CN1935349A - Gas-solid fluidized coupling equipment and coupling method for particle mixing-classifying by utilizing same - Google Patents

Abstract

The invention provides a gas-solid fluidization coupling device, which comprises at least one stage of gas-solid fluidized bed body, the fluidized bed body is a vertically arranged cylinder, the top is a tapered diameter-reduced structure, and the diameter-reduced structure The upper part forms a small particle outlet pipe, and the bottom of the fluidized bed is provided with a large particle outlet pipe, and the side wall is provided with a particle inlet pipe; the gas distribution plate is arranged in an inverted cone shape in the cylinder, and the upper part of the fluidized bed The lower end is closed, and the lower part is connected to the large particle outlet pipe, so that the gas distribution plate, the large particle outlet pipe, part of the cylinder and the lower head of the gas-solid fluidized bed form a closed space for the particles, and the closed space corresponds to the cylinder The body wall is provided with an air inlet pipe for introducing fluidization gas. The invention also provides a coupling method for realizing multi-stage mixing, heat exchange, reaction and classification of large difference particles by using the equipment of the invention.

Description

Gas-solid fluidization coupling equipment and coupling method for particle mixing and grading using the equipment

technical field

The invention relates to a gas-solid fluidization coupling device and a coupling method for particle mixing and grading by using the device, especially a method that can completely mix particles of different sizes to facilitate the completion of processing steps such as reaction and heat exchange. , and the coupling device and method that can classify the mixed particles again can be widely used in the fields of petroleum refining, chemical industry, metallurgy, agriculture and the like that involve the treatment of granular materials.

Background technique

At present, granular materials are widely used in many industries, such as solid catalysts widely used in petroleum refining or other chemical industries, minerals in the mining industry, and grains in agriculture. Particle size and particle size distribution have certain requirements, and particle size distribution often has a great or even crucial impact on the process or material performance or product performance involved. Therefore, sometimes it is necessary to uniformly mix particles of different size distributions, and sometimes it is necessary to size classify the mixed state of granular materials.

At present, the commonly used particle classification methods in industry include sieving method, centrifugation method, sedimentation method, etc., among which sieving method is the most widely used. The sieving method adopts the cooperation of screens with different mesh sizes to sort out granular materials in different particle size ranges. The sorting accuracy is mainly determined by the mesh size accuracy and particle shape. In order to strengthen the screening process, sometimes it can be equipped with vibration and other measures. However, the sieving method has the disadvantage that the sieve is easy to be blocked. At the same time, the separation accuracy has a great relationship with the shape of the particles. For the special-shaped particles with a large length and diameter ratio such as rods, it is difficult to guarantee the screening accuracy. For the screening process that introduces external forces such as vibration, due to the existence of moving parts, the sealing problem is difficult to solve, and it is difficult to apply to petroleum refining or other chemical industries that often involve flammable and explosive media and high temperature and high pressure operations. . Relatively speaking, centrifugal grading equipment has no rotating parts and simple structure, and has been widely used in chemical industries such as petroleum refining. However, centrifugal grading equipment has low internal particle concentration, short particle residence time, and inability The defect of mixing makes it difficult to adapt to occasions where large and small particles need to be uniformly mixed to complete operations such as reaction and heat exchange. The simple sedimentation method also has the same problem.

With the development of chemical industries such as petroleum refining, various coupling technologies that can greatly improve equipment utilization and save energy are being adopted more and more. For example, the "Catalytic Gasoline Auxiliary Riser Reactor Modification and Olefin Reduction Technology" developed to reduce the olefin content in gasoline ("Refining Technology and Engineering" 2005, Vol.35, No.6, "Binzhou Petrochemical Catalytic Cracking Gasoline Auxiliary Riser Industrialization of Olefin Modification Technology", author: Gao Jinsen, Xu Chunming, Lu Chunxi, etc.), is to add a riser reactor using a special catalyst to process catalytic gasoline in the existing heavy oil catalytic cracking unit. The catalytic cracking reaction environment reduces the olefin content in catalytic gasoline, while ensuring that the octane number and liquid yield do not decrease. The biggest engineering problem in this technology is that the amount of catalyst coking in the newly developed catalytic gasoline reaction process is relatively low, and the heat released by catalyst burnt regeneration cannot maintain the heat balance of its own reaction-catalyst regeneration system. If it is solved by adding fuel Energy consumption is too high. In addition, in this new technology, a reactor and a regenerator need to be installed at the same time, and the equipment investment is high. Considering the high amount of catalyst coke in the heavy oil catalytic cracking process, and the heat released by catalyst burnt regeneration, there is still a large amount of surplus in addition to maintaining the heat balance of its own system, and it is necessary to use an external heat extractor to obtain heat. If a practical technology can be developed and The equipment can not only make the catalysts in the two processes mix and exchange heat, but also catalyze the regeneration of the catalysts in the gasoline upgrading process, and then re-separate the two different catalysts, which will not only solve the problem of high energy consumption in new technologies, In addition, the regenerator in the new technology can be combined with the external heat collector of the original heavy oil catalytic cracking unit, which greatly reduces the equipment investment of the new technology. Similar problems are common in various new processes that have been developed and are currently being developed, such as catalytic gasoline aromatization, C4 olefin aromatization, and catalytic gasoline catalytic cracking to ethylene and propylene. In a similar process, how to ensure the good mixing of gas, solid, and solid to efficiently complete the processing steps such as reaction and heat exchange, and at the same time efficiently classify the mixed particles has become a bottleneck problem restricting the application of coupling technology.

Contents of the invention

The invention provides a gas-solid fluidization coupling device that can realize effective mixing and grading of particles. The device can not only uniformly mix particle materials with different particle size distributions to complete processing steps such as reaction and heat exchange, but also can The mixed particles are reclassified according to the predetermined particle size distribution requirements.

The invention also provides a coupling method for realizing mixing and grading of particles by using the above-mentioned equipment.

The invention provides a gas-solid fluidization coupling device, which comprises at least one stage of gas-solid fluidized bed body, the fluidized bed body is a vertically arranged cylinder, the top is a tapered diameter-reduced structure, and the diameter-reduced structure The upper part forms a small particle outlet pipe, and the bottom of the fluidized bed is provided with a large particle outlet pipe, and the side wall is provided with a particle inlet pipe; an inverted cone-shaped gas distribution plate is provided in the cylinder, and the upper part of the fluidized bed will The lower end of the body is closed, and the lower part is connected to the large particle outlet pipe, so that the gas distribution plate, the large particle outlet pipe, part of the cylinder body and the lower head of the gas-solid fluidized bed form a closed space for the particles, and the closed space corresponds to An air inlet pipe for introducing fluidization gas is arranged on the wall of the cylinder body.

In the above-mentioned equipment, there is at least one particle inlet pipe, preferably including a large particle inlet pipe and a small particle inlet pipe respectively arranged to introduce large and small particles into the bed respectively, and the large particle inlet pipe is set at a position higher than the small particle inlet pipe. Import pipe. When mixing and classifying particles, the particles that have been mixed in advance can be directly added to the equipment from the particle inlet pipe. If there are two particle inlet pipes, add from one of them (preferably from the large particle inlet pipe) ); for materials with a large difference in particle size or size, the large particles and small particles are sent into the gas-solid fluidized bed from the large particle inlet pipe and the small particle inlet pipe respectively, and interact with the gas entering through the gas distribution plate. , can form completely mixed dense-phase bed and dilute-phase bed, obviously, the dilute-phase bed is formed above the dense-phase bed. Part of the small particles in the dense-phase bed will be transferred to the dilute-phase bed under the action of the airflow, and will be entrained by the airflow to leave the gas-solid fluidized bed through the small particle outlet pipe, while the large particles will be discharged from the large particle outlet pipe to realize particle separation. Blend and regrade.

According to the specific design scheme of the present invention, the acute angle between the hypotenuse of the tapered diameter reduction at the top of the gas-solid fluidized bed and the vertical direction can be designed to be 20°-60°;

The mouth of the particle inlet pipe is inclined upward and is set at an acute angle of 15°-45° with the vertical cylinder of the fluidized bed;

More preferably, the distance between the opening position of the large particle inlet pipe of the bed and the large port of the tapered diameter reducing section at the top of the gas-solid fluidized bed is at least 1000mm, so that the large particles entrained by the airflow into the dilute phase space There is a chance to settle and return to the dense phase, and the distance between the small particle inlet pipe and the upper end of the inverted cone of the gas distribution plate is at least 200mm to avoid the influence area of the distribution plate; the setting angles of the large and small particle inlet pipes can be the same or different , but they can all form an acute angle of 15°-45° with the vertical cylinder, which can generally vary between 30°-45°;

The acute angle between the inverted conical hypotenuse of the gas distribution plate and the vertical direction is 45°-75°;

Furthermore, the surface of the gas distribution plate has small holes, and the direction of the holes is not limited, but preferably the angle (acute angle) with the horizontal direction is controlled between 0°-75°, and the opening ratio is controlled at 0.5%. In the range of -10% (based on the cross-section of the gas-solid fluidized bed). The opening ratio defined in the present invention is defined as the ratio of the area of the openings on the gas distribution plate (the sum of the areas of all holes) to the cross-sectional area in the bed.

As a specific embodiment, a gas distributor is arranged in the gas-solid fluidized bed between the particle inlet pipe (if two inlet pipes are set, then refer to the small particle inlet pipe) and the gas distribution plate, and an air inlet and a gas distributor are provided in addition. connected. Preferably, the opening ratio of the gas distributor is 0.5%-10%, the opening faces downward, and the angle with the vertical direction is within the range of ±45°.

In order to achieve the expected mixing and/or classification effect, the gas-solid fluidized coupling device of the present invention can use the above-mentioned gas-solid fluidized bed as a basic unit, and implement a two-stage or multi-stage series design, and the large particle outlet pipe of the previous stage It is connected with the particle inlet pipe of the latter stage, and it is also called a two-stage fluidized bed structure when two stages are connected in series (it can also be called similarly when more stages are connected in series). In this way, the large particles that have removed some small particles in the previous stage directly enter the fluidized bed of the next stage through the large particle outlet pipe at the bottom of the dense phase bed, and form a dense phase bed and a dilute phase bed again under the action of the fluidizing gas again. , the small particles are separated from the small particle outlet pipe again, and the large particles are discharged from the large particle outlet pipe again until the predetermined classification requirements are met.

The plurality of separation units can have separate gas-solid fluidized beds respectively, or two or more gas-solid fluidized beds can be arranged as an integrated two-stage or multi-stage structure, so as to be applicable to different Process requirements or environmental conditions.

In order to achieve the expected mixing and/or classification effect, the equipment of the present invention can also be combined with other devices for realizing particle classification, specifically, the equipment of the present invention also includes at least one horizontal particle classification box for further classification of particles, flow The large particle outlet pipe of the chemical bed body is connected with the inlet pipe provided on the top plate side of the horizontal particle classification box; a gas inlet is arranged at the side end of the horizontal particle classification box near the inlet pipe, and a gas distribution pipe is arranged in the box relative to the gas inlet. A device that allows the incoming gas to blow into the box in the direction perpendicular to the entry of the particles, and a baffle plate is set on the other side of the box to make the box form a baffle chamber on the side away from the inlet pipe, and the top of the baffle chamber is set For the gas outlet, there are more than one particle outlets distributed on the bottom plate of the box, and baffles that rise sequentially from the bottom plate are arranged on the side of each particle outlet away from the inlet pipe. Of course, according to the performance of the materials to be processed and the classification accuracy requirements, more than one horizontal particle classification box can also be connected in series.

The present invention also provides a coupling method for mixing and/or grading particles by using the above-mentioned fluidized coupling device, so that the particles to be mixed and/or classified enter the fluidized bed from the particle inlet pipe, and the fluidized gas flows from the inlet pipe to the fluidized bed. The gas pipe enters the fluidized bed through the gas distribution plate, and interacts with the particles to form a completely mixed dense-phase bed and a dilute-phase bed from bottom to top. The outlet pipe is entrained by the air flow to leave the fluidized bed body to realize the classification between particles.

The coupling method of the present invention is especially suitable for completely mixing particles of different sizes, and enables the mixed particles to be classified again according to requirements. Equipment and reasonable matching of gas velocity can achieve a classification efficiency of more than 98%. At this time, the mixing and grading operation of two or more stages is adopted, and the large particles and small particles are respectively sent into the first-stage fluidized bed body from the large particle inlet pipe and the small particle inlet pipe of the gas-solid fluidized bed body, Wherein the addition ratio (weight) of large and small particles is 0.2～1.0: 1; Regulate the superficial gas velocity in the first-stage fluidized bed body to be 0.2～1.0 m/s, large and small particles are blown in from the gas distribution plate Under the action of the gas, a fluidized bed is formed to achieve uniform mixing; the classification efficiency range is adjusted between 60% and 90% by adjusting the superficial gas velocity, forming a dense phase bed and a dilute phase bed; some small particles are entrained by the airflow The dilute-phase bed leaves the small particle outlet pipe, and the large particles enter the second-stage fluidized bed through the large-particle outlet pipe at the bottom of the dense-phase bed. grading again, the grading operation can be repeated as needed.

It can be understood that the above-mentioned mixing and grading operation can be realized by using a fluidized coupling device composed of a fluidized bed body and a horizontal particle classification box, so that the large particles leaving from the large particle outlet pipe enter the horizontal particle classification box, so that the particles are in the airflow. The movement trajectory under the action is a parabolic drop, and the particles leave from the particle outlet on the bottom plate of the box according to the difference in particle size to achieve classification.

It can be seen from the above that the gas-solid fluidization coupling device of the present invention utilizes the agitation of the bubbles in the gas-solid bubbling fluidized bed to complete the complete mixing between large and small particles, so that the gas, solid, and solid contacts are sufficient and very effective. It is conducive to the efficient progress of the reaction and heat exchange process; at the same time, it utilizes the special phenomenon of particle classification that occurs inside the dense phase bed at a specific gas velocity during the two-component gas-solid fluidization process and the general gas-solid fluidized bed. Analyzing the classification phenomenon, through the optimized combination of the structure, the classification efficiency can be greatly improved and the fluidization air volume required for classification can be reduced; the outstanding feature of this equipment is to realize the coupling of the mixing of two different particles and the classification process. At the same time, the equipment has a compact structure, no moving parts, and can run continuously. It is very suitable for operations involving high temperature and high pressure, such as petroleum refining or other chemical industries. For example, in view of the current engineering problems in the petroleum refining industry: mixing heat exchange between two catalysts with different particle sizes and different temperatures, and classifying again after mixing heat exchange, and one of the catalysts has to be mixed with fluidization gas carry out the reaction, and the present invention can be used to obtain a very effective solution. The coupling device and treatment method of the present invention are especially suitable for processing catalytic cracking catalyst particles in petroleum oil refining, that is, it can be used to treat mixed particles containing catalytic cracking catalysts Mixing and classification are carried out, and the small particles in it are used as catalyst particles for catalytic cracking in petroleum oil refining.

In summary, the gas-solid fluidization coupling device of the present invention and the coupling method for particle mixing and grading using the device have obvious advantages compared with the prior art:

Based on the fluidization technology that has been widely used in industry at present, the present invention can not only complete the mixing of particles with different particle sizes, but also efficiently classify the mixed particles through the optimized combination and reasonable matching of structures. While completely mixing particles of different sizes to efficiently complete the processing steps such as reaction and heat exchange, it can also efficiently classify the mixed particles in the same equipment. The whole equipment has a compact and simple structure and can operate continuously. Compared with the existing particle classification equipment, it has no moving parts or moving structures and is easy to seal. It is especially suitable for high temperature, high pressure and particle processing capacity in the fields of petroleum refining and chemical industry. Great occasion.

Description of drawings

Fig. 1 is the schematic diagram of specific embodiment 1 of the present invention;

Figure 2 is a schematic diagram of a second embodiment of the present invention;

FIG. 3 is a schematic diagram of a third embodiment of the present invention;

Figure 4 is a schematic diagram of a fourth embodiment of the present invention;

Figure 5A is a schematic front view of a gas distribution plate;

5B is a schematic top view of the gas distribution plate;

Fig. 6 is the schematic perspective view of the horizontal particle classification box in embodiment four;

Fig. 7 has shown the variation trend curve of classification efficiency with superficial gas velocity in the embodiment of the present invention;

Fig. 8 shows the results of analyzing the composition of the materials mixed in the first-stage gas-solid fluidized bed in Example 1 of the present invention.

Detailed ways

Below in conjunction with accompanying drawing and specific embodiment the present invention is described in further detail:

Embodiment one

Please refer to Fig. 1, which is a schematic structural diagram of a specific embodiment 1 of the gas-solid fluidization coupling device of the present invention, two gas-solid fluidized beds 1 form an integrated two-stage fluidized bed in series, The entire two-stage gas-solid fluidized bed body 1 is a vertically arranged cylinder body. The top of the first-stage fluidized bed body is a tapered diameter-reducing structure, and the upper part forms the small particle outlet pipe 6 of this stage. The particle inlet pipe 3 and the small particle inlet pipe 4, the distance between the large particle inlet pipe 3 and the large conical port on the top is greater than 1000 mm, and the gas distribution plate 2 is arranged in an inverted cone shape in the cylinder, and the upper part of the cylinder closes the lower end of the fluidized bed body 1, And the distance from the small particle inlet pipe 4 is at least 200mm. In the present embodiment, the total height of each fluidized bed body is about 1500mm. As shown in Figure 1, the bottom of the gas distribution plate 2 is in phase with the large particle outlet pipe 5 A space that can be closed to particles is formed at the lower part of the fluidized bed body of this stage, and a fluidization gas inlet (as indicated by an arrow) is provided on the cylinder wall corresponding to this space. The large particle outlet pipe 5 of the first-stage fluidized bed body directly extends from the top into the cylinder body of the rear stage fluidized bed body to form the particle inlet pipe of this stage, while the small particle outlet pipe of the second-stage fluidized bed body 6 is arranged on the cylinder side wall.

As shown in Figure 1, the angle a between the hypotenuse and the vertical direction can vary from 30° to 60°; the angles b, c between the large particle inlet pipe 3 and the small particle inlet pipe 4 and the bed body 1 According to the difference in the flow characteristics of the large and small particles and the difference in the mutual position between the bed body 1 and the source equipment of the large and small particles, it can be adjusted, generally between 30°-45°.

The bottom of each section of the two-stage gas-solid fluidized bed body 1 in this embodiment is provided with an inverted conical gas distribution plate 2, the upper part of the inverted conical shape closes the lower end of the bed 1, and the lower part is connected with a large particle outlet pipe 5, According to the particle size of the particles to be classified and the classification efficiency, the angle d between the hypotenuse of the inverted cone and the vertical direction can be controlled to vary between 45°-75°; the surface of the distribution plate 2 has small holes with a general diameter It is 3-8mm, the opening direction is not limited, preferably the angle e with the horizontal direction can be controlled between 0°-75° according to the particle size of the particles to be classified and the classification efficiency (please also refer to Figure 5A As shown in Figure 5B, which are respectively the front view schematic diagram and the top view schematic diagram of the gas distribution plate of this embodiment), the opening ratio is controlled in the range of 0.5%-10% according to the separation requirements (taking the cross section of the gas-solid fluidized bed body 1 as benchmark). The gas passes through the gas distribution plate 2 to form rising bubbles in the dense phase, and the particles are in countercurrent contact with the bubbles in the process of passing through the distribution plate 2 to the outlet pipe 5, and the small particles are carried by the bubbles from the bottom of the dense phase to the top, and some of them are removed. A mixture of small particles leaves the first stage through pipe 5 and enters the next stage. In this way, the mixing and preliminary classification of large and small particles are completed.

The structure of the second section is similar to the first section, but the main task is to complete the further classification of the particles, so the openings of the gas distribution plate 2 can be relatively slightly higher in aperture and opening ratio than the first section (but still Adjust within the above range), so that most of the small particles in the mixed particles leave the device through the small particle outlet pipe 6 of this section, while the large particles that have removed the small particles leave the device through the large particle outlet pipe 5 at the bottom.

The large and small particles entering the first stage of the two-stage gas-solid fluidized bed body 1 from the large particle inlet pipe 3 and the small particle inlet pipe 4 respectively form a drum in the lower half under the action of the gas blown through the gas distribution plate 2 Bubble fluidized bed, due to the agitation of the bubbles in the bed, between the horizontal line above the large end of the gas distribution plate and the upper interface of the dense phase, the gas, solid and solid are fully mixed, which greatly reduces the reaction and heat transfer process. transfer resistance.

The large and small particles in the dense phase partly enter the dilute phase space under the action of the air flow. Due to the different particle sizes, the number of large particles entering the dilute phase space is small, and after rising to a certain height, they settle again and return to the dense phase. The number of small particles entering the dilute phase space is larger, and the rising height is higher, forming a denser distribution in the dilute phase space. Since the velocity of the airflow increases when passing through the tapered diameter-reducing structure, it is difficult for the small particles entrained in it to settle back into the dense phase, but are carried out by the airflow from the outlet 6.

Referring to Fig. 3, a gas distributor 19 can also be set between the small particle inlet pipe 4 and the gas distribution plate 2, so that another stream of gas enters the gas through the gas distributor 19 arranged in the middle of the dense phase bed. The upper half of the solid fluidized bed body 1 interacts with large and small particles to form a fully mixed dense bed and a dilute bed above the dense bed.

The following are the test results using the device and method of this embodiment. In the test, the feed of large particles with a particle size greater than 500 μm is 1998 kg/h, and the feed of small particles with a particle size of less than 200 μm is 1229 kg/h. Figure 7 shows the grading effect achieved. It can be seen that the classification efficiency increases with the increase of the superficial gas velocity, and at a suitable superficial gas velocity, the classification efficiency can reach 95%. Fig. 8 shows the results of simultaneous analysis of the material composition in the first stage of the gas-solid fluidized bed 1 (all represented by the mass percentage of small particles). The whole bed body is divided into 5 layers in the axial direction, and 4 sampling points are set in each layer according to different radial directions. Among the 20 sampling points, the lowest concentration is 27.01%, the highest is 36.03%, the average is 32.03%, and the standard deviation is 2.33%. This figure can illustrate that while achieving a good classification effect, the large and small particles in the material in the bed body 1 are mixed quite uniformly.

Embodiment two

Fig. 2 is the front view of the second embodiment of the present invention, as can be seen, the difference with Fig. 1 is that each fluidized bed body is an independent single-stage gas-solid fluidized bed body, and the first stage fluidized bed body 1 The large particle outlet pipe 5 communicates with the side wall of the fluidized bed body 7 of the second stage to form a second stage particle inlet pipe. According to the needs of classification accuracy and operation, it can be connected in series in this way to adapt to different venues and adopt more flexible operations.

Similarly, a gas distributor 19 may also be arranged in the fluidized bed body.

Embodiment three

Fig. 3 is the front view of the third embodiment of the present invention, a gas distributor 19 is added in the dense phase between the small particle inlet pipe 4 and the gas distribution plate 2, according to the site, operation, classification requirements, etc., the fluidized bed The body can be used alone in a single-stage (single-stage) type, or can be combined into multi-stage (or multi-stage) in the manner of Embodiment 1 and Embodiment 2.

When implemented in combination according to the method of Example 2, the amount of gas entering through the gas distribution plate 2 is smaller than that of the solution of Example 1, and the fluidized bed containing both large and small particles is utilized at a lower gas velocity, and the bottom of the dense bed Can form almost pure large particle layer, can form the phenomenon of mixed particle layer on the large particle layer, form almost pure large particle layer between distribution plate 2 and distributor 19, thereby make classification efficiency be further improved, and The total gas volume required can then be reduced. The mixing and primary separation of large and small particles is accomplished in the mixed particle layer above the large particle layer by the gas entering from the distributor 19 .

Embodiment four

Fig. 4 is a front view of a fourth embodiment of the present invention, which uses the fluidized bed of the present invention in series with a horizontal particle classification box. As shown in the figure, the large particle outlet pipe 5 communicates with the horizontal particle classification box 8 to meet higher classification requirements. Similarly, the structure of the fluidized bed can be any one of the first, second and third embodiments.

Figure 6 is a sectional view of the horizontal particle classification box 8, the large particle outlet pipe 5 of the fluidized bed body communicates with the inlet pipe 10 provided on the top plate 9 side of the horizontal particle classification box, the horizontal particle classification box is close to the inlet pipe The end plate 11 on one side of the box is provided with a gas inlet, and a gas distributor 12 is arranged in the box body 8 opposite to the gas inlet, so that the incoming gas can be blown into the box body in a direction perpendicular to the entry of the particles, and a baffle plate is set on the other side of the box body 17. Make the box body form a baffle chamber 16 on the side away from the inlet pipe 10, and the top of the baffle chamber 16 is provided with a gas outlet 18. According to the requirements of particle classification, there are more than one particle outlets distributed on the bottom plate 13 of the box body 8 15, and on the side of each particle outlet 15 away from the inlet pipe, baffles 14 that rise in sequence are arranged upward from the bottom plate.

As shown in Figures 4 and 6, the large particles leaving the gas-solid fluidized bed body 1 through the large particle outlet pipe 5 enter the horizontal particle classification box 8, and the further classification of the particles can be realized through the following continuous steps:

(a), the large particles entrained with some small particles leaving the gas-solid fluidized bed body 1 from the large particle outlet pipe 5 enter from the upper inlet pipe 10 arranged at one end of the top plate 9 of the horizontal particle classification box 8, and form a fan. fall;

(b), gas enters from the gas distributor 12 that is arranged on the end plate 11 of the horizontal particle classification box 8 and is parallel to the particle fan that falls, and blows through in the direction perpendicular to the fan;

(c) Under the action of the airflow, the trajectory of the falling particles changes from a vertical drop to a parabolic drop. The throwing distance of large particles is shorter, and the throwing distance of small particles is longer;

(d), the particles falling in a parabolic shape collide with the baffle plate 14 arranged on the bottom plate 13 of the horizontal particle classification box 8 and change the direction of motion, and fall downwards into the outlet pipe 15 arranged on the bottom plate 13 and positioned at the front of the baffle plate 14 , leaving the horizontal particle classification box 8; due to the different parabolic falling trajectories of the large and small particles, the larger particles will be discharged from the outlet 15 that is closer to the inlet pipe 10, while the smaller particles will be discharged from the outlet 15 that is farther away from the inlet pipe 10 Discharge, the sequentially rising baffles 14 are also helpful for the classified discharge of particles;

(e), the air flow entrains the powder that fails to fall into the baffle chamber 16 arranged at the other end of the horizontal particle classification box 8, and leaves through the gas outlet pipe 18 arranged at the other end on the top plate 9 after bypassing the baffle plate 17, During deflection, larger particles of the powder fall into the bottom of the deflection chamber 16 and exit through the outlet 15 provided there.

Finally, it should be noted that: the above embodiments are only used to illustrate the design ideas and beneficial effects of the present invention, rather than limit the scope of implementation of the technical solutions of the present invention; However, those skilled in the art can still make modifications or equivalent replacements to the present invention under the inspiration of this; and all technical solutions and improvements that do not depart from the spirit and scope of the present invention should be covered by the present invention. within the scope of protection.

Claims (16)

1. A gas-solid fluidization coupling device, which includes at least one stage of gas-solid fluidized bed body, the fluidized bed body is a vertically arranged cylinder, the top is a tapered diameter-reducing structure, and the upper part of the diameter-reducing structure is formed Small particle outlet pipe, while the bottom of the fluidized bed is provided with a large particle outlet pipe, and the side wall is provided with a particle inlet pipe; an inverted cone-shaped gas distribution plate is provided in the cylinder, and its upper part connects the lower end of the fluidized bed. Closed, the lower part is connected to the large particle outlet pipe, so that the gas distribution plate, the large particle outlet pipe, part of the cylinder and the lower head of the gas-solid fluidized bed form a closed space for the particles, and the cylinder corresponding to this closed space The wall is provided with an inlet pipe for introducing fluidization gas. 2. The gas-solid fluidization coupling device according to claim 1, wherein the particle inlet pipe includes a large particle inlet pipe and a small particle inlet pipe respectively, and the large particle inlet pipe is located higher than the small particle inlet Tube. 3. The gas-solid fluidization coupling device according to claim 1, wherein the acute angle between the hypotenuse of the tapered diameter reduction at the top of the gas-solid fluidized bed and the vertical direction is 20°-60°. 4. The gas-solid fluidization coupling device according to claim 2, wherein the mouth of the particle inlet pipe is upward and is set at an acute angle of 15°-45° with the vertical cylinder of the fluidized bed. 5. The gas-solid fluidization coupling device according to claim 2, wherein the distance between the large particle inlet pipe and the tapered diameter-reduced large port on the top of the gas-solid fluidized bed is at least 1000 mm, and the distance between the small particle inlet pipe The distance at the top of the gas distribution plate is at least 200 mm. 6. The gas-solid fluidization coupling device according to claim 1, wherein the acute angle between the inverted tapered hypotenuse of the gas distribution plate and the vertical direction is 45°-75°. 7. The gas-solid fluidization coupling device according to claim 1, wherein the surface of the gas distribution plate is provided with through holes with a diameter of 3-8mm, and the angle between the opening direction and the horizontal direction is 0°-75°. °, the opening ratio is controlled within the range of 0.5% to 10% based on the cross section of the gas-solid fluidized bed. 8. The gas-solid fluidization coupling device according to any one of claims 1-7, wherein a gas distributor is arranged in the gas-solid fluidized bed between the particle inlet pipe and the gas distribution plate, and an additional The air inlet is connected with it. 9. The gas-solid fluidization coupling device according to any one of claims 1-7, which is composed of more than one level of gas-solid fluidized beds connected in series. At this time, the large particle outlet pipe of the previous level and the rear The particle inlet pipes of the first stage are connected. 10. The gas-solid fluidization coupling device according to claim 9, wherein each fluidized bed is connected in series in such a way that the large particle outlet pipe of the previous fluidized bed directly extends from the top into the subsequent fluidized bed The particle inlet pipe of this stage is formed in the cylinder of the fluidized bed, and the small particle outlet pipe of the fluidized bed from the second stage is arranged on the side wall of the cylinder. 11. The gas-solid fluidization coupling device according to claim 9, wherein each fluidized bed is an independent single-stage gas-solid fluidized bed, and the large particle outlet pipe of the previous stage is connected to the fluidized bed of the subsequent stage. The side wall of the bed is connected to form the particle inlet pipe of the next stage. 12. The gas-solid fluidization coupling device according to any one of claims 1-7, which further comprises at least one horizontal particle classification box for further classification of particles, and the large particle outlet pipe of the fluidized bed is connected to the horizontal particle classification box. The inlet pipe provided on one side of the top plate of the particle classification box is connected; the side end of the horizontal particle classification box near the inlet pipe is provided with a gas inlet, and a gas distributor is arranged in the box relative to the gas inlet, so that the incoming gas can flow vertically to the particles. The direction of entry is blown into the box body, and a baffle plate is set on the other side of the box body, so that the box body forms a baffle chamber on the side away from the inlet pipe, and the top of the baffle chamber is provided with a gas outlet. There are more than one particle outlets, and successively rising baffles are arranged upward from the bottom plate on the side of each particle outlet away from the inlet pipe. 13. A coupling method for mixing and/or classifying particles, which is to use the fluidized coupling device described in any one of claims 1-12 to make the particles to be mixed and/or classified enter the fluid flow from the particle inlet pipe In the fluidized bed body, the fluidized gas enters the fluidized bed from the inlet pipe through the gas distribution plate, and interacts with the particles to form a completely mixed dense-phase bed and dilute-phase bed from bottom to top, and controls the superficial gas velocity of the gas flow to make the particles The large particle outlet pipe and the small particle outlet pipe are respectively entrained by the airflow to leave the fluidized bed to realize the classification between particles. 14. The coupling method according to claim 13, wherein two or more stages of mixing and grading operations are used to separate large particles and small particles from the large particle inlet pipe and the small particle inlet of the gas-solid fluidized bed, respectively. The pipe is sent into the first-stage fluidized bed body, wherein the adding ratio of large and small particle weight is 0.2～1.0:1; the superficial gas velocity in the first-stage fluidized bed body is adjusted to be 0.2～1.0 m/s, by adjusting The superficial gas velocity adjusts the classification efficiency range between 60% and 90%, forming a dense phase bed and a dilute phase bed; some small particles are entrained by the air flow through the dilute phase bed and leave the small particle outlet pipe, and large particles pass through the dense phase bed The large particle outlet pipe at the bottom enters the second-stage fluidized bed body, and the superficial gas velocity in the second stage is controlled to 0.6-1.2 m/s to realize re-classification of particles. This classification operation can be repeated as required. 15. The coupling method according to claim 13, wherein the fluidized coupling equipment formed by the combination of the fluidized bed body and the horizontal particle classification box is used to allow the large particles leaving from the large particle outlet pipe to enter the horizontal particle classification box, The trajectory of the particles under the action of the airflow is a parabolic drop, and the particles leave from the particle outlet on the bottom plate of the box according to the difference in particle size to achieve classification. 16. The coupling method according to any one of claims 13-15, which is used for mixing and classifying particles containing catalytic cracking catalysts, wherein the small particles are used as catalytic cracking catalyst particles for petroleum oil refining.

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