CN211896823U - Supercritical water gasification hydrogen production and slurry supercritical water heat combustion coupling system - Google Patents
Supercritical water gasification hydrogen production and slurry supercritical water heat combustion coupling system Download PDFInfo
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Abstract
A supercritical water gasification hydrogen production and slurry supercritical water heat combustion coupling system adopts carbon-based energy, and coal slurry enters a high-pressure preheater after being boosted to exchange heat with supercritical water flowing out of the bottom of a supercritical water gasification reactor; the preheated coal slurry enters a supercritical water gasification reactor to be gasified; the gasification product flowing out of the bottom outlet of the supercritical water gasification reactor enters a separator through the hot fluid side of a high-pressure preheater for separation, and the separated slag slurry enters the supercritical water combustion reactor for supercritical water heat combustion reaction after sequentially passing through a mass component recovery unit, a high-pressure slurry pump and the cold fluid side of a high-pressure heat regenerator; carbon dioxide obtained by the separator and the three-phase separator is sent to the microalgae photosynthetic reactor for microalgae cultivation, the cultivated microalgae enters the centrifugal separator, concentrated algae slurry discharged from the bottom of the centrifugal separator enters the coal slurry preparation unit for water supplement and/or the hydrothermal liquefaction reactor to produce bio-crude oil, and gas such as carbon dioxide obtained by separation returns to the microalgae photosynthetic reactor through a top outlet.
Description
Technical Field
The utility model belongs to the technical field of the clean high-efficient conversion of charcoal base energy utilizes, in particular to supercritical water gasification hydrogen manufacturing and supercritical water heat burning coupled system of thick liquid.
Background
The hydrogen is taken as the most potential new energy, and has the advantages of rich sources, light weight, high heat value, no carbon emission, water as a combustion product, direct application to a hydrogen fuel cell and the like. With the increasing importance of society on the environmental quality, and the wide application of hydrogen in the industrial fields of petroleum, chemical industry, metallurgy, medicine, aerospace and the like, the hydrogen becomes a research hotspot of various countries in recent years. In 2018, the proportion of the Chinese coal accounting for primary energy consumption is close to 60%, clean utilization of the coal is realized, the method has important significance for energy conservation and emission reduction and ecological strengthening, and scale production of hydrogen sources by taking the coal as a raw material is a hydrogen production route which has Chinese characteristics and accords with China's actual solution of hydrogen source problems in the hydrogen energy industry. The traditional coal gasification hydrogen production process has low hydrogen gasification rate and low hydrogen selectivity; the adaptability of coal types is poor, and the requirement on coal quality is high; the service life of the burner and the refractory brick is short, and the burner and the refractory brick are easy to damage; the synthesis gas is easy to carry ash and water, and the synthesis gas cooler is easy to deposit ash; the gasification device has the technical problems of difficult slag discharge, easy blockage and the like.
The supercritical water gasification technology (SCWG) utilizes the special property of supercritical water (SCW), reactants are added into an SCWG reactor to carry out pyrolysis gasification reaction on the premise of not adding an oxidant, high-calorific-value gas such as hydrogen, methane and the like is prepared, and organic matters can not generate byproducts such as coke and the like in the reaction process. The SCWG hydrogen production technology is the most potential hydrogen production technology, and compared with the conventional coal gasification technology, the SCWG hydrogen production technology has high reaction efficiency and high hydrogen selectivity. But is limited by the temperature resistance limit of materials of a high-pressure reactor and a preheater, the current SCWG process is mostly carried out at the temperature of 400-600 ℃, the conversion of coal to H2 in the SCWG process is seriously influenced, and the yield of hydrogen is limited; the low gasification temperature leads to high carbon residue content after gasification, and the residual slurry after gas separation needs to be subjected to harmless treatment and has high energy utilization value. In addition, a large amount of CO is generated in the hydrogen production process of coal SCWG2The direct discharge of the carbon-containing slag slurry brings about a plurality of problems of greenhouse effect and the like, and how to improve the hydrogen efficiency and realize the reutilization of the carbon-containing slag slurry with high energy utilization value and CO2Low cost reuse of (a) becomes a major obstacle limiting the development of SCWG processes.
Disclosure of Invention
In order to overcome the defects of the conventional SCWG hydrogen production process in the prior art, the utility model aims to provide a supercritical water gasification hydrogen production and slurry supercritical water heat combustion coupling system.
In order to realize the purpose, the utility model discloses a technical scheme is:
a supercritical water gasification hydrogen production and slurry supercritical water heat combustion coupling system adopts carbon-based energy, the system is characterized by comprising a coal slurry preparation unit 1, wherein an outlet of the coal slurry preparation unit 1 is connected to a cold fluid side inlet of a high-pressure preheater 3 through a high-pressure coal slurry pump 2, a cold fluid side outlet of the high-pressure preheater 3 is communicated with a first inlet on the upper side surface of a supercritical water gasification reactor 4, a bottom outlet of the supercritical water gasification reactor 4 is connected with a separator through a hot fluid side of the high-pressure preheater 3, a liquid phase outlet of the separator sequentially passes through a mass component recovery unit 9, a high-pressure slurry pump 10 and a cold fluid side of a high-pressure heat regenerator 11 and is connected to a top inlet of a supercritical water heat combustion reactor 12, a side outlet on the bottom surface of the supercritical water heat combustion reactor 12 is connected to an inlet of a three-phase separator 18 through a regulating valve three V3, a hot fluid side of the high-pressure heat regenerator 11; the carbon dioxide discharged from the separator and the three-phase separator 18 is gathered and connected with a first inlet of a microalgae photosynthetic reactor 19, an outlet of the microalgae photosynthetic reactor 19 is communicated with a centrifugal separator 20, a liquid phase outlet at the bottom of the centrifugal separator 20 is connected to the coal slurry preparation unit 1 and/or the hydrothermal liquefaction reactor 21, and a gas phase outlet at the top of the centrifugal separator 20 is connected to a second inlet of the microalgae photosynthetic reactor 19.
Further, the separator comprises a high-pressure gas separator 5 and a low-pressure gas separator 8, an outlet on the hot fluid side of the high-pressure preheater 3 is connected with an inlet of the high-pressure gas separator 5, a gas-phase outlet on the top of the high-pressure gas separator 5 is connected to a component separation unit 15, a liquid-phase outlet on the bottom of the high-pressure gas separator 5 is sequentially connected to the low-pressure gas separator 8 through a temperature regulator 6 and a pressure regulator 7, and a liquid-phase outlet on the bottom of the low-pressure gas separator 8 is connected with an inlet of a component recovery unit 9.
Further, the component separation unit 15 is provided with three outlets, a first outlet outputs hydrogen, a third outlet outputs gas mainly containing carbon dioxide, a second outlet outputs other gases including methane, and the third outlet of the component separation unit 15, the top gas phase outlet of the low-pressure gas separator 8 and the top outlet of the three-phase separator 18 are connected with the first inlet of the microalgae photosynthetic reactor 19 in a converging manner.
Further, an air separation device 13 is used for generating oxygen, an oxygen outlet of the air separation device is connected to a high-pressure oxygen compressor 14, the outlet of the high-pressure oxygen compressor 14 is divided into two paths, the first path is connected to the top inlet of the supercritical water heat combustion reactor 12 through a regulating valve II V2, and the second path is connected to the second inlet on the upper side face of the supercritical water gasification reactor 4 through a regulating valve I V1.
Furthermore, the center of the bottom of the supercritical water hot combustion reactor 12 is communicated with the top of the supercritical water gasification reactor 4, and a flow guide part is arranged at the communicated position; the periphery of the supercritical hydrothermal combustion reactor 12 is provided with a high-efficiency cooling jacket to prevent the wall surface from being over-heated; and an outlet at the side surface of the bottom of the supercritical hydrothermal combustion reactor 12 is used for outputting high-temperature and high-pressure burnt-out slag slurry.
Further, the first inlet of upper portion side and the second inlet of upper portion side of supercritical water gasification reactor 4 all are ring channel structure, and the ring channel inboard is equipped with a plurality of incident spouts.
Further, the utility model also provides a technology based on supercritical water gasification hydrogen manufacturing and thick liquid supercritical water heat burning coupled system lets in high-temperature high-pressure supercritical water in supercritical water heat burning reactor 12 inside, when waiting that supercritical water heat burning reactor 12 and supercritical water gasification reactor 4 inside temperature rise to supercritical state, the coal thick liquid that coal thick liquid preparation unit 1 prepared enters high-pressure preheater 3 after high-pressure coal thick liquid pump 2 steps up, carries out the heat transfer with the supercritical water that flows out in supercritical water gasification reactor 4 bottom; the preheated coal slurry flows out of a cold fluid side outlet of the high-pressure preheater 3 and then enters the supercritical water gasification reactor 4 through a first inlet on the upper side surface of the supercritical water gasification reactor 4 to complete gasification;
the gasification product flowing out from the bottom outlet of the supercritical water gasification reactor 4 enters a separator through the hot fluid side of the high-pressure preheater 3 for separation, and the obtained slag slurry sequentially passes through the mass component recovery unit 9, the high-pressure slurry pump 10 and the cold fluid side of the high-pressure heat regenerator 11 and then enters the supercritical water heat combustion reactor 12 from the top inlet of the supercritical water heat combustion reactor 12 for supercritical water heat combustion reaction;
carbon dioxide obtained by the third outlet of the component separation unit 15, the low-pressure gas separator 8 and the three-phase separator 18 is sent to a microalgae photosynthetic reactor 19 for microalgae cultivation, the cultivated microalgae enters a centrifugal separator 20, concentrated algae slurry discharged from the bottom of the centrifugal separator 20 enters a coal slurry preparation unit 1 for water supplement and/or a hydrothermal liquefaction reactor 21 for producing bio-crude oil, and gas such as carbon dioxide obtained by separation by the centrifugal separator 20 returns to the microalgae photosynthetic reactor 19 through a top outlet.
Further, 4 bottom outlet outflow's of supercritical water gasification reactor gasification result separates in 3 heat fluid sides entering high-pressure gas separator 5 of high-pressure preheater, and the gaseous product that the separation obtained enters into component separation unit 15 through the top export and carries out the component separation, and bottom outlet exhaust sediment thick liquid gets into low pressure gas separator 8 and carries out degasification processing after thermoregulator 6, the pressure regulator 7 adjusts the temperature and adjusts the pressure in proper order, and the sediment thick liquid after the degasification is sent into there is matter component recovery unit 9, there is matter component recovery unit 9 to retrieve sulphur simple substance, aqueous ammonia and ammonium sulfate.
Further, oxygen is obtained by separation through an air separation device 13, and is divided into two paths after being boosted by a high-pressure oxygen compressor 14, the first path enters a supercritical water hot combustion reactor 12 to be uniformly mixed with preheated slag slurry and then is rapidly combusted to release heat, and combusted combustion materials enter a supercritical water gasification reactor 4 to realize intermolecular direct mixing heat exchange with the gasification materials; the second path enters a supercritical water gasification reactor 4 to assist in carrying out a supercritical water gasification reaction; after being discharged from the outlet on the side surface of the bottom of the supercritical hydrothermal combustion reactor 12, the high-temperature high-pressure burned-out slag slurry after the supercritical hydrothermal combustion reaction sequentially enters a three-phase separator 18 through the heat fluid side of a high-pressure heat regenerator 11, a cooler 16 and a decompressor 17, and harmless coal ash obtained by separation is discharged from the bottom of the three-phase separator 18 and then enters a coal slurry preparation unit 1 to be mixed with coal.
Further, wait that supercritical water heat combustion reactor 12 and supercritical water gasification reactor 4 inside temperature rise to supercritical state, the high-efficient coolant jacket that supercritical water heat combustion reactor 12 periphery set up lets in the coolant, prevents that the wall from overtemperature.
Compared with the prior art, the beneficial effects of the utility model are that:
1. supercritical water gasification technology is used for replacing the traditional gasification technology: water is not only a reaction medium but also can transfer part of hydrogen to a gas-phase product through water vapor reforming (SRR) and water vapor conversion (WGSR) reactions in the supercritical water gasification reaction process, and the hydrogen production efficiency is greatly improved while the byproduct CO is consumed, so that the hydrogen gasification efficiency is far over 100 percent.
2. The supercritical water heat combustion technology and the supercritical water gasification technology are innovatively and organically coupled, the carbon-containing slag slurry which is generated by coal in the SCWG process and has higher energy utilization value is combusted in the supercritical water heat combustion reactor to release heat, and the gasified materials are heated through intermolecular direct heat transfer, so that the overall energy consumption of the system is greatly reduced, the emission of harmful substances is reduced, and high-value clean conversion and thorough utilization of the coal are fully realized.
3. CO generated in supercritical hydrothermal combustion and hydrothermal gasification processes of coal by using microalgae photosynthetic reactor2The microalgae is collected and utilized, the cultivated microalgae is subjected to preliminary treatment and has various application forms, not only can be subjected to hydrothermal liquefaction to prepare biological crude oil, but also can be mixed with coal slurry and then is gasified together to prepare hydrogen, and zero carbon emission of coal conversion and utilization is really realized.
Drawings
Fig. 1 is a schematic diagram of the system structure of the present invention.
Wherein: 1. a coal slurry preparation unit; 2. a high pressure coal slurry pump; 3. a high-pressure preheater; 4. a supercritical water gasification reactor; 5. a high pressure gas separator; 6. a thermostat; 7. a voltage regulator; 8. a low pressure gas separator; 9. a mass component recovery unit; 10. a high pressure slurry pump; 11. a high pressure regenerator; 12. a supercritical hydrothermal combustion reactor; 13. an air separation plant; 14. a high pressure oxygen compressor; 15. a component separation unit; 16. a temperature reducer; 17. a pressure reducer; 18. a three-phase separator; 19. a microalgae photosynthetic reactor; 20. a centrifugal separator; 21. a hydrothermal liquefaction reactor.
Detailed Description
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "one side", "one end", "one side", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore should not be construed as limiting the present invention. In addition, in the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
As shown in fig. 1, the embodiment provides a carbon-based energy high-temperature supercritical water gasification hydrogen production and carbon residue slurry supercritical water heat combustion coupling process system, which comprises a coal slurry preparation unit 1 and a high-pressure coal slurry pump 2, wherein an outlet of the coal slurry preparation unit 1 is connected to a cold fluid side inlet of a high-pressure preheater 3 through the high-pressure coal slurry pump 2, a cold fluid side outlet of the high-pressure preheater 3 is communicated with a first inlet on the upper side surface of a supercritical water gasification reactor 4, a bottom outlet of the supercritical water gasification reactor 4 is communicated with an inlet of a high-pressure gas separator 5 through a hot fluid side of the high-pressure preheater 3, a bottom outlet of the high-pressure gas separator 5 is connected to a low-pressure gas separator 8 through a temperature regulator 6 and a pressure regulator 7 in sequence, a bottom outlet of the low-pressure gas separator 8 is connected to a top inlet of a supercritical water heat combustion reactor 12 through a mass, the outlet of the side face of the bottom of the supercritical hydrothermal combustion reactor 12 is connected to the inlet of the three-phase separator 18 through a regulating valve III V3, the heat fluid side of the high-pressure heat regenerator 11, the cooler 16 and the pressure reducer 17, and the liquid phase outlet of the lower part of the three-phase separator 18 is communicated with the coal slurry preparation unit 1.
When the system starts, let in high-temperature high-pressure supercritical water in supercritical water heat combustion reactor 12 inside, wait that supercritical water heat combustion reactor 12 and supercritical water gasification reactor 4 inside temperature rise to supercritical state time, the high-efficient coolant jacket that supercritical water heat combustion reactor 12 periphery set up lets in the coolant, prevents that the wall from overtemperature. Meanwhile, coal is treated by the coal slurry preparation unit 1, then is boosted by the high-pressure coal slurry pump 2 and then enters the high-pressure preheater 3, and exchanges heat with supercritical water flowing out of the bottom of the supercritical water gasification reactor 4. The preheated coal slurry flows out from a cold fluid side outlet of the high-pressure preheater 3 and then enters the supercritical water gasification reactor 4 through a first inlet on the upper side surface of the supercritical water gasification reactor 4 to complete gasification. The gasification product that 4 bottom outlets of supercritical water gasification reactor flow gets into high-pressure gas separator 5 through 3 heat fluid sides of high-pressure preheater and separates, the gaseous phase product that obtains of separation gets into component separation unit 15 through the top export and carries out subsequent processing, the sediment thick liquid that the bottom outlet was discharged gets into low pressure gas separator 8 after the thermoregulator 6, pressure regulator 7 adjusts the temperature and adjusts the pressure in proper order and carries out the degasification treatment, the sediment thick liquid after the degasification gets into in supercritical water heat combustion reactor 12 from supercritical water heat combustion reactor 12 top entry behind having matter component recovery unit 9 in proper order, high-pressure thick liquid pump 10, 11 cold fluid sides of high-pressure regenerator.
The oxygen separated by the air separation device 13 is boosted by a high pressure oxygen compressor 14 and then divided into two paths. First way is through governing valve two V2 and gets into supercritical water heat combustion reactor 12 by supercritical water heat combustion reactor 12 top entry, and it burns fast with the sediment thick liquid after the homogeneous mixing in the reactor after preheating and releases heat, and the burning material after the burning gets into supercritical water gasification reactor 4 and the direct mixing heat transfer between the molecule is realized to the gasification material. The second way passes through a second inlet on the upper side surface of the supercritical water gasification reactor 4 through a regulating valve V1, and the oxygen inlet amount of the second way changes according to the material components and the change of the operation conditions in the reactor, so that the higher hydrogen yield of the material in the supercritical water gasification reactor 4 is realized. After the reacted high-temperature high-pressure burned-out slag slurry is discharged from an outlet at the bottom side of the supercritical hydrothermal combustion reactor 12, the high-temperature high-pressure burned-out slag slurry respectively passes through a heat fluid side of the high-pressure heat regenerator 11, the cooler 16 and the depressor 17 and then enters the three-phase separator 18, and the separated harmless coal ash is discharged from the bottom of the three-phase separator 18 and then enters the coal slurry preparation unit 1 to be mixed with coal.
The gas phase product obtained by the separation of the high-pressure gas separator 5 is delivered to the component separation unit 15 through the top outlet, and the third outlet gas of the component separation unit 15, the top outlet gas of the low-pressure gas separator 8 and the top outlet gas of the three-phase separator 18 are converged and then introduced into the first inlet of the microalgae photosynthetic reactor 19 to provide CO2 for the cultivation of microalgae. The cultivated microalgae enter a centrifugal separator 20 through an outlet of the microalgae photosynthetic reactor 19, concentrated algae slurry discharged from the bottom of the centrifugal separator 20 enters the coal slurry preparation unit 1 or the hydrothermal liquefaction reactor 21, and gas such as carbon dioxide obtained by separation returns to the microalgae photosynthetic reactor 19 through a top outlet.
The first entry of upper portion side and the second entry of upper portion side of supercritical water gasification reactor 4 all are the ring channel structure, and the ring channel inboard is equipped with a plurality of injection spouts, and this structure can guarantee the quick homogeneous mixing of gasification slurry and required oxygen in the reactor inside.
The component separation unit 15 is provided with three outlets, a first outlet outputs hydrogen, a third outlet outputs gas mainly comprising carbon dioxide, and a second outlet outputs other gases such as methane. Gas separation methods include, but are not limited to, pressure swing adsorption, molecular sieve adsorption, and the like, which are determined by the specific gas composition and process scale. The separated hydrogen enters a hydrogen storage unit or is directly utilized by a hydrogen energy utilization device. The active ingredient recovery unit 9 is used for recovering elemental sulfur, ammonia water, ammonium sulfate, and the like.
To sum up, the utility model discloses a carbon back energy high temperature supercritical water gasification hydrogen manufacturing and carbon residue thick liquid supercritical water heat burning coupling process system, it is with supercritical water heat burning technology, supercritical water gasification technology and CO2The microalgae trapping and cultivating technologies are organically coupled, so that high-value conversion and utilization of coal and zero carbon emission are realized. The carbon-containing slag slurry with high energy utilization value generated by coal in the SCWG process is combusted in the supercritical water heat combustion reactor to release heat, and the gasified material is heated through direct heat transfer among molecules, so that the overall energy consumption of the system is greatly reduced, the emission of harmful substances is reduced, and high-value clean conversion and thorough utilization of the coal are fully realized. CO generated in the process of coal combustion and gasification2The separation and collection are carried out and the microalgae are used for photosynthesis cultivation, and the carbon energy source complementary collection utilization is effectively completed. The device can realize high-value clean conversion and utilization of coal, can be applied to clean utilization of biomass energy sources such as microalgae and lignin, and resource recycling of municipal/industrial sludge, kitchen garbage and the like, and accordingly can prepare hydrogen with low consumption and high efficiency.
The above contents are only for explaining the technical idea of the present invention, and the protection scope of the present invention cannot be limited thereby, and any modification made on the basis of the technical solution according to the technical idea of the present invention all fall within the protection scope of the claims of the present invention.
Claims (6)
1. The utility model provides a supercritical water gasification hydrogen production and thick liquid supercritical water heat combustion coupling system, adopt the carbon base energy, a serial communication port, including coal thick liquid preparation unit (1), coal thick liquid preparation unit (1) export is connected to high-pressure preheater (3) cold fluid side entry through high-pressure coal thick liquid pump (2), high-pressure preheater (3) cold fluid side export and supercritical water gasification reactor (4) upper portion side first entry switch-on, supercritical water gasification reactor (4) bottom export is through high-pressure preheater (3) hot-fluid side separator, separator liquid phase export is in proper order through having mass component recovery unit (9), high-pressure slurry pump (10), high-pressure regenerator (11) cold fluid side to supercritical water heat combustion reactor (12) top entry, supercritical water heat combustion reactor (12) bottom side export is through governing valve three (V3), high-pressure slurry pump (11) side hot-fluid side, The cooler (16) and the decompressor (17) are connected to an inlet of the three-phase separator (18), and a liquid phase outlet at the lower part of the three-phase separator (18) is communicated with the coal slurry preparation unit (1); the carbon dioxide discharged from the separator and the three-phase separator (18) is converged and connected with a first inlet of the microalgae photosynthetic reactor (19), an outlet of the microalgae photosynthetic reactor (19) is communicated with a centrifugal separator (20), a liquid phase outlet at the bottom of the centrifugal separator (20) is connected to the coal slurry preparation unit (1) and/or the hydrothermal liquefaction reactor (21), and a gas phase outlet at the top of the centrifugal separator (20) is connected to a second inlet of the microalgae photosynthetic reactor (19).
2. The supercritical water gasification hydrogen production and slurry supercritical water hot combustion coupling system of claim 1, wherein the separator comprises a high-pressure gas separator (5) and a low-pressure gas separator (8), the outlet of the hot fluid side of the high-pressure preheater (3) is connected with the inlet of the high-pressure gas separator (5), the gas phase outlet at the top of the high-pressure gas separator (5) is connected to the component separation unit (15), the liquid phase outlet at the bottom of the high-pressure gas separator (5) is connected to the low-pressure gas separator (8) sequentially through a temperature regulator (6) and a pressure regulator (7), and the liquid phase outlet at the bottom of the low-pressure gas separator (8) is connected with the inlet of the mass component recovery unit (9).
3. The supercritical water gasification hydrogen production and slurry supercritical water thermal combustion coupling system of claim 2, characterized in that the component separation unit (15) is provided with three outlets, the first outlet outputs hydrogen, the third outlet outputs gas mainly comprising carbon dioxide, the second outlet outputs other gases including methane, and the third outlet of the component separation unit (15), the gas phase outlet at the top of the low-pressure gas separator (8) and the gas phase outlet at the top of the three-phase separator (18) are converged and connected with the first inlet of the microalgae photosynthetic reactor (19).
4. The supercritical water gasification hydrogen production and slurry supercritical water thermal combustion coupling system as claimed in claim 1, wherein oxygen is produced by air separation unit (13), the oxygen outlet is connected to high pressure oxygen compressor (14), the outlet of high pressure oxygen compressor (14) is divided into two paths, the first path is connected to the top inlet of supercritical water thermal combustion reactor (12) via regulating valve two (V2), and the second path is connected to the second inlet of the upper side of supercritical water gasification reactor (4) via regulating valve one (V1).
5. The supercritical water gasification hydrogen production and slurry supercritical water hot combustion coupling system of claim 1, wherein the bottom center of the supercritical water hot combustion reactor (12) is communicated with the top of the supercritical water gasification reactor (4), and a flow guide piece is arranged at the communication position; the periphery of the supercritical hydrothermal combustion reactor (12) is provided with an efficient cooling jacket to prevent the wall surface from being over-heated; the outlet on the side surface of the bottom of the supercritical hydrothermal combustion reactor (12) is used for outputting high-temperature and high-pressure burnt-out slag slurry.
6. The supercritical water gasification hydrogen production and slurry supercritical water thermal combustion coupling system of claim 1, wherein the first inlet on the upper side and the second inlet on the upper side of the supercritical water gasification reactor (4) are both in a ring channel structure, and the inner side of the ring channel is provided with a plurality of injection nozzles.
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| CN114740141A (en) * | 2022-04-27 | 2022-07-12 | 西安交通大学 | Experimental measurement system and method for hydrogen supercritical water thermal combustion characteristics |
| CN114740141B (en) * | 2022-04-27 | 2023-04-28 | 西安交通大学 | Experiment measurement system and method for hydrogen supercritical hydrothermal combustion characteristics |
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