A free-flow channel type forced disturbance granulator and a granulation method

Abstract

A free flow channel type forced disturbance granulator comprises a material channel, a rack, a first granulating device and a second granulating device; the material channel is a channel structure with an open top, the rack is a frame structure, and the material channel is located below the rack; the first and second granulating devices are arranged on the rack and suspended in the material channel through the rack; a feeding port is arranged on the upper portion of the front end of the material channel, and a discharge flow channel is arranged on the rear end of the material channel from top to bottom. The granulator is designed in an inclined manner with the front being higher and the rear being lower. The free flow channel type granulator provided by the application continuously applies external forces in different directions to growing material particles, so that the material is more easily agglomerated and granulated, the critical condition of material agglomeration and granulation is reduced, the tightness of the particles is increased, and the granulation quality is improved. The granulator can greatly improve the granulation efficiency and has good economic benefits.

Description

Technical Field

[0001] This invention relates to a forced perturbation granulator and granulation method, specifically to a free-flowing channel type forced perturbation granulator and granulation method, belonging to the field of sintering granulation. Background Technology

[0002] In the steel industry, sintering machines are used to sinter concentrates, rich ore powders and secondary iron-containing raw materials of different compositions and particle sizes into blocks, and to partially remove harmful impurities such as sulfur and phosphorus contained in the ore for use in blast furnace ironmaking.

[0003] Since concentrate powder, rich ore powder and secondary iron-containing raw materials are all fine powders, they cannot be sintered directly. They need to be processed into granular materials of a certain volume before they can be put into the sintering machine for sintering. Therefore, granulation is an important step in the sintering process.

[0004] Current sintering raw material granulation technology mainly uses cylindrical granulators. A cylindrical granulator is a hollow cylinder arranged at a certain angle and continuously rotating around its center line. Material enters the cylindrical granulator from the higher end, and as the cylinder rotates, the material rolls from the higher end to the lower end under the influence of gravity, and is discharged from the lower end. The principle of cylindrical granulation is as follows: Figure 6a and Figure 6b As shown, during the rotation of the pellet mill cylinder, the material inside the cylinder is lifted. When the material rises to a certain height, the lifting angle is greater than the angle of repose, causing the material pile to collapse. The material slides relative to the surface, and the particles grow during this sliding process, thus achieving granulation. Cylindrical pellet mills are passive pelleting equipment. The material experiences weak pelleting motion, and the core material cannot achieve regular relative sliding, failing to meet the conditions for pelleting. Therefore, the pelleting effect is poor, and the critical conditions for particle formation are high, such as high moisture content and a high binder ratio. This results in a persistently high proportion of non-ferrous components in the raw materials, making it difficult to meet the requirements of modern technological advancements and creating a technological bottleneck. Summary of the Invention

[0005] To address the problems of poor granulation effect and high critical conditions for material granulation in existing cylindrical granulation technologies, this invention proposes a free-flowing channel forced disturbance granulator and granulation method. This invention employs a free-flowing channel granulator, causing the material to roll along the granulation spiral within the granulator, adhering to fine particles and growing them into larger particles that meet the granulation requirements. Simultaneously, this invention utilizes multiple granulation processes, resulting in particles of uniform coarseness and size with controllable particle size.

[0006] According to a first embodiment of the present invention, a free-flowing channel type forced disturbance granulator is provided.

[0007] A free-flow forced disturbance granulator is characterized by comprising a material trough, a frame, a first granulating device, and a second granulating device. The material trough is an open-topped trough structure, and the frame is a frame structure with the material trough located below the frame. Both the first and second granulating devices are mounted on the frame and suspended within the material trough by the frame. A feed inlet is located at the upper front of the material trough, and a discharge trough is located at the rear of the material trough from top to bottom. The granulator has an overall inclined design, with a higher front and lower rear.

[0008] Preferably, the frame includes longitudinal beams and crossbeams. Several longitudinal beams and several crossbeams together form a loading frame platform, and the plane of the loading frame platform is parallel to the bottom surface of the material trough.

[0009] Preferably, the pellet mill also includes a base; the base is disposed at the bottom of the material trough. The frame is connected to the base via columns.

[0010] Preferably, the first granulation device includes a bearing housing, a granulation shaft, a granulation screw, and a drive wheel; the top end of the granulation shaft extends upward through the frame and is movably connected to the frame via the bearing housing. The bottom end of the granulation shaft extends into the material trough. The drive wheel is located at the top end of the granulation shaft and drives the granulation shaft to rotate. The granulation screw is mounted on the granulation shaft located within the material trough.

[0011] Preferably, the granulating spiral has a spiral plate-like structure. Inside the material tank, the granulating spiral is arranged around the outer surface of the granulating shaft and spirals upward from the bottom of the granulating shaft to the top of the granulating shaft.

[0012] Preferably, the structure of the second granulating device is the same as that of the first granulating device. Within the material tank, the second granulating device is located downstream of the first granulating device, according to the material's direction, and a partition wall is provided between the first and second granulating devices. One first granulating device and one second granulating device together constitute a granulating unit.

[0013] Preferably, the granulator includes m granulation units, which are evenly distributed along the width of the granulator. A partition wall simultaneously separates all the first granulation devices and all the second granulation devices along the width of the granulator. Preferably, m is an integer between 1 and 30.

[0014] Preferably, the tilt angle of the spiral granulation ascent is 5-80°, more preferably 10-60°, and even more preferably 15-45°.

[0015] Preferably, the angle between the bottom surface of the material trough and the horizontal plane is 1~60°, more preferably 5~45°, and even more preferably 10~30°. Preferably, the base is a height-adjustable telescopic structure.

[0016] According to a second embodiment of the present invention, a method for granulation using a free-flowing channel type forced disturbance granulator is provided.

[0017] A method for granulation using a free-flowing, forced-disturbance granulator, the method comprising the following steps:

[0018] 1) Start the granulator and add the fine material into the material tank through the feed inlet. The material will be granulated once under the action of the first granulation device.

[0019] 2) After the first granulation is completed, the material crosses the partition wall and is then granulated a second time by the second granulation device;

[0020] 3) After the secondary granulation is completed, the material is discharged through the discharge channel to obtain large particles.

[0021] Preferably, the method further includes: step 4) adjusting the rotational speed ratio of the first granulating device and the second granulating device so that the amount of material discharged from the first granulation per unit time and the amount of material discharged from the second granulation per unit time are consistent. Specifically: the rotational speed ratio of the first granulating device and the second granulating device is set to R. The amount of material discharged from the first granulation per unit time is Q1, t / h. The amount of material discharged from the second granulation per unit time is Q2, t / h; then:

[0022] Q1=47β1φ1ρ1D1 2 S1n1...1;

[0023] Q2=47β2φ2ρ2D2 2 S2n2...2;

[0024] Where β1 is the correction coefficient of the first granulation device, and β2 is the correction coefficient of the second granulation device. φ1 is the material filling coefficient at the first granulation device, and φ2 is the material filling coefficient at the second granulation device. ρ1 is the material bulk density at the first granulation device, t / m³. 3 ρ2 is the bulk density of the material at the second granulation unit, t / m³. 3 D1 is the diameter of the spiral blade of the first granulating device, in meters (m); D2 is the diameter of the spiral blade of the second granulating device, in meters (m). S1 is the pitch of the first granulating device, in meters (m); S2 is the pitch of the second granulating device, in meters (m). n1 is the rotational speed of the first granulating device, in r / min; n2 is the rotational speed of the second granulating device, in r / min (r / min).

[0025] When Q1 = Q2, then:

[0026] 47β1φ1ρ1D1 2 S1n1=47β2φ2ρ2D2 2 S2n2...3;

[0027] The conversion yields:

[0028] R=n1 / n2=(β2φ2ρ2D2 2 S2) / (β1φ1ρ1D1 2 S1)...4;

[0029] Preferably, the rotational speed ratio R between the first granulating device and the second granulating device is 1:1-1.2, and more preferably 1:1.05-1.1.

[0030] Preferably, the method further includes: step 5) controlling the particle size of the granulated material by adjusting the tilt angle of the granulator. Specifically, the particle size of the material after two granulations is set to [d]. min d max The average particle size of the material discharged from the discharge chute in real time is recorded as d0, mm.

[0031] 501) When d0 > d max At this time, increase the tilt angle of the granulator until d0∈[d min d max ];

[0032] 502) When d min ≤d0≤d max At this time, maintain the current state unchanged;

[0033] 503) When d0 < d min At that time, reduce the tilt angle of the granulator until d0∈[d min d max ].

[0034] Preferably, 501) specifically refers to:

[0035] 501a) When d0 > 150%d max hour, ;

[0036] 501b) When 130%d max <d0≤150%d max hour, ;

[0037] 501c) When d max <d0≤130%d max hour, ;

[0038] Where k1, k2, and k3 are the angle adjustment coefficients, with k1 ranging from 0.6 to 1.0, k2 from 0.3 to 0.6, and k3 from 0.1 to 0.3. θ0 is the initial angle between the bottom of the material trough and the ground, and θ1 is the adjusted angle between the bottom of the material trough and the ground. The value of d0 is detected in real time, and the particle size of the granulated material is controlled to meet production requirements by adjusting the tilt angle of the granulator.

[0039] Preferably, 503) specifically refers to:

[0040] 503a) When d0 ≤ 50%d min hour, ;

[0041] 503b) When 50%d min <d0≤80%d min hour, ;

[0042] 503c) When 80%d min <d0<d min hour, ;

[0043] Wherein, k7, k8, and k9 are the angle adjustment coefficients, with k7 ranging from 0.6 to 0.9, k8 from 0.35 to 0.7, and k9 from 0.15 to 0.4. θ0 is the initial angle between the bottom of the material trough and the ground, and θ1 is the adjusted angle between the bottom of the material trough and the ground. The value of d0 is detected in real time, and the particle size of the granulated material is controlled by adjusting the tilt angle of the granulator.

[0044] In existing technologies, because cylindrical pellet mills are inclined, the pelleting process relies on the rolling of the cylinder to drive the material to roll and thus lift it. When the material is lifted to a certain height, the lifting angle is greater than the angle of repose, causing the material pile to collapse. The material then slides relative to the surface, completing particle growth during this sliding process, thus achieving granulation. However, the granulation effect on the material is weak during this process. Furthermore, because the material has a certain volume of accumulation inside the cylinder, the core material cannot achieve regular relative sliding during the aforementioned sliding pelleting process, failing to meet the conditions for pelleting, resulting in poor pelleting performance. This is mainly manifested in the high requirements for critical conditions for material pelleting, such as high moisture content and high binder ratios, leading to a persistently high proportion of non-ferrous components in the raw materials, making it difficult to meet the requirements of modern technological advancements.

[0045] In this invention, a free-flowing, forced-disturbance granulator is used for granulation. Material is fed into the granulator from the inlet and enters the first mixing chamber (where the first granulating device is located). Once a certain quantity of material is reached, the granulating spiral of the first granulating device stirs and lifts the material above the partition wall, then across the partition wall into the second mixing chamber (where the second granulating device is located). When a certain quantity of material to be granulated is reached in the second mixing chamber, it is lifted by the granulating spiral of the second granulating device for secondary granulation. Finally, it is lifted across the side wall of the material trough and enters the discharge trough, from where it is guided to the transport equipment.

[0046] In this invention, the pellet mill is equipped with a partition wall that divides the pellet mill vertically into two mixing chambers. This prevents material from rapidly falling to the discharge chute side of the pellet mill in the absence of a partition wall, ensuring sufficient pelleting time in each mixing chamber and fixing the material flow direction, resulting in more uniform particle size of the granulated material. Furthermore, due to the overall inclined design of the pellet mill (higher at the front and lower at the back), the pelleting devices are all close to the partition wall. As the material is lifted upwards on the pelleting device, the partition wall provides support.

[0047] In this invention, the free-flowing forced perturbation granulator generally includes two granulating devices, arranged sequentially according to the material flow direction (one granulating device is located downstream of the other). The purpose of using two granulating devices is that the primary function of the first granulating device is to transform fine material into coarser core particles. These core particles then rapidly grow into larger particles that meet granulation requirements under the action of the second granulating device by continuously adhering to finer particles. Through the synergistic effect of the two granulating devices, both granulation efficiency and the quality of large particles are greatly improved. Furthermore, the particle size of the finished product can be adjusted by controlling the rotation speed of the perturbation granulating device. The free-flowing forced perturbation granulator can also be equipped with multiple granulating devices, the specific number determined according to actual production needs.

[0048] In this invention, the material receives forces from the granulating spiral in different directions during the granulation process, causing the material to generate partial velocities in different directions (mainly due to simultaneous vertical lifting force and horizontal rotational centrifugal force). Under the influence of these partial velocities, the material rolls along the surface of the granulating spiral. Coarser particles act as cores, continuously adhering to surrounding finer particles during this rolling process, thus rapidly growing. Simultaneously, the granulating spiral continuously applies external forces in different directions to the growing material particles, making it easier for the material to agglomerate into granules, lowering the critical condition for agglomeration, increasing particle density, and improving granulation quality.

[0049] like Figure 7 , Figure 8As shown, the forces acting on the material at any point on the propeller blade of the granulating spiral at any time mainly include the supporting force F. N (Perpendicular to the supporting surface upwards), friction f The forces consist of three parts: (opposite to the relative motion of the particles), gravity G (vertically downwards), and force analysis. Let the direction along the blade diameter be the x-axis, the tangential direction be the y-axis, and the axial direction be the z-axis.

[0050] Support force F N Component F along the y-axis Ny The component F along the z-axis Nz ;

[0051] friction f :along x Components in the axial direction f x It provides the centripetal force for the circular motion of the particles, along... y Components in the axial direction f y Components along the z-axis f z ;

[0052] Combined, obtain

[0053]

[0054] In the formula, α For F N The angle with the positive z-axis, β for f exist xoy Projection on the surface and x The angle between the positive axis and the positive axis.

[0055] Assuming the particle is spherical with a radius of... d , F 向 The initial centripetal force for the particle to undergo circular motion. r Let be the radius of the circle. w Let be the angular velocity of the blade rotation, then the resultant force in all directions is:

[0056] x direction: , ,

[0057] y direction: , ,

[0058] z-direction: ,

[0059] Combined, obtain

[0060] .

[0061] Based on the force analysis results, the motion state of the particles at any point on the propeller blade was analyzed, and it was found that, due to... f x The force is insufficient to provide the centripetal force needed for the particles to maintain circular motion with the propeller blades. Under the influence of inertia, the particles gradually deviate from the center of the circle, generating centrifugal motion, until they are ejected tangentially from the blade edge. Their trajectory is approximately as follows: Figure 9 As shown.

[0062] In this invention, the movement process of the particles is mainly manifested as follows: xoy The motion is circular within the plane, with acceleration along the positive z-axis. The overall trajectory is a spiral with a gradually increasing radius along the positive z-axis.

[0063] xoy flat: ;

[0064] Circumference radius: ;

[0065] Z-axis direction: .

[0066] In the formula, The initial rotation angle of the propeller blades. The angular velocity of the propeller blades. Let be the radius of the circle in which the particle moves in circular motion. The tangential acceleration of the particle in circular motion. Let be the initial coordinates of the particle along the Z-axis. Let x be the acceleration of the particle along the positive z-axis. This represents the displacement of the particle along the positive z-axis.

[0067] In this invention, the material is stirred from the bottom of the granulator by a propeller blade, rolls on the blade, and is lifted. However, due to insufficient centripetal force, the material... xoy The radius of the material undergoing circular motion in the plane gradually increases, and upon reaching the top of the baffle, it detaches from the propeller blades and enters the next mixing chamber. Similarly, the material repeats the above process in the second mixing chamber.

[0068] In this invention, as a preferred embodiment, the pellet mill is provided with n pelleting units, all of which are located in the material trough and are evenly distributed in the horizontal direction perpendicular to the material flow direction. According to the actual production needs, n is a positive integer greater than or equal to 1, and preferably n is an integer from 1 to 30.

[0069] In this invention, adjusting the tilt angle of the pellet mill or the rotation speed of the propeller blades can control the particle size of the material. The pelleting time in the pellet mill has a significant impact on the particle size. As the material continuously adheres to fine particles in the pellet mill, the longer the mixing time, the more fine particles adhere, resulting in a larger particle size. A longer pelleting time leads to larger particle sizes, while a shorter pelleting time results in smaller particle sizes. The pellet mill base provided by this invention is height-adjustable. When the pellet mill tilt angle needs to be increased, the height of the base at the feed end is increased, while the height of the base near the discharge end remains unchanged, and the remaining bases are adjusted sequentially according to their positions. Similarly, when the pellet mill tilt angle needs to be decreased, the height of the base at the feed end is decreased, while the height of the base near the discharge end remains unchanged, and the remaining bases are adjusted sequentially according to their positions.

[0070] In this invention, to prevent inconsistent particle size and idling of the granulation device, the rotational speed of the propeller blades is limited. Calculations show that with the same propeller blade rotational speed, the output per unit time of each granulation device is equal. Controlling the propeller blade rotational speed to be constant prevents material accumulation and idling of the granulation device, ensuring that the produced material particles have a consistent particle size.

[0071] In this invention, the front end is the feed end of the pellet mill, and the rear end is the discharge end of the pellet mill. The feed end of the pellet mill is higher than the discharge end.

[0072] Compared with the prior art, the present invention has the following beneficial effects:

[0073] 1. This invention uses a free-flowing trough granulator to continuously apply external forces in different directions to the growing material particles, making the material easier to agglomerate into granules, reducing the critical conditions for material agglomeration into granules, increasing the compactness of the particles, and improving the granulation quality.

[0074] 2. The present invention uses a multiple granulation method, which results in more uniform particle size and coarseness compared to single granulation.

[0075] 3. The granulator provided by this invention can granulate continuously without stopping the machine to feed, thus improving granulation efficiency. Attached Figure Description

[0076] Figure 1 This is a schematic diagram of the structure of a free-flowing channel type forced disturbance granulator provided by the present invention.

[0077] Figure 2 This is a schematic diagram of the structure of a free-flowing channel type forced disturbance granulator provided by the present invention.

[0078] Figure 3 This is a structural schematic diagram of a free-flowing channel type forced disturbance granulator in operation, provided by the present invention.

[0079] Figure 4 This is a schematic diagram of the structure of a free-flowing channel forced disturbance granulator provided by the present invention when it is equipped with multiple granulation devices.

[0080] Figure 5 This is a schematic diagram of the frame structure of a free-flowing channel type forced disturbance granulator provided by the present invention.

[0081] Figure 6a This is a schematic diagram of the structure of a cylindrical pellet mill in the prior art.

[0082] Figure 6b This is a schematic diagram of material sliding in a cylindrical pellet mill in the prior art.

[0083] Figure 7 This is a force analysis diagram of a material particle at any point on the granulation propeller blade.

[0084] Figure 8 This is a force analysis diagram of a material particle at any point on the granulation propeller blade.

[0085] Figure 9 This is a schematic diagram of the trajectory of material particles at any point on the granulation propeller blade.

[0086] Reference numerals in the attached drawings: 1: Material trough; 2: Frame; 201: Longitudinal beam; 202: Crossbeam; 203: Column; 3: Base; 4: First granulation device; 401: Bearing seat; 402: Granulation shaft; 403: Granulation screw; 404: Drive wheel; 5: Partition wall; 6: Second granulation device; 7: Discharge chute. Detailed Implementation

[0087] The technical solution of the present invention will be illustrated below with examples. The scope of protection sought by the present invention includes, but is not limited to, the following embodiments.

[0088] According to a first embodiment of the present invention, a free-flowing channel type forced disturbance granulator is provided.

[0089] A free-flow forced disturbance granulator is characterized by comprising a material trough 1, a frame 2, a first granulating device 4, and a second granulating device 6. The material trough 1 is an open-topped trough structure, and the frame 2 is a frame structure, with the material trough 1 located below the frame 2. Both the first granulating device 4 and the second granulating device 6 are mounted on the frame 2 and suspended within the material trough 1 by the frame 2. A feed inlet is located at the upper front of the material trough 1, and a discharge trough 7 is located at the rear of the material trough 1 from top to bottom. The granulator has an overall inclined design, with the front higher than the rear.

[0090] Preferably, the frame 2 includes longitudinal beams 201 and cross beams 202. Several longitudinal beams 201 and several cross beams 202 together form a loading frame platform, and the plane of the loading frame platform is parallel to the bottom surface of the material tank 1.

[0091] Preferably, the pellet mill also includes a base 3; the base 3 is disposed at the bottom of the material trough 1. The frame 2 is connected to the base 3 via a column 203.

[0092] Preferably, the first granulating device 4 includes a bearing seat 401, a granulating shaft 402, a granulating screw 403, and a drive wheel 404; the top end of the granulating shaft 402 extends upward through the frame 2 and is movably connected to the frame 2 via the bearing seat 401. The bottom end of the granulating shaft 402 extends into the material tank 1. The drive wheel 404 is located at the top end of the granulating shaft 402 and drives the granulating shaft 402 to rotate. The granulating screw 403 is located on the granulating shaft 402 within the material tank 1.

[0093] Preferably, the granulating spiral 403 has a spiral sheet structure. Inside the material tank 1, the granulating spiral 403 is arranged around the outer surface of the granulating shaft 402, and spirals upward from the bottom of the granulating shaft 402 to the upper part of the granulating shaft 402.

[0094] Preferably, the structure of the second granulating device 6 is the same as that of the first granulating device 4. Within the material tank 1, the second granulating device 6 is located downstream of the first granulating device 4 according to the material's direction, and a partition wall 5 is provided between the first granulating device 4 and the second granulating device 6. One first granulating device 4 and one second granulating device 6 together constitute a granulating unit.

[0095] Preferably, the granulator includes m granulation units, which are evenly distributed along the width of the granulator. A partition wall 5 simultaneously separates all the first granulation devices 4 and all the second granulation devices 6 along the width of the granulator. Preferably, m is an integer between 1 and 30.

[0096] Preferably, the tilt angle of the spiral 403 as it spirals upward is 5-80°, more preferably 10-60°, and even more preferably 15-45°.

[0097] Preferably, the angle between the bottom surface of the material trough 1 and the horizontal plane is 1~60°, more preferably 5~45°, and even more preferably 10~30°. Preferably, the base 3 is a height-adjustable telescopic structure.

[0098] According to a second embodiment of the present invention, a method for granulation using a free-flowing channel type forced disturbance granulator is provided.

[0099] A method for granulation using a free-flowing, forced-disturbance granulator, the method comprising the following steps:

[0100] 1) Start the granulator and add the fine material into the material tank 1 through the feed inlet. The material is then granulated once under the action of the first granulation device 4.

[0101] 2) After the first granulation is completed, the material crosses the partition wall 5 and is then subjected to a second granulation under the action of the second granulation device 6;

[0102] 3) After the secondary granulation is completed, the material is discharged through the discharge channel 7 to obtain large particles.

[0103] Preferably, the method further includes: step 4) adjusting the rotational speed ratio of the first granulating device 4 and the second granulating device 6 so that the amount of material discharged from the first granulation per unit time and the amount of material discharged from the second granulation per unit time are consistent. Specifically: the rotational speed ratio of the first granulating device 4 and the second granulating device 6 is set to R. The amount of material discharged from the first granulation per unit time is Q1, t / h. The amount of material discharged from the second granulation per unit time is Q2, t / h; then:

[0104] Q1=47β1φ1ρ1D1 2 S1n1...1;

[0105] Q2=47β2φ2ρ2D2 2 S2n2...2;

[0106] Where β1 is the correction coefficient of the first granulation device 4, and β2 is the correction coefficient of the second granulation device 6. φ1 is the material filling coefficient at the first granulation device 4, and φ2 is the material filling coefficient at the second granulation device 6. ρ1 is the material bulk density at the first granulation device 4, t / m³. 3 ρ2 is the bulk density of the material at point 6 of the second granulation device, in t / m³. 3 D1 is the diameter of the spiral blade of the first granulating device 4, in meters (m); D2 is the diameter of the spiral blade of the second granulating device 6, in meters (m). S1 is the pitch of the first granulating device 4, in meters (m); S2 is the pitch of the second granulating device 6, in meters (m); n1 is the rotational speed of the first granulating device 4, in r / min; n2 is the rotational speed of the second granulating device 6, in r / min (m).

[0107] When Q1 = Q2, then:

[0108] 47β1φ1ρ1D1 2 S1n1=47β2φ2ρ2D2 2 S2n2...3;

[0109] The conversion yields:

[0110] R=n1 / n2=(β2φ2ρ2D22 S2) / (β1φ1ρ1D1 2 S1)...4;

[0111] Preferably, the rotational speed ratio R of the first granulating device 4 and the second granulating device 6 is 1:1-1.2, and more preferably 1:1.05-1.1.

[0112] Preferably, the method further includes: step 5) controlling the particle size of the granulated material by adjusting the tilt angle of the granulator. Specifically, the particle size of the material after two granulations is set to [d]. min d max The average particle size of the material discharged from the discharge chute 7 in real time is recorded as d0, mm.

[0113] 501) When d0 > d max At this time, increase the tilt angle of the pellet mill or increase the rotation speed of the pelletizing unit until d0∈[d min d max ];

[0114] 502) When d min ≤d0≤d max At this time, maintain the current state unchanged;

[0115] 503) When d0 < d min At this time, reduce the tilt angle of the pellet mill or slow down the rotation speed of the pelletizing unit until d0∈[d min d max ].

[0116] Preferably, 501) specifically refers to:

[0117] 501a) When d0 > 150%d max hour, ;

[0118] 501b) When 130%d max <d0≤150%d max hour, ;

[0119] 501c) When d max <d0≤130%d max hour, ;

[0120] Where k1, k2, and k3 are the angle adjustment coefficients, with k1 ranging from 0.6 to 1.0, k2 from 0.3 to 0.6, and k3 from 0.1 to 0.3. θ0 is the initial angle between the bottom of material trough 1 and the ground, and θ1 is the adjusted angle between the bottom of material trough 1 and the ground. The value of d0 is detected in real time, and the particle size of the granulated material is controlled to meet production requirements by adjusting the tilt angle of the granulator.

[0121] Preferably, 503) specifically refers to:

[0122] 503a) When d0 ≤ 50%d min hour, ;

[0123] 503b) When 50%d min <d0≤80%d min hour, ;

[0124] 503c) When 80%d min <d0<d min hour, ;

[0125] Wherein, k7, k8, and k9 are the angle adjustment coefficients, with k7 ranging from 0.6 to 0.9, k8 from 0.35 to 0.7, and k9 from 0.15 to 0.4. θ0 is the initial angle between the bottom of the material trough and the ground, and θ1 is the adjusted angle between the bottom of the material trough and the ground. The value of d0 is detected in real time, and the particle size of the granulated material is controlled by adjusting the tilt angle of the granulator. Example 1

[0126] A free-flow forced disturbance granulator is characterized by comprising a material trough 1, a frame 2, a first granulating device 4, and a second granulating device 6. The material trough 1 is an open-topped trough structure, and the frame 2 is a frame structure, with the material trough 1 located below the frame 2. Both the first granulating device 4 and the second granulating device 6 are mounted on the frame 2 and suspended within the material trough 1 by the frame 2. A feed inlet is located at the upper front of the material trough 1, and a discharge trough 7 is located at the rear of the material trough 1 from top to bottom. The granulator has an overall inclined design, with the front higher than the rear. Example 2

[0127] The embodiment 1 is repeated, except that the frame 2 includes longitudinal beams 201 and cross beams 202. Several longitudinal beams 201 and several cross beams 202 together form a loading frame platform, and the plane of the loading frame platform is parallel to the bottom surface of the material tank 1.

[0128] The pellet mill also includes a base 3; the base 3 is located at the bottom of the material trough 1. The frame 2 is connected to the base 3 via a column 203. Example 3

[0129] The embodiment 2 is repeated, except that the first granulating device 4 includes a bearing seat 401, a granulating shaft 402, a granulating screw 403, and a drive wheel 404. The top end of the granulating shaft 402 extends upward through the frame 2 and is movably connected to the frame 2 via the bearing seat 401. The bottom end of the granulating shaft 402 extends into the material tank 1. The drive wheel 404 is located at the top end of the granulating shaft 402 and drives the granulating shaft 402 to rotate. The granulating screw 403 is located on the granulating shaft 402 within the material tank 1. Example 4

[0130] Example 3 is repeated, except that the granulating spiral 403 has a spiral sheet structure. In the material tank 1, the granulating spiral 403 is arranged around the outer surface of the granulating shaft 402, and spirals upward from the bottom of the granulating shaft 402 to the upper part of the granulating shaft 402. Example 5

[0131] Example 4 is repeated, except that the structure of the second granulating device 6 is the same as that of the first granulating device 4. Within the material tank 1, the second granulating device 6 is located downstream of the first granulating device 4 according to the material's direction, and a partition wall 5 is provided between the first granulating device 4 and the second granulating device 6. One first granulating device 4 and one second granulating device 6 together constitute a granulating unit. Example 6

[0132] Example 5 is repeated, except that the granulator includes three granulation units, which are evenly distributed along the width of the granulator. A partition wall 5 simultaneously separates all the first granulation devices 4 and all the second granulation devices 6 along the width of the granulator. Example 7

[0133] Repeat Example 6, except that the tilt angle of the spiral 403 spiraling upward is 30°. Example 8

[0134] Example 7 is repeated, except that the angle between the bottom surface of the material tank 1 and the horizontal plane is 20°. The base 3 is a height-adjustable telescopic structure. Example 9

[0135] A method for granulation using a free-flowing, forced-disturbance granulator, the method comprising the following steps:

[0136] 1) Start the granulator and add the fine material into the material tank 1 through the feed inlet. The material is then granulated once under the action of the first granulation device 4.

[0137] 2) After the first granulation is completed, the material crosses the partition wall 5 and is then subjected to a second granulation under the action of the second granulation device 6;

[0138] 3) After the secondary granulation is completed, the material is discharged through the discharge channel 7 to obtain large particles. Example 10

[0139] Repeat Example 9, except that the method further includes: Step 4) Adjusting the rotational speed ratio of the first granulating device 4 and the second granulating device 6 so that the amount of material discharged from the first granulation per unit time and the amount of material discharged from the second granulation per unit time are consistent. Specifically: Set the rotational speed ratio of the first granulating device 4 and the second granulating device 6 to R. The amount of material discharged from the first granulation per unit time is Q1, t / h. The amount of material discharged from the second granulation per unit time is Q2, t / h; then:

[0140] Q1=47β1φ1ρ1D1 2 S1n1...1;

[0141] Q2=47β2φ2ρ2D2 2 S2n2...2;

[0142] Where β1 is the correction coefficient of the first granulation device 4, and β2 is the correction coefficient of the second granulation device 6. φ1 is the material filling coefficient at the first granulation device 4, and φ2 is the material filling coefficient at the second granulation device 6. ρ1 is the material bulk density at the first granulation device 4, t / m³. 3 ρ2 is the bulk density of the material at point 6 of the second granulation device, in t / m³. 3 D1 is the diameter of the spiral blade of the first granulating device 4, in meters (m); D2 is the diameter of the spiral blade of the second granulating device 6, in meters (m). S1 is the pitch of the first granulating device 4, in meters (m); S2 is the pitch of the second granulating device 6, in meters (m); n1 is the rotational speed of the first granulating device 4, in r / min; n2 is the rotational speed of the second granulating device 6, in r / min (m).

[0143] When Q1 = Q2, then:

[0144] 47β1φ1ρ1D1 2 S1n1=47β2φ2ρ2D2 2 S2n2...3;

[0145] The conversion yields:

[0146] R=n1 / n2=(β2φ2ρ2D2 2 S2) / (β1φ1ρ1D1 2 S1)...4;

[0147] The rotational speed ratio R between the first granulating device 4 and the second granulating device 6 is 1:1.1. Example 11

[0148] Repeat Example 10, except that the method further includes: step 5) controlling the particle size of the granulated material by adjusting the tilt angle of the granulator. Specifically, the particle size of the material after two granulations is set to [d]. min d max The average particle size of the material discharged from the discharge chute 7 in real time is recorded as d0, mm.

[0149] 501) When d0 > d max At this time, increase the tilt angle of the granulator until d0∈[d min d max ];

[0150] 502) When d min ≤d0≤d max At this time, maintain the current state unchanged;

[0151] 503) When d0 < d min At that time, reduce the tilt angle of the granulator until d0∈[d min d max ]. Example 12

[0152] Repeat Example 11, except that 501) specifically refers to:

[0153] 501a) When d0 > 150%d max hour, ;

[0154] 501b) When 130%d max <d0≤150%d max hour, ;

[0155] 501c) When d max <d0≤130%d max hour, ;

[0156] Where k1, k2, and k3 are angle adjustment coefficients, with k1 taking a value of 0.8, k2 taking a value of 0.45, and k3 taking a value of 0.2. θ0 is the initial angle between the bottom surface of material trough 1 and the ground, and θ1 is the adjusted angle between the bottom surface of material trough 1 and the ground. The value of d0 is detected in real time, and the particle size of the granulated material is controlled to meet production requirements by adjusting the tilt angle of the granulator. Example 13

[0157] Repeat Example 11, except that 503) specifically refers to:

[0158] 503a) When d0 ≤ 50%d min hour, ;

[0159] 503b) When 50%d min <d0≤80%d min hour, ;

[0160] 503c) When 80%d min <d0<d min hour, ;

[0161] Where k7, k8, and k9 are the angle adjustment coefficients, with k7 taking the value of 0.8, k8 taking the value of 0.5, and k9 taking the value of 0.2. θ0 is the initial angle between the bottom of the material trough and the ground, and θ1 is the adjusted angle between the bottom of the material trough and the ground. The value of d0 is detected in real time, and the particle size of the granulated material is controlled by adjusting the tilt angle of the granulator.

[0162] Application Example 1

[0163] The method described in Example 12 was used for granulation of refined iron ore powder. The average particle size d0 of the material discharged from the discharge chute 7 was monitored in real time, with a value of 5 mm. The maximum particle size d0 of the mineral particles was set according to the sintering requirements. max =3mm, minimum d min =1mm; the initial tilt angle of the pellet mill is 15°; the included angle adjustment coefficient k1 is 0.8;

[0164] Since d0 > 150%d max ,

[0165] ;

[0166] Adjust the tilt angle of the granulator to 23° so that the average particle size d0 ∈ [d min d max ].

[0167] Application Example 2

[0168] The method described in Example 12 was used for granulation of refined iron ore powder. The average particle size d0 of the material discharged from the discharge chute 7 was monitored in real time and found to be 4.5 mm. The maximum particle size d0 of the mineral particles was set according to the sintering requirements. max =3mm, minimum d min =1mm; the initial tilt angle of the pellet mill is 20°; the included angle adjustment coefficient k2 is 0.5;

[0169] Due to 130%d max<d0≤150%d max , ;

[0170] Adjust the tilt angle of the granulator to 25° so that the average particle size of the material d0 ∈ [d min d max ].

[0171] Application Example 3

[0172] The method described in Example 12 was used for granulation of refined iron ore powder. The average particle size d0 of the material discharged from the discharge chute 7 was monitored in real time and found to be 3.5 mm. The maximum particle size d0 of the mineral particles was set according to the sintering requirements. max =3mm, minimum d min =0.5mm; the initial tilt angle of the pellet mill is 23°; the included angle adjustment coefficient k3 is 0.2;

[0173] Since d0 > 150%d max , ;

[0174] Adjust the tilt angle of the granulator to 24° so that the average particle size d0 ∈ [d min d max ].

[0175] Application Example 4

[0176] The method described in Example 11 was applied to the granulation of refined iron ore powder. The average particle size d0 of the material discharged from the discharge chute 7 was monitored in real time, with a value of 5 mm. The maximum particle size d0 of the mineral particles was set according to the sintering requirements. max =6mm, minimum d min =3mm; d0∈[d min d max To meet production needs and maintain current process conditions.

[0177] Application Example 5

[0178] The method described in Example 13 was used for granulation of refined iron ore powder. The average particle size d0 of the material discharged from the discharge chute 7 was monitored in real time, with a value of 2 mm. The maximum particle size d0 of the mineral particles was set according to the sintering requirements. max =5mm, minimum d min =3mm; the initial tilt angle of the pellet mill is 35°; the included angle adjustment coefficient k8 is 0.5;

[0179] Due to 50%d min <d0≤80%d min , ;

[0180] Adjust the tilt angle of the granulator to 29° so that the average particle size of the material d0∈[d min d max ].

[0181] Application Example 6

[0182] The method described in Example 13 was used for granulation of refined iron ore powder. The average particle size d0 of the material discharged from the discharge chute 7 was monitored in real time and found to be 0.5 mm. The maximum particle size d0 of the mineral particles was set according to the sintering requirements. max =5mm, minimum d min =3mm; the initial tilt angle of the pellet mill is 55°; the included angle adjustment coefficient k7 is 0.7;

[0183] Since d0≤50%d min , ;

[0184] Adjust the tilt angle of the granulator to 23° so that the average particle size d0 ∈ [d min d max ].

[0185] Application Example 7

[0186] The method described in Example 13 was used for granulation of refined iron ore powder. The average particle size d0 of the material discharged from the discharge chute 7 was monitored in real time to be 2.5 mm. The maximum particle size d0 of the mineral particles was set according to the sintering requirements. max =5mm, minimum d min =3mm; the initial tilt angle of the pellet mill is 30°; the included angle adjustment coefficient k9 is 0.2;

[0187] Due to 80%d min <d0<d min hour, ;

[0188] Adjust the tilt angle of the granulator to 29° so that the average particle size of the material d0∈[d min d max ].

Claims

1. A free-flowing, forced-disturbance granulator, characterized in that: The pellet mill includes a material trough (1), a frame (2), a first pelletizing device (4), and a second pelletizing device (6); wherein, the material trough (1) is a trough-shaped structure with an open top, the frame (2) is a frame structure, and the material trough (1) is located below the frame (2); the first pelletizing device (4) and the second pelletizing device (6) are both mounted on the frame (2) and suspended in the material trough (1) by the frame (2); the material trough (1) has a feed inlet at the upper front end and a discharge trough (7) at the rear end from top to bottom; the pellet mill is designed with a high front and low rear; the first pelletizing device (4) includes a bearing seat (401), a pelletizing shaft (402), a pelletizing screw (403), and a drive wheel (404); the top of the pelletizing shaft (402) extends upward through The second granulating device (6) is connected to the frame (2) via a bearing seat (401); the bottom end of the granulating shaft (402) extends into the material tank (1); the drive wheel (404) is set at the top of the granulating shaft (402) and drives the granulating shaft (402) to rotate; the granulating screw (403) is set on the granulating shaft (402) located in the material tank (1); the structure of the second granulating device (6) is the same as that of the first granulating device (4); in the material tank (1), according to the direction of the material, the second granulating device (6) is located downstream of the first granulating device (4), and a partition wall (5) is set between the first granulating device (4) and the second granulating device (6); a first granulating device (4) and a second granulating device (6) together constitute a granulating unit.

2. The granulator according to claim 1, characterized in that: The frame (2) includes longitudinal beams (201) and transverse beams (202); several longitudinal beams (201) and several transverse beams (202) together form a loading frame platform, and the plane of the loading frame platform is parallel to the bottom surface of the material tank (1); The pellet mill also includes a base (3); the base (3) is located at the bottom of the material trough (1); the frame (2) is connected to the base (3) via a column (203).

3. The granulator according to claim 1, characterized in that: The granulating spiral (403) has a spiral sheet structure; in the material tank (1), the granulating spiral (403) is arranged around the outer surface of the granulating shaft (402) and spirals up from the bottom of the granulating shaft (402) to the top of the granulating shaft (402).

4. The granulator according to claim 1, characterized in that: The pellet mill includes m pelleting units, which are evenly distributed in the width direction of the pellet mill; the partition wall (5) separates all the first pelleting devices (4) and all the second pelleting devices (6) in the width direction of the pellet mill; m is an integer between 1 and 30.

5. The granulator according to claim 3, characterized in that: The granulation spiral (403) ascends at an angle of 5-80°.

6. The granulator according to claim 5, characterized in that: The granulation spiral (403) ascends at an angle of 10-60°.

7. The granulator according to claim 6, characterized in that: The granulation spiral (403) ascends at an angle of 15-45°.

8. The pellet mill according to any one of claims 1-7, characterized in that: The angle between the bottom surface of the material tank (1) and the horizontal plane is 1~60°.

9. The granulator according to claim 8, characterized in that: The angle between the bottom surface of the material tank (1) and the horizontal plane is 5~45°.

10. The granulator according to claim 9, characterized in that: The angle between the bottom surface of the material tank (1) and the horizontal plane is 10~30°.

11. The pellet mill according to any one of claims 1-7, characterized in that: The base (3) is a height-adjustable telescopic structure.

12. A method for granulation using a free-flowing, forced-disturbance granulator as described in any one of claims 1-11, the method comprising the following steps: 1) Start the granulator and add the fine material into the material tank (1) through the feed port. Under the action of the first granulation device (4), the material is granulated once. 2) After the first granulation is completed, the material crosses the partition wall (5) and is then granulated a second time under the action of the second granulation device (6); 3) After the secondary granulation is completed, the material is discharged through the discharge channel (7) to obtain large particles.

13. The method according to claim 12, characterized in that: The method further includes: step 4) adjusting the rotation speed ratio of the first granulating device (4) and the second granulating device (6) so that the amount of material discharged from the first granulation per unit time and the amount of material discharged from the second granulation per unit time are consistent; the rotation speed ratio R of the first granulating device (4) and the second granulating device (6) is 1:1-1.

2.

14. The method according to claim 12 or 13, characterized in that: The method further includes: step 5) controlling the particle size of the granulated material by adjusting the tilt angle of the granulator; specifically: setting the particle size of the material after two granulations to be [d]. min d max ], mm; The average particle size of the material discharged from the discharge chute (7) in real time is recorded as d0, mm; 501) When d0 > d max At this time, increase the tilt angle of the granulator until d0∈[d min d max ]; 502) When d min ≤d0≤d max At this time, maintain the current state unchanged; 503) When d0 < d min At that time, reduce the tilt angle of the granulator until d0∈[d min d max ].

15. The method according to claim 14, characterized in that: 501) Specifically: 501a) When d0 > 150%d max hour, ; 501b) When 130%d max <d0≤150%d max hour, ; 501c) When d max <d0≤130%d max hour, ; Among them, k1, k2, and k3 are the angle adjustment coefficients, with k1 ranging from 0.6 to 1.0, k2 ranging from 0.3 to 0.6, and k3 ranging from 0.1 to 0.3; θ0 is the initial angle between the bottom of the material tank (1) and the ground, and θ1 is the angle between the bottom of the material tank (1) and the ground after adjustment; the size of d0 is detected in real time, and the particle size of the granulated material is controlled to meet the production requirements by adjusting the tilt angle of the granulator.

16. The method according to claim 14, characterized in that: 503) Specifically: 503a) When d0 ≤ 50%d min hour, ; 503b) When 50%d min <d0≤80%d min hour, ; 503c) When 80%d min <d0<d min hour, ; Among them, k7, k8, and k9 are the angle adjustment coefficients, with k7 ranging from 0.6 to 0.9, k8 ranging from 0.35 to 0.7, and k9 ranging from 0.15 to 0.4; θ0 is the initial angle between the bottom of the material trough and the ground, and θ1 is the adjusted angle between the bottom of the material trough and the ground; the size of d0 is detected in real time, and the particle size of the granulated material is controlled by adjusting the tilt angle of the granulator.

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