CN108970813B - Fluidized coarse grain flotation equipment and flotation method - Google Patents
Fluidized coarse grain flotation equipment and flotation method Download PDFInfo
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- CN108970813B CN108970813B CN201811246340.7A CN201811246340A CN108970813B CN 108970813 B CN108970813 B CN 108970813B CN 201811246340 A CN201811246340 A CN 201811246340A CN 108970813 B CN108970813 B CN 108970813B
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Abstract
The invention discloses a fluidized coarse grain flotation device, which comprises: the top of the flotation column body is provided with an overflow trough and a feeding device; a bubble generator disposed on the flotation column; the bubble distributor is arranged in the flotation column body and communicated with the bubble generator so as to uniformly distribute bubbles generated by the bubble generator in the flotation column body; the flotation device comprises a flotation column body, a liquid inlet and a bubble distributor, and is characterized by further comprising a liquid supply device communicated with the liquid inlet at the lower end of the flotation column body to form an ascending liquid flow in the flotation column body, wherein the bubble distributor is located above the liquid inlet, and a turbulent plate is arranged between the liquid inlet and the bubble distributor in the flotation column body. The invention combines the bubble distributor and the turbulent flow plate to form a gas-liquid composite fluidized interference bed of bubbles and ascending water flow in the cylinder, thereby realizing the flotation recovery of coarse particle minerals with the particle size of about 150-1000 mu m.
Description
Technical Field
The invention belongs to the technical field of flotation of mining equipment, and particularly relates to fluidized coarse grain flotation equipment and a fluidized coarse grain flotation method.
Background
In the field of mineral processing, flotation is the most common method for recovering valuable minerals. The flotation has high requirement on the granularity of the selected mineral, the specific gravity of the fed material granularity of which is generally required to be below 74 microns is about 60-90%, the upper limit of the fed material granularity is generally 100-150 microns, and the flotation recovery effect of the particles with relatively thick granularity of more than 150 microns is poor, so that the coarse particles generally need to be returned to a ball mill for fine grinding to reach the fed material granularity of the flotation. And for the ore with the grain size of about 150-1000 μm, the ore is easy to be over-crushed by re-grinding, so that the amount of fine mud is unnecessarily increased, and the ore grinding cost is increased. The grade of valuable minerals in coarse-grained ores is generally lower than that of fine-grained ores, and the grinding operation is completely carried out on the coarse-grained ores, so that energy waste is caused to a certain extent. Therefore, in the process flow of 'grinding-flotation', the pre-tailing discarding of the ores with the grain size of about 150-1000 μm has important practical significance.
The effect of recovering coarse particles by using the traditional flotation equipment is poor. The dissociation degree of the coarse particle ore monomer is poor, the exposure of valuable minerals on the surface of the ore is low, the effect of the coarse particle ore monomer on a collecting agent is poor, the hydrophobicity of the surface of the ore particle is insufficient, and the adhesion probability of the coarse particle ore monomer on bubbles is low; the coarse particles are relatively heavy, bubbles with larger volume and strength are needed for floating, and the buoyancy force formed by common bubbles is not enough to bring the coarse particles into a foam layer; the coarse particles have relatively small specific surface area and relatively poor adhesion to the bubbles, cannot maintain the adhesion time and strength required by flotation, and are easily separated from the bubbles. As a result, coarse minerals tend to sink into the tailings during flotation, resulting in loss of valuable minerals. And for the interference bed classifier for classifying the coarse particles, the classification effect depends on the particle size and the density of the minerals, and because the valuable minerals in the coarse particles are generally low in grade and fine in dispersion and embedment particle size, the specific gravity of the ore particles with the same particle size is almost not different, so that the interference bed classifier has poor identification capability on the valuable minerals in the coarse particles, and the valuable minerals are also lost. Therefore, neither single conventional flotation equipment nor gravity separation equipment can achieve efficient recovery of coarse-grained minerals.
Disclosure of Invention
The present application is directed to solving at least one of the problems in the prior art. Accordingly, an object of the present invention is to provide a fluidized coarse grain flotation apparatus and a flotation method, which can recover a coarse target mineral by flotation and can perform ore pretreatment by discarding a tailing of the coarse gangue mineral.
In order to solve the technical problems, the invention adopts the following technical scheme:
a fluidized coarse flotation plant comprising:
the top of the flotation column body is provided with an overflow trough and a feeding device;
a bubble generator disposed on the flotation column;
the bubble distributor is arranged in the flotation column body and communicated with the bubble generator;
the lower end of the flotation column body is provided with a liquid inlet, the bubble distributor is positioned above the liquid inlet, and a turbulent flow plate is arranged between the liquid inlet and the bubble distributor in the flotation column body.
Further, the bubble generator comprises a contraction pipe, a throat pipe and a diffusion pipe which are communicated in sequence, the output end of the diffusion pipe is in butt joint with the output pipe, the inlet end of the contraction pipe is in butt joint with the closed gas-liquid mixing chamber, the gas-liquid mixing chamber is provided with a pressure gas inlet pipe and a fluid injection pipe, the output pipe is internally provided with a spiral blade, and the output pipe is in butt joint with the bubble inlet of the bubble distributor.
Further, the bubble generators are uniformly arranged along the circumferential direction of the flotation column body, each bubble distributor comprises at least two annular air distribution pipes which are concentrically and horizontally arranged and communicated through a connecting pipe, air outlet holes are uniformly distributed in each annular air distribution pipe, and a bubble inlet which corresponds to each bubble generator one by one is formed in the outermost annular air distribution pipe.
Furthermore, the axis of the fluid injection pipe coincides with the axis of the throat pipe, the fluid injection pipe and the air inlet pipe are arranged at an included angle, and the included angle is 40-45 degrees.
Furthermore, the taper angle of the contraction pipe is 30-35 degrees, the taper angle of the diffusion pipe is 35-40 degrees, and the longitudinal length proportion of the contraction pipe, the throat pipe and the diffusion pipe is 1:4: 2.
Further, the nozzle of the fluid injection pipe is a conical nozzle with a cone angle of 15-20 degrees.
Furthermore, a material distributor is arranged in a feeding port at the top of the flotation column body.
Furthermore, the turbulent flow plate is in a reverse rhombus conical shape, perforations for liquid flow to pass through are uniformly distributed on the turbulent flow plate, the conical bottom of the turbulent flow plate is directly communicated with the ore discharge port at the bottom of the flotation column body, and an automatically controlled ore discharge valve is arranged at the ore discharge port.
Further, the liquid inlets are uniformly arranged along the peripheral wall of the flotation column.
Further, the flotation column overcoat is equipped with annular feed liquor pipe, be equipped with on the annular feed liquor pipe with each the liquid outlet of inlet one-to-one intercommunication, be equipped with the feed liquor on the annular feed liquor pipe and always mouthful, the axis of always mouthful of feed liquor with the axis of annular feed liquor pipe is tangent.
A flotation process using the fluidized coarse flotation plant described above, comprising the steps of:
s1, starting the liquid supply device, allowing pressurized water flow to enter the flotation column from the liquid inlet at the lower end of the flotation column, and forming uniform ascending water flow in the flotation column after passing through the turbulent plate;
s2, air is compressed by an air compressor and then enters a bubble generator through an air inlet of a bubble generator, a foaming agent is emulsified by an emulsifier and then is added into water flow pressurized by a second pressurizing pump, and enters the micro-bubble generator through a water inlet of the bubble generator, a large number of micro-fine bubbles generated by the bubble generator are introduced into a bubble distributor, the bubbles are uniformly dispersed in a flotation column by the bubble distributor, and the bubbles and ascending water flow form a stable gas-liquid composite fluidized interference bed layer in the flotation column;
s3, after the ore pulp and the flotation reagent fully act through a pulp mixing and stirring barrel, the ore pulp and the flotation reagent are dispersed from the top of a flotation column body through an ore separator through a feeding device, then enter the flotation column body and slowly descend along the whole section of the flotation column body, the action of ore particles, bubbles and ascending water flow in an air-liquid compound fluidization interference bed layer is realized, finally, the target mineral continuously ascends through the buoyancy force of the bubbles and the vertical lifting force of the ascending water flow, then overflows from the column body and enters an overflow groove to form concentrate, and gangue minerals sink in the column body and finally are discharged from an ore discharge port to form tailings.
Compared with the prior art, the invention has the following beneficial effects:
1. through the comprehensive action of the bubbles and the ascending water flow, a gas-liquid composite fluidized interference bed layer of the bubbles and the ascending water flow is formed in the column body, the advantages of the dense medium separation principle and the flotation principle of the interference bed layer are fully exerted, and the flotation recovery of coarse particle minerals with the particle size of about 150-1000 microns is realized.
2. The ascending water flow increases the ascending force of mineral particles in the vertical direction, greatly reduces the average density of the target mineral, overcomes the defect that the adhesive force between the valuable mineral and bubbles is weak due to the coarse particles, enables the target mineral to enter the concentrate along with the ascending of the bubbles, and enables the gangue mineral to sink into tailings without the buoyancy of the bubbles, thereby realizing the flotation recovery of coarse particle minerals.
3. The tailings obtained by the equipment have extremely low grade of target minerals, can be directly used as final tailings for tailing discarding in a 'grinding-flotation' mineral separation process, and gangue minerals are removed from the process in time, so that the load of a ball mill is reduced, the treatment capacity of the flotation process is reduced, and the energy consumption is obviously reduced.
4. The equipment has good separation effect on sulphide ores such as copper sulphide ores and molybdenite and oxide ores such as scheelite, cassiterite and white lead ores.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a schematic view of an annular liquid inlet pipe according to the present invention;
FIG. 3 is a schematic view of a turbulator in accordance with the present invention;
FIG. 4 is a schematic view of a bubble generator according to the present invention;
FIG. 5 is a schematic view of a bubble generator and bubble distributor combination according to the present invention;
FIG. 6 is a schematic diagram of a process device connection in accordance with an embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1-6, a fluidized coarse flotation device comprises a flotation column 1, a bubble generator 14 and a bubble distributor 15, wherein the bottom of the flotation column 1 is provided with a bracket 7, the top of the flotation column 1 is provided with an overflow trough 2 and a feeding device butted with a flotation column feeding port 3, and the overflow trough 2 is provided with an overflow port 6. A bubble generator 14 is mounted on the outer wall of the flotation column 1 and a bubble distributor 15 is horizontally disposed within the flotation column 1 and is in communication with the bubble generator 14 to evenly distribute bubbles generated by the bubble generator within the flotation column 1. The lower end of the flotation column 1 is provided with a liquid inlet 11, a bubble distributor 15 is positioned above the liquid inlet 11, a turbulent plate 12 is arranged in the flotation column 1 between the liquid inlet 11 and the bubble distributor 15, and liquid entering from the liquid inlet 11 passes through the turbulent plate 12 to form an ascending liquid flow in the flotation column.
In the embodiment, the ascending liquid flow is formed in the flotation column 1, and the gas-liquid composite fluidized interference bed layer of the bubbles and the ascending water flow is formed in the column through the comprehensive action of the bubbles and the ascending water flow, so that the advantages of the dense medium separation principle and the flotation principle of the interference bed layer are fully exerted, and the flotation recovery of coarse particle minerals is realized. The ascending water flow increases the ascending force of mineral particles in the vertical direction, greatly reduces the average density of the target mineral, overcomes the defect that the adhesive force between the valuable mineral and bubbles is weak due to the coarse particles, enables the target mineral to enter the concentrate along with the ascending of the bubbles, and enables the gangue mineral to sink into tailings without the buoyancy of the bubbles, thereby realizing the flotation recovery of coarse particle minerals.
In order to improve the stability of ascending liquid flow, the liquid inlets 11 are uniformly arranged along the peripheral wall of the flotation column body 1, an annular liquid inlet pipe 10 is sleeved outside the flotation column body 1, liquid outlets which are communicated with the liquid inlets 10 in a one-to-one correspondence mode through branch pipes are arranged on the annular liquid inlet pipe 10, a liquid inlet main port 9 is arranged on the annular liquid inlet pipe 10, the axis of the liquid inlet main port 9 is tangent to the axis of the annular liquid inlet pipe 10, and the liquid inlet main port 9 is communicated with the liquid supply device through a pipe.
It should be noted that, in practical application, the bubble generator 14 includes a tube 19, the tube 19 is composed of a contraction tube, a throat tube and a diffusion tube which are sequentially communicated, an output end of the diffusion tube is in butt joint with an output tube, an inlet end of the contraction tube is in butt joint with a sealed gas-liquid mixing chamber, the gas-liquid mixing chamber is provided with a pressure gas inlet tube 22 and a fluid injection tube 21, a helical blade 29 is arranged in the output tube, and the output tube is in butt joint with a bubble inlet of the bubble distributor 15. The bubble generator with the structure integrates a high-pressure dissolved gas precipitation method and a Venturi tube jet flow foaming method, and the size of formed bubbles is stabilized at 0.1-0.3 mm. It should be noted that, in the practical design, the bubble generators 14 are uniformly arranged along the circumferential direction of the flotation column 1, the bubble distributor 15 includes at least two annular air distribution pipes 152 concentrically and horizontally arranged and communicated with each other through a connecting pipe 151, air outlet holes (not shown) are uniformly distributed on each annular air distribution pipe 152, and the annular air distribution pipe 152 located at the outermost layer is provided with bubble inlets corresponding to the bubble generators 14 one by one.
Specifically, the embodiment adopts two annular air distribution pipes 152, the diameter ratio of the two annular air distribution pipes 152 is 1:2, the connecting pipes 151 are uniformly distributed in an annular space between the two annular air distribution pipes, the annular air distribution pipe 152 at the outermost layer is provided with four air inlets, and each air inlet is butted with one bubble distributor. Pressurized water flow enters from a fluid jet pipe of the bubble generator, pressurized air enters from an air inlet pipe of the bubble generator, a large amount of micro bubbles are formed at the position of the diffusion pipe, the bubbles enter the shape air distribution pipe through the air inlet and are sprayed out through air outlet holes in the shape air distribution pipe, and ascending bubbles which are uniformly and stably distributed are formed in the flotation column body.
Preferably, in order to further refine the bubbles, the axis of the fluid jet pipe 21 is coincident with the axis of the throat pipe, the fluid jet pipe 21 and the air inlet pipe 22 are arranged at an included angle, the included angle is 40-45 degrees, the cone angle of the contraction pipe is 30-35 degrees, the cone angle of the diffusion pipe is 35-40 degrees, the longitudinal length ratio of the contraction pipe, the throat pipe and the diffusion pipe is 1:4:2, and the nozzle of the fluid jet pipe 21 is a conical nozzle with the cone angle of 15-20 degrees.
As a preferred scheme of the fluidized coarse grain flotation equipment, the turbulent flow plate 12 is formed by splicing three inclined fan-shaped plates from head to tail, the shape of the turbulent flow plate is inverted-rhombohedra, the included angle between the inclination angle of the fan-shaped plates and the horizontal plane is 30-35 degrees, through holes 13 for liquid flow to pass through are uniformly distributed on the turbulent flow plate 12, the axis of the through holes 13 is parallel to the axis of the flotation column 1, an outlet 8 communicated with a mine discharge port at the bottom of the flotation column is arranged at the cone bottom of the turbulent flow plate 12, and an automatically controlled mine discharge valve 18 is arranged at the mine discharge port. A sensor 17 for detecting the density of a composite interference bed layer in the column body is arranged in the flotation column body 1, a controller 5 which is in communication connection with the sensor 17 is installed at the top of the flotation column body 1 through a support 4, the controller 5 controls an ore discharge valve 18 to perform ore discharge operation according to the density of the interference bed layer, and when the density reaches a certain degree, the controller opens the ore discharge valve 18 to discharge tailings.
The working principle of the invention is as follows: fluidization coarse grain flotation equipment during operation, the foaming that mixes in fluid jet 21 and intake pipe 22 entering bubble generator are respectively followed to pressurized water stream and pressurized air, forms a large amount of small bubbles at the output tube output end, and the bubble gets into bubble distributor 15 through the air inlet, spouts through the venthole on the bubble distributor 15 to be full of the cross section of whole cylinder, form the even stable micro-fine bubble of distribution in the cylinder. The water flow enters the annular liquid inlet pipe 10 through the liquid inlet main port 9 under the driving of pressure, then enters the bottom of the column body along each liquid inlet 11, and then is vertically and upwards sprayed out from the through holes 13 on the turbulent flow plate 12, so that stable ascending water flow is formed in the column body and the cross section of the whole column body is filled. The micro-bubbles generated by the bubble distributor 15 and the ascending water flow formed by the turbulent flow plate 12 exist in the cylinder body at the same time and form a cooperative ascending situation, a stable gas-liquid composite fluidization interference bed layer can be formed in the cylinder body by reasonably adjusting the air pressure of the fed air and the water pressure of the water flow, and in the gas-liquid composite fluidization interference bed layer, coarse particles containing target minerals are subjected to the buoyancy of the bubbles and the vertical lift force of the ascending water flow at the same time, so that the particles can adhere to the bubbles and continuously ascend and enter the overflow chute 2 to become concentrate, gangue minerals are not adhered by the bubbles and finally sink to pass through the ore discharge port 8 to be discharged to become tailings.
A fluidized coarse grain flotation method comprises the steps that water flow 23 is pressurized by a first pressurizing pump 24, enters a flotation column 1 through a liquid inlet header 9 and an annular liquid inlet pipe 10, is sprayed out through perforations 13 in a turbulent flow plate 12, and forms ascending water flow in the column. Air 29 is compressed by an air compressor 28 and then enters the bubble generator 14 through an air inlet pipe 22, water flow 23 is pressurized by a second pressurizing pump 25, a foaming agent 27 is emulsified by an emulsifier 26 and then added into the water flow pressurized by the second pressurizing pump 25, the emulsified foaming agent enters the bubble generator 14 through a fluid injection pipe 21, the bubble generator 14 generates a large number of micro bubbles and leads the micro bubbles to the bubble distributor 15, and the bubbles are uniformly dispersed in the column body by the bubble distributor 15. The bubbles and the ascending water flow form a stable gas-liquid composite fluidization interference bed layer in the column body. The ore pulp 30 is conveyed into a pulp mixing barrel 32 through a first conveying pump 31, a pH regulator 33 is added into the pulp mixing barrel 32, the stirred ore pulp enters the pulp mixing barrel 32, a collecting agent 35 is added for stirring, the mixed pulp is conveyed into a feeding barrel 37 through a second conveying pump 36, the feeding barrel 37 is fixed at the upper part of a column body, the ore pulp in the feeding barrel 37 enters a feeding port 3 through a pipeline 39, and is dispersed by an ore separator 16 (the ore separator is preferably an umbrella-shaped ore separator) and then enters the column body and slowly descends along the whole section of the column body, the action of ore particles, bubbles and ascending water flow is disturbed in a gas-liquid composite bed layer, finally, the target minerals continuously ascend through the buoyancy force of the bubbles and the vertical lifting force of the ascending water flow, then overflow the column body and enter an overflow groove to become ore concentrates, and the gangue minerals sink in the column body and finally are discharged from an ore discharge port to become tailings. The obtained concentrate can be further treated and recycled, and the tailings can be directly used as final tailings to be discharged from the process flow of grinding-flotation, so that tailing discarding of gangue minerals is realized.
The present invention will be further described with reference to specific application examples.
Application example 1
The test material was a copper sulphide ore. The ore is ground by a ball mill and then enters a cyclone for classification, and the obtained ore pulp with the particle size of about 150-1000 mu m is used as an experimental ore feeding raw material, wherein the copper grade is 0.52%, and the proportion of the particle size fraction below 600 mu m is about 85%. Adding a pH regulator into the ore pulp to adjust the pH value of the ore pulp to 8.0, then adding a collecting agent butyl xanthate, stirring and mixing the pulp, adding a pine oil foaming agent, fully mixing the pulp, feeding the pulp into fluidized coarse grain flotation equipment from a feeding port for flotation, wherein overflow products are coarse ore concentrates, underflow products are discharged through a discharge port to form tailings, and the tailings are directly used as final tailings. The addition amount of the collecting agent relative to the raw ore is 200g/t, the foaming agent is 30g/t, the pH regulator is sodium carbonate, and the flotation temperature is 25 ℃. The test results in 1.29% of the Cu grade of the rough concentrate, 92.78% of recovery rate, 0.06% of the Cu grade of the tailings, 62.60% of yield and only 7.22% of copper loss of the tailing part (see table 1).
TABLE 1 test results of fluidized coarse-grained flotation equipment for certain copper sulfide ores
Application example 2
The test material was some molybdenite. After being ground by a ball mill, the ore enters a cyclone for classification, and the obtained ore pulp with the particle size of about 150-1000 mu m is used as an experimental ore feeding raw material, wherein the molybdenum grade is 0.17%, and the proportion of the particle size fraction below 600 mu m is about 90%. Adding a pH regulator into the ore pulp to adjust the pH value of the ore pulp to 8.0, then adding collecting agents including xanthate and black powder, stirring and mixing the mixture, adding a pine alcohol oil foaming agent, fully mixing the mixture, feeding the mixture into fluidized coarse grain flotation equipment from a feeding port to perform flotation, wherein overflow products are coarse ore concentrates, underflow products are discharged through a discharge port to form tailings, and the tailings are directly used as final tailings. The adding amount of the collecting agent relative to the raw ore is 150g/t of xanthate, 50g/t of black powder, 20g/t of foaming agent, sodium carbonate as a pH regulator and the flotation temperature is 25 ℃. The test results show that the Mo grade of the rough concentrate is 0.373 percent, the recovery rate is 94.21 percent, the Mo grade of the tailings is 0.017 percent, the yield is 57.40 percent, and the molybdenum loss of the tailing part is only 5.79 percent (shown in a table 2).
TABLE 2 test results of fluidized coarse-grained flotation equipment for certain molybdenite
Application example 3
The test material was a scheelite. Grinding ores by a ball mill, and then grading the ores by a cyclone to obtain ore pulp with the particle size of about 150-1000 mu m as an experimental ore feeding raw material, namely WO3The grade is 0.41%, and the fraction below 600 μm is about 78%. Adding a pH regulator into the ore pulp to adjust the pH value of the ore pulp to 9.5, then adding a complex collecting agent to stir and regulate the pulp, adding a pine oil foaming agent to perform full pulp regulation, feeding the obtained product into fluidized coarse-grain flotation equipment from a feeding port to perform flotation, wherein overflow products are coarse concentrates, bottom flows are discharged through a discharge port to form tailings, and the tailings are directly used as final tailings. The adding amount of the collecting agent relative to the raw ore is 600g/t of lead nitrate, 500g/t of benzohydroxamic acid, 40g/t of foaming agent, sodium carbonate as pH regulator and 25 ℃ of flotation temperature. The rough concentrate WO is obtained by the test3Grade 0.86%, recovery 87.02%, tailings WO3Grade 0.091%, yield 58.50%, reject fraction WO3Loss of powerOnly 12.98% (as in table 3).
TABLE 3 test results of fluidized coarse-grained flotation equipment for certain scheelite
Application example 4
The test material was a tin ore. Grinding ores by a ball mill, and then grading the ores by a cyclone to obtain ore pulp with the particle size of about 150-1000 mu m as an experimental ore feeding raw material, wherein SnO of the ore pulp2The grade is 0.332%, and the fraction below 600 μm is about 75%. Adding a pH regulator into the ore pulp to adjust the pH value of the ore pulp to 8.5, then adding a complex collecting agent, stirring and mixing the slurry, adding a pine oil foaming agent, fully mixing the slurry, feeding the slurry into fluidized coarse-grain flotation equipment from a feeding port for flotation, wherein overflow products are coarse concentrates, underflow is discharged through a discharge port to form tailings, and the tailings are directly used as final tailings. The adding amount of the collecting agent relative to the raw ore is 400g/t of lead nitrate, 400g/t of benzohydroxamic acid, 50g/t of foaming agent, sodium carbonate as pH regulator and 25 ℃ of flotation temperature. Crude ore concentrate SnO obtained by experiment2Grade of 0.78%, recovery rate of 86.10%, and tailing SnO2Grade 0.073%, yield 63.30%, SnO of reject fraction2The loss was only 13.90% (as in table 4).
TABLE 4 fluidized coarse-grained flotation equipment test results for a cassiterite
Application example 5
The test material was some white lead ore. After being ground by a ball mill, the ore enters a cyclone for classification, and the obtained ore pulp with the particle size of about 150-1000 mu m is used as an experimental ore feeding raw material, wherein the Pb grade is 4.36%, and the proportion of the particle size fraction below 600 mu m is about 91%. Adding a pH regulator into the ore pulp to adjust the pH value of the ore pulp to 8.0, then adding a collecting agent, stirring and mixing the pulp, adding a pine oil foaming agent, fully mixing the pulp, feeding the pulp into fluidized coarse grain flotation equipment from a feeding port for flotation, wherein overflow products are coarse concentrates, underflow is discharged through a discharge port to form tailings, and the tailings are directly used as final tailings. The adding amount of the collecting agent relative to the raw ore is 4000g/t of sodium sulfide, 300g/t of butyl xanthate, 20g/t of foaming agent, sodium carbonate as pH regulator and 25 ℃ of flotation temperature. The test results in 7.72% Pb grade of the rough concentrate, 90.60% recovery rate, 0.84% Pb grade of the tailings, 48.80% yield and 9.40% lead loss of the tailing part (see Table 5).
TABLE 5 fluidized coarse-grain flotation equipment test results for certain galena
The above examples are merely illustrative for clearly illustrating the present invention and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. Nor is it intended to be exhaustive of all embodiments. And obvious variations or modifications of the invention may be made without departing from the scope of the invention.
Claims (7)
1. A fluidized coarse flotation plant comprising:
the top of the flotation column body is provided with an overflow trough and a feeding device;
a bubble generator disposed on the flotation column;
the bubble distributor is arranged in the flotation column body and communicated with the bubble generator;
the method is characterized in that: a liquid inlet is formed in the lower end of the flotation column body, the bubble distributor is positioned above the liquid inlet, and a turbulent flow plate is arranged between the liquid inlet and the bubble distributor in the flotation column body;
the bubble generator comprises a contraction pipe, a throat pipe and a diffusion pipe which are sequentially communicated, the output end of the diffusion pipe is in butt joint with an output pipe, the inlet end of the contraction pipe is in butt joint with a closed gas-liquid mixing chamber, a pressure gas inlet pipe and a fluid injection pipe are arranged on the gas-liquid mixing chamber, a spiral blade is arranged in the output pipe, and the output pipe is in butt joint with a bubble inlet of the bubble distributor;
the bubble generators are uniformly arranged along the circumferential direction of the flotation column, the bubble distributor comprises at least two annular gas distribution pipes which are concentrically and horizontally arranged and communicated through a connecting pipe, gas outlet holes are uniformly distributed on each annular gas distribution pipe, and bubble inlets which are in one-to-one correspondence with the bubble generators are arranged on the annular gas distribution pipe positioned on the outermost layer; a material distributor is arranged in the feeding port at the top of the flotation column body.
2. The fluidized coarse flotation plant of claim 1, characterized in that: the axis of the fluid injection pipe is coincided with the axis of the throat pipe, the fluid injection pipe and the air inlet pipe are arranged in an included angle, and the included angle is 40-45 degrees.
3. The fluidized coarse flotation plant of claim 1, characterized in that: the taper angle of the contraction pipe is 30-35 degrees, the taper angle of the diffusion pipe is 35-40 degrees, the longitudinal length proportion of the contraction pipe, the throat pipe and the diffusion pipe is 1:4:2, and the nozzle of the fluid jet pipe is a conical nozzle with the taper angle of 15-20 degrees.
4. Fluidized coarse flotation plant according to any one of claims 1 to 3, characterized in that: the turbulent flow plate is in a reversed rhombus conical shape, perforations for liquid flow to pass through are uniformly distributed on the turbulent flow plate, the conical bottom of the turbulent flow plate is directly communicated with the ore discharge port at the bottom of the flotation column, and the ore discharge port is provided with an automatically controlled ore discharge valve.
5. The fluidized coarse flotation plant of claim 4, characterized in that: the liquid inlets are uniformly arranged along the peripheral wall of the flotation column.
6. The fluidized coarse flotation plant of claim 5, characterized in that: the flotation column overcoat is equipped with annular feed liquor pipe, be equipped with on the annular feed liquor pipe with each the liquid outlet of inlet one-to-one intercommunication, be equipped with the total mouth of feed liquor on the annular feed liquor pipe, the axis of the total mouth of feed liquor with the axis of annular feed liquor pipe is tangent.
7. A flotation process using the fluidized coarse flotation plant of any one of claims 1 to 6, comprising the steps of:
s1, starting the liquid supply device, allowing pressurized water flow to enter the flotation column from the liquid inlet at the lower end of the flotation column, and forming uniform ascending water flow in the flotation column after passing through the turbulent plate;
s2, air is compressed by an air compressor and then enters a bubble generator through an air inlet of a bubble generator, a foaming agent is emulsified by an emulsifier and then is added into water flow pressurized by a pressurizing pump, and enters the bubble generator through a water inlet of the bubble generator, a large number of micro-fine bubbles generated by the bubble generator are introduced into a bubble distributor, the bubbles are uniformly dispersed in a flotation column by the bubble distributor, and the bubbles and ascending water flow form a stable gas-liquid composite fluidization interference bed layer in the flotation column;
s3, after the ore pulp and the flotation reagent fully act through a pulp mixing and stirring barrel, the ore pulp and the flotation reagent are dispersed from the top of a flotation column body through a material distributor through a feeding device, then enter the flotation column body and slowly descend along the whole section of the flotation column body, the action of ore particles, bubbles and ascending water flow in a gas-liquid compound fluidization interference bed layer is realized, finally, the target mineral continuously ascends through the buoyancy force of the bubbles and the vertical lifting force of the ascending water flow, then overflows from the column body and enters an overflow groove to form concentrate, and gangue minerals sink in the column body and are finally discharged from a mine discharge port to form tailings.
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| US5431286A (en) * | 1994-01-06 | 1995-07-11 | Inco Limited | Recirculating column flotation apparatus |
| US9085000B2 (en) * | 2007-02-26 | 2015-07-21 | Newcastle Innovation Limited | Method and apparatus for flotation in a fluidized bed |
| CN201399385Y (en) * | 2009-03-11 | 2010-02-10 | 湖南省电力粉煤灰开发有限公司 | Dedicated flotation column for fly ash |
| CN101844104A (en) * | 2010-04-15 | 2010-09-29 | 河南理工大学 | Hydraulic classifier |
| CN103464057A (en) * | 2013-09-06 | 2013-12-25 | 天津聚贤达科技有限公司 | Novel gas distributor |
| CN103657839B (en) * | 2013-12-09 | 2015-12-09 | 中国矿业大学 | Gas-liquid-solid three-phase fluid bed separator and method for separating thereof |
| CN104632216B (en) * | 2015-01-16 | 2017-04-05 | 中国矿业大学 | Bulb apparatus are produced in the self-priming short distance reinforcing of rotating jet for coal-winning machine dust suppression |
| CN105689155B (en) * | 2016-04-08 | 2017-10-24 | 中国矿业大学 | Multi-product flotation column device and method |
| CN209020582U (en) * | 2018-10-24 | 2019-06-25 | 中南大学 | A kind of fluidization coarse flotation equipment |
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