Non-ferrous metal coarse-grained mineral pre-concentration and waste-throwing system and process based on fluidization separation

Abstract

The present application relates to a non-ferrous metal coarse-grained mineral pre-selection waste-throwing system and process based on fluidization separation, and belongs to the technical field of coarse-grained mineral separation. The present application solves the problem of high energy consumption in the prior art of non-ferrous metal coarse-grained mineral separation. The present application comprises a classification cyclone, a stirring barrel, a fluidization flotation machine, a thickener and a ball mill. The stirring barrel is arranged downstream of the classification cyclone, the fluidization flotation machine is arranged downstream of the stirring barrel, the thickener is arranged downstream of the fluidization flotation machine, and the ball mill is arranged downstream of the thickener. In the present application, the underflow of the classification cyclone is directly subjected to separation, coarse-grained tailings are thrown away in advance, and the fluidization flotation concentrate is concentrated by the thickener and then enters the ball mill. The overflow water of the thickener can be returned to the fluidization flotation machine for recycling. Through the pre-throwing of the fluidization flotation machine, the tailing throwing rate can be as high as 30%, the grinding energy consumption can be significantly reduced, and the grinding capacity of the mill can be improved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of coarse-grained mineral separation, and particularly to a non-ferrous metal coarse-grained mineral pre-selection waste-throwing system and process based on fluidization separation. BACKGROUND

[0002] With the rapid development of China's social economy, mineral resources are being mined in large quantities, leading to the depletion of high-quality mineral resources. The valuable metals are increasingly characterized by 'poor, fine and impure', resulting in a sharp rise in energy consumption for grinding operations. At the same time, the problem of fine-grained separation is more prominent. On the one hand, due to the low collision probability between fine particles and bubbles, the flotation recovery rate is greatly reduced. On the other hand, the water entrainment effect of fine particles will further worsen the selectivity of flotation. The high cost, long process and low efficiency of flotation caused by low-quality ores have become a major problem that needs to be solved in the low-carbon separation and recovery of mineral resources. According to research statistics, the grinding energy consumption accounts for 45% to 55% of the total energy consumption of the ore dressing plant. Increasing the upper limit of the mineral flotation particle size and realizing pre-selection waste throwing can greatly reduce the grinding energy consumption.

[0003] However, the conventional coarse-grained mineral flotation equipment has limitations in processing the particle size of minerals. On the one hand, coarse particles are easily detached due to the influence of turbulent flow of the slurry. On the other hand, the bubble-particle aggregate passing through the froth interface will also cause detachment, which puts higher requirements on the ore dressing process and equipment. At the same time, the existing coarse coal slime separation equipment has high grinding energy consumption and low mill processing capacity. SUMMARY

[0004] In view of the above analysis, the embodiments of the present application aim to provide a non-ferrous metal coarse-grained mineral pre-selection waste-throwing system and process based on fluidization separation to solve the problem of high energy consumption in the separation of non-ferrous metal coarse-grained minerals.

[0005] On the one hand, the present application provides a non-ferrous metal coarse-grained mineral pre-selection waste-throwing system based on fluidization separation, which comprises a classification cyclone, a stirring barrel, a fluidization flotation machine, a thickener and a ball mill. The stirring barrel is arranged downstream of the classification cyclone, the fluidization flotation machine is arranged downstream of the stirring barrel, the thickener is arranged downstream of the fluidization flotation machine, and the ball mill is arranged downstream of the thickener.

[0006] Further, it further comprises a slurry pre-treater and a flotation column. The slurry pre-treater is arranged downstream of the classification cyclone, and the flotation column is arranged downstream of the slurry pre-treater.

[0007] Further, the underflow port of the classification cyclone is in communication with the feed inlet of the stirring barrel, and a first slurry pump is arranged between the underflow port of the classification cyclone and the feed inlet.

[0008] Further, the discharge port of the stirring barrel is communicated with the feeder of the fluidized flotation machine, and a second slurry pump is arranged between the discharge port and the feeder.

[0009] Further, the concentrate pipe of the fluidized flotation machine is communicated with the input port of the thickener, and the underflow outlet of the thickener is communicated with the feeding port of the ball mill.

[0010] Further, the overflow port of the classification cyclone is communicated with the feeding port of the ore slurry pretreater, and the discharge port of the ore slurry pretreater is communicated with the flotation column.

[0011] Further, the fluidized flotation machine comprises a column body, the column body comprises a column cylinder and a conical cylinder, and the conical cylinder is arranged at the bottom of the column cylinder.

[0012] Further, an inspection opening is arranged on the conical cylinder, and a tailing pipe is arranged at the bottom of the conical cylinder.

[0013] Further, the taper angle of the conical cylinder is 50°-70°.

[0014] In another aspect, the present application provides a non-ferrous metal coarse-grained mineral pre-selection waste-throwing process based on fluidized separation, which uses the above-mentioned non-ferrous metal coarse-grained mineral pre-selection waste-throwing system based on fluidized separation to pre-select and throw away the non-ferrous metal coarse-grained mineral.

[0015] Compared with the prior art, the present application can at least achieve one of the following beneficial effects:

[0016] (1) The present application directly enters the classification cyclone underflow into the selection, throws away the coarse-grained tailings in advance, and the fluidized flotation concentrate is concentrated by the thickener and then enters the ball mill. The overflow water of the thickener can be returned to the fluidized flotation machine for recycling. Through the pre-throwing tailings of the fluidized flotation machine, the throw-away rate can reach up to 30%, which can significantly reduce the grinding energy consumption, improve the grinding capacity, and at the same time, the fluidized flotation tailings have high gangue content and can be used as building materials.

[0017] (2) The present application forms a water-gas mixture through the Venturi tube jet suction, and the water-gas mixture is fed into the column body through the fluid distributor. During the process, the water-gas mixture is stored and released through the fluid distributor, so that the gas bubbles are more dispersed in the column body. The drag force generated by the rising water flow counteracts the gravity of the particles, so that the particle group is suspended and forms a loose bed layer, and at the same time, a suitable static flow field environment is created for the particles. The dispersed gas bubbles are selectively adsorbed on the particles, increasing the density difference between the non-ferrous metal and the gangue, and finally realizing effective separation.

[0018] (3) The fluidized flotation machine of the present application can control the rising water speed and gas holdup by adjusting the water flow rate and the gas flow rate, increasing the water flow rate can increase the rising water speed, improve the concentrate recovery rate, and at the same time improve the tailings grade, and increasing the gas flow rate can increase the gas holdup, improve the concentrate recovery rate, and at the same time improve the grade.

[0019] (4) The fluidized flotation machine of the present application has a static flow field environment inside, which avoids the detachment of coarse particle minerals from the bubble surface caused by high turbulent field shear, and at the same time, the thin foam layer can also avoid the coalescence detachment of bubble-particle aggregates at the foam phase interface, greatly improving the upper limit of the separation particle size; through the structural design of the water flow distribution ring and the gas flow distribution ring, the water flow is uniformly distributed to the Venturi tube, and it is beneficial to the full inhalation of the gas flow and the dispersion in each Venturi tube, realizing the uniform mixing of water and gas; narrow flow channels are formed in the middle layer of the fluid distributor, realizing the pressure storage process of the water-gas mixture, and the water-gas mixture is discharged through the pressure relief of the upper porous sieve plate, which is beneficial to the refinement of the bubbles and promotes the secondary dispersion of the bubbles.

[0020] In the present application, the above technical solutions can be combined with each other to realize more preferred combination schemes. Other features and advantages of the present application will be described in the subsequent specification, and some advantages will become apparent from the specification, or will be understood by implementing the present application. The purposes and other advantages of the present application can be realized and obtained through the contents specifically indicated in the specification and the drawings. BRIEF DESCRIPTION OF DRAWINGS

[0021] The accompanying drawings are included to provide a further understanding of the present application and are incorporated in and constitute a part of this specification, illustrate embodiments of the present application and together with the description serve to explain the principles of the present application. In the drawings:

[0022] Figure 1 It is a structural schematic diagram of the pre-throwing waste system of the specific embodiment;

[0023] Figure 2 It is a structural schematic diagram of the fluidized flotation machine of the specific embodiment;

[0024] Figure 3 It is a structural schematic diagram of the fluid distributor of the specific embodiment;

[0025] Figure 4 It is a structural schematic diagram of the upper layer of the distributor of the specific embodiment;

[0026] Figure 5 It is a structural schematic diagram of the middle layer of the distributor of the specific embodiment;

[0027] Figure 6 It is a structural schematic diagram of the baffle of the specific embodiment.

[0028] Reference signs:

[0029] 100 - Grading hydrocyclone; 200 - Mixing tank; 201 - Inlet; 202 - Outlet;

[0030] 300-Fluorescent flotation machine; 301-Column; 302-Airflow distribution ring; 303-Waterflow distribution ring; 304-Venturi tube; 305-Fluid distributor; 306-Airflow distribution branch pipe; 307-Waterflow distribution branch pipe; 308-Connecting pipe; 309-Column; 310-Conical; 311-First flange; 312-Second flange; 313-Lower layer of distributor; 314-Middle layer of distributor; 315-Upper layer of distributor; 316-Baffle; 317-Inlet pipe; 318-Inspection port; 319-Tailgating pipe; 320-Feeder; 321-Overflow weir; 322-Concentrate pipe;

[0031] 400 - Thickening tank; 500 - Ball mill; 600 - Slurry preprocessor; 700 - Flotation column; 800 - First slurry pump; 900 - Second slurry pump; 1000 - Third slurry pump. Detailed Implementation

[0032] The preferred embodiments of the present invention will now be described in detail with reference to the accompanying drawings, which constitute a part of the present invention and are used together with the embodiments of the present invention to illustrate the principles of the present invention, but are not intended to limit the scope of the present invention.

[0033] Example 1

[0034] A specific embodiment of the present invention, such as Figure 1 As shown, a pre-beneficiation waste disposal system for coarse-grained non-ferrous metal minerals based on fluidized bed separation (hereinafter referred to as the pre-beneficiation waste disposal system) is disclosed, including a classifying hydrocyclone 100, a stirring tank 200, a fluidized bed flotation machine 300, a thickening tank 400, a ball mill 500, a slurry pre-processor 600, and a flotation column 700. The stirring tank 200 is located downstream of the classifying hydrocyclone 100, the fluidized bed flotation machine 300 is located downstream of the stirring tank 200, the thickening tank 400 is located downstream of the fluidized bed flotation machine 300, the ball mill 500 is located downstream of the thickening tank 400, the slurry pre-processor 600 is located downstream of the classifying hydrocyclone 100, and the flotation column 700 is located downstream of the slurry pre-processor 600.

[0035] In practice, after the minerals are classified by the classifying hydrocyclone 100, the overflow fine products directly enter the flotation system, while the underflow coarse products of the classifying hydrocyclone 100 are discarded by the fluidized flotation machine 300 and then enter the ball mill 500 for grinding. The product of the ball mill 500 is then returned to the classifying hydrocyclone 100 for further classification. A portion of the low-grade tailings is discharged before the ball mill 500, reducing the feed rate of the ball mill 500 and thus reducing grinding energy consumption.

[0036] Compared with the prior art, the pre-throwing waste system provided by the embodiment can directly enter the classification cyclone underflow into the preparation, throw away coarse tailings in advance, and concentrate the flotation concentrate through the thickener, and then the concentrated flotation concentrate enters the ball mill, the thickener overflow water can be returned to the fluidized flotation machine for recycling, the tailings are thrown away in advance through the fluidized flotation machine, and the throwing tailings rate can reach 30%, which can significantly reduce the grinding energy consumption and improve the grinding capacity of the mill.

[0037] In the embodiment, part of the low-grade coarse tailings is thrown away in advance, the useful minerals are enriched in the concentrate, the concentrate enters the ball mill for grinding, the ball mill feed quantity is reduced, the ball mill operation energy consumption is reduced, and the ball mill grinding efficiency is improved. Meanwhile, the fluidized flotation tailings have high gangue content and can be used as building materials.

[0038] As shown in Figure 1 In order to send the ore pulp raw material into the stirring barrel 200 and output the stirred ore pulp outside the stirring barrel 200, the stirring barrel 200 is provided with a feeding port 201 and a discharging port 202. The feeding port 201 is located at the upper part of the stirring barrel body, the discharging port 202 is arranged at the lower part of the stirring barrel body, and the feeding port 201 and the discharging port 202 are respectively arranged at the two sides of the stirring barrel body.

[0039] As shown in Figure 1 and Figure 2 The fluidized flotation machine 300 includes a column body 301, an air flow distribution ring 302 and a water flow distribution ring 303. The air flow distribution ring 302 and the water flow distribution ring 303 are both arranged outside the column body 301, and the water flow distribution ring 303 is arranged above the air flow distribution ring 302.

[0040] The fluidized flotation machine 300 further includes a Venturi tube 304 and a fluid distributor 305. The air flow distribution ring 302 is in communication with the air inlet of the Venturi tube 304, the water flow distribution ring 303 is in communication with the water inlet of the Venturi tube 304, the outlet of the Venturi tube 304 is in communication with the fluid distributor 305, and the fluid distributor 305 is arranged in the column body 301. The outer diameter of the fluid distributor 305 should be kept a certain distance from the inner diameter of the column body 301 to facilitate the discharge of tail coal from the gap between them. Preferably, the ratio of the outer diameter of the fluid distributor 305 to the inner diameter of the column body 301 is 4.5:5-4:5. The Venturi tube 304 should be as close as possible to the air flow distribution ring 302 to facilitate the distribution and control of the gas, and therefore the Venturi tube 304 is arranged below the water flow distribution ring 303.

[0041] In the implementation, the prepared ore pulp from the stirring barrel 200 is transported to the fluidized flotation machine 300 through the discharging port 106, the air flow distribution ring 302 and the water flow distribution ring 303 supply air and water to the Venturi tube 304 respectively, the air and water are mixed by the Venturi tube 304, and then distributed to the inside of the column body 301 through the fluid distributor 305 for fluidized flotation.

[0042] The Venturi tubes 304 are arranged on the outer side of the column 301 in a uniform manner around the column 301, the airflow distribution ring 302 is provided with a plurality of airflow distribution branches 306, the airflow distribution branches 306 are arranged in a uniform manner around the airflow distribution ring 302, each airflow distribution branch 306 is communicated with one Venturi tube 304, the water flow distribution ring 303 is provided with a plurality of water flow distribution branches 307, the water flow distribution branches 307 are arranged in a uniform manner around the water flow distribution ring 303, each water flow distribution branch 307 is communicated with one Venturi tube 304, the number of Venturi tubes 304, the number of airflow distribution branches 306 and the number of water flow distribution branches 307 are equal.

[0043] The Venturi tubes 304, the airflow distribution branches 306 and the water flow distribution branches 307 are each provided with 3-8, preferably 6. The 6 Venturi tubes 304 are arranged in a uniform manner around the column 301, the 6 airflow distribution branches 306 are arranged in a uniform manner around the airflow distribution ring 302, the 6 water flow distribution branches 307 are arranged in a uniform manner around the water flow distribution ring 303, and one Venturi tube 304 corresponds to one airflow distribution branch 306 and one water flow distribution branch 307 in position, so that the airflow distribution ring 302, the water flow distribution ring 303 and the Venturi tubes 304 are regularly distributed around the column 301, and the components on the outer side of the column 301 are arranged in a neat manner.

[0044] It can be understood that the plurality of Venturi tubes 304 forms a plurality of output ports, and correspondingly, the output ports of the Venturi tubes 304 are communicated with the fluid distributor 305 through the connecting pipes 308, the number of the connecting pipes 308 is equal to the number of the Venturi tubes 304, one end of the connecting pipe 308 is communicated with the output port of the Venturi tube 304, and the other end is communicated with the fluid distributor 305.

[0045] In this embodiment, the airflow distribution ring 302, the water flow distribution ring 303 and the Venturi tubes 304 are arranged on the outer side of the column 301, the water flow distribution ring 303 is communicated with the water inlet of the Venturi tube 304 through the water flow distribution branch 307, the airflow distribution ring 302 is communicated with the air inlet of the Venturi tube 304 through the airflow distribution branch 306, the mixed gas and water of the Venturi tube 304 is transported to the fluid distributor 305 through the connecting pipe 308, and then is distributed into the column 301 through the fluid distributor 305.

[0046] The column 301 comprises a column cylinder 309 and a conical cylinder 310, the conical cylinder 310 is arranged at the bottom of the column cylinder 309, the bottom of the column cylinder 309 is provided with a first flange 311, the top of the conical cylinder 310 is provided with a second flange 312, the first flange 311 and the second flange 312 are connected, so that the column cylinder 309 and the conical cylinder 310 are connected together. It should be noted that the conical cylinder 310 is a circular truncated cone-shaped cylinder, and the large bottom surface of the conical cylinder 310 is connected with the bottom of the column cylinder 309.

[0047] Preferably, in order to facilitate the discharge of tailings, the height ratio of the cylinder 309 to the cone 310 is 3:1 to 5:1, and the taper angle of the cone 310 is 50° to 70°.

[0048] Understandably, since the fluid distributor 305 is arranged in the column 301, specifically in the space of the cone 310, the Venturi tube 304 is arranged outside the column 301, and the connecting pipe 308 penetrates through the side wall of the cone 310 into the interior thereof and is connected with the fluid distributor 305.

[0049] As shown in Figs. Figure 3 , Figure 4 , Figure 5 and Figure 6 , the fluid distributor 305 comprises a three-layer structure, specifically a lower layer 313, a middle layer 314 and an upper layer 315. The lower layer 313 comprises a baffle 316 and a water inlet pipe 317, the lower end of which is in communication with the connecting pipe 308, and the upper end thereof is in communication with the central hole of the baffle 316. The middle layer 314 is a flow channel, and the liquid entering from the water inlet pipe 317 flows into the middle layer 314. The upper layer 315 is a porous sieve plate, which is arranged above the middle layer 314, and the liquid in the middle layer 314 enters the column 301 through the holes in the upper layer 315.

[0050] It is worth noting that the top surface of the fluid distributor 305 is flush with the second flange 312.

[0051] In this embodiment, the lower side of the middle layer 314 is provided with the lower layer 313, and the upper side thereof is provided with the upper layer 315. The middle layer 314 is in communication with the connecting pipe 308 through the water inlet pipe 317. The gas-water mixture output from the Venturi tube 304 enters the space of the middle layer 314 to store pressure, and then is discharged from the micro-holes in the upper layer 315 to enter the column 301. After the storage and discharge, the gas-water mixture is further dispersed, and the bubble dispersion is more uniform.

[0052] In order to facilitate the maintenance of the equipment, the cone 310 is provided with a maintenance opening 318. In order to facilitate the discharge of tailings, the bottom of the cone 310 is provided with a tailings pipe 319. In order to facilitate the feeding of materials and the recovery of concentrates, the upper end of the cylinder 309 is provided with a feeder 320 and an overflow weir 321, and the overflow weir 321 is connected with a concentrate pipe 322.

[0053] In this embodiment, the water stream containing the frother is fed into the water stream distribution ring 303, the water stream is evenly distributed to the six water stream distribution branches 307 via the water stream distribution ring 303, and the water stream jets through the Venturi tube 304 to suck in air and form a water-air mixture at a pressure of 0.1-0.3 MPa. The air fed into the air stream distribution ring 302 is evenly fed into the six air stream distribution branches 306, and finally into the Venturi tube 304. The water-air mixture is fed into the six connecting tubes 308 via the Venturi tube 304, gathered through the water inlet tube 317, and fed into the fluid distributor 305. The water-air mixture is blown out from the upper layer of the fluid distributor 305 and uniformly distributed in the column 301.

[0054] The rough mineral particles treated by the collector are fed into the upper part of the column 301 by the feeder 320 without pressure, and part of the rough mineral particles form a loose bed layer under the action of the rising water stream. The feeding rough mineral particles make a disturbed settling motion in the bed layer, increase the residence time of the particles in the bed layer, and increase the collision probability of the particles and the bubbles. The bubbles are selectively adsorbed on the surface of the concentrate particles, thereby reducing the effective density of the concentrate particles and expanding the apparent density difference between the concentrate particles and the gangue particles. Finally, the bubble-particle aggregates float to form the concentrate and flow out from the overflow weir 321 via the concentrate pipe 322 to form the concentrate. The gangue particles not adsorbed by the bubbles slowly pass through the bed layer and enter the conical cylinder 310, and are discharged via the tailings pipe 319 at the lower part of the conical cylinder 310 to form the tailings.

[0055] In this embodiment, the rising water speed and the gas holdup can be controlled by adjusting the water stream flow rate and the air stream flow rate. Increasing the water stream flow rate can increase the rising water speed, improve the concentrate recovery rate, and increase the tailings grade. Increasing the air stream flow rate can increase the gas holdup, improve the concentrate recovery rate, and increase the grade.

[0056] The internal part of the fluidized flotation machine in this embodiment is a static flow field environment, which avoids the detachment of coarse mineral particles from the bubble surface caused by high turbulent field shear, and the bubble-particle aggregates are also prevented from causing coalescence detachment at the foam phase interface, which greatly improves the upper limit of the separation particle size. Through the structural design of the water stream distribution ring and the air stream distribution ring, the water stream is evenly distributed to the Venturi tube, which is beneficial to the full suction of the air stream and the dispersion of the air stream in each Venturi tube, and the uniform mixing of the water and air is realized. A narrow flow channel is formed in the middle layer of the fluid distributor, which realizes the pressure storage process of the water-air mixture, and the water-air mixture is discharged through the upper layer of the porous sieve plate, which is beneficial to the bubble refinement and promotes the secondary dispersion of the bubbles.

[0057] As Figure 1As shown, the underflow of the classifying cyclone 100 is communicated with the feeding port 201 of the stirring barrel 200, and a first slurry pump 800 is arranged between the underflow of the classifying cyclone 100 and the feeding port 201 of the stirring barrel 200; the discharge port 202 of the stirring barrel 200 is communicated with the feeder 320 of the fluidized flotation machine 300, and a second slurry pump 900 is arranged between the discharge port 202 of the stirring barrel 200 and the feeder 320 of the fluidized flotation machine 300; the ore slurry in the stirring barrel 200 is transported to the fluidized flotation machine 300 through the first slurry pump 800; the concentrate pipe 322 of the fluidized flotation machine 300 is communicated with the input port of the thickener 400; the underflow outlet of the thickener 400 is communicated with the feeding port of the ball mill 500 through a third slurry pump 1000; the overflow outlet of the thickener 400 is communicated with the water distribution ring 303 of the fluidized flotation machine 300; the discharge port of the ball mill 500 is communicated with the feeding port of the classifying cyclone 100; the overflow port of the classifying cyclone 100 is communicated with the feeding port of the ore slurry pretreater 600; and the discharge port of the ore slurry pretreater 600 is communicated with the flotation column 700.

[0058] Embodiment 2

[0059] Another specific embodiment of the present application, as shown in Figures 1-6 A non-ferrous metal coarse-grained mineral pre-concentration and waste-throwing process based on fluidized separation is disclosed, which adopts the non-ferrous metal coarse-grained mineral pre-concentration and waste-throwing system based on fluidized separation of embodiment 1, and the steps include:

[0060] Step 1: The ore slurry is fed into the classifying cyclone 100 for pre-classification; the underflow of the classifying cyclone 100 is fed into the stirring barrel 200 through the first slurry pump 800, and the ore slurry is supplemented with a collector and is thickened in the stirring barrel 200. The ore slurry is fed into the fluidized flotation machine 300 through the second slurry pump 900 for separation, and the coarse tailings are discharged from the tailings pipe 319. This process is a pre-throwing tailings operation.

[0061] Through the pre-throwing tailings operation, part of the low-grade coarse tailings is thrown out, and the useful minerals are enriched in the concentrate, and the concentrate is ground in the ball mill, thereby reducing the ball mill feeding amount, reducing the energy consumption of the ball mill operation, and increasing the grinding efficiency of the ball mill.

[0062] Step 2: The separated concentrate of the fluidized flotation machine 300 is fed into the thickener 400 for settlement, and the overflow of the thickener 400 returns to the water distribution ring 303 of the fluidized flotation machine 300 after being supplemented with a frother, forming a cycle. The underflow of the thickener 400 is fed into the ball mill 500 through the third slurry pump 1000 for grinding operation, and the grinding product of the ball mill 500 returns to the feeding port of the classifying cyclone 100.

[0063] The step concentrates the flow state flotation concentrate by the thickening tank, increases the grinding concentration, and the overflow water of the thickening tank contains part of the foaming agent, so that the flow state flotation machine can realize closed loop circulation of water flow and save water after adding the foaming agent.

[0064] Step 3: The overflow of the grading cyclone 100 is fed into the ore slurry pre-treater 600 for slurry adjustment, the ore slurry is pre-treated and then fed into the flotation column 700 for flotation, the overflow product of the flotation column 700 is the concentrate, and the underflow product is the tailings.

[0065] The step can realize effective adsorption of the collector on the surface of the useful mineral particles by adding the collector to the ore slurry in advance, can realize effective adsorption of the bubbles and the useful mineral particles in the flow state flotation process, and further increases the density difference between the useful mineral particles and the gangue particles, so that the useful mineral can be effectively recovered.

[0066] The above only describes the preferred specific embodiments of the present application, but the protection scope of the present application is not limited to this. Any person skilled in the art can easily think of changes or replacements within the technical range disclosed by the present application, which should be covered within the protection scope of the present application.

Claims

1. A pre-concentration reject system for non-ferrous bulk mineral based on fluidization separation, characterized in that, The system comprises a classifying cyclone, a stirring barrel, a fluidized flotation machine, a thickener and a ball mill, the stirring barrel is arranged downstream of the classifying cyclone, the fluidized flotation machine is arranged downstream of the stirring barrel, the thickener is arranged downstream of the fluidized flotation machine, and the ball mill is arranged downstream of the thickener. The underflow coarse product of the classifying cyclone is thrown away by the fluidized flotation machine and then enters the ball mill for grinding, the ore pulp is fed into the fluidized flotation machine for separation, the coarse tailings are discharged from the tailings pipe of the fluidized flotation machine, the concentrate pipe of the fluidized flotation machine is communicated with the input port of the thickener, the underflow outlet of the thickener is communicated with the feeding port of the ball mill, and the product of the ball mill is returned to the classifying cyclone for classification. The fluidized flotation machine comprises a fluid distributor, the fluid distributor comprises a lower layer, a middle layer and an upper layer, the middle layer is a flow channel, and the upper layer is a porous sieve plate, a narrow flow channel is formed in the middle layer of the fluid distributor to realize a pressure storage process of a water-gas mixture, and the water-gas mixture is discharged through the porous sieve plate of the upper layer of the fluid distributor.

2. A fluidized-based sorting pre-concentration and discard system for coarse particles of non-ferrous metal ores according to claim 1, characterized in that, The system further comprises an ore pulp pre-treater and a flotation column, the ore pulp pre-treater is arranged downstream of the classifying cyclone, and the flotation column is arranged downstream of the ore pulp pre-treater.

3. The fluidized-based sorting pre-concentration and discard system for coarse particles of non-ferrous metal ores according to claim 1, characterized in that, The underflow port of the classifying cyclone is communicated with the feeding port of the stirring barrel, and a first slurry pump is arranged between the underflow port of the classifying cyclone and the feeding port.

4. The fluidized-based sorting pre-concentration and discard system for coarse particles of non-ferrous metal ores according to claim 1, characterized in that, The discharge port of the stirring barrel is communicated with the feeder of the fluidized flotation machine, and a second slurry pump is arranged between the discharge port and the feeder.

5. The fluidized-based sorting pre-concentration and discard system for non-ferrous crude mineral concentrates of claim 2, wherein, The overflow port of the classifying cyclone is communicated with the feeding port of the ore pulp pre-treater, and the discharge port of the ore pulp pre-treater is communicated with the flotation column.

6. A fluidized sorting based pre-concentration and waste rejection system for coarse particulate non-ferrous mineral ores as claimed in any one of claims 1 to 5, wherein, The fluidized flotation machine comprises a column body, the column body comprises a column cylinder and a cone cylinder, and the cone cylinder is arranged at the bottom of the column cylinder.

7. A fluidized sorting based pre-concentration reject throw off system for non-ferrous lumpy mineral ores as claimed in claim 6 wherein, An inspection opening is arranged on the cone cylinder, and a tailings pipe is arranged at the bottom of the cone cylinder.

8. The fluidized-based sorting of non-ferrous lump mineral pre-concentration and rejection system according to claim 6, characterized in that, The cone angle of the cone cylinder is 50°-70°.

9. A process for pre-concentration and rejection of coarse mineral of non-ferrous metals based on fluidization separation, characterized in that, The system is used for pre-throwing away coarse non-ferrous metal minerals. The system is used for pre-throwing away coarse non-ferrous metal minerals.

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