A supercritical water oxidation system for treating organic waste adapted to thermal power peak regulation

Abstract

The present invention relates to the technical fields of coal-fired power generation and organic waste treatment, and specifically to a supercritical water oxidation system for treating organic waste that is adapted for thermal power peak regulation. The system comprises a reaction device, an oxidant delivery system, a material delivery system, a steam delivery system, and a product waste heat utilization system; an air separation unit is connected to an air preheater, which is connected to a second heat exchange unit; the second heat exchange unit is connected to a first oxygen delivery pipeline and a second oxygen delivery pipeline; the first oxygen delivery pipeline is connected to a compressor, which is connected to the oxygen inlet of the reaction device; the second oxygen delivery pipeline is connected to the air preheater, which is connected to a steam delivery system; the steam delivery system is connected to the compressor, which is connected to the reaction device. The present invention reduces the amount of heat absorbed by the material in the reaction device by preheating the oxygen, accelerates the reaction rate, and solves the problems of safe variable load operation of the boiler and the high cost of supercritical water oxidation treatment of organic waste.

Description

Technical Field

[0001] The present invention relates to the technical field of coal-fired thermal power generation and organic waste treatment, and in particular to a supercritical water oxidation system for treating organic waste adapted for thermal power peak regulation. Background Art

[0002] To fully leverage the flexible operating capabilities of thermal power units, deep peak shaving will become the norm for coal-fired units. During deep peak shaving, power plant boilers will alternate between full load, low load, and even lower loads. This not only reduces power generation efficiency but also increases the risk of safety incidents such as abnormal flameout, high-temperature heating surface tube bursts, and creep fracture failures.

[0003] When the power plant's power load is reduced, to ensure the economy and safety of boiler operation, the power plant boiler can be operated at a relatively safe, stable, and economical load. At this time, while meeting the power load, the supercritical steam generated by the remaining load can undergo a supercritical water oxidation reaction. Supercritical water oxidation is the full name of the English term "Supercritical Water Oxidation," or SCWO for short. SCWO utilizes the unique physical and chemical properties of supercritical water to achieve efficient oxidative degradation of toxic and hazardous organic pollutants. Supercritical water oxidation relies on the exothermic reaction to maintain the system's thermal balance, eliminating the need for external heat supplementation. The equipment is small, safe, and meets containment requirements. Supercritical water oxidation technology has demonstrated significant technical advantages in treating difficult-to-degrade, toxic, and hazardous organic matter. However, there are relatively high costs associated with the safe operation of boilers with variable loads and the treatment of organic waste with supercritical water oxidation. Summary of the Invention

[0004] In order to solve the problem of high cost in the safe operation of boilers with variable loads and the supercritical water oxidation treatment of organic waste, the purpose of the present invention is to provide a supercritical water oxidation treatment system for organic waste that is adapted to thermal power peak regulation.

[0005] To achieve the above objectives, the technical solutions of the present invention are as follows.

[0006] A first aspect of the present invention provides a supercritical water oxidation system for treating organic waste that is adapted for thermal power peak regulation, comprising a reaction device, an oxidant delivery system, a material delivery system, a steam delivery system, and a product waste heat utilization system; the material inlet of the reaction device is connected to the material delivery system; the oxidant delivery system comprises an air separation unit and an air preheater; the product waste heat utilization system comprises a second heat exchange unit; the first oxygen outlet of the air separation unit is connected to the first inlet of the air preheater, and the second oxygen outlet of the air separation unit is connected to the second heat exchange unit; the oxygen outlet of the second heat exchange unit is connected to a first oxygen delivery pipeline and a second oxygen delivery pipeline; the first oxygen delivery pipeline is connected to a compressor, and the compressor is connected to the oxygen inlet of the reaction device; the second oxygen delivery pipeline is connected to the second inlet of the air preheater, and the first outlet of the air preheater is connected to the steam delivery system; the first steam outlet of the steam delivery system is connected to the compressor, and the third steam outlet of the steam delivery system is connected to the reaction device.

[0007] The present invention provides oxygen, material, and steam to a reaction device through an oxidant delivery system, a material delivery system, and a steam delivery system to achieve a supercritical water oxidation reaction. This allows efficient and clean utilization of the boiler's residual load. Specifically, when the power generation load is adjusted, the residual steam at the steam delivery system outlet is utilized for supercritical water oxidation treatment. This allows the steam delivery system to operate under a safe load while utilizing the residual load for supercritical water oxidation treatment of coal slime wastewater. By preheating oxygen, the present invention reduces the amount of heat absorbed by the material in the reaction device, accelerates the reaction rate, and solves the high cost problem associated with variable-load safe operation of the boiler and supercritical water oxidation treatment of organic waste.

[0008] Preferably, the steam delivery system includes an oxygen-enriched combustion boiler, the first inlet of the oxygen-enriched combustion boiler is connected to the first outlet of the air preheater, and the first steam outlet of the oxygen-enriched combustion boiler is connected to the compressor, and is configured to utilize the steam generated by the oxygen-enriched combustion boiler to provide a power source for driving the compressor.

[0009] Preferably, the outer wall of the reaction device has an interlayer chamber, which is filled with cold wall water; the inlet of the interlayer chamber is connected to the condensate pipeline; the outlet of the interlayer chamber is connected to the first inlet of the high-pressure heater, and the first outlet of the high-pressure heater is connected to the oxygen-enriched combustion boiler.

[0010] The reaction device of the present invention is provided with cold wall water to prevent the wall temperature of the reaction device from being too high. The cold wall water is the condensed water of the boiler. After absorbing heat, it enters the high-pressure heater, thereby increasing the steam temperature of the high-pressure heater, reducing the steam extraction of the turbine, and improving the power generation efficiency of the unit.

[0011] Preferably, the material conveying system includes a material mixing device, a material conveying pump and a material preheating unit, the outlet of the material mixing device is connected to the inlet of the material conveying pump, the outlet of the material conveying pump is connected to the first inlet of the material preheating unit; the first outlet of the material preheating unit is connected to the material inlet of the reaction device.

[0012] Preferably, the product waste heat utilization system includes a first heat exchange unit, a second heat exchange unit and a third heat exchange unit, the heat exchange medium outlet of the material preheating unit is connected to the heat exchange medium inlet of the first heat exchange unit; the product inlet of the first heat exchange unit is connected to the product outlet of the reaction device, the product outlet of the first heat exchange unit is connected to the inlet of the second heat exchange unit, the outlet of the second heat exchange unit is connected to the inlet of the third heat exchange unit, and the outlet of the third heat exchange unit is connected to the gas-solid-liquid separation device; the heat exchange medium inlet of the third heat exchange unit is connected to the condensate pipeline, and the heat exchange medium outlet of the third heat exchange unit is connected to the first inlet of the low-pressure heater.

[0013] Preferably, the second inlet of the low-pressure heater is connected to the condensate pipeline, the outlet of the low-pressure heater is connected to the deaerator, the outlet of the deaerator is connected to the feed water pump, and the feed water pump is connected to the high-pressure heater.

[0014] Preferably, the second steam outlet of the steam delivery system is connected to a power generation system.

[0015] Beneficial effects of the present invention:

[0016] 1. The present invention provides oxygen, material and steam to the reaction unit through an oxidant delivery system, a material delivery system and a steam delivery system to realize supercritical water oxidation reaction, which can efficiently and cleanly utilize the residual load of the boiler, that is, when adjusting the power generation load, the residual steam at the steam delivery system outlet is used for supercritical water oxidation treatment, so that the steam delivery system can be operated under a safe load while utilizing the residual load to carry out supercritical water oxidation treatment of coal slime wastewater. The present invention reduces the heat absorption of the material in the reaction unit by preheating oxygen, accelerates the reaction speed, and solves the problem of high cost when the boiler is operated safely with variable load and when the supercritical water oxidation is used to treat organic waste.

[0017] 2. The present invention utilizes the waste heat of the product after supercritical water oxidation treatment in a graded manner, and uses the waste heat of the product to preheat the material, preheat the oxygen at the inlet of the oxygen-enriched combustion boiler, and heat the condensate, thereby reducing the amount of heat absorbed by the material in the reaction device, accelerating the reaction speed, and improving the thermal efficiency and power generation efficiency of the unit. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1This is a system layout diagram of a supercritical water oxidation system for treating organic waste adapted for thermal power peak regulation, provided in one embodiment of the present invention.

[0019] Description of reference numerals:

[0020] 1. Material mixing device; 2. Material conveying pump; 3. Compressor; 4. Material preheating unit; 5. Air separation unit; 6. Air preheater; 7. Oxygen-enriched combustion boiler; 8. Deaerator; 9. Feedwater pump; 10. High-pressure heater; 11. Reactor; 12. Low-pressure heater; 13. Gas-solid-liquid separation device; 14. Third heat exchange unit; 15. Second heat exchange unit; 16. First heat exchange unit; 17. Steam turbine; 18. Condenser. DETAILED DESCRIPTION

[0021] In order to make the purpose, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below in conjunction with the embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention.

[0022] Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making any creative work shall fall within the scope of protection of the present invention.

[0023] Currently, the costs of safely operating boilers with variable loads and treating organic waste with supercritical water oxidation are relatively high. This is due to the high equipment and operating costs of supercritical water oxidation treatment equipment. Based on this, the present invention provides a supercritical water oxidation treatment system for organic waste that is adapted for thermal power peak regulation. When the power supply load decreases, the boiler is maintained at a safe load. While meeting the power supply load, the remaining load is efficiently utilized for harmless waste treatment. This not only ensures safe operation of the boiler when the power supply load changes, but also achieves harmless waste treatment and generates a certain amount of economic income.

[0024] The technical solution of the present invention is further described below by means of specific examples. In the following examples, the methods described are conventional methods unless otherwise specified; the reagents and materials described are commercially available unless otherwise specified.

[0025] See Figure 1 A supercritical water oxidation system for treating organic waste adapted for thermal power peak regulation comprises a reaction device 11, an oxidant conveying system, a material conveying system, a steam conveying system and a product waste heat utilization system.

[0026] The material inlet of the reaction device 11 is connected to the material conveying system; the oxidant conveying system includes an air separation unit 5 and an air preheater 6; the product waste heat utilization system includes a second heat exchange unit 15; the first oxygen outlet of the air separation unit 5 is connected to the first inlet of the air preheater 6, and the second oxygen outlet of the air separation unit 5 is connected to the second heat exchange unit 15; the oxygen outlet of the second heat exchange unit 15 is connected to a first oxygen delivery pipeline and a second oxygen delivery pipeline; the first oxygen delivery pipeline is connected to a compressor 3, and the compressor 3 is connected to the oxygen inlet of the reaction device 11; the second oxygen delivery pipeline is connected to the second inlet of the air preheater 6, and the first outlet of the air preheater 6 is connected to the steam delivery system; the first steam outlet of the steam delivery system is connected to the compressor 3, and the third steam outlet of the steam delivery system is connected to the reaction device 11.

[0027] Specifically, the embodiment of the present invention provides oxygen, material and steam to the reaction device through an oxidant delivery system, a material delivery system and a steam delivery system to achieve a supercritical water oxidation reaction, which can efficiently and cleanly utilize the residual load of the boiler, that is, when the power generation load is adjusted, the residual steam at the outlet of the steam delivery system is used for supercritical water oxidation treatment, so that the steam delivery system can be operated under a safe load while utilizing the residual load to carry out supercritical water oxidation treatment of coal slime wastewater. By preheating oxygen, the present invention reduces the heat absorption of the material in the reaction device, accelerates the reaction speed, and solves the problem of high cost when the boiler is operated safely under variable load and when supercritical water is oxidized to treat organic waste.

[0028] On the basis of the above embodiment, as a more preferred embodiment, the oxidant delivery system includes an air separation unit 5 and an air preheater 6, and the product waste heat utilization system includes a second heat exchange unit 15; the air separation unit 5 is used to separate air into nitrogen and oxygen, and the first oxygen outlet of the air separation unit 5 is connected to the first inlet of the air preheater 6, and the second oxygen outlet of the air separation unit 5 is connected to the second heat exchange unit 15, and the oxygen outlet of the second heat exchange unit 15 is connected to the first oxygen delivery pipeline and the second oxygen delivery pipeline; the first oxygen delivery pipeline is connected to the compressor 3, and the compressor 3 is connected to the oxygen inlet of the reaction device 11; the second oxygen delivery pipeline is connected to the second inlet of the air preheater 6.

[0029] Based on the above embodiment, as a more preferred embodiment, the steam delivery system includes an oxygen-enriched combustion boiler 7, the first outlet of the air preheater 6 is connected to the first inlet of the oxygen-enriched combustion boiler 7, and the first steam outlet of the oxygen-enriched combustion boiler 7 is connected to the compressor 3, and is configured to utilize the steam generated by the oxygen-enriched combustion boiler 7 to provide a power source for driving the compressor 3.

[0030] Specifically, the oxidant delivery system includes an air separation unit 5, which is used to separate air into nitrogen and oxygen. The oxygen separated by the air separation unit 5 enters the second heat exchange unit 15 for heat exchange, and then the oxygen is divided into two oxygen delivery pipelines. The first oxygen delivery pipeline is pressurized by the compressor 3 and enters the reaction device 11; the second oxygen delivery pipeline enters the air preheater 6, and after coming out of the air preheater 6, it is mixed with coal powder and then enters the oxygen-enriched combustion boiler 7 for combustion; wherein, the compressor 3 is driven by steam generated by the oxygen-enriched combustion boiler 7.

[0031] On the basis of the above embodiment, as a more preferred embodiment, the material conveying system includes a material mixing device 1, a material conveying pump 2 and a material preheating unit 4. The material mixing device 1 is used to mix the material ratio. The outlet of the material mixing device 1 is connected to the inlet of the material conveying pump 2, and the outlet of the material conveying pump 2 is connected to the first inlet of the material preheating unit 4; the first outlet of the material preheating unit 4 is connected to the material inlet of the reaction device 11.

[0032] Specifically, the material mixing device 1 is used to mix the material ratio. The material in the material conveying system includes coal slime wastewater. After being mixed by the material mixing device 1, the material is conveyed by the material conveying pump 2, and then passes through the material preheating unit 4 for heat exchange, and finally enters the reaction device 11.

[0033] On the basis of the above embodiment, as a more preferred embodiment, the steam delivery system includes an oxygen-enriched combustion boiler 7, the first steam outlet of the oxygen-enriched combustion boiler 7 is connected to the compressor 3, and is configured to use the steam generated by the oxygen-enriched combustion boiler 7 to provide a power source for driving the compressor 3; the second steam outlet of the oxygen-enriched combustion boiler 7 is connected to the power generation system; and the third steam outlet of the oxygen-enriched combustion boiler 7 is connected to the reaction device 11.

[0034] Specifically, the steam delivery system includes an oxygen-enriched combustion boiler 7. The first part of the steam generated by the oxygen-enriched combustion boiler 7 enters the compressor to provide a power source for driving the compressor 3; the second part of the steam generated by the oxygen-enriched combustion boiler 7 is used to generate electricity; and the third part of the steam generated by the oxygen-enriched combustion boiler 7 enters the reaction device 11.

[0035] Specifically, the power generation system includes a steam turbine 17 and a condenser 18. The second portion of steam generated by the oxygen-enriched combustion boiler 7 drives the steam turbine 17 to perform work, converting thermal energy into mechanical energy. The specific operating principle is as follows: high-temperature, high-pressure steam enters the steam turbine 17, passes through the nozzle chamber, and converts thermal energy into kinetic energy, forming a high-speed airflow. The nozzle chamber primarily functions to reduce the pressure, increase the speed, and redirect the steam flow. The high-speed airflow is sprayed toward the moving blades of the steam turbine 17 in a specific direction, exerting an impact force on the blades. Simultaneously, the airflow continues to expand and accelerate within the moving blade flow path, generating a reaction force on the moving blades. Under the combined action of the impact force and reaction force, the moving blades rotate the main shaft of the steam turbine 17, thereby converting the kinetic energy of the steam into mechanical energy. The rotational motion of the main shaft of the steam turbine 17 drives the generator to generate electricity, further converting mechanical energy into electrical energy. Condenser 18 is a key device in the power generation system used to cool steam and condense it into water. The working principle of condenser 18 is as follows: Steam exhausted from turbine 17 enters condenser 18, which is usually filled with cooling water. The steam and cooling water undergo heat exchange, and the steam's heat is absorbed by the cooling water, gradually lowering its temperature and condensing it into water. The condensed water is collected, treated, and then sent back to the oxygen-enriched combustion boiler 7 for heating, forming new high-temperature, high-pressure steam, thereby achieving water recycling. The use of condenser 18 can greatly improve the efficiency of the power generation system. By cooling the exhausted steam into water and recycling it, heat loss can be reduced, allowing more thermal energy to be converted into electrical energy.

[0036] On the basis of the above embodiment, as a more preferred embodiment, the outer wall of the reaction device 11 has an interlayer chamber, which is filled with cold wall water; the inlet of the interlayer chamber is connected to the condensate pipeline, and the outlet of the interlayer chamber is connected to the first inlet of the high-pressure heater 10, and the first outlet of the high-pressure heater 10 is connected to the oxygen-enriched combustion boiler 7.

[0037] Specifically, the interlayer chamber of the reaction device 11 is provided with cold wall water to cool the wall surface of the reaction device 11, wherein the cold wall water is condensed water provided by the condensed water pipeline; after cooling, the cold wall water enters the high-pressure heater 10 and finally enters the oxygen-enriched combustion boiler 7.

[0038] On the basis of the above embodiment, as a more preferred embodiment, the product waste heat utilization system includes a first heat exchange unit 16, a second heat exchange unit 15 and a third heat exchange unit 14, the heat exchange medium outlet of the material preheating unit 4 is connected to the heat exchange medium inlet of the first heat exchange unit 16; the product inlet of the first heat exchange unit 16 is connected to the product outlet of the reaction device 11, the product outlet of the first heat exchange unit 16 is connected to the inlet of the second heat exchange unit 15, the outlet of the second heat exchange unit 15 is connected to the inlet of the third heat exchange unit 14, and the outlet of the third heat exchange unit 14 is connected to the gas-solid-liquid separation device 13; the heat exchange medium inlet of the third heat exchange unit 14 is connected to the condensate pipeline, and the heat exchange medium outlet of the third heat exchange unit 14 is connected to the first inlet of the low-pressure heater 12.

[0039] Specifically, the reaction products in the product waste heat utilization system sequentially pass through the first heat exchange unit 16, the second heat exchange unit 15, and the third heat exchange unit 14 before entering the gas-solid-liquid separator 13, where they undergo three-phase separation into gas, solid, and liquid. The intermediate heat exchange medium in the third heat exchange unit 14 is condensed water, which, after absorbing heat, enters the low-pressure heater 12.

[0040] On the basis of the above embodiment, as a more preferred embodiment, the first inlet of the low-pressure heater 12 is connected to the heat exchange medium outlet of the third heat exchange unit 14, the second inlet of the low-pressure heater 12 is connected to the condensate pipeline, the outlet of the low-pressure heater 12 is connected to the inlet of the deaerator, the inlet of the deaerator is connected to the feed water pump, the feed water pump is connected to the inlet of the high-pressure heater, and the outlet of the high-pressure heater is connected to the oxygen-enriched combustion boiler 7.

[0041] Specifically, a portion of the condensate from the low-pressure heater 12 is supplied by the third heat exchange unit 14. After absorbing heat, the condensate enters the low-pressure heater 12. Another portion of the condensate from the low-pressure heater 12 is supplied by the condensate pipeline. The condensate from the low-pressure heater 12 passes through the low-pressure heater, deaerator, and high-pressure heater before entering the oxy-fuel combustion boiler 7. The low-pressure heater, deaerator, and high-pressure heater are all inherent equipment in the power plant system. After being purified by the low-pressure heater, deaerator, and high-pressure heater, the water enters the oxy-fuel combustion boiler 7.

[0042] The specific implementation of the supercritical water oxidation system for treating organic waste adapted to thermal power peak regulation is as follows:

[0043] When the oxyfuel combustion boiler 7 is operating at a safe load and the power generation load needs to be reduced, it can maintain operation at the safe load. A portion of the steam is used to power the steam turbine 17, and the remaining steam enters the reaction unit 11 for the supercritical water oxidation reaction. A small portion of this remaining steam drives the compressor to compress oxygen. Coal slime wastewater, as the feed material in the supercritical water oxidation treatment system, enters the material preparation device 1, is transported by the material delivery pump 2 to the material preheating unit 4, where it is preheated and then enters the reaction unit 11.

[0044] The oxidant is the oxygen separated by the air separation unit 2. Part of the separated oxygen enters the second heat exchange unit 15 to absorb heat and then enters the compressor 3 and the air preheater 6 respectively. The oxygen entering the compressor 3 is pressurized by the compressor 3 and then enters the reaction device 11. The oxygen entering the air preheater 6 is then mixed with coal powder and enters the oxygen-enriched combustion boiler 7 for combustion and heat release.

[0045] During the reaction process, the boiler condensate is used as the cold wall water in the reaction device 11 to cool the wall temperature of the reaction device 11, and the outlet cold wall water enters the high-pressure heater, thereby increasing the steam temperature of the high-pressure heater 10, reducing the steam extraction of the turbine 17, and improving the power generation efficiency.

[0046] The reaction product passes through the first heat exchange unit 16 and exchanges heat with the material preheating unit 4 before entering the second heat exchange unit 15. The second heat exchange unit 15 exchanges heat with oxygen and enters the third heat exchange unit 14. After heat exchange in the third heat exchange unit 14, it enters the gas-solid-liquid separation device 13. The heat exchange medium of the third heat exchange unit 14 is condensed water. After absorbing heat, the condensed water enters the low-pressure heater, reducing the steam extraction of the turbine 17 and improving the power generation efficiency.

[0047] The above are only preferred embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should be included in the scope of protection of the present invention.

Claims

1. A supercritical water oxidation system for treating organic waste adapted for thermal power peak regulation, characterized in that: It includes a reaction device (11), an oxidant conveying system, a material conveying system, a steam conveying system and a product waste heat utilization system; The material inlet of the reaction device (11) is connected to the material conveying system; The oxidant delivery system includes an air separation unit (5) and an air preheater (6); the product waste heat utilization system includes a second heat exchange unit (15); a first oxygen outlet of the air separation unit (5) is connected to a first inlet of the air preheater (6), and a second oxygen outlet of the air separation unit (5) is connected to the second heat exchange unit (15); The oxygen outlet of the second heat exchange unit (15) is connected to a first oxygen delivery pipeline and a second oxygen delivery pipeline; the first oxygen delivery pipeline is connected to a compressor (3), and the compressor (3) is connected to the oxygen inlet of the reaction device (11); the second oxygen delivery pipeline is connected to the second inlet of the air preheater (6), and the first outlet of the air preheater (6) is connected to the steam delivery system; The first steam outlet of the steam delivery system is connected to the compressor (3), and the third steam outlet of the steam delivery system is connected to the reaction device (11); The steam delivery system comprises an oxy-combustion boiler (7), a first inlet of the oxy-combustion boiler (7) is connected to a first outlet of the air preheater (6), and a first steam outlet of the oxy-combustion boiler (7) is connected to the compressor (3), and is configured to utilize steam generated by the oxy-combustion boiler (7) to provide a power source for driving the compressor (3); The outer wall of the reaction device (11) has an interlayer chamber, and the interlayer chamber is filled with cold wall water; the inlet of the interlayer chamber is connected to the condensate pipeline; the outlet of the interlayer chamber is connected to the first inlet of the high-pressure heater (10), and the first outlet of the high-pressure heater (10) is connected to the oxygen-enriched combustion boiler (7); The material conveying system comprises a material mixing device (1), a material conveying pump (2) and a material preheating unit (4), wherein the outlet of the material mixing device (1) is connected to the inlet of the material conveying pump (2), and the outlet of the material conveying pump (2) is connected to the first inlet of the material preheating unit (4); the first outlet of the material preheating unit (4) is connected to the material inlet of the reaction device (11); The product waste heat utilization system comprises a first heat exchange unit (16), a second heat exchange unit (15) and a third heat exchange unit (14); the heat exchange medium outlet of the material preheating unit (4) is connected to the heat exchange medium inlet of the first heat exchange unit (16); the product inlet of the first heat exchange unit (16) is connected to the product outlet of the reaction device (11); the product outlet of the first heat exchange unit (16) is connected to the inlet of the second heat exchange unit (15); the outlet of the second heat exchange unit (15) is connected to the inlet of the third heat exchange unit (14); and the outlet of the third heat exchange unit (14) is connected to the gas-solid-liquid separation device (13); The heat exchange medium inlet of the third heat exchange unit (14) is connected to the condensate pipeline, and the heat exchange medium outlet of the third heat exchange unit (14) is connected to the first inlet of the low-pressure heater (12).

2. The supercritical water oxidation treatment system for treating organic waste adapted for thermal power peak regulation according to claim 1 is characterized in that: The second inlet of the low-pressure heater (12) is connected to the condensate pipeline, the outlet of the low-pressure heater (12) is connected to the deaerator (8), the outlet of the deaerator (8) is connected to the feed water pump (9), and the feed water pump (9) is connected to the high-pressure heater (10).

3. The supercritical water oxidation system for treating organic waste adapted for thermal power peak regulation according to claim 1 is characterized in that: The second steam outlet of the steam delivery system is connected to the power generation system.

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