Coarse mineral sorting device and method with flow field characteristics matched with sorting process

Abstract

The invention relates to a coarse grain mineral sorting device and method with flow field characteristics matched with a sorting process, belongs to the technical field of mineral processing and resource recovery, and solves the problem of poor sorting effect of coarse grain sorting equipment in the prior art. The device comprises a fluidized bed column and a rotational flow feed bin which are concentrically arranged, the cyclone feeding bin is arranged below the fluidized bed column, and the upper end of the cyclone feeding bin is communicated with the lower end of the fluidized bed column; an agent feeding port and an ore pulp feeding port are formed in the two sides of the upper end of the rotational flow feeding bin, the agent feeding port and the ore pulp feeding port are both tangentially communicated with the rotational flow feeding bin, and a medium adding pipe for a gravity separation medium to pass through is arranged on the lower portion of the rotational flow feeding bin. The sorting process is effectively shortened, and the sorting efficiency is improved.

Description

Technical Field

[0001] This invention relates to the field of mineral processing and resource recycling technology, and in particular to a coarse-grained mineral sorting device and method adapted to the flow field characteristics and sorting process. Background Technology

[0002] With the intensification of global resource competition, the efficient development and utilization of coal and mineral resources plays a crucial role in ensuring energy supply security and promoting the development of emerging industries. As high-quality mineral resources are gradually depleted, low-grade and complex-composition mineral resources are increasing, leading to a gradual deterioration in mineral selectivity. Problems such as the simplistic structure and unsuitable flow field design of traditional coarse-grained separation equipment have increased the difficulty of separation.

[0003] Coarse-grained fluidized bed column separation technology is gradually becoming a research focus due to its significant potential in reducing energy consumption and utilizing tailings resources. Compared with traditional methods that rely on photoelectric separation and gravity separation to process large ore blocks, fluidization technology enables the efficient separation of millimeter-sized materials through precise control of gas-liquid flow to form a stable bed with clear density stratification and a continuously adjustable dynamic separation process for materials of different particle sizes and densities. This opens up new avenues for the deep pre-selection and disposal of low-grade mineral resources.

[0004] Mineralization is an indispensable part of the flotation process. High turbulence intensity promotes collisions between bubbles and mineral particles, as well as the spreading and modification of reagents on the particle surface. However, excessive turbulence during transport can cause desorption of flocculants, worsening mineral flotation recovery and reducing separation efficiency. Furthermore, the volatility of the rising water flow also affects the stability of the material bed during fluidized bed separation, resulting in unclear particle stratification by density, impacting bed uniformity, and deteriorating the fluidized bed separation environment for coarse materials. Summary of the Invention

[0005] Based on the above analysis, the present invention aims to provide a coarse mineral sorting device and method with flow field characteristics adapted to the sorting process, in order to solve the problem of poor sorting effect of existing coarse mineral sorting equipment.

[0006] On the one hand, the present invention provides a coarse mineral sorting device with flow field characteristics adapted to the sorting process, including a fluidized bed column and a cyclone feed hopper arranged concentrically; the cyclone feed hopper is located below the fluidized bed column, and the upper end of the cyclone feed hopper is connected to the lower end of the fluidized bed column;

[0007] The upper two sides of the cyclone feed hopper are provided with reagent inlets and slurry inlets, which are tangentially connected to the cyclone feed hopper. The lower part of the cyclone feed hopper is provided with a medium addition pipe for the passage of gravity separation medium.

[0008] Furthermore, the vortex feed hopper includes a first cylindrical section and a first inverted frustum section, with the first cylindrical section located at the upper end of the first inverted frustum section.

[0009] Furthermore, both the reagent inlet and the slurry inlet are located on the first cylindrical section, and the medium addition pipe is located at the lower part of the first inverted frustum section.

[0010] Furthermore, it also includes a slurry supply unit, which includes a slurry pump and two slurry delivery pipes. One end of one of the slurry delivery pipes is connected to the slurry inlet, and the other end is connected to the slurry pump. One end of the other slurry delivery pipe is connected to the slurry pump, and the other end is the slurry inlet.

[0011] Furthermore, it also includes a pharmaceutical unit, which includes a pharmaceutical delivery pipe and a pharmaceutical infeeding device. One end of the pharmaceutical delivery pipe is connected to the pharmaceutical inlet, and the other end is connected to the pharmaceutical infeeding device.

[0012] Furthermore, the fluidized bed column includes an overflow weir, a column body, and an overflow transition pipe arranged sequentially from top to bottom.

[0013] Furthermore, the column includes a second cylindrical section and a second inverted frustum section, the second cylindrical section being located above the second inverted frustum section, the upper end of the overflow transition pipe being connected to the bottom of the second inverted frustum section, and the lower end of the overflow transition pipe being connected to the top of the vortex feed hopper.

[0014] Furthermore, the fluidized bed column also includes pressure sensors, and multiple pressure sensors are provided on the column from top to bottom.

[0015] Furthermore, it also includes a water replenishment unit, an air supply unit, a bubble generator, and an air-water delivery unit, wherein the water replenishment unit, the air supply unit, and the air-water delivery unit are connected to the bubble generator.

[0016] Furthermore, the air-water delivery unit includes an air-water delivery pipe and multiple water distribution plates. One end of the air-water delivery pipe is connected to the bubble generator, and the other end is located in the upper part of the column and connected to the water distribution plates.

[0017] Furthermore, the fluidized bed column also includes an umbrella-shaped retardation block, which is disposed at the bottom of the inner cavity of the column; the umbrella-shaped retardation block includes a disc segment and a retardation segment, the disc segment is disposed on the retardation segment, the diameter of the retardation segment gradually increases from its bottom to the disc segment, and the outer wall of the retardation segment is a concave arc surface.

[0018] Furthermore, the fluidized bed column also includes a water inlet pipe, an air inlet pipe, and a filling block with an annular sleeve structure. The filling block is disposed in the column body and forms a variable diameter area. The water inlet pipe and the air inlet pipe are both arranged in annular array around the filling block.

[0019] Furthermore, one end of the water inlet pipe is located outside the column, and the other end is located in the filling block, and the outlet of the water inlet pipe is connected to the inner cavity of the column and faces upward; one end of the air inlet pipe is located outside the column, and the other end is located in the filling block, and the outlet of the air inlet pipe is connected to the inner cavity of the column and faces the gap between the umbrella-shaped blocking block and the column.

[0020] On the other hand, the present invention provides a method for sorting coarse minerals, which uses the above-mentioned coarse mineral sorting device to perform coarse mineral sorting operations.

[0021] Compared with the prior art, the present invention can achieve at least one of the following beneficial effects:

[0022] (1) The present invention has a cyclone feed hopper at the bottom of the fluidized bed column, and a reagent feed inlet and a slurry feed inlet at the upper end of the cyclone feed hopper. The reagent feed inlet and the slurry feed inlet are located on both sides of the fluidized bed column and are tangentially connected to the fluidized bed column. Before the fluidized bed separation stage, a "coupling of opposing feed cyclone mineralization and heavy medium pre-selection" structural design is adopted. On the one hand, the cyclone field generated by the cyclone structure can fully mix the slurry and collector fed into the cyclone chamber from opposite directions, optimize the contact effect between reagent molecules and mineral particles, replace the slurry conditioning tank to play an efficient slurry conditioning role, effectively shorten the separation process and improve the separation efficiency. On the other hand, the heavy medium density adjustment of the cyclone field can separate high and low density particles in the slurry, pre-remove some of the easier-to-separate tailings, effectively reduce the separation pressure of the subsequent fluidized bed column flotation stage and improve the flotation efficiency.

[0023] (2) The present invention adopts a structure of bottom umbrella-shaped blocking block and upper radial multi-layer water distribution plate working together. The umbrella-shaped blocking block at the bottom of the column impedes the flow velocity of the heavy medium swirling overflow into the feed, so that the feed slurry is fed into the bottom of the column in a relatively gentle manner, effectively avoiding the increase in turbulence intensity in the column caused by the introduction of swirling overflow into the feed, and constructing a microgravity static environment suitable for fluidized bed flotation, which effectively improves the flotation recovery rate of coarse minerals. The radial multi-layer water distribution plate is set in the column, and the feed water containing frother is fed into the column through the opening on the multi-layer water distribution plate, which overcomes the disadvantage of uneven bubble distribution caused by the bottom arrangement of the traditional water distribution plate, optimizes the radial distribution of bubbles in the column, and significantly improves the contact probability between bubbles and mineral particles in the static area, further promoting bubble-particle collision and optimizing the flotation effect.

[0024] (3) This invention adopts a "column with variable diameter based on the arrangement of annular openings for water supply at the top and air supply at the bottom" structure. By setting a filling block in the upper part of the column to reduce the cross-section of this area, the water velocity in the upper part of the fluidized bed is significantly increased while the flow rate remains unchanged. This effectively solves the problem of reduced water velocity in the upper part of the fluidized bed caused by uneven water velocity distribution at the bottom of the traditional fluidized bed, and effectively improves the static transport rate of particles. At the same time, an air inlet pipe and a water inlet pipe are introduced in the variable diameter area. The lower air supply hole is directly opposite the outer area of ​​the lower umbrella-shaped block. Before the slurry moves upward from all sides through the umbrella-shaped block, the particles are in full contact with the microbubbles fed in through the upper air supply hole. This effectively achieves efficient mineralization of the pre-selected slurry in the turbulent area under the umbrella-shaped block, and promotes the strengthening of the flotation process in the fluidized bed "float-gravity coupling" separation. The upper water supply is fed in through the water supply hole at a low speed. Without causing bubble-particle desorption, it works with the entire variable diameter structure to improve the gas floc transport rate. At the same time, the weak upward water flow can locally disturb the foam layer at the top of the fluidized bed, inducing the tailings particles carried by the water flow to fall off the foam layer, effectively improving the concentrate grade of fluidized bed flotation.

[0025] (4) This invention introduces gravity separation media into the cyclone section for pre-separation. While achieving efficient slurry conditioning, the introduction of media promotes the construction of a density-based cyclone field within the cyclone section. Furthermore, the quality of media addition can be adjusted according to the slurry density and the ideal separation density, thereby efficiently removing some easily separable coarse gangue minerals in advance. Simultaneously, permanent magnet rollers are installed at the concentrate overflow weir and tailings outlet to collect the lost media and recycle it within the device. This provides a certain reference and guidance for beneficiation plants to achieve cost reduction and efficiency improvement in separation equipment and flexible control of the separation process.

[0026] In this invention, the above-described technical solutions can be combined with each other to achieve more preferred combinations. Other features and advantages of this invention will be set forth in the following description, and some advantages may become apparent from the description or be learned by practicing the invention. The objects and other advantages of this invention can be realized and obtained from what is particularly pointed out in the description and drawings. Attached Figure Description

[0027] The accompanying drawings are for illustrative purposes only and are not intended to limit the invention. Throughout the drawings, the same reference numerals denote the same parts.

[0028] Figure 1 This is a schematic diagram of the coarse-grained mineral sorting device according to a specific embodiment;

[0029] Figure 2 This is a schematic diagram of the connection structure between the fluidized bed column and the vortex feed hopper in a specific embodiment;

[0030] Figure 3This is a schematic diagram of the connection structure between the overflow transition section and the vortex feed hopper in a specific embodiment;

[0031] Figure 4 This is a schematic diagram of the connection structure of the air-water delivery unit, the column, and the water inlet pipe and air inlet pipe in a specific embodiment.

[0032] Figure 5 This is a schematic diagram of the coarse-grained mineral sorting process in a specific embodiment.

[0033] Figure label:

[0034] 1-Fluidized bed column; 11-Overflow weir; 111-Concentrate discharge port; 12-Column; 121-Second cylindrical section; 122-Second inverted frustum section; 123-Tailgate; 124-Emergency discharge port; 125-Variable diameter zone; 13-Overflow transition pipe; 14-Pressure sensor; 15-Umbrella-shaped dam; 151-Disc section; 152-Damage section; 16-Filling block; 17-Water inlet pipe; 18-Air inlet pipe; 2-Swirl feed silo; 21-Reagent inlet; 22-Slurry inlet; 23-Media addition pipe; 24-Bottom Flow outlet; 25-First cylindrical section; 26-First inverted frustum section; 3-Slurry supply unit; 31-Slurry conveying pipe; 32-Slurry pump; 4-Reagent unit; 41-Reagent conveying pipe; 42-Reagent feeding device; 5-Water replenishment unit; 51-Clear water tank; 52-Water conveying pipe; 53-Centrifugal pump; 54-Liquid flow meter; 55-Solenoid control valve; 6-Air supply unit; 61-Air pump; 62-Air conveying pipe; 63-Gas flow meter; 7-Bubble generator; 8-Air-water conveying unit; 81-Air-water conveying pipe; 82-Water distribution tray. Detailed Implementation

[0035] The preferred embodiments of the present invention will now be described in detail with reference to the accompanying drawings, which constitute a part of the present invention and are used together with the embodiments of the present invention to illustrate the principles of the present invention, but are not intended to limit the scope of the present invention.

[0036] Example 1

[0037] A specific embodiment of the present invention discloses a coarse-grained mineral separation device (hereinafter referred to as the coarse-grained mineral separation device) adapted to the flow field characteristics and separation process, specifically relating to a coarse-grained separation and recovery equipment for mineral resources and secondary resources such as coal. This device is particularly suitable for the combined process of pre-crushing gangue removal and separation of coarse-grained minerals, aiming to achieve a highly efficient and precise flotation process for coarse-grained minerals, thereby improving their flotation efficiency and recovery rate.

[0038] like Figure 1 , Figure 2 and Figure 3As shown, the coarse mineral separation device includes a fluidized bed column 1 and a cyclone feed hopper 2 arranged concentrically. The cyclone feed hopper 2 is located below the fluidized bed column 1, and the upper end of the cyclone feed hopper 2 is connected to the lower end of the fluidized bed column 1. The upper end of the cyclone feed hopper 2 is provided with a reagent inlet 21 and a slurry inlet 22 on both sides. The reagent inlet 21 and the slurry inlet 22 are tangentially connected to the cyclone feed hopper 2. The lower part of the cyclone feed hopper 2 is provided with a medium addition pipe 23 for the passage of gravity separation medium.

[0039] Compared with the prior art, the coarse mineral separation device provided in this embodiment has a cyclone feed hopper 2 at the bottom of the fluidized bed column 1. The upper end of the cyclone feed hopper 2 has a reagent inlet 21 and a slurry inlet 22. The reagent inlet 21 and the slurry inlet 22 are located on both sides of the fluidized bed column 1 and are tangentially connected to the fluidized bed column 1. Before the fluidized bed separation stage, a "coupled structure of opposing feed cyclone mineralization and heavy medium pre-selection" is adopted. On the one hand, the cyclone field generated by the cyclone structure can fully mix the slurry and collector fed into the opposing cyclone chamber, optimize the contact effect between reagent molecules and mineral particles, and replace the slurry conditioning tank to play a high-efficiency slurry conditioning role, effectively shortening the separation process and improving the separation efficiency. On the other hand, the heavy medium density adjustment based on the cyclone field can separate high and low density particles in the slurry, pre-removing some of the easier-to-separate tailings, effectively reducing the separation pressure of the subsequent fluidized bed column flotation stage and improving the flotation efficiency. The pre-selection of the cyclone section effectively introduces slurry conditioning into the separation process, while providing technical reference for the concentrator to achieve a flexible separation and flotation process that combines high efficiency and speed, thereby reducing costs and increasing efficiency.

[0040] The feed vortexes of the reagent inlet 21 and the slurry inlet 22 are the same, meaning that the feed vortexes of the reagent and slurry after entering the vortex feed hopper 2 are the same, or the feed vortexes of the reagent inlet 21 and the slurry inlet 22 are opposite, meaning that the feed vortexes of the reagent and slurry after entering the vortex feed hopper 2 are opposite.

[0041] Furthermore, such as Figure 1 and Figure 2 As shown, the vortex feed hopper 2 has a bottom outlet 24 at its lower part. The vortex feed hopper 2 includes a first cylindrical section 25 and a first inverted frustum section 26. The first cylindrical section 25 is located at the upper end of the first inverted frustum section 26. The reagent inlet 21 and the slurry inlet 22 are both located on the first cylindrical section 25. The medium addition pipe 23 is located at the lower part of the first inverted frustum section 26 and communicates with the side wall of the first inverted frustum section 26. The bottom outlet 24 is located at the bottom of the first inverted frustum section 26. It should be noted that the first cylindrical section 25 and the first inverted frustum section 26 are distinguished by their external shape; their interiors are hollow.

[0042] For example, the inner diameter of the first cylindrical section 25 is selected to be 400-600 mm, preferably 500 mm, and the length is generally selected to be 100-300 mm, preferably 200 mm; the inclination angle of the first frustum section 26 is selected to be 45-75°, preferably 60°, and the height is generally selected to be 300-500 mm, preferably 400 mm. The density of the magnetite powder is 5.2 g / cm³. 3 The diameter is set to 0.045 mm, and the particle size content is above 90%.

[0043] It is worth noting that the lower walls of the reagent inlet 21 and the slurry inlet 22 are flush with the lower edge of the first cylindrical section 25.

[0044] Traditional slurry preparation processes rely on slurry preparation tanks, resulting in long and inefficient separation processes. This embodiment employs a cyclone separator structure (i.e., cyclone feed hopper 2), utilizing a tangential feeding method and cyclone chamber design to create a cyclone field that induces swirl, achieving forced mixing of mineral particles and reagents. Simultaneously, it introduces heavy media to construct a gravity field for density-based sedimentation, enhancing the pre-disposal process of easier-to-separate tailings particles, which are then separated according to density.

[0045] The slurry and collector enter the first cylindrical section 25 tangentially through the slurry inlet 22 and the reagent inlet 21, respectively. The slurry and collector are fed tangentially into the vortex chamber opposite each other, where they are thoroughly sheared and mixed under high-speed vortex action. The reagent is evenly dispersed and fully contacts the mineral particles, achieving efficient surface modification of the minerals. The addition of heavy media creates a density gradient based on the vortex field, causing high-density particles to spiral outwards and downwards under centrifugal force, and be discharged from the bottom outlet 24. Low-density particles experience less centrifugal force, remain in the internal space, gather towards the center, and spiral upwards into the fluidized bed separation stage, thus achieving pre-separation of coarse ore particles that would otherwise be discarded. The vortex feed silo 2 replaces the slurry conditioning tank, shortening the separation process and improving reagent utilization. At the same time, it pre-discards easily sorted tailings, reducing the load on subsequent fluidized bed separation. It achieves integrated "slurry conditioning-pre-separation," providing the concentrator with efficient and flexible process options and reducing investment and operating costs.

[0046] Understandably, such as Figure 1 As shown, the coarse mineral separation device also includes a slurry supply unit 3 and a reagent unit 4. The slurry supply unit 3 includes a slurry conveying pipe 31 and a slurry pump 32. The reagent unit 4 includes a reagent conveying pipe 41 and a reagent feeding device 42. One end of the slurry conveying pipe 31 is connected to the slurry inlet 22, and the other end is connected to the slurry pump 32. One end of the other slurry conveying pipe 31 is connected to the slurry pump 32, and the other end is the slurry inlet. One end of the reagent conveying pipe 41 is connected to the reagent inlet 21, and the other end is connected to the reagent feeding device 42.

[0047] Combination Figure 1 and Figure 2As shown, the fluidized bed column 1 includes an overflow weir 11, a column body 12, and an overflow transition pipe 13. The overflow weir 11 is located at the top of the column body 12, and the overflow transition pipe 13 is located at the bottom of the column body 12. The upper and lower ends of the overflow transition pipe 13 are respectively connected to the lower end of the column body 12 and the upper end of the vortex feed hopper 2. The overflow weir 11 is provided with a concentrate discharge port 111.

[0048] Preferably, combined with Figure 1 and Figure 2 As shown, the column 12 includes a second cylindrical section 121 and a second inverted frustum section 122. The second cylindrical section 121 is located above the second inverted frustum section 122. The upper end of the overflow transition pipe 13 is connected to the bottom of the second inverted frustum section 122, and the lower end of the overflow transition pipe 13 is connected to the top of the vortex feed hopper 2. The arrangement of the second inverted frustum section 122 is beneficial for the discharge of tailings. The inclination angle of the second inverted frustum section 122 is generally 10-30°, preferably 15°.

[0049] Understandably, such as Figure 2 As shown, the second inverted truncated cone section 122 is equipped with a tailings outlet 123 and an emergency discharge outlet 124. The length of one section of the inverted L-shaped tailings outlet 123 should not be too long, generally 0.1-0.3m, preferably 0.1m.

[0050] For example, the inner diameter of the second cylindrical section 121 is generally 0.4-1.0m, preferably 0.7m. Considering the sorting rate and efficiency, the height of the second cylindrical section 121 is generally 1.5-2.5 times its inner diameter, preferably 1.5m. The height of the second inverted frustum section 122 is generally set to 0.2m. The upper part of the overflow weir 11 is 0.1m higher than the top of the column 12, and the inclination angle is generally set to 15-35°. Considering increasing the coarse discharge rate and suppressing the clogging phenomenon, it is preferably 25°.

[0051] To monitor the pressure distribution within column 12 during the sorting process to determine whether ore discharge or equipment parameter adjustments are necessary, such as... Figure 1 and Figure 2 As shown, the fluidized bed column 1 also includes pressure sensors 14. Multiple pressure sensors 14 are installed on the column 12 from top to bottom, generally 3-8, preferably 4.

[0052] like Figure 1 As shown, the coarse mineral sorting device also includes a water replenishment unit 5, an air supply unit 6, a bubble generator 7, and an air-water conveying unit 8. The water replenishment unit 5 and the air supply unit 6 are connected to the bubble generator 7, and the air-water conveying unit 8 is connected to the bubble generator 7. That is, after the air and water are introduced into the bubble generator 7, they are conveyed to the column 12 by the air-water conveying unit 8.

[0053] Furthermore, such as Figure 1As shown, the water replenishment unit 5 includes a clean water tank 51, a water supply pipe 52, and a centrifugal pump 53. One end of the water supply pipe 52 is connected to the clean water tank 51, and the other end is connected to the centrifugal pump 53. Another water supply pipe 52 has one end connected to the centrifugal pump 53 and the other end connected to the bubble generator 7. To regulate the delivery of clean water, the water replenishment unit 5 also includes a liquid flow meter 54 and an electromagnetic control valve 55, both of which are mounted on the water supply pipe 52.

[0054] like Figure 1 As shown, the gas supply unit 6 includes a gas pump 61, a gas delivery pipe 62, and a gas flow meter 63. One end of the gas delivery pipe 62 is connected to the gas pump 61, and the other end is connected to the bubble generator 7. The gas flow meter 63 is installed on the gas delivery pipe 62.

[0055] like Figure 1 As shown, the air-water delivery unit 8 includes an air-water delivery pipe 81 and multiple water distribution plates 82. One end of the air-water delivery pipe 81 is connected to the bubble generator 7, and the other end is located in the upper part of the column 12 and connected to the water distribution plate 82.

[0056] In this embodiment, a multi-layer water distribution plate 82 is provided in the column 12. Water containing foaming agent is uniformly injected through the openings of the water distribution plate 82, forming a microbubble cluster and optimizing the radial distribution of bubbles in the fluidized bed space, promoting efficient bubble-particle contact. By optimizing the compatibility distribution of bubbles and water flow in the fluidized bed space through the multi-layer water distribution plate 82, the water distribution plate 82 forms an upward water flow, promoting particle sedimentation according to density interference, strengthening the gravity separation process in the "float-gravity coupling", and at the same time promoting faster flotation of concentrate particles in the upper space of the fluidized bed, increasing the flotation rate and improving the throughput of the device.

[0057] For example, the diameter of the water distribution tray 82 is generally 300-500mm, preferably 400mm. The spacing between the water distribution trays 82 is generally 200-400mm, preferably 300mm.

[0058] Considering that traditional fluidized beds are prone to introducing additional turbulence during feeding, disrupting the static separation environment, and that uneven bubble distribution at the bottom of column 12 can lead to poor separation of coarse mineral particles, this paper combines... Figure 1 and Figure 2 As shown, the fluidized bed column 1 also includes an umbrella-shaped hindrance block 15, which is located at the bottom of the inner cavity of the column body 12. The umbrella-shaped hindrance block 15 includes a disc segment 151 and a hindrance segment 152. The disc segment 151 is located on top of the hindrance segment 152. The diameter of the hindrance segment 152 gradually increases from its bottom towards the disc segment 151, and the outer wall of the hindrance segment 152 is a concave arc surface. The umbrella-shaped hindrance block 15 is integrally formed.

[0059] It should be noted that the umbrella-shaped blocking block 15 is welded and fixed to the bottom of the column 12 by a cross-shaped steel rod. Because the umbrella-shaped blocking block 15 is impacted by the slurry flow, a high-hardness wear-resistant steel plate made of wear-resistant material is required, with a Brinell hardness of up to 500 HBW, effectively suppressing the impact of particles in the slurry flow and the cavitation effect caused by the water flow. The umbrella-shaped blocking block 15 has a rectangular shape with two semicircles cut off in its side view. While blocking the slurry, the umbrella-shaped blocking block 15 utilizes its upward and outward guiding structure to direct the slurry flow to the sidewall of the column 12.

[0060] For example, the diameter of the umbrella-shaped blocking block 15 is generally 300-500 mm, preferably 400 mm. The height of the canopy is generally 50-100 mm, preferably 75 mm. The lower part has a symmetrical circular outline with a radius of generally 100-200 mm, preferably 150 mm.

[0061] In this embodiment, an umbrella-shaped deceleration block 15 is provided at the bottom of the column 12. The bottom of the umbrella-shaped deceleration block 15 breaks through the slurry flow that enters the bottom of the fluidized bed through the overflow transition pipe 13, and the particle flow velocity is gradually reduced along the concave transition sidewall of the lower part of the umbrella-shaped deceleration block 15 to avoid the additional turbulence disturbance induced by particle movement from affecting the separation flow field environment inside the fluidized bed. By slowing down the feed through the umbrella-shaped deceleration block 15, the additional kinetic energy of the particles is dissipated, and the slurry is fed in a gentle manner to promote the construction of a static separation environment.

[0062] In this embodiment, during the fluidized bed separation stage, a "bottom umbrella-shaped blocking block 15 - radial multi-layer water distribution plate 82 collaborative" structural design is adopted. An umbrella-shaped blocking block 15 is placed at the bottom of the fluidized bed to impede the flow velocity of the heavy medium swirling overflow into the feed, allowing the feed slurry to enter the bottom of the fluidized bed in a gentler manner. This effectively avoids the increased turbulence intensity within the column 12 caused by the introduction of swirling overflow, creating a microgravity static environment suitable for fluidized bed flotation and effectively improving the recovery rate of coarse minerals. On the other hand, a radial multi-layer water distribution plate 82 is set inside the column 12. Feed water containing frother is introduced into the fluidized bed through the multi-layer water distribution plate 82, overcoming the drawbacks of uneven bubble distribution caused by the traditional bottom arrangement of the water distribution plate. This optimizes the radial distribution of bubbles within the fluidized bed and significantly increases the contact probability between bubbles and mineral particles in the static area, further promoting bubble-particle collisions and optimizing the flotation effect. Meanwhile, the radial multi-layer water distribution plate 82 effectively constructs a microgravity environment suitable for particle fluidization, overcoming the interference of bottom water supply method that cannot achieve particle stratification along density within the entire column 12, and promoting the enhancement of gravity separation process in the fluidized bed "buoyancy-gravity coupling" separation.

[0063] Considering the insufficient water flow velocity at the top of traditional fluidized beds, slow particle transport, and low bubble-particle mineralization efficiency, in order to increase the flow velocity at the top of column 12, such as... Figure 1 and Figure 2As shown, the upper part of the inner cavity of the column 12 is a variable diameter area 125. The diameter of the variable diameter area 125 is smaller than the inner diameter of the upper and lower chambers. The water distribution plate 82 at the top is located in the variable diameter area 125.

[0064] To achieve the variable diameter at the upper part of column 12, combined with Figure 1 and Figure 2 As shown, the fluidized bed column 1 also includes a filling block 16, which is an annular sleeve structure located in the upper region of the fluidized bed column 1. A variable diameter region 125 is formed within the filling block 16. Exemplarily, the height of the filling block 16 is generally 150-250 mm, preferably 200 mm, and the upper end of the filling block 16 is positioned 200 mm from the top of the column 12. The thickness of the filling block 16 is generally 100-200 mm, preferably 150 mm.

[0065] Furthermore, combined Figure 1 , Figure 2 and Figure 4 As shown, the fluidized bed column 1 also includes a water inlet pipe 17 and an air inlet pipe 18. Multiple water inlet pipes 17 and air inlet pipes 18 are provided, arranged in a ring array around the filling block 16. One end of the water inlet pipe 17 is located outside the column 12, and the other end is located in the filling block 16, with its outlet communicating with the inner cavity of the column 12 and facing upwards, i.e., towards the overflow weir 11. One end of the air inlet pipe 18 is located outside the column 12, and the other end is located in the filling block 16, with its outlet communicating with the inner cavity of the column 12 and facing the gap between the umbrella-shaped blocking block 15 and the column 12. There are 6-10 water inlet pipes 17 and air inlet pipes 18, preferably 8.

[0066] The upper part of column 12 has a reduced cross-sectional area due to its variable diameter, which increases the water flow velocity while maintaining the same flow rate, accelerating the transport of concentrate particles in the upper space of column 12. The lower air inlet faces the outer area of ​​the umbrella-shaped retaining block 15, releasing microbubbles that come into contact with the rising slurry, increasing the probability of bubble-particle collision and achieving efficient mineralization. The upper water inlet disturbs the foam layer with an upward low-speed water flow, causing some of the entrained tailings to fall off, achieving secondary separation of concentrate particles. In addition, the introduction of low-speed water flow compensates for the inability of the central multi-layer water distribution plate 82 to simultaneously improve the transport of particles in the outer wall space, promoting rapid floating of particles across the entire cross-section and improving separation efficiency. This structure improves the upper particle transport rate, avoids particle deposition in the fluidized bed caused by high feed rates, enhances bubble-particle collision and mineralization efficiency, improves flotation rate, optimizes foam layer stability, improves concentrate grade, and achieves synergistic enhancement of flotation and gravity separation processes.

[0067] In this embodiment, a column diameter-variable structure design based on an upper water supply and lower air supply ring-shaped opening arrangement is adopted. By setting a filling block 16 in the upper region of the column 12 to reduce the cross-section of this region, the water velocity in the upper part of the fluidized bed is significantly increased while the flow rate remains unchanged. This effectively solves the problem of reduced water velocity in the upper part of the fluidized bed caused by uneven water velocity distribution at the bottom of the traditional fluidized bed, and effectively improves the static transport rate of particles. At the same time, an air inlet pipe 18 and a water inlet pipe 17 are introduced in the variable diameter zone 125. The lower air supply hole is directly opposite the outer region of the lower umbrella-shaped hindrance block 15. Before the slurry moves upward from all sides through the umbrella-shaped hindrance block 15, the particles are in full contact with the microbubbles fed in through the upper air supply hole. In the turbulent region below the umbrella-shaped hindrance block 15, efficient mineralization of the pre-selected slurry is effectively achieved, promoting the intensification of the flotation process in the fluidized bed "float-gravity coupling" separation. The upper water supply is fed in through the water supply hole at a low speed. Without causing bubble-particle desorption, it works with the entire variable diameter structure (i.e., the filling block 16) to increase the gas floc transport rate. At the same time, the weak upward water flow can locally disturb the foam layer at the top of the fluidized bed, inducing the tailings particles carried by the water flow to fall off the foam layer, effectively improving the concentrate grade of fluidized bed flotation.

[0068] It is worth noting that when the separation time is long, the material should be discharged in time through the emergency discharge port 124 to reduce the separation density. The heavy medium suspension is then recovered as qualified medium via the permanent magnet rollers after passing through the concentrate overflow weir 11, tailings port 123, and underflow port 24. During the separation period, qualified medium can also be added from the qualified medium tank in a timely manner according to the pressure difference signal feedback medium replenishment pipe to ensure the stability of the suspension separation density. For example, permanent magnet roller structures are set at the concentrate overflow weir 11 and tailings port 123 to adsorb magnetic heavy medium, which is then returned to the cyclone stage for reuse after rinsing, thereby reducing medium consumption and saving separation costs. The separation density can also be flexibly controlled by adjusting the amount of medium added to adapt to different ore properties.

[0069] This embodiment takes a fluidized bed device as the basic object and starts from the perspective of turbulent mixing-static separation coupling. It sets up a local structure adapted to the flotation process of coarse-grained minerals, and from the perspective of mineralization, introduces air-water flow to promote collision and adhesion and inhibit desorption. From the perspective of turbulent mineralization-static transport function design adapted to the flow field characteristics and separation process, it realizes the enhancement and quality improvement of the fluidized bed flotation process of coarse-grained minerals.

[0070] Example 2

[0071] Another specific embodiment of the present invention, such as Figure 5 As shown, a method for separating coarse-grained minerals is disclosed, using the coarse-grained mineral separating device of Example 1, including the following steps:

[0072] Step S1: Pre-filling of heavy medium in the cyclone section of fluidized bed column sorting

[0073] First, confirm that the accident discharge port 124 and tailings port 123 are closed to prevent accidental leakage of mineral particles to be sorted. After a thorough inspection confirms everything is correct, add heavy medium into the vortex section through the medium addition pipe 23. Once the medium reaches a reasonable mass range, close the medium addition pipe 23 and begin operation.

[0074] It should be noted that the amount of medium added is based on the liquid-to-solid ratio (i.e., the slurry volume (t / h) and the medium volume (m³)). 3 The liquid-to-solid ratio ( / h) is generally 1:5-1:3, preferably 1:4. That is, if the feed rate is 100t / h and the liquid-to-solid ratio is 4:1, then the amount of medium added is approximately 400m³. 3 / h.

[0075] In this step, a gravity separation medium is introduced for pre-sorting. While achieving efficient slurry conditioning, the introduction of the medium promotes the construction of a swirling field that separates according to density within the swirling section, thereby efficiently removing some of the more easily separated coarse gangue minerals in advance.

[0076] Step S2: Add foaming agent to pre-fluidize water

[0077] Add a foaming agent (generally 5-15 mg / L, adjusted according to the dispersion of bubbles) dropwise to the water tank 51 and introduce it into the column 12 along with the water. Foaming agents typically include pine oil (No. 2 oil), methyl isobutyl alcohol (MIBC), and diethyl phthalate, with pine oil (No. 2 oil) being preferred.

[0078] Open the electromagnetic control valve 55 on the water supply pipe 52 and simultaneously turn on the air pump 61. The clean water is pressurized by the centrifugal pump 53 and delivered to the bubble generator 7. The gas is delivered to the bubble generator 7. When the gas and water pass through the bubble generator 7, cavitation occurs due to the negative pressure in the throat, generating micro-nano-sized bubbles. These bubbles enter the column 12 through the water distribution plate 82 and disperse in the space of the column 12.

[0079] Once the pressure difference inside column 12 has stabilized, i.e. the fluidization state has stabilized (i.e. the reading of pressure sensor 14 inside column 12 shows no significant fluctuation), then close the clean water valve.

[0080] Step S3: Add collector to slurry section for conditioning

[0081] Collectors are introduced tangentially through the reagent inlet 21 (the dosage is generally set at 200-800 mg / L, adjusted according to the specific separation conditions). Common collectors include sodium ethyl xanthate, sodium isopropyl xanthate, sodium (potassium) butyl xanthate, and sodium (potassium) isobutyl xanthate, with sodium ethyl xanthate (ethyl xanthate) being the preferred choice. The concentration of the reagent in the slurry is controlled by adjusting the quality of the introduced reagent. Simultaneously, the slurry is tangentially fed into the vortex section (i.e., the vortex feed hopper 2) through the slurry inlet 22 via the slurry pump 32. The slurry concentration is set at 30-40% based on relevant research (adjusted according to specific experimental conditions and mineral properties).

[0082] After 1 minute of slurry conditioning in the cyclone section, the valve on the overflow transition pipe 13 is opened to allow the slurry to be fed into the column 12. High-density particles (generally magnetite powder) are used as the gravity separation additive in the cyclone section. While ensuring sufficient contact between the collector and the particles to achieve slurry conditioning, the particles are also encouraged to undergo density-based sedimentation according to Archimedes' principle to complete the separation process. Low-density concentrate rises through the overflow transition pipe 13 into the column 12, while tailings sink and are discharged through the underflow outlet 24. Permanent magnet rollers are installed at the tailings outlet 123 and the overflow weir 11 to recover the medium, enabling its recycling.

[0083] In this step, the slurry entering the bottom of the column 12 through the overflow transition pipe 13 first encounters the umbrella-shaped slurry block 15. The bottom of the umbrella-shaped slurry block 15 breaks through the slurry flow and gradually reduces the particle velocity along the concave transition sidewall of the slurry section 152, thus avoiding the additional turbulence disturbance induced by particle movement from affecting the separation flow field environment inside the column 12 and improving the recovery rate of coarse minerals.

[0084] Step S4: Concentrate collection and tailings discharge

[0085] When the slurry covers the top water distribution plate 82, the electromagnetic control valve 55 is opened, and the fluidized water mixed by the bubble generator 7 enters the column 12 through the multi-layer water distribution plate 82. When the slurry covers the top of the filling block 16, the water inlet pipe 17 and the air inlet pipe 18 are opened simultaneously to supply water and air.

[0086] In this step, the air inlet of the air inlet pipe 18 is positioned directly opposite the gap between the umbrella-shaped blocking block 15 and the column 12, so that the released microbubbles come into contact with the rising slurry, increasing the collision probability between the bubbles and the particles and achieving efficient mineralization. The water inlet of the water inlet pipe 17 disturbs the foam layer with an upward low-speed water flow, causing some of the entrained tailings to fall off, achieving secondary separation of the concentrate particles. In addition, the introduction of low-speed water flow compensates for the shortcomings of the multi-layer water distribution plate 82 in the center of the column 12 in not being able to improve the transport of particles in the outer wall space, promoting the rapid floating of particles across the entire cross section and improving the separation efficiency.

[0087] After sorting, the concentrate particles float upwards and are collected through the overflow weir 11 to the concentrate discharge port 111 for discharge. The tailings particles sink to the bottom of the column 12, and the tailings accumulation status is monitored in real time by the pressure sensor 14. When the pressure reaches the preset upper limit, the tailings port 123 valve is automatically opened to discharge the tailings; when the pressure drops to the preset lower limit, the valve closes to prevent excessive discharge from causing a sudden change in fluidized bed pressure and to ensure the stability of the fluidized bed layer.

[0088] The above description is only a preferred embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any changes or substitutions that can be easily conceived by those skilled in the art within the scope of the technology disclosed in the present invention should be included within the scope of protection of the present invention.

Claims

1. A coarse-grained mineral sorting device with flow field characteristics adapted to the sorting process, characterized in that, It includes a concentrically arranged fluidized bed column (1) and a vortex feed hopper (2); the vortex feed hopper (2) is located below the fluidized bed column (1), and the upper end of the vortex feed hopper (2) is connected to the lower end of the fluidized bed column (1); The upper two sides of the cyclone feed hopper (2) are provided with a reagent inlet (21) and a slurry inlet (22). The reagent inlet (21) and the slurry inlet (22) are tangentially connected to the cyclone feed hopper (2). The lower part of the cyclone feed hopper (2) is provided with a medium addition pipe (23) for the passage of gravity separation medium.

2. The coarse-grained mineral sorting device according to claim 1, characterized in that, The vortex feed hopper (2) includes a first cylindrical section (25) and a first inverted frustum section (26), with the first cylindrical section (25) located at the upper end of the first inverted frustum section (26).

3. The coarse-grained mineral sorting device according to claim 2, characterized in that, The reagent inlet (21) and the slurry inlet (22) are both located on the first cylindrical section (25), and the medium addition pipe (23) is located at the lower part of the first inverted frustum section (26).

4. The coarse-grained mineral sorting device according to any one of claims 1-3, characterized in that, It also includes a slurry supply unit (3), which includes a slurry pump (32) and two slurry conveying pipes (31). One end of one of the slurry conveying pipes (31) is connected to the slurry inlet (22), and the other end is connected to the slurry pump (32). One end of the other slurry conveying pipe (31) is connected to the slurry pump (32), and the other end is the slurry inlet.

5. The coarse-grained mineral sorting device according to any one of claims 1-3, characterized in that, It also includes a pharmaceutical unit (4), which includes a pharmaceutical delivery pipe (41) and a pharmaceutical feeding device (42). One end of the pharmaceutical delivery pipe (41) is connected to the pharmaceutical inlet (21), and the other end is connected to the pharmaceutical feeding device (42).

6. The coarse-grained mineral sorting device according to any one of claims 1-3, characterized in that, The fluidized bed column (1) includes an overflow weir (11), a column (12), and an overflow transition pipe (13) arranged sequentially from top to bottom.

7. The coarse-grained mineral sorting device according to claim 6, characterized in that, The column (12) includes a second cylindrical section (121) and a second inverted frustum section (122). The second cylindrical section (121) is located above the second inverted frustum section (122). The upper end of the overflow transition pipe (13) is connected to the bottom of the second inverted frustum section (122), and the lower end of the overflow transition pipe (13) is connected to the top of the vortex feed hopper (2).

8. The coarse-grained mineral sorting device according to claim 6, characterized in that, The fluidized bed column (1) also includes pressure sensors (14), and the column body (12) is provided with multiple pressure sensors (14) from top to bottom.

9. The coarse-grained mineral sorting device according to any one of claims 1-3 and 7-8, characterized in that, It also includes a water replenishment unit (5), an air supply unit (6), a bubble generator (7), and an air-water delivery unit (8), wherein the water replenishment unit (5), the air supply unit (6), and the air-water delivery unit (8) are all connected to the bubble generator (7).

10. A method for separating coarse-grained minerals, characterized in that, The coarse-grained mineral sorting device according to any one of claims 1-9 is used for coarse-grained mineral sorting operations.

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