A fluidized bed flotation device and separation method for mineralization and sorting

Abstract

The present invention provides a fluidized bed flotation device and a sorting method for mineralization and sorting separation, which relate to the field of mineral processing technology and aim to solve the technical problem of waste disposal of coarse-grained mineral particles before selection. The fluidized bed flotation device for mineralization and sorting separation comprises a fluidized bed column, a first foam flow generator, a flotation column, a feed pipe, a first overflow trough, and an annular distributor; the flotation column passes through the bottom wall of the first overflow trough and extends to the middle of the first overflow trough, and the fluidized bed column passes through the bottom wall of the flotation column and extends to the middle of the flotation column; the distributor surrounds the periphery of the fluidized bed column and is located near the bottom wall of the flotation column, and the distributor is connected to the first foam flow generator; the feed pipe passes through the first overflow trough from above the first overflow trough and extends to a position near the bottom wall of the fluidized bed column. The flotation device can effectively increase the upper limit of the flotation particle size of coarse particles.

Description

Technical Field

[0001] The present invention relates to the technical field of mineral processing, and in particular to a fluidized bed flotation device and a separation method for mineralization and separation. Background Art

[0002] Pre-selection and tailings discarding technology refers to a mineral separation technology that pre-selects and discards some low-grade ores before crushing, grinding and other operations to achieve pre-enrichment of the original ore. It has the advantages of improving the grade of ore entering the selection, reducing the amount of grinding and the discharge of fine tailings, improving the comprehensive utilization rate of ore, and reducing environmental pollution.

[0003] In related technologies, low-grade complex non-ferrous metal ores are generally finely embedded and evenly distributed, and there is no obvious density and magnetic difference at the coarse-grained scale. It is difficult to achieve pre-selection waste disposal through gravity separation and magnetic separation. It is urgent to develop a pre-selection waste disposal technology for non-ferrous metal ores at the millimeter scale. Summary of the Invention

[0004] The object of the present invention is to provide a fluidized bed flotation device and a separation method for mineralization and sorting, so as to solve the technical problem of discarding coarse-grained mineral particles before sorting.

[0005] In order to achieve the above object, the present invention provides the following technical solutions:

[0006] In a first aspect, the present invention provides a fluidized bed flotation device for mineralization-sorting separation, comprising a fluidized bed column, a first foam flow generator, a flotation column, a feed pipe, a first overflow trough, and an annular distributor;

[0007] The flotation column passes through the bottom wall of the first overflow tank and extends to the middle of the first overflow tank, and the fluidized bed column passes through the bottom wall of the flotation column and extends to the middle of the flotation column;

[0008] The distributor surrounds the periphery of the fluidized bed column and is located near the bottom wall of the flotation column. The distributor is connected to the first foam flow generator.

[0009] The feeding pipe passes through the first overflow trough from above the first overflow trough and extends to a position close to the bottom wall of the fluidized bed column.

[0010] According to at least one embodiment of the present invention, the flotation device further comprises a second froth flow generator, and one end of the fluidized bed column located outside the flotation column is in communication with the second froth flow generator.

[0011] According to at least one embodiment of the present invention, the feeding pipe is used to inject slurry into the fluidized bed column, and the second foam flow generator is used to form a fluidized bed layer from the slurry in the fluidized bed column.

[0012] According to at least one embodiment of the present invention, the height of the fluidized bed layer is consistent with the height of the fluidized bed column.

[0013] According to at least one embodiment of the present invention, the first foam flow generator forms an ascending foam flow in the flotation column through the distributor.

[0014] According to at least one embodiment of the present invention, the flotation column, the fluidized bed column, the feed pipe, and the distributor are all coaxial.

[0015] According to at least one embodiment of the present invention, the orthographic projection of the fluidized bed column on a preset plane is located within the orthographic projection of the flotation column on a preset plane, and the preset plane is parallel to a horizontal plane.

[0016] According to at least one embodiment of the present invention, the cross-sections of the flotation column and the fluidized bed column are both circular, and the ratio of the inner diameters of the flotation column to the fluidized bed column is in the range of (1.5-5):1.

[0017] According to at least one embodiment of the present invention, the flotation device further comprises a second overflow trough, wherein the first overflow trough penetrates the bottom wall of the second overflow trough and extends to the middle of the second overflow trough;

[0018] The feeding pipe passes through the second overflow trough and the first overflow trough in sequence from above the second overflow trough, and extends to a position close to the bottom wall of the fluidized bed column.

[0019] According to at least one embodiment of the present invention, the orthographic projection of the flotation column on a preset plane is located within the orthographic projection of the first overflow trough on the preset plane, and the preset plane is parallel to a horizontal plane.

[0020] According to at least one embodiment of the present invention, the cross-sections of the flotation column and the first overflow trough are both circular, and the ratio of the inner diameter of the flotation column to the inner diameter of the first overflow trough is in the range of 1:(1.2-3).

[0021] According to at least one embodiment of the present invention, the ratio of the height of the axis of the flotation column to the height of the axis of the first overflow tank is in the range of 1:(0.5-1).

[0022] According to at least one embodiment of the present invention, the orthographic projection of the first overflow trough on the preset plane is located within the orthographic projection of the second overflow trough on the preset plane.

[0023] According to at least one embodiment of the present invention, the flotation device further includes a controller and a second liquid level gauge and a second valve respectively communicatively connected to the controller, the second liquid level gauge being provided in the first overflow tank, and the second valve being provided on the bottom wall of the first overflow tank;

[0024] The controller is used to control the liquid level in the first overflow trough, and the liquid level is flush with the top of the first overflow trough.

[0025] According to at least one embodiment of the present invention, the flotation device further comprises a first level gauge and a first valve respectively connected to the controller for communication, the first level gauge being provided on the flotation column, and the first valve being provided on the bottom wall of the flotation column;

[0026] The controller is also used to control the amount of solids in the flotation column.

[0027] According to at least one embodiment of the present invention, the bottom wall of the flotation column, the bottom wall of the first overflow trough, and the bottom wall of the second overflow trough are all bottom walls inclined downward;

[0028] The first valve is located at the lower end of the bottom wall of the flotation column, and the second valve is located at the lower end of the bottom wall of the first overflow tank; and / or,

[0029] The flotation device further includes a third valve provided on the bottom wall of the second overflow trough, wherein the third valve is located at the lower end of the bottom wall of the second overflow trough.

[0030] According to at least one embodiment of the present invention, the distributor has a plurality of through holes, and the plurality of through holes are formed on the top surface of the distributor.

[0031] According to at least one embodiment of the present invention, both the first foam flow generator and the second foam flow generator include a Venturi tube.

[0032] According to at least one embodiment of the present invention, there are a plurality of first foam flow generators, and the first foam flow generators are evenly distributed along the circumference of the distributor.

[0033] In a second aspect, the present invention further provides a sorting method, which uses the flotation device described in the first aspect for sorting.

[0034] One or more technical solutions provided in the exemplary embodiments of the present invention can achieve at least one of the following beneficial effects.

[0035] The fluidized bed flotation device for mineralization and sorting separation of the exemplary embodiment of the present invention injects the slurry into the fluidized bed column through a feed pipe to form a fluidized bed layer, providing a low-turbulence flow field environment. Compared with the flotation equipment in the prior art, it makes the coarse particle mineralization environment more static, while increasing the phase content of the solid phase, significantly increasing the probability of collision between particles and bubbles, and providing an ideal mineralization environment for coarse particles. On the other hand, the slurry that undergoes preliminary mineralization in the fluidized bed column enters the flotation column from the top of the fluidized bed column, and the annular distributor arranged near the bottom wall of the flotation column can form a low-turbulence rising foam flow environment in the flotation column as an air floc separation environment, reducing the probability of desorption of coarse particle air flocs, while providing upward water flow drag for the coarse particle air flocs, significantly enhancing the flotation process of the coarse particles. Based on this, by separating mineralization from sorting, the coarse particle sorting efficiency can be significantly improved, and the upper limit of the flotation particle size can be increased, for example, the flotation of millimeter-scale mineral particles can be achieved.

[0036] Furthermore, as conventional fluidized bed flotation equipment scales up, the amount of particles required to be fluidized increases significantly with the equipment's size. Due to the inability to effectively control the amount of fluidized particles, the equipment requires a very large amount of circulating water to fluidize the particle bed, hindering the large-scale application of fluidized bed flotation equipment. The flotation apparatus of an exemplary embodiment of the present invention utilizes fluidized bed columns with controllable dimensions, thereby enabling control of the particle size in the fluidized bed. By separating the mineralization and sorting phases, the amount of circulating water required in the fluidized bed flotation columns is effectively reduced. BRIEF DESCRIPTION OF THE DRAWINGS

[0037] The accompanying drawings illustrate exemplary embodiments of the present invention and, together with the description, serve to explain the principles of the present invention. These drawings are included to provide a further understanding of the present invention and are incorporated in and constitute a part of this specification.

[0038] Figure 1 is a schematic diagram of the main structure of a fluidized bed flotation device according to an embodiment of the present invention;

[0039] Figure 2 It is a schematic diagram of the main structure of a fluidized bed flotation device according to another embodiment of the present invention.

[0040] Figure numerals: 10, flotation column; 11, first liquid level gauge; 12, first valve; 20, first overflow tank; 21, second liquid level gauge; 22, second valve; 30, second overflow tank; 32, third valve; 40, fluidized bed column; 41, second foam flow generator; 42, feeding pipe; 43, first pressure sensor; 44, second pressure sensor; 50, distributor; 51, first foam flow generator. DETAILED DESCRIPTION

[0041] In order to make the technical problems, technical solutions and beneficial effects to be solved by the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention.

[0042] Before introducing the embodiments of the present invention, the following definitions are given for the relevant terms involved in the embodiments of the present invention:

[0043] Mineralization refers to an important operation in the flotation process, that is, before flotation, necessary flotation reagents such as adjusters, inhibitors, sulfiding agents, dispersants, activators and collectors are added to the pulp, stirred in stages, and the pH value of the pulp or the inhibitory, activating and collecting effects of the reagents are adjusted in turn to make the pulp reach a state suitable for flotation requirements.

[0044] Figure 1 Schematic diagram of the main structure of the fluidized bed flotation device according to the embodiment of the present invention. Figure 1 As shown, the fluidized bed flotation apparatus for mineralization and sorting separation provided by an exemplary embodiment of the present invention includes a fluidized bed column 40, a first froth flow generator 51, a flotation column 10, a feed pipe 42, a first overflow trough 20, and an annular distributor 50. The flotation column 10 penetrates the bottom wall of the first overflow trough 20 and extends to the middle of the first overflow trough 20. The fluidized bed column 40 penetrates the bottom wall of the flotation column 10 and extends to the middle of the flotation column 10. The distributor 50 surrounds the periphery of the fluidized bed column 40 and is located near the bottom wall of the flotation column 10. The distributor 50 is connected to the first froth flow generator 51. The feed pipe 42 penetrates the first overflow trough 20 from above and extends to a position near the bottom wall of the fluidized bed column 40. The flotation apparatus also includes a second froth flow generator 41. One end of the fluidized bed column 40 located outside the flotation column 10 is connected to the second froth flow generator 41.

[0045] In actual application, the first foam flow generator 51 generates a foam flow that enters the annular distributor 50. Since the distributor 50 is located near the bottom wall of the flotation column 10, the foam flow enters the flotation column 10 through the openings on the surface of the annular distributor. The gas phase concentration in the flotation column 10 is high, while the solid phase concentration is low. The flotation column 10 generally presents an upward flow state, forming a low-turbulence rising foam flow sorting environment. The flotation column 10 is mainly a dilute phase rising foam flow environment, which provides a low-turbulence-rising drag floating environment for coarse particle gas flocs, and at the same time provides a secondary mineralization environment for some valuable minerals.

[0046] The low-turbulence dilute-phase rising foam flow environment formed in the flotation column 10 is conducive to the floating of coarse-grained gas flocs. It has the following two mechanisms: 1) it provides upward fluid drag for the coarse-grained gas flocs in addition to buoyancy; 2) the low-turbulence environment is conducive to reducing the probability of particle-bubble desorption.

[0047] Furthermore, compared to conventional fluidized bed flotation equipment, since the slurry particles are fluidized within the fluidized bed column 40 and sorted within the flotation column 10, the velocity of the rising froth flow within the flotation column 10 for sorting can be lower than that required for fluidization. Consequently, the amount of circulating water in the equipment is reduced during the process of increasing the size of the entire equipment.

[0048] The second foam flow generator 41 generates a foam flow that is injected into the fluidized bed column 40 at the bottom. After the rising foam flow in the flotation column 10 and the mineralized foam flow within the fluidized bed column 40 stabilize, slurry is injected into the fluidized bed column 40 from the top of the feed pipe 42. The slurry flows downward into the fluidized bed column 40 and gradually forms a fluidized bed layer under the action of the mineralized foam flow within the fluidized bed column 40. The movement speed of particles and bubbles in the fluidized bed layer is simultaneously reduced, thereby significantly enhancing the coarse particle-bubble mineralization efficiency.

[0049] Compared with traditional mechanical flotation machines, the fluidized bed flotation of the exemplary embodiment of the present invention realizes the separation of valuable minerals and gangue minerals in a stable three-phase fluidized bed based on the gravity-flotation coupling principle, its turbulence is significantly reduced, and the upper limit of flotation particle size is significantly improved.

[0050] After the mineralized foam flow of the fluidized bed column 40 of the exemplary embodiment of the present invention fills the entire fluidized bed column 40, a low-turbulence, high-phase-content dense-phase fluidized bed environment is formed. The mechanisms for enhancing the mineralization efficiency of coarse particles and bubbles include: 1) changing the free settling of particles in the dilute phase environment to interference settling, significantly reducing the movement speed of coarse particles; 2) the obstruction of the bubble bed by the particle bed significantly reduces the movement speed of bubbles, thereby increasing the particle-bubble interaction time and the probability of particle-bubble adhesion; 3) the high solid phase concentration and high gas phase concentration in the fluidized bed layer within the fluidized bed column 40 increase the particle-bubble collision frequency; 4) the low-turbulence mineralization environment within the fluidized bed column 40 reduces particle desorption, especially the desorption of coarse particles.

[0051] As can be seen from the above, by arranging the low-turbulence upwelling flow field environment of the flotation column 10 and the low-turbulence-high phase content dense phase fluidized bed environment of the fluidized bed column 40 in the same flotation device, an ideal mineralization and sorting environment is provided for coarse particles at the same time, thereby effectively improving the coarse particle sorting efficiency.

[0052] Exemplarily, the above-mentioned coarse particles refer to coarse particles of millimeter size. For example, non-ferrous metal mineral particles of about 1 mm are coarse particles, and coal particles larger than 1 mm are coarse particles.

[0053] Considering that in actual factory production, the flotation column 10 is relatively large, for example, having a diameter of several meters, this results in uneven rising foam flow in the flotation column 10. Exemplarily, there are multiple first foam flow generators 51, and each first foam flow generator 51 is evenly distributed along the circumference of the distributor 50. For example, two first foam flow generators 51 are symmetrically arranged on both sides of the distributor 50 so that the rising foam flow generated by various parts of the distributor 50 within the flotation column 10 is evenly distributed, thereby providing a low-turbulence rising foam flow environment and facilitating the secondary mineralization of mineral particles.

[0054] Specifically, the first foam flow generator 51 forms an ascending foam flow in the flotation column 10 through the distributor 50. Water is introduced into the inlet of the water flow distribution chamber, where it is split into two streams that flow into two venturi tubes and draw in air, forming a foam flow containing dispersed bubbles. The foam flow enters through the micropores on the surface of the annular distributor 50 and gradually fills the flotation column 10. The annular distributor 50 is located midway between the annular space between the flotation column 10 and the fluidized bed column 40.

[0055] In some embodiments, the second foam flow generator 41 has the same structure as the first foam flow generator 51. The second foam flow generator 41 introduces water into the inlet of the water flow distribution chamber, and the water flow is divided into two streams and flows into two venturi tubes respectively, and air is sucked in to form foam flows containing dispersed bubbles. The two foam flows enter the fluidized bed column 40 from the bottom of the fluidized bed column 40 to form a fluidized bed layer together with the slurry.

[0056] In some embodiments, as Figure 2 As shown, the distributor 50 has a plurality of through holes formed on the top surface of the distributor 50. The through holes are used for the foam flow to enter the flotation column 10 to form a low-turbulence rising foam flow.

[0057] For example, Figure 1 As shown, the flotation column 10, fluidized bed column 40, feed pipe 42, and distributor 50 are all coaxial. After undergoing primary mineralization in the fluidized bed column 40, the mineral particles overflow from the top of the fluidized bed column 40 and spread outward from the center of the flotation column 10. In the rising froth flow provided by the annular distributor 50, some of the particles undergo secondary mineralization, while the majority of the particles float upward and enter the first overflow trough 20.

[0058] In some embodiments, the height of the fluidized bed layer corresponds to the height of the fluidized bed column 40 .

[0059] Considering that fluidized bed flotation requires the use of an ascending water flow to suspend the particle bed, when the particle density is high and the particle size is coarse, the water circulation volume of the fluidized bed flotation equipment is extremely large. This significantly limits the application progress of fluidized bed flotation equipment and has become a practical problem that needs to be solved urgently in the process of large-scale fluidized bed flotation columns. The exemplary embodiment of the present invention uses a small-diameter fluidized bed column 40 arranged in the middle of a large-diameter flotation column 10 to solve this problem.

[0060] like Figure 1 As shown, the orthographic projection of the fluidized bed column 40 on the preset plane is located within the orthographic projection of the flotation column 10 on the preset plane, and the preset plane is parallel to the horizontal plane. The cross-sections of the flotation column 10 and the fluidized bed column 40 are both circular, and the ratio of the inner diameters of the flotation column 10 to the fluidized bed column 40 is in the range of (1.5-5):1. For example, the ratio of the inner diameters of the flotation column 10 to the fluidized bed column 40 is in the range of (2-5):1, optionally (2.5-4):1, and further optionally (3-3.5):1.

[0061] Because the diameter of the fluidized bed column 40 is smaller than, or even significantly smaller than, the diameter of the flotation column 10, the amount of particles requiring fluidization can be limited within the fluidized bed column 40 during the process of increasing the size of the flotation column equipment, while the size of the flotation column 10 used for separation can be increased. Therefore, the size of the fluidized bed and the amount of particles can be limited, thereby reducing the amount of circulating water required for fluidization. Furthermore, the amount of water within the flotation column 10 used for separation is also reduced, as fluidization is no longer required.

[0062] Figure 2 FIG. 1 is a schematic diagram of the main structure of a wide particle size material flotation device according to another embodiment of the present invention. Figure 2 As shown, the flotation device provided by the exemplary embodiment of the present invention further includes a second overflow trough 30, the first overflow trough 20 penetrates the bottom wall of the second overflow trough 30 and extends to the middle of the second overflow trough 30; the feeding pipe 42 penetrates the second overflow trough 30 and the first overflow trough 20 in sequence from above the second overflow trough 30, and extends to a position near the bottom wall of the fluidized bed column 40.

[0063] The flotation column 10, the first overflow trough 20, and the second overflow trough 30 are sequentially connected from bottom to top. The flotation column 10 penetrates the bottom wall of the first overflow trough 20 and extends to the middle of the first overflow trough 20. The first overflow trough 20 penetrates the bottom wall of the second overflow trough 30 and extends to the middle of the second overflow trough 30. The fluidized bed column 40 penetrates the bottom wall of the flotation column 10 and extends to the middle of the flotation column 10. It should be noted that the middle of each flotation column mentioned above refers to the middle position in the height direction.

[0064] Exemplarily, the orthographic projection of the flotation column 10 on the preset plane is located within the orthographic projection of the first overflow trough 20 on the preset plane, and the preset plane is parallel to the horizontal plane.

[0065] In actual application, coarse-grained nonferrous metal mineral materials are fed into the bottom of the fluidized bed column 40 through the top of the feed pipe 42. Under the action of the rising mineralized foam flow, a coarse-grained fluidized bed layer is gradually formed. The bed layer height continues to rise and fills the entire fluidized bed column 40, and finally flows into the flotation column 10. In this column, the coarse particles that have formed gas flocs float up under the action of the rising foam flow, and some valuable minerals that have not formed gas flocs undergo secondary mineralization and float up, while the gangue sinks to become tailings, which can be discharged from the flotation column 10. The mineralized gas flocs continue to flow upward into the first overflow trough 20. Since the inner diameter of the first overflow trough 20 is larger than that of the flotation column 10, the fluid slows down and becomes static. A fluid interface exists at the top of the first overflow trough 20. Therefore, in the first overflow trough 20, some coarse particles that are desorbed at the fluid interface at the top of the first overflow trough 20, as well as some extremely coarse particles with excessive mass, sink in the trough and become medium ore; while most of the gas flocs float up and enter the second overflow trough 30 to become concentrate.

[0066] When the flotation device is not provided with the second overflow trough 30, there is a fluid interface between the flotation column 10 and the first overflow trough 20. The coarse particles at this interface will increase the desorption probability, so that after the second overflow trough 30 is added (eliminating the fluid interface between the flotation column 10 and the first overflow trough 20), the middlings that should have been deposited in the first overflow trough 20 are desorbed at the fluid interface of the flotation column 10 to become tailings, which makes the grade of the tailings higher and the sorting effect worse.

[0067] In some embodiments, the cross-sections of the flotation column 10 and the first overflow trough 20 are both circular, and the ratio of the inner diameters of the flotation column 10 to the first overflow trough 20 is in the range of 1:(1.2-3), optionally 1:(1.5-2.5), and further optionally 1:2. The ratio of the heights of the axis of the flotation column 10 to the axis of the first overflow trough 20 is in the range of 1:(0.5-1).

[0068] It should be noted that the height of the axis of the flotation column 10 refers to the distance from the center point of the bottom wall of the flotation column 10 to its top opening. Similarly, the height of the axis of the first overflow trough 20 refers to the distance from the center point of the bottom wall of the first overflow trough 20 to its top opening.

[0069] In some embodiments, the orthographic projection of the first overflow trough 20 on a predetermined plane is located within the orthographic projection of the second overflow trough 30 on the predetermined plane. When the cross-section of the second overflow trough 30 is circular, the inner diameter of the second overflow trough 30 is larger than the inner diameter of the first overflow trough 20. A fluid interface exists at the top opening of the first overflow trough 20, and most of the gas flocs float up to the bottom wall of the second overflow trough 30, becoming concentrate.

[0070] In order to maintain the fluid interface at the top opening of the first overflow trough 20, the flotation device also includes a controller and a second liquid level gauge 21 and a second valve 22 respectively connected to the controller. The second liquid level gauge 21 is provided in the first overflow trough 20, and the second valve 22 is provided on the bottom wall of the first overflow trough 20. The controller is used to control the liquid level in the first overflow trough 20 so that the liquid level is flush with the top of the first overflow trough 20.

[0071] In practice, a second level gauge 21 is located near the bottom wall of the first overflow trough 20 to measure the liquid level there. A second valve 22 is located on the bottom wall of the first overflow trough 20 to discharge the middlings deposited there. A controller controls the opening of the second valve 22 based on the liquid level measured by the second level gauge 21, thereby adjusting the liquid level and maintaining a fluid interface at the top of the first overflow trough 20. This allows some coarse particles to desorb at this interface and allows some excessively coarse particles (gas flocs) to sink and become middlings.

[0072] When the material in the fluidized bed column 40 is mineralized, it is affected by Archimedes' principle and flows upward, overflows the fluidized bed column 40, and enters the flotation column 10. The gangue minerals settle in the flotation column 10, and the valuable mineral flocs float up. If too much material accumulates in the flotation column 10, it may cause bubble merger and deterioration of bubble distribution.

[0073] In order to solve the above problems, the flotation device of the exemplary embodiment of the present invention further includes a first liquid level gauge 11 and a first valve 12 respectively connected to the controller for communication. The first liquid level gauge 11 is provided on the flotation column 10, and the first valve 12 is provided on the bottom wall of the flotation column 10; the controller is also used to control the amount of solids in the flotation column 10.

[0074] In actual application, the first liquid level gauge 11 is set near the bottom wall of the flotation column 10. The controller can obtain the solid amount in the flotation column 10 through the difference between the second liquid level gauge 21 of the first overflow tank 20 and the above-mentioned first liquid level gauge 11. The controller controls the opening of the first valve 12, and then controls the discharge speed of the tailings to maintain the balance of the deposited solid amount in the flotation column 10.

[0075] To maintain a certain fluidized bed height in the fluidized bed column 40, the top opening of the fluidized bed column 40 is maintained at the middle of the height of the flotation column 10. Half of the fluidized bed column 40 can be located within the flotation column 10, while the other half is located in the external environment, providing sufficient space for fluidized mineralization of the slurry. Alternatively, two-thirds of the fluidized bed column 40 can be located within the flotation column 10, while the remaining one-third is located in the external environment below the bottom wall of the fluidized bed column 40.

[0076] In some embodiments, as Figure 2As shown, the bottom wall of the flotation column 10, the bottom wall of the first overflow trough 20, and the bottom wall of the second overflow trough 30 are all bottom walls inclined downward; the first valve 12 is located at the lower end of the bottom wall of the flotation column 10, and the second valve 22 is located at the lower end of the bottom wall of the first overflow trough 20; the flotation device also includes a third valve 32 provided on the bottom wall of the second overflow trough 30, and the third valve 32 is located at the lower end of the bottom wall of the second overflow trough 30.

[0077] When the cross-sections of the flotation column 10, the first overflow trough 20, and the second overflow trough 30 are all circular, the bottom walls of the three are all sloped to facilitate solid deposition and collection at the lower end of the bottom wall. For example, the first valve 12 is located at the lower end of the bottom wall of the flotation column 10, the second valve 22 is located at the lower end of the bottom wall of the first overflow trough 20, and the third valve 32 is located at the lower end of the bottom wall of the second overflow trough 30. The third valve 32 controls the discharge of concentrate, the second valve 22 controls the discharge of middlings, and the first valve 12 controls the discharge of tailings. Coarse tailings can be discarded, the concentrate is qualified, and the middlings are graded in a grading cyclone, then reground and flotation treated. Based on this, by raising the flotation upper limit of coarse particles, the coarse particle separation effect is enhanced, and the coarse particle minerals can be discarded before selection, reducing the amount of ore entering the mill and the amount of fine tailings discharged. At the same time, the coarse tailings are easier to dewater, transport, and recycle.

[0078] In some embodiments, as Figure 2 As shown, the flotation device of the exemplary embodiment of the present invention further includes a first pressure sensor 43 and a second pressure sensor 44. The first pressure sensor 43 and the second pressure sensor 44 are respectively arranged at the portion of the fluidized bed column 40 below the flotation column 10, and the first pressure sensor 43 is located below the second pressure sensor 44.

[0079] In practical applications, by adjusting the water volume or flow rate of the second foam flow generator 41, the pressure difference between the first pressure sensor 43 and the second pressure sensor 44 is maintained constant, thereby maintaining the fluidization state of the gas-liquid composite fluidized interference bed in the fluidized bed column 40, that is, the looseness of the fluidized bed can be controlled.

[0080] The exemplary embodiment of the present invention further provides a separation method, which uses the flotation device of the above embodiment to perform separation, and may include the following steps:

[0081] Step 101 : Generate a uniform rising foam flow through the distributor 50 and the first foam flow generator 51 and introduce it into the flotation column 10 .

[0082] Step 102: introducing water flow into the fluidized bed column 40 through the second foam flow generator 41 to generate a uniform rising foam flow.

[0083] Step 103: After the rising foam flows in steps 101 and 102 are stabilized, slurry is fed into the top of the feed pipe 42. The slurry flows downward into the fluidized bed column 40 and gradually forms a fluidized bed layer under the action of the foam flow in the column. The movement speed of the particles and bubbles in the fluidized bed layer is also reduced, thereby significantly improving its mineralization efficiency.

[0084] Step 104 : The controller controls the opening of the first valve 12 to maintain the amount of solid accumulation in the flotation column 10 .

[0085] Step 105 : The controller controls the opening of the second valve 22 according to the signal feedback from the second liquid level meter 21 to maintain the liquid level in the first overflow tank 20 at the same height as the first overflow tank 20 .

[0086] When the liquid level in the first overflow trough 20 is at the same height as the first overflow trough 20, there is no fluid interface between the first overflow trough 20 and the flotation column 10, thereby reducing the desorption probability of the coarse particle interface area. When the coarse particle gas flocs flow out of the flotation column 10 and directly enter the first overflow trough 20, due to the relatively increased inner diameter of the first overflow trough 20, some extremely coarse particle gas flocs and some coarse particle gas flocs desorbed due to the fluid interface between the first overflow trough 20 and the second overflow trough 30 all settle in the first overflow trough 20 and become medium ore.

[0087] Step 106: Through the combined effect of bubbles and rising water flow, a gas-liquid composite fluidized interference bed layer of bubbles and rising water flow is formed in the column body of the fluidized bed column 40. By adjusting the water volume or flow rate of the second foam flow generator 41, the pressure difference between the first pressure sensor 43 and the second pressure sensor 44 is maintained constant, thereby maintaining the fluidized state of the gas-liquid composite fluidized interference bed layer in the fluidized bed column 40, that is, the looseness of the fluidized bed layer can be controlled.

[0088] The technical advantages of the above-mentioned separation method over the prior art are the same as those of the above-mentioned flotation device, which will not be described in detail here.

[0089] It should be understood by those skilled in the art that the above embodiments are merely for the purpose of illustrating the present invention clearly, and are not intended to limit the scope of the present invention. For those skilled in the art, other changes or modifications may be made based on the above disclosure, and such changes or modifications are still within the scope of the present invention.

Claims

1. A fluidized bed flotation device for mineralization and separation, characterized in that: It includes a fluidized bed column, a first foam flow generator, a flotation column, a feed pipe, a first overflow tank and an annular distributor; The flotation column passes through the bottom wall of the first overflow tank and extends to the middle of the first overflow tank. The fluidized bed column passes through the bottom wall of the flotation column and extends to the middle of the flotation column. The flotation device also includes a second foam flow generator. One end of the fluidized bed column located outside the flotation column is connected to the second foam flow generator. The feeding pipe is used to inject the slurry into the fluidized bed column, and the second foam flow generator is used to form a fluidized bed layer with the slurry in the fluidized bed column; The flotation device further includes a second overflow trough, wherein the first overflow trough penetrates the bottom wall of the second overflow trough and extends to the middle of the second overflow trough; The feeding pipe passes through the second overflow trough and the first overflow trough in sequence from above the second overflow trough, and extends to a position close to the bottom wall of the fluidized bed column.

2. The flotation device according to claim 1, characterized in that The height of the fluidized bed layer is consistent with the height of the fluidized bed column.

3. The flotation device according to claim 1, characterized in that The first foam flow generator forms an ascending foam flow in the flotation column through the distributor.

4. The flotation device according to claim 1, characterized in that The flotation column, the fluidized bed column, the feed pipe and the distributor are all coaxial.

5. The flotation device according to claim 1, characterized in that The orthographic projection of the first overflow trough on a preset plane is located within the orthographic projection of the second overflow trough on the preset plane, and the preset plane is parallel to a horizontal plane.

6. The flotation device according to claim 1, wherein: The first foam flow generator and the second foam flow generator both include a Venturi tube.

7. A sorting method, characterized in that: The flotation device according to any one of claims 1 to 6 is used for separation.

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