A high-efficiency combined supply multi-stage hydrogen production and cs2 recovery system based on high-magnification light

Abstract

The application discloses a high-multiple-concentration high-efficiency combined multi-stage hydrogen production and CS2 recovery system based on high-multiple-concentration, which comprises a household garbage treatment system, a methane separation system and a pressure separation gas system; the methane separation system, a methyl chloride preparation system and the pressure separation gas system are sequentially connected to form a closed loop; the methanol preparation system is respectively connected with a sodium chloride electrolytic cell electrolysis system and a hydrogen production system; a CS2 preparation system; and a solar high-multiple-concentration photoelectric and photo-thermal system; garbage is converted into organic gas through a fermentation system, the organic gas generated through fermentation is converted into hydrogen and byproduct carbon disulfide by combining the Fresnel high-multiple-concentration photoelectric and photo-thermal system, garbage is efficiently utilized, and the energy crisis is relieved. Furthermore, the Fresnel high-multiple-concentration photoelectric and photo-thermal comprehensive utilization technology is coupled with the continuous phase change technology to continuously and efficiently utilize solar energy, the stable operation of the whole system is maintained, garbage can be continuously treated, and hydrogen and byproduct carbon disulfide can be prepared in three stages.

Description

Technical Field

[0001] This invention relates to the field of solar energy application technology, and in particular to a multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency combined power supply. Background Technology

[0002] Hydrogen, as a clean energy source, has considerable commercial value. In particular, it can play a very important role in promoting the transformation and upgrading of energy structures in various countries and achieving the global goal of "carbon neutrality". This drives major economies to accelerate the development and utilization of hydrogen energy.

[0003] Waste-to-hydrogen technology is a "waste-to-treasure" technology that is being actively researched both domestically and internationally. Currently, in my country, waste is mainly treated through landfill or incineration; these methods generate compounds, heavy metals, and fly ash that can easily cause secondary environmental pollution. This not only places stringent requirements on the site selection of waste treatment plants but also consumes large amounts of land resources and can even pollute the environment. The advantage of waste-to-hydrogen technology lies in its ability to transform toxic and harmful substances through fermentation, which has significant environmental benefits. In addition to producing green hydrogen, it also generates a large amount of byproducts, which have a wide range of applications.

[0004] Carbon disulfide, a byproduct of production, is an important organic intermediate and a raw material for the production of rayon, celluloid, carbon tetrachloride, pesticides, fungicides, and rubber additives. It is also an excellent solvent in the production of oils, waxes, resins, rubber, and sulfur. Furthermore, it can be used as a wool degreasing agent, a stain remover for clothing, a metal flotation agent, a release agent for paints and varnishes, and an additive for aviation kerosene.

[0005] Ethanolamine is a colorless, viscous liquid at room temperature. Due to its excellent absorption of certain chemicals (such as carbon dioxide, hydrogen sulfide, and other acidic gases), it is commonly used as a gas purifier in petroleum refining. This device also focuses on utilizing its gas purification properties; in the further processing of the municipal solid waste recycling unit, ethanolamine is used to absorb acidic gases such as carbon dioxide and hydrogen sulfide from the mixed gas, achieving methane separation. Furthermore, its good solubility and release properties for these gases have been utilized to establish a reusable recycling system, achieving industrial process objectives while improving resource utilization.

[0006] Supercritical carbon dioxide is an excellent thermodynamic working fluid, offering numerous advantages over traditional water-based fluids. Furthermore, carbon dioxide's critical temperature and pressure are significantly lower than water's, allowing it to easily reach a supercritical state at normal temperatures. Supercritical carbon dioxide possesses the density of a liquid, resulting in high heat transfer efficiency, while also exhibiting the fluidity of a gas, with low viscosity and high flowability, leading to minimal system circulation losses. Its overall performance surpasses that of other working fluids.

[0007] Solar energy has become an important part of human energy use and continues to develop. Applying solar energy technology to other technological fields has always been an industry development goal. High-concentration solar photovoltaic and solar thermal integrated utilization technology is superior to traditional solar energy utilization technology, and solar energy is currently a new energy source with huge potential, producing almost no pollution during its development and utilization.

[0008] In summary, how to achieve hydrogen production and CS2 recovery during waste treatment has become an urgent problem for researchers in this field. Summary of the Invention

[0009] The technical problem to be solved by this invention is: how to achieve hydrogen production and CS2 recovery during waste treatment; To solve the above-mentioned technical problems, the technical solution adopted by the present invention is as follows: This invention is a multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency cogeneration, comprising: A municipal solid waste treatment system is connected to a methane separation system and a pressure gas separation system; the municipal solid waste treatment system is used to produce a mixed gas containing methane, carbon dioxide and hydrogen sulfide through anaerobic fermentation and then transport it to the methane separation system; The methane separation system, the chloromethane production system, and the pressure gas separation system are sequentially connected to form a closed loop. The methane separation system is used to separate and purify methane from the mixed gas through an ethanolamine absorption-desorption process combined with membrane separation and then transport it to the chloromethane production system, while simultaneously separating and recovering carbon dioxide and hydrogen sulfide. The chloromethane production system is used to prepare chloromethane by reacting methane and chlorine under heating and catalytic conditions, and then producing a mixed gas containing chloromethane and methane after washing with sodium hydroxide to remove hydrogen chloride and chlorine. The pressure separation gas system includes: a supercritical carbon dioxide production chamber, the upper end of which is connected to an elastic balloon inside a rigid wall cavity via a transmission pipe; The inner wall of the device provides expansion space for the elastic balloon inside the rigid wall cavity; The rigid wall cavity is equipped with a temperature sensor and an electronic temperature control device. The separated carbon dioxide is transported to the supercritical carbon dioxide production chamber to produce supercritical carbon dioxide and then introduced into the elastic balloon, which expands and compresses the chloromethane and methane mixture in the rigid wall cavity. The electronic temperature control device is used to liquefy and separate the chloromethane. The methanol production system is connected to a sodium chloride electrolytic cell system, a hydrogen production system, and a chloromethane production system. The sodium chloride electrolytic cell system is used to electrolyze the sodium chloride solution produced in the sodium hydroxide alkaline washing process. Hydrogen is produced at the cathode, and chlorine is regenerated at the anode and circulated to the chloromethane production system. The methanol production system is used to react purified chloromethane with sodium hydroxide to produce methanol. After distillation and purification, methanol undergoes a methanol-water catalytic cracking reaction to produce a cracked mixture containing hydrogen, carbon monoxide, and carbon dioxide. The methane separation system and the hydrogen production system are connected in parallel to the CS2 production system. The hydrogen production system is used to sequentially decarbonize and purify the methanol cracking mixture with hydrogen membrane separation to obtain hydrogen product, while separating carbon monoxide and conveying it to the CS2 production system. The CS2 production system is used to use hydrogen sulfide produced by the methane separation system and carbon monoxide produced by the hydrogen production system as raw materials to catalytically synthesize carbonyl sulfide, perform disproportionation reaction and condensation separation, and recover carbon disulfide product.

[0010] Furthermore, it includes a high-concentration solar photovoltaic-thermal system, wherein the high-concentration solar photovoltaic-thermal system comprises: The support frame contains a semiconductor power generation panel; A high-magnification condenser lens assembly is mounted above the support. Microchannels are attached to the underside of the semiconductor power generation panel; The third pipe interface on one side of the microchannel pipe is connected to the energy storage box; The CO2 heat exchange pipe exits through the energy storage tank, connects sequentially to the chloromethane reaction chamber in the chloromethane production system, returns to the energy storage tank, and then sequentially enters the first ethanolamine separation chamber in the methane separation system, the supercritical carbon dioxide production chamber in the pressure separation gas system, the reaction chamber in the CS2 production system, the methanol cracking reaction and substitution reaction chamber in the methanol production system, and finally connects to the third pipe interface.

[0011] Furthermore, the municipal solid waste treatment system includes: The waste pretreatment chamber has a transmission pipeline equipped with a gas-liquid transfer pump connected to its top and a biogas digester treatment chamber equipped with a temperature sensor connected to its bottom. A gas collection chamber is connected to one side of the biogas digester treatment chamber. The biogas digester treatment chamber is equipped with a stirring propeller and an electric heating plate.

[0012] Furthermore, the methane separation system includes: The first ethanolamine absorption chamber has a first absorbent storage chamber and a first ethanolamine separation chamber connected sequentially at its bottom, and its top is connected to the gas collection chamber via a pipe. The bottom of the first ethanolamine separation chamber is connected to the nozzle via a transmission pipe equipped with a gas-liquid transfer pump, circulating the ethanolamine to the first ethanolamine absorption chamber. A mixed gas storage chamber and a first gas separation chamber are sequentially connected to one side of the first ethanolamine separation chamber; A carbon dioxide separation membrane is installed inside the first gas separation chamber; The first ethanolamine separation chamber includes: an inner wall of a first heating chamber, a first CO2 heating chamber, and an outer wall of a first heating chamber; The first CO2 heating chamber is located between the inner wall of the first heating chamber and the outer wall of the first heating chamber.

[0013] Furthermore, the monochloromethane production system includes: A methane storage chamber, one end of which is connected to the first ethanolamine absorption chamber, and the other end of which is connected to a chloromethane reaction chamber containing the first catalyst. The top of the chloromethane reaction chamber is connected to a chlorine storage chamber, and the bottom is connected to a by-product storage chamber. The other side of the chloromethane reaction chamber is sequentially connected to a mixed gas processing chamber and a sodium chloride solution storage chamber. The monochloromethane reaction chamber includes: The second CO2 heating chamber is located between the inner wall of the second heating chamber and the outer wall of the second heating chamber.

[0014] Furthermore, the pressure-separated gas system also includes: A carbon dioxide storage chamber, one end of which is connected to the first gas separation chamber, and the other end of which is sequentially connected to the supercritical carbon dioxide production chamber and the first pipeline interface; One side of the rigid wall cavity is connected to a chloromethane storage chamber; The rigid wall cavity is connected to the mixed gas processing chamber; The supercritical carbon dioxide production chamber includes: The third CO2 heating chamber is located between the inner wall of the third heating chamber and the outer wall of the third heating chamber.

[0015] Furthermore, the sodium chloride electrolytic cell electrolysis system includes: The storage box is connected to the graphite electrodes installed in the electrolytic cell via wires; The electrolytic cell is connected to a sodium hydroxide storage chamber on one side, a sodium chloride solution storage chamber on the other side, and a hydrogen storage chamber on the top. The sodium hydroxide storage chamber is connected to the mixed gas processing chamber; The top of the electrolytic cell is also connected to the chlorine gas storage chamber; The semiconductor power generation panel is connected to the energy storage box via wires.

[0016] Furthermore, the methanol production system includes: The substitution reaction chamber is equipped with a nozzle, and its bottom is connected in sequence to a product storage chamber and a distillation chamber with an electric heating plate at the bottom; The bottom of the distillation chamber is connected to a sodium chloride solution storage chamber, and the top is connected in sequence to a methanol collection chamber, a methanol cracking reaction chamber containing a second catalyst, and a water tank. The top of the substitution reaction chamber is connected to the sodium hydroxide storage chamber, one side is connected to the chloromethane storage chamber, and the other side is connected to the third pipeline interface; A gas mixing chamber is provided at the top of the methanol cracking reaction; The substitution reaction chamber includes: The fourth CO2 heating chamber is located between the inner wall of the fourth heating chamber and the outer wall of the fourth heating chamber; The methanol collection chamber includes: The fifth CO2 heating chamber is located between the inner wall of the fifth heating chamber and the outer wall of the fifth heating chamber.

[0017] Furthermore, the hydrogen production system includes: The second ethanolamine absorption chamber is connected at its bottom to the second absorbent storage chamber and at its top to the second gas separation chamber equipped with a hydrogen separation membrane; one side of the second ethanolamine absorption chamber is connected to the methanol cracking reaction via the gas mixing chamber. The second gas separation chamber, the carbon monoxide storage chamber, and the second pipeline interface are connected in series in sequence, and the other side of the second gas separation chamber is connected to the hydrogen storage chamber. The second ethanolamine separation chamber is equipped with a temperature sensor. Its upper side is connected to the second absorbent storage chamber and the carbon dioxide storage chamber, respectively. Its lower side is connected to the nozzle through a transmission pipe to circulate to the second ethanolamine absorption chamber. The methanol cracking reaction chamber and the substitution reaction chamber are respectively connected to one side of the second ethanolamine separation chamber; The second ethanolamine separation chamber includes: The sixth CO2 heating chamber is located between the inner wall of the sixth heating chamber and the outer wall of the sixth heating chamber.

[0018] Furthermore, the CS2 preparation system includes: The hydrogen sulfide storage chamber and the second pipeline interface are connected to the reaction chamber containing the third catalyst; The other end of the hydrogen sulfide storage chamber is connected to the first gas separation chamber; The mixed gas storage chamber is connected to the reaction chamber on one side and to a second gas separation chamber equipped with a hydrogen separation membrane on the other side, and is sequentially connected to the COS storage chamber and the disproportionation reaction chamber to the evaporation chamber; The upper side of the evaporation chamber is equipped with a spherical drying tube, and one side is connected to the carbon dioxide storage chamber and the CS2 storage chamber. The hydrogen storage chamber is connected to the bottom of the second gas separation chamber; The top of the reaction chamber is connected to a methanol cracking reaction.

[0019] The beneficial effects of this invention are as follows: This device is a multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic (PCP) high-efficiency combined power supply. It converts waste into organic gas through a fermentation system, and combines this with a Fresnel high-concentration photovoltaic-thermal system to convert the fermented organic gas into hydrogen and associated biomass carbon disulfide, achieving efficient waste utilization and alleviating the energy crisis. Furthermore, it couples the Fresnel high-concentration photovoltaic-thermal integrated utilization technology with continuous phase change technology to continuously and efficiently utilize solar energy, maintaining stable operation of the entire system and sustainably processing waste while simultaneously producing hydrogen and associated biomass carbon disulfide in three stages. Attached Figure Description

[0020] The present invention will be further described below with reference to the accompanying drawings and embodiments.

[0021] Figure 1 This is a schematic diagram of the plan; Figure 2 This is a schematic diagram of the structure of a chloromethane reaction chamber; Figure 3 This is a schematic diagram of the ethanolamine separation chamber; Figure 4 This is a schematic diagram of the methanol cracking reaction; Figure 5 This is a schematic diagram of the supercritical carbon dioxide production chamber; Figure 6 This is a schematic diagram of the structure of the substitution reaction chamber; Figure 7 This is a schematic diagram of the structure of a high-concentration solar photovoltaic and photothermal system; In the diagram: 1-Household waste treatment system; 11-Transmission pipeline; 12-Gas-liquid transfer pump; 13-Waste pretreatment chamber; 14-Biogas digester treatment chamber; 15-Temperature sensor; 16-Agitator propeller; 17-Electric heating plate; 18-Residue; 19-Gas collection chamber; 2-Methane separation system; 21-First ethanolamine absorption chamber; 22-First ethanolamine separation chamber; 221-Inner wall of the first heating chamber; 222-First CO2 heating chamber; 223-Outer wall of the first heating chamber; 23-Nozzle; 24-First absorbent storage chamber; 25-Mixed gas storage chamber; 26-First gas separation chamber; 27-Carbon dioxide separation membrane; 3-Chloromethane production system; 31-Methane storage chamber; 32-Chloromethane reaction chamber; 321-Inner wall of the second heating chamber; 322-Second CO2 heating chamber; 323-Outer wall of the second heating chamber; 33-Chlorine storage chamber; 34-First catalyst; 35-By-product storage chamber; 36-Mixed gas processing chamber; 37-Sodium chloride solution storage chamber; 4-Pressure separation gas system; 41-Carbon dioxide storage chamber; 42-Supercritical carbon dioxide production chamber; 421-Inner wall of the third heating chamber; 422-Third CO2 heating chamber; 423-Outer wall of the third heating chamber; 43-First pipeline interface; 44-Elastic rubber balloon; 45-Electrically controlled temperature device; 46-Rigid wall cavity; 47-Inner wall of the device; 48-Methyl chloride storage chamber; 5-Sodium chloride electrolytic cell electrolysis system; 51-Storage box; 52-Wire; 53-Graphite electrode; 54-Electrolytic cell; 55-Sodium hydroxide storage chamber; 56-Hydrogen storage chamber; 6-Methanol production system; 61-Substitution reaction chamber; 611-Inner wall of the fourth heating chamber; 612-Fourth CO2 heating chamber; 613-Outer wall of the fourth heating chamber; 62-Product storage chamber; 63-Distillation chamber; 64-Methanol collection chamber; 65-Second catalyst; 66-Methanol cracking reaction; 641-Inner wall of the fifth heating chamber; 642-Fifth CO2 heating chamber; 643-Outer wall of the fifth heating chamber; 67-Water tank; 68-Gas mixing chamber; 7-Hydrogen production system; 71-Second ethanolamine absorption chamber; 72-Second absorbent storage chamber; 73-Second ethanolamine separation chamber; 731-Inner wall of the sixth heating chamber; 732-Sixth CO2 heating chamber; 733-Outer wall of the sixth heating chamber; 74-Hydrogen separation membrane; 75-Second gas separation chamber; 76-Carbon monoxide storage chamber; 77-Second pipeline interface; 8-CS2 production system; 81-Hydrogen sulfide storage chamber; 82-Reaction chamber; 83-Third catalyst; 84-Mixed gas storage chamber; 85-COS storage chamber; 86-Disproportionation reaction chamber; 87-Spherical drying tube; 88-Evaporation chamber; 89-CS2 storage chamber; 9-Solar high-concentration photovoltaic and photothermal system; 91-High-concentration lens group; 92-Bracket; 93-Third pipe interface; 94-Semiconductor power generation panel; 95-CO2 heat exchange pipe; 96-Microchannel pipe; 97-Energy storage box. Detailed Implementation

[0022] The present invention will now be described in further detail with reference to the accompanying drawings. These drawings are simplified schematic diagrams, illustrating only the basic structure of the invention, and therefore only show the components relevant to the invention.

[0023] like Figure 1-7As shown, this invention proposes a multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency co-generation. It mainly consists of a municipal solid waste treatment system 1, a methane separation system 2, a chloromethane production system 3, a pressure gas separation system 4, a sodium chloride electrolysis cell system 5, a methanol production system 6, a hydrogen production system 7, a CS2 production system 8, and a high-concentration photovoltaic-thermal system 9. The municipal solid waste treatment system 1 is connected to the methane separation system 2 and the pressure gas separation system 4. The methane separation system 2, chloromethane production system 3, and pressure gas separation system 4 are sequentially connected to form a closed loop. The methanol production system 6 is connected to the sodium chloride electrolysis cell system 5 on the left and to the hydrogen production system 7 on the right. The methane separation system 2 and the hydrogen production system 7 are connected in parallel to the CS2 production system 8. The high-concentration photovoltaic-thermal system 9 runs through the entire device via pipelines. The municipal solid waste treatment system 1 consists of a transmission pipeline 11, a gas-liquid transfer pump 12, a waste pretreatment chamber 13, a biogas digester chamber 14, a temperature sensor 15, a stirring propeller 16, an electric heating plate 17, residue 18, and a gas collection chamber 19. The transmission pipeline 11, equipped with the gas-liquid transfer pump 12, is connected to the waste pretreatment chamber 13, and then to the biogas digester chamber 14, which is equipped with the temperature sensor 15. The bottom of the biogas digester chamber 14, which is connected to the gas collection chamber 19 on the left, is equipped with a stirring propeller 16 and an electric heating plate 17. The methane separation system 2 consists of a first ethanolamine absorption chamber 21, a first ethanolamine separation chamber 22, a nozzle 23, a first absorbent liquid storage chamber 24, a mixed gas storage chamber 25, a first gas separation chamber 26, and a carbon dioxide separation membrane 27. The first ethanolamine absorption chamber 21 is connected to the first absorbent liquid storage chamber 24 and the first ethanolamine separation chamber 22 in sequence on its lower side. The first ethanolamine separation chamber 22 is connected to the nozzle 23 via a transmission pipe 11 equipped with a gas-liquid transfer pump, circulating to the first ethanolamine absorption chamber 21. The mixed gas storage chamber 25 and the first gas separation chamber 26 are connected to the right side in sequence. The carbon dioxide separation membrane 27 is installed inside the first gas separation chamber 26. The first ethanolamine separation chamber 22 is composed of a first heating chamber inner wall 221, a first CO2 heating chamber 222, and a first heating chamber outer wall 223. The first CO2 heating chamber 222 is located between the first heating chamber inner wall 221 and the first heating chamber outer wall 223. The monochloromethane production system 3 comprises a methane storage chamber 31, a monochloromethane reaction chamber 32, a chlorine storage chamber 33, a first catalyst 34, a by-product storage chamber 35, a mixed gas processing chamber 36, and a sodium chloride solution storage chamber 37. The methane storage chamber 31 is connected to the monochloromethane reaction chamber 32, which contains the first catalyst 34. The monochloromethane reaction chamber 32 is connected to the chlorine storage chamber 33 above, the by-product storage chamber 35 below, and the mixed gas processing chamber 36 and the sodium chloride solution storage chamber 37 sequentially on its right side. The chloromethane reaction chamber 32 consists of an inner wall 321 of the second heating chamber, a second CO2 heating chamber 322, and an outer wall 323 of the second heating chamber. Its structure is the same as that of the ethanolamine separation chamber. The pressure-separated gas system 4 comprises a carbon dioxide storage chamber 41, a supercritical carbon dioxide production chamber 42, a first pipeline interface 43, an elastic balloon 44, an electronically controlled temperature device 45, a rigid wall cavity 46, an inner wall 47, and a chloromethane storage chamber 48. The carbon dioxide storage chamber 41 is sequentially connected to the supercritical carbon dioxide production chamber 42 and the first pipeline interface 43 via a transmission pipeline. The upper end of the supercritical carbon dioxide production chamber 42 is connected to the elastic balloon 44 inside the rigid wall cavity 46 via a transmission pipeline. The inner wall 47 provides expansion space for the elastic balloon 44. The rigid wall cavity 46 houses a temperature sensor and an electronically controlled temperature device, and its right side is connected to the chloromethane storage chamber 48. The supercritical carbon dioxide production chamber 42 consists of an inner wall 421 of the third heating chamber, a third CO2 heating chamber 422, and an outer wall 423 of the third heating chamber. Its structure is the same as that of the ethanolamine separation chamber. The sodium chloride electrolytic cell electrolysis system 5 consists of a battery storage box 51, wires 52, graphite electrodes 53, an electrolytic cell 54, a sodium hydroxide storage chamber 55, and a hydrogen storage chamber 56. The battery storage box 51 is connected to the graphite electrodes 53 installed in the electrolytic cell 54 via wires 52. The right side of the electrolytic cell 54 is connected to the sodium hydroxide storage chamber 55, and the top side is connected to the hydrogen storage chamber 56. The methanol production system 6 comprises a substitution reaction chamber 61, a product storage chamber 62, a distillation chamber 63, a methanol collection chamber 64, a second catalyst 65, a methanol cracking reaction 66, a water tank 67, and a gas mixing chamber 68. The substitution reaction chamber 61 is equipped with a nozzle 23, and its lower side is connected to the product storage chamber 62 and the distillation chamber 63, which has an electric heating plate 17 at the bottom. The distillation chamber 63 is connected to a sodium chloride solution storage chamber 37 below it, and its upper side is connected to the methanol collection chamber 64, the methanol cracking reaction 66 containing the second catalyst 65, and the water tank 67. The substitution reaction chamber 61 consists of an inner wall 611 of the fourth heating chamber, a fourth CO2 heating chamber 612, and an outer wall 613 of the fourth heating chamber. Its structure is the same as that of the first ethanolamine separation chamber 22. The methanol collection chamber 64 consists of the inner wall 641 of the fifth heating chamber, the fifth CO2 heating chamber 642, and the outer wall 643 of the fifth heating chamber. Its structure is the same as that of the first ethanolamine separation chamber 22. The hydrogen production system 7 comprises a second ethanolamine absorption chamber 71, a second absorbent storage chamber 72, a second ethanolamine separation chamber 73, a hydrogen separation membrane 74, a second gas separation chamber 75, a carbon monoxide storage chamber 76, and a second pipeline interface 77. The second ethanolamine absorption chamber 71 is connected to the second absorbent storage chamber 72 at its lower side. The second ethanolamine separation chamber 73 is equipped with a temperature sensor 15 and is connected to the second absorbent storage chamber 72 and the carbon dioxide storage chamber 41 at its upper side. Its lower side is connected to a nozzle 23 via a transmission pipeline 11, circulating the gas to the second ethanolamine absorption chamber 71. The second ethanolamine absorption chamber 71 is connected to the second gas separation chamber 75, which is equipped with a hydrogen separation membrane 74. The second gas separation chamber 75, the carbon monoxide storage chamber 76, and the second pipeline interface 77 are connected in series. The second ethanolamine separation chamber 73 consists of the inner wall 731 of the sixth heating chamber, the sixth CO2 heating chamber 732, and the outer wall 733 of the sixth heating chamber. Its structure is the same as that of the first ethanolamine separation chamber 22. The CS2 production system 8 consists of a hydrogen sulfide storage chamber 81, a reaction chamber 82, a third catalyst 83, a mixed gas storage chamber 84, a COS storage chamber 85, a disproportionation reaction chamber 86, a spherical drying tube 87, an evaporation chamber 88, and a CS2 storage chamber 89. The hydrogen sulfide storage chamber 81 and the second pipeline interface 77 are connected to the reaction chamber 82 containing the third catalyst 83. The mixed gas storage chamber 84 is connected to the reaction chamber 82 on its left side and to the second gas separation chamber 75 containing a hydrogen separation membrane 74 on its right side. Subsequently, the COS storage chamber 85 and the disproportionation reaction chamber 86 are sequentially connected to the evaporation chamber 88. The evaporation chamber 88 is equipped with a spherical drying tube 87 on its upper side and is connected to the carbon dioxide storage chamber 41 and the CS2 storage chamber 89 on its right side. The solar high-concentration photovoltaic-thermal system 9 consists of a high-concentration concentrating lens assembly 91, a support 92, a third pipe interface 93, a semiconductor power generation panel 94, a CO2 heat exchange pipe 95, a microchannel pipe 96, and an energy storage tank 97. The semiconductor power generation panel 94 is connected to the energy storage tank 51 via wires 52. The high-concentration concentrating lens assembly 91 is supported on the upper side by the support 92, and the lower side is close to the microchannel pipe 96. The microchannel pipe 96 is connected to the third pipe interface 93 on the left and then to the energy storage tank 97. The CO2 heat exchange pipe 95 exits from the energy storage tank 97 and sequentially connects to the chloromethane reaction chamber 32 before returning to the energy storage tank 97. In this manner, it successively enters the first ethanolamine separation chamber 22, the supercritical carbon dioxide production chamber 42, the reaction chamber 82, the methanol cracking reaction 66, and the substitution reaction generation chamber 61, finally returning to the third pipe interface 93. When the entire device starts working, municipal solid waste is transported through a transmission pipeline 11 equipped with a gas-liquid transfer pump 12 into a waste pretreatment chamber 13 for crushing. It then receives supercritical carbon dioxide from the first pipeline interface 43 for sterilization and disinfection. Subsequently, it enters a biogas digester treatment chamber 14 containing fixed microbial cultures. The stirring propeller 16 and electric heating plate 17 simultaneously begin working, crushing and heating the waste fragments. When the temperature sensor 15 detects that the temperature has reached 40°C, the electric heating plate 17 stops working. After a period of treatment, the added microbial cultures undergo a biochemical reaction to produce CH4, CO2, and H2S gases. The mixed gas is transported to a gas collection chamber 19 via the gas-liquid transfer pump 12, while the solids are temporarily stored in residue 18 for agricultural fertilization. The mixed gas then enters the first ethanolamine absorption chamber 21, while the nozzle 23 sprays ethanolamine into the first ethanolamine absorption chamber 21 to absorb CO2 and H2S, which then enter the first absorbent liquid storage chamber 24. Unabsorbed CH4 enters the methane storage chamber 31 through the transfer pipe 11. The liquid in the first absorbent liquid storage chamber 24 enters the first ethanolamine separation chamber 22 through the transfer pipe 11. Subsequently, a working medium is introduced into the first CO2 heating chamber 222 to heat the chamber. When the temperature sensor 15 detects that the temperature has reached above 100°C, heating is stopped. At this time, CO2 and H2S are released by the ethanolamine at high temperature and enter the mixed gas storage chamber 25, and are then transported by the gas-liquid transfer pump 12 into the first gas separation chamber 26 equipped with a carbon dioxide separation membrane 27. 7. CO2 is selectively filtered out and stored in the carbon dioxide storage chamber 41. The remaining H2S that cannot pass through the carbon dioxide separation membrane 27 is pressurized by the gas-liquid transfer pump and sent to the hydrogen sulfide storage chamber 81. CH4 and Cl2 are simultaneously introduced into the chloromethane reaction chamber 32 from the methane temporary storage chamber 31 and the chlorine temporary storage chamber 33. The gas ratio is controlled by the gas-liquid transfer pump 12. At the same time, the second CO2 heating chamber 322 heats the chamber. When the temperature sensor 15 detects that the temperature has reached 325°C, further heating is stopped. The chloromethane reaction chamber 32 is equipped with a first catalyst 34, which can cause CH4 and Cl2 to undergo a substitution reaction and increase the yield of CH3Cl. The reaction produces CH3Cl gas and a small amount of CH2Cl2, CHCl3 and CCl4. An oily liquid is transported through a pipeline into a byproduct storage chamber 35. CH3Cl gas, HCl, and unreacted Cl2 and CH4 enter a mixed gas treatment chamber 36. Simultaneously, NaOH in the sodium hydroxide storage chamber 55 is sprayed into the mixed gas treatment chamber 36 through a nozzle 23 via a pipeline 11 to absorb HCl and Cl2. A certain amount of NaOH solution is absorbed and reacted to become sodium chloride solution, which is then circulated into the electrolytic cell 54. The storage tank 51 forms a closed circuit with the electrolytic cell 54 through wires 52 and graphite electrodes 53. When electricity is applied, the sodium chloride solution is electrolyzed. Hydrogen gas is generated at the cathode and stored in the hydrogen storage chamber 56. Chlorine gas is generated at the anode and circulated into the chlorine storage chamber 33. The solution after electrolysis is a NaOH solution, which is then stored in the sodium hydroxide storage chamber 55. CO2 in the carbon dioxide storage chamber 41 is pressurized to above 7 MPa through the transmission pipe 11 and enters the supercritical carbon dioxide production chamber 42. The working medium in the third CO2 heating chamber 422 heats the chamber until the temperature sensor 15 displays above 31°C, at which point the CO2 is converted into supercritical carbon dioxide and transmitted through the transmission pipe 11 to the first pipe interface 43. When the inner wall 47 of the device receives CH4 and CH3Cl from the mixed gas processing chamber 36, a portion of the gas in the supercritical carbon dioxide production chamber 42 is introduced into the elastic balloon 44. Due to the supercritical carbon dioxide... Carbon dioxide has high pressure. The balloon collides with the gas inside the inner wall 47 of the compression device. The rigid wall cavity 46 prevents the cavity from deforming. By controlling the internal volume of the inner wall 47, the gas pressure compressed by the expansion of the elastic balloon 44 reaches 5MPa. At this time, the boiling point of CH3Cl is 22℃. The temperature is reduced to 15-20℃ by the electric temperature control device 45, CH3Cl liquefies, CH4 remains a gas and is returned to the chloromethane reaction chamber 32. Subsequently, the electric temperature control device 45 raises the temperature to above 22℃, CH3Cl vaporizes and enters the chloromethane storage chamber 48. The chloromethane storage chamber 48 leads to the substitution reaction chamber 61. Simultaneously, nozzle 23 connects to sodium hydroxide storage chamber 55, spraying NaOH into the substitution reaction chamber 61 for heating and substitution reaction, generating CH3OH and NaCl, which are stored in product storage chamber 62. Subsequently, it enters distillation chamber 63, where it is heated to 65°C by bottom electric heating plate 17 to distill off CH3OH, which is then passed into methanol collection chamber 64. The waste liquid is stored in sodium chloride solution storage chamber 37. The CH3OH in methanol collection chamber 64 enters methanol cracking reaction 66 containing a second catalyst 65, where it undergoes cracking reaction with H2O in water tank 67 to generate H2. CO2 and CO are passed into gas mixing chamber 68 for cooling. After cooling, the H2, CO2, and CO in gas mixing chamber 68 are passed into the second ethanolamine absorption chamber 71. Then, nozzle 23 sprays ethanolamine from the second ethanolamine separation chamber 73 into the second ethanolamine absorption chamber 71 to absorb CO2, which then enters the second absorption liquid temporary storage chamber 72. Unabsorbed H2 and... CO is introduced into the second gas separation chamber 75, which is equipped with a hydrogen separation membrane 74. The hydrogen separation membrane 74 selectively allows H2 to pass through into the hydrogen storage chamber 56, while the remaining CO that does not pass through enters the carbon monoxide storage chamber 76. H2S in the hydrogen sulfide storage chamber 81 and CO in the carbon monoxide storage chamber 76 enter the reaction chamber 82, which is equipped with a third catalyst 83, through the second pipe interface 77. The heating chamber cavity 822 heats the reaction chamber 82 and is coupled with the temperature sensor 15 to raise the temperature to 300°C. The third catalyst 83 causes H2S and CO to react and produce COS, which is temporarily stored in the COS storage chamber 85. Subsequently, it is introduced into the disproportionation reaction chamber 86 to undergo a disproportionation reaction to generate CS2. The mixed gas after the reaction is introduced into the evaporation chamber 88, which is equipped with a water-cooled spherical drying tube 87 at its upper end. The hot CS2 vapor is condensed in the spherical drying tube 87 and flows back into the evaporation chamber 88. After the chamber returns to room temperature, the CS2 enters the CS2 storage chamber 89, and other gases enter the carbon dioxide storage chamber 41. A high-concentration concentrating lens group 91, mounted on a bracket 92, focuses sunlight onto a semiconductor power generation plate 94 to generate a photoelectric effect. The waste heat generated during power generation is carried away by the working fluid in the microchannel pipe 96. The CO2 after heat exchange enters the energy storage box 97 through the third pipe interface 93 to store some of the heat. The CO2 heat exchange pipe 95 exits from the energy storage box 97 and connects sequentially to the chloromethane reaction chamber 32 to provide the required temperature for the device. Then it returns to the energy storage box 97 and enters the first ethanolamine separation chamber 22, the supercritical carbon dioxide production chamber 42, the reaction chamber 82, the methanol cracking reaction 66, and the substitution reaction generation chamber 61 in this manner to provide a suitable temperature for the device before finally returning to the third pipe interface 93. To avoid the heat inside the energy storage box being limited by solar energy and weather, an electric heating plate is installed inside the energy storage box. The electricity is provided by high-concentration solar photovoltaic and photothermal energy.

[0024] Based on the above-described preferred embodiments of the present invention, and through the foregoing description, those skilled in the art can make various changes and modifications without departing from the inventive concept. The technical scope of this invention is not limited to the contents of the specification, but must be determined according to the scope of the claims.

Claims

1. A multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency cogeneration, characterized in that, include: A municipal solid waste treatment system (1) is connected to a methane separation system (2) and a pressure gas separation system (4); the municipal solid waste treatment system (1) is used to produce a mixed gas containing methane, carbon dioxide and hydrogen sulfide through anaerobic fermentation and transport it to the methane separation system (2). The methane separation system (2), the chloromethane production system (3), and the pressure separation gas system (4) are connected in sequence to form a closed loop. The methane separation system (2) is used to separate and purify methane from the mixed gas through an ethanolamine absorption-desorption process combined with membrane separation and transport it to the chloromethane production system (3), while simultaneously separating and recovering carbon dioxide and hydrogen sulfide. The chloromethane production system (3) is used to prepare chloromethane by reacting methane and chlorine under heating and catalytic conditions, and then produce a mixed gas containing chloromethane and methane after washing with sodium hydroxide to remove hydrogen chloride and chlorine. The pressure separation gas system (4) includes a supercritical carbon dioxide production chamber (42), the upper end of which is connected to an elastic balloon (44) inside a rigid wall cavity (46) via a transmission pipe (11). The inner wall (47) of the device provides expansion space for the elastic balloon (44) inside the rigid wall cavity (46); The rigid wall cavity (46) is equipped with a temperature sensor (15) and an electric temperature control device (45). The separated carbon dioxide is transported to the supercritical carbon dioxide production chamber (42) to produce supercritical carbon dioxide and is introduced into the elastic balloon (44) to expand and compress the chloromethane and methane mixture in the rigid wall cavity. The electric temperature control device is used to liquefy and separate the chloromethane. The methanol production system (6) is connected to the sodium chloride electrolysis cell system (5), the hydrogen production system (7), and the chloromethane production system (3). The sodium chloride electrolysis cell system (5) is used to electrolyze the sodium chloride solution produced in the sodium hydroxide alkaline washing process. Hydrogen is produced at the cathode, chlorine is regenerated at the anode and circulated to the chloromethane production system (3). The methanol production system (6) is used to react the purified chloromethane with sodium hydroxide to produce methanol. After distillation and purification, methanol is subjected to a methanol-water catalytic cracking reaction to produce a cracked mixed gas containing hydrogen, carbon monoxide and carbon dioxide. The methane separation system (2) and the hydrogen production system (7) are connected in parallel to the CS2 production system (8). The hydrogen production system (7) is used to sequentially decarbonize and purify the methanol cracking mixture with hydrogen membrane separation to obtain hydrogen products, while separating carbon monoxide and transporting it to the CS2 production system (8). The CS2 production system (8) is used to use hydrogen sulfide produced by the methane separation system (2) and carbon monoxide produced by the hydrogen production system (7) as raw materials to catalytically synthesize carbonyl sulfide, disproportionate reaction and condensation separation to recover carbon disulfide products.

2. The multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency cogeneration as described in claim 1, characterized in that, It also includes a high-concentration solar photovoltaic and photothermal system (9), which comprises: A bracket (92) is provided with a semiconductor power generation plate (94) inside it. A high-magnification condenser lens assembly (91) is disposed above the support (92); Microchannels (96) are attached to the underside of the semiconductor power generation plate (94); The third pipe interface (93) on one side of the microchannel pipe (96) is connected to the energy storage box (97). The CO2 heat exchange pipe (95) exits through the energy storage tank (97) and connects sequentially to the chloromethane reaction chamber (32) in the chloromethane production system (3) before returning to the energy storage tank (97). In this manner, it enters the first ethanolamine separation chamber (22) in the methane separation system (2), the supercritical carbon dioxide production chamber (42) in the pressure separation gas system (4), the reaction chamber (82) in the CS2 production system (8), the methanol cracking reaction (66) and substitution reaction generation chamber (61) in the methanol production system (6), and finally connects to the third pipe interface (93).

3. The multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency cogeneration as described in claim 2, characterized in that, The municipal solid waste treatment system (1) includes: The waste pretreatment chamber (13) is connected to a transmission pipe (11) equipped with a gas-liquid transfer pump (12) at its top and to a biogas digester treatment chamber (14) equipped with a temperature sensor (15) at its bottom. A gas collection chamber (19) is connected to one side of the biogas digester treatment chamber (14). The biogas digester treatment chamber (14) is equipped with a stirring propeller (16) and an electric heating plate (17).

4. The multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency cogeneration as described in claim 3, characterized in that, The methane separation system (2) includes: The first ethanolamine absorption chamber (21) is connected in sequence to the bottom of the first absorption liquid storage chamber (24) and the first ethanolamine separation chamber (22), and its top is connected to the gas collection chamber (19) through a pipe. The bottom of the first ethanolamine separation chamber (22) is connected to the nozzle (23) through a transmission pipe (11) equipped with a gas-liquid transfer pump (12) and circulates to the first ethanolamine absorption chamber (21). A mixed gas storage chamber (25) and a first gas separation chamber (26) are sequentially connected to one side of the first ethanolamine separation chamber (22); A carbon dioxide separation membrane (27) is installed inside the first gas separation chamber (26); The first ethanolamine separation chamber (22) includes: a first heating chamber inner wall (221), a first CO2 heating chamber (222), and a first heating chamber outer wall (223); The first CO2 heating chamber (222) is located between the inner wall (221) and the outer wall (223) of the first heating chamber.

5. The multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency cogeneration as described in claim 4, characterized in that, The monochloromethane production system (3) includes: The methane storage chamber (31) is connected at one end to the first ethanolamine absorption chamber (21) and at the other end to the chloromethane reaction chamber (32) containing the first catalyst (34). The top of the chloromethane reaction chamber (32) is connected to a chlorine storage chamber (33), and the bottom is connected to a by-product storage chamber (35). The other side of the chloromethane reaction chamber (32) is connected in sequence to a mixed gas processing chamber (36) and a sodium chloride solution storage chamber (37). The chloromethane reaction chamber (32) includes: The second CO2 heating chamber (322) is located between the inner wall (321) and the outer wall (323) of the second heating chamber.

6. The multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency cogeneration as described in claim 5, characterized in that, The pressure separation gas system (4) also includes: The carbon dioxide storage chamber (41) is connected at one end to the first gas separation chamber (26) and at the other end to the supercritical carbon dioxide production chamber (42) and the first pipeline interface (43). One side of the rigid wall cavity (46) is connected to a chloromethane storage chamber (48). The rigid wall cavity (46) is connected to the mixed gas processing chamber (36); The supercritical carbon dioxide production chamber (42) includes: The third CO2 heating chamber (422) is located between the inner wall (421) and the outer wall (423) of the third heating chamber.

7. The multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency cogeneration as described in claim 6, characterized in that, The sodium chloride electrolytic cell electrolysis system (5) includes: The battery storage box (51) is connected to the graphite electrode (53) installed in the electrolytic cell (54) via wires (52); The electrolytic cell (54) is connected to a sodium hydroxide storage chamber (55) on one side, a sodium chloride solution storage chamber (37) on the other side, and a hydrogen storage chamber (56) on the top. The sodium hydroxide storage chamber (55) is connected to the mixed gas processing chamber (36); The top of the electrolytic cell (54) is also connected to the chlorine storage chamber (33); The semiconductor power generation board (94) is connected to the battery storage box (51) via a wire (52).

8. The multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency cogeneration as described in claim 7, characterized in that, The methanol production system (6) includes: The substitution reaction chamber (61) is equipped with a nozzle (23) and is connected in sequence to a product storage chamber (62) and a distillation chamber (63) with an electric heating plate (17) at the bottom. The bottom of the distillation chamber (63) is connected to a sodium chloride solution storage chamber (37), and the top is connected in sequence to a methanol collection chamber (64), a methanol cracking reaction chamber (66) containing a second catalyst (65), and a water tank (67). The top of the substitution reaction chamber (61) is connected to the sodium hydroxide storage chamber (55), one side is connected to the chloromethane storage chamber (48), and the other side is connected to the third pipeline interface (93). A gas mixing chamber (68) is provided at the top of the methanol cracking reaction (66). The substitution reaction chamber (61) includes: The fourth CO2 heating chamber (612) is disposed between the inner wall (611) and the outer wall (613) of the fourth heating chamber; The methanol collection chamber (64) includes: The fifth CO2 heating chamber (642) is located between the inner wall (641) and the outer wall (643) of the fifth heating chamber.

9. The multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency cogeneration as described in claim 8, characterized in that, The hydrogen production system (7) includes: The second ethanolamine absorption chamber (71) is connected at its bottom to the second absorbent storage chamber (72) and at its top to the second gas separation chamber (75) equipped with a hydrogen separation membrane (74); one side of the second ethanolamine absorption chamber (71) is connected to the methanol cracking reaction (66) through the gas mixing chamber (68). The second gas separation chamber (75), the carbon monoxide storage chamber (76), and the second pipeline interface (77) are connected in series. The other side of the second gas separation chamber (75) is connected to the hydrogen storage chamber (56). The second ethanolamine separation chamber (73) is equipped with a temperature sensor (15), and its upper side is connected to the second absorption liquid storage chamber (72) and the carbon dioxide storage chamber (41) respectively. Its lower side is connected to the nozzle (23) through the transmission pipe (11) to circulate to the second ethanolamine absorption chamber (71). The methanol cracking reaction (66) and the substitution reaction generation chamber (61) are respectively connected to one side of the second ethanolamine separation chamber (73). The second ethanolamine separation chamber (73) includes: The sixth CO2 heating chamber (732) is located between the inner wall (731) and the outer wall (733) of the sixth heating chamber.

10. The multi-stage hydrogen production and CS2 recovery system based on high-concentration photovoltaic power generation and high-efficiency cogeneration as described in claim 9, characterized in that, The CS2 preparation system (8) includes: The hydrogen sulfide storage chamber (81) and the second pipeline interface (77) are connected to the reaction chamber (82) containing the third catalyst (83); The hydrogen sulfide storage chamber (81) is connected to the first gas separation chamber (26) at the other end. The mixed gas storage chamber (84) is connected to the reaction chamber (82) on one side and to the second gas separation chamber (75) equipped with a hydrogen separation membrane (74) on the other side, and is connected to the COS storage chamber (85) and the disproportionation reaction chamber (86) in sequence to the evaporation chamber (88). The evaporation chamber (88) is equipped with a spherical drying tube (87) on its upper side, and is connected to the carbon dioxide storage chamber (41) and the CS2 storage chamber (89) on one side. The bottom of the second gas separation chamber (75) is connected to the hydrogen storage chamber (56); The top of the reaction chamber (82) is connected to a methanol cracking reaction (66).

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