Enhanced carbon dioxide trapping system

Abstract

The utility model provides an enhanced carbon dioxide trapping system which comprises a multi-stage enhanced reaction tower, and the multi-stage enhanced reaction tower is provided with a flue gas pipeline, a pregnant solution feed port and a discharge port; a strengthening unit is arranged in the multi-stage strengthening reaction tower, a circulating pipeline is further arranged on the outer side of the multi-stage strengthening reaction tower, and a circulating pump and a flow control valve are sequentially arranged on the circulating pipeline. According to the enhanced carbon dioxide capture system disclosed by the utility model, the CO2 existing in the flue gas can be efficiently captured in a manner of combining the multi-stage enhanced reaction tower and the circulating pipeline, meanwhile, the regeneration energy consumption is greatly reduced, and the CO2 absorption rate can be well improved.

Description

TECHNICAL FIELD

[0001] The utility model belongs to flue gas purification technical field, concretely relates to a kind of enhanced carbon dioxide capture system. BACKGROUND

[0002] In the field of carbon capture, decarbonization technology is widely used. Today, carbon capture technology is used to capture and store carbon dioxide, effectively reducing the concentration of carbon dioxide in the atmosphere, thereby combating climate change. Direct capture of carbon dioxide can substantially reduce the concentration of carbon dioxide in the atmosphere to form negative emissions, reduce greenhouse gas emissions, and promote energy transformation and sustainable development. Therefore, achieving negative emissions of carbon is a very critical technology.

[0003] However, current carbon capture technologies are mostly high in cost, including the expense of building and operating carbon capture facilities, and the process of carbon capture itself requires a large amount of energy, especially when using chemical absorption method, which requires a large amount of energy to provide heat and pressure. Despite this, the capture efficiency is limited when a large amount of energy is consumed to capture carbon dioxide. Most current carbon capture methods have low capture efficiency. Therefore, how to achieve efficient capture of carbon dioxide while reducing the energy consumption of the decarbonization process is the key to carbon capture technology.

[0004] Therefore, the present utility model is proposed. SUMMARY

[0005] The first purpose of the present utility model is to provide an enhanced carbon dioxide capture system that can efficiently capture CO2 in flue gas while significantly reducing regeneration energy consumption and improve CO2 absorption rate by setting up multiple enhanced reaction towers and a combination of circulating pipelines.

[0006] To achieve the above-mentioned purposes of the present utility model, the following technical solutions are adopted:

[0007] An enhanced carbon dioxide capture system includes multiple enhanced reaction towers, a flue gas pipeline, a rich liquid feed inlet, and a discharge outlet. The multiple enhanced reaction towers are provided with an enhanced unit, and the outside of the multiple enhanced reaction towers is further provided with a circulating pipeline. The circulating pipeline is sequentially provided with a circulating pump and a flow control valve.

[0008] In the system, the multi-stage intensified reaction tower is used to realize intensified capture of carbon dioxide, the intensified unit is arranged in the tower of the multi-stage intensified reaction tower, so that the load of the reaction liquid flowing into the reaction tower is improved, the gas-liquid phase mass transfer process is effectively promoted, the removal rate of CO2 in flue gas is improved, the reaction liquid flowing into the top of the intensified reaction tower is input into the tower top again from the tower bottom through the circulation pipeline, the reaction time of the reaction liquid in the intensified reaction tower is increased, the removal rate of CO2 in flue gas is further improved, and the flow control valve is arranged on the circulation pipeline to control the flow of the rich liquid flowing into the intensified reaction tower, so that the removal of carbon dioxide in flue gas can achieve excellent effect when the reaction liquid flows into the intensified reaction tower, because in order to realize intensified absorption of carbon dioxide, the almost saturated rich liquid and flue gas need to flow into the intensified reaction tower at a certain flow rate, the flue gas is broken into micro-bubbles after being treated by the intensified unit, the flue gas broken into micro-bubbles forms a stable gas-liquid mixture with the rich liquid, the load of the reaction liquid is greatly improved in this way, and the removal of CO2 is improved, if the flow rate is too low, the reaction system in the intensified reaction tower is saturated too early, and the capture of carbon dioxide in flue gas is affected, and if the flow rate is too high, the load in the reaction liquid is too low, the reaction liquid cannot absorb carbon dioxide in flue gas, and then the removal effect of carbon dioxide is affected. 3 / h-8m 3 / h, so that the removal of carbon dioxide in flue gas can achieve excellent effect when the reaction liquid flows into the intensified reaction tower, because in order to realize intensified absorption of carbon dioxide, the almost saturated rich liquid and flue gas need to flow into the intensified reaction tower at a certain flow rate, the flue gas is broken into micro-bubbles after being treated by the intensified unit, the flue gas broken into micro-bubbles forms a stable gas-liquid mixture with the rich liquid, the load of the reaction liquid is greatly improved in this way, and the removal of CO2 is improved, if the flow rate is too low, the reaction system in the intensified reaction tower is saturated too early, and the capture of carbon dioxide in flue gas is affected, and if the flow rate is too high, the load in the reaction liquid is too low, the reaction liquid cannot absorb carbon dioxide in flue gas, and then the removal effect of carbon dioxide is affected.

[0009] Preferably, as a further implementable scheme, the multi-stage intensified reaction tower is a two-stage intensified reaction tower, wherein the two-stage intensified reaction tower comprises a first-stage intensified reaction tower and a second-stage intensified reaction tower.

[0010] Preferably, as a further implementable scheme, the first-stage intensified reaction tower is provided with a first intensified unit at the top, and a disc-shaped guide pipe is arranged below the first intensified unit; the rich liquid feeding port and the flue gas pipeline are sequentially arranged at the top of the first-stage intensified reaction tower, and a discharge port and a circulation feeding port are arranged on the two sides of the first-stage intensified reaction tower.

[0011] The utility model discloses a reinforced carbon dioxide capture system, which comprises a first reinforced reaction tower and a second reinforced reaction tower.

[0012] Preferably, as a further implementable solution, the circulation pipeline is arranged outside the first reinforced reaction tower, and the circulation pump is connected to the circulation feed port.

[0013] In the utility model, the first reinforced reaction tower and the circulation pipeline are combined, so that the reaction liquid can flow into the top of the reinforced reaction tower, the reaction time of the reaction liquid in the reinforced reaction tower is increased by the disc-shaped conduit, and the reaction liquid can reach the bottom of the reinforced reaction tower from top to bottom. Then, the reaction liquid reaching the bottom is introduced from the top of the reaction tower again through the treatment of the circulation pipeline, the reaction time of the reaction liquid is further increased, the decarburization reaction is more complete, and the removal of carbon dioxide in flue gas is further improved. In the utility model, the reaction liquid is introduced from the top of the reinforced reaction tower, so that the reaction liquid moves from top to bottom in the reaction tower. When the reaction liquid drops to the bottom of the reaction tower, its speed decreases until it stops. Since the reaction liquid moves from top to bottom, the gas phase in the reaction liquid gradually rises in the liquid phase under the influence of buoyancy. The speed of the gas phase gradually decreases during the rising process. The gas phase stays in the liquid phase for a longer time through such an arrangement, the removal of carbon dioxide is improved, and the combination of the disc-shaped conduit and the circulation pipeline greatly increases the residence time of the gas phase in the liquid phase, so that the decarburization reaction is more complete and the removal of carbon dioxide is further improved.

[0014] Preferably, as a further implementable scheme, the second stage enhanced reaction tower is provided with flue gas pipelines at the top and the bottom, and is provided with super-saturated rich liquid feeding ports and super-saturated rich liquid discharging ports at two sides respectively, the super-saturated rich liquid feeding ports and the discharging ports are connected; a second enhancement unit is arranged at the bottom of the second stage enhanced reaction tower, and the second enhancement unit is connected with the super-saturated rich liquid feeding ports.

[0015] In the utility model, the second stage enhanced reaction tower is arranged to realize preliminary gas-liquid separation, and the second enhancement unit is arranged at the bottom of the second stage enhanced reaction tower, so that the introduced saturated rich liquid can further absorb carbon dioxide in flue gas, because the second enhancement unit can improve the load of the saturated rich liquid, and the flue gas with high carbon dioxide concentration can make the saturated rich liquid break through the bottleneck and further absorb carbon dioxide in flue gas, thereby improving the absorption effect of carbon dioxide, and in the second stage enhanced reaction tower, the saturated rich liquid and high-concentration flue gas are introduced from the bottom of the second stage enhanced reaction tower, and a stable gas-liquid mixture is formed after being treated by the second enhancement unit, at this time, the gas-liquid mixture moves from bottom to top in the second stage enhanced reaction tower, and the flue gas after decarbonization can be discharged through the flue gas pipeline at the top of the second stage enhanced reaction tower, thereby achieving preliminary gas-liquid separation effect.

[0016] Preferably, as a further implementable scheme, the absorption tower is further provided with a flow control valve between the absorption tower and the rich liquid feeding port, so as to control the flow rate of the rich liquid flowing into the enhanced reaction tower.

[0017] Preferably, as a further implementable scheme, the absorption tower is further provided with a flow control valve between the absorption tower and the rich liquid feeding port, so as to control the flow rate of the rich liquid flowing into the enhanced reaction tower.

[0018] Preferably, as a further implementable scheme, the absorption tower is further provided with a flow control valve between the absorption tower and the rich liquid feeding port, so as to control the flow rate of the rich liquid flowing into the enhanced reaction tower.

[0019] This invention primarily utilizes an absorption tower for the initial removal of carbon dioxide from flue gas. The absorbent is stored in an connected absorbent storage tank. During flue gas removal, the absorbent flows out of the storage tank and then into the absorbent inlet at the top of the absorption tower, where a flow control valve regulates its flow rate to ensure a complete reaction. Upon entering the absorption tower, the absorbent mixes with the decarbonized flue gas entering through the flue gas pipeline, producing a rich liquid. The initially decarbonized flue gas is discharged from the flue gas outlet at the top of the absorption tower, while the rich liquid flows into the first-stage enhanced reaction tower via a flow control valve. The amount of rich liquor allows for better removal of carbon dioxide from the flue gas. After entering the first-stage enhanced reaction tower through the feed inlet, it mixes with the flue gas entering through the flue gas duct at the top of the first-stage enhanced reaction tower. After being processed by the first enhanced unit, a stable gas-liquid mixture is formed for further decarbonization reaction. After the reaction is complete, saturated rich liquor is obtained. Subsequently, the saturated rich liquor flows into the second-stage enhanced reaction tower through the discharge port on the side of the first-stage enhanced reaction tower. It mixes with the flue gas entering through the flue gas duct at the bottom of the second-stage enhanced reaction tower. After being processed by the second-stage enhanced unit, a stable gas-liquid mixture is obtained, further improving the removal of carbon dioxide from the flue gas and thus obtaining supersaturated rich liquor.

[0020] Preferably, as a further feasible option, it also includes a heat exchanger, a gas-liquid separator, and a regeneration tower connected in sequence, wherein the gas-liquid separator is connected to the second-stage enhanced reaction tower; an interstage heating unit and a heat exchanger are respectively provided on both sides of the regeneration tower, and a regeneration gas cooler and a gas-liquid separator are also provided in sequence at the top of the regeneration tower, and a reboiler is connected to the bottom of the regeneration tower.

[0021] After decarbonization, the resulting gas-liquid emulsion flows out through the supersaturated rich liquid outlet on the side of the second-stage enhanced reaction tower and into the connected gas-liquid separator for gas-liquid separation. The gas is then discharged from the top of the gas-liquid separator, while the separated liquid flows into a heat exchanger for lean and rich liquid heat exchange. When the lean liquid is heated to 40°C by the heat exchanger, it is circulated to the absorbent storage tank for circulation. The rich liquid is then fed into the regeneration tower for regeneration. The regeneration tower heats the incoming rich liquid through the regeneration tower heating unit and reboiler on the outside, causing a large amount of CO2 to be released. The CO2 is then transported to the regeneration gas cooler at the top of the regeneration tower for cooling, and then separated into gas and liquid by the gas-liquid separator to obtain high-purity CO2.

[0022] Compared with the prior art, the beneficial effects of this utility model are as follows:

[0023] (1) The present invention provides an enhanced carbon dioxide capture system. The enhanced carbon dioxide capture system can efficiently capture CO2 in flue gas while significantly reducing regeneration energy consumption and greatly improving CO2 absorption rate by setting up multi-stage enhanced reaction towers and circulation pipelines. Attached Figure Description

[0024] Various other advantages and benefits will become apparent to those skilled in the art upon reading the following detailed description of preferred embodiments. The accompanying drawings are for illustrative purposes only and are not intended to limit the scope of the invention. Furthermore, the same reference numerals denote the same parts throughout the drawings. In the drawings:

[0025] Figure 1 This is a structural diagram of an enhanced carbon dioxide capture system provided by the present invention;

[0026] Figure 2 This is a schematic flowchart of the CO2 absorption method for flue gas provided by this utility model.

[0027] The attached diagram lists the components represented by each number as follows:

[0028] 1. First-stage enhanced reaction tower; 2. Second-stage enhanced reaction tower; 3. First enhanced unit; 4. Second enhanced unit; 5. Flue gas duct; 6. Rich liquor inlet; 7. Flow control valve 1; 8. Circulating pump; 9. Circulating inlet; 10. Flow control valve 2; 11. Discharge port; 12. Flue gas duct; 13. Supersaturated rich liquor discharge port; 14. Gas-liquid separator 1; 15. Heat exchanger; 16. Flow control valve 3; 17. Absorbent tower; 18. Absorbent storage tank; 19. Regeneration tower; 20. Interstage heating unit; 21. Gas-liquid separator 2; 22. Regenerated gas cooler; 23. Reboiler. Detailed Implementation

[0029] The technical solution of this utility model will be clearly and completely described below with reference to the accompanying drawings and specific embodiments. However, those skilled in the art will understand that the embodiments described below are only some embodiments of this utility model, not all embodiments, and are only used to illustrate this utility model, and should not be regarded as limiting the scope of this utility model. Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are within the protection scope of this utility model. Where specific conditions are not specified in the embodiments, conventional conditions or conditions recommended by the manufacturer shall be followed. Where the manufacturers of reagents or instruments are not specified, they are all conventional products that can be purchased commercially.

[0030] In the description of this utility model, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," etc., indicating the orientation or positional relationship, are based on the orientation or positional relationship shown in the accompanying drawings and are only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0031] In the description of this utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.

[0032] To more clearly illustrate the technical solution of this utility model, the following description is provided in the form of specific embodiments.

[0033] Example 1

[0034] Please see Figure 1 As shown, this utility model is an enhanced carbon dioxide capture system, including: 1. a first-stage enhanced reaction tower; 2. a second-stage enhanced reaction tower; 3. a first enhanced unit; 4. a second enhanced unit; 5. a flue gas duct; 6. a rich liquor inlet; 7. a flow control valve 1; 8. a circulating pump; 9. a circulating inlet; 10. a flow control valve 2; 11. a discharge port; 12. a flue gas duct; 13. a supersaturated rich liquor discharge port; 14. a gas-liquid separator 1; 15. a heat exchanger; 16. a flow control valve 3; 17. an absorption tower; 18. an absorbent storage tank; 19. a regeneration tower; 20. an interstage heating unit; 21. a gas-liquid separator 2; 22. a regenerated gas cooler; and 23. a reboiler.

[0035] In this embodiment, the flue gas used is the flue gas produced by coal-fired power plants and chemical industries. The pretreatment feed gas conditions are set as follows: pressure 0.11MPa, temperature 40℃, and the composition distribution of the flue gas is 5% H2O, 10.2% CO2, 79.8% N2, and 5% O2.

[0036] The absorbent in the absorbent storage tank 18 is formulated as amine-water, consisting of 30wt% 2-(dimethylamino)ethanol (DMAE) and 70wt% H2O;

[0037] See Figure 2 The specific carbon dioxide capture process is as follows: the absorbent is introduced into the absorbent storage tank 18, and then the absorbent flows into the absorption tower 17 from the absorbent inlet at the top of the absorption tower 17 through the absorbent storage tank 18. When the absorbent flows into the absorption tower 17, the flow control valve 3 16 causes the absorbent to flow at a rate of 2m³ / min. 3 A flow rate of / h flows into the absorption tower 17, and at the same time, flue gas is introduced into the absorption tower 17 from the flue gas feed pipe set at the bottom of the absorption tower 17. After the absorbent and flue gas undergo a preliminary decarbonization reaction in the absorption tower 17, the preliminarily decarbonized flue gas is discharged from the flue gas outlet set at the top of the absorption tower 17, while the resulting rich liquid flows out from the absorption tower 17 and flows into the first-stage enhanced reaction tower 1 through the rich liquid feed port 6 set at the top of the first-stage enhanced reaction tower. A new round of flue gas is also introduced from the flue gas pipe set at the top of the first-stage enhanced reaction tower 1 and is introduced into the first enhanced unit 3 together with the rich liquid. After being processed by the first enhanced unit 3, the rich liquid and flue gas can form a stable gas-liquid mixture for further decarbonization reaction. Then, it gradually descends from top to bottom to the bottom of the first-stage enhanced reaction tower 1 through the disc-shaped conduit set below the first enhanced unit 3. Then, the circulating pump 8 sucks out the reaction liquid inside the first-stage enhanced reaction tower 1 and then enters the first-stage enhanced reaction tower 1 again from the circulating feed port 9 set at the top of the first-stage enhanced reaction tower 1.

[0038] The saturated rich liquor will flow out from the discharge port 11 set on the side of the first-stage enhanced reaction tower 2, and then flow into the second-stage enhanced reaction tower 2. At the same time, a new round of flue gas will also be introduced from the flue gas pipe 12 set at the bottom of the second-stage enhanced reaction tower 2, and together with the saturated rich liquor, it will be introduced into the second enhanced unit 4. After being processed by the second enhanced unit 4, the saturated rich liquor and flue gas form a stable gas-liquid mixture for further decarbonization reaction. Then, the decarbonized flue gas will be discharged from the top of the second-stage enhanced reaction tower 2, and the supersaturated rich liquor will flow out from the supersaturated rich liquor discharge port 13 set on the side of the second-stage enhanced reaction tower 2.

[0039] The supersaturated rich liquid then flows into the gas-liquid separator 14 for gas-liquid separation. Due to gravity, the supersaturated rich liquid in the separator 14 undergoes natural gas-liquid separation. The separated gas is discharged from the top of the separator 14, while the separated liquid flows into the heat exchanger 15 for heat exchange. After heat exchange, the lean liquid flows from the top of the heat exchanger through the top of the absorbent storage tank into the absorbent storage tank for recycling. The rich liquid flows from the heat exchanger 15 into the regeneration tower 19. The interstage heating unit 20 and reboiler 23 installed on the outside of 19 heat the liquid flowing into the regeneration tower, thereby releasing a large amount of CO2 in the liquid. The released CO2 is sent to the top of the regeneration tower and transported to the regeneration gas cooler for cooling. After cooling, it passes through the gas-liquid separator 21 again to achieve gas-liquid separation. The high-purity CO2 obtained after separation is discharged from the top of the gas-liquid separator 21, and the liquid flows back into the regeneration tower 19 from the bottom of the gas-liquid separator 21 for circulating heating.

[0040] Comparative Example 1

[0041] The specific implementation method is the same as in Example 1, except that the disc-shaped conduit is not provided.

[0042] Comparative Example 2

[0043] The specific implementation method is the same as in Example 1, except that the first intensifier unit is not used, and instead the disc-shaped duct is connected to the flue gas duct and the rich liquid inlet.

[0044] Comparative Example 3

[0045] The specific implementation method is the same as in Example 1, except that a circulation pipe is not used.

[0046] Comparative Example 4

[0047] The specific implementation method is the same as in Example 1, except that the second intensifying unit is not used.

[0048] Comparative Example 5

[0049] The specific implementation method is the same as in Example 1, except that the flow control valve 8 is not used.

[0050] Experimental Example 1: CO2 Load and Regeneration Energy Consumption Measurement

[0051] The supersaturated rich solutions obtained after treatment according to Example 1 and Comparative Examples 1-5 were titrated to determine the final CO2 absorption load. The specific determination method is as follows:

[0052] Detection steps: Take 1g of supersaturated rich solution and add it to 30g of water for absorption. Add the diluted solution to a closed reactor connected to the gas measuring tube. Add dilute sulfuric acid to the reactor to release the absorbed CO2 from the liquid phase. Measure the change in the total gas volume in the gas measuring tube and use the formula to determine the total CO2 load 'a'.

[0053] The calculation formula is as follows:

[0054]

[0055] In the formula, a is the carbon dioxide load (mol / kg), and mabs is the sample mass of the absorbent (kg). and These represent the volume changes in the trachea and the acid burette, respectively.

[0056] The above-mentioned test methods are not only applicable to the CO2 absorption process, but also to the determination of CO2 regeneration energy consumption. The regeneration test is carried out in a pilot-scale equipment and measured with an electric meter. The measured energy consumption consists of three parts: reaction heat, sensible heat used for solution heating, and evaporation heat used for water evaporation.

[0057] Testing steps: The regeneration temperature is maintained at 373.15 K, the liquid flow rate is 0 to 100 mL / min, and the gas flow rate is 0 to 30 L / min; the regeneration energy consumption is measured using an electricity meter.

[0058] The final measurement results are shown in Table 1 below:

[0059]

[0060] As shown in Table 1 above, the enhanced carbon dioxide capture system and decarbonization method provided by this utility model, by setting up a multi-stage enhanced reaction tower and installing an enhanced unit inside the multi-stage enhanced reaction tower, increases the load of the reaction liquid entering the reaction tower, which can effectively promote the gas-liquid phase mass transfer process, improve the CO2 removal rate in flue gas, reduce regeneration energy consumption, and realize the deflection of the reaction liquid through the external circulation pipe, so that the reaction liquid entering from the top of the enhanced reaction tower can be reintroduced from the bottom of the tower to the top of the tower through the circulation pipe when it reaches the bottom of the tower, thereby greatly increasing the residence time of the reaction liquid in the enhanced reaction tower and further improving the CO2 removal rate in flue gas.

[0061] By comparing Example 1 and Comparative Example 1, it can be seen that the disc-shaped conduit is necessary for this invention. This is because placing the disc-shaped conduit below the first intensifier unit further increases the residence time of the reaction liquid in the first-stage intensifier reaction tower. During the downward flow of the reaction liquid, its descent speed gradually decreases until it stops after reaching the bottom of the reactor, while the gas phase in the reaction liquid gradually rises in the liquid phase due to buoyancy. By setting up the disc-shaped conduit, the residence time of the gas phase in the liquid phase can be extended, thereby further improving the removal of carbon dioxide from the flue gas.

[0062] Comparing Example 1 and Comparative Example 2, it can be seen that the setting of the first intensifier unit is very necessary for this utility model. This is because by setting the first intensifier unit inside the first-stage intensifier reaction tower, the flue gas is broken into microbubbles and mixed with rich liquid to form a stable gas-liquid mixture. The treated gas-liquid mixture, i.e. the reaction liquid, has a high loading capacity, which enhances the reaction liquid's ability to capture carbon dioxide in the flue gas, effectively promotes the gas-liquid phase mass transfer process, and improves the CO2 removal rate in the flue gas.

[0063] Comparing Example 1 and Comparative Example 3, it can be seen that the setting of the circulation pipeline is very important for this utility model. This is because this utility model mainly uses the combination of the first-stage enhanced reaction tower and the circulation pipeline to allow the reaction liquid to flow in from the top of the enhanced reaction tower. The conduit increases the residence time of the reaction liquid in the enhanced reaction tower and allows the reaction liquid to reach the bottom of the enhanced reaction tower from top to bottom. Then, the reaction liquid that has reached the bottom is introduced back from the top of the reaction tower through the circulation pipeline, further increasing the residence time of the reaction liquid, making the decarbonization reaction more complete and thorough, and further improving the removal of carbon dioxide from the flue gas. This invention introduces the reaction liquid from the top of the enhanced reaction tower, allowing it to move downwards within the tower. As the reaction liquid descends to the bottom, its velocity decreases until it stops. Because the reaction liquid moves downwards, the gas phase within it is affected by buoyancy and gradually rises in the liquid phase. During this rise, the gas velocity gradually decreases. This design also increases the residence time of the gas phase in the liquid phase, further improving the carbon dioxide removal effect. Therefore, this invention, through the combination of a disc-shaped conduit and a circulation pipe, greatly increases the residence time of the gas phase in the liquid phase, making the decarbonization reaction more complete and further enhancing the carbon dioxide removal effect.

[0064] Comparing Example 1 and Comparative Example 4, it can be seen that the second intensifier unit can further absorb carbon dioxide in the flue gas for this invention. This is because the second intensifier unit can effectively increase the load in the supersaturated rich liquid. With the flue gas having a high carbon dioxide concentration, the supersaturated rich liquid can break through the bottleneck and absorb carbon dioxide in the flue gas again, achieving a highly efficient carbon dioxide absorption effect. In the second-stage intensifier tower, this invention introduces supersaturated rich liquid and high-concentration flue gas from the bottom of the tower. After being processed by the second intensifier unit, a stable gas-liquid mixture is formed. At this time, the gas-liquid mixture moves from bottom to top in the second-stage intensifier tower. As the gas-liquid mixture rises, the decarbonized flue gas can be discharged through the flue gas pipe at the top of the second-stage intensifier tower, achieving a preliminary gas-liquid separation effect.

[0065] Comparing Example 1 and Comparative Example 5, it can be seen that the present invention controls the amount of absorbent flowing into the first-stage enhanced reaction tower by setting a flow control valve, keeping it at 2m. 3 / h-8m 3 At a flow rate of / h, the reaction liquid achieves excellent removal of carbon dioxide from flue gas when flowing into the enhanced reaction tower. This is because, to achieve enhanced carbon dioxide absorption, this invention requires nearly saturated rich liquid and flue gas to flow into the enhanced reaction tower at a certain flow rate. After being processed by the enhanced unit, the flue gas is broken into microbubbles, allowing the broken-up flue gas to form a stable gas-liquid mixture with the rich liquid. This significantly increases the load on the reaction liquid and improves CO2 removal. If the flow rate is too low, the reaction system in the enhanced reaction tower will become saturated prematurely, affecting the capture of carbon dioxide from the flue gas. Conversely, if the flow rate is too high, the load on the reaction liquid will be too low, preventing the reaction liquid from absorbing carbon dioxide from the flue gas and thus affecting the carbon dioxide removal effect.

[0066] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this utility model, and are not intended to limit it. Although the utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this utility model.

Claims

1. An enhanced carbon dioxide capture system, characterized in that, The system includes a multi-stage enhanced reaction tower, which is equipped with a flue gas duct, a rich liquid inlet, and a discharge outlet. An enhanced unit is installed inside the multi-stage enhanced reaction tower, and a circulation pipe is installed outside the multi-stage enhanced reaction tower. A circulation pump and a flow control valve are installed sequentially on the circulation pipe.

2. The enhanced carbon dioxide capture system according to claim 1, characterized in that, The multi-stage enhanced reaction tower is a two-stage enhanced reaction tower, which includes a first-stage enhanced reaction tower and a second-stage enhanced reaction tower.

3. The enhanced carbon dioxide capture system according to claim 2, characterized in that, The first stage enhanced reaction tower is equipped with a first enhanced unit at the top, and a disc-shaped duct is installed below the first enhanced unit; the rich liquid inlet and the flue gas pipe are sequentially installed at the top of the first stage enhanced reaction tower, and the first stage enhanced reaction tower is equipped with a discharge port and a circulating feed port on both sides respectively.

4. The enhanced carbon dioxide capture system according to claim 3, characterized in that, The circulation pipeline is located outside the first-stage enhanced reaction tower, and the circulation pump is connected to the circulation inlet.

5. The enhanced carbon dioxide capture system according to claim 2, characterized in that, The second-stage enhanced reaction tower is equipped with flue gas pipes at both the top and bottom. Supersaturated rich liquor inlet and supersaturated rich liquor outlet are respectively provided on both sides of the second-stage enhanced reaction tower, and the supersaturated rich liquor inlet and the outlet are connected. A second enhanced unit is provided at the bottom of the second-stage enhanced reaction tower, and the second enhanced unit is connected to the supersaturated rich liquor inlet.

6. The enhanced carbon dioxide capture system according to claim 2, characterized in that, It also includes an absorption tower, which is connected to the first-stage enhanced reaction tower through the rich liquid inlet. A flow control valve is provided between the absorption tower and the rich liquid inlet to control the flow rate of the rich liquid flowing into the enhanced reaction tower.

7. The enhanced carbon dioxide capture system according to claim 6, characterized in that, The absorption tower is provided with a flue gas outlet and an absorbent inlet at the top, and a flue gas feed pipe is provided at the bottom of the absorption tower for introducing decarbonized flue gas.

8. The enhanced carbon dioxide capture system according to claim 7, characterized in that, The absorbent inlet is connected to the absorbent storage tank, and the absorbent storage tank is connected to the absorption tower through the absorbent inlet; a flow control valve is also provided between the absorbent storage tank and the absorbent inlet to control the flow rate of the absorbent when it flows into the absorption tower.

9. The enhanced carbon dioxide capture system according to claim 8, characterized in that, It also includes a gas-liquid separator, a heat exchanger and a regeneration tower connected in sequence. The gas-liquid separator is connected to the second-stage enhanced reaction tower. An interstage heating unit is provided on the outside of the regeneration tower. A regeneration gas cooler and a gas-liquid separator are also connected in sequence at the top of the regeneration tower. A reboiler is connected to the bottom of the regeneration tower.

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