A flue gas carbon dioxide recovery system

Abstract

The utility model relates to a kind of flue gas carbon dioxide recovery system, it includes adsorption-desorption unit, cooling separation unit, gas inlet unit and power device, adsorption-desorption unit includes two groups of adsorption-desorption components arranged side by side, and each group of adsorption-desorption components includes adsorption tower and temperature control equipment;Cooling separation unit includes two groups of cooling separation components with adsorption-desorption component corresponding arrangement, and each group of cooling separation component inlet and corresponding adsorption tower can selectively communicate;Gas inlet unit includes controllably with any adsorption tower gas inlet selective communication or cut-off process gas inlet pipeline and controllably with any adsorption tower gas outlet selective communication or cut-off purge gas inlet pipeline.The flue gas carbon dioxide recovery system can regulate and control the temperature, pressure in adsorption tower, to couple temperature swing adsorption and pressure swing adsorption mechanism in the same adsorption tower;While double-tower integrated design makes adsorption and desorption process parallel, realizes the continuous, stable, efficient operation of entire system.

Description

Technical Field

[0001] This utility model relates to the field of carbon dioxide recovery technology, specifically to a flue gas carbon dioxide recovery system. Background Technology

[0002] Currently, the main technical routes for separating and recovering CO2 from flue gas include absorption, membrane separation, cryogenic distillation, and adsorption. Among these, physical adsorption has attracted widespread attention due to its advantages such as relatively low energy consumption, flexible process, and no corrosive waste liquid generation. The core of physical adsorption lies in utilizing the selective adsorption capacity of solid adsorbents (such as activated carbon, molecular sieves, and metal-organic framework materials) for CO2 in gas mixtures, and restoring the adsorbent's activity through specific regeneration methods, thereby achieving a cyclical operation.

[0003] Based on the different adsorbent regeneration methods, physical adsorption methods are mainly divided into two categories: Firstly, Pressure Swing Adsorption (PSA): This technology achieves adsorption and desorption by periodically changing the system pressure near the ambient temperature. CO2 is adsorbed under high pressure (or atmospheric pressure) and then desorbed and regenerated under low pressure. PSA technology has advantages such as short cycle time, fast operation speed, and ease of automation, and is widely used in industry. However, PSA technology has significant limitations when treating feed gases with high humidity and containing strongly adsorbable impurities, such as flue gas: water vapor competes with CO2 for adsorption sites, and may even cause irreversible failure of some adsorbents (such as molecular sieves); at the same time, simple depressurization desorption is often not thorough enough, leaving some strongly adsorbed components in the adsorbent bed, causing the adsorption capacity to gradually decrease with the operating cycle, affecting long-term separation efficiency and product purity.

[0004] Second, Temperature Variable Adsorption (TSA): This technology achieves regeneration by periodically changing the system temperature under constant pressure. Adsorption typically occurs at a lower temperature, and then the bed is heated to a higher temperature by an external heat source (such as steam or electric heating), causing the adsorbed CO2 to desorb. The advantage of TSA technology is its thorough desorption, effectively removing strongly adsorbed impurities, including water vapor, and restoring the original capacity of the adsorbent. It is particularly suitable for processing feed gases with complex compositions. However, its main disadvantages are the large thermal inertia required for the heating and cooling processes, resulting in long cycle times (usually several hours), large equipment size, and high energy consumption, making it difficult to achieve continuous, large-scale, rapid processing.

[0005] In summary, both existing PSA and TSA technologies have inherent bottlenecks that are difficult to overcome. Therefore, there is an urgent need in this field for a novel adsorption separation system that can combine the advantages of both technologies to achieve more efficient, economical, and stable recovery of CO2 from flue gas. Utility Model Content

[0006] The purpose of this invention is to provide a novel flue gas carbon dioxide recovery system.

[0007] To achieve the above objectives, the technical solution adopted by this utility model is as follows: This utility model provides a flue gas carbon dioxide recovery system, which includes: The adsorption-desorption unit includes two sets of adsorption-desorption components arranged in parallel for continuous gas processing. Each set of adsorption-desorption components includes an adsorption tower and a temperature control device. The adsorption tower has an inner chamber for containing the adsorption medium and a heating jacket surrounding the inner chamber. The inner chamber has a gas inlet and a gas outlet, and the heating jacket has a heat medium inlet and a heat medium outlet. The temperature control device is connected to the heat medium inlet and the heat medium outlet to provide heating medium to the adsorption tower and form a circulation loop for the heating medium. The cooling separation unit includes two sets of cooling separation components that correspond one-to-one with the two sets of adsorption-desorption components. The inlet of each set of cooling separation components is selectively connected to the corresponding adsorption tower through a first pipeline. An intake unit includes a process gas intake pipeline and a purge gas intake pipeline, wherein the process gas intake pipeline is controllably selectively connected to or disconnected from the gas inlet of any of the adsorption towers, and the purge gas intake pipeline is controllably selectively connected to or disconnected from the gas outlet of any of the adsorption towers; and, A power unit is located on the process gas inlet pipe; The system is configured to: when executing an adsorption-desorption procedure, control the process gas inlet pipeline to supply the flue gas to be treated to one adsorption tower for adsorption; and simultaneously control the purge gas inlet pipeline to supply gas to another adsorption tower so that the desorbed gas is discharged through the corresponding cooling and separation components.

[0008] In some embodiments, the cooling separation assembly includes a cooler and a gas-water separator. The inlet of the cooler is connected to the corresponding first pipeline, and its outlet is connected to the inlet of the gas-water separator. The gas-water separator has a drain outlet and an exhaust outlet, and an exhaust pipeline is connected to the exhaust outlet.

[0009] In some embodiments, the exhaust pipeline includes a main exhaust pipe connected to the exhaust port, a first exhaust branch pipe and a second exhaust branch pipe located at the end of the main exhaust pipe, and an exhaust three-way solenoid valve disposed between the main exhaust pipe and the first and second exhaust branch pipes. Further, a carbon dioxide analyzer is installed on the main exhaust pipe; when the carbon dioxide analyzer detects that the carbon dioxide purity in the pipeline reaches a preset purity, the exhaust three-way solenoid valve connects the first exhaust branch pipe to the main exhaust pipe and disconnects the second exhaust branch pipe from the main exhaust pipe; when the carbon dioxide analyzer detects that the carbon dioxide purity in the pipeline does not reach the preset purity, the exhaust three-way solenoid valve connects the second exhaust branch pipe to the main exhaust pipe and disconnects the first exhaust branch pipe from the main exhaust pipe.

[0010] In some embodiments, the cooler is provided with a cooling channel for gas passage and a cooling jacket covering the outside of the cooling channel. The cooling channel has a gas inlet and a gas outlet. The gas inlet of the cooling channel is connected to a corresponding first pipeline, and the gas outlet of the cooling channel is connected to the feed port of a corresponding gas-water separator through a pipeline. The cooling jacket has a refrigerant inlet and a refrigerant outlet. The cooling separation unit further includes a cooling device connected to the refrigerant inlet and refrigerant outlet for providing cooling medium into the cooling jacket and forming a cooling medium circulation loop.

[0011] In some specific implementations, the two sets of cooling separation components share a single cooling device.

[0012] In some embodiments, the purge gas inlet pipeline includes a main purge gas inlet pipe, a first purge gas inlet branch pipe and a second purge gas inlet branch pipe located at the end of the main purge gas inlet pipe, and a first purge gas inlet three-way solenoid valve located between the main purge gas inlet pipe and the first and second purge gas inlet branch pipes; the main purge gas inlet pipe has two parallel arranged pipes, one of which is equipped with a pressure transmitter, and the other is equipped with a valve to control the on / off state of the main purge gas inlet pipe. A one-way valve is installed after the confluence point; a second purge gas inlet three-way solenoid valve is installed between the first purge gas inlet branch pipe and the first pipeline. By switching the second purge gas inlet three-way solenoid valve, the first purge gas inlet branch pipe and the first pipeline can be selectively connected to the same adsorption tower; a third purge gas inlet three-way solenoid valve is installed between the second purge gas inlet branch pipe and another first pipeline. By switching the third purge gas inlet three-way solenoid valve, the second purge gas inlet branch pipe and another first pipeline can be selectively connected to another adsorption tower.

[0013] In some embodiments, the system further includes a heat exchanger and a spray tower disposed on the process gas inlet pipeline.

[0014] In some embodiments, the heat exchanger is provided with a first inlet, a first outlet, a second inlet, and a second outlet; the arrangement of the process gas inlet pipeline includes: the gas first enters the heat exchanger through the first inlet, exits through the first outlet, and then enters the spray tower; subsequently, the gas flows out of the spray tower, re-enters the heat exchanger through the second inlet, and finally exits through the second outlet.

[0015] In some embodiments, the process gas inlet pipeline includes a main process gas inlet pipe, a first process gas inlet branch pipe and a second process gas inlet branch pipe located at the end of the main process gas inlet pipe, and a first process gas inlet three-way solenoid valve located between the main process gas inlet pipe and the first and second process gas inlet branch pipes; the main process gas inlet pipe has two parallel-arranged pipes, one of which is equipped with a pressure transmitter, and the other is equipped with a valve to control the passage of the main process gas inlet pipe. A one-way valve is installed after the confluence point; a second process gas inlet three-way solenoid valve is installed between the first process gas inlet branch pipe and the first pipeline. By switching the second process gas inlet three-way solenoid valve, either the first process gas inlet branch pipe or the first pipeline can be connected to the same adsorption tower; a third process gas inlet three-way solenoid valve is installed between the second process gas inlet branch pipe and another first pipeline. By switching the third process gas inlet three-way solenoid valve, either the second process gas inlet branch pipe or the other first pipeline can be connected to another adsorption tower.

[0016] In some embodiments, the adsorption medium is a modified hydrotalcite material.

[0017] Due to the application of the above technical solution, this utility model has the following advantages compared with the prior art: The flue gas carbon dioxide recovery system of this invention can regulate the temperature and pressure inside the adsorption tower, and couple the temperature swing adsorption and pressure swing adsorption mechanisms within the same adsorption tower, thereby releasing the optimal performance of the adsorbent. At the same time, the dual-tower integrated design allows the adsorption and desorption processes to be carried out in parallel, realizing the continuous, stable and efficient operation of the entire system, and significantly improving energy efficiency and economic benefits. Attached Figure Description

[0018] Figure 1 A schematic diagram of the flue gas carbon dioxide recovery system provided in Example 1; Figure 2 This is a schematic diagram of the adsorption tower provided in Example 1; Figure 3An external frame diagram of the flue gas carbon dioxide recovery system provided in Example 1; Among them, 1. Adsorption tower; 11. Inner chamber; 12. Heating jacket; 2. Temperature control equipment; 3. Cooler; 4. Gas-liquid separator; 5. Cooling equipment; 6. Pump; 7. Heat exchanger; 8. Spray tower; V101, First ball valve; V102, Second ball valve; V103, Third ball valve; V104, First check valve; V105, Fourth ball valve; V106, Fifth ball valve; V107, Sixth ball valve; V108, Second check valve; BV101, First process gas inlet three-way solenoid valve; BV102, Second process gas inlet three-way solenoid valve; BV103, Third process gas inlet three-way solenoid valve; BV104, Outlet three-way solenoid valve; BV105, Second purge gas inlet three-way solenoid valve; BV106, First purge gas inlet three-way solenoid valve; BV107, Third purge gas inlet three-way solenoid valve; BV108, Outlet three-way solenoid valve; PIC1-PIC2, ​​Pressure transmitters; FT1-FT2, Mass flow meters; AIA1-AIA2, Carbon dioxide analyzers; a. Air inlet; b. Air outlet; c. Exhaust gas outlet; d. Purge gas outlet; e. Refrigerant inlet; f. Refrigerant outlet. Detailed Implementation

[0019] The present invention will be further described below with reference to the embodiments shown in the accompanying drawings.

[0020] In the following description, only certain exemplary embodiments are briefly described. As those skilled in the art will recognize, the described embodiments can be modified in various ways without departing from the spirit or scope of the present invention. Therefore, the drawings and description are considered to be exemplary in nature and not restrictive.

[0021] In the description of the embodiments of this utility model, it should be understood that the descriptions of directions such as up and down, left and right, front and back, inside and outside are all based on Figure 1 The orientation is defined.

[0022] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of embodiments of this utility model, "a plurality of" means two or more, unless otherwise explicitly specified.

[0023] In this embodiment of the invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can include direct contact between the first and second features, or contact between the first and second features through another feature between them. Furthermore, "above," "over," and "on top" of the second feature includes the first feature directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature includes the first feature directly below or diagonally below the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature.

[0024] The following disclosure provides many different implementations or examples for different structures of the embodiments of the present invention. To simplify the disclosure of the embodiments of the present invention, specific examples of components and arrangements are described below. Of course, these are merely examples and are not intended to limit the embodiments of the present invention. Furthermore, reference numerals and / or reference letters may be repeated in different examples of the embodiments of the present invention; such repetition is for simplification and clarity and does not in itself indicate a relationship between the various implementations and / or arrangements discussed.

[0025] Example 1: A flue gas carbon dioxide recovery system, such as Figure 1 As shown, it includes an adsorption / desorption unit, a cooling / separation unit, an air intake unit, and a power unit.

[0026] The adsorption-desorption unit includes two sets of adsorption-desorption components arranged in parallel for continuous gas processing. Each set of adsorption-desorption components includes an adsorption tower 1 and a temperature control device 2. The adsorption tower 1 has an inner chamber 11 for containing the adsorption medium and a heating jacket 12 surrounding the inner chamber. The inner chamber 11 has a gas inlet and a gas outlet, and the heating jacket 12 has a heat medium inlet and a heat medium outlet. The temperature control device 2 is connected to the heat medium inlet and outlet, and is used to provide heating medium to the adsorption tower 1 and form a circulation loop for the heating medium.

[0027] As a preferred option, such as Figure 2As shown, the core of the inner chamber 11 is a stainless steel tube, with both ends sealed by detachable flanges. Each flange is fitted with a compression fitting, serving as the gas inlet and outlet of the inner chamber 11, respectively. The heating jacket 12 adopts a concentric sleeve structure, consisting of two stainless steel tubes of different diameters. The annular ends of the two tubes are welded together by a sealing ring plate, forming a sealed annular heating channel. Two compression fittings are welded to the outer tube wall of the jacket, serving as the heat medium inlet and outlet, respectively. The adsorption medium can be a modified hydrotalcite material, such as Mg-Al based hydrotalcite or hydrotalcite / carbon composite materials. This type of material has an adjustable layer structure, abundant surface alkaline sites, and good thermal stability. It can achieve high-capacity, high-selectivity capture and efficient desorption of CO2 through controlled chemical adsorption under coupled temperature and pressure control. The heating medium is a high-heat-capacity and high-boiling-point heat transfer oil. This medium can provide uniform, stable, and controllable heating to the adsorption medium bed during circulation.

[0028] The cooling separation unit includes two sets of cooling separation components, each corresponding to one of the two sets of adsorption-desorption components. The inlet of each cooling separation component is selectively connected to the corresponding adsorption tower 1 via a first pipeline. Each cooling separation component includes a cooler 3 and a gas-liquid separator 4; wherein the inlet of the cooler 3 is connected to the corresponding first pipeline, and its outlet is connected to the inlet of the gas-liquid separator 4. The gas-liquid separator 4 has a liquid drain port and an exhaust port, with an exhaust pipeline connected to the exhaust port.

[0029] As a preferred embodiment, the cooler 3 is provided with a cooling channel for gas passage and a cooling jacket covering the outside of the cooling channel. The cooling channel has a gas inlet and a gas outlet. The gas inlet of the cooling channel is connected to a corresponding first pipeline, and the gas outlet of the cooling channel is connected to the feed inlet of the corresponding gas-water separator 4 via a pipeline. The cooling jacket has a refrigerant inlet e and a refrigerant outlet f. The cooling separation unit also includes a cooling device 5, which is connected to the refrigerant inlet e and the refrigerant outlet f, for providing cooling medium into the cooling jacket and forming a cooling medium circulation loop. In this embodiment, the two sets of cooling separation components share one cooling device 5. In other embodiments, the two sets of cooling separation components may also use a single cooling device 5 independently.

[0030] Furthermore, the exhaust pipeline includes a main exhaust pipe connected to the exhaust port, a first exhaust branch pipe and a second exhaust branch pipe located at the end of the main exhaust pipe, and an exhaust three-way solenoid valve BV104 / BV108 located between the main exhaust pipe and the first and second exhaust branch pipes. A carbon dioxide analyzer AIA1 / AIA2 is installed on the main exhaust pipe. When the carbon dioxide analyzer AIA1 / AIA2 detects that the carbon dioxide purity in the pipeline reaches a preset purity, the exhaust three-way solenoid valve BV104 / BV108 connects the first exhaust branch pipe to the main exhaust pipe and disconnects the second exhaust branch pipe from the main exhaust pipe, allowing the process gas to be discharged through exhaust port b. When the carbon dioxide analyzer AIA1 / AIA2 detects that the carbon dioxide purity in the pipeline does not reach the preset purity, the exhaust three-way solenoid valve BV104 / BV108 connects the second exhaust branch pipe to the main exhaust pipe and disconnects the first exhaust branch pipe from the main exhaust pipe, allowing the process gas to be discharged through exhaust port c.

[0031] The air intake unit includes a process gas intake line and a purge gas intake line. The process gas intake line can be selectively connected to or disconnected from the gas inlet of any adsorption tower 1, and the purge gas intake line can be selectively connected to or disconnected from the gas outlet of any of the adsorption towers 1.

[0032] Specifically, the process gas inlet pipeline includes a main process gas inlet pipe, a first process gas inlet branch pipe and a second process gas inlet branch pipe located at the end of the main process gas inlet pipe, and a first process gas inlet three-way solenoid valve BV101 located between the main process gas inlet pipe and the first and second process gas inlet branch pipes. The main process gas inlet pipe has two parallel sections. One main process gas inlet pipe is sequentially equipped with a first ball valve V101, a pressure transmitter PIC1, a mass flow meter FT1, and a second ball valve V102. The other main process gas inlet pipe is equipped with a valve (i.e., a third ball valve V103) to control the passage of this main process gas inlet pipe. A first check valve V104 is located after the confluence of the two main process gas inlet pipes. A second process gas inlet three-way solenoid valve BV102 is installed between the first process gas inlet branch pipe and the first pipeline. By switching the second process gas inlet three-way solenoid valve BV102, either the first process gas inlet branch pipe or the first pipeline can be connected to the gas inlet of the same adsorption tower 1. A third process gas inlet three-way solenoid valve BV103 is installed between the second process gas inlet branch pipe and another first pipeline. By switching the third process gas inlet three-way solenoid valve BV103, either the second process gas inlet branch pipe or the other first pipeline can be connected to the gas inlet of another adsorption tower 1.

[0033] The purge gas inlet pipeline includes a purge gas inlet main pipe, a first purge gas inlet branch pipe and a second purge gas inlet branch pipe located at the end of the purge gas inlet main pipe, and a first purge gas inlet three-way solenoid valve BV106 located between the purge gas inlet main pipe and the first and second purge gas inlet branch pipes. The purge gas inlet main pipe has two parallel sections. One section is equipped with a fourth ball valve V105, a pressure transmitter PIC2, ​​a mass flow meter FT2, and a fifth ball valve V106 in sequence. The other section has a valve (i.e., a sixth ball valve V107) to control the on / off state of the purge gas inlet main pipe. A second check valve V108 is located after the confluence of the two purge gas inlet main pipes. A second purge gas inlet three-way solenoid valve BV105 is installed between the first purge gas inlet branch pipe and the first pipeline. By switching the second purge gas inlet three-way solenoid valve BV105, either the first purge gas inlet branch pipe or the first pipeline can be connected to the gas outlet of the same adsorption tower 1. A third purge gas inlet three-way solenoid valve BV107 is installed between the second purge gas inlet branch pipe and another first pipeline. By switching the third purge gas inlet three-way solenoid valve BV107, either the second purge gas inlet branch pipe or the other first pipeline can be connected to the gas outlet of another adsorption tower 1.

[0034] The power unit is located on the process gas inlet pipeline. In this embodiment, it is a pump 6. The system also includes a heat exchanger 7 and a spray tower 8 located on the process gas inlet pipeline. The heat exchanger 7 has a first inlet, a first outlet, a second inlet, and a second outlet; the process gas inlet pipeline is arranged such that the gas first enters the heat exchanger 7 through the first inlet, exits through the first outlet, and then enters the spray tower 8; subsequently, the gas flows out of the spray tower 8, re-enters the heat exchanger 7 through the second inlet, and finally exits through the second outlet, entering the downstream adsorption tower 1.

[0035] In an exemplary layout of this embodiment, such as Figure 3 As shown, the main components of the system are integrated within the same equipment frame. Specifically, the adsorption tower 1 is located in the upper-middle area of ​​the equipment; the temperature control device 2 is located in the lower left and lower-middle areas; and the cooling device 5 is located in the lower right area. The remaining space of the equipment can be used to accommodate other equipment or pipelines configured according to actual process requirements.

[0036] Working principle: System purging procedure: like Figure 1As shown, open the third ball valve V103, close the first ball valve V101 and the second ball valve V102, de-energize the first process gas inlet three-way solenoid valve BV101 and the second process gas inlet three-way solenoid valve BV102, energize the second purge gas inlet three-way solenoid valve BV105, and de-energize the outlet three-way solenoid valve BV104, so that the process gas inlet main pipe is connected to the adsorption tower 1 on the left, and the gas outlet of the adsorption tower 1 on the left is connected to the corresponding cooler 3. Nitrogen gas is introduced into the inlet a, passes through the heat exchanger 7 and the spray tower 8, exits again through the heat exchanger 7, and sequentially enters the adsorption tower 1 on the left, the cooler 3, and the gas-liquid separator 4, and is discharged from the exhaust port c. Purge for 10 minutes.

[0037] Open the third ball valve V103, close the first ball valve V101 and the second ball valve V102, energize the first process gas inlet three-way solenoid valve BV101, de-energize the third process gas inlet three-way solenoid valve BV103, energize the third purge gas inlet three-way solenoid valve BV107, and de-energize the outlet three-way solenoid valve BV108, connecting the process gas inlet main pipe to the adsorption tower 1 on the right, and connecting the gas outlet of the adsorption tower 1 on the right to the corresponding cooler 3. Introduce nitrogen into inlet a, which passes through heat exchanger 7 and spray tower 8, exits again through heat exchanger 7, and sequentially enters the adsorption tower 1 on the right, cooler 3, and gas-liquid separator 4, before being discharged from exhaust port c. Purge for 10 minutes.

[0038] Open the sixth ball valve V107, close the fourth ball valve V105 and the fifth ball valve V106, de-energize the first purge gas inlet three-way solenoid valve BV106 and the second purge gas inlet three-way solenoid valve BV105, energize the second process gas inlet three-way solenoid valve BV102, and de-energize the outlet three-way solenoid valve BV104. Introduce nitrogen into the purge gas port d. The nitrogen enters the adsorption tower 1 from the gas outlet on the left side and exits from the gas inlet of the adsorption tower 1. Then, it passes sequentially through the cooler 3 and the gas-liquid separator 4 on the left side, and finally exits from the waste gas port c on the left side. Purge for 5 minutes.

[0039] Open the sixth ball valve V107, close the fourth ball valve V105 and the fifth ball valve V106, energize the first purge gas inlet three-way solenoid valve BV106, de-energize the third purge gas inlet three-way solenoid valve BV107, energize the third process gas inlet three-way solenoid valve BV103, and de-energize the outlet three-way solenoid valve BV108. Introduce nitrogen into the purge gas port d. The nitrogen enters the adsorption tower 1 from the gas outlet on the right and exits from the gas inlet of the adsorption tower 1. Then, it passes sequentially through the cooler 3 and the gas-liquid separator 4 on the right, and finally exits from the exhaust port c on the right. Purge for 5 minutes.

[0040] Adsorption-desorption process: Close the third ball valve V103 and the sixth ball valve V107, and open the first ball valve V101, the second ball valve V102, the fourth ball valve V105, and the fifth ball valve V106. Adjust the mass flow meters FT1 / FT2 to achieve a flow range of 10~50 Nm³. 3 / h; Adjust the pressure of pump 6, the pressure boosting range of pump 6 is 0.1~0.6MPa.

[0041] The adsorption tower 1 on the left performs adsorption, while the adsorption tower 1 on the right performs desorption, with a running time of 30 minutes. During this time, the first process gas inlet three-way solenoid valve BV101 and the second process gas inlet three-way solenoid valve BV102 are de-energized, the third process gas inlet three-way solenoid valve BV103 is energized, the first purge gas inlet three-way solenoid valve BV106 and the second purge gas inlet three-way solenoid valve BV105 are energized, the third purge gas inlet three-way solenoid valve BV107 is de-energized, the right-side outlet three-way solenoid valve BV108 is de-energized, and the left-side outlet three-way solenoid valve BV104 can be selectively de-energized or energized. The temperature control device 2 on the left adjusts the temperature of the heating medium to 100℃ (this is just an example and can be designed according to actual needs), and the temperature control device 2 on the right adjusts the temperature of the heating medium to 300℃ (this is just an example and can be designed according to actual needs). When the CO2 purity on the left side meets the standard, the three-way solenoid valve BV104 on the left side is energized, and the process gas is discharged from outlet b; when the CO2 purity on the left side does not meet the standard, the three-way solenoid valve BV104 on the left side is de-energized, and the process gas is discharged from exhaust outlet c.

[0042] The adsorption tower 1 on the left side performs desorption, while the adsorption tower 1 on the right side performs adsorption, with a running time of 30 minutes. At this time, the first process gas inlet three-way solenoid valve BV101 is energized, the second process gas inlet three-way solenoid valve BV102 is energized, the third process gas inlet three-way solenoid valve BV103 is de-energized, the first purge gas inlet three-way solenoid valve BV106 and the second purge gas inlet three-way solenoid valve BV105 are de-energized, the third purge gas inlet three-way solenoid valve BV107 is energized, the left outlet three-way solenoid valve BV104 is de-energized, and the right outlet three-way solenoid valve BV108 can be selectively de-energized or energized. The temperature control device 2 on the left side adjusts the temperature of the heating medium to 300℃, and the temperature control device 2 on the right side adjusts the temperature of the heating medium to 100℃. When the CO2 purity on the right side meets the standard, the three-way solenoid valve BV108 on the right side is energized, and the process gas is discharged from outlet b; when the CO2 purity on the right side does not meet the standard, the three-way solenoid valve BV108 on the right side is de-energized, and the process gas is discharged from exhaust outlet c.

[0043] The above embodiments are only for illustrating the technical concept and features of this utility model, and are intended to enable those skilled in the art to understand the content of this utility model and implement it accordingly. They should not be construed as limiting the scope of protection of this utility model. All equivalent changes or modifications made in accordance with the spirit and essence of this utility model should be included within the scope of protection of this utility model.

Claims

1. A flue gas carbon dioxide recovery system, characterized in that, include: The adsorption-desorption unit includes two sets of adsorption-desorption components arranged in parallel for continuous gas processing. Each set of adsorption-desorption components includes an adsorption tower (1) and a temperature control device (2). The adsorption tower (1) has an inner chamber (11) for containing the adsorption medium and a heating jacket (12) surrounding the outer side of the inner chamber. The inner chamber (11) is provided with a gas inlet and a gas outlet, and the heating jacket (12) is provided with a heat medium inlet and a heat medium outlet. The temperature control device (2) is connected to the heat medium inlet and the heat medium outlet for providing a heating medium to the adsorption tower (1) and forming a circulation loop for the heating medium. The cooling separation unit includes two sets of cooling separation components that correspond one-to-one with the two sets of adsorption-desorption components. The inlet of each set of cooling separation components is selectively connected to the corresponding adsorption tower (1) through a first pipeline. An intake unit includes a process gas intake pipe and a purge gas intake pipe, wherein the process gas intake pipe is controllably selectively connected to or disconnected from the gas inlet of any of the adsorption towers (1), and the purge gas intake pipe is controllably selectively connected to or disconnected from the gas outlet of any of the adsorption towers (1); and, A power unit is located on the process gas inlet pipe; The system is configured to: when performing an adsorption-desorption procedure, control the process gas inlet pipeline to supply the flue gas to be treated to one adsorption tower (1) for adsorption; and at the same time control the purge gas inlet pipeline to supply gas to another adsorption tower (1) so that the desorbed gas is discharged through the corresponding cooling separation component.

2. The flue gas carbon dioxide recovery system according to claim 1, characterized in that, The cooling separation assembly includes a cooler (3) and a gas-water separator (4). The inlet of the cooler (3) is connected to the corresponding first pipeline, and its outlet is connected to the inlet of the gas-water separator (4). The gas-water separator (4) has a liquid drain port and an exhaust port, and an exhaust pipe is connected to the exhaust port.

3. The flue gas carbon dioxide recovery system according to claim 2, characterized in that, The air outlet pipeline includes an air outlet main pipe connected to the exhaust port, a first air outlet branch pipe and a second air outlet branch pipe located at the end of the air outlet main pipe, and an air outlet three-way solenoid valve located between the air outlet main pipe and the first air outlet branch pipe and the second air outlet branch pipe. The main exhaust pipe is equipped with a carbon dioxide analyzer. When the carbon dioxide analyzer detects that the carbon dioxide purity in the pipe reaches a preset purity, the three-way solenoid valve connects the first exhaust branch pipe to the main exhaust pipe and disconnects the second exhaust branch pipe from the main exhaust pipe. When the carbon dioxide analyzer detects that the carbon dioxide purity in the pipe does not reach the preset purity, the three-way solenoid valve connects the second exhaust branch pipe to the main exhaust pipe and disconnects the first exhaust branch pipe from the main exhaust pipe.

4. The flue gas carbon dioxide recovery system according to claim 2, characterized in that, The cooler (3) is provided with a cooling channel for gas to pass through and a cooling jacket covering the outside of the cooling channel. The cooling channel is provided with a gas inlet and a gas outlet. The gas inlet of the cooling channel is connected to the corresponding first pipeline, and the gas outlet of the cooling channel is connected to the feed port of the corresponding gas-water separator (4) through a pipeline. The cooling jacket is provided with a refrigerant inlet and a refrigerant outlet. The cooling separation unit also includes a cooling device (5), which is connected to the refrigerant inlet and refrigerant outlet and is used to provide cooling medium to the cooling jacket and form a cooling medium circulation loop.

5. The flue gas carbon dioxide recovery system according to claim 4, characterized in that, The two sets of cooling separation components share one cooling device (5).

6. The flue gas carbon dioxide recovery system according to claim 1, characterized in that, The purge gas inlet pipeline includes a purge gas inlet main pipe, a first purge gas inlet branch pipe and a second purge gas inlet branch pipe located at the end of the purge gas inlet main pipe, and a first purge gas inlet three-way solenoid valve located between the purge gas inlet main pipe and the first purge gas inlet branch pipe and the second purge gas inlet branch pipe. The purge gas inlet main has two parallel arranged mains. One of the purge gas inlet mains is equipped with a pressure transmitter, and the other purge gas inlet main is equipped with a valve to control the opening and closing of the purge gas inlet main. A check valve is provided after the confluence of the two purge gas inlet mains. A second purge gas inlet three-way solenoid valve is provided between the first purge gas inlet branch pipe and the first pipeline. By switching the second purge gas inlet three-way solenoid valve, the first purge gas inlet branch pipe and the first pipeline can be connected to the same adsorption tower (1) by choice. A third purge gas inlet three-way solenoid valve is provided between the second purge gas inlet branch pipe and another first pipeline. By switching the third purge gas inlet three-way solenoid valve, the second purge gas inlet branch pipe and another first pipeline can be connected to another adsorption tower (1) by choice.

7. The flue gas carbon dioxide recovery system according to claim 1, characterized in that, The system also includes a heat exchanger (7) and a spray tower (8) installed on the process gas inlet pipeline.

8. The flue gas carbon dioxide recovery system according to claim 7, characterized in that, The heat exchanger (7) is provided with a first inlet, a first outlet, a second inlet, and a second outlet; The arrangement of the process gas inlet pipeline includes: the gas first enters the heat exchanger (7) through the first inlet, and after being discharged from the first outlet, it enters the spray tower (8); subsequently, the gas flows out of the spray tower (8), enters the heat exchanger (7) again through the second inlet, and is finally discharged from the second outlet.

9. The flue gas carbon dioxide recovery system according to claim 1, characterized in that, The process gas inlet pipeline includes a process gas inlet main pipe, a first process gas inlet branch pipe and a second process gas inlet branch pipe located at the end of the process gas inlet main pipe, and a first process gas inlet three-way solenoid valve located between the process gas inlet main pipe and the first and second process gas inlet branch pipes. The process gas inlet main has two parallel arranged mains. One of the process gas inlet mains is equipped with a pressure transmitter, and the other process gas inlet main is equipped with a valve to control the passage of the process gas inlet main. A one-way valve is provided after the confluence of the two process gas inlet mains. A second process gas inlet three-way solenoid valve is provided between the first process gas inlet branch pipe and the first pipeline. By switching the second process gas inlet three-way solenoid valve, the first process gas inlet branch pipe and the first pipeline can be connected to the same adsorption tower (1). A third process gas inlet three-way solenoid valve is provided between the second process gas inlet branch pipe and another first pipeline. By switching the third process gas inlet three-way solenoid valve, the second process gas inlet branch pipe and another first pipeline can be connected to another adsorption tower (1).

10. The flue gas carbon dioxide recovery system according to claim 1, characterized in that, The adsorption medium is a modified hydrotalcite material.

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