CN114700181B - Flotation device and method suitable for coarse slime separation - Google Patents
Flotation device and method suitable for coarse slime separation Download PDFInfo
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- CN114700181B CN114700181B CN202110831650.0A CN202110831650A CN114700181B CN 114700181 B CN114700181 B CN 114700181B CN 202110831650 A CN202110831650 A CN 202110831650A CN 114700181 B CN114700181 B CN 114700181B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/02—Froth-flotation processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/14—Flotation machines
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/14—Flotation machines
- B03D1/1443—Feed or discharge mechanisms for flotation tanks
- B03D1/1456—Feed mechanisms for the slurry
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/14—Flotation machines
- B03D1/24—Pneumatic
- B03D1/245—Injecting gas through perforated or porous area
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2203/00—Specified materials treated by the flotation agents; specified applications
- B03D2203/02—Ores
- B03D2203/04—Non-sulfide ores
- B03D2203/08—Coal ores, fly ash or soot
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Abstract
The invention relates to a flotation device and a flotation method suitable for coarse slime separation, belongs to the technical field of mineral separation and recovery, and solves the problems of low coarse slime recovery rate and poor separation precision in the prior art. The invention comprises a flotation column and a gas-water distribution unit, wherein the gas-water distribution unit is arranged at the lower part of the flotation column and is concentrically arranged, the gas-water distribution unit comprises a first gas distribution unit and a gas-water mixing distribution unit, and the gas-water mixing distribution unit is arranged above the first gas distribution unit. The invention has simple structure and good sorting effect.
Description
Technical Field
The invention relates to the technical field of mineral separation and recovery, in particular to a flotation device and a flotation method suitable for coarse slime separation.
Background
Coal has an indispensable function in national economy in China, and the industries of energy, chemical industry, steel and the like closely related to people's life all need to directly or indirectly use coal or processed products of the coal, so that the efficient utilization of coal resources has great significance for sustainable development in China. The washing and selecting process of coal is an important premise for realizing the high-efficiency utilization of coal resources, and along with the popularization and application of mechanized mining technology in China, the heavy medium separation is becoming the mainstream coal separation technology, and the content of fine fraction (-3 mm) in raw coal entering a coal dressing factory is increasing.
The fine fraction (-3 mm) of the raw coal is generally divided into coarse slime (0.25-3 mm) and fine slime (-0.25 mm), a classification cyclone is usually used for classifying the fine fraction in a coal preparation plant, and then different processes are adopted for separation and recovery. The common coarse slime separation equipment is used for separation according to the density difference between coal and gangue particles, the typical equipment is TBS (teeter bed separator, an interference bed separator), a slime dense medium cyclone and the like, but the problem that coarse slime has serious phenomenon of 'equal sedimentation', namely that coarse low-density coal particles and fine high-density gangue particles have the same sedimentation speed, so that the ash content of a clean coal product is higher, a plurality of sets of dehydration and high-ash fine slime removal processes are needed in the clean coal product treatment process, the quality of the clean coal product is lower, and the process is slightly complicated; flotation is the most effective micro-particle fraction sorting technology in the prior art, and mainly uses bubbles as sorting and conveying media for sorting according to the hydrophobicity difference between the surfaces of fine coal slime particles and gangue fine slime particles, and common flotation equipment is a flotation machine and a flotation column.
The existing coarse slime separation device and method based on density difference between coal and gangue are low in separation effect, and the problem of serious coarse slime ' etc. sinking phenomenon can be well avoided by a flotation process based on particle surface property difference, but the coarse slime separation device and method are remarkable in that coarse slime particles are high in inertia, are easily desorbed under turbulence effect in flotation to cause low recovery rate, namely ' coarse-run ' phenomenon occurs, abundant turbulence environments exist in flotation columns and flotation machines widely used nowadays, and serious ' coarse-run ' problem occurs for particles with the size of +0.5mm in feeding. Therefore, developing a static flotation device and method with small turbulence disturbance and suitable for coarse grain separation has great significance for the efficient separation and recovery of coarse slime.
Disclosure of Invention
In view of the above analysis, the embodiment of the invention aims to provide a flotation device and a flotation method suitable for coarse slime separation, which are used for solving the problems of low recovery rate and poor separation precision of the conventional coarse slime and providing a high-efficiency separation recovery device and a high-efficiency separation recovery method with simple structure and good separation effect for the separation recovery of the coarse slime.
In one aspect, the invention provides a flotation device suitable for coarse slime separation, which comprises a flotation column and a gas-water distribution unit, wherein the gas-water distribution unit is arranged at the lower part of the flotation column and is concentrically arranged, the gas-water distribution unit comprises a first gas distribution unit and a gas-water mixing distribution unit, and the gas-water mixing distribution unit is arranged above the first gas distribution unit.
Further, the gas-water mixing and distributing unit comprises an annular water tank, a fluid distributing plate and a strip-shaped gas-water mixing chamber, wherein two ends of the strip-shaped gas-water mixing chamber are communicated with the annular water tank, and the fluid distributing plate is arranged at the top of the strip-shaped gas-water mixing chamber.
Further, a plurality of strip-shaped air-water mixing chambers are arranged in the inner ring of the annular water tank, and the strip-shaped air-water mixing chambers are arranged in parallel.
Further, the first gas distribution unit comprises a first annular high-pressure gas chamber and a first strip-shaped high-pressure gas chamber, and two ends of the first strip-shaped high-pressure gas chamber are communicated with the first annular high-pressure gas chamber.
Further, the first strip-shaped high-pressure air chamber is arranged in the inner ring of the first annular high-pressure air chamber and is opposite to the strip-shaped air-water mixing chamber, and the upper end of the first strip-shaped high-pressure air chamber is connected with the lower end of the strip-shaped air-water mixing chamber.
Further, the gas-water distribution unit further comprises a first bubble generation plate, wherein the first bubble generation plate is arranged at the joint of the strip-shaped gas-water mixing chamber and the first strip-shaped high-pressure air chamber and is used for separating the strip-shaped gas-water mixing chamber and the first strip-shaped high-pressure air chamber.
Further, the flotation column, the annular water tank and the first annular high-pressure air chamber are arranged concentrically.
Further, the device also comprises a water pipe and a first air input pipe, wherein the water pipe is communicated with the annular water tank, and the first air input pipe is communicated with the first annular high-pressure air chamber.
Further, the water delivery pipe and the first air input pipe on the same side of the flotation column are vertically aligned, the water delivery pipe is perpendicular to the first strip-shaped high-pressure air chamber, and the first air input pipe is perpendicular to the strip-shaped air-water mixing chamber.
In another aspect, the present invention provides a flotation method suitable for coarse slime separation, adopting the flotation device suitable for coarse slime separation, comprising the steps of:
step 1: injecting fluidizing water containing foaming agent into the annular water tank through a water pipe, inputting air into the first annular high-pressure air chamber through a first air input pipe, enabling the air to enter the first strip-shaped high-pressure air chamber, dispersing the air into microbubbles through a first bubble generating plate to form rising microbubble flows, fully mixing the rising microbubbles with the fluidizing water in the strip-shaped air-water mixing chamber, forming rising water flows with high microbubble contents through a fluid distribution plate shape, and entering a flotation column;
step 2: after the flotation column is filled with fluidized water, injecting coarse coal slime into the flotation column;
coarse slime particles in ore pulp sink along with the ore pulp, collide with rising bubbles in a countercurrent mineralization area, hydrophobic coal particles adhere to the bubbles to form particle bubble aggregates, coal particles which are not adhered to the bubbles continue to sink to a scavenging area, collide and adhere again with the bubbles at the lower side of a flotation column to form particle bubble aggregates, and the particle bubble aggregates float upwards to form clean coal under the dual effects of bubble buoyancy and rising water flow;
the hydrophilic gangue particles are collided with bubbles and then sink to a tailing pre-dewatering area formed by the fluid distribution plate to form tailings.
Compared with the prior art, the invention has at least one of the following beneficial effects:
(1) The air-water distribution unit comprises a first air distribution unit and an air-water mixing unit which are arranged up and down, wherein air bubbles generated by the first air distribution unit enter the air-water mixing distribution unit to be mixed with fluidized water and then enter the upper part of the flotation column, and the air flow and the water flow of the flotation process are independently controlled through the serial arrangement of the air-water mixing distribution unit and the air distribution unit, so that the creation of a flotation flow field environment with low fluid disturbance and high micro-bubble content is realized; through the flotation flow field environment with low fluid disturbance and high micro-bubble content, the desorption probability of the coarse slime on bubbles is reduced, the stability of particle bubble aggregates is improved, and the high-efficiency separation and recovery of the coarse slime are realized.
(2) The multi-stage gas distribution units are distributed in the flotation column from bottom to top, ore pulp in the flotation column is subjected to gradient gas inlet through the multi-stage gas distribution units, so that the content of microbubbles in the ore pulp is ensured, meanwhile, the independent control of the gas flow and the water flow in the flotation process is realized, and the construction of a flotation environment with small disturbance of fluid and sufficient content of microbubbles suitable for coarse-grain flotation is realized; by constructing a flotation environment with small fluid disturbance and sufficient micro-bubble content, the probability of desorbing coarse-grain coal slime from bubbles is reduced, the phenomenon of coarse-grain running of flotation is improved, and the high-efficiency separation of the coarse-grain coal slime is realized.
(3) The annular high-pressure air chambers are all single annular, and compared with the high-pressure air chambers formed by a plurality of annular, the high-pressure air chambers formed by the single annular are simple in structure and easy to process and shape, fluid distribution is uniform, and coarse particle flotation recovery is facilitated.
(4) The strip-shaped high-pressure air chamber is perpendicular to the air input pipe, so that the situation that high-pressure air entering the annular high-pressure air chamber from the air input pipe directly enters the strip-shaped high-pressure air chamber is avoided, and further the air pressure in the strip-shaped high-pressure air chamber opposite to the air input pipe is obviously higher than that of bubbles, and the micro bubbles are unevenly distributed is avoided.
In the invention, the technical schemes can be mutually combined to realize more preferable combination schemes. Additional features and advantages of the invention will be set forth in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. The objectives and other advantages of the invention may be realized and attained by the structure particularly pointed out in the written description and drawings.
Drawings
The drawings are only for purposes of illustrating particular embodiments and are not to be construed as limiting the invention, like reference numerals being used to refer to like parts throughout the several views.
FIG. 1 is a schematic diagram of a flotation device with a single stage gas distribution unit according to an embodiment;
FIG. 2 is a top view of a gas-water distribution unit structure of an embodiment;
FIG. 3 is a cross-sectional view of A-A of FIG. 2 of an exemplary embodiment;
FIG. 4 is a B-B cross-sectional view of FIG. 2 of an embodiment;
FIG. 5 is a schematic diagram of a flotation device with a multi-stage gas distribution unit according to an embodiment;
FIG. 6 is a schematic diagram of a second air distribution unit according to an embodiment;
FIG. 7 is a cross-sectional view A-A of FIG. 6 of an exemplary embodiment;
FIG. 8 is a B-B cross-sectional view of FIG. 6 of an embodiment;
FIG. 9 is a schematic diagram of a third air distribution unit according to an embodiment;
FIG. 10 is a cross-sectional view A-A of FIG. 9 of an exemplary embodiment;
fig. 11 is a B-B cross-sectional view of fig. 9 of an embodiment.
Reference numerals:
1-a feeding pipe; 2-a feeding distributor; 3-a clean coal overflow tank; 4-a flotation column; 5-an annular water tank; 6-a water delivery pipe; 7-a fluid distribution plate; 8-a first air input tube; 9-a first annular high pressure plenum; 10-a first bubble generating plate; 11-tail coal dehydration cone; 12-tail coal discharging pipe; 13-a strip-shaped air-water mixing chamber; 14-a first strip-shaped high-pressure air chamber;
15-a second gas distribution unit; 16-a third gas distribution unit; 17-a second annular high pressure plenum; 18-a second air input; 19-a second bubble generating plate; 20-a second strip-shaped high-pressure air chamber; 21-a third annular high pressure plenum; 22-a third air input; 23-a third bubble generating plate; 24-third strip-shaped high-pressure air chamber.
Detailed Description
The following detailed description of preferred embodiments of the invention is made in connection with the accompanying drawings, which form a part hereof, and together with the description of the embodiments of the invention, are used to explain the principles of the invention and are not intended to limit the scope of the invention.
In describing embodiments of the present invention, it should be noted that, unless explicitly stated and limited otherwise, the term "coupled" should be interpreted broadly, for example, as being fixedly coupled, detachably coupled, integrally coupled, mechanically coupled, electrically coupled, directly coupled, or indirectly coupled via an intermediate medium. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
The terms "top," "bottom," "above … …," "below," and "on … …" are used throughout the description to refer to the relative positions of components of the device, such as the relative positions of the top and bottom substrates inside the device. It will be appreciated that the devices are versatile, irrespective of their orientation in space.
Example 1
In one embodiment of the invention, as shown in fig. 1, a flotation device suitable for coarse slime separation is disclosed, which comprises a flotation column 4 and a gas-water distribution unit, wherein the gas-water distribution unit is arranged concentrically with the flotation column 4 and is positioned at the lower part of the flotation column 4, the gas-water distribution unit comprises a first gas distribution unit and a gas-water mixing distribution unit, the gas-water mixing distribution unit is positioned above the first gas distribution unit, and bubbles generated by the first gas distribution unit are mixed with fluidization water through the gas-water mixing distribution unit and then enter the upper part of the flotation column 4.
Compared with the prior art, the flotation device suitable for coarse slime separation comprises a gas-water distribution unit, wherein the gas-water distribution unit comprises a first gas distribution unit and a gas-water mixing unit which are arranged up and down, and bubbles generated by the first gas distribution unit enter the gas-water mixing distribution unit to be mixed with fluidized water and then enter the upper part of a flotation column, and through the serial arrangement of the gas-water mixing distribution unit and the gas distribution unit, the independent control of the gas flow and the water flow in the flotation process is realized, and the creation of a flotation flow field environment with low fluid disturbance and high microbubble content is realized; through the flotation flow field environment with low fluid disturbance and high micro-bubble content, the desorption probability of the coarse slime on bubbles is reduced, the stability of particle bubble aggregates is improved, and the high-efficiency separation and recovery of the coarse slime are realized.
The flotation device further comprises a feeding pipe 1 and a feeding distributor 2, wherein the lower end of the feeding pipe 1 is connected with the feeding distributor 2, the feeding distributor 2 is positioned in the flotation column 4, coarse coal slime feeding is injected through the feeding pipe 1, and the coarse coal slime feeding is uniformly distributed in the flotation column 4 through the feeding distributor 2.
The bottom of the flotation column 4 is provided with a tail coal dehydration cone 11, the tail coal dehydration cone 11 and the flotation column 4 are concentrically arranged, and the gas-water distribution unit is nested at the lower part of the flotation column 4 and is positioned above the tail coal dehydration cone 11. The bottom of the tail coal dehydration cone 11 is provided with a tail coal discharge pipe 12 so that the tail coal sinking in the flotation column 4 is discharged from the tail coal discharge pipe 12 after being dehydrated at the tail coal dehydration cone 11, and a tail coal product is obtained.
In this embodiment, the tailings discharge pipe 12 is arranged concentrically with the flotation column 4, so that tailings are conveniently concentrated and discharged to the middle of the flotation column 4.
As shown in fig. 3-4, the gas-water mixing and distributing unit comprises an annular water tank 5, a fluid distribution plate 7 and a strip-shaped gas-water mixing chamber 13, wherein the annular water tank 5 and the flotation column 4 are concentrically arranged, two ends of the strip-shaped gas-water mixing chamber 13 are communicated with the annular water tank 5, and the strip-shaped gas-water mixing chamber 13 is arranged in the inner ring of the annular water tank 5. The fluid distribution plate 7 is arranged on top of the strip-shaped air-water mixing chamber 13.
It is worth noting that both ends and up and down of the strip-shaped air-water mixing chamber 13 are not closed, both ends of the strip-shaped air-water mixing chamber 13 are communicated with the annular water tank 5, so that vulcanized water in the annular water tank 5 can enter the strip-shaped air-water mixing chamber 13, the upper part of the strip-shaped air-water mixing chamber 13 is opened and provided with a fluid distribution plate 7, and the lower part of the strip-shaped air-water mixing chamber is opened and provided with a first bubble generating plate 10.
As shown in fig. 2, a plurality of strip-shaped air-water mixing chambers 13 are provided in the inner ring of the annular water tank 5, and the plurality of strip-shaped air-water mixing chambers 13 are arranged in parallel so that a large number of microbubbles are generated from the fluidizing water flowing out of the air-water mixing unit.
The first gas distribution unit comprises a first annular high-pressure gas chamber 9 and a first strip-shaped high-pressure gas chamber 14, the first annular high-pressure gas chamber 9 and the flotation column 4 are concentrically arranged, two ends of the first strip-shaped high-pressure gas chamber 14 are communicated with the first annular high-pressure gas chamber 9, and the first strip-shaped high-pressure gas chamber 14 is arranged in the inner ring of the first annular high-pressure gas chamber 9. The first strip-shaped high-pressure air chamber 14 is of a U-shaped structure, the upper end of the first strip-shaped high-pressure air chamber 14 is connected with the lower end of the strip-shaped air-water mixing chamber 13, the length of the first strip-shaped high-pressure air chamber 14 is equal to that of the strip-shaped air-water mixing chamber 13, the width of the first strip-shaped high-pressure air chamber 14 is equal to that of the strip-shaped air-water mixing chamber 13, the first strip-shaped high-pressure air chamber 14 is just right opposite to the strip-shaped air-water mixing chamber 13, and air flowing out of the first strip-shaped high-pressure air chamber 14 directly enters the strip-shaped air-water mixing chamber 13.
A plurality of first strip-shaped high-pressure air chambers 14 are arranged in the inner ring of the first annular high-pressure air chamber 9, and the plurality of first strip-shaped high-pressure air chambers 14 are arranged in parallel, so that a large number of microbubbles are generated by the fluidized water flowing out of the air-water mixing unit.
The first annular high-pressure air chamber 9 is equal to the annular water tank 5 in inner diameter and outer diameter, the annular water tank 5 is positioned above the first annular high-pressure air chamber 9, and an annular sealing plate is adopted in the middle for spacing.
The gas-water distribution unit further comprises a first gas bubble generation plate 10, wherein the first gas bubble generation plate 10 is in a long strip shape, and the first gas bubble generation plate 10 is arranged at the joint of the strip-shaped gas-water mixing chamber 13 and the first strip-shaped high-pressure air chamber 14 and is used for separating the strip-shaped gas-water mixing chamber 13 and the first strip-shaped high-pressure air chamber 14.
In order to form micro bubbles, through holes are uniformly distributed on the first bubble generation plate 10, the diameter of each through hole is 5-10 mu m, and the size of the generated bubbles is more suitable for flotation.
The first bubble generating plate 10 is a microporous ceramic plate, so that the reliability of bubble generation is ensured; the first bubble generating plate 10 is horizontally arranged, so that the flotation column 4 is simple to install and manufacture, and bubbles are ensured to vertically rise in the air-water mixing chamber 7, and turbulence is avoided.
In view of the input of fluidizing water and high pressure air, the flotation device further comprises a water pipe 6 and a first air input pipe 8, as shown in fig. 1, 3, the water pipe 6 being in communication with the annular water tank 5, the first air input pipe 8 being in communication with the first annular high pressure air chamber 9. The water pipe 6 and the first air input pipe 8 are all provided with a plurality of water pipes, and are uniformly distributed along the radial direction of the flotation column 4, preferably, the water pipe 6 is provided with two water pipes, and the first air input pipe 8 is provided with two water pipes.
Specifically, the water pipe 6 is symmetrically arranged along two sides of the diameter direction of the annular water tank 5, the first air input pipe 8 is symmetrically arranged along two sides of the diameter direction of the first annular high-pressure air chamber 9, the water pipe 6 and the first air input pipe 8 on the same side of the flotation column 4 are vertically aligned, the water pipe 6 is vertical to the first strip-shaped high-pressure air chamber 14, the first air input pipe 8 is vertical to the strip-shaped air-water mixing chamber 13, high-pressure air entering the first annular high-pressure air chamber 9 from the first air input pipe 8 is prevented from directly entering the first strip-shaped high-pressure air chamber 14, and then the air pressure in the first strip-shaped high-pressure air chamber 14 opposite to the first air input pipe 8 is obviously higher than that of bubbles, so that microbubbles are unevenly distributed.
The flotation device also comprises a clean coal overflow groove 3, and the clean coal overflow groove 3 is arranged at the upper end of the flotation column 4 and is used for precise recovery.
Further, in order to realize gradient air intake in the flotation column 4, the flotation device is provided with a multi-stage air distribution unit, as shown in fig. 5, the flotation device is provided with a three-stage air distribution unit, and the flotation device further comprises a second air distribution unit 15 and a third air distribution unit 16 which are horizontally arranged besides the first air distribution unit, wherein the second air distribution unit 15 is positioned above the first air distribution unit, the third air distribution unit 16 is positioned above the second air distribution unit 15, and both the second air distribution unit 15 and the third air distribution unit 16 are connected with the flotation column 4.
Compared with the prior art, the flotation device provided by the embodiment has the advantages that the multistage gas distribution units are distributed in the flotation column from bottom to top, the multistage gas distribution units are used for carrying out gradient gas inlet on ore pulp in the flotation column, so that the micro-bubble content in the ore pulp is ensured, the independent control of the gas flow and the water flow in the flotation process is realized, and the construction of a flotation environment with small fluid disturbance and sufficient micro-bubble content suitable for coarse-grain flotation is realized; by constructing a flotation environment with small fluid disturbance and sufficient micro-bubble content, the probability of desorbing coarse-grain coal slime from bubbles is reduced, the phenomenon of coarse-grain running of flotation is improved, and the high-efficiency separation of the coarse-grain coal slime is realized.
As shown in fig. 6, the second air distribution unit 15 includes a second annular high-pressure air chamber 17 and a second air input pipe 18, the second annular high-pressure air chamber 17 is concentrically arranged with the flotation column 4, and the second air input pipe 18 is symmetrically arranged on the cylindrical surface of the second annular high-pressure air chamber 17 and is communicated with the second annular high-pressure air chamber 17.
As shown in fig. 7 and 8, the second air distribution unit 15 further includes a second air bubble generating plate 19 and a second strip-shaped high-pressure air chamber 20, the second strip-shaped high-pressure air chamber 20 has a "U" -shaped structure, and the second air bubble generating plate 19 is disposed on an opening side of the second strip-shaped high-pressure air chamber 20, so that high-pressure air in the second strip-shaped high-pressure air chamber 20 flows out from the second air bubble generating plate 19 to form microbubbles. The second bubble generating plate 19 is a microporous ceramic plate having a pore diameter of 5 μm to 10. Mu.m.
As shown in fig. 6, both ends of the second strip-shaped high-pressure air chamber 20 are communicated with the second annular high-pressure air chamber 17, and a plurality of second strip-shaped high-pressure air chambers 20 are provided, and a plurality of second strip-shaped high-pressure air chambers 20 are arranged in parallel. This structure enables the second gas distribution unit 15 to generate a large number of uniform microbubbles.
It should be noted that the second strip-shaped high-pressure air chamber 20 is disposed perpendicular to the second air input tube 18, so that the high-pressure air entering the second annular high-pressure air chamber 17 from the second air input tube 18 directly enters the second strip-shaped high-pressure air chamber 20, and the air pressure in the second strip-shaped high-pressure air chamber 20 opposite to the second air input tube 18 is obviously higher than that of air bubbles, so that micro bubbles are unevenly distributed.
As shown in fig. 9, the third air distribution unit 16 includes a third annular high-pressure air chamber 21 and a third air input pipe 22, the third annular high-pressure air chamber 21 is concentrically arranged with the flotation column 4, and the third air input pipe 22 is provided with two, symmetrically arranged on the cylindrical surface of the third annular high-pressure air chamber 21, and is communicated with the third annular high-pressure air chamber 21.
As shown in fig. 10 and 11, the third air distribution unit 16 further includes a third air bubble generating plate 23 and a third strip-shaped high-pressure air chamber 24, the third strip-shaped high-pressure air chamber 24 has a "U" shape, and the third air bubble generating plate 23 is disposed on an opening side of the third strip-shaped high-pressure air chamber 24, so that the high-pressure air in the third strip-shaped high-pressure air chamber 24 flows out from the third air bubble generating plate 23 to form microbubbles. The third bubble generating plate 23 is a microporous ceramic plate having a pore diameter of 5 μm to 10. Mu.m.
As shown in fig. 9, both ends of the third strip-shaped high-pressure air chamber 24 are communicated with the third annular high-pressure air chamber 21, and a plurality of third strip-shaped high-pressure air chambers 24 are provided, and a plurality of third strip-shaped high-pressure air chambers 24 are arranged in parallel. This structure enables the third gas distribution unit 16 to generate a large number of uniform microbubbles.
It should be noted that the third strip-shaped high-pressure air chamber 24 is disposed perpendicular to the third air input tube 22, so that the high-pressure air entering the third annular high-pressure air chamber 21 from the third air input tube 22 directly enters the third strip-shaped high-pressure air chamber 24, and the air pressure in the third strip-shaped high-pressure air chamber 24 opposite to the third air input tube 22 is obviously higher than that of air bubbles, so that the micro bubbles are unevenly distributed.
In this embodiment, the projection of the second strip plenum 20 toward the horizontal plane of the third strip plenum 24 may be parallel to or intersect with the third strip plenum 24. To facilitate coarse slime particle sinking, the second strip-shaped high pressure plenum 20 is preferably parallel to the third strip-shaped high pressure plenum 24.
Because the flotation column 4 is internally provided with the first gas distribution unit, the second gas distribution unit 15 and the third gas distribution unit 16 from bottom to top in sequence, considering that the second gas distribution unit 15 has part of bubbles generated by the first gas distribution unit, the third gas distribution unit 16 has bubbles generated by the first gas distribution unit and the second gas distribution unit 13, and the second gas distribution unit 15 and the third gas distribution unit 16 mainly supplement and share the air inflow of the first gas distribution unit, when the flotation device is started up, the air flow of each stage of gas distribution unit is as follows: the first gas distribution unit, the second gas distribution unit 15, and the third gas distribution unit 16 decrease in order.
It is worth noting that the second gas distribution unit 15 and the third gas distribution unit 16 are both located between the clean coal enrichment zone and the tailing pre-dewatering zone in the flotation column 4. The first annular high-pressure air chamber 9, the second annular high-pressure air chamber 17 and the third annular high-pressure air chamber 21 are all single annular, and compared with the high-pressure air chambers formed by a plurality of annular structures, the high-pressure air chamber formed by the single annular structure is simple in structure and easy to process and shape, the high-pressure air chambers formed by the plurality of annular structures are difficult to manufacture, and the air and/or water quantity of the annular structures on the outer side is/are obviously higher than that of the annular structures on the inner side, so that uneven fluid distribution is caused, and coarse particle flotation recovery is not facilitated.
Example 2
In another embodiment of the present invention, a flotation method suitable for coarse slime separation is disclosed, wherein the flotation device suitable for coarse slime separation of embodiment 1 is used, and when only a primary gas distribution unit is present in the flotation column 4, the steps include:
step 1: injecting fluidizing water containing foaming agent into the annular water tank 5 through the water pipe 6, and enabling the fluidizing water containing the foaming agent to enter the strip-shaped air-water mixing chamber 13 through the annular water tank 5; compressed air is input into the first annular high-pressure air chamber 9 through the first air input pipe 8, the air enters the first strip-shaped high-pressure air chamber 14 through the first annular high-pressure air chamber 9, is dispersed into microbubbles through the first bubble generating plate 10 to form rising microbubble flows, and enters the strip-shaped air-water mixing chamber 13 to be fully mixed with fluidization water in the rising microbubble flows, and then the rising water flows with high microbubble content are formed through the fluid distribution plate 7 and enter the flotation column 4 to form a flotation flow field environment with small turbulence disturbance and sufficient microbubble content.
The air in the high-pressure air chamber 9 is dispersed into series of small bubbles through the first bubble generating plate 10 to form a micro-bubble ascending flow, and after entering the air-water mixing chamber 7, the bubbles are uniformly dispersed in the vulcanized water, and the whole air-water presents the property of fluid, so that the flotation environment with small fluid disturbance and sufficient micro-bubble content is formed.
Step 2: after the flotation column 4 is filled with fluidized water, coarse slime feed is injected through the feed pipe 1 and uniformly distributed in the flotation column 4 through the feed distributor 2.
Coarse coal slime particles sink along with ore pulp, meet with rising microbubbles in a countercurrent mineralization area, collide with particle bubbles, most hydrophobic coal particles are adhered to the surfaces of the bubbles to form particle bubble aggregates, a small amount of coal particles which are not adhered to the bubbles continue to sink to a scavenging area, collide with the bubbles again at the lower side of a flotation column to adhere to the bubbles again to form the particle bubble aggregates. Under the combined action of rising water flow and bubble buoyancy, the particle bubble aggregate rises to a foam layer and is discharged through the clean coal overflow groove 3, and finally the clean coal product is obtained.
Hydrophilic gangue particles in the feeding cannot adhere after collision with bubbles, and sink to a tailing pre-dewatering area, part of water is primarily removed in the area, and finally the gangue particles are discharged through a tailing discharging pipe 12 to form a tailing product.
When a multi-stage gas distribution unit exists in the flotation column 4, the steps include:
step 1: injecting fluidizing water containing foaming agent into the annular water tank 5 through the water pipe 6, and allowing the fluidizing water containing foaming agent to enter the strip-shaped air-water mixing chamber 13 through the annular water tank 5; while air is input to the respective stages of air distribution units (the first air distribution unit, the second air distribution unit 15, and the third air distribution unit 16 in the present embodiment) through the first air input pipe 8, the second air input pipe 18, and the third air input pipe 22.
The air in the first annular high-pressure air chamber 9 of the first air distribution unit enters the first strip-shaped high-pressure air chamber 14, forms a first-stage rising micro-bubble flow through the first air bubble generating plate 10 and enters the strip-shaped air-water mixing chamber 13 to be fully mixed with fluidization water, and then the fluidization water and a large number of micro-bubbles pass through the fluid distribution plate 7 to form a rising water flow with high micro-bubble content to uniformly enter the upper part of the flotation column 4.
In the second air distribution unit 15, air input by the second air input pipe 18 enters the second strip-shaped high-pressure air chamber 20 through the second annular high-pressure air chamber 17, and then is dispersed into uniform microbubbles through the second bubble generating plate 19, so that a second-stage rising microbubble flow is formed in the flotation column 4.
In the third air distribution unit 16, air input by the third air input pipe 22 enters the third strip-shaped high-pressure air chamber 24 through the third annular high-pressure air chamber 21, and then is dispersed into uniform microbubbles through the third bubble generating plate 23, so that a third-stage rising microbubble flow is formed in the flotation column 4.
Thus, a flotation flow field environment with small fluid disturbance and sufficient micro-bubble content is formed in the flotation column 4 by gradient air intake of the multistage air distribution unit.
Step 2: after the flotation column 4 is filled with fluidized water, coarse slime feed is injected through the feed pipe 1, and the coarse slime feed is uniformly distributed in the flotation column 4 through the feed distributor 2.
Coarse slime particles sink along with ore pulp under the action of gravity and inertia, the ore pulp meets with rising microbubble flow, collision occurs among particle bubbles, and hydrophobic coarse slime particles are adhered to the surfaces of the bubbles to form particle bubble aggregates; part of the coal particles which are not adhered to the bubbles continuously sink, collide with the bubbles at the lower side of the flotation column 4 and adhere to the bubbles, and form particle bubble aggregates; under the combined action of rising water flow and bubble buoyancy, the particle bubble aggregate rises and finally is discharged through the clean coal overflow groove 3 to become a clean coal product.
Gangue particles in the feeding cannot adhere after collision with bubbles due to the hydrophilic surface property of the gangue particles, sink to a tailing pre-dewatering area, and finally become a tailing product through a tailing discharging pipe 12.
The present invention is not limited to the above-mentioned embodiments, and any changes or substitutions that can be easily understood by those skilled in the art within the technical scope of the present invention are intended to be included in the scope of the present invention.
Claims (3)
1. The flotation device suitable for coarse slime separation is characterized by comprising a flotation column (4), a gas-water distribution unit, a water delivery pipe (6) and a first air input pipe (8), wherein the gas-water distribution unit is arranged at the lower part of the flotation column (4) and is concentrically arranged, the gas-water distribution unit comprises a first gas distribution unit, a second gas distribution unit (15), a third gas distribution unit (16) and a gas-water mixing distribution unit, the gas-water mixing distribution unit is arranged above the first gas distribution unit, the second gas distribution unit (15) is arranged above the gas-water mixing distribution unit, and the third gas distribution unit (6) is arranged above the second gas distribution unit (15); the air flow of the first air distribution unit, the second air distribution unit (15) and the third air distribution unit (16) is sequentially reduced;
the gas-water mixing and distributing unit comprises an annular water tank (5), a fluid distributing plate (7) and a strip-shaped gas-water mixing chamber (13), wherein two ends of the strip-shaped gas-water mixing chamber (13) are communicated with the annular water tank (5), and the fluid distributing plate (7) is arranged at the top of the strip-shaped gas-water mixing chamber (13);
a plurality of strip-shaped air-water mixing chambers (13) are arranged in the inner ring of the annular water tank (5), and the strip-shaped air-water mixing chambers (13) are arranged in parallel;
the first air distribution unit comprises a first annular high-pressure air chamber (9) and a first strip-shaped high-pressure air chamber (14), and two ends of the first strip-shaped high-pressure air chamber (14) are communicated with the first annular high-pressure air chamber (9);
the first strip-shaped high-pressure air chamber (14) is arranged in the inner ring of the first annular high-pressure air chamber (9) and is opposite to the strip-shaped air-water mixing chamber (13), and the upper end of the first strip-shaped high-pressure air chamber (14) is connected with the lower end of the strip-shaped air-water mixing chamber (13);
the gas-water distribution unit further comprises a first gas bubble generation plate (10), wherein the first gas bubble generation plate (10) is arranged at the joint of the strip-shaped gas-water mixing chamber (13) and the first strip-shaped high-pressure air chamber (14) and is used for separating the strip-shaped gas-water mixing chamber (13) and the first strip-shaped high-pressure air chamber (14);
the water delivery pipe (6) is communicated with the annular water tank (5), and the first air input pipe (8) is communicated with the first annular high-pressure air chamber (9);
the flotation column (4), the annular water tank (5) and the first annular high-pressure air chamber (9) are concentrically arranged.
2. Flotation device suitable for coarse slime separation according to claim 1, characterized in that the water pipe (6) and the first air input pipe (8) on the same side of the flotation column (4) are aligned up and down, the water pipe (6) is perpendicular to the first strip-shaped high-pressure air chamber (14), and the first air input pipe (8) is perpendicular to the strip-shaped air-water mixing chamber (13).
3. A flotation method suitable for coarse slime separation, characterized in that a flotation device suitable for coarse slime separation according to claim 1 or 2 is used, the steps comprising:
step 1: injecting fluidizing water containing foaming agent into the annular water tank (5) through the water pipe (6), inputting air into the first annular high-pressure air chamber (9) through the first air input pipe (8), dispersing the air into microbubbles through the first bubble generating plate (10) to form rising microbubble flow, entering the strip-shaped air-water mixing chamber (13) to be fully mixed with the fluidizing water, forming rising water flow with high microbubble content through the fluid distribution plate (7), and entering the flotation column (4);
step 2: after the flotation column (4) is filled with fluidized water, injecting coarse coal slime into the flotation column (4);
coarse slime particles in ore pulp sink along with the ore pulp, collide with rising bubbles in a countercurrent mineralization area, hydrophobic coal particles adhere to the bubbles to form particle bubble aggregates, coal particles which are not adhered to the bubbles continue to sink to a scavenging area, collide and adhere again with the bubbles at the lower side of a flotation column (4) to form particle bubble aggregates, and the particle bubble aggregates float upwards to form clean coal under the dual effects of bubble buoyancy and rising water flow;
hydrophilic gangue particles are collided with bubbles and then sink to a tailing pre-dewatering area formed by the fluid distribution plate (5) to form tailings.
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