Carbon capture system with solid amine material suitable for various particle sizes

Abstract

To provide a carbon capture system for adsorbing carbon dioxide in flue gas / air by a solid amine material, capable of achieving screening of a particle size and matching different desorption processes according to the particle size of a solid amine, and achieving large-scale industrial application of a carbon capture technology by a solid amine method.SOLUTION: A carbon capture system is provided, including an adsorption assembly 1, a separation unit 2, a first desorption unit 3, a fine powder recycling assembly 4, a second desorption unit 5 and a fine powder bin assembly 6, wherein the adsorption assembly adsorbs carbon dioxide in external flue gas / air by solid amines with mixed particle sizes, the separation unit separates the solid amines with mixed particle sizes, the first desorption unit desorbs the separated solid amines by bubbling, the fine powder recycling assembly screens out the solid amines leaked from an exhaust end of the first desorption unit, and the second desorption unit feeds the recycled solid amine particles into the second desorption unit for vacuum desorption.SELECTED DRAWING: Figure 1

Description

[Technical Field]

[0001] This application relates to the field of carbon capture, and more particularly to a solid amine material carbon capture system suitable for a variety of particle sizes. [Background technology]

[0002] Solid amine adsorbents are an emerging carbon dioxide capture material. By modifying porous materials with amino groups, the large specific surface area of ​​the porous material can improve the uniformity of the amine dispersion and increase the contact area between the amine and gas. They also have advantages such as ease of operation and low regeneration energy consumption, making them a hot research topic in the field of carbon dioxide capture.

[0003] During use, as the material is transported and cycled through the adsorption or desorption process, the particle size of the solid amine particles gradually decreases, resulting in an increasing proportion of solid amine in powder form. It is well known that large-particle solid amine powder materials and small-particle solid materials require different desorption reaction systems. Generally, solid amine particles typically have a particle size greater than 3 mm and are primarily used in fixed-bed systems, while powdered materials have a broad particle size distribution, typically between 10 μm and 1000 μm, and are primarily used in fluidized-bed systems. Generally, powdered materials react with low-concentration carbon dioxide in flue gas or other application conditions in fluidized-bed systems, resulting in more thorough mixing and higher reaction efficiency. However, the broad initial particle size distribution of powdered materials and their susceptibility to attrition in fluidized-bed systems limit the capture scale of this technology.

[0004] Solid amines with different particle sizes require different desorption devices. Therefore, in order to meet the desorption requirements of solid amine particles with different particle sizes in a specific production process, the solid amine particles need to be sieved after being discharged from the adsorption system and then entered into different desorption devices, which reduces the operating efficiency. Solid amine desorption must be carried out under oxygen-free conditions, and in order to collect high-purity CO2, desorption can only be carried out under vacuum or pure CO2 conditions. Furthermore, the desorbed material will be re-adsorbed when the temperature drops, so it is necessary to create a process flow and fabricate equipment for solid amine carbon capture technology.

[0005] Based on this, urgent research and development of carbon capture systems using solid amine materials suitable for various particle sizes is awaited. Summary of the Invention [Problem to be solved by the invention]

[0006] The present application provides a carbon capture system using solid amine materials suitable for various particle sizes, which can solve at least one technical problem in the prior art. [Means for solving the problem]

[0007] Specifically, the technical solutions are as follows:

[0008] an adsorption assembly connected to the outside, which is used to adsorb carbon dioxide in the external flue gas / air with solid amines of mixed particle sizes to obtain mixed particles after carbon capture; a separation unit connected to the discharge end of the adsorption assembly, the separation unit being used to separate the mixed particle size solid amine and collect the separated solid amine; a first desorption unit disposed at the solid discharge end of the separation unit, for desorbing the separated solid amine by bubbling; a fines collection assembly provided at the exhaust end of the first desorption unit, the fines collection assembly being used to sieve the solid amine leaked from the exhaust end of the first desorption unit to obtain collected solid amine particles; and a second desorption unit connected to the discharge end of the fines collection assembly and used to deliver the collected solid amine particles to the second desorption unit for vacuum desorption.

[0009] The fines collection assembly includes: an auxiliary separation unit connected to the exhaust end of the first desorption unit, for collecting the leaked solid amine particles and obtaining a gas to be recovered; an air-sorting separation unit connected to the exhaust end of the auxiliary separation unit, for air-sorting the solid amine particles leaking from the exhaust end of the auxiliary separation unit to obtain the recovered solid amine particles; The solid discharge end of the air separation unit is connected to the feed end of the second desorption unit, and is used to feed the recovered solid amine particles into the second desorption unit for vacuum desorption.

[0010] The wind sorting separation unit comprises: a housing connected to the exhaust end of the auxiliary separation unit, for collecting the gas to be air-filtered containing the leaked solid amine particles, which is discharged from the exhaust end of the auxiliary separation unit; a dividing mechanism provided at an intake end of the housing, for dividing the gas to be air-filtered that has entered the housing, to obtain a divided gas containing solid amine particles; an air separation mechanism provided on one side of the housing and used for air separation of solid amine particles in the diverted gas; a collection mechanism provided on the other side of the housing and facing the air separation mechanism, for collecting the recovered solid amine particles obtained after air separation by the air separation mechanism and sending them to the second desorption unit.

[0011] The wind sorting mechanism includes: a gas storage member connected to an external gas source; and at least two communication members provided in communication between the gas storage member and the housing, and used to send a pulsed airflow into the housing to air-separate solid amine particles in the diverted gas.

[0012] The flow dividing mechanism includes: a heating tube set provided at the intake end of the housing and used to heat the gas to be air-filtered that has entered the housing; a guide group provided at the intake end of the housing and located on the side of the heating pipe group facing the bottom of the housing, for grouping and guiding the gas to be air-filtered; The present invention also includes a partition plate set that is provided between the air separation mechanism and the collection mechanism and is used to decelerate the gas to be air separated after being grouped and guided, thereby facilitating the air separation by the air separation mechanism and the collection of solid amine particles by the collection mechanism.

[0013] The partition plate set includes: at least three divider members; A ventilation hole for passing gas is provided between any two laterally adjacent partition members, Any two adjacent partition members in the vertical direction are alternately arranged, and the space between any two adjacent partition members in the vertical direction serves as a communication passage between the air sorting mechanism and the collecting mechanism.

[0014] The collection mechanism includes: a connecting member provided on one side of the housing and facing the wind sorting mechanism; a collection tube disposed between the connecting member and the inner wall of the housing; The connecting member is provided with at least two conduits that communicate with the collection pipe, the collection tube is disposed at the discharge end of the air separator and is used to collect the recovered solid amine particles; The delivery end of the collection tube is connected to the delivery end of the second detachment unit.

[0015] The housing includes: a rectangular segment used to arrange the flow diverter, the wind separator, and the collector; and an enlarged segment connected to the rectangular segment, the size of the end remote from the rectangular segment being at least twice the size of the rectangular segment.

[0016] The adsorption assembly comprises: a lower unit having a solid inlet end connected to the solid outlet end of the first desorption unit for receiving solid amine of mixed particle size and a gas inlet end connected to external flue gas / air; a middle unit, the inlet end of which is connected to the outlet end of the lower unit, the middle unit being used to capture carbon by solid amine of mixed particle sizes that has entered the middle unit and to lower the reaction temperature during carbon capture; an upper unit, the inlet end of which is connected to the outlet end of the middle unit and is used to increase the flow rate and thoroughly mix the solid amine of mixed particle sizes; a first venturi pipe provided between the lower unit and the middle unit; a second venturi tube provided between the middle unit and the upper unit.

[0017] The middle unit is The middle housing and At least one heat exchange tube provided on the inner wall of the middle housing and used to lower the reaction temperature during carbon capture; a fin unit provided on the outside of the heat exchange tube, which is used to increase the heat exchange area and at the same time break up agglomerated materials in the mixed particle size solid amine.

[0018] The solid amine material carbon capture system suitable for various particle sizes further comprises a fines silo assembly; The fines silo assembly is disposed between the separation unit and the second desorption unit and is used to store the solid amine particles provided by the separation unit and the fines recovery assembly.

[0019] The fine powder silo assembly comprises: a cloth bag collecting unit, the inlet end of which is connected to the gas outlet end of the separation unit and which is used to collect solid amine particles leaking from the gas outlet end of the separation unit; a silo connected to the solid discharge end of the cloth bag collecting unit and used to collect the solid amine particles collected in the cloth bag collecting unit; a vacuum silo connected to the discharge end of the silo and the fines collection assembly, respectively, and used to store the solid amine particles provided by the separation unit and the fines collection assembly; The vacuum silo is connected to the second desorption unit and is used to vacuum desorb the solid amine particles provided by the separation unit, the fines recovery assembly.

[0020] The cloth bag collecting unit includes: a screen layer used to collect solid amine particles while simultaneously allowing gas to escape; a heating element disposed in the middle of the screen layer and used to dry the solid amine particles.

[0021] The first detachable unit is a first detachable housing having an air intake port at a bottom portion close to the ground for introducing flowing air; at least two partition plates provided in the first detachable housing, for moving the solid amine particles in a bubbling state within the first detachable housing when a flowing air stream is introduced; a heating pipe provided between any two adjacent partition plates and used to provide heat during desorption; a screen disposed within the first desorption housing and used to block solid amine leaking from the exhaust end of the first desorption unit; a vibrating and beating mechanism provided on the screen, which is used to intermittently vibrate and beate the screen to cause solid amine adhering to the screen to fall into the first detachment housing.

[0022] an outlet of the solids discharge end of the separation unit is located at the bottom of the first desorption unit; In the fine powder recovery assembly, the outlet of the delivery end of the auxiliary separation unit is located at the bottom of the first detachment unit, and the outlet position of the delivery end of the auxiliary separation unit is lower than the outlet position of the solid delivery end of the separation unit.

[0023] The solid amine material carbon capture system suitable for various particle sizes further comprises a booster fan; The booster fan is disposed between the gas discharge end of the fine powder recovery assembly and the intake end of the first detachment unit, and is used to provide a flowing wind to the first detachment unit. [Effects of the Invention]

[0024] The present application has at least the following beneficial effects:

[0025] The carbon capture system for various particle sizes described in this application uses an adsorption assembly to adsorb carbon dioxide from external flue gas / air using solid amines of mixed particle sizes, obtaining mixed particles after carbon capture, then separating the solid amines of mixed particle sizes using a separation unit and collecting the separated solid amines, using a first desorption unit to desorb the separated solid amines by bubbling, and using a fine powder recovery assembly to sieve the solid amines leaking from the exhaust end of the first desorption unit to obtain recovered solid amine particles, and finally sending the recovered solid amine particles to the second desorption unit for vacuum desorption. The carbon capture system for various particle sizes described in this application can achieve particle size sieving and match different desorption processes according to the particle size of the solid amine, not only solving the difficulty of repeated use of solid amine materials, but also realizing large-scale engineering applications of the technology and achieving optimal energy consumption and efficiency ratios.

[0026] The system described in this application overcomes the drawbacks of vacuum desorption equipment, such as low throughput and fluidized bed desorption equipment, and can better control materials of different particle sizes to react with the highest efficiency. By combining different desorption methods, the system achieves larger equipment size and higher efficiency in solid amine material carbon capture technology. [Brief explanation of the drawings]

[0027] In order to more clearly explain the technical solutions of the embodiments of the present application, the following will briefly describe the drawings used in the embodiments. The following drawings only illustrate some embodiments of the present application, and should not be considered as limiting the scope. It should be understood that those skilled in the art can conceive of other related drawings based on these drawings without any creative efforts. [Figure 1] 1 is a structural schematic diagram of a carbon capture system according to the present application. [Figure 2] FIG. 2 is a structural schematic diagram of the adsorption assembly in FIG. 1. [Figure 3] FIG. 3 is a cross-sectional view taken along the line AA in FIG. 2. [Figure 4] FIG. 2 is a structural schematic diagram of the fine powder recovery assembly in FIG. 1. [Figure 5] FIG. 5 is a structural schematic diagram of the wind sorting and separation unit in FIG. 4. [Figure 6] 6 is a structural schematic diagram of a housing, a flow dividing mechanism, an air sorting mechanism, and a collecting mechanism in FIG. 5. [Figure 7] FIG. 2 is a structural schematic diagram of the fine powder silo assembly in FIG. 1. [Figure 8] FIG. 8 is a cross-sectional view taken along the line BB in FIG. [Figure 9] FIG. 2 is a structural schematic diagram of a first detachable unit. DETAILED DESCRIPTION OF THE INVENTION

[0028] As will be understood by those skilled in the art, the modules in the devices in the scenarios can be distributed among the devices in the scenarios according to the description of the scenarios, and may be located in one or more devices different from the scenarios with corresponding variations. The modules in the scenarios may be combined into one module or may be further separated into multiple sub-modules.

[0029] To elaborate on the present application, the following examples are particularly provided, and the technical solutions of the present application are described in detail with reference to the drawings.

[0030] Specific Example I: This application provides one example.

[0031] As shown in FIG. 1, the system includes an adsorption assembly 1, a separation unit 2, a first desorption unit 3, a fine powder recovery assembly 4, a second desorption unit 5, a fine powder silo assembly 6, and a booster fan 7. The adsorption assembly 1 is connected to the outside and is used to adsorb carbon dioxide in the external flue gas / air with solid amines of mixed particle sizes to obtain mixed particles after carbon capture. The separation unit 2 is connected to the discharge end of the adsorption assembly 1 and is used to separate the solid amines of mixed particle sizes and collect the separated solid amines. The first desorption unit 3 is connected to the discharge end of the separation unit 2. The first desorption unit 3 is provided at the solid discharge end and is used to desorb the separated solid amine by bubbling. The fine powder collection assembly 4 is provided at the exhaust end of the first desorption unit 3 and is used to sieve the solid amine leaked from the exhaust end of the first desorption unit 3 to obtain recovered solid amine particles. The second desorption unit 5 is connected to the discharge end of the fine powder collection assembly 4 and is used to send the recovered solid amine particles to the second desorption unit 5 for vacuum desorption. This carbon collection system is made of solid amine material suitable for various particle sizes.

[0032] Preferably, in this embodiment, the adsorption assembly 1 is a device for carbon capture with mixed particle size solid amine particles, the first desorption unit 3 is a bubbling fluidized bed, and the second desorption unit 5 is a vacuum desorber.

[0033] Specifically, as shown in FIG. 2, the adsorption assembly 1 includes a lower unit 101, a middle unit 102, an upper unit 103, a first Venturi tube 104, and a second Venturi tube 105. The solid inlet end of the lower unit 101 is connected to the solid outlet end of the first desorption unit 3 to receive solid amines of mixed particle sizes. The gas inlet end of the lower unit 101 is connected to external flue gas / air. The inlet end of the middle unit 102 is connected to the outlet end of the first Venturi tube 104. The solid amine of mixed particle sizes that enters unit 102 is used to capture carbon, and the middle unit 102 is used to lower the reaction temperature during carbon capture. The inlet end of the upper unit 103 is connected to the outlet end of a second Venturi pipe 105, which is used to increase the flow rate and thoroughly mix the solid amine of mixed particle sizes. A first Venturi pipe 104 is located between the lower unit 101 and the middle unit 102, and the second Venturi pipe 105 is located between the middle unit 102 and the upper unit 103.

[0034] In this embodiment, the adsorption assembly 1 includes a secondary venturi structure, which allows the flue gas containing carbon dioxide to flow rapidly through the lower unit 101, while adding large-particle solid amine from the lower unit 101, thereby increasing the flow rate and breaking up the agglomerated bulk particles. The air then enters the middle unit 102, achieving thorough mixing and adsorption of the solid amine material with the flue gas. The adsorption can be performed at room temperature. To dissipate heat during the adsorption reaction, the middle unit 102 is equipped with a cooling water coil and a cooling water jacket to facilitate the adsorption reaction. The upper unit 103 is installed above the middle unit 102, and the upper unit 103 is designed with an inlet for adding small-particle materials. Since no cooling coil is installed, the flow rate increases as the flue gas passes through the upper unit 103, allowing the large-particle materials to mix thoroughly with the small-particle materials and further adsorb the carbon dioxide in the flue gas. The added small-particle materials can lower the average temperature of the materials, which helps the reaction proceed. As a result, the carbon dioxide concentration in the upper unit 103 is low and the heat dissipation from the adsorption reaction is small. The upper unit 103 is designed with only a water-cooled jacket rather than a cooling coil, which reduces the wear of the small-particle materials. The connection between the lower unit 101, middle unit 102, upper unit 103, and the first Venturi tube 104 and second Venturi tube 105 achieves a uniform bed temperature, high adsorption efficiency, and low wear rate.

[0035] 3, the middle unit 102 includes a middle housing 1021, at least one heat exchange tube 1022, and a fin unit 1023. The heat exchange tube 1022 is located on the inner wall of the middle housing 1021 and serves to reduce the reaction temperature during carbon capture. The fin unit 1023 is located on the outside of the heat exchange tube 1022 and serves to increase the heat exchange area and simultaneously break down agglomerated materials in the mixed particle size solid amine. Preferably, the middle unit 102 has a jacket-like structure, where cooling water is introduced between the layers to instantly remove heat dissipated during the adsorption reaction. The middle unit 102 is equipped with a heat exchange tube bundle with parallel fins in the cross-sectional direction, which allows vigorous convection to remove heat dissipated during the adsorption reaction. The sharp edges of the fins can disperse and break down large particle size agglomerated materials. The cross-sectional flow velocity of the middle unit 102 is 1 to 1.5 m / s, the first venturi tube 104 and the second venturi tube 105 are both 2 to 3 m / s, and the total height of the adsorption assembly 1 is 25 to 30 m.

[0036] Specifically, separation unit 2 is installed at the discharge end of adsorption assembly 1 to separate the mixed-particle size solid amine and collect the separated solid amine. Preferably, separation unit 2 is a cyclone with a separation efficiency of 85% to 90%. The material that reaches the cyclone resides in adsorption assembly 1 for at least 30 seconds, meeting the adsorption reaction time for the solid amine material and achieving an adsorption efficiency of over 95%. Larger particles enter the bubbling fluidized bed desorber through the cyclone inlet. However, due to the operating characteristics of the bubbling fluidized bed, some mixed-particle size solid amine particles in the 1-100 μm particle size range will leak from the top of the bubbling fluidized bed, i.e., the gas discharge end, during collection in separation unit 2. The separation unit 2 described in this example collects solid amine particles between 50 and 1000 μm, and an appropriate separation efficiency must be selected. If the separation efficiency is too high, the inlet flow rate will be too high, resulting in severe material wear. If the separation efficiency is too low, the proportion of small-particle materials in the material transported to the subsequent bubbling fluidized bed will be high, and these small-particle materials will not be able to reach the heating time required for the desorption reaction, resulting in reduced desorption efficiency. Therefore, for such materials, a separator efficiency of 85% to 90% is optimized through experimentation and allocation of the processing capacity of the downstream desorber. The inner surface of the separation unit 2 is specially coated to reduce surface roughness and reduce material wear within the device.

[0037] In order to return this solid amine to the desorption process and improve the desorption rate, this embodiment provides a fine powder recovery assembly 4. As shown in Figure 4, the fine powder recovery assembly 4 includes an auxiliary separation unit 401 and a pneumatic sorting separation unit 402. The auxiliary separation unit 401 is connected to the exhaust end of the first desorption unit 3 and is used to collect the leaked solid amine particles and obtain the gas to be recovered. The pneumatic sorting separation unit 402 is connected to the exhaust end of the auxiliary separation unit 401 and is used to pneumatically sort the solid amine particles with a particle size of 1 to 100 μm that have leaked from the exhaust end of the auxiliary separation unit 401 and obtain the recovered solid amine particles. The solid discharge end of the pneumatic sorting separation unit 402 is connected to the inlet end of the second desorption unit 5 and is used to send the recovered solid amine particles to the second desorption unit 5 for vacuum desorption. Preferably, the auxiliary separation unit 401 is a cyclone, which selectively collects solid amine particles of 50-100 μm. However, some solid amine particles will also leak from the gas discharge end. In order to collect these solid amine particles, the present embodiment adopts a wind-based separation unit 402.

[0038] The auxiliary separation unit 401 is used to capture the small amount of powder material that escapes with the carbon dioxide gas. Its collection efficiency is over 90%. By controlling the inlet air velocity, it primarily separates fine particles between 50 and 100 μm in size. Approximately 10% of the fine particles exit the upper airflow outlet of the separation unit 2 and enter the fine particle collection assembly 4. While this fraction of fine particles is small, the total mass is still large. If the fine particles are not collected, the downstream equipment will become clogged. Furthermore, the adsorbent material is expensive. Therefore, to operate the system economically, as much as possible must be collected. The auxiliary separation unit 401 differs most from the separation unit 2 in its low inlet flow velocity. Because the particle size of this powder is very small, excessively high inlet air velocity will result in severe material wear and excessive loss of adsorbent material.

[0039] The bottom outlet of the auxiliary separation unit 401 enters the material layer of the first desorption unit 3, collects the material that has not completely reacted, and forms a small material circulation system, thereby reducing the leakage of powder material, improving the reaction efficiency, and increasing the residence time of the material in the bed, thereby enabling the carbon dioxide to be thoroughly desorbed.

[0040] Specifically, as shown in FIG. 5, the pneumatic separation unit 402 includes a housing 4021, a dividing mechanism 4022, a pneumatic separation mechanism 4023, and a collecting mechanism 4024, of which the housing 4021 is connected to the exhaust end of the auxiliary separation unit 401 and is used to collect the gas to be pneumatically separated containing the leaked solid amine particles that comes out of the exhaust end of the auxiliary separation unit 401; the dividing mechanism 4022 is provided at the intake end of the housing 4021 and is used to collect the gas to be pneumatically separated that comes into the housing 4021. The housing 4021 is provided with an air separation mechanism 4023 which is used to separate the solid amine particles from the separated gas and obtain a separated gas containing solid amine particles. The air separation mechanism 4023 is provided on one side of the housing 4021 and is used to separate the solid amine particles from the separated gas by air separation. The collection mechanism 4024 is provided on the other side of the housing 4021 and is opposite to the air separation mechanism 4023 and is used to collect the recovered solid amine particles obtained after air separation by the air separation mechanism 4023 and send them to the second desorption unit 5.

[0041] 6, the air separation mechanism 4023 preferably includes a gas storage member 40231 and three communication members 40232, of which the gas storage member 40231 is connected to an external gas source, and the communication member 40232 is provided to communicate between the gas storage member 40231 and the housing 4021, and is used to send a pulsed airflow into the housing 4021 to air separate the solid amine particles in the diverted gas. In use, the gas storage member 40231 provides the gas source, and the three parallel communication members 40232 sequentially blow pulsed airflows into the housing 4021. Since the solid amine particles have different sizes and weights, the air separation blows out and collects solid amine particles of different particle sizes, mainly solid amine particles of 1 to 50 μm in size.

[0042] In order to completely blow up the solid amine particles and facilitate their air separation, as shown in FIG. 6 , the flow dividing mechanism 4022 includes a heating pipe set 40221, a guide set 40222, and a partition plate set 40223, of which the heating pipe set 40221 is located at the intake end of the housing 4021 and can heat the gas to be air-separated entering the housing 4021. The guide set 40222 is located at the intake end of the housing 4021 and is located on the side of the heating pipe set 40221 facing the bottom of the housing 4021 and is used to group and guide the gas to be air-separated. The partition plate set 40223 is located between the air-separating mechanism 4023 and the collecting mechanism 4024 and is used to slow down the gas to be air-separated after being grouped and guided, thereby facilitating the air-separating by the air-separating mechanism 4023 and the collection of the solid amine particles by the collecting mechanism 4024.

[0043] The bottom outlet of the auxiliary separation unit 401 enters the material layer of the bubbling fluidized bed, collecting any unreacted material and forming a small material cycle, thereby reducing powder leakage, improving reaction efficiency, and increasing the residence time of the material in the bed, allowing for thorough desorption of carbon dioxide. The material entering the air sorting separation unit 402 has a short residence time in the first desorption unit 3, is not heated sufficiently, and desorption is insufficient. As a result, carbon dioxide will easily be re-adsorbed once the temperature drops. To avoid this, the airflow first passes through the heating pipe set 40221, the temperature of which is controlled at 110-160°C to ensure that the temperature of the material does not drop as it flows through the heating pipe set 40221, and further heating desorption is performed.

[0044] Preferably, as shown in Figure 6, the partition plate set 40223 includes at least three partition plate members 40223A, and ventilation holes 40222B for passing gas are provided between any two horizontally adjacent partition plate members 40223A, and ventilation holes 40222B are provided alternately between any two vertically adjacent partition plate members 40223A, and the space between any two vertically adjacent partition plate members 40223A serves as a communication passage between the air sorting mechanism 4023 and the collection mechanism 4024.

[0045] As shown in Figure 6, the collection mechanism 4024 includes a connecting member 40241 and a collection pipe 40242, of which the connecting member 40241 is arranged on one side of the housing 4021 and facing the air separation mechanism 4023, the collection pipe 40242 is arranged between the connecting member 40241 and the inner wall of the housing 4021, the connecting member 40241 has at least two pipes 40241A communicating with the collection pipe 40242, the collection pipe 40242 is arranged at the discharge end of the air separation mechanism 4023 and is used to collect the recovered solid amine particles, and the discharge end of the collection pipe 40242 is connected to the feed end of the second detachment unit 5.

[0046] As shown in Figure 6, the housing 4021 includes a rectangular segment 40211 and an enlarged segment 40212, of which the rectangular segment 40211 is used to arrange the diverting mechanism 4022, the wind sorting mechanism 4023 and the collecting mechanism 4024, and the enlarged segment 40212 is connected to the rectangular segment 40211, and the size of the end away from the rectangular segment 40211 is more than twice that of the rectangular segment 40211.

[0047] In use, in the direction of the airflow, above the heating pipe set 40221 is the guide set 40222, and the structure of the guide set 40222 can increase the strength of the airflow, enhance the flow, and prevent powder from falling and blocking the pores. The powder, accompanied by the airflow, passes through the intake holes formed by the guide group 40222 and then enters the partition group 40223. The partition group 40223 blocks the fine powder using semicircular partition members 40223A that are tightly connected in multiple layers. The airflow escapes through the gaps between the partition members 40223A, and most of the fine powder is blocked by the partition members 40223A, moving downward and falling to the bottom or the surface of the next partition member 40223A. Carbon dioxide is sprayed in pulses from the connecting member 40232 on the side, blowing the powder into the opposite pipeline 40241A. Since the collection pipe 40242 is connected to the inclined pipeline 40241A, the powder merges with the collection pipe 40242, and the specified material position is always maintained within the pipeline 40241A, thereby achieving a material sealing effect. Within the housing 4021, a small amount of fine powder escapes with the airflow after passing through the multi-stage partition members 40223A. Above the partition member 40223A, an enlarged segment 40212 is installed. This enlarged segment 40212 is an eccentric, normal-flow region with a spatial cross-section three to five times larger than that of the rectangular segment 40211. This rapidly reduces the airflow velocity, allowing the powder material to circulate internally along the eccentric structure under the force of gravity and be collected by the collection pipe 40242. The gas inlet of the housing 4021 is located at the top of the auxiliary separation unit 401, and pure carbon dioxide is obtained after air separation. The outlet of the housing 4021 is an exhaust port, which may be connected to a rear-end carbon dioxide storage device or a booster fan to be introduced into the air chamber at the bottom of the bubbling fluidized bed to serve as a fluidized airflow. It may also be connected to a compressed pulse tank to serve as a gas source for the gas storage member 40231.

[0048] Specifically, as shown in FIG. 7, the fine powder silo assembly 6 is disposed between the separation unit 2 and the second desorption unit 5, and is used to store the solid amine particles provided by the separation unit 2 and the fine powder recovery assembly 4. Preferably, the fine powder silo assembly 6 includes a cloth bag collecting unit 601, a silo 602, and a vacuum silo 603, of which the cloth bag collecting unit 601 has its inlet end connected to the gas outlet end of the separation unit 2, and is used to collect the solid amine particles leaked from the gas outlet end of the separation unit 2; The silo 602 is connected to the solid discharge end of the cloth bag collecting unit 601 and is used to collect the solid amine particles collected in the cloth bag collecting unit 601; the vacuum silo 603 is connected to the discharge ends of the silo 602 and the fine powder collecting assembly 4 respectively and is used to store the solid amine particles provided by the separation unit 2 and the fine powder collecting assembly 4; the vacuum silo 603 is connected to the second desorption unit 5 and is used to vacuum desorb the solid amine particles provided by the separation unit 2 and the fine powder collecting assembly 4.

[0049] Preferably, conventional powder collection generally adopts the cloth bag method, but the technical conditions in the embodiment are not suitable for the cloth bag collection method, mainly because the volume of the cloth bag needs to be very large to match the large throughput of fine powder and high temperature, and an anaerobic environment is required in the desorption stage, and pure carbon dioxide can only be introduced as a pulsed separation gas, which requires the consumption of a large amount of carbon dioxide and cannot meet the desorption gas volume.

[0050] As shown in FIG. 8, the cloth bag collecting unit 601 includes a screen layer 6011 and a heating element 6012, of which the screen layer 6011 is used to collect solid amine particles and discharge gas at the same time, and the heating element 6012 is located in the middle of the screen layer 6011 and is used to dry the solid amine particles.

[0051] In concrete use, the screen layer 6011 is a metal filter capable of collecting materials of 5 to 50 μm in size. The flue gas passes through the screen layer 6011 and then flows out. A heating element 6012, such as an electric heating rod, is provided along the central axis of each screen layer 6011. The temperature is controlled to 90°C. The heating element 6012 heats the material to 70°C through radiant heat exchange, and a first drying step is performed. The purpose of this is to increase the temperature of the material entering the second desorption unit, shorten the vacuum desorption reaction time, and dry the water adsorbed on the material, thereby reducing the energy consumption of the desorption device and the vacuum pump 5A.

[0052] As shown in FIG. 9 , the first desorption unit 3 includes a first desorption housing 301, at least two partitions 302, a heating tube 303, a screen 304, and a vibration and beating mechanism 305. The first desorption housing 301 has an air inlet at its bottom near the ground for introducing flowing air. The at least two partitions 302 are provided within the first desorption housing 301 and are used to move the solid amine particles within the first desorption housing 301 in a bubbling state when flowing air is introduced. The heating tube 303 is provided between any two adjacent partitions 302 and is used to provide heat during desorption. The screen 304 is provided within the first desorption housing 301 and is used to block solid amine leaking from the exhaust end of the first desorption unit 3. The vibration and beating mechanism 305 is provided on the screen 304 and is used to intermittently vibrate and beate the solid amine adhering to the screen 304 so that it falls into the first desorption housing 301.

[0053] In use, the first desorption unit 3 is a bubbling fluidized bed desorption device, with multiple vertically alternating sawtooth partition plates 302 allowing large-particle materials to flow in a bubbling state from the material inlet to the outlet while carbon dioxide fluidizing air is introduced at the bottom. Heating tubes 303 are horizontally and densely arranged within each partition plate 302, and steam at 110-160°C flows through the heating tubes 303. As the material flows, it is continuously heated by the steam tube bundle until it reaches the desorption temperature, releasing a large amount of carbon dioxide gas. A portion of this carbon dioxide gas, approximately 20-30%, returns to the bubbling fluidized bed and circulates as fluidizing air, while the other portion is collected and condensed and compressed together with the carbon dioxide gas discharged from the second desorption unit. The flow area at the bottom of the first desorption unit 3 has a rectangular cross section, wider at the top, and a cross-sectional area more than twice that of the bottom, as shown in part C in Figure 9. This reduces the airflow velocity, allowing the fine powder rising with the desorbed carbon dioxide to fall and reduce the amount of fine powder entering the fine powder collection assembly 4. By controlling the flow velocity, a small amount of fine powder in the bed with a size of 50-100 μm enters the auxiliary separation unit 401, accounting for 1-3% of the total mass in the bubbling fluidized bed. A very small amount of fine powder is attrited and reduced in size during flow within the bed. Fine powder in the 1-100 μm particle size range enters the fine powder collection assembly 4 with the airflow. Material below 1 μm is not collected because it is difficult to reuse. The outlet end of the first desorption unit 3 is cooled gradually to below 100°C using a water-cooled jacket. The descending segment after the spiral segment mainly relies on natural cooling to gradually cool to below 60°C, and then enters the adsorption assembly 1 by air transport for the next cycle of reaction.

[0054] A metal screen 304 is further provided on top of the first desorption unit 3 to block some of the solid amine powder that leaks along with the gas. Vibration and beating mechanisms 305 are provided at the four corners of the metal screen, which perform intermittent vibration and beating to cause the material adhering to the screen 304 to fall into the bubbling fluidized bed, reducing the resistance within the bed. The screen 304 comes into tight, sealed contact with the periphery of the bubbling fluidized bed. The volume of the first desorption unit 3 is 30 to 50 m. 3The height of the stationary material layer is 0.5 to 0.8 m, and the height of the heating layer is 1.5 to 2.0 m.

[0055] The second desorption unit 5 includes four upper and lower hollow shafts and connected hollow screw blades. Heated steam flows through the hollow structure, propelling the screw blades to heat and move the material while simultaneously inverting and stirring the material, improving heat transfer and shortening heating time. The material inlet and outlet of the screw vacuum desorption device are equipped with a sealed shutoff valve, a vacuum supply chamber, and a vacuum cooling chamber. When the sealed shutoff valve is turned on, the material from the vacuum supply chamber is introduced into the vacuum desorption device, ensuring continuous operation of the desorption device. The desorption time is 1 hour, the desorption efficiency is above 95%, the desorption temperature is 80-130°C, the material processing capacity is 1-3 t / h, and carbon dioxide is produced at 100-300 kg / h. The second desorption unit 5 employs a four-shaft, two-tiered arrangement. The lower spiral transports the material, while the upper spiral rotates in the opposite direction to the lower spiral, moving the propelled material in the opposite direction, enhancing the reversal effect and improving heat transfer. Both ends of the spiral bearing are equipped with mechanical seals on both end faces to ensure sealing effect even under extremely low vacuum.Two metal screen bundle exhaust covers are designed at the exhaust ports, both of which are connected to the vacuum pump 5A. During normal desorption, one is turned on and the other is turned off, allowing carbon dioxide to be blown back into the closed screen bundle, eliminating the impact on desorption caused by small particles clogging the screen. The metal screen bundle operates by switching between the two exhaust ports. Because the particle size of the material in the vacuum desorption device is very small, it is easily discharged along with the intake of the vacuum pump 5A during desorption, causing clogging of the screen. In order to reduce the blowback and the frequency of switching the screen, each set of exhaust covers is equipped with 10 to 20 metal screens, each with a filtration accuracy of 1 μm, which are combined and installed in front of the exhaust port to ensure that the pressure before and after the screen reaches the set value. This allows the carbon dioxide to be blown back onto the screen bundle to ensure the purity of the collected gas, but it is not possible to blow back other gases. If the powder is too fine, the screen will easily become clogged, causing frequent blowback. Therefore, above the spiral axis and in front of the exhaust port, a single screen layer covering the entire spiral desorber is installed. Its filtration accuracy is 10 micrometers, and vibration beaters are placed at the four corners of the screen layer to set the vibration beater interval time. In this way, most of the small-particle materials that leak from the floor of the desorber along with the gas can be blocked. There is a 3 mm gap between the screen layer and the periphery of the inner wall of the desorber, and the screen has a tip structure. It is used to allow the small amount of small-particle materials that are blown back by the screen bundle and adhere to the wall to fall back into the desorber. In addition, the flowing air used in the second desorption unit is superheated steam at 110 to 150°C. Under the flowing action of the superheated steam, the material is quickly heated to the desorption temperature, and within 1 hour of desorption, the desorption efficiency is above 90%. The densely arranged coils heat the desorption material and provide the heat necessary for the reaction. At the exhaust port of the second desorption unit, the steam remains superheated. Under this state, the mixed gas is introduced into the heating spiral of the second desorption unit and continues to provide heat to the vacuum desorption device. After the mixed gas releases the latent heat of gasification, the exhaust port separates the carbon dioxide gas and water vapor, not only achieving flowing desorption but also realizing the gradual utilization of the heat of the steam.

[0056] Specifically, the outlet of the solid discharge end of the separation unit 2 is located at the bottom of the first detachment unit 3, and in the fine powder recovery assembly 4, the outlet of the discharge end of the auxiliary separation unit 401 is located at the bottom of the first detachment unit 3, and the outlet position of the discharge end of the auxiliary separation unit 401 is lower than the outlet position of the solid discharge end of the separation unit 2. In addition, the booster fan 7 is installed between the gas discharge end of the fine powder recovery assembly 4 and the intake end of the first detachment unit 3, and is used to provide a turbulent wind to the first detachment unit 3.

[0057] The system described in this application employs two different desorption methods and desorption units. The combination of the two methods utilizes the advantages of each device, allowing the use of solid amine powder materials with a large particle size distribution, and realizing large-scale industrial collection of solid amine materials. Furthermore, the vacuum desorption method is limited by factors such as the difficulty of processing the material and the amount of steel consumed, making it difficult to scale up. The general processing capacity of solid amine materials is 1-3 t / h. When the processing scale exceeds 3 t / h, the axis length exceeds 10 m and the volume exceeds 30 m. 3This makes the processing of the equipment more difficult, reduces the sealing effect of the rotating shaft, and requires steel consumption and costs more than five times that of the fluidized bed desorption equipment, resulting in low technical and economical efficiency. Furthermore, although bubbling fluidized bed desorbers can process larger amounts of solid amine material, they require high material particle size uniformity. As the reaction progresses, some of the material will be severely worn, causing large-particle materials to become smaller. Furthermore, new large-particle materials are continuously added to the adsorption device, which prevents the material uniformity requirement from being met. Therefore, when small-particle materials enter the bubbling fluidized bed desorber, they are quickly blown out of the bed by the fluidizing air and cannot be heated to the desorption temperature in time, and the 1-hour residence reaction time cannot be met. This results in low desorption efficiency for small-particle materials and blocks the rear piping. Therefore, the small-particle portion of the material is processed separately, while the bubbling fluidized bed is used to process larger-particle materials with more uniform particle size, thereby utilizing their performance advantages. Furthermore, the absence of a rotating device in the bubbling fluidized bed significantly reduces processing difficulty and steel consumption. By combining the two processes for desorption, a total desorption efficiency of over 95% can be achieved.

[0058] In addition, the system described in this application can control particle size and, by combining with different desorption processes, find the optimal energy consumption ratio and efficiency ratio. 10% of particles smaller than 50 μm can be separated and put into a second desorption unit for vacuum desorption, while particles larger than 50 μm can be desorbed in a bubbling fluidized bed, thereby realizing efficient desorption of solid amine materials.

[0059] Specific Example 2: In a solid amine carbon dioxide capture project at the end of the flue gas discharge of a power plant, the scale corresponds to the capture volume of 10,000 t / a. In the adsorption stage, a secondary Venturi fluidized bed adsorption tower is used, and the intake volume is 10,000 m 3 / h, the flue gas entering the system described in specific Example 1 is first pretreated to further remove liquid water and solid particulate matter therein, the cross-sectional flow rate is 1 m / s, the solid amine powder is adsorbed and saturated while rising with the flue gas in the bed, the residence time is 20-30 s, the height of the adsorption tower is 25 m, the flue gas and material temperature rises from 25 ° C to 55 ° C, the material adsorption efficiency is above 90%, and 90% of the large particle size materials are captured after passing through separation unit 2. The cloth bag collecting unit 601 captures 10% of small-sized materials, that is, the large-sized materials to be desorbed are 9t / h and the small-sized materials are 1t / h. If the system design described in specific Example 1 is not adopted and all the corresponding desorption devices are vacuum spiral desorption devices, the maximum material processing capacity of a single vacuum desorption device is 2-3t / h, so five desorption devices need to be connected in parallel, each of which will cost approximately 5 million yen, and the total investment for the desorption stage will be 25 million yen.

[0060] By adopting the system described in specific Example 1, only one vacuum desorption device is required, and most materials are desorbed in a bubbling fluidized bed. This reduces the processing difficulty of vacuum desorption devices, consumes less steel, and makes continuous desorption easy to achieve. An investment of 3 million won per device can significantly reduce costs and reduce the occupied area by more than half. The bubbling fluidized bed has a four- to six-stage structure. Generally, the first stage is the heating stage, with the largest airflow and the largest number of heat exchange tubes, allowing the material to heat up quickly from 70°C to 110-150°C. It then moves on to the middle stage, which is the main desorption reaction segment. Its airflow is smallest, forming micro-bubbles, which helps to release the desorbed CO2 gas and ensures the material stays at the appropriate temperature. The last stage is the drying and pre-cooling stage, which primarily serves to form a self-sealing desorption material to prevent the material from being oxidized by contact with air at high temperatures. The solid amine material at the outlet of the last stage is connected to an S-shaped cooling channel, which has a water-cooled jacket structure. A small amount of N2 is introduced at the corners as a spray air for the material. Through the dual action of water cooling and air cooling, the material is cooled to below 80°C. After contacting the air, the material is cooled by a water-cooled spiral and air conveyance, and then transported to the silo before the adsorption tower. The cross-sectional flow velocity in the bubbling fluidized bed is 0.1 to 0.3 m / s, the corresponding residence time is 1 h, the desorption temperature is 110 to 150°C, the desorption efficiency is 95%, and the only electricity consumer during desorption is the booster fan 7, which saves more than 70% of the electricity consumed by five vacuum desorbers and a vacuum pump 5A connected in parallel.

[0061] The advantages and disadvantages of the three types of desorption methods at the same processing volume are compared as follows: [Table 1]

[0062] The above disclosure is merely a few specific implementation scenarios of the present application, however, the present application is not limited thereto, and any variations conceivable by those skilled in the art are included in the scope of protection of the present application. The numbers in the above application are for illustrative purposes only and do not represent the superiority or inferiority of the implementation scenarios. [Explanation of symbols]

[0063] 1. Adsorption Assembly 2 Separation Unit 3 First detachable unit 4 Fines Collection Assembly 5 Second detachable unit 6 Fines Silo Assembly 7 Booster Fan 5A vacuum pump 101 Lower Unit 102 Middle Unit 103 Upper Unit 104 First Venturi Tube 105 Second Venturi Tube 301 First detachable housing 302 Partition 303 Heating tube 304 screens 305 Vibration Beating Mechanism 401 Auxiliary Separation Unit 402 Wind-powered sorting and separation unit 601 Hotei Collection Unit 602 Silo 603 Vacuum Silo 1021 Middle housing 1022 Heat exchange tube 1023 Fin Unit 4021 Housing 4022 Diversion mechanism 4023 Wind sorting mechanism 4024 Collection Organization 6011 Screen layer 6012 Heating element 40231 Gas storage components 40232 Connecting member 40221 Heating tube assembly 40222 Guide Group 40223 Divider plate set 40241 Connection parts 40242 Collection tube 40211 Rectangular Segment 40212 Huge Segment 40223A Partition Plate Material 40222B Ventilation hole

Claims

1. an adsorption assembly connected to the outside, used to adsorb carbon dioxide in the external flue gas / air with solid amines of mixed particle sizes to obtain mixed particles after carbon capture; a separation unit connected to the discharge end of the adsorption assembly, the separation unit being used to separate the mixed particle size solid amine and collect the separated solid amine; a first desorption unit disposed at the solid discharge end of the separation unit, for desorbing the separated solid amine by bubbling; a fines collection assembly provided at the exhaust end of the first desorption unit, for sieving solid amine leaked from the exhaust end of the first desorption unit to obtain recovered solid amine particles; a second desorption unit connected to the discharge end of the fines collection assembly and used to deliver the collected solid amine particles to the second desorption unit for vacuum desorption; The fines collection assembly includes: an auxiliary separation unit connected to the exhaust end of the first desorption unit, for collecting the leaked solid amine particles and obtaining a gas to be recovered; an air-sorting separation unit connected to the exhaust end of the auxiliary separation unit, for air-sorting the solid amine particles leaking from the exhaust end of the auxiliary separation unit to obtain the recovered solid amine particles; a solid discharge end of the air separation unit is connected to an inlet end of the second desorption unit, and is used to deliver the recovered solid amine particles to the second desorption unit for vacuum desorption; The wind sorting separation unit comprises: a housing connected to the exhaust end of the auxiliary separation unit, for collecting the gas to be air-filtered containing the leaked solid amine particles discharged from the exhaust end of the auxiliary separation unit; a dividing mechanism provided at the intake end of the housing, for dividing the gas to be air-filtered that has entered the housing, to obtain a divided gas containing solid amine particles; an air separation mechanism provided on one side of the housing for air separation of solid amine particles in the diverted gas; a collecting mechanism provided on the other side of the housing and facing the air separation mechanism, for collecting the recovered solid amine particles obtained after air separation by the air separation mechanism and sending the collected solid amine particles to the second desorption unit; The wind sorting mechanism includes: a gas storage member connected to an external gas source; at least two communication members provided in communication between the gas storage member and the housing, the communication members being used to send pulsed airflows into the housing to air-separate solid amine particles in the diverted gas; The flow dividing mechanism includes: a heating tube set provided at the intake end of the housing and used to heat the gas to be air-filtered that has entered the housing; a guide group provided at the intake end of the housing and located on the side of the heating pipe group facing the bottom of the housing, for grouping and guiding the gas to be air-filtered; a partition plate set provided between the air separation mechanism and the collection mechanism, for decelerating the gas to be air-separated after being grouped and guided, and for facilitating the air separation by the air separation mechanism and the collection of solid amine particles by the collection mechanism; The partition plate set includes: at least three divider members; a ventilation hole for allowing gas to pass therethrough is provided between any two laterally adjacent partition members; Any two adjacent partition members in the vertical direction are alternately arranged, and the space between any two adjacent partition members in the vertical direction is used as a communication passage between the air sorting mechanism and the collecting mechanism; The collection mechanism includes: a connecting member provided on one side of the housing and facing the wind sorting mechanism; a collection tube disposed between the connecting member and the inner wall of the housing; The connecting member is provided with at least two conduits that communicate with the collection pipe, the collection tube is disposed at the discharge end of the air separator and is used to collect the recovered solid amine particles; the delivery end of the collection tube is connected to the delivery end of the second detachment unit; The housing includes: a rectangular segment used to arrange the flow diverter, the wind separator, and the collector; and an enlarged segment connected to the rectangular segment, the enlarged segment having an end remote from the rectangular segment that is at least twice as large as the rectangular segment.

2. The adsorption assembly comprises: a lower unit having a solid inlet end connected to the solid outlet end of the first desorption unit for receiving solid amine of mixed particle size and a gas inlet end connected to external flue gas / air; a middle unit, the inlet end of which is connected to the outlet end of the lower unit, the middle unit being used to capture carbon by solid amine of mixed particle sizes that has entered the middle unit and to lower the reaction temperature during carbon capture; an upper unit, the inlet end of which is connected to the outlet end of the middle unit and is used to increase the flow rate and thoroughly mix the solid amine of mixed particle sizes; a first venturi pipe provided between the lower unit and the middle unit; 2. The solid amine material carbon capture system suitable for various particle sizes according to claim 1, further comprising a second venturi tube disposed between the middle unit and the upper unit.

3. The middle unit is The middle housing and At least one heat exchange tube provided on the inner wall of the intermediate housing and used to lower the reaction temperature during carbon capture; and a fin unit disposed on the outside of the heat exchange tube, the fin unit being used to increase the heat exchange area and at the same time break up agglomerated materials in the mixed particle size solid amine.

4. further comprising a fines silo assembly; 2. The carbon capture system using solid amine materials suitable for various particle sizes according to claim 1, wherein the fine powder silo assembly is provided between the separation unit and the second desorption unit and is used to store the solid amine particles provided by the separation unit and the fine powder recovery assembly.

5. The fine powder silo assembly comprises: a cloth bag collecting unit, the inlet end of which is connected to the gas outlet end of the separation unit and which is used to collect solid amine particles leaking from the gas outlet end of the separation unit; a silo connected to the solid discharge end of the cloth bag collecting unit and used to collect the solid amine particles collected in the cloth bag collecting unit; a vacuum silo connected to the discharge end of the silo and the fines collection assembly, respectively, and used to store the solid amine particles provided by the separation unit and the fines collection assembly; 5. The carbon capture system using solid amine materials suitable for various particle sizes according to claim 4, wherein the vacuum silo is connected to the second desorption unit and is used to vacuum desorb the solid amine particles provided by the separation unit and the fines recovery assembly.

6. The cloth bag collecting unit includes: a screen layer used to collect solid amine particles while simultaneously allowing gas to escape; and a heating element disposed in the middle of the screen layer and used to dry the solid amine particles.

7. The first detachable unit is a first detachable housing having an air intake port at a bottom portion close to the ground for introducing flowing air; at least two partition plates provided in the first detachable housing, for moving the solid amine particles in a bubbling state within the first detachable housing when a flowing air stream is introduced; a heating pipe provided between any two adjacent partition plates and used to provide heat during desorption; a screen disposed within the first desorption housing and used to block solid amine leaking from the exhaust end of the first desorption unit; and a vibrating and beating mechanism provided on the screen for intermittently vibrating and beating the solid amine adhering to the screen to cause it to fall into the first detachment housing.

8. an outlet of the solids discharge end of the separation unit is located at the bottom of the first desorption unit; 8. The carbon capture system using solid amine material suitable for various particle sizes as described in claim 7, characterized in that in the fine powder recovery assembly, the outlet of the discharge end of the auxiliary separation unit is located at the bottom of the first desorption unit, and the outlet position of the discharge end of the auxiliary separation unit is lower than the outlet position of the solid discharge end of the separation unit.

9. It also includes a booster fan.

2. The solid amine material carbon collection system suitable for various particle sizes according to claim 1, wherein the booster fan is provided between the gas discharge end of the fine powder recovery assembly and the intake end of the first desorption unit, and is used to provide a flowing wind to the first desorption unit.

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