A variable diameter fluidized bed flotation device and method suitable for coarse particle recovery

Abstract

The present application relates to a kind of rough particle recovery suitable for variable-diameter fluidized bed flotation device and method, belong to mineral processing and resource recovery technical field, solve the problems of one of the existing technology in the process of coarse-grained mineral preselection, gas flocculation is difficult to stabilize and float, particle is easy to detach and the problem of insufficient separation adaptability.The variable-diameter fluidized bed flotation device of the present application, including flotation column and static mixer, the static mixer is equipped with two, the flotation column includes fluidized bed column body, inlet is equipped in the middle lower part of the fluidized bed column body, two the static mixers are all arranged in the inside of the fluidized bed column body and respectively located the upper and lower sides of the inlet.The present application not only optimizes flow field distribution and mineralization environment, reduces the risk of rough particle loss, also enhances the adaptability of device under different ore conditions and multiple fluidization conditions.

Description

Technical Field

[0001] This invention relates to the field of mineral processing and resource recovery technology, and in particular to a variable diameter fluidized bed flotation device and method suitable for coarse particle recovery. Background Technology

[0002] Against the backdrop of declining ore grades and increasing pressure for energy conservation and emission reduction, traditional flotation equipment suffers from low efficiency and high energy consumption when processing coarse-grained minerals, making it difficult to meet modern mineral processing needs. Coarse-grained pre-selection and waste disposal technology has gradually become a research hotspot due to its ability to reduce grinding load, decrease tailings treatment pressure, and improve feed grade. Among these technologies, fluidized bed flotation technology, relying on the synergistic effect of gas-liquid-solid three-phase processes, demonstrates unique advantages in the flotation and recovery of millimeter-scale materials.

[0003] Fluidized bed flotation is a composite force field separation technology based on the gravity-buoyancy coupling effect. It relies on the synergistic effect of the gas-liquid-solid three-phase system, using the co-current upward flow of gas and liquid to propel mineral particles into a stable fluidized system, achieving highly selective separation of particles based on differences in density and floatability. Based on the spatial distribution of mineral particle concentration, fluidized bed flotation is typically divided into a main fluidized zone and a free space zone. In the main fluidized zone, particles collide with and adhere to air bubbles, achieving particle mineralization and forming flocs. These flocs, with a lower density than the bed, float according to Archimedes' principle and enter the free space zone. In the free space zone, the flocs rely on fluid drag and air bubble buoyancy for lifting and transport. However, when the flocs cross the interface between the main fluidized zone and the free space zone, the reduced fluid drag and density difference with the surrounding fluid cause them to struggle to float to the free space zone, remain suspended in the free space zone, or even fall back from it, resulting in low fluidized bed flotation efficiency. To address this issue, a common approach is to increase the upward flow velocity of the fluidized bed to enhance the stress on the air flocs. However, this approach introduces excessive turbulence into the main fluidized zone, deteriorating bed stability, which in turn reduces the probability of particle mineralization and increases the probability of desorption of the formed air flocs, ultimately affecting the overall flotation recovery rate. Summary of the Invention

[0004] Based on the above analysis, the present invention aims to provide a variable diameter fluidized bed flotation device and method suitable for coarse particle recovery, in order to solve one of the problems of existing equipment in the pre-selection process of coarse minerals, such as the difficulty in stable flotation of gas flocs, easy desorption of particles, and insufficient sorting adaptability.

[0005] On one hand, the present invention provides a variable diameter fluidized bed flotation device suitable for coarse particle recovery, including a flotation column and two static mixers. The flotation column includes a fluidized bed column, and a feed inlet is provided in the lower middle part of the fluidized bed column. The two static mixers are both located inside the fluidized bed column and are respectively located on the upper and lower sides of the feed inlet.

[0006] Furthermore, the flotation column also includes an overflow weir, which is located at the top of the fluidized bed column and has an overflow outlet.

[0007] Furthermore, the flotation column also includes a tailings cone and a discharge port, wherein the tailings cone is located at the bottom of the fluidized bed column and the discharge port is located at the bottom of the tailings cone.

[0008] Furthermore, the flotation column also includes an electromagnetic valve, which is disposed on the discharge port.

[0009] Furthermore, it also includes a slurry supply unit, an air supply unit, and a venturi tube, wherein the slurry supply unit and the air supply unit are both connected to the venturi tube, and the venturi tube is connected to the feed inlet.

[0010] Furthermore, the slurry supply unit includes a mixing tank, a conveying pump, and a conveying pipe.

[0011] Furthermore, the gas supply unit includes a gas pump, a first gas flow meter, and a gas delivery pipe.

[0012] Furthermore, it also includes a water supply unit, which comprises a water tank, a water pipe, and a water pump.

[0013] Furthermore, the water supply pipe and the gas supply pipe are connected by a pipeline.

[0014] Furthermore, it also includes a hydraulic variable diameter structure, which is located in the free space region. The hydraulic variable diameter structure includes a hydraulic rod assembly and an integrated sensing patch. The integrated sensing patch is uniformly arranged along the column of the free space region, and the hydraulic rod assembly is connected to the integrated sensing patch.

[0015] Furthermore, several through holes are made on the spiral blades of the static mixer.

[0016] On the other hand, the present invention provides a variable diameter fluidized bed flotation method, which uses the above-mentioned variable diameter fluidized bed flotation device to separate coarse-grained minerals.

[0017] Compared with the prior art, the present invention can achieve at least one of the following beneficial effects: (1) The present invention provides a static mixer in the fluidized bed column, and the static mixer is located on the upper and lower sides of the feed inlet. The static mixer is set within the axial range of the feed inlet. During the bidirectional flow process, it has the dual functions of enhancing mixing and stabilizing separation: on the one hand, it enhances the interaction of the gas-liquid-solid three-phase rising fluid, promotes the refinement and redispersion of bubbles, and increases the contact probability between particles and bubbles; on the other hand, the turbulence gradually decreases in the outlet area, forming a uniform flow field, which is conducive to the stable floating of mineralized particles and the secondary mineralization of unmineralized particles. At the same time, the static mixer plays a redispersion role on the sinking particles, reduces the particle settling velocity, increases the probability of its interaction with the rising gas and liquid, and realizes the secondary mineralization of particles.

[0018] (2) The present invention has multiple static mixers distributed in the bottom feeding area. This arrangement restricts the turbulence introduced by the jet slurry to the vicinity of the axial region of the feed inlet, which promotes the physical separation of the turbulent mineralization zone and the static separation zone. Under the premise of achieving stepwise mineralization, it constructs a low-turbulence, high-phase fluidized bed flotation static environment required for coarse particle flotation and promotes more concentrated and effective mixing of the gas-liquid-solid three phases. In addition, the lower static mixer also has the function of interception (avoiding slurry short circuit).

[0019] (3) The present invention uses a matrix hydraulic structure in the free space region to change the hydraulic diameter of the free space region in order to adjust the buoyancy behavior of the air flocs. This structure can maintain the balance and stability of the sorting environment under different mineral types, particle size compositions and various fluidization intensities, and ensure that the sorting density limit and sorting accuracy are not significantly affected by fluctuations within a wide range of working conditions, thereby significantly improving the adaptability and process stability of the device.

[0020] (4) This invention creates through-holes in the spiral blades of the static mixer, allowing some fluid to pass through. This generates accelerated flow and local eddies in the orifice region, enhancing convection and exchange between different fluid layers. The fluid flows along the spiral direction and undergoes radial exchange through the through-holes, resulting in more thorough mixing. The through-holes provide additional passageways for particles in the fluid; even if large particles are blocked in the spiral channel, they can still pass through the through-holes, reducing the probability of blockage. The through-hole structure allows the cleaning fluid to penetrate the blade layer and reach areas that are difficult to reach in traditional structures, reducing cleaning dead zones.

[0021] (5) This invention constructs a "two-stage gas replenishment-multi-stage mineralization" mode by optimizing the feed and bed fluidization conditions. In the feed stage, the slurry and gas are fully mixed to form a gas-containing jet, achieving initial collision mineralization; subsequently, in the local high-shear zone of the bed, the gas-liquid-solid three phases are fully dispersed and efficiently contacted, promoting secondary mineralization of particles; finally, in the main fluidization zone, the low-turbulence, high-phase-content bed environment maintains the stable buoyancy of mineralized particles, further improving mineralization efficiency. This multi-stage mineralization process significantly increases the collision and adhesion probability of particles and bubbles, increases the number of gas flocs, and thus effectively improves the recovery rate of coarse-grained minerals.

[0022] 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

[0023] 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.

[0024] Figure 1 This is a schematic diagram of the structure of a variable-diameter fluidized bed flotation device according to a specific embodiment; Figure 2 This is a schematic diagram of the flotation column in a specific embodiment; Figure 3 This is a schematic diagram of the internal structure of the flotation column in a specific embodiment; Figure 4 This is a schematic diagram of the static mixer in a specific embodiment; Figure 5 This is a schematic diagram of the automated control process for a hydraulic variable diameter structure according to a specific embodiment.

[0025] Figure label: 1-Flotation column; 11-Fluidized bed column; 12-Feed inlet; 13-Overflow weir; 131-Overflow outlet; 14-Tailings cone; 141-Discharge outlet; 15-Solenoid valve; 16-Free space zone; 17-Main fluidized zone; 18-Bowl-type water distribution plate; 2-Static mixer; 3-Slurry supply unit; 31-Agitator; 32-Feed pump; 33-Feed pipe; 34-Valve; 4-Air supply unit; 41-Air pump; 42-First gas flow meter; 43-Air pipe; 5-Venturi tube; 6-Water supply unit; 61-Water tank; 62-Water pipe; 63-Water pump; 64-Liquid flow meter; 7-Backflow check valve; 8-Second gas flow meter; 9-Hydraulic variable diameter structure; 91-Hydraulic rod assembly; 92-Integrated sensing patch. Detailed Implementation

[0026] 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.

[0027] Example 1 To address one of the problems existing equipment faces in the pre-selection of coarse-grained minerals, namely, difficulty in stable flotation of gaseous flocculation, easy particle detachment, and insufficient sorting adaptability, a specific embodiment of the present invention, combined with... Figure 1 , Figure 3 and Figure 4 As shown, a variable diameter fluidized bed flotation device suitable for coarse particle recovery is disclosed, including a flotation column 1 and two static mixers 2. The flotation column 1 includes a fluidized bed column 11, and a feed inlet 12 is provided in the lower middle part of the fluidized bed column 11. The two static mixers 2 are both located inside the fluidized bed column 11 and are located on the upper and lower sides of the feed inlet 12, respectively.

[0028] Compared with existing technologies, the variable-diameter fluidized bed flotation device for coarse particle recovery provided in this embodiment has a static mixer 2 installed inside the fluidized bed column 11. The static mixer 2 is located on both the upper and lower sides of the feed inlet 12, and is installed within the axial range of the feed inlet 12. During bidirectional flow, the static mixer 2 has a dual function of enhancing mixing and stabilizing separation: on the one hand, it enhances the interaction of the gas-liquid-solid three-phase rising fluid, promoting bubble refinement and redispersion, and increasing the contact probability between particles and bubbles; on the other hand, the turbulence gradually decreases in the outlet area, forming a uniform flow field, which is conducive to the stable flotation of mineralized particles and the secondary mineralization of unmineralized particles. At the same time, the static mixer 2 redisperses the sinking particles, reduces the particle settling velocity, and increases the probability of their interaction with the rising gas and liquid, thereby achieving secondary mineralization of the particles.

[0029] Considering the collection of concentrates, such as Figure 1 As shown, the flotation column 1 also includes an overflow weir 13, which is located at the top of the fluidized bed column 11.

[0030] To facilitate the discharge of concentrate, such as Figure 1 As shown, the overflow weir 13 is provided with an overflow outlet 131.

[0031] Considering the discharge of tailings, such as Figure 1 As shown, the flotation column 1 also includes a tailings cone 14 and a discharge port 141. The tailings cone 14 is located at the bottom of the fluidized bed column 11, and the discharge port 141 is located at the bottom of the tailings cone 14.

[0032] Understandably, in order to control the opening and closing of the ore discharge port 141, such as Figure 1As shown, the flotation column 1 also includes a solenoid valve 15, which is installed on the discharge port 141.

[0033] like Figure 1 As shown, the fluidized bed column 11 is divided into a main fluidized zone 17 and a free space zone 16 from bottom to top, and the feed inlet 12 and the static mixer 2 are located in the main fluidized zone 17.

[0034] Considering the supply of slurry and air to flotation column 1, such as Figure 1 As shown, the variable diameter fluidized bed flotation device also includes a slurry supply unit 3, an air supply unit 4, and a venturi tube 5. The slurry supply unit 3 and the air supply unit 4 are both connected to the venturi tube 5, and the venturi tube 5 is connected to the cross-shaped feed inlet 12.

[0035] like Figure 1 As shown, the slurry supply unit 3 includes a mixing tank 31, a conveying pump 32, and a conveying pipe 33. One end of the conveying pipe 33 is connected to the mixing tank 31, and the other end is connected to the venturi tube 5. The conveying pump 32 is connected to the conveying pipe 33, and the slurry in the mixing tank 31 is conveyed to the venturi tube 5 by the power of the conveying pump 32.

[0036] Considering the opening and closing of the conveying pipe 33, such as Figure 1 As shown, the slurry supply unit 3 also includes a valve 34, which is located on the conveying pipe 33 and is used to control the opening and closing of the conveying pipe 33 and to adjust the flow rate.

[0037] like Figure 1 As shown, the gas supply unit 4 includes a gas pump 41, a first gas flow meter 42, and a gas delivery pipe 43. One end of the gas delivery pipe 43 is connected to the gas pump 41, and the other end is connected to the venturi tube 5. The first gas flow meter 42 is installed on the gas delivery pipe 43 to monitor the gas flow rate.

[0038] like Figure 1 As shown, the variable diameter fluidized bed flotation device also includes a water supply unit 6, which includes a water tank 61, a water supply pipe 62 and a water pump 63. One end of the water supply pipe 62 is connected to the water tank 61, and the other end is connected to the inner cavity of the fluidized bed column 11.

[0039] In order to monitor water flow, such as Figure 1 As shown, the water supply unit 6 also includes a liquid flow meter 64, which is installed on the water supply pipe 62.

[0040] It is worth noting that, such as Figure 1 As shown, the water supply pipe 62 and the gas supply pipe 43 are connected by a pipeline, and a backflow check valve 7 is installed on this connecting pipeline. A second gas flow meter 8 is installed downstream of the backflow check valve 7.

[0041] like Figure 1 and Figure 3As shown, the flotation column 1 also includes a bowl-shaped water distribution plate 18, which is disposed inside the fluidized bed column 11.

[0042] Specifically, the bowl-shaped water distribution plate 18 has an internal pressure equalization cavity, and the bottom of the cavity is connected to the water supply pipe 62 introduced from the bottom of the bowl. The bowl-shaped structure wall is uniformly provided with a large number of micro-holes for spraying the mixed fluid into the fluidized bed column 11.

[0043] like Figure 1 , Figure 2 and Figure 3 As shown, the variable diameter fluidized bed flotation device also includes a hydraulic variable diameter structure 9, which is located in the free space region 16.

[0044] Specifically, such as Figure 2 and Figure 3 As shown, the hydraulic variable diameter structure 9 includes a hydraulic rod assembly 91 and an integrated sensing patch 92. The integrated sensing patch 92 is uniformly arranged along the cylinder of the free space region 16, and the hydraulic rod assembly 91 is connected to the integrated sensing patch 92. The integrated sensing patch 92 uses a high-strength wear-resistant material as the substrate, and an ERT electrode array distributed in a ring is integrated inside it through an in-situ pre-embedding process. Due to the high rigidity of the integrated sensing patch 92, the relative geometric spatial relationship between the electrodes remains constant as the electrode array moves radially with the hydraulic rod, thus providing stable static boundary conditions for the ERT imaging algorithm and ensuring the reconstruction accuracy of the flow field perception under dynamic variable diameter conditions.

[0045] In this embodiment, the hydraulic variable diameter structure 9 includes a circumferentially distributed hydraulic rod assembly 91 along the outer edge of the cylinder. The hydraulic rods are connected to the column frame (not shown in the figure) and the inner wall structure via circumferential patches. The patch near the cylinder contains an embedded high-performance flexible film. This film possesses unique dual characteristics of support and extensibility: its support is demonstrated by providing sufficient radial support force to ensure the cylinder's shape remains stable and does not deform under high-pressure flow field impacts during the diameter change process; its extensibility is demonstrated by its ability to synchronously stretch and compress with the stroke of the circumferential hydraulic rods, thereby driving a continuous change in the cylinder diameter. This "pattern + embedded film" design ensures the sealing performance and smoothness of the flow channel during the diameter change process. This design allows the hydraulic variable diameter structure 9 to achieve stepless adjustment of the cross-sectional area while maintaining sealing performance according to changes in bed conditions.

[0046] Example 2 Furthermore, to address the limited mixing effect of existing spiral static mixers, especially their poor performance under high viscosity or low flow rate conditions, another specific embodiment of the present invention discloses a variable-diameter fluidized bed flotation device suitable for coarse particle recovery. The difference from Embodiment 1 is that several through-holes are formed on the spiral blades, creating a "perforated" static mixer. Specifically, circular through-holes are uniformly arranged along the fluid flow direction on the surface of each section of the spiral blade. The inner diameter of the through-holes is preferably 10% to 20% of the blade width, and should not be too large to avoid damaging the spiral flow guiding channel. The spacing between adjacent through-holes is approximately 2 to 3 times the hole diameter.

[0047] In this embodiment, after creating through-holes in the helical blades, some fluid passes through the holes, generating accelerated flow and local eddies in the orifice region, enhancing convection and exchange between different fluid layers. The fluid flows along the helical direction and also undergoes radial exchange through the through-holes, resulting in more thorough mixing. The through-holes provide additional passageways for particles in the fluid; even if large particles are obstructed in the helical channels, they can still pass through the through-holes, reducing the probability of clogging. The through-hole structure allows the cleaning fluid to penetrate the blade layer and flush areas that are difficult to reach in traditional structures, reducing cleaning dead zones.

[0048] Example 3 To address one of the problems in the pre-selection process of coarse-grained minerals, namely, the difficulty in stable flotation of gaseous flocculation, easy desorption of particles, and insufficient adaptability to sorting, another specific embodiment of the present invention is as follows: Figure 5 As shown, a variable-diameter fluidized bed flotation method is disclosed, which uses the variable-diameter fluidized bed flotation device of Example 1 or 2 to separate coarse-grained minerals, including the following steps: Step 1: Safety check, start the equipment.

[0049] Specifically, before the sorting operation begins, first confirm that the solenoid valve 15 at the discharge port 141 is in the closed position to prevent accidental leakage of the minerals to be sorted. After confirming that everything is in order, start the rising medium flow system.

[0050] Step 2: Supply water and gas to create a mineralized environment.

[0051] Specifically, water pump 63 is turned on to deliver clean water from water tank 61 to bowl-shaped water distribution plate 18 and then into fluidized bed column 11. The water velocity is regulated by liquid flow meter 64. After the water velocity stabilizes, air pump 41 is turned on, and the air velocity is regulated by second gas flow meter 8. The gas is evenly distributed from bowl-shaped water distribution plate 18 into fluidized bed column 11, mixing with the water to form a stable gas-liquid co-current upward flow field. After the gas and water velocities stabilize, foaming agent is added to water tank 61 as needed to make the bubbles evenly distributed in fluidized bed column 11, further optimizing the mineralization environment.

[0052] Step 3: Feeding and flotation.

[0053] Specifically, the raw slurry is thoroughly mixed with the collector in the mixing tank 31 and then pumped to the inlet 12 by the feed pump 32. During the transportation process, gas is introduced into the slurry through the Venturi tube 5 and thoroughly mixed to form an aerated slurry, which then enters the main fluidization zone 17. The aerated slurry enters the main fluidization zone 17 in a high-speed jet manner, where it undergoes collision mineralization within the area defined by the static mixer 2, and is simultaneously impacted by the upward flow of gas and liquid provided by the bowl-shaped water distribution plate 18. The slurry enters the upper static mixer 2 and is redispersed and rapidly mixed along the mixer path under its shearing and disturbance effects, resulting in thorough mineralization of the particles. After passing through the upper static mixer 2, the particles form a stable fluidized bed in the upper half of the main fluidization zone 17, and further mineralization is achieved under the influence of the upward flow of gas and liquid and the density effect. Under the Archimedes effect, the mineralized particles gradually rise to the interface between the main fluidized zone 17 and the free space zone 16, and are transported to the free space zone 16 under conditions that overcome gravity. Meanwhile, the lower static mixer 2 plays a "secondary interception" role for the unmineralized particles: on the one hand, the particles are further dispersed in the channel due to local shear and structural disturbance, reducing their equivalent settling velocity and preventing rapid falling; on the other hand, the increased contact between the rising medium and the particles promotes the secondary mineralization of the unmineralized particles, thereby significantly improving the recovery rate of coarse particles.

[0054] Step 4: Variable diameter control.

[0055] Specifically, the mineralized particles float to the interface between the main fluidized zone 17 and the free space zone 16. The cross-sectional area of ​​the free space zone 16 is adjusted by the hydraulic variable diameter structure 9, thereby improving the buoyancy of the air floc. This structure achieves dynamic adjustment of the cylinder cross-sectional area based on the hydraulic rod drive principle. To facilitate understanding of the working principle of this structure, its buoyancy mechanism and integrated sensing principle are explained below: The buoyancy stability of aeroflocs in a fluidized field essentially depends on their force equilibrium state. Due to the large equivalent density and terminal settling velocity of coarse-particle aeroflocs, their dynamic behavior follows a high-precision settling model based on a modified Schiller-Naumann correlation, used to quantify their equivalent terminal settling velocity in the fluid. v t :

[0056] In this model, ρ p and ρ f These represent the equivalent density of the gas floc and the density of the slurry (kg / m³), respectively. μ The dynamic viscosity of the slurry is expressed in Pa·s. d pThe equivalent diameter of the air floc (m) is given. The coefficients 4 / 18.5 and the exponent 0.865 in the formula were experimentally quantified to represent the pressure drag on the particle surface in the transition flow region and the non-spherical characteristics of the air floc, respectively. When the local upward linear velocity... v The resulting kinetic margin is insufficient to overcome the equivalent final settlement velocity. v t When this happens, the particles will become stuck in the phase interface region, causing instability in the buoyancy process.

[0057] To eliminate such instability, the hydraulic diameter-changing structure 9 of this device adopts an integrated design of flexible coating film and flexible circuit patch. Its key feature is that an ERT (Electrical Resistance Tomography) electrode array is embedded in a ring array on the inner surface of the rigid patch. This design achieves spatial integration of the sensor and actuator: when the hydraulic rod drives the flexible patch to contract centripetally to change its cross-sectional area, the embedded electrode array undergoes synchronous radial displacement. This process ensures that the conductivity sensing point is always in close contact with the dynamic boundary of the flow field, effectively eliminating the measurement gain fluctuations and sensing blind spots of traditional fixed sensors during the diameter-changing process. Dynamic compensation is achieved using its axially distributed rectangular array actuator. (Uplift drag force) F d The compensation logic is as follows: According to the definition of fluid dynamics, the drag force on a particle is the fluid dynamic pressure acting on its projected area. A P The result (unit: square meters) is...

[0058] in, C d Let be a dimensionless drag coefficient. In exploring the unsteady state of variable diameter compensation, is explicitly introduced... A P This is used to accurately quantify the physical load generated by hydraulic action. When the hydraulic structure reduces the cylinder diameter from d1 to d2, the diameter reduction ratio is defined as... X ( ). This represents the actual flow velocity of the air-fluidized mass. Based on the fluid continuity equation, the local velocity after the diameter change is... v 2 evolves into initial flow velocity v A gain that is 1 times the square of the sum of its parts, i.e. .

[0059] Substituting this flow rate multiplication relationship into the drag force equation, we obtain the dynamic criterion after the diameter change:

[0060] This shows that as the diameter ratio X decreases, the local upflow velocity increases significantly, and the drag force rapidly increases. (At the equivalent settlement terminal velocity...) v tWhen the impact is relatively small, the traction force F d The relationship between the diameter ratio X and the diameter is approximately the negative fourth power, i.e. Therefore, even a small radial displacement of the hydraulic rod can bring about a significant dynamic compensation effect.

[0061] Ultimately, the entire regulation process is affected by the buoyancy stability factor. S f Closed-loop drive. This factor is defined as the upward force (buoyancy). F b With drag force F d (sum of) and downward gravity G The ratio is used to quantify the safety margin for particle buoyancy:

[0062] in V P and m P These represent the equivalent volume and mass of the air floc, respectively. The system will... S f It maintains a stable value above 1 in real time. Combined with the eddy current suppression and rectification effect of the static mixer 2 above, the device enhances... S f While increasing strength, it also prevents the desorption of air flocs caused by shear forces induced by sudden changes in local flow velocity during the control process, thus ensuring the efficient recovery of coarse particles in principle.

[0063] Based on this theoretical model, this device constructs a closed-loop adaptive control process through the integrated sensing patch 92. The system captures the electrical fingerprint of the built-in electrodes of the integrated sensing patch 92 in real time and extracts the axial velocity of the particle swarm using a cross-correlation algorithm. v And reconstruct the solid content of the cross section S The control unit inputs the above multi-parameter data into the dynamic evaluation model in real time to calculate the buoyancy stability factor. S f Once determined S f If the value is ≤1, the system immediately drives the integrated sensing patch 92 to perform a centripetal displacement. This action not only generates significant dynamic compensation, but also reconstructs the radial pressure gradient by utilizing the strong constraint effect of the rigid boundary on the flow field, achieving instantaneous intervention in the risk of coarse particle retention.

[0064] In summary, the hydraulic variable diameter structure 9 achieves cross-sectional contraction in the free space region, effectively controlling the buoyancy of the gas flocs and ensuring their stable transport to the overflow weir 13 before discharge from the overflow port 131. Unmineralized particles settle to the bottom of the device as tailings, and their accumulation status is monitored in real time by sensors. When the pressure reaches the upper limit, the tailings outlet solenoid valve 15 is opened to discharge the tailings, and it automatically closes when the pressure drops to the lower limit to avoid excessive discharge that could lead to bed instability.

[0065] Through the above steps, efficient recovery of coarse-grained minerals is achieved. The cross-shaped feed avoids disturbance in the free space region, the static mixer 2 enhances the gas-liquid-solid interaction and achieves interception of unmineralized particles, and the hydraulic variable diameter structure 9 gives the device good adaptability and sorting accuracy. The overall design not only improves sorting efficiency and stability, but also takes into account operational safety and ease of maintenance, and has significant application value and promotion prospects.

[0066] This invention, by introducing a cross-shaped feeder at the bottom, a static mixer, and a hydraulically variable diameter structure in the free space region, not only optimizes the flow field distribution and mineralization environment, reducing the risk of coarse particle loss, but also enhances the adaptability of the device under different ore conditions and various fluidization processes. While ensuring separation accuracy and recovery rate, the device maintains a simple structure and operational stability, providing a reliable technical solution for the efficient recovery and green treatment of coarse minerals.

[0067] 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 variable-diameter fluidized bed flotation device suitable for coarse particle recovery, characterized in that, It includes a flotation column (1) and a static mixer (2). There are two static mixers (2). The flotation column (1) includes a fluidized bed column (11). A feed inlet (12) is provided in the lower middle part of the fluidized bed column (11). The two static mixers (2) are located inside the fluidized bed column (11) and are respectively located on the upper and lower sides of the feed inlet (12).

2. The variable-diameter fluidized bed flotation device for coarse particle recovery according to claim 1, characterized in that, The flotation column (1) also includes an overflow weir (13), which is located at the top of the fluidized bed column (11) and has an overflow port (131).

3. The variable-diameter fluidized bed flotation device for coarse particle recovery according to claim 1, characterized in that, The flotation column (1) also includes a tailings cone (14) and a discharge port (141). The tailings cone (14) is located at the bottom of the fluidized bed column (11), and the discharge port (141) is located at the bottom of the tailings cone (14).

4. The variable-diameter fluidized bed flotation device for coarse particle recovery according to claim 3, characterized in that, The flotation column (1) also includes an electromagnetic valve (15), which is disposed on the discharge port (141).

5. The variable-diameter fluidized bed flotation device for coarse particle recovery according to any one of claims 1-4, characterized in that, It also includes a slurry supply unit (3), an air supply unit (4) and a venturi tube (5), wherein the slurry supply unit (3) and the air supply unit (4) are both connected to the venturi tube (5), and the venturi tube (5) is connected to the feed inlet (12).

6. The variable-diameter fluidized bed flotation device for coarse particle recovery according to claim 5, characterized in that, The slurry supply unit (3) includes a mixing tank (31), a conveying pump (32), and a conveying pipe (33).

7. The variable-diameter fluidized bed flotation device for coarse particle recovery according to claim 5, characterized in that, The gas supply unit (4) includes a gas pump (41), a first gas flow meter (42), and a gas delivery pipe (43).

8. The variable-diameter fluidized bed flotation device for coarse particle recovery according to claim 7, characterized in that, It also includes a water supply unit (6), which includes a water tank (61), a water pipe (62) and a water pump (63).

9. The variable-diameter fluidized bed flotation device for coarse particle recovery according to claim 8, characterized in that, The water pipe (62) and the gas pipe (43) are connected by a pipeline.

10. A variable-diameter fluidized bed flotation method, wherein the variable-diameter fluidized bed flotation device according to any one of claims 1-9 is used to separate coarse-grained minerals.

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