Axial flow adsorption coupled purification device and its operation method

Abstract

This invention discloses an axial flow adsorption coupled purification device and its operating method, relating to the field of gas purification technology. The axial flow adsorption coupled purification device includes: a shell extending along an axis, the shell having a first cylindrical section and a second cylindrical section located below the first cylindrical section, with its radial dimensions gradually decreasing from top to bottom; a gas outlet is provided at the upper end of the side wall of the first cylindrical section, and a dust outlet is provided at the lower end of the second cylindrical section; a first particle moving bed assembly, including: a first hopper for loading first collected particles, a first moving bed tube extending along the axis, a first material leg, and a first inclined tube for waiting to be collected, etc. This application can simultaneously perform the separation of solid and liquid particulate impurities and the adsorption separation of impurity gases in the same device through the coupling of multiple separation mechanisms, and has the advantages of simple process flow, low energy loss, large processing capacity, high separation accuracy, and wide applicability.

Description

Technical Field

[0001] This invention relates to the field of gas purification technology, and in particular to an axial flow adsorption coupling purification device and its operation method. Background Technology

[0002] Emissions of industrial waste gas and particulate pollutants are increasing daily. Pollutants generated during the extraction, processing, transportation, and combustion of fossil fuels such as coal, oil, and natural gas are exacerbating environmental pressures. Therefore, facing increasingly severe environmental pollution problems, the requirements for gas purification technologies are becoming increasingly stringent.

[0003] Currently, among gas purification technologies for treating particulate solid and liquid impurities in gases, cyclone separators are the most widely used due to their simple structure, high separation efficiency, and low pressure drop. However, cyclone separators have limited separation capabilities for particles smaller than 10μm, which can no longer meet increasingly stringent environmental emission requirements. Moreover, the gases to be treated generally contain not only particulate solid and liquid impurities but also gaseous impurities. For example, newly extracted natural gas contains a large amount of solid particles, liquid water, and gaseous impurities such as H2S and CO2. These impurities can cause serious damage to pipelines and the environment; therefore, natural gas must be purified before transportation and use.

[0004] Gas purification in industrial production is often carried out in steps, meaning the separation of particulate solid-liquid impurities from gaseous impurities occurs separately. This results in cumbersome processes, large equipment footprints, high energy consumption, and problems such as complex processes and high costs. For example, impurities in industrial process gases or natural gas (such as H2S and CO2) are typically removed using desulfurization and decarbonization absorption towers, which utilize single or compound solvents such as alkanolamines to absorb and remove acidic gases. Finally, a dehydration absorption tower removes moisture. Therefore, there is an urgent need for highly efficient equipment or impurity removal systems that couple different separation mechanisms to simplify processes, reduce costs, and improve gas purification efficiency. Summary of the Invention

[0005] In order to overcome the above-mentioned defects of the prior art, the technical problem to be solved by the embodiments of the present invention is to provide an axial flow adsorption coupling purification device and its operation method, which can simultaneously separate solid and liquid particulate impurities and adsorb impurity gas through the coupling of multiple separation mechanisms. It has the advantages of simple process flow, low energy loss, large processing capacity, high separation accuracy and wide applicability.

[0006] The specific technical solution of this invention is as follows:

[0007] An axial flow adsorption coupling purification device, the axial flow adsorption coupling purification device comprising:

[0008] A housing extending along an axis, the housing having a first cylindrical section and a second cylindrical section located below the first cylindrical section, the second cylindrical section having a radial dimension that gradually decreases from top to bottom; a gas outlet is provided at the upper end of the sidewall of the first cylindrical section, and a dust outlet is provided at the lower end of the second cylindrical section;

[0009] The first particle moving bed assembly includes: a first hopper for loading the first collected particles, a first moving bed tube extending along an axis, a first material leg, and a first waiting inclined tube, wherein the lower end of the first hopper forms a first material sealing area by tapering, the upper end of the first moving bed tube is connected to the first material sealing area, the side wall of the first moving bed tube has a mesh structure, the upper end of the first material leg is connected to the lower end of the first moving bed tube, the upper end of the first waiting inclined tube is connected to the lower end of the first material leg, and the first waiting inclined tube extends out of the second section of the cylinder;

[0010] The first lifting component is used to lift the particles discharged from the first inclined tube and input them into the first hopper;

[0011] An axial cyclone assembly includes a cyclone tube extending along an axis, inserted from the upper end of the first hopper into the first moving bed tube body, the upper end of the cyclone tube being a gas inlet, and a mesh structure on the side wall of the cyclone tube located in the first moving bed tube body; a cyclone mechanism disposed in the cyclone tube to generate swirling flow of gas; and a cyclone stabilizer disposed at the bottom of the cyclone tube to eliminate the tailing phenomenon of airflow in the cyclone tube.

[0012] Preferably, the first lifting assembly includes: a lifting pipe, comprising a pre-lifting pipe body and a lifting pipe body, the pre-lifting pipe body being connected to the first regenerated inclined pipe; a spouting bed shell forming a storage space, the lifting pipe body being inserted into the spouting bed shell from its lower end, the upper end of the spouting bed shell having a regeneration gas outlet; and a regeneration inclined pipe, one end of which is connected to the lower end of the side wall of the spouting bed shell.

[0013] Preferably, there are multiple axial flow cyclone components, and the multiple axial flow cyclone components are circumferentially distributed around the center line of the first particle moving bed component.

[0014] Preferably, each cyclone tube is disposed close to and sealed with adjacent cyclone tubes, and the sidewall of each cyclone tube between the two contact points of the two adjacent cyclone tubes and facing the center line of the first particle moving bed assembly is closed. The sidewall of each cyclone tube between the two contact points of the two adjacent cyclone tubes and facing away from the center line of the first particle moving bed assembly has a mesh structure. The swirling mechanism is located above the interior of the cyclone tubes. The plurality of cyclone tubes form an intermediate space, which is closed.

[0015] Preferably, the axial flow adsorption coupling purification device further includes:

[0016] The second particle moving bed assembly includes: a second hopper for loading second collected particles, a second moving bed tube extending along an axis, a second material leg, and a second pre-cooking inclined tube. The first hopper is disposed within the second hopper. The lower end of the second hopper forms a second material sealing zone with the lower end of the first hopper via a tapering section. The second moving bed tube is sleeved outside the first moving bed tube. The upper end of the second moving bed tube is connected to the second material sealing zone. The sidewall of the second moving bed tube has a mesh structure. The upper end of the second material leg is connected to the lower end of the second moving bed tube and is sleeved outside the first material leg. The upper end of the second pre-cooking inclined tube is connected to the lower end of the second material leg and extends out of the second section of the cylindrical body. The first pre-cooking inclined tube extends out of the second pre-cooking inclined tube and then out of the second section of the cylindrical body.

[0017] The second lifting component is used to lift the particles discharged from the second inclined tube and input them into the second hopper, and to discharge the regeneration gas.

[0018] Preferably, the second moving bed tube is coaxially arranged with the first moving bed tube; the gaps in the mesh structure extend in the circumferential direction, or in the axial direction, or in the oblique direction; the ratio of the width of the gap on the second moving bed tube to the diameter of the second captured particle is between 0.13 and 0.25; the ratio of the width of the gap on the first moving bed tube to the diameter of the first captured particle is between 0.13 and 0.25.

[0019] Preferably, when the axial flow adsorption coupling purification device needs to separate solid and liquid phase particulate impurities in the gas, the particle size of the first collected particles is between 1.5 mm and 2.5 mm, and the particle bed thickness in the first moving bed tube is between 0.1 d and 3 d, where d represents the diameter of the cyclone tube; the particle size of the second collected particles is between 0.8 mm and 1.2 mm, and the particle bed thickness in the second moving bed tube is between 0.05 d and 2.5 d.

[0020] Preferably, when the axial flow adsorption coupling purification device needs to separate gaseous impurities from the gas, and the gas contains particulate impurities, the first collecting particle is a collecting particle with the ability to collect solid and liquid particulate impurities and the ability to adsorb gaseous impurities; the second collecting particle is a collecting particle with the ability to collect solid and liquid particulate impurities and the ability to adsorb gaseous impurities.

[0021] Preferably, the ratio of the average particle size of the second trapping particle to the average particle size of the first trapping particle is between 0.3 and 0.8.

[0022] An operating method for an axial flow adsorption coupling purification device as described above, comprising:

[0023] The impure gas is introduced from the gas inlet at the top of the cyclone tube, and the impure gas is transformed into a swirling state by the swirling mechanism and moves downward;

[0024] The first hopper is loaded with the first collecting particles, and the first collecting particles enter the first moving bed tube after passing through the first material sealing area, and then continue to move downward.

[0025] The particulate impurities in the impure gas that cannot pass through the mesh structure move to the inner wall of the cyclone tube under the action of centrifugal force and slide down into the first moving bed tube body along the inner wall of the cyclone tube.

[0026] The impurity-containing gas flows radially outward through the mesh structure on the side wall of the cyclone tube and forms a cross-flow moving bed with the first collecting particles moving downward in the first moving bed tube. The impurity gas and / or particulate impurities that can pass through the mesh structure are filtered, adsorbed, or intercepted by the first collecting particles to form purified gas. The purified gas is discharged through the mesh structure of the first moving bed tube to the gas outlet of the shell.

[0027] After the particles that have been filtered, adsorbed or intercepted in the first moving bed tube are combined with the particulate impurities that have slid down the inner wall of the cyclone tube into the first moving bed tube, they are lifted by the first material leg and the first waiting inclined tube, and then fed into the first material bin.

[0028] The technical solution of the present invention has the following significant beneficial effects:

[0029] This axial-flow adsorption-coupled purification device incorporates a built-in cyclone tube. The diameter of the cyclone tube can be effectively controlled to ensure sufficient cyclone separation and cleaning of the inner wall of the cyclone tube by the swirling gas, based on the required throughput and cyclone intensity. Simultaneously, the moving bed forming the particle-collecting moving bed is externally fitted outside the cyclone tube. This allows the axial-flow adsorption-coupled purification device to flexibly adjust the number and thickness of the particle-collecting moving bed layers according to the required throughput, properties, collection efficiency, and residence time of the impurity gas. Because the gas flow containing impurities moves centrifugally, the cross-flow velocity in the particle-collecting moving bed gradually decreases with the airflow, effectively reducing the secondary entrainment of fine particles deposited in the bed by the cross-flow gas. This ensures the separation efficiency of the axial-flow adsorption-coupled purification device for submicron particles, facilitates improved processing capacity, and provides a longer residence time, laying the foundation for the coupling of adsorption. Finally, the axial flow adsorption coupling purification device can increase the processing capacity by configuring multiple axial flow cyclone components, but the scale-up effect is not obvious.

[0030] Specific embodiments of the invention are disclosed in detail below with reference to the description and accompanying drawings, indicating how the principles of the invention can be employed. It should be understood that the embodiments of the invention are not therefore limited in scope. Features described and / or shown for one embodiment may be used in the same or similar manner in one or more other embodiments, combined with features in other embodiments, or substituted for features in other embodiments. Attached Figure Description

[0031] The accompanying drawings described herein are for illustrative purposes only and are not intended to limit the scope of the invention in any way. Furthermore, the shapes and proportions of the components in the drawings are merely illustrative to aid in understanding the invention and do not specifically limit the shapes and proportions of the components. Those skilled in the art, guided by the teachings of this invention, can select various possible shapes and proportions to implement the invention according to specific circumstances.

[0032] Figure 1 This is a schematic diagram of the axial flow adsorption coupling purification device in the first embodiment of the present invention;

[0033] Figure 2 This is a schematic diagram of the axial flow adsorption coupling purification device in the second embodiment of the present invention;

[0034] Figure 3 for Figure 2 Cross-sectional view at point AA;

[0035] Figure 4This is a schematic diagram of the axial flow adsorption coupling purification device in the third embodiment of the present invention;

[0036] Figure 5 This is a schematic diagram of the axial flow adsorption coupling purification device in the fourth embodiment of the present invention;

[0037] Figure 6 for Figure 5 Schematic diagram of the structure at point BB;

[0038] Figure 7 This is a schematic diagram of the swirl stabilizer.

[0039] The reference numerals in the above figures are as follows:

[0040] 1. Axial flow cyclone assembly; 11. Gas inlet; 12. Cyclone tube; 13. Cyclone mechanism; 14. Cyclone stabilizer; 2. First particle moving bed assembly; 21. First hopper; 22. First material sealing zone; 23. First moving bed tube; 24. First material leg; 25. First waiting inclined tube; 3. Shell; 31. Gas outlet; 32. First section of cylinder; 33. Second section of cylinder; 34. Dust outlet; 35. Dust discharge pipe; 36. On / off valve; 4. First lifting assembly; 41. Pre-lifting tube; 42. Lifting tube; 43. Sprayed bed shell; 44. Regeneration inclined tube; 45. Regeneration gas outlet; 5. Second particle moving bed assembly; 51. Second hopper; 52. Second material sealing zone; 53. Second moving bed tube; 54. Second material leg; 55. Second waiting inclined tube; 6. Second lifting assembly. Detailed Implementation

[0041] The details of the present invention can be more clearly understood by referring to the accompanying drawings and the description of specific embodiments. However, the specific embodiments of the present invention described herein are for illustrative purposes only and should not be construed as limiting the invention in any way. Under the teachings of this invention, those skilled in the art can conceive of any possible modifications based on the invention, all of which should be considered within the scope of the invention. It should be noted that when an element is referred to as being "set on" another element, it can be directly on the other element or there may be an intervening element. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or there may be an intervening element. The terms "mounted," "connected," and "connected" should be interpreted broadly, for example, they can refer to mechanical or electrical connections, or internal communication between two elements, and can be direct or indirect connections through an intermediate medium. Those skilled in the art can understand the specific meaning of the above terms according to the specific circumstances. The terms "vertical," "horizontal," "upper," "lower," "left," "right," and similar expressions used herein are for illustrative purposes only and do not represent the only embodiments.

[0042] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. The term "and / or" as used herein includes any and all combinations of one or more of the associated listed items.

[0043] To enable the simultaneous separation of solid and liquid particulate impurities and the adsorption and separation of impurity gases through the coupling of multiple separation mechanisms, offering advantages such as simple process flow, low energy consumption, large throughput, high separation accuracy, and wide applicability, this application proposes an axial flow adsorption coupling purification device. Figure 1 This is a schematic diagram of the axial flow adsorption coupling purification device in the first embodiment of the present invention, as shown below. Figure 1 As shown, the axial flow adsorption coupling purification device includes: a shell 3, a first particle moving bed assembly 2, a first lifting assembly 4, and an axial flow cyclone assembly 1.

[0044] Among them, such as Figure 1As shown, the shell 3 extends along the axis, that is, in the vertical direction. The shell 3 has a first cylindrical section 32 and a second cylindrical section 33 located below the first cylindrical section 32, whose radial dimensions gradually decrease from top to bottom. The cross-section of the first cylindrical section 32 in the radial direction can be circular. A gas outlet 31 is provided at the upper end of the side wall of the first cylindrical section 32, and the gas outlet 31 can be located at the uppermost end of the side wall of the first cylindrical section 32. A dust outlet 34 is provided at the lower end of the second cylindrical section 33, and a dust discharge pipe 35 can be connected to the lowermost end of the second cylindrical section 33. An on / off valve 36 can be provided on the dust discharge pipe 35 to control the opening and closing of the dust discharge pipe 35 to meet the need for dust discharge. The area of ​​the second cylindrical section 33 can be used as a dust collection chamber.

[0045] like Figure 1 As shown, the first particle moving bed assembly 2 may include: a first hopper 21 for loading the first captured particles, a first moving bed tube 23 extending along an axis, a first feed leg 24, and a first waiting inclined tube 25. The lower end of the first hopper 21 tapers to form a first material sealing area 22, the diameter of which is smaller than the diameter of the first hopper 21 above it. The upper end of the first moving bed tube 23 is connected to the first material sealing area 22 for communication. That is, the upper end of the first moving bed tube 23 is connected to the lower end of the first hopper 21. The sidewall of the first moving bed tube 23 has a mesh structure, which allows gas to flow through the first moving bed tube 23 in a cross-flow manner and enter the housing 3. The lower end of the first moving bed tube 23 may taper gradually from top to bottom to allow the first captured particles to converge towards the center. The upper end of the first feed leg 24 is connected to the lower end of the first moving bed tube 23, and the upper end of the first waiting inclined tube 25 is connected to the lower end of the first feed leg 24. The first waiting inclined tube 25 extends out of the second section of the cylinder 33. The first collecting particles can remove unwanted impurity gaseous components from the impure gas, and simultaneously collect and remove solid and liquid phase particles from the impure gas. When the first collecting particles need to remove unwanted impurity gaseous components from the impure gas, the first collecting particles are collecting particles with the ability to adsorb unwanted impurity gaseous components.

[0046] Furthermore, the gaps in the mesh structure can extend in the circumferential direction, in the axial direction, or in the oblique direction. The ratio of the width of the gaps on the first moving bed tube 23 to the diameter of the first captured particle is between 0.13 and 0.25. In this way, the blocking of the first captured particle can be ensured while ensuring the gas flow rate.

[0047] like Figure 1As shown, the axial flow cyclone assembly 1 may include a cyclone tube 12 extending along the axis, inserted from the upper end of the first hopper 21 into the first moving bed tube 23, a cyclone mechanism 13, and a cyclone stabilizer 14. The cyclone tube 12 may be coaxially arranged with the first hopper 21 and the first moving bed tube 23, with the lower end of the cyclone tube 12 extending to the vicinity of the lower end of the first moving bed tube 23. The upper end of the cyclone tube 12 is a gas inlet 11 for introducing the impurity-containing gas to be treated. The side wall of the cyclone tube 12 located in the first moving bed tube 23 has a mesh structure, through which the gas in the cyclone tube 12 can enter the first moving bed tube 23. The cyclone mechanism 13 is disposed in the cyclone tube 12 to generate swirling flow of the gas. The cyclone mechanism 13 may be located above the interior of the cyclone tube 12, thereby improving the utilization rate of the mesh structure on the side wall of the cyclone tube 12 located in the first moving bed tube 23. A swirl stabilizer 14 is disposed at the bottom of the cyclone tube 12, and is used to eliminate the tailing phenomenon of the airflow in the cyclone tube 12. The lower end of the cyclone tube 12 is open and communicates with the interior of the first moving bed tube 23. Furthermore, the inner wall of the cyclone tube 12 can be made into a smooth surface to reduce the obstruction of the wall surface to solid phase particle impurities in the swirling gas. The swirl mechanism 13 may include guide vanes or swirl arms, etc. The downward swirl angle of the guide vanes is preferably 10° to 30°, so that the gas entering through the gas inlet 11 changes from axial downward movement to swirling motion with a certain downward tilt angle.

[0048] As a feasible option, Figure 7 This is a schematic diagram of the swirl stabilizer, as shown below. Figure 7 As shown, the swirl stabilizer 14 may include a cylindrical portion and a conical portion located above the cylindrical portion, with the apex of the conical portion facing the gas inlet 11 of the cyclone tube 12. The airflow tailing phenomenon, also known as the "vortex core oscillation phenomenon," refers to the phenomenon where the center of the rotating vortex core periodically deviates from the central axis at the end of the cyclone tube 12. At the end of the axial-flow cyclone tube 12, the swirling intensity of the rotating gas decreases due to energy dissipation and reduced gas volume, ultimately causing the central axis of the gas rotation to repeatedly change within a certain range. The swirling airflow tailing can re-entrain particulate impurities that have been separated onto the inner wall of the cyclone tube 12 into the swirling gas, potentially entering the particle bed in the subsequent first moving bed tube 23 through the side wall of the cyclone tube 12, thus increasing the filtration load on the particle bed in the first moving bed tube 23. Furthermore, the swirling airflow tailing can also cause the flow field inside the cyclone tube 12 to become more complex and irregular, leading to an increase in equipment pressure drop. The cyclone stabilizer 14 in this application can avoid the above-mentioned problems, reduce the filtration load of the particle bed in the first moving bed tube 23, and reduce the pressure drop of the cyclone tube 12.

[0049] like Figure 1As shown, the first lifting component 4 is used to lift the particles discharged from the first waiting inclined tube 25 and input them into the first hopper 21.

[0050] As an option, the first lifting assembly 4 may include: a lifting pipe, including a pre-lifting pipe body 41 and a lifting pipe body 42, the pre-lifting pipe body 41 being connected to the first pre-regenerated inclined pipe 25; a spouting bed shell 43 having a storage space, the lifting pipe body 42 being inserted into the spouting bed shell 43 from its lower end, the upper end of the spouting bed shell 43 having a regeneration gas outlet 45; and a regeneration inclined pipe 44, one end of which is connected to the lower end of the side wall of the spouting bed shell 43. To lift the particles in the lifting pipe, the lower end of the lifting pipe may have a regeneration gas inlet for inputting regeneration gas. The regeneration gas is pneumatically conveyed to lift the particles into the spouting bed shell 43, and then the regeneration gas is discharged from the regeneration gas outlet 45.

[0051] The operation method of the above-mentioned axial flow adsorption coupling purification device may include the following steps:

[0052] The impurity-laden gas is input through the gas inlet 11 at the upper end of the cyclone tube 12. The impurity-laden gas is transformed into a swirling state by the swirling mechanism 13 and moves downward. The impurity-laden gas may include solid, liquid particulate impurities, and gaseous impurities.

[0053] The first hopper 21 is loaded with the first captured particles, and the first captured particles enter the first moving bed tube 23 after passing through the first material sealing zone 22, and then continue to move downward.

[0054] Particulate impurities in the impure gas that cannot pass through the mesh structure move to the inner wall of the cyclone tube 12 under the action of centrifugal force and slide down into the first moving bed tube 23. This step can achieve the pre-removal of particulate impurities.

[0055] The impurity-laden gas flows radially outward through the mesh structure on the sidewall of the cyclone tube 12, forming a cross-flow moving bed with the first collecting particles moving downward in the first moving bed tube 23. Impurities in the impurity-laden gas and / or particulate impurities that can pass through the mesh structure are filtered, adsorbed, or intercepted by the first collecting particles, thus forming purified gas. The purified gas is discharged through the mesh structure of the first moving bed tube 23 to the gas outlet 31 of the shell 3. In the above process, the first collecting particles can intercept and filter fine particulate impurities that are not separated by the cyclone in the cyclone tube 12, and adsorb and separate gaseous impurity components, thereby further enhancing the gas-solid separation effect and achieving synergistic enhancement of multiple separation mechanisms. This process simultaneously performs solid and liquid phase particle separation and impurity gas adsorption and separation, offering advantages such as simple process flow, low energy consumption, large throughput, and high separation accuracy.

[0056] The particles collected in the first moving bed tube 23 after filtration, adsorption, or interception, and the particulate impurities that slide down the inner wall of the cyclone tube 12, merge with the particles in the first moving bed tube 23. They then enter the first lifting assembly 4 via the first feed leg 24 and the first waiting inclined tube 25, where they are lifted and then fed into the first hopper 21. This process completes the entire circulation loop of the first collected particles. In the first lifting assembly 4, the first collected particles, under the drag of the regeneration gas, enter the combination of the lifting tube and the spouted bed shell 43 for regeneration. Finally, they are transported to the first hopper 21 through the regeneration inclined tube 44. The regeneration gas can enter from the regeneration gas inlet at the lower end of the lifting tube and finally exit from the regeneration gas outlet 45. The discharged regeneration gas can be further processed and then transported back to the regeneration gas inlet for recirculation.

[0057] As a feasible option, Figure 2 This is a schematic diagram of the axial flow adsorption coupling purification device in a second embodiment of the present invention. Figure 3 for Figure 2 Cross-sectional view at point AA, as shown Figure 2 and Figure 3 As shown, there are multiple axial flow cyclone components 1, which can be circumferentially distributed around the center line of the first particle moving bed assembly 2. Further, the number of axial flow cyclone components 1 is preferably 4 to 12, and the multiple axial flow cyclone components 1 can be evenly distributed or symmetrically arranged around the center line of the first particle moving bed assembly 2.

[0058] Furthermore, each cyclone tube 12 is disposed close to and sealed with its adjacent cyclone tube 12. The sidewall of each cyclone tube 12, between the two contact points of each of the two adjacent cyclone tubes 12 and facing the centerline of the first particle moving bed assembly 2, is closed to prevent impurity gas from entering the intermediate space formed by the multiple cyclone tubes 12. The sidewall of each cyclone tube 12, between the two contact points of each of the two adjacent cyclone tubes 12 and facing away from the centerline of the first particle moving bed assembly 2, has a mesh structure, thereby ensuring that the impurity gas flows outward substantially along the radial direction of the first moving bed tube 23, ensuring that it all comes into contact with the first captured particles within the first moving bed tube 23, thereby further removing impurities. The swirling mechanism 13 is located above the interior of the cyclone tube 12 to improve the utilization rate of the mesh structure on the sidewall of the cyclone tube 12. The multiple cyclone tubes 12 form an intermediate space, which is closed.

[0059] The above structure can improve the gas handling capacity of the axial flow adsorption coupling purification device. The inlet velocity of a single axial flow cyclone assembly 1 has an upper limit; therefore, under conditions of large gas volumes, a single axial flow cyclone assembly 1 cannot quickly and effectively separate the gas. In the structure described in this application, the flow area of ​​the gas after setting multiple cyclone tubes 12 is greatly increased, meaning the contact area between the airflow and the first collected particles is also significantly increased. This not only benefits the filtration / adsorption / interception of impurity-laden gas by the first collected particles but also facilitates the circulation of the first collected particles. Furthermore, since the multiple cyclone tubes 12 form a closed space, impurity-laden gas will not flow inward from the cyclone tubes 12 along the radial direction of the first moving bed tube 23, preventing airflow disturbances that could affect the pre-removal of particulate impurities.

[0060] As a feasible option, Figure 4 This is a schematic diagram of the axial flow adsorption coupling purification device in a third embodiment of the present invention, as shown below. Figure 4 As shown, the axial flow adsorption coupling purification device may further include a second particle moving bed assembly 5. The second particle moving bed assembly 5 may include a second hopper 51 for loading the second collected particles, a second moving bed tube 53 extending along the axis, a second material leg 54, and a second waiting inclined tube 55. The first hopper 21 is disposed within the second hopper 51. The lower end of the second hopper 51 forms a second material sealing zone 52 with the lower end of the first hopper 21 through a tapering transition, and the second moving bed tube 53 is sleeved outside the first moving bed tube 23. The upper end of the second moving bed tube 53 is connected to the second material sealing zone 52. The side wall of the second moving bed tube 53 has a mesh structure. The upper end of the second material leg 54 is connected to the lower end of the second moving bed tube 53. The second material leg 54 is sleeved outside the first material leg 24. The upper end of the second waiting inclined tube 55 is connected to the lower end of the second material leg 54 and extends out of the second section of the cylinder 33. The first waiting inclined tube 25 extends out of the second waiting inclined tube 55 and then out of the second section of the cylinder 33. The second lifting assembly 6 is used to lift the particles discharged from the second waiting inclined tube 55 and input them into the second hopper 51, and to discharge the regeneration gas.

[0061] The specific structure of the second lifting component 6 can be the same as that of the first lifting component 4, and will not be described in detail here.

[0062] Furthermore, the second moving bed tube 53 is coaxially arranged with the first moving bed tube 23. The gaps in the mesh structure of the second moving bed tube 53 can extend in the circumferential direction, the axial direction, or the oblique direction. The ratio of the width of the gaps on the second moving bed tube 53 to the diameter of the second trapping particle is between 0.13 and 0.25.

[0063] The first collected particles in the first moving bed assembly 2 flow down from the first hopper 21 under gravity, enter the first moving bed tube 23 through the first sealing zone 22, and then flow downwards. The downward-flowing first collected particles first form a cross-flow moving bed with the radially centrifugally flowing impurity-laden gas, performing primary filtration / adsorption of the impurity-laden gas. Furthermore, the first collected particles can intercept and filter particulate impurities that were not separated by the cyclone in the cyclone tube 12, thereby further enhancing the gas-solid separation effect. The gas filtered by the first moving bed tube 23 then enters the second moving bed tube 53 radially in the cross-flow zone. The second collected particles in the second moving bed tube 53 also flow down from the second hopper 51 under gravity. The downward-flowing second collected particles form a cross-flow moving bed with the radially centrifugally flowing impurity-laden gas, performing secondary filtration / adsorption of the impurity-laden gas, achieving the purpose of fine separation. Furthermore, the particle size of the second collected particles is smaller than that of the first collected particles, thus ensuring a finer separation effect. The purified gas passes through the second moving bed tube 53 and enters the first section of the shell 3, 32, and is finally discharged from the gas outlet 31. The second collected particles in the second moving bed tube 53 pass through the second material leg 54 and the second waiting inclined tube 55 at the bottom and enter the second lifting assembly 6, and are then fed into the second hopper 51 through the second lifting assembly 6.

[0064] The axial flow adsorption coupling purification device can also include more particle moving bed components, which are arranged sequentially from the inside out. Furthermore, from the inside out, the particle size of the captured particles in different particle moving bed components gradually decreases. The specific number of particle moving bed components, the thickness of the bed, and the captured particles can be flexibly adjusted according to industrial requirements such as the separation target, capture efficiency, and residence time.

[0065] Furthermore, Figure 5 This is a schematic diagram of the axial flow adsorption coupling purification device in the fourth embodiment of the present invention. Figure 6 for Figure 5 A structural diagram of section BB is shown below. Figure 5 and Figure 6As shown, in this embodiment, there are multiple axial flow cyclone assemblies 1, which are circumferentially distributed around the centerline of the first particle moving bed assembly 2. Each cyclone tube 12 is tightly fitted and sealed to its adjacent cyclone tubes 12. The sidewall of each cyclone tube 12 facing the centerline of the first particle moving bed assembly 2 between the two contact points of each of the two adjacent cyclone tubes 12 is closed. The sidewall of each cyclone tube 12 facing away from the centerline of the first particle moving bed assembly 2 between the two contact points of each of the two adjacent cyclone tubes 12 has a mesh structure. The swirling mechanism 13 is located above the interior of the cyclone tubes 12. The multiple cyclone tubes 12 form an intermediate space, which is closed. There are at least two particle moving bed assemblies. When there are multiple particle moving bed assemblies, the number of particle moving bed assemblies is preferably 2 to 4, and the multiple particle moving bed assemblies are all nested outside the multiple axial flow cyclone assemblies 1 with the axis of the circumference of the axial flow cyclone assemblies 1 as the center. The side walls of the moving bed tube body all have a mesh structure.

[0066] The impurity-laden gas exiting from the side wall of the cyclone tube 12 first centrifugally passes radially through the first moving bed tube 23, forming the first layer of particle moving bed, and then radially centrifugally passes laterally through the particle moving bed formed by subsequent moving bed tubes, thus achieving multi-stage purification. Simultaneously, as the cross-flow velocity gradually decreases during the radial outward movement of the airflow, the entrainment of dust particles within the particle moving bed is reduced, further improving the separation effect of the axial flow adsorption coupling purification device on fine particulate matter, achieving the purpose of multi-stage fine separation.

[0067] When an axial flow adsorption-coupled purification device needs to separate solid and liquid phase particulate impurities from a gas, the particle size of the first collecting particles is between 1.5 mm and 2.5 mm, and the particle bed thickness in the first moving bed tube 23 is between 0.1d and 3d, where d represents the diameter of the cyclone tube 12. The particle size of the second collecting particles is between 0.8 mm and 1.2 mm, and the particle bed thickness in the first moving bed tube 23 is between 0.05d and 2.5d. Within the above parameter range, PM2.5 solid and liquid phase particulate impurities in the contaminated gas can be basically completely removed. Depending on the gas treatment requirements, the collecting particles can be selected that have adsorption properties, such as CO2, H2S, and SO2. x NO x Particulate adsorbents.

[0068] When an axial flow adsorption coupled purification device needs to separate gaseous impurities from a gas, and the gas contains both solid and liquid particulate impurities, the first collecting particles are those with the ability to collect both solid and liquid particulate impurities and adsorb gaseous impurities; the second collecting particles are those with the ability to collect both solid and liquid particulate impurities and adsorb gaseous impurities. Furthermore, the particle size of the second collecting particles is smaller than that of the first collecting particles, with a ratio between 0.3 and 0.8. For example, taking integrated desulfurization, denitrification, and dust removal purification as an example, the collecting particles in the particle bed are correspondingly set as individual or mixed particles of desulfurizing and denitrifying agents. Larger-diameter collecting particles serve as the first collecting particles, and smaller-diameter collecting particles serve as the second particle bed collecting particles, thereby achieving cascade filtration in the axial flow adsorption coupled purification device. In one embodiment, the first collecting particles are a mixture of desulfurizing and denitrifying agents, and the second collecting particles are also a mixture of desulfurizing and denitrifying agents. In another embodiment, the first collecting particles are desulfurizing agent particles, and the second collecting particles are denitrifying agent particles. The particle bed formed by the denitrifying agent particles can simultaneously filter and remove submicron-sized particulate impurities from the gas. Depending on the time required for desulfurization and denitrification, the thickness of the particle bed formed by the first collecting particles is preferably 0.1–3d (d is the diameter of the axial cyclone tube); the thickness of the particle bed formed by the second collecting particles is preferably 0.05–2.5d.

[0069] The gas first undergoes preliminary removal of particulate impurities by passing through an axial-flow cyclone separator 12. Then, the gas passes through a multi-layered particle bed. In the first particle bed, larger particles undergo deep filtration, while in the second particle bed, smaller particles undergo surface filtration, thus trapping PM2.5 in the gas for further dust removal and improving dust collection accuracy. Simultaneously, based on the adsorption capacity of the selected particles, unwanted gaseous impurities can be removed from the gas. This allows for simultaneous gas dust removal and impurity gas separation within the same device, resulting in a simple process flow, low energy consumption, large throughput, high separation accuracy, and wide applicability. Furthermore, as the impurity-laden gas flows centrifugally through the particle bed, the flow area gradually increases while the gas velocity continuously decreases. This significantly reduces the gas's ability to entrain submicron-sized particulate impurities, and the extended residence time facilitates the adsorption of gaseous impurities by the particles.

[0070] This axial flow adsorption-coupled purification device incorporates a built-in cyclone tube 12. The diameter of the cyclone tube 12 can be effectively controlled to ensure sufficient cyclone separation and cleaning of the inner wall of the cyclone tube 12 by the cyclone gas, according to the required throughput and cyclone intensity. Simultaneously, the moving bed forming the particle-collecting moving bed is externally sleeved on the cyclone tube 12, ensuring that the number of layers and the thickness of each layer of the particle-collecting moving bed can be flexibly adjusted according to the required throughput, properties, collection efficiency, and residence time of the impurity gas. Because the gas flow containing impurities moves centrifugally, the cross-flow velocity in the particle-collecting moving bed gradually decreases with the airflow, effectively reducing the secondary entrainment of fine particles deposited in the bed by the cross-flow gas. This ensures the separation efficiency of the axial flow adsorption-coupled purification device for submicron particles, facilitates improved processing capacity, and provides a longer residence time, laying the foundation for the coupling of adsorption. Finally, the axial flow adsorption coupling purification device can increase the processing capacity by configuring multiple axial flow cyclone components 1, but the scale-up effect is not obvious.

[0071] All articles and references disclosed herein, including patent applications and publications, are incorporated herein by reference for various purposes. The term “substantially constitutes…” used to describe a combination should include the identified element, component, part, or step, as well as other elements, components, parts, or steps that do not substantially affect the essential novelty of the combination. The use of the terms “comprising” or “including” to describe combinations of elements, components, parts, or steps herein also contemplates embodiments substantially constituted by such elements, components, parts, or steps. The use of the term “may” herein is intended to indicate that any described attribute “may” include is optional. Multiple elements, components, parts, or steps can be provided by a single integrated element, component, part, or step. Alternatively, a single integrated element, component, part, or step can be divided into multiple separate elements, components, parts, or steps. The disclosure of “a” or “an” used to describe an element, component, part, or step does not imply exclusion of other elements, components, parts, or steps.

[0072] The various embodiments in this specification are described in a progressive manner, with each embodiment focusing on its differences from other embodiments. Similar or identical parts between embodiments can be referred to interchangeably. The above embodiments are only for illustrating the technical concept and features of the present invention, and are intended to enable those skilled in the art to understand the content of the present invention and implement it accordingly. They should not be construed as limiting the scope of protection of the present invention. All equivalent changes or modifications made according to the spirit and essence of the present invention should be covered within the scope of protection of the present invention.

Claims

1. An axial flow adsorption coupling purification device, characterized in that, The axial flow adsorption coupling purification device includes: A housing extending along an axis, the housing having a first cylindrical section and a second cylindrical section located below the first cylindrical section, the second cylindrical section having a radial dimension that gradually decreases from top to bottom; a gas outlet is provided at the upper end of the sidewall of the first cylindrical section, and a dust outlet is provided at the lower end of the second cylindrical section; The first particle moving bed assembly includes: a first hopper for loading the first collected particles, a first moving bed tube extending along an axis, a first material leg, and a first waiting inclined tube, wherein the lower end of the first hopper forms a first material sealing area by tapering, the upper end of the first moving bed tube is connected to the first material sealing area, the side wall of the first moving bed tube has a mesh structure, the upper end of the first material leg is connected to the lower end of the first moving bed tube, the upper end of the first waiting inclined tube is connected to the lower end of the first material leg, and the first waiting inclined tube extends out of the second section of the cylinder; The first lifting component is used to lift the particles discharged from the first inclined tube and input them into the first hopper; An axial cyclone assembly includes a cyclone tube extending along an axis, inserted from the upper end of the first hopper into the first moving bed tube body, the upper end of the cyclone tube being a gas inlet, and a mesh structure on the side wall of the cyclone tube located in the first moving bed tube body; a cyclone mechanism disposed in the cyclone tube to generate swirling flow of gas; and a cyclone stabilizer disposed at the bottom of the cyclone tube to eliminate the tailing phenomenon of airflow in the cyclone tube.

2. The axial flow adsorption coupling purification device according to claim 1, characterized in that, The first lifting assembly includes: a lifting pipe, comprising a pre-lifting pipe body and a lifting pipe body, the pre-lifting pipe body being connected to the first regenerated inclined pipe; a spouting bed shell forming a storage space, the lifting pipe body being inserted into the spouting bed shell from its lower end, the upper end of the spouting bed shell having a regeneration gas outlet; and a regeneration inclined pipe, one end of which is connected to the lower end of the side wall of the spouting bed shell.

3. The axial flow adsorption coupling purification device according to claim 1, characterized in that, There are multiple axial flow cyclone components, and the multiple axial flow cyclone components are circumferentially distributed around the center line of the first particle moving bed component.

4. The axial flow adsorption coupling purification device according to claim 3, characterized in that, Each cyclone tube is disposed close to and sealed with the adjacent cyclone tubes. The sidewall of each cyclone tube, which is closed between the two contact points of the two adjacent cyclone tubes and faces the center line of the first particle moving bed assembly, has a mesh structure between the two contact points of the two adjacent cyclone tubes and faces away from the center line of the first particle moving bed assembly. The swirling mechanism is located above the interior of the cyclone tubes. The plurality of cyclone tubes form an intermediate space, which is closed.

5. The axial flow adsorption coupling purification device according to claim 1, characterized in that, The axial flow adsorption coupling purification device also includes: The second particle moving bed assembly includes: a second hopper for loading second collected particles, a second moving bed tube extending along an axis, a second material leg, and a second pre-cooking inclined tube. The first hopper is disposed within the second hopper. The lower end of the second hopper forms a second material sealing zone with the lower end of the first hopper via a tapering section. The second moving bed tube is sleeved outside the first moving bed tube. The upper end of the second moving bed tube is connected to the second material sealing zone. The sidewall of the second moving bed tube has a mesh structure. The upper end of the second material leg is connected to the lower end of the second moving bed tube and is sleeved outside the first material leg. The upper end of the second pre-cooking inclined tube is connected to the lower end of the second material leg and extends out of the second section of the cylindrical body. The first pre-cooking inclined tube extends out of the second pre-cooking inclined tube and then out of the second section of the cylindrical body. The second lifting component is used to lift the particles discharged from the second inclined tube and input them into the second hopper, and to discharge the regeneration gas.

6. The axial flow adsorption coupling purification device according to claim 5, characterized in that, The second moving bed tube is coaxially arranged with the first moving bed tube; the gaps in the mesh structure extend in the circumferential direction, or in the axial direction, or in the diagonal direction; the ratio of the width of the gaps on the second moving bed tube to the diameter of the second captured particle is between 0.13 and 0.25; the ratio of the width of the gaps on the first moving bed tube to the diameter of the first captured particle is between 0.13 and 0.

25.

7. The axial flow adsorption coupling purification device according to claim 5, characterized in that, When the axial flow adsorption coupling purification device needs to separate solid and liquid phase particulate impurities in the gas, the particle size of the first collected particles is between 1.5 mm and 2.5 mm, and the particle bed thickness in the first moving bed tube is between 0.1 d and 3 d, where d represents the diameter of the cyclone tube; the particle size of the second collected particles is between 0.8 mm and 1.2 mm, and the particle bed thickness in the second moving bed tube is between 0.05 d and 2.5 d.

8. The axial flow adsorption coupling purification device according to claim 5, characterized in that, When the axial flow adsorption coupling purification device needs to separate gaseous impurities from the gas, and the gas contains solid and liquid particulate impurities, the first collecting particle is a collecting particle with the ability to collect solid and liquid particulate impurities and the ability to adsorb gaseous impurities; the second collecting particle is a collecting particle with the ability to collect solid and liquid particulate impurities and the ability to adsorb gaseous impurities.

9. The axial flow adsorption coupling purification device according to claim 8, characterized in that, The ratio of the average particle size of the second captured particle to the average particle size of the first captured particle is between 0.3 and 0.

8.

10. A method for operating the axial flow adsorption coupling purification device as described in claim 1, characterized in that, include: The impure gas is introduced from the gas inlet at the top of the cyclone tube, and the impure gas is transformed into a swirling state by the swirling mechanism and moves downward; The first hopper is loaded with the first collecting particles, and the first collecting particles enter the first moving bed tube after passing through the first material sealing area, and then continue to move downward. The particulate impurities in the impure gas that cannot pass through the mesh structure move to the inner wall of the cyclone tube under the action of centrifugal force and slide down into the first moving bed tube body along the inner wall of the cyclone tube. The impurity-containing gas flows radially outward through the mesh structure on the side wall of the cyclone tube and forms a cross-flow moving bed with the first collecting particles moving downward in the first moving bed tube. The impurity gas and / or particulate impurities that can pass through the mesh structure are filtered, adsorbed or intercepted by the first collecting particles to form purified gas. The purified gas is discharged through the mesh structure of the first moving bed tube to the gas outlet of the shell. After the particles that have been filtered, adsorbed or intercepted in the first moving bed tube are combined with the particulate impurities that have slid down the inner wall of the cyclone tube into the first moving bed tube, they are lifted by the first material leg and the first waiting inclined tube, and then fed into the first material bin.

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