A wet decarbonization technology regeneration gas heat recovery process system

Abstract

The present invention discloses a regeneration gas heat recovery process system of wet decarbonization technology, which comprises an absorption unit, a lean-rich liquid heat exchange unit and a regeneration unit connected in sequence; the regeneration unit comprises a regeneration tower, and the regeneration tower is provided with a regeneration section and a regeneration gas water washing system in sequence from bottom to top; a one-way metal pipe is introduced into the regeneration gas water washing system to transport the condensate to the front end of the rich liquid pump in the lean-rich liquid heat exchange unit; the present invention adopts a method of adding a regeneration gas water washing section at the upper part of the regeneration tower, and reduces the water vapor content in the regeneration gas by circulating spraying of washing liquid, reduces the heat brought out by the regeneration gas, and thus reduces the load of the tower top condenser and the regeneration energy consumption in the desorption process; secondly, forced circulation spraying can enhance the gas-liquid mass transfer effect and reduce the absorbent operation loss; in addition, all the condensed liquid in this process is collected at the rich liquid, which can reduce the alkalinity of the rich liquid and is conducive to the full desorption of carbon dioxide.

Description

Technical Field

[0001] The present invention relates to the technical field of carbon dioxide capture, and in particular to a wet decarbonization technology regeneration gas heat recovery process system. Background Art

[0002] Currently, with the continued advancement of the "dual carbon" strategy, the demand for carbon emission reduction in industries such as cement, steel, thermal power, and chemicals is rising year by year. To address the issue of capturing carbon dioxide from low-pressure gas sources, current large-scale capture projects mostly employ chemical absorption methods using alcoholamine absorbents. Based on current carbon capture project applications and technological research progress, wet carbon capture technology remains the foundational technology for achieving the "dual carbon" goals.

[0003] The organic amine method primarily involves absorption and regeneration processes in its carbon dioxide capture process. The energy consumption of a CO2 capture system is primarily determined by the steam consumption of the regeneration stage. In traditional regeneration processes, the high-calorific-value regeneration gas, after exiting the regeneration tower, is directly cooled and condensed through a heat exchanger, wasting heat energy and not being recovered by the system. Furthermore, the overhead condenser utilizes a partitioning heat exchange principle. Due to the thermal resistance of the solid wall and the thermal resistance of dirt in this partitioning heat exchange process, heat transfer efficiency is somewhat lower than that of direct contact heat exchange. Furthermore, due to the influence of aerosols and the vapor pressure properties of the amine itself, amine leakage from the regeneration gas is inevitable. Furthermore, most organic amine-based carbon capture systems use only a gas-liquid separator (with a wire mesh) for gas-liquid separation of the regeneration gas, which is generally ineffective. Consequently, some organic amine-based carbon capture systems produce a carbon dioxide product with an amine odor. Summary of the Invention

[0004] The main purpose of the present invention is to provide a wet decarbonization technology regeneration gas heat recovery process system, aiming to solve the existing technical problems.

[0005] To achieve the above object, the present invention provides a wet decarbonization technology regeneration gas heat recovery process system, comprising an absorption unit, a lean-rich liquid heat exchange unit and a regeneration unit connected in sequence;

[0006] The regeneration unit includes a regeneration tower, which is provided with a regeneration section for making the rich liquid contact with the high-temperature steam in reverse direction and a regeneration gas water washing system for forming a washing liquid circulation loop to transfer the heat value in the regeneration gas to the washing liquid.

[0007] The regenerated gas water washing system comprises a regenerated gas water washing section, a regenerated gas water washing tank, a regenerated gas washing pump and a regenerated gas water washing cooler connected in sequence;

[0008] A one-way metal pipe is introduced from the outlet of the regeneration gas washing pump to transport the washing condensate to the front end of the rich liquid pump in the lean-rich liquid heat exchange unit, so that the washing liquid is mixed with the rich liquid to increase the heat in the rich liquid flow.

[0009] Furthermore, the absorption unit includes an absorption tower, which includes, from bottom to top, an absorption section for making the carbon-containing gas and the lean liquid contact in countercurrent, and a water washing system for forming a washing liquid circulation loop.

[0010] Furthermore, the water washing system includes a purified gas water washing section, a washing tank, a washing pump and a water washing cooler connected in sequence, wherein a one-way metal pipe is led from the outlet of the washing pump to transport the condensate to the front end of the rich liquid pump.

[0011] Furthermore, the regenerated gas water washing system is used to recover the calorific value of the regenerated gas, and the temperature of the circulating washing liquid is controlled by adjusting the circulating water volume of the regenerated gas water washing cooler, wherein the spraying temperature of the circulating washing liquid is controlled to be between 50-90°C.

[0012] Furthermore, the washing flow rate of the washing liquid in contact with the regeneration gas is 30-120% of the rich liquid circulation volume.

[0013] Furthermore, fillers are provided in the absorption section and the regeneration section, and the absorbent added to the filler can be any one of an organic amine absorbent, an amino acid salt absorbent, a phase change absorbent, and an ionic liquid absorbent.

[0014] Furthermore, the regeneration unit also includes a condensation separation system consisting of a regeneration gas condenser and a gas-liquid separator. The inlet end of the regeneration gas condenser is connected to the regeneration gas outlet at the top of the regeneration tower through a one-way metal pipe, and the outlet end is connected to the inlet end of the gas-liquid separator.

[0015] Furthermore, a one-way metal pipe is led from the liquid outlet of the gas-liquid separator to transport the condensed water to the regeneration gas-water washing tank.

[0016] Furthermore, the regeneration unit further comprises a reboiler, which is connected in parallel with the regeneration tower via a one-way metal pipe and is used to provide heat required for desorption of the rich liquid.

[0017] Furthermore, the lean and rich liquid heat exchange unit further includes a lean and rich liquid heat exchanger, a lean liquid cooler, and a lean liquid pump, which form a lean and rich liquid circulation circuit between the absorption unit and the regeneration unit together with the rich liquid pump.

[0018] The beneficial effects of the present invention are embodied in:

[0019] The present invention adopts the method of adding a regeneration gas water washing section at the upper part of the regeneration tower to pre-cool the regeneration gas by circulating spraying of washing liquid, thereby reducing the water vapor content in the regeneration gas and further reducing the heat brought out by the regeneration gas.

[0020] The washing liquid circulated and sprayed in the present invention obtains a part of the heat in the regeneration gas and obtains a temperature rise. After a part of the washing liquid after the temperature rise is mixed with the rich liquid out of the absorption tower, it can increase the heat in the rich liquid flow to a certain extent. The heat of the regeneration gas is recycled in the system in the form of washing liquid, thereby reducing the overall regeneration energy consumption and the use of external steam in the desorption process.

[0021] The present invention can improve the heat exchange efficiency between gas and liquid and reduce the workload of the regeneration gas condenser by spraying the scrubbing liquid directly to exchange heat with the regeneration gas.

[0022] The present invention can enhance the mass transfer and separation effect of gas-liquid contact through water washing and spraying, reduce the amount of organic amine carried in the regenerated gas, thereby avoiding the rear-end carbon dioxide product from having an amine odor, and effectively reducing the operating loss of the organic amine liquid.

[0023] The present invention collects all the condensed liquid of the capture system to the rich liquid, thereby reducing the alkalinity of the rich liquid and further facilitating the full desorption of carbon dioxide. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] Figure 1 The overall process flow chart of the flue gas carbon capture section provided by the present invention;

[0025] Figure 2 A process flow chart of the absorption unit provided by the present invention;

[0026] Figure 3 A process flow chart of the lean-rich liquid heat exchange unit provided by the present invention;

[0027] Figure 4 This is a process flow chart of the regeneration unit provided by the present invention.

[0028] Drawing numbers: 101, absorption tower; 102, water washing cooler; 103, washing tank; 104, washing pump; 201, lean and rich liquid heat exchanger; 202, lean liquid cooler; 203, rich liquid pump; 204, lean liquid pump; 301, regeneration tower; 302, reboiler; 303, regeneration gas water washing cooler; 304, regeneration gas washing pump; 305, regeneration gas water washing tank; 306, regeneration gas condenser; 307, gas-liquid separator. DETAILED DESCRIPTION

[0029] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the embodiments described are only part of the embodiments of the present invention, not all of the embodiments. In the absence of conflict, the embodiments in this application and the features in the embodiments can be combined with each other. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of the present invention.

[0030] See also Figure 1 , the present invention provides a wet decarbonization technology regeneration gas heat recovery process system, including an absorption unit, a lean-rich liquid heat exchange unit and a regeneration unit;

[0031] The absorption unit is the place where the carbon-containing gas contacts and reacts with the organic amine absorbent, forming a carbon-less purified gas and a high-load carbon dioxide-rich liquid. After the purified gas is processed by the purified gas water washing section, the temperature drops to the preset value and is discharged out of the system.

[0032] The lean and rich liquid heat exchange unit allows the rich liquid generated by the absorption unit to fully exchange heat with the lean liquid generated by the regeneration unit, so that the temperature of the rich liquid increases and the temperature of the lean liquid decreases, thereby realizing the recovery and utilization of the heat of the lean liquid.

[0033] The steam from the regeneration unit heats the rich liquid produced by the stripping absorption unit, and forms lean liquid for circulation between absorption and regeneration, as well as regeneration gas with high calorific value. After being treated by the gas-liquid separation equipment, the regeneration gas forms heterogeneous carbon dioxide product gas and condensed water.

[0034] For further information, see Figure 2 The absorption unit includes an absorption tower 101, which includes, from bottom to top, an absorption section for making the carbon-containing gas and the lean liquid contact in countercurrent and a water washing system for forming a washing liquid circulation loop.

[0035] It should be noted that the carbon-containing gas enters the inner cavity of the absorption section from the bottom of the absorption tower 101 and flows from bottom to top, while the lean liquid is sprayed into the inner cavity of the absorption section from top to bottom. Fillers are provided in the absorption section. The carbon-containing gas and the lean liquid react in countercurrent, and mass transfer and heat transfer occur on the fillers. The absorbent after the reaction will load carbon dioxide to form a rich liquid, and the carbon-containing gas will form a purified gas with less carbon.

[0036] It should be noted that the absorbent can be traditional organic amine absorbents represented by monoethanolamine, diethanolamine, N-methyldiethanolamine, hydroxyethylethylenediamine, etc., or amino acid salt absorbents such as potassium (sodium) glycinate and potassium (sodium) alanine, phase change absorbents, ionic liquid absorbents, etc.

[0037] Further, see Figure 2The water washing system includes a purified gas water washing section, a water washing cooler 102, a washing tank 103, and a washing pump 104, which are connected to each other by metal pipes to form a washing liquid circulation loop;

[0038] Specifically, the purified gas water washing section is a place where the purified gas contacts the washing water sprayed on the upper part of the absorption tower 101 in countercurrent. The purified gas water washing section is located above the absorption section, and a liquid accumulation tray and an air riser are provided at the connection.

[0039] The liquid inlet of the washing tank 103 is connected to the outlet end at the bottom of the water washing section, and the liquid outlet is connected to the liquid inlet end of the washing pump 104. The washing tank 103 is used to store circulating washing water.

[0040] The liquid inlet of the washing pump 104 is connected to the outlet end of the washing tank 103, and the liquid outlet is connected to the liquid inlet end of the water washing cooler 102, so as to drive the washing liquid to flow in the pipeline.

[0041] The liquid inlet of the water washing cooler 102 is connected to the outlet end of the washing pump 104, and the liquid outlet is connected to the liquid inlet end of the purified gas water washing section. The function of the water washing cooler 102 is to cool and reduce the temperature of the circulating washing liquid.

[0042] It should be noted that after the purified gas leaves the absorption section, its temperature is relatively high and it carries a large amount of amine liquid. After the purified gas enters the purified gas water washing section through the riser pipe, it is sprayed with washing water from top to bottom in countercurrent contact with the purified gas. The purified gas temperature is reduced and discharged out of the system, and the washing liquid accumulates on the liquid accumulation tray.

[0043] It should be noted that, in the order of flow of the washing liquid, the equipment it passes through are the washing tank 103, the washing pump 104, and the water washing cooler 102. The washing liquid enters the washing tank 103 by gravity. The washing tank 103 has the function of storing liquid and buffering. The washing liquid in the washing tank 103 is forced to circulate in the water washing system by the suction action of the washing pump 104. The washing liquid enters the water washing cooler 102, and the temperature of the washing liquid is reduced to a preset value through indirect heat exchange with water cooling. The cooled washing liquid flows into the absorption tower 101 again.

[0044] It should be noted that the equipment in the water washing system is arranged and designed according to the flow direction of the washing liquid, forming a closed loop in series, and the connection between the equipment is connected by one-way metal pipe elements.

[0045] Preferably, a one-way metal pipe is introduced from the outlet of the washing pump 104 to transport the condensate to the front end of the rich liquid pump 203. After the washing liquid is mixed with the rich liquid, the heat in the rich liquid flow can be increased, which can reduce the overall regeneration energy consumption during the desorption process.

[0046] Further, see Figure 3The lean and rich liquid heat exchange unit includes a lean and rich liquid heat exchanger 201, a lean liquid cooler 202, a rich liquid pump 203 and a lean liquid pump 204, which are interconnected in the form of pipes to form a lean and rich liquid circulation loop between the absorption unit and the regeneration unit.

[0047] Specifically, the lean-rich liquid heat exchanger 201 is a component for exchanging heat between the rich liquid produced by the absorption tower 101 and the lean liquid flowing out of the regeneration tower 301 .

[0048] The liquid inlet of the lean liquid cooler 202 is connected to the outlet of the lean liquid pump 204, and the liquid outlet is connected to the lean liquid feed end of the absorption tower 101. The function of the lean liquid cooler 202 is to further reduce the lean liquid temperature.

[0049] The inlet of the rich liquid pump 203 is connected to the bottom discharge port of the absorption tower 101, and the outlet of the rich liquid pump 203 is connected to the rich liquid feed port of the lean-rich liquid heat exchanger 201. The rich liquid pump 203 is used to drive the rich liquid to flow in the pipeline.

[0050] The inlet of the lean liquid pump 204 is connected to the lean liquid outlet of the lean-rich liquid heat exchanger 201, the outlet of the lean liquid pump 204 is connected to the lean liquid feed port of the lean liquid cooler 202, and the rich liquid pump 203 is used to drive the lean liquid to flow in the pipeline.

[0051] The equipment in the lean and rich liquid heat exchange unit is interconnected in the form of metal pipes to form a lean and rich liquid circulation loop between the absorption unit and the regeneration unit. The connection sequence between the equipment is based on the flow direction of the lean and rich liquid.

[0052] It should be noted that the rich liquid flowing out of the bottom of the absorption tower 101 is forcibly driven by the rich liquid pump 203 to flow through the lean-rich liquid heat exchanger 201 and enter the regeneration unit, and the lean liquid flowing out of the regeneration unit is forcibly driven by the lean liquid pump 204 to flow through the lean-rich liquid heat exchanger 201, and the high-temperature lean liquid and the low-temperature rich liquid converge at the lean-rich liquid heat exchanger 201 for heat exchange. The lean liquid after heat exchange is driven by the lean liquid pump 204 to enter the lean liquid cooler 202 to be further cooled to a preset temperature and flow into the absorption tower 101.

[0053] It should be noted that the rich solution is the absorbent that has been saturated, and the lean solution is the absorbent that has not yet been saturated.

[0054] Further, see Figure 4 The regeneration unit includes a regeneration tower 301, a reboiler 302, and a condensation separation system.

[0055] Specifically, the regeneration tower 301 includes a regeneration section and a regeneration gas water washing system from bottom to top.

[0056] The regeneration section is where the rich liquid is sprayed from top to bottom and contacts the high-temperature steam generated by the reboiler 302 in reverse. The rich liquid is heated and stripped to release carbon dioxide.

[0057] It should be noted that the rich liquid enters the regeneration section from the lean and rich liquid heat exchange unit, and flows into the reboiler 302 from top to bottom. The rich liquid is heated to boiling by heat exchange through the reboiler 302 by externally supplied high-temperature steam, and the water in the rich liquid is vaporized into steam. The steam has a stripping effect that can reduce the partial pressure of carbon dioxide and release the carbon dioxide in the rich liquid. Packing is provided in the regeneration tower 301, and the gas-liquid two phases contact on the packing to cause mass transfer and heat transfer. After stripping and desorption, the rich liquid forms an unsaturated lean liquid and a regenerated gas rich in water vapor and carbon dioxide.

[0058] Furthermore, the regeneration gas water washing system is composed of a regeneration gas water washing section, a regeneration gas water washing tank 305, a regeneration gas washing pump 304 and a regeneration gas water washing cooler 303, which are connected to each other by metal pipes to form a washing liquid circulation loop.

[0059] Specifically, the regeneration gas water washing section is the place where the regeneration gas and the sprayed washing water come into countercurrent contact. The regeneration gas water washing section is located above the regeneration section, and a liquid accumulation tray and an air riser are provided at the connection.

[0060] The inlet of the regeneration gas water washing tank 305 is connected to the outlet end of the bottom of the regeneration gas water washing section, and the liquid outlet is connected to the liquid inlet end of the regeneration gas washing pump 304. The regeneration gas water washing tank 305 is used to store circulating washing water.

[0061] The inlet of the regeneration gas washing pump 304 is connected to the bottom outlet of the regeneration gas water washing tank 305, and the liquid outlet is connected to the liquid inlet of the regeneration gas water washing cooler 303. The regeneration gas washing pump 304 is used to drive the washing liquid to flow in the pipeline.

[0062] The liquid inlet of the regeneration gas water washing cooler 303 is connected to the outlet of the regeneration gas washing pump 304, and the liquid outlet is connected to the liquid inlet of the regeneration tower 301. The function of the regeneration gas water washing cooler 303 is to reduce the washing liquid temperature to a preset temperature.

[0063] The reboiler 302 is connected to the regeneration tower 301 through a one-way metal pipe, and is used to provide the heat required for desorption of the rich liquid.

[0064] Specifically, the reboiler 302 is connected in parallel with the regeneration tower 301 through a one-way metal pipe.

[0065] It should be noted that the regenerated gas is rich in high-temperature water vapor in addition to the captured carbon dioxide, and the high-temperature steam has a high latent heat value. After the regenerated gas enters the regenerated gas water washing section through the riser from the regeneration section, it is sprayed with washing water from top to bottom in countercurrent contact with the regenerated gas. The temperature of the regenerated gas is reduced and discharged to the condensation separation system, and the washing liquid accumulates on the liquid accumulation tray.

[0066] It should be noted that, in the order of flow of the washing liquid, the equipment it passes through are the regeneration gas water washing tank 305, the regeneration gas washing pump 304, and the regeneration gas water washing cooler 303. The washing liquid enters the regeneration gas water washing tank 305 by gravity. The regeneration gas water washing tank 305 has the function of storing liquid and buffering. The washing liquid in the regeneration gas water washing tank 305 is driven by the suction action of the regeneration gas washing pump 304 to circulate in the regeneration gas water washing system. The washing liquid enters the regeneration gas water washing cooler 303, and the temperature of the washing liquid is reduced to a preset value through water-cooled indirect heat exchange. The cooled washing liquid flows into the regeneration tower 301 again.

[0067] It should be noted that the equipment in the regeneration gas water washing system is arranged and designed according to the flow direction of the washing liquid, forming a closed loop in series, and the connection between the equipment is connected by one-way metal pipe elements.

[0068] When the regenerated gas water washing system is in use, the temperature of the washing liquid at the outlet of the regenerated gas water washing cooler 303 is controlled by adjusting the circulating cooling water flow rate to reach a preset temperature, thereby changing the temperature of the regenerated gas leaving the regenerated gas water washing section to achieve different effects of recovering heat value. The spray temperature of the circulating washing liquid is generally between 50-90°C, preferably 65-80°C.

[0069] The washing flow rate of the washing liquid in contact with the regeneration gas is 30-120% of the rich liquid circulation volume, preferably 60-100%, more preferably 60-100%, and more preferably 80-100%.

[0070] Preferably, a one-way metal pipe is introduced from the outlet of the regeneration gas washing pump 304 to transport the condensate to the front end of the rich liquid pump 203. After the washing liquid is mixed with the rich liquid, the heat in the rich liquid flow can be increased, which can reduce the overall regeneration energy consumption during the desorption process.

[0071] Preferably, a one-way metal pipe is led from the liquid outlet of the gas-liquid separator 307 to transport the condensed water to the regeneration gas washing tank 103, and the heat value in the regeneration gas is transferred to the washing liquid through gas-liquid conversion.

[0072] It should be noted that the position indicated by the front end of the rich liquid pump 203 is the position between the rich liquid kettle at the bottom of the absorption tower 101 and the rich liquid outlet at the bottom and the liquid inlet of the rich liquid pump 203 .

[0073] Furthermore, the condensation separation system mainly includes a regeneration gas condenser 306 and a gas-liquid separator 307;

[0074] The regeneration gas condenser 306 has its inlet connected to the regeneration gas outlet at the top of the regeneration tower 301 through a one-way metal pipe, and its outlet is connected to the inlet of the gas-liquid separator 307. The regeneration gas condenser 306 is used to reduce the regeneration gas temperature.

[0075] Gas-liquid separator 307, gas-liquid separator 307 is used to separate product carbon dioxide gas and condensed water.

[0076] It should be noted that after the regeneration gas is discharged from the regeneration gas water washing section, it enters the regeneration gas condenser 306, where the temperature of the regeneration gas is further reduced to form a heterogeneous flow of gaseous carbon dioxide and liquid condensed water.

[0077] It should be noted that the gas-liquid separator 307 separates the above-mentioned heterogeneous two-phase flow to form product carbon dioxide gas and condensed water; a one-way metal pipe is led from the liquid outlet of the gas-liquid separator 307 to transport the condensed water to the regeneration gas water washing tank 305.

[0078] To better demonstrate the beneficial effects of the present invention, the above-mentioned carbon capture process system is compared with a conventional carbon capture process system. This comparison takes a 10,000 t / a carbon dioxide capture project at a power plant as an example, using a 20 wt% ethanol-ammonia aqueous solution as the absorbent. The comparison results are shown in Table 1 below:

[0079]

[0080] Table 1

[0081] The above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit the same.

[0082] It should be noted that if the embodiments of the present invention involve directional indications such as up, down, left, right, front, and back, such directional indications are only used to explain the relative position relationship, movement status, etc. between the various components under a certain specific posture as shown in the accompanying drawings. If the specific posture changes, the directional indication will also change accordingly.

[0083] In addition, if there are descriptions involving "first", "second", etc. in the embodiments of the present invention, the descriptions of "first", "second", etc. are only for descriptive purposes and cannot be understood as indicating or suggesting their relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of such features. In addition, the meaning of "and / or" appearing throughout the text includes three parallel schemes. Taking "A and / or B" as an example, it includes scheme A, or scheme B, or schemes in which A and B are satisfied at the same time. In addition, "multiple" refers to more than two. In addition, the technical solutions between the various embodiments can be combined with each other, but it must be based on the ability of ordinary technicians in this field to implement. When the combination of technical solutions is mutually contradictory or cannot be implemented, it should be deemed that such a combination of technical solutions does not exist.

[0084] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the scope of protection of the present invention.

Claims

1. A wet decarbonization technology regeneration gas heat recovery process system, characterized by: It includes an absorption unit, a lean and rich liquid heat exchange unit and a regeneration unit connected in sequence; The regeneration unit comprises a regeneration tower (301), wherein the regeneration tower (301) is provided with a regeneration section for making the rich liquid contact with the high-temperature steam in reverse direction and a regeneration gas water washing system for forming a washing liquid circulation loop to transfer the heat value in the regeneration gas to the washing liquid in sequence from bottom to top; The regeneration gas water washing system comprises a regeneration gas water washing section, a regeneration gas water washing tank (305), a regeneration gas washing pump (304) and a regeneration gas water washing cooler (303) connected in sequence; A one-way metal pipe is led from the outlet of the regeneration gas washing pump (304) to transport the washing condensate to the front end of the rich liquid pump (203) in the lean-rich liquid heat exchange unit, so that the washing liquid is mixed with the rich liquid to increase the heat in the rich liquid flow; The absorption unit comprises an absorption tower (101), and the absorption tower (101) comprises, from bottom to top, an absorption section for making the carbon-containing gas and the lean liquid contact in countercurrent, and a water washing system for forming a washing liquid circulation loop; The water washing system comprises a purified gas water washing section, a washing tank (103), a washing pump (104), and a water washing cooler (102) connected in sequence, wherein a one-way metal pipe is led from the outlet of the washing pump (104) to transport the condensate to the front end of the rich liquid pump (203).

2. A wet decarbonization technology regeneration gas heat recovery process system according to claim 1, characterized in that: The regeneration gas water washing system is used to recover the calorific value of the regeneration gas, and the temperature of the circulating washing liquid is controlled by adjusting the circulating water volume of the regeneration gas water washing cooler (303), wherein the spraying temperature of the circulating washing liquid is controlled to be between 50-90°C.

3. The wet decarbonization technology regeneration gas heat recovery process system according to claim 1, characterized in that: The washing flow rate of the washing liquid in contact with the regeneration gas is 30-120% of the rich liquid circulation volume.

4. A wet decarbonization technology regeneration gas heat recovery process system according to claim 1, characterized in that: Fillers are provided in the absorption section and the regeneration section, and the absorbent added to the fillers can be any one of organic amine absorbent, amino acid salt absorbent, phase change absorbent, and ionic liquid absorbent.

5. The wet decarbonization technology regeneration gas heat recovery process system according to claim 1, characterized in that: The regeneration unit further includes a condensation separation system consisting of a regeneration gas condenser (306) and a gas-liquid separator (307), wherein the inlet end of the regeneration gas condenser (306) is connected to the regeneration gas outlet at the top of the regeneration tower through a one-way metal pipe, and the outlet end is connected to the inlet end of the gas-liquid separator (307).

6. A wet decarbonization technology regeneration gas heat recovery process system according to claim 5, characterized in that: A one-way metal pipe is led from the liquid outlet of the gas-liquid separator (307) to transport the condensed water to the regeneration gas-water washing tank (305).

7. The wet decarbonization technology regeneration gas heat recovery process system according to claim 1, characterized in that: The regeneration unit further comprises a reboiler (302), which is connected in parallel with the regeneration tower (301) via a one-way metal pipe and is used to provide heat required for desorption of the rich liquid.

8. The wet decarbonization technology regeneration gas heat recovery process system according to claim 1, characterized in that: The lean and rich liquid heat exchange unit further includes a lean and rich liquid heat exchanger (201), a lean liquid cooler (202), and a lean liquid pump (204), which together with the rich liquid pump (203) form a lean and rich liquid circulation loop between the absorption unit and the regeneration unit.

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