Wide-fraction material flotation equipment and method based on flow field regulation and control and multi-field coupling

Abstract

The invention relates to wide-fraction material flotation equipment and method based on flow field regulation and control and multi-field coupling, belongs to the technical field of mineral processing and resource recovery, and solves the problems of high mineral separation cost and poor flexibility in the prior art. The invention provides wide-fraction material flotation equipment based on flow field regulation and control and multi-field coupling. The wide-fraction material flotation equipment comprises a first grading cyclone, a coarse grain fluidized bed and a flotation machine. The coarse grain fluidized bed comprises a first column body, a first-stage distribution disc, a second-stage distribution disc and a second grading cyclone; the first grading cyclone is communicated with the first-stage distribution disc and the second-stage distribution disc, the second grading cyclone is communicated with the first-stage distribution disc and the second-stage distribution disc, the flotation machine is connected with the second-stage distribution disc, the first column body is communicated with the first-stage distribution disc, and the first grading cyclone is simultaneously communicated with the first column body and the second-stage distribution disc. The mineral separation effect is good, the energy utilization rate is high, cost is low, and flexibility is high.

Description

Technical Field

[0001] The present invention relates to the technical field of mineral processing and resource recovery, and particularly to a flotation equipment and method for wide-size particle materials based on flow field regulation and multi-field coupling. Background Art

[0002] With the gradual consumption of high-quality mineral resources, the low-grade, fine-grained, and complex-component mineral resources are increasing day by day. At the same time, the proportion of coarse and fine-grained minerals that are difficult to separate in minerals has increased significantly, showing a wide-size particle distribution, and it is difficult for traditional flotation equipment technology to effectively recover. Secondary resources such as smelting slag with recovery value also show a two-pole distribution of coarse and fine, increasing the separation difficulty.

[0003] The coarse particle fluidized bed column separation technology is gradually becoming the focus of research due to its significant potential in reducing energy consumption and tailings resources. Compared with the traditional methods that rely on optoelectronic beneficiation and gravity separation to process large ore pieces, the emergence of the fluidized bed column separation technology makes the efficient separation of millimeter-sized materials possible, opening up a new path for the deep preselection and abandonment of low-grade mineral resources. Traditional flotation machines have good separation effects for conventional materials below 0.5 mm. However, in the actual separation process, due to the wide particle size distribution of the materials, they often need to be classified and fed into different separation systems for separation. On the one hand, this requires the design of corresponding classification systems, greatly increasing the separation cost; on the other hand, the separation process is relatively complex, and the lack of a suitable control and detection system will affect the flexibility of the separation process and the prevention and maintenance of faults. Summary of the Invention

[0004] In view of the above analysis, the embodiments of the present invention aim to provide a flotation equipment and method for wide-size particle materials based on flow field regulation and multi-field coupling to solve the problems of high separation cost and poor separation flexibility caused by the wide-size particle distribution of existing complex minerals.

[0005] On the one hand, the present invention provides a flotation equipment for wide-size particle materials based on flow field regulation and multi-field coupling, including a first classification cyclone, a coarse particle fluidized bed, and a flotation machine; the coarse particle fluidized bed includes a first column body, a primary distribution plate, a secondary distribution plate, and a second classification cyclone;

[0006] The first classification cyclone is simultaneously connected to the first column body and the secondary distribution plate, the second classification cyclone connects the primary distribution plate and the secondary distribution plate, the flotation machine is connected to the secondary distribution plate, and the first column body is connected to the primary distribution plate.

[0007] Further, it further includes a slurry unit, and the slurry unit is connected to the first classification cyclone.

[0008] Further, the primary distribution plate and the secondary distribution plate are both arranged on the first cylinder, and the primary distribution plate is located above the secondary distribution plate.

[0009] Further, there are multiple second classification cyclones and multiple flotation machines, and the multiple second classification cyclones and the multiple flotation machines are evenly arranged around the first cylinder.

[0010] Further, the second classification cyclone is arranged between the primary distribution plate and the secondary distribution plate, and the flotation machine is arranged below the secondary distribution plate.

[0011] Further, the slurry unit includes a slurry mixing tank, a first centrifugal pump, and a first pipeline. The first centrifugal pump is arranged on the first pipeline. One end of the first pipeline is connected to the slurry mixing tank, and the other end is connected to the feed inlet of the first classification cyclone.

[0012] Further, it further includes a water and gas unit. The water and gas unit includes a water tank, a fourth pipeline, and a water distribution plate. One end of the fourth pipeline is connected to the water tank, and the other end is connected to the water distribution plate.

[0013] Further, the water and gas unit further includes an air pump, a fifth pipeline, and a first bubble generator. Both ends of the fifth pipeline are respectively communicated with the air pump and the first bubble generator.

[0014] Further, it further includes a medicine adding component.

[0015] On the other hand, the present invention provides a flotation method, which uses the above-mentioned wide particle size material flotation equipment based on flow field regulation and multi-field coupling to perform flotation operations on materials.

[0016] Compared with the prior art, the present invention can at least achieve one of the following beneficial effects:

[0017] (1) In the present invention, a primary distribution plate, a secondary distribution plate, and a flotation machine are arranged on the outer side of the first cylinder. The flotation machine is communicated with the secondary distribution plate. The primary distribution plate is connected to the secondary distribution plate through a second classification cyclone. The first cylinder is connected to the primary distribution plate. The slurry unit is connected to the first classification cyclone. The first classification cyclone is also connected to the first cylinder and the secondary distribution plate at the same time. The pulp first passes through the first classification cyclone for classification. Some fine-grained materials after classification enter the secondary distribution plate from the upper opening of the first classification cyclone through pumping. Other coarse-grained materials enter the coarse-grained fluidized bed for separation. The fine-grained minerals after separation are then distributed by the primary distribution plate and then classified by the second classification cyclone. The fine-grained minerals after classification are mixed with the fine-grained materials in the secondary distribution plate and then enter the flotation machine for separation, which can reduce the ineffective treatment amount of the fluidized bed in the coarse-grained separation stage, improve the energy utilization rate, and improve the flexibility of separation.

[0018] (2) In the present invention, an array - type multi - layer ultrasonic oscillator group formed by ultrasonic oscillators and connecting rods is provided near the inner wall of the first cylinder. When the feedstock after classification by the first classifier cyclone is fed into the fluidized bed, the ultrasonic oscillators are started. The multi - layer ultrasonic oscillator group arranged in an array along the wall can optimize the spatial distribution of the ultrasonic force field by releasing ultrasonic waves, strip and disperse the fine mud adhered to the coarse - grained materials, effectively reduce the pollution of the coarse - grained concentrate tailings, strengthen the crushing of aggregates, and at the same time further promote the dispersion of emulsifying agents to improve the separation efficiency. The ultrasonic oscillators, together with the magnetic field regulator via a proportional logic circuit, realize the loosening and separation of the materials in the fluidized bed. At the same time, magnetic field regulators are provided at the upper and lower ends of the first cylinder. The double - layer magnetic field regulator controls the dispersion of the magnetite fluidization medium by regulating the magnetic field intensity, thereby realizing the density classification of the bed layer, constructing a micro - gravity environment for material density classification, effectively realizing the "float - gravity coupling" in the coarse - grained separation stage, and reducing the separation cost.

[0019] (3) In the present invention, a track groove is provided inside the second cylinder. One end of the driven block is connected to the track groove, and the other end is connected to the annular baffle. One end of the traction wire is connected to the driven block, and the other end bypasses the fixed pulley and is connected to the stepping motor. The fixed pulley is provided at the top of the second cylinder. The rotation of the stepping motor drives the driven block to move up and down along the track groove, thereby adjusting the position of the annular baffle inside the second cylinder. Below the annular baffle is the area of intense collision and mineralization, which promotes the three - phase interaction of particles, bubbles, and reagents, improving the mineralization efficiency. Above the annular baffle is the static separation and transportation area. The approximately static space is more suitable for the separation and transportation after the adhesion of particles - bubbles, effectively suppressing the phenomenon of turbulent desorption and improving the final recovery rate of mineral particles.

[0020] In the present invention, the above - mentioned technical solutions can also be combined with each other to achieve more preferred combined solutions. Other features and advantages of the present invention will be described in the subsequent specification. And some advantages can be made obvious from the specification, or understood by implementing the present invention. The objectives and other advantages of the present invention can be realized and obtained from the content specifically pointed out in the specification and the drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] The drawings are only for the purpose of showing specific embodiments and are not considered as a limitation to the present invention. Throughout the drawings, the same reference signs represent the same components.

[0022] Figure 1 It is a schematic structural diagram of a wide - particle - size material flotation device for a specific embodiment;

[0023] Figure 2 It is a schematic connection structure diagram of an ultrasonic oscillator, a magnetic field regulator, and the first cylinder for a specific embodiment;

[0024] Figure 3Top view schematic diagram of the flotation equipment for wide particle size materials in a specific embodiment;

[0025] Figure 4 Schematic diagram of the connection relationship between the second cylinder and the annular baffle in a specific embodiment;

[0026] Figure 5 Schematic diagram of the structure of the spiral conveying pipeline in a specific embodiment.

[0027] Reference numerals:

[0028] 100 - slurry unit; 101 - slurry mixing tank; 102 - first centrifugal pump; 103 - first flowmeter; 104 - first pipeline; 105 - first valve; 200 - first classification cyclone; 201 - feed pipe; 202 - second pipeline;

[0029] 300 - coarse particle fluidized bed; 301 - first cylinder; 302 - primary distribution plate; 303 - secondary distribution plate; 304 - second classification cyclone; 305 - overflow weir; 306 - concentrate outlet; 307 - emergency discharge port; 308 - tailing outlet; 309 - first solenoid valve; 310 - third pipeline; 311 - second centrifugal pump; 312 - first pressure sensor; 313 - ultrasonic vibrator; 314 - magnetic field regulator; 315 - connecting rod;

[0030] 400 - flotation machine; 401 - second cylinder; 402 - electrically controlled stirring shaft; 403 - excitation motor; 404 - impeller; 405 - stirrer; 406 - make - up water pipe; 407 - discharge pipe; 408 - second solenoid valve; 409 - second pressure sensor; 410 - rotating scraper; 411 - spiral scraper discharge device; 412 - annular baffle; 413 - driven block; 414 - towing line; 415 - fixed pulley; 416 - stepping motor; 417 - track groove;

[0031] 500 - water - gas unit; 501 - water tank; 502 - fourth pipeline; 503 - water distribution plate; 504 - first bubble generator; 505 - second flowmeter; 506 - third centrifugal pump; 507 - second valve; 508 - air pump; 509 - fifth pipeline; 510 - third flowmeter; 600 - chemical addition assembly; 601 - sixth pipeline; 602 - fourth centrifugal pump; 603 - second bubble generator; 700 - qualified medium tank; 701 - make - up pipe. Detailed implementation manners

[0032] The following will specifically describe the preferred embodiments of the present invention in conjunction with the accompanying drawings, in which the accompanying drawings form a part of the present invention and are used together with the embodiments of the present invention to explain the principles of the present invention, rather than to limit the scope of the present invention.

[0033] Embodiment 1

[0034] A specific embodiment of the present invention, in combination with Figure 1 and Figure 3 As shown, a flotation equipment for wide-size materials based on flow field regulation and multi-field coupling is disclosed, which includes a first classification cyclone 200, a coarse particle fluidized bed 300 and a flotation machine 400. The coarse particle fluidized bed 300 includes a first cylinder 301, a primary distribution plate 302, a secondary distribution plate 303 and a second classification cyclone 304. The primary distribution plate 302 and the secondary distribution plate 303 are both arranged on the first cylinder 301. The second classification cyclone 304 connects the primary distribution plate 302 and the secondary distribution plate 303. The flotation machine 400 is connected to the secondary distribution plate 303. The first classification cyclone 200 is simultaneously connected to the first cylinder 301 and the secondary distribution plate 303, and the first cylinder 301 is connected to the primary distribution plate 302.

[0035] Compared with the prior art, in the flotation equipment for wide-size materials provided in this embodiment, a primary distribution plate 302, a secondary distribution plate 303 and a flotation machine 400 are arranged on the outer side of the first cylinder 301. The flotation machine 400 is connected to the secondary distribution plate 303. The primary distribution plate 302 is connected to the secondary distribution plate 303 through the second classification cyclone 304. The first cylinder 301 is connected to the primary distribution plate 302. The first classification cyclone 200 is simultaneously connected to the first cylinder 301 and the secondary distribution plate 303. The pulp first passes through the first classification cyclone 200 for classification. Some fine particle materials are pumped into the secondary distribution plate 303 from the upper opening of the first classification cyclone 200 after classification. Other coarse particle materials enter the coarse particle fluidized bed 300 for separation. The fine particle minerals after separation are then distributed by the primary distribution plate 302 and classified by the second classification cyclone 304. The fine particle minerals after classification are mixed with the fine particle materials in the secondary distribution plate 303 and then enter the flotation machine 400 for separation, which can reduce the ineffective treatment amount of the fluidized bed in the coarse particle separation stage, improve the energy utilization rate and the flexibility of separation.

[0036] Preferably, the first classification cyclone 200 and the second classification cyclone 304 have the same structure. The inner diameter of the classification cylinder section of the classification cyclone is selected to be 100 - 300 mm, preferably 200 mm. The length is generally selected to be 100 - 300 mm, preferably 200 mm. The inclination angle of the conical section is selected to be 45 - 75°, preferably 60°. The height is generally selected to be 200 - 300 mm.

[0037] As Figure 1As shown, there are multiple second-stage classification cyclones 304 and multiple flotation machines 400. The multiple second-stage classification cyclones 304 and the multiple flotation machines 400 are both arranged evenly around the first cylinder 301. The first-stage distribution plate 302 is located above the second-stage distribution plate 303, and both the first-stage distribution plate 302 and the second-stage distribution plate 303 are located in the upper-middle part of the coarse particle fluidized bed 300. The second-stage classification cyclone 304 is arranged between the first-stage distribution plate 302 and the second-stage distribution plate 303. The flotation machine 400 is arranged below the second-stage distribution plate 303.

[0038] Preferably, the number of the second-stage classification cyclones 304 is the same as that of the flotation machines 400. There are 4 flotation machines 400, and the 4 flotation machines 400 are arranged in an array on the outer side of the first cylinder 301, with an interval of 90°. The relative arrangement position with the built-in fluidized bed is generally: the upper edge of the sorting tank of the flotation machine 400 is located at 1 / 5 - 1 / 3 of the length of the lower cylinder section of the fluidized bed, preferably 1 / 4 of the length of the cylinder section.

[0039] As Figure 1 shown, the wide particle size material flotation equipment further includes a slurry unit 100, and the slurry unit 100 is communicated with the first-stage classification cyclone 200. Considering the transportation of pulp into the first cylinder 301, as Figure 1 shown, the slurry unit 100 includes a pulp mixing tank 101, a first centrifugal pump 102, a first flow meter 103 and a first pipeline 104. The first centrifugal pump 102 and the first flow meter 103 are both arranged on the first pipeline 104. One end of the first pipeline 104 is connected to the pulp mixing tank 101, and the other end is connected to the feed inlet of the first-stage classification cyclone 200. One outlet of the first-stage classification cyclone 200 is connected to the first cylinder 301 through the raw ore feed pipe 201, and the other outlet of the first-stage classification cyclone 200 is connected to the second-stage distribution plate 303 through the second pipeline 202. Understandably, a first valve 105 is also arranged on the first pipeline 104.

[0040] In this embodiment, a first centrifugal pump 102 is arranged in the first pipeline 104, and the pulp in the pulp mixing tank 101 is transported to the first-stage classification cyclone 200 by the first centrifugal pump 102 for classification. Some of the classified fine particles directly enter the second-stage distribution plate 303 and do not participate in the flotation of the coarse particle fluidized bed 300, which can reduce the ineffective processing amount of the fluidized bed; at the same time, the first flow meter 103 monitors the pulp flow in the first pipeline 104 to adjust the power of the first centrifugal pump 102 so as to transport an appropriate amount of pulp into the first cylinder 301.

[0041] As Figure 1As shown, the first cylinder 301 adopts an upper cylindrical and lower conical structure. The coarse particle fluidized bed 300 further includes an overflow weir 305. The overflow weir 305 is provided at the top of the first cylinder 301, and a concentrate outlet 306 is provided on the overflow weir 305. An accident discharge port 307 and a tailings port 308 are provided at the bottom of the first cylinder 301. A first solenoid valve 309 is provided on the tailings port 308. The concentrate outlet 306 is communicated with the first-stage distribution plate 302 through a third pipeline 310, and a second centrifugal pump 311 is provided on the third pipeline 310. The length of the tailings discharge port should not be too long, generally selected as 0.1 - 0.3 m, preferably 0.1 m.

[0042] In this embodiment, the rough concentrate minerals formed by flotation in the coarse particle fluidized bed 300 enter the overflow weir 305, are discharged through the concentrate outlet 306 under the action of the second centrifugal pump 311, enter the first-stage distribution plate 302 through the third pipeline 310, and then are classified by the second classification cyclone 304.

[0043] For the convenience of ore discharge, the bottom of the first cylinder 301 adopts a conical structure, and the cone angle is generally 10 - 30°, preferably 15°; the inner diameter of the first cylinder 301 is generally 0.4 - 1.0 m, preferably 0.7 m. Considering the sorting rate and efficiency, the working conditions are arranged. The height of the cylindrical section of the first cylinder 301 is generally 1.5 - 2.5 times the inner diameter, that is, 0.6 - 2.5 m, preferably 1.5 m, and the height of the bottom tailings cone is generally set to 0.2 m. The upper part of the top overflow weir 305 is set 0.1 m higher than the upper part of the sorting tank, and the inclination angle is generally set to 15 - 35°, and considering increasing the rough selection discharge speed and suppressing the plugging phenomenon here, 25° is preferred.

[0044] In order to monitor the pressure distribution in the first cylinder 301 during the sorting process to judge whether ore discharge is required or equipment parameters need to be adjusted, such as Figure 1 and Figure 3 As shown, the coarse particle fluidized bed 300 further includes a first pressure sensor 312. There are multiple first pressure sensors 312, and the multiple first pressure sensors 312 are arranged at equal intervals from top to bottom along the height direction of the first cylinder 301. The number of the first pressure sensors 312 is generally 3 - 8, preferably 4.

[0045] As Figure 1 and Figure 3As shown, the coarse particle fluidized bed 300 further includes ultrasonic vibrators 313 and a magnetic field regulator 314. There are multiple ultrasonic vibrators 313, and the multiple ultrasonic vibrators 313 are arranged in columns along the height direction of the first cylinder 301. Exemplarily, the ultrasonic vibrators 313 are installed on a connecting rod 315. The connecting rod 315 is arranged inside the first cylinder 301 and is disposed close to the wall surface of the first cylinder 301. A multi-layer ultrasonic vibrator group is formed by the ultrasonic vibrators 313 and the connecting rod 315. There are two magnetic field regulators 314, which are respectively located above the cylindrical section and at the conical section of the first cylinder 301, that is, a double-layer magnetic field regulation structure is formed.

[0046] In this embodiment, an array-type multi-layer ultrasonic vibrator group formed by ultrasonic vibrators 313 and a connecting rod 315 is provided near the inner wall of the first cylinder 301. When the feedstock classified by the first classification cyclone 200 is fed into the fluidized bed, the ultrasonic vibrators 313 are started. The multi-layer ultrasonic vibrator group arranged in an array along the wall can optimize the spatial distribution of the ultrasonic force field by releasing ultrasonic waves to strip and disperse the fine mud adhering to the coarse particles, effectively reducing the pollution of the coarse particle concentrate tailings, strengthening the crushing of agglomerates, and at the same time further promoting the dispersion of the emulsifying agent to improve the separation efficiency. The ultrasonic vibrators 313, together with the magnetic field regulator 314 via a proportional logic circuit, realize the loosening and separation of the materials in the fluidized bed. At the same time, magnetic field regulators 314 are provided at the upper and lower ends of the first cylinder 301. The double-layer magnetic field regulator 314 controls the dispersion of the magnetite fluidization medium by regulating the magnetic field strength, thereby realizing the density classification of the bed layer, constructing the density classification of materials in a microgravity environment, effectively realizing the "float-gravity coupling" in the coarse particle separation stage, and reducing the separation cost.

[0047] As Figure 1 As shown, the flotation machine 400 includes a second cylinder 401, an electrically controlled stirring shaft 402, and an excitation motor 403. The upper end of the electrically controlled stirring shaft 402 extends out from the top of the second cylinder 401 and is connected to the excitation motor 403. The lower end of the electrically controlled stirring shaft 402 is arranged inside the second cylinder 401. The excitation motor 403 drives the electrically controlled stirring shaft 402 to rotate. The flotation machine 400 further includes an impeller 404 and a stirrer 405. Both the impeller 404 and the stirrer 405 are arranged on the electrically controlled stirring shaft 402. The stirrer 405 is arranged at the lower end of the electrically controlled stirring shaft 402, and the impeller 404 is arranged above the stirrer 405. It should be noted that the electrically controlled stirring shaft 402 can be telescopic.

[0048] It is worth noting that a makeup water pipe 406 is further provided on the connecting pipe between the flotation machine 400 and the secondary distribution plate 303. The secondary distribution plate 303 is used for mixing two fine particle materials with different concentrations and then redistributing them.

[0049] Preferably, the bottom of the second cylinder 401 is square, generally 100 - 200 mm in length, preferably 150 mm. The height is generally 200 - 400 mm, preferably 300 mm. The initial position of the bottom of the electric control stirring shaft 402 from the bottom of the groove of the second cylinder 401 is generally set at 30 - 70 mm, preferably 50 mm. Considering the energy utilization rate and the mineralization effect, the initial rotation speed of the electric control stirring shaft 402 is generally selected as 1600 - 2000 rpm, preferably 1800 rpm. The length of the impeller 404 is generally selected as 30 - 70 mm, preferably 50 mm, and the width of the impeller 404 is generally selected as 10 - 30 mm, preferably 20 mm. The spacing between adjacent upper and lower impellers 404 is generally selected as 50 - 150 mm, preferably 100 mm.

[0050] As Figure 1 shown, a discharge pipe 407 is provided at the bottom of the second cylinder 401, a second electromagnetic valve 408 is provided on the discharge pipe 407, and a second pressure sensor 409 is provided along the height direction of the second cylinder 401. The action of the second electromagnetic valve 408 is controlled by the second pressure sensor 409 to realize the opening and closing of the discharge pipe 407. A rotary scraper 410 is provided at the top of the second cylinder 401, and the fine concentrate is scraped out from the top of the second cylinder 401 by using the rotary scraper 410.

[0051] As Figure 1 shown, a spiral scraper discharging device 411 is provided at the bottom of the flotation machine 400, and the discharge pipe 407 is communicated with the spiral scraper discharging device 411. Considering the influence of fine tailings deposition on the discharging efficiency, the inclination angle of the spiral scraper pipeline is generally 20 - 40°, and preferably 20° to adapt to the general limited height working conditions and layout requirements. The rotation speed of the spiral scraper is generally 800 - 1000 rpm, and preferably 900 rpm considering the motor guarantee for use and the rapid discharging of tailings.

[0052] As Figure 4 shown, the flotation machine 400 further includes an annular baffle 412, a driven block 413, a traction wire 414, a fixed pulley 415 and a stepping motor 416. A track groove 417 is provided in the second cylinder 401. One end of the driven block 413 is connected to the track groove 417, and the other end is connected to the annular baffle 412. One end of the traction wire 414 is connected to the driven block 413, and the other end bypasses the fixed pulley 415 and is connected to the stepping motor 416. The fixed pulley 415 is provided at the top of the second cylinder 401. The rotation of the stepping motor 416 drives the driven block 413 to move up and down along the track groove 417, thereby adjusting the position of the annular baffle 412 in the second cylinder 401.

[0053] Below the annular baffle 412 is the area of intense collision and mineralization, which promotes the three-phase interaction of particles, bubbles, and reagents, improving the mineralization efficiency. Above the annular baffle 412 is the static separation and transportation area. The approximately static space is more suitable for the separation and transportation after the adhesion of particles and bubbles, effectively suppressing the phenomenon of turbulent desorption and improving the final recovery rate of mineral particles. It should be noted that the installation of components such as the annular baffle 412 in the second cylinder 401 should not interfere with the rotation of the electrically controlled stirring shaft 402, and the installation of the second pressure sensor 409 does not prevent the up and down movement of the annular baffle 412.

[0054] In this embodiment, the height of the annular baffle 412 is determined by the particle size of the minerals in the tank. When the particle size distribution is relatively fine, the height of the annular baffle 412 will be appropriately increased to increase the turbulent collision area and promote the full collection of reagents. When the particle size distribution is relatively coarse, the height of the annular baffle 412 can be reduced to reduce the desorption probability during the transportation of coarse particles loaded by bubbles.

[0055] As Figure 1 shown, the wide particle size material flotation equipment further includes a water-gas unit 500. The water-gas unit 500 includes a water tank 501, a fourth pipeline 502, and a water distribution plate 503. One end of the fourth pipeline 502 is connected to the water tank 501, and the other end is connected to the water distribution plate 503. The water distribution plate 503 is arranged below in the second cylinder 401.

[0056] As Figure 1 shown, the water-gas unit 500 further includes a first bubble generator 504, a second flow meter 505, and a third centrifugal pump 506. The first bubble generator 504, the second flow meter 505, and the third centrifugal pump 506 are all arranged on the fourth pipeline 502. In this embodiment, the water in the water tank 501 is transported to the first bubble generator 504 by the third centrifugal pump 506, and the second flow meter 505 is used to monitor the water flow for adjustment according to the demand. Understandably, a second valve 507 is also arranged on the fourth pipeline 502.

[0057] As Figure 1 shown, the water-gas unit 500 further includes an air pump 508, a fifth pipeline 509, and a third flow meter 510. The third flow meter 510 is arranged on the fifth pipeline 509. The two ends of the fifth pipeline 509 are respectively connected to the air pump 508 and the first bubble generator 504.

[0058] In order to add reagents to the first cylinder 301, as Figure 1As shown in the figure, the flotation equipment for wide particle size materials further includes a chemical dosing assembly 600. The chemical dosing assembly 600 includes a sixth pipeline 601, a fourth centrifugal pump 602, and a second bubble generator 603. One end of the sixth pipeline 601 is the chemical dosing port, and the other end is connected to the flotation machine 400, preferably connected to the pipeline where the secondary distribution plate 303 communicates with the flotation machine 400. The fourth centrifugal pump 602 and the second bubble generator 603 are both arranged on the sixth pipeline 601. The second bubble generator 603 is used for emulsifying the chemical agent, so that the chemical agent contacts the minerals more fully.

[0059] When the separation time is relatively long, timely discharging should be carried out through the accident discharge port 307 to prevent the separation density from decreasing. The heavy medium suspension can recover qualified medium via the magnetic separator. During the separation period, qualified medium can also be added in a timely manner from the qualified medium tank 700 through the medium makeup pipe 701 according to the differential pressure signal feedback to ensure the stability of the separation density of the suspension.

[0060] It should be noted that, as Figure 5 shown in the figure, the inlet section pipelines of the coarse and fine particle materials in the transportation pipeline are both designed with threaded pipes. The spiral flow field inside the threaded pipes can make the incoming materials fully loose in the pipeline, prevent local siltation of the materials in the pipeline from causing blockage, and at the same time improve the subsequent separation efficiency. As required by the separation process, when the concentration rises, the granular materials can still be fully dispersed compared with the cylindrical pipeline.

[0061] Embodiment 2

[0062] Another specific embodiment of the present invention discloses a flotation method, which uses the flotation equipment for wide particle size materials based on flow field regulation and multi-field coupling in Embodiment 1, and includes the following steps:

[0063] Step 1: Check the combined flotation device of the fluidized bed flotation machine.

[0064] First, confirm that the valves (including electrically controlled valves) at the accident discharge port 307, tailings port 308, fine particle tailings discharge pipe 407, etc. are in the closed state to prevent accidental leakage of the mineral particles to be separated. After a comprehensive inspection without errors, the separation process can be started.

[0065] Step 2: Add frother and pre-fluidize with water.

[0066] Step 2.1: Add frother.

[0067] The selection of frothers usually includes pine oil (No. 2 oil), methyl isobutyl carbinol (MIBC), and diethyl phthalate, among which pine oil (No. 2 oil) is preferred. Add the frother (the dosage is generally set at 5 - 15 g / m 3 , adjusted according to the bubble dispersion situation) into the water tank 501, so that it is mixed with clean water and then enters the inside of the first cylinder 301 together.

[0068] Step 2.2: Feed water pre-fluidization.

[0069] Open the pipeline valve of the water tank 501, and at the same time, turn on the air pump 508. The clear water is pressurized by the third centrifugal pump 506, and the flow rate of the pressurized water can be precisely adjusted by the second flow meter 505. The gas velocity flowing through the fifth pipeline 509 can be adjusted within the range of 0.3 - 1.2 m / s according to the separation conditions. When the high-speed flowing clear water (the velocity can be adjusted between 2.0 - 8.0 m / s, adjusted according to the feed properties) flows through the first bubble generator 504, due to the action of the throat negative pressure, cavitation will occur, generating micro-nano sized bubbles. These bubbles then enter the bottom of the first column 301 through the water distribution plate 503 and are dispersed upward from bottom to top in the entire space of the first column 301 along with the obliquely upward water flow. After the bubbles are evenly dispersed in the space of the first column 301, the preparation work for the rough selection stage of the fluidized bed begins.

[0070] Step 3: Optimization of the spatial distribution of the ultrasonic force field.

[0071] The ultrasonic oscillator 313 is turned on after the pre-fluidization ends. It should be noted that the opening of the magnetic field regulator 314 needs to be determined according to the specific composition and content of the magnetic minerals in the feed to ensure the maximum energy utilization efficiency. When the mass fraction of the magnetic minerals is relatively high (generally greater than 10%), it can be turned on together with the ultrasonic oscillator 313. Preferably, the density of the magnetite powder is 5.2 g / cm 3 , and the diameter is set to 0.045 mm with the particle size fraction content above 90%.

[0072] In this embodiment, the ultrasonic oscillator 313 optimizes the spatial distribution of the ultrasonic force field by releasing ultrasonic waves, which can strip and disperse the fine mud adhering to the coarse-grained materials, effectively reduce the tailing pollution of the coarse-grained concentrate, strengthen the fragmentation of the aggregates, and at the same time further promote the dispersion of the emulsified reagent to improve the separation efficiency; the magnetic field regulator 314 regulates the magnetic field strength to control the dispersion of the magnetite fluidization medium, and then realizes the density classification of the bed layer, constructs the density classification of the materials in the microgravity environment, and effectively realizes the "float - gravity coupling" in the coarse-grained separation stage.

[0073] Step 4: Add collector for pre-slurrying.

[0074] Drop the collector into the slurry mixing tank 101 (the dosage is generally set to 200 - 800 g / m 3, adjusted according to the specific separation situation), the collectors generally include sodium ethyl xanthate, sodium isopropyl xanthate, sodium butyl xanthate (potassium), sodium isobutyl xanthate (potassium), etc., and sodium ethyl xanthate (ethyl xanthate) is preferred. The pulp concentration can be set to 30-40% based on relevant research (adjusted according to the specific separation situation and mineral properties). The pulp conditioning time can be set to 3-5 minutes (the specific time can be adjusted according to the content of fine-grained minerals in the pulp and the separation efficiency, etc.). The feed enters the first column 301 through the pipeline valve of the conditioning tank 101, and the raw pulp enters the inside of the first column 301 through the pulp feed pipe 201 that extends into the first column 301 after being pressurized by the first centrifugal pump 102.

[0075] Step 5: Regulation and control of the combined flotation process.

[0076] The feed is discharged from the conditioning tank 101 through the first centrifugal pump 102 and the feed pipe 201 into the first column 301 for rough selection. At the same time, the pumping pressure of the first centrifugal pump 102 can be adjusted according to the dispersion situation of the feed. To save water, the makeup water valve can be opened 3-5 minutes after the start of feeding. The roughing concentrate is sent to the first-stage distribution tray 302 through the second centrifugal pump 311 over the overflow weir 305 and is distributed to four roughing concentrate classification cyclones (i.e., the second classification cyclone 304) for classification. The coarse (granular) concentrate is discharged from the underflow pipe of the second classification cyclone 304. The rough tailings are discharged from the tailing port 308. The roughing concentrate overflow is fully mixed with the reagent in the second-stage distribution tray 303 and is fed into the flotation cell 400 through the excitation control of the rotating shaft from the bottom stirrer 405 at the bottom of the pneumatic flotation machine 400 for the second-stage fine-grained separation. In the flotation cell stage of the second-stage fine-grained separation, the flow field regulation is achieved by the regulation of the annular baffle 412 and the telescoping and rotation of the electric control stirring shaft 402.

[0077] It should be noted that after the rough concentrate particles sorted by the first column 301 float up and pass through the overflow weir 305, they are gathered from the rough concentrate discharge port and pressurized by an intelligent control centrifugal pump (the second centrifugal pump 311) and fed into the first-stage distribution plate 302, and then sent to the second classification cyclone 304 for classification. The underflow is the rough concentrate product, and the overflow is the fine-grained material. Here, it is necessary to monitor the pumping pressure and control the discharge speeds of the coarse and fine particles to control the subsequent feeding speed and pulp concentration of the fine-grained flotation. The tailing particles sink to the bottom of the trough (the first column 301). Here, it is necessary to monitor the tailing accumulation state in real time through the second pressure sensor 409. When the pressure reaches the preset upper limit, the second electromagnetic valve 408 of the fine tailing port is automatically opened to discharge the tailings; when the pressure drops to the preset lower limit, the valve closes to prevent the sudden change of the fluidized bed pressure caused by excessive discharge of tailings and ensure the stability of the fluidized bed layer. After the roughing tailings are classified by the second classification cyclone 304, the underflow is the rough tailings, and the overflow is the fine-grained material. The fine-grained material after the classification of the roughing tailings by the classification cyclone, together with the overflow after the classification of the rough concentrate and the reagent injected through the reagent distribution pipe, is sent to the second-stage distribution plate 303 by the slurry pump and then mixed and distributed into the flotation machine 400 for sorting of the fine-grained material. Sampling windows need to be set on the first-stage distribution plate 302 and the second-stage distribution plate 303 to realize the dynamic monitoring feedback of the sorting process and subsequent parameter adjustment. In the fine-grained flotation stage of the flotation machine 400, the electric control stirring shaft 402 and the excitation motor 403 expand and contract according to the feedback signal of the differential pressure sensor and the signal of the operation console to realize the flow field regulation of the flotation machine 400 suitable for the fine-grained material.

[0078] This embodiment adopts the design of "magnetic-acoustic-fluid" multi-field coupling and reagent jet emulsification control, realizing the directional control of the interaction among particles, bubbles, and reagents and the density stratification under microgravity fluidization state in the fluidized bed separation process of coarse-grained materials, achieving precise control of the fluidized bed coarse particle flotation process. The feed pulp is fed into the first classification cyclone 200 from the pulp mixing tank 101. Under the action of the centrifugal force field, the fine-grained materials enter the secondary distribution plate 303 through the overflow pipe as the overflow, and the coarse-grained materials enter the fluidized bed as the underflow. The self-aspiration-induced emulsification phenomenon occurs in the reagent jet in the gas-water pipe. According to the flowmeter information, the reagent emulsification is directionally controlled to efficiently adjust the bubble size on the water distribution plate 503 and the particle size of the emulsified reagent. At the same time, multiple ultrasonic oscillator groups are arranged in an array along the wall. By releasing ultrasonic waves and optimizing the spatial distribution of the ultrasonic force field, the fine mud adhering to the coarse-grained materials can be peeled off and dispersed, effectively reducing the pollution of the coarse-grained concentrate tailings, strengthening the fragmentation of aggregates, and further promoting the dispersion of the emulsified reagent to improve the separation efficiency. The double-layer magnetic field regulator 314 controls the dispersion of the magnetite fluidization medium by regulating the magnetic field intensity, thereby realizing the density classification of the bed layer, constructing the density classification of materials in the microgravity environment, and effectively realizing the "flotation-gravity coupling" in the coarse-grained separation stage. According to the signal feedback of the fluidized bed wall differential pressure sensor, the change of the bed layer pressure drop is monitored and controlled in real time for the turbulent intensity of the fluidized bed layer. From the perspective of "magnetic-acoustic-fluid" multi-field coupling control, this structural design constructs a fluidized separation environment under microgravity with the help of PID signal control, effectively realizing the stable separation and process intensification of coarse-grained materials under the microgravity field, providing an innovative and reliable technical route for the coal preparation plant to remove gangue before crushing coarse-grained materials and recover resources.

[0079] In this embodiment, a "pressurized swirling - jet cavitation directional coupling" energy - transport and utilization structure design is adopted, which realizes the coarse and fine classification of the rough - selected ore pulp, the fine - tail classification, shear dispersion, and cavitation nucleation, achieving the effects of multi - directional classification of wide - particle - size materials and enhanced separation of fine - particle materials. Compared with the traditional segmented - process operation, the integrated structure design of pressurized swirling flow and jet transportation improves the energy utilization rate in the coarse - and - fine particle feeding stage, and realizes the additional cavitation effect of the ore pulp on the basis of the existing classification function. The energy of the centrifugal pump is used to construct a centrifugal swirling force field in the rough - selection feeding stage to pre - classify the rough - selection feeding. In the stage before the fine - particle feeding, the fluid pressure after the ore pulp classification enables the fine - particle jet to enter the peripheral array - type flotation machine 400. The intelligent adjustment of the feeding pressure by the centrifugal pump during the classification process is adopted to design the swirling force field, realizing the dynamic classification particle - size control with the zero - velocity envelope surface as the boundary, with fine particles in the inner overflow and coarse particles in the outer underflow, avoiding the problem that the single feeding pressure of the traditional classification cyclone does not match the dynamic feeding properties, resulting in a reduction in the subsequent separation efficiency, and achieving the directional classification and dynamic regulation of the materials in the classification stage to match the material properties. At the same time, the flotation machine 400 is fed under pressure, and the electro - controlled stirring shaft 402 is adjusted. When the pressure decreases, gas precipitates from the supersaturated state to form bubbles. The gas nuclei adsorb on the solid particles or interfaces in the liquid and rapidly expand to form bubbles when the pressure decreases, realizing the bubble cavitation nucleation on the surface of the fine - particle materials. The nano - bubbles can directly adhere to the surface of hydrophobic particles during the flotation process, significantly increasing the collision efficiency between the particles and the bubbles and reducing the desorption probability of the particles, thereby improving the flotation efficiency. This functional structure design solves the problem of the inability to utilize the energy of traditional pressurized pipelines, effectively improves the energy utilization efficiency of material separation, and provides a technical reference for the green and low - carbon production of the concentrator and the strengthening of the fine - particle material separation process.

[0080] As described above, it is only the preferred specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto. Any changes or substitutions that can be easily thought of by those skilled in the art within the technical scope disclosed by the present invention should be covered by the protection scope of the present invention.

Claims

1. A flotation equipment for wide-size fraction materials based on flow field regulation and multi-field coupling, characterized in that, It includes a first classification cyclone (200), a coarse particle fluidized bed (300) and a flotation machine (400); the coarse particle fluidized bed (300) includes a first cylinder (301), a primary distribution plate (302), a secondary distribution plate (303) and a second classification cyclone (304); The first classification cyclone (200) is simultaneously connected to the first cylinder (301) and the secondary distribution plate (303), the second classification cyclone (304) is connected to the primary distribution plate (302) and the secondary distribution plate (303), the flotation machine (400) is connected to the secondary distribution plate (303), and the first cylinder (301) is connected to the primary distribution plate (302).

2. The flotation equipment for wide particle size materials based on flow field regulation and multi-field coupling according to claim 1, wherein It further includes a slurry unit (100), and the slurry unit (100) is connected to the first classification cyclone (200).

3. The wide-size particle material flotation equipment based on flow field regulation and multi-field coupling according to claim 1, characterized in that, Both the primary distribution plate (302) and the secondary distribution plate (303) are arranged on the first cylinder (301), and the primary distribution plate (302) is located above the secondary distribution plate (303).

4. The flotation equipment for wide - sized materials based on flow field regulation and multi - field coupling according to claim 1, wherein, There are multiple second classification cyclones (304) and multiple flotation machines (400), and the multiple second classification cyclones (304) and the multiple flotation machines (400) are evenly arranged around the first cylinder (301).

5. The flotation equipment for wide - sized materials based on flow field regulation and multi - field coupling according to claim 1, characterized in that, The second classification cyclone (304) is arranged between the primary distribution plate (302) and the secondary distribution plate (303), and the flotation machine (400) is arranged below the secondary distribution plate (303).

6. The flotation equipment for wide-size fraction materials based on flow field regulation and multi-field coupling according to claim 2, wherein, The slurry unit (100) includes a slurry mixing tank (101), a first centrifugal pump (102) and a first pipeline (104), the first centrifugal pump (102) is arranged on the first pipeline (104), one end of the first pipeline (104) is connected to the slurry mixing tank (101), and the other end is connected to the feed inlet of the first classification cyclone (200).

7. The flotation equipment for wide particle size materials based on flow field regulation and multi-field coupling according to any one of claims 1-6, characterized in that It further includes a water and gas unit (500), and the water and gas unit (500) includes a water tank (501), a fourth pipeline (502) and a water distribution plate (503), one end of the fourth pipeline (502) is connected to the water tank (501), and the other end is connected to the water distribution plate (503).

8. The flotation equipment for wide - sized materials based on flow field regulation and multi - field coupling according to claim 7, characterized in that, The water and gas unit (500) further includes an air pump (508), a fifth pipeline (509) and a first bubble generator (504), and both ends of the fifth pipeline (509) are respectively connected to the air pump (508) and the first bubble generator (504).

9. The flotation equipment for wide particle size materials based on flow field regulation and multi-field coupling according to any one of claims 1-6 and 8, characterized in that, It further includes a chemical addition component (600).

10. A flotation method, characterized in that, Use the wide particle size material flotation equipment based on flow field regulation and multi-field coupling according to any one of claims 1-9 to float minerals.

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