Classification and pulverization high efficiency drying system of water-containing material

Abstract

The application discloses a kind of dry sludge equipment, including pulverization drying unit;Pulverization drying unit includes pulverization device, drying device, pulverization device is communicated with drying device each other;Wherein, pulverization device includes pulverization shell, feed inlet, main shaft and impeller, main shaft and impeller are arranged in pulverization shell, impeller can rotate around main shaft;Feed inlet is opened on the sidewall in pulverization shell, the sidewall of the pulverization shell where feed inlet is arranged intersects with main shaft or main shaft prolongation line, and there is gap between the outer peripheral end of impeller and the wall of shell.The moisture is efficiently and deeply dried sludge without phase change.The sludge is classified, pulverized and dried, and the moisture is removed by liquid centrifugal separation and non-full phase change during the pulverization and drying process.

Description

[0001] This application is a divisional application of Chinese Patent Application No. 202310165912.3, filed on February 27, 2023, entitled "Classified Powdering and Efficient Drying System for Water-containing Material". TECHNICAL FIELD

[0002] The present application relates to a sludge drying device, in particular, to a classified powdering and drying device for deep drying of sludge, belonging to the field of sludge treatment. BACKGROUND

[0003] With the increasing production of urban sewage, the number of sewage treatment facilities also increases accordingly, and the production of by-products of sewage treatment, i.e., residual sludge, also increases. How to properly handle and dispose of these continuously generated and increasingly large amounts of sludge has become a problem that needs to be solved in environmental protection in China. The residual sludge generally has a moisture content of more than 80%. Sludge dewatering is a key step in its treatment process. The characteristics of sludge being difficult to dewater deeply have become a bottleneck problem that limits the harmless and resourceful treatment of sludge.

[0004] Filter pressing is a conventional method for dewatering high-moisture materials (such as residual sludge). After filter pressing dewatering, water cannot be completely removed, and there is still a considerable amount of water remaining in the moisture-containing material. This part of the water remaining in the material includes interstitial water, adsorbed water, capillary water, etc., and needs to be further dried to remove it. In the deep drying of moisture-containing materials, the most common way to remove water is evaporation. That is, water is absorbed by heat and evaporated into water vapor, and then the water is separated from the material. The evaporation technology mainly includes thermal drying, heat pump drying, solar drying, and natural ventilation drying. These drying methods have obvious shortcomings in energy consumption or efficiency.

[0005] When water evaporates, it will undergo a phase change process of "heating-vaporization-condensation-liquefaction". The heat absorbed by water heating is 4.2 kJ / kg·℃, and the heat absorbed by 100℃ liquid water vaporization under standard atmospheric pressure is 2260 kJ / kg. These absorbed heat is released as low-grade waste heat when water condenses, which is difficult to be efficiently recovered and utilized. Therefore, thermal drying and heat pump drying technologies have high energy consumption and are difficult to be effectively optimized for energy saving. In solar drying and natural ventilation drying, heat is derived from nature, without active energy supply, and has the characteristics of low-energy drying. However, the amount of heat that can be provided by solar energy and natural wind is limited, and the drying speed is much slower than that of thermal drying and heat pump drying, resulting in the shortcoming of slow drying speed and low efficiency. SUMMARY

[0006] One objective of this application is to efficiently and deeply dry sludge at ambient temperature. The sludge is graded, pulverized, and dried. During the pulverization and drying process, water is removed through centrifugal separation via liquefaction, resulting in a non-total phase change of water.

[0007] The deep drying of sludge described in this application can also be applied to the efficient and deep drying of other water-containing materials. A sludge drying device includes a pulverizing and drying unit; the pulverizing and drying unit includes a pulverizing device and a drying device, which are interconnected; wherein, the pulverizing device includes a pulverizing shell, a feed inlet, a main shaft, and an impeller, the main shaft and impeller being disposed within the pulverizing shell, and the impeller being rotatable around the main shaft; the feed inlet is located on the side wall inside the pulverizing shell, the side wall of the pulverizing shell where the feed inlet is located intersects with the main shaft or its extension line, and there is a gap between the outer peripheral end of the impeller and the wall of the shell.

[0008] After crushed material (such as sludge) enters the pulverizing shell through the feed inlet, the centrifugal force generated by the rotating impeller drives the crushed material to move towards the shell wall and collide with it, pulverizing the crushed material into finer particles. This process fully exposes the moisture in the material, weakens the binding strength between the ultrafine particles, and facilitates the separation of water and solid matter in the subsequent drying process, thus improving the efficiency of sludge drying. Attached Figure Description

[0009] Figure 1 A schematic diagram of one embodiment of the sludge drying equipment of this application.

[0010] Figure 2 A schematic diagram of one embodiment of the pulverizing and drying unit of this application.

[0011] Figure 3 , Figure 2 Schematic diagram of the CC cross-sectional structure within the pulverization and drying unit

[0012] Figure 4 A schematic diagram of one embodiment of the pulverizing and drying unit of this application.

[0013] Figure 5 , Figure 2 A partial enlarged view of the pulverizing device

[0014] Figure 6 , Figure 4 A partial enlarged view of the pulverizing device

[0015] Figure 7 A schematic diagram of one embodiment of the crushing unit of this application.

[0016] Figure 8 , Figure 2 A partial enlarged view of the drying device

[0017] Figure 9 , Figure 2 schematic view of the D-D cross-sectional structure inside the pulverizing-drying unit of

[0018] Figure 10 , Figure 2 schematic view of the E-E cross-sectional structure inside the pulverizing-drying unit of

[0019] Figure 11 , Figure 2 side view of the drying device of

[0020] Figure 12 , Figure 2 top view of the drying device of

[0021] Figure 13 schematic view of the structure of the gas-solid separation unit of the present application

[0022] Figure 14 schematic view of the structure of one embodiment of the device for water phase change of the present application

[0023] Figure 15 schematic view of the structure of the finished product distribution-re-mixing unit of the present application DETAILED DESCRIPTION

[0024] The equipment for drying sludge of the present application is described in further detail below. The present application is not limited by the specific details which are set forth in the description and claims. Certain specific details are provided for the purpose of providing a thorough understanding of the various embodiments disclosed. However, one skilled in the relevant art will recognize that embodiments can be practiced without one or more of the specific details or with other methods, components, materials, etc.

[0025] Unless the context clearly requires otherwise, throughout the description and the claims, the words "comprise," "comprising," and the like are to be construed in an open, inclusive sense, as

[0026] Reference throughout this specification to "an embodiment", "one embodiment", "another embodiment", or "certain embodiments" means that a described feature, structure, or characteristic being described in connection with the embodiment is included in at least one embodiment. Therefore, the appearances of the phrases "an embodiment", "one embodiment", "another embodiment", or "certain embodiments" in various places throughout this specification are not necessarily referring to the same embodiment. Furthermore, the particular features, structures, or characteristics can be combined in any suitable manner on one or more embodiments. It will be apparent to those skilled in the art that various features or aspects of the disclosed embodiments can be expressed differently, but equally effectively. Therefore, the disclosure is intended to be

[0027] The up, down, left, right, front and back orientation terms in the present application file are established based on the positional relationship shown in the drawings. Different drawings may change the corresponding positional relationship, so it cannot be understood as a limitation on the scope of protection.

[0028] The sludge drying device of the present application can be used as a solid-liquid separation device in other fields, especially in the treatment of coal slime, drug residues and other water-containing materials. The above-mentioned materials have sufficient crushability at a certain moisture content, and it is difficult to use conventional methods for deep solid-liquid separation or the energy consumption is high. The use of the solid-liquid separation device of the present application can well achieve deep drying. Specifically, at ambient temperature, that is, without providing additional heat source to the solid-liquid separation device of the present application, deep drying of the water-containing material can be achieved.

[0029] The primary goal of sludge drying is water removal, not the form of water removal. The phase change of liquid water to water vapor is not the only way to remove water. The present application proposes a high-efficiency drying system for graded pulverization of water-containing materials (such as sludge), which is a deep drying device system with non-full phase change of water removal. Through the two action mechanisms of liquid centrifugal separation of water and water evaporation without additional energy consumption, the ambient temperature deep and efficient drying of water-containing materials (such as sludge) is realized, while taking into account low energy consumption and high efficiency.

[0030] A sludge drying device, comprising a pulverization and drying unit; the pulverization and drying unit comprises a pulverization device and a drying device, and the pulverization device and the drying device are in communication with each other; wherein the pulverization device comprises a pulverization shell, a feed inlet, a main shaft and an impeller, the main shaft and the impeller are arranged in the pulverization shell, and the impeller can rotate around the main shaft; the feed inlet is arranged on the sidewall of the pulverization shell, the sidewall of the pulverization shell where the feed inlet is arranged intersects with the main shaft or the extension line of the main shaft, and there is a gap between the outer peripheral end of the impeller and the wall of the shell.

[0031] The sludge drying device can also be a solid-liquid separation device for other water-containing materials. A solid-liquid separation device, comprising a pulverization and drying unit; the pulverization and drying unit comprises a pulverization device and a drying device, and the pulverization device and the drying device are in communication with each other; wherein the pulverization device comprises a pulverization shell, a feed inlet, a main shaft and an impeller, the main shaft and the impeller are arranged in the pulverization shell, and the impeller can rotate around the main shaft; the feed inlet is arranged on the sidewall of the pulverization shell, the sidewall of the pulverization shell where the feed inlet is arranged intersects with the main shaft or the extension line of the main shaft, and there is a gap between the outer peripheral end of the impeller and the wall of the shell.

[0032] The impeller comprises blades, which can be directly fixed on the main shaft or connected in other ways.

[0033] The pulverization device

[0034] In some embodiments, the cross-sectional area of the pulverizing shell perpendicular to the main axis is variable along the main axis direction, and the cross-sectional area of the side wall with the feeding port is the smallest.

[0035] Preferably, the cross-sectional area of the pulverizing shell perpendicular to the main axis gradually increases along the main axis direction from the side wall with the feeding port.

[0036] More preferably, the cross-sectional shape of the pulverizing shell perpendicular to the main axis is circular, i.e., the pulverizing shell is in the shape of a circular truncated cone.

[0037] In some embodiments, the pulverizing shell is in the shape of a circular truncated cone, and annular ribs are arranged on the inner wall of the circumferential wall of the pulverizing shell. In the main axis direction, the annular ribs are arranged on the inner wall of the pulverizing shell between adjacent impellers.

[0038] In the main axis direction, one annular rib can be arranged between every two pulverizing blades. Alternatively, one annular rib can be arranged between every 1-n pulverizing blades, i.e., two or more impellers are arranged in the space between two annular ribs.

[0039] The cross-sectional shape of the annular rib can be triangular, trapezoidal, or circular arc, or other irregular shapes.

[0040] In some embodiments, the maximum length of the annular rib in the radial direction within the pulverizing shell is greater than the distance between the pulverizing blade and the inner wall of the pulverizing shell.

[0041] In this way, the annular rib functions to separate the pulverizing area within the pulverizing shell, increases the pulverizing time, and lowers the particle size of the pulverized material.

[0042] In some embodiments, the main axis within the pulverizing shell is parallel to the horizontal direction. In the vertical direction, the feeding port is arranged above the main axis.

[0043] Through the above-mentioned arrangement of the cross-section of the shell, the cross-sectional area perpendicular to the main axis is relatively small near the feeding port, and the corresponding impeller diameter is also relatively small, resulting in a relatively low linear velocity. In turn, the reaction force generated on the material input into the feeding port is small, ensuring smooth entry of the material into the pulverizing shell. As the cross-sectional area of the pulverizing shell increases, the corresponding impeller diameter can also be set to be larger, resulting in a larger linear velocity, which can increase the degree of collision between the material and the inner wall of the shell and improve the pulverizing efficiency.

[0044] A plurality of impellers are arranged along the main axis direction. Each impeller includes 2-8 pulverizing blades arranged uniformly. Preferably, the pulverizing blades are arranged uniformly around the main axis.

[0045] In some embodiments, the blade strip is in the shape of a strip, and in the horizontal direction, the distal end of the blade away from the main axis is arranged obliquely.

[0046] The inclination direction of the blade tip is basically consistent with the inclination of the shell wall of the pulverizing shell. In this way, the distance between the blade tip and the inner wall of the conical cylindrical shell is basically kept consistent, or the change is controlled within a small range.

[0047] Preferably, the distance between the blade tip and the inner wall of the pulverizing shell is controlled within 0.5-5 cm.

[0048] In some embodiments, the pulverizing blade is in a strip shape, and the angle between the pulverizing blade and the axial direction of the main shaft is greater than 0° and less than or equal to 10°.

[0049] The pulverizing blade slightly deviates from the axial direction, which can push the material to move in the direction of the principle inlet.

[0050] The strip-shaped pulverizing blade is vertically fixed on the main shaft, and the direction from the first side edge of the pulverizing blade to the second side edge is the direction of material pushing. The second side edge deviates from the axis of the first side edge by an angle in the direction opposite to the rotation direction of the pulverizing blade, and the angle is greater than 0° and less than or equal to 10°.

[0051] Preferably, the angle between the pulverizing blade and the axial direction of the main shaft is the same at the same cross section.

[0052] As a preferred solution, the pulverizing shell of the present application is in a circular truncated cone structure, including a first end face, a second end face, and a peripheral wall. The area of the first end face is smaller than that of the second end face. The main shaft is arranged along the center line of the circular truncated cone pulverizing shell, and the inlet is arranged on the first end face of the pulverizing shell and above the main shaft.

[0053] During pulverization, the material enters the pulverizing device from the first end face and is discharged from the second end face or the peripheral wall close to the second end face.

[0054] In the pulverizing device, the blade rotates at high speed to crush the particles to be dried into superfine powder particles. The interstitial water, adsorbed water, and capillary water in the superfine powder particles are fully exposed and migrate to the surface of the superfine powder particles. The combination state of the water and the superfine powder particles changes, the combination strength is weakened, and the surface water with weak combination strength with the superfine powder particles is formed.

[0055] Structure of the drying device.

[0056] The drying device includes a drying shell, an air inlet, a discharge outlet, a main shaft, and an impeller. The main shaft and the impeller are arranged in the drying shell, and the impeller can rotate around the main shaft. The air inlet and the discharge outlet are arranged on the shell wall of the drying shell.

[0057] The air inlet and the discharge outlet are arranged on the wall of the drying shell close to the two ends of the main shaft.

[0058] Preferably, the drying shell is a cylindrical structure. That is, the cross section is a circle with equal radius. The drying shell includes a first end and a second end, the first end is close to the air inlet, and the second end is close to the discharge outlet.

[0059] In some embodiments, a guide groove is arranged on the inner wall of the drying shell, the main shaft is substantially parallel to the horizontal direction, and the guide groove is arranged on the inner wall of the drying shell above the main shaft.

[0060] The guide groove extends along the circumferential direction of the inner wall of the drying shell, and the angle between the guide groove and the drying main shaft is 60-88° (direction: from the front end feeding end to the tail end discharging end) on the top projection plane.

[0061] In the rotation direction of the impeller, the drying blade of the impeller first passes through the first end of the guide groove, and then passes through the second end of the drying blade, and the distance between the first end of the guide groove and the side wall provided with the air inlet is less than the distance between the second end and the side wall provided with the air inlet.

[0062] In some embodiments, a guide groove is arranged on the inner wall of the drying shell above the main shaft, at least on the inner wall of the first half in the feeding direction.

[0063] The cross-sectional area of the guide groove can be trapezoidal, triangular, or circular arc-shaped.

[0064] In some embodiments, a partition ring is arranged on the inner wall of the circumferential wall of the drying shell along the circumferential direction. In the extension direction of the main shaft, the partition ring is arranged on the inner wall of the drying shell between adjacent impellers.

[0065] In the circumferential direction of the drying shell, the partition ring is arranged on the inner wall of the drying shell at least on more than 1 / 3 of the circumference. Preferably, the partition ring is symmetrically arranged with respect to the vertical plane passing through the main shaft.

[0066] In some embodiments, a guide vane is arranged on the same cross section as the partition ring, and the partition ring surface includes an inclined surface facing the first end of the drying shell. In other words, the cross section of the partition ring is a polygon with an inclined side facing the first end of the drying shell, such as a trapezoid or a right triangle. In the radial direction from the center of the drying shell to the circumferential wall, the distance between the inclined side of the partition ring and the first end of the drying shell gradually increases.

[0067] In the cross section where the partition ring is located, a guide vane is arranged. The guide vane includes more than 3 guide vanes.

[0068] In some embodiments, the guide vane is in the shape of a strip, the first end of the guide vane is fixed in the axial direction, and the second end opposite to the first end is inclined.

[0069] The inclination direction of the second end of the guide vane is consistent with the inclination direction of the inclined side of the partition ring. In this way, the distance between the end edge of the guide vane and the inclined side of the partition ring is substantially consistent, or the distance is controlled within a small range of variation.

[0070] Preferably, the distance between the second end of the guide vane and the inclined side of the partition ring is controlled to be 1.0 cm-8.0 cm.

[0071] In some embodiments, the guide vane is in a strip shape, and the included angle between the guide vane and the main shaft is greater than 0° and less than or equal to 30°.

[0072] The guide vane in a strip shape is vertically fixed on the main shaft, and the direction from the first side to the second side of the guide vane perpendicular to the main shaft is the direction of material pushing. The second side deviates from the axis on which the first side is located by an angle in the direction opposite to the rotation direction of the guide vane, and the angle is greater than 0° and less than or equal to 30°.

[0073] One or more partition rings can be arranged in the axial direction in the drying shell. One or more drying impellers are arranged between adjacent partition rings.

[0074] Through the arrangement of the partition ring and the guide vane, the drying reaction module is formed by the one or more drying impellers, the one partition ring, the one guide vane, and the peripheral wall of the drying shell in which the one or more drying impellers, the one partition ring, and the one guide vane are arranged. The drying device contains one or more drying reaction modules. The material in the drying device is repeatedly subjected to high-frequency impact by the inner wall, and the water is separated.

[0075] Each drying impeller includes a plurality of drying vanes.

[0076] In some embodiments, the drying vane is in a strip shape.

[0077] In some embodiments, the discharge port is arranged on the peripheral wall of the drying shell close to the second end, and the push flow impeller is arranged on the main shaft. In the direction perpendicular to the main shaft, the discharge port and the rotation plane of the push flow impeller at least partially coincide.

[0078] Preferably, the push flow impeller includes a push flow vane in a strip shape, and the length of the push flow vane in the axial direction is less than or equal to the length of the discharge port.

[0079] The dried material is pushed out of the drying device by the push flow impeller along the tangent direction of the rotation of the discharge port. The push flow vane on the push flow impeller is arranged in the axial direction of the drying main shaft and is in a straight line with the axial direction, and the angle between the push flow vane and the axial direction is 0°.

[0080] In some embodiments, a cylindrical extension is arranged on the outer periphery of the discharge port, and the extension is arranged in the tangent direction of the cylindrical drying shell.

[0081] The discharge port can be arranged on the peripheral wall of the cylindrical drying shell near the second end portion at any position in the circumferential direction.

[0082] The drying device and the pulverizing device of the present application can be integrally arranged or separately arranged.

[0083] In one embodiment, the pulverizing device and the drying device are integrated. The second end portion of the pulverizing device is open, the first end portion of the drying device is open, the second end portion of the pulverizing device is connected to the first end portion of the drying device, and the pulverized material directly enters the drying device along the axial direction of the pulverizing spindle and the drying spindle.

[0084] Preferably, the axes of the pulverizing spindle and the drying spindle are on the same line, and the two are connected by a shaft seat. The pulverizing spindle and the drying spindle can be independently rotated.

[0085] In another embodiment, the pulverizing device and the drying device are two independent devices.

[0086] The second end portion of the pulverizing device is closed, and the discharge port is arranged on the peripheral wall of the pulverizing shell near the second end portion. The discharge port is a pipeline in communication with the interior of the pulverizing shell. The discharge port is tangent to the peripheral wall of the shell and extends in the direction of rotation of the pulverizing blade.

[0087] The first end portion of the drying device is closed, and the feeding port is arranged on the peripheral wall of the drying shell near the first end portion. The feeding port is a pipeline in communication with the interior of the drying shell. The feeding port is tangent to the peripheral wall of the drying shell and extends in the direction opposite to the direction of rotation of the drying blade.

[0088] The discharge port of the pulverizing device and the feeding port of the drying device are connected by a pipeline.

[0089] By arranging the rotation direction of the pulverizing blade and the extension direction of the conveying pipe in the same direction, the pulverized material can be discharged from the pulverizing shell under the rotation of the pulverizing blade. By arranging the rotation direction of the pulverizing blade and the extension direction of the conveying pipe in opposite directions, the pulverized material can be brought into the drying shell under the rotation of the drying blade.

[0090] In the drying device of the present application, under the action of high-speed centrifugal stirring, the superfine powder particles are impacted and pushed by the drying blade to make high-speed centrifugal motion in the drying device. Under the action of high-intensity centrifugal acceleration, the water in the superfine powder particles is separated from the superfine powder particles themselves. In addition, the superfine powder particles repeatedly collide with the drying blade and the inner wall of the cylindrical shell in the drying device at high frequency. The superfine powder particles switch between the states of accelerated high-speed motion, collision stop and force receiving, and accelerated high-speed motion again at high frequency. Therefore, the water on the superfine powder particles is separated efficiently by the high acceleration.

[0091] Under the action of the push-flow impeller and the guide groove, the superfine powder particles move from the front end to the rear end of the drying device. The superfine powder particles with reduced moisture content are more likely to pass through the partition ring to the rear end, while the material with high moisture content is intercepted until the moisture content is reduced to the predetermined range. By adjusting the height of the partition ring, the angle of the cross-section bevel, and the range of the circular ring (1 / 3 circle to full circle), the drying effect can be adjusted.

[0092] In the drying device of the present application, the drying blades, the guide blades, and the push-flow blades rotate at high speed to generate a negative pressure air induction effect in the drying device. The external natural air enters the drying device from the air inlet at the first end of the drying shell. The natural air is introduced into the drying device and mixed with the superfine powder particles to generate a convective drying effect. The moisture in the superfine powder particles absorbs heat from the natural air, evaporates into water vapor, and further improves the drying effect.

[0093] The pulverizing and drying unit of the present application can be used in combination with other crushing units and gas-solid separation devices of the prior art.

[0094] Crushing unit

[0095] The equipment for drying sludge of the present application further comprises a crushing unit. The material is first subjected to crushing treatment before entering the pulverizing and drying unit.

[0096] The crushing unit comprises a crushing shell, a main shaft arranged in the crushing shell, and a plate hammer fixed on the main shaft. The main shaft is arranged vertically to the horizontal plane.

[0097] In some embodiments, a plurality of groups of plate hammers are arranged along the extension direction of the main shaft, and each group of plate hammers is spaced apart by a certain distance. Each group of plate hammers rotates around the main shaft on the same horizontal plane.

[0098] The crushing shell is provided with a feed inlet at the top and a discharge outlet at the bottom.

[0099] The crushed material entering the crushing shell through the feed inlet is driven to rotate around the shaft by the main shaft, and the material is crushed by the plate hammer during rotation. The crushed material is discharged from the conical discharge outlet at the lower end.

[0100] In some embodiments, a limiting ring is arranged on the peripheral wall of the crushing shell in the circumferential direction perpendicular to the main shaft. The limiting ring protrudes into the crushing shell, and the limiting ring is arranged close to the lower side of the plate hammer.

[0101] Preferably, in the direction perpendicular to the main shaft, the length of the limiting ring is greater than the distance between the end of the plate hammer and the inside of the shell.

[0102] In this way, the material to be crushed is not directly dropped to the next layer after being hit by the hammer, but is dropped to the limiting ring and bounced back to the hammer, and then repeatedly hit, thereby increasing the crushing effect of each layer of the hammer.

[0103] The crushing shell can be a cylindrical shell. The number of groups of hammers and the number of hammers in each group can be determined according to the properties of the material to be crushed and the degree of crushing.

[0104] The discharge port of the crushing shell is connected to the inlet of the pulverizing device through a pipeline.

[0105] Gas-solid separation unit

[0106] The material after drying (such as dry sludge) is separated into gas and solid by the gas-solid separation unit, significantly reducing the dust content discharged into the atmosphere.

[0107] The gas-solid separation unit includes a cyclone separator, a device for water phase change, and a bag filter, and the device for water phase change is connected to the cyclone separator and the bag filter, respectively.

[0108] The device for water phase change includes a cavity, the upper end of the cavity for water phase change is provided with an air inlet, the lower end of the cavity is provided with an air outlet, and a rotatable blade is arranged at the air inlet.

[0109] The dust-containing wet air discharged from the cyclone separator is mixed with fresh air by stirring with the blade and then enters the cavity. In the cavity, liquid droplets absorb heat from the fresh low-humidity air under the action of unsaturated vapor pressure and convective evaporation, and change from liquid to gas. In this way, the humidity of the dust-containing gas entering the bag filter is reduced, and the occurrence of hardening and blocking during the separation process in the bag filter due to the presence of too much liquid water is prevented as much as possible.

[0110] In some embodiments, the cross-sectional area of the middle part of the cavity for water phase change is greater than the cross-sectional area of the upper and lower ends. Preferably, the device for water phase change includes a plurality of cavities for water phase change that are connected to each other, and a rotatable blade is arranged at the connection between adjacent cavities.

[0111] The device for water phase change includes a plurality of cavities, each cavity is provided with an air inlet at the upper end and an air outlet at the lower end; the air inlet of the cavity is connected to the air outlet of the adjacent cavity above, and a rotatable blade is arranged at the connection. The dust-containing wet air discharged from the cyclone separator is mixed with fresh air through the air inlet of the uppermost cavity and enters the cavity, and is discharged from the device for water phase change through the air outlet of the lowermost cavity.

[0112] The device for water phase change comprises a plurality of cavities connected in series, dust-containing wet air and fresh air are mixed at an air inlet to form mixed air, the mixed air is then moved downward, is mixed uniformly by mixed blades, and enters the cavities for water phase change; the mixed air is subjected to one or more times of mixing-water phase change (mixed by the mixed blades and water phase change in the cavities), and the unsaturated air is used to change liquid water into gaseous water by using the water containing capacity of the unsaturated air, and the relative humidity of the unsaturated air is increased, so that the bag separator can be effectively prevented from being caked and blocked due to the presence of liquid water.

[0113] The cross section of the middle part of the cavity for fusion is circular, rectangular or polygonal.

[0114] The air outlet of the device for water phase change is connected with the inlet of the bag separator.

[0115] The gas-solid separation unit of the application can effectively realize gas-solid separation, and solid particles contained in the gas are effectively removed before the gas is discharged to the atmosphere.

[0116] The gas-solid separation unit of the application can also be used with other pulverization drying devices in the prior art.

[0117] Finished product distribution-return mixing unit

[0118] The material after drying treatment is subjected to gas-solid separation, the gas is discharged, and the separated solid enters the finished product distribution-return mixing unit.

[0119] In another aspect, the method for sludge drying comprises:

[0120] 1) crushing the water-containing sludge into to-be-dried particles with a particle size of ≤5 mm;

[0121] 2) the to-be-dried particles enter a pulverization device, under the rotation of blades in the pulverization device, the to-be-dried particles are impacted and pushed by the blades to make centrifugal motion in the pulverization drying unit, and are differentiated into superfine powder particles;

[0122] 3) the superfine powder particles enter a drying device, and water in the superfine powder particles is evaporated under the action of dry air to obtain dried powder particles;

[0123] 4) the mixture after drying enters a gas-solid separation unit to separate the gas from the solid powder particles;

[0124] 5) the separated solid powder particles meet the drying requirements and are discharged from the solid-liquid separation system; the separated solid powder particles do not meet the drying requirements, and the solid powder particles are mixed with the to-be-dried particles to be subjected to the treatment of steps 2)-4) until the drying requirements are met, and then the sludge drying system is discharged.

[0125] The particle size of the superfine powder particles is within 20-250 μm.

[0126] In some embodiments, the rotation speed of the blade in the pulverizing device is 1000-3000 r / min.

[0127] The rotation speed of the blade in the drying device is 1500-3000 r / min.

[0128] The linear speed of the blade end in the drying device is 15-150 m / s, or ≥15 m / s.

[0129] In the crushing step 1), the rotation speed of the plate hammer is 200-1000 r / min.

[0130] The sludge drying method of the present application can also be used for the solid-liquid separation of other water-containing materials.

[0131] The above rotation speeds can be adjusted according to the properties of the materials and the drying degree requirements.

[0132] The above solid-liquid separation method of the water-containing materials can be performed in the solid-liquid separation system disclosed in the prior art. Preferably, it is operated in the sludge drying device or the solid-liquid separation device of the present application.

[0133] For the residual sludge with a water content of 35%-55%; after the deep drying of the sludge drying device of the present application, the water content of the dried sludge powder is 10%-30%. In the entire pulverization, drying process, etc., no additional heat source is needed, and the sludge can be efficiently and deeply dried at the ambient temperature.

[0134] The sludge drying device of the present application is further described below in combination with the accompanying drawings.

[0135] Referring to the accompanying drawings Figure 1 In one embodiment of the sludge drying device, the crushing unit 1 is connected to the feeding port of the pulverizing and drying unit 2 through the distributor 4-6 of the finished product distribution and back mixing unit 4, the discharging port of the pulverizing and drying unit 2 is connected to the gas-solid separation unit 3, and the gas-solid separation unit 3 is connected to the distribution bin 4-2 of the finished product distribution and back mixing unit 4. The circulating drying material can be realized until the material drying conditions are met.

[0136] In one embodiment, the crushing unit is a vertical structure, as shown in Figure 7 The crushing unit includes a driving motor 1-1, a speed reducer or a speed reduction belt 1-2, a cylindrical shell 1-4, and a crushing rotating shaft 1-5 arranged in the shell 1-4. The driving motor drives the crushing rotating shaft 1-5 to rotate through the speed reducer.

[0137] The upper and lower ends of the cylindrical shell 1-4 are respectively provided with a feeding port 1-3 and a discharging port 1-8. A plurality of plate hammers 1-6 are fixed on a crushing shaft 1-5. The crushing shaft 1-5 is arranged with a plurality of plate hammer groups (for example, 2-6 layers) from top to bottom, each layer of plate hammer group includes 2-8 plate hammers and is basically located at the same horizontal plane. A limiting ring 1-7 is arranged between adjacent two layers of plate hammer groups, close to the lower side of the upper plate hammer 1-6. In the horizontal direction, the width L1 of the limiting ring 1-7 is equal to or slightly greater than the width L2 of the gap between the plate hammer 1-6 and the shell 1-4 (as shown in Figure 8

[0138] The material to be crushed enters the crushing unit 1 through the feeding port 1-3; the driving motor 1-1 rotates and drives the vertical crushing shaft 1-5 to rotate through the speed reducer or speed reduction belt 1-2, and the rotating speed of the shaft is 200-1000r / min; the plate hammer 1-6 fixed on the crushing shaft 1-5 rotates with it; the plate hammer 1-6 rotates and beats the material falling from the feeding port 1-3, and the particle size of the crushed material is (≤10mm); the crushed material is discharged from the conical discharging port 1-8 at the lower end.

[0139] The pulverizing and drying unit 2 is composed of a pulverizing device 2-1 and a drying device 2-2.

[0140] The pulverizing device 2-1 and the drying device 2-2 can be an integral whole, or two independent devices connected through pipelines.

[0141] As shown in Figure 2 , the pulverizing device 2-1 and the drying device 2-2 are an integral whole. As shown in Figure 2 , the front end and the end of each device are from left to right. The rear end of the pulverizing device 2-1 is open, the front end of the drying device 2-2 is open, and the end of the pulverizing device 2-1 is connected with the front end of the drying device 2-2. The pulverized material directly enters the drying device 2-2 along the axial direction of the pulverizing main shaft and the drying main shaft. The shaft centers of the pulverizing main shaft 2-1-5 and the drying main shaft 2-2-3 are on the same straight line, and the two are connected by a shaft seat 2-3 (share the shaft seat 2-3). The shaft seat 2-3 includes a support 2-3-1 and a shaft box 2-3-2 fixed on the support. The support 2-3-1 includes two linear branches, and the cross-sectional view of the support 2-3-1 perpendicular to the pulverizing main shaft is as shown in the accompanying Figure 3 , which can be T-shaped, X-shaped, or vertically intersecting. The shaft box 2-3-2 simultaneously contains the pulverizing main shaft 2-1-5 and the drying main shaft 2-2-3, and ensures that the pulverizing main shaft 2-1-5 and the drying main shaft 2-2-3 rotate independently.

[0142] As shown in the accompanying Figure 4 , the pulverizing device 2-1 and the drying device 2-2 are two independent devices. As shown in Figure 4 ​The front end and the end of each device are shown from left to right. The end of the pulverizing device 2-1 is closed, and the front end of the drying device 2-2 is closed. The pulverizing device 2-1 and the drying device 2-2 are connected by a pipeline.

[0143] The end of the pulverizing device 2-1 is provided with a discharge port 2-1-8 (cross section F-F) at the tangent direction of the rotation of the pulverizing blade 2-1-6, and the front end of the drying device 2-2 is provided with a feed port 2-2-12 (cross section G-G) at the tangent direction opposite to the rotation of the drying blade 2-2-6. The discharge port 2-1-8 is connected to the feed port 2-2-12. The crushed material is pushed out of the pulverizing device 2-1 by the pulverizing blade 2-1-6 in the tangent direction, enters the feed port 2-2-12, and then moves in the drying device under the driving of the drying blade 2-2-6.

[0144] Referring to the drawings Figure 2 ,4,6, the pulverizing device 2-1 comprises a driving motor 2-1-1, a speed reducer 2-1-2, a conical cylindrical shell 2-1-3, a pulverizing main shaft 2-1-5 arranged in the shell, and a pulverizing impeller 2-1-6 on the pulverizing main shaft. The driving motor 2-1-1 drives the pulverizing main shaft to rotate through the speed reducer 2-1-2.

[0145] The conical cylindrical shell 2-1-3 comprises two circular end faces of the front end and the rear end, and a conical side surface connecting the two end faces, wherein the front end face is smaller than the rear end face. The feed port 2-1-4 is arranged at the front end face (cross section B-B) of the conical cylindrical shell 2-1-3 and above the pulverizing main shaft 2-1-5. During pulverizing, the material enters the pulverizing device from the front end and is discharged from the rear end or the side surface close to the rear end.

[0146] At least one pulverizing impeller 2-1-6 is arranged along the pulverizing main shaft, and each pulverizing impeller comprises 2-8 pulverizing blades arranged on the same circumferential surface of the pulverizing main shaft. The end of the pulverizing blade is shaped obliquely, so that the distance between the end edge of the pulverizing blade and the inner wall of the conical cylindrical shell 2-1-3 is consistent, for example, the distance is 0.5-5 cm. The pulverizing blade has a strip-shaped structure, and the size of the three dimensions is: length>width>height, the length is perpendicular to the pulverizing main shaft, the width is along the main shaft, and the thickness of the pulverizing blade is the height. The width direction of the pulverizing blade is arranged along the axial direction of the pulverizing main shaft, and the angle a between the width direction and the axial direction is 0°-10°, preferably greater than 0° (see Figure 5 ).

[0147] As shown in the drawings Figure 2 and Figure 6, the annular protrusions 2-1-7 are arranged on the inner wall of the conical cylindrical shell 2-1-3 between adjacent pulverizing blades. In the axial direction, one annular protrusion can be arranged between every 2 pulverizing blades, or one annular protrusion can be arranged between every 1-n pulverizing blades.

[0148] The shape of the cross section of the annular protrusion is triangular, trapezoidal or circular arc. In the radial direction, the thickness L3 of the annular protrusion 2-1-7 is greater than the spacing L4 between the pulverizing blade 2-1-6 and the inner wall of the conical cylindrical shell 2-1-3 (as shown in Figure 6

[0149] Referring to the accompanying Figure 2 , 4, the drying device 2-2 comprises a driving motor 2-2-1, a speed reducer 2-2-2, a drying main shaft 2-2-3, a cylindrical shell 2-2-4, a drying impeller 2-2-6 arranged in the shell and fixed on the drying main shaft, a guide vane impeller 2-2-7, and a push-flow impeller 2-2-8.

[0150] Each drying impeller 2-2-6, each guide vane impeller 2-2-7, and each push-flow impeller 2-2-8 comprises a plurality of blades, which are strip-shaped structures with the size in three dimensions being long>wide>high.

[0151] Figure 2 As shown in the drawings, the partition ring 2-2-9 is arranged on the inner wall of the shell 2-2-4, and the guide vane impeller 2-2-7 is arranged in the space enclosed by the partition ring, i.e. the guide vane impeller 2-2-7 is arranged in the radial space where the partition ring 2-2-9 is located. The drying impeller 2-2-6 is arranged in the space between the partition ring and the front / terminal end of the shell 2-2-4, and / or the space between adjacent partition rings. The discharge port 2-2-10 is arranged on the peripheral wall close to the terminal end of the shell, the push-flow impeller 2-2-8 is arranged in the radial space where the discharge port 2-2-10 is located, and in the axial direction, the width of the discharge port is greater than the width of the blade of the guide vane impeller.

[0152] As shown in the drawings, Figure 2 The cross section of the partition ring is a right-angled triangle or a right-angled trapezoid, and the hypotenuse of the right-angled triangle or the hypotenuse of the right-angled trapezoid faces the front end of the shell 2-2-4. The partition ring can be freely adjusted between 1 / 3 of a circular ring and a full circular ring as needed (as shown in the drawings Figure 9 As shown in the drawings, Figure 2 , 8, the first end of the guide vane blade is fixed on the main shaft, and the second end opposite to the first end is shaped as an inclined surface, so that the distance from each position of the edge of the second end of the guide vane blade to the inclined surface of the partition ring 2-2-9 is consistent, and the distance is 1-8 cm. The guide vane blade is arranged in the axial direction of the drying main shaft, and the angle c between the guide vane blade and the axial direction is 0°-30°,

[0153] ​One or more drying impellers 2-2-6 are respectively arranged in the space between the front end and the end of the housing 2-2-4 and / or in the space between adjacent dividing rings. Each space constitutes a drying reaction module. The drying device 2-2 contains one or more drying reaction modules.

[0154] The dried material inside the shell 2-2-4 is pushed out of the drying device 2-2 by the impeller 2-2-8 along the tangential direction of rotation through the discharge port 2-2-10.

[0155] The discharge port 2-2-10 is located on the rear side of the cylindrical shell 2-2-4, along the tangent direction of the cylindrical shell 2-2-4. The angle d between the discharge port 2-2-10 and the tangent at the bottom of the rear end of the cylindrical shell 2-2-4 is 0-180° (e.g., ...). Figure 10 ).

[0156] The upper part of the inner wall of the shell 2-2-4 is provided with guide lines 2-2-11, such as Figure 11 As shown in Figure 12.

[0157] Guide lines 2-2-11 are located on the top of the inner wall of the upper half of the shell 2-2-4, along the circumferential direction of the shell. The cross-section of the guide lines consists of trapezoidal, triangular, or arc-shaped ribs. In the axial direction, guide lines 2-2-11 are provided from half the inner wall of shell 2-2-4 to the entire upper half of the shell; no guide lines are provided in the area where the partition ring is located. (On the top projection plane...) Figure 12 As shown), the angle between the guide pattern 2-2-11 and the drying main shaft 2-2-3 is 60-88° (direction: from the front feed end to the tail discharge end). In the rotation direction of the drying impeller, the drying blades of the impeller first pass through the first end of the guide pattern, and then pass through the second end of the drying blades. The distance from the first end of the guide pattern to the front end of the casing is less than the distance from the second end to the front end.

[0158] Similar to the arrangement of the pulverizing blades, the angle b between the drying blades of the drying impeller 2-2-6 and the axial direction of the drying main shaft 2-2-3 is 0-5° (see attached diagram). Figure 8 The distance between the end of the drying impeller and the inner wall of the casing 2-2-4 is 0.5-4cm, and the number of drying blades on each drying impeller is 2-10.

[0159] The air inlet 2-2-5 is located at the upper part of the front end of the cylindrical shell 2-2-4.

[0160] The material processed by the pulverization and drying unit is then separated into gas and solid components by the gas-solid separation unit.

[0161] like Figure 13As shown, the gas-solid separation unit of the present embodiment includes a cyclone separator 3-1, a device for water phase change 3-2, a cloth bag separator 3-3, and an induced draft fan 3-4. The device for water phase change 3-2 is connected to the cyclone separator 3-1 and the cloth bag separator 3-3 respectively, and the induced draft fan 3-4 is connected to the cloth bag separator 3-3.

[0162] The device for water phase change 3-2 includes a cavity 3-2-3, the upper end of the cavity is provided with an air inlet, the lower end of the cavity is provided with an air outlet 3-2-6, and a mixing blade 3-2-4 is arranged at the air inlet, which can rotate in the horizontal direction about the shaft. The air inlet is respectively communicated with a dust-containing wet air inlet 3-2-1 and a fresh air inlet 3-2-2.

[0163] The horizontal cross section of the cavity 3-2-3 is in the shape of small at the top and bottom and large in the middle, the cross section in the middle is circular, rectangular or polygonal, and one or more cavities 3-2-3 are vertically connected in series. For example, Figure 14 As shown, the air inlets or air outlets between adjacent cavities are provided with blades 3-2-4, and the dust-containing wet air inlet 3-2-1 and the fresh air inlet 3-2-2 are located at the top of the uppermost cavity; a fresh air fan 3-2-5 introduces fresh low-humidity air from the fresh air inlet 3-2-2 and combines it with the dust-containing wet air introduced from the dust-containing wet air inlet 3-2-1 to form mixed air. The mixed air then moves downward, enters the cavity 3-2-3 after being mixed uniformly by the mixing blade 3-2-4. In the cavity, the liquid micro-droplets absorb heat from the fresh low-humidity air under the action of the unsaturated vapor pressure and the convective evaporation, and change from liquid to gas, which is the process of water phase change. After the mixed gas undergoes one or more mixing-water phase changes (mixing by the mixing blade 3-2-4 and water phase change in the cavity 3-2-3), the caking and blocking of the cloth bag separator due to the presence of liquid water are effectively prevented.

[0164] The solid after gas-solid separation enters the finished product distribution-return mixing unit for processing.

[0165] The finished product distribution-return mixing unit includes a finished product conveyor 4-1, a finished product distribution bin 4-2, a finished product unloading conveyor 4-3, a finished product return mixing conveyor 4-4, a crushed material conveyor 4-5, a material uniformizer 4-6, and a mixed material conveyor 4-7.

[0166] As shown, Figure 15 The finished product distribution-return mixing unit includes a first conveyor 4-1, a finished product distribution bin 4-2, a second conveyor 4-3, and a third conveyor 4-4, and the first conveyor 4-1, the second conveyor 4-3, and the third conveyor 4-4 are connected to the finished product distribution bin 4-2 respectively.

[0167] The first conveyor 4-1 is used to convey the solid material separated from the gas-solid separation unit to the finished product distribution bin; the second and third conveyors 4-3 and 4-4 are used to output the solid material in the distribution bin.

[0168] In some embodiments, the finished product distribution-recirculation unit further comprises a material homogenizer 4-6 connected to the finished product distribution bin 4-2 through the third conveyor 4-4.

[0169] The finished product distribution-recirculation unit further comprises a fourth conveyor 4-7, and the homogenizer 4-6 is connected to the pulverization-drying unit through the fourth conveyor 4-7. The solid material that does not meet the drying requirement is conveyed to the pulverization-drying unit through the third and fourth conveyors 4-3 and 4-4 and the homogenizer 4-6 for drying treatment, and the cycle is repeated until the drying requirement is met.

[0170] In a preferred embodiment, the finished product distribution bin 4-2 is a cavity for storing the material, and the lower part of the cavity is shaped as two inverted conical bodies, and the lower parts of the two inverted conical bodies are respectively connected to the second conveyor 4-3 and the third conveyor 4-4.

[0171] The dried material is conveyed by the first conveyor 4-1 to the distribution bin 4-2 below the first conveyor 4-1, and the first conveyor 4-1 has two discharge ports 4-1-1 and 4-1-2 below it; the finished product distribution bin 4-2 has two inverted conical storage bins 4-2-1 and 4-2-2. The finished product material discharged from the discharge port 4-1-1 enters the inverted conical storage bin 4-2-1, and then is unloaded and discharged through the second conveyor 4-3. The finished product material discharged from the discharge port 4-1-2 enters the inverted conical storage bin 4-2-2, and then is sent to the homogenizer 4-6 through the third conveyor 4-4; the water-containing material crushed by the crushing unit is sent to the homogenizer 4-6 through the crushed material conveyor 4-5.

[0172] The homogenizer 4-6 comprises a material bin 4-6-1, a stirring motor 4-6-2, and a stirrer 4-6-3; the stirrer is arranged in the material bin, and the stirring motor is connected to the stirrer.

[0173] In some embodiments, the homogenizer 4-6 is connected to the crushing unit through a fifth conveyor 4-5.

[0174] The material crushed by the crushing unit and the material in the finished product distribution bin are mixed uniformly in the homogenizer, and the mixed material is conveyed from the fourth conveyor 4-7 to the feed port 2-1-4 of the pulverization-drying unit, and then enters the drying system for drying treatment.

[0175] Experimental Example 1

[0176] In this experimental example, sludge is dried in the drying device shown in FIG. 1. Figure 1 The drying device is used to dry the sludge.

[0177] The sludge with water content of 54.5% is broken into to-be-dried particles with particle size ≤5 mm; the to-be-dried particles enter the pulverizing device, under the rotation of the blade in the pulverizing device at 2500 r / min, the to-be-dried particles are impacted and pushed by the blade to make centrifugal motion in the pulverizing and drying unit, and are differentiated into superfine powder particles with particle size in the range of 20-250 μm; the superfine powder particles enter the drying device, under the action of dry air, the 2500 r / min of the blade, the separated moisture is evaporated, and dried powder particles are obtained; the mixture after drying enters the gas-solid separation unit to separate the gas from the solid powder particles, and the water content of the finally separated solid powder particles is 26.3%.

Claims

1. A device for drying sludge, comprising a pulverizing and drying unit and a gas-solid separation unit; the pulverizing and drying unit includes a pulverizing device and a drying device, the pulverizing device and the drying device being interconnected; the gas-solid separation unit is connected to the drying device; wherein, The pulverizing device includes a truncated cone-shaped pulverizing shell. The area of ​​the first end face of the pulverizing shell is smaller than the area of ​​the second end face. The pulverizing main shaft is arranged along the center line of the truncated cone-shaped pulverizing shell. The pulverizing feed inlet is arranged on the first end face of the pulverizing shell and is located above the pulverizing main shaft. The drying device includes: a cylindrical drying shell, a drying air inlet, a drying discharge outlet, a drying main shaft, and a drying impeller. The drying main shaft and the drying impeller are located inside the drying shell. The drying main shaft is basically parallel to the horizontal direction, and the drying impeller can rotate around the drying main shaft. The drying air inlet and the drying discharge outlet are located on the shell wall of the drying shell near both ends of the drying main shaft. The first end of the drying shell is close to the air inlet, and the second end is close to the drying outlet. Guide lines are provided on the inner wall of the drying shell. The guide lines are located inside the drying shell at a height not lower than the drying main axis. The guide lines extend continuously along the circumferential direction of the inner wall of the drying shell. On the top projection plane, the angle between the guide lines and the drying main axis is 60-88°. Multiple partition rings are arranged in the axial direction on the inner wall of the drying shell, and one or more drying impellers are arranged between adjacent partition rings, with each partition ring arranged along the circumferential direction; The separating ring has an inclined surface facing the first end of the drying shell; the separating ring is symmetrically arranged with respect to the vertical plane passing through the drying main shaft. A guide impeller is set on the same cross section as the separator ring. The guide impeller includes multiple guide blades. The guide blades are strip-shaped. The first end of the guide blade is fixed in the axial direction. The guide blade extends in the radial direction of the drying shell. The second end opposite to the first end is inclined. The inclination direction of the second end of the guide blade is consistent with the inclination direction of the inclined side of the separator ring. Both the second end of the pulverizing device and the first end of the drying device are open. The second end of the pulverizing device is connected to the first end of the drying device, and the axes of the pulverizing main shaft and the drying main shaft are on the same straight line.

2. The device according to claim 1, characterized in that, The gas-solid separation unit includes a cyclone separator, a device for water phase change, and a bag filter, with the device for water phase change connected to both the cyclone separator and the bag filter. The device for water phase change includes a cavity, the cross-section of which is larger in the middle than the cross-sectional area of ​​the upper and lower ends.

3. The device according to claim 2, characterized in that, The cavity used for water phase change has an air inlet at the upper end and an air outlet at the lower end. Rotatable blades are installed at the air inlet, and the blades can rotate horizontally around an axis.

4. The device according to claim 2, characterized in that, The cross-section of the cavity used for fusion is circular, rectangular, or polygonal.

5. The device according to claim 2, characterized in that, The device for water phase change includes multiple interconnected chambers for water phase change, with rotatable blades provided at the connection between adjacent chambers.

6. The device according to claim 3, characterized in that, A device for water phase change including multiple chambers, each chamber having an air inlet at the upper end and an air outlet at the lower end; the air inlet of the chamber is connected to the air outlet of the adjacent chamber above it, and a rotatable blade is provided at the connection.

7. The device according to claim 1, characterized in that, The cross-section of the separator ring is a right triangle or a right trapezoid, with the hypotenuse of the right triangle or the hypotenuse of the right trapezoid facing the first end of the drying shell.

8. The device according to claim 1, characterized in that, The distance between the second end of the guide vane and the inclined surface of the separator ring is controlled between 1.0cm and 8.0cm.

9. The device according to claim 1 or 2, characterized in that, The pulverizing impeller is located inside the pulverizing housing and can rotate around the pulverizing main shaft; there is a gap between the outer peripheral end of the pulverizing impeller and the wall of the pulverizing housing; Multiple pulverizing impellers are arranged along the pulverizing main axis. Each pulverizing impeller includes multiple pulverizing blades evenly arranged around the pulverizing main axis. The pulverizing blades are strip-shaped.

10. The device according to claim 9, characterized in that, The pipeline for conveying materials connected to the pulverizing inlet gradually moves away from the pulverizing main shaft in the direction away from the pulverizing inlet.

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