Wet desulphurization process mixed water-saving type flue gas waste heat power generation system

Abstract

The utility model discloses a wet desulphurization process mixed water-saving type flue gas waste heat power generation system, and relates to the technical field of flue gas waste heat power generation. Comprising a desulfurizing tower, an intra-tower raw water spraying layer and an intra-tower water collecting disc are arranged on the upper portion in the desulfurizing tower, the intra-tower raw water spraying layer is arranged above the intra-tower water collecting disc and communicated with a raw water tank, the raw water tank is communicated with a condensate water storage tank and a raw water heating assembly through a three-way valve, the condensate water storage tank is communicated with the intra-tower water collecting disc, and the raw water heating assembly is communicated with the intra-tower water collecting disc. The raw water heating assembly is communicated with a power generation assembly through the cold end plate type heat exchanger, the power generation assembly is communicated with a raw flue gas heat removal assembly through the hot end plate type heat exchanger, and the raw flue gas heat removal assembly is communicated with the desulfurization tower. Flue gas in the desulfurization tower can be cooled through the raw water spraying layer in the tower, moisture in the flue gas is recycled through the water collecting disc in the tower, and the problem that water consumption is too high is solved; and flue gas waste heat is deeply recycled through the original flue gas heat removal assembly, and power is generated through the power generation assembly.

Description

Technical Field

[0001] The utility model relates to the technical field of flue gas waste heat power generation, in particular to a wet desulfurization process hybrid water-saving flue gas waste heat power generation system. Background Art

[0002] Flue gas desulfurization systems for thermal power generators mostly use wet desulfurization. A large amount of water is evaporated in the desulfurization tower and discharged into the atmosphere through the chimney, resulting in a waste of water and visual pollution such as colored smoke plumes. The flue gas after the wet desulfurization device is wet saturated flue gas, which contains a large amount of water vapor, has a certain temperature, and contains a large amount of latent heat of vaporization. The use of flue gas condensation water extraction technology can recover the moisture in the wet saturated flue gas to meet the water needs of the wet desulfurization system or the raw water needs of the water treatment workshop.

[0003] The desulfurization process in the power industry generally adopts wet desulfurization, which has high desulfurization efficiency and low operating costs. In the wet desulfurization process of coal-fired flue gas, the circulating slurry and the high-temperature raw flue gas flow in countercurrent, and the chemical reaction removes sulfur oxides in the flue gas. During the reaction, the heat in the raw flue gas is transferred to the slurry. After the slurry absorbs heat, part of the water evaporates and is carried away by the flue gas, eventually forming saturated wet flue gas discharged from the tower outlet. In this process, a large amount of water is discharged into the atmosphere with the flue gas. Utility Model Content

[0004] The utility model aims to provide a wet desulfurization process hybrid water-saving flue gas waste heat power generation system to solve the problems existing in the above-mentioned prior art.

[0005] To achieve the above-mentioned purpose, the utility model provides the following scheme: The utility model provides a wet desulfurization process hybrid water-saving flue gas waste heat power generation system, including a desulfurization tower, wherein the upper part of the desulfurization tower is provided with a raw water spray layer in the tower and a water collecting tray in the tower, the raw water spray layer in the tower is arranged above the water collecting tray in the tower, the raw water spray layer in the tower is connected to a raw water tank, the raw water tank is connected to a condensate storage tank and a raw water heating component through a three-way valve, the condensate storage tank is connected to the water collecting tray in the tower, the raw water heating component is connected to a power generation component through a cold end plate heat exchanger, the power generation component is connected to an original flue gas heat extraction component through a hot end plate heat exchanger, and the original flue gas heat extraction component is connected to the desulfurization tower.

[0006] Preferably, a plurality of raw water spray layers are provided in the tower.

[0007] Preferably, the raw water tank is connected to a water inlet of a raw water booster pump, and a water outlet of the raw water booster pump is connected to a raw water spray layer in the tower.

[0008] Preferably, a water quality regulator is connected above the condensate storage tank, the condensate storage tank is connected to the water inlet end of the condensate booster pump, and the water outlet end of the condensate booster pump is connected to the raw water tank and the raw water heating assembly through the three-way valve.

[0009] Preferably, the raw water heating component includes a raw water flow regulating valve connected to the three-way valve, the raw water flow regulating valve is connected to a desalted water preparation device, the desalted water preparation device is connected to the water inlet end of a desalted water booster pump, and the water outlet end of the desalted water booster pump is connected to the cold end plate heat exchanger.

[0010] Preferably, the power generation component includes a generator, the generator is electrically connected to a reducer, the reducer is electrically connected to a screw machine, the air outlet end of the screw machine is connected to the cold end plate heat exchanger, and the air inlet end of the screw machine is connected to the cold end plate heat exchanger through the hot end plate heat exchanger.

[0011] Preferably, the raw flue gas heat extraction component includes a high-temperature section fluoroplastic heat exchanger, the water inlet end of the high-temperature section fluoroplastic heat exchanger is connected to the water outlet end of a heat medium desalted water circulation pump, the water inlet end of the heat medium desalted water circulation pump is connected to the water outlet end of the high-temperature section fluoroplastic heat exchanger through the hot end plate heat exchanger, and the exhaust end of the high-temperature section fluoroplastic heat exchanger is connected to the lower part of the desulfurization tower.

[0012] Preferably, the top of the desulfurization tower is fixedly connected and communicated with a chimney, and the chimney is arranged above the raw water spray layer in the tower.

[0013] The utility model discloses the following technical effects:

[0014] The utility model can cool the flue gas in the desulfurization tower through the raw water spray layer in the tower, and recover the moisture in the flue gas through the water collecting tray in the tower for secondary utilization, thereby solving the problem of excessive water consumption; it also deeply recovers the flue gas waste heat through the original flue gas heat extraction component, and generates electricity through the power generation component, thereby saving energy and reducing carbon emissions, and improving the operating efficiency of the unit. BRIEF DESCRIPTION OF THE DRAWINGS

[0015] In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0016] Figure 1 It is a schematic diagram of the overall structure of the utility model;

[0017] Among them, 1-1, raw water tank; 1-2, raw water booster pump; 1-3, low-temperature raw water; 1-4, raw water spray layer in the tower; 1-5, water collection tray in the tower; 1-6, high-temperature condensed water; 1-7, condensed water storage tank; 1-8, water quality regulator; 1-9, condensed water booster pump; 1-10, raw water replenishment; 1-11, raw water flow regulating valve; 1-12, desalted water preparation device; 1-13, desalted water booster pump; 1-14, cold end plate heat exchanger; 1-1 5. High-temperature desalted water; 2-1. High-temperature section fluoroplastic heat exchanger; 2-2. Heat medium desalted water circulation pump; 2-3. Low-temperature heat medium desalted water; 2-4. High-temperature heat medium desalted water; 2-5. Hot end plate heat exchanger; 2-6. High-temperature raw flue gas; 2-7. Low-temperature raw flue gas; 3-1. High-temperature working fluid steam; 3-2. Screw machine; 3-3. Reducer; 3-4. Generator; 3-5. Medium-temperature working fluid exhaust steam; 3-6. Low-temperature working fluid; 4. Desulfurization tower; 5. Chimney. DETAILED DESCRIPTION

[0018] The following will be combined with the drawings in the embodiments of the utility model to clearly and completely describe the technical solutions in the embodiments of the utility model. Obviously, the described embodiments are only part of the embodiments of the utility model, not all of the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the utility model.

[0019] In order to make the above-mentioned purposes, features and advantages of the present invention more obvious and easy to understand, the present invention is further described in detail below in conjunction with the accompanying drawings and specific implementation methods.

[0020] Reference Figure 1 The utility model discloses a wet desulfurization process hybrid water-saving flue gas waste heat power generation system, comprising a desulfurization tower 4, wherein a raw water spray layer 1-4 and a water collecting tray 1-5 are arranged in the upper part of the desulfurization tower 4, wherein the raw water spray layer 1-4 is arranged above the water collecting tray 1-5, wherein the raw water spray layer 1-4 is connected to a raw water tank 1-1, wherein the raw water tank 1-1 is connected to a condensed water storage tank 1-7 and a raw water heating component through a three-way valve, wherein the condensed water storage tank 1-7 is connected to the water collecting tray 1-5 in the tower, wherein the raw water heating component is connected to a power generation component through a cold end plate heat exchanger 1-14, wherein the power generation component is connected to an original flue gas heat extraction component through a hot end plate heat exchanger 2-5, wherein the original flue gas heat extraction component is connected to the desulfurization tower 4. The raw water tank 1-1 is replenished with water through the raw water replenishment 1-10.

[0021] The utility model can cool the flue gas in the desulfurization tower 4 through the raw water spray layers 1-4 in the tower, and recover the moisture in the flue gas through the water collecting trays 1-5 in the tower for secondary utilization, thereby solving the problem of excessive water consumption; it also deeply recovers the flue gas waste heat through the original flue gas heat extraction components, and generates electricity through the power generation components, thereby saving energy and reducing carbon emissions, and improving the operating efficiency of the unit.

[0022] To further optimize the solution, several raw water spray layers 1-4 are provided in the tower.

[0023] The desulfurization tower 4 can be provided with 3 raw water spray layers 1-4, 2 for use and 1 for reserve. A number of nozzles are provided on each raw water spray layer 1-4. The arrangement of the nozzles can ensure that there is no short circuit in the flue gas in the entire desulfurization tower 4, and there will be no weak spraying area, thereby achieving effective flue gas water collection.

[0024] The water collecting tray 1-5 in the tower, which is arranged at the lower part of the raw water spray layer 1-4 in the tower, can ensure that the raw water and flue gas condensate are collected and discharged to the outside of the desulfurization tower 4, and prevent the refrigerant water from leaking into the slurry pool of the desulfurization tower 4. The water collecting tray 1-5 in the tower is made of high nickel-based alloy to prevent corrosion and wear.

[0025] By arranging the raw water spray layer 1-4 and the water collecting tray 1-5 in the upper part of the desulfurization tower 4, the low-temperature raw water 1-3 in the raw water tank 1-1 can directly exchange heat with the saturated flue gas, and the heat exchange efficiency is high. The flue gas cooling and the precipitation of condensed water can be achieved without additional equipment. The system is simple and the initial investment is low.

[0026] To further optimize the solution, the raw water tank 1-1 is connected to the water inlet of the raw water booster pump 1-2, and the water outlet of the raw water booster pump 1-2 is connected to the raw water spray layer 1-4 in the tower.

[0027] The raw water spray layer 1-4 in the tower can cool the flue gas in the desulfurization tower 4, and the high-temperature condensed water 1-6 generated during the flue gas cooling process can be collected through the water collecting tray 1-5 in the tower arranged below the raw water spray layer 1-4 in the tower. The collected high-temperature condensed water 1-6 is transported to the cold end plate heat exchanger 1-14 through the condensed water storage tank 1-7 and the raw water heating component in turn to continue heating up; the heat exchange process of the utility model does not generate waste heat and waste water, and saves energy while taking into account environmental protection.

[0028] To further optimize the solution, the top of the condensate storage tank 1-7 is connected to a water quality regulator 1-8, the condensate storage tank 1-7 is connected to the water inlet end of the condensate booster pump 1-9, and the water outlet end of the condensate booster pump 1-9 is connected to the raw water tank 1-1 and the raw water heating component through a three-way valve.

[0029] To further optimize the solution, the raw water heating component includes a raw water flow regulating valve 1-11 connected to the three-way valve, the raw water flow regulating valve 1-11 is connected to the desalted water preparation device 1-12, the desalted water preparation device 1-12 is connected to the water inlet end of the desalted water booster pump 1-13, and the water outlet end of the desalted water booster pump 1-13 is connected to the cold end plate heat exchanger 1-14.

[0030] After the saturated flue gas is cooled, a large amount of latent heat is released, and this part of heat is transferred to the low-temperature raw water 1-3. After the temperature is raised, the low-temperature raw water 1-3 becomes high-temperature condensed water 1-6 and enters the desalted water preparation device 1-12 to produce desalted water, and then enters the cold-end plate heat exchanger 1-14 to exchange heat with the medium-temperature working fluid exhaust steam 3-5 to continue to heat up. After the waste heat of the flue gas is recovered, the desalted water is turned into high-temperature desalted water 1-15 and sent to the deaerator and other subsequent processes. It can save water while making full use of the waste heat of the flue gas, generating higher economic benefits. Through the cold-end plate heat exchanger 1-14, the heat exchange process does not discharge waste heat to the external environment, avoiding thermal pollution.

[0031] After the saturated flue gas is cooled, a large amount of latent heat is released. This part of heat is transferred to the cold end plate heat exchanger 1-14, which can replace the water heater and effectively save the plant steam consumption. The heat exchange process between desalted water and flue gas can utilize both the latent heat and the sensible heat of the flue gas, and the heat recovery amplitude is high.

[0032] Further optimization scheme, the power generation component includes a generator 3-4, the generator 3-4 is electrically connected to the reducer 3-3, the reducer 3-3 is electrically connected to the screw machine 3-2, the air outlet end of the screw machine 3-2 is connected to the cold end plate heat exchanger 1-14, and the air inlet end of the screw machine 3-2 is connected to the cold end plate heat exchanger 1-14 through the hot end plate heat exchanger 2-5.

[0033] A further optimized solution is provided, in which the original flue gas heat extraction component includes a high-temperature section fluoroplastic heat exchanger 2-1, the water inlet end of the high-temperature section fluoroplastic heat exchanger 2-1 is connected to the water outlet end of the heat medium desalted water circulation pump 2-2, the water inlet end of the heat medium desalted water circulation pump 2-2 is connected to the water outlet end of the high-temperature section fluoroplastic heat exchanger 2-1 through the hot end plate heat exchanger 2-5, and the exhaust end of the high-temperature section fluoroplastic heat exchanger 2-1 is connected to the lower part of the desulfurization tower 4.

[0034] By operating the high-temperature section fluoroplastic heat exchanger 2-1 in conjunction with the screw machine 3-2, the waste heat of flue gas can be effectively utilized to generate electricity.

[0035] According to a further optimization scheme, the top of the desulfurization tower 4 is fixedly connected and communicated with a chimney 5, which is arranged above the raw water spray layers 1-4 in the tower.

[0036] The high-temperature raw flue gas 2-6 generated by the boiler exhaust is cooled after heat exchange through the high-temperature section fluoroplastic heat exchanger 2-1, and becomes low-temperature raw flue gas 2-7 which enters the desulfurization tower 4. The total heat entering the desulfurization tower 4 is reduced, and the flue gas volume flow rate in the desulfurization tower 4 is reduced, and the flue gas flow rate is reduced, so that the desulfurization efficiency is improved during the desulfurization and cooling process of the flue gas, and the amount of water lost by evaporation in the desulfurization tower 4 is reduced, thereby achieving a deeper water-saving effect.

[0037] The high-temperature section fluoroplastic heat exchanger 2-1 is arranged at the entrance of the desulfurization tower 4, and the high-temperature section fluoroplastic heat exchanger 2-1 and the low-temperature heat medium desalted water 2-3 inside are used to cool down the high-temperature original flue gas 2-6 at the entrance of the desulfurization tower 4; the low-temperature heat medium desalted water 2-3 enters the high-temperature section fluoroplastic heat exchanger 2-1 driven by the heat medium desalted water circulation pump 2-2 to heat up, so that the low-temperature heat medium desalted water 2-3 is heated to become high-temperature heat medium desalted water 2-4 after heating, and the high-temperature heat medium desalted water 2-4 enters the hot end plate heat exchanger 2-5 to release heat, and this process is repeated to realize the conversion of flue gas heat to the working medium side; the hot end plate heat exchanger 2-5 The low-temperature working fluid 3-6 in the system is heated by heat exchange with the high-temperature heat medium desalted water 2-4 to become high-temperature working fluid steam 3-1. The high-temperature working fluid steam 3-1 enters the screw machine 3-2 for work, and drives the generator 3-4 to generate electricity through the reducer 3-3. After working, the high-temperature working fluid steam 3-1 becomes medium-temperature working fluid exhaust steam 3-5 and enters the cold-end plate heat exchanger 1-14 for heat exchange with desalted water to obtain low-temperature working fluid 3-6. This process is repeated to realize the conversion of working fluid chemical energy into electrical energy. By exchanging heat between the worked high-temperature working fluid steam 3-1 and the desalted water, low-quality waste heat is deeply utilized without the need to set up a cooling tower and without discharging waste heat to the external environment.

[0038] The utility model adopts a 1000MW unit. When the 1000MW unit is adopted, the working process is as follows:

[0039] A raw water spray layer 1-4 is arranged on the upper part of the desulfurization tower 4, and the low-temperature raw water 1-3 sprayed from the raw water spray layer 1-4 is directly mixed with the flue gas in the desulfurization tower 4 for cooling. The saturated flue gas temperature after heat exchange can be controlled by controlling the amount and temperature of the low-temperature raw water 1-3 entering the desulfurization tower 4. During the circulation process, the high-temperature saturated clean flue gas starts to cool down from an initial temperature of 50°C according to the design requirements, and the low-temperature saturated clean flue gas is about 45°C after cooling. The amount of flue gas condensed water in this process is about 90t / h.

[0040] The low-temperature raw water 1-3 required for flue gas condensation adopts an open cycle and is driven by a raw water booster pump 1-2. The temperature of the low-temperature raw water 1-3 is about 5°C. It enters the desulfurization tower 4 to heat exchange with the saturated flue gas to increase its temperature. After the heat exchange, the low-temperature raw water 1-3 becomes high-temperature condensed water 1-6. The high-temperature condensed water 1-6 is about 25°C.

[0041] The flue gas temperature is accompanied by the generation of high-temperature condensed water 1-6. It is estimated that 90 tons of high-temperature condensed water 1-6 will be generated per hour. The high-temperature condensed water 1-6 is discharged into the condensed water storage tank 1-7. After the pH value is adjusted by the water quality regulator 1-8, it is discharged into the raw water tank 1-1 driven by the condensed water booster pump 1-9. The condensed water recovery process is thus realized, and the water collection capacity is about 90t / h.

[0042] After heat exchange, the high-temperature condensed water 1-6 is about 25°C. The amount of raw water can be adjusted by adjusting the opening of the raw water flow regulating valve 1-11 as needed. The raw water enters the desalted water preparation device 1-12 to produce normal desalted water. The desalted water enters the cold-end plate heat exchanger 1-14 driven by the desalted water booster pump 1-13 to exchange heat with the medium-temperature working fluid exhaust steam 3-5 after processing. The medium-temperature working fluid exhaust steam 3-5 is reduced from 45°C to a low-temperature working fluid 3-6 of 30°C. The desalted water is heated to about 40°C to become high-temperature desalted water 1-15 and enters the deaerator and other subsequent processes.

[0043] The high-temperature section fluoroplastic heat exchanger 2-1 is arranged at the entrance of the desulfurization tower 4, and the high-temperature raw flue gas 2-6 at the entrance of the desulfurization tower 4 is cooled by the low-temperature heat medium desalted water 2-3 inside the high-temperature section fluoroplastic heat exchanger 2-1. During the circulation process, the high-temperature raw flue gas 2-6 starts to cool down from 140°C according to the design requirements, and the high-temperature raw flue gas 2-6 becomes low-temperature raw flue gas 2-7 after cooling down, and the low-temperature raw flue gas 2-7 is about 110°C. Driven by the heat medium desalted water circulation pump 2-2, the low-temperature heat medium desalted water 2-3 enters the high-temperature section fluoroplastic heat exchanger 2-1 to heat up, and the heated high-temperature heat medium desalted water 2-4 enters the hot end plate heat exchanger 2-5 to release heat. This process is repeated to realize the conversion of flue gas heat to the working fluid side.

[0044] The low-temperature working fluid 3-6 is heated by heat exchange with the high-temperature heat medium desalted water 2-4 to become high-temperature working fluid steam 3-1. The high-temperature working fluid steam 3-1 enters the screw machine 3-2 for work, and drives the generator 3-4 to generate electricity through the reducer 3-3. The medium-temperature working fluid exhaust steam 3-5 after work enters the cold-end plate heat exchanger 1-14 for heat exchange with the desalted water to obtain the low-temperature working fluid 3-6. This process is repeated to realize the conversion of the chemical energy of the working fluid into electrical energy.

[0045] The utility model can solve the problem of water balance of the unit, and for a 1000MW unit, the water saving per hour is more than 90 tons.

[0046] After the latent heat of the wet saturated flue gas in the desulfurization tower 4 is absorbed by raw water, the temperature is raised to about 25°C and discharged from the desulfurization tower 4. Then, it enters the desalted water preparation device 1-14 to produce desalted water. For a 1000MW unit, more than 150GJ of net flue gas heat is recovered per hour, and the heat absorption of the desalted water and the working fluid is about 25GJ / h, with a total recovered heat of 175GJ / h.

[0047] By adding a waste heat power generation system, the original flue gas temperature was reduced from 140°C to 100°C. Based on 8,000 hours of operating time throughout the year, the annual power generation can be increased by 30,000MW.h.

[0048] The utility model directly mixes the low-temperature raw water 1-3 in the raw water tank 1-1 with the saturated flue gas through the raw water spray layer 1-4 in the tower for heat exchange, and extracts the moisture in the saturated clean flue gas at the upper part of the desulfurization tower 4 through the water collecting tray 1-5 in the tower; the flue gas condensate recovered by the water collecting tray 1-5 in the tower can be reused, thereby reducing the problem of excessive water consumption in the operation process of the enterprise, and at the same time, the waste heat of the flue gas can be deeply utilized for power generation through the original flue gas heat extraction component and the power generation component, which has high economic benefits, and the system does not generate waste heat and waste water during operation, and can be applied in large thermal power generating units.

[0049] In the description of the present invention, it should be understood that the terms "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside" and "outside" etc., indicating orientations or positional relationships, are based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as a limitation on the present invention.

[0050] The embodiments described above are only descriptions of the preferred methods of the present invention, and are not intended to limit the scope of the present invention. Without departing from the design spirit of the present invention, various modifications and improvements made to the technical solutions of the present invention by ordinary technicians in this field should fall within the protection scope determined by the claims of the present invention.

Claims

1. A wet desulfurization process hybrid water-saving flue gas waste heat power generation system, characterized by: The invention comprises a desulfurization tower (4), wherein the upper part of the desulfurization tower (4) is provided with a raw water spray layer (1-4) in the tower and a water collecting tray (1-5) in the tower, wherein the raw water spray layer (1-4) in the tower is arranged above the water collecting tray (1-5) in the tower, wherein the raw water spray layer (1-4) in the tower is connected to a raw water tank (1-1), wherein the raw water tank (1-1) is connected to a condensate storage tank (1-7) and a raw water heating component through a three-way valve, wherein the condensate storage tank (1-7) is connected to the water collecting tray (1-5) in the tower, wherein the raw water heating component is connected to a power generation component through a cold end plate heat exchanger (1-14), wherein the power generation component is connected to a raw flue gas heat extraction component through a hot end plate heat exchanger (2-5), and wherein the raw flue gas heat extraction component is connected to the desulfurization tower (4).

2. The wet desulfurization process hybrid water-saving flue gas waste heat power generation system according to claim 1 is characterized by: A plurality of raw water spray layers (1-4) are arranged in the tower.

3. The wet desulfurization process hybrid water-saving flue gas waste heat power generation system according to claim 1 is characterized by: The raw water tank (1-1) is connected to the water inlet of a raw water booster pump (1-2), and the water outlet of the raw water booster pump (1-2) is connected to the raw water spray layer (1-4) in the tower.

4. The wet desulfurization process hybrid water-saving flue gas waste heat power generation system according to claim 1 is characterized by: The condensate storage tank (1-7) is connected to a water quality regulator (1-8) above, the condensate storage tank (1-7) is connected to the water inlet of a condensate booster pump (1-9), and the water outlet of the condensate booster pump (1-9) is connected to the raw water tank (1-1) and the raw water heating component through the three-way valve.

5. The wet desulfurization process hybrid water-saving flue gas waste heat power generation system according to claim 1 is characterized by: The raw water heating component comprises a raw water flow regulating valve (1-11) connected to the three-way valve, the raw water flow regulating valve (1-11) is connected to a desalted water preparation device (1-12), the desalted water preparation device (1-12) is connected to a water inlet end of a desalted water booster pump (1-13), and the water outlet end of the desalted water booster pump (1-13) is connected to the cold end plate heat exchanger (1-14).

6. The wet desulfurization process hybrid water-saving flue gas waste heat power generation system according to claim 1 is characterized by: The power generation component comprises a generator (3-4), the generator (3-4) is electrically connected to a reducer (3-3), the reducer (3-3) is electrically connected to a screw machine (3-2), the air outlet end of the screw machine (3-2) is connected to the cold end plate heat exchanger (1-14), and the air inlet end of the screw machine (3-2) is connected to the cold end plate heat exchanger (1-14) through the hot end plate heat exchanger (2-5).

7. The wet desulfurization process hybrid water-saving flue gas waste heat power generation system according to claim 1 is characterized by: The raw flue gas heat extraction component comprises a high-temperature section fluoroplastic heat exchanger (2-1); the water inlet end of the high-temperature section fluoroplastic heat exchanger (2-1) is connected to the water outlet end of a heat medium desalted water circulation pump (2-2); the water inlet end of the heat medium desalted water circulation pump (2-2) is connected to the water outlet end of the high-temperature section fluoroplastic heat exchanger (2-1) through the hot end plate heat exchanger (2-5); the smoke exhaust end of the high-temperature section fluoroplastic heat exchanger (2-1) is connected to the lower part of the desulfurization tower (4).

8. The wet desulfurization process hybrid water-saving flue gas waste heat power generation system according to claim 1 is characterized by: The top of the desulfurization tower (4) is fixedly connected and communicated with a chimney (5), and the chimney (5) is arranged above the raw water spray layer (1-4) in the tower.

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