Carbon capture device

Abstract

The invention provides a carbon capture device. The carbon capture device comprises a dust removal device; the membrane separation device is connected with the dust removal device; the multiple absorption towers are sequentially connected in the direction from upstream to downstream, each absorption tower is provided with a smoke inlet, a smoke purifying opening, a first liquid inlet and a first liquid outlet, the smoke inlet of the first absorption tower is connected with the membrane separation device, and the smoke outlet of the second absorption tower is connected with the second liquid outlet; in two adjacent absorption towers, the smoke purifying opening of the previous absorption tower is connected with the smoke inlet of the next absorption tower; the regeneration tower is provided with a second liquid inlet, a second liquid outlet and a carbon discharge port, the second liquid inlet is connected with the first liquid outlet of each absorption tower, and the second liquid outlet is connected with the first liquid inlet of each absorption tower. According to the technical scheme provided by the invention, the problem of relatively high energy consumption in the regeneration process caused by mixing of the heavy-phase solvent and the light-phase solvent in related technologies is effectively solved.

Description

Technical Field

[0001] The present invention relates to the field of carbon dioxide capture, and in particular to a carbon capture device. Background Art

[0002] The capture cost is inversely proportional to the concentration of the carbon dioxide emission source. The capture of low-concentration carbon dioxide requires more energy and cost. For example, low-concentration point sources (5%-15% flue gas concentration) mainly come from point sources in large-scale emission reduction-difficult industries, such as power plants and cement plants. Capture methods include chemical solvents, solid material adsorbents, membrane separation, etc., but these methods are less efficient at low concentrations. Because the above methods separate less carbon dioxide from a large amount of gas. This results in a higher regeneration heat consumption per unit of carbon dioxide, which increases the overall energy consumption and cost.

[0003] Moreover, the solvent fails to effectively separate after absorbing carbon dioxide, causing the heavy phase and light phase solvent to mix together. Some solvents fail to form a clear liquid-liquid phase transition after absorbing carbon dioxide, making it difficult to separate the absorbent and the absorbed product. For example, in the traditional chemical absorption method, the separation of the absorbent and the absorbed product is not obvious, resulting in high energy consumption during the regeneration process. Summary of the invention

[0004] The main purpose of the present invention is to provide a carbon capture device to solve the problem in the related art that heavy phase and light phase solvents are mixed together, resulting in high energy consumption during the regeneration process.

[0005] In order to achieve the above-mentioned purpose, the present invention provides a carbon capture device, comprising: a dust removal device; a membrane separation device, connected to the dust removal device; a plurality of absorption towers, the plurality of absorption towers are connected in sequence from upstream to downstream, each absorption tower has a smoke inlet, a clean smoke outlet, a first liquid inlet and a first liquid outlet, wherein the smoke inlet of the first absorption tower is connected to the membrane separation device, and the clean smoke outlet of the first absorption tower of two adjacent absorption towers is connected to the smoke inlet of the second absorption tower; a regeneration tower, having a second liquid inlet, a second liquid outlet and a carbon discharge outlet, the second liquid inlet is connected to the first liquid outlet of each absorption tower, and the second liquid outlet is connected to the first liquid inlet of each absorption tower.

[0006] Furthermore, there are multiple regeneration towers, and the multiple regeneration towers are connected in sequence from upstream to downstream, wherein the second liquid inlet of the first regeneration tower is connected to the first liquid outlet of each absorption tower, the second liquid outlet of the first regeneration tower of two adjacent regeneration towers is connected to the second liquid inlet of the second regeneration tower, and the second liquid outlet of the last regeneration tower is connected to the first liquid inlet of each absorption tower.

[0007] Furthermore, the carbon capture device also includes a first connecting pipeline and a plurality of first branch pipelines, the first end of the first connecting pipeline is connected to the second liquid outlet of the last regeneration tower, the second end of the first connecting pipeline is connected to the first liquid inlet of the first absorption tower through a first branch pipeline, the first connecting pipeline is connected to the first liquid inlets of the remaining absorption towers one by one through the remaining first branch pipelines, and each first branch pipeline is provided with a first control valve.

[0008] Furthermore, a first liquid level sensor is arranged at the bottom of each absorption tower, the first control valve is a first solenoid valve, the carbon capture device further comprises a controller, and the first liquid level sensor and the first solenoid valve are both connected to the controller.

[0009] Furthermore, the first connecting pipeline is connected to the last regeneration tower through a third connecting pipeline, and a reboiler is connected to the third connecting pipeline.

[0010] Furthermore, the first liquid outlet of each absorption tower is connected to the second liquid inlet of the first regeneration tower through a second branch pipeline, and a second control valve is arranged on each second branch pipeline.

[0011] Furthermore, a second liquid level sensor is provided at the bottom of each regeneration tower, the second control valve is a second solenoid valve, the carbon capture device further comprises a controller, and the second liquid level sensor and the second solenoid valve are both connected to the controller.

[0012] Furthermore, the membrane separation device includes a container and a separation membrane, the separation membrane separates the container into an enrichment chamber and a permeation chamber, the container is provided with an air inlet connected to the permeation chamber, the air inlet is connected to the smoke inlet of the first absorption tower, and the container is also provided with an air outlet connected to the enrichment chamber.

[0013] Furthermore, a coil heat exchanger connected to the second liquid outlet is installed inside the regeneration tower.

[0014] Furthermore, a first pump body is connected between the smoke inlet of the first absorption tower and the membrane separation device, and the second liquid outlet is connected to the first liquid inlet of each absorption tower through the second pump body.

[0015] Applying the technical solution of the present invention, the carbon capture device includes: a dust removal device, a membrane separation device, a plurality of absorption towers and a regeneration tower. The membrane separation device is connected to the dust removal device. When the original flue gas passes through the dust removal device, the dust removal device can remove dust and particulate matter in the original flue gas. The membrane separation device can increase the concentration of carbon dioxide. A plurality of absorption towers are connected in sequence from upstream to downstream, and each absorption tower has a smoke inlet, a clean smoke outlet, a first liquid inlet and a first liquid outlet, wherein the smoke inlet of the first absorption tower is connected to the membrane separation device, and the clean smoke outlet of the first absorption tower of the two adjacent absorption towers is connected to the smoke inlet of the next absorption tower. The regeneration tower has a second liquid inlet, a second liquid outlet and a carbon discharge outlet, the second liquid inlet is connected to the first liquid outlet of each absorption tower, and the second liquid outlet is connected to the first liquid inlet of each absorption tower. The liquid storage tank of each absorption tower corresponds to different concentrations of absorption liquid, and multiple absorption towers are connected in sequence from upstream to downstream to achieve step-by-step transfer and regeneration of the absorption liquid, enhance the solvent stratification effect, reduce the mixing of heavy phase and light phase, and reduce the heat consumption during the regeneration process. Therefore, the technical solution of the present application effectively solves the problem in the related art that the heavy phase and light phase solvents are mixed together, resulting in high energy consumption during the regeneration process. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] The drawings constituting a part of the present application are used to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention. In the drawings:

[0017] Figure 1 A piping connection diagram of an embodiment of a carbon capture device according to the present invention is shown.

[0018] The above drawings include the following reference numerals:

[0019] 10. Dust removal device;

[0020] 20. membrane separation device; 21. container; 22. separation membrane; 23. air inlet; 24. air outlet;

[0021] 30. Absorption tower; 31. Smoke inlet; 32. Smoke outlet; 33. First liquid inlet; 34. First liquid outlet;

[0022] 40. regeneration tower; 41. second liquid inlet; 42. second liquid outlet; 43. carbon discharge outlet;

[0023] 50. first connecting pipeline; 51. first branch pipeline; 52. first control valve; 53. second branch pipeline; 54. second control valve; 55. third connecting pipeline; 56. reboiler;

[0024] 61. First pump body; 62. Second pump body; 63. First liquid level sensor; 64. Second liquid level sensor. DETAILED DESCRIPTION

[0025] 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 described embodiments are only part of the embodiments of the present invention, rather than all the embodiments. The following description of at least one exemplary embodiment is actually only illustrative and is by no means intended to limit the present invention and its application or use. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0026] It should be noted that the terms used herein are only for describing specific embodiments and are not intended to limit the exemplary embodiments according to the present application. As used herein, unless the context clearly indicates otherwise, the singular form is also intended to include the plural form. In addition, it should be understood that when the terms "comprise" and / or "include" are used in this specification, it indicates the presence of features, steps, operations, devices, components and / or combinations thereof.

[0027] Unless otherwise specifically stated, the relative arrangement, numerical expressions and numerical values ​​of the parts and steps set forth in these embodiments do not limit the scope of the present invention. Meanwhile, it should be understood that, for ease of description, the sizes of the various parts shown in the accompanying drawings are not drawn according to the actual proportional relationship. The technology, method and equipment known to those of ordinary skill in the relevant art may not be discussed in detail, but in appropriate cases, the technology, method and equipment should be considered as a part of the specification. In all examples shown and discussed here, any specific value should be interpreted as being merely exemplary, rather than as a limitation. Therefore, other examples of exemplary embodiments may have different values. It should be noted that similar reference numerals and letters represent similar items in the following drawings, and therefore, once a certain item is defined in an accompanying drawing, it does not need to be further discussed in subsequent drawings.

[0028] like Figure 1As shown, the present application provides a carbon capture device, and an embodiment of the carbon capture device includes: a dust removal device 10, a membrane separation device 20, a plurality of absorption towers 30 and a regeneration tower 40. The membrane separation device 20 is connected to the dust removal device 10. When the original flue gas passes through the dust removal device 10, the dust removal device 10 can remove dust and particulate matter in the original flue gas. The membrane separation device 20 can increase the concentration of carbon dioxide. A plurality of absorption towers 30 are connected in sequence from upstream to downstream, and each absorption tower 30 has a smoke inlet 31, a clean smoke outlet 32, a first liquid inlet 33 and a first liquid outlet 34, wherein the smoke inlet 31 of the first absorption tower 30 is connected to the membrane separation device 20, and the clean smoke outlet 32 ​​of the first absorption tower 30 (the absorption tower located upstream of the two adjacent absorption towers) of the two adjacent absorption towers 30 is connected to the smoke inlet 31 of the latter absorption tower 30 (the absorption tower located downstream of the two adjacent absorption towers). The regeneration tower 40 has a second liquid inlet 41, a second liquid outlet 42 and a carbon discharge port 43. The second liquid inlet 41 is connected to the first liquid outlet 34 of each absorption tower 30, and the second liquid outlet 42 is connected to the first liquid inlet 33 of each absorption tower 30. The dust removal device 10 is preferably an electrostatic dust removal device.

[0029] Applying the technical solution of this embodiment, the carbon capture device includes: a dust removal device 10, a membrane separation device 20, a plurality of absorption towers 30 and a regeneration tower 40. The liquid storage tank of each absorption tower 30 corresponds to an absorption liquid of different concentrations, and the plurality of absorption towers 30 are sequentially connected from upstream to downstream to achieve step-by-step transfer and regeneration of the absorption liquid, enhance the solvent stratification effect, reduce the mixing of the heavy phase and the light phase, and reduce the heat consumption during the regeneration process. Therefore, the technical solution of this embodiment effectively solves the problem in the related art that the heavy phase and the light phase solvent are mixed together, resulting in high energy consumption during the regeneration process.

[0030] like Figure 1 As shown, there are multiple regeneration towers 40, and the multiple regeneration towers 40 are connected in sequence from upstream to downstream, wherein the second liquid inlet 41 of the first regeneration tower 40 is connected to the first liquid outlet 34 of each absorption tower 30, the second liquid outlet 42 of the first regeneration tower 40 of the two adjacent regeneration towers 40 is connected to the second liquid inlet 41 of the next regeneration tower 40, and the second liquid outlet 42 of the last regeneration tower 40 is connected to the first liquid inlet 33 of each absorption tower 30. The original flue gas passes through the electrostatic precipitator to remove particulate matter. The clean flue gas enters the membrane separation device, and the carbon dioxide is enriched and exported to the multiple absorption towers 30 behind. The enriched carbon dioxide enters the multiple absorption towers 30 and is absorbed by the absorbent step by step. The absorbed rich liquid is stored in the liquid storage tanks of the multiple absorption towers 30 in stages. And the absorbed rich liquid enters the multiple regeneration towers for regeneration, so that the above-mentioned decoupled absorption-desorption process can use valley electricity to generate electricity and can reduce the capture cost and energy consumption of unit carbon dioxide.

[0031] The term "plurality" in this application refers to a number of two or more.

[0032] like Figure 1 As shown, the carbon capture device further includes a first connecting pipeline 50 and a plurality of first branch pipelines 51, wherein the first end of the first connecting pipeline 50 is connected to the second liquid outlet 42 of the last regeneration tower 40, and the second end of the first connecting pipeline 50 is connected to the first liquid inlet 33 of the first absorption tower 30 through a first branch pipeline 51, and the first connecting pipeline 50 is connected to the first liquid inlets 33 of the remaining absorption towers 30 in a one-to-one correspondence through the remaining first branch pipelines 51, and each first branch pipeline 51 is provided with a first control valve 52. The first control valve 52 can control the flow rate of the lean liquid flowing through the first connecting pipeline 50, so that the lean liquid flowing into each absorption tower 30 can flow smoothly to the liquid storage tank of the absorption tower 30, thereby improving the phase separation effect, and the static liquid surface phase separation position is clear, and there is no disturbance caused by droplets.

[0033] like Figure 1 As shown, a first liquid level sensor 63 is provided at the bottom of each absorption tower 30, the first control valve 52 is a first electromagnetic valve, and the carbon capture device further includes a controller, and the first liquid level sensor 63 and the first electromagnetic valve are both connected to the controller. The first liquid level sensor 63 can detect the liquid level at the bottom of each absorption tower 30, and after multiple absorption and regeneration, the heavy phase liquid level is known from low to high.

[0034] like Figure 1 As shown, the first connecting pipeline 50 is connected to the last regeneration tower 40 through the third connecting pipeline 55, and the third connecting pipeline 55 is connected to a reboiler 56. The reboiler 56 is used to heat the lean liquid flowing through the first connecting pipeline 50 and desorb carbon dioxide. The desorbed carbon dioxide gas enters the subsequent processing flow and is prepared for storage or utilization. The decoupled absorption-desorption process allows operation during the low-energy period, reducing operating costs.

[0035] The operating voltage of the electrostatic precipitator of this embodiment is: 40KV-60KV.

[0036] Operating pressure of membrane separation device: 1bar-2bar.

[0037] Selection of absorbent: solvent with stable chemical properties and strong carbon dioxide absorption capacity.

[0038] Operating temperature of absorption tower: 30℃-50℃.

[0039] Reboiler temperature: 120℃-140℃.

[0040] like Figure 1As shown, the first liquid outlet 34 of each absorption tower 30 is connected to the second liquid inlet 41 of the first regeneration tower 40 through the second branch pipeline 53, and a second control valve 54 is provided on each second branch pipeline 53. The second control valve 54 is provided so that the solution in the regeneration tower can be continuously fed and can be pumped from each absorption tower 30 into the first regeneration tower, with less gas content and better regeneration effect, so that the overall heating time is short and the thermal degradation products are also less.

[0041] like Figure 1 As shown, a second liquid level sensor 64 is provided at the bottom of each regeneration tower 40, the second control valve 54 is a second electromagnetic valve, and the carbon capture device further comprises a controller, and the second liquid level sensor 64 and the second electromagnetic valve are both connected to the controller. The second liquid level sensor 64 can detect the liquid level at the bottom of each regeneration tower 40, and the density detector connected to each second liquid level sensor 64 can not only know the heavy phase liquid level but also determine the position of the phase separation interface, so as to facilitate gradual regeneration from concentrated to diluted.

[0042] The configuration of the controller of this embodiment facilitates the automatic control of the carbon capture device, thereby effectively improving the overall performance and stability of the carbon capture device.

[0043] like Figure 1 As shown, the membrane separation device 20 includes a container 21 and a separation membrane 22. The separation membrane 22 separates the container 21 into an enrichment chamber and a permeation chamber. The container 21 is provided with an air inlet 23 connected to the permeation chamber. The air inlet 23 is connected to the smoke inlet 31 of the first absorption tower 30. The container 21 is also provided with an air outlet 24 connected to the enrichment chamber. The enrichment chamber collects the enriched carbon dioxide gas that passes through the separation membrane 22, and the permeation chamber stores other gases that do not pass through the separation membrane 22. Through the membrane separation technology of the separation membrane 22, the loading amount of carbon dioxide is significantly increased, and the capture efficiency of carbon dioxide is effectively improved.

[0044] like Figure 1 As shown, a coil heat exchanger connected to the second liquid outlet 42 is installed inside the regeneration tower 40. The coil heat exchanger is used to heat and regenerate the absorption liquid, thereby improving thermal efficiency and reducing thermal degradation products. The regenerated solution is transported back to the liquid storage tanks of the multiple absorption towers 30 through the first connecting pipeline 50.

[0045] like Figure 1 As shown, in order to provide kinetic energy for the enriched carbon dioxide separated from the membrane separation device 20, a first pump body 61 is connected between the smoke inlet 31 of the first absorption tower 30 and the membrane separation device 20, and in order to provide kinetic energy for the lean liquid desorbed from the second liquid outlet 42, the second liquid outlet 42 is connected to the first liquid inlet 33 of each absorption tower 30 through the second pump body 62.

[0046] A carbon capture device comprises: a dust removal device 10; a membrane separation device 20, connected to the dust removal device 10; a plurality of absorption towers 30, wherein the plurality of absorption towers 30 are sequentially connected from upstream to downstream, each of the absorption towers 30 having a smoke inlet 31, a clean smoke outlet 32, a first liquid inlet 33 and a first liquid outlet 34, wherein the smoke inlet 31 of the first absorption tower 30 is connected to the membrane separation device 20, and the clean smoke outlet 32 ​​of the first absorption tower 30 of two adjacent absorption towers 30 is connected to the smoke inlet 31 of the second absorption tower 30; a regeneration tower 40, having a second liquid inlet 41, a second liquid outlet 42 and a carbon discharge outlet 43, wherein the second liquid inlet 41 is connected to the first liquid outlet 34 of each absorption tower 30, and the second liquid outlet 42 is connected to the first liquid inlet 33 of each absorption tower 30.

[0047] The carbon capture device of the present invention removes dust and particulate matter from the original flue gas through a dust removal device 10, and a membrane separation device 20 increases the concentration of carbon dioxide, thereby reducing the energy consumption of the subsequent absorption process. The arrangement of multiple absorption towers 30 enables the absorption process to be carried out step by step, and the concentration of the absorption liquid in each absorption tower 30 is different, which can more effectively capture carbon dioxide. The function of the regeneration tower 40 is to desorb the rich liquid after absorption, release carbon dioxide, and regenerate the absorption liquid for recycling. The principle of this design is to reduce the mixing of heavy phase and light phase solvents through graded absorption and regeneration, and reduce the heat consumption in the regeneration process, thereby improving the energy efficiency and economy of the entire carbon capture device. The implementation effect is reflected in the significant improvement of the capture efficiency of carbon dioxide and the reduction of the capture cost and energy consumption of unit carbon dioxide. The application scenarios include but are not limited to the flue gas treatment of large-scale emission reduction difficult industries such as power plants and cement plants, and are particularly suitable for the capture of low-concentration carbon dioxide.

[0048] There are multiple regeneration towers 40, and the multiple regeneration towers 40 are connected in sequence from upstream to downstream, wherein the second liquid inlet 41 of the first regeneration tower 40 is connected to the first liquid outlet 34 of each absorption tower 30, the second liquid outlet 42 of the first regeneration tower 40 of two adjacent regeneration towers 40 is connected to the second liquid inlet 41 of the second regeneration tower 40, and the second liquid outlet 42 of the last regeneration tower 40 is connected to the first liquid inlet 33 of each absorption tower 30.

[0049] The hierarchical setting of the regeneration tower 40 allows the absorption liquid to be regenerated at different concentrations, which helps to improve the efficiency of the regeneration process and reduce energy consumption. The first regeneration tower 40 receives the rich liquid from the absorption tower 30. After heating and desorbing carbon dioxide, the lean liquid is transported to the subsequent regeneration tower 40 for further regeneration until the lean liquid is completely regenerated, and then returns to the absorption tower 30 through the first connecting pipeline 50. The principle of this design is to utilize the different heat requirements of absorption liquids of different concentrations during the regeneration process, and to achieve optimal energy utilization through step-by-step regeneration. The implementation effect is that the regeneration process is more efficient and can significantly reduce the regeneration heat consumption per unit of carbon dioxide. The application scenarios are mainly in industrial facilities that require large-scale carbon dioxide capture, such as thermal power plants, chemical plants, etc. Through graded regeneration, the operating costs can be effectively reduced and the economic benefits can be improved.

[0050] The carbon capture device also includes a first connecting pipeline 50 and a plurality of first branch pipelines 51, wherein the first end of the first connecting pipeline 50 is connected to the second liquid outlet 42 of the last regeneration tower 40, the second end of the first connecting pipeline 50 is connected to the first liquid inlet 33 of the first absorption tower 30 through one of the first branch pipelines 51, the first connecting pipeline 50 is connected to the first liquid inlet 33 of the remaining absorption towers 30 in a one-to-one correspondence through the remaining first branch pipelines 51, and each of the first branch pipelines 51 is provided with a first control valve 52.

[0051] The design of the control system is a key part of the present invention, which ensures the precise transfer of the absorption liquid between the absorption tower 30 and the regeneration tower 40. The setting of the first control valve 52 can control the flow of the lean liquid from the regeneration tower 40 to the absorption tower 30, ensuring the smooth progress of the absorption process. The principle of this design is to avoid excessive or insufficient absorption liquid through precise flow control, thereby improving the absorption efficiency and regeneration efficiency. The implementation effect is that the operation of the entire carbon capture device is more stable and can adapt to the needs under different working conditions. The application scenario is that in a large-scale carbon capture system that requires automated operation, the control system can achieve 24-hour uninterrupted and efficient operation, reducing the need for manual intervention and improving the reliability and safety of the system.

[0052] A first liquid level sensor 63 is disposed at the bottom of each absorption tower 30 . The first control valve 52 is a first solenoid valve. The carbon capture device further includes a controller. Both the first liquid level sensor 63 and the first solenoid valve are connected to the controller.

[0053] The coordinated use of the liquid level sensor and the solenoid valve is the key to achieving precise control of the absorption liquid. The first liquid level sensor 63 can monitor the liquid level at the bottom of the absorption tower 30 in real time. When the liquid level reaches the preset value, the controller will automatically adjust the opening of the first solenoid valve to control the inflow of the lean liquid, ensuring that the liquid level in the absorption tower 30 is stable within the optimal working range. The principle of this design is to utilize the real-time monitoring function of the liquid level sensor and the rapid response characteristics of the solenoid valve to achieve automatic control and improve the stability and efficiency of the system. The implementation effect is that the transfer of the absorption liquid is more precise, unnecessary energy consumption is reduced, and the efficiency of carbon capture is improved. The application scenario is that in industrial carbon capture systems that require high-precision control, the coordination of the liquid level sensor and the solenoid valve can achieve precise control of the absorption liquid, thereby improving the overall performance of the system.

[0054] The first connecting pipeline 50 is connected to the last regeneration tower 40 via a third connecting pipeline 55 , and a reboiler 56 is connected to the third connecting pipeline 55 .

[0055] The setting of the reboiler 56 is an important link in the regeneration process. It is used to heat the lean liquid flowing out of the regeneration tower 40 to reach the temperature required for desorption of carbon dioxide. The principle of this design is to use the heating function of the reboiler 56 to increase the temperature of the lean liquid, thereby promoting the desorption of carbon dioxide and improving the regeneration efficiency. The implementation effect is that the regeneration process is more efficient and can significantly reduce the regeneration heat consumption of unit carbon dioxide. The application scenario is in industrial facilities that require large-scale carbon dioxide regeneration, such as thermal power plants, chemical plants, etc. The setting of the reboiler 56 can effectively reduce operating costs and improve economic benefits. The use process is that when the lean liquid flows out of the regeneration tower 40, it enters the reboiler 56 through the third connecting pipeline 55, and the reboiler 56 heats the lean liquid to the set temperature, and then the lean liquid returns to the absorption tower 30 through the first connecting pipeline 50 and the first branch pipeline 51 for a new round of absorption.

[0056] The first liquid outlet 34 of each absorption tower 30 is connected to the second liquid inlet 41 of the first regeneration tower 40 through a second branch pipeline 53 , and a second control valve 54 is disposed on each second branch pipeline 53 .

[0057] The management of the control valve by the control system is the key to ensuring the smooth progress of the regeneration process. The setting of the second control valve 54 can control the flow of rich liquid from the absorption tower 30 to the regeneration tower 40 to ensure the continuity and stability of the regeneration process. The principle of this design is to avoid excessive or insufficient rich liquid through the precise control of the second control valve 54 by the control system, thereby improving the regeneration efficiency and the recycling efficiency of the absorption liquid. The implementation effect is that the regeneration process is more efficient and can significantly reduce the regeneration heat consumption per unit of carbon dioxide. The application scenario is that in large-scale carbon capture systems that require automated operation, the management of the control valve by the control system can realize the automation of the regeneration process, reduce the need for manual intervention, and improve the reliability and safety of the system.

[0058] A second liquid level sensor 64 is disposed at the bottom of each regeneration tower 40 . The second control valve 54 is a second solenoid valve. The carbon capture device further includes a controller. Both the second liquid level sensor 64 and the second solenoid valve are connected to the controller.

[0059] The integrated management function of the controller is the core of realizing the automated operation of the entire carbon capture device. It can receive signals from the first liquid level sensor 63 and the second liquid level sensor 64, and adjust the opening of the first solenoid valve and the second solenoid valve according to the signals, so as to control the flow of the lean liquid and the rich liquid, and ensure the smooth progress of the absorption and regeneration process. The principle of this design is to use the integrated management function of the controller to achieve unified control of multiple sensors and solenoid valves, and improve the automation and efficiency of the system. The implementation effect is that the operation of the carbon capture device is more stable, can adapt to the needs under different working conditions, and reduce the operating cost. The application scenario is that in large-scale carbon capture systems that require high-precision control and automated operation, through the integrated management of the controller, precise control of the entire system can be achieved, thereby improving the overall performance and economic benefits of the system.

[0060] The membrane separation device 20 includes a container 21 and a separation membrane 22, wherein the separation membrane 22 separates the container 21 into an enrichment chamber and a permeation chamber, and the container 21 is provided with an air inlet 23 connected to the permeation chamber, and the air inlet 23 is connected to the smoke inlet 31 of the first absorption tower 30, and the container 21 is also provided with an air outlet 24 connected to the enrichment chamber.

[0061] The structure and function of the membrane separation device 20 are the key to improving the efficiency of carbon dioxide capture. The separation membrane 22 inside the container 21 can selectively permeate carbon dioxide, enriching the carbon dioxide in the enrichment chamber, while other gases remain in the permeation chamber. The principle of this design is to utilize the gas separation characteristics of the separation membrane 22 to increase the concentration of carbon dioxide, thereby reducing the energy consumption of the subsequent absorption process. The implementation effect is to significantly improve the capture efficiency of carbon dioxide and reduce the capture cost and energy consumption of unit carbon dioxide. The application scenario is in industrial facilities where the concentration of carbon dioxide needs to be increased, such as thermal power plants, chemical plants, etc. Through the setting of the membrane separation device 20, the capture efficiency of carbon dioxide can be effectively improved, the operating cost can be reduced, and the economic benefits can be improved.

[0062] A coil heat exchanger connected to the second liquid outlet 42 is installed inside the regeneration tower 40 .

[0063] The design of the heat exchanger inside the regeneration tower 40 is the key to improving regeneration efficiency and reducing energy consumption. The coil heat exchanger can efficiently heat the lean liquid, promote the desorption of carbon dioxide, and reduce the generation of thermal degradation products. The principle of this design is to use the efficient heat exchange characteristics of the coil heat exchanger to increase the temperature of the lean liquid, thereby promoting the desorption of carbon dioxide and improving the regeneration efficiency. The implementation effect is that the regeneration process is more efficient and can significantly reduce the regeneration heat consumption per unit of carbon dioxide. The application scenario is in industrial facilities that require large-scale carbon dioxide regeneration, such as thermal power plants, chemical plants, etc. The setting of the coil heat exchanger can effectively reduce operating costs and improve economic benefits.

[0064] A first pump body 61 is connected between the smoke inlet 31 of the first absorption tower 30 and the membrane separation device 20 , and the second liquid outlet 42 is connected to the first liquid inlet 33 of each absorption tower 30 through the second pump body 62 .

[0065] The setting and function of the pump body are the key to ensuring the smooth flow of fluid in the carbon capture device. The setting of the first pump body 61 and the second pump body 62 can provide the necessary conveying kinetic energy for the enriched carbon dioxide and the lean liquid, ensuring that they can flow smoothly from one component to another. The principle of this design is to use the conveying function of the pump body to provide power for the fluid to ensure the continuity and stability of the absorption and regeneration process. The implementation effect is that the operation of the carbon capture device is more stable, can adapt to the needs under different working conditions, and reduce the operating cost. The application scenario is that in a large-scale carbon capture system that requires high-precision control and automated operation, the setting of the pump body can achieve smooth delivery of the fluid, thereby improving the overall performance and economic benefits of the system. The use process is that when the enriched carbon dioxide flows out of the membrane separation device 20, the first pump body 61 provides it with conveying kinetic energy so that it can smoothly enter the first absorption tower 30; when the lean liquid flows out of the regeneration tower 40, the second pump body 62 provides it with conveying kinetic energy so that it can smoothly return to the absorption tower 30 for a new round of absorption.

[0066] In the description of the present invention, it is necessary to understand that the directions or positional relationships indicated by directional words such as "front, back, up, down, left, right", "lateral, vertical, perpendicular, horizontal" and "top, bottom" are usually based on the directions or positional relationships shown in the drawings. They are only for the convenience of describing the present invention and simplifying the description. Unless otherwise specified, these directional words do not indicate or imply that the devices or elements referred to must have a specific direction or be constructed and operated in a specific direction. Therefore, they cannot be understood as limiting the scope of protection of the present invention. The directional words "inside and outside" refer to the inside and outside relative to the contours of each component itself.

[0067] For ease of description, spatially relative terms such as "above", "above", "on the upper surface of", "above", etc. may be used here to describe the spatial positional relationship between a device or feature and other devices or features as shown in the figure. It should be understood that spatially relative terms are intended to include different orientations of the device in use or operation in addition to the orientation described in the figure. For example, if the device in the accompanying drawings is inverted, the device described as "above other devices or structures" or "above other devices or structures" will be positioned as "below other devices or structures" or "below other devices or structures". Thus, the exemplary term "above" can include both "above" and "below". The device can also be positioned in other different ways (rotated 90 degrees or in other orientations), and the spatially relative descriptions used here are interpreted accordingly.

[0068] In addition, it should be noted that the use of terms such as "first" and "second" to limit components is only for the convenience of distinguishing the corresponding components. If not otherwise stated, the above terms have no special meaning and therefore cannot be understood as limiting the scope of protection of the present invention.

[0069] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A carbon capture device, characterized in that: include: Dust removal device (10); A membrane separation device (20) connected to the dust removal device (10); A plurality of absorption towers (30), wherein the plurality of absorption towers (30) are connected in sequence from upstream to downstream, and each of the absorption towers (30) has a smoke inlet (31), a clean smoke outlet (32), a first liquid inlet (33) and a first liquid outlet (34), wherein the smoke inlet (31) of the first absorption tower (30) is connected to the membrane separation device (20), and the clean smoke outlet (32) of the first absorption tower (30) of two adjacent absorption towers (30) is connected to the smoke inlet (31) of the second absorption tower (30); The regeneration tower (40) has a second liquid inlet (41), a second liquid outlet (42) and a carbon discharge port (43), wherein the second liquid inlet (41) is connected to the first liquid outlet (34) of each absorption tower (30), and the second liquid outlet (42) is connected to the first liquid inlet (33) of each absorption tower (30).

2. The carbon capture device according to claim 1, characterized in that: There are a plurality of regeneration towers (40), and the plurality of regeneration towers (40) are connected in sequence from upstream to downstream, wherein the second liquid inlet (41) of the first regeneration tower (40) is connected to the first liquid outlet (34) of each absorption tower (30), the second liquid outlet (42) of the first regeneration tower (40) of two adjacent regeneration towers (40) is connected to the second liquid inlet (41) of the second regeneration tower (40), and the second liquid outlet (42) of the last regeneration tower (40) is connected to the first liquid inlet (33) of each absorption tower (30).

3. The carbon capture device according to claim 2, characterized in that: The carbon capture device further comprises a first connecting pipeline (50) and a plurality of first branch pipelines (51); the first end of the first connecting pipeline (50) is connected to the second liquid outlet (42) of the last regeneration tower (40); the second end of the first connecting pipeline (50) is connected to the first liquid inlet (33) of the first absorption tower (30) through one of the first branch pipelines (51); the first connecting pipeline (50) is connected to the first liquid inlet (33) of the remaining absorption towers (30) in a one-to-one correspondence through the remaining first branch pipelines (51); and each of the first branch pipelines (51) is provided with a first control valve (52).

4. The carbon capture device according to claim 3, characterized in that: A first liquid level sensor (63) is arranged at the bottom of each absorption tower (30); the first control valve (52) is a first solenoid valve; the carbon capture device further comprises a controller; and the first liquid level sensor (63) and the first solenoid valve are both connected to the controller.

5. The carbon capture device according to claim 3, characterized in that: The first connecting pipeline (50) is connected to the last regeneration tower (40) via a third connecting pipeline (55), and a reboiler (56) is connected to the third connecting pipeline (55).

6. The carbon capture device according to claim 2, characterized in that: The first liquid outlet (34) of each absorption tower (30) is connected to the second liquid inlet (41) of the first regeneration tower (40) via a second branch pipeline (53), and each second branch pipeline (53) is provided with a second control valve (54).

7. The carbon capture device according to claim 6, characterized in that: A second liquid level sensor (64) is provided at the bottom of each regeneration tower (40); the second control valve (54) is a second solenoid valve; the carbon capture device further comprises a controller; the second liquid level sensor (64) and the second solenoid valve are both connected to the controller.

8. The carbon capture device according to claim 1, characterized in that: The membrane separation device (20) comprises a container (21) and a separation membrane (22), wherein the separation membrane (22) separates the container (21) into an enrichment chamber and a permeation chamber, and the container (21) is provided with an air inlet (23) connected to the permeation chamber, and the air inlet (23) is connected to the smoke inlet (31) of the first absorption tower (30). The container (21) is also provided with an air outlet (24) connected to the enrichment chamber.

9. The carbon capture device according to claim 1, characterized in that: A coil heat exchanger connected to the second liquid outlet (42) is installed inside the regeneration tower (40).

10. The carbon capture device according to claim 1, characterized in that: A first pump body (61) is connected between the smoke inlet (31) of the first absorption tower (30) and the membrane separation device (20), and the second liquid outlet (42) is connected to the first liquid inlet (33) of each absorption tower (30) through the second pump body (62).

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