CN208244386U - Separator - Google Patents

Abstract

The utility model discloses a separation device, which comprises: a three-rotation shell, a separation structure monomer and a particle recycling mechanism, and the separation structure monomer is arranged inside the three-rotation shell, which includes: a coupled cyclone separator and The moving bed; the particle circulation regeneration mechanism includes from bottom to top: a riser, a spouted bed regenerator, and a regeneration inclined pipe connecting the spouted bed regenerator and the moving bed; the spouted bed regenerator has opposite upper and lower ends, wherein, The upper end of the spouted bed regenerator is provided with a sleeve with an opening downward. The sleeve divides the interior of the spouted bed regenerator into a fountain area and an annulus area. The side wall of the spouted bed regenerator is provided with a ring The regeneration gas outlet connected to the interstitial area. The utility model can simultaneously realize the centrifugal separation and the interception and filtration of the fine powder particles by the moving particle bed, so that the fine powder particles can be efficiently separated under low pressure drop, and the intercepted dust particles can be efficiently separated from the particle bed particles continuously. Ensures sustainable circulation of pellet bed pellets.

Description

separation device

technical field

The utility model relates to the technical field of petroleum refining and chemical equipment, in particular to a separation device for gas-solid separation in an energy recovery system of a catalytic cracking device.

Background technique

It is estimated that in an oil refinery catalytic cracking (FCC (Fluid Catalytic Cracking)) unit, the energy taken away by the flue gas at the outlet of the regenerator accounts for about 26% of the energy consumption of the whole unit. At present, in order to avoid the energy in the flue gas from being wasted, flue gas turbines are generally used to recover the energy in the flue gas. In addition, in order to ensure the long-term safe operation of the flue gas turbine, it is generally required to reduce the concentration of fine powder particles in the inlet gas of the flue gas turbine to below 200mg/ ^m3 , and to ensure that the particles above 10μm are basically removed. However, the flue gas at the outlet of the regenerator is a high-temperature dusty gas. The catalyst concentration in the flue gas (under standard conditions, the same below) is generally 300 to 1200 mg/m ³ , and the average particle size is 15 to 30 μm, which cannot meet the long-term requirements of the flue gas turbine. Safe operation requirements. In order to ensure the long-term safe operation of the hood of the FCC device, save energy and reduce consumption, and reduce the dust contained in the flue gas to cause air pollution, a third-stage cyclone separator (three-stage cyclone for short) is generally installed in the flue gas energy recovery system of the FCC device.

At present, the three-cyclone system generally uses a multi-tubular cyclone separator to purify the dusty flue gas. The so-called multi-tubular cyclone separator is to use a plurality of cyclone tubes with smaller diameters (generally less than 300mm in diameter), which are installed side by side in a pressure-bearing shell. According to the installation method of the cyclone tube, it can be divided into vertical multi-tube three-rotor and horizontal multi-tube three-rotor. For catalytic cracking units with small processing capacity, considering comprehensive factors such as manufacturing construction, application effect, and investment economy, vertical three-rotors are mostly used. For example, Chinese patents CN 2568308Y and CN 201304370Y both relate to a vertical multi-tube three-rotor. For catalytic cracking units with large processing capacity, due to the large number of single tubes, the diameter of the vertical three-rotor is too large, the partition is too thick and easy to deform, and the horizontal three-rotor is mostly used. For example, Chinese patents CN 2275907Y, CN 2526075Y and CN 201132137Y all relate to a horizontal multi-tube trirotary.

However, there are some problems in the application process of the multi-tube three-rotation. Especially with the enlargement of my country's FCC equipment, the increase of raw material slag mixing ratio, and the increase of regeneration temperature, etc., the operation of the equipment has become very unstable, and the main problems of the three-rotation system caused by this are as follows:

First: In order to achieve higher gas-solid separation efficiency, the diameter of the cyclone tube is generally designed to be small. Correspondingly, the gas volume processed by a single tube is small. In order to ensure the processing capacity, the number of single tubes can only be increased. Due to the large number of single tubes, the floor area and material costs of the three-rotation system increase accordingly; and the arrangement structure is complicated, which is inconvenient for installation and maintenance;

Second: Due to the excessive pursuit of single-tube efficiency, the linear velocity of the three-rotation single-tube inlet is too high, and the single-tube wears seriously. The dust increased, and the fouling near the three-rotation single-pipe dust outlet was serious, which affected the operation of the hood.

Third: Due to the high linear velocity of the single pipe inlet, the pressure drop of the three-spin is as high as 15-20kPa, which increases the system pressure drop and energy consumption.

The BSX-type three-rotor (patents CN 201006498Y and CN201205524Y) developed by China Petroleum and Chemical Corporation uses multiple large-diameter PV-type cyclone separators, suspended inside the three-rotor shell, and the diameter of the monomer is 800-1200 (1300 ) between mm. Compared with the multi-tube three-rotator, the BSX type three-rotor cancels the thicker double-layer partition and the small-diameter single tube with higher manufacturing precision requirements, and uses several large cyclones with simple structure, which reduces the manufacturing cost. , The difficulty of construction and installation, easy maintenance and replacement of three-rotation. In addition, since there is no problem of partition deformation and single-pipe blow-by gas backmixing, the overall efficiency of the equipment will not decrease after the combination of multiple cyclones, and the reliability is high and the adaptability is strong. However, the single-tube separation efficiency of the large-diameter cyclone in the BSX type triple cyclone is lower than that of the single tube in the multi-tube triple cyclone, and in order to achieve higher separation efficiency, the linear velocity of the BSX triple cyclone inlet has reached 32m/ s or more, the three-rotation system not only has a high pressure drop but also has obvious vibration during operation, which is very prominent in the wear of equipment and the crushing of catalysts.

At present, the dust concentration at the outlet of the three-rotation gas is generally around 150 mg/m ³ , and the corresponding pressure drop of the three-rotation system is between 15 and 20 kPa. The overall separation efficiency of the three-rotation system is not ideal, and the pressure drop is relatively high. room for improvement.

In order to improve the separation efficiency and reduce the pressure drop, a moving bed can be coupled in the separation system. A moving bed refers to a gas-solid two-phase flow system in which the particle velocity is between a fixed bed and a fluidized bed, and mainly includes three forms: countercurrent, cocurrent and crossflow. Because the moving bed has the advantages of high temperature resistance, simple structure, no rotating components, long operation period and continuous operation, it is widely used in particle drying, filtration, catalytic reforming and other processes. Because the particle bed has a good ability to filter and capture fine particles, and is suitable for high temperature and high pressure conditions, the moving bed has also been used in the field of gas purification in the past two decades.

For example, the Chinese patent (CN 2042374U) proposes an automatic moving bed filter for particulate matter, the granular bed adopts a louver structure to realize the continuous utilization of the bed particles. The feeding pipe at the bottom of the equipment adopts U-shaped pipe conveying structure, and adopts the method of pulse air flow to realize the conveying of particles.

The countercurrent moving bed granular layer dust collector (CN 1552503A and CN1552504A) developed by Guodian Thermal Engineering Research Institute is used for dust removal of gas flue gas under high temperature and high pressure. When in use, the countercurrent contact between coal gas flue gas and particles can achieve higher separation efficiency. However, due to the local fluidization of the bed and dust particles, the equipment has the problems of small processing gas volume, low operating flexibility, uneven distribution of particles and gas, and high pressure drop.

Shanxi Institute of Coal Chemistry, Chinese Academy of Sciences coupled a cross-flow granular bed with a surface filter plate (CN1236660A), which was used to improve the collection ability of the cross-flow granular bed for micron-sized particles, and use the flow of descending particles to limit the surface of the filter plate Filter cake formation, resulting in a stable operating pressure drop. However, due to the clogging of the filter plate and the formation of filter cake on the surface, the pressure drop of the equipment is high. In addition, using the scouring effect of freely descending particles to achieve the purpose of limiting the surface filter cake, the balance process is not easy to guarantee, and there are certain difficulties in actual implementation.

Other devices for coupling a bed of particles to a separator exist in the prior art. However, on the whole, the existing equipment is not ideal for the separation of dust particles and particle bed particles. During use, more dust particles will inevitably be mixed into the particle bed particles, which will affect the sustainable circulation of the subsequent particle bed. use.

Utility model content

The purpose of this utility model is to provide a separation device, which can overcome the defects of the prior art, and can realize centrifugal separation and the interception and filtration of fine powder particles by the moving particle bed at the same time, so that the fine powder particles can be separated with high efficiency under low pressure drop, and It can continuously and efficiently separate the intercepted dust particles from the particle bed particles to ensure the sustainable circulation of the particle bed particles.

Above-mentioned purpose of the utility model can adopt following technical scheme to realize:

A separation device, which includes: a three-rotation housing, a separation structure monomer and a particle recycling mechanism, wherein,

The separation structure unit is arranged inside the three-rotation shell, which includes: a coupled cyclone separator and a moving bed;

The particle circulation regeneration mechanism includes from bottom to top: a riser, a spouted bed regenerator, and a regeneration inclined pipe connecting the spouted bed regenerator and the moving bed; the spouted bed regenerator has an opposite upper end and the lower end, wherein, the upper end of the spouted bed regenerator is provided with a sleeve with an opening downward, and the sleeve divides the interior of the spouted bed regenerator into a fountain area and an annulus area, and the spouted bed regenerator The side wall of the bed regenerator is provided with a regenerating gas outlet communicating with the annulus.

In a preferred embodiment, the three-rotation housing includes a gas collection chamber, a dust collection chamber located at the lower part of the gas collection chamber, and a gas inlet pipe located in the three-rotation housing. A gas outlet is provided, and a particle outlet is provided on the dust collecting chamber;

The cyclone separator includes from top to bottom: a central exhaust pipe, a cylinder, a cone, an ash hopper, and a material leg, wherein the upper end opening of the central exhaust pipe communicates with the gas collection chamber, and the A gas inlet connected to the gas inlet pipe is provided on the cylinder wall of the cylinder; wherein, the lower end opening of the dipleg communicates with the dust collection chamber;

The moving bed includes, from top to bottom, a silo, a material sealing area, a cross-flow area, a moving bed material leg, and an inclined pipe to be produced.

In a preferred embodiment, the wall surface of the cross-flow zone adopts a Johnson mesh structure, and the mesh wire gap of the mesh structure is between 0.25 mm and 0.75 mm.

In a preferred embodiment, the number of the separation structural units is 3 to 20, and the plurality of separation structural units are center-symmetrical and uniformly distributed along the circumference with the gas inlet pipe as the axis.

In a preferred embodiment, the cyclone separator adopts a cut-flow reverse structure with a diameter of less than 1.5 meters, and the gas inlet provided on the cylinder is a volute gas inlet.

In a preferred embodiment, the sleeve is a cylindrical barrel with an open lower end, and the superficial gas velocity in the annulus region is equal to the superficial gas velocity in the sleeve.

In a preferred embodiment, the riser includes a pre-lift section and a riser section from bottom to top, the diameter of the pre-lift section is larger than the diameter of the riser section, and the pre-lift section is provided with The bottom opening where the inclined pipes to be produced are connected; the upper end outlet of the riser section is located in the spouted bed regenerator and is located at the lower end of the sleeve at a predetermined distance;

The riser is located in the three-rotation housing or the riser is located outside the three-rotation housing.

In a preferred embodiment, an air stripping loop is further provided in the annular gap between the riser section and the silo, and at least one injection hole and a plurality of air holes are provided on the air stripping loop.

In a preferred embodiment, the superficial gas velocity of the section where the stripping loop is located is 0.5 to 0.8 times the initial fluidization velocity of the particles in the moving bed; the diameter of the stripping loop is the The average value of the diameters of the riser section and the spouted bed regenerator, the distance from the stripping ring pipe to the upper outlet of the riser section is 3 times the diameter of the riser.

In a preferred embodiment, a pre-screening structure is provided at the inclined pipe to be produced or at the position downstream of the inclined pipe to be produced.

The characteristics and advantages of the present utility model are: a separation device is provided in the embodiment of the application, a moving bed interlayer is arranged inside the larger diameter cyclone separator monomer of the catalytic cracking third-stage separation system, and the cyclone separator and the particle bed The filter is organically coupled to realize the synergistic enhancement of the gas-solid separation effect of cyclone separation and filtration separation, which can control the dust concentration of the outlet gas of the triple cyclone system within 50mg/ ^m3 , and reduce the pressure drop of the triple cyclone system to 5~ 10kPa.

The single cyclone separator with a larger diameter can reduce the number of single cyclone separators in the three-cyclone system, and reduce the difficulty of installation and maintenance; it can also reduce the inlet line speed while ensuring the processing capacity, effectively reducing the pressure of the cyclone separator. and equipment wear and tear. By setting the moving bed, the problem of efficiency drop caused by the decrease of the inlet linear velocity can be avoided, so as to ensure the effective separation efficiency of the triple-rotation system. The cross-flow area of the moving bed adopts Johnson mesh structure as the wall surface, and the gap between the mesh wires is between 0.25 and 0.75mm. The gas flow area is large and the flow resistance is small. The moving bed has a simple structure, no rotating parts, and a long operating period. The organic coupling of the two can effectively reduce the footprint of the equipment and make the device more compact.

In particular, the separation device provided by the present application is equipped with a corresponding particle circulation regeneration mechanism as required, wherein the particle circulation regeneration mechanism includes from bottom to top: a riser, a spouted bed regenerator, a spouted bed regeneration The regenerating inclined tube of the device and the moving bed; the spouted bed regenerator has opposite upper and lower ends, wherein, the upper end of the spouted bed regenerator is provided with a sleeve with an opening downward, and the sleeve will The interior of the spouted bed regenerator is divided into a fountain area and an annulus area, and the side wall of the spouted bed regenerator is provided with a regeneration gas outlet communicating with the annulus area, and the gas is ejected from the riser Finally, the dust particles can be efficiently separated from the particle bed particles through the spouted bed regenerator, thereby realizing the recycling of the moving bed particles.

On the whole, the separation device provided by this application can reduce the overall pressure drop of the three-rotation system, improve the separation efficiency of the system, reduce the concentration of exhausted flue gas dust, and improve the energy efficiency and environmental protection level of the device.

With reference to the following description and accompanying drawings, specific embodiments of the present application are disclosed in detail, indicating the manner in which the principles of the application may be employed. It should be understood that the embodiments of the present application are not limited thereby in scope. Embodiments of the present application encompass many changes, modifications and equivalents within the spirit and scope of the appended claims.

Features described and/or illustrated with respect to one embodiment can be used in the same or similar manner in one or more other embodiments, in combination with, or instead of features in other embodiments .

It should be emphasized that the term "comprising/comprising" when used herein refers to the presence of a feature, integer, step or component, but does not exclude the presence or addition of one or more other features, integers, steps or components.

Description of drawings

Fig. 1 is a schematic structural view of a separation device in the first embodiment of the present application;

Fig. 2 is the A-A sectional view of a kind of separating device in the first embodiment of the present application;

Fig. 3 is a partial schematic diagram of a particle circulation system in a separation device in the first embodiment of the present application;

Fig. 4 is a B-B cross-sectional view of a particle circulation system in a separation device in the first embodiment of the application;

Fig. 5 is a schematic structural view of a separation device in the second embodiment of the present application;

Fig. 6 is a schematic structural diagram of a separation device in the third embodiment of the present application.

Explanation of reference signs:

100. Three-rotation shell;

101. Gas inlet pipe; 102. Gas collection chamber; 103. Gas outlet; 104. Dust collection chamber; 105. Particle outlet;

200. Separation of structural monomers;

210. Cyclone separator;

211, gas inlet; 212, cylinder; 213, cone; 214, ash hopper; 215, material leg; 216, central exhaust pipe;

220. Moving bed;

221. Feed bin; 222. Material sealing area; 223. Cross-flow area; 224. Moving bed material leg; 225. Inclined pipe to be produced; 226. Particle collection bin; 227. Pre-screening structure;

300. Particle recycling system;

301. Pre-lift section; 302. Riser section; 303. Spouted bed regenerator; 304. Regeneration gas outlet; 305. Regeneration inclined tube; 306. Sleeve; , support frame; 310, air hole; 311 injection hole.

Detailed ways

The technical scheme of the utility model will be described in detail below in conjunction with the accompanying drawings and specific embodiments. It should be understood that these embodiments are only used to illustrate the utility model and are not intended to limit the scope of the utility model. After reading the utility model, Modifications to various equivalent forms of the present utility model by those skilled in the art all fall within the scope defined by the appended claims of the present application.

It should be noted that when an element is referred to as being “disposed on” another element, it may be directly on the other element or there may also 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 intervening elements may also be present. As used herein, the terms "vertical", "horizontal", "upper", "lower", "left", "right" and similar expressions are for the purpose of illustration only and are not intended to represent the only embodiment.

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

The utility model provides a separation device, which can overcome the defects of the prior art, and can realize centrifugal separation and interception and filtration of fine powder particles by a moving particle bed at the same time, so that fine powder particles can be separated with high efficiency under low pressure drop, and can continuously Efficiently separating the intercepted dust particles from the particle bed particles to ensure the sustainable circulation of the particle bed particles has better practical application prospects.

Specifically, this application mainly couples the moving bed structure inside the large-diameter cyclone separator of the third-stage separation system of catalytic cracking, which can reduce the pressure drop of the three-cyclone system and improve the gas-solid separation effect, and at the same time separate the dust particles from the particle bed particles Realize high-efficiency separation, and better ensure the sustainable recycling of particle bed particles.

Please refer to FIG. 1 to FIG. 4 , a separation device provided in an embodiment of the present application may include: a three-rotation housing 100 , a separation structure unit 200 and a particle recycling mechanism 300 . Wherein, the separation structure unit 200 is arranged inside the three-rotation housing 100, which includes: a coupled cyclone separator 210 and a moving bed 220; the particle recycling mechanism 300 includes from bottom to top: Pipe, spouted bed regenerator 303, regeneration inclined pipe 305 connecting said spouted bed regenerator 303 and said moving bed 220; said spouted bed regenerator 303 has opposite upper end and lower end, wherein said spouted bed regenerator The upper end of the moving bed regenerator 303 is provided with a sleeve 306 with an opening downward, and the sleeve 306 divides the interior of the spouted bed regenerator 303 into a fountain area and an annulus area 307. The spouted bed regenerator A regeneration gas outlet 304 communicating with the annulus 307 is provided on the side wall of 303 .

In this embodiment, the three-rotation housing 100 includes a gas collection chamber 102, a dust collection chamber 104 located at the lower part of the gas collection chamber 102, and a gas inlet pipe 101 located in the three-rotation housing 100, so The gas collection chamber 102 is provided with a gas outlet 103 , and the dust collection chamber 104 is provided with a particle outlet 105 . The cyclone separator 210 comprises from top to bottom: a central exhaust pipe 216, a cylindrical body 212, a cone 213, an ash hopper 214, and a material leg 215, wherein the upper end opening of the central exhaust pipe 216 is connected to the collector The air chamber 102 is connected, the cylinder wall of the cylinder 212 is provided with a gas inlet 211 connected with the gas inlet pipe 101 , and the lower opening of the dipleg 215 is connected with the dust collection chamber 104 . The moving bed 220 includes, from top to bottom, a silo 221 , a sealing area 222 , a cross-flow area 223 , a material leg 224 of the moving bed, and an inclined pipe 225 for raw materials. The coupling between the cyclone separator 210 and the moving bed 220 mainly means that the two can achieve a synergistic separation effect on the substances to be separated entering from the gas inlet pipe 101 through mutual cooperation.

Wherein, the wall surface of the cross-flow area 223 adopts a Johnson mesh structure, and the mesh wire gap of the mesh structure is between 0.25 mm and 0.75 mm. When the wall surface of the cross-flow area 223 of the moving bed 220 adopts a Johnson mesh structure, the gap between the mesh wires is between 0.25 and 0.75 mm, which can provide a larger gas flow area, thereby reducing the flow resistance when the gas cross-flow passes through.

Wherein, the number of the separation structural units 200 may be 3 to 20, and a plurality of the separation structural units 200 are centrally symmetrical with the gas inlet pipe 101 as the axis and evenly distributed along the circumference.

The cyclone separator 210 adopts a cut-flow reverse structure with a diameter of less than 1.5m, and the gas inlet 211 provided on the cylinder 212 is a volute gas inlet. The cyclone separator 210 with a larger diameter is selected for the three-cyclone system, which can reduce the number of cyclone separators 210 in the three-cyclone system, reduce the difficulty of installation and maintenance, and effectively reduce the pressure drop of the cyclone separator 210 and equipment wear.

In one embodiment, the riser is located in the three-rotation housing 100, the moving bed 220 adopts a sleeve-type interlayer structure, coaxial with the cyclone separator 210, and the inner wall of the interlayer is in contact with the central exhaust pipe of the cyclone separator 210. The walls of 216 overlap, and the thickness of the interlayer is between 0.05 and 0.3 times the diameter of the cyclone separator 210 . When the dust-laden flue gas enters the cyclone separator 210 tangentially, under the action of centrifugal force, the catalyst particles with larger particle size are separated first; and the moving bed 220 will trap the cyclone separator 210 which cannot be separated, or which requires extremely high Small-sized catalyst particles that can only be separated under gas velocity conditions, thereby further enhancing the effect of gas-solid separation.

Referring to Fig. 3 and Fig. 4, in this embodiment, a sleeve 306 with an opening downward is arranged on the top of the spouted bed regenerator 303, and the sleeve 306 divides the spouted bed regenerator 303 into : Fountain area and annulus area 307. Specifically, the sleeve 306 may be a cylindrical barrel with an open lower end, and its diameter D _s is determined by the superficial gas velocity u _g of the gas at the outlet of the riser section in the sleeve 306 .

Among them, the superficial gas velocity is a kind of superficial velocity, which generally refers to the plate tower or packed tower used in rectification, absorption and other operations. When calculating the gas velocity through the fluidized bed, the gas velocity in the bed is not considered Components, the average flow rate of gas passing through the tower is calculated according to the empty tower, and the value obtained by dividing the gas flow by the total cross-sectional area of the bed. The superficial velocity can be: the flow Q passing through the area per unit time divided by the cross-sectional area A of the area.

Wherein, the superficial gas velocity in the riser section 302 is generally taken as 1.3 u _t , where u _t is the drag-out velocity of bed particles in the moving bed. The superficial gas velocity u _g of the gas in the sleeve 306 should be less than the u _mf (i.e. the initial fluidization velocity) of the particles in the moving bed 220 bed, but greater than the drag-out velocity of the separated dust. Generally, the superficial gas velocity is taken as 0.5 ~0.8 times the initial fluidization velocity of moving bed particles. Since the ejected gas volume Q and the superficial gas velocity _ug of the sleeve 306 are known, the cross-sectional area of the fountain area can be determined according to the above known quantities, so as to determine the diameter D _s of the sleeve 306 . The height H _s of the sleeve 306 is greater than the ejection height of the bed particles.

The spray height at the outlet of the riser section 302 can be calculated by an empirical formula, and the ratio of its diameter D _s to the sleeve 306 can also be controlled between 0.5 and 10. The distance H _i between the outlet of the riser section 302 and the sleeve 306 is mainly determined based on the principle that the sleeve 306 can completely cover the sprayed-up bed particles, so that the bed particles and dust are fully separated in the sleeve 306 .

The diameter D of the annulus is determined by the superficial gas velocity of the section of the annulus 307 . When the diameter of the annulus 307 is D, the cross-sectional area of the corresponding annulus 307 is: The superficial gas velocity in the annulus region 307 is smaller than the initial fluidization velocity of the bed particles of the moving bed 220 and greater than the drag-out velocity of the dust particles. Generally, it is guaranteed that the superficial gas velocity in the annular gap area 307 (section) is equal to the superficial gas velocity in the sleeve 306. On the premise that the flow rate Q is known, the superficial gas velocity in the annular gap area 307 can be determined, and then the annular gap area 307 can be determined. diameter D.

In order to promote the further separation of bed particles and dust in the moving bed 220, an air stripping ring pipe 308 is arranged at the middle and lower part of the spouted bed regenerator 303 (i.e. the bin 221), at a distance from the outlet Hst (i.e. 3D _r ) of the riser section 301 . At least one injection hole 311 and a plurality of air holes 310 are provided on the stripping loop pipe 308 . After being separated by the fountain area and the annulus area 307, there may still be a small amount of small particle dust doped in the bed particles. After passing through the stripping ring pipe 308, the stripping gas is injected through the injection hole 311, And sprayed from the plurality of air holes 310, the bed particles doped with a small amount of dust can be further purified and separated, so as to ensure that there is basically no dust in the bed particles entering the silo 221 .

Specifically, the diameter of the stripping loop pipe 308 is (D+D _r )/2. The stripping loop 308 can be supported by a support frame 309 welded on the wall of the spouted bed regenerator 303 . Specifically, there may be 6 pairs of the support frames 309 . 6 secondary support frames 309 may be evenly distributed along the circumference of the spouted bed regenerator 303 .

The air stripping ring pipe 308 adopts a plurality of air holes 310 on the bottom surface to prevent the air holes 310 from being blocked by particles. A plurality of air holes 310 are uniformly distributed along the circumference of the annular tube. Specifically, the number of air holes 310 can be determined according to actual needs, for example, it can be 24. Of course, the number of air holes 310 can be more or less, and the present application does not make a unique limitation here.

Wherein, the gas volume of the stripping ring pipe 308 passes through the section where the ring pipe is controlled (cross-sectional area ) to determine the corresponding superficial gas velocity. Control the superficial gas velocity of the section where the stripping loop pipe 308 is located at 0.5 to 0.8 times the initial fluidization velocity of the bed particles of the moving bed 220 to ensure that the dust is completely carried out, and the bed particles of the moving bed 220 can fall freely.

The depth at which the riser section 302 penetrates into the spouted bed regenerator 303 can be determined according to the number of bed particles in the moving bed 220 that needs to be stored in the bin 221 of the spouted bed regenerator 303 in practical applications. For example, the spouted bed regenerator 303 is a cylindrical structure with a diameter D, and stores the number of bed particles of the moving bed 220 as required. In addition, the height and diameter of the feed bin 221 can also be increased or expanded, and the specific height and diameter of the feed bin 221 can be determined according to actual needs.

The separation device provided by this application is provided with a moving bed interlayer inside the larger diameter cyclone separator 210 of the catalytic cracking third-stage separation system, and the cyclone separator 210 is organically coupled with the moving bed 220 to realize the pairing of cyclone separation and filtration separation. The synergistic strengthening of the gas-solid separation can control the dust concentration of the outlet gas of the triple-rotation system within 50mg/m ³ and control the pressure drop of the triple-rotation system within 5-10kPa.

The single cyclone separator 210 with a larger diameter can reduce the number of cyclone separators 210 in the three-cyclone system and reduce the difficulty of installation and maintenance; it can also reduce the inlet line speed while ensuring the processing capacity, effectively reducing the cyclone separator 210. Pressure drop and equipment wear. By setting the moving bed 220, the efficiency drop problem caused by the decrease of the inlet linear velocity can be avoided, thereby ensuring the effective separation efficiency of the triple-rotation system. The cross-flow area 223 of the moving bed 220 adopts a Johnson network structure as the wall surface, and the gap between the network cables is between 0.25 mm and 0.75 mm, so that the gas circulation area is large and the circulation resistance is small. The moving bed 220 has a simple structure, no rotating parts, and a long operation period. The organic coupling between the cyclone separator 210 and the moving bed 220 can effectively reduce the footprint of the equipment and make the device more compact.

In particular, the separation device provided by the present application is equipped with a corresponding particle circulation regeneration mechanism 300 according to needs, wherein, the particle circulation regeneration mechanism 300 includes from bottom to top: a riser, a spouted bed regenerator 303, a The movable bed regenerator 303 and the regeneration inclined pipe 225 of the moving bed 220; the spouted bed regenerator 303 has opposite upper and lower ends, wherein the upper end of the spouted bed regenerator 303 is provided with a downward opening A sleeve 306, the sleeve 306 divides the interior of the spouted bed regenerator 303 into a fountain area and an annulus area 307, and the side wall of the spouted bed regenerator 303 is provided with a 307 is connected to the regeneration gas outlet 304. After the gas is ejected from the riser, the dust particles can be efficiently separated from the particle bed particles through the spouted bed regenerator 303, thereby realizing the recycling of the moving bed particles.

On the whole, the separation device provided by this application can reduce the overall pressure drop of the three-rotation system, improve the separation efficiency of the system, reduce the concentration of exhausted flue gas dust, and improve the energy efficiency and environmental protection level of the device.

In addition, a corresponding particle recycling mechanism 300 can be configured as required to realize recycling of the moving bed 220 particles. The structure of the device can be set in at least three different forms: a built-in particle regeneration system, an external particle regeneration system, and a pre-screening structure in the inclined tube for particle waiting and the particle collection bin, respectively, corresponding to the following of three implementations. The following describes in detail in conjunction with specific implementation methods and accompanying drawings.

Fig. 1 is a schematic structural diagram of the separation device in the first embodiment of the present application, specifically, a schematic structural diagram of the FCC third-stage separation system with a built-in particle recycling mechanism. FIG. 2 is a schematic plan view of the arrangement of the separation structural units in the three-rotation housing 100 in the first embodiment of the present application. The arrangement of the separation structural units in the three-rotation housing 100 in other embodiments is the same.

The separation device may include a three-rotation housing 100 , a separation structure unit 200 and a particle recycling mechanism 300 . The particle recycling mechanism 300 is specifically a built-in particle recycling mechanism.

Wherein, a gas inlet pipe 101 , a gas collection chamber 102 and a gas outlet 103 are arranged on the upper part of the three-rotation housing 100 , and a dust collection chamber 104 and a particle outlet 105 are arranged on the lower part.

The separation structure unit 200 can be formed by coupling a cyclone separator 210 and a moving bed 220 , which are suspended inside the three-rotation shell 100 . The number of separation structural monomers 200 can be set to n according to the processing gas volume, where 3≤n≤20. A plurality of separation structural units 200 are centrally symmetrical and uniformly distributed along the circumference with the gas inlet pipe 101 as the axis, as shown in FIG. 2 .

The cyclone separator 210 may include: a volute gas inlet 211 , a cylinder 212 , a cone 213 , an ash hopper 214 , a dipleg 215 and a central exhaust pipe 216 .

The moving bed 220 may include a silo 221 , a material seal area 222 , a cross-flow area 223 , a moving bed material leg 224 , and an inclined pipe 225 for raw materials from top to bottom.

In this embodiment, the particle circulation regeneration mechanism 300 can adopt the combined structure of the riser and the spouted bed to carry out the cycle regeneration process of the moving bed particles. 303 , regeneration gas outlet 304 and regeneration inclined pipe 305 . The riser section 302 is arranged inside the three-rotation shell 100. The riser section 302 passes through the central axis of the gas inlet pipe 101 and is connected to the spouted bed regenerator 303 arranged on the upper part of the three-rotation shell 100. The bottom of the spouted bed regenerator 303 is It communicates with the feed bin 221 of the moving bed through the regeneration inclined pipe 305 .

The working process of the separation device provided by this embodiment is as follows.

Firstly, the flue gas uniformly enters into each separation component unit 200 from the gas inlet pipe 101 on the upper part of the three-rotation housing 100 (the following description takes one separation unit unit 200 as an example). Then the flue gas enters tangentially along the volute inlet 211 of the cyclone separator 210 , forming a swirl flow inside the cylinder body 212 and the cone body 213 . During the rotation and downward movement of the main flue gas flow, part of the gas gradually radially passes through the cross-flow region 223 of the moving bed 220 , collects in the central exhaust pipe 216 and then enters the gas collection chamber 102 on the upper part of the tri-rotary housing 100 . At the same time, the catalyst particles contained in the flue gas are thrown towards the side wall of the cyclone separator 210 under the action of centrifugal force, slide down to the ash hopper 214 along the cylinder body 212 and the cone body 213, and then are discharged to the tri-rotary shell through the material leg 215 The dust collection chamber 104 at the bottom of the body 100 plays the role of cyclone separation of gas and solid.

Along the lower end of the central exhaust pipe 216 of the cyclone separator 210, a moving bed 220 coaxial with the cylinder body 212 and the cone body 213 of the cyclone separator is arranged. The moving bed particles naturally flow down from the silo 221 arranged outside the three-rotation shell 100 under the action of gravity, and flow through the material sealing area 222 and the cross-flow area 223 of each moving bed 220 located inside the cyclone separator 210 . During the rotation and downward movement of the main flue gas flow, part of the gas gradually radially passes through the cross-flow region 223 of the moving bed 220 . The wall surface of the cross-flow area 223 is a network structure. Specifically, the wall surface of the cross-flow area 223 may adopt a Johnson mesh structure, so that the flue gas and the particles are in cross-flow contact to complete the filtration and separation process.

For tiny catalyst particles that cannot be separated by the cyclone separator 210 or need to be separated at a very high gas velocity, the moving bed 220 can play the role of interception and filtration, thereby effectively improving the gas-solid separation efficiency. The purified flue gas is discharged through the central exhaust pipe 216 of the cyclone separator 210 to the gas collection chamber 102 on the upper part of the three-rotation housing 100 , and then discharged through the gas outlet 103 . The moving bed particles and the captured catalyst particles are transported to the pre-lift section 301 through the moving bed material leg 224 and the inclined pipe 225, and are transported to the upper part of the three-rotation shell 100 along the riser section 302 under the action of the lifting gas. Bed regenerator 303.

The moving bed particles enter the spouted bed regenerator 303 provided with a sleeve 306 under the action of spouted air separation, and are separated from the trapped catalyst particles to realize regeneration. Specifically, the moving bed particles with larger particle size settle under the action of gravity, while the catalyst particles with smaller particle size flow out of the particle circulation regeneration mechanism 300 through the regeneration gas outlet 304 on the upper part of the spouted bed regenerator 303 following the regeneration gas. The regenerated moving bed particles are transported to the bin 221 of the moving bed 220 through the regeneration inclined pipe 305 to complete the entire particle regeneration cycle.

Referring to Fig. 3 and Fig. 4, in this embodiment, a sleeve 306 with an opening downward is arranged on the top of the spouted bed regenerator 303, and the sleeve 306 divides the spouted bed regenerator 303 into : Fountain area and annulus area 307. Specifically, the sleeve 306 may be a cylindrical barrel with an open lower end, and its diameter D _s is determined by the superficial gas velocity _ug of the gas at the outlet of the riser section 302 in the sleeve 306 .

Among them, the superficial gas velocity is a kind of superficial velocity, which generally refers to the plate tower or packed tower used in rectification, absorption and other operations. When calculating the gas velocity through the fluidized bed, the gas velocity in the bed is not considered Components, the average flow rate of gas passing through the tower is calculated according to the empty tower, and the value obtained by dividing the gas flow by the total cross-sectional area of the bed. The superficial velocity can be: the flow Q passing through the area per unit time divided by the cross-sectional area A of the area.

Wherein, the superficial gas velocity in the riser section 302 is generally taken as 1.3 u _t (u _t is the drag-out velocity of bed particles in the moving bed). The superficial gas velocity u _g of the gas in the sleeve 306 should be less than the u _mf of the bed particles of the moving bed 220 (that is, the initial fluidization velocity), but greater than the take-out velocity of the separated dust. The diameter D _s of the sleeve 306 is determined according to the superficial gas velocity u _g inside the sleeve 306 . The height H _s of the sleeve 306 is greater than the ejection height of the bed particles.

The injection height at the outlet of the riser section 302 can be calculated by an empirical formula, or it can also be obtained by controlling the ratio of its diameter D _s to the sleeve 306 (between 0.5 and 10). The distance H _i between the outlet of the riser section 302 and the sleeve 306 is mainly determined based on the principle that the sleeve 306 can completely cover the sprayed-up bed particles, so that the bed particles and dust are fully separated in the sleeve 306 .

The diameter D of the annulus 307 is determined by the superficial gas velocity of the section of the annulus. When the diameter of the annulus 307 is D, the cross-sectional area of the corresponding annulus 307 is: The superficial gas velocity of the cross-section in the annulus area 307 is smaller than the initial fluidization velocity of the bed particles of the moving bed 220, and greater than the drag-out velocity of the dust particles. Generally, it is ensured that the superficial gas velocity of the cross section of the annular gap area 307 is equal to the superficial gas velocity of the sleeve 306, so that the diameter D of the annular gap area 307 is determined.

In order to promote the complete separation of particles and dust in the bed layer of the moving bed 220, an air stripping ring pipe is arranged at the middle and lower part of the spouted bed regenerator 303 (i.e., the position of the bin 221), at a distance from the outlet H _st (i.e. 3D _r ) of the riser section 301 308. The diameter of the stripping loop 308 is (D+D _r )/2. The stripping loop 308 can be supported by a support frame 309 welded on the wall of the spouted bed regenerator 303 .

Specifically, there may be 6 pairs of the support frames 309 . 6 secondary support frames 309 may be evenly distributed along the circumference of the spouted bed regenerator 303 . The air stripping ring pipe 308 adopts air holes 310 on the bottom surface to prevent the air holes 310 from being blocked by particles. The air holes 310 are evenly distributed along the circumference of the ring pipe. Specifically, the number of air holes 310 can be determined according to actual needs, for example, it can be 24. Of course, the number of air holes 310 can be more or less, and the present application does not make a unique limitation here.

Wherein, the gas volume of the stripping ring pipe 308 passes through the section where the ring pipe is controlled (cross-sectional area ) to determine the corresponding superficial gas velocity. Control the superficial gas velocity of the section where the stripping loop pipe 308 is located at 0.5 to 0.8 times the initial fluidization velocity of the bed particles of the moving bed 220 to ensure that the dust is completely carried out, and the bed particles of the moving bed 220 can fall freely.

The depth at which the riser section 302 penetrates into the spouted bed regenerator 303 can be determined according to the number of bed particles in the moving bed 220 that needs to be stored in the bin 221 of the spouted bed regenerator 303 in practical applications. For example, the spouted bed regenerator 303 is a cylindrical structure with a diameter D, and stores the number of bed particles of the moving bed 220 as required. In addition, the height and diameter of the feed bin 221 can also be increased or expanded, and the specific height and diameter of the feed bin 221 can be determined according to actual needs.

Fig. 5 is a schematic diagram of the mechanism of the separation device in the second embodiment of the present application, specifically, a schematic structural diagram of the FCC third-stage separation system with an external particle recycling mechanism.

The separation device may include a three-rotation housing 100 , a separation structure unit 200 and a particle recycling mechanism 300 . The particle recycling mechanism 300 is specifically an external particle recycling mechanism.

Wherein, a gas inlet pipe 101 , a gas collection chamber 102 and a gas outlet 103 are arranged on the upper part of the three-rotation housing, and a dust collection chamber 104 and a particle outlet 105 are arranged on the lower part.

The separation structure unit 200 is composed of a cyclone separator 210 coupled with a built-in moving bed 220 , which is suspended inside the three-rotation shell 100 . The number of separation structural monomers 200 can be set to n according to the processing gas volume, where 3≤n≤20. A plurality of separation structural units 200 are symmetrical about the center and uniformly distributed along the circumference with the gas inlet pipe 101 as the axis.

The cyclone separator 210 includes a volute gas inlet 211 , a barrel 212 , a cone 213 , an ash hopper 214 , a dipleg 215 and a central exhaust pipe 216 .

The moving bed 220 includes, from top to bottom, a feed bin 221 , a material sealing area 222 , a cross-flow area 223 , a moving bed material leg 224 , an inclined pipe 225 to be produced, and a particle collection bin 226 .

In this embodiment, the particle circulation regeneration mechanism 300 can adopt the combined structure of the riser and the spouted bed to carry out the regeneration cycle process of the moving bed particles. , the regeneration gas outlet 304 and the regeneration inclined pipe 305. The riser section 302 is arranged outside the three-rotation shell 100, and the riser section 302 is connected with the spouted bed regenerator 303 arranged outside the three-rotation shell 100. The warehouse 221 is connected.

The working process of the separation device provided by this embodiment is as follows.

Firstly, the flue gas uniformly enters each separation structural unit 200 from the gas inlet pipe 101 on the upper part of the three-rotation housing 100 (the following description takes one separation structural unit 200 as an example). Then the flue gas enters tangentially along the volute inlet 211 of the cyclone separator 210 , forming a swirl flow inside the cylinder 212 and the cone 213 . During the rotation and downward movement of the main flue gas flow, part of the gas gradually radially passes through the cross-flow area 223 of the built-in moving bed 220, gathers in the central exhaust pipe 216, and then enters the gas collection chamber 102 on the upper part of the tri-rotary housing 100 . At the same time, the catalyst particles contained in the flue gas are thrown towards the side wall of the cyclone separator 210 under the action of centrifugal force, slide down along the cylinder body 212 and the cone body 213 to the ash hopper 214, and are discharged to the tri-rotary shell through the material leg 215 The dust collection chamber 104 at the bottom of the body 100 plays the role of cyclone separation of gas and solid.

Along the central exhaust pipe 216 of the cyclone separator 210 is disposed a moving bed 220 coaxial with the cyclone separator barrel 212 and cone 213 . The moving bed particles naturally flow down from the silo 221 outside the three-rotation housing 100 under the action of gravity, and flow through the sealing area 222 and the cross-flow area 223 of each moving bed 220 inside the cyclone separator 210 respectively. During the rotation and downward movement of the main flue gas flow, part of the gas gradually radially passes through the cross-flow region 223 of the moving bed 220 . The wall surface of the cross-flow area 223 is a network structure. Specifically, the wall surface of the cross-flow area 223 may adopt a Johnson mesh structure, so that the flue gas and the particles are in cross-flow contact to complete the filtration and separation process.

For tiny catalyst particles that cannot be separated by the cyclone separator 210 or need to be separated at a very high gas velocity, the moving bed 220 can play the role of interception and filtration, thereby effectively improving the gas-solid separation efficiency. The purified flue gas is discharged through the central exhaust pipe 216 of the cyclone separator 210 into the gas collection chamber 102 on the upper part of the three-rotation housing 100 , and then discharged through the gas outlet 103 . The moving bed particles and the captured catalyst particles are transported to the pre-lift section 301 through the moving bed material leg 224 and the inclined pipe 225, and are transported to the upper spouted bed regenerator 303 along the riser section 302 under the action of the lifting gas .

The moving bed particles enter the spouted bed regenerator 303 provided with a sleeve 306 under the action of spouted air separation, and are separated from the trapped catalyst particles to realize regeneration. Specifically, the larger moving bed particles settle under the action of gravity, while the trapped catalyst particles follow the regeneration gas and flow out of the particle circulation regeneration mechanism through the regeneration gas outlet 304 on the upper part of the spouted bed regenerator 303 . The regenerated moving bed particles are transported to the bin 221 of the moving bed 220 through the regeneration inclined pipe 305 to complete the entire particle regeneration cycle.

Fig. 6 is a schematic structural view of the separation device in the third embodiment of the present application, specifically, a schematic structural view of the third-stage separation system of the FCC particle recycling mechanism provided with a pre-screening structure.

In this embodiment, on the basis of the structure of the first embodiment or the second embodiment, a pre-screening structure 227 is set in the equipment's standby inclined pipe 225 and particle collection bin 226, so as to realize the collection of catalyst particles. The particles in the moving bed are pre-separated to reduce the load of the subsequent particle circulation regeneration mechanism 300 .

Wherein, the pre-screening structure 227 refers to adopting a net-like structure as the lower wall at parts such as the inclined pipe 225 and the particle collection bin 226 where the particles flow. Specifically, the mesh structure may be a mesh screening structure such as a Johnson mesh. The above-mentioned pre-screening structure 227 can pre-screen the moving bed particles trapped in the catalyst. During the working process, when the moving bed particles flow from the moving bed material leg 215 through the standby inclined pipe 225 and the particle collection bin 226, the pre-screening structure can screen out part of the catalyst particles captured by the moving bed in advance, thereby reducing the subsequent The regeneration load of the particle recycling mechanism 300 .

Any numerical value cited herein includes all values from the lower value to the upper value in increments of one unit for the lower and upper values, with a separation of at least two units between any lower value and any higher value That's it. For example, if it is stated that a component quantity or process variable (such as temperature, pressure, time, etc.) has a value from 1 to 90, preferably from 20 to 80, more preferably from 30 to 70, the purpose Values such as 15 to 85, 22 to 68, 43 to 51, 30 to 32, etc. are also explicitly listed in the specification. For values less than 1, one unit is considered to be 0.0001, 0.001, 0.01, 0.1, as appropriate. These are merely examples intended to be expressly stated, and it is considered that all possible combinations of numerical values recited between the lowest value and the highest value are expressly set forth in this specification in a similar manner.

Unless otherwise indicated, all ranges include the endpoints and all numbers between the endpoints. "About" or "approximately" used with a range applies to both endpoints of the range. Thus, "about 20 to 30" is intended to cover "about 20 to about 30", inclusive of at least the indicated endpoints.

All articles and references disclosed, including patent applications and publications, are hereby incorporated by reference for all purposes. The term "consisting essentially of" describing a combination shall include the identified elements, ingredients, parts or steps as well as other elements, ingredients, parts or steps that do not substantially affect the basic novel characteristics of the combination. Use of the terms "comprising" or "comprising" to describe a combination of elements, ingredients, parts or steps herein also contemplates an embodiment that consists essentially of these elements, ingredients, parts or steps. By using the term "may" herein, it is intended that inclusion of "may" in any of the described attributes is optional.

Multiple elements, ingredients, parts or steps can be provided by a single integrated element, ingredient, part or step. Alternatively, a single integrated element, ingredient, part or step may be divided into separate plural elements, ingredients, parts or steps. The disclosure of "a" or "an" to describe an element, ingredient, component or step is not meant to exclude other elements, ingredients, components or steps.

The above-mentioned implementations in this specification are described in a progressive manner, the same and similar parts of the implementations may be referred to each other, and each implementation focuses on the differences from other implementations.

The above descriptions are only a few implementations of the present utility model. Although the disclosed implementations of the present utility model are as above, the content described above is only for the convenience of understanding the present utility model and is not intended to limit the present utility model. Anyone skilled in the technical field to which the utility model belongs can make any modifications and changes in the form and details of the implementation without departing from the spirit and scope disclosed in the utility model, but the patent of the utility model The scope of protection must still be based on the scope defined in the appended claims.

Claims (10)

1. a kind of separator characterized by comprising three rotation shells, separated structure monomer and particle circular regeneration mechanism, In,

The inside of the three rotations shell is arranged in the separated structure monomer comprising: the cyclone separator being coupled and movement Bed；

Particle circular regeneration mechanism includes: riser, spouted bed regenerator, the connection spouted bed regenerator from bottom to top With the regenerator sloped tube of the moving bed；The spouted bed regenerator has opposite top and bottom, wherein the spouted bed is again The upper end of raw device is provided with the sleeve that Open Side Down, the sleeve by the inside division of the spouted bed regenerator be fountain area and Annular space area is provided with the regeneration gas outlet being connected with the annular space area on the side wall of the spouted bed regenerator.

2. separator as described in claim 1, which is characterized in that it is described three rotation shell include collection chamber and be located at the collection The dust storage chamber of gas chamber lower part, and it is located at the three rotations intracorporal gas inlet pipe of shell, gas, which is provided with, on the collection chamber goes out Mouthful, particle outlet is provided on the dust storage chamber；

The cyclone separator includes: center exhaust pipe, cylinder, cone, ash bucket, dipleg from top to bottom, wherein the central row The upper end opening of tracheae is connected with the collection chamber, is provided on the barrel of the cylinder and is connected with the gas inlet pipe Gas access；Wherein, the lower ending opening of the dipleg is connected with the dust storage chamber；

The moving bed successively includes: feed bin, the area Liao Feng, cross-flow area, moving bed dipleg and inclined tube to be generated from top to bottom.

3. separator as claimed in claim 2, which is characterized in that the wall surface in the cross-flow area uses the netted knot of Johnson Structure, the cable gap of the reticular structure is between 0.25 millimeter to 0.75 millimeter.

4. separator as claimed in claim 2, which is characterized in that the number of the separated structure monomer is 3 to 20, more A separated structure monomer is centrosymmetric and is circumferentially uniformly distributed using the gas inlet pipe as axis.

5. separator as claimed in claim 4, which is characterized in that the cyclone separator is using diameter less than 1.5 meters Stream reversible type structure is cut, the gas access being arranged on the cylinder is scroll casing type gas access.

6. separator as claimed in claim 5, which is characterized in that the sleeve is the cylindrical tube of lower ending opening, institute The superficial gas velocity for stating annular space area is equal with the superficial gas velocity in sleeve.

7. separator as claimed in claim 6, which is characterized in that the riser includes pre lift zone and mentions from bottom to top Riser section, the caliber of the pre lift zone are greater than the caliber for promoting pipeline section, be provided on the pre lift zone with it is described to The bottom opening that raw inclined tube is connected；The upper end outlet for promoting pipeline section is located in the spouted bed regenerator and is spaced predetermined Distance is located at the lower end of the sleeve；

The riser is located in the three rotations shell or the riser is located at outside the three rotations shell.

8. separator as claimed in claim 7, which is characterized in that the annular space between the promotion pipeline section and the feed bin It is additionally provided with air lift endless tube, is provided at least one injection hole and multiple stomatas on the air lift endless tube.

9. separator as claimed in claim 8, which is characterized in that the superficial gas velocity in section is institute where the air lift endless tube 0.5~0.8 times for stating moving bed bed particle minimum fluidizing velocity；The diameter of the air lift endless tube is the promotion pipeline section and institute The average value of spouted bed regenerator diameter is stated, the distance of the air lift endless tube to the upper end outlet for promoting pipeline section is 3 times The riser diameter.

10. separator as claimed in claim 9, which is characterized in that in the inclined tube to be generated or the inclined tube to be generated and Position is provided with pre-sifted separation structure downstream.