Supercritical water oxidation treatment organic waste system adaptive to thermal power peak regulation

Abstract

The invention relates to the technical field of coal-fired thermal power generation and organic waste treatment, in particular to a supercritical water oxidation treatment organic waste system adaptive to thermal power peak regulation. The system comprises a reaction device, an oxidant conveying system, a material conveying system, a steam conveying system and a product waste heat utilization system, the air separation unit is connected with the air pre-heater and the second heat exchange unit; the second heat exchange unit is connected with a first oxygen conveying pipeline and a second oxygen conveying pipeline; the first oxygen conveying pipeline is connected with a compressor which is connected with an oxygen inlet of the reaction device; the second oxygen conveying pipeline is connected with an air pre-heater; the air pre-heater is connected with a steam conveying system; the steam conveying system is connected with the compressor and the reaction device. By preheating oxygen, the heat absorption capacity of materials in the reaction device is reduced, the reaction speed is increased, and the problems of variable-load safe operation of the boiler and high cost of supercritical water oxidation treatment of organic waste are solved.

Description

Technical Field

[0001] The 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 to thermal power peak regulation. Background Art

[0002] In order to give full play to the flexible operation capacity of thermal power units, deep peak load regulation will be the normal operation of coal-fired units. During deep peak load regulation, power plant boilers will operate alternately at full load, low load and lower load, which not only reduces the power generation efficiency of power plant boilers, but also increases the risk of safety accidents such as abnormal flameout of power plant boilers, high temperature heating surface tube burst and creep fracture failure.

[0003] When the power supply load of the power plant is reduced, in order to ensure the economy and safety of the boiler operation, the power plant boiler can be operated at a relatively safe, stable and economical load. At this time, while meeting the power supply load, the supercritical steam generated by the remaining load can undergo supercritical water oxidation reaction. The full name of supercritical water oxidation in English is Supercritical Water Oxidation, referred to as SCWO. SCWO uses the unique physical and chemical properties of supercritical water to achieve efficient oxidation and degradation of toxic and harmful organic pollutants. Supercritical water oxidation can rely on the heat release of the reaction to maintain the heat balance of the system without the need for external heat supplementation; the equipment is small in size, safe, and meets the requirements of closedness. Supercritical water oxidation technology has shown great technical advantages in treating difficult-to-degrade, toxic and harmful organic matter. However, there is a relatively high cost problem when the boiler is operated safely with variable load and when supercritical water oxidation is used to treat organic waste. 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 solution of the present invention is as follows.

[0006] A first aspect of the present invention provides a supercritical water oxidation treatment system for organic waste adapted to 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 the reaction device through an oxidant delivery system, a material delivery system and a steam delivery system to realize supercritical water oxidation reaction, and can efficiently and cleanly utilize the residual load of the boiler, that is, when adjusting the power generation load, 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 the residual load is used for supercritical water oxidation treatment of coal slime wastewater. The present invention reduces the heat absorption of the material in the reaction device by preheating oxygen, accelerates the reaction speed, and solves the problem of high cost when the boiler is operated safely with variable load and the supercritical water oxidation treatment of organic waste.

[0008] Preferably, the steam delivery system includes an oxygen-enriched combustion boiler, a first inlet of the oxygen-enriched combustion boiler is connected to a first outlet of the air preheater, and a 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 wall-cooling 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 condensed water of the boiler, which enters the high-pressure heater after absorbing heat, 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, materials and steam to the reaction device through an oxidant delivery system, a material delivery system and a steam delivery system to realize supercritical water oxidation reaction, and can efficiently and cleanly utilize the residual load of the boiler, that is, when adjusting the power generation load, 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 the residual load is used for supercritical water oxidation treatment of coal slime wastewater. The present invention reduces the heat absorption of the material in the reaction device by preheating oxygen, accelerates the reaction speed, and solves the problem of high cost when the boiler is operated safely with variable load and the supercritical water oxidation treatment of organic waste.

[0017] 2. The present invention utilizes the waste heat of the products after supercritical water oxidation treatment in a graded manner, and utilizes the waste heat of the products to preheat materials, preheat oxygen at the inlet of the oxygen-enriched combustion boiler, and heat condensate, thereby reducing the heat absorption of the materials 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 1A 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. Reaction device; 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 solution 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 used to limit the present invention.

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

[0023] At present, the cost of boiler variable load safe operation and supercritical water oxidation treatment of organic waste is relatively high. Due to the high equipment and operation costs of supercritical water oxidation treatment devices. Based on this, the present invention provides a supercritical water oxidation treatment system for organic waste adapted to thermal power peak regulation. When the power supply load is reduced, the boiler is maintained to operate under a safe load. While meeting the power supply load, the remaining load is efficiently used for harmless treatment of waste. It can not only ensure the safe operation of the boiler when the power supply load changes, but also achieve harmless treatment of waste and achieve a certain 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 also 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 the first oxygen conveying pipeline and the second oxygen conveying pipeline; the first oxygen conveying 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 conveying 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 conveying system; the first steam outlet of the steam conveying system is connected to the compressor 3, and the third steam outlet of the steam conveying system is connected to the reaction device 11.

[0027] Specifically, the embodiment of the present invention provides oxygen, materials and steam to the reaction device through an oxidant delivery system, a material delivery system and a steam delivery system to realize a supercritical water oxidation reaction, and can efficiently and cleanly utilize the residual load of the boiler, that is, when adjusting the power generation load, 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 the residual load is used for supercritical water oxidation treatment of coal slime wastewater. The present invention reduces the heat absorption of the material in the reaction device by preheating oxygen, 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 used to oxidize 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, the first oxygen outlet of the air separation unit 5 is connected to the first inlet of the air preheater 6, 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, 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, mixes with coal powder after coming out of the air preheater 6, 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-mentioned 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, 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 material ratios. The materials in the material conveying system include coal slime wastewater. After being mixed by the material mixing device 1 , the materials are conveyed by the material conveying pump 2 , and then heat exchanged by the material preheating unit 4 , and finally enter the reaction device 11 .

[0033] On the basis of the above-mentioned 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 part of steam generated by the oxygen-enriched combustion boiler 7 drives the steam turbine 17 to work, so as to convert thermal energy into mechanical energy. The specific working principle is: high-temperature and high-pressure steam enters the steam turbine 17, passes through the nozzle chamber, converts thermal energy into kinetic energy, and forms a high-speed airflow. Among them, the main function of the nozzle chamber is to reduce the pressure, increase the speed, and turn the steam flow. The high-speed airflow is sprayed toward the moving blades of the steam turbine 17 in a certain direction, generating an impact force on the blades. At the same time, the airflow continues to expand and accelerate in the moving blade flow channel, generating a reaction force on the moving blades. Under the combined action of the impulse force and the reaction force, the moving blades push the main shaft of the steam turbine 17 to rotate, thereby converting the kinetic energy of the steam into mechanical energy. The rotational motion of the main shaft of the steam turbine 17 can drive the generator to generate electricity, further converting the mechanical energy into electrical energy. The condenser 18 is a key device in the power generation system for cooling and condensing steam into water. The working principle of the condenser 18 is as follows: the steam discharged from the turbine 17 enters the condenser 18. The interior of the condenser 18 is usually filled with cooling water. The steam and the cooling water perform heat exchange, and the heat of the steam is absorbed by the cooling water, and the temperature gradually decreases and condenses into water. The condensed water is collected, and after treatment, it is sent to the oxygen-enriched combustion boiler 7 for heating again to form new high-temperature and high-pressure steam, thereby realizing the recycling of water. The use of the condenser 18 can greatly improve the efficiency of the power generation system. By cooling the discharged steam into water and recycling it, the heat loss can be reduced, so that more thermal energy can be converted into electrical energy.

[0036] On the basis of the above-mentioned embodiment, as a more preferred embodiment, 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, 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 a 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 pass through the first heat exchange unit 16, the second heat exchange unit 15, and the third heat exchange unit 14 in sequence, and finally enter the gas-solid-liquid separation device 13, and the three-phase separation of gas, solid and liquid is achieved in the gas-solid-liquid separation device 13. The intermediate heat exchange medium of the third heat exchange unit 14 is condensed water, and the condensed water enters the low-pressure heater 12 after absorbing heat.

[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, part of the condensate of the low-pressure heater 12 is provided by the third heat exchange unit 14, and the condensate after absorbing heat enters the low-pressure heater 12; another part of the condensate of the low-pressure heater 12 is provided by the condensate pipeline. The condensate in the low-pressure heater 12 enters the oxygen-enriched combustion boiler 7 after passing through the low-pressure heater, deaerator and high-pressure heater. The low-pressure heater, deaerator and high-pressure heater are all inherent equipment of the power station system. After the water is purified by the low-pressure heater, deaerator and high-pressure heater, it enters the oxygen-enriched combustion boiler 7.

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

[0043] When the oxygen-enriched combustion boiler 7 needs to reduce the power generation load when operating under the safe load, the oxygen-enriched combustion boiler 7 can be maintained to operate under the safe load, a part of the steam is used to supply the steam turbine 17 to generate power, and the remaining part of the steam enters the reaction device 11 for supercritical water oxidation reaction, and a small part of the remaining steam drives the compressor to compress oxygen. Coal slime wastewater is the material in the supercritical water oxidation treatment system. After entering the material preparation device 1, the material is transported to the material preheating unit 4 by the material delivery pump 2 for preheating and then enters the reaction device 11.

[0044] The oxidant is the oxygen separated by the air separation unit 2. A 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 to increase the steam temperature of the high-pressure heater 10, reduce the steam extraction of the turbine 17, and improve 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 before entering the third heat exchange unit 14. After heat exchange in the third heat exchange unit 14, the product 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, which reduces the steam extraction of the turbine 17 and improves 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 protection scope of the present invention.

Claims

1. A supercritical water oxidation system for treating organic waste adapted to thermal power peak regulation, characterized in that: It comprises 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 comprises an air separation unit (5) and an air preheater (6); the product waste heat utilization system comprises 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).

2. The supercritical water oxidation system for treating organic waste adapted to thermal power peak load regulation according to claim 1 is characterized in that: The steam delivery system comprises an oxygen-enriched combustion boiler (7), a first inlet of the oxygen-enriched combustion boiler (7) is connected to a first outlet of the air preheater (6), and a 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).

3. The supercritical water oxidation system for treating organic waste adapted to thermal power peak load regulation according to claim 2 is characterized in that: 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).

4. The supercritical water oxidation system for treating organic waste adapted to thermal power peak load regulation according to claim 1 is characterized in that: The material conveying system comprises a material mixing device (1), a material conveying pump (2) and a material preheating unit (4); the outlet of the material mixing device (1) is connected to the inlet of the material conveying pump (2), the outlet of the material conveying pump (2) is connected to the first inlet of the material preheating unit (4); and the first outlet of the material preheating unit (4) is connected to the material inlet of the reaction device (11).

5. The supercritical water oxidation treatment system for treating organic wastes adapted to thermal power peak load regulation according to claim 4 is characterized in that: 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).

6. The supercritical water oxidation treatment system for treating organic wastes adapted to thermal power peak load regulation according to claim 5 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).

7. The supercritical water oxidation system for treating organic waste adapted to thermal power peak load 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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