A grading, drying and dry cooling device and method

Abstract

The present invention discloses a grading, drying and dry cooling device and method, which utilizes a device including a cyclone separator and a sedimentation separator, and adjusts the speed and temperature of each air inlet to achieve the regulation of the drying degree of materials with different particle sizes while grading, or effectively cools solid materials while achieving the grading of materials and the removal of dust carried by them. The device has a simple structure, is easy to operate, and the grading particle size and device function can be flexibly switched, and has excellent grading, drying and dry cooling effects.

Description

Technical Field

[0001] This invention belongs to the field of powder processing technology, and relates to an apparatus and method for simultaneous grading and drying, as well as dry cooling and simultaneous grading and dust removal. Background Technology

[0002] The classification and drying of solid particulate materials is an important pretreatment technology in chemical processes. Conventional classification and drying processes are carried out in separate reactors, resulting in two process paths: classification followed by drying and drying followed by classification. If the particulate material is classified first and then dried, the classifier is under heavy load, costly, and the presence of moisture causes particle adhesion, leading to low classification efficiency. If the particulate material is dried first and then classified, the different drying rates of different particles make it impossible to effectively control the moisture content of the particulate material fed into the dryer and discharged simultaneously, thus failing to meet the requirements of subsequent processing.

[0003] Furthermore, coke quenching technology is an important energy-saving and environmentally friendly technology in the coking industry. Dry quenching refers to the gradual cooling of high-temperature coke by inert circulating gas within a dry quenching oven. The design of domestic dry quenching ovens has consistently followed the dry quenching technology concept invented in Japan, which includes a pre-storage section, inclined ducts, annular air ducts, and a cooling section. However, the pre-storage section, acting as a buffer, accounts for nearly 30% of the oven's height, resulting in a larger structural structure, higher investment in construction and equipment, and higher operating and maintenance costs. The inclined ducts, with their more than 20 single-bracket support structures, experience high stress and short service life. The annular air ducts, due to their suspended support and large internal and external pressure differences, are prone to abnormal collapse. Moreover, because the circulating gas flows rapidly within the annular air duct, the retaining walls bear significant impact forces, and the upper retaining walls, subjected to long-term thermal expansion, are prone to deformation, reduced strength, and brick detachment, weakening their support capacity and even causing the entire retaining wall to sink. Furthermore, to remove the coke dust carried by the heated circulating gas and recover its heat, the quenching medium must undergo treatment through a primary dust collector, a waste heat boiler, a secondary dust collector, a circulating fan, and a shell-and-tube heat exchanger before it can be recycled. Because traditional dry quenching furnaces lack an upper space for separating coke dust, a significant amount of coke dust is carried away by the circulating gas. Even after dust removal, the circulating gas still contains some coke dust, which can easily cause wear and tear on the steam and water pipes of the waste heat boiler, affecting its service life and, in severe cases, even causing pipe rupture, thus impacting the normal operation of the dry quenching equipment. Simultaneously, the cooled coke must be graded to meet the particle size requirements of subsequent processes. This results in dry quenching, dust removal of the quenching gas, and coke grading occurring in different reactors, leading to a complex process and high costs.

[0004] Chinese invention patent CN201710298244.6 and Chinese utility model patent CN201720468785.4 disclose a particle classification method and apparatus. The apparatus includes a cyclone separator, a sedimentation classifier, a coarse / heavy particle group collector, and a fine / light particle group trap. The top center of the cyclone separator cylinder is connected to the inlet end of the tail air outlet pipe, which does not extend into the interior of the cyclone separator. The outlet end of the tail air outlet pipe is connected to the fine / light particle group trap. A primary air inlet pipe is provided in the lower middle part of the cyclone separator cylinder. The bottom of the cyclone separator cylinder has a conical structure and is connected to the top of the sedimentation classifier. The bottom of the sedimentation classifier is connected to the coarse / heavy particle group collector, and a secondary air inlet pipe is provided in the lower part of the sedimentation classifier or the upper part of the coarse / heavy particle group collector. The device utilizes the differences in centrifugal force and terminal velocity between coarse / heavy particles and fine / light particles in mixed particle size / density materials. By adjusting the primary and secondary air velocities, the cutting particle size can be flexibly adjusted, and the device has a simple structure and is easy to operate. Although this device can be applied to particle classification environments at both ambient and high temperatures, the mixed particles and primary air are tangentially input into the cyclone separator from the same inlet. This results in significant localized impact forces of particles and airflow on the device walls, which is even more severe when classifying high-temperature materials, thus affecting the device's service life. Simultaneously, the tangential air intake at the bottom of the cyclone separator leads to a short residence time for particles within the primary cyclone separator, limiting the dispersion effect and impacting classification efficiency. Furthermore, to ensure particle conveying and classification, a large volume of primary air is required, resulting in a large exhaust gas volume and high operating costs. Summary of the Invention

[0005] In order to overcome the shortcomings of existing separate grading, drying and dry quenching technologies, this invention provides an apparatus and method that can achieve simultaneous grading and drying of particles with a wide particle size range, as well as simultaneous dry cooling, grading and dust removal.

[0006] A grading, drying, and dry cooling device includes a fine / light particle collector (1), a secondary cyclone separator (2), a cyclone-like separator (3), a settling drying / cooling pipe (4), and a coarse / heavy particle collector (5); wherein the fine / light particle collector (1) and the secondary cyclone separator (2) are connected as one unit, and the secondary cyclone separator (2) has an exhaust gas outlet (6) inserted into its top center; the secondary cyclone separator (2) is connected to the cyclone-like separator (3) through a connecting pipe (7). The cyclone separator (3) is composed of a cylindrical part and upper and lower conical parts. The cylindrical part is provided with a primary air inlet (8) tangentially, and the upper part of the cylindrical part is provided with a particle inlet (9). The upper conical part is connected to the connecting pipe (7), and the lower conical part is connected to the upper part of the settling drying / cooling pipe (4). The lower part of the settling drying / cooling pipe (4) is connected to the upper part of the coarse / heavy particle collector (5). A secondary air inlet (10) is provided at the lower part of the settling drying / cooling pipe (4) or on the upper side of the coarse / heavy particle collector (5).

[0007] The particle inlet (9) is a vertical or inclined input port, and the primary air inlet (8) is located below the particle inlet (9); or the primary air inlet (8) and the particle inlet (9) are the same tangential inlet, which can be located at the upper, middle or lower part of the cylindrical part of the cyclone separator (3); when located at the upper part of the cylindrical part of the cyclone separator (3), it is flush with the lower edge of the upper cone; when located at the lower part of the cylindrical part of the cyclone separator (3), it is flush with the upper edge of the lower cone.

[0008] The ratio of the diameter of the cylindrical part of the primary cyclone separator (3) to the diameter of the settling drying / cooling pipe (4) is 8:1 to 2:1;

[0009] The height-to-diameter ratio of the settling drying / cooling pipe (4) is 20:1 to 5:1;

[0010] A tertiary air inlet (11) can be provided on the lower side of the coarse / heavy particle collector (5) to enhance the drying or dry cooling effect.

[0011] A method for simultaneous particle classification and drying, the process is as follows:

[0012] After the mixed particulate material and the primary drying medium enter the cyclone separator (3) through the particulate inlet (9) and the primary air inlet (8), the primary drying medium forms a rotating upward airflow. Due to centrifugal force, the particulate material gradually moves towards the wall of the cyclone separator (3). The coarse / heavy particulate material has a larger mass and a greater movement / segregation velocity than the fine / light particulate material. This causes the coarse / heavy particulate material to carry some fine / light particulate material and collide and rub against the wall before settling. The settled particulate material falls into the settling drying tube (4) at a certain initial velocity under the action of gravity. At the same time, a secondary drying medium at a certain temperature is introduced through the secondary air inlet (10) and / or a tertiary drying medium at a certain temperature is introduced through the tertiary air inlet (11). At this time, the secondary and tertiary air also serve as classifying gases. The particle classification is achieved based on the relative magnitude of the terminal velocity of the particulate material and the drying medium gas velocity formed by the secondary and / or tertiary drying media in the settling drying tube (4). When the terminal velocity of the settling coarse / heavy particles is greater than the air velocity of the drying medium, the drag force is less than the gravity, and they accelerate downwards and eventually pass through the settling drying tube (4) into the coarse / heavy particle collector (5). At the same time, the coarse / heavy particles directly contact the primary air for heat exchange in the cyclone separator (3) and directly contact the drying medium input at the upper end of the coarse / heavy particle collector (5) during the descent of the settling drying tube (4). The particles are gradually preheated and their moisture is gradually removed. When the tertiary drying medium is input into the tertiary air inlet (11), the coarse / heavy particles and the tertiary drying medium continue to heat up in the coarse / heavy particle collector (5) in a countercurrent contact, so as to prolong the contact time between the large particles and the drying medium, effectively control the moisture content of the large particles, and finally store the coarse / heavy particles that meet the drying requirements in the coarse / heavy particle collector (5). At this time, the particle size of the coarse / heavy particles is large, and the tertiary drying medium can pass smoothly through the bed formed in the coarse / heavy particle collector (5), and the pressure fluctuation of the device is small. The terminal velocity of the entrained fine / light particulate material is less than that of the drying medium, and the drag force is greater than that of gravity. It first decelerates and moves downward and is then blown back into the cyclone separator (3). The fine / light particulate material carried by the primary air is carried by the rising airflow formed by the primary, secondary and / or tertiary drying media and enters the secondary cyclone separator (2) through the connecting pipe (7). At the same time, the fine / light particulate material comes into contact with the airflow for heat exchange, and its moisture is gradually removed. After gas-solid separation in the secondary cyclone separator (2), it is stored in the fine / light particulate collector (1), and the gas is discharged from the tail air outlet (6).

[0013] The temperature of the secondary and tertiary drying media is 120-300℃, and the flow rate of the secondary or / and tertiary drying media in the settling drying tube (4) is 2-30m / s;

[0014] The temperature of the primary drying medium is less than 300℃;

[0015] The particle size of the solid particulate material is no greater than 25 mm, and the feeding rate is 3 to 25 kg / h;

[0016] The solid particulate materials mentioned are solid materials such as coal, coal gangue, petroleum coke, grains, and plastics;

[0017] The drying medium is one or more of inert gas, flue gas, coal gas, and air.

[0018] One method involves simultaneous dry cooling, grading, and dust removal; another process is as follows:

[0019] High-temperature materials and primary cooling media enter the cyclone separator (3) through the particle inlet (9) and primary air inlet (8). The primary cooling media forms a rotating upward airflow. Due to centrifugal force, the high-temperature coarse / heavy materials, along with some fine / light materials, move towards the wall of the cyclone separator (3). Because of their large mass, the coarse / heavy materials move / segregate faster than the fine / light materials, and are deposited after colliding and rubbing against the wall. The deposited high-temperature materials fall into the settling cooling tube (4) at a certain initial velocity under the action of gravity. At the same time, secondary cooling media is introduced through the secondary air inlet (10) and / or tertiary cooling media through the tertiary air inlet (11). The particles are classified according to the relative magnitude of the terminal velocity of the particle material and the air velocity of the secondary and / or tertiary cooling media in the settling cooling tube (4). The terminal velocity of the settling high-temperature coarse / heavy material is greater than the air velocity of the cooling medium, and the drag force it experiences is less than its gravity. It accelerates downward and eventually passes through the settling cooling pipe (4) and enters the coarse / heavy particle collector (5). At the same time, the high-temperature coarse / heavy material directly contacts the primary cooling medium for heat exchange in the cyclone separator (3), and directly contacts the secondary and / or tertiary cooling medium for heat exchange during the falling process of the settling cooling pipe (4). The high-temperature material is gradually cooled, and the cooling medium gradually heats up. The cooled solid coarse / heavy material is collected in the coarse / heavy particle collector (5). When the tertiary air is used as the cooling medium, the coarse / heavy material continues to cool down in countercurrent contact with the tertiary cooling medium to enhance the coking effect. The fine / light material carried by the coarse / heavy material has a terminal velocity lower than that of the secondary and / or tertiary cooling media. The drag force it experiences is greater than its gravity. It first decelerates and moves downwards before being blown back into the cyclone separator (3). The remaining fine / light material carried by the primary cooling media is carried by the rising airflow formed by the primary, secondary and / or tertiary quenching media and enters the secondary cyclone separator (2) through the connecting pipe (7). At the same time, the fine / light particles in the secondary cyclone separator (2) are separated from the airflow due to gravity and are cooled by the airflow. Finally, they are captured and stored in the fine / light particle collector (1), and the airflow is discharged from the tail outlet (6).

[0020] The temperature of the high-temperature material is not higher than 900℃, the feeding rate is 3-20kg / h, and the particle size is not greater than 25mm.

[0021] The flow rate of the primary cooling medium is 2.5–20 m / s;

[0022] The flow velocity of the secondary and / or tertiary cooling medium in the settling cooling pipe (4) is 2.5 to 25 m / s;

[0023] The cooling medium is one or more of inert gas, circulating quenching gas and flue gas, and the temperature is not higher than 150°C;

[0024] The solid products are coal coke, activated carbon, plastics, etc.; furthermore, the method of simultaneous dry cooling, grading and dust removal is applicable to the cooling, grading and dust removal of solid materials in solid products in chemical production.

[0025] This invention integrates particle grading and drying processes, as well as particle dry cooling, grading, and dust removal processes into a single device. By adjusting the gas velocity and temperature at different inlet positions, the degree of drying for materials of different particle sizes can be individually controlled. This enables effective dry cooling of solid materials, material grading, and effective removal of carried dust. The device effectively reduces the localized impact force of high-temperature materials on the device walls, prevents erosion of the device by high-temperature gases, and effectively extends the device's service life. Simultaneously, the gas consumption is small and recyclable, effectively reducing operating costs and ensuring energy efficiency and safety. This method offers high drying and grading efficiency, high cooling, dust removal, and grading efficiency, low dust content in the cooling medium allowing for effective recycling, simple operation, and flexible controllable operation. Attached Figure Description

[0026] Figure 1 This is a schematic diagram of the device structure of the present invention, which is provided with a primary air inlet and a particle inlet.

[0027] Figure 2 This is a schematic diagram of the device structure of the present invention, where the primary air inlet and the particle inlet are the same.

[0028] In the picture:

[0029] 1. Fine / light particle collector; 2. Two-stage cyclone separator; 3. Type III cyclone separator;

[0030] 4. Settling dryer / cooling pipe; 5. Coarse / heavy particle collector; 6. Tail air outlet; 7. Connecting pipe; 8. Primary air inlet;

[0031] 9. Particle inlet; 10. Secondary air inlet; 11. Tertiary air inlet. Detailed Implementation

[0032] The present invention will be described in detail below with reference to the technical solutions and accompanying drawings through embodiments.

[0033] Example 1

[0034] This invention utilizes the appendix Figure 1 The apparatus shown is used for coal grading and drying. The apparatus has a separate primary air inlet (8) and a particle inlet (9). Coal with a particle size less than 10 mm and a moisture content of 15% falls into the cyclone separator (3) through the particle inlet (9) at a certain feeding rate. Flue gas at a certain temperature enters the cyclone separator (3) tangentially from the primary air inlet (8) at a certain speed. At this time, the coal is dispersed under the action of the flue gas, and simultaneously, due to centrifugal force, the coal collides and rubs against the wall of the cyclone separator (3) and settles. Large coal particles, carrying some small particles, fall into the settling and drying tube (4) under gravity. During the descent of the settling drying tube (4), the coal particles are in direct contact with the flue gas at a certain temperature and velocity input through the secondary air inlet (10), and are gradually heated to remove moisture. The preheated and dried large-diameter coal particles fall into the coarse / heavy particle collector (5); while the entrained small-diameter coal particles are blown back to the cyclone separator (3) by the flue gas. They enter the secondary cyclone separator (2) under the combined influence of the primary and secondary drying media, where gas-solid separation occurs, and the small-diameter coal particles fall into the fine / light particle collector (1). In this process, the particles are gradually heated and dried by contact with the airflow, and the dried waste flue gas is discharged from the tail air outlet (6). The discharged waste flue gas is recycled after heat recovery, or it can be used directly as a medium for dry quenching. The volume fractions of each component in the dried flue gas are: 3% O2, 73% N2, and 24% CO2. The drying results are shown in Table 1.

[0035] Example 2

[0036] This invention utilizes the appendix Figure 2The apparatus shown performs coal grading and drying. At this time, the primary air inlet (8) and the particle inlet (9) of the apparatus are the same inlet. Coal with a particle size of less than 25 mm and a moisture content of 20% enters the cyclone separator (3) tangentially from the same inlet (9) and primary air inlet (8) at a certain feeding rate and at a certain speed with ambient temperature flue gas. At this time, the coal is pre-dried and dispersed under the action of the primary drying medium. At the same time, due to the centrifugal force, the coal collides and rubs against the wall of the cyclone separator (3) and is deposited. Large coal particles, along with some small particles, fall into the settling and drying tube (4) under the action of gravity. During the descent of the settling drying tube (4), the coal particles are in direct contact with the flue gas at a certain speed and temperature input through the secondary air inlet (9), and are gradually heated to remove moisture. The preheated and dried large-diameter coal particles fall into the coarse / heavy particle collector (5). At the same time, a certain amount of tertiary drying medium is input into the tertiary air inlet (11) at the bottom of the coarse / heavy particle collector (5), so that the coarse / heavy particles from the settling drying tube (4) continue to be in contact with the drying flue gas in the coarse / heavy particle collector (5), extending the drying time. The small coal particles entrained are blown back to the cyclone separator (3) by the flue gas, and under the combined carry of the primary and secondary drying media, they enter the secondary cyclone separator (2), and after gas-solid separation, the small-diameter coal particles fall into the fine / light particle collector (1). In this process, the particles are gradually heated and dried by contact with the airflow, and the dried waste flue gas is discharged from the tail air outlet (6). The discharged waste flue gas can be recycled after heat recovery, or it can be used directly as a medium for dry quenching. The volume fractions of each component in the dried flue gas were: 3% O2, 73% N2, and 24% CO2. The drying results are shown in Table 1.

[0037] Example 3

[0038] Using the attached Figure 1The device shown simultaneously performs dry quenching, dust removal, and classification of semi-coke. The device has separate primary air inlet (8) and particle inlet (9). Semi-coke with a particle size less than 25mm at a certain temperature, of which coke powder less than 0.5mm accounts for 8% of the mass, falls from the particle inlet (9) into the cyclone separator (3) at a certain feed rate. At room temperature, N2 is tangentially input into the cyclone separator (3) from the primary air inlet (8) at a certain gas velocity. At this time, the semi-coke and dust are pre-cooled and dispersed under the action of the primary air as the quenching medium, and fall into the settling cooling pipe (4). During the descent of the settling cooling pipe (4), it comes into direct contact with the secondary quenching medium input from the secondary air inlet (10) at a certain gas velocity. The classified and cooled large particles of semi-coke greater than 6mm enter the coarse / heavy particle collector (5). The coke powder and semi-coke smaller than 6 mm are blown back to the cyclone separator (3) by the secondary quenching medium. They are carried by the upward airflow formed by the primary quenching medium and enter the secondary cyclone separator (2) through the connecting pipe (7). In the secondary cyclone separator (2), the semi-coke smaller than 6 mm is separated from the airflow and cooled, and finally stored in the fine / light particle collector (1). The quenching gas carrying coke powder is discharged from the tail air outlet (6). The discharged quenching medium can be used as a drying medium for raw coal. The quenching results are shown in Table 2.

[0039] Example 4

[0040] Using the attached Figure 2 The device shown simultaneously performs dry quenching, dust removal, and classification of semi-coke. At this time, the primary air inlet (8) and particle inlet (9) of the device are the same inlet. At a certain temperature, semi-coke with a particle size of less than 13 mm, of which coke powder with a mass ratio of less than 0.1 mm accounts for 10%, is tangentially fed into the cyclone separator (3) from the same inlet (9) and (8) at a certain feed rate under the carrying of flue gas at a certain gas velocity. At this time, the semi-coke and dust are pre-cooled and dispersed under the action of primary air as the quenching medium, and fall into the settling cooling tube (4). During the descent of the settling cooling pipe (4), a certain amount of ambient temperature quenching medium input from the secondary air inlet (10) is directly contacted and gradually cooled. The semi-coke particles larger than 6 mm that are classified and cooled enter the coarse / heavy particle collector (5), and a certain amount of quenching medium is input from the tertiary air inlet (11), so that the secondary and tertiary air form a certain graded air velocity in the settling cooling pipe (4). Meanwhile, the coke powder smaller than 0.1 mm and the semi-coke smaller than 6 mm are blown back to the cyclone separator (3) by the secondary quenching gas, and together with the upward airflow formed by the primary quenching medium, they enter the secondary cyclone separator (2) through the connecting pipe (7). In the secondary cyclone separator (2), the semi-coke airflow smaller than 6 mm is separated and cooled and remains in the fine / light particle collector (1), while the quenching gas carrying coke powder smaller than 0.1 mm is discharged from the tail air outlet (6). The discharged quenching medium can be used as a drying medium for raw coal. The quenching results are shown in Table 2.

[0041] As can be seen from the above embodiments, by using the integrated dry quenching, dust removal and grading device, the semi-coke can be cooled effectively, the dust carried by the quenching medium can be effectively removed, the load on the subsequent grader can be reduced, the high-temperature quenching gas can be recycled, and the particle size of the semi-coke can be flexibly adjusted by changing the gas velocity of the quenching medium to meet the needs of different processes.

[0042] Table 1 Grading and drying effects of different embodiments

[0043]

[0044] Table 2. Coke quenching, grading, and dust removal effects of different embodiments.

[0045]

Claims

1. A grading, drying and dry cooling device, characterized in that: The invention comprises a fine / light particle collector (1), a secondary cyclone separator (2), a quasi-cyclone separator (3), a settling drying / cooling pipe (4) and a coarse / heavy particle collector (5); the fine / light particle collector (1) and the secondary cyclone separator (2) are connected and integrated into one body, and an exhaust gas outlet (6) inserted into the secondary cyclone separator (2) is arranged at the top center thereof; the secondary cyclone separator (2) is connected to the quasi-cyclone separator (3) via a connecting pipe (7); the quasi-cyclone separator (3) is connected to the cyclone separator (3) via a connecting pipe (7); The separator (3) is composed of a cylindrical portion, an upper conical portion and a lower conical portion. A primary air inlet (8) is tangentially arranged on the cylindrical portion, a particle inlet (9) is arranged on the upper portion of the cylindrical portion, the upper conical portion is connected to a connecting pipe (7), and the lower conical portion is connected to the upper portion of a settling drying / cooling pipe (4); the lower portion of the settling drying / cooling pipe (4) is connected to the upper portion of a coarse / heavy particle collector (5); a secondary air inlet (10) is arranged on the lower portion of the settling drying / cooling pipe (4) or on the upper side of the coarse / heavy particle collector (5); The particle inlet (9) is a vertical or inclined input port, and the primary air inlet (8) is arranged below the particle inlet (9).

2. The grading, drying and dry cooling device according to claim 1, characterized in that: The diameter ratio of the cylindrical part of the primary cyclone separator (3) to the settling drying / cooling pipe (4) is 8:1 to 2:1; the height-to-diameter ratio of the settling drying / cooling pipe (4) is 20:1 to 5:

1.

3. The grading, drying and dry cooling device according to claim 2, characterized in that: A tertiary air inlet (11) is arranged at the lower side of the coarse / heavy particle collector (5).

4. A method for synchronously performing classification and drying according to any one of claims 1 to 3, characterized in that: After the mixed granular material and the primary drying medium enter the cyclone-like separator (3) through the granular inlet (9) and the primary air inlet (8), the primary drying medium forms a rotating upward airflow, and the granular material gradually moves toward the wall of the cyclone-like separator (3) due to the centrifugal force; the coarse / heavy granular material has a large mass, and the moving / segregation speed is greater than that of the fine / light granular material, so that the coarse / heavy granular material carries part of the fine / light granular material and collides and rubs against the wall and then deposits, and the deposited granular material falls into the sedimentation drying tube (4) at a certain initial speed under the action of gravity; at the same time, the secondary drying medium or / and the secondary air inlet (10) inputs a certain temperature. A tertiary drying medium of a certain temperature is inputted through the tertiary air inlet (11), and the secondary air and the tertiary air are also used as classification air at this time; the particle classification is realized according to the relative size of the terminal velocity of the particle material and the drying medium gas velocity formed by the secondary drying medium and / or the tertiary drying medium in the settling drying tube (4); when the terminal velocity of the settled coarse / heavy particle material is greater than the gas velocity of the drying medium, the drag force it receives is less than the gravity, and it accelerates downward movement and finally passes through the settling drying tube (4) into the coarse / heavy particle collector (5); at the same time, the coarse / heavy particle material directly contacts with the primary air for heat exchange in the cyclone-like separator (3), and in the settling drying tube (4) During the descent process, the coarse / heavy particle material is directly contacted with the drying medium input from the upper end of the coarse / heavy particle collector (5) for heat exchange, and the particle material is gradually preheated and its moisture is gradually removed; when the tertiary drying medium is input from the tertiary air inlet (11), the coarse / heavy particle material and the tertiary drying medium are in countercurrent contact in the coarse / heavy particle collector (5) and continue to heat up, so as to prolong the contact time between the large particles and the drying medium, effectively control the moisture content of the large particles, and finally the coarse / heavy particles that meet the drying requirements are stored in the coarse / heavy particle collector (5); at this time, the particle size of the coarse / heavy particles is large, and the tertiary drying medium can smoothly pass through the particles formed in the coarse / heavy particle collector (5). The bed layer is formed, and the pressure fluctuation of the device is small; the terminal velocity of the entrained fine / light particle material is lower than the velocity of the drying medium, and the drag force it receives is greater than the gravity, so it first decelerates and moves downward and is then blown back to the cyclone-like separator (3), and the fine / light particle material carried by the primary air is carried by the rising airflow formed by the primary, secondary and / or tertiary drying media through the connecting pipe (7) and enters the secondary cyclone separator (2); at the same time, the fine / light particle material contacts the airflow for heat exchange, and its moisture is gradually removed. After gas-solid separation in the secondary cyclone separator (2), it is stored in the fine / light particle collector (1), and the airflow is discharged from the tail air outlet (6); The temperature of the secondary and tertiary drying medium is 120-300° C., and the flow rate of the secondary and / or tertiary drying medium in the sedimentation drying tube (4) is 2-30 m / s; The temperature of the primary drying medium is less than 300°C.

5. The synchronous classification and drying method according to claim 4, characterized in that: The particle size of the solid particulate material is not greater than 25 mm, and the feed rate is 3 to 25 kg / h.

6. The synchronous classification and drying method according to claim 4, characterized in that: The solid particulate materials are coal, coal gangue, petroleum coke, grains, and plastics; the drying medium is one or more of inert gas, flue gas, coal gas, and air.

7. A method for synchronous dry cooling, classification and dust removal according to any one of claims 1 to 3, characterized in that: The high-temperature material and the primary cooling medium enter the cyclone-like separator (3) through the particle inlet (9) and the primary air inlet (8), and the primary cooling medium forms a rotating upward airflow. Due to the centrifugal force, the high-temperature coarse / heavy material carries part of the fine / light material and moves toward the wall of the cyclone-like separator (3). The coarse / heavy material has a larger mass and a moving / segregating speed than the fine / light material, so it collides and rubs against the wall and then deposits. The deposited high-temperature material falls into the sedimentation cooling tube (4) at a certain initial speed under the action of gravity. At the same time, the secondary cooling medium is input into the secondary air inlet (10) or / and the tertiary cooling medium is input into the tertiary air inlet (11). The particles are classified according to the relative size of the terminal velocity of the particle material and the gas velocity of the secondary and / or tertiary cooling medium in the sedimentation cooling tube (4). The terminal velocity of the settled high-temperature coarse / heavy material is greater than the gas velocity of the cooling medium, and the drag force it receives is less than the gravity. It accelerates downward and finally passes through the sedimentation cooling tube (4) and enters the coarse / heavy particle collector (5). At the same time, the high-temperature coarse / heavy material in the cyclone-like separator (3) and the primary cooling medium The medium directly contacts the heat exchanger, and the medium directly contacts the heat exchanger with the secondary and / or tertiary cooling medium during the falling process of the settling cooling pipe (4), the high-temperature material is gradually cooled, the cooling medium gradually heats up, and the cooled solid coarse / heavy material is collected in the coarse / heavy particle collector (5); when the tertiary air is input as the cooling medium, the coarse / heavy material contacts the tertiary cooling medium in countercurrent to continue cooling, so as to enhance the quenching effect; and the terminal velocity of the fine / light material entrained by the coarse / heavy material is lower than the velocity of the secondary and / or tertiary cooling medium, and the drag force is greater than the gravity, so the coarse / heavy material first decelerates and moves downward and is then blown back to the cyclone-like separator (3), and the remaining fine / light material carried by the primary cooling medium is carried by the rising airflow formed by the primary, secondary and / or tertiary quenching medium through the connecting pipe (7) and enters the secondary cyclone separator (2); at the same time, the fine / light particle material in the secondary cyclone separator (2) is separated from the airflow due to gravity, and is cooled by the airflow at the same time, and is finally captured and stored in the fine / light particle collector (1), and the airflow is discharged from the tail air outlet (6); The temperature of the high-temperature material is not higher than 900°C, the feed rate is 3-20kg / h, and the particle size is not greater than 25mm; The flow rate of the primary cooling medium is 2.5 to 20 m / s.

8. The method for synchronous dry cooling, classification and dust removal according to claim 7, characterized in that: The flow rate of the secondary and / or tertiary cooling medium in the sedimentation cooling pipe (4) is 2.5-25 m / s.

9. The method for synchronous dry cooling, classification and dust removal according to claim 7, characterized in that: The cooling medium is one or more of inert gas, circulating coke quenching gas and flue gas, and the temperature is not higher than 150°C; the solid material is coal tar, activated carbon and plastic.

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