Thermoelectric self-sufficient hydrogen energy preparation system

Abstract

The application provides a thermoelectric self-sufficient hydrogen energy preparation system, which comprises a reactor for realizing supercritical water gasification treatment of organic waste liquid and outputting gasification reaction products; a waste liquid branch for pretreating the organic waste liquid and providing the pretreated organic waste liquid to the reactor; an oxygen branch for providing oxygen to the reactor; a waste heat recovery branch for driving a steam turbine to drive a generator to generate power by using the gasification reaction products output by the reactor, and simultaneously treating the gasification reaction products to obtain hydrogen-rich gas and residual liquid; and a residual liquid circulation branch connected with the reactor and the waste heat recovery branch, for treating the residual liquid output by the waste heat recovery branch to obtain circulating residual liquid, and a hydrogen gas purification and supply system connected with the waste heat recovery branch, for purifying the hydrogen-rich gas to obtain high-purity hydrogen gas and fuel gas. The system provided by the application belongs to a thermoelectric self-sufficient independent distributed hydrogen preparation system, which does not need external power and fuel input, and has the dual effects of environmental protection and energy saving.

Description

Technical Field

[0001] This invention relates to the field of hydrogen energy production, and more particularly to a thermoelectric self-sufficient hydrogen energy production system. Background Technology

[0002] With the increasing environmental impact of the massive consumption of fossil fuels and the growing demands for sustainable development, the development and utilization of renewable energy are receiving increasing attention. Hydrogen energy, with its high calorific value, zero emissions, and light weight, and its ability to be converted into various energy sources, has garnered widespread attention as a recyclable green energy source. Currently, large-scale industrial hydrogen production relies on traditional gasification furnace technology using natural gas, coal, and other mineral energy sources as raw materials. This technology suffers from drawbacks such as low gasification efficiency, high energy consumption, and high carbon emission intensity. Other novel hydrogen production routes include solar-powered electrolysis and photolysis, but these methods still have relatively high costs.

[0003] Supercritical water gasification has unique advantages over other biomass thermochemical hydrogen production technologies. It allows for the direct gasification of wet materials with high water content, eliminating the need for energy-intensive drying processes and preventing intermediate pollution. Supercritical water refers to water with special properties whose temperature and pressure are both above their critical point (temperature greater than 374℃, pressure greater than 22.1MPa). Its application in the degradation and energy utilization of organic waste shows great promise. In a supercritical water environment, organic matter and gas are completely miscible, the gas-liquid interface disappears, forming a homogeneous system, and the reaction rate is greatly accelerated. Within a short residence time, organic matter rapidly gasifies to produce hydrogen-rich gas.

[0004] Since supercritical water gasification for hydrogen production from organic matter is an endothermic reaction, the reactants and media need to be preheated to the supercritical temperature. Furthermore, to improve reaction efficiency, preheating to even higher temperatures is required, a process that generally consumes a large amount of electrical energy. The high-temperature conditions of existing supercritical water gasification reactions, requiring materials to be preheated to the supercritical temperature, typically necessitate substantial heat energy input, resulting in high energy consumption and costs. Organic waste is prone to scaling and clogging in the preheating section, and the presence of particles in high-solid-content waste liquids easily leads to solid particle accumulation, significantly increasing heat and mass transfer resistance, resulting in low supercritical water gasification efficiency and inhibiting reaction rate and gas production. Conventional solutions involve mechanical stirring within the reactor, but under supercritical water reaction conditions, stirring devices are difficult to install and seal. Alternatively, an excessively long reaction residence time can be used, but this results in excessively large reactor size and investment. Forming a hydrothermal flame within the reactor can achieve rapid preheating of the waste liquid, thus solving the preheating problem and improving gasification efficiency; however, this process relies on auxiliary fuel input, negatively impacting system energy consumption and economics. Summary of the Invention

[0005] In view of the above-mentioned shortcomings of the prior art, the present invention provides a thermoelectric self-sufficient hydrogen production system, which effectively solves the problems of high energy consumption, low efficiency and the need for a large amount of external power and fuel input to produce hydrogen from supercritical water of organic waste, which affect the energy consumption and economy of the system.

[0006] This invention provides a thermoelectric self-sufficient hydrogen production system, comprising: a reactor, a waste liquid branch, an oxygen branch, a waste heat recovery branch, a residual liquid circulation branch, and a hydrogen purification and supply system, wherein:

[0007] The reactor comprises a top circular end cap, an upper cylindrical shell, a lower conical shell, and a bottom circular end cap connected in sequence. A cylindrical inner shell is coaxially disposed inside the upper cylindrical shell. The upper edge of the inner shell is connected to the top circular end cap, and the lower edge of the inner shell is higher than the lower edge of the upper cylindrical shell. The interior of the inner shell is a gasification reaction zone. The annular gap between the inner shell and the upper cylindrical shell is a waste liquid preheating zone. The gasification product outlet of the gasification reaction zone is located at the center of the top circular end cap. A waste liquid injection port is located at the intersection of the waste liquid preheating zone and the top circular end cap. A coaxial nozzle is coaxially disposed on the bottom circular end cap. The coaxial nozzle includes an inner tube and an outer tube. An oxygen injection port is located on the outer tube, and a circulating residual liquid injection port is located on the inner tube. The outlet of the coaxial nozzle extends into the interior space of the lower conical shell, and the outlet position does not exceed the lower edge of the upper cylindrical shell. The bottom circular end cap also has a slag discharge outlet.

[0008] The waste liquid branch is connected to the waste liquid inlet, and the waste liquid branch is used to pretreat the organic waste liquid and provide the pretreated organic waste liquid to the reactor.

[0009] The oxygen branch is connected to the oxygen injection port and is used to supply oxygen to the reactor;

[0010] The waste heat recovery branch is connected to the gasification product outlet. The waste heat recovery branch uses the gasification reactants output from the reactor to drive a steam turbine to drive a generator to generate electricity. At the same time, the gasification reactants are processed to obtain hydrogen-rich gas and residual liquid.

[0011] The residual liquid circulation branch is connected to the circulating residual liquid injection port and is used to process the residual liquid output from the waste heat recovery branch to obtain circulating residual liquid. The circulating residual liquid and the oxygen provided by the oxygen branch undergo a violent supercritical water oxidation reaction in the internal space of the lower conical shell to form a hydrothermal flame.

[0012] The hydrogen purification and supply system is connected to the waste heat recovery branch and is used to purify the hydrogen-rich gas output from the waste heat recovery branch to obtain high-purity hydrogen and fuel gas.

[0013] Preferably, a plurality of conical folding plate groups are coaxially and uniformly arranged inside the cylindrical inner shell. The conical folding plate group includes an upper conical folding plate and a lower conical folding plate, and the minimum distance between the upper conical folding plate and the lower conical folding plate is less than the radius of the cylindrical inner shell.

[0014] Preferably, the waste liquid branch includes a waste liquid tank, a waste liquid booster pump, and a first preheater. The organic waste liquid in the waste liquid tank is pressurized to above 23 MPa by the waste liquid booster pump, and then preheated by the first preheater before entering the reactor through the waste liquid inlet. The concentration of solid particles in the organic waste liquid is 1-20%, and the solid particle size is less than 50 μm.

[0015] Preferably, the oxygen branch includes an oxygen tank and an oxygen booster pump. The oxygen in the oxygen tank is pressurized to above 23 MPa by the oxygen booster pump and injected into the reactor from the oxygen injection port. The oxygen flow rate is 1.05-1.25 times the amount of oxygen required for the complete oxidation of residual organic matter.

[0016] Preferably, the waste heat recovery branch includes a first branch, a second branch, and a high-pressure gas-liquid separator, wherein:

[0017] The first branch includes a steam turbine, a generator, and a first pressure regulating valve. The gasified reactants output from the reactor drive the steam turbine to drive the generator. The generator supplies electricity to the pumps and valves in the system. Excess electricity is stored or output externally. The gasified reactants enter the high-pressure gas-liquid separator after being pressure regulated by the first pressure regulating valve.

[0018] The second branch includes a second preheater and a second pressure regulating valve. The gasified reactants output from the reactor enter the second preheater to preheat the residual liquid. The temperature of the gasified reactants is initially cooled to below 350°C, and then enters the high-pressure gas-liquid separator after being pressure regulated by the second pressure regulating valve.

[0019] Preferably, the first pressure regulating valve and the second pressure regulating valve are linked pressure regulating valves, used to control the fluid pressure of the first branch and the second branch to be consistent.

[0020] Preferably, the waste heat recovery branch further includes a back pressure valve and an atmospheric pressure gas-liquid separator. The high-pressure gas-liquid separator obtains hydrogen-rich gas and residual liquid by separating the gasification reactants. The high-pressure gas-liquid separator is provided with an upper outlet and a lower outlet, wherein:

[0021] The hydrogen-rich gas is output from the upper outlet. The hydrogen-rich gas is further cooled by the first preheater, then depressurized to atmospheric pressure by the back pressure valve, and enters the atmospheric pressure gas-liquid separator to separate the discharge liquid.

[0022] The lower outlet outputs residual liquid into the residual liquid circulation branch.

[0023] Preferably, the residual liquid circulation branch includes a circulation pump, an ejector, and a second preheater. After being pressurized by the circulation pump, the residual liquid enters the ejector for mixing and pressure regulation, and then is preheated by the second preheater before being injected into the reactor from the circulating residual liquid injection port. The pressure after being pressurized by the circulation pump is 2-5 MPa higher than the pressure after being pressurized by the oxygen booster pump.

[0024] Preferably, the hydrogen purification and supply system includes a purification device, a fuel gas tank, and a hydrogen storage tank. The hydrogen-rich gas output from the atmospheric pressure gas-liquid separator is purified by the purification device to obtain high-purity hydrogen and fuel gas. The high-purity hydrogen enters the hydrogen storage tank and is output externally, while the fuel gas enters the fuel gas tank. The fuel gas tank is connected to the injector to replenish the concentration of organic matter in the circulating residual liquid.

[0025] Preferably, the purification device includes one or more of a pressure swing adsorption device, a membrane separation device, and a chemical absorption device.

[0026] This invention provides a reactor design for a thermoelectric self-sufficient hydrogen production system, divided into a hydrothermal flame zone, a material preheating zone, and a gasification zone. This structural design allows for rapid preheating of the material via a hydrothermal flame after initial preheating of the waste liquid, improving gasification efficiency and hydrogen production efficiency. The reactor's internal flue gas purification structure separates solid particles from the product, facilitating subsequent power generation. Simultaneously, the solid particles falling into the flame zone enhance gasification. The thermal energy of the gasification products is utilized in stages (power generation, waste liquid and residual liquid preheating), and the pressure energy of the products is also fully recovered, achieving efficient cascaded energy utilization without the need for external power supply. The gasification products are separated into residual liquid, hydrogen, and fuel gas. The fuel gas and residual liquid are mixed and pressurized to supplement the hydrothermal flame, thus forming the hydrothermal flame of the system. No external auxiliary fuel is required to form the hydrothermal flame. Excess oxygen in the hydrothermal flame can cause partial oxidation of the waste, accelerating product degradation and gas production rate. This system does not require external electricity or fuel input. By utilizing the chemical energy of organic matter in the waste liquid and the thermal and pressure energy of the gasification reaction process in a branched and graded manner, organic waste can be treated without secondary emissions. At the same time, hydrogen and fuel gas can be produced for external output, which has the dual effect of environmental protection and energy saving. Attached Figure Description

[0027] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0028] Figure 1This is a schematic diagram of the thermoelectric self-sufficient hydrogen production system provided in an embodiment of the present invention;

[0029] Figure 2 This is a schematic diagram of the reactor structure in the thermoelectric self-sufficient hydrogen production system provided in an embodiment of the present invention;

[0030] in, Figure 1 and Figure 2 The correspondence between the reference numerals and components in the attached drawings is as follows:

[0031] 1. Reactor; 2. Generator; 3. Steam turbine; 4. Hydrogen storage tank; 5. Purification unit; 6. Atmospheric pressure gas-liquid separator; 7. Back pressure valve; 8. Fuel gas tank; 9. Waste liquid tank; 10. Waste liquid booster pump; 11. First preheater; 12. High-pressure gas-liquid separator; 13. First pressure regulating valve; 14. Second pressure regulating valve; 15. Circulation pump; 16. Ejector; 17. Second preheater; 18. Oxygen booster pump; 19. Oxygen tank; 101. Top circular end cap; 102. Gasification product outlet; 103. Waste liquid inlet; 104. Upper cylindrical outer shell; 105. Cylindrical inner shell; 106. Lower conical outer shell; 107. Outer pipe; 108. Slag outlet; 109. Inner pipe; 110. Circulating residual liquid inlet; 111. Oxygen inlet; 112. Bottom circular end cap; 113. Lower conical baffle; 114. Upper conical baffle. Detailed Implementation

[0032] To make the objectives, technical solutions, and advantages of this invention clearer, the technical solutions of this invention will be further described clearly and completely below with reference to the accompanying drawings of the embodiments of this invention. It should be noted that the described embodiments are merely some embodiments of this invention, and not all embodiments. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without creative effort are within the scope of protection of this invention.

[0033] The terms "first" and "second" used in the embodiments of this application are for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this application, the terms "comprising" and "having," and any variations thereof, are intended to cover non-exclusive inclusion. For example, a system, product, or device that includes a series of components or units is not limited to the listed components or units, but may optionally include unlisted components or units, or may optionally include other components or units inherent to such products or devices. In the description of this application, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0034] Since supercritical water gasification for hydrogen production from organic matter is an endothermic reaction, the reactants and media need to be preheated to the supercritical temperature. Furthermore, to improve reaction efficiency, preheating to even higher temperatures is required, a process that generally consumes a large amount of electrical energy. The high-temperature conditions of existing supercritical water gasification reactions, requiring materials to be preheated to supercritical temperatures, typically necessitate significant heat energy input, resulting in high energy consumption and costs. Organic waste is prone to scaling and clogging in the preheating section, and the presence of particles in high-solid-content waste liquids easily leads to solid particle accumulation, significantly increasing heat and mass transfer resistance, resulting in low supercritical water gasification efficiency and inhibiting reaction rate and gas production. Conventional solutions involve mechanical stirring within the reactor, but under supercritical water reaction conditions, stirring devices are difficult to install and seal; alternatively, excessively long reaction residence times can be used, but this results in excessively large reactor sizes and investment costs. Forming a hydrothermal flame within the reactor can achieve rapid preheating of the waste liquid, thus solving the preheating problem and improving gasification efficiency; however, this process relies on auxiliary fuel input, negatively impacting system energy consumption and economics.

[0035] This invention provides a thermoelectric self-sufficient hydrogen production system, effectively solving the problems of high energy consumption and low efficiency in supercritical water gasification of organic waste for hydrogen production, which requires a large amount of external electricity and fuel input, affecting the system's energy consumption and economic efficiency. Figure 1 The diagram below shows the structure of a thermoelectric self-sufficient hydrogen production system provided in an embodiment of the present invention. The system includes a reactor 1, a waste liquid branch, an oxygen branch, a waste heat recovery branch, a residual liquid circulation branch, and a hydrogen purification and supply system.

[0036] Figure 2This is a schematic diagram of the reactor structure in the thermoelectric self-sufficient hydrogen production system provided in an embodiment of the present invention. The reactor 1 includes a top circular end cap 101, an upper cylindrical outer shell 104, a lower conical outer shell 106, and a bottom circular end cap 112 connected in sequence. A cylindrical inner shell 105 is coaxially arranged inside the upper cylindrical outer shell 104. The upper edge of the cylindrical inner shell 105 is connected to the top circular end cap 101, and the lower edge of the cylindrical inner shell 105 is higher than the lower edge of the upper cylindrical outer shell 104. The interior of the cylindrical inner shell 105 is a gasification reaction zone. The annular gap between the cylindrical inner shell 105 and the upper cylindrical outer shell 104 is a waste liquid preheating zone. A gasification product outlet 102 of the gasification reaction zone is located at the center of the top circular end cap 101. A waste liquid inlet 103 is located at the intersection of the annular gap between the cylindrical inner shell 105 and the upper cylindrical outer shell 104 and the top circular end cap 101. A coaxial nozzle is coaxially mounted on the bottom circular end cap 112. The coaxial nozzle includes an inner tube 109 and an outer tube 107. An oxygen injection port 111 is provided on the outer tube 107, and a circulating residual liquid injection port 110 is provided on the inner tube 109. The outlet of the coaxial nozzle extends into the internal space of the lower conical outer shell 106, and its high end is lower than the lower edge of the upper cylindrical outer shell 104. A slag discharge outlet 108 is provided on the outer ring where the bottom circular end cap 112 and the coaxial nozzle intersect. Several conical folding plate groups are coaxially and evenly arranged inside the cylindrical inner shell 105. The conical folding plate groups include an upper conical folding plate 114 and a lower conical folding plate 113. The upper and lower conical folding plates are arranged in parallel, and the minimum distance between them is less than the radius of the cylindrical inner shell 105.

[0037] The waste liquid branch is used for the pretreatment of organic waste liquid and to supply pretreated organic waste liquid to the reactor. It includes waste liquid tank 9, waste liquid booster pump 10 and first preheater 11. The organic waste liquid in waste liquid tank 9 is pressurized to above 23MPa by waste liquid booster pump 10 and preheated by first preheater 11 before entering reactor 1 through waste liquid inlet 103. The concentration of solid particles in the organic waste liquid is 1-20% and the size of solid particles is less than 50μm.

[0038] The oxygen branch is used to supply oxygen to the reactor, including an oxygen tank 19 and an oxygen booster pump 18. The oxygen in the oxygen tank 19 is boosted to more than 23 MPa by the oxygen booster pump 18 and injected into the reactor 1 through the oxygen injection port 111 of the coaxial nozzle outer pipe 107. The injected oxygen flow rate is 1.05-1.25 times the amount of oxygen required for the complete oxidation of residual organic matter. The excess oxygen not only ensures the complete oxidation of organic matter in the hydrothermal flame, but the residual oxygen can also cause partial oxidation of the waste liquid, accelerating the efficient degradation and full vaporization of the waste liquid.

[0039] The waste heat recovery branch is used to process the gasification reactants output from the reactor to obtain hydrogen-rich gas and residual liquid. The waste heat recovery branch includes a first branch, a second branch, a high-pressure gas-liquid separator 12, a back pressure valve 7, and an atmospheric pressure gas-liquid separator 6. The first branch includes a steam turbine 3, a generator 2, and a first pressure regulating valve 13. In this branch, the gasification reactants output from the reactor drive the steam turbine 3 to drive the generator 2 to operate, supplying electricity to the pumps and valves in the system. Excess electricity is stored or output externally. The gasification reaction products are then pressure-regulated by the first pressure regulating valve 13 and enter the high-pressure gas-liquid separator 12. The second branch includes a second preheater 17 and a second pressure regulating valve 14. In this branch, the gasification reactants output from the reactor enter the second preheater 17 to preheat the residual liquid and initially cool it to below 350°C. Then, the pressure is reduced by 10-20 MPa by the second pressure regulating valve 14 before entering the high-pressure gas-liquid separator 12. The first pressure regulating valve 13 and the second pressure regulating valve 14 are linked pressure regulating valves used to control the fluid pressure of the two branches to be consistent. The high-pressure gas-liquid separator 12 obtains high-temperature hydrogen-rich gas and residual liquid by separating the gasification reactants. The high-pressure gas-liquid separator 12 is provided with an upper outlet and a lower outlet. The upper outlet outputs high-temperature hydrogen-rich gas, which is further cooled by the first preheater 11, then depressurized to atmospheric pressure by the back pressure valve 7, and enters the atmospheric pressure gas-liquid separator 6 to separate hydrogen-rich gas and effluent. The hydrogen-rich gas is input into the hydrogen purification and supply system for further processing, while the effluent is discharged through the outlet of the atmospheric pressure gas-liquid separator 6. The lower outlet of the high-pressure gas-liquid separator 12 outputs residual liquid to the residual liquid circulation branch.

[0040] The residual liquid circulation branch is used to process the residual liquid output from the waste heat recovery branch to obtain circulating residual liquid. It includes a circulation pump 15, an ejector 16, and a second preheater 17. The residual liquid output from the lower outlet of the high-pressure gas-liquid separator 12 is pressurized by the circulation pump 15. The pressure after pressurization is 2-5 MPa higher than the pressure after pressurization by the oxygen booster pump. After being mixed and pressure regulated by the ejector 16, it is preheated by the second preheater 17 and then injected into the reactor 1 from the circulating residual liquid injection port 110.

[0041] The residual liquid provided by the residual liquid circulation branch and the oxygen provided by the oxygen branch undergo a violent supercritical water oxidation reaction in the internal space of the lower conical shell 106, forming a hydrothermal flame to achieve efficient and thorough degradation of the residual liquid. The high-temperature, low-density gas flow moves upward. The waste liquid gradually flows downward in the annular gap between the cylindrical inner shell 105 and the upper cylindrical outer shell 104 for preheating (approaching or exceeding 374°C). It is further rapidly preheated by the hydrothermal flame in the lower conical space. The waste liquid, which has been fully preheated by the hydrothermal flame, flows upward in a countercurrent manner. Under the coordinated action of the hydrothermal flame and residual oxygen, it is fully vaporized in the inner shell of the cylindrical inner shell 105 to form hydrogen-rich gas, which is discharged from the product outlet 102 of reactor 1. Meanwhile, several conical baffles arranged coaxially and uniformly inside the cylindrical inner shell 105 can achieve gas-solid separation of gasification products. The separated solid particles are recycled into the hydrothermal flame for further degradation. The efficient reaction of the solid particles in the cycle achieves the removal of solid particles from the products, improves the degradation effect, and facilitates subsequent power generation. The unreacted ash is discharged from the ash outlet 108 under the action of gravity.

[0042] The hydrogen purification and supply system is used to purify the hydrogen-rich gas output from the waste heat recovery branch. It includes a purification unit 5, a fuel gas tank 8, and a hydrogen storage tank 4. The hydrogen-rich gas separated by the atmospheric pressure gas-liquid separator 6 is purified by the purification unit 5 to obtain high-purity hydrogen and fuel gas (CH4, CO, etc.). The purification unit 5 includes one or more of the following: pressure swing adsorption (PSA), membrane separation, and chemical absorption. The fuel gas enters the fuel gas tank 8 and connects to the injector 16. The fuel gas and circulating residual liquid are mixed and pressure-regulated to supplement the hydrothermal flame, achieving the formation of the hydrothermal flame without the need for external auxiliary fuel input. The high-purity hydrogen enters the hydrogen storage tank 4 for external output.

[0043] In summary, the reactor design for the thermoelectric self-sufficient hydrogen production system provided by this invention is divided into a hydrothermal flame zone, a material preheating zone, and a gasification zone. This structural design allows for rapid preheating of the material via a hydrothermal flame after initial preheating of the waste liquid, improving both gasification efficiency and hydrogen production efficiency. An internal flue gas purification structure separates solid particles from the product, facilitating subsequent power generation, while the solid particles falling into the flame zone enhance gasification. Supercritical water gasification products are cooled and pressurized before entering a high-pressure gas-liquid separator. The resulting residual liquid is recycled to avoid secondary emissions. Part of the gasification reaction product is used to power the system, while the other part serves as a heat source for preheating the residual liquid and waste liquid, ensuring the formation and stability of the hydrothermal flame. The hydrogen-rich gas separated by the high-pressure gas-liquid separator is purified; high-purity hydrogen is stored and output, while other fuels (CH4, CO, etc.) are used to replenish the organic concentration of the residual liquid, ensuring the stability of the hydrothermal flame. This forms a thermoelectric self-sufficient, independently distributed hydrogen production system. This system requires no external power or fuel input. It utilizes the chemical energy of organic matter in waste liquid and the thermal and pressure energy of the gasification reaction process in a branched and graded manner to treat organic waste without secondary emissions. At the same time, it can generate hydrogen and fuel gas for external output, thus having the dual effects of environmental protection and energy saving.

[0044] In this document, the term "embodiment" means that a particular feature, structure, or characteristic described in connection with an embodiment may be included in at least one embodiment of this application. The appearance of this phrase in various places throughout the specification does not necessarily refer to the same embodiment, nor is it a separate or alternative embodiment mutually exclusive with other embodiments. It will be explicitly and implicitly understood by those skilled in the art that the embodiments described herein can be combined with other embodiments.

[0045] The embodiments described above are merely illustrative of several implementations of the present invention, and while the descriptions are specific and detailed, they should not be construed as limiting the scope of the present invention. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of the present invention, and these modifications and improvements all fall within the scope of protection of the present invention. Therefore, the scope of protection of this patent should be determined by the appended claims.

[0046] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims

1. A thermoelectric self-sufficient hydrogen energy production system, characterized by, The system comprises a reactor, a waste liquid branch, an oxygen branch, a waste heat recovery branch, a residual liquid circulation branch and a hydrogen purification and gas supply system, wherein: The reactor comprises a top circular end cover, an upper cylindrical shell, a lower conical shell and a bottom circular end cover connected in sequence, a cylindrical inner shell is coaxially arranged inside the upper cylindrical shell, the upper edge of the cylindrical inner shell is connected with the top circular end cover, the lower edge of the cylindrical inner shell is higher than the lower edge of the upper cylindrical shell, the inside of the cylindrical inner shell is a gasification reaction zone, the annular gap between the cylindrical inner shell and the upper cylindrical shell is a waste liquid preheating zone, the center of the top circular end cover is provided with a gasification product outlet of the gasification reaction zone, the waste liquid preheating zone is provided with a waste liquid injection inlet at the intersection ring of the waste liquid preheating zone and the top circular end cover, a coaxial nozzle is coaxially arranged on the bottom circular end cover, the coaxial nozzle comprises an inner tube and an outer tube, the outer tube is provided with an oxygen injection inlet, the inner tube is provided with a circulating residual liquid injection inlet, the coaxial nozzle outlet extends into the internal space of the lower conical shell, the coaxial nozzle outlet position does not exceed the lower edge of the upper cylindrical shell, and the bottom circular end cover is further provided with a slag discharge outlet. The waste liquid branch is connected with the waste liquid injection inlet, and is used for pretreating organic waste liquid and providing the pretreated organic waste liquid to the reactor. The oxygen branch is connected with the oxygen injection inlet and is used for providing oxygen to the reactor. The waste heat recovery branch is connected with the gasification product outlet, and the waste heat recovery branch drives a steam turbine to drive a generator to generate electricity by using the gasification reactant output by the reactor, and simultaneously processes the gasification reactant to obtain hydrogen-rich gas and residual liquid. The residual liquid circulation branch is connected with the circulating residual liquid injection inlet and is used for processing the residual liquid output by the waste heat recovery branch to obtain circulating residual liquid, and the circulating residual liquid and the oxygen provided by the oxygen branch occur violent supercritical water oxidation reaction in the internal space of the lower conical shell to form a hot liquid flame. The hydrogen purification and gas supply system is connected with the waste heat recovery branch and is used for purifying the hydrogen-rich gas output by the waste heat recovery branch to obtain high-purity hydrogen and fuel gas.

2. The thermoelectric self-contained hydrogen energy production system of claim 1, wherein, A plurality of conical folded plate groups are coaxially and uniformly arranged in the cylindrical inner shell, each conical folded plate group comprises an upper conical folded plate and a lower conical folded plate, and the minimum distance between the upper conical folded plate and the lower conical folded plate is less than the radius of the cylindrical inner shell.

3. The thermoelectric self-contained hydrogen energy production system of claim 1, wherein, The waste liquid branch comprises a waste liquid tank, a waste liquid booster pump and a first preheater, the organic waste liquid in the waste liquid tank is pressurized to 23 MPa or above by the waste liquid booster pump, then preheated by the first preheater and then enters the reactor from the waste liquid injection inlet, wherein the solid particle concentration in the organic waste liquid is 1-20%, and the size of the solid particles is less than 50 um.

4. The thermoelectric self-contained hydrogen energy production system of claim 3, wherein, The oxygen branch comprises an oxygen tank and an oxygen booster pump, the oxygen in the oxygen tank is pressurized to 23 MPa or above by the oxygen booster pump, and then injected into the reactor from the oxygen injection inlet, and the oxygen flow is 1.05-1.25 times the amount of oxygen required for complete oxidation of residual liquid organic matter.

5. The thermoelectric self-contained hydrogen energy production system of claim 4, wherein, The waste heat recovery branch comprises a first branch, a second branch and a high-pressure gas-liquid separator, wherein: The first branch includes a steam turbine, a generator and a first pressure regulating valve, the gasification reactant output by the reactor drives the steam turbine to drive the generator to operate, the generator supplies power to the pumps and valves in the system, and the surplus power is stored or output externally, and the gasification reactant enters the high-pressure gas-liquid separator after pressure regulation by the first pressure regulating valve. The second branch includes a second preheater and a second pressure regulating valve, the gasification reactant output by the reactor enters the second preheater to preheat the residual liquid, the temperature of the gasification reactant is preliminarily cooled to below 350℃, and then enters the high-pressure gas-liquid separator after pressure regulation by the second pressure regulating valve.

6. The thermoelectric self-contained hydrogen energy production system of claim 5, wherein, The first pressure regulating valve and the second pressure regulating valve are linkage pressure regulating valves for controlling the fluid pressure of the first branch and the second branch to be consistent.

7. The thermoelectric self-contained hydrogen energy production system of claim 5, wherein, The waste heat recovery branch further includes a back pressure valve and a normal-pressure gas-liquid separator, the high-pressure gas-liquid separator obtains hydrogen-rich gas and residual liquid by separating the gasification reactant, and the high-pressure gas-liquid separator is provided with an upper outlet and a lower outlet, wherein: The upper outlet outputs the hydrogen-rich gas, the hydrogen-rich gas is further cooled by the first preheater, then is reduced to normal pressure by the back pressure valve, and enters the normal-pressure gas-liquid separator to separate the discharge liquid; The lower outlet outputs the residual liquid to the residual liquid circulation branch.

8. The thermoelectric self-contained hydrogen energy production system of claim 7, wherein, The residual liquid circulation branch includes a circulating pump, an ejector and a second preheater, the residual liquid enters the ejector after pressure increase by the circulating pump, is mixed and pressure-regulated, and then is preheated by the second preheater before being injected into the reactor from the circulating residual liquid injection port, and the pressure of the circulating pump after pressure increase is 2-5Mpa higher than the pressure of the oxygen gas pressurizing pump after pressure increase.

9. The thermoelectric self-contained hydrogen energy production system of claim 8, wherein, The hydrogen gas purification and supply system includes a purification device, a fuel gas tank and a hydrogen storage tank, the hydrogen-rich gas output by the normal-pressure gas-liquid separator is purified by the purification device to obtain high-purity hydrogen gas and fuel gas, the high-purity hydrogen gas enters the hydrogen storage tank for external output, and the fuel gas enters the fuel gas tank, the fuel gas tank is connected with the ejector, and is used to supplement the concentration of organic matter in the circulating residual liquid.

10. The thermoelectric self-contained hydrogen energy production system of claim 9, wherein, The purification device includes one or more of a pressure swing adsorption device, a membrane separation device and a chemical absorption device.

Images