Cold heat electricity hydrogen carbon co-production system and method based on transcritical carbon dioxide energy storage

Abstract

The application discloses a cold-heat-electricity-hydrogen-carbon co-production system and method based on cross-critical carbon dioxide energy storage, and the method is as follows: carbon dioxide is compressed by a carbon dioxide compressor set and then enters an expander set to work and generate electricity; heat energy generated in the carbon dioxide compression process provides heat for a methanol water vapor reforming hydrogen production process and a methanol cracking hydrogen production process through a first heat exchanger and a second heat exchanger respectively; a solar power generation unit generates electricity to provide electric energy for the carbon dioxide compressor set, a methanol water vapor reforming hydrogen production reactor and a methanol cracking hydrogen production reactor; carbon dioxide generated in the methanol water vapor reforming hydrogen production is input into the carbon dioxide compressor set; carbon monoxide generated in the methanol cracking hydrogen production is combusted to generate high-temperature flue gas, and the high-temperature flue gas provides heat for the expansion of compressed carbon dioxide in the expander set; the carbon dioxide compression provides heat energy for a hydrogen production reaction of methanol, and solar power generation provides electric energy for the hydrogen production of methanol, so that the system energy consumption is reduced, and carbon monoxide is consumed in the system.

Description

Technical Field

[0001] This invention belongs to the field of multi-energy coupled energy storage cogeneration technology, specifically relating to a cogeneration system and method for cooling, heating, power, hydrogen and carbon based on transcritical carbon dioxide energy storage. Background Technology

[0002] Compared to air, carbon dioxide has a moderate critical pressure and a relatively high critical temperature (7.38 MPa, 30.98 °C), making it easier to achieve a liquid or supercritical state. Liquid and supercritical carbon dioxide have high densities, significantly reducing storage volume; therefore, using it as a storage medium is beneficial for improving system energy density. Current compressed carbon dioxide energy storage systems suffer from insufficient utilization of low-grade compression heat and require low-pressure storage tanks, hindering system efficiency and economic viability. Hydrogen possesses advantages such as high density, cleanliness, and no pollution, making hydrogen production and storage a current research hotspot. Methanol is abundant, inexpensive, and easy to store and transport as a liquid at ambient temperature and pressure. Compared to other hydrogen production methods, such as industrial hydrogen production, methanol-based hydrogen production has lower energy consumption and cost. However, the methanol-to-hydrogen reaction requires significant heat absorption, increasing energy consumption. The transportation of carbon monoxide produced by methanol cracking also increases transportation costs, impacting the economics of hydrogen production. Summary of the Invention

[0003] To address the problems existing in the prior art, this invention provides a combined cooling, heating, electricity, hydrogen, and carbon production system and method based on transcritical carbon dioxide energy storage. By coupling a transcritical carbon dioxide energy storage system, a methanol steam reforming hydrogen production system, a methanol cracking hydrogen production system, and a jet refrigeration system, the system achieves full utilization of the low-grade compression heat of the transcritical carbon dioxide energy storage system, avoids the use of low-pressure storage tanks, and enables on-site utilization of carbon monoxide generated from cracking. It also has the advantages of combined cooling, heating, electricity, hydrogen, and carbon production, significantly improving the system's economy and energy storage density.

[0004] To achieve the above objectives, the technical solution adopted in this invention is: a method for combined cooling, heating, power, hydrogen, and carbon production based on transcritical carbon dioxide energy storage. Carbon dioxide is compressed from ambient temperature and pressure to a supercritical state by a carbon dioxide compressor unit and stored in a carbon dioxide storage tank. The supercritical carbon dioxide enters an expander unit from the carbon dioxide storage tank to generate electricity. The heat generated during the carbon dioxide compression process provides heat to the methanol steam reforming hydrogen production process and the methanol cracking hydrogen production process through a first heat exchanger and a second heat exchanger, respectively. A solar power generation unit generates electricity to provide power to the carbon dioxide compressor unit, the methanol steam reforming hydrogen production reactor, and the methanol cracking hydrogen production reactor. The carbon dioxide produced by the methanol steam reforming hydrogen production process is input into the carbon dioxide compressor unit, and the carbon monoxide produced by the methanol cracking hydrogen production process is burned to generate high-temperature flue gas. The high-temperature flue gas provides heat to the expanded carbon dioxide in the expander unit for expansion and energy release through a heat exchanger.

[0005] Furthermore, the product temperatures of the methanol steam reforming and methanol cracking hydrogen production reactions are 200℃-300℃. The hydrogen produced by these reactions is stored. The heat energy carried by the hydrogen from these reactions heats water into high-temperature steam via a heat exchanger, providing energy for the jet refrigeration unit. Hydrogen undergoes countercurrent heat exchange in the heat exchanger. The low-pressure, low-temperature steam and the high-pressure, high-temperature steam are mixed by an ejector and then condensed. The condensed water is divided into two parts: one part is pressurized by a booster pump and stored in a water storage tank, while the other part provides cooling for the cold storage.

[0006] Furthermore, after supercritical carbon dioxide expands and generates electricity, it provides heat energy to the compression heat pump unit through a heat exchanger. The carbon dioxide after it has done work exchanges heat in the heat exchanger in a countercurrent manner. The supercritical carbon dioxide exchanges heat with high-temperature flue gas in a countercurrent manner in the expander unit.

[0007] Based on the same inventive concept, this invention also provides a combined cooling, heating, power, hydrogen, and carbon production system based on transcritical carbon dioxide energy storage, including a solar power generation unit, a methanol-to-hydrogen unit, and a carbon dioxide compressor unit, a carbon dioxide storage tank, and an expander unit connected in sequence; the methanol-to-hydrogen unit includes a methanol steam reforming hydrogen production reactor, a methanol cracking hydrogen production reactor, a methanol storage tank, and a methanol-water storage tank; the carbon dioxide compressor unit includes a first heat exchanger and a second heat exchanger, with the methanol steam reforming hydrogen production reactor located at the hot side inlet of the first heat exchanger, and the methanol cracking hydrogen production reactor located at the hot side inlet of the second heat exchanger. The outlet of the alcohol-water storage tank is connected in sequence to the cold side of the first heat exchanger and the methanol steam reforming hydrogen production reactor; the outlet of the methanol storage tank is connected in sequence to the cold side of the second heat exchanger and the methanol cracking hydrogen production reactor; the power output of the solar power generation unit is connected to the power input of the carbon dioxide compressor unit, the methanol steam reforming hydrogen production reactor, and the methanol cracking hydrogen production reactor; a heat exchanger is installed in the expander unit, the combustion chamber outlet is connected to the hot side inlet of the heat exchanger in the expander unit, the carbon monoxide outlet of the methanol hydrogen production unit is connected to the inlet of the combustion chamber; the carbon dioxide outlet of the methanol hydrogen production unit is connected to the air inlet of the carbon dioxide compressor unit.

[0008] Furthermore, it also includes a jet refrigeration unit, which includes an ejector, a condenser, a first throttling valve, and a cold storage unit connected in sequence; the outlet of the condenser is also connected in sequence to a booster water pump, a water storage tank, and a heat exchanger, and the outlet of the heat exchanger is connected to the inlet of the ejector; the outlet of the methanol steam reforming hydrogen production reactor is equipped with a first separator and a heat exchanger, the outlet of the methanol cracking hydrogen production reactor is equipped with a second separator and a heat exchanger, and the water storage tank is equipped with two outlets that are respectively connected to the heat exchangers at the outlets of the methanol steam reforming hydrogen production reactor and the methanol cracking hydrogen production reactor.

[0009] Furthermore, the outlet of the first separator is also connected to the outlet of the methanol-water storage tank or the cold-side inlet of the first heat exchanger, and the outlet of the methanol cracking hydrogen production reactor is also connected to the cold-side inlet of the second heat exchanger or the outlet of the methanol storage tank.

[0010] Furthermore, the compression heat pump unit includes a seventh heat exchanger, a gas-liquid separator, a third compressor, a heating module, a liquid storage tank, and a second throttle valve connected in sequence. The hot-side inlet of the seventh heat exchanger is connected to the gas outlet of the expander unit.

[0011] Furthermore, the methanol steam reforming hydrogen production reactor adopts a shell-and-tube reactor, including a spiral flow channel, flow channel baffle, electromagnetic induction core, catalyst, electromagnetic induction coil, outer reactor tube, and inner reactor tube; the electromagnetic induction core is installed in the inner reactor tube, and the catalyst is filled in the gap between the inner reactor tube and the electromagnetic induction core; the flow channel is divided into a spiral flow channel between the outer reactor tube and the inner reactor tube by the flow channel baffle; the electromagnetic induction coil is wound around the outer wall of the outer reactor tube; the methanol cracking hydrogen production reactor and the methanol steam reforming hydrogen production reactor adopt the same structure.

[0012] Furthermore, the electromagnetic induction core inside the reactor inner tube is evenly distributed radially, and the length of the electromagnetic induction core gradually decreases from the inner circle to the outer circle; the reactor outer tube is made of heat insulation material, and the reactor inner tube and flow channel baffle are made of heat-conducting material; the slope of the reactor inner tube and reactor outer tube gradually increases from the reactor inlet to the reactor outlet.

[0013] Compared with the prior art, the present invention has the following beneficial technical effects:

[0014] This invention couples transcritical carbon dioxide energy storage, methanol steam reforming for hydrogen production, and methanol cracking for hydrogen production, achieving energy storage while simultaneously producing hydrogen and carbon. The methanol reforming and methanol cracking reactors are heated by a high-temperature carbon dioxide external heat source and internal electric heating. Solar energy is used to power the carbon dioxide compressor unit, the methanol steam reforming reactor, and the methanol cracking reactor, reducing wind and solar power curtailment and improving energy utilization. The carbon dioxide produced by the methanol reforming reaction is used as the energy storage medium, and the carbon dioxide can be sold after energy release, increasing system revenue while avoiding investment in low-pressure carbon dioxide storage tanks, significantly improving system economics.

[0015] Furthermore, both the methanol reforming hydrogen production reactor and the methanol cracking hydrogen production reactor use electromagnetic induction internal heat source heating, which can effectively prevent the "cold spot effect" of the reactor and ensure that the catalyst is heated evenly throughout, which is beneficial to improving hydrogen production efficiency.

[0016] Furthermore, the electromagnetic induction cores are densely distributed at the reactor inlet, and the spiral pipe has a gentle slope, thus providing more heat at the reactor inlet where more heat is absorbed and less heat at the outlet where less heat is absorbed, making rational use of the heat source and further improving the reactor efficiency.

[0017] Furthermore, the carbon monoxide produced by the methanol cracking reaction is briefly stored and then burned in the combustion chamber to provide heat for the high-pressure carbon dioxide, thus achieving on-site consumption of carbon monoxide, avoiding transportation, and helping to improve the system's economic efficiency.

[0018] Furthermore, the system can achieve combined cooling, heating, electricity, hydrogen, and carbon production, making full use of resources and exhibiting high economic efficiency.

[0019] Furthermore, the electromagnetic induction cores in the methanol steam reforming hydrogen production reactor and the methanol cracking hydrogen production reactor are uniformly distributed to prevent the "cold spot effect" of the reactor. Attached Figure Description

[0020] Figure 1 This is a combined cooling, heating, power, hydrogen, and carbon production system based on transcritical carbon dioxide energy storage.

[0021] Figure 2 This is a front cross-sectional view of a reactor designed according to the present invention.

[0022] Figure 3 This is a front view of a reactor designed according to the present invention.

[0023] Figure 4 This is a top view of a reactor designed according to the present invention.

[0024] In the attached diagram: 1. Solar power generation unit; 2. First compressor; 3. Methanol-water vapor reforming hydrogen production reactor; 4. First heat exchanger; 5. Second compressor; 6. Methanol cracking hydrogen production reactor; 7. Second heat exchanger; 8. Carbon dioxide storage tank; 9. Third heat exchanger; 10. First expander; 11. Fourth heat exchanger; 12. Second expander; 13. Fifth heat exchanger; 14. Methanol-water storage tank; 15. Water storage tank; 16. Sixth heat exchanger; 17. Ejector; 18. Condenser; 19. First throttle valve; 2 0. Cold storage; 21. Booster pump; 22. Methanol storage tank; 23. Carbon monoxide storage tank; 24. Combustion chamber; 25. Seventh heat exchanger; 26. Third compressor; 27. Heating module; 28. Second throttle valve; 29. ​​Liquid storage tank; 30. First separator; 31. Second separator; 32. Gas-liquid separator; 33. Power grid; 34. Spiral flow channel; 35. Flow channel baffle; 36. Electromagnetic induction core; 37. Catalyst; 38. Electromagnetic induction coil; 39. Reactor outer tube; 40. Reactor inner tube. Detailed Implementation

[0025] The present invention will now be described in detail with reference to specific embodiments and accompanying drawings.

[0026] This invention couples a transcritical carbon dioxide energy storage system, a methanol steam reforming hydrogen production system, a methanol cracking hydrogen production system, and a jet refrigeration system. This achieves full utilization of the low-grade compression heat of the transcritical carbon dioxide energy storage system, avoids the use of low-pressure storage tanks, and enables on-site utilization of carbon monoxide generated during cracking. It offers the advantages of combined cooling, heating, electricity, hydrogen, and carbon production, significantly improving the system's economics and energy density. Simultaneously, this invention designs a novel methanol steam reforming hydrogen production reactor and a methanol cracking hydrogen production reactor, further enhancing hydrogen production efficiency.

[0027] like Figure 1 As shown, a combined cooling, heating, power, hydrogen, and carbon production system based on transcritical carbon dioxide energy storage includes a transcritical carbon dioxide energy storage unit, a methanol-to-hydrogen unit, a jet refrigeration unit, and a compression heat pump unit; specifically, it includes a solar power generation unit 1, a first compressor 2, a methanol steam reforming hydrogen production reactor 3, a first heat exchanger 4, a second compressor 5, a methanol cracking hydrogen production reactor 6, a second heat exchanger 7, a carbon dioxide storage tank 8, a third heat exchanger 9, a first expander 10, and a fourth heat exchanger 11. The system includes: a second expander 12, a fifth heat exchanger 13, a methanol-water storage tank 14, a water storage tank 15, a sixth heat exchanger 16, an ejector 17, a condenser 18, a first throttle valve 19, a cold storage 20, a booster water pump 21, a methanol storage tank 22, a carbon monoxide storage tank 23, a combustion chamber 24, a seventh heat exchanger 25, a third compressor 26, a heating module 27, a second throttle valve 28, a liquid storage tank 29, a first separator 30, a second separator 31, a gas-liquid separator 32, and a power grid 33.

[0028] The transcritical carbon dioxide energy storage unit includes a compressor unit, a heat exchanger unit, a carbon dioxide storage tank 8, an expander unit, and a combustion chamber 24 connected in sequence. A methanol steam reforming hydrogen production reactor 3 is installed between the outlet of the first compressor 2 and the hot-side inlet of the first heat exchanger 4. The hot-side outlet of the first heat exchanger 4 is connected to the inlet of the second compressor 5. A methanol cracking hydrogen production reactor 6 is installed between the outlet of the second compressor 5 and the hot-side inlet of the second heat exchanger 7. The hot-side outlet of the second heat exchanger 7 is connected in sequence to the carbon dioxide storage tank 8 and the expander unit. The methanol hydrogen production unit includes a methanol steam reforming hydrogen production reactor 3, a methanol cracking hydrogen production reactor 6, a hydrogen transport module, and a carbon monoxide storage tank 2. 3. Methanol storage tank 22 and methanol-water storage tank 14. The cold-side inlet of the first heat exchanger 4 is connected to the methanol-water storage tank 14. The outlet of the methanol-water reforming hydrogen production reactor 3 is sequentially connected to the first separator 30 and the fifth heat exchanger 13. The outlet of the first separator 30 is also connected to the outlet of the methanol-water storage tank 14 or the cold-side inlet of the first heat exchanger 4. The outlet of the methanol storage tank 22 is sequentially connected to the cold-side inlet of the second heat exchanger 7 and the methanol cracking hydrogen production reactor 6. The outlet of the methanol cracking hydrogen production reactor 6 is sequentially connected to the second separator 31 and the sixth heat exchanger 16. The outlet of the methanol cracking hydrogen production reactor 6 is also connected to the cold-side inlet of the second heat exchanger 7 or the outlet of the methanol storage tank 22. A heat exchanger is installed in the expander unit. The outlet of the combustion chamber 24 is connected to the hot-side inlet of the heat exchanger in the expander unit, and the carbon monoxide storage tank 23 is connected to the inlet of the combustion chamber 24.

[0029] The jet refrigeration unit includes an ejector 17, a condenser 18, a first throttle valve 19, and a cold storage 20 connected in sequence; the outlet of the condenser 18 is also connected in sequence to a booster water pump 21, a water storage tank 15, and a heat exchanger; the compression heat pump unit includes a seventh heat exchanger 25, a gas-liquid separator 32, a third compressor 26, a heating module 27, a liquid storage tank 29, and a second throttle valve 28 connected in sequence, and the hot-side inlet of the seventh heat exchanger 25 is connected to the gas outlet of the expander unit.

[0030] The expander unit includes a third heat exchanger 9, a first expander 10, a fourth heat exchanger 11, and a second expander 12 connected in sequence. Both the first expander 10 and the second expander 12 are connected to a generator. The power output terminal of the generator is connected to the power grid 33. The hot-side inlets of the third heat exchanger 9 and the fourth heat exchanger 11 are connected to the outlet of the combustion chamber 24.

[0031] like Figure 2 The diagram shown is a cross-sectional view of a reactor designed according to the present invention, which specifically includes a spiral flow channel 34, a flow channel baffle 35, an electromagnetic induction iron core 36, a catalyst 37, an electromagnetic induction coil 38, an outer reactor tube 39, and an inner reactor tube 40.

[0032] The methanol steam reforming hydrogen production reactor 3 and the methanol cracking hydrogen production reactor 6 are coaxial reactors. Taking the methanol steam reforming hydrogen production reactor 3 as an example, an electromagnetic induction iron core 36 is installed in the inner tube 40 of the reactor, and a catalyst 37 is filled in the gap between the inner tube 40 and the electromagnetic induction iron core 36. The flow channel between the outer tube 39 of the reactor and the inner tube 40 of the reactor is divided into a spiral flow channel 34 by a flow channel baffle 35. An electromagnetic induction coil 38 is wound around the outer wall of the outer tube of the reactor.

[0033] In a preferred embodiment, the electromagnetic induction core 36 inside the reactor inner tube 40 is evenly distributed radially, and the length of the electromagnetic induction core 36 gradually decreases from the inner ring to the outer ring.

[0034] Furthermore, the slope of the spiral flow channel 34 gradually increases from the reactor inlet to the outlet, and the heat exchange time between the hot fluid and the reactants in the reactor decreases from the inlet to the outlet. That is, the heat exchange time is longer closer to the inlet, thereby enhancing the heat exchange at the inlet and solving the problem of a large reaction rate and a large amount of heat absorption at the reactor inlet.

[0035] The outer tube 39 of the reactor is made of thermal insulation material, while the inner tube 40 and the flow channel baffle 35 are made of thermally conductive material. Both the inner tube 40 and the outer tube 39 are made of non-electromagnetic shielding materials, and therefore do not shield against electromagnetic induction. The electricity generated by the solar power generation unit 1 is converted into alternating current by an inverter to power the electromagnetic induction coil 38.

[0036] The specific operation method of the combined cooling, heating, power, hydrogen, and carbon production system based on transcritical carbon dioxide energy storage described in this invention is as follows:

[0037] During energy storage, the methanol-water in the methanol-water storage tank 14 absorbs heat through the first heat exchanger 4 and then enters the methanol-water steam reforming hydrogen production reactor 3 for reforming and hydrogen production. At this time, solar power generation and high-temperature carbon dioxide simultaneously supply heat to the methanol-water steam reforming hydrogen production reactor 3. After the reforming reaction products are separated by the first separator 30, the unconverted raw materials re-enter the methanol-water steam reforming hydrogen production reactor 3 for reaction. The generated hydrogen and carbon dioxide are released by the fifth heat exchanger 13 and then transported and sold, and enter the first compressor 2, respectively. After being compressed by the first compressor 2, the high-temperature carbon dioxide supplies heat to the methanol-water steam reforming hydrogen production reactor 3, and the heating ends. The liquid methanol-water mixture then enters the first heat exchanger 4 to release heat, converting it into methanol vapor and water vapor. After releasing heat, it enters the second compressor 5 for further compression. The compressed carbon dioxide then sequentially enters the methanol cracking hydrogen production reactor 6 and the second heat exchanger 7 to release heat, before entering the carbon dioxide storage tank 8 for storage. The methanol in the methanol storage tank 22 absorbs heat in the second heat exchanger 7 and becomes gaseous methanol, which then enters the methanol cracking hydrogen production reactor 6. After the cracking products are separated by the second separator 31, the unreacted raw materials enter the methanol cracking hydrogen production reactor 6 for re-reaction. The carbon monoxide and hydrogen produced by cracking are released heat in the sixth heat exchanger 16 and then stored and sold respectively. The carbon dioxide is compressed from room temperature and pressure to a supercritical state for storage.

[0038] Meanwhile, the water in the storage tank 15 is heated into high-temperature steam by the fifth heat exchanger 13 and the sixth heat exchanger 16 and then enters the high-pressure gas inlet of the ejector 17. The low-pressure gas from the outlet of the cold storage 20 enters the low-pressure gas inlet of the ejector 17, and after being mixed by the ejector 17, it enters the condenser 18 to release heat. After condensing into water, it is divided into two parts. One part is pressurized by the booster water pump 21 and enters the storage tank 15, and the other part enters the cold storage 20 to absorb heat and provide cooling capacity for the cold storage 20.

[0039] During energy release, the high-pressure carbon dioxide in the carbon dioxide storage tank 8 absorbs heat through the third heat exchanger 9 and then enters the first expander 10 to perform work. The exhaust gas from the first expander 10 enters the fourth heat exchanger 11 to absorb heat and then enters the second expander 12 to perform work and release energy. The exhaust gas from the second expander 12 enters the seventh heat exchanger 25 to heat the heat pump working fluid before it is transported and sold. The heated working fluid enters the gas-liquid separator 32 and then enters the third compressor 26 for compression. The compressed high-temperature and high-pressure heat pump working fluid supplies heat to the heating module 27. After heating, the high-temperature and high-pressure heat pump working fluid passes through the liquid storage tank 29 and then enters the second throttle valve 28 for expansion and cooling. At the same time, the carbon monoxide in the carbon monoxide storage tank 23 enters the combustion chamber 24 for combustion, and the resulting high-temperature flue gas supplies heat to the third heat exchanger 9 and the fourth heat exchanger 11.

[0040] The heat exchanger, methanol cracking hydrogen production reactor 6, methanol steam reforming hydrogen production reactor 3, and high-temperature carbon dioxide are all arranged in countercurrent; the product temperature of methanol cracking hydrogen production reactor 6 and methanol steam reforming hydrogen production reactor 3 is 200℃-300℃; to prevent the "cold spot effect" of the reactor, the electromagnetic induction iron core 36 is evenly distributed.

[0041] The working fluid in a heat pump can be water, but it is not limited to water.

[0042] like Figure 3 As shown, this is a front view of the reactor designed in this invention, with the electromagnetic induction coil 38 uniformly wound on the outer tube 39 of the reactor.

[0043] like Figure 4 The diagram shows a top view of the reactor designed in this invention, which illustrates the arrangement density of the electromagnetic induction core 36 in the catalyst 37 and the slope structure of the spiral flow channel 34 as needed.

Claims

1. A combined cooling, heating, power, hydrogen, and carbon production system based on transcritical carbon dioxide energy storage, characterized in that, The system includes a solar power generation unit, a methanol-to-hydrogen unit, and a carbon dioxide compressor unit, a carbon dioxide storage tank (8), an expander unit, and a compression heat pump unit connected in sequence. The methanol-to-hydrogen unit is equipped with a methanol steam reforming hydrogen production reactor (3), a methanol cracking hydrogen production reactor (6), a methanol storage tank (22), and a methanol-water storage tank (14). The carbon dioxide compressor unit is equipped with a first heat exchanger (4) and a second heat exchanger (7). The methanol steam reforming hydrogen production reactor (3) is installed at the hot side inlet of the first heat exchanger (4), and the methanol cracking hydrogen production reactor is installed at the hot side inlet of the second heat exchanger (7). (6) The outlet of the methanol-water storage tank (14) is connected in sequence to the cold side of the first heat exchanger (4) and the methanol-water steam reforming hydrogen production reactor (3), and the outlet of the methanol storage tank (22) is connected in sequence to the cold side of the second heat exchanger (7) and the methanol-fired hydrogen production reactor (6); the power output terminal of the solar power generation unit is connected to the power input terminal of the carbon dioxide compressor unit, the methanol-water steam reforming hydrogen production reactor (3) and the methanol-fired hydrogen production reactor (6); a heat exchanger is installed in the expander unit, and the outlet of the combustion chamber (24) is connected to the hot side inlet of the heat exchanger in the expander unit, and the carbon monoxide outlet of the methanol-fired hydrogen production unit is connected to the heat output terminal of the expander unit. The inlet of the combustion chamber (24) is connected; the carbon dioxide outlet of the methanol-to-hydrogen unit is connected to the inlet of the carbon dioxide compressor unit; the compression heat pump unit includes a seventh heat exchanger (25), a gas-liquid separator (32), a third compressor (26), a heating module (27), a liquid storage tank (29), and a second throttle valve (28) connected in sequence, and the hot-side inlet of the seventh heat exchanger (25) is connected to the gas outlet of the expander unit; the methanol steam reforming hydrogen production reactor (3) adopts a shell-and-tube reactor, including a spiral flow channel (34), a flow channel baffle (35), an electromagnetic induction iron core (36), and a catalyst. The reactor consists of a catalyst (37), an electromagnetic induction coil (38), an outer tube (39) of the reactor, and an inner tube (40) of the reactor. An electromagnetic induction core (36) is installed in the inner tube (40), and a catalyst (37) is filled in the gap between the inner tube (40) and the electromagnetic induction core (36). The flow channel between the outer tube (39) and the inner tube (40) is divided into a spiral flow channel (34) by a flow channel baffle (35). An electromagnetic induction coil (38) is wound around the outer wall of the outer tube of the reactor. The methanol cracking hydrogen production reactor (6) and the methanol steam reforming hydrogen production reactor (3) adopt the same structure.

2. The combined cooling, heating, power, hydrogen, and carbon production system based on transcritical carbon dioxide energy storage according to claim 1, characterized in that, It also includes a jet refrigeration unit, which includes an ejector (17), a condenser (18), a first throttle valve (19), and a cold storage (20) connected in sequence. The outlet of the condenser (18) is also connected in sequence to a booster water pump (21), a water storage tank (15), and a heat exchanger. The outlet of the heat exchanger is connected to the inlet of the ejector (17). The outlet of the methanol steam reforming hydrogen production reactor (3) is equipped with a first separator (30) and a heat exchanger. The outlet of the methanol cracking hydrogen production reactor (6) is equipped with a second separator (31) and a heat exchanger. The water storage tank (15) is equipped with two outlets that are respectively connected to the heat exchangers at the outlets of the methanol steam reforming hydrogen production reactor (3) and the methanol cracking hydrogen production reactor (6).

3. The combined cooling, heating, power, hydrogen, and carbon production system based on transcritical carbon dioxide energy storage according to claim 1, characterized in that, The outlet of the first separator (30) is also connected to the outlet of the methanol-water storage tank (14) or the cold-side inlet of the first heat exchanger (4), and the outlet of the methanol cracking hydrogen production reactor (6) is also connected to the cold-side inlet of the second heat exchanger (7) or the outlet of the methanol storage tank (22).

4. The combined cooling, heating, power, hydrogen, and carbon production system based on transcritical carbon dioxide energy storage according to claim 1, characterized in that, The electromagnetic induction core (36) inside the reactor inner tube (40) is evenly distributed radially, and the length of the electromagnetic induction core (36) gradually decreases from the inner circle to the outer circle; the reactor outer tube (39) is made of heat insulation material, and the reactor inner tube (40) and flow channel baffle (35) are made of heat-conducting material. The materials used for the reactor inner tube (40) and reactor outer tube (39) are all non-electromagnetic shielding materials.

5. The combined cooling, heating, power, hydrogen, and carbon production system based on transcritical carbon dioxide energy storage according to claim 1, characterized in that, The slope of the spiral flow channel (34) gradually increases from the reactor inlet to the outlet.

6. A method for combined cooling, heating, power, hydrogen, and carbon production based on transcritical carbon dioxide energy storage, characterized in that, Based on the combined cooling, heating, power, hydrogen, and carbon production system according to any one of claims 1-5, carbon dioxide is compressed from ambient temperature and pressure to a supercritical state by a carbon dioxide compressor unit and stored in a carbon dioxide storage tank (8). The supercritical carbon dioxide enters the expander unit from the carbon dioxide storage tank (8) to generate electricity. The heat generated during the carbon dioxide compression process provides heat to the methanol steam reforming hydrogen production process and the methanol cracking hydrogen production process through the first heat exchanger (4) and the second heat exchanger (7), respectively. The solar power generation unit generates electricity to provide power to the carbon dioxide compressor unit, the methanol steam reforming hydrogen production reactor (3), and the methanol cracking hydrogen production reactor (6). The carbon dioxide generated from the methanol steam reforming hydrogen production process is input into the carbon dioxide compressor unit, and the carbon monoxide generated from the methanol cracking hydrogen production process is burned to generate high-temperature flue gas. The high-temperature flue gas provides heat to the expanded carbon dioxide in the expander unit for expansion and energy release through the heat exchanger. The product temperatures of methanol steam reforming and methanol cracking for hydrogen production are 200℃-300℃. The hydrogen produced by these processes is stored. The heat energy carried by the hydrogen from these processes heats water into high-temperature steam via a heat exchanger, providing energy for the jet refrigeration unit. The hydrogen undergoes countercurrent heat exchange in the heat exchanger. The low-pressure, low-temperature steam and the high-pressure, high-temperature steam are mixed by an ejector and then condensed. The condensed water is divided into two parts: one part is pressurized by a booster pump and stored in a water storage tank, while the other part provides cooling for the cold storage. After supercritical carbon dioxide expands and generates electricity, it provides heat energy to the compression heat pump unit through a heat exchanger. The carbon dioxide after it has done work exchanges heat in the heat exchanger in a countercurrent manner. The supercritical carbon dioxide exchanges heat with high-temperature flue gas in a countercurrent manner in the expander unit.

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