System for capturing carbon dioxide in flue gas of rotary kiln

Abstract

The utility model discloses a system for capturing carbon dioxide in flue gas of a rotary kiln, which relates to the technical field of waste gas treatment and comprises a flue gas purification tower, a booster fan and a regeneration tower are arranged at the front end of the flue gas purification tower, and a carbon dioxide removal tower is arranged between the regeneration tower and the flue gas purification tower. A decarburizing agent recovery tower and an acid gas treatment assembly are arranged above the carbon dioxide removal tower, the acid gas treatment assembly comprises an acid gas condenser, an acid gas extraction device connected with the rear end of the acid gas condenser, and the acid gas condenser is connected with the flue gas purification tower and the regeneration tower; the heat exchange assembly comprises a lean and rich liquid heat exchanger located between the regeneration tower and the carbon dioxide removal tower and used for conducting heat exchange on rich liquid discharged from the carbon dioxide removal tower and lean liquid discharged from the regeneration tower, heat exchange is conducted through solutions with different temperatures generated in the system, the use amount of heat exchange media is reduced, and the purpose of reducing cost is achieved.

Description

Technical Field

[0001] The utility model relates to the technical field of waste gas treatment, and more specifically to a rotary kiln flue gas carbon dioxide capture system. Background Art

[0002] Excessive carbon dioxide emissions are widely recognized as one of the most significant contributors to global climate change. To reduce carbon dioxide emissions, developing economical, efficient, and scalable carbon dioxide capture technologies is imperative. Carbon dioxide capture, utilization, and storage are key approaches to reducing carbon dioxide emissions. Currently, commonly used carbon dioxide capture technologies include chemical absorption and pressure swing adsorption, with organic amine absorption being the most common chemical absorption method.

[0003] The traditional organic amine decarbonization process is mainly as follows: after the flue gas passes through the deep dust removal and acid mist removal in the pretreatment tower, it is cooled and enters the decarbonization absorption tower. The decarbonization absorbent in the absorption tower contacts with carbon dioxide to capture it. The rich liquid that absorbs carbon dioxide is sent to the regeneration tower for desorption after the lean and rich liquid heat exchange. After regeneration and desorption, the lean liquid is sent to the absorption tower for recycling after the lean and rich liquid heat exchange and lean liquid condensation. The acid gas generated by the rich liquid after heat exchange in the regeneration tower and the reboiler is cooled by heat exchange from the top of the regeneration tower. The condensate obtained after the acid gas is cooled is directly returned to the upper part of the regeneration tower. The condensed acid gas is separated by gas and liquid to obtain high-purity carbon dioxide gas.

[0004] Organic amine flue gas CO2 capture offers high CO2 removal efficiency and mature technology, but this technology still faces challenges such as high decarbonization solution loss, high energy consumption for desorption of the decarbonization absorbent, and high CO2 removal costs. The flue gas from lime rotary kilns in steel plants can reach temperatures of 1000°C after preheating and heat exchange. This flue gas has high gas volume, low partial pressure, and low CO2 concentration, resulting in high costs when using traditional decarbonization processes.

[0005] In summary, how to provide a low-cost carbon dioxide capture system suitable for lime rotary kiln flue gas is an urgent problem to be solved by those skilled in the art. Utility Model Content

[0006] In view of this, the purpose of the present invention is to provide a rotary kiln flue gas carbon dioxide capture system, which fully utilizes the heat of the flue gas itself and reduces the cost of the decarbonization process.

[0007] In order to achieve the above purpose, the present invention provides the following technical solutions:

[0008] A rotary kiln flue gas carbon dioxide capture system, comprising:

[0009] A flue gas purification tower, wherein a booster fan is provided at the front end of the flue gas purification tower;

[0010] A regeneration tower, wherein a carbon dioxide removal tower is provided between the regeneration tower and the flue gas purification tower, and a decarbonizing agent recovery tower is provided above the carbon dioxide removal tower;

[0011] an acid gas treatment component, the acid gas treatment component comprising an acid gas condenser and an acid gas extraction device connected to the rear end of the acid gas condenser, the acid gas condenser being connected to the flue gas purification tower and the regeneration tower;

[0012] The heat exchange component includes a lean and rich liquid heat exchanger located between the regeneration tower and the carbon dioxide removal tower, and is used to exchange heat between the rich liquid discharged from the carbon dioxide removal tower and the lean liquid discharged from the regeneration tower.

[0013] The present invention further includes:

[0014] A flue gas diversion device and a bag dust collector, wherein the bag dust collector is located between the flue gas diversion device and the flue gas purification tower, and a flue gas mixer is provided between the flue gas diversion device and the bag dust collector;

[0015] The heat exchange assembly also includes a rich liquid reheater, which is connected to the flue gas diversion device and the flue gas mixer respectively, and is used to heat the rich liquid discharged from the carbon dioxide removal tower and passed through the lean and rich liquid heat exchanger.

[0016] Furthermore, the present invention provides that the flue gas enters the lime rotary kiln preheater for heat exchange before entering the flue gas diversion device.

[0017] Furthermore, the utility model provides that the flue gas purification tower includes at least two levels of washing.

[0018] The utility model further adopts that the first stage washing of the flue gas purification tower adopts alkaline solution, and the second stage washing of the flue gas purification tower adopts desalted water.

[0019] The utility model further comprises:

[0020] Wire mesh capture device, used to capture the decarbonizer entrained in the flue gas;

[0021] The recovery liquid tank is used to wash the flue gas and discharge the washed flue gas after de-atomization.

[0022] Furthermore, the utility model adopts desalted water as the washing solution of the recovery tank.

[0023] Furthermore, the heat exchange component of the present invention further includes:

[0024] an acid gas heat exchanger, the rich liquid reheater being connected to the rich liquid reheater and being located between the lean and rich liquid heat exchanger and the regeneration tower;

[0025] a reboiler connected to the rich liquid outlet of the regeneration tower;

[0026] The lean liquid recooler is used to cool the lean liquid that has passed through the lean-rich liquid heat exchanger again.

[0027] Furthermore, the acid gas treatment component of the present invention further includes:

[0028] a gas-liquid separator, the gas-liquid separator being located between the acid gas cooler and the acid gas extraction device;

[0029] An acid gas dehydration device is connected to the acid gas extraction device.

[0030] The utility model further provides a rich liquid tank between the carbon dioxide removal tower and the regeneration tower, and the rich liquid tank is provided with two outlets. One of the outlets of the rich liquid tank is connected to the regeneration tower after passing through the lean and rich liquid heat exchanger and the rich liquid reheater in sequence, and the other outlet of the rich liquid tank is connected to the regeneration tower through the rich liquid acid gas heat exchanger.

[0031] The rotary kiln flue gas carbon dioxide capture system provided by the utility model, when in use, the treated flue gas is first pressurized by a booster fan to increase the air pressure of the entire capture system, which is beneficial to the reaction and capture of carbon dioxide; a carbon dioxide removal tower is provided between the regeneration tower and the flue gas purification tower; a decarbonizer recovery tower is provided above the carbon dioxide removal tower; an acid gas treatment component comprises an acid gas condenser and an acid gas exhaust device connected to the rear end of the acid gas condenser; the acid gas condenser is connected to the flue gas purification tower and the regeneration tower; a heat exchange component comprises a lean and rich liquid heat exchanger located between the regeneration tower and the carbon dioxide removal tower, for exchanging heat between the rich liquid discharged from the carbon dioxide removal tower and the lean liquid discharged from the regeneration tower; and by utilizing solutions of different temperatures generated within the system itself for heat exchange, the amount of heat exchange medium used is reduced, thereby achieving the purpose of reducing costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are merely embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on the provided drawings without paying any creative work.

[0033] Figure 1 This is a schematic diagram of the overall process provided by the utility model;

[0034] Figure 2 This is a structural diagram of the system process flow provided by the utility model;

[0035] Figure 1-Figure 2 , the reference numerals include:

[0036] 1. Booster fan; 2. Flue gas purification tower; 3. Acid gas dehydration unit; 4. Carbon dioxide removal tower; 5. Decarbonizer recovery tower; 6. Recovery tank; 7. Rich liquid tank; 8. Lean and rich liquid heat exchanger; 9. Lean liquid recooler; 10. Rich liquid reheater; 11. Regeneration tower; 12. Reboiler; 13. Acid gas heat exchanger; 14. Acid gas condenser; 15. Gas-liquid separator; 16. Acid gas extraction unit DETAILED DESCRIPTION

[0037] 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. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.

[0038] The core of the utility model is to provide a rotary kiln flue gas carbon dioxide capture system, which fully utilizes the heat of the flue gas itself and reduces the cost of the decarbonization process.

[0039] Please refer to Figure 1-Figure 2 A rotary kiln flue gas carbon dioxide capture system includes a flue gas purification tower 2, a regeneration tower 11, an acid gas treatment component and a heat exchange component. A booster fan 1 is provided at the front end of the flue gas purification tower 2, a carbon dioxide removal tower 4 is provided between the regeneration tower 11 and the flue gas purification tower 2, and a decarbonizer recovery tower 5 is provided above the carbon dioxide removal tower 4. The acid gas treatment component includes an acid gas condenser 14 and an acid gas extraction device 16 connected to the rear end of the acid gas condenser 14. The acid gas condenser 14 is connected to the flue gas purification tower 2 and the regeneration tower 11. The heat exchange component includes a lean and rich liquid heat exchanger 8 located between the regeneration tower 11 and the carbon dioxide removal tower 4, which is used to exchange heat between the rich liquid discharged from the carbon dioxide removal tower 4 and the lean liquid discharged from the regeneration tower 11.

[0040] Optionally, in order to further improve the utilization rate of flue gas preheating, in some embodiments, the flue gas first enters the lime rotary kiln preheater for preheating of the lime rotary kiln before being collected and processed. On the one hand, it can achieve the purpose of lowering the flue gas temperature, and on the other hand, it can improve the utilization rate of the flue gas temperature and reduce energy loss.

[0041] During use, the treated flue gas is first pressurized by the booster fan 1 to increase the air pressure of the entire capture system, which is beneficial to the reaction and capture of carbon dioxide. A carbon dioxide removal tower 4 is provided between the regeneration tower 11 and the flue gas purification tower 2. A decarbonizer recovery tower 5 is provided above the carbon dioxide removal tower 4. The acid gas treatment component includes an acid gas condenser 14 and an acid gas extraction device 16 connected to the rear end of the acid gas condenser 14. The acid gas condenser 14 is connected to the flue gas purification tower 2 and the regeneration tower 11. The heat exchange component includes a lean and rich liquid heat exchanger 8 located between the regeneration tower 11 and the carbon dioxide removal tower 4, which is used to exchange heat between the rich liquid discharged from the carbon dioxide removal tower 4 and the lean liquid discharged from the regeneration tower 11. By utilizing the solutions of different temperatures generated by the system itself for heat exchange, the amount of heat exchange medium used is reduced, thereby achieving the purpose of reducing costs.

[0042] Please refer to Figure 1-Figure 2 In order to further improve the utilization of flue gas heat and reduce energy waste, in some embodiments, It also includes a flue gas diversion device and a bag dust collector. The bag dust collector is located between the flue gas diversion device and the carbon dioxide purification tower. A flue gas mixer is provided between the flue gas diversion device and the bag dust collector. The heat exchange component also includes a rich liquid reheater 10. The rich liquid reheater 10 is connected to the flue gas diversion device and the flue gas mixer respectively. The rich liquid reheater 10 is used to heat the rich liquid discharged from the carbon dioxide removal tower 4 and passed through the lean-rich liquid heat exchanger 8. That is to say, by diverting the flue gas, a part of the flue gas is used as the heat source medium of the lean-rich liquid heat exchanger 8 to heat the rich liquid discharged from the carbon dioxide removal tower 4, thereby further improving the utilization effect of thermal energy and reducing energy loss. At the same time, the flue gas used as the heat source medium is fully mixed with the other part of the diverted flue gas in the flue gas mixer after heat exchange. After mixing, the flue gas temperature can be reduced by about 30°C, which reduces the temperature of the flue gas entering the bag dust collector, reduces the loss to the bag dust collector, and also realizes the comprehensive utilization of heat in the exhaust gas.

[0043] Optionally, in order to further enhance the control of the heat exchange flue gas, in some embodiments, the flue gas diversion device includes a solenoid valve for controlling the flow of the diverted flue gas, thereby controlling the heat exchange efficiency of the lean-rich liquid heat exchanger 8.

[0044] Optionally, in order to further improve the efficiency of flue gas mixing, in some embodiments, a stirring device is provided in the flue gas mixer, including a main shaft and several mixing plates mounted on the main shaft. The main shaft is driven to rotate by a motor, so that the several mixing plates can quickly mix the flue gas, thereby improving the mixing efficiency of the flue gas.

[0045] Optionally, in order to further accelerate the mixing of the flue gas, in some embodiments, the two inlets of the flue gas entering the flue gas mixer after diversion are arranged relative to each other, so that the flue gas entering from the two inlets collide with each other, which is conducive to accelerating the mixing of the flue gas.

[0046] The flue gas purification tower 2 is used to cool the flue gas, remove dust, remove acidic gases, and remove mist. In some embodiments, the flue gas purification tower 2 includes at least two levels of washing to ensure sufficient cooling, dust removal, removal of acidic gases, and demisting of the flue gas.

[0047] Optionally, in some embodiments, the first stage washing of the flue gas purification tower 2 uses alkaline solution to remove acid mist in the flue gas and reduce temperature and remove dust, and the second stage washing of the flue gas purification tower 2 uses desalted water to further remove dust and mist.

[0048] The purified flue gas after passing through the above-mentioned flue gas purification tower 2 enters the carbon dioxide removal tower 4, in which an organic amine solution is used to selectively absorb and remove carbon dioxide in the flue gas. After removal, the flue gas is demisted and then enters the flue gas decarbonizer recovery device. The purified flue gas washed and removed by the recovery device is demisted and then discharged.

[0049] Please refer to Figure 1-Figure 2 In order to reduce the cost of system maintenance, in some embodiments, a decarbonizer recovery tower 5 is set up to recover and reuse the decarbonizer. The decarbonizer recovery tower 5 includes a wire mesh capture device for capturing the decarbonizer entrained in the flue gas. Most of the decarbonizer entrained in the flue gas is captured by the wire mesh capture device through droplet condensation and returned to the carbon dioxide removal tower 4 to achieve the purpose of reuse, thereby reducing the cost of system maintenance. It also includes a recovery liquid tank 6 for washing the flue gas and de-atomizing the washed flue gas before discharging it. The flue gas is contact-washed in the recovery liquid tank 6 and the washed flue gas is de-atomized and discharged.

[0050] Optionally, the washing solution in the recovery tank 6 is desalted water, and the washing solution is recycled. When the concentration of the decarbonizing agent in the washing solution reaches a certain concentration, it is sent to the carbon dioxide removal tower 4 to further improve the effect of reusing the decarbonizing agent.

[0051] In some embodiments, the heat exchange component also includes a rich liquid reheater 10 and an acid gas heat exchanger 13. The rich liquid reheater 10 is connected to the rich liquid reheater 10 and is located between the lean and rich liquid heat exchanger 8 and the regeneration tower 11. That is, a portion of the flue gas passing through the flue gas diversion device flows through the rich liquid reheater 10 to heat the rich liquid and exchange heat with this portion of the flue gas at the same time. After heat exchange, part of the flue gas is sent into the flue gas mixer for mixing to cool down the other part of the flue gas, thereby making full use of the flue gas preheating and reducing energy loss.

[0052] In some embodiments, a rich liquid tank 7 is provided between the carbon dioxide removal tower 4 and the regeneration tower 11. The rich liquid tank 7 is provided with two outlets. One of the outlets of the rich liquid tank 7 is connected to the regeneration tower 11 after passing through the lean and rich liquid heat exchanger 8 and the rich liquid reheater 10 in sequence, and the other outlet of the rich liquid tank 7 is connected to the regeneration tower 11 through the rich liquid acid gas heat exchanger 13.

[0053] In the regeneration tower 11, the high-temperature rich liquid that has passed through the rich liquid reheater 10 is fed into the regeneration tower 11 and is flashed in the regeneration tower 11. The flashed high-temperature gas flows upward along the regeneration tower 11, and the flashed rich liquid flows downward into the reboiler 12, where it is heated with the high-temperature acid gas from the acid gas heat exchanger 13 to desorb carbon dioxide. The desorbed acid gas flows toward the top of the regeneration tower 11 together with the acid gas from the bottom of the tower. The rich liquid heated in the tower is further fed into the reboiler 12 for deep heating and desorption. The desorbed vapor-liquid mixture flows into the bottom of the regeneration tower 11, and the high-temperature acid gas is separated into gas and liquid in the bottom of the tower. The high-temperature acid gas flows to the top of the tower through the gas riser. The high-temperature lean liquid in the regeneration tower 11 is pumped into the lean-rich liquid heat exchanger 8 for heat exchange with the rich liquid flowing through, again making full use of the system's own heat for exchange, greatly reducing the demand for external heat and reducing the cost required for the system.

[0054] In some embodiments, the acid gas treatment assembly further includes a gas-liquid separator 15 and an acid gas dehydration device 3 . The gas-liquid separator 15 is located between the acid gas cooler and the acid gas extraction device 16 . The acid gas dehydration device 3 is connected to the acid gas extraction device 16 .

[0055] Specifically, another stream of rich liquid from the rich liquid tank 7 is mixed with the condensate from the acid gas condenser 14 and then fed into the acid gas heat exchanger 13. The rich liquid after heat exchange is fed into the regeneration tower 11 to cool the high-temperature acid gas from the bottom of the tower. The heated rich liquid flows into the reboiler 12 in the regeneration tower 11, and the cooled acid gas is fed into the acid gas heat exchanger 13 for cooling. The cooled acid gas is further fed into the gas-liquid separator 15. The carbon dioxide acid gas after gas-liquid separation is fed into the dryer through the exhaust device for further dehydration.

[0056] Optionally, in some embodiments, the condensate from the acid gas condenser 14 is mixed with the rich liquid before being sent to the reboiler 12 .

[0057] Among them, high-temperature flue gas with a temperature of 260°C is used, and water-based medium is used for heat exchange. After heat exchange, a high-temperature liquid of about 150°C is obtained. After the flue gas after heat exchange is mixed with the original flue gas purification, the temperature of the mixed flue gas can be reduced by 45°C. The flue gas entering the flue gas purification tower 2 after dust removal is at 110~150°C. The flue gas temperature after cooling, dust removal and acid removal is about 40~60°C. The temperature of the lean liquid entering the decarbonization absorption tower is 35~55°C. The enriched carbon dioxide obtained after removing carbon dioxide is The temperature of the rich liquid of carbon is 35~50°C, the temperature of the rich liquid after heat exchange in the lean-rich liquid heat exchanger 8 is 75~85°C, the temperature of the lean liquid after heat exchange in the lean-rich liquid heat exchanger 8 is 60~70°C, the temperature of the lean liquid after heat exchange in the lean-rich liquid heat exchanger 8 is 35~55°C, the pressure at the top of the regeneration tower 11 is 0~20Kpa, the temperature of the acid gas at the top is 90~100°C, the temperature of the rich liquid after heat exchange in the heat exchanger is 80~90°C, and the temperature of the acid gas after cooling in the acid gas condenser 14 is less than 40°C.

[0058] That is to say, the focus of the present invention is that the treated flue gas is first pressurized by the booster fan 1 to increase the air pressure of the entire capture system, which is beneficial to the reaction and capture of carbon dioxide. A carbon dioxide removal tower 4 is provided between the regeneration tower 11 and the flue gas purification tower 2, and a decarbonizer recovery tower 5 is provided above the carbon dioxide removal tower 4. The acid gas treatment component includes an acid gas condenser 14 and an acid gas extraction device 16 connected to the rear end of the acid gas condenser 14. The acid gas condenser 14 is connected to the flue gas purification tower 2 and the regeneration tower 11. The heat exchange component includes a lean and rich liquid heat exchanger 8 located between the regeneration tower 11 and the carbon dioxide removal tower 4, which is used to exchange heat between the rich liquid discharged from the carbon dioxide removal tower 4 and the lean liquid discharged from the regeneration tower 11. By utilizing the solutions of different temperatures generated by the system itself for heat exchange, the amount of heat exchange medium used is reduced, thereby achieving the purpose of reducing costs.

[0059] The various embodiments in this specification are described in a progressive manner, and each embodiment focuses on the differences from other embodiments. The same or similar parts between the various embodiments can be referenced to each other.

[0060] The above describes in detail the rotary kiln flue gas carbon dioxide capture system provided by the present invention. This article uses specific examples to illustrate the principles and implementation methods of the present invention. The description of the above examples is intended only to facilitate understanding of the method and core concept of the present invention. It should be noted that those skilled in the art may make various improvements and modifications to the present invention without departing from the principles of the present invention, and such improvements and modifications also fall within the scope of protection of the claims of the present invention.

Claims

1. A rotary kiln flue gas carbon dioxide capture system, characterized in that: include: A flue gas purification tower (2), wherein a booster fan (1) is provided at the front end of the flue gas purification tower (2); A regeneration tower (11), wherein a carbon dioxide removal tower (4) is provided between the regeneration tower (11) and the flue gas purification tower (2), and a decarbonizing agent recovery tower (5) is provided above the carbon dioxide removal tower (4); an acid gas treatment component, the acid gas treatment component comprising an acid gas condenser (14), an acid gas extraction device (16) connected to the rear end of the acid gas condenser (14), the acid gas condenser (14) being connected to the flue gas purification tower (2) and the regeneration tower (11); A heat exchange component, comprising a lean-rich liquid heat exchanger (8) located between the regeneration tower (11) and the carbon dioxide removal tower (4), for exchanging heat between the rich liquid discharged from the carbon dioxide removal tower (4) and the lean liquid discharged from the regeneration tower (11).

2. A rotary kiln flue gas carbon dioxide capture system according to claim 1, characterized in that: Also includes: A flue gas diversion device and a bag dust collector, wherein the bag dust collector is located between the flue gas diversion device and the flue gas purification tower (2), and a flue gas mixer is provided between the flue gas diversion device and the bag dust collector; The heat exchange assembly further comprises a rich liquid reheater (10), the rich liquid reheater (10) being connected to the flue gas diversion device and the flue gas mixer, respectively, and the rich liquid reheater (10) being used to heat the rich liquid discharged from the carbon dioxide removal tower (4) and passing through the lean-rich liquid heat exchanger (8).

3. A rotary kiln flue gas carbon dioxide capture system according to claim 2, characterized in that: The flue gas first enters the lime rotary kiln preheater for heat exchange before entering the flue gas diversion device.

4. A rotary kiln flue gas carbon dioxide capture system according to claim 2, characterized in that: The flue gas purification tower (2) includes at least two levels of scrubbing.

5. The rotary kiln flue gas carbon dioxide capture system according to claim 3, characterized in that: The first stage of washing of the flue gas purification tower (2) uses alkaline solution, and the second stage of washing of the flue gas purification tower (2) uses desalted water.

6. The rotary kiln flue gas carbon dioxide capture system according to claim 1, characterized in that: The decarbonizing agent recovery tower (5) comprises: Wire mesh capture device, used to capture the decarbonizer entrained in the flue gas; The recovery liquid tank (6) is used to wash the flue gas and discharge the washed flue gas after de-atomization.

7. A rotary kiln flue gas carbon dioxide capture system according to claim 6, characterized in that: The washing solution in the recovery tank (6) is desalted water.

8. The rotary kiln flue gas carbon dioxide capture system according to claim 2, characterized in that: The heat exchange component further includes: an acid gas heat exchanger (13), the rich liquid reheater (10) being connected to the rich liquid reheater (10) and being located between the lean and rich liquid heat exchanger (8) and the regeneration tower (11); a reboiler (12), the reboiler (12) being connected to the rich liquid outlet of the regeneration tower (11); The lean liquid recooler (9) is used to cool the lean liquid that has passed through the lean-rich liquid heat exchanger (8) again.

9. A rotary kiln flue gas carbon dioxide capture system according to claim 8, characterized in that: The acid gas treatment assembly further comprises: a gas-liquid separator (15), the gas-liquid separator (15) being located between the acid gas cooler and the acid gas extraction device (16); An acid gas dehydration device (3), wherein the acid gas dehydration device (3) is connected to the acid gas extraction device (16).

10. A rotary kiln flue gas carbon dioxide capture system according to claim 9, characterized in that: A rich liquid tank (7) is provided between the carbon dioxide removal tower (4) and the regeneration tower (11). The rich liquid tank (7) is provided with two outlets. One outlet of the rich liquid tank (7) is connected to the regeneration tower (11) after passing through the lean and rich liquid heat exchanger (8) and the rich liquid reheater (10) in sequence, and the other outlet of the rich liquid tank (7) is connected to the regeneration tower (11) through the rich liquid acid gas heat exchanger (13).

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