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

Abstract

The invention relates to an integrated system and method for co-producing ammonium bicarbonate and methanol through air energy storage. According to the integrated system, the air energy storage subsystem, the ammonia synthesis subsystem, the methanol synthesis subsystem and the ammonium bicarbonate synthesis subsystem are coupled and connected, and coupled co-production of ammonia gas, methanol and ammonium bicarbonate is realized in the process of energy storage and power generation by using the air energy storage subsystem; and large-scale energy storage and consumption of each subsystem and cyclic utilization of various by-products can be realized, and the realization of the dual-carbon target can be assisted in multiple directions. Wherein the ammonia synthesis subsystem and the methanol synthesis subsystem are respectively connected with the air energy storage subsystem through at least one group of synthesis heat recovery loops, so that reaction heat of each subsystem is recycled for heating compressed air, the temperature of an expansion acting inlet of the air energy storage subsystem is increased, and the power generation efficiency of the air energy storage system is improved.

Description

Technical Field

[0001] The present invention relates to the field of energy storage technology, and in particular to an integrated system and method for air energy storage and co-production of ammonium bicarbonate and methanol. Background Art

[0002] The intermittent, volatile and unstable nature of renewable energy generation such as wind power and photovoltaic power makes large-scale long-term energy storage technology a key technology for the development of future power systems. Air energy storage technology represented by compressed air and liquid air energy storage has outstanding advantages such as clean, low-carbon, safe and long life, and is one of the most promising and competitive long-term energy storage technologies.

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

[0004] In summary, the existing integrated systems and methods for air energy storage and co-production of other products still have problems such as difficulty in long-term storage of co-produced products and low efficiency of air energy storage systems. Summary of the invention

[0005] The present invention provides an integrated system and method for air energy storage and co-production of ammonium bicarbonate and methanol, which are used to solve the defects in the prior art that it is difficult to store the co-produced products for a long time and the air energy storage system has low efficiency.

[0006] The present invention provides an integrated system for air energy storage and co-production of ammonium bicarbonate and methanol, comprising: an air energy storage subsystem, suitable for connecting to a power grid, the air energy storage subsystem can generate compressed air in the energy storage stage, and use the compressed air to expand and do work to transmit electricity to the power grid in the energy release stage; a synthetic ammonia subsystem, connected to the air energy storage subsystem, the synthetic ammonia subsystem can use hydrogen and nitrogen generated from compressed air to react to prepare ammonia; a synthetic methanol subsystem, connected to the synthetic ammonia subsystem, the synthetic methanol subsystem can use carbon dioxide and hydrogen to react to synthesize methanol, and can separate and extract water from methanol; a synthetic ammonium bicarbonate subsystem, respectively connected to the synthetic ammonia subsystem and the synthetic methanol subsystem, the synthetic ammonium bicarbonate subsystem can use water, carbon dioxide and ammonia to react to produce ammonium bicarbonate; wherein the synthetic ammonia subsystem and the synthetic methanol subsystem are respectively connected to the air energy storage subsystem through at least one set of synthetic heat recovery loops.

[0007] According to the present invention, an integrated system for air energy storage and co-production of ammonium bicarbonate and methanol is provided, wherein the air energy storage subsystem comprises an air compressor, a compressor-stage aftercooler, a compressed air storage tank, a first heat exchanger and an expander, wherein 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 in sequence, 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 synthetic ammonia subsystem via a nitrogen preparation subsystem; and the compressor-stage aftercooler is connected to the heat release side of the first heat exchanger via at least one set of the synthetic heat recovery loop.

[0008] According to an integrated system for air energy storage and co-production of ammonium bicarbonate and methanol provided by the present invention, the synthetic ammonia subsystem comprises an ammonia synthesis tower, a second heat exchanger, an ammonia compressor, an ammonia cooler and an ammonia storage tank, and the ammonia synthesis tower, the second heat exchanger, the ammonia compressor, the ammonia cooler and the ammonia storage tank are connected in sequence; the nitrogen preparation subsystem is connected to the hydrogen preparation subsystem, and the nitrogen preparation subsystem and the hydrogen preparation subsystem are both connected to the ammonia synthesis tower; the ammonia storage tank is connected to the synthetic ammonium bicarbonate subsystem; the second heat exchanger is connected to the heat release side of the first heat exchanger through at least one set of the synthetic heat recovery loop.

[0009] According to an integrated system for air energy storage and co-production of ammonium bicarbonate and methanol provided by the present invention, the hydrogen preparation 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 an integrated system for air energy storage and co-production of ammonium bicarbonate and methanol provided by the present invention, 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 through the air separation device, and the air separation device is used to separate part of the compressed air in the compressed air storage tank to generate nitrogen; the input end of the buffer tank is connected to the nitrogen storage tank and the hydrogen preparation subsystem, the output end of the buffer tank is connected to the ammonia synthesis tower, and the buffer tank is used to preheat the mixture of hydrogen and nitrogen.

[0011] According to an integrated system for air energy storage and co-production of ammonium bicarbonate and methanol provided by the present invention, the synthetic ammonia subsystem also 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 synthetic methanol subsystem, and the ammonia separator is used to separate and extract unreacted hydrogen from the ammonia.

[0012] According to an integrated system for air energy storage and co-production of ammonium bicarbonate and methanol provided by the present invention, the synthetic methanol subsystem includes a synthetic methanol reactor, a third heat exchanger, a methanol separator, a methanol distillation tower and a methanol storage tank, and the synthetic methanol reactor, the third heat exchanger, the methanol separator, the methanol distillation tower and the methanol storage tank are connected in sequence; the synthetic methanol reactor is connected to a carbon dioxide capture subsystem; the separation output end of the methanol separator is connected to the synthetic methanol reactor and the hydrogen production subsystem, and the methanol separator is used to separate and extract unreacted hydrogen from methanol; the distillation output end of the methanol distillation tower is respectively connected to the hydrogen production subsystem and the synthetic ammonium bicarbonate subsystem, and the methanol distillation tower 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 synthetic heat recovery loop.

[0013] According to an integrated system for air energy storage and co-production of ammonium bicarbonate and methanol provided by the present invention, the synthetic ammonium bicarbonate subsystem includes an ammonium bicarbonate reactor, a crystallizer, a three-in-one filter device and an ammonium bicarbonate storage tank, and the ammonium bicarbonate reactor, the crystallizer, the three-in-one filter device and the ammonium bicarbonate storage tank are connected in sequence; the input end of the ammonium bicarbonate reactor is respectively connected to the methanol distillation tower, the carbon dioxide capture subsystem and the ammonia storage tank.

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

[0015] The present invention provides an integrated method for air energy storage and co-production of ammonium bicarbonate and methanol, which is performed using the above-mentioned integrated system for air energy storage and co-production of ammonium bicarbonate and methanol; the integrated method for air energy storage and co-production of ammonium bicarbonate and methanol 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.

[0016] The air energy storage and power transmission steps include an energy storage stage and an energy release stage. The energy storage stage uses an air energy storage subsystem to prepare compressed air, and the energy release stage heats the compressed air and expands it to perform work to achieve power generation.

[0017] The ammonia synthesis step uses the compressed air prepared in the air energy storage and power transmission step to prepare nitrogen, and uses the synthetic ammonia subsystem to react nitrogen and hydrogen to synthesize ammonia.

[0018] The methanol synthesis step utilizes the synthetic methanol subsystem to react carbon dioxide with hydrogen to synthesize methanol, and separates and extracts water from the methanol.

[0019] The ammonium bicarbonate synthesis step uses an 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.

[0020] The synthetic 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] The integrated system for air energy storage and co-production of ammonium bicarbonate and methanol provided by the present invention comprises an air energy storage subsystem, a synthetic ammonia subsystem, a synthetic methanol subsystem and a synthetic ammonium bicarbonate subsystem. The air energy storage subsystem is suitable for connection to a power grid, and the air energy storage subsystem can generate compressed air in the energy storage stage, and use the compressed air expansion to do work to transmit electricity to the power grid in the energy release stage. The synthetic ammonia subsystem is connected to the air energy storage subsystem, and the synthetic ammonia subsystem can use hydrogen and nitrogen generated by compressed air to react to prepare ammonia. The synthetic methanol subsystem is connected to the synthetic ammonia subsystem, and the synthetic methanol subsystem can use carbon dioxide and hydrogen to react to synthesize methanol, and can separate and extract water from methanol. The synthetic ammonium bicarbonate subsystem is respectively connected to the synthetic ammonia subsystem and the synthetic methanol subsystem, and the synthetic ammonium bicarbonate subsystem can use water, carbon dioxide and ammonia to react to produce ammonium bicarbonate. The integrated system couples the air energy storage subsystem, synthetic ammonia subsystem, synthetic methanol subsystem and synthetic ammonium bicarbonate subsystem. In the process of storing energy and generating electricity using the air energy storage subsystem, it realizes the coupled co-production of ammonia, methanol and ammonium bicarbonate, and helps to achieve large-scale energy storage and consumption of each subsystem and the recycling of various by-products, assisting in the realization of dual carbon goals from multiple aspects.

[0022] Moreover, in the integrated system of air energy storage for the co-production of ammonium bicarbonate and methanol, the synthetic ammonia subsystem and the synthetic methanol subsystem are respectively connected to the air energy storage subsystem through at least one set of synthetic heat recovery loops. This arrangement can recycle the reaction heat of each of the above subsystems and utilize it in the process of heating compressed air by the air energy storage subsystem; that is, by recovering the heat energy of the outlet high-temperature gas of the synthetic ammonia reaction and the outlet high-temperature gas of the synthetic methanol reaction, the air energy storage subsystem is supplemented with heat during the energy release stage, which helps to increase the inlet temperature of the expansion work of the air energy storage subsystem, thereby improving the power generation efficiency of the air energy storage system.

[0023] Moreover, in the integrated system of air energy storage and co-production of 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, and methanol is a liquid product at room temperature and pressure. Compared with the existing air energy storage and co-production of other gaseous products, non-gaseous co-products are easier to store and transport, making the key chains of the entire industrial chain where the integrated system is located have the advantages of high efficiency, energy saving, and environmental protection.

[0024] The present invention also provides an integrated method for air energy storage and co-production of ammonium bicarbonate and methanol, which is performed using the above-mentioned integrated system. The 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 that match the integrated system. By setting each step corresponding to the above-mentioned integrated system and associating each step, the integrated method has all the advantages of the above-mentioned integrated system, and the details are not repeated here. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] In order to more clearly illustrate the technical solutions in the present invention or the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

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

[0027] Reference numerals: 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 separation unit; 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. Synthetic methanol reactor; 27. Third heat exchanger; 28. Methanol separator; 29. ​​Methanol distillation tower; 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 DESCRIPTION

[0028] In order to make the purpose, technical solution and advantages of the present invention clearer, the technical solution of the present invention will be clearly and completely described below in conjunction with the drawings of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0029] Combine the following Figure 1 The integrated system and method for co-producing ammonium bicarbonate and methanol with air energy storage of the present invention are described. The integrated system for co-producing ammonium bicarbonate and methanol with air energy storage of the present invention can be referred to as an "integrated system" or "system". The integrated method for co-producing ammonium bicarbonate and methanol with air energy storage of the present invention can be referred to as an "integrated method" or "method".

[0030] Figure 1 Schematic diagram of the structure of the integrated system provided by the present invention. Figure 1 As shown, the integrated system described in the embodiment of the present invention includes an air energy storage subsystem and multiple co-production subsystems of the air energy storage subsystem. The multiple co-production subsystems of the air energy storage subsystem specifically include a synthetic ammonia subsystem, a synthetic methanol subsystem and a synthetic ammonium bicarbonate subsystem.

[0031] The air energy storage subsystem is suitable for connection to the power grid. The air energy storage subsystem is provided with an energy storage stage and an energy release stage. In the energy storage stage, the air energy storage subsystem can generate compressed air. In the energy release stage, the air energy storage subsystem uses the compressed air generated in the energy storage stage to expand and do work to achieve power transmission to the power grid. The synthetic ammonia subsystem is connected to the air energy storage subsystem. The synthetic ammonia subsystem can use hydrogen and nitrogen generated from compressed air to react and prepare ammonia. The synthetic methanol subsystem is connected to the synthetic ammonia subsystem. The synthetic methanol subsystem can synthesize methanol by reacting carbon dioxide with hydrogen, and can separate and extract water from methanol. The synthetic ammonium bicarbonate subsystem is connected to the synthetic ammonia subsystem and the synthetic methanol subsystem respectively. The synthetic ammonium bicarbonate subsystem can use water, carbon dioxide and ammonia to react and prepare ammonium bicarbonate. The integrated system couples the air energy storage subsystem, synthetic ammonia subsystem, synthetic methanol subsystem and synthetic ammonium bicarbonate subsystem. In the process of storing energy and generating electricity using the air energy storage subsystem, it realizes the coupled co-production of ammonia, methanol and ammonium bicarbonate, and helps to achieve large-scale energy storage and consumption of each subsystem and the recycling of various by-products, assisting in the realization of dual carbon goals from multiple aspects.

[0032] It should be noted that the hydrogen described in the embodiments of the present invention can be hydrogen introduced from an external hydrogen source, or it can be hydrogen separated and recovered during the ammonia synthesis and post-treatment reaction in the synthetic ammonia subsystem for reuse, or it can be hydrogen synthesized by related reactions in other subsystems of the co-production and separated and extracted from the co-product for reuse.

[0033] It should be noted that the carbon dioxide described in the embodiment of the present invention can be captured and stored from a carbon dioxide source outside the system by the carbon dioxide capture device 20 of the carbon dioxide capture subsystem. The carbon dioxide source is preferably a tail gas enriched with carbon dioxide, such as tail gas from a chemical plant or tail gas from biomass combustion.

[0034] It should be noted that the water participating in the reaction described in the embodiments of the present invention can be obtained from a water source outside the system, or can be a by-product of a related subsystem co-produced within the system. For example, the water generated in the synthesis methanol subsystem during the distillation post-treatment of the generated methanol after the synthesis reaction is recycled and can be introduced into the hydrogen preparation subsystem to prepare hydrogen, or can be directly introduced into the synthesis ammonium bicarbonate subsystem to participate in the synthesis reaction to prepare ammonium bicarbonate.

[0035] It can be seen that the above-mentioned setting is interconnected through the coupled subsystems, so that the by-products and energy generated by the coupled subsystems in the relevant reactions and working processes can be reliably recovered, recycled and reasonably consumed, avoiding energy waste and assisting in the realization of the dual carbon goals in multiple aspects.

[0036] It should be noted that in this integrated system, the co-products prepared by the co-production subsystem of the air energy storage subsystem are liquid or solid at room temperature and pressure. For example, the co-product methanol finally prepared by the synthetic methanol subsystem is liquid at room temperature and pressure, and the co-product ammonium bicarbonate finally prepared by the synthetic ammonium bicarbonate subsystem is solid at room temperature and pressure. It can be seen that compared with the proposed scheme of co-producing other products (hydrogen, methane and other products, which are gaseous at room temperature and pressure) by air energy storage, the present invention obtains co-products that are liquid / solid at room temperature and pressure, which are easier to store and transport, and have greater room for promotion.

[0037] Furthermore, in the integrated system, the synthetic ammonia subsystem and the synthetic methanol subsystem are respectively connected to the air energy storage subsystem via at least one set of synthetic heat recovery loops. This arrangement can recycle the reaction heat of the above-mentioned subsystems and utilize it in the process of heating the compressed air by the air energy storage subsystem; that is, by recovering the heat energy of the outlet high-temperature gas of the synthetic ammonia reaction and the outlet high-temperature gas of the synthetic methanol reaction, the air energy storage subsystem is supplemented with heat during the energy release stage, which helps to increase the inlet temperature of the expansion work of the air energy storage subsystem, thereby improving the power generation efficiency of the air energy storage system. The reaction heat is recycled to improve the system efficiency, making the integrated system highly efficient, energy-saving, and environmentally friendly. In some embodiments, Figure 1 As shown, the air energy storage subsystem includes an air compressor 1, a compressor stage aftercooler 2, a compressed air storage tank 3, a first heat exchanger 4 and an expander 5. The air compressor 1, the compressor stage aftercooler 2, the compressed air storage tank 3, the heat absorption side of the first heat exchanger 4 and the expander 5 are connected in sequence, the air compressor 1 is connected to the air source, and the expander 5 is connected to the power grid through a generator, so that the air energy storage subsystem is used to connect the air source and the power grid, so that the system uses compressed air to store energy and generate electricity.

[0038] In some specific embodiments, the compressed air storage tank 3 is connected to the synthetic ammonia subsystem through a nitrogen preparation subsystem. The nitrogen preparation subsystem can draw out a portion of the compressed air stored in the compressed air storage tank 3 and prepare nitrogen using air separation technology, so that the nitrogen can be reliably stored and introduced into the synthetic ammonia subsystem to participate in the reaction, thereby realizing the co-production and coupling connection between the air energy storage subsystem and the synthetic ammonia subsystem. That is, the nitrogen prepared from the compressed air, an intermediate product of the air energy storage subsystem, can be used as a raw material for the synthetic ammonia subsystem to participate in the synthesis reaction, realizing the coupling connection and reliable co-production between the subsystems.

[0039] 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 the outlet airflow temperature of the air compressor 1 in the energy storage stage through the compressor-stage aftercooler 2 and utilizes it in the process of heating the inlet airflow at the input end of the expander 5 in the energy release stage, thereby realizing energy heat supplement and heat recovery within the same subsystem, which helps to increase the inlet temperature of the expansion work of the air energy storage subsystem, thereby greatly improving the power generation efficiency of the air energy storage system. The specific composition and working principle of the synthetic heat recovery loop set in the air energy storage subsystem are described in detail in the subsequent content and will not be repeated here.

[0040] In some embodiments, Figure 1 As shown, the synthetic ammonia 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 in sequence to form a reaction process for preparing ammonia. The nitrogen preparation subsystem is connected to the hydrogen preparation subsystem, and the nitrogen preparation subsystem and the hydrogen preparation subsystem are both connected to the ammonia synthesis tower 14, so that the nitrogen preparation subsystem is used to introduce compressed air from the air energy storage subsystem to prepare nitrogen, and the hydrogen preparation subsystem can be used to prepare hydrogen, and then the prepared nitrogen and hydrogen are introduced into the ammonia synthesis tower 14 to participate in the synthesis reaction to prepare ammonia, so that the synthetic ammonia subsystem and the air energy storage subsystem are coupled and associated through the nitrogen preparation subsystem, and the efficient co-production of the synthetic ammonia subsystem and the air energy storage subsystem is achieved through the joint action of the nitrogen preparation subsystem and the hydrogen preparation subsystem. In this process, the nitrogen prepared by compressed air, the intermediate product of the air energy storage subsystem, can be used as a raw material for the synthetic ammonia subsystem to participate in the synthesis reaction. The ammonia storage tank 19 is connected to the synthetic ammonium bicarbonate subsystem, thereby coupling the synthetic ammonia subsystem with the synthetic ammonium bicarbonate subsystem, and using the final product ammonia of the synthetic ammonia subsystem as a raw material for the synthetic ammonium bicarbonate subsystem to participate in the synthesis reaction. It can be seen that the above setting can greatly improve the efficient utilization of joint products between systems.

[0041] It should be noted that the synthetic ammonia subsystem adopts a high temperature and high pressure synthesis method. The main reaction occurring in the ammonia synthesis tower is: N2+3H2→2NH3. The temperature of the synthetic ammonia reactor is preferably controlled at 400°C to 500°C.

[0042] In some specific embodiments, 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 synthetic heat recovery loops. That is, the synthetic ammonia subsystem recovers the high temperature after the ammonia synthesis reaction and utilizes it in the process of heating the inlet airflow of the expander 5 of the air energy storage subsystem during the energy release stage, thereby realizing energy heat supplement and heat recovery between different subsystems of co-production, which helps to increase the inlet temperature of the expansion work of the air energy storage subsystem, thereby greatly improving the power generation efficiency of the air energy storage system. The specific composition and working principle of the synthetic heat recovery loop connected to the synthetic ammonia subsystem are explained in detail in the subsequent content, and will not be repeated here.

[0043] In some specific embodiments, Figure 1 As shown, the hydrogen preparation subsystem includes an electrolyzer 10 and a hydrogen storage tank 11. The input end of the electrolyzer 10 is connected to a water source, the output end of the electrolyzer 10 is connected to the hydrogen storage tank 11, and the hydrogen storage tank 11 is connected to the ammonia synthesis tower 14. The electrolyzer 10 introduces clean water resources 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 it is difficult to store gaseous co-products on a large scale, and hydrogen is a flammable gas, large-scale storage is prone to danger, so the hydrogen in the hydrogen storage tank 11 is passed into the ammonia synthesis tower 14 for consumption as soon as possible, which can reduce the danger of large-scale storage of hydrogen and improve the safety of system operation.

[0044] In some specific embodiments, 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 through the air separation device 8, and the air separation device 8 is used to separate part of the compressed air in the compressed air storage tank 3 to generate nitrogen. 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 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 preheat the mixture of hydrogen and nitrogen to improve the synthesis reaction efficiency and synthesis sufficiency in the ammonia synthesis tower 14.

[0045] In some specific embodiments, Figure 1As shown, the synthetic ammonia subsystem also includes an ammonia separator 18. The ammonia cooler 17 is connected to the ammonia storage tank 19 through the ammonia separator 18. The ammonia separator 18 is provided with 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 the nitrogen preparation subsystem and the synthetic methanol 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 the buffer tank 13, so as to separate and introduce the unreacted hydrogen in the prepared ammonia, recycle and input into the buffer tank 13 to be fully mixed with nitrogen for preheating, so as to realize 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 synthetic methanol reactor 26 of the synthetic methanol subsystem, so as to separate the unreacted hydrogen in the prepared ammonia, and can be introduced into the synthetic methanol reactor 26 as the raw material of the synthetic methanol subsystem to participate in the synthesis reaction of methanol, thereby realizing the coupling connection between the synthetic ammonia subsystem and the synthetic methanol subsystem, and further realizing reliable and efficient co-production between the two subsystems.

[0046] In some embodiments, Figure 1 As shown, the synthetic methanol subsystem includes a synthetic methanol reactor 26, a third heat exchanger 27, a methanol separator 28, a methanol distillation tower 29 and a methanol storage tank 30. The synthetic methanol reactor 26, the third heat exchanger 27, the methanol separator 28, the methanol distillation tower 29 and the methanol storage tank 30 are connected in sequence to form a reaction process for preparing methanol. The synthetic methanol reactor 26 is connected to the carbon dioxide capture subsystem to achieve reliable capture of carbon dioxide and use carbon dioxide as a raw material for methanol preparation. The input end of the synthetic methanol reactor 26 is respectively connected to the hydrogen storage tank 11 and the carbon dioxide storage tank 21 of the carbon dioxide capture subsystem. The hydrogen storage tank 11 and the carbon dioxide storage tank 21 respectively input hydrogen and carbon dioxide into the synthetic methanol reactor 26, so that the hydrogen and carbon dioxide in the synthetic methanol reactor 26 react to prepare methanol. The prepared methanol is cooled by the second heat exchanger 15 and then enters the methanol separator 28. The methanol separator 28 separates a portion of the unreacted water in the prepared methanol, thereby increasing the methanol concentration. The separated methanol and water are passed into the methanol distillation tower 29 to obtain methanol with a higher concentration through distillation. The methanol is finally stored in the methanol storage tank 30 in a safer liquid form.

[0047] It should be noted that the methanol synthesis subsystem uses carbon dioxide and hydrogen to synthesize methanol in a one-step process. The main reaction in the methanol synthesis reactor is: CO2+3H2→CH3OH+H2O. The temperature of the methanol synthesis reactor 26 is preferably controlled at 200 degrees Celsius to 300 degrees Celsius.

[0048] In some specific embodiments, the methanol separator 28 is provided with 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 tower 29. The separation output end of the methanol separator 28 is connected to the synthetic methanol reactor 26 and the hydrogen preparation 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 synthetic methanol reactor 26, so that the recovered hydrogen is re-introduced into the methanol reactor to participate in the reaction of synthesizing methanol, and energy recovery and utilization within the same subsystem is realized. Preferably, the separation output end of the methanol separator 28 is connected to the input end of the buffer tank 13 of the hydrogen preparation subsystem, so that the unreacted hydrogen in the prepared ammonia is separated and introduced, and is re-recovered and input into the buffer tank 13 to be fully mixed and preheated with nitrogen, so as to realize the coupling connection between the synthetic methanol subsystem and the hydrogen preparation subsystem, that is, to realize the coupling connection between the synthetic methanol subsystem and the synthetic ammonia subsystem, and then realize the reliable and efficient co-production between the three subsystems of co-production.

[0049] In some specific embodiments, the methanol distillation tower 29 is provided with an input end, an output end and a distillation output end. The input end of the methanol distillation tower 29 is connected to the output end of the methanol separator 28. The output end of the methanol distillation tower 29 is connected to the methanol storage tank 30. The distillation output end of the methanol distillation tower 29 is respectively connected to the hydrogen preparation subsystem and the synthetic ammonium bicarbonate subsystem. The methanol distillation tower 29 is used to distill water from methanol. Preferably, the distillation output end of the methanol distillation tower 29 is connected to the input end of the electrolyzer 10 of the hydrogen preparation subsystem, so as to recover the byproduct water in the synthetic methanol subsystem and replenish it into the hydrogen preparation subsystem, improve the output and efficiency of hydrogen preparation, and realize the coupling connection between the synthetic methanol subsystem and the hydrogen preparation subsystem, that is, realize the coupling connection between the synthetic methanol subsystem and the synthetic ammonia subsystem, and then realize the reliable and efficient co-production between the three subsystems of co-production. Preferably, the distillation output end of the methanol distillation tower 29 is connected to the input end of the ammonium bicarbonate reactor 22 of the synthetic ammonium bicarbonate subsystem, so that the by-product water in the synthetic methanol subsystem can be recovered and introduced into the ammonium bicarbonate reactor 22 as a raw material participating in the ammonium bicarbonate synthesis reaction, thereby realizing the coupling connection between the synthetic methanol subsystem and the synthetic ammonium bicarbonate subsystem, and further realizing reliable and efficient co-production between the two subsystems.

[0050] 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 synthetic heat recovery loops. That is, the synthetic methanol subsystem recovers the high temperature after the methanol synthesis reaction and utilizes it in the process of heating the inlet airflow of the expander 5 of the air energy storage subsystem during the energy release stage, thereby realizing energy heat supplement and heat recovery between different subsystems of co-production, which helps to increase the inlet temperature of the expansion work of the air energy storage subsystem, thereby greatly improving the power generation efficiency of the air energy storage system. The specific composition and working principle of the synthetic heat recovery loop connected to the synthetic methanol subsystem are described in detail in the subsequent content and will not be repeated here.

[0051] In some embodiments, Figure 1 As shown, the synthetic ammonium bicarbonate subsystem includes an ammonium bicarbonate reactor 22, a crystallizer 23, a three-in-one filter device 24 and an ammonium bicarbonate storage tank 25. The ammonium bicarbonate reactor 22, the crystallizer 23, the three-in-one filter device 24 and the ammonium bicarbonate storage tank 25 are connected in sequence to form a reaction process for preparing ammonium bicarbonate. The input end of the ammonium bicarbonate reactor 22 is respectively connected to a methanol distillation tower 29, a carbon dioxide capture subsystem and an ammonia storage tank 19. The water generated by the methanol distillation tower 29 is passed into the ammonium bicarbonate reactor 22, the carbon dioxide captured and stored in the carbon dioxide capture subsystem can be passed into the ammonium bicarbonate reactor 22, and the ammonia stored in the ammonia storage tank 19 can be passed into the ammonium bicarbonate reactor 22. Water, carbon dioxide and ammonia fully react in the ammonium bicarbonate reactor 22 to generate ammonium bicarbonate. The crystallizer 23 is used to concentrate and crystallize the ammonium bicarbonate generated by the reaction. The three-in-one filtering 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.

[0052] It should be noted that in the above-mentioned ammonium bicarbonate synthesis subsystem, the main reaction occurring in the ammonium bicarbonate reactor is: NH3+H2O+CO2→NH4HCO3.

[0053] 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 can capture carbon dioxide from an external carbon dioxide source such as tail gas from a chemical plant, tail gas from biomass combustion, and other tail gas enriched with carbon dioxide, and store the carbon dioxide in the carbon dioxide storage tank 21. The carbon dioxide storage tank 21 is respectively connected to the synthetic methanol reactor 26 of the synthetic methanol subsystem and the ammonium bicarbonate reactor 22 of the synthetic ammonium bicarbonate subsystem, so as to transport carbon dioxide for the methanol synthesis reaction and the ammonium bicarbonate synthesis reaction.

[0054] It should be noted that the above-mentioned hydrogen preparation subsystem's process of preparing hydrogen through water electrolysis and the carbon dioxide capture process of the carbon dioxide capture subsystem both require the consumption of a large amount of electricity resources. Therefore, incorporating the hydrogen preparation subsystem and the carbon dioxide capture subsystem into the integrated system and coupling them with the air energy storage subsystem can achieve complementary advantages among the co-production subsystems and improve the overall work efficiency of the integrated system.

[0055] In some specific embodiments, Figure 1 As shown, each synthetic heat recovery loop includes a high-temperature heat storage medium storage tank and a low-temperature heat storage medium storage tank. The output end of the high-temperature heat storage medium storage tank is connected to the input end of the low-temperature heat storage medium storage tank through the heat release side of the first heat exchanger 4, and the output end of the low-temperature heat storage medium storage tank is connected to the input end of the high-temperature heat storage medium storage tank through the heat absorption side of each subsystem heat exchanger of the co-production. This setting can realize the reliable flow of the heat storage medium in the synthetic heat recovery loop, realize reliable heat exchange and energy recovery, and transport the heat from the heat exchangers of each subsystem to the first heat exchanger 4 of the air energy storage subsystem, thereby maximizing the inlet temperature of the expansion work of the air energy storage subsystem, thereby greatly improving the power generation efficiency of the air energy storage system.

[0056] It should be noted that each subsystem heat exchanger includes at least one of the compressor stage aftercooler 2, the second heat exchanger 15 of the synthetic ammonia subsystem, and the third heat exchanger 27 of the synthetic methanol subsystem. That is, part of the inlet heat of the compressed air expansion work in the energy release stage of the air energy storage subsystem comes from the compression heat of the energy storage stage recovered inside the same subsystem, part of it comes from the heat of the outlet high-temperature gas at the output end of the ammonia synthesis tower 14, and part of it comes from the heat of the outlet high-temperature gas at the output end of the synthetic methanol reactor 26.

[0057] In some specific embodiments, the at least one group of synthetic heat recovery loops includes a first heat recovery loop, a second heat recovery loop, and a third heat recovery loop.

[0058] Corresponding to the above-mentioned air energy storage subsystem, the compressor-stage aftercooler 2 is connected to the first heat exchanger 4 through the 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 through the heat absorption side of the compressor-stage aftercooler 2, and the heat release side of the compressor-stage aftercooler 2 is connected to the energy storage pipeline of the air energy storage subsystem, and the two ends of the energy storage pipeline are respectively connected to the output end of the air compressor 1 and the input end of the compressed air storage tank 3. 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 through 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, and the two ends of the energy release pipeline are respectively connected to the compressed air storage tank 3 and the input end of the expander 5. This setting utilizes the low-temperature heat storage medium to flow through the heat absorption side of the compressor stage aftercooler 2, thereby absorbing the compression heat of the air energy storage subsystem during the energy storage stage and storing it in the first high-temperature heat storage medium tank 6; then the high-temperature heat storage medium is used to flow through the first heat release side of the first heat exchanger 4, thereby releasing the compression heat to the air energy storage subsystem during the energy release stage, thereby increasing the inlet temperature of the expansion work of the air energy storage subsystem, thereby greatly improving the power generation efficiency of the air energy storage system.

[0059] Corresponding to the above-mentioned synthetic ammonia subsystem, the second heat exchanger 15 is connected to the first heat exchanger 4 through the second heat recovery loop. Preferably, the output end of the second low-temperature heat storage medium storage tank 31 is connected to the input end of the second high-temperature heat storage medium storage tank 32 through 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, and the two ends of the ammonia synthesis pipeline are respectively connected to the output end of the ammonia synthesis tower 14 and the input end of the ammonia compressor 16. The output end of the second high-temperature heat storage medium storage tank 32 is connected to the input end of the second low-temperature heat storage medium storage tank 31 through the second heat release side of the first heat exchanger 4. This setting utilizes the low-temperature heat storage medium to flow through the heat absorption side of the second heat exchanger 15, thereby absorbing the synthesis heat during the ammonia synthesis process and storing it in the second high-temperature heat storage medium storage tank 32; then the high-temperature heat storage medium is used to flow through the second heat release side of the first heat exchanger 4, so as to release the compression heat to the air energy storage subsystem in the energy release stage, thereby increasing the inlet temperature of the expansion work of the air energy storage subsystem, thereby greatly improving the power generation efficiency of the air energy storage system.

[0060] Corresponding to the above-mentioned synthetic methanol subsystem, the third heat exchanger 27 is connected to the first heat exchanger 4 through the third heat recovery loop. Preferably, the output end of the third low-temperature heat storage medium storage tank 33 is connected to the input end of the third high-temperature heat storage medium storage 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, and the two ends of the methanol synthesis pipeline are respectively connected to the output end of the synthetic methanol reactor 26 and the input end of the methanol separator. The output end of the third high-temperature heat storage medium storage tank 34 is connected to the input end of the third low-temperature heat storage medium storage tank 33 through the third heat release side of the first heat exchanger 4. This setting utilizes the low-temperature heat storage medium to flow through the heat absorption side of the third heat exchanger 27, thereby absorbing the synthesis heat during the methanol synthesis process and storing it in the third high-temperature heat storage medium storage tank 34; then the high-temperature heat storage medium is used to flow through the third heat release side of the first heat exchanger 4, so as to release the compression heat to the air energy storage subsystem in the energy release stage, increase the inlet temperature of the expansion work of the air energy storage subsystem, and thus greatly improve the power generation efficiency of the air energy storage system.

[0061] An embodiment of the present invention provides an integrated method for air energy storage and co-production of ammonium bicarbonate and methanol. The integrated method can be performed using the above-mentioned integrated system. The integrated method provided by the present invention is described in detail below. The integrated method described below and the integrated system described above can be referenced to each other.

[0062] 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, the air energy storage subsystem is used to prepare compressed air. In the energy release stage, the compressed air is heated and expanded to generate power. The ammonia synthesis step uses the compressed air prepared in the air energy storage and power transmission step to prepare nitrogen, and uses the synthetic ammonia subsystem to react nitrogen and hydrogen to synthesize ammonia. The methanol synthesis step uses the synthetic methanol subsystem to react carbon dioxide and hydrogen to synthesize methanol, and separates and extracts water from methanol. In the ammonium bicarbonate synthesis step, the synthetic ammonium bicarbonate subsystem is used 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 various steps corresponding to the above-mentioned integrated system and associating various steps, the integrated method has all the advantages of the above-mentioned integrated system, and the details are not repeated here.

[0063] Each step of the integration method of this embodiment is executed by each subsystem of the above-mentioned integration system. The operation principle of the above-mentioned integration system in the process of executing the integration method is as follows.

[0064] In the air energy storage and power transmission step, the air energy storage subsystem is in the energy storage stage, using off-peak electricity such as wind power and photovoltaic power as power input, controlling the air source to send the purified air into the air compressor 1, and the air is compressed to a high temperature and high pressure state in the air compressor 1, and then the compression heat is recovered through the compressor stage aftercooler 2, and the cooled air is stored in the compressed air storage tank 3. The air energy storage subsystem is in the energy release stage, and the compressed air in the compressed air storage tank 3 is heated by the first heat exchanger 4, and then enters the expander 5 to expand and do work, thereby driving the generator to generate electricity.

[0065] 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, and the air separation device 8 separates nitrogen from the compressed air and stores the nitrogen in the nitrogen storage tank 9. The electrolyzer 10 prepares hydrogen and oxygen from clean water by electrolysis, stores the prepared hydrogen in the hydrogen storage tank 11, and stores the prepared oxygen in the oxygen storage tank 12. The nitrogen in the sighing tank and the hydrogen in the hydrogen storage tank 11 are both input into the buffer tank 13 for mixing and preheating, and then the mixed gas is passed into the ammonia synthesis tower 14, and the reaction temperature of the ammonia synthesis tower 14 is controlled at 400 degrees Celsius to 500 degrees Celsius. The mixed gas in the ammonia synthesis tower 14 fully reacts to generate high-temperature gas, which 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 be cooled and then enters the ammonia separator 18, which separates the unreacted hydrogen from the ammonia for recycling, and stores the cooled liquid ammonia in the ammonia storage tank 19.

[0066] In the methanol synthesis step, the tail gas enriched with carbon dioxide, such as the tail gas of chemical plants and the tail gas of biomass combustion, is rich in carbon dioxide. The integrated system uses the carbon dioxide capture device 20 to capture the carbon dioxide and stores it in the carbon dioxide storage tank 21. The hydrogen in the hydrogen storage tank 11 and the carbon dioxide in the carbon dioxide storage tank 21 are both introduced into the synthetic methanol reactor 26, and the temperature of the synthetic methanol reactor 26 is controlled at 200 degrees Celsius to 300 degrees Celsius. The outlet high-temperature gas at the output end of the synthetic methanol reactor 26 is cooled by the third heat exchanger 27 and enters the methanol separator 28. The methanol separator 28 separates the unreacted hydrogen from the methanol as a raw material to participate in the next methanol synthesis reaction; the remaining methanol and water enter the methanol distillation tower 29, and the methanol distilled by the methanol distillation tower 29 is stored in the methanol storage tank 30. The water separated by the methanol distillation tower 29 is treated and then re-enters at least one of the electrolyzer 10 and the ammonium bicarbonate reactor 22 for recycling.

[0067] In the ammonium bicarbonate synthesis step, the water produced in the above-mentioned co-production subsystem is first introduced into the ammonium bicarbonate reactor 22, and then the ammonia produced in the above-mentioned co-production subsystem is introduced into the ammonium bicarbonate reactor 22 to form ammonia water, and then the carbon dioxide produced in the above-mentioned co-production subsystem is introduced into the ammonium bicarbonate reactor 22 containing ammonia water to form an ammonium bicarbonate product, such as an ammonium bicarbonate reaction solution. The ammonium bicarbonate in the ammonium bicarbonate reaction solution is concentrated and crystallized by a crystallizer 23, and the obtained product is filtered, washed, and dried by a three-in-one filter device 24 and stored in an ammonium bicarbonate storage tank 25.

[0068] In the synthesis heat recovery step, synthesis heat recovery is performed between the above-mentioned co-production subsystems. Preferably, the air energy storage subsystem realizes the recovery and utilization of compression heat within the same subsystem through the first heat recovery loop during the energy storage stage and the energy release stage. Preferably, the synthetic ammonia subsystem recycles the reaction synthesis heat through the second heat recovery loop and reuses it in the energy release stage of the air energy storage subsystem. Preferably, the synthetic methanol subsystem recycles the reaction synthesis heat through the third heat recovery loop and reuses it in the energy release stage of the air energy storage subsystem. That is, part of the heat absorbed by the compressed air in the air energy storage subsystem during the energy release stage comes from the compression heat recovered inside the subsystem; the other part comes from the heat of the high-temperature gas at the outlet of the synthetic ammonia reactor and the high-temperature gas at the outlet of the synthetic methanol reactor 26.

[0069] The heat recovery process between the co-generation subsystems is as follows. In the energy storage stage, the outlet high-temperature gas of the ammonia synthesis tower 14 in the synthetic ammonia subsystem exchanges heat with the heat storage medium in the second heat exchanger 15, and the heated heat storage medium is stored in the second high-temperature heat storage medium storage tank 32; the outlet high-temperature gas of the methanol reactor in the synthetic methanol subsystem exchanges heat with the heat storage medium in the third heat exchanger 27, and the heated heat storage medium is stored in the third high-temperature heat storage medium storage tank 34. In the energy release stage, the second high-temperature heat storage medium storage tank 32 and the third high-temperature heat storage medium storage tank 34 respectively input the corresponding heat storage medium into the first heat exchanger 4 for heating the compressed air before the inlet of the input end of the expander 5, thereby improving the inlet temperature of the expander 5 and the power generation efficiency.

[0070] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or make equivalent replacements for some of the technical features therein. However, these modifications or replacements do not deviate the essence of the corresponding technical solutions 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 a power grid, wherein the air energy storage subsystem can generate compressed air during the energy storage phase and utilize the compressed air to expand and perform work to transmit electricity to the power grid during the energy release phase; A synthetic ammonia subsystem, connected to the air energy storage subsystem, the synthetic ammonia subsystem can utilize hydrogen and nitrogen generated from compressed air to react and prepare ammonia; A synthetic methanol subsystem connected to the synthetic ammonia subsystem, the synthetic methanol subsystem can synthesize methanol by reacting carbon dioxide with hydrogen, and can separate and extract water from methanol; An ammonium bicarbonate synthesis subsystem is connected to the ammonia synthesis subsystem and the methanol synthesis subsystem respectively, and the ammonium bicarbonate synthesis subsystem can produce ammonium bicarbonate by reacting water, carbon dioxide and ammonia; The synthetic ammonia subsystem and the synthetic methanol subsystem are respectively connected to the air energy storage subsystem via at least one set of synthetic heat recovery loops.

2. The integrated system for air energy storage and co-production of ammonium bicarbonate and methanol according to claim 1 is characterized in that: 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, wherein 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 in sequence, 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 synthetic ammonia subsystem via a nitrogen preparation subsystem; The compressor stage aftercooler is connected to the heat-releasing side of the first heat exchanger via at least one set of the synthetic heat recovery circuits.

3. The integrated system for air energy storage and co-production of ammonium bicarbonate and methanol according to claim 2 is characterized in that: The synthetic ammonia subsystem comprises an ammonia synthesis tower, a second heat exchanger, an ammonia compressor, an ammonia cooler and an ammonia storage tank, wherein the ammonia synthesis tower, the second heat exchanger, the ammonia compressor, the ammonia cooler and the ammonia storage tank are connected in sequence; 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 synthetic ammonium bicarbonate subsystem; The second heat exchanger is connected to the heat release side of the first heat exchanger through at least one set of the synthetic heat recovery circuits.

4. The integrated system for air energy storage and co-production of ammonium bicarbonate and methanol according to claim 3 is characterized in that: The hydrogen preparation 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.

5. The integrated system for air energy storage and co-production of ammonium bicarbonate and methanol according to claim 3 is 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, and the air separation device is used to separate part of the compressed air in the compressed air storage tank to generate nitrogen; The input end of the buffer tank is connected to the nitrogen storage tank and the hydrogen preparation subsystem, and the output end of the buffer tank is connected to the ammonia synthesis tower. The buffer tank is used to preheat the mixture of hydrogen and nitrogen.

6. The integrated system for air energy storage and co-production of ammonium bicarbonate and methanol according to claim 3, characterized in that: The synthetic ammonia subsystem also 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 synthetic methanol subsystem, and the ammonia separator is used to separate and extract unreacted hydrogen from ammonia.

7. The integrated system for air energy storage and co-production of ammonium bicarbonate and methanol according to claim 3, characterized in that: The synthetic methanol subsystem comprises a synthetic methanol reactor, a third heat exchanger, a methanol separator, a methanol distillation tower and a methanol storage tank, wherein the synthetic methanol reactor, the third heat exchanger, the methanol separator, the methanol distillation tower and the methanol storage tank are connected in sequence; The synthetic methanol reactor is connected to a carbon dioxide capture subsystem; The separation output end of the methanol separator is connected to the synthetic methanol reactor and the hydrogen preparation subsystem, and the methanol separator is used to separate and extract unreacted hydrogen from methanol; The distillation output end of the methanol distillation tower is connected to the hydrogen preparation subsystem and the ammonium bicarbonate synthesis subsystem respectively, and the methanol distillation tower is used to distill methanol to generate water; The third heat exchanger is connected to the heat release side of the first heat exchanger through at least one set of the synthetic heat recovery circuits.

8. The integrated system for air energy storage and co-production of ammonium bicarbonate and methanol according to claim 7, characterized in that: The synthetic ammonium bicarbonate subsystem comprises an ammonium bicarbonate reactor, a crystallizer, a three-in-one filter device and an ammonium bicarbonate storage tank, wherein the ammonium bicarbonate reactor, the crystallizer, the three-in-one filter device and the ammonium bicarbonate storage tank are connected in sequence; The input end of the ammonium bicarbonate reactor is respectively connected to the methanol distillation tower, the carbon dioxide capture subsystem and the ammonia storage tank.

9. The integrated system for air energy storage and co-production of ammonium bicarbonate and methanol according to any one of claims 2 to 8, characterized in that: The synthetic heat recovery loop includes a high-temperature heat storage medium storage tank and a low-temperature heat storage medium storage tank, wherein the output end of the high-temperature heat storage medium storage tank is connected to the input end of the low-temperature heat storage medium storage tank via the heat release side of the first heat exchanger, and the output end of the low-temperature heat storage medium storage tank is connected to the input end of the high-temperature heat storage medium storage tank via the heat absorption side of each subsystem heat exchanger; Each of the subsystem heat exchangers includes at least one of the compressor stage aftercooler, the second heat exchanger of the synthetic ammonia subsystem, and the third heat exchanger of the synthetic methanol subsystem.

10. An integrated method for air energy storage and co-production of ammonium bicarbonate and methanol, characterized in that: The method is implemented by using the integrated system for co-producing ammonium bicarbonate and methanol by air energy storage as described in any one of claims 1 to 9; The integrated method for air energy storage and co-production of ammonium bicarbonate and methanol comprises: The air energy storage and power transmission step includes an energy storage stage and an energy release stage. The energy storage stage uses the air energy storage subsystem to prepare compressed air. The energy release stage heats the compressed air and then expands it to perform work to generate electricity. an ammonia synthesis step, using the compressed air prepared in the air energy storage and power transmission step to prepare nitrogen, and using a synthetic ammonia subsystem to react nitrogen and hydrogen to synthesize ammonia; A methanol synthesis step, using the methanol synthesis subsystem to react carbon dioxide with hydrogen to synthesize methanol, and separating and extracting water from the methanol; an ammonium bicarbonate synthesis step, using an 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 synthetic 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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