogen production subsystem, that is, realizing the coupling connection between the methanol synthesis subsystem and the ammonia synthesis subsystem, thereby realizing reliable and efficient co-production among the three subsystems.

[0051] In some specific embodiments, the methanol distillation column 29 is provided with an input end, an output end, and a distillation output end. The input end of the methanol distillation column 29 is connected to the output end of the methanol separator 28. The output end of the methanol distillation column 29 is connected to the methanol storage tank 30. The distillation output end of the methanol distillation column 29 is connected to the hydrogen production subsystem and the ammonium bicarbonate synthesis subsystem, respectively. The methanol distillation column 29 is used to distill water from methanol. Preferably, the distillation output end of the methanol distillation column 29 is connected to the input end of the electrolyzer 10 of the hydrogen production subsystem, so as to recover the by-product water in the methanol synthesis subsystem and replenish it into the hydrogen production subsystem, thereby improving the yield and efficiency of hydrogen production, and realizing the coupling connection between the methanol synthesis subsystem and the hydrogen production subsystem, that is, realizing the coupling connection between the methanol synthesis subsystem and the ammonia synthesis subsystem, and thus realizing reliable and efficient co-production among the three subsystems. Preferably, the distillation output end of the methanol distillation column 29 is connected to the input end of the ammonium bicarbonate reactor 22 of the ammonium bicarbonate synthesis subsystem, so as to recover the by-product water in the methanol synthesis subsystem and pass it into the ammonium bicarbonate reactor 22 as a raw material to participate in the ammonium bicarbonate synthesis reaction, thereby realizing the coupling connection between the methanol synthesis subsystem and the ammonium bicarbonate synthesis subsystem, and thus realizing reliable and efficient co-production between the two subsystems.

[0052] In some specific embodiments, the third heat exchanger 27 is connected to the heat release side of the first heat exchanger 4 through at least one set of synthesis heat recovery loops. That is, the methanol synthesis subsystem recovers and utilizes the high temperature after the methanol synthesis reaction in the air energy storage subsystem during the energy release phase of the expander 5 inlet gas heating process. This achieves energy supplementation and heat recovery between different subsystems in the co-production process, helping to increase the inlet temperature of the air energy storage subsystem during expansion work, thereby significantly improving the power generation efficiency of the air energy storage system. The specific structure and working principle of the synthesis heat recovery loops connected to the methanol synthesis subsystem will be described in detail later and will not be repeated here.

[0053] In some embodiments, such as Figure 1 As shown, the ammonium bicarbonate synthesis subsystem includes an ammonium bicarbonate reactor 22, a crystallizer 23, a three-in-one filtration device 24, and an ammonium bicarbonate storage tank 25. The ammonium bicarbonate reactor 22, crystallizer 23, three-in-one filtration device 24, and ammonium bicarbonate storage tank 25 are connected sequentially to form a reaction flow for preparing ammonium bicarbonate. The input end of the ammonium bicarbonate reactor 22 is connected to a methanol distillation column 29, a carbon dioxide capture subsystem, and an ammonia storage tank 19. Water generated in the methanol distillation column 29 is fed into the ammonium bicarbonate reactor 22; carbon dioxide captured and stored in the carbon dioxide capture subsystem is fed into the ammonium bicarbonate reactor 22; and ammonia stored in the ammonia storage tank 19 is fed into the ammonium bicarbonate reactor 22. Water, carbon dioxide, and ammonia react fully in the ammonium bicarbonate reactor 22 to produce ammonium bicarbonate. The crystallizer 23 is used to concentrate and crystallize the ammonium bicarbonate produced in the reaction. The three-in-one filtration device 24 is used to filter, wash and dry the concentrated and crystallized ammonium bicarbonate, so that the ammonium bicarbonate can be stored in the ammonium bicarbonate storage tank 25 in a safer solid form.

[0054] It should be noted that in the above-mentioned ammonium bicarbonate synthesis subsystem, the main reaction occurring in the ammonium bicarbonate reactor is as follows: .

[0055] In some embodiments, the carbon dioxide capture subsystem includes a carbon dioxide capture device 20 and a carbon dioxide storage tank 21. The carbon dioxide capture device 20 captures carbon dioxide from external carbon dioxide sources such as chemical plant exhaust gas and biomass combustion exhaust gas, and stores the carbon dioxide in the carbon dioxide storage tank 21. The carbon dioxide storage tank 21 is connected to the methanol synthesis reactor 26 of the methanol synthesis subsystem and the ammonium bicarbonate reactor 22 of the ammonium bicarbonate synthesis subsystem, thereby supplying carbon dioxide for the methanol synthesis reaction and the ammonium bicarbonate synthesis reaction.

[0056] It should be noted that the hydrogen production subsystem and the carbon dioxide capture subsystem both require a large amount of electricity. Therefore, integrating the hydrogen production subsystem and the carbon dioxide capture subsystem into this integrated system and coupling them with the air energy storage subsystem can achieve complementary advantages among the various subsystems and improve the overall working efficiency of the integrated system.

[0057] In some specific embodiments, such as Figure 1 As shown, each synthesis heat recovery loop includes a high-temperature thermal storage medium tank and a low-temperature thermal storage medium tank. The output end of the high-temperature thermal storage medium tank is connected to the input end of the low-temperature thermal storage medium tank through the heat release side of the first heat exchanger 4, and the output end of the low-temperature thermal storage medium tank is connected to the input end of the high-temperature thermal storage medium tank through the heat absorption side of the heat exchangers of each subsystem in the cogeneration. This configuration enables reliable flow of the thermal storage medium in the synthesis heat recovery loop, achieving reliable heat exchange and energy recovery and utilization. Heat is transported from the heat exchangers of each subsystem to the first heat exchanger 4 of the air energy storage subsystem, maximizing the inlet temperature for the expansion work of the air energy storage subsystem, thereby significantly improving the power generation efficiency of the air energy storage system.

[0058] It should be noted that the heat exchangers in each subsystem include at least one of the following: the compressor-stage aftercooler 2, the second heat exchanger 15 of the ammonia synthesis subsystem, and the third heat exchanger 27 of the methanol synthesis subsystem. That is, in the energy release stage of the air energy storage subsystem, the inlet heat from the expansion of compressed air comes partly from the compression heat recovered within the same subsystem from the energy storage stage, partly from the heat of the high-temperature gas exiting the ammonia synthesis tower 14, and partly from the heat of the high-temperature gas exiting the methanol synthesis reactor 26.

[0059] In some specific embodiments, the above-described at least one set of synthetic heat recovery loops includes a first heat recovery loop, a second heat recovery loop, and a third heat recovery loop.

[0060] Corresponding to the aforementioned air energy storage subsystem, the compressor-stage aftercooler 2 is connected to the first heat exchanger 4 via a first heat recovery loop. Preferably, the output end of the first low-temperature heat storage medium tank 7 is connected to the input end of the first high-temperature heat storage medium tank 6 via the heat absorption side of the compressor-stage aftercooler 2. The heat release side of the compressor-stage aftercooler 2 is connected to the energy storage pipeline of the air energy storage subsystem, with its two ends connected to the output end of the air compressor 1 and the input end of the compressed air tank 3, respectively. The output end of the first high-temperature heat storage medium tank 6 is connected to the input end of the first low-temperature heat storage medium tank 7 via the first heat release side of the first heat exchanger 4. The heat absorption side of the first heat exchanger 4 is connected to the energy release pipeline of the air energy storage subsystem, with its two ends connected to the input ends of the compressed air tank 3 and the expander 5, respectively. This setup utilizes a low-temperature heat storage medium flowing through the heat absorption side of the compressor stage aftercooler 2 to absorb the compression heat of the air energy storage subsystem during the energy storage phase and store it in the first high-temperature heat storage medium tank 6. Then, the high-temperature heat storage medium flows through the first heat release side of the first heat exchanger 4 to release the compression heat to the air energy storage subsystem during the energy release phase, thereby increasing the inlet temperature of the air energy storage subsystem for expansion and work, and thus significantly improving the power generation efficiency of the air energy storage system.

[0061] Corresponding to the aforementioned ammonia synthesis subsystem, the second heat exchanger 15 is connected to the first heat exchanger 4 via a second heat recovery loop. Preferably, the output end of the second low-temperature thermal storage medium tank 31 is connected to the input end of the second high-temperature thermal storage medium tank 32 via the heat absorption side of the second heat exchanger 15, and the heat release side of the second heat exchanger 15 is connected to the ammonia synthesis pipeline, the two ends of which are connected to the output end of the ammonia synthesis tower 14 and the input end of the ammonia compressor 16, respectively. The output end of the second high-temperature thermal storage medium tank 32 is connected to the input end of the second low-temperature thermal storage medium tank 31 via the second heat release side of the first heat exchanger 4. This configuration utilizes the low-temperature thermal storage medium flowing through the heat absorption side of the second heat exchanger 15 to absorb the synthesis heat during the ammonia synthesis process and store it in the second high-temperature thermal storage medium tank 32; then, the high-temperature thermal storage medium flows through the second heat release side of the first heat exchanger 4 to release the compression heat to the air energy storage subsystem during the energy release stage, increasing the inlet temperature of the air energy storage subsystem for expansion work, thereby significantly improving the power generation efficiency of the air energy storage system.

[0062] Corresponding to the above-mentioned methanol synthesis subsystem, the third heat exchanger 27 is connected to the first heat exchanger 4 through a third heat recovery loop. Preferably, the output end of the third low-temperature thermal storage medium tank 33 is connected to the input end of the third high-temperature thermal storage medium tank 34 through the heat absorption side of the third heat exchanger 27, and the heat release side of the third heat exchanger 27 is connected to the methanol synthesis pipeline. The two ends of the methanol synthesis pipeline are respectively connected to the output end of the methanol synthesis reactor 26 and the input end of the methanol separator. The output end of the third high-temperature thermal storage medium tank 34 is connected to the input end of the third low-temperature thermal storage medium tank 33 through the third heat release side of the first heat exchanger 4. This configuration utilizes the low-temperature thermal storage medium flowing through the heat absorption side of the third heat exchanger 27 to absorb the synthesis heat during the methanol synthesis process and store it in the third high-temperature thermal storage medium tank 34; then, the high-temperature thermal storage medium flows through the third heat release side of the first heat exchanger 4 to release the compression heat to the air energy storage subsystem during the energy release stage, thereby increasing the inlet temperature of the air energy storage subsystem for expansion work and significantly improving the power generation efficiency of the air energy storage system.

[0063] This invention provides an integrated method for co-producing ammonium bicarbonate and methanol using air energy storage. This integrated method can be executed using the integrated system described above. The integrated method provided by this invention will be described in detail below. The integrated method described below can be referred to in correspondence with the integrated system described above.

[0064] like Figure 1 As shown, the integrated method includes an air energy storage and power transmission step, an ammonia synthesis step, a methanol synthesis step, an ammonium bicarbonate synthesis step, and a synthesis heat recovery step. The air energy storage and power transmission step includes an energy storage stage and an energy release stage. In the energy storage stage, compressed air is prepared using an air energy storage subsystem. In the energy release stage, the compressed air is heated and expanded to generate electricity. The ammonia synthesis step uses the compressed air prepared in the air energy storage and power transmission step to prepare nitrogen, and then uses the ammonia synthesis subsystem to react nitrogen and hydrogen to synthesize ammonia. The methanol synthesis step uses the methanol synthesis subsystem to react carbon dioxide and hydrogen to synthesize methanol, and then separates and extracts water from the methanol. The ammonium bicarbonate synthesis step uses the ammonium bicarbonate synthesis subsystem to react carbon dioxide, water extracted from the methanol synthesis step, and ammonia prepared in the ammonia synthesis step to prepare ammonium bicarbonate. The synthesis heat recovery step recovers the heat generated in the energy storage stage, ammonia synthesis step, and methanol synthesis step of the air energy storage and power transmission step, and introduces the recovered heat into the energy release stage of the air energy storage and power transmission step to heat the compressed air. By setting up each step corresponding to the above-mentioned integrated system and associating each step, this integration method possesses all the advantages of the above-mentioned integrated system, which will not be elaborated here.

[0065] Each step of the integration method in this embodiment is executed by a corresponding subsystem of the aforementioned integration system. The operating principle of the aforementioned integration system during the execution of the integration method is as follows.

[0066] In the air energy storage and power transmission process, the air energy storage subsystem is in the energy storage phase. It uses off-peak electricity such as wind power and photovoltaic power as the power input, controlling the air source to send purified air into air compressor 1. The air is compressed to a high temperature and high pressure state in air compressor 1, and then the compression heat is recovered through compressor-stage aftercooler 2. The cooled air is stored in compressed air storage tank 3. In the energy release phase, the compressed air in compressed air storage tank 3 is heated by the first heat exchanger 4 and then enters expander 5 to expand and do work, thereby driving a generator to generate electricity.

[0067] In the ammonia synthesis step, a portion of the compressed air stored in the compressed air storage tank 3 of the air energy storage subsystem enters the air separation device 8. The air separation device 8 separates nitrogen from the compressed air and stores the nitrogen in the nitrogen storage tank 9. The electrolyzer 10 electrolyzes clean water to produce hydrogen and oxygen. The produced hydrogen is stored in the hydrogen storage tank 11, and the produced oxygen is stored in the oxygen storage tank 12. The nitrogen in the hydrogen storage tank and the hydrogen in the hydrogen storage tank 11 are both fed into the buffer tank 13 for mixing and preheating. Then, the mixed gas is fed into the ammonia synthesis tower 14, where the reaction temperature is controlled between 400 and 500 degrees Celsius. The high-temperature gas generated by the full reaction of the mixed gas in the ammonia synthesis tower 14 is cooled by the second heat exchanger 15 and then enters the ammonia compressor 16 to be compressed to the critical pressure of ammonia. The compressed gas enters the ammonia cooler 17 to cool down and then enters the ammonia separator 18. The ammonia separator 18 separates the unreacted hydrogen from the ammonia gas for recycling and reuse, and cools the ammonia into liquid state and stores it in the ammonia storage tank 19.

[0068] In the methanol synthesis step, the tail gas from chemical plants and biomass combustion, which is rich in carbon dioxide, is captured by the integrated system using a carbon dioxide capture device 20 and stored in a carbon dioxide storage tank 21. Hydrogen from the hydrogen storage tank 11 and carbon dioxide from the carbon dioxide storage tank 21 are both fed into the methanol synthesis reactor 26, where the temperature is controlled between 200 and 300 degrees Celsius. The high-temperature gas exiting the methanol synthesis reactor 26 is cooled by a third heat exchanger 27 and then enters a methanol separator 28. The methanol separator 28 separates unreacted hydrogen from the methanol as a raw material for the next methanol synthesis reaction. The remaining methanol and water enter a methanol distillation column 29. The methanol distilled from the methanol distillation column 29 is stored in a methanol storage tank 30, and the water separated from the methanol distillation column 29 is treated and recycled back into at least one of the electrolyzer 10 and the ammonium bicarbonate reactor 22.

[0069] In the ammonium bicarbonate synthesis step, water produced in the aforementioned co-production subsystem is first passed into ammonium bicarbonate reactor 22. Then, ammonia gas produced in the same subsystem is passed into reactor 22 to form ammonia water. Next, carbon dioxide produced in the same subsystem is passed into the ammonium bicarbonate reactor 22 containing ammonia water to form ammonium bicarbonate product, such as ammonium bicarbonate reaction solution. The ammonium bicarbonate in the reaction solution is concentrated and crystallized using crystallizer 23. The resulting product is then filtered, washed, and dried by a three-in-one filtration device 24 before being stored in ammonium bicarbonate storage tank 25.

[0070] In the synthesis heat recovery step, synthesis heat recovery is performed between the various subsystems of the co-production process. Preferably, the air energy storage subsystem recovers and utilizes the compression heat within the same subsystem through a first heat recovery loop during both the energy storage and release phases. Preferably, the ammonia synthesis subsystem recovers and utilizes the reaction synthesis heat to the release phase of the air energy storage subsystem through a second heat recovery loop. Preferably, the methanol synthesis subsystem recovers and utilizes the reaction synthesis heat to the release phase of the air energy storage subsystem through a third heat recovery loop. That is, the heat absorbed by the compressed air in the release phase of the air energy storage subsystem comes partly from the compression heat recovered within the subsystem; and partly from the heat of the high-temperature gas at the outlet of the ammonia synthesis reactor and the high-temperature gas at the outlet of the methanol synthesis reactor 26.

[0071] The heat recovery process between the cogeneration subsystems is as follows. In the energy storage stage, the high-temperature gas exiting the ammonia synthesis tower 14 in the ammonia synthesis subsystem exchanges heat with the heat storage medium in the second heat exchanger 15. The heated heat storage medium is then stored in the second high-temperature heat storage medium tank 32. In the methanol synthesis subsystem, the high-temperature gas exiting the methanol reactor exchanges heat with the heat storage medium in the third heat exchanger 27. The heated heat storage medium is then stored in the third high-temperature heat storage medium tank 34. In the energy release stage, the second high-temperature heat storage medium tank 32 and the third high-temperature heat storage medium tank 34 respectively input their respective heat storage media into the first heat exchanger 4 to heat the compressed air before the inlet of the expander 5, thereby increasing the inlet temperature of the expander 5 and the power generation efficiency.

[0072] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention 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; and these 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 the present invention.

Claims

1. An integrated system for air energy storage and co-production of ammonium bicarbonate and methanol, characterized in that, include: An air energy storage subsystem, suitable for connection to the power grid, wherein the air energy storage subsystem can generate compressed air during the energy storage phase and use the expansion of compressed air to do work and transmit power to the power grid during the energy release phase; An ammonia synthesis subsystem is connected to the air energy storage subsystem. The ammonia synthesis subsystem can produce ammonia by reacting hydrogen and nitrogen generated from compressed air. The ammonia synthesis subsystem includes an ammonia synthesis tower, a second heat exchanger, an ammonia compressor, an ammonia cooler, and an ammonia storage tank, which are connected in sequence. A methanol synthesis subsystem is connected to the ammonia synthesis subsystem. The methanol synthesis subsystem can synthesize methanol by reacting carbon dioxide with hydrogen and can separate and extract water from methanol. The methanol synthesis subsystem includes a methanol synthesis reactor, a third heat exchanger, a methanol separator, a methanol distillation column, and a methanol storage tank, which are connected in sequence. An ammonium bicarbonate synthesis subsystem is connected to the ammonia synthesis subsystem and the methanol synthesis subsystem, respectively. The ammonium bicarbonate synthesis subsystem can produce ammonium bicarbonate by reacting water, carbon dioxide and ammonia. The ammonia synthesis subsystem and the methanol synthesis subsystem are respectively connected to the air energy storage subsystem through at least one set of synthesis heat recovery loops; The air energy storage subsystem includes an air compressor, a compressor-stage aftercooler, a compressed air storage tank, a first heat exchanger, and an expander. The air compressor, the compressor-stage aftercooler, the compressed air storage tank, the heat absorption side of the first heat exchanger, and the expander are connected sequentially. The air compressor is connected to an air source, and the expander is connected to the power grid via a generator. The compressed air storage tank is connected to the ammonia synthesis subsystem via a nitrogen production subsystem. The compressor-stage aftercooler is connected to the heat release side of the first heat exchanger via at least one set of synthesis heat recovery loops. Each of the subsystem heat exchangers includes at least one of the compressor-stage aftercooler, the second heat exchanger of the ammonia synthesis subsystem, and the third heat exchanger of the methanol synthesis subsystem; at least one set of synthesis heat recovery loops includes a first heat recovery loop, a second heat recovery loop, and a third heat recovery loop; the compressor-stage aftercooler is connected to the first heat exchanger through the first heat recovery loop; the second heat exchanger is connected to the first heat exchanger through the second heat recovery loop; and the third heat exchanger is connected to the first heat exchanger through the third heat recovery loop. The synthesis heat recovery loop includes a high-temperature heat storage medium tank and a low-temperature heat storage medium tank. The output end of the high-temperature heat storage medium tank is connected to the input end of the low-temperature heat storage medium tank through the heat release side of the first heat exchanger. The output end of the low-temperature heat storage medium tank is connected to the input end of the high-temperature heat storage medium tank through the heat absorption side of each subsystem heat exchanger. The ammonia synthesis subsystem further includes an ammonia separator, and the ammonia cooler is connected to the ammonia storage tank through the ammonia separator; the separation output end of the ammonia separator is connected to the nitrogen preparation subsystem and the methanol synthesis subsystem, and the ammonia separator is used to separate and extract unreacted hydrogen from ammonia.

2. The integrated system for co-producing ammonium bicarbonate and methanol from air energy storage according to claim 1, characterized in that, The nitrogen preparation subsystem is connected to the hydrogen preparation subsystem, and both the nitrogen preparation subsystem and the hydrogen preparation subsystem are connected to the ammonia synthesis tower; The ammonia storage tank is connected to the ammonium bicarbonate synthesis subsystem; The second heat exchanger is connected to the heat release side of the first heat exchanger through at least one set of the synthesis heat recovery loops.

3. The integrated system for co-producing ammonium bicarbonate and methanol from air energy storage according to claim 2, characterized in that, The hydrogen production subsystem includes an electrolyzer and a hydrogen storage tank. The input end of the electrolyzer is connected to a water source, and the output end of the electrolyzer is connected to the hydrogen storage tank. The hydrogen storage tank is connected to the ammonia synthesis tower.

4. The integrated system for co-producing ammonium bicarbonate and methanol from air energy storage according to claim 2, characterized in that, The nitrogen preparation subsystem includes an air separation device, a nitrogen storage tank, and a buffer tank; The compressed air storage tank is connected to the nitrogen storage tank via the air separation device, which is used to separate nitrogen from a portion of the compressed air in the compressed air storage tank. The buffer tank's input end is connected to the nitrogen storage tank and the hydrogen production subsystem, and the buffer tank's output end is connected to the ammonia synthesis tower. The buffer tank is used to mix and preheat hydrogen and nitrogen.

5. The integrated system for co-producing ammonium bicarbonate and methanol from air energy storage according to any one of claims 2-4, characterized in that, The methanol synthesis reactor is connected to a carbon dioxide capture subsystem; The methanol separator is connected to the methanol synthesis reactor and the hydrogen production subsystem. The methanol separator is used to separate and extract unreacted hydrogen from methanol. The methanol distillation column is connected to the hydrogen production subsystem and the ammonium bicarbonate synthesis subsystem, respectively, and is used to distill water from methanol. The third heat exchanger is connected to the heat release side of the first heat exchanger through at least one set of the synthesis heat recovery loops.

6. The integrated system for co-producing ammonium bicarbonate and methanol using air energy storage according to claim 5, characterized in that, The ammonium bicarbonate synthesis subsystem includes an ammonium bicarbonate reactor, a crystallizer, a three-in-one filtration device, and an ammonium bicarbonate storage tank, which are connected in sequence. The input end of the ammonium bicarbonate reactor is connected to the methanol distillation column, the carbon dioxide capture subsystem, and the ammonia storage tank, respectively.

7. An integrated method for co-producing ammonium bicarbonate and methanol using air energy storage, characterized in that, Performed using an integrated system for co-producing ammonium bicarbonate and methanol using air energy storage as described in any one of claims 1-6; The integrated method for co-producing ammonium bicarbonate and methanol from air energy storage includes: The air energy storage and power transmission process includes an energy storage stage and an energy release stage. The energy storage stage uses an air energy storage subsystem to generate compressed air, and the energy release stage heats the compressed air and expands it to generate electricity. In the ammonia synthesis step, nitrogen is prepared using the compressed air generated in the air energy storage and power transmission step, and ammonia is synthesized by reacting nitrogen and hydrogen using the ammonia synthesis subsystem. The methanol synthesis step involves using the methanol synthesis subsystem to react carbon dioxide and hydrogen to synthesize methanol, and then separating and extracting water from the methanol. The ammonium bicarbonate synthesis step involves reacting carbon dioxide, water extracted from the methanol synthesis step, and ammonia prepared from the ammonia synthesis step using a subsystem for synthesizing ammonium bicarbonate. The synthesis heat recovery step recovers the heat generated in the energy storage stage of the air energy storage and power transmission step, the ammonia synthesis step, and the methanol synthesis step, and introduces the recovered heat into the energy release stage of the air energy storage and power transmission step to heat the compressed air.

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