A wet flue gas hydrothermal recovery system and a regeneration method thereof

Abstract

The present application belongs to the field of extraction, and particularly relates to a wet flue gas hydrothermal recovery system and a regeneration method thereof, comprising: a desulfurization tower, a hydrothermal recovery tower, a flash tank, an absorption heat pump and a mixer; the flue gas outlet of the desulfurization tower is connected with the flue gas inlet of the hydrothermal recovery tower, the high-temperature desulfurization slurry outlet of the desulfurization tower is connected with the high-temperature desulfurization slurry inlet of the flash tank, the exhaust port of the hydrothermal recovery tower is connected with the atmosphere, the dilute absorbent outlet of the hydrothermal recovery tower is connected with the dilute absorbent inlet of the absorption heat pump through the mixer, the low-temperature desulfurization slurry outlet of the flash tank is connected with the low-temperature desulfurization slurry inlet of the desulfurization tower, the steam outlet of the flash tank is connected with the steam inlet of the absorption heat pump, the extractant outlet of the absorption heat pump is connected with the extractant inlet of the hydrothermal recovery tower through the mixer, and the drainage port of the absorption heat pump is connected with the atmosphere. By setting the flash tank, the mixer and the absorption heat pump, the water and heat in the low-temperature saturated wet flue gas after desulfurization are recovered, the flash evaporation of the desulfurization slurry is coupled, and the effect of water saving and energy saving is achieved.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of extraction, and particularly relates to a wet flue gas hydrothermal recovery system and a regeneration method thereof. BACKGROUND

[0002] For a cogeneration unit, the waste heat in the recovery system is one of the best ways to increase the heating capacity without expanding the unit size. At present, power plants usually use the water spraying method to reduce the flue gas to 50-60 DEG C before discharging, and the heat in the flue gas is not recovered, resulting in waste of energy. At the same time, the saturated wet flue gas discharged after spraying still contains part of the heat and a large amount of water vapor, which is easy to form white smoke plume when discharged into the air. It is a direction worth paying attention to to recover the water heat in the saturated wet flue gas by using the absorption heat pump, but the regeneration of the absorbent needs to consume a lot of energy.

[0003] Based on the direct heating and vacuum flash evaporation, the most common solution regeneration process is direct heating and vacuum flash evaporation. Flash evaporation reduces the boiling point of the solution by reducing the evaporation environment pressure, thereby improving the evaporation intensity. Compared with direct heating, a certain amount of heat input is reduced, but the latent heat of vaporization still needs to be overcome fundamentally.

[0004] In the existing hydrothermal recovery system, the absorption agent regeneration technology by direct heating evaporation and vacuum flash evaporation has high energy consumption, so that the economy of the whole system is low. SUMMARY

[0005] The present application provides a wet flue gas hydrothermal recovery system and a regeneration method thereof to solve the technical problem of absorbent regeneration.

[0006] In order to achieve the above purpose, the present application adopts the following technical scheme:

[0007] In the first aspect, the present application provides a wet flue gas hydrothermal recovery system, comprising: a desulfurization tower, a hydrothermal recovery tower, a flash tank, an absorption heat pump, a mixer, a first dilute absorbent pipeline, a high-temperature desulfurization slurry pipeline, a low-temperature desulfurization slurry pipeline, a flash steam pipeline, a first water pipeline, a first flue gas pipeline, a saturated wet flue gas pipeline and a second flue gas pipeline.

[0008] Flue gas is connected to the flue gas inlet of the desulfurization tower through the first flue gas pipeline. The desulfurization tower is connected to the flue gas inlet of the hydrothermal recovery tower through the saturated wet flue gas pipeline. The high-temperature desulfurization slurry outlet at the bottom of the desulfurization tower is connected to the high-temperature desulfurization slurry inlet of the flash tank through the high-temperature desulfurization slurry pipeline. The second flue gas pipeline of the hydrothermal recovery tower leads to the outside. The dilute absorbent outlet of the hydrothermal recovery tower is connected to the dilute absorbent inlet of the mixer through the first dilute absorbent pipeline. The low-temperature desulfurization slurry outlet of the flash tank is connected to the low-temperature desulfurization slurry inlet of the desulfurization tower through the low-temperature desulfurization slurry pipeline. The steam outlet of the flash tank is connected to the steam inlet of the absorption heat pump through the flash steam pipeline. The first water pipe of the absorption heat pump leads to the outside.

[0009] Furthermore, it also includes: a first separator, a second separator, a cooler, a heat exchanger, a second dilute absorbent pipeline, a third dilute absorbent pipeline, a concentrated absorbent pipeline, a fourth extractant pipeline, a fourth dilute absorbent pipeline, a first extractant pipeline, a second extractant pipeline, a third extractant pipeline, and a second water pipeline.

[0010] The dilute absorbent outlet of the mixer is connected to the dilute absorbent inlet of the cooler via a second dilute absorbent pipeline. The dilute absorbent outlet of the cooler is connected to the dilute absorbent inlet of the first separator via a third dilute absorbent pipeline. The concentrated absorbent outlet of the first separator is connected to the concentrated absorbent inlet of the hydrothermal recovery tower via a concentrated absorbent pipeline. The dilute absorbent outlet of the first separator is connected to the dilute absorbent inlet of the heat exchanger via a fourth dilute absorbent pipeline. The extractant outlet of the heat exchanger is connected to the extractant inlet of the absorption heat pump via a first extractant pipeline. The extractant outlet of the absorption heat pump is connected to the extractant inlet of the second separator via a second extractant pipeline. The extractant outlet of the second separator is connected to the extractant inlet of the heat exchanger via a third extractant pipeline. The extractant outlet of the heat exchanger is connected to the extractant inlet of the mixer via a fourth extractant pipeline. The second water pipe of the second separator leads to the outside.

[0011] Furthermore, absorption heat pumps are driven by an electric motor or a steam turbine.

[0012] Furthermore, the product of the second flue gas pipeline of the hydrothermal recovery tower leading to the outside is dry flue gas, and the product of the first water pipe of the absorption heat pump and the second water pipe of the second separator leading to the outside is condensate.

[0013] Secondly, the present invention provides a method for hydrothermal recovery and regeneration of wet flue gas, comprising:

[0014] Step 1: Flue gas enters the desulfurization tower through the first flue gas pipeline and exchanges heat with the low-temperature desulfurization slurry. The flue gas and the low-temperature desulfurization slurry react to generate saturated wet flue gas and high-temperature desulfurization slurry.

[0015] Step 2: Saturated wet flue gas enters the hydrothermal recovery tower through the saturated wet flue gas pipeline and comes into contact with the concentrated absorbent to generate dry flue gas and dilute absorbent; high-temperature desulfurization slurry enters the flash tank through the high-temperature desulfurization slurry pipeline for flash evaporation to generate low-temperature desulfurization slurry and flash steam.

[0016] Step 3: Dry flue gas is discharged through the second flue gas pipeline of the hydrothermal recovery tower; dilute absorbent enters the mixer through the first dilute absorbent pipeline and is mixed with the extractant before separation, generating concentrated absorbent and dilute extractant; low-temperature desulfurization slurry enters the desulfurization tower through the low-temperature desulfurization slurry pipeline, and then the first step is repeated; flash steam enters the absorption heat pump through the flash steam pipeline, reacts with the extractant in the absorption heat pump to generate condensate, and the condensate is discharged through the first water pipe; low-temperature desulfurization slurry enters the desulfurization tower, and then the first step is repeated; flash steam enters the absorption heat pump to react and generate condensate, which is then discharged;

[0017] Step 4: The concentrated absorbent enters the hydrothermal recovery tower, and Step 2 is repeated; the dilute extractant enters the absorption heat pump for heat exchange to generate extractant, and Step 3 is repeated.

[0018] Furthermore, the flash evaporator operates in a vacuum environment during flash evaporation.

[0019] Furthermore, after the dilute absorbent and extractant are mixed in the mixer, they enter the cooler through the second dilute absorbent pipeline for cooling, and are separated in the first separator to generate concentrated absorbent and water. The concentrated absorbent enters the hydrothermal recovery tower through the concentrated absorbent pipeline, and the water enters the heat exchanger to exchange heat with the extractant.

[0020] Furthermore, after water and extractant exchange heat in the heat exchanger, a dilute extractant is generated. The dilute extractant enters the absorption heat pump through the first extractant pipeline to be heated. The flash steam and dilute extractant react in the absorption heat pump to generate condensate and extractant. The condensate is discharged directly from the first water pipe of the absorption heat pump.

[0021] Furthermore, the dilute extractant enters the second separator through the second extractant pipeline for separation, generating condensate and extractant. The condensate is discharged directly from the second water pipe of the second separator, while the extractant enters the heat exchanger through the third extractant pipeline.

[0022] Furthermore, the high-temperature desulfurization slurry and the low-temperature desulfurization slurry circulate and react in the desulfurization tower and flash tank; the concentrated absorbent and the dilute absorbent circulate and react in the mixer, cooler and heat exchanger; and the extractant and the dilute extractant circulate and react in the absorption heat pump, the second separator, the heat exchanger and the mixer.

[0023] The present invention has at least the following beneficial effects:

[0024] 1. This invention provides a wet flue gas hydrothermal recovery system, comprising: a desulfurization tower, a hydrothermal recovery tower, a flash tank, an absorption heat pump, and a mixer; flue gas is connected to the flue gas inlet of the desulfurization tower via a first flue gas pipeline; the flue gas outlet at the top of the desulfurization tower is connected to the flue gas inlet of the hydrothermal recovery tower via a saturated wet flue gas pipeline; the high-temperature desulfurization slurry outlet at the bottom of the desulfurization tower is connected to the high-temperature desulfurization slurry inlet of the flash tank via a high-temperature desulfurization slurry pipeline; a second flue gas pipeline of the hydrothermal recovery tower leads to the outside; the dilute absorbent outlet of the hydrothermal recovery tower is connected to the dilute absorbent inlet of the mixer via a first dilute absorbent pipeline; the low-temperature desulfurization slurry outlet of the flash tank is connected to the low-temperature desulfurization slurry inlet of the desulfurization tower via a low-temperature desulfurization slurry pipeline; the steam outlet of the flash tank is connected to the steam inlet of the absorption heat pump via a flash steam pipeline; and the first water pipe of the absorption heat pump leads to the outside. By setting up flash tanks, mixers and absorption heat pumps to recover moisture and heat from the low-temperature saturated wet flue gas after desulfurization, and coupling the flash heating of desulfurization slurry, significant water and energy saving effects are achieved.

[0025] 2. This invention provides a method for hydrothermal recovery and regeneration of wet flue gas, comprising: Step 1: Flue gas enters a desulfurization tower through a first flue gas pipeline and exchanges heat with a low-temperature desulfurization slurry, where the flue gas and the low-temperature desulfurization slurry react to generate saturated wet flue gas and high-temperature desulfurization slurry; Step 2: The saturated wet flue gas enters a hydrothermal recovery tower through a saturated wet flue gas pipeline and contacts a concentrated absorbent to generate dry flue gas and a dilute absorbent; the high-temperature desulfurization slurry enters a flash tank through a high-temperature desulfurization slurry pipeline for flash evaporation to generate low-temperature desulfurization slurry and flash steam; Step 3: The dry flue gas is discharged through a second flue gas pipeline of the hydrothermal recovery tower; the dilute absorbent is discharged through a first dilute absorbent... The liquid enters the mixer through the pipeline and mixes with the extractant, then separates to generate concentrated absorbent and dilute extractant. The low-temperature desulfurization slurry enters the desulfurization tower through the low-temperature desulfurization slurry pipeline, repeating the first step. Flash steam enters the absorption heat pump through the flash steam pipeline, reacting with the extractant to generate condensate, which is discharged through the first water pipe. The low-temperature desulfurization slurry enters the desulfurization tower, repeating the first step. Flash steam enters the absorption heat pump to react and generate condensate, which is then discharged. Fourth step: The concentrated absorbent enters the hydrothermal recovery tower, repeating the second step; the dilute extractant enters the absorption heat pump for heat exchange to generate extractant, repeating the third step. This energy recycling effectively reduces energy consumption and achieves water and energy conservation.

[0026] 3. This invention provides a method for hydrothermal recovery and regeneration of wet flue gas. A dilute extractant enters a second separator through a second extractant pipeline for separation, generating condensate and extractant. The condensate is discharged directly from the second water pipe of the second separator, while the extractant enters a heat exchanger through a third extractant pipeline. The absorption heat pump uses the steam flashed from the desulfurization slurry as a low-temperature heat source and the extractant as a cold source. Because the temperature required for the extractant is not high, the heat pump has high efficiency and effectively recovers the heat from the desulfurization slurry. Attached Figure Description

[0027] The accompanying drawings, which form part of this specification, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an undue limitation of the invention. In the drawings:

[0028] Figure 1 This is a schematic diagram of a wet flue gas hydrothermal recovery system according to the present invention.

[0029] The components are as follows: 1. Desulfurization tower; 2. Hydrothermal recovery tower; 3. Flash tank; 4. Absorption heat pump; 5. Mixer; 6. First separator; 7. Second separator; 8. Cooler; 9. Heat exchanger; 10. First dilute absorbent pipeline; 11. Second dilute absorbent pipeline; 12. Third dilute absorbent pipeline; 13. Concentrated absorbent pipeline; 14. Fourth extractant pipeline; 15. Fourth dilute absorbent pipeline; 16. First extractant pipeline; 17. Second extractant pipeline; 18. Third extractant pipeline; 19. Second water pipeline; 20. High-temperature desulfurization slurry pipeline; 21. Low-temperature desulfurization slurry pipeline; 22. Flash steam pipeline; 23. First water pipeline; 24. First flue gas pipeline; 25. Saturated wet flue gas pipeline; 26. Second flue gas pipeline. Detailed Implementation

[0030] The present invention will now be described in detail with reference to the accompanying drawings and embodiments. It should be noted that, unless otherwise specified, the embodiments and features described herein can be combined with each other.

[0031] The following detailed description is exemplary and intended to provide further detailed explanation of the invention. Unless otherwise specified, all technical terms used in this invention have the same meaning as commonly understood by one of ordinary skill in the art. The terminology used in this invention is for describing particular embodiments only and is not intended to limit the scope of exemplary embodiments according to the invention.

[0032] Example 1

[0033] Please see Figure 1As shown, the present invention provides a wet flue gas hydrothermal recovery system, comprising a desulfurization tower 1, a hydrothermal recovery tower 2, a flash tank 3, an absorption heat pump 4, a mixer 5, a first separator 6, a second separator 7, a cooler 8, a heat exchanger 9, a first dilute absorbent pipeline 10, a second dilute absorbent pipeline 11, a third dilute absorbent pipeline 12, a concentrated absorbent pipeline 13, a fourth extractant pipeline 14, a fourth dilute absorbent pipeline 15, a first extractant pipeline 16, a second extractant pipeline 17, a third extractant pipeline 18, a third water pipe 19, a high-temperature desulfurization slurry pipeline 20, a low-temperature desulfurization slurry pipeline 21, a flash steam pipeline 20, a low-temperature desulfurization slurry pipeline 21, a flash steam pipeline 22, a second water pipe 23, a flue gas pipeline 24, a saturated wet flue gas pipeline 25, and a first water pipe 26. Flue gas is connected to the flue gas inlet of desulfurization tower 1 via the first flue gas pipeline 24. Flue gas from the top of desulfurization tower 1 is connected to the flue gas inlet of hydrothermal recovery tower 2 via the outlet of saturated wet flue gas pipeline 25. The high-temperature desulfurization slurry outlet at the bottom of desulfurization tower 1 is connected to the high-temperature desulfurization slurry inlet of flash tank 3 via high-temperature desulfurization slurry pipeline 20. The second flue gas pipeline 26 of hydrothermal recovery tower 2 leads to the outside. The dilute absorbent outlet of hydrothermal recovery tower 2 is connected to the dilute absorbent inlet of mixer 5 via the first dilute absorbent pipeline 10. The dilute absorbent outlet of cooler 8 is connected to the dilute absorbent inlet of first separator 6 via the third dilute absorbent pipeline 12. The concentrated absorbent outlet of first separator 6 is connected to the concentrated absorbent inlet of hydrothermal recovery tower 2 via concentrated absorbent pipeline 13. The dilute absorbent outlet of first separator 6 is connected to the dilute absorbent inlet of heat exchanger 9 via the fourth dilute absorbent pipeline 15. The extractant outlet is connected to the extractant inlet of the absorption heat pump 4 via the first extractant pipeline 16. The extractant outlet of the absorption heat pump 4 is connected to the extractant inlet of the second separator 7 via the second extractant pipeline 17. The extractant outlet of the second separator 7 is connected to the extractant inlet of the heat exchanger 9 via the third extractant pipeline 18. The extractant outlet of the heat exchanger 9 is connected to the extractant inlet of the mixer 5 via the fourth extractant pipeline 14. The second water pipe 19 of the second separator 7 leads to the outside. The dilute absorbent outlet of the mixer 5 is connected to the dilute absorbent inlet of the cooler 8 via the second dilute absorbent pipeline 11. The low-temperature desulfurization slurry outlet of the flash tank 3 is connected to the low-temperature desulfurization slurry inlet of the desulfurization tower 1 via the low-temperature desulfurization slurry pipeline 21. The steam outlet of the flash tank 3 is connected to the steam inlet of the absorption heat pump 4 via the flash steam pipeline 22. The first water pipe 23 of the absorption heat pump 4 leads to the outside.

[0034] Example 2

[0035] This invention provides a method for hydrothermal recovery and regeneration of wet flue gas, comprising: Step 1: Flue gas enters desulfurization tower 1 through a first flue gas pipeline 24 and exchanges heat with low-temperature desulfurization slurry, reacting to generate saturated wet flue gas and high-temperature desulfurization slurry; Step 2: Saturated wet flue gas enters hydrothermal recovery tower 2 through a saturated wet flue gas pipeline 25 and contacts concentrated absorbent to generate dry flue gas and dilute absorbent; the high-temperature desulfurization slurry enters flash tank 3 through a high-temperature desulfurization slurry pipeline 20 for flash evaporation, generating low-temperature desulfurization slurry and flash steam; Step 3: Dry flue gas is discharged through a second flue gas pipeline 26 of hydrothermal recovery tower 2; the dilute absorbent enters through a first dilute absorbent pipeline 10... After mixing with the extractant in mixer 5, the mixture is separated to produce concentrated absorbent and dilute extractant. The low-temperature desulfurization slurry enters desulfurization tower 1 through low-temperature desulfurization slurry pipeline 21, and the first step is repeated. Flash steam enters absorption heat pump 4 through flash steam pipeline 22, where it reacts with the extractant to generate condensate, which is discharged through the first water pipe 23. The low-temperature desulfurization slurry enters desulfurization tower 1, and the first step is repeated. Flash steam enters absorption heat pump 4 to react and generate condensate, which is then discharged. Fourth step: The concentrated absorbent enters hydrothermal recovery tower 2, and the second step is repeated. The dilute extractant enters absorption heat pump 4 for heat exchange to generate extractant, and the third step is repeated.

[0036] Flue gas enters desulfurization tower 1 and exchanges heat with low-temperature desulfurization slurry sprayed from the top of the tower, and is purified to generate saturated wet flue gas and high-temperature desulfurization slurry. The high-temperature desulfurization slurry at the bottom of desulfurization tower 1 enters flash tank 3, where flash evaporation occurs under vacuum, generating flash steam and low-temperature desulfurization slurry. The low-temperature desulfurization slurry enters desulfurization tower 1 to continue the reaction, and heat is transferred from the desulfurization slurry to the flash steam. The flash steam enters absorption heat pump 4 as a low-temperature heat source to heat the dilute extractant. The saturated wet flue gas exits from the top of desulfurization tower 1 and enters hydrothermal recovery tower 2, where it comes into countercurrent contact with concentrated absorbent. The water vapor and its latent heat of vaporization in the saturated wet flue gas are transferred to the concentrated absorbent, which becomes dilute absorbent and flows out from the bottom of hydrothermal recovery tower 2. The dilute absorbent and extractant are mixed in mixer 5 and cooled by cooler 8. At low temperature, the water in the dilute absorbent is extracted into the extractant. The absorbent is then separated by first separator 6 to generate concentrated absorbent and water. The concentrated absorbent is returned to the absorption tower for recycling. Water enters heat exchanger 9 to exchange heat with the extractant and is heated. It then enters absorption heat pump 4 for further heating. At high temperature, the condensate and dilute extractant are separated. The dilute extractant is separated into condensate and extractant in the second separator 7. The extractant is returned to the mixer for recycling.

[0037] As is known from common technical knowledge, this invention can be implemented through other embodiments that do not depart from its spirit or essential characteristics. Therefore, the disclosed embodiments described above are merely illustrative in all respects and are not the only ones. All modifications within the scope of this invention or its equivalents are included in this invention.

[0038] In this invention, the term "a plurality of" refers to two or more unless otherwise expressly defined. The term "and / or" as used herein includes any and all combinations of one or more of the associated listed items. The terms "installed," "connected," "linked," "fixed," etc., should be interpreted broadly. For example, "connected" can be a fixed connection, a detachable connection, or an integral connection; "linked" can be a direct connection or an indirect connection via an intermediate medium. Those skilled in the art will understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0039] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention and not to limit it. Although the present invention has been described in detail with reference to the above embodiments, those skilled in the art should understand that modifications or equivalent substitutions can still be made to the specific implementation of the present invention. Any modifications or equivalent substitutions that do not depart from the spirit and scope of the present invention should be covered within the scope of protection of the claims of the present invention.

Claims

1. A wet flue gas hydrothermal recovery system, characterized in that, include: Desulfurization tower (1), hydrothermal recovery tower (2), flash tank (3), absorption heat pump (4), mixer (5), first dilute absorbent pipeline (10), high temperature desulfurization slurry pipeline (20), low temperature desulfurization slurry pipeline (21), flash steam pipeline (22), first water pipeline (23), first flue gas pipeline (24), saturated wet flue gas pipeline (25) and second flue gas pipeline (26); The first flue gas pipeline (24) is connected to the flue gas inlet of the desulfurization tower (1). The flue gas outlet at the top of the desulfurization tower (1) is connected to the flue gas inlet of the hydrothermal recovery tower (2) through the saturated wet flue gas pipeline (25). The high-temperature desulfurization slurry outlet at the bottom of the desulfurization tower (1) is connected to the high-temperature desulfurization slurry inlet of the flash tank (3) through the high-temperature desulfurization slurry pipeline (20). The second flue gas pipeline (26) of the hydrothermal recovery tower (2) leads to the outside. The dilute absorbent outlet of the hydrothermal recovery tower (2) is connected to the dilute absorbent inlet of the mixer (5) through the first dilute absorbent pipeline (10). The low-temperature desulfurization slurry outlet of the flash tank (3) is connected to the low-temperature desulfurization slurry inlet of the desulfurization tower (1) through the low-temperature desulfurization slurry pipeline (21). The steam outlet of the flash tank (3) is connected to the steam inlet of the absorption heat pump (4) through the flash steam pipeline (22). The first water pipe (23) of the absorption heat pump (4) leads to the outside. It also includes: a first separator (6), a second separator (7), a cooler (8), a heat exchanger (9), a second dilute absorbent pipeline (11), a third dilute absorbent pipeline (12), a concentrated absorbent pipeline (13), a fourth extractant pipeline (14), a fourth dilute absorbent pipeline (15), a first extractant pipeline (16), a second extractant pipeline (17), a third extractant pipeline (18), and a second water pipeline (19); The dilute absorbent outlet of mixer (5) is connected to the dilute absorbent inlet of cooler (8) via a second dilute absorbent pipeline (11). The dilute absorbent outlet of cooler (8) is connected to the dilute absorbent inlet of first separator (6) via a third dilute absorbent pipeline (12). The concentrated absorbent outlet of first separator (6) is connected to the concentrated absorbent inlet of hydrothermal recovery tower (2) via a concentrated absorbent pipeline (13). The dilute absorbent outlet of first separator (6) is connected to the dilute absorbent inlet of heat exchanger (9) via a fourth dilute absorbent pipeline (15). The extractant outlet of the heat pump (4) is connected to the extractant inlet of the absorption heat pump (4) through the first extractant pipeline (16). The extractant outlet of the absorption heat pump (4) is connected to the extractant inlet of the second separator (7) through the second extractant pipeline (17). The extractant outlet of the second separator (7) is connected to the extractant inlet of the heat exchanger (9) through the third extractant pipeline (18). The extractant outlet of the heat exchanger (9) is connected to the extractant inlet of the mixer (5) through the fourth extractant pipeline (14). The second water pipe (19) of the second separator (7) leads to the outside.

2. The wet flue gas hydrothermal recovery system according to claim 1, characterized in that, Absorption heat pump (4) is driven by a motor or a steam turbine.

3. The wet flue gas hydrothermal recovery system according to claim 1, characterized in that, The product of the second flue gas pipe (26) of the hydrothermal recovery tower (2) leading to the outside is dry flue gas, and the product of the first water pipe (23) of the absorption heat pump (4) and the second water pipe (19) of the second separator (7) leading to the outside is condensate.

4. A method for hydrothermal recovery and regeneration of wet flue gas, implemented based on the wet flue gas hydrothermal recovery system of claim 1, characterized in that, include: Step 1: Flue gas enters the desulfurization tower (1) through the first flue gas pipeline (24) and exchanges heat with the low-temperature desulfurization slurry, reacting to generate saturated wet flue gas and high-temperature desulfurization slurry; Step 2: Saturated wet flue gas enters the hydrothermal recovery tower (2) through the saturated wet flue gas pipeline (25) and comes into contact with the concentrated absorbent to generate dry flue gas and dilute absorbent; high-temperature desulfurization slurry enters the flash tank (3) through the high-temperature desulfurization slurry pipeline (20) for flash evaporation to generate low-temperature desulfurization slurry and flash steam. Step 3: Dry flue gas is discharged through the second flue gas pipeline (26) of the hydrothermal recovery tower (2); dilute absorbent enters the mixer (5) through the first dilute absorbent pipeline (10) and is mixed with the extractant and then separated to generate concentrated absorbent and dilute extractant; low-temperature desulfurization slurry enters the desulfurization tower (1) through the low-temperature desulfurization slurry pipeline (21) and then the first step is repeated; flash steam enters the absorption heat pump (4) through the flash steam pipeline (22) and reacts with the extractant in the absorption heat pump (4) to generate condensate, which is discharged through the first water pipe (23); low-temperature desulfurization slurry enters the desulfurization tower (1) and then the first step is repeated; flash steam enters the absorption heat pump (4) and reacts to generate condensate, which is then discharged; Step 4: The concentrated absorbent enters the hydrothermal recovery tower (2), and Step 2 is repeated; the dilute extractant enters the absorption heat pump (4) to exchange heat and generate extractant, and Step 3 is repeated.

5. The wet flue gas hydrothermal recovery and regeneration method according to claim 4, characterized in that, The flash tank (3) is in a vacuum environment when flash evaporation occurs.

6. The wet flue gas hydrothermal recovery and regeneration method according to claim 4, characterized in that, After the dilute absorbent and extractant are mixed in the mixer (5), they enter the cooler (8) through the second dilute absorbent pipeline (11) for cooling, and are separated in the first separator (6) to generate concentrated absorbent and water. The concentrated absorbent enters the hydrothermal recovery tower (2) through the concentrated absorbent pipeline (13), and the water enters the heat exchanger (9) to exchange heat with the extractant.

7. The wet flue gas hydrothermal recovery and regeneration method according to claim 4, characterized in that, After water and extractant exchange heat in heat exchanger (9), dilute extractant is generated. The dilute extractant enters the absorption heat pump (4) through the first extractant pipeline (16) to raise the temperature. Flash steam and dilute extractant react in absorption heat pump (4) to generate condensate and extractant. The condensate is discharged directly from the first water pipe (23) of absorption heat pump (4).

8. The wet flue gas hydrothermal recovery and regeneration method according to claim 7, characterized in that, The dilute extractant enters the second separator (7) through the second extractant pipeline (17) for separation, generating condensate and extractant. The condensate is discharged directly from the second water pipe (19) of the second separator (7), and the extractant enters the heat exchanger (9) through the third extractant pipeline (18).

9. The wet flue gas hydrothermal recovery and regeneration method according to claim 4, characterized in that, High-temperature desulfurization slurry and low-temperature desulfurization slurry are circulated and reacted in desulfurization tower (1) and flash tank (3); concentrated absorbent and dilute absorbent are circulated and reacted in mixer (5), cooler (8) and heat exchanger (9); extractant and dilute extractant are circulated and reacted in absorption heat pump (4), second separator (7), heat exchanger (9) and mixer (5).

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