Carbon capture device

Abstract

This invention provides a carbon capture device, comprising: a dust removal device; a membrane separation device connected to the dust removal device; multiple absorption towers connected sequentially from upstream to downstream, each absorption tower having a flue gas inlet, a clean flue gas inlet, a first liquid inlet, and a first liquid outlet, wherein the flue gas inlet of the first absorption tower is connected to the membrane separation device, and the clean flue gas inlet of the preceding absorption tower and the flue gas inlet of the following absorption tower in any two adjacent absorption towers are connected; and a regeneration tower having a second liquid inlet, a second liquid outlet, and a carbon discharge outlet, the second liquid inlet being connected to the first liquid outlet of each absorption tower, and the second liquid outlet being connected to the first liquid inlet of each absorption tower. The technical solution of this application effectively solves the problem in related technologies where the heavy and light phase solvents are mixed together, leading to high energy consumption during the regeneration process.

Description

Technical Field

[0001] This invention relates to the field of carbon dioxide capture, and more specifically, to a carbon capture device. Background Technology

[0002] Capture costs are inversely proportional to the concentration of carbon dioxide emissions from the source; capturing low-concentration carbon dioxide requires more energy and higher costs. For example, low-concentration point sources (5%-15% concentration in flue gas) mainly originate from large-scale, emission-difficult-to-reduce industries, such as power plants and cement plants. Capture methods include chemical solvents, solid adsorbent materials, and membrane separation, but these methods are less efficient at low concentrations. Because these methods separate relatively little carbon dioxide from a large amount of gas, the regeneration heat consumption per unit of carbon dioxide is high, increasing overall energy consumption and costs.

[0003] Furthermore, the solvent failed to effectively separate into layers after absorbing carbon dioxide, resulting in the heavy and light phases of the solvent mixing together. Some solvents failed to undergo a significant liquid-liquid phase transition after absorbing carbon dioxide, making it difficult to separate the absorbent and the absorption products. For example, in traditional chemical absorption methods, the separation of the absorbent and absorption products is not obvious, leading to high energy consumption during regeneration. Summary of the Invention

[0004] The main objective of this invention is to provide a carbon capture device to solve the problem of high energy consumption during regeneration caused by the mixing of heavy and light phase solvents in related technologies.

[0005] To achieve the above objectives, the present invention provides a carbon capture device, comprising: a dust removal device; a membrane separation device connected to the dust removal device; multiple absorption towers connected sequentially from upstream to downstream, each absorption tower having a flue gas inlet, a clean flue gas inlet, a first liquid inlet, and a first liquid outlet, wherein the flue gas inlet of the first absorption tower is connected to the membrane separation device, and the clean flue gas inlet of the preceding absorption tower and the flue gas inlet of the following absorption tower in two adjacent absorption towers are connected; and a regeneration tower having a second liquid inlet, a second liquid outlet, and a carbon discharge outlet, wherein 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 connected sequentially from upstream to downstream. The second inlet of the first regeneration tower is connected to the first outlet of each absorption tower. The second outlet of the first regeneration tower in two adjacent regeneration towers is connected to the second inlet of the second regeneration tower. The second outlet of the last regeneration tower is connected to the first inlet of each absorption tower.

[0007] Furthermore, the carbon capture device also includes a first connecting pipe and multiple first branch pipes. The first end of the first connecting pipe is connected to the second outlet of the last regeneration tower, and the second end of the first connecting pipe is connected to the first inlet of the first absorption tower through a first branch pipe. The first connecting pipe is connected to the first inlet of the remaining absorption towers one by one through the remaining first branch pipes. Each first branch pipe is equipped with a first control valve.

[0008] Furthermore, each absorption tower is equipped with a first liquid level sensor at its bottom, and the first control valve is a first solenoid valve. The carbon capture device also includes a controller, and both the first liquid level sensor and the first solenoid valve are connected to the controller.

[0009] Furthermore, the first connecting pipe is connected to the last regeneration tower via a third connecting pipe, which is connected to a reboiler.

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

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

[0012] Furthermore, the membrane separation device includes a container and a separating membrane, which divides the container into an enrichment chamber and a permeation chamber. The container is provided with an air inlet communicating with the permeation chamber and the air inlet is connected to the flue gas inlet of the first absorption tower. The container is also provided with an air outlet communicating with the enrichment chamber.

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

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

[0015] According to the technical solution of this invention, the carbon capture device includes: a dust removal device, a membrane separation device, multiple absorption towers, and a regeneration tower. The membrane separation device is connected to the dust removal device. When the raw flue gas passes through the dust removal device, the dust removal device can remove dust and particulate matter from the raw flue gas. The membrane separation device can increase the carbon dioxide concentration. Multiple absorption towers are connected sequentially from upstream to downstream. Each absorption tower has a flue gas inlet, a clean flue gas inlet, a first liquid inlet, and a first liquid outlet. The flue gas inlet of the first absorption tower is connected to the membrane separation device, and the clean flue gas inlet of the preceding absorption tower and the flue gas inlet of the following absorption tower are connected in any two adjacent absorption towers. 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. Each absorption tower has a storage tank corresponding to an absorbent of different concentrations. Multiple absorption towers are connected sequentially from upstream to downstream, enabling step-by-step transfer and regeneration of the absorbent. This enhances solvent stratification, reduces the mixing of heavy and light phases, and lowers heat consumption during regeneration. Therefore, the technical solution of this application effectively solves the problem of high energy consumption during regeneration caused by the mixing of heavy and light phase solvents in related technologies. Attached Figure Description

[0016] The accompanying drawings, which form part of this application, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an undue limitation of the invention. In the drawings:

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

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

[0019] 10. Dust removal device;

[0020] 20. Membrane separation device; 21. Container; 22. Separating membrane; 23. Air inlet; 24. Air outlet;

[0021] 30. Absorption tower; 31. Flue gas inlet; 32. Clean flue gas inlet; 33. First liquid inlet; 34. First liquid outlet;

[0022] 40. Regeneration tower; 41. Second liquid inlet; 42. Second liquid outlet; 43. Carbon discharge port;

[0023] 50. First connecting pipe; 51. First branch pipe; 52. First control valve; 53. Second branch pipe; 54. Second control valve; 55. Third connecting pipe; 56. Reboiler;

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

[0025] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. The following description of at least one exemplary embodiment is merely illustrative and is in no way intended to limit the present invention or its application or use. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0026] It should be noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the exemplary embodiments according to this application. As used herein, the singular form is intended to include the plural form as well, unless the context clearly indicates otherwise. Furthermore, it should be understood that when the terms "comprising" and / or "including" are used in this specification, they indicate the presence of features, steps, operations, devices, components, and / or combinations thereof.

[0027] Unless otherwise specifically stated, the relative arrangement, numerical expressions, and values ​​of the components and steps set forth in these embodiments do not limit the scope of the invention. It should also be understood that, for ease of description, the dimensions of the various parts shown in the drawings are not drawn to actual scale. Techniques, methods, and devices known to those skilled in the art may not be discussed in detail, but where appropriate, such techniques, methods, and devices should be considered part of the specification. In all examples shown and discussed herein, any specific values ​​should be interpreted as merely exemplary and not as limitations. Therefore, other examples of exemplary embodiments may have different values. It should be noted that similar reference numerals and letters in the following figures denote similar items; therefore, once an item is defined in one figure, it need not be further discussed in subsequent figures.

[0028] like Figure 1As shown, this application provides a carbon capture device. An embodiment of the carbon capture device includes: a dust removal device 10, a membrane separation device 20, multiple absorption towers 30, and a regeneration tower 40. The membrane separation device 20 is connected to the dust removal device 10. When the raw flue gas passes through the dust removal device 10, the dust removal device 10 can remove dust and particulate matter from the raw flue gas. The membrane separation device 20 can increase the carbon dioxide concentration. Multiple absorption towers 30 are connected sequentially from upstream to downstream. Each absorption tower 30 has a flue gas inlet 31, a clean flue gas inlet 32, a first liquid inlet 33, and a first liquid outlet 34. The flue gas inlet 31 of the first absorption tower 30 is connected to the membrane separation device 20. The clean flue gas inlet 32 ​​of the preceding absorption tower 30 (the upstream absorption tower among two adjacent absorption towers) is connected to the flue gas inlet 31 of the following absorption tower 30 (the downstream absorption tower among 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] The carbon capture device using the technical solution of this embodiment includes: a dust removal device 10, a membrane separation device 20, multiple absorption towers 30, and a regeneration tower 40. Each absorption tower 30 has a storage tank corresponding to an absorbent of different concentrations. Multiple absorption towers 30 are connected sequentially from upstream to downstream, enabling step-by-step transfer and regeneration of the absorbent, enhancing solvent stratification, reducing the mixing of heavy and light phases, and lowering heat consumption during regeneration. Therefore, the technical solution of this embodiment effectively solves the problem in related technologies where the heavy and light phases of the solvent mix together, leading to high energy consumption during regeneration.

[0030] like Figure 1 As shown, there are multiple regeneration towers 40 connected sequentially from upstream to downstream. The second inlet 41 of the first regeneration tower 40 is connected to the first outlet 34 of each absorption tower 30. The second outlet 42 of the preceding regeneration tower 40 is connected to the second inlet 41 of the following regeneration tower 40. The second outlet 42 of the last regeneration tower 40 is connected to the first inlet 33 of each absorption tower 30. The raw flue gas passes through an electrostatic precipitator to remove particulate matter. The clean flue gas enters a membrane separator, where carbon dioxide is enriched and discharged to the subsequent absorption towers 30. The enriched carbon dioxide enters the absorption towers 30 and is absorbed by the absorbent in stages. The enriched liquid is stored in the storage tanks of the absorption towers 30 in stages. The enriched liquid then enters the regeneration towers for regeneration. This decoupled absorption-desorption process allows for the generation of electricity using off-peak electricity and reduces the unit cost and energy consumption of carbon dioxide capture.

[0031] In this application, "multiple" refers to two or more items.

[0032] like Figure 1 As shown, the carbon capture device also includes a first connecting pipe 50 and multiple first branch pipes 51. The first end of the first connecting pipe 50 is connected to the second outlet 42 of the last regeneration tower 40, and the second end of the first connecting pipe 50 is connected to the first inlet 33 of the first absorption tower 30 through a first branch pipe 51. The first connecting pipe 50 is connected to the first inlet 33 of the remaining absorption towers 30 one by one through the remaining first branch pipes 51. Each first branch pipe 51 is equipped 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 pipe 50, so that the lean liquid flowing into each absorption tower 30 can flow smoothly into the storage tank of the absorption tower 30, improve the phase separation effect, and make the static liquid surface phase separation position clear without the disturbance caused by droplets.

[0033] like Figure 1 As shown, each absorption tower 30 is equipped with a first liquid level sensor 63 at its bottom, and the first control valve 52 is a first solenoid valve. The carbon capture device also includes a controller, and both the first liquid level sensor 63 and the first solenoid valve are connected to the controller. The first liquid level sensor 63 can detect the liquid level at the bottom of each absorption tower 30. After multiple absorptions and regeneration, the liquid level rises from low to high until the heavy phase liquid level is reached.

[0034] like Figure 1 As shown, the first connecting pipe 50 is connected to the last regeneration tower 40 via a third connecting pipe 55, on which a reboiler 56 is connected. The reboiler 56 is used to heat the lean liquid flowing from the first connecting pipe 50 and desorb carbon dioxide. The desorbed carbon dioxide gas enters subsequent processing steps, ready for storage or utilization. The decoupled absorption-desorption process allows operation during off-peak hours, reducing operating costs.

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

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

[0037] The absorbent should be a chemically stable solvent with a strong carbon dioxide absorption capacity.

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

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

[0040] like Figure 1As shown, the first outlet 34 of each absorption tower 30 is connected to the second inlet 41 of the first regeneration tower 40 via a second branch pipe 53. Each second branch pipe 53 is equipped with a second control valve 54. The second control valve 54 ensures continuous solution feeding into the regeneration tower and allows solution to be pumped from each absorption tower 30 into the first regeneration tower. This results in low gas content, good regeneration effect, shorter overall heating time, and fewer thermal degradation products.

[0041] like Figure 1 As shown, a second liquid level sensor 64 is installed at the bottom of each regeneration tower 40, and the second control valve 54 is a second solenoid valve. The carbon capture device also includes a controller, and both the second liquid level sensor 64 and the second solenoid valve are 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 determine the heavy phase liquid level but also the position of the phase separation interface, facilitating gradual regeneration from concentrated to dilute.

[0042] The controller configuration in this embodiment facilitates automated control of the carbon capture device, 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 separator membrane 22. The separator membrane 22 divides the container 21 into an enrichment chamber and a permeation chamber. The container 21 is provided with an inlet 23 communicating with the permeation chamber, and the inlet 23 is connected to the flue gas inlet 31 of the first absorption tower 30. The container 21 is also provided with an outlet 24 communicating with the enrichment chamber. The enrichment chamber collects enriched carbon dioxide gas that permeates through the separator membrane 22, while the permeation chamber stores other gases that have not permeated through the separator membrane 22. The membrane separation technology using the separator membrane 22 significantly increases the carbon dioxide loading capacity and effectively improves the carbon dioxide capture efficiency.

[0044] like Figure 1 As shown, a coil-type heat exchanger connected to the second outlet 42 is installed inside the regeneration tower 40. The coil-type heat exchanger is used to heat and regenerate the absorbent, improving thermal efficiency and reducing thermal degradation products. The regenerated solution is transported back to the storage tank of the multiple absorber towers 30 through the first connecting pipe 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 flue gas inlet 31 of the first absorption tower 30 and the membrane separation device 20. In order to provide kinetic energy for the lean liquid desorbed from the second outlet 42, the second outlet 42 is connected to the first inlet 33 of each absorption tower 30 through the second pump body 62.

[0046] A carbon capture device includes: a dust removal device 10; a membrane separation device 20 connected to the dust removal device 10; multiple absorption towers 30 connected sequentially from upstream to downstream, each absorption tower 30 having a flue gas inlet 31, a clean flue gas inlet 32, a first liquid inlet 33, and a first liquid outlet 34, wherein the flue gas inlet 31 of the first absorption tower 30 is connected to the membrane separation device 20, and the clean flue gas inlet 32 ​​of the first absorption tower 30 and the flue gas inlet 31 of the second absorption tower 30 in two adjacent absorption towers 30 are connected; and 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 this invention removes dust and particulate matter from the raw flue gas using a dust removal device 10 and a membrane separation device 20 to increase the carbon dioxide concentration, thereby reducing the energy consumption of subsequent absorption processes. The arrangement of multiple absorption towers 30 allows the absorption process to proceed in stages, with each tower containing a different concentration of absorbent liquid, enabling more effective carbon dioxide capture. The regeneration tower 40 desorbs the rich absorbent liquid after absorption, releasing carbon dioxide, and simultaneously regenerates the absorbent liquid for recycling. This design principle reduces the mixing of heavy and light phase solvents through staged absorption and regeneration, lowering heat consumption during regeneration and thus improving the overall energy efficiency and economy of the carbon capture device. The implementation results in a significantly improved carbon dioxide capture efficiency and reduced unit carbon dioxide capture cost and energy consumption. Application scenarios include, but are not limited to, flue gas treatment in large-scale, emission-difficult industries such as power plants and cement plants, and it is particularly suitable for capturing low-concentration carbon dioxide.

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

[0049] The staged design of regeneration tower 40 allows the absorbent to be regenerated at different concentrations, which helps improve the efficiency of the regeneration process and reduce energy consumption. The first regeneration tower 40 receives the rich solution from absorption tower 30. After heating and desorbing carbon dioxide, the lean solution is transported to subsequent regeneration towers 40 for further regeneration until it is completely regenerated. Then, it returns to absorption tower 30 through the first connecting pipe 50. The principle of this design is to utilize the different heat demands of absorbents at different concentrations during the regeneration process, achieving optimized energy utilization through staged regeneration. The implementation effect is a more efficient regeneration process, significantly reducing the heat consumption per unit of carbon dioxide regeneration. The main application scenarios are in industrial facilities requiring large-scale carbon dioxide capture, such as thermal power plants and chemical plants. Staged regeneration can effectively reduce operating costs and improve economic efficiency.

[0050] The carbon capture device also includes a first connecting pipe 50 and a plurality of first branch pipes 51. The first end of the first connecting pipe 50 is connected to the second outlet 42 of the last regeneration tower 40. The second end of the first connecting pipe 50 is connected to the first inlet 33 of the first absorption tower 30 through a first branch pipe 51. The first connecting pipe 50 is connected to the first inlet 33 of the remaining absorption towers 30 one by one through the remaining first branch pipes 51. Each first branch pipe 51 is provided with a first control valve 52.

[0051] The design of the control system is a key part of this invention, ensuring the precise transfer of the absorbent between the absorption tower 30 and the regeneration tower 40. The first control valve 52 controls the flow rate of the lean absorbent from the regeneration tower 40 to the absorption tower 30, guaranteeing a smooth absorption process. This design principle avoids excessive or insufficient absorbent flow through precise flow control, thereby improving absorption and regeneration efficiency. The implementation results in more stable operation of the entire carbon capture device, adapting to different operating conditions. The application scenario is in large-scale carbon capture systems requiring automated operation. Through the control system, 24-hour uninterrupted high-efficiency operation can be achieved, reducing the need for manual intervention and improving system reliability and safety.

[0052] Each of the absorption towers 30 is provided with a first liquid level sensor 63 at its bottom. The first control valve 52 is a first solenoid valve. The carbon capture device also includes a controller. The first liquid level sensor 63 and the first solenoid valve are both connected to the controller.

[0053] The combined use of a level sensor and a solenoid valve is key to achieving precise control of the absorbent liquid. The first level sensor 63 monitors the liquid level at the bottom of the absorption tower 30 in real time. When the level reaches a preset value, the controller automatically adjusts the opening of the first solenoid valve to control the inflow of lean liquid, ensuring the liquid level in the absorption tower 30 remains stable within the optimal operating range. This design utilizes the real-time monitoring function of the level sensor and the rapid response characteristics of the solenoid valve to achieve automated control, improving system stability and efficiency. The implementation results in more precise transfer of the absorbent liquid, reduced unnecessary energy consumption, and improved carbon capture efficiency. The application scenario is in industrial carbon capture systems requiring high-precision control; the combination of a level sensor and a solenoid valve enables precise control of the absorbent liquid, thereby improving the overall system performance.

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

[0055] The reboiler 56 is a crucial component of the regeneration process. It heats the lean liquor exiting the regeneration tower 40 to the temperature required for carbon dioxide desorption. The principle behind this design is to utilize the heating function of the reboiler 56 to increase the temperature of the lean liquor, thereby promoting carbon dioxide desorption and improving regeneration efficiency. The result is a more efficient regeneration process and a significant reduction in the heat consumption per unit of carbon dioxide. Application scenarios include industrial facilities requiring large-scale carbon dioxide regeneration, such as thermal power plants and chemical plants. The reboiler 56 can effectively reduce operating costs and improve economic efficiency. The process involves the lean liquor exiting the regeneration tower 40 and entering the reboiler 56 through the third connecting pipe 55. The reboiler 56 heats the lean liquor to the set temperature, and then the lean liquor returns to the absorption tower 30 through the first connecting pipe 50 and the first branch pipe 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 pipe 53, and a second control valve 54 is provided on each second branch pipe 53.

[0057] The management of control valves by the control system is crucial to ensuring the smooth operation of the regeneration process. The second control valve 54 controls the flow rate of the rich liquid from the absorber 30 to the regeneration tower 40, ensuring the continuity and stability of the regeneration process. This design principle involves precise control of the second control valve 54 by the control system, preventing excessive or insufficient rich liquid flow, thereby improving regeneration efficiency and absorbent recycling efficiency. The result is a more efficient regeneration process and a significant reduction in the heat consumption per unit of carbon dioxide during regeneration. The application scenario is in large-scale carbon capture systems requiring automated operation. By managing the control valves through the control system, the regeneration process can be automated, reducing the need for manual intervention and improving system reliability and safety.

[0058] Each of the regeneration towers 40 is provided with a second liquid level sensor 64 at its bottom. The second control valve 54 is a second solenoid valve. The carbon capture device also includes a controller. The second liquid level sensor 64 and the second solenoid valve are both connected to the controller.

[0059] The integrated management function of the controller is the core of achieving automated operation of the entire carbon capture device. It receives signals from the first liquid level sensor 63 and the second liquid level sensor 64, and adjusts the opening of the first and second solenoid valves according to the signals, thereby controlling the flow rate of lean and rich solutions and ensuring the smooth operation of the absorption and regeneration process. The principle of this design is to utilize the integrated management function of the controller to achieve unified control of multiple sensors and solenoid valves, improving the system's automation level and efficiency. The implementation effect is that the carbon capture device operates more stably, can adapt to different operating conditions, and reduces operating costs. The application scenario is in large-scale carbon capture systems requiring 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 system performance and economic benefits.

[0060] The membrane separation device 20 includes a container 21 and a separator membrane 22. The separator membrane 22 divides the container 21 into an enrichment chamber and a permeation chamber. The container 21 is provided with an air inlet 23 that communicates with the permeation chamber. The air inlet 23 is connected to the flue gas inlet 31 of the first absorption tower 30. The container 21 is also provided with an air outlet 24 that communicates with the enrichment chamber.

[0061] The structure and function of the membrane separation device 20 are key to improving carbon dioxide capture efficiency. The separator membrane 22 inside the container 21 selectively allows carbon dioxide to permeate, enriching it in the enrichment chamber, while other gases remain in the permeation chamber. This design utilizes the gas separation characteristics of the separator membrane 22 to increase the concentration of carbon dioxide, thereby reducing the energy consumption of subsequent absorption processes. The implementation effect is a significant improvement in carbon dioxide capture efficiency and a reduction in the unit capture cost and energy consumption of carbon dioxide. Application scenarios include industrial facilities requiring increased carbon dioxide concentration, such as thermal power plants and chemical plants. By installing the membrane separation device 20, carbon dioxide capture efficiency can be effectively improved, operating costs reduced, and economic benefits increased.

[0062] The regeneration tower 40 is equipped with a coil heat exchanger that is connected to the second liquid outlet 42.

[0063] The heat exchanger design inside the regeneration tower 40 is key to improving regeneration efficiency and reducing energy consumption. The coil-type heat exchanger efficiently heats the lean solution, promoting carbon dioxide desorption while reducing the formation of thermal degradation products. This design utilizes the high heat exchange characteristics of the coil-type heat exchanger to increase the temperature of the lean solution, thereby promoting carbon dioxide desorption and improving regeneration efficiency. The result is a more efficient regeneration process, significantly reducing the heat consumption per unit of carbon dioxide. Application scenarios include industrial facilities requiring large-scale carbon dioxide regeneration, such as thermal power plants and chemical plants. By installing coil-type heat exchangers, operating costs can be effectively reduced, and economic benefits improved.

[0064] A first pump body 61 is connected between the flue gas 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 placement and function of the pumps are crucial for ensuring smooth fluid flow in the carbon capture device. The first pump 61 and the second pump 62 provide the necessary transport kinetic energy for enriched carbon dioxide and lean liquid, ensuring a smooth flow from one component to another. This design utilizes the pump's transport function to power the fluid, ensuring the continuity and stability of the absorption and regeneration processes. The result is more stable operation of the carbon capture device, adaptability to different operating conditions, and reduced operating costs. Application scenarios include large-scale carbon capture systems requiring high-precision control and automated operation. The pump placement enables smooth fluid transport, thereby improving the overall system performance and economic efficiency. In practice, when enriched carbon dioxide flows out of the membrane separation unit 20, the first pump 61 provides transport kinetic energy, allowing it to smoothly enter the first absorption tower 30; when lean liquid flows out of the regeneration tower 40, the second pump 62 provides transport kinetic energy, allowing it to smoothly return to the absorption tower 30 for a new round of absorption.

[0066] In the description of this invention, it should be understood that the orientation or positional relationship indicated by directional terms such as "front, back, up, down, left, right", "horizontal, vertical, horizontal" and "top, bottom" is generally based on the orientation or positional relationship shown in the accompanying drawings, and is only for the convenience of describing this invention and simplifying the description. Unless otherwise stated, these directional terms 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 on the scope of protection of this invention; the directional terms "inner" and "outer" refer to the inner and outer contours relative to the outline of each component itself.

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

[0068] Furthermore, it should be noted that the use of terms such as "first" and "second" to define components is merely for the purpose of distinguishing the corresponding components. Unless otherwise stated, the above terms have no special meaning and therefore should not be construed as limiting the scope of protection of this invention.

[0069] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A carbon capture device, characterized in that, include: Dust removal device (10); A membrane separation device (20) is connected to the dust removal device (10); Multiple absorption towers (30) are connected sequentially from upstream to downstream. Each absorption tower (30) has a flue gas inlet (31), a clean flue gas inlet (32), a first liquid inlet (33), and a first liquid outlet (34). The flue gas inlet (31) of the first absorption tower (30) is connected to the membrane separation device (20). The clean flue gas inlet (32) of the first absorption tower (30) and the flue gas inlet (31) of the second absorption tower (30) of two adjacent absorption towers (30) are connected. 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 of the absorption towers (30), and the second liquid outlet (42) is connected to the first liquid inlet (33) of each of the absorption towers (30). There are multiple regeneration towers (40), which are connected sequentially from upstream to downstream. The second inlet (41) of the first regeneration tower (40) is connected to the first outlet (34) of each absorption tower (30). The second outlet (42) of the first regeneration tower (40) and the second inlet (41) of the second regeneration tower (40) are connected in two adjacent regeneration towers. The second outlet (42) of the last regeneration tower (40) is connected to the first inlet (33) of each absorption tower (30). The carbon capture device further includes a first connecting pipe (50) and a plurality of first branch pipes (51). The first end of the first connecting pipe (50) is connected to the second outlet (42) of the last regeneration tower (40). The second end of the first connecting pipe (50) is connected to the first inlet (33) of the first absorption tower (30) through a first branch pipe (51). The first connecting pipe (50) is connected to the first inlet (33) of the remaining absorption towers (30) one by one through the remaining first branch pipes (51). Each first branch pipe (51) is provided with a first control valve (52). Each of the absorption towers (30) has a storage tank corresponding to an absorbent of different concentrations. Multiple absorption towers (30) are connected sequentially from upstream to downstream to realize the step-by-step transfer and regeneration of the absorbent. The first outlet (34) of each of the absorption towers (30) is connected to the second inlet (41) of the first regeneration tower (40) through a second branch pipe (53), and a second control valve (54) is provided on each of the second branch pipes (53). Each of the regeneration towers (40) is provided with a second liquid level sensor (64) at the bottom. The second control valve (54) is a second solenoid valve. Both the second liquid level sensor (64) and the second solenoid valve are connected to the controller. The second liquid level sensor (64) is used to detect the liquid level height at the bottom of each of the regeneration towers (40). Each second liquid level sensor (64) is used to determine the position of the phase separation interface.

2. The carbon capture device according to claim 1, characterized in that, Each of the absorption towers (30) is provided with a first liquid level sensor (63) at the bottom, the first control valve (52) is a first solenoid valve, the carbon capture device also includes a controller, and the first liquid level sensor (63) and the first solenoid valve are both connected to the controller.

3. The carbon capture device according to claim 1, characterized in that, The first connecting pipe (50) is connected to the last regeneration tower (40) via a third connecting pipe (55), and a reboiler (56) is connected to the third connecting pipe (55).

4. The carbon capture device according to claim 1, characterized in that, The membrane separation device (20) includes a container (21) and a separator membrane (22). The separator membrane (22) divides the container (21) into an enrichment chamber and a permeation chamber. The container (21) is provided with an air inlet (23) communicating with the permeation chamber. The air inlet (23) is connected to the flue gas inlet (31) of the first absorption tower (30). The container (21) is also provided with an air outlet (24) communicating with the enrichment chamber.

5. The carbon capture device according to claim 1, characterized in that, The regeneration tower (40) is equipped with a coil heat exchanger connected to the second liquid outlet (42).

6. The carbon capture device according to claim 1, characterized in that, A first pump body (61) is connected between the flue gas 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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