An internal heat generation type high temperature supercritical water gasification system and process

Abstract

An endothermic high-temperature supercritical water gasification system includes an endothermic supercritical water gasification reactor with a hydrothermal flame zone at the center upper part, a cold fluid side inlet of a supercritical pressure regenerator connected to fossil fuels or organic waste, a cold fluid side outlet connected to the inlet of a material collecting pipe, and the outlet of the material collecting pipe is divided into two paths, one path is connected to a hydrothermal combustion nozzle at the inlet of the hydrothermal flame zone through a combustion material distribution pipe, and the other path is connected to a plurality of gasification material nozzles at the outlet of the hydrothermal flame zone through a gasification material distribution pipe, wherein the hydrothermal combustion nozzle is also connected to a high-pressure oxidant supply pipeline, and the material sprayed by the gasification material nozzle meets the supercritical hydrothermal flame at the outlet of the hydrothermal flame zone to achieve molecular contact mixing heating; the lower part of the endothermic supercritical water gasification reactor is a material gasification reaction zone. The present invention also provides a corresponding process, which can ensure that the temperature of the gasification reaction zone of the gasification reactor can reach a high temperature of 700°C or above, and it is expected to obtain an organic hydrogenation rate of more than 200%.

Description

Technical Field

[0001] The present invention belongs to the technical field of clean and efficient conversion and utilization of energy, and in particular relates to an internal heat generation type high-temperature supercritical water gasification system and process. Background Art

[0002] With the gradual increase in the consumption of traditional fossil fuels, the greenhouse effect and environmental pollution caused by it are becoming more and more serious, which makes the research and development of clean renewable new energy a major issue in the world. As the most promising new energy, hydrogen energy has the advantages of abundant sources, light weight, high calorific value, no carbon emissions, and can be directly used in hydrogen fuel cells, making it a research hotspot in various countries in recent years. In 2018, China's coal accounted for nearly 60% of primary energy consumption. The clean conversion and utilization of coal is of great significance for energy conservation and emission reduction and building an ecological power. In addition, the output of urban / industrial sludge is huge, with an organic matter content of up to 50-85% and a calorific value of 5-18MJ / kg, which has the potential for resource utilization. However, in the traditional utilization of coal and sludge, inefficiency is the biggest problem. Converting it into gaseous fuel, especially hydrogen energy, is a more efficient utilization method. The traditional coal gasification process has the following technical problems: low hydrogen yield; poor adaptability to coal types and high coal quality requirements; short service life of burners and refractory bricks and easy damage; syngas easily carries ash and water, and syngas coolers are prone to ash accumulation; gasification equipment is difficult to discharge slag and easy to clog, etc.

[0003] Supercritical water gasification technology (SCWG) utilizes the special properties of supercritical water (SCW) to add reactants into the SCWG reactor for pyrolysis and gasification without adding oxidants to produce high calorific value gases such as hydrogen and methane, and organic matter will not generate byproducts such as coke during the reaction. SCWG hydrogen production technology is one of the most promising hydrogen production technologies, with high reaction efficiency and high hydrogen selectivity. However, due to the temperature resistance limit of high-pressure reactors and preheater materials, the current large-scale SCWG process reaction temperature is mostly carried out at 400-600℃. The low gasification temperature seriously affects the conversion of fossil fuels / organic waste to H2 in the SCWG process, and the hydrogen yield is limited. In addition, due to the low temperature of the SCWG gasification process, the polycyclic aromatic hydrocarbons in the material cannot be completely degraded, and the reaction products need to be further processed, which greatly increases the system process and equipment cost. How to achieve a higher temperature supercritical water gasification reaction has become an important bottleneck restricting the development of the SCWG process. Summary of the invention

[0004] In order to overcome the shortcomings of the conventional SCWG hydrogen production process in the above-mentioned prior art, the purpose of the present invention is to provide an endothermic high-temperature supercritical water gasification system and process, which utilizes organic matter such as coal, urban / industrial sludge, etc. to prepare hydrogen-rich gas. The fuel material is rapidly released heat and heated to a high temperature of more than 1000°C through hydrothermal combustion in the hydrothermal flame zone at the top of the gasification reactor, and then flows downward to directly mix with the gasification material to complete intermolecular heat transfer, thereby ensuring that the temperature of the gasification reaction zone of the gasification reactor can reach a high temperature of 700°C or above, and it is expected to obtain an organic matter hydrogenation rate of more than 200%.

[0005] In order to achieve the above object, the technical solution adopted by the present invention is:

[0006] The invention discloses an internal heat generation type high temperature supercritical water gasification system, comprising a supercritical pressure regenerator 1 and an internal heat type supercritical water gasification reactor 2, wherein the upper center of the internal heat type supercritical water gasification reactor 2 is surrounded by a refractory heat storage material 7 to form a hydrothermal flame zone, the cold fluid side inlet of the supercritical pressure regenerator 1 is connected to fossil fuel or organic waste, and the cold fluid side outlet is connected to the inlet of a material collecting and transporting pipe 12, the outlet of the material collecting and transporting pipe 12 is divided into two paths, one path is connected to a hydrothermal combustion nozzle 6 at the inlet of the hydrothermal flame zone through a combustion material distribution pipe 13, and the other path is connected to a plurality of gasification material nozzles 8 at the outlet of the hydrothermal flame zone through a gasification material distribution pipe 14, wherein the hydrothermal combustion nozzle 6 is also connected to a high pressure oxidant supply pipeline 11, and the material sprayed by the gasification material nozzle 8 meets the supercritical hydrothermal flame at the outlet of the hydrothermal flame zone to realize molecular contact mixing heating; the lower middle part of the internal heat type supercritical water gasification reactor 2 is a material gasification reaction zone.

[0007] Furthermore, the outlet of the internal heat type supercritical water gasification reactor 2 is connected to the inlet of the hot fluid side of the supercritical pressure regenerator 1 , and the outlet of the hot fluid side of the supercritical pressure regenerator 1 is connected to the inlet of the high pressure separator 3 .

[0008] Furthermore, the hydrothermal combustion nozzle 6 is arranged at the top center of the hydrothermal flame zone, with the spraying direction facing downward.

[0009] Furthermore, the shape of the hydrothermal flame zone is spherical or ellipsoidal, and the lower part is open as an outlet. Each gasification material nozzle 8 is located near the lower outlet of the hydrothermal flame zone and is installed on the side of the internal heating supercritical water gasification reactor 2, with the injection direction obliquely downward.

[0010] Furthermore, a wall cooling jacket 10 is disposed around the main wall 9 of the internal heating type supercritical water gasification reactor 2 , and the wall cooling jacket 10 is provided with a coolant inlet 15 and a coolant outlet 16 .

[0011] Furthermore, the wall cooling jacket 10 has a structure of a jacket, a single-layer or multi-layer spiral channel.

[0012] Furthermore, the top outlet of the high-pressure separator 3 is connected to the gas separation unit 5 , and the bottom outlet is connected to the pressure reduction-liquid-solid separation unit 4 .

[0013] Furthermore, the present invention also provides an internal heat generation type high temperature supercritical water gasification process based on the internal heat generation type high temperature supercritical water gasification system, and the process is as follows:

[0014] High-temperature and high-pressure supercritical water is introduced into the inner part of the inner-heating supercritical water gasification reactor 2. When the inner temperature of the inner-heating supercritical water gasification reactor 2 rises to the supercritical condition, the fossil fuel or organic waste enters through the cold fluid side inlet of the supercritical pressure regenerator 1, and exchanges heat with the supercritical water flowing out from the bottom of the inner-heating supercritical water gasification reactor 2;

[0015] The preheated fossil fuel or organic waste is divided into two at the outlet of the material collecting and transporting pipe 12, one of which is connected to the hydrothermal combustion nozzle 6 through the combustion material distribution pipe 13, and the other is connected to a plurality of gasification material nozzles 8 through the gasification material distribution pipe 14. The fossil fuel or organic waste is mixed with the preheated high-pressure oxidant at the hydrothermal combustion nozzle 6 and enters the hydrothermal flame zone at the top of the endothermic supercritical water gasification reactor 2;

[0016] Fossil fuel or organic waste forms flames in the hydrothermal flame zone, instantly releasing heat and raising the temperature to above 1000°C. The gasified material sprayed by the gas materialization nozzle 8 meets the supercritical hydrothermal flame at the lower part of the hydrothermal flame zone, thereby realizing molecular contact mixing heating, ensuring that the temperature of the material gasification reaction zone in the lower part of the internal heat type supercritical water gasification reactor 2 is not lower than 700°C.

[0017] Furthermore, the internal heat type supercritical water gasification reactor 2 transports the high temperature and high pressure fluid after the reaction to the hot fluid side inlet of the supercritical pressure regenerator 1 for preliminary heat exchange and heating of the fossil fuel or organic waste. The cooled high pressure fluid enters the high pressure separator 3 through the hot fluid side outlet of the supercritical pressure regenerator 1, and the high pressure separator 3 separates the high pressure fluid between the gas phase and the liquid-solid phase.

[0018] Furthermore, during the reaction process, the coolant enters the wall cooling jacket 10 through the coolant inlet 15 and flows out through the coolant outlet 16 at the bottom. The outflowing high-temperature coolant is used for waste heat recovery power generation, or is used to supplement the preheating heat of fossil fuels or organic waste through a multi-stage supercritical pressure regenerator 1.

[0019] Compared with the prior art, the present invention has the following beneficial effects:

[0020] 1. Use supercritical water gasification technology to replace traditional gasification technology: In the supercritical water gasification reaction, water is not only a reaction medium, but also can transfer part of its own hydrogen to the gas phase product through water steam reforming (SRR) and water gas shift (WGSR) reactions, consuming the by-product CO while greatly improving the hydrogen production efficiency, making the hydrogen gasification rate in organic matter exceed 200%.

[0021] 2. Coupling supercritical hydrothermal combustion technology can further increase the supercritical water gasification reaction temperature, thereby further increasing the hydrogen yield. Some materials undergo supercritical hydrothermal combustion reaction, and then instantly release heat and heat up to above 1000°C, and then directly mix with the gasified material to achieve the latter's rapid heating to a higher temperature, without the need for physical heat exchange area, avoiding the need for high temperature and high pressure equipment.

[0022] 3. It can effectively classify and recycle various gas products, and will not emit pollutants such as sulfur oxides, nitrogen oxides, and dust outside the system. It uses a high-pressure separator to effectively separate H2 and CO2, and can relatively easily achieve zero carbon dioxide emissions, reducing the cost of subsequent gas separation units, and has very good environmental benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 It is a schematic diagram of the system structure of the present invention.

[0024] Among them: 1. Supercritical pressure regenerator; 2. Internal heating supercritical water gasification reactor; 3. High-pressure separator; 4. Pressure reduction-liquid-solid separation unit; 5. Gas separation unit; 6. Hydrothermal combustion nozzle; 7. Refractory heat storage material; 8. Gasification material nozzle; 9. Main body wall; 10. Wall cooling jacket; 11. High-pressure oxidant supply pipeline; 12. Material gathering and transportation pipeline; 13. Combustion material piping; 14. Gasification material piping; 15. Coolant inlet; 16. Coolant outlet. DETAILED DESCRIPTION

[0025] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "one side", "one end", "one side" and the like indicate positions or positional relationships based on the positions or positional relationships shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, in the description of the present invention, unless otherwise specified, "multiple" means two or more.

[0026] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0027] like Figure 1 As shown, in this embodiment, a supercritical water thermal combustion internal heat generation type high-temperature supercritical water gasification system is provided, including a supercritical pressure regenerator 1 for preheating fossil fuels or organic wastes, an internal heat type supercritical water gasification reactor 2 connected to the cold fluid outlet side of the supercritical pressure regenerator 1, and a high-pressure separator 3 connected to the hot fluid outlet side of the supercritical pressure regenerator 1. The liquid outlet of the high-pressure separator 3 is connected to a pressure reduction-liquid-solid separation unit 4, and the gas phase outlet is connected to a gas fractionation unit 5. The outlet of the internal heat type supercritical water gasification reactor 2 is connected to the hot fluid side inlet of the supercritical pressure regenerator 1.

[0028] The upper center of the endothermic supercritical water gasification reactor 2 is surrounded by a refractory heat storage material 7 to form a hydrothermal flame zone. In this embodiment, the hydrothermal flame zone is spherical or ellipsoidal in shape, and the lower part is open as an outlet. A hydrothermal combustion nozzle 6 with a downward spray direction is arranged at the top center of the endothermic supercritical water gasification reactor 2, that is, the top center of the hydrothermal flame zone. Obviously, the hydrothermal combustion nozzle 6 is located at the entrance of the hydrothermal flame zone; a plurality of gasification material nozzles 8 are arranged near the lower outlet of the hydrothermal flame zone. The gasification material nozzles 8 can be installed on the side of the endothermic supercritical water gasification reactor 2 on the mechanical mounting structure, and their spray direction is obliquely downward, and preferably symmetrically centered.

[0029] A wall cooling jacket 10 may be provided around the main wall 9 of the internal heating type supercritical water gasification reactor 2. The wall cooling jacket 10 is provided with a coolant inlet 15 and a coolant outlet 16. The structure of the wall cooling jacket 10 may be in the form of a jacket, a single-layer or multi-layer spiral channel, etc.

[0030] The cold fluid side inlet of the supercritical pressure regenerator 1 is connected to fossil fuel or organic waste, and the cold fluid side outlet is connected to the inlet of the material collecting pipe 12. The outlet of the material collecting pipe 12 is divided into two paths, one of which is connected to the hydrothermal combustion nozzle 6 through the combustion material distribution pipe 13, and the other is connected to each gasification material nozzle 8 through the gasification material distribution pipe 14, wherein the gasification material distribution pipe 14 is outside the reactor 2, and the hydrothermal combustion nozzle 6 is also connected to the high-pressure oxidant supply pipeline 11. The material sprayed by the gasification material nozzle 8 meets the supercritical hydrothermal flame at the outlet of the hydrothermal flame zone to realize molecular contact mixing heating; the lower part of the internal heat type supercritical water gasification reactor 2 is the material gasification reaction zone.

[0031] According to the above structure, the process of the internal heat generation type high temperature supercritical water gasification process of the present invention is as follows:

[0032] When the system is started, high-temperature and high-pressure supercritical water is introduced into the internal heat type supercritical water gasification reactor 2, and when the internal temperature of the internal heat type supercritical water gasification reactor 2 rises to the supercritical condition. The coolant enters the wall cooling jacket 10 through the coolant inlet 15 and flows out through the coolant outlet 16 at the bottom. At the same time, the fossil fuel or organic waste enters through the cold fluid side inlet of the supercritical pressure regenerator 1, and exchanges heat with the supercritical water flowing out from the bottom of the internal heat type supercritical water gasification reactor 2. The preheated fossil fuel or organic waste is divided into two at the outlet of the material gathering pipe 12, one is connected to the hydrothermal combustion nozzle 6 through the combustion material distribution pipe 13, and the other is connected to a plurality of gasification material nozzles 8 through the gasification material distribution pipe 14. The fossil fuel or organic waste is mixed with the preheated high-pressure oxidant at the hydrothermal combustion nozzle 6 and enters the top of the internal heat type supercritical water gasification reactor 2. The fossil fuel or organic waste forms a flame in the hydrothermal flame zone, and instantly releases heat and rises to more than 1000°C. The gasified material sprayed by the gas materialization nozzle 8 meets the supercritical hydrothermal flame in the lower part of the hydrothermal flame zone, thereby realizing molecular contact mixing heating, ensuring that the temperature of the material gasification reaction zone in the lower part of the internal heating supercritical water gasification reactor 2 is not lower than 700°C.

[0033] The hydrothermal flame zone surrounded by the refractory heat storage material 7 can not only isolate the high-temperature fluid from the main wall 9 at the upper part of the reactor to prevent the main wall 9 from being too hot, but also store heat to ensure that the combustion material can burn stably after passing through the hydrothermal combustion nozzle 6.

[0034] The internal heat type supercritical water gasification reactor 2 transports the high temperature and high pressure fluid after the reaction to the hot fluid side inlet of the supercritical pressure regenerator 1, which can be used to perform preliminary heat exchange and temperature increase for fossil fuels or organic waste, thereby reducing the energy consumption of the system, improving the efficiency of waste heat utilization, and helping to save costs. The cooled high pressure fluid enters the high pressure separator 3 through the hot fluid side outlet of the supercritical pressure regenerator 1.

[0035] The high-pressure separator 3 separates the high-pressure fluid into gas phase and liquid-solid phase. Under the high-pressure conditions of the high-pressure separator 3, CO2 is in a supercritical state (t>31.27℃, p>7.3MPa) and is very soluble in water. Therefore, in addition to completing the conventional separation of gas phase and liquid-solid phase, the high-pressure separator 3 can also separate non-polar gases such as H2 and H2S from polar supercritical CO2.

[0036] The pressure reduction-liquid-solid separation unit 4 is connected to the discharge end of the high-pressure separator 3. The CO2 in the fluid is removed after the pressure is reduced for subsequent recycling; the liquid phase and the solid phase are separated by liquid-solid separation to form inorganic residues and reaction water for subsequent treatment and discharge. The liquid-solid separation equipment in the pressure reduction-liquid-solid separation unit 4 includes but is not limited to a filter press, a belt filter, a filter centrifuge, etc., which can be reasonably selected according to the process requirements and the processing scale.

[0037] The gas separation unit 5 is connected to the gas phase outlet of the high-pressure separator 3. The gas separation method includes but is not limited to pressure swing adsorption, molecular sieve adsorption, etc., which is determined according to the specific gas composition and processing scale. The separated hydrogen enters the hydrogen storage unit or is directly utilized by the hydrogen energy utilization device.

[0038] The main wall 9 of the internal heat type supercritical water gasification reactor 2 is cooled by the coolant flowing in the wall cooling jacket 10. The high temperature coolant flowing out of the coolant outlet 16 can be used for waste heat recovery power generation, or can be used to supplement the preheating heat of fossil fuels or organic wastes through the multi-stage supercritical pressure regenerator 3, further improving the waste heat utilization efficiency of the system and saving costs.

[0039] In summary, the present invention discloses a supercritical hydrothermal combustion internal heat generation type high-temperature supercritical water gasification system and process, which innovatively realizes the hydrothermal flame preheating inside the supercritical water gasification reactor. The fuel material is rapidly released to a high temperature of more than 1000°C through hydrothermal combustion in the hydrothermal flame zone at the top of the gasification reactor, and then flows downward to directly mix with the gasified material to complete the intermolecular heat transfer, thereby ensuring that the temperature of the gasification reaction zone of the gasification reactor can reach a high temperature of more than 700°C. Through the high-temperature supercritical water gasification process, while consuming the by-product CO, the material gasification rate efficiency is greatly improved, and the hydrogenation efficiency is expected to exceed 200%. By hydrothermal combustion for internal heat generation and direct intermolecular heat transfer for preheating the gasified material, not only the temperature resistance limit problem of the high-pressure heat exchanger material is effectively solved, thereby realizing the high-temperature SCWG process above 700°C, but also the physical heat exchange area is greatly reduced, saving the heat exchanger investment. In addition, by setting a supercritical pressure regenerator, the energy of the gasification reactor can be effectively recovered, further improving the system waste heat utilization efficiency and saving costs. This device can realize the clean utilization of energy such as coal and biomass, and can also realize the resource recycling of urban / industrial sludge, thereby preparing hydrogen with low consumption and high efficiency.

[0040] The above contents are only for explaining the technical idea of ​​the present invention and cannot be used to limit the protection scope of the present invention. Any changes made on the basis of the technical solution in accordance with the technical idea proposed by the present invention shall fall within the protection scope of the claims of the present invention.

Claims

1. An internal heat generation type high temperature supercritical water gasification system, comprising a supercritical pressure regenerator (1) and an internal heat type supercritical water gasification reactor (2), characterized in that: The upper center of the internal heat type supercritical water gasification reactor (2) is surrounded by a refractory heat storage material (7) to form a hydrothermal flame zone. The cold fluid side inlet of the supercritical pressure regenerator (1) is connected to fossil fuel or organic waste, and the cold fluid side outlet is connected to the inlet of the material collecting pipe (12). The outlet of the material collecting pipe (12) is divided into two paths, one of which is connected to the hydrothermal combustion nozzle (6) at the inlet of the hydrothermal flame zone through the combustion material distribution pipe (13), and the other is connected to a plurality of gasification material nozzles (8) at the outlet of the hydrothermal flame zone through the gasification material distribution pipe (14). The hydrothermal combustion nozzle (6) is also connected to the high-pressure oxidant supply pipeline (11). The gasification material nozzle (8) ) The injected material meets the supercritical hydrothermal flame at the outlet of the hydrothermal flame zone, realizing molecular contact mixing and heating; the lower middle part of the internal heating type supercritical water gasification reactor (2) is a material gasification reaction zone; the outlet of the internal heating type supercritical water gasification reactor (2) is connected to the inlet of the hot fluid side of the supercritical pressure regenerator (1), and the outlet of the hot fluid side of the supercritical pressure regenerator (1) is connected to the inlet of the high-pressure separator (3); the shape of the hydrothermal flame zone is spherical or ellipsoidal, and the lower part is open as an outlet. Each gasification material nozzle (8) is located near the lower outlet of the hydrothermal flame zone and is installed on the side of the internal heating type supercritical water gasification reactor (2), and the injection direction is obliquely downward.

2. The internal heat generation type high temperature supercritical water gasification system according to claim 1, characterized in that: The hydrothermal combustion nozzle (6) is arranged at the top center of the hydrothermal flame zone, with the spray direction facing downward.

3. The internal heat generation type high temperature supercritical water gasification system according to claim 1, characterized in that: A wall cooling jacket (10) is arranged around the main body wall (9) of the internal heating type supercritical water gasification reactor (2), and the wall cooling jacket (10) is provided with a coolant inlet (15) and a coolant outlet (16).

4. The internal heat generation type high temperature supercritical water gasification system according to claim 3, characterized in that: The wall cooling jacket (10) has a structure of a jacket, a single-layer or multi-layer spiral channel.

5. The internal heat generation type high temperature supercritical water gasification system according to claim 1, characterized in that: The top outlet of the high-pressure separator (3) is connected to a gas separation unit (5), and the bottom outlet is connected to a pressure reduction-liquid-solid separation unit (4).

6. The internal heat generation type high temperature supercritical water gasification process based on the internal heat generation type high temperature supercritical water gasification system according to claim 1 is characterized in that: High-temperature and high-pressure supercritical water is introduced into the internal part of the internal thermal supercritical water gasification reactor (2). When the internal temperature of the internal thermal supercritical water gasification reactor (2) rises to a supercritical condition, fossil fuel or organic waste enters through the cold fluid side inlet of the supercritical pressure regenerator (1) and exchanges heat with the supercritical water flowing out from the bottom of the internal thermal supercritical water gasification reactor (2); The preheated fossil fuel or organic waste is divided into two at the outlet of the material collecting and transporting pipe (12), one of which is connected to the hydrothermal combustion nozzle (6) through the combustion material distribution pipe (13), and the other is connected to a plurality of gasification material nozzles (8) through the gasification material distribution pipe (14). The fossil fuel or organic waste is mixed with the preheated high-pressure oxidant at the hydrothermal combustion nozzle (6) and enters the hydrothermal flame zone at the top of the endothermic supercritical water gasification reactor (2); The fossil fuel or organic waste forms a flame in the hydrothermal flame zone, which instantly releases heat and rises to above 1000°C. The gasified material sprayed by the gasification material nozzle (8) meets the supercritical hydrothermal flame at the lower part of the hydrothermal flame zone, thereby achieving molecular contact mixing heating, ensuring that the temperature of the material gasification reaction zone in the lower part of the internal heating type supercritical water gasification reactor (2) is not less than 700°C.

7. The internal heat generation type high temperature supercritical water gasification process according to claim 6, characterized in that: The internal heat type supercritical water gasification reactor (2) transports the high temperature and high pressure fluid after the reaction to the hot fluid side inlet of the supercritical pressure regenerator (1) for preliminary heat exchange and heating of the fossil fuel or organic waste. The high pressure fluid after cooling enters the high pressure separator (3) through the hot fluid side outlet of the supercritical pressure regenerator (1). The high pressure separator (3) separates the high pressure fluid into a gas phase and a liquid-solid phase.

8. The internal heat generation type high temperature supercritical water gasification process according to claim 6, characterized in that: During the reaction process, the coolant enters the wall cooling jacket (10) through the coolant inlet (15) and flows out through the coolant outlet (16) at the bottom. The outflowing high-temperature coolant is used for waste heat recovery power generation, or is used to supplement the preheating heat of fossil fuels or organic waste through a multi-stage supercritical pressure regenerator (1).

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