Adsorptive pipe membrane carbon dioxide capture system and method thereof

Abstract

The present application discloses a kind of adsorptive tube membrane carbon dioxide capture system and method thereof, mainly through three tower type adsorption bed design to carry out adsorption, desorption and cooling cycle operation, and the carbon dioxide concentrated gas after desorption is sent to the first gas storage tank by the gas by-pass delivery pipeline, and the carbon dioxide concentrated gas is heated by the heating device after heating, enters the first adsorptive tube membrane module, the second adsorptive tube membrane module or the third adsorptive tube membrane module, and the hollow fiber tube type membrane adsorbent is heated, after reaching the set temperature, then the gas by-pass delivery control valve is closed, and the gas delivery valve remains open, at this time, the vacuum pump starts to heat the first adsorptive tube membrane module, the second adsorptive tube membrane module or the third adsorptive tube membrane module for vacuum desorption (TVSA) procedure, to improve desorption efficiency by heating and vacuum degree, and the gas production increases, and the capacity of adsorption increases.

Description

Technical Field

[0001] This invention relates to an adsorption membrane carbon dioxide capture system and method, and particularly to a system that optimizes desorption efficiency, increases gas production, and increases adsorption capacity, making it suitable for petrochemical plants, oil storage facilities, technology manufacturing plants, or similar areas. Background Technology

[0002] In recent years, the concentration of greenhouse gases in the atmosphere has risen sharply due to human factors. These human factors refer to the rapid increase in carbon dioxide emissions caused by the burning of fossil fuels since the Industrial Revolution, which has intensified the greenhouse effect.

[0003] Currently, the existing method involves using two zeolite tanks with granular material for the adsorption and desorption of carbon dioxide, which operate alternately in a cycle. The desorption process is performed using vacuum desorption, which is typically done at room temperature without additional heating. As a result, the regeneration capacity is only about 1 / 5 to 1 / 10 of the original maximum adsorption capacity, and the adsorption capacity cannot be increased.

[0004] Currently, most tubular membranes used in water treatment (see Figures 1 and 2) are manufactured using polymer materials, typically PVDF, PES, and PSf, with a high polymer content of approximately 80–99.99% wt. Only small amounts of other additives, such as clouding agents and zeolite powder, are added. Their working principle primarily involves controlling the pore size and distribution of the membrane a to control the flow rate and the selectivity for the particle size of the substances to be separated, thus achieving filtration and separation. The feed liquid (referred to as raw liquid b) flows over the surface of the membrane a and, under pressure, passes through the membrane a to form filtrate c, achieving the separation and filtration effect. The feed liquid (referred to as raw liquid b) then becomes concentrated liquid d (as shown in Figure 2) and is transported to the next stage (not shown in the figure).

[0005] Therefore, in view of the above-mentioned deficiencies, the inventors wish to propose an adsorption membrane carbon dioxide capture system and method that improves adsorption-desorption efficiency, allowing users to easily operate and assemble it. Thus, the inventors devoted themselves to research, design and assembly to provide convenience for users, which is the motivation for the invention. Summary of the Invention

[0006] The main objective of this invention is to provide an adsorption membrane carbon dioxide capture system and method. This system utilizes a three-tower adsorption bed design for cyclical adsorption, desorption, and cooling. The desorbed concentrated carbon dioxide gas is transported to a first gas storage tank via a gas production bypass pipeline. This concentrated carbon dioxide gas is then heated by a heating device before entering one of the first, second, or third adsorption membrane modules to heat the hollow fiber tubular membrane adsorption material. Once the set temperature is reached, the gas production bypass control valve is closed, while the gas production delivery valve remains open. At this point, a vacuum pump initiates a heated vacuum desorption (TVSA) process on the first, second, or third adsorption membrane modules. This process optimizes desorption efficiency and increases gas production through temperature and vacuum, thereby increasing the adsorption capacity during subsequent adsorption and enhancing overall practicality.

[0007] Another objective of this invention is to provide an adsorption membrane carbon dioxide capture system and method, wherein when the gas generation bypass control valve of the gas generation bypass pipeline is closed and the gas generation control valve of the gas generation pipeline is open, the gas generation pipeline delivers the concentrated carbon dioxide gas to a gas generation collection point by heating and using a vacuum pump to perform a so-called temperature vacuum swing adsorption (TVSA) process. The gas generation collection point can be any one of a carbon dioxide concentration storage tank, a carbon dioxide concentration water tank, or a carbon dioxide concentration collection tank. The concentration of the concentrated carbon dioxide gas in the gas generation pipeline is not diluted after multiple cycles, so the purity of the gas produced is good, and a large amount of concentrated carbon dioxide gas can be captured for subsequent application or storage, thereby increasing the overall usability.

[0008] Another object of the present invention is to provide an adsorption membrane carbon dioxide capture system and method, wherein the air supply pipeline has two embodiments. In the first embodiment, the air supply pipeline is directly connected to a second gas source pipeline, which supplies a second gas, either nitrogen or air, allowing the second gas to enter the first, second, or third adsorption membrane module for cooling. In the second embodiment, the air supply pipeline and the air outlet pipeline are connected to a second gas storage tank, which is connected to a second gas source pipeline that supplies a second gas, either nitrogen or air, allowing for recycling and reuse through the storage tank. When the second gas in the storage tank is insufficient, it is replenished by the second gas source pipeline, thereby increasing overall operability.

[0009] To further understand the features, characteristics, and technical content of this invention, please refer to the following detailed description and accompanying drawings. The accompanying drawings are for reference and illustration only and are not intended to limit the invention. Attached Figure Description

[0010] Figure 1 This is a schematic diagram illustrating the working principle of a tubular membrane.

[0011] Figure 2 This is a schematic diagram of how the original solution is converted into a concentrated solution.

[0012] Figure 3 A schematic diagram of the system architecture in which the air supply pipeline is directly connected to the second gas source pipeline.

[0013] Figure 4 This is a schematic diagram of another system architecture where the air supply pipeline is directly connected to the second gas source pipeline.

[0014] Figure 5 A schematic diagram of the system architecture for opening the gas production bypass control valve of the gas production bypass pipeline and closing the gas production control valve of the gas production pipeline.

[0015] Figure 6 A schematic diagram of the system architecture where the gas bypass control valve of the gas production bypass pipeline is closed and the gas production control valve of the gas production pipeline is open.

[0016] Figure 7 This is a schematic diagram of the adsorption principle of the membrane.

[0017] Figure 8 This is a three-dimensional schematic diagram showing the adsorption layer and pores being adjacent.

[0018] Figure 9 A three-dimensional schematic diagram of the channels located between the adsorption layers.

[0019] Figure 10 This is a flowchart of the main steps of the present invention.

[0020] Explanation of reference numerals in the attached figures

[0021] 1. First adsorbent membrane module; 2. Second adsorbent membrane module

[0022] 3. Third Adsorption Membrane Module

[0023] 4. Tubular hollow fiber membrane adsorbent material

[0024] 101. First intake pipe; 1011. First intake control valve

[0025] 102. First exhaust pipe; 1021. First exhaust control valve

[0026] 103. First hot gas pipeline; 1031. First hot gas control valve

[0027] 104. First gas production pipeline; 1041. First gas production control valve

[0028] 105. First air supply duct; 1051. First air supply control valve

[0029] 106. First air outlet duct; 1061. First air outlet control valve

[0030] 201. Second intake pipe; 2011. Second intake control valve

[0031] 202. Second exhaust pipe; 2021. Second exhaust control valve

[0032] 203. Second hot gas pipeline; 2031. Second hot gas control valve

[0033] 204. Second gas production pipeline; 2041. Second gas production control valve

[0034] 205. Second air supply duct; 2051. Second air supply control valve

[0035] 206. Second air outlet duct; 2061. Second air outlet control valve

[0036] 301, Third intake pipe; 3011, Third intake control valve

[0037] 302. Third exhaust pipe; 3021. Third exhaust control valve

[0038] 303, Third hot gas pipeline; 3031, Third hot gas control valve

[0039] 304. Third gas production pipeline; 3041. Third gas production control valve

[0040] 305. Third air supply duct; 3051. Third air supply control valve

[0041] 306. Third air outlet duct; 3061. Third air outlet control valve

[0042] 10. Gas delivery pipeline 11. Gas delivery control valve

[0043] 20. Exhaust gas delivery pipeline 21. Exhaust gas equipment

[0044] 30. Hot gas delivery pipeline; 31. Heating device

[0045] 40. Gas production and delivery pipeline 41. Vacuum pump

[0046] 42. Gas production and delivery control valves; 50. Air supply pipelines

[0047] 51. Air supply and conveying control valves 52. Air supply equipment

[0048] 60. Air delivery pipeline; 70. First gas storage tank

[0049] 71. Gas production bypass pipeline; 711. Gas production bypass control valve

[0050] 72. First gas delivery pipeline; 90. Second gas source pipeline

[0051] 91. Second gas source control valve Detailed Implementation

[0052] To make the objectives, technical solutions, and advantages of the present invention clearer, the present invention will be further described in detail below with reference to specific embodiments and accompanying drawings.

[0053] Please refer to Figures 3 to 10, which are schematic diagrams of embodiments of the present invention. The preferred implementation of the adsorption membrane carbon dioxide capture system and method of the present invention is to be used in petrochemical plants, oil storage plants, technology manufacturing plants or similar areas, mainly to optimize the desorption efficiency and increase the gas production, thereby increasing the adsorption capacity.

[0054] The adsorption membrane carbon dioxide capture system of the present invention is used to treat a gas containing carbon dioxide. It mainly includes a first adsorption membrane module 1, a second adsorption membrane module 2, a third adsorption membrane module 3, a gas conveying pipeline 10, an exhaust conveying pipeline 20, a hot gas conveying pipeline 30, a gas production conveying pipeline 40, an air supply conveying pipeline 50, an exhaust air conveying pipeline 60, and a first gas storage tank 70 (e.g., ...). Figures 3 to 6 As shown), the adsorption, desorption, and cooling cycle is achieved through a three-tower adsorption bed design consisting of a first adsorption membrane module 1, a second adsorption membrane module 2, and a third adsorption membrane module 3. Each of the three modules is filled with multiple tubular hollow fiber tubular membrane adsorption materials 4 (e.g., ...). Figures 3 to 6 As shown), its filling rate is 75% to 95%, mainly to increase its adsorption area. Furthermore, the tubular hollow fiber membrane adsorbent 4 is any one or a combination of zeolite (e.g., X-type zeolite (e.g., 13X)), anion exchange resin, and metal-organic framework (MOF) materials.

[0055] The tubular hollow fiber membrane adsorbent material 4 includes at least one channel 401 and at least one adsorbent layer 402 (e.g., Figures 8 to 9 As shown), the at least one adsorption layer 402 surrounds the at least one channel 401, wherein the adsorption layer 402 and the channel 401 are adjacent (e.g. Figure 8 As shown), multiple channels 401 can also be disposed between the adsorption layers 402 (e.g. Figure 9 As shown, the number of channels 401 and the number of adsorption layers 402 are not limited to the present invention, and gas or liquid can pass through the at least one channel 401, wherein the inner diameter of the at least one channel 401 is any between 0.3 mm and 1.0 mm, so as to be designed to suit different applications. The tubular hollow fiber membrane adsorbent 4 has a diameter of D1, and the opening diameter of the at least one pore 401 is d1, satisfying the condition 1 < D1 / d1 < 99. The tubular hollow fiber membrane adsorbent 4 can be arranged into any one of rectangular (not shown), fan-shaped (not shown), or cylindrical shapes, and combined using these shapes to minimize the gaps between the assembled tubular hollow fiber membrane adsorbents 4. The porosity of the tubular hollow fiber membrane adsorbent 4 is 20%-80%, where porosity is the ratio of the volume of the hollow pores to the total volume of the material. Gas or liquid can only enter through the pores. Furthermore, the specific surface area of ​​the tubular hollow fiber membrane adsorbent 4 is greater than 500 square meters per cubic meter (m³). 2 / m3 The specific surface area refers to the surface area per unit volume of a porous solid material, and the so-called surface area refers to the internal surface area, so as to have better adsorption effect.

[0056] Furthermore, the tubular hollow fiber membrane adsorbent 4 comprises at least an amine-modified anion exchange resin material and a polymer material (not shown in the figure), primarily made of the amine-modified anion exchange resin material and the polymer material. The polymer material is at least one of the following groups: polysulfone, polyethersulfone, polyvinylidene fluoride, polyphenylene sulfone, polyacrylonitrile, cellulose acetate, cellulose diacetate, polyimide, polyetherimide, polyamide, polyvinyl alcohol, polylactic acid, polyglycolic acid, polylactic-glycolic acid, polycaprolactone, polyvinylpyrrolidone, ethylene-vinyl alcohol, polydimethylsiloxane, polytetrafluoroethylene, and cellulose acetate. The amine-modified anion exchange resin is designed to exchange with negatively charged ions. Based on the reversible equilibrium principle of ion exchange reactions, the bound exchange ion is a hydroxyl radical (OH). - ) or carbonate (CO3) 2- Any of these components can be used in a displacement reaction of ion-exchange resins to restore them to their original state. This amine-modified anion-exchange resin material is an anion-exchange resin modified by any one or a combination of primary amines (-NH2), secondary amines (-NHR), tertiary amines (-NR2), and quaternary ammonium salts (-NR3OH). Modification refers to altering the material's properties, and performance is improved through physical processes such as heating, cooling, ion bombardment, and implantation, as well as chemical treatments. The amine group (-NH2) is the functional group of amines. Amines can be further classified according to the number of hydrogen atoms substituted on the nitrogen molecule, into primary amines (-NH2), secondary amines (-NHR), tertiary amines (-NR2), and quaternary ammonium salts (-NR3OH). Primary amines (-NH2), secondary amines (-NHR), and tertiary amines (-NR2) are weakly basic functional groups, which can dissociate into OH groups in water. - It exhibits weak alkalinity. The positively charged groups of this resin can adsorb and bind with anions in solution, thereby generating anion exchange. Furthermore, the quaternary ammonium salts (-NR3OH) are strongly basic functional groups, which can dissociate into OH- ions in water. - It is strongly alkaline. The positively charged groups of this resin can adsorb and bind with anions in the solution, thereby producing anion exchange.

[0057] Furthermore, the tubular hollow fiber membrane adsorbent material 4 used in this invention, in addition to the aforementioned polymer material, also requires at least one adsorbent (not shown in the figure). This adsorbent may be, for example, zeolite powder, resin, activated carbon, etc., and is in powder form, with a micron-sized particle size and an average particle size between 1 and 99 micrometers, where one micrometer equals 1 x 10⁻⁶. -6Meters. Furthermore, the membrane 403 of the tubular hollow fiber tubular membrane adsorbent material 4 is manufactured by a dry-wet spinning phase transfer process. The membrane 403 of the tubular hollow fiber tubular membrane adsorbent material 4 has a structure similar to a sponge or foam, and has interconnected micron-sized pores, allowing gas molecules to move and diffuse freely between these micron-sized pores. These gas molecules are sub-nanometer or angstrom-sized. Abbreviation: Ang, symbol The molecular size of ).

[0058] Furthermore, the polymer content is lower than that of the adsorbent, ranging from 5% to 55% wt, while the adsorbent (such as zeolite) accounts for 95% to 45% wt. Generally, the preferred ratio is 10% to 30% wt for the polymer. The tubular hollow fiber membrane adsorbent material 4 used in this invention is mainly used for separating or purifying mixed gases containing two or more gases through the principle of adsorption. The principle is that the source feed gas A flows over the surface of the membrane 403 of the tubular hollow fiber membrane adsorbent material 4 and is output as concentrated gas B. Through diffusion as the source feed gas A flows over the surface of the membrane 403, one or more gases are easily adsorbed by the adsorbent contained in the membrane 403, while other gas components are less easily adsorbed. Therefore, the more easily adsorbed gases are adsorbed onto the adsorbent within the membrane 403 (as shown in Figure 7), achieving separation or purification. Factors influencing the adsorption of the source feed gas A include the micropore size of the adsorbent, the size of gas molecules, van der Waals forces, polarity, and the hydrophilicity or hydrophobicity of the adsorbent, etc. The flow rate of the feed gas A through the surface of the membrane 403 of the tubular hollow fiber tubular membrane adsorbent material 4 is usually controlled at 0.01 m / s to 1 m / s. Sometimes, when the processing efficiency requirement is low, it can be adjusted to a maximum of 2.5 m / s.

[0059] The first absorbent membrane module 1 is provided with a first air inlet pipe 101, a first exhaust pipe 102, a first hot air pipe 103, a first gas production pipe 104, a first air supply pipe 105, and a first air outlet pipe 106. The second absorbent membrane module 2 is provided with a second air inlet pipe 201, a second exhaust pipe 202, a second hot air pipe 203, a second gas production pipe 204, a second air supply pipe 205, and a second air outlet pipe 206. The third absorbent membrane module 3 is provided with a third air inlet pipe 301, a third exhaust pipe 302, a third hot air pipe 303, a third gas production pipe 304, a third air supply pipe 305, and a third air outlet pipe 306 (e.g., ...). Figures 3 to 6(As shown). The first intake pipe 101 is equipped with a first intake control valve 1011, the second intake pipe 201 is equipped with a second intake control valve 2011, and the third intake pipe 301 is equipped with a third intake control valve 3011 (as shown). Figures 3 to 6 (As shown), the first intake control valve 1011, the second intake control valve 2011, and the third intake control valve 3011 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first intake pipe 101, the second intake pipe 201, and the third intake pipe 301 to be controlled by the first intake control valve 1011, the second intake control valve 2011, and the third intake control valve 3011. Additionally, the first exhaust pipe 102 is equipped with a first exhaust control valve 1021, the second exhaust pipe 202 is equipped with a second exhaust control valve 2021, and the third exhaust pipe 302 is equipped with a third exhaust control valve 3021 (e.g., ...). Figures 3 to 6 As shown), the first exhaust control valve 1021, the second exhaust control valve 2021, and the third exhaust control valve 3021 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first exhaust pipeline 102, the second exhaust pipeline 202, and the third exhaust pipeline 302 to be controlled by the first exhaust control valve 1021, the second exhaust control valve 2021, and the third exhaust control valve 3021.

[0060] Additionally, the first hot gas pipeline 103 is equipped with a first hot gas control valve 1031, the second hot gas pipeline 203 is equipped with a second hot gas control valve 2031, and the third hot gas pipeline 303 is equipped with a third hot gas control valve 3031 (e.g., Figures 3 to 6 (As shown), the first hot gas control valve 1031, the second hot gas control valve 2031, and the third hot gas control valve 3031 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first hot gas pipeline 103, the second hot gas pipeline 203, and the third hot gas pipeline 303 to be controlled by the first hot gas control valve 1031, the second hot gas control valve 2031, and the third hot gas control valve 3031. Additionally, the first gas production pipeline 104 is equipped with a first gas production control valve 1041, the second gas production pipeline 204 is equipped with a second gas production control valve 2041, and the third gas production pipeline 304 is equipped with a third gas production control valve 3041 (e.g., ...). Figures 3 to 6(As shown), the first gas generation control valve 1041, the second gas generation control valve 2041, and the third gas generation control valve 3041 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first gas generation pipeline 104, the second gas generation pipeline 204, and the third gas generation pipeline 304 to be controlled by the first gas generation control valve 1041, the second gas generation control valve 2041, and the third gas generation control valve 3041. Additionally, the first air supply pipeline 105 is equipped with a first air supply control valve 1051, the second air supply pipeline 205 is equipped with a second air supply control valve 2501, and the third air supply pipeline 305 is equipped with a third air supply control valve 3051 (e.g., ...). Figures 3 to 6 (As shown), the first air supply control valve 1051, the second air supply control valve 2051, and the third air supply control valve 3051 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first air supply pipeline 105, the second air supply pipeline 205, and the third air supply pipeline 305 to be controlled by the first air supply control valve 1051, the second air supply control valve 2051, and the third air supply control valve 3051. Additionally, the first air outlet pipeline 106 is equipped with a first air outlet control valve 1061, the second air outlet pipeline 206 is equipped with a second air outlet control valve 2061, and the third air outlet pipeline 306 is equipped with a third air outlet control valve 3061 (e.g., ...). Figures 3 to 6 As shown), the first air outlet control valve 1061, the second air outlet control valve 2061, and the third air outlet control valve 3061 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first air outlet duct 106, the second air outlet duct 206, and the third air outlet duct 306 to be controlled by the first air outlet control valve 1061, the second air outlet control valve 2061, and the third air outlet control valve 3061.

[0061] The gas delivery pipeline 10 is connected to the first inlet pipeline 101, the second inlet pipeline 201, and the third inlet pipeline 301, respectively. The gas delivery pipeline 10 delivers a gas to be treated containing carbon dioxide (CO2). This gas, in addition to carbon dioxide (CO2), also contains other gases such as oxygen (O2) and nitrogen (N2), not limited to those mentioned above. The gas is delivered through the first inlet pipeline 101, the second inlet pipeline 201, and the third inlet pipeline 301 to the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3 for adsorption. The gas delivery pipeline 10 is equipped with a gas delivery control valve 11 (e.g., Figures 3 to 6(As shown), the gas delivery control valve 11 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the gas delivery pipeline 10 to be controlled by the gas delivery control valve 11. The exhaust delivery pipeline 20 is connected to the first exhaust pipeline 102, the second exhaust pipeline 202, and the third exhaust pipeline 302, respectively. The exhaust delivery pipeline 20 is connected to an exhaust device 21, wherein the exhaust device 21 can be any one of a chimney, an exhaust stack, or other exhaust facilities, not limited to the embodiments of the present invention, to deliver the adsorbed gas after adsorption by the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3 to the exhaust delivery pipeline 20 (e.g., Figures 3 to 6 (as shown), and then discharged into the atmosphere or other suitable locations through the exhaust device 21.

[0062] Furthermore, the hot gas delivery pipeline 30 is connected to the first hot gas pipeline 103, the second hot gas pipeline 203, and the third hot gas pipeline 303, and the hot gas delivery pipeline 30 is equipped with a heating device 31 (e.g., Figures 3 to 6 As shown), the heating device 31 is any one of a gas heater, an electric heater, or a hot kerosene heater. The gas production pipeline 40 is connected to the first gas production pipeline 104, the second gas production pipeline 204, and the third gas production pipeline 304, respectively. The gas production pipeline 40 is equipped with a vacuum pump 41 and a gas production control valve 42 (e.g., ...). Figures 3 to 6 (As shown), and the gas production and delivery control valve 42 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the gas production and delivery pipeline 40 to be controlled by the gas production and delivery control valve 42. Additionally, the first gas storage tank 70 is provided with a gas production bypass delivery pipeline 71 and a first gas delivery pipeline 72 (as shown). Figures 3 to 6 As shown, the first gas delivery pipeline 72 is connected to the heating device 31, and the gas production bypass delivery pipeline 71 is connected to the gas production delivery pipeline 40. The gas production bypass delivery pipeline 71 is provided with a gas production bypass delivery control valve 711. The gas production bypass delivery control valve 711 can be any one of a check valve, an electric valve, or a pneumatic valve, so that the gas flow direction of the gas production bypass delivery pipeline 71 can be controlled by the gas production bypass delivery control valve 711.

[0063] Furthermore, when the gas production bypass control valve 711 of the gas production bypass pipeline 71 is opened and the gas production control valve 42 of the gas production pipeline 40 is closed (e.g. Figure 5As shown), the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3 is used for desorption, and a concentrated carbon dioxide gas is generated after desorption. The concentrated carbon dioxide gas after desorption is transported to the gas production delivery pipeline 40 through the first gas production pipeline 104, the second gas production pipeline 204, or the third gas production pipeline 304, respectively. The gas production delivery pipeline 40 is subjected to a so-called temperature vacuum swing by heating and vacuum pump 41 in a vacuum manner. The carbon dioxide concentrate is transported to the first gas storage tank 70 via the gas bypass pipeline 71 using adsorption (TVSA). The first gas storage tank 70 then transports the carbon dioxide concentrate to the heating device 31 via the first gas delivery pipeline 72 for heating (to temperatures such as 100°C, 120°C, or even lower than 100°C, not limited to the specification). After heating, a heated gas is released. This heated gas system is a heated carbon dioxide concentrate, and the heated gas is transported through the first hot gas pipeline 103 and the second... Hot gas pipeline 203 or the third hot gas pipeline 303 respectively delivers heat to the first adsorbent tubular membrane module 1, the second adsorbent tubular membrane module 2, or the third adsorbent tubular membrane module 3 to heat the hollow fiber tubular membrane adsorbent material 4. Since the first adsorbent tubular membrane module 1, the second adsorbent tubular membrane module 2, or the third adsorbent tubular membrane module 3 is entered by the heated gas, the first adsorbent tubular membrane module 1, the second adsorbent tubular membrane module 2, or the third adsorbent tubular membrane module 3 is also heated, so that the desorption efficiency is optimized and the gas production is increased, so that the adsorption capacity can be increased during subsequent adsorption.

[0064] Furthermore, since the heating gas is a concentrated carbon dioxide gas with a certain temperature, and it is used for desorption to produce the concentrated carbon dioxide gas, which is then circulated to the heating device 31 through the gas production bypass pipeline 71 for heating and temperature increase, the concentrated carbon dioxide gas with a certain temperature and its concentration are not diluted during the circulation process, so the purity of the produced gas is good, and a large amount of concentrated carbon dioxide gas can be captured. After a set period of time or when the concentrated carbon dioxide gas reaches the set temperature, the gas production bypass pipeline 71's gas production bypass control valve 711 is closed, while the gas production pipeline 40's gas production control valve 42 is opened (e.g., Figure 6As shown), the gas production pipeline 40 delivers the concentrated carbon dioxide gas to a gas production collection point (not shown) by heating and the vacuum pump 41 using a so-called temperature vacuum swing adsorption (TVSA) method, wherein the gas production collection point is any one of a carbon dioxide concentration storage tank, a carbon dioxide concentration water tank, or a carbon dioxide concentration collection tank, for subsequent application or storage.

[0065] Furthermore, when the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3 is used for cooling, the air outlet delivery pipe 50 is connected to the first air outlet pipe 105, the second air outlet pipe 205, and the third air outlet pipe 305, respectively, and the air supply delivery pipe 50 is connected to the first air supply pipe 105, the second air supply pipe 205, and the third air supply pipe 305, respectively. The air supply delivery pipe 50 is equipped with an air supply control valve 51 (e.g., ...). Figures 3 to 6 As shown), the air supply and delivery control valve 51 can be any one of a check valve, an electric valve, or a pneumatic valve, so that the air supply and delivery control valve 51 can control the gas flow direction of the air supply and delivery pipeline 50.

[0066] In addition, the air supply pipeline 50 has two implementation methods, the first of which is (e.g.) Figure 3 and Figure 4As shown, the air supply pipeline 50 is directly connected to a second gas source pipeline 90, which supplies a second gas, either nitrogen or air. The second gas source pipeline 90 is equipped with a second gas source control valve 91, which can be any of a check valve, an electric valve, or a pneumatic valve, allowing the gas flow direction of the second gas source pipeline 90 to be controlled. The second gas in the second gas source pipe 90 enters the air supply pipe 50 and is then transported by the air supply pipe 50 to the first air supply pipe 105, the second air supply pipe 205, or the third air supply pipe 305. The second gas is then cooled by the first air supply pipe 105, the second air supply pipe 205, or the third air supply pipe 305. The cooled second gas is then transported to the air outlet pipe 60 through the first air outlet pipe 106, the second air outlet pipe 206, or the third air outlet pipe 306, and then discharged through the air outlet pipe 60. The aforementioned air supply pipeline 50 is equipped with an air supply device 52, which is either an air pump or a blower, to push the second gas in the air supply pipeline 52 into the first air supply pipeline 105, the second air supply pipeline 205 or the third air supply pipeline 305, and then deliver it to the first adsorbent membrane module 1, the second adsorbent membrane module 2 or the third adsorbent membrane module 3 for cooling.

[0067] The second embodiment involves connecting the air supply pipe 50 and the air outlet pipe 60 to a second gas storage tank 80 (e.g., ...). Figure 5 and Figure 6As shown, the second gas storage tank 80 is connected to a second gas source pipeline 90, which supplies a second gas, either nitrogen or air. The second gas source pipeline 90 is equipped with a second gas source control valve 91, which can be any of a check valve, an electric valve, or a pneumatic valve, allowing control of the gas flow direction through the second gas source pipeline 90. The second gas first enters the second gas storage tank 80 through the second gas source pipeline 90 for storage. Once a certain capacity is reached or the storage tank's capacity is met, the second gas source control valve is closed, allowing the second gas stored in the second gas storage tank 80 to be used. Then, the air supply control valve 51 on the air supply pipeline 50 is opened to allow the second gas in the second gas storage tank 80 to enter the air supply pipeline 50, and the air supply pipeline 50 delivers the gas to the first air supply pipeline 105, the second air supply pipeline 205, or the third air supply pipeline 305, and then the gas enters the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 305 respectively. The second gas is used for cooling within the membrane module 3. After cooling, the second gas is transported to the outlet conveying pipeline 60 through the first outlet pipeline 106, the second outlet pipeline 206, or the third outlet pipeline 306. The outlet conveying pipeline 60 then returns the gas to the second gas storage tank 80, enabling it to be recycled and reused through the second gas storage tank 80. When the second gas in the second gas storage tank 80 is insufficient, it is replenished by the second gas source pipeline 90, thereby increasing the overall operability. The aforementioned air supply pipeline 50 is equipped with an air supply device 52, which is either an air pump or a blower, to push the second gas in the air supply pipeline 50 into the first air supply pipeline 105, the second air supply pipeline 205 or the third air supply pipeline 305, and then deliver it to the first adsorbent membrane module 1, the second adsorbent membrane module 2 or the third adsorbent membrane module 3 for cooling.

[0068] Furthermore, the present invention utilizes a three-tower adsorption bed design consisting of a first adsorption membrane module 1, a second adsorption membrane module 2, and a third adsorption membrane module 3 to perform cyclic operations of adsorption, desorption, and cooling. These cyclic operations run simultaneously, and after a set time (which may be 5 minutes, 10 minutes, 20 minutes, 30 minutes, 40 minutes, etc., and is not limited to the above time), the first adsorption membrane module 1, the second adsorption membrane module 2, and the third adsorption membrane module 3 sequentially switch between adsorption, desorption, and cooling.

[0069] The carbon dioxide capture method using an adsorbent membrane of the present invention mainly includes a first adsorbent membrane module 1, a second adsorbent membrane module 2, a third adsorbent membrane module 3, a gas conveying pipeline 10, an exhaust conveying pipeline 20, a hot gas conveying pipeline 30, a gas production conveying pipeline 40, an air supply conveying pipeline 50, an exhaust air conveying pipeline 60, and a first gas storage tank 70 (e.g., Figures 3 to 6 As shown), the adsorption, desorption, and cooling cycle is achieved through a three-tower adsorption bed design consisting of a first adsorption membrane module 1, a second adsorption membrane module 2, and a third adsorption membrane module 3. Each of the three modules is filled with multiple tubular hollow fiber tubular membrane adsorption materials 4 (e.g., ...). Figures 3 to 6 As shown), its filling rate is 75% to 95%, mainly to increase its adsorption area. Furthermore, the tubular hollow fiber membrane adsorbent 4 is any one or a combination of zeolite (e.g., X-type zeolite (e.g., 13X)), anion exchange resin, and metal-organic framework (MOF) materials.

[0070] The tubular hollow fiber membrane adsorbent material 4 includes at least one channel 401 and at least one adsorbent layer 402 (e.g., Figures 8 to 9 As shown), the at least one adsorption layer 402 surrounds the at least one channel 401, wherein the adsorption layer 402 and the channel 401 are adjacent (e.g. Figure 8 As shown), porous channels 401 can also be disposed in the spaces between the adsorption layers 402 (e.g., Figure 9 As shown, the number of channels 401 and the number of adsorption layers 402 are not limited to the present invention, and gas or liquid can pass through the at least one channel 401, wherein the inner diameter of the at least one channel 401 is one of 0.3 mm to 1.0 mm, so as to be designed to suit different applications. The tubular hollow fiber membrane adsorbent 4 has a diameter of D1, and the opening diameter of the at least one pore 401 is d1, satisfying the condition 1 < D1 / d1 < 99. The tubular hollow fiber membrane adsorbent 4 can be arranged into any one of the following shapes: rectangular (not shown), fan-shaped (not shown), or cylindrical, and combined using these shapes to minimize the gaps between the assembled tubular hollow fiber membrane adsorbents 4. The porosity of the tubular hollow fiber membrane adsorbent 4 is 20%-80%, where porosity is the ratio of the volume of the hollow pores to the total volume of the material. Gas or liquid can only enter through the pores. Furthermore, the specific surface area of ​​the tubular hollow fiber membrane adsorbent 4 is greater than 500 square meters per cubic meter (m³). 2 / m 3The specific surface area refers to the surface area per unit volume of a porous solid material, and the so-called surface area refers to the internal surface area, so as to have better adsorption effect.

[0071] Furthermore, the tubular hollow fiber membrane adsorbent 4 comprises at least an amine-modified anion exchange resin material and a polymer material (not shown in the figure), primarily made of the amine-modified anion exchange resin material and the polymer material. The polymer material is at least one of the following groups: polysulfone, polyethersulfone, polyvinylidene fluoride, polyphenylene sulfone, polyacrylonitrile, cellulose acetate, cellulose diacetate, polyimide, polyetherimide, polyamide, polyvinyl alcohol, polylactic acid, polyglycolic acid, polylactic-glycolic acid, polycaprolactone, polyvinylpyrrolidone, ethylene-vinyl alcohol, polydimethylsiloxane, polytetrafluoroethylene, and cellulose acetate. The amine-modified anion exchange resin exchanges with negatively charged ions. Based on the reversible equilibrium principle of ion exchange reactions, the bound exchange ion is a hydroxyl radical (OH). - ) or carbonate (CO3) 2- Any of these components can be used in a displacement reaction of ion-exchange resins to restore them to their original state. This amine-modified anion-exchange resin material is an anion-exchange resin modified by any one or a combination of primary amines (-NH2), secondary amines (-NHR), tertiary amines (-NR2), and quaternary ammonium salts (-NR3OH). Modification refers to altering the material's properties, and performance is improved through physical processes such as heating, cooling, ion bombardment, and implantation, as well as chemical treatments. The amine group (-NH2) is the functional group of amines. Amines can be further classified according to the number of hydrogen atoms substituted on the nitrogen molecule, into primary amines (-NH2), secondary amines (-NHR), tertiary amines (-NR2), and quaternary ammonium salts (-NR3OH). Primary amines (-NH2), secondary amines (-NHR), and tertiary amines (-NR2) are weakly basic functional groups, which can dissociate into OH groups in water. - It exhibits weak alkalinity. The positively charged groups of this resin can adsorb and bind with anions in solution, thereby generating anion exchange. Furthermore, the quaternary ammonium salt (-NR3OH) is a strongly basic functional group, which can dissociate in water to release OH-. - It is strongly alkaline. The positively charged groups of this resin can adsorb and bind with anions in the solution, thereby producing anion exchange.

[0072] Furthermore, the tubular hollow fiber tubular membrane adsorbent material 4 used in this invention, in addition to the aforementioned polymer material, also includes at least one adsorbent (not shown in the figure). This adsorbent may be, for example, zeolite powder, resin, activated carbon, etc., and is in powder form, with a micron-sized particle size and an average particle size between 1 and 99 micrometers, where one micrometer equals 1 x 10⁻⁶ meters. The membrane body 403 of this tubular hollow fiber tubular membrane adsorbent material 4 is manufactured using a dry-wet spinning phase transfer process. The membrane body 403 of this tubular hollow fiber tubular membrane adsorbent material 4 has a structure similar to a sponge or foam, and has interconnected micron-sized pores. Gas molecules can move and diffuse between these micron-sized pores, where the gas molecules are sub-nanometer or angstrom-sized. Abbreviation: Ang, symbol The molecular size of ).

[0073] Furthermore, the polymer content is lower than that of the adsorbent, ranging from 5% to 55% wt, while the adsorbent (such as zeolite) accounts for 95% to 45% wt. Generally, a preferred ratio is 10% to 30% wt for the polymer. The tubular hollow fiber membrane adsorbent material 4 used in this invention is mainly used for separating or purifying mixed gases containing two or more gases through the principle of adsorption. The principle is that the source feed gas A flows over the surface of the membrane 403 of the tubular hollow fiber membrane adsorbent material 4 and is output as concentrated gas B. Through diffusion as the source feed gas A flows over the surface of the membrane 403, one or more gases are easily adsorbed by the adsorbent contained in the membrane 403, while other gas components are less easily adsorbed. Therefore, the more easily adsorbed gases are adsorbed onto the adsorbent within the membrane 403 (as shown in Figure 7), achieving separation or purification. Factors influencing the adsorption of the source feed gas A include the micropore size of the adsorbent, the size of gas molecules, van der Waals forces, polarity, and the hydrophilicity or hydrophobicity of the adsorbent. The flow rate of the feed gas A through the surface of the membrane 403 of the tubular hollow fiber tubular membrane adsorbent material 4 is usually controlled at 0.01 m / s to 1 m / s. Sometimes, depending on the need for lower processing efficiency, it can be adjusted to a maximum of 2.5 m / s.

[0074] The first absorbent membrane module 1 is provided with a first air inlet pipe 101, a first exhaust pipe 102, a first hot air pipe 103, a first gas production pipe 104, a first air supply pipe 105, and a first air outlet pipe 106. The second absorbent membrane module 2 is provided with a second air inlet pipe 201, a second exhaust pipe 202, a second hot air pipe 203, a second gas production pipe 204, a second air supply pipe 205, and a second air outlet pipe 206. The third absorbent membrane module 3 is provided with a third air inlet pipe 301, a third exhaust pipe 302, a third hot air pipe 303, a third gas production pipe 304, a third air supply pipe 305, and a third air outlet pipe 306 (e.g., ...). Figures 3 to 6 (As shown). The first intake pipe 101 is equipped with a first intake control valve 1011, the second intake pipe 201 is equipped with a second intake control valve 2011, and the third intake pipe 301 is equipped with a third intake control valve 3011 (as shown). Figures 3 to 6 (As shown), the first intake control valve 1011, the second intake control valve 2011, and the third intake control valve 3011 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first intake pipe 101, the second intake pipe 201, and the third intake pipe 301 to be controlled by the first intake control valve 1011, the second intake control valve 2011, and the third intake control valve 3011. Additionally, the first exhaust pipe 102 is equipped with a first exhaust control valve 1021, the second exhaust pipe 202 is equipped with a second exhaust control valve 2021, and the third exhaust pipe 302 is equipped with a third exhaust control valve 3021 (e.g., ...). Figures 3 to 6 As shown), the first exhaust control valve 1021, the second exhaust control valve 2021, and the third exhaust control valve 3021 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first exhaust pipeline 102, the second exhaust pipeline 202, and the third exhaust pipeline 302 to be controlled by the first exhaust control valve 1021, the second exhaust control valve 2021, and the third exhaust control valve 3021.

[0075] Additionally, the first hot gas pipeline 103 is equipped with a first hot gas control valve 1031, the second hot gas pipeline 203 is equipped with a second hot gas control valve 2031, and the third hot gas pipeline 303 is equipped with a third hot gas control valve 3031 (e.g., Figures 3 to 6(As shown), the first hot gas control valve 1031, the second hot gas control valve 2031, and the third hot gas control valve 3031 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first hot gas pipeline 103, the second hot gas pipeline 203, and the third hot gas pipeline 303 to be controlled by the first hot gas control valve 1031, the second hot gas control valve 2031, and the third hot gas control valve 3031. Additionally, the first gas production pipeline 104 is equipped with a first gas production control valve 1041, the second gas production pipeline 204 is equipped with a second gas production control valve 2041, and the third gas production pipeline 304 is equipped with a third gas production control valve 3041 (e.g., ...). Figures 3 to 6 (As shown), the first gas generation control valve 1041, the second gas generation control valve 2041, and the third gas generation control valve 3041 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first gas generation pipeline 104, the second gas generation pipeline 204, and the third gas generation pipeline 304 to be controlled by the first gas generation control valve 1041, the second gas generation control valve 2041, and the third gas generation control valve 3041. Additionally, the first air supply pipeline 105 is equipped with a first air supply control valve 1051, the second air supply pipeline 205 is equipped with a second air supply control valve 2501, and the third air supply pipeline 305 is equipped with a third air supply control valve 3051 (e.g., ...). Figures 3 to 6 (As shown), the first air supply control valve 1051, the second air supply control valve 2051, and the third air supply control valve 3051 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first air supply pipeline 105, the second air supply pipeline 205, and the third air supply pipeline 305 to be controlled by the first air supply control valve 1051, the second air supply control valve 2051, and the third air supply control valve 3051. Additionally, the first air outlet pipeline 106 is equipped with a first air outlet control valve 1061, the second air outlet pipeline 206 is equipped with a second air outlet control valve 2061, and the third air outlet pipeline 306 is equipped with a third air outlet control valve 3061 (e.g., ...). Figures 3 to 6 As shown), the first air outlet control valve 1061, the second air outlet control valve 2061, and the third air outlet control valve 3061 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the first air outlet duct 106, the second air outlet duct 206, and the third air outlet duct 306 to be controlled by the first air outlet control valve 1061, the second air outlet control valve 2061, and the third air outlet control valve 3061.

[0076] The main steps of this adsorption membrane carbon dioxide capture method (such as...) Figure 10The procedure (shown) includes step S100, an adsorption and exhaust process: the gas delivery pipeline 10 supplies a gas containing carbon dioxide to be treated. The first inlet pipeline 101 of the gas containing carbon dioxide is delivered to the first adsorption membrane module 1 for adsorption. After adsorption, the first adsorption membrane module 1 delivers adsorbed gas. The first exhaust pipeline 102 of the adsorbed gas is delivered to the exhaust delivery pipeline 20 and discharged through the exhaust delivery pipeline 202. After completing step S100, the next step S110 is performed.

[0077] The gas delivery pipeline 10 is connected to the first inlet pipeline 101, the second inlet pipeline 201, and the third inlet pipeline 301. The gas delivery pipeline 10 delivers a gas to be treated containing carbon dioxide (CO2). This gas contains oxygen (O2), nitrogen (N2), and other gases besides carbon dioxide (CO2). It may also contain volatile organic compounds (VOCs) or other factory waste gases. The gas containing carbon dioxide (CO2) is delivered from the first inlet pipeline 101, the second inlet pipeline 201, or the third inlet pipeline 301 to the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3 for adsorption. The gas delivery pipeline 10 is equipped with a gas delivery control valve 11 (e.g., Figures 3 to 6 As shown), the gas delivery control valve 11 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling the gas flow direction of the gas delivery pipeline 10 to be controlled through the gas delivery control valve 11.

[0078] Furthermore, the aforementioned exhaust delivery pipeline 20 is connected to the first exhaust pipeline 102, the second exhaust pipeline 202, and the third exhaust pipeline 302, respectively. The exhaust delivery pipeline 20 is also connected to an exhaust device 21, which can be any of a chimney, an exhaust stack, or other exhaust facilities, not limited to the embodiments of this invention. The adsorbed gas, after being adsorbed by the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3, is respectively transported through the first exhaust pipeline 102, the second exhaust pipeline 202, or the third exhaust pipeline 302 into the exhaust delivery pipeline 20 (e.g., Figures 3 to 6 (As shown), the exhaust device 21 is then used to discharge the exhaust into the atmosphere or other suitable locations.

[0079] In addition, the next step, S110, involves a heating process: the heating device 31 raises the temperature and delivers a heating gas. This heating gas is then transported through the hot gas delivery pipe 30 to the second hot gas pipe 203, which in turn delivers it to the second adsorbent membrane module 2, raising the temperature within the second adsorbent membrane module 2 to a set temperature. After completing step S110, the next step, S120, is then performed.

[0080] Furthermore, the hot gas delivery pipeline 30 is connected to the first hot gas pipeline 103, the second hot gas pipeline 203, and the third hot gas pipeline 303, and the hot gas delivery pipeline 30 is equipped with a heating device 31 (e.g., Figures 3 to 6 As shown), the heating device 31 can be any one of a gas heater, an electric heater, or a heat transfer oil heater. The first gas delivery pipeline 72 delivers the concentrated carbon dioxide gas to the heating device 31 for heating (to a temperature higher than 100°C or 120°C, or below 100°C, not limited to the specification). After heating, a heated gas, which is concentrated carbon dioxide gas with a temperature, is delivered. The first hot gas pipeline 103, the second hot gas pipeline 203, or the third hot gas pipeline 303 delivers the heated gas to the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3 for heating. The hollow fiber tubular membrane adsorbent 4 allows the temperature inside the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3 to be raised to a set temperature. This set temperature can be 100°C, 120°C, or higher, or lower than 100°C, and is not limited to the specification. Since the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3 is heated by the heated gas, the temperature inside the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3 is also raised, optimizing the desorption efficiency and increasing the gas production, thereby increasing the adsorption capacity during subsequent adsorption.

[0081] Furthermore, the next step, S120, is a vacuum desorption process: The second adsorbent membrane module 2 undergoes desorption via the heated gas, and a concentrated carbon dioxide gas is emitted after desorption. This concentrated carbon dioxide gas is then transported through the second gas-generating pipeline 204 to the gas-generating delivery pipeline 40, where it is extracted by the vacuum pump 41 and transported to a gas-generating collection point. After completing step S120, the next step, S130, is performed.

[0082] Furthermore, the gas production and delivery pipeline 40 is connected to the first gas production pipeline 104, the second gas production pipeline 204, and the third gas production pipeline 304, respectively. The gas production and delivery pipeline 40 is equipped with a vacuum pump 41 and a gas production and delivery control valve 42 (e.g., ...). Figures 3 to 6 As shown), the gas production and delivery control valve 42 can be any one of a check valve, an electric valve, or a pneumatic valve, so that the gas flow direction of the gas production and delivery pipeline 40 can be controlled by the gas production and delivery control valve 42.

[0083] Furthermore, since the heating gas is a concentrated carbon dioxide gas with a temperature, and it is used for desorption to produce the concentrated carbon dioxide gas, the gas production bypass pipeline 71 then circulates to the heating device 31 for heating. The concentrated carbon dioxide gas with a temperature is not diluted during the circulation process, resulting in high purity of the produced gas and the capture of a large amount of concentrated carbon dioxide gas. After a set period of time or when the concentrated carbon dioxide gas reaches the set temperature, the gas production bypass pipeline 71's bypass control valve 711 is closed, while the gas production pipeline 40's gas production control valve 42 is opened (e.g., ...). Figure 6 As shown), the gas production pipeline 40 delivers the concentrated carbon dioxide gas to a gas production collection point (not shown) by heating and the vacuum pump 41 using a so-called temperature vacuum swing adsorption (TVSA) method, which is performed by evacuation. The gas production collection point is any one of a carbon dioxide concentration storage tank, a carbon dioxide concentration water tank, or a carbon dioxide concentration collection tank, for subsequent application or storage.

[0084] Furthermore, the next step, S130, is a cooling operation: the air supply pipeline 50 carries a second gas, which is delivered to the third adsorption membrane module 3 via the third air supply pipeline 305 for cooling. After cooling, the third adsorption membrane module 3 delivers the second gas to the outlet air supply pipeline 60 via the third outlet air supply pipeline 306 for discharge. After completing step S130, the next step, S140, is then performed.

[0085] When the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3 are used for cooling, the air outlet delivery pipe 60 is connected to the first air outlet pipe 106, the second air outlet pipe 206, and the third air outlet pipe 306, respectively, and the air supply delivery pipe 50 is connected to the first air supply pipe 105, the second air supply pipe 205, and the third air supply pipe 305, respectively. The air supply delivery pipe 50 is equipped with an air supply control valve 51 (e.g., Figures 3 to 6As shown), the air supply and delivery control valve 51 can be any one of a check valve, an electric valve, or a pneumatic valve, so that the air supply and delivery control valve 51 can control the gas flow direction of the air supply and delivery pipeline 50.

[0086] Furthermore, the air supply pipeline 50 has two implementations, the first of which is that the air supply pipeline 50 is directly connected to a second gas source pipeline 90 (e.g., Figure 3 and Figure 4 As shown), the second gas source pipeline 90 delivers a second gas, which is either nitrogen or air. The second gas source pipeline 90 is equipped with a second gas source control valve 91, which can be any one of a check valve, an electric valve, or a pneumatic valve, so that the gas flow direction of the second gas source pipeline 90 can be controlled by the second gas source control valve 91. The second gas in the second gas source pipe 90 enters the air supply pipe 50 and is then transported by the air supply pipe 50 to the first air supply pipe 105, the second air supply pipe 205, or the third air supply pipe 305. The second gas is then cooled by the first air supply pipe 105, the second air supply pipe 205, or the third air supply pipe 305. The cooled second gas is then transported to the air outlet pipe 60 through the first air outlet pipe 106, the second air outlet pipe 206, or the third air outlet pipe 306, and then discharged through the air outlet pipe 60. The aforementioned air supply pipeline 50 is equipped with an air supply device 52, which is either an air pump or a blower, to push the second gas in the air supply pipeline 52 into the first air supply pipeline 105, the second air supply pipeline 205 or the third air supply pipeline 305, and then deliver it to the first adsorbent membrane module 1, the second adsorbent membrane module 2 or the third adsorbent membrane module 3 for cooling.

[0087] The second embodiment involves connecting the air supply pipe 50 and the air outlet pipe 60 to a second gas storage tank 80 (e.g., ...). Figure 5 and Figure 6As shown, the second gas storage tank 80 is connected to a second gas source pipeline 90, which supplies a second gas, either nitrogen or air. The second gas source pipeline 90 is equipped with a second gas source control valve 91, which can be any of a check valve, an electric valve, or a pneumatic valve, allowing control of the gas flow direction through the second gas source pipeline 90. The second gas first enters the second gas storage tank 80 through the second gas source pipeline 90 for storage. Once a certain capacity is reached or the storage tank's capacity is met, the second gas source control valve is closed, allowing the second gas stored in the second gas storage tank 80 to be used. Then, the air supply control valve 51 on the air supply pipeline 50 is opened to allow the second gas in the second gas storage tank 80 to enter the air supply pipeline 50, and the air supply pipeline 50 delivers the gas to the first air supply pipeline 105, the second air supply pipeline 205, or the third air supply pipeline 305, and then the gas enters the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 305 respectively. The second gas is used for cooling within the membrane module 3. After cooling, the second gas is transported to the outlet conveying pipeline 60 through the first outlet pipeline 106, the second outlet pipeline 206, or the third outlet pipeline 306. The outlet conveying pipeline 60 then returns the gas to the second gas storage tank 80, enabling it to be recycled and reused through the second gas storage tank 80. When the second gas in the second gas storage tank 80 is insufficient, it is replenished by the second gas source pipeline 90, thereby increasing the overall operability. The aforementioned air supply pipeline 50 is equipped with an air supply device 52, which is one of an air pump or a blower, to push the second gas in the air supply pipeline 50 into the first air supply pipeline 105, the second air supply pipeline 205 or the third air supply pipeline 305, and then deliver it to the first adsorbent membrane module 1, the second adsorbent membrane module 2 or the third adsorbent membrane module 3 for cooling.

[0088] In addition, the next step, S140, involves switching the operating procedures: the adsorption and degassing operating procedure S100, the heating operating procedure S110, the vacuum desorption operating procedure S120, and the cooling operating procedure S130 run simultaneously, and after a set time, the first adsorption membrane module 1, the second adsorption membrane module 2, and the third adsorption membrane module 3 sequentially switch between the adsorption and degassing operating procedure S100, the heating operating procedure S110, the vacuum desorption operating procedure S120, and the cooling operating procedure S130.

[0089] Furthermore, the present invention utilizes a three-tower design consisting of a first adsorbent membrane module 1, a second adsorbent membrane module 2, and a third adsorbent membrane module 3 to perform cyclical adsorption, desorption, and cooling operations. These cyclical operations run simultaneously, and after a set time (which may be 5 minutes, 10 minutes, 20 minutes, 30 minutes, 40 minutes, etc., and is not limited to the aforementioned time), the first adsorbent membrane module 1, the second adsorbent membrane module 2, and the third adsorbent membrane module 3 sequentially switch between adsorption, desorption, and cooling.

[0090] Furthermore, the first gas storage tank 70 is provided with a gas production bypass pipeline 71 and a first gas delivery pipeline 72. The first gas delivery pipeline 72 is connected to the heating device 31, and the gas production bypass pipeline 71 is connected to the gas production delivery pipeline 40. The gas production bypass pipeline 71 is provided with a gas production bypass delivery control valve 711 (e.g., Figures 1 to 4 As shown, the gas bypass delivery control valve 711 can be any one of a check valve, an electric valve, or a pneumatic valve, enabling control of the gas flow direction in the gas bypass delivery pipeline 71. By closing the gas delivery control valve 42 of the gas delivery pipeline 40 and opening the gas bypass delivery control valve 711 of the gas bypass delivery pipeline 71, concentrated carbon dioxide gas entering the gas delivery pipeline 40 can be delivered into the gas bypass delivery pipeline 71. Furthermore, the gas delivery control valve 42 of the gas delivery pipeline 40 and the gas bypass delivery control valve 711 of the gas bypass delivery pipeline 71 have time-controlled, manual-controlled, and automatic-controlled operation modes.

[0091] When the gas production bypass control valve 711 of the gas production bypass pipeline 71 is opened and the gas production control valve 42 of the gas production pipeline 40 is closed (e.g.) Figure 5As shown), the first adsorbent membrane module 1, the second adsorbent membrane module 2, or the third adsorbent membrane module 3 is used for desorption, and a concentrated carbon dioxide gas is generated after desorption. The concentrated carbon dioxide gas after desorption is then transported to the gas production pipeline 40 via the first gas production pipeline 104, the second gas production pipeline 204, or the third gas production pipeline 304, respectively. The gas production pipeline 40 undergoes a so-called temperature vacuum swing through heating and vacuum pump 41 in a vacuum-assisted manner. The carbon dioxide concentrate gas is transported by adsorption (TVSA) through the bypass pipeline 71 to the first gas storage tank 70 for storage. The first gas storage tank 70 then transports the carbon dioxide concentrate gas through the first gas delivery pipeline 72 to the heating device 31 for heating (to a temperature of 100°C, 120°C, or higher, or below 100°C, not limited to the specification). After heating, a heated gas, which is the carbon dioxide concentrate gas with a temperature, is discharged. The first hot gas pipeline 103 and the second hot gas pipeline... Pipeline 203 or the third hot gas pipeline 303 respectively delivers heat to the first adsorbent tubular membrane module 1, the second adsorbent tubular membrane module 2, or the third adsorbent tubular membrane module 3 to heat the hollow fiber tubular membrane adsorbent material 4. Since the first adsorbent tubular membrane module 1, the second adsorbent tubular membrane module 2, or the third adsorbent tubular membrane module 3 is entered by the heated gas, the first adsorbent tubular membrane module 1, the second adsorbent tubular membrane module 2, or the third adsorbent tubular membrane module 3 are also heated, so that the desorption efficiency is optimized and the gas production is increased, so that the adsorption capacity can be increased during subsequent adsorption.

[0092] Finally, the present invention mainly uses a three-tower adsorption bed design to perform a cycle of adsorption, desorption, and cooling. The desorbed carbon dioxide concentrated gas is transported to the first gas storage tank 70 via the bypass pipeline 71. The carbon dioxide concentrated gas is then heated by the heating device 31 and enters the first adsorbent tubular membrane module 1, the second adsorbent tubular membrane module 2, or the third adsorbent tubular membrane module 3 to heat the hollow fiber tubular membrane adsorbent material 4. After reaching the set temperature, the gas production bypass control valve 711 is closed, while the gas production delivery valve 42 remains open. At this time, the vacuum pump 41 starts to perform a heated vacuum desorption (TVSA) procedure on the first adsorbent tubular membrane module 1, the second adsorbent tubular membrane module 2, or the third adsorbent tubular membrane module 3. By increasing the temperature and vacuum, the desorption efficiency is optimized, and the gas production is increased, which increases the adsorption capacity during subsequent adsorption and thus increases the overall practicality.

[0093] The specific embodiments described above further illustrate the purpose, technical solution, and beneficial effects of the present invention. It should be understood that the above descriptions are merely specific embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. An adsorption membrane carbon dioxide capture system for treating a gas containing carbon dioxide, comprising: A first adsorbent membrane module, the first adsorbent membrane module being provided with a first air inlet pipe, a first exhaust pipe, a first hot gas pipe, a first gas production pipe, a first air supply pipe and a first air outlet pipe. A second adsorbent membrane module, the second adsorbent membrane module being provided with a second air inlet pipe, a second exhaust pipe, a second hot gas pipe, a second gas production pipe, a second air supply pipe and a second air outlet pipe. A third adsorption membrane module, which is provided with a third air inlet pipe, a third exhaust pipe, a third hot gas pipe, a third gas production pipe, a third air supply pipe and a third air outlet pipe. A gas delivery pipeline is connected to the first air inlet pipeline, the second air inlet pipeline and the third air inlet pipeline respectively; An exhaust delivery pipeline is provided, which is connected to the first exhaust pipeline, the second exhaust pipeline and the third exhaust pipeline respectively; A hot gas delivery pipeline is connected to a first hot gas pipeline, a second hot gas pipeline and a third hot gas pipeline respectively, and the hot gas delivery pipeline is equipped with a heating device. A gas production and delivery pipeline is connected to the first gas production pipeline, the second gas production pipeline and the third gas production pipeline respectively. The gas production and delivery pipeline is equipped with a vacuum pump and a gas production and delivery control valve. An air supply pipeline is provided, which is connected to the first air supply pipeline, the second air supply pipeline and the third air supply pipeline respectively; An air outlet delivery duct, which is connected to the first air outlet duct, the second air outlet duct, and the third air outlet duct respectively; and A first gas storage tank is provided with a gas production bypass pipeline and a first gas delivery pipeline. The first gas delivery pipeline is connected to the heating device. The gas production bypass pipeline is connected to the gas production delivery pipeline. The gas production bypass pipeline is provided with a gas production bypass delivery control valve.

2. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The first, second, and third adsorbent tubular membrane modules are further filled with multiple tubular hollow fiber tubular membrane adsorbent materials.

3. The adsorption membrane carbon dioxide capture system according to claim 2, wherein, The tubular hollow fiber tubular membrane adsorbent is further comprising any one or a combination of zeolite, anion exchange resin, and metal-organic framework materials.

4. The adsorption membrane carbon dioxide capture system according to claim 2, wherein, The tubular hollow fiber membrane adsorbent material further includes at least one channel and at least one adsorbent layer, which further includes an amine-modified anion exchange resin material and a polymer material.

5. The adsorption membrane carbon dioxide capture system according to claim 4, wherein, The tubular hollow fiber membrane adsorbent material has a further diameter of D1, and the at least one pore has a further opening diameter of d1, wherein the condition is 1 < D1 / d1 < 99.

6. The adsorption membrane carbon dioxide capture system according to claim 2, wherein, The tubular hollow fiber tubular membrane adsorbent material has a further fill rate of 75% to 95%.

7. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The gas delivery pipeline further delivers the gas to be treated, which contains carbon dioxide, and the gas delivery pipeline is equipped with a gas delivery control valve.

8. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The first intake pipe is further provided with a first intake control valve, the second intake pipe is further provided with a second intake control valve, and the third intake pipe is further provided with a third intake control valve.

9. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The exhaust delivery pipeline is further connected to an exhaust device.

10. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The first exhaust pipe is further provided with a first exhaust control valve, the second exhaust pipe is further provided with a second exhaust control valve, and the third exhaust pipe is further provided with a third exhaust control valve.

11. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The first hot gas pipeline is further provided with a first hot gas control valve, the second hot gas pipeline is further provided with a second hot gas control valve, and the third hot gas pipeline is further provided with a third hot gas control valve.

12. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The heating device is further classified as a gas heater, an electric heater, or a hot kerosene heater.

13. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The first gas production pipeline is further provided with a first gas production control valve, the second gas production pipeline is further provided with a second gas production control valve, and the third gas production pipeline is further provided with a third gas production control valve.

14. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The first air supply duct is further provided with a first air supply control valve, the second air supply duct is further provided with a second air supply control valve, and the third air supply duct is further provided with a third air supply control valve.

15. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The air supply pipeline is further equipped with an air supply control valve.

16. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The air supply pipeline is further connected to a second gas source pipeline, which supplies a second gas, either nitrogen or air.

17. The adsorption membrane carbon dioxide capture system according to claim 16, wherein, The second gas source pipeline is further equipped with a second gas source control valve.

18. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The air supply pipeline and the air outlet pipeline are further connected to a second gas storage tank so that they can be recycled.

19. The adsorption membrane carbon dioxide capture system according to claim 18, wherein, The second gas storage tank is further connected to a second gas source pipeline, which delivers a second gas, either nitrogen or air.

20. The adsorption membrane carbon dioxide capture system according to claim 19, wherein, The second gas source pipeline is further equipped with a second gas source control valve.

21. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The air supply pipeline is further provided with an air supply device, which is either an air pump or a blower.

22. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The first air outlet duct is further provided with a first air outlet control valve, the second air outlet duct is further provided with a second air outlet control valve, and the third air outlet duct is further provided with a third air outlet control valve.

23. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, The gas production pipeline further delivers the gas to a gas collection point. When the gas production bypass pipeline's gas production bypass control valve is closed and the gas production pipeline's gas production control valve is open, the gas production pipeline delivers a concentrated carbon dioxide gas to the gas collection point via the vacuum pump in a vacuum manner.

24. The adsorption membrane carbon dioxide capture system according to claim 23, wherein, The gas collection point is further comprised of any one of the following: a carbon dioxide concentration storage tank, a carbon dioxide concentration water pool, or a carbon dioxide concentration collection tank.

25. The adsorption membrane carbon dioxide capture system according to claim 1, wherein, When the gas production bypass control valve of the gas production bypass pipeline is opened and the gas production control valve of the gas production pipeline is closed, the gas production pipeline delivers a concentrated carbon dioxide gas into the gas production bypass pipeline by means of vacuum pump in a vacuum manner, and then delivers it to the first gas storage tank through the gas production bypass pipeline.

26. A method for capturing carbon dioxide using an adsorbent membrane, mainly used in an adsorbent membrane carbon dioxide capture system, comprising a first adsorbent membrane module, a second adsorbent membrane module, a third adsorbent membrane module, a gas delivery pipeline, an exhaust delivery pipeline, a hot gas delivery pipeline, a gas production pipeline, an air supply pipeline, an air outlet pipeline, and a first gas storage tank. The first adsorbent membrane module is provided with a first air inlet pipeline, a first exhaust pipeline, a first hot gas pipeline, and a first gas production pipeline. The first air supply duct and the second air outlet duct are provided. The second absorbent membrane module is provided with a second air inlet duct, a second air outlet duct, a second hot air duct, a second gas production duct, a second air supply duct, and a second air outlet duct. The third absorbent membrane module is provided with a third air inlet duct, a third air outlet duct, a third hot air duct, a third gas production duct, a third air supply duct, and a third air outlet duct. The gas delivery ducts are respectively connected to the first air inlet duct, the second air inlet duct, and the third air inlet duct to form... The exhaust delivery pipeline is connected to the first exhaust pipeline, the second exhaust pipeline, and the third exhaust pipeline. The hot gas delivery pipeline is connected to the first hot gas pipeline, the second hot gas pipeline, and the third hot gas pipeline, and is equipped with a heating device. The gas production delivery pipeline is connected to the first gas production pipeline, the second gas production pipeline, and the third gas production pipeline, and is equipped with a vacuum pump and a gas production delivery control valve. The air supply delivery pipeline is connected to the first air supply pipeline, The second and third air supply ducts are connected, and the air outlet pipeline is connected to the first, second, and third air outlet ducts respectively. The first gas storage tank is equipped with a gas production bypass pipeline and a first gas delivery pipeline. The first gas delivery pipeline is connected to the heating device, and the gas production bypass pipeline is connected to the gas production delivery pipeline. The gas production bypass pipeline is equipped with a gas production bypass control valve. The main steps of the adsorption membrane carbon dioxide capture method include: Adsorption and exhaust operation procedure: The gas delivery pipeline is used to deliver a gas containing carbon dioxide to be treated. The gas containing carbon dioxide is delivered to the first adsorption membrane module through the first inlet pipeline for adsorption. After adsorption, the first adsorption membrane module sends out an adsorbed gas. The adsorbed gas is delivered to the exhaust delivery pipeline through the first exhaust pipeline and discharged through the exhaust delivery pipeline. Heating operation procedure: The heating device raises the temperature and sends out a heating gas. The heating gas is delivered to the second hot gas pipeline through the hot gas delivery pipeline, and then delivered to the second adsorbent membrane module through the second hot gas pipeline, so that the temperature inside the second adsorbent membrane module can be raised to a set temperature. Vacuum desorption operation procedure: When the second adsorbent membrane module is desorbed by the heated gas, a carbon dioxide concentrated gas is sent out after desorption. The carbon dioxide concentrated gas is transported to the gas production delivery pipeline through the second gas production pipeline, and then extracted by the vacuum pump to become a gas production and transported to a gas production collection point. Cooling operation procedure: The air supply pipeline has a second gas, which is delivered to the third adsorption membrane module through the third air supply pipeline for cooling. After cooling, the third adsorption membrane module delivers the second gas through the third air outlet pipeline to the air outlet pipeline for discharge; and Operating procedure switching: The adsorption and degassing operating procedure, the heating operating procedure, the vacuum desorption operating procedure, and the cooling operating procedure run simultaneously, and after a set time, the first adsorbent membrane module, the second adsorbent membrane module, and the third adsorbent membrane module sequentially switch between the adsorption and degassing operating procedure, the heating operating procedure, the vacuum desorption operating procedure, and the cooling operating procedure.

27. The carbon dioxide capture method using an adsorbent membrane according to claim 26, wherein, The gas production pipeline further uses the vacuum pump to pump the concentrated carbon dioxide gas through the gas production bypass pipeline to the first gas storage tank, and the first gas storage tank pumps the concentrated carbon dioxide gas through the first gas delivery pipeline to the heating device.

28. The method for capturing carbon dioxide using an adsorbent membrane according to claim 26, wherein, The gas collection point is further comprised of any one of the following: a carbon dioxide concentration storage tank, a carbon dioxide concentration water pool, or a carbon dioxide concentration collection tank.

29. The carbon dioxide capture method using an adsorbent membrane according to claim 26, wherein, The first, second, and third adsorbent tubular membrane modules are further filled with multiple tubular hollow fiber tubular membrane adsorbent materials.

30. The carbon dioxide capture method using an adsorbent membrane according to claim 29, wherein, The tubular hollow fiber tubular membrane adsorbent is further comprising any one or a combination of zeolite, anion exchange resin, and metal-organic framework materials.

31. The carbon dioxide capture method using an adsorbent membrane according to claim 29, wherein, The tubular hollow fiber membrane adsorbent material further includes at least one channel and at least one adsorbent layer, which further includes an amine-modified anion exchange resin material and a polymer material.

32. The carbon dioxide capture method using an adsorbent membrane according to claim 31, wherein, The tubular hollow fiber tubular membrane adsorbent material is further characterized by a diameter of D1, and the at least one pore is further characterized by an opening diameter of d1, wherein the condition is 1 < D1 / d1 < 99.

33. The carbon dioxide capture method using an adsorbent membrane according to claim 29, wherein, The tubular hollow fiber tubular membrane adsorbent further increases its fill rate to 75% to 95%.

34. The carbon dioxide capture method using an adsorption membrane according to claim 26, wherein, The gas delivery pipeline further delivers the gas to be treated, which contains carbon dioxide, and the gas delivery pipeline is equipped with a gas delivery control valve.

35. The carbon dioxide capture method using an adsorbent membrane according to claim 26, wherein, The first intake pipe is further provided with a first intake control valve, the second intake pipe is further provided with a second intake control valve, and the third intake pipe is further provided with a third intake control valve.

36. The carbon dioxide capture method using an adsorbent membrane according to claim 26, wherein, The exhaust delivery pipeline is further connected to an exhaust device.

37. The carbon dioxide capture method using an adsorbent membrane according to claim 26, wherein, The first exhaust pipe is further provided with a first exhaust control valve, the second exhaust pipe is further provided with a second exhaust control valve, and the third exhaust pipe is further provided with a third exhaust control valve.

38. The carbon dioxide capture method using an adsorbent membrane according to claim 26, wherein, The first hot gas pipeline is further provided with a first hot gas control valve, the second hot gas pipeline is further provided with a second hot gas control valve, and the third hot gas pipeline is further provided with a third hot gas control valve.

39. The carbon dioxide capture method using an adsorption membrane according to claim 26, wherein, The heating device is further classified as a gas heater, an electric heater, or a hot kerosene heater.

40. The carbon dioxide capture method using an adsorption membrane according to claim 26, wherein, The first gas production pipeline is further provided with a first gas production control valve, the second gas production pipeline is further provided with a second gas production control valve, and the third gas production pipeline is further provided with a third gas production control valve.

41. The carbon dioxide capture method using an adsorption membrane according to claim 26, wherein, The first air supply duct is further provided with a first air supply control valve, the second air supply duct is further provided with a second air supply control valve, and the third air supply duct is further provided with a third air supply control valve.

42. The carbon dioxide capture method using an adsorption membrane according to claim 26, wherein, The air supply pipeline is further equipped with an air supply control valve.

43. The carbon dioxide capture method using an adsorbent membrane according to claim 26, wherein, The air supply pipeline is further connected to a second gas source pipeline, which supplies a second gas, either nitrogen or air.

44. The carbon dioxide capture method using an adsorption membrane according to claim 43, wherein, The second gas source pipeline is further equipped with a second gas source control valve.

45. The carbon dioxide capture method using an adsorbent membrane according to claim 26, wherein, The air supply pipeline and the air outlet pipeline are further connected to a second gas storage tank so that they can be recycled.

46. ​​The carbon dioxide capture method using an adsorption membrane according to claim 45, wherein, The second gas storage tank is further connected to a second gas source pipeline, which delivers a second gas, either nitrogen or air.

47. The carbon dioxide capture method using an adsorption membrane according to claim 46, wherein, The second gas source pipeline is further equipped with a second gas source control valve.

48. The method for capturing carbon dioxide using an adsorbent membrane according to claim 26, wherein, The air supply pipeline is further provided with an air supply device, which is either an air pump or a blower.

49. The carbon dioxide capture method using an adsorbent membrane according to claim 26, wherein, The first air outlet duct is further provided with a first air outlet control valve, the second air outlet duct is further provided with a second air outlet control valve, and the third air outlet duct is further provided with a third air outlet control valve.

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