CN214880242U

CN214880242U - Carbon dioxide absorption capture and heat supply network coupling system

Info

Publication number: CN214880242U
Application number: CN202120684936.6U
Authority: CN
Inventors: 王争荣; 王凯亮; 汪洋; 孙路长; 耿宣; 苏军划; 胡小夫; 何佳
Original assignee: China Huadian Engineering Group Co Ltd; Huadian Environmental Protection Engineering and Technology Co Ltd
Current assignee: China Huadian Engineering Group Co Ltd; Huadian Environmental Protection Engineering and Technology Co Ltd
Priority date: 2021-04-02
Filing date: 2021-04-02
Publication date: 2021-11-26
Anticipated expiration: 2031-04-02

Abstract

The utility model provides a carbon dioxide absorbs entrapment and heat supply network coupled system belongs to carbon dioxide entrapment technical field, include: the system comprises an absorption tower, a regeneration tower and a reboiler, wherein the regeneration tower is communicated with rich liquid in the absorption tower through a pipeline, a crude gas exhaust port is formed in the regeneration tower, a first cooling heat exchanger is communicated with the rear end of the crude gas exhaust port of the regeneration tower, and the first cooling heat exchanger is communicated with a heat supply pipe network of a thermal power plant; the reboiler is communicated with the regeneration tower and is used for heating the rich liquid in the regeneration tower; the utility model discloses a carbon dioxide absorbs entrapment and heat supply network coupled system, the coarse gas vent rear end intercommunication at the regenerator tower has first cooling heat exchanger, this first cooling heat exchanger and the heat supply pipe network intercommunication of thermal power plant for heat supply water to the heat supply pipe network heats, thereby reduce the steam turbine that is used for carrying out the heating to the heat supply water of heat supply pipe network and bleed the power consumption, thereby reduce the power consumption of carbon dioxide entrapment system on the whole, reach energy-conserving purpose.

Description

Carbon dioxide absorption capture and heat supply network coupling system

Technical Field

The utility model relates to a carbon dioxide entrapment technical field, concretely relates to carbon dioxide absorbs entrapment and heat supply network coupled system.

Background

CCS technology is an abbreviation for Carbon Capture and Storage, a technology that captures and sequesters Carbon dioxide (CO 2). The CCS technology is a carbon capture technology that separates carbon dioxide produced by industry and related energy industries, and then transports and stores the separated carbon dioxide to places isolated from the atmosphere, such as the sea floor or the underground, by means of carbon storage.

CCS technology consists of two parts, carbon capture and carbon sequestration. Among them, the carbon capture technology is applied to industries such as oil refining and chemical industry for the earliest time. Due to the high concentration and pressure of CO2 emitted by these industries, the capture cost is not high. The opposite is true for CO2 emitted from coal-fired power plants, and carbon dioxide capture from power plant emissions has problems of high energy consumption and high cost.

The energy consumption of the carbon dioxide capture system is mainly the regeneration steam consumption of the regeneration tower, because the temperature difference between the lean solution at the bottom of the regeneration tower and the regeneration gas at the top of the regeneration tower is not large, the heat contained in the lean solution at the bottom of the regeneration tower and the heat contained in the regeneration gas at the top of the regeneration tower are relatively close, if the heat is recovered by the rich solution at the bottom of the absorption tower, the heat recovery of one stream in the lean solution at the bottom of the tower or the regenerator at the top of the tower can only be realized, the temperature difference between the heated rich solution and the temperature of the other stream is not large, the heat recovery of the other stream can not be realized, and the other stream can only be cooled by circulating cooling water at present, so that about half of the heat is wasted.

SUMMERY OF THE UTILITY MODEL

Therefore, the to-be-solved technical problem of the utility model lies in overcoming the too high defect of energy consumption of the carbon dioxide entrapment system for power plant among the prior art to a carbon dioxide absorbs entrapment and heat supply network coupled system is provided.

In order to solve the technical problem, the utility model provides a carbon dioxide absorbs entrapment and heat supply network coupled system is applicable to the carbon dioxide entrapment of steam power plant, include:

one end of the absorption tower is communicated with a flue gas outlet of the thermal power plant, the absorption tower is suitable for containing absorption liquid, and the absorption liquid in the absorption tower absorbs carbon dioxide in the flue gas and then becomes rich liquid;

the regeneration tower is communicated with rich liquid in the absorption tower through a pipeline, a crude gas exhaust port is formed in the regeneration tower, the rear end of the crude gas exhaust port of the regeneration tower is communicated with a first cooling heat exchanger, and the first cooling heat exchanger is communicated with a heat supply pipe network of a thermal power plant;

and the reboiler is communicated with the regeneration tower and is used for heating the rich liquid entering the regeneration tower, the rich liquid is heated to separate out carbon dioxide gas, and the carbon dioxide gas is discharged from a crude gas exhaust port of the regeneration tower.

Optionally, a cooling water inlet of the first cooling heat exchanger is communicated with return water of the heat supply pipe network, and a cooling water outlet of the first cooling heat exchanger is communicated with a heat supply primary station of the heat supply pipe network.

Optionally, the absorption tower is provided with a self-circulation pipeline, one end of the self-circulation pipeline is communicated with the tower bottom absorption liquid of the absorption tower, and the other end of the self-circulation pipeline is communicated with the tower top inner cavity of the absorption tower.

Optionally, a self-circulation heat exchanger is arranged on the self-circulation pipeline.

Optionally, a spraying device is arranged on an outlet of one end of the self-circulation pipeline, which leads to the tower top inner cavity of the absorption tower.

Optionally, a tail gas emptying port is arranged on the absorption tower, a tail gas heat exchanger is arranged at the front end of the tail gas emptying port, and the tail gas heat exchanger is arranged above the self-circulation pipeline.

Optionally, a demister is further arranged at the front end of the tail gas evacuation port of the absorption tower.

Optionally, a demister is arranged at the front end of the raw gas exhaust port of the regeneration tower.

Optionally, the crude gas exhaust port of the regeneration tower is communicated with a gas-liquid separator, and the separated water of the gas-liquid separator flows back into the regeneration tower.

Optionally, a second cooling heat exchanger is further disposed at the rear end of the first cooling heat exchanger, and the separated water discharged from the gas-liquid separator is firstly used as cooling water of the second cooling heat exchanger and then flows back to the regeneration tower.

The utility model discloses technical scheme has following advantage:

1. the utility model provides a carbon dioxide absorbs entrapment and heat supply network coupled system, the coarse gas vent rear end intercommunication at the regenerator tower has first cooling heat exchanger, this first cooling heat exchanger and the heat supply pipe network intercommunication of thermal power plant for heat supply water to the heat supply pipe network heats, thereby reduce the steam turbine that is used for carrying out the heating to the heat supply water of heat supply pipe network and bleed the power consumption, thereby reduce the power consumption of carbon dioxide entrapment system on the whole, reach energy-conserving purpose.

The utility model provides a heat supply initial station refers to the heat supply initial station of power plant for it bleeds and supplies hot water and carries out the heat transfer to provide the steam turbine.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the technical solutions in the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.

Fig. 1 is a schematic diagram of a carbon dioxide absorption capture and heat supply network coupling system provided in an embodiment of the present invention.

FIG. 2 is a schematic view of a portion of the carbon dioxide capture system of FIG. 1.

Fig. 3 is a schematic view of a portion of the absorption column and the regeneration column of fig. 2.

Description of reference numerals:

1. a user; 2. a heat supply network circulation pump; 3. a preheater; 4. a heat supply primary station; 5. pre-washing the tower; 6. an absorption tower; 7. a regeneration tower; 8. a reboiler; 9. a gas-liquid separator; 10. a flue gas inlet; 11. a booster fan; 12. a pre-washing pump; 13. a washing liquid heat exchanger; 14. a pH value detection element; 15. a self-circulating heat exchanger; 16. a self-circulating pump; 17. a tail gas evacuation port; 18. a tail gas heat exchanger; 19. a lean-rich liquid heat exchanger; 20. a barren liquor heat exchanger; 21. a crude gas vent; 22. a first cooling heat exchanger; 23. a second cooling heat exchanger.

Detailed Description

The technical solution of the present invention will be described clearly and completely with reference to the accompanying drawings, and obviously, the described embodiments are some, but not all embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.

In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but 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 thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.

Furthermore, the technical features mentioned in the different embodiments of the invention described below can be combined with each other as long as they do not conflict with each other.

The embodiment provides a carbon dioxide absorbs entrapment and heat supply network coupled system, as shown in fig. 1, this system is applicable to the carbon dioxide entrapment of the steam power plant that has the heat supply pipe network, specifically includes: a carbon dioxide capture system and a heat net system. Wherein the heat supply network system includes: the heat supply pipeline is used for supplying heat to a user 1, the heat supply pipeline performs circulating flow of internal hot water through a heat supply network circulating pump 2, and is also connected with a preheater 3, and the hot water is preliminarily heated through the preheater 3; the heat supply pipeline is also connected with a heat supply initial station 4, and heat exchange is carried out by the heat supply initial station 4 through air exhaust of a steam turbine and hot water supply, so that the hot water supply meets the heat supply requirement; in a conventional heat supply network system, return water of a heat supply network generally needs to be circulated by a heat supply network circulating pump 2 for supplying hot water, the hot water is heated by a preheater 3, a heating heat source of the preheater 3 is used for extracting steam for a steam turbine auxiliary machine, the hot water is sent to a first station of the heat supply network by the heat supply network circulating pump 2 for heating, and the temperature is respectively heated to 90-130 ℃ according to different city sizes and conveying distances. The heat supply pipeline is connected with the user 1 and supplies heat to the user 1 through hot water supply.

According to the carbon dioxide absorption, collection and heat supply network coupling system, before return water of a heat supply network enters the heat supply network circulating pump 2, part of hot water is distributed to the carbon dioxide collection system, the hot water is preheated by utilizing waste heat of the carbon dioxide collection system and then enters the heat supply primary station 4, and therefore the steam turbine air extraction energy consumption of the heat supply primary station 4 for heating the hot water is reduced.

Specifically, as shown in fig. 1 and 2, the carbon dioxide capture system includes: a prewashing tower 5, an absorption tower 6 and a regeneration tower 7. The regeneration tower 7 is provided with a crude gas exhaust port 21, the rear end of the crude gas exhaust port 21 of the regeneration tower 7 is communicated with a first cooling heat exchanger 22, and the first cooling heat exchanger 22 is communicated with a heat supply pipe network of a thermal power plant; that is, the cooling water inlet of the first cooling heat exchanger 22 is communicated with the return water of the heat supply network, and the cooling water outlet of the first cooling heat exchanger 22 is communicated with the heat supply primary station 4 of the heat supply network. In addition, it can be understood that the cooling water inlet of the first cooling heat exchanger 22 may be communicated before the heat supply network circulating pump 2 of the heat supply network, or may be connected after the heat supply network circulating pump 2, specifically, the cooling water inlet may be set according to the needs of the site.

As shown in fig. 2, the pre-washing tower 5 is provided with a flue gas inlet 10, the flue gas inlet 10 is used for communicating with flue gas after desulfurization, and the flue gas enters the pre-washing tower 5 through the flue gas inlet 10; the prewashing tower 5 is mainly used for removing trace acid gases in the flue gas, reducing the temperature of the flue gas through circulating spraying of alkali liquor, and reducing the moisture content and the volume of the flue gas. The top of the pre-washing column 5 has an outlet which is connected to the inlet of the absorption column 6 via a booster fan 11. The pre-washing tower 5 is provided with a circulating pipeline, two ends of the circulating pipeline are respectively communicated with the bottom end and the top end of the pre-washing tower 5, the circulating pipeline is connected with a pre-washing pump 12, washing liquid in the pre-washing tower 5 is conveyed to the tower top from the tower bottom through the pre-washing pump 12, and the washing liquid returns to the tower bottom again in the tower top in a spraying mode; in the process that the flue gas flows from the flue gas inlet 10 to the flue gas outlet in the pre-washing tower 5, the flue gas and the washing liquid flow in a convection manner, so that the flue gas is pre-washed by the washing liquid. In addition, as a preferred embodiment, a washing liquid heat exchanger 13 is further connected to the circulation pipeline, and the washing liquid heat exchanger 13 is used for cooling the washing liquid, so as to control the outlet flue gas temperature of the prewashing tower, namely the inlet temperature of the absorption tower, and adjust the water balance of the absorption liquid of the absorption and collection system. In addition, as a preferred embodiment, a PH value detecting element 14 is further connected in parallel to the circulating pipeline, and the PH value detecting element 14 is used for detecting the PH value of the washing solution in real time so as to supplement the alkaline washing solution in time.

As shown in fig. 3, an inlet at one end of the absorption tower 6 is connected with an outlet of the pre-washing tower 5 so as to communicate with flue gas of the thermal power plant, and the inside of the absorption tower 6 is adapted to contain an absorption liquid, and the absorption liquid in the absorption tower 6 becomes a rich liquid after absorbing carbon dioxide in the flue gas. Specifically, the absorption tower 6 is provided with a self-circulation pipeline, one end of the self-circulation pipeline is communicated with the tower bottom absorption liquid of the absorption tower 6, the other end of the self-circulation pipeline is communicated with the tower top inner cavity of the absorption tower 6, a spraying device is arranged at an outlet of one end of the self-circulation pipeline, which is communicated with the tower top inner cavity of the absorption tower 6, and the absorption liquid is sprayed downwards from the tower top through the spraying device so as to be fully contacted with the flue gas. The self-circulation pipeline is provided with a self-circulation heat exchanger 15 and a self-circulation pump 16, the self-circulation heat exchanger 15 is used for recycling the temperature of the flue gas, and the self-circulation pump 16 is used for keeping the circulating flow of the absorption liquid. The temperature in the absorption tower 6 is controlled by the absorption tower 6 through the heat exchange of the self-circulation heat exchanger 15, the lower temperature and the higher pressure are more beneficial to the absorption of carbon dioxide by the absorbent, the absorption liquid at the bottom of the absorption tower 6 is pumped out to the self-circulation heat exchanger 15 from the circulating pump 16 on a self-circulation pipeline arranged outside the absorption tower 6 to exchange heat with cooling circulation water, the cooled absorption liquid can be sent to the top of the absorption tower 6 or the middle part of the absorption tower 6, the cold absorption liquid is contacted with the flue gas in the absorption tower 6 to exchange heat, so that the tower temperature of the absorption tower 6 is controlled, the absorption capacity of the absorption liquid per unit mass is increased, and the absorption capacity of the absorption liquid is changed by controlling the tower temperature of the absorption tower 6 through the self-circulation system.

As shown in fig. 3, the absorption tower 6 is provided with a tail gas vent 17, a tail gas heat exchanger 18 is provided at the front end of the tail gas vent 17, the tail gas heat exchanger 18 is disposed above the spray opening of the self-circulation pipeline, and the temperature of the flue gas discharged from the absorption tower 6 is recovered by the tail gas heat exchanger 18. Specifically, the tail gas heat exchanger 18 is a wide-channel plate heat exchanger, the escape rate of the absorbent from the top of the absorption tower 6 can be reduced through the plate heat exchanger, and the wide-channel plate heat exchanger has the advantages of small heat exchange end difference, large heat exchange coefficient and the like. The cooling circulating water exchanges heat with the flue gas through the partition wall, the temperature of the flue gas at the top of the absorption tower 6 is saturated flue gas, water is separated out after the heat exchange with the cooling circulating water, absorption liquid carried in the flue gas is also separated out, and the separated water and the absorbent flow back to the absorption tower 6 again along the heat exchange wall of the plate heat exchanger for recycling. In addition, the absorption tower 6 is also provided with a demister between the tail gas heat exchanger 18 and the tail gas evacuation port 17, and the demister is used for reducing the water content in the flue gas.

As shown in fig. 3, the regeneration tower 7 is communicated with the rich liquid in the absorption tower 6 through a rich liquid supply pipe, one end of the rich liquid supply pipe extends into the absorption tower 6 from the tower bottom of the absorption tower 6, the other end of the rich liquid supply pipe extends into the regeneration tower 7 from the tower top of the regeneration tower 7, the rich liquid enters the tower top of the regeneration tower 7 from the absorption tower 6, and is sprayed downward from the inside of the tower top of the regeneration tower 7 in a spraying manner, so that the carbon dioxide gas contained in the rich liquid is precipitated. In addition, a lean liquid return pipe is connected between the regeneration tower 7 and the absorption tower 6, one end of the lean liquid return pipe is communicated to the inside of the bottom end of the regeneration tower 7, the other end of the lean liquid return pipe is communicated to the inside of the tower top of the absorption tower 6, and the lean liquid return pipe sprays water in the tower top of the absorption tower 6 in a spraying mode. In addition, the lean liquid return pipe and the rich liquid supply pipe are connected through a lean-rich liquid heat exchanger 19, that is, after the hot lean liquid in the lean liquid return pipe transfers heat to the rich liquid in the rich liquid supply pipe through the lean-rich liquid heat exchanger 19, the lean liquid in the lean liquid return pipe returns to the absorption tower 6 again, so that the heat of the lean liquid in the regeneration tower 7 is absorbed; in addition, the rich solution is heated by the lean solution in the lean and rich solution heat exchanger 19 and then enters the top of the regeneration tower 7, the reboiler 8 is arranged at the bottom of the regeneration tower 7, steam used by the reboiler 8 is extracted from a steam turbine, the steam turbine is extracted from the reboiler 8 and subjected to heat exchange and condensation, condensed water returns to a deaerator of a thermodynamic system, exhaust gas at the top of the regeneration tower 7 exchanges heat with heat supply return water of a heat supply network, and the heat supply return water is heated by the exhaust gas and then sent to a first station of the heat supply network, so that the preheating of the heat supply network return water is realized, the steam turbine extraction used by the preheater 3 of the original heat supply network is reduced or is not used at all, and the waste heat recovery of the regenerated gas of the carbon dioxide capture system is realized. In addition, a barren liquor heat exchanger 20 is arranged on the barren liquor return pipe, and the barren liquor is cooled through the barren liquor heat exchanger 20 to recover the absorption of carbon dioxide in the flue gas by the absorption liquid.

As shown in fig. 3, the top of the regeneration tower 7 has a raw gas outlet 21, and a demister is provided at the front end of the raw gas outlet 21 to reduce the water content in the exhaust gas. The raw gas outlet 21 of the regeneration tower 7 is communicated with the gas-liquid separator 9, and the separated water of the gas-liquid separator 9 flows back into the regeneration tower 7.

As shown in fig. 3, the regeneration tower 7 communicates with a reboiler 8, and the reboiler 8 vaporizes the rich liquid introduced into the regeneration tower 7 into a gas-liquid two-phase, and also, carbon dioxide gas in the rich liquid is precipitated by heating to change the rich liquid into a lean liquid, and the carbon dioxide gas in the rich liquid is discharged from a raw gas exhaust port 21 of the regeneration tower 7. The reboiler 8 can be understood as a heat exchanger, the reboiler 8 being in communication with the steam extraction for heating the absorption liquid by the steam extraction.

As shown in fig. 3, the raw gas exhaust port 21 of the regeneration tower 7 is communicated with a first cooling heat exchanger 22, and the first cooling heat exchanger 22 is used for exchanging heat with hot water in a heating pipeline network, so as to recover heat of carbon dioxide saturated gas precipitated in the regeneration tower 7. Further, a second cooling heat exchanger 23 is provided at the rear end of the first cooling heat exchanger 22, and the separated water discharged from the gas-liquid separator 9 is first used as the cooling water of the second cooling heat exchanger 23 and then returned to the regeneration tower 7, thereby further recovering heat from the carbon dioxide gas. In addition, as an alternative embodiment, the separated water discharged from the gas-liquid separator 9 may be subjected to heat exchange without passing through the second cooling heat exchanger 23, or may be partially subjected to heat exchange by passing through the second cooling heat exchanger 23, and partially directly introduced into the regeneration tower 7. In addition, the separated water discharged from the gas-liquid separator 9, if excessive, may be sent to a desulfurization system of a power plant for reuse.

As shown in fig. 3, the gas discharged from the gas-liquid separator 9 is compressed by a compressor and then used, thereby completing the capture of carbon dioxide in the flue gas. The carbon dioxide capturing and heat supply network backwater coupling system provided by the embodiment can realize gradient utilization of energy of extracted steam, reduce the overall steam consumption of the carbon dioxide capturing and heat supply network system, and realize that the steam consumption for capturing carbon dioxide is reduced by 30-40%.

It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious changes and modifications may be made without departing from the scope of the present invention.

Claims

1. A carbon dioxide absorption capture and heat supply network coupling system is characterized in that the system is suitable for capturing carbon dioxide of a thermal power plant and comprises:

one end of the absorption tower (6) is communicated with a flue gas outlet of the thermal power plant, the absorption tower is suitable for containing absorption liquid, and the absorption liquid in the absorption tower (6) absorbs carbon dioxide in the flue gas and then becomes rich liquid;

the regeneration tower (7) is communicated with rich liquid in the absorption tower (6) through a pipeline, a crude gas exhaust port (21) is formed in the regeneration tower (7), a first cooling heat exchanger (22) is communicated with the rear end of the crude gas exhaust port (21) of the regeneration tower (7), and the first cooling heat exchanger (22) is communicated with a heat supply pipe network of a thermal power plant;

and the reboiler (8) is communicated with the regeneration tower (7) and is used for heating the rich liquid entering the regeneration tower (7), the rich liquid is heated to separate out carbon dioxide gas, and the carbon dioxide gas is discharged from a crude gas exhaust port (21) of the regeneration tower (7).

2. The carbon dioxide absorption, capture and heat supply network coupling system according to claim 1, wherein the cooling water inlet of the first cooling heat exchanger (22) is communicated with the return water of the heat supply network, and the cooling water outlet of the first cooling heat exchanger (22) is communicated with the heat supply primary station (4) of the heat supply network.

3. The carbon dioxide absorption, capture and heat supply network coupling system according to claim 1, wherein the absorption tower (6) is provided with a self-circulation pipeline, one end of the self-circulation pipeline is opened into the tower bottom absorption liquid of the absorption tower (6), and the other end of the self-circulation pipeline is opened into the tower top inner cavity of the absorption tower (6).

4. The carbon dioxide absorption, capture and heat supply network coupling system of claim 3, wherein the self-circulating conduit is provided with a self-circulating heat exchanger (15).

5. The carbon dioxide absorption, capture and heat supply network coupling system of claim 3, wherein a spray device is arranged on an outlet of one end of the self-circulation pipeline, which leads to the tower top inner cavity of the absorption tower (6).

6. The carbon dioxide absorption, capture and heat supply network coupling system according to claim 3, wherein the absorption tower (6) is provided with a tail gas evacuation port (17), a tail gas heat exchanger (18) is arranged at the front end of the tail gas evacuation port (17), and the tail gas heat exchanger (18) is arranged above the self-circulation pipeline.

7. The carbon dioxide absorption, capture and heat supply network coupling system of claim 6, wherein the front end of the tail gas vent (17) of the absorption tower (6) is further provided with a demister.

8. The carbon dioxide absorption, capture and heat network coupling system according to any one of claims 1-7, wherein the front end of the raw gas exhaust port (21) of the regeneration tower (7) is provided with a demister.

9. The carbon dioxide absorption, capture and heat network coupling system according to any one of claims 1 to 7, wherein the raw gas exhaust port (21) of the regeneration tower (7) is communicated with a gas-liquid separator (9), and separated water of the gas-liquid separator (9) is refluxed into the regeneration tower (7).

10. The carbon dioxide absorption, capture and heat network coupling system according to claim 9, wherein a second cooling heat exchanger (23) is further provided at the rear end of the first cooling heat exchanger (22), and the separated water discharged from the gas-liquid separator (9) is firstly used as the cooling water of the second cooling heat exchanger (23) and then is refluxed into the regeneration tower (7).