CN111171876A - High-temperature supercritical water gasification carbon-based energy hydrogen production system and method - Google Patents
High-temperature supercritical water gasification carbon-based energy hydrogen production system and method Download PDFInfo
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- CN111171876A CN111171876A CN202010168149.6A CN202010168149A CN111171876A CN 111171876 A CN111171876 A CN 111171876A CN 202010168149 A CN202010168149 A CN 202010168149A CN 111171876 A CN111171876 A CN 111171876A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Abstract
The invention discloses a high-temperature supercritical water gasification carbon-based energy hydrogen production system and a method, which belong to the field of clean and efficient energy conversion and utilization. The high temperature that produces further promotes supercritical fluid temperature, directly takes place the mixing of molecule contact formula with the coal slurry that treats gasification in supercritical water gasifier and preheats, has broken through the temperature resistant restriction that indirect heat transfer high pressure was equipped structural alloy, realizes the supercritical water gasification reaction of higher temperature, maximize hydrogen production efficiency. The invention fully utilizes the heat generated in the hydrogen production process, reduces the energy consumption, realizes the direct and efficient conversion of the chemical energy of the coal-based energy sources such as coal and the like into the hydrogen energy by coupling the supercritical water thermal combustion and the supercritical water gasification and combining various heat energy recycling measures such as a heat regenerator and the like, simultaneously meets the requirement of environmental protection and does not discharge any harmful gas such as nitrogen oxide and the like.
Description
Technical Field
The invention belongs to the technical field of clean and efficient energy conversion and utilization, and particularly relates to a high-temperature supercritical water gasification carbon-based energy hydrogen production system and method.
Background
Hydrogen energy is considered as the most promising clean energy source in the 21 st century. Under the background of coping with global warming and energy transformation, hydrogen energy is listed in the national energy strategy deployment by multiple countries due to the advantages of various sources, cleanness, low carbon, flexibility, high efficiency, rich application scenes and the like. Hydrogen belongs to a secondary energy source, and free hydrogen does not exist in nature, but exists in the forms of compounds such as hydrocarbon, water, biomass and the like, so that the hydrogen almost cannot be directly obtained from nature although the reserves are abundant and considerable. Today's hydrogen production, storage and utilization technologies are also being developed and perfected, and about 48% of hydrogen is derived from natural gas, 30% is derived from petroleum, 18% is derived from coal, and the rest is derived from water and biomass worldwide. The hydrogen production product produced by water electrolysis is clean, but the cost is high and far exceeds that of fossil fuel, so the method is not suitable for large-scale industrial production. China is a country taking coal as a main energy source, the coal is taken as a raw material to prepare hydrogen for end users to use, harmful waste is intensively treated to reduce pollution to the lowest level, and the method is a relatively environment-friendly hydrogen production route. Although the traditional coal gasification hydrogen production process is mature, the investment cost is high, pure oxygen is required, the gas separation cost is high, the hydrogen production efficiency is low, and CO is generated2The large discharge amount and incomplete utilization of the chemical energy of coal hinder large-scale industrial popularization.
The supercritical hydrothermal combustion produces a flame in water above the critical point, referred to as the hydrothermal flame, which is a more vigorous oxidation reaction. The removal rate and the removal rate of organic matters can be accelerated by the local high temperature of more than 1000 ℃ generated by the hydrothermal flame, and meanwhile, the extra heat released by combustion can be used as a heat source to maintain the self-reaction without extra heating to keep the supercritical state. The supercritical gasification technology utilizes the special physical and chemical properties of water when the temperature and the pressure reach or are higher than the critical point (374.3 ℃ and 22.1MPa) of the water to gasify and convert carbon, hydrogen and oxygen elements in coal into hydrogen and carbon dioxide, simultaneously thermochemically decomposes part of supercritical water to prepare hydrogen, and directly and efficiently converts the chemical energy of the coal into hydrogen energy. Compared with the traditional method of burning coal by one fire, the method has the advantages that the power generation and hydrogen production efficiency is obviously improved, and the one-time investment and the operation cost after large-scale production are obviously reduced. The gasification product can generate electricity, supply heat and steam, and can also produce chemical products with high added value, thereby realizing the high-efficiency, clean and pollution-free conversion and utilization of coal energy. But is limited by the temperature resistance limit of materials of a high-pressure reactor and a preheater, the current supercritical water gasification process is mostly carried out at the temperature of 400-500 ℃, the hydrogen generation efficiency is low, and a part of energy in coal can be concentrated in solid-phase products after reaction. Secondly, the low gasification temperature can also cause polycyclic aromatic hydrocarbons in the materials to be incapable of being completely degraded, and further treatment is needed to be carried out on reaction products, thereby increasing the system flow and the equipment cost. Therefore, on the premise of not additionally consuming external energy, how to improve the operating temperature of the supercritical water gasification process and fully utilize the energy contained in the coal is a key problem for further improving the industrial prospect of the supercritical water gasification process.
Disclosure of Invention
In order to overcome the defects of the prior art, reasonably utilize coal, particularly further release considerable energy in a gasified solid-phase product, improve the gasification temperature, improve the hydrogen production efficiency and reduce the hydrogen production cost, the invention aims to provide a high-temperature supercritical water gasification carbon-based energy hydrogen production system and method with the function of self-separation of heat-mineralized residues in the combustion of carbon residue water phase, and the high-efficiency clean hydrogen production by carbon-based energy such as coal can be realized.
In order to achieve the purpose, the invention adopts the technical scheme that:
a high-temperature supercritical water gasification carbon-based energy hydrogen production system comprises a cyclone supercritical water heating combustion reactor 10 and a supercritical water gasification reactor 3, a coal slurry input pipe 1 is connected to a cold fluid side inlet of a heat regenerator 2, a hot fluid side outlet of the heat regenerator 2 is communicated with a plurality of gasification nozzles 24 in the supercritical water gasification reactor 3, an outlet of the supercritical water gasification reactor 3 is connected to a hot fluid side inlet of the heat regenerator 2, a cold fluid side outlet of the heat regenerator 2 is communicated with an inlet of a gas phase separator A5 through a temperature regulating pressure regulator A4, a top outlet of the gas phase separator A5 is connected to a hydrogen separation purification unit 6, a bottom outlet is connected to a temperature regulating pressure regulator B7, an outlet of the temperature regulating pressure regulator B7 is communicated with an inlet of a gas phase separator B8, a bottom outlet of the gas phase separator B8 is connected to a water heating flame nozzle 14 arranged on the upper portion of the cyclone supercritical water heating combustion reactor 10 through a boosting unit 9, a bottom center of the cyclone The chemical reactor 3 is communicated; the side surface of the bottom of the spiral-flow supercritical water heat combustion reactor 10 is provided with a slurry outlet 23.
The supercritical hot fluid guide cone 22 is positioned at the top of the supercritical water gasification reactor 3, and the plurality of gasification nozzles 24 are uniformly distributed at the same horizontal height at the upper part of the side surface of the supercritical water gasification reactor 3.
The hydrothermal flame nozzle 14 is positioned at the upper part of the side surface of the supercritical water-heating combustion reactor 10, the hydrothermal flame nozzle 14 is provided with two input ports, one input port is communicated with the high-pressure oxidant input pipe 13, and the other input port is connected to the outlet of the pressure boosting unit 9.
Supercritical hot fluid guide cone 22 is the round platform shape, with the sunken profile matching in supercritical water heat combustion reactor 10 bottom, and supercritical water gasification reactor 3 is in the center of round platform with the intercommunication mouth of spiral-flow type supercritical water heat combustion reactor 10.
Pressure-bearing wall A25 of supercritical water gasification reactor 3 is wrapped up by high-efficient cooling jacket A20, pressure-bearing wall B17 of supercritical water hot combustion reactor 10 is wrapped up by high-efficient cooling jacket B16, be equipped with coolant import 19 and coolant export 21 on the high-efficient cooling jacket A20, be equipped with coolant import 15 and coolant export 18 on the high-efficient cooling jacket B16, the structure of high-efficient cooling jacket A20 and high-efficient cooling jacket B16 can be for pressing from both sides cover, individual layer screw channel or multilayer screw channel etc..
The slag slurry outlet 23 is communicated with the waste heat recovery and subsequent treatment unit 12 through the flow regulating valve 11.
The invention also provides a hydrogen production method based on the high-temperature supercritical water gasification carbon-based energy hydrogen production system, wherein a product discharged by the supercritical water gasification reactor 3 flows back to the heat regenerator 2 to preheat a new coal slurry material in the coal slurry input pipe 1, and the preheated new coal slurry is sprayed into the supercritical water gasification reactor 3 through a plurality of gasification nozzles 24 to be gasified;
the product after heat exchange changes the temperature and pressure state in the temperature and pressure regulating device A4, the separation of hydrogen is realized in the gas phase separator A5, the remaining product is continuously transported to the temperature and pressure regulating device B7 to regulate the temperature and pressure, and the separation of the gas mainly containing carbon dioxide from the product is realized; after the solid phase product mainly containing carbon residue is pressurized in the boosting unit 9, the solid phase product and the oxidant of the high-pressure oxidant input pipe 13 are injected into the supercritical water heat combustion reactor 10 together through the hydrothermal flame nozzle 14 again, and complete release of carbon-based energy is realized after the solid phase product and the oxidant are ignited, so that heat is provided for the supercritical hot fluid required by subsequent supercritical water gasification, and the reaction in the supercritical water gasifier 3 is maintained to continue.
When the operation of removing the burning-out slag slurry is carried out, the flow of the coal slurry and the air is firstly reduced to one third of the stable operation flow, then the flow of the burning-out slag slurry is controlled through the flow control valve 11, the phenomenon that the outflow speed influences the outflow stability of the resultant of the supercritical hot fluid guide cone 22 is prevented, and the discharged burning-out slag slurry enters a waste heat recovery and subsequent processing unit for further operation.
The heat regenerator 2 preheats the new coal slurry material in the coal slurry input pipe 1 to 300-450 ℃;
the temperature and pressure states of the temperature and pressure regulator A4 are changed to 80-150 ℃ and 6-10MPa, and the specific numerical value is determined according to the flow. The temperature and pressure regulating device B7 regulates the temperature and pressure to 20-60 deg.C and 0.1-3 MPa. The pressure in the pressure boosting unit 9 is increased to 25-30 MPa.
The oxidant can be liquid oxygen, oxygen or air, and the coolant can be water, air, heat conduction oil, organic slurry or oxidant.
Compared with the prior art, the invention has the beneficial effects that:
1. according to the invention, by coupling supercritical water thermal combustion and supercritical water gasification, a high-temperature supercritical hot fluid generated by hydrothermal combustion of a gasified solid-phase product is directly mixed and preheated with coal slurry to be gasified in a molecular contact manner, so that the temperature resistance limit of an indirect heat exchange high-pressure equipment structural alloy is broken through, a supercritical water gasification reaction at a higher temperature can be realized, and the hydrogen production efficiency is maximized.
2. The invention adopts the spiral-flow supercritical water heat combustion reactor to ensure that the spiral-flow is generated in the reactor, the burning slag slurry after the hydrothermal combustion is deposited around the supercritical hot fluid guide cone with a special structure by means of inertia, and then flows out through the slag slurry outlet, and further carries out waste heat recovery for subsequent treatment.
3. According to the invention, the heat regenerator is used for preheating the new coal slurry, so that the high-quality heat energy of the gasification product is fully recovered, the temperature of supercritical water gasification is fully increased on the premise of not introducing external energy, and the yield of hydrogen is increased.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention.
Wherein, 1, a coal slurry input pipe; 2. a heat regenerator; 3. a supercritical water gasification reactor; 4. a temperature and pressure regulating device A; 5. a gas phase separator A; 6. a hydrogen separation purification unit; 7. a temperature and pressure regulating device B; 8. a gas phase separator B; 9. a voltage boosting unit; 10. a cyclone supercritical hydrothermal combustion reactor; 11. a flow regulating valve; 12. a waste heat recovery and subsequent processing unit; 13. a high pressure oxidant input pipe; 14. a hydrothermal flame nozzle; 15. a coolant inlet; 16. a high-efficiency cooling jacket B; 17. a pressure bearing wall B; 18. a coolant outlet; 19. a coolant inlet; 20. a high-efficiency cooling jacket A; 21. a coolant outlet; 22. a supercritical thermal fluid guide cone; 23. a slurry outflow port; 24. a gasification nozzle; 25. the pressure-bearing wall A.
Detailed Description
The present invention will now be described in further detail with reference to specific examples, which are intended to be illustrative, but not limiting, of the invention.
Referring to fig. 1, an outlet of a supercritical water gasification reactor 3 is connected to a hot fluid side inlet of a heat regenerator 2, a hot fluid side outlet of the heat regenerator 2 is communicated with an inlet of a gas phase separator a5 through a temperature and pressure regulating and regulating device a4, a top outlet of the gas phase separator a5 is connected to a hydrogen separation and purification unit 6, a bottom outlet of the gas phase separator a is connected to a temperature and pressure regulating and regulating device B7, an outlet of the temperature and pressure regulating and regulating device B7 is communicated with a gas phase separator B8, a bottom outlet of the gas phase separator B8 is connected to a hydrothermal flame nozzle 14 mounted on the upper part of a cyclone supercritical water heat combustion reactor 10 through a boosting unit 9 and a high-temperature oxidant input pipe 13, and the center of the bottom of the cyclone supercritical; the side surface of the bottom of the spiral-flow supercritical water thermal combustion reactor 10 is provided with a slurry outlet 23 which is communicated with a waste heat recovery and subsequent treatment unit 12 through a flow control valve 11; the coal slurry input pipe 1 is connected to the cold fluid side inlet of the heat regenerator 2, and the hot fluid side outlet of the heat regenerator 2 is communicated with a plurality of gasification nozzles 24.
In the operation process, the product discharged from the supercritical water gasification reactor 3 flows back to the heat regenerator 2 to preheat the new coal slurry material in the coal slurry input pipe 1, and the preheated new coal slurry is sprayed into the supercritical water gasification reactor 3 through a plurality of gasification nozzles 24 distributed on the same horizontal height on the upper part of the side surface of the supercritical water gasification reactor 3 to be gasified. The heat-exchanged product was further subjected to temperature and pressure changes in a temperature and pressure regulator a4, and hydrogen separation was achieved in a gas phase separator a 5. The remaining product is continuously conveyed to a temperature and pressure regulating device B7 to further regulate the temperature and the pressure, and the separation of the gas mainly containing carbon dioxide from the product is realized. Therefore, after the solid phase product mainly containing carbon residue is pressurized to 25MPa in the pressure boosting unit 9, the solid phase product is injected into the supercritical water heat combustion reactor 10 together with the oxidant of the high-pressure oxidant input pipe 13 through the hydrothermal flame nozzle 14 again, complete release of carbon-based energy is further realized after ignition, heat is provided for the supercritical hot fluid required by the subsequent supercritical water gasification, and the reaction in the supercritical water gasifier 3 is maintained to continue. In the operation process, the high-efficiency cooling jacket A20 and the high-efficiency cooling jacket B16 are kept open, so that the wall surface is prevented from being over-heated.
After a period of stable operation, the composition of the effluent from the burnt slag slurry outlet 23 is observed to determine whether the operation of removing the burnt slag slurry is carried out. When the device is used for removing the burning-out slag slurry, the flow of the coal slurry and the air is firstly reduced to one third of the stable operation flow, so that the additional waste caused by insufficient reaction is avoided. And then the flow of the burnout slag slurry is controlled by the flow control valve 11, the phenomenon that the outflow speed influences the outflow stability of the product of the supercritical hot fluid guide cone 22 is prevented, and the discharged burnout slag slurry enters a waste heat recovery and subsequent processing unit for further operation. The high-efficiency cooling jacket A20 and the high-efficiency cooling jacket B16 are kept open, and the wall surface is prevented from being over-heated.
In conclusion, the invention has the function of self-separation of hot-mineralized residues in carbon residue water phase combustion, after solid-liquid-gas separation of gasified products, the carbon residue in the solid-liquid phase is reused for supercritical water heat combustion in a supercritical water heat combustion reactor, and the chemical energy of carbon-based energy such as coal and the like is thoroughly utilized. The high temperature that produces further promotes supercritical fluid temperature, directly takes place the mixing of molecule contact formula with the coal slurry that treats gasification in supercritical water gasifier and preheats, has broken through the temperature resistant restriction that indirect heat transfer high pressure was equipped structural alloy, realizes the supercritical water gasification reaction of higher temperature, maximize hydrogen production efficiency. The whole process flow comprises the use of a heat regenerator and a waste heat recovery and post-treatment unit, so that the heat generated in the hydrogen production process is fully utilized, and the energy consumption is reduced. The invention realizes the direct and high-efficiency conversion of the chemical energy of the coal-based energy sources such as coal and the like into hydrogen energy by coupling supercritical water thermal combustion and supercritical water gasification and combining various heat energy recycling measures such as a heat regenerator and the like, meets the requirement of environmental protection and does not discharge any harmful gas such as nitrogen oxide and the like.
Claims (10)
1. The utility model provides a high temperature supercritical water gasification carbon base energy hydrogen manufacturing system, including spiral-flow type supercritical water heat combustion reactor (10) and supercritical water gasification reactor (3), a serial communication port, coal slurry input tube (1) connects to regenerator (2) cold fluid side entry, a plurality of gasification nozzle (24) switch-on in regenerator (2) hot fluid side export and the supercritical water gasification reactor (3), export of supercritical water gasification reactor (3) connects to regenerator (2) hot fluid side entry, regenerator (2) cold fluid side export is through temperature regulation voltage regulator A (4) and gas phase separator A (5) entry switch-on, gas phase separator A (5) top export connects to hydrogen separation purification unit (6), the bottom export connects to temperature regulation voltage regulator B (7), supercritical water voltage regulator B (7) export and gas phase separator B (8) entry switch-on, gas phase separator B (8) bottom export is installed in spiral-flow type supercritical water heat combustion reactor (10) and supercritical water gasification reactor (3) through booster unit (9), a plurality of gasification nozzles in A hydrothermal flame nozzle (14) at the upper part of the thermal combustion reactor (10), the center of the bottom of the cyclone supercritical water thermal combustion reactor (10) is communicated with the supercritical water gasification reactor (3) through a supercritical hot fluid guide cone (22); the side surface of the bottom of the spiral-flow supercritical water heat combustion reactor (10) is provided with a slurry outlet (23).
2. The high-temperature supercritical water gasification carbon-based energy hydrogen production system according to claim 1, wherein the supercritical hot fluid guide cone (22) is located at the top of the supercritical water gasification reactor (3), and the plurality of gasification nozzles (24) are uniformly distributed at the same level at the upper part of the side surface of the supercritical water gasification reactor (3).
3. The high-temperature supercritical water gasification carbon-based energy hydrogen production system according to claim 1, wherein the hydrothermal flame nozzle (14) is located at the upper side of the supercritical water hot combustion reactor (10), and the hydrothermal flame nozzle (14) has two input ports, one of which is communicated with the high-pressure oxidant input pipe (13), and the other of which is connected to the outlet of the pressure boosting unit (9).
4. The high-temperature supercritical water gasification carbon-based energy hydrogen production system according to claim 1, 2 or 3, wherein the supercritical hot fluid guide cone (22) is in the shape of a circular truncated cone and is matched with a bottom concave profile of the supercritical water hot combustion reactor (10), and a communication port between the supercritical water gasification reactor (3) and the cyclone supercritical water hot combustion reactor (10) is arranged in the center of the circular truncated cone.
5. The high-temperature supercritical water gasification carbon-based energy hydrogen production system according to claim 1, 2 or 3, wherein the pressure-bearing wall A (25) of the supercritical water gasification reactor (3) is wrapped by a high-efficiency cooling jacket A (20), the pressure-bearing wall B (17) of the supercritical water heat combustion reactor (10) is wrapped by a high-efficiency cooling jacket B (16), the high-efficiency cooling jacket A (20) is provided with a coolant inlet (19) and a coolant outlet (21), the high-efficiency cooling jacket B (16) is provided with a coolant inlet (15) and a coolant outlet (18), and the high-efficiency cooling jacket A (20) and the high-efficiency cooling jacket B (16) are structured as a jacket, a single-layer spiral channel or a multi-layer spiral channel.
6. The high-temperature supercritical water gasification carbon-based energy hydrogen production system according to claim 5, wherein the slurry outlet (23) is communicated with the waste heat recovery and subsequent treatment unit (12) through a flow control valve (11).
7. The hydrogen production method of the high-temperature supercritical water gasification carbon-based energy hydrogen production system according to claim 1, characterized in that the product discharged from the supercritical water gasification reactor (3) flows back to the heat regenerator (2) to preheat the new coal slurry material in the coal slurry input pipe (1), and the preheated new coal slurry is sprayed into the supercritical water gasification reactor (3) through a plurality of gasification nozzles (24) to be gasified;
the product after heat exchange changes the temperature and pressure state in the temperature and pressure regulating device A (4), the separation of hydrogen is realized in the gas phase separator A (5), the remaining product is continuously conveyed to the temperature and pressure regulating device B (7) to regulate the temperature and pressure, and the separation of the gas mainly containing carbon dioxide from the product is realized; after the solid phase product mainly containing carbon residue is pressurized in the pressure boosting unit (9), the solid phase product and the oxidant of the high-pressure oxidant input pipe (13) are injected into the supercritical water heat combustion reactor (10) through the hydrothermal flame nozzle (14) again, and after the solid phase product and the oxidant are ignited, the complete release of carbon-based energy is realized, heat is provided for the supercritical hot fluid required by the subsequent supercritical water gasification, and the reaction in the supercritical water gasifier (3) is maintained to be continuously carried out.
8. The hydrogen production method according to claim 7, wherein the operation of removing the cinder slurry is performed by firstly reducing the flow rates of the coal slurry and air to one third of the stable operation flow rate, then controlling the flow rate of the cinder slurry through the flow control valve (11) to prevent the outflow too fast from affecting the outflow stability of the product of the supercritical hot fluid guide cone (22), and the discharged cinder slurry enters a waste heat recovery and subsequent processing unit for further operation.
9. The hydrogen production method according to claim 7, characterized in that the regenerator (2) preheats the fresh coal slurry material in the coal slurry input pipe (1) to 300-450 ℃; the temperature and pressure states of the temperature and pressure regulator A (4) are changed to 80-150 ℃ and 6-10MPa, and the specific numerical value is determined according to the flow; the temperature and pressure of the temperature and pressure regulating device B (7) are regulated until the temperature range is 20-60 ℃ and the pressure range is 0.1-3 MPa; the pressure in the pressure boosting unit (9) is increased to 25-30 MPa.
10. The method for producing hydrogen according to claim 7, wherein the oxidant is liquid oxygen, oxygen or air, and the coolant is water, air, heat transfer oil, organic slurry or oxidant.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111569780A (en) * | 2020-05-24 | 2020-08-25 | 西安交通大学 | Internal mixing type supercritical hydrothermal synthesis nano powder reactor |
| CN113048465A (en) * | 2021-03-26 | 2021-06-29 | 中国科学院工程热物理研究所 | Coal-fired power generation system and method for coal gasification with supercritical water |
| CN114408859A (en) * | 2021-11-18 | 2022-04-29 | 杨家华 | Novel method and device for producing hydrogen by using liquid oxide and supercritical water |
| CN114655924A (en) * | 2022-04-27 | 2022-06-24 | 西安交通大学 | Yield regulation and control system and method for coal supercritical water gasification hydrogen production |
| CN116606675A (en) * | 2023-07-20 | 2023-08-18 | 太原理工大学 | Method and device for improving gasification efficiency of lump coal |
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2020
- 2020-03-11 CN CN202010168149.6A patent/CN111171876A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111569780A (en) * | 2020-05-24 | 2020-08-25 | 西安交通大学 | Internal mixing type supercritical hydrothermal synthesis nano powder reactor |
| CN113048465A (en) * | 2021-03-26 | 2021-06-29 | 中国科学院工程热物理研究所 | Coal-fired power generation system and method for coal gasification with supercritical water |
| CN113048465B (en) * | 2021-03-26 | 2022-08-12 | 中国科学院工程热物理研究所 | Coal-fired power generation system and method for coal gasification with supercritical water |
| CN114408859A (en) * | 2021-11-18 | 2022-04-29 | 杨家华 | Novel method and device for producing hydrogen by using liquid oxide and supercritical water |
| CN114655924A (en) * | 2022-04-27 | 2022-06-24 | 西安交通大学 | Yield regulation and control system and method for coal supercritical water gasification hydrogen production |
| CN116606675A (en) * | 2023-07-20 | 2023-08-18 | 太原理工大学 | Method and device for improving gasification efficiency of lump coal |
| CN116606675B (en) * | 2023-07-20 | 2023-09-29 | 太原理工大学 | Method and device for improving gasification efficiency of lump coal |
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