Reverse cyclone type particle bed flue gas purification system and purification method thereof

Abstract

The application discloses a reverse cyclone type particle bed flue gas purification system and a purification method thereof, and relates to the technical field of high-temperature flue gas purification. The reverse cyclone type particle bed flue gas purification system comprises a reverse cyclone type moving bed unit, which comprises a storage bin, a feeding mechanism connected with an outlet of the storage bin, a moving bed body, an outlet of the feeding mechanism being communicated with the moving bed body, a gas outlet being arranged at a side wall of the moving bed body, a cyclone unit, an outlet at a lower end of the moving bed body being communicated with the cyclone unit through a gas-solid contact unit, a gas inlet being arranged at a side wall of the cyclone unit, an elutriation cyclone separator, a solid outlet of the cyclone separator being communicated with the storage bin, and an outlet at a lower end of the cyclone unit being communicated with a tangential inlet of the cyclone separator through a lifting mechanism. The application can realize efficient dust removal under a higher treatment capacity and meet the requirement of long-period stable operation.

Description

Technical Field

[0001] This invention relates to the field of high-temperature flue gas purification technology, and in particular to a counter-cyclone granular bed flue gas purification system and its purification method. Background Technology

[0002] In the petrochemical industry, common catalytic cracking processes require the removal of particles larger than 10 micrometers from the regenerator outlet flue gas to protect downstream flue gas turbines. In energy conversion, the flue gas produced by biomass combustion also contains a large amount of fine particulate matter, which needs to be removed before entering subsequent power generation equipment. The feed gas from ammonia synthesis units also needs to have fine dust removed before entering large centrifuges to ensure the safe and stable operation of the compressor.

[0003] To address the problems in the aforementioned fields, efficient gas-solid separation technologies are needed. Currently, wet dust removal technology for flue gas is widely used; however, it brings secondary pollution problems such as "white smoke" and wastewater discharge. Particle bed filters, as a dry dust removal technology, have developed rapidly in recent years, possessing the ability to capture dust while removing harmful gases. Moving bed filtration is a typical particle bed filtration technology, with advantages such as corrosion resistance and high-temperature resistance. Even using inexpensive filter media particles, it can achieve good dust collection capabilities, and it has promising development prospects.

[0004] Based on the relative flow state of the gas and solid phases within the moving bed filter, moving bed filters can be broadly classified into three types: counter-current, co-current, and cross-flow. In cross-flow moving beds, due to the cross-flow contact between the gas and solid phases, abnormal operating conditions such as cavities and wall adhesion often occur when the filtration gas velocity is high. Furthermore, cross-flow moving beds typically have a small and fixed bed thickness, resulting in a shorter gas residence time, which is detrimental to the purification of harmful gases. In co-current moving beds, the gas and solid phases move in the same direction along with the gravitational field. The dust-laden gas moves in the same direction along with the filter media particles carrying the dust, increasing the possibility of dust escape during the flow. Smaller dust particles are more easily carried out of the filter, resulting in even lower particle size efficiency for fine dust. In contrast, in counter-current moving beds, the gas and solid phases contact in opposite directions. The flue gas always comes into contact with regenerated particles during the flow, resulting in less dust adsorption on the surface and a larger effective capture surface area. Countercurrent contact increases the interaction between dust and filter media particles, resulting in higher overall dust collection efficiency. Furthermore, the smooth movement of solid filter media minimizes dead zones, allowing dust deposited within the filter to be discharged along with the media, reducing the likelihood of clogging and ensuring long-term stable operation. However, with increasing gas throughput in various fields, even existing countercurrent moving bed filters cannot fully meet the requirements of both high-efficiency dust removal at high throughput and long-term stable operation. Therefore, further improvements to existing countercurrent moving bed filters are necessary to adapt to these new performance demands. 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 a counter-cyclone granular bed flue gas purification system and purification method, which can achieve efficient dust removal at a high throughput and meet the requirements of long-term stable operation.

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

[0007] A counter-cyclone granular bed flue gas purification system, the counter-cyclone granular bed flue gas purification system comprising:

[0008] A reverse vortex moving bed unit includes: a storage bin; a feeding mechanism connected to the outlet of the storage bin; a moving bed body, the outlet of the feeding mechanism being connected to the moving bed body, and a gas outlet on the side wall of the moving bed body; and a vortex unit, the outlet at the lower end of the moving bed body being connected to the vortex unit via a gas-solid contact unit, and a gas inlet on the side wall of the vortex unit.

[0009] The solids outlet of the Taoxi cyclone separator can be connected to the storage silo.

[0010] The outlet at the lower end of the cyclone unit can be connected to the tangential inlet of the cyclone separator via a lifting mechanism.

[0011] Preferably, the cyclone separator is located above the counter-cyclone moving bed unit; the diameter of the filter media particles used in the counter-cyclone granular bed flue gas purification system is between 0.5 mm and 3 mm.

[0012] Preferably, the gas-solid contact unit includes: a variable-diameter section, a constant-diameter section, and an anti-entrapment section arranged sequentially from top to bottom. The variable-diameter section includes a plurality of first components that gradually decrease in size from top to bottom. The constant-diameter section includes a plurality of second components of the same size. The second component includes a tapered portion that gradually decreases in size from top to bottom and a constant-diameter portion connected to the lower end of the tapered portion. The constant-diameter portion at least partially extends into the tapered portion of the adjacent second component. There is a gap between the sidewalls of adjacent first components to allow the flue gas to be treated to flow into the gas-solid contact unit through the gap. There is also a gap between the sidewalls of adjacent second components to allow the flue gas to be treated to flow into the gas-solid contact unit through the gap.

[0013] Preferably, the vertical height of the variable diameter section is between 1:2.5 and 1:4 compared to the vertical height of the constant diameter section; the vertical height of the anti-slip section is between 1:3 and 1:4 compared to the vertical height of the constant diameter section; the ratio of the diameter at the maximum point of the variable diameter section to the diameter at the maximum point of the constant diameter section is between 2:1 and 3:1; the angle Φ of the first component is between 45 degrees and 70 degrees; and the angle β of the second component is between 60 degrees and 80 degrees.

[0014] Preferably, the storage silo is provided with a first flow guiding mechanism, which is formed by two cones joined together, with the vertices of the two cones facing upwards and downwards respectively; the ratio of the bottom diameter of the cone in the first flow guiding structure to the diameter of the storage silo is between 1:1.5 and 1:2.5; the ratio of the height of the upper cone to the height of the lower cone in the first flow guiding structure is between 1:3.5 and 1:5.5.

[0015] And / or,

[0016] The swirling unit is provided with a second flow guiding mechanism, which is formed by two cones joined together, with the vertices of the two cones facing upwards and downwards respectively; the ratio of the bottom diameter of the cone in the second flow guiding structure to the diameter of the largest part of the swirling unit is between 1:1.5 and 1:2.5; the ratio of the height of the upper cone to the height of the lower cone in the second flow guiding structure is between 1:3.5 and 1:5.5; the lower part of the swirling unit is tapered, and the sidewall of the lower cone in the second flow guiding structure is parallel to the sidewall of the tapered lower part of the swirling unit.

[0017] Preferably, the moving bed is cylindrical, with an annular space between its outer side wall and the inner side wall of the swirl unit. The gas inlet is tangentially located on the side wall of the swirl unit so that the flue gas to be treated input from the gas inlet rotates into the moving bed. The gas inlet is higher than the uppermost end of the gas-solid contact unit.

[0018] Preferably, at the location of the gas inlet, the cross-sectional area of ​​the annular space between the outer wall of the moving bed and the inner wall of the vortex unit in the horizontal direction is greater than or equal to the inlet area of ​​the gas inlet and less than or equal to the gas-solid two-phase contact area of ​​the gas-solid contact unit; the ratio of the diameter of the constant diameter portion of the moving bed to the diameter of the smallest part of the vortex unit is between 1:1.5 and 1:3.

[0019] The gas-solid two-phase contact area of ​​the gas-solid contact unit should be less than or equal to the cross-sectional area of ​​the moving bed in the horizontal direction.

[0020] Preferably, the apparent gas velocity within the moving bed is between 0.05 m / s and 0.875 m / s;

[0021] The movable bed is designed with a bed layer thickness of h.

[0022]

[0023] Where η represents efficiency and δ represents the filtering factor, which is related to the Stokes number Stk.

[0024]

[0025] ε0 represents the bed porosity, and the Stokes number Stk in the formula is as follows:

[0026]

[0027] u g d represents apparent gas velocity, in m / s. p ρ represents the average particle size of the filter media, in meters (m). p This indicates the particle density of the filter media, expressed in kg / m³. 3 μ represents the dynamic viscosity coefficient, with units of N·s / m²; d s This indicates the average particle size of dust particles, expressed in meters (m).

[0028] Preferably, the cyclone separator is a tangential cyclone separator;

[0029] The cyclone separator includes: a cyclone shell, which includes a constant diameter section and a tapered section located below the constant diameter section that tapers from top to bottom; a cyclone material cylinder connected to the lower end of the cyclone shell; a cyclone exhaust pipe extending from top to bottom into the upper part of the cyclone shell; and a back-blowing mechanism disposed on the side wall of the tapered section of the cyclone shell, the back-blowing mechanism being used to spray gas upward.

[0030] The diameter of the constant-diameter section of the cyclone shell and the inlet cross-section of the cyclone separator satisfy the following relationship:

[0031] k a =πD1 2 / 4ab;

[0032] Where, k a The value ranges from 2 to 8; D1 represents the diameter of the constant diameter section of the cyclone shell; the inlet of the cyclone separator is rectangular, with a height and b respectively;

[0033] The height h of the cyclone shell and the diameter D1 of the constant diameter section of the cyclone shell satisfy the following relationship:

[0034]

[0035] in,

[0036] The value ranges from 2 to 4; The value ranges from 1.5 to 3;

[0037] h1 represents the height of the constant-diameter section of the cyclone shell, and h2 represents the height of the tapered section of the cyclone shell. This indicates the ratio between the height h of the cyclone shell and the diameter D1 of the constant diameter section of the cyclone shell. This indicates the ratio between the height of the constant diameter section of the cyclone shell and the diameter D1 of the constant diameter section of the cyclone shell; This indicates the ratio between the height of the tapered section of the cyclone shell and the diameter D1 of the constant diameter section of the cyclone shell;

[0038] The insertion depth h4 of the cyclone exhaust pipe and the inlet height a of the cyclone separator satisfy the following relationship:

[0039]

[0040] in, The value ranges from 0.4 to 0.8;

[0041] The ratio between the height h5 of the back-blowing mechanism from the cyclone barrel and the height h2 of the tapered section of the cyclone shell is between 1:4 and 1:6; the ratio between the air velocity at the outlet of the back-blowing mechanism and the air velocity at the inlet of the cyclone separator is between 1:10 and 1:15; and the angle γ between the centerline of the back-blowing mechanism and the horizontal plane is between 65° and 85°.

[0042] The ratio between the diameter D3 of the cyclone barrel and the diameter D1 of the constant diameter section of the cyclone shell is between 1.1:1 and 1.5:1; the ratio between the height h3 of the cyclone barrel and the diameter D3 of the cyclone barrel is between 2:1 and 4:1; and the ratio between the diameter of the outlet of the cyclone barrel and the diameter D3 of the cyclone barrel is between 0.8:1 and 0.9:1.

[0043] A purification method employing any of the counter-current vortex granular bed flue gas purification systems described above, the purification method comprising:

[0044] The flue gas to be treated is input into the air inlet at the side wall of the cyclone unit. The flue gas enters the cyclone unit and flows in a swirling motion. Under the action of inertial force, larger dust particles are thrown to the side wall of the cyclone unit, and the flue gas to be treated carrying smaller dust particles enters the gas-solid contact unit.

[0045] The flue gas to be treated flows upward through the gas-solid contact unit and enters the moving bed. The filter media particles flow downward from the storage bin into the moving bed and enter the cyclone unit through the gas-solid contact unit. In the cyclone unit, the gas-solid contact unit, and the moving bed, the filter media particles come into contact with the flue gas to adsorb and filter the dust particles in the flue gas.

[0046] The filter media particles containing dust particles that enter the cyclone unit are conveyed to the cyclone separator by the lifting mechanism;

[0047] The filtered flue gas that enters the moving bed is discharged from the gas outlet on the side wall of the moving bed.

[0048] The filter media particles adsorbed with dust particles are separated by a cyclone separator under the action of swirling inertia and gravity settling, so that the filter media particles are discharged from the solid outlet at the bottom of the cyclone separator into the storage bin, and the dust particles are discharged from the cyclone exhaust pipe.

[0049] The technical solution of the present invention has the following significant beneficial effects:

[0050] 1. The counter-cyclone granular bed flue gas purification system in this application mainly includes a counter-cyclone moving bed unit and a sifting cyclone separator. The counter-cyclone moving bed unit comprises a cyclone unit and a moving bed body. It utilizes the centrifugal separation effect of the cyclone unit and the interception and filtration effect of the moving bed to jointly achieve the filtration and purification of the flue gas to be treated. The sifting cyclone separator regenerates the filter media particles through centrifugation and sifting. Unlike conventional cyclone separators, the sifting cyclone separator in this application only needs to collect the filter media particles; for dust, the optimal collection efficiency is 0, meaning complete separation of filter media particles and dust is desired.

[0051] 2. The counter-cyclone granular bed flue gas purification system in this application adopts a gas-solid counter-current contact method and a gas cyclone method, which can achieve good flue gas purification effect at a high throughput. This counter-cyclone granular bed flue gas purification system enhances the interaction (collision, interception, etc.) between dust and filter particles, resulting in high overall dust filtration efficiency, especially for fine dust (less than 10 micrometers), where the efficiency can reach almost 100%. Dust-laden gas "swirls" into the cyclone unit. Larger dust particles are thrown to the sidewall by inertial and centrifugal forces, while smaller dust particles come into counter-current contact with the gas-solid contact unit and the filter particles in the moving bed, thus being intercepted and captured. Compared with previous systems, this system uses gas-solid counter-current contact, resulting in higher gas-solid separation efficiency.

[0052] 3. Secondly, the height of the filter media particle bed can be changed by altering the relative position of the first flow guiding mechanism within the storage silo 1. A calculation method for determining the appropriate bed thickness is provided, allowing for design calculations based on efficiency requirements. Furthermore, the flow guiding mechanism effectively reduces the amount of filter media particles used in non-filtration areas. The Taoxi cyclone separator overcomes the limitations of traditional cyclone separators, which can only achieve gas-solid separation. By combining the Taoxi cyclone separator with a backflushing mechanism, effective separation of the dust phase and filter media particle phase can be achieved with lower energy consumption, enabling filter media particle regeneration.

[0053] 4. The gas-solid contact unit in this counter-cyclone granular bed flue gas purification system adopts a louvered structure formed by components, which can better contact the dust in the dust-laden gas with the filter particles. Compared with the previous Johnson mesh structure, this invention can avoid the problem of dust scaling on the Johnson mesh surface, blocking the gas passage and causing increased pressure drop.

[0054] 5. The counter-cyclone granular bed flue gas purification system in this application has a relatively simple structure, is easy to operate, and requires no backflushing. It minimizes energy consumption while meeting environmental emission requirements. The system offers high operational flexibility and can operate stably for extended periods. Furthermore, the counter-cyclone granular bed flue gas purification system has a simple process flow, effectively reducing its footprint, and has a wide range of applications, meeting the needs of dry purification of high-temperature, pressurized flue gas.

[0055] 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

[0056] 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.

[0057] Figure 1 This is a schematic diagram of the counter-cyclone granular bed flue gas purification system in an embodiment of the present invention;

[0058] Figure 2 This is a partial cross-sectional schematic diagram of the gas-solid contact unit in an embodiment of the present invention;

[0059] Figure 3 This is a top view of the gas-solid contact unit in an embodiment of the present invention;

[0060] Figure 4 This is a half-sectional schematic diagram of the first flow guiding mechanism in an embodiment of the present invention;

[0061] Figure 5 This is a half-sectional schematic diagram of the second flow guiding mechanism in an embodiment of the present invention;

[0062] Figure 6 This is a schematic diagram of the structure of the cyclone separator in an embodiment of the present invention;

[0063] Figure 7 This is a top view of the cyclone separator in an embodiment of the present invention.

[0064] The reference numerals in the above figures are as follows:

[0065] 1. Storage bin; 2. First flow guiding mechanism; 3. Feeding mechanism; 4. Moving bed; 5. Gas inlet; 6. Cyclone unit; 7. Gas-solid contact unit; 71. Anti-entrapment section; 72. Constant diameter section; 721. Second component; 73. Variable diameter section; 731. First component; 74. Connecting rod; 8. Second flow guiding mechanism; 9. Waiting bend; 10. Gas outlet; 11. Second valve; 12. Lifting air inlet; 13. Lifting mechanism; 14. Regeneration riser; 15. Cyclone separator; 151. Cyclone exhaust pipe; 152. Cyclone shell; 153. Back-blowing mechanism; 154. Cyclone material cylinder; 16. Bag filter; 17. First valve. Detailed Implementation

[0066] 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.

[0067] 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.

[0068] To achieve both high-efficiency dust removal at high throughput and stable operation over long periods, this application proposes a counter-cyclone granular bed flue gas purification system. Figure 1 This is a schematic diagram of the counter-cyclone granular bed flue gas purification system in an embodiment of the present invention, as shown below. Figure 1 As shown, the counter-cyclone granular bed flue gas purification system may include: a counter-cyclone moving bed unit, which includes: a storage bin 1; a feeding mechanism 3 connected to the outlet of the storage bin 1; a moving bed body 4, the outlet of the feeding mechanism 3 being connected to the moving bed body 4, and a gas outlet 10 on the side wall of the moving bed body 4; a cyclone unit 6, the outlet at the lower end of the moving bed body 4 being connected to the cyclone unit 6 through a gas-solid contact unit 7, and a gas inlet 5 on the side wall of the cyclone unit 6; a cyclone separator 15, the solid outlet of which can be connected to the storage bin 1; and the outlet at the lower end of the cyclone unit 6 being connected to the tangential inlet of the cyclone separator 15 through a lifting mechanism 13.

[0069] Among them, such as Figure 1As shown, the storage bin 1, feeding mechanism 3, moving bed body 4, and cyclone unit 6 in the counter-cyclone moving bed unit are generally distributed from top to bottom. The entire counter-cyclone moving bed unit can be cylindrical. The storage bin 1 can be composed of a cylindrical body and a sealed head that seals the upper part of the body. The middle part of the sealed head can have a feed inlet, which can be connected to the solid outlet at the bottom of the cyclone separator 15 through the first valve 17. The storage bin 1 is used to store a certain amount of filter media particles. The lower side wall of the storage bin 1 can be tapered from top to bottom, which can facilitate the flow of filter media particles in the storage bin 1 into the feeding mechanism 3 and reduce the possibility of dead corners due to filter media particle accumulation.

[0070] like Figure 1 As shown, the inlet of the feeding mechanism 3 is connected to the lower part of the storage bin 1, so that the filter particles in the storage bin 1 can enter the inlet of the feeding mechanism 3 under the action of gravity. The outlet of the feeding mechanism 3 is located in the moving bed 4. There can be multiple feeding mechanisms 3, which can be evenly distributed circumferentially. The feeding mechanism 3 can also be located in the middle of the storage bin 1. The feeding mechanism 3 can include a conical feeding section and a cylindrical feeding section, with the cylindrical feeding section located below the conical feeding section. The sidewall of the conical feeding section can be connected to the sidewall of the lower end of the storage bin 1. Furthermore, the sidewall of the conical feeding section and the sidewall of the lower end of the storage bin 1 can have the same slope, which can increase the smoothness of the flow of filter particles near the sidewall of the lower end of the storage bin 1 into the feeding mechanism 3. The height ratio of the conical feeding section and the cylindrical feeding section is between 1:2.5 and 1:5. The optimal angle between the sidewall of the conical feeding section and the horizontal plane can be between 65° and 80°. Of course, the angle between the sidewall of the conical feeding section and the horizontal plane can also be within other ranges. By changing the position of the feeding mechanism 3 in the vertical direction, the height of the filter material granular bed layer inside the moving bed 4 can be adjusted accordingly during the operation of the counter-cyclone granular bed flue gas purification system.

[0071] like Figure 1As shown, the moving bed 4 is generally cylindrical, with its upper end connected to the side wall of the storage bin 1, and it can also connect to the upper edge of the tapered lower portion of the storage bin 1. Alternatively, the upper half of the moving bed 4 has a constant diameter, while the diameter of the lower half gradually decreases from top to bottom. The optimal angle between the side wall of the lower half of the moving bed 4 and the horizontal plane is between 75 and 85 degrees. The outlet at the lower end of the moving bed 4 is connected to the vortex unit 6 via a gas-solid contact unit 7. The uppermost end of the gas-solid contact unit 7 is connected to the bottom of the moving bed 4. The gas-solid contact unit 7 is located within the vortex unit 6. The moving bed 4 has a gas outlet 10 on its side wall, which can be tangentially positioned. The gas outlet 10 can be located in the upper half of the constant diameter section of the moving bed 4, which facilitates the direct discharge of gas through the side wall of the moving bed 4 to the outside of the counter-cyclone granular bed flue gas purification system without obstructing the gas inlet 5 at the side wall of the cyclone unit 6. The cross-section of the gas outlet 10 is generally rectangular or circular, and its area can be equal to that of the gas inlet 5.

[0072] As a feasible option, Figure 2 This is a partial cross-sectional schematic diagram of the gas-solid contact unit in an embodiment of the present invention. Figure 3 This is a top view of the gas-solid contact unit in an embodiment of the present invention, as shown below. Figures 2 to 3 As shown, the gas-solid contact unit 7 may include: a variable-diameter section 73, a constant-diameter section 72, and an anti-entrapment section 71 arranged sequentially from top to bottom. The variable-diameter section 73 includes a plurality of first members 731 that taper downwards from top to bottom, with the size of the plurality of first members 731 gradually decreasing from top to bottom. The constant-diameter section 72 may include a plurality of second members 721 of the same size, each second member 721 including a tapered portion that tapers downwards from top to bottom and a constant-diameter portion connected to the lower end of the tapered portion, the constant-diameter portion at least partially extending into the tapered portion of the adjacent second member 721. There is a gap between the sidewalls of adjacent first members 731 to allow the flue gas to be treated to flow into the gas-solid contact unit 7 through the gap; there is also a gap between the sidewalls of adjacent second members 721 to allow the flue gas to be treated to flow into the gas-solid contact unit 7 through the gap. In this way, the entire gas-solid contact unit 7 forms a louver-like structure through the gap between the variable diameter section 73 and the constant diameter section 72. This ensures that the filter media particles can flow smoothly from top to bottom within the gas-solid contact unit 7, and also allows the flue gas to better enter the gas-solid contact unit 7 through the gap between the variable diameter section 73 and the constant diameter section 72 and flow upwards, thus contacting the filter media particles to achieve adsorption, capture, and interception of dust particles in the flue gas. This process effectively reduces air resistance, prevents a significant increase in pressure drop, and increases the gas-solid contact area, better utilizing the filtration function of the particle bed. The anti-entrainment section 71 can be a straight pipe extending a certain length vertically, which prevents filter media particles from being entrained as the flue gas moves upwards.

[0073] Preferably, the vertical height of the variable diameter section 73 is optimally between 1:2.5 and 1:4 compared to the vertical height of the constant diameter section 72. The vertical height of the anti-slip section 71 is optimally between 1:3 and 1:4 compared to the vertical height of the constant diameter section 72. The ratio of the diameter at its maximum point of the variable diameter section 73 to the diameter at its maximum point of the constant diameter section 72 is optimally between 2:1 and 3:1. The angle Φ of the first component 731 is optimally between 45 degrees and 70 degrees; the angle β of the second component 721 is optimally between 60 degrees and 80 degrees. Furthermore, the sidewalls of the components are as smooth as possible. This structure effectively prevents dust from flowing poorly along the sidewalls of the components.

[0074] In order to fix the first component 731 and the second component 721, such as Figure 2 As shown, the gas-solid contact unit 7 has a connecting rod 74 extending vertically inside. The connecting rod 74 passes through the first component 731 and the second component 721. The inner sidewalls of the first component 731 and the second component 721 are fixedly connected to the connecting rod 74, for example, by welding. There can be multiple connecting rods 74, which are evenly distributed along the inner circumferential wall of the component. At the diameter-changing section 73, the connecting rod 74 is kept directly connected to the inner sidewall of the first component 731 by a certain bend.

[0075] Alternatively, the number of feeding mechanism 3 and gas-solid contact unit 7 can be the same, and the two can be arranged coaxially.

[0076] like Figure 1 As shown, the swirl unit 6 can be cylindrical, with its upper end connected to the side wall of the moving bed 4. Alternatively, the upper end of the swirl unit 6 can be connected to the lower edge of the constant-diameter section of the upper half of the moving bed 4, thus avoiding obstruction of the gas outlet 10, which does not need to pass through the swirl unit 6. An annular space exists between the outer side wall of the moving bed 4 and the inner side wall of the swirl unit 6. The gas inlet 5 is tangentially positioned on the side wall of the swirl unit 6, allowing the flue gas to be treated to enter the moving bed 4 in a rotating manner from the gas inlet 5. The flue gas enters the swirl unit 6 tangentially from the gas inlet 5. Under the action of inertial force, larger dust particles in the flue gas are thrown to the side wall. The airflow carrying smaller dust particles enters the moving bed 4 after contacting the filter media particles through the gas-solid contact unit 7, and then passes through the filter media particle bed of the moving bed 4 from bottom to top. As the flue gas ascends through the filter media particle bed, dust particles in the flue gas are intercepted and captured by the downward-moving filter media particles. After passing through the gas-solid contact unit 7, the filter media particles flow downwards out of the swirl unit 6. The purified gas then flows upwards out of the gas outlet 10.

[0077] like Figure 1As shown, the gas inlet 5 is higher than the top of the gas-solid contact unit 7. Furthermore, the gas inlet 5 is positioned in the annular space. This allows the flue gas entering through the gas inlet 5 to first flow downwards, with most of the flue gas entering the gas-solid contact unit 7 from the side and then flowing upwards, thus reducing obstruction to the downward-moving filter particles within the gas-solid contact unit 7. The gas inlet 5 is generally rectangular.

[0078] Furthermore, at the gas inlet 5, the annular space between the outer wall of the moving bed 4 and the inner wall of the swirl unit 6 has a horizontal cross-sectional area greater than or equal to the inlet area of ​​the gas inlet 5, and less than or equal to the gas-solid two-phase contact area of ​​the gas-solid contact unit 7. The ratio of the diameter of the constant-diameter portion of the moving bed 4 to the diameter of the smallest point of the swirl unit 6 is between 1:1.5 and 1:3. The gas-solid two-phase contact area of ​​the gas-solid contact unit 7 should be less than or equal to the horizontal cross-sectional area of ​​the moving bed 4. This structure effectively reduces gas resistance during the flow of the flue gas to be treated, preventing an increase in pressure drop. The gas-solid two-phase contact area of ​​the gas-solid contact unit 7 is the sum of the annular areas of the gaps aa'bb' between all components. Furthermore, the minimum value of the gas-solid two-phase contact area of ​​the gas-solid contact unit 7 is equal to the cross-sectional area of ​​the filter bed. The gaps between components can be adjusted according to the required gas-solid two-phase contact area of ​​the gas-solid contact unit 7.

[0079] As a feasible option, Figure 4 This is a half-sectional schematic diagram of the first flow guiding mechanism in an embodiment of the present invention, as shown below. Figure 1 and Figure 4 As shown, a first flow guiding mechanism 2 is installed inside the storage silo 1. The first flow guiding structure is formed by the joining of two cones, with the apexes of the two cones facing upwards and downwards respectively. The optimal ratio of the base diameter of the cones in the first flow guiding structure to the diameter of the storage silo 1 is between 1:1.5 and 1:2.5. The optimal ratio of the height of the upper cone to the height of the lower cone in the first flow guiding structure is between 1:3.5 and 1:5.5. The function of the first flow guiding mechanism 2 is to reduce the amount of filter media particles used in the counter-vortex granular bed flue gas purification system, thereby achieving the purpose of saving materials.

[0080] As feasible, the apparent gas velocity within the moving bed 4 generally does not exceed 2 m / s. Furthermore, the average velocity of the filter media particles within the moving bed 4 should preferably be controlled within the range of 0.0001 m / s to 0.006 m / s. Further experimental results show that 0.05 m / s to 0.875 m / s is the optimal operating apparent gas velocity. The height of the filter media bed in the moving bed 4 can be adjusted according to actual dust removal needs. Generally, the higher the filter media bed, the longer the gas residence time in the bed, and the better the dust removal effect. However, the height of the filter media bed needs to be determined based on the gas velocity. Because at higher gas velocities, the dust removal efficiency will decrease, which necessitates increasing the height of the moving bed filter media bed to compensate. Based on experimental results and actual efficiency requirements, the designed filter media bed height within the moving bed 4 is h:

[0081]

[0082] Where η represents efficiency and δ represents the filtering factor, which is related to the Stokes number Stk.

[0083]

[0084] ε0 represents the bed porosity, and the Stokes number Stk in the formula is as follows:

[0085]

[0086] u g d represents apparent gas velocity, in m / s. p ρ represents the average particle size of the filter media, in meters (m). p This indicates the particle density of the filter media, expressed in kg / m³. 3 μ represents the dynamic viscosity coefficient, with units of N·s / m²; d s This indicates the average particle size of dust particles, expressed in meters (m).

[0087] As a feasible option, Figure 5 This is a half-sectional schematic diagram of the second flow guiding mechanism in an embodiment of the present invention, as shown below. Figure 1 and Figure 5 As shown, a second flow guiding mechanism 8 is provided within the swirl unit 6. The second flow guiding structure is formed by the joining of two cones, with the vertices of the two cones facing upwards and downwards respectively. The optimal ratio of the base diameter of the cone in the second flow guiding structure to the diameter at the largest point of the swirl unit 6 is between 1:1.5 and 1:2.5; the optimal ratio of the height of the upper cone to the height of the lower cone in the second flow guiding structure is between 1:3.5 and 1:5.5. Similarly, the function of the second flow guiding mechanism 8 is to reduce the amount of filter media particles used in the counter-swirling granular bed flue gas purification system, thereby achieving the purpose of saving materials.

[0088] Furthermore, such as Figure 1 As shown, the lower part of the swirl unit 6 is tapered, and the cone at the bottom of the second flow guiding mechanism 8 is disposed within the tapered swirl unit 6. The sidewall of the lower cone in the second flow guiding structure is parallel to the sidewall of the tapered swirl unit 6. This minimizes the amount of filter media particles used in the counter-swirling granular bed flue gas purification system and prevents clogging between the sidewall of the cone at the bottom of the second flow guiding mechanism 8 and the sidewall of the swirl unit 6.

[0089] like Figure 1 As shown, the outlet at the lower end of the cyclone unit 6 can be connected to the inlet of the cyclone separator 15 via the lifting mechanism 13. Alternatively, the outlet at the lower end of the cyclone unit 6 can be connected first to the regeneration bend 9, then to the second valve 11, and finally to the lower inlet of the lifting mechanism 13. The lifting mechanism 13 can be a lifting pipe with a lifting air inlet 12 at its bottom, used to input gas to lift the filter media particles upwards. The solid outlet at the lower end of the cyclone separator 15 can be connected to the storage silo 1 via the regeneration riser 14 and the first valve 17. Filter media particles adsorbed with dust particles are fed into the cyclone separator 15 via the lifting mechanism 13. The filter media particles adsorbed with dust particles are separated by the cyclone separator 15 under the action of swirling inertia and gravity settling, so that the filter media particles are discharged from the solid outlet at the lower end of the cyclone separator 15 into the storage silo 1, while the dust particles are discharged from the cyclone exhaust pipe 151.

[0090] As a feasible option, Figure 6 This is a schematic diagram of the structure of the cyclone separator in an embodiment of the present invention. Figure 7 This is a top view of the cyclone separator in an embodiment of the present invention, as shown below. Figure 1 , Figure 6 and Figure 7 As shown, the cyclone separator 15 can be a tangential cyclone separator.

[0091] Furthermore, such as Figure 6 As shown, the cyclone separator 15 may include: a cyclone shell 152, which includes a constant diameter section and a tapered section below the constant diameter section that gradually narrows from top to bottom; a cyclone cylinder 154 connected to the lower end of the cyclone shell 152; a cyclone exhaust pipe 151 extending downwards into the upper part of the cyclone shell 152; and a back-blowing mechanism 153 disposed on the side wall of the tapered section of the cyclone shell 152, the back-blowing mechanism 153 being used to spray gas upwards. The outlet of the cyclone exhaust pipe 151 can be connected to a bag filter 16 to collect and process dust particles for recycling.

[0092] Unlike conventional cyclone separators, the Taoxi cyclone separator 15 used in this application separates dust and filter media particles, which have significantly different particle sizes. Traditional cyclone separators, on the other hand, are used for gas-solid separation. From the perspective of reducing energy consumption and preventing filter media particle wear, it is not necessary to use excessively high air velocities to achieve high fine dust removal efficiency; therefore, the optimal air velocity range is designed to be between 6 m / s and 15 m / s. The Taoxi cyclone separator 15 used in this application employs a conventional tangential inlet, the cross-section of which is generally rectangular. Furthermore, the aspect ratio a / b of the tangential inlet cross-section is generally between 1 and 3.

[0093] Unlike the conventional design concept of cyclone separators 15 for gas-solid two-phase separation, the shorter the residence time of the filter media particles in the cyclone separator 15 of this application, the more beneficial it is to achieving the separation of the dust phase and the filter media particle phase. Therefore, the following special design was carried out:

[0094] like Figure 6 As shown, the diameter of the constant-diameter section of the cyclone shell 152 and the inlet cross-section of the cyclone separator 15 satisfy the following relationship:

[0095] k a =πD1 2 / 4ab;

[0096] It can be observed that decreasing k a This means that the diameter D1 of the constant-diameter section of the cyclone shell 152 is reduced, and the residence time of gas in the cyclone separator 15 is reduced, which is beneficial to improving the separation efficiency of dust and filter media particles. However, k a Too small a value will lead to an increased voltage drop, therefore, k a The value of needs to be between 2 and 8. Wherein, D1 represents the diameter of the constant diameter section of the cyclone shell 152; the inlet of the cyclone separator 15 is rectangular, with a height and b respectively.

[0097] The height h of the cyclone shell 152 and the diameter D1 of the constant diameter section of the cyclone shell 152 satisfy the following relationship:

[0098]

[0099] The smaller the height h of the cyclone shell 152, the smaller the separation space height, and the shorter the gas residence time, which is beneficial to improving the dust separation efficiency. Therefore, The value range needs to be controlled between 2 and 4.

[0100] The height of the constant diameter section of the cyclone shell 152 should be determined taking into account the possibility of filter media particles accumulating inside the cyclone separator 15. The height of the constant diameter section of the cyclone shell 152 should be higher than the height of the inlet section of the cyclone separator 15. therefore, The value range needs to be controlled between 1.5 and 3.

[0101] Where h1 represents the height of the constant diameter section of the cyclone shell 152, and h2 represents the height of the tapered section of the cyclone shell 152. This indicates the ratio between the height h of the cyclone shell 152 and the diameter D1 of the constant diameter section of the cyclone shell 152. This indicates the ratio between the height of the constant diameter section of the cyclone shell 152 and the diameter D1 of the constant diameter section of the cyclone shell 152; This indicates the ratio between the height of the tapered section of the cyclone shell 152 and the diameter D1 of the constant diameter section of the cyclone shell 152.

[0102] In order to allow the filter media particles to flow easily into the cyclone barrel 154, the angle between the tapered section of the cyclone shell 152 and the horizontal plane is optimally between 80° and 87°.

[0103] When the insertion depth h4 of the cyclone exhaust pipe 151 is small, dust particles and filter media particles can easily short-circuit together and enter the bag filter 16 from the cyclone exhaust pipe 151. Therefore, the insertion depth h4 of the cyclone exhaust pipe 151 and the inlet height a of the cyclone separator 15 satisfy the following relationship:

[0104]

[0105] in, The value ranges from 0.4 to 0.8. The cyclone exhaust pipe 151 can be either cylindrical or conical. Taking the cylindrical type as an example, the diameter D5 of the cyclone exhaust pipe 151 should not be too small, otherwise it will lead to an increase in pressure drop. Therefore, D5 is generally taken as 0.4 to 0.6 times D1.

[0106] The presence of the back-flushing mechanism 153 promotes efficient separation of dust and filter media particles within the cyclone separator 15. It is highly effective at separating solids of different particle sizes, facilitating the discharge of smaller dust particles from the cyclone exhaust pipe 151. To maximize the effectiveness of the back-flushing mechanism 153, the optimal ratio between the height h5 of the back-flushing mechanism 153 from the cyclone cylinder 154 and the height h2 of the tapered section of the cyclone shell 152 is between 1:4 and 1:6. The optimal ratio between the air velocity at the outlet of the back-flushing mechanism 153 and the air velocity at the inlet of the cyclone separator 15 is between 1:10 and 1:15. The optimal angle γ between the centerline of the back-flushing mechanism 153 and the horizontal plane is between 65° and 85°.

[0107] The ratio between the diameter D3 of the cyclone filter cylinder 154 and the diameter D1 of the constant diameter section of the cyclone shell 152 ranges from 1:1.1 to 1:1.5. Generally, a diameter D3 of 154 is 1.1 to 1.5 times D2. The ratio between the height h3 of the cyclone filter cylinder 154 and its diameter D3 ranges from 2:1 to 4:1. The outlet diameter of the cyclone filter cylinder 154 affects the movement of the filter media particles; therefore, the ratio between the outlet diameter of the cyclone filter cylinder 154 and its diameter D3 ranges from 0.8:1 to 0.9:1.

[0108] In this application, the cyclone separator 15 can be located above the counter-cyclone moving bed unit. The counter-cyclone granular bed flue gas purification system uses filter media particles with a diameter between 0.5 mm and 3 mm. The filter media particles can be one or more of the following: quartz sand, glass beads, molecular sieve adsorbents, desulfurizing agents, dechlorinating agents, and heavy metal removal agents. This counter-cyclone granular bed flue gas purification system is particularly suitable for high-temperature, pressurized tail gas purification processes requiring continuous operation, such as coal gasification upgrading and emission control in petroleum refining industries.

[0109] In one specific embodiment, the filter media particles are spherical with a diameter of 1.55 mm. The optimal operating apparent gas velocity is 0.315 m / s. The filtration section height of the moving bed 4 is 0.9 m, and the maximum diameter of the moving bed 4 is 0.5 m. The circulation rate of the filter media particles is 0.31 kg / s.

[0110] This application also proposes a purification method using the above-mentioned counter-cyclone granular bed flue gas purification system, the purification method may include:

[0111] The flue gas to be treated is fed into the air inlet on the side wall of the cyclone unit 6. The flue gas enters the cyclone unit 6 and swirls within it. Under the action of inertial force, larger dust particles are thrown to the side wall of the cyclone unit 6, while the flue gas carrying smaller dust particles enters the gas-solid contact unit 7. The intercepted dust particles, along with the filter media particles, enter the conical feeding area at the bottom of the cyclone unit 6.

[0112] The flue gas to be treated flows upward through the gas-solid contact unit 7 and enters the moving bed 4. The filter media particles flow downward from the storage bin 1 into the moving bed 4 and enter the cyclone unit 6 through the gas-solid contact unit 7. In the cyclone unit 6, the gas-solid contact unit 7 and the moving bed 4, the filter media particles come into contact with the flue gas to be treated, so as to adsorb and filter the dust particles in the flue gas.

[0113] The filter media particles containing dust particles that enter the cyclone unit 6 are conveyed to the cyclone separator 15 via the lifting mechanism 13. Specifically, the intercepted dust particles enter the bottom of the cyclone unit 6 along with the filter media particles and are conveyed together with the filter media particles to the cyclone separator 15 via the lifting mechanism 13.

[0114] The filtered flue gas that enters the moving bed 4 is discharged from the gas outlet 10 on the side wall of the moving bed 4.

[0115] Filter media particles adsorbed with dust are separated by a cyclone separator 15 under the action of swirling inertia and gravity settling. The filter media particles are discharged from the solid outlet at the bottom of the cyclone separator 15 into the storage silo 1, while the dust particles are discharged from the cyclone exhaust pipe 151. The dust particles discharged from the cyclone exhaust pipe 151 can be collected and processed by a bag filter 16 for recycling.

[0116] The counter-cyclone granular bed flue gas purification system in this application mainly includes a counter-cyclone moving bed unit and a sifting cyclone separator 15. The counter-cyclone moving bed unit comprises a cyclone unit 6 and a moving bed body 4. It utilizes the centrifugal separation effect of the cyclone and the interception and filtration effect of the moving bed to jointly achieve the filtration and purification of the flue gas to be treated. The sifting cyclone separator 15 regenerates the filter media particles through centrifugation and sifting. Unlike conventional cyclone separators, the sifting cyclone separator 15 in this application only needs to collect the filter media particles; for dust, the optimal collection efficiency is 0, meaning that complete separation of filter media particles and dust is desired.

[0117] The counter-cyclone granular bed flue gas purification system in this application employs both gas-solid counter-current and gas cyclone mechanisms, achieving excellent flue gas purification results at high throughput. This counter-cyclone granular bed flue gas purification system enhances the interaction (collision, interception, etc.) between dust and filter particles, resulting in high overall dust filtration efficiency, especially for fine dust (less than 10 micrometers), where it can achieve almost 100% efficiency. Dust-laden gas "swirls" into the cyclone unit 6. Larger dust particles are thrown to the sidewalls by inertial and centrifugal forces, while smaller dust particles counter-currently contact the filter particles in the moving bed 4 and the gas-solid contact unit 7, thus being intercepted and captured. Compared to previous systems, this system utilizes gas-solid counter-current contact, resulting in higher gas-solid separation efficiency.

[0118] Secondly, the height of the filter media particle bed can be changed by altering the relative position of the first flow guiding mechanism 2 within the storage silo 1, and a calculation method for determining the appropriate bed thickness is provided, allowing for design calculations based on efficiency requirements. Furthermore, the flow guiding mechanism effectively reduces the amount of filter media particles used in non-filtration areas. The Taoxi cyclone separator 15 overcomes the limitation of traditional cyclone separators that can only achieve gas-solid separation. Through the combination of the Taoxi cyclone separator 15 and the backflushing mechanism 153, effective separation of the dust phase and the filter media particle phase can be achieved with lower energy consumption, enabling the regeneration of the filter media particles.

[0119] Furthermore, the gas-solid contact unit 7 in the counter-cyclone granular bed flue gas purification system adopts a louvered structure formed by components, which can better contact the dust in the dust-laden gas with the filter particles. Compared with the previous Johnson mesh structure, this application can avoid the problem of dust scaling on the Johnson mesh surface, blocking the gas passage and causing an increase in pressure drop.

[0120] The counter-cyclone granular bed flue gas purification system in this application has a relatively simple structure, is easy to operate, requires no backflushing, and minimizes energy consumption while meeting environmental emission requirements. The system offers high operational flexibility and can operate stably for extended periods. Furthermore, the counter-cyclone granular bed flue gas purification system has a simple process flow, effectively reducing its footprint, and has a wide range of applications, meeting the needs of dry purification of high-temperature, pressurized flue gas.

[0121] 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.

[0122] 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. A reverse cyclone particulate bed flue gas cleaning system characterized by, The reverse cyclone type particle bed flue gas purification system comprises: a reverse cyclone type moving bed unit, which comprises a storage bin, a feeding mechanism connected with the outlet of the storage bin, a moving bed body, the outlet of the feeding mechanism being communicated with the moving bed body, the side wall of the moving bed body being provided with a gas outlet, the outlet of the feeding mechanism being located in the moving bed body, the gas outlet being located in the upper half of the moving bed body, a cyclone unit, the outlet of the lower end of the moving bed body being communicated with the cyclone unit through a gas-solid contact unit, the side wall of the cyclone unit being provided with a gas inlet; an elutriation cyclone separator, the solid outlet of which can be communicated with the storage bin; the elutriation cyclone separator is a tangential cyclone separator; the elutriation cyclone separator comprises a cyclone shell comprising a constant diameter section and a tapered section tapering from top to bottom below the constant diameter section, a cyclone cylinder connected with the lower end of the cyclone shell, a cyclone exhaust pipe extending into the upper part of the cyclone shell from top to bottom, and a blowback mechanism arranged at the side wall of the tapered section of the cyclone shell, the blowback mechanism being used for spraying gas upwardly; the outlet of the lower end of the cyclone unit can be communicated with the tangential inlet of the elutriation cyclone separator through a lifting mechanism; the moving bed body is in the shape of a cylinder, and an annular space is formed between the outer side wall of the moving bed body and the inner side wall of the cyclone unit, the gas inlet being arranged at the side wall of the cyclone unit in a tangential direction, so that the flue gas to be treated input from the gas inlet rotates into the moving bed body; the gas inlet is higher than the uppermost end of the gas-solid contact unit.

2. The reverse cyclonic particulate bed flue gas cleaning system according to claim 1, characterized in that, The elutriation cyclone separator is located above the reverse cyclone type moving bed unit; the filter material particles used in the reverse cyclone type particle bed flue gas purification system have a diameter of 0.5 mm to 3 mm.

3. The reverse cyclonic particulate bed flue gas cleaning system according to claim 1, wherein, The gas-solid contact unit comprises a variable diameter section, a constant diameter section and an anti-entrainment section arranged in sequence from top to bottom, the variable diameter section comprising a plurality of first members tapering from top to bottom, the sizes of the plurality of first members gradually decreasing from top to bottom; the constant diameter section comprising a plurality of second members of the same size, each of the second members comprising a tapered portion tapering from top to bottom and a constant diameter portion connected with the lower end of the tapered portion, the constant diameter portion at least partially extending into the tapered portion of the adjacent second member below; gaps are formed between the side walls of the adjacent first members, so that the flue gas to be treated flows into the gas-solid contact unit through the gaps, and gaps are formed between the side walls of the adjacent second members, so that the flue gas to be treated flows into the gas-solid contact unit through the gaps.

4. The reverse cyclonic particulate bed flue gas cleaning system of claim 3, wherein, The vertical height of the variable diameter section and the vertical height of the constant diameter section are in the range of 1:2.5 to 1:4, the vertical height of the anti-entrainment section and the vertical height of the constant diameter section are in the range of 1:3 to 1:4, the ratio of the diameter of the variable diameter section at the maximum to the diameter of the constant diameter section at the maximum is in the range of 2:1 to 3:1, the angle Φ of the first member is in the range of 45 degrees to 70 degrees, and the angle β of the second member is in the range of 60 degrees to 80 degrees.

5. The reverse cyclonic particulate bed flue gas cleaning system of claim 1, wherein, The first flow guide mechanism is formed by two cones which are connected in abutment, and the vertexes of the two cones are respectively directed upward and downward; the ratio of the diameter of the bottom surface of the cone in the first flow guide mechanism to the diameter of the storage bin is between 1:1.5 and 1:2.5; the ratio of the height of the upper cone to the height of the lower cone in the first flow guide mechanism is between 1:3.5 and 1:5.5; And / or, The second flow guide mechanism is formed by two cones which are connected in abutment, and the vertexes of the two cones are respectively directed upward and downward; the ratio of the diameter of the bottom surface of the cone in the second flow guide mechanism to the maximum diameter of the cyclone unit is between 1:1.5 and 1:2.5; the ratio of the height of the upper cone to the height of the lower cone in the second flow guide mechanism is between 1:3.5 and 1:5.5; the lower part of the cyclone unit is tapered, and the side wall of the lower cone in the second flow guide mechanism is parallel to the side wall of the tapered lower part of the cyclone unit.

6. The reverse cyclonic particulate bed flue gas cleaning system of claim 1, wherein, At the horizontal position of the gas inlet, the cross-sectional area of the annular space between the outer side wall of the moving bed body and the inner side wall of the cyclone unit in the horizontal direction is greater than or equal to the inlet area of the gas inlet, and less than or equal to the gas-solid two-phase contact area of the gas-solid contact unit; the ratio of the diameter of the constant-diameter part of the moving bed body to the diameter of the minimum part of the cyclone unit is between 1:1.5 and 1:3; Wherein, the gas-solid two-phase contact area of the gas-solid contact unit should be less than or equal to the cross-sectional area of the constant-diameter part of the moving bed body in the horizontal direction.

7. The reverse cyclonic particulate bed flue gas cleaning system of claim 1, wherein, The superficial gas velocity in the moving bed body is between 0.05 m / s and 0.875 m / s; The designed bed layer thickness in the moving bed body is h, ， wherein η represents the efficiency, δ represents the filter factor, which is related to the Stokes number Stk relates to the Stokes number, ； ε0 represents the bed voidage, the Stokes number in the formula Stk In detail, as follows, u g U represents superficial gas velocity, unit: m / s; d p U represents average particle size of filter material, unit: m; p p U represents particle density of filter material, unit: kg / m 3 U represents dynamic viscosity coefficient, unit: N·s / m2; d s U represents average particle size of dust particles, unit: m.

8. The reverse cyclonic particulate bed flue gas cleaning system of claim 1, wherein, The diameter of the constant-diameter section of the cyclone shell and the cross section of the inlet of the elutriation cyclone separator satisfy the following relationship: k a = 1 2 / 4 b； wherein, k a the value range of the ratio of the height of the inlet to the height of the outlet is between 2 and 8; 1 represents the diameter of the constant diameter section of the cyclone housing; the inlet of the elutriation cyclone separator is rectangular, with height and width of a, b respectively; the height h of the cyclone housing and the diameter of the constant diameter section of the cyclone housing 1 satisfies the following relationship: h = h1 + h2 = 1; wherein h1 = 1 1 , h2 = ( - ) = 1; the value of X is in the range of 2 to 4; the value of X is in the range of 1.5 to 3; h1 represents the height of the constant-diameter section of the cyclone shell, and h2 represents the height of the tapered section of the cyclone shell. This indicates the relationship between the height h of the cyclone shell and the diameter of the constant diameter section of the cyclone shell. The ratio relationship between 1 and 1 This indicates the height and diameter of the constant-diameter section of the cyclone shell. The ratio relationship between 1 and 1; This indicates the height of the tapered section of the cyclone shell and the diameter of the constant-diameter section of the cyclone shell. The ratio relationship between 1 and 1; The cyclone exhaust pipe insertion depth h4 and the height of the inlet of the elutriation cyclone separator satisfy the following relationship: between them satisfies the following relationship: h4= a; wherein, the value of R is in the range of 0.4 to 0.8; The ratio of the height h5 of the blowback mechanism to the height h2 of the tapered section of the cyclone shell is between 1:4 and 1:6; the ratio of the gas velocity of the outlet of the blowback mechanism to the gas velocity of the inlet of the elutriation cyclone separator is between 1:10 and 1:15; the included angle γ between the center line of the blowback mechanism and the horizontal plane is between 65° and 85°; The ratio of the diameter D3 of the cyclone cylinder to the diameter D1 of the constant-diameter section of the cyclone shell is between 1:1.1 and 1:1.5; the ratio of the height h3 of the cyclone cylinder to the diameter D3 of the cyclone cylinder is between 2:1 and 4:1; the ratio of the diameter of the outlet of the cyclone cylinder to the diameter D3 of the cyclone cylinder is between 0.8:1 and 0.9:

1.

9. A method of purification using the reverse cyclonic particle bed flue gas cleaning system as claimed in claim 1, characterized in that, The purification method comprises: The treated flue gas is input to the gas inlet at the side wall of the cyclone unit, and the treated flue gas enters the cyclone unit and flows in a cyclone manner therein, under the action of inertial force, dust particles with a larger particle size are thrown to the side wall of the cyclone unit, and the treated flue gas carrying dust particles with a smaller particle size enters the gas-solid contact unit; The flue gas to be treated flows from bottom to top through the gas-solid contact unit into the moving bed body, the filter material particles flow from top to bottom from the storage bin into the moving bed body, and pass through the gas-solid contact unit into the cyclone unit, in the cyclone unit, the gas-solid contact unit and the moving bed body, the filter material particles contact with the flue gas to be treated to adsorb and filter the dust particles in the flue gas to be treated; The filter material particles adsorbing dust particles entering the cyclone unit are conveyed to the elutriation cyclone separator by the lifting mechanism; The flue gas filtered into the moving bed body is discharged from the gas outlet at the side wall of the moving bed body; The filter material particles adsorbing dust particles are separated by the elutriation cyclone separator under the action of cyclone inertia and gravity sedimentation, so that the filter material particles are discharged from the solid outlet at the lower part of the elutriation cyclone separator into the storage bin, and the dust particles are discharged from the cyclone exhaust pipe.

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