WO2020025853A1 - Cellule de flottation - Google Patents

Cellule de flottation Download PDF

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Publication number
WO2020025853A1
WO2020025853A1 PCT/FI2018/050568 FI2018050568W WO2020025853A1 WO 2020025853 A1 WO2020025853 A1 WO 2020025853A1 FI 2018050568 W FI2018050568 W FI 2018050568W WO 2020025853 A1 WO2020025853 A1 WO 2020025853A1
Authority
WO
WIPO (PCT)
Prior art keywords
flotation
tank
slurry
flotation cell
flotation tank
Prior art date
Application number
PCT/FI2018/050568
Other languages
English (en)
Inventor
Peter Bourke
Steve Schmidt
Antti Rinne
Jere Tuominen
Valtteri VAARNA
Aleksi Peltola
Original Assignee
Outotec (Finland) Oy
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Outotec (Finland) Oy filed Critical Outotec (Finland) Oy
Priority to PE2021000149A priority Critical patent/PE20210791A1/es
Priority to PCT/FI2018/050568 priority patent/WO2020025853A1/fr
Priority to AU2018434575A priority patent/AU2018434575A1/en
Priority to MX2021001128A priority patent/MX2021001128A/es
Priority to EP18928263.5A priority patent/EP3829773A4/fr
Priority to AU2019100825A priority patent/AU2019100825A4/en
Priority to CL2019002141U priority patent/CL2019002141U1/es
Priority to PE2019001516U priority patent/PE20191428Z/es
Priority to CN201921240866.4U priority patent/CN210965531U/zh
Priority to CN201910708168.0A priority patent/CN110787916B/zh
Publication of WO2020025853A1 publication Critical patent/WO2020025853A1/fr
Priority to ZA2021/01401A priority patent/ZA202101401B/en

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Classifications

    • 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
    • B03D1/1462—Discharge mechanisms for the froth
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
    • B01F23/232—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles
    • B01F23/2323—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles by circulating the flow in guiding constructions or conduits
    • B01F23/23231—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles by circulating the flow in guiding constructions or conduits being at least partially immersed in the liquid, e.g. in a closed circuit
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/20—Jet mixers, i.e. mixers using high-speed fluid streams
    • B01F25/21—Jet mixers, i.e. mixers using high-speed fluid streams with submerged injectors, e.g. nozzles, for injecting high-pressure jets into a large volume or into mixing chambers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/20—Jet mixers, i.e. mixers using high-speed fluid streams
    • B01F25/25—Mixing by jets impinging against collision plates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/50—Mixing receptacles
    • B01F35/53—Mixing receptacles characterised by the configuration of the interior, e.g. baffles for facilitating the mixing of components
    • 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
    • B03D1/1406—Flotation machines with special arrangement of a plurality of flotation cells, e.g. positioning a flotation cell inside another
    • 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
    • B03D1/1475—Flotation tanks having means for discharging the pulp, e.g. as a bleed stream
    • 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
    • B03D1/1493—Flotation machines with means for establishing a specified flow pattern
    • 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
    • B03D1/242—Nozzles for injecting gas into the flotation tank
    • 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
    • B03D1/247—Mixing gas and slurry in a device separate from the flotation tank, i.e. reactor-separator type
    • 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

Definitions

  • the current disclosure relates to a flotation cell for separating valuable material containing particles from particles suspended in slurry and to a flotation line and its use.
  • the flotation cell according to the current disclosure is characterized by what is presented in claim 1.
  • a flotation cell for treating particles suspended in slurry and for separating the slurry into an underflow and an overflow.
  • the flotation cell comprises a flotation tank comprising a centre, a perimeter, a substantially horizontal, level bottom, and a side wall; a launder and a launder lip surrounding the perimeter of the tank; and a bottom structure arranged on the bottom and having a shape that allows particles suspended in slurry to be mixed in a mixing zone over the bottom structure, and to settle down in a settling zone surrounding the bottom structure.
  • the flotation cell is characterized in that the flotation tank further comprises blast tubes for introducing slurry infeed into the flotation tank.
  • a blast tube comprises an inlet nozzle for feeding slurry infeed into the blast tube; an inlet for pressurized gas, the slurry infeed subjected to the pressurized gas as it is discharged from the inlet nozzle; an elongated chamber arranged to receive under pressure the slurry infeed; and an outlet nozzle configured to restrict flow of slurry infeed from the outlet nozzle, and to maintain slurry infeed in the elongated chamber under pressure; and in that the blast tubes are disposed at a position relative to the bottom structure so as to induce mixing at the mixing zone.
  • a flotation line comprises a number of fluidly connected flotation cells, and it is characterized in that at least one of the flotation cells is a flotation cell according to the invention.
  • use of the flotation line according to the invention is intended for recovering particles comprising a valuable material suspended in slurry.
  • the particles may, for example, comprise mineral ore particles such as particles comprising a metal .
  • upgrading the concentrate is directed to an intermediate particle size range between 40 ym to 150 ym. Fine particles are thus particles with a diameter of 0 to 40 ym, and ultrafine particles can be identified as falling in the lower end of the fine particle size range. Coarse particles have a diameter greater than 150 ym. In froth flotation of coal, upgrading the concentrate is directed to an intermediate particle size range between 40 ym to 300 ym. Fine particles in coal treatment are particles with a diameter of 0 to 40 ym, and ultrafine particles those that fall into the lower end of the fine particle size range. Coarse coal particles have a diameter greater than 300 ym.
  • flotation gas is introduced into a flotation cell or tank via a mechanical agitator.
  • the thus generated flotation gas bubbles have a relatively large size range, typically from 0,8 to 2,0 mm, or even larger, and are not particularly suitable for collecting particles having a finer particle size.
  • Fine particle recovery may be improved by increasing the number of flotation cells within a flotation line, or by recirculating the once-floated material (overflow) or the tailings flow (underflow) back into the beginning of the flotation line, or to precedent flotation cells.
  • a cleaner flotation line may be used in order to improve recovery of fine particles.
  • a number of flotation arrangements employing fine flotation gas bubbles or even so-called microbubbles have been devised. Introduction of these smaller bubbles or microbubbles may be done prior to feeding the slurry into the flotation cell, i.e.
  • the ore particles are subjected to fine bubbles in a feed connection or the like to promote formation of ore particle-fine bubble agglomerates, which may then be floated in flotation cells such as flash flotation cells or column cells.
  • flotation cells such as flash flotation cells or column cells.
  • fine bubbles or microbubbles may be introduced directly into the flotation cell, for example by spargers utilising cavitation.
  • Column flotation cells act as three phase settlers where particles move downwards in a hindered settling environment counter-current to a flow of rising flotation gas bubbles generated by spargers located near the bottom of the cell. While column flotation cells may improve the recovery of finer particles, the particle residence time is dependent on settling velocity, which may impact on the flotation of large particles. In other words, while the aforementioned flotation solutions may have a beneficial effect for recovery of fine particles, the overall flotation performance (recovery of all valuable material, grade of recovered material) may be undermined by the negative effect on recovery of larger particles.
  • Such control of pressure is advantageous also in view of the pressure at which flotation gas bubbles are formed (effect on bubble size) , but also for the adjustment of relative pressure at which they are to be used in the flotation tank. In that way, the coalescence of bubbles may be minimized after their formation. This is especially advantageous, as the rate of entrapment of particles by flotation gas bubbles decreases as the bubble size increases (provided that the air to liquid ratio remains the same) .
  • the problems may be alleviated to some extent by minimizing the use of frothers in the flotation line, but if not enough frother is added into the flotation process, the froth formation in blast tubes according to state of the art may suffer, which leads to unstable process conditions and especially unstable downcomer operation and froth layer in a flotation cell, which in turn affects the recovery of desired particles negatively. Recovery of particles within the entire particle size distribution of a slurry is affected as bubble size increases with lower frother dosage, in particular that of coarse particles.
  • the amount of frother required to optimize the flotation process may be significantly reduced without significantly compromising bubble formation, bubble to particle engagement, stable froth layer formation or the recovery of desired material.
  • problems associated with recirculating process water from downstream circuit to front circuit can be alleviated.
  • a blast tube operating under pressure is completely independent of the flotation tank.
  • a better flotation gas flowrate may be reached, and finer bubbles created, and frother usage optimized, as the blast tube operation is not dependent of frother dosage.
  • flotation of fine and ultrafine particles comprising for example mineral ore or coal may be improved by reducing the size of the flotation gas bubbles introduced to slurry infeed in a blast tube, by increasing the flotation gas supply rate relative to the flow rate of particles suspended in the slurry, and by increasing the shear intensity or energy dissipation rate either in or adjacent to the blast tube.
  • ultra-fine bubbles may be created to ensure efficient entrapment of fine ore particles.
  • ultra-fine bubbles may have a bubble size distribution of 0,05 mm to 0,7 mm.
  • decreasing the mean flotation gas bubble size to a diameter of 0,3 to 0,4 mm means that the number of bubbles in 1 m 3 of slurry may be as high as 30 to 70 million, and the total mean surface area of the bubbles 15 to 20 m 2 .
  • recovery of coarser particles may be kept at an acceptable level by achieving a high flotation gas fraction in the slurry, and by the absence of high turbulence areas in the region below the forth layer.
  • the known benefits of mechanical flotation cells may be employed, even though there may not necessarily be any mechanical agitation present in the flotation cell.
  • the upwards motion of slurry or pulp within the flotation tank increases the probability of also coarser particles rise towards the froth layer with the flow of slurry.
  • the probability of collisions between flotation gas bubbles, as well as between gas bubbles and particles can be increased.
  • Having a number of blast tubes may ensure an improved distribution of flotation gas bubbles within a flotation tank, and the bubbles exiting the blast tubes are distributed evenly throughout the flotation tank, the distribution areas of individual blast tubes have the possibility of intersecting each other and converging, thus promoting an extensively even flotation gas bubble distribution into the flotation tank, which in turn may affect the recovery of especially smaller particles beneficially, and also contribute to the aforementioned even and thick froth layer.
  • the outlet nozzles of the blast tubes may be disposed at a suitable depth, i.e. disposing them at a specific vertical distance from the launder lip, the distribution of flotation gas bubbles may be optimized in an even and constant manner.
  • the residence time of bubbles within a mixing zone may be kept high enough by a suitable depth of the blast tube outlet nozzles, the bubbles may be able to contact and adhere to the fine particles in the slurry efficiently, thus improving the recovery of smaller particles, and also promoting froth depth, stability and evenness at the top of the flotation tank.
  • a mixing zone is meant herein a vertical part or region of the flotation tank in which active mixing of particles suspended in slurry with flotation gas bubbles takes place.
  • this mixing zone created into an entire vertical section of the flotation tank, separate and regional individual mixing subzones may be created at areas where slurry flows directed radially outwards by individual impingers meet and become intermingled. This may further promote contacts between flotation gas bubbles and particles, thereby increasing the recovery of valuable particles. Further, this additional mixing may eliminate the need for a mechanical mixer for suspending solids in the slurry.
  • flotation aims at recovering a concentrate of ore particles comprising a valuable mineral.
  • concentrate herein is meant the part of slurry recovered in overflow or underflow led out of a flotation cell.
  • valuable mineral is meant any mineral, metal or other material of commercial value.
  • Flotation involves phenomena related to the relative buoyancy of objects.
  • the term flotation includes all flotation techniques.
  • Flotation can be for example froth flotation, dissolved air flotation (DAF) or induced gas flotation.
  • DAF dissolved air flotation
  • Froth flotation is a process for separating hydrophobic materials from hydrophilic materials by adding gas, for example air or nitrogen or any other suitable medium, to the process.
  • Froth flotation could be made based on natural hydrophilic/hydrophobic difference or based on hydrophilic/hydrophobic differences made by addition of a surfactant or collector chemical.
  • Gas can be added to the feedstock subject of flotation (slurry or pulp) by a number of different ways.
  • a flotation cell meant for treating mineral ore particles suspended in slurry by flotation.
  • flotation line herein is meant a flotation arrangement where a number of flotation cells are arranged in fluid connection with each other so that the underflow of each preceding flotation cell is directed to the following or subsequent flotation cell as a infeed until the last flotation cell of the flotation line, from which the underflow is directed out of the line as tailings or reject flow.
  • Slurry is fed through a feed inlet to the first flotation cell of the flotation line for initiating the flotation process.
  • a flotation line may be a part of a larger flotation plant or arrangement containing one or more flotation lines. Therefore, a number of different pre-treatment and post-treatment devices or stages may be in operational connection with the components of the flotation arrangement, as is known to the person skilled in the art.
  • the flotation cells in a flotation line are fluidly connected to each other.
  • the fluid connection may be achieved by different lengths of conduits such as pipes or tubes, the length of the conduit depending on the overall physical construction of the flotation arrangement.
  • the flotation cells may be arranged in direct cell connection with each other.
  • direct cell connection herein is meant an arrangement, whereby the outer walls of any two subsequent flotation cells are connected to each other to allow an outlet of a first flotation cell to be connected to the inlet of the subsequent flotation cell without any separate conduit.
  • a direct contact reduces the need for piping between two adjacent flotation cells. Thus, it reduces the need for components during construction of the flotation line, speeding up the process. Further, it might reduce sanding and simplify maintenance of the flotation line.
  • the fluid connections between flotation cells may comprise various regulation mechanisms.
  • neighboredjacent or “adjoining” flotation cell herein is meant the flotation cell immediately following or preceding any one flotation cell, either downstream or upstream, or either in a rougher flotation line, in a scavenger flotation line, or the relationship between a flotation cell of a rougher flotation line and a flotation cell of a scavenger flotation line into which the underflow from the flotation cell of the rougher flotation line is directed .
  • a flotation cell is herein meant a tank or vessel in which a step of a flotation process is performed.
  • a flotation cell is typically cylindrical in shape, the shape defined by an outer wall or outer walls.
  • the flotation cells regularly have a circular cross-section.
  • the flotation cells may have a polygonal, such as rectangular, square, triangular, hexagonal or pentagonal, or otherwise radially symmetrical cross-section, as well.
  • the number of flotation cells may vary according to a specific flotation line and/or operation for treating a specific type and/or grade of ore, as is known to a person skilled in the art.
  • the flotation cell may be a froth flotation cell, such as a mechanically agitated cell, for example a TankCell, a column flotation cell, a Jameson cell, or a dual flotation cell.
  • a dual flotation cell the cell comprises at least two separate vessels, a first mechanically agitated pressure vessel with a mixer and a flotation gas input, and a second vessel with a tailings output and an overflow froth discharge, arranged to receive the agitated slurry from the first vessel.
  • the flotation cell may also be a fluidized bed flotation cell (such as a HydroFloatTM cell) , wherein air or other flotation gas bubbles which are dispersed by the fluidization system percolate through the hindered-setting zone and attach to the hydrophobic component altering its density and rendering it sufficiently buoyant to float and be recovered. In a fluidized bed flotation cell axial mixing is not needed.
  • the flotation cell may also be an overflow flotation cell operated with constant slurry overflow. In an overflow flotation cell, the slurry is treated by introducing flotation gas bubbles into the slurry and by creating a continuous upwards flow of slurry in the vertical direction of the first flotation cell.
  • At least part of the valuable metal containing ore particles are adhered to the gas bubbles and rise upwards by buoyancy, at least part of the valuable metal containing ore particles are adhered to the gas bubbles and rise upwards with the continuous upwards flow of slurry, and at least part of the valuable metal containing ore particles rise upwards with the continuous upwards flow of slurry.
  • the valuable metal containing ore particles are recovered by conducting the continuous upwards flow of slurry out of the at least one overflow flotation cell as slurry overflow. As the overflow cell is operated with virtually no froth depth or froth layer, effectively no froth zone is formed on the surface of the pulp at the top part of the flotation cell. The froth may be non-continuous over the cell. The outcome of this is that more valuable mineral containing ore particles may be entrained into the concentrate stream, and the overall recovery of valuable material may be increased .
  • All of the flotation cells of a flotation line according to the invention may be of a single type, that is, rougher flotation cells in the rougher part, scavenger flotation cells in the scavenger part, and scavenger cleaner flotation cells of the scavenger cleaner flotation line may be of one single flotation cell type so that the flotation arrangement comprises only one type of flotation cells as listed above.
  • a number of flotation cells may be of one type while other cells are of one or more type so that the flotation line comprises two or more types of flotation cells as listed above.
  • a froth crowder herein is meant a froth blocker, a froth baffle, or a crowding board, or a crowding board device, or any other such structure or side structure, for example a sidewall, inclined or vertical, having a crowding effect, i.e. a crowding sidewall, which can also be a crowding sidewall internal to the flotation tank, i.e. an internal perimeter crowder .
  • a froth crowder By utilising a froth crowder, it may be possible to direct so-called "brittle froth", i.e. a loosely textured froth layer comprising generally larger flotation gas bubbles agglomerated with the mineral ore particles intended for recovery, more efficiently and reliably towards the forth overflow lip and froth collection launder.
  • a brittle froth can be easily broken, as the gas bubble-ore particle agglomerates are less stable and have a reduced tenacity.
  • Such froth or forth layer cannot easily sustain the transportation of ore particles, and especially coarser particles, towards the froth overflow lip for collection into the launder, therefore resulting in particle drop-back to the pulp or slurry within the flotation cell or tank, and reduced recovery of the desired material.
  • Brittle froth is typically associated with low mineralization, i.e. gas bubble-ore particle agglomerates with limited amount of ore particles comprising a desired mineral that have been able to attach onto the gas bubbles during the flotation process within a flotation cell or tank.
  • the problem is especially pronounced in large-sized flotation cells or tanks with large volume and/or large diameter.
  • it may be possible to crowd and direct the froth towards the froth overflow lip, to reduce the froth transportation distance (thereby reducing the risk of drop-back) , and, at the same time, maintain or even reducing the overflow lip length.
  • the handling and directing of the froth layer in a froth flotation cell or tank may become more efficient and straightforward.
  • the area of froth on the surface of the slurry inside a flotation tank may be decreased in a robust and simple mechanical manner.
  • the overall overflow lip length in a froth flotation unit may be decreased. Robust in this instance is to be taken to mean both structural simplicity and durability.
  • the froth flotation unit as a whole may be a simpler construction, for example because there is no need to lead the collected froth and/or overflow out of the added crowder. In contrast, from an extra launder, the collected overflow would have to be led out, which would increase the constructional parts of the flotation unit.
  • the amount of desired material that can be trapped into the froth within the slurry may be very low.
  • the froth surface area should be decreased.
  • the crowder may be utilised to direct or guide the upwards-flowing slurry within the flotation tank closer to a froth overflow lip of a froth collection launder, thereby enabling or easing froth formation very close to the froth overflow lip, which may increase the collection of valuable ore particles.
  • the froth crowder may also influence the overall convergence of flotation gas bubbles and/or gas bubble-ore particle agglomerates into the froth layer. For example, if the gas bubbles and/or gas bubble-ore particle agglomerate flow becomes directed towards the centre of a flotation tank, a froth crowder may be utilised to increase the froth area at the perimeter of the tank, and/or closer to any desired froth overflow lip. In addition, it may be possible to reduce the open froth surface in relation to the lip length, thereby improving the efficiency of recovery in the froth flotation cell.
  • a blast tube By a blast tube is meant a dual high-shear device in which flotation gas is introduced into slurry infeed, thereby creating finer flotation gas bubbles that are able entrap also finer particles already during the bubble formation in the blast tube.
  • a blast tube in a flotation cell according to the invention operates under pressure, and not vacuum is needed .
  • overflow herein is meant the part of the slurry collected into the launder of the flotation cell and thus leaving the flotation cell.
  • Overflow may comprise froth, froth and slurry, or in certain cases, only or for the largest part slurry.
  • overflow may be an accept flow containing the valuable material particles collected from the slurry.
  • the overflow may be a reject flow. This is the case in when the flotation arrangement, plant and/or method is utilized in reverse flotation .
  • underflow herein is meant the fraction or part of the slurry which is not floated into the surface of the slurry in the flotation process.
  • the underflow may be a reject flow leaving a flotation cell via an outlet which typically is arranged in the lower part of the flotation cell.
  • the underflow may be an accept flow containing the valuable mineral particles. This is the case in when the flotation cell or flotation line is utilized in reverse flotation .
  • reverse flotation herein is meant an inverse flotation process typically utilized in the recovery of iron.
  • the flotation process is directed for collecting the non-valuable part of the slurry flow into the overflow.
  • the overflow in reverse flotation process for iron contains typically silicates, while the valuable iron-containing mineral particles are collected in the underflow.
  • Reverse flotation may also be used for industrial minerals, i.e. geological mineral mined for their commercial values which are not fuel, nor sources of metals, such as bentonite, silica, gypsum, and talc.
  • concentrate herein is meant the floated part or fraction of slurry of ore particles comprising a valuable mineral.
  • concentrate is the part of the slurry that is floated into the froth layer and thereby collected into the launders as overflow.
  • a first concentration concentrate may comprise ore particles comprising one valuable mineral, where as a second concentration concentrate may comprise ore particles comprising another valuable mineral.
  • the distinctive definitions first, second may refer to two concentrations concentrates of ore particles comprising the same valuable mineral but two distinctly different particle size distributions.
  • a rougher flotation rougher part of the flotation line, rougher stage and/or rougher cells herein is meant a flotation stage that produces a concentrate.
  • the objective is to remove a maximum amount of the valuable mineral at as coarse a particle size as practical.
  • the primary objective of a rougher stage is to recover as much of the valuable minerals as possible, with less emphasis on the quality of the concentrate produced .
  • the rougher concentrate is normally subjected to further stages of cleaner flotation in a rougher cleaner flotation line to reject more of the undesirable minerals that have also reported to the froth, in a process known as cleaning.
  • the product of cleaning is known as cleaner concentrate or final concentrate.
  • scavenger flotation a scavenger part of the flotation line, scavenger stage and/or a scavenger cell is meant a flotation stage wherein the objective is to recover any of the valuable mineral material that was not recovered during the initial rougher stage. This might be achieved by changing the flotation conditions to make them more rigorous than the initial roughing, or, in some embodiments of the invention, by the introduction of microbubble into the slurry.
  • the concentrate from a scavenger cell or stage could be returned to the rougher feed for re-floating or directed to a regrinding step and thereafter to a scavenger cleaner flotation line.
  • cleaner flotation a rougher/scavenger cleaner line, cleaner/cleaning stage and/or a cleaner cell is meant a flotation stage wherein the objective of cleaning is to produce as high a concentrate grade as possible.
  • pre-treatment and/or post-treatment and/or further processing is meant for example comminution, grinding, separation, screening, classification, fractioning, conditioning or cleaning, all of which are conventional processes as known to a person skilled in the art.
  • a further processing may include also at least one of the following: a further flotation cell, which may be a conventional cleaner flotation cell, a recovery cell, a rougher cell, or a scavenger cell.
  • slurry surface level herein is meant the height of the slurry surface within the flotation cell as measured from the bottom of the flotation cell to the launder lip of the flotation cell.
  • the height of the slurry is equal to the height of a launder lip of a flotation cell as measured from the bottom of the flotation cell to the launder lip of the flotation cell.
  • any two subsequent flotation cells may be arranged in a stepwise fashion in a flotation line so that the slurry surface level of such flotation cells is different (i.e. the slurry surface level of the first of such flotation cells is higher than the slurry surface level of the second of such flotation cells) .
  • step This difference in the slurry surface levels is defined herein as "step" between any two subsequent flotation cells.
  • the step or the difference in slurry surface levels is a difference allowing the flow of slurry be driven by gravity or gravitation force, by creating a hydraulic head be-tween the two subsequent flotation cells.
  • a flotation line herein is meant an assembly or arrangement comprising a number of flotation units or flotation cells in which a flotation stage is performed, and which are arranged in fluid connection with each other for allowing either gravity-driven or pumped slurry flow between flotation cells, to form a flotation line.
  • a flotation line a number of flotation cells are arranged in fluid connection with each other so that the underflow of each preceding flotation cell is directed to the following or subsequent flotation cell as a infeed until the last flotation cell of the flotation line, from which the underflow is directed out of the line as tailings or reject flow.
  • a flotation line may comprise only one flotation stage performed either in one flotation cell or for example in two or more parallel flotation cells.
  • Flotation line may be a part of a larger treatment plant containing one or more flotation lines, and a number of other process stages for the liberation, cleaning and other treatment of a desired material. Therefore, a number of different pre treatment and post-treatment devices or arrangements may be in operational connection with the components of the flotation line, as is known to the person skilled in the art.
  • ultra-fine bubbles herein is meant flotation gas bubbles falling into a size range of 0,05 mm to 0,7 mm, introduced into the slurry in a blast tube.
  • "normal" flotation gas bubbles utilized in froth flotation display a size range of approximately 0,8 to 2 mm. Larger flotation gas bubbles may have a tendency to coalesce into even larger bubbles during their residence in the mixing zone where collisions between particles and flotation gas bubbles, as well as only between flotation gas bubbles take place.
  • the outlet nozzle is configured to produce a supersonic shockwave into the slurry infeed, the supersonic shockwave inducing formation of flotation gas bubble - particle agglomerates .
  • a supersonic shockwave is created when the velocity of slurry infeed passing through the outlet nozzle exceeds the speed of sound, i.e. the flow of slurry infeed becomes choked when the ratio of the absolute pressure upstream the outlet nozzle to the absolute pressure downstream of the throttle of the outlet nozzle exceeds a critical value.
  • the pressure ratio is above the critical value, flow of slurry infeed downstream of the throttle part of the outlet nozzle becomes supersonic and a shock wave is formed. Small flotation gas bubbles in slurry infeed mixture are split into even smaller by being forced through the shock wave, and forced into contact with hydrophobic ore particles in slurry infeed, thus creating flotation gas bubble-ore particle agglomerates.
  • a height of the flotation tank measured as the distance from the bottom to the launder lip, is at the perimeter of the flotation tank at most 20 % lower than at the centre of the flotation tank.
  • the vertical cross-section of the bottom structure is a functional triangle comprising a first vertex pointing away from the bottom of the flotation tank, a second vertex and a third vertex; a first side between the first vertex and the second vertex; a second side between the first vertex and the third vertex; and a base between the second and third vertexes on the bottom of the flotation tank; and a central axis substantially concentric with the centre of the flotation tank.
  • the base angle between the first side and the base, or second side and the base in relation to the bottom of the flotation tank is 20 to 60°.
  • the included angle between the first side and the second side is 20 to 100°, preferably 20 to 80°.
  • the bottom structure comprises a base on the bottom of the flotation tank and defined by the base of the functional triangle, and a mantle defined at least by the first, second and third vertexes of the functional triangle .
  • the mantle is at least partly defined by the first and second sides of the functional triangle.
  • a height of the bottom structure is greater than 1/5 and less than 3/4 of a height of the flotation tank (10), measured as the distance from the bottom to the launder lip .
  • the flotation tank bottom nearer the tank perimeter has a zone of a sufficient depth that allows for unfloated, most likely valueless particles to settle down and descend to be efficiently removed from the flotation tank.
  • This settling zone is not affected by the slurry infeed flow from the blast tubes. Further, such relatively calm zone may inhibit formation of short circuiting of the slurry flows within the flotation tank, where the same slurry material keeps recirculating within the tank without being properly separated or settled. The above features may promote increased recovery of fine particles.
  • a height of the bottom structure is 1/3 to 3/4 of the distance of the central froth crowder from the bottom of the flotation tank.
  • the flotation tank further comprises an internal perimeter froth crowder, a lowest point of the internal perimeter froth crowder arranged at a distance from the bottom of the flotation tank.
  • the ratio of a height of the bottom structure to the distance of the lowest point of the internal perimeter forth crowder from the bottom of the flotation tank is 1,0 or lower .
  • a diameter of a base of the bottom structure is 1/4 to 3/4 of a diameter of the bottom of the flotation tank.
  • the surface area of a base of the bottom structure is 25 to 80 % of the surface area of the bottom of the flotation tank .
  • the ratio of height of the flotation tank, measured as the distance from the bottom to the launder lip, to diameter of the flotation tank, measured at a height of the outlet nozzle from the bottom is 0,5 to 1,5; i.e. the ratio of tank height to tank diameter is 0,5 to 1,5.
  • the volume of the flotation tank is at least 20 m 3 , preferably 20 to 1000 m 3 .
  • a flotation tank By arranging a flotation tank to have a sufficient volume the flotation process may be better controlled.
  • the ascent distance to the froth layer on the top part of the flotation tank does not become too large, which may help to ensure that the flotation gas bubble-ore particle agglomerates remain together until the froth layer and particle drop-back may be reduced. Further, a suitable bubble rise velocity may be reached to maintain a good concentrate quality.
  • Utilizing flotation cells with a sufficient volumetric size of increases the probability of collisions between gas bubbles created into the flotation cells for example by means of a rotor, and the particles comprising valuable mineral, thus improving the recovery rate for the valuable mineral, as well as the overall efficiency of the flotation arrangement.
  • the flotation cells downstream from the first flotation cell or cells may be smaller and therefore more efficient.
  • flotation processes of certain minerals it may be easy to float a significant part of the ore particles comprising valuable mineral with high grade. In that case it may be possible to have flotation cells of smaller volume downstream in the flotation line and still achieve high recovery rate.
  • the flotation cell comprises 2 to 40 blast tubes, preferably 4 to 24 blast tubes .
  • the number of blast tubes directly influences the amount of flotation gas that can be dispersed in the slurry.
  • dispersing an increasing amount of flotation gas would lead to increased flotation gas bubble size.
  • an air-to-bubble ratio of 0,50 to 0,60 is utilized.
  • Increasing the average bubble size will affect the bubble surface area flux (Sb) detrimentally, which means that recovery may be decreased.
  • Sb bubble surface area flux
  • a flotation cell according to the invention with pressurized blast tubes, significantly more flotation gas may be introduced into the process without increasing the bubble size or decreasing Sb, as the flotation gas bubbles created into the slurry infeed remain relatively small in comparison to the conventional processes.
  • the number of blast tubes as small as possible, costs of refitting existing flotation cells, or capital expenditure of setting up such flotation cells may be kept in check without causing any loss of flotation performance of the flotation cells.
  • the blast tubes are arranged concentric to the perimeter of the flotation tank at a distance from the centre of the flotation tank.
  • the blast tubes are arranged parallel to the sidewall of the flotation tank, at a distance from the side wall.
  • the exact number of blast tubes within a flotation cell may depend on the flotation tank size or volume, on the type of material to be collected and other process parameters. By arranging a sufficient number of blast tubes into a flotation cell, and by arranging them in a specific manner in relation to the flotation tank centre and perimeter and/or side wall, even distribution of ultra-fine bubbles may be ensured, as well as even mixing effect caused by the shear forces within tank secured.
  • An impinger deflects the flow of slurry infeed radially outwards to the flotation tank sidewall and upwards towards the flotation tank upper surface (i.e. to the froth layer) so the fine flotation gas bubble - ore particle agglomerates do not short circuit into the tailings. All of the slurry infeed from the blast tubes are forced to rise up towards the froth layer at the top region of the flotation tank before gravity has the chance to influence the particles not adhered to flotation gas bubbles, forcing them to descend and eventually report to tailings flow or underflow. Thereby the probability of valuable material containing particles short-circuiting may be diminished.
  • Slurry is highly agitated by the energy of the deflected flow, and forms mixing vortexes in which the size of the bubbles may be further reduced by the shear forces acting upon them.
  • the high-shear conditions favourably also induce high number of contacts between flotation gas bubbles and particles in the slurry within the flotation tank.
  • turbulence reduces and the flow becomes relatively uniform, which may contribute to the stability of the already formed bubbles, and flotation gas bubble- particle agglomerates, especially those comprising coarser particles.
  • the impinger may be configured to deflect and direct the flow of slurry infeed radially outwards and upwards of the impinger to create the earlier mentioned mixing zones within the flotation tank, and to promote the ascent of particles towards the froth layer. At the same time, it may be necessary to minimise the wear caused by high- velocity flows of slurry on the impinger.
  • the volume of the flotation tank taken by the bottom structure is 30 to 70 % of the volume of the flotation tank taken by the mixing zone.
  • the flotation cell further comprises a conditioning circuit.
  • the outlet is arranged at the sidewall of the flotation tank, at a distance from the bottom of the flotation tank.
  • the distance of the outlet from the bottom of the flotation tank is 0 to 50 % of the height of the flotation tank.
  • the conditioning circuit further comprises a pump arranged to intake the slurry fraction from the flotation tank and to forward slurry infeed from the pump tank.
  • the conditioning circuit further comprises a distribution unit arranged to distribute slurry infeed.
  • the recirculated fraction becomes thus obtained at a zone where the slurry by most parts comprises particles descending or settling towards the tank bottom. Due to the probabilistic nature of a flotation process, the particles may, however, still comprise valuable material. Especially at the settling zone closest to the flotation tank side wall, the slurry may comprise such valuable material comprising particles that have not been captured by the flotation gas bubbles and/or by the upwards directed flow of slurry near the impingers at the mixing zone. At this position, the slurry is also affected by the flow of slurry infeed from a single blast tube creating turbulence.
  • the flotation tank further comprises a tailings outlet for removing underflow.
  • the tailings outlet is arranged at the side wall of the flotation tank, at a distance from the bottom of the flotation tank.
  • the distance of the tailings outlet from the bottom of the flotation tank is 1 to 15 % of a height of the flotation tank, measured as the distance from the bottom to the launder lip.
  • the tailings outlet may be positioned at the bottom of the flotation tank, or at the side wall of the flotation tank, at the settling zone.
  • underflow may be removed at a zone where the slurry by most parts comprises particles descending or settling towards the tank bottom.
  • the settling zone is deeper near the side wall of the flotation tank.
  • mixing action and turbulence created by the blast tubes does not affect the settling particles, which, for the most part, do not comprise any valuable material, or comprise only a very small amount of valuable material.
  • the settling action is also most pronounced due to the lack of turbulence interfering the descent by gravity of the particles.
  • friction forces created by the tank side wall further decrease the turbulence and/or flows.
  • the volume of the flotation tank may be decreased at the centre of then tank, thereby decreasing the volume of the settling zone where the turbulence caused by slurry infeed from the blast tubes may influence the probability of particles settling towards the bottom of the tank, and allowing full use of the flotation tank volume.
  • the volume of the flotation tank may be decreased at the centre of the tank for example by arranging a bottom structure at the flotation tank bottom, at the centre of the tank.
  • the flotation cell according to the invention is preceded by a flotation cell.
  • the preceding flotation cell may be of any suitable type.
  • the flotation cell according to the invention is preceded by a mechanical flotation cell.
  • the flotation line comprises a rougher part with a flotation cell; a scavenger part with a flotation cell arranged to receive underflow from the rougher part; and a scavenger cleaner part with a flotation cell arranged to receive overflow from the scavenger part, wherein the last flotation cell of the scavenger part and/or the scavenger cleaner part is a flotation cell according to the invention.
  • the flotation cell according to the invention is preceded by a mechanical flotation cell.
  • An embodiment of the use of the flotation line according to the invention is particularly intended for recovering mineral ore particles comprising nonpolar minerals such as graphite, sulphur, molybdenite, coal, and talc.
  • Treatment of slurries for the recovery of such industrial minerals as bentonite, silica, gypsum, or talc, may be improved by using reverse flotation.
  • the goal of flotation may be, for example, the removal of dark particles into the overflow reject, and recovery of white particles into the underflow accept. In that kind of process, some of the lighter, finer white particles may end up into the overflow. Those particles could be efficiently recovered by the invention according to the present disclosure.
  • a further embodiment of the use of the flotation line is particularly intended in recovering particles comprising Pt .
  • An embodiment of the use of the flotation line is particularly intended in recovering particles comprising Cu from minerals having a Mohs hardness from 3 to 4.
  • a further embodiment of the use of the flotation line is particularly intended in recovering particles comprising Cu from low grade ore.
  • Valuable mineral may be for example Cu, or Zn, or Fe, or pyrite, or metal sulfide such as gold sulfide.
  • Mineral ore particles comprising other valuable mineral such as Pb, Pt, PGMs (platinum group metals Ru, Rh, Pd, Os, Ir, Pt) , oxide mineral, industrial minerals such as Li (i.e. spodumene) , petalite, and rare earth minerals may also be recovered, according to the different aspects of the present invention.
  • the copper amounts may be as low as 0,1 % by weight of the feed, i.e. infeed of slurry into the flotation line.
  • the flotation line according to the invention may be very practical for recovering copper, as copper is a so-called easily floatable mineral. In the liberation of ore particles comprising copper, it may be possible to get a relatively high grade from the first flotation cells of the flotation line. Recovery may be further increased by a flotation cell according to the invention .
  • the recovery of such low amounts of valuable mineral for example copper
  • the recovery of such low amounts of valuable mineral may be efficiently increased, and even poor deposits cost- effectively utilized.
  • the known rich deposits have increasingly already been used, there is a tangible need for processing the less favourable deposits as well, which previously may have been left unmined due to lack of suitable technology and processes for recovery of the valuable material in very low amounts in the ore.
  • Fig. 1 is a 3D projection of a flotation cell according to an embodiment of the invention
  • Fig. 2 depicts a flotation cell according to an embodiment of the invention, as seen from above,
  • Fig. 3 depicts a flotation cell according to an embodiment of the invention in side view
  • Fig. 4a is a vertical cross-section of the flotation cell of Fig. 3 along a section A-A,
  • Fig. 4b shows a vertical cross-section of a further embodiment of the flotation cell of Fig. 3 along the section A-A,
  • Fig. 5 is a schematic illustration of a flotation cell according to the invention, detailing the dimensions of the flotation cell,
  • Fig. 6a and 6b are schematic drawings of flotation lines according to embodiments of the invention.
  • Fig. 7 shows schematic vertical cross-sections of embodiments of flotation tanks according to the invention
  • Fig. 8 is a schematic presentation of forms of the bottom structure according to embodiments of the flotation cell.
  • FIG. 1-5 and 7-8 illustrate a flotation cell 1 in some detail.
  • the figures are not drawn to proportion, and many of the components of the flotation cell 1 are omitted for clarity.
  • Figures 6a and 6b illustrate in a schematic manner embodiments of the flotation line. The direction of flows of slurry is shown in the figures by arrows.
  • the flotation cell 1 is intended for treating mineral ore particles suspended in slurry and for separating the slurry into an underflow 400 and an overflow 500, the overflow 500 comprising a concentrate of a desired mineral .
  • the flotation cell 1 comprises a flotation tank 10 that has a centre 11, a perimeter 12, a bottom 13 and a side wall 14.
  • the flotation cell 1 further comprises a launder 2 and a launder lip 21 surrounding the perimeter 12 of the flotation tank 10.
  • launder 2 is a perimeter launder. It is to be understood that a launder 2 may comprise, alternatively or additionally, a central launder arranged at the centre 11 of the flotation tank 10, as is known in the technical field. A launder lip of a central launder may face towards the perimeter 12 of the flotation tank 10, or towards the centre 11 of the flotation tank 10, or both.
  • the overflow 500 is collected into the launder 2 or launders as it passes over a launder lip 21, from a froth layer formed in the upper part of the flotation tank 10.
  • the froth layer comprises an open froth surface A f at the top of the flotation tank 10.
  • Underflow 400 is removed from or led out of the flotation tank via a tailings outlet 140.
  • the tailings outlet 140 may be arranged at the side wall 14 of the flotation tank 10 (see Fig. 5) .
  • the tailings outlet 140 may be arranged at the side wall 14 of the flotation tank 10 at a distance L 6 from the bottom 13 of the flotation tank 10.
  • the distance is to be understood as the distance of the lowest point of the tailings outlet 140 or outlet opening in the side wall 14 of the flotation tank 10 from the tank bottom 13.
  • the distance Lg may be 1 to 15 % of the height H of the flotation tank 10.
  • the distance Lg may be 2 %, or 5 % or 7,5 %, or 12 % of the height H.
  • the tailings outlet 140 may be arranged at the bottom 13 of the flotation tank 10 (see Fig. 1) .
  • the tailing outlet 140 is arranged at a settling zone B, at the lower part of the flotation tank 10.
  • the tailings outlet 140 may be controlled by a dart valve, or by any other suitable manner known in the field, to control the flow rate of underflow from the flotation tank 10.
  • the tailings outlet 140 is ideally located at the lower part of the flotation tank 10, i.e. near or adjacent to the bottom 13 of the flotation tank, or even at the bottom 13 of the flotation tank 10. More specifically, underflow 400 or tailings are removed from the lower part of the flotation tank 10, and at or near the side wall 14 of the flotation tank 10.
  • the flotation tank 10 has a height H, measured as the distance from the bottom 13 of the flotation tank 10 to the launder lip 21. At the perimeter 12 of the flotation tank 10, the height H is substantially equal to or greater than the height H at the centre 11 of the flotation tank 10. In other words, the flotation tank 10 may have different vertical cross-sections (see Fig. 7) - for example, the side wall 14 of the flotation tank 10 may include at its lower part a section that is inclined towards the centre 11 of the flotation tank 10.
  • the flotation tank 10 has a diameter D, measured at a distance hi of an outlet nozzle 43 from the bottom 13 of the flotation tank 10.
  • the height H to diameter D ratio H/D of the flotation tank 10 is 0,5 to 1,5.
  • the flotation tank 10 may have a volume of at least 20 m 3 .
  • the flotation tank 10 may have a volume ranging from 20 to 1000 m 3 .
  • the volume of the flotation tank 10 may be 100 m 3 , or 200 m 3 , or 450 m 3 , or 630 m 3 .
  • the flotation tank 10 comprises blast tubes 4 for introducing slurry infeed 100 into the flotation tank 10.
  • a blast tube 4 comprises an inlet nozzle 41 for feeding slurry infeed 100 into the blast tube 4; an inlet 42 for pressurized air or other gas, so that the slurry infeed 100 may be subjected to pressurized air or other gas as it is discharged from the inlet nozzle 41; an elongated chamber 40 arranged to receive under pressure the slurry infeed 100; an outlet nozzle 43 configured to restrict flow of slurry infeed 100 from the outlet nozzle 43, and to maintain slurry infeed in the elongated chamber 40 under pressure.
  • Flotation gas is entrained through a turbulent mixing action brought about by the jet, and is dispersed into small bubbles in the slurry infeed 100 as it travels downwards through the elongated chamber 40 to an outlet nozzle 43 configured to restrict the flow of slurry infeed 100 from the outlet nozzle 43, and further configured to maintain slurry infeed 100 under pressure in the elongated chamber 40.
  • the outlet nozzle 43 may further be configured to produce a supersonic shockwave into the slurry infeed, the supersonic shockwave inducing formation of flotation gas bubble - particle agglomerates.
  • the supersonic shockwave may extend to the slurry adjacent or surrounding the outlet nozzle so that even outside the blast tube, the creation of small size flotation gas bubble - particle agglomerates is thus possible .
  • An outlet nozzle 43 may be disposed inside the flotation tank 10 at a desired depth.
  • An outlet nozzle 43 may be positioned at a vertical distance L 5 from the launder lip 21, the distance L 5 being at least 1,5 m.
  • the length of the portion of a blast tube 4 disposed inside the flotation tank 10 below the launder lip 21 level is at least 1,5 m.
  • the distance L 5 is at least 1,7 m
  • the distance hi of the outlet nozzle 43 from the bottom 13 of the flotation tank 10 is at least 0,4 m.
  • the distance L 5 may be 1,55 m, or 1,75 m, or 1,8 m, or 2,2 m, or 2,45m, or 5,25 m; and the distance hi, irrespective of the distance L 5 , may be 0,45 m, 0,55 m, 0,68 m, 0,9 m, or 1,2 m.
  • the ratio of the distance L 5 to the height H of the flotation tank 10 may be 0,9 or lower.
  • the depth at which the blast tubes 4 are disposed inside the flotation tank 10 may depend on a number of factors, for example on the characteristics of the slurry and/or valuable mineral to be treated in the flotation cell 1, or on the configuration of a flotation line in which the flotation cell 1 is arranged.
  • hi/H may be 0,1 to 0,75.
  • a diameter of an outlet nozzle 43 may be 10 to 30 % of the diameter of an elongated chamber 40 of a blast tube 4.
  • the diameter of an outlet nozzle 43 may be 40 to 100 mm.
  • the diameter of an outlet nozzle 43 may be 55 mm, or 62 mm, or 70 mm.
  • the velocity of the slurry infeed may be maintained at a level favourable for the creation of small size flotation gas bubbles, and for the probability of these bubbles to contact the ore particles in the slurry.
  • a slurry velocity of 10 m/s or higher needs to be maintained.
  • a blast tube 4 may further comprise an impinger
  • a distance L 3 from a bottom 440 of the impinger 44 to the outlet nozzle 43 may be 2 to 20 times the diameter of the outlet nozzle 43.
  • the distance L 3 may be 5 times, 7 times, or 12 times, or 15 times the diameter of the outlet nozzle 43.
  • the ratio of the distance L 3 to the distance hi of an outlet nozzle 43 from the bottom 13 of the flotation tank 10, Ls/hi, may be lower than 1,0.
  • a distance h 3 of a bottom 440 of the impinger 44 from the bottom 13 of the flotation tank 10 may be at least 0,3 m.
  • the distance h 3 may be 0,4 m, or 0,55 m, or 0,75 m, or 1,0 m.
  • the impinger 44 may comprise an impingement surface intended for contacting the flow of slurry infeed 100 exiting the outlet nozzle 43.
  • the impingement surface may be made of wear-resistant material to reduce the need for replacements or maintenance.
  • the slurry which in essence is a three-phase gas-liquid-solids mixture, rising out of the impinger 44 enters the upper part of the flotation tank 10, and the flotation gas bubbles rise upwards and separate from the liquid to form a froth layer.
  • the froth rises upwards and discharges over the launder lip 21 into the launder 2 and out of the flotation cell 1 as overflow 500.
  • the tailings or underflow 400 from which the desired material has substantially been removed, pass out from the flotation tank 10 through an outlet arranged at or near the bottom 13 of the flotation tank 10.
  • Some of the coarse hydrophobic particles that are carried into the froth may subsequently disengage from flotation gas bubbles and drop back into the flotation tank 10, as a result of bubble coalescence in the froth. However, the majority of such particles fall back into the flotation tank 10 in such a way and position that they may be captured by bubbles newly entering the flotation tank 10 from the blast tubes 4, and carried once more into the froth layer.
  • blast tubes 4 There may be 2-40 blast tubes 4, or 4-24 blast tubes 4 arranged in a flotation cell 1. In an embodiment, there are 16 blast tubes 4. In another embodiment, there are 24 blast tubes 4. In yet another embodiment, there are 8 blast tubes 4. The exact number of blast tubes 4 may be chosen according to the specific operation, for example the type of slurry being treated within the flotation cell 1, the volumetric feed flowrate to the flotation cell 1, the mass throughput feed to the flotation cell 1, or the volume or dimensions of the flotation tank 10. In order to properly disperse flotation gas within the flotation tank 10, 4 to 6 blast tubes 4 may be employed.
  • the blast tubes 4 may be arranged concentric to the perimeter 12 of the flotation tank 10 at a distance from the centre 11 of the flotation tank 10. This may be the case when the flotation tank 10 is circular in cross-section.
  • the blast tubes 4 may be further arranged so that each blast tube 4 is located at a distance Li of an outlet nozzle 43 from the centre 11 of the flotation tank 10, the distance being preferably equal for each blast tube 4.
  • the distance Li may be 10 to 40 % of the diameter D of the flotation tank 10.
  • the distance LI may be 12,5 %, or 15 %, or 25 % or 32,5% of the diameter D of the flotation tank 10.
  • the blast tubes 4 may be arranged parallel to the side wall 14 of the flotation tank 10, at a distance from the side wall 14. This may be the case when the flotation tank 10 is rectangular in cross-section.
  • a distance L2 of the outlet nozzle 43 of a blast tube 4 from the side wall 14 of the flotation tank 10 may be 10 to 40 % of the diameter D of the flotation tank 10. In an embodiment, the distance L2 is 25 % of the diameter D of the flotation tank 10. According to different embodiments of the flotation cell 10, the distance L2 may be 12,5 %, or 15 %, or 27 % or 32,5% of the diameter D of the flotation tank 10.
  • the parallel arranged blast tubes 4 may be further arranged at a straight line within the flotation tank 10.
  • the blast tubes 4 may be arranged at equal distance from each other so that a distance between any two adjacent outlet nozzle 43 is the same.
  • the flotation tank 10 comprises a bottom structure 7 (see esp. Figs. 2, 4a, 4b, 5 and 8), arranged on the bottom (13), and having a shape that allows particles suspended in slurry to be mixed in a mixing zone A created by the flow of slurry infeed 100 from the outlet nozzles 43 of the blast tubes 4 over the bottom structure 7, and to settle down in a settling zone B surrounding the bottom structure 7.
  • the shape of the bottom structure 7 may be defined as follows (see Fig. 8) : the vertical cross- section of the bottom structure may be understood to display a form of a functional triangle 700 that comprises a first (top) vertex 71, pointing away from the bottom 13 of the flotation tank 10; a second vertex 71a; and a third vertex 71b, the two latter disposed at the bottom 13 of the flotation tank 10.
  • a first side a is formed between the first vertex 71 and the second vertex 71a.
  • a second side b is formed between the first vertex 71 and the third vertex 71b.
  • a base c is formed between the second vertex 71a and the third vertex 71b, the base c being thus parallel to and on the bottom 13 of the flotation tank 10.
  • a central axis 70 of the functional triangle 700 is substantially concentric with the centre 11 of the flotation tank 10. "Substantially” in this context is to be understood so that during manufacturing and/or installation of the bottom structure 7, it is possible that slight deviations from the centre 11 of the flotation tank 10 may naturally occur. The intention is, nevertheless, that the two axes, central axis 70 of the functional triangle (which is also the central axis of the bottom structure 7) and the centre of the flotation tank 10 are coaxial .
  • a base angle between the first side a and the base c (and/or between the second side b and the base c) , in relation to the bottom 13 of the flotation tank 10 is 20 to 60°.
  • the angle may be 22°, or 27,5° or 35°, or 45°, or 53,75°.
  • an included angle b between the first side a and the second side b is 20 to 100°.
  • the included angle b is 20 to 80°.
  • the included angle b may be 22°, or 33,5°, or 45°, or 57,75°, or 64°, or 85,5°.
  • the functional triangle may therefore be an isosceles triangle or an equilateral triangle.
  • the functional triangle is in essence a form which may be identified though the abovementioned features, regardless of the actual form of the bottom structure 7, which may be, depending on the cross- section and other structural details of the flotation tank 10, for example a cone, a truncated cone, a pyramid, or a truncated pyramid.
  • a cone or a truncated cone may be suitable from for a flotation tank with a circular cross-section.
  • a pyramid or a truncated pyramid may be a suitable form for a flotation tank with a rectangular cross-section.
  • the bottom structure 7 comprises a base 73, corresponding to the base c of the functional triangle 700 (i.e. the base c of the functional triangle 700 defines the base 73 of the bottom structure 7), and arranged on the bottom 13 of the flotation tank 10. Further, the bottom structure comprises a mantle 72.
  • the mantle 72 is defined at least by the first vertex 71, the second vertex 71a and the third vertex 71b of the functional triangle 700. Therefore, irrespective of the actual form of the bottom structure 7, the functional triangle 700 defines the extreme physical dimensions of the bottom structure 7. For example, in case the bottom structure 7 has an irregular form yet being rotationally symmetrical, it would fit into the functional triangle 700 in its entirety (see the last image of Fig. 8) .
  • the bottom structure 7 has a height h 4 , measured from the topmost part of the bottom structure 7 to the bottom 13 of the flotation tank 10.
  • the topmost part is also the first vertex 71 of the functional triangle 700.
  • the height h 4 is measured from the level top of the truncated form (see middle image of Fig. 8) to the bottom 13 of the flotation tank 10.
  • the height h 4 is greater than 1/5 and less than 3/4 of the height H of the flotation tank 10.
  • the diameter d3 of the base 73 of the bottom structure 7 may be 1/4 to 3/4 of a diameter d 4 of the bottom 13 of the flotation tank 10.
  • the diameters are measured as the maximal diagonals of the respective parts (base 73 and bottom 13) .
  • the surface area of a base 73 of the bottom structure 7 is less than 80 % of the surface area of the bottom 13 of the flotation tank 10.
  • the surface area of the base 73 may be 25 to 80 % of the surface area of the bottom 13 of the flotation tank 10.
  • volume of the flotation tank 10 taken by the bottom structure 7 may be 30 to 70 % of the volume of the flotation tank 10 taken by the mixing zone A.
  • the bottom structure 7 may additionally comprise any suitable support structures and/or connecting structures for installing the bottom structure 7 into the flotation tank 10, on the bottom 13 of the flotation tank 10.
  • the bottom structure 7 may be made of any suitable material such as metal, for example stainless steel.
  • the flotation tank 10 may further comprise a froth crowder 6 shaped to direct froth in the open froth surface A f towards the launder lip 21, as shown in Figs. 4b and 5.
  • the forth crowder 6 may be a central froth crowder 61, and/or an internal perimeter froth crowder arranged within the flotation tank 10 at a desired depth, at the sidewall of the flotation tank 10.
  • a central froth crowder 61 is arranged concentric to the centre 11 of the flotation tank 10.
  • the central froth crowder 61 may have a shape of a cone or a truncated cone.
  • the central froth crowder 61 may have a shape of a pyramid or a truncated pyramid.
  • a vertical cross-section of a central froth crowder 61 may be an inverted triangle with a vertex pointing towards the bottom 13 of the flotation tank.
  • the vertex is only functional, i.e.
  • the central froth crowder 61 is arranged to block 25 to 40 % of the open froth surface A f .
  • the flotation tank may comprise an internal perimeter crowder 62, arranged in the side wall 14 of the flotation tank 10 so that a lowest point 620 of the internal perimeter crowder is located at a distance h 2 from the bottom 13 of the flotation tank 10.
  • the distance h 2 may be 1/2 to 2/3 of the height H of the flotation tank 10.
  • the internal perimeter crowder 62 may be arranged to block 1/5 to 1 ⁇ 4 of a pulp area A p , which is measured at a distance hi of an outlet nozzle 43 of a blast tube 4 from the bottom 13 of the flotation tank 10, at a mixing area A.
  • the mixing area A i.e. the part or zone of the flotation tank in vertical direction where the slurry is agitated or otherwise induced to mix the ore particles suspended in the slurry with the flotation gas bubbles, is formed roughly at a vertical section of the flotation tank 10 around the lower parts of the blast tubes 4 and the impingement bowls 44 (see Fig. 5) .
  • the slurry infeed 100 comprises 100 % of fresh slurry 200, for example from a previous flotation cell (that is, underflow 400 from a previous flotation cell), or from a previous process step.
  • the slurry fraction 300 may be recirculated to all of the blast tubes 4 of the flotation tank 10, or, alternatively, to some of the blast tubes 4, while other blast tubes 4 receive fresh slurry 200, comprising either the underflow 400 of a previous flotation cell, or a slurry flow from some preceding process step, depending on the location of the flotation cell 1 within a flotation line 8.
  • the outlet 31 may be arranged at a distance L 4 from the bottom 13 of the flotation tank 10. The distance is to be understood as the distance of the lowest point of the outlet or outlet opening in the side wall 14 of the flotation tank 10 from the tank bottom 13.
  • the distance L 4 is 0 to 50 % of the height H of the flotation tank 10.
  • the outlet 31 may advantageously be positioned at a settling zone where the particles suspended in slurry and not captured by the flotation gas bubbles and/or the upwards flow of slurry descend towards the bottom 13 of the flotation tank 10.
  • the outlet 31 is arranged at the lower part of the flotation tank 10.
  • the distance L 4 may be 2 %, or 8 %, or 12,5 %, or 17, or 25 % of the height H of the flotation tank 10.
  • the outlet 31 is ideally located at the lower part of the flotation tank 10, i.e. near or adjacent to the bottom 13 of the flotation tank. More specifically, slurry fraction 300 is removed from the lower part of the flotation tank 10.
  • the flotation cell 1 may also comprise a conditioning circuit 3.
  • the conditioning circuit 3 may comprise a pump tank 30, or other such additional vessel, in fluid communication with the flotation tank 10.
  • the fresh slurry 200 may be for example underflow 400 from a preceding flotation cell, or in case the flotation cell 1 is the first flotation cell of a flotation line, an infeed of slurry coming from a grinding unit/step or a classification unit/step. It is also possible that slurry fraction 300 and fresh slurry 200 are distributed into the blast tubes 4 without being first combined in a pump tank 30.
  • the combined slurry may be recirculated to all of the blast tubes 4 of the flotation tank 10, or, alternatively, to some of the blast tubes 4, while other blast tubes 4 receive fresh slurry 200, comprising either the underflow 400 of a previous flotation cell, or a slurry flow from some preceding process step, depending on the location of the flotation cell 1 within a flotation line 8.
  • the outlet 31 may be arranged at the side wall 14 of the flotation tank 10, at a distance L 4 from the bottom 13 of the flotation tank 10.
  • the distance L 4 may be 0 to 50 % of the height H of the flotation tank 10.
  • the distance L 4 may be 2 %, or 8 %, or 12,5 %, or 20 %, or 33 % of the height H of the flotation tank 10.
  • the conditioning circuit may comprise a pump 32 arranged to intake the slurry fraction 300 from the flotation tank 10, and to forward slurry infeed 100 from the pump tank 30 to the blast tubes 4.
  • the slurry fraction 300 may comprise low settling velocity particles such as fine, slow-floating particles.
  • the slurry fraction may be taken from or near the bottom of the flotation tank 10.
  • the conditioning circuit 3 may further comprise a distribution unit (not shown in the figures), arranged to distribute slurry infeed 100 into the blast tubes 4.
  • the pump 32 may also be used to forward the slurry infeed 100 into the blast tubes 4. In order to distribute the slurry infeed 100 evenly into the blast tubes 4, a distribution unit may be utilized.
  • the distribution unit may, for example, comprise a feed pipe inside the flotation tank 10, configured to distribute slurry fraction 300 directly into the blast tubes 4.
  • the distribution unit may comprise conduits arranged outside the flotation tank 10, leading to a separate feed distributor configured to distribute slurry fraction 300, or a combination of slurry fraction 300 and fresh slurry 200 into the blast tubes 4.
  • the flotation line 8 it comprises a rougher part 81 with a flotation cell la; a scavenger part 82 with a flotation cell la arranged to receive underflow 400 for the rougher part 81; and a scavenger cleaner part 820 with a flotation cell la arranged to receive overflow 500 from the scavenger part 82 (see Fig. 6b) .
  • the last flotation cell 1 of the scavenger part 82, and alternatively or additionally, the last flotation cell 1 of the scavenger cleaner part 820 is a flotation cell 1 according to the invention, with blast tubes 4.
  • the flotation cell 1 according to the invention, with blast tubes 4 may be preceded by a mechanical flotation cell lb.
  • the flotation line 8 may be preceded by other processes such as grinding, classification, screening, heavy-medium process, coarse particle recovery process, spirals, and other separation processes; and other flotation processes.
  • a number of processes may follow the flotation line 8, such as regrinding, cleaner or other flotation processes, centrifuging, filtering, screening or dewatering.
  • the flotation line 8 may be used in recovering particles comprising a valuable material suspended in slurry.
  • the use may be directed to recovering particles comprising nonpolar minerals such as graphite, sulphur, molybdenite, coal, talc .
  • the use may be directed to recovering particles comprising polar minerals .
  • the use is directed to recovering particles from minerals having a Mohs hardness of 2 to 3, such as galena, sulfide minerals, PGMs, REO minerals.
  • the use is specifically directed to recovering particles comprising platinum.
  • the use is directed to recovering particles comprising copper from mineral particles having a Mohs hardness of 3 to 4. In a yet further embodiment, the use is specifically directed to recovering particles comprising copper from low grade ore .
  • a flotation cell to which the disclosure is related may comprise at least one of the embodiments described hereinbefore. It is obvious to a person skilled in the art that with the advancement of technology, the basic idea of the invention may be implemented in various ways. The invention and its embodiments are thus not limited to the examples described above; instead they may vary within the scope of the claims.

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  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Biotechnology (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Physical Water Treatments (AREA)
  • Paper (AREA)
  • Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
  • Disintegrating Or Milling (AREA)

Abstract

L'invention concerne une cellule de flottation (1) permettant de traiter des particules en suspension dans une boue et de séparer la boue en une sousverse (400) et en une surverse (500). La cellule de flottation comprend un réservoir de flottation (10) ayant un centre (11), un périmètre (12), un fond de niveau sensiblement horizontal (13) et une paroi latérale (14) ; une rigole (2) et un rebord de rigole (21) entourant le périmètre (12) du réservoir (11) ; et une structure inférieure (7), disposée sur le fond (13) et dont la forme permet le mélange de particules en suspension dans une boue dans une zone de mélange (A) de la structure inférieure et leur décantation dans une zone de décantation (B) entourant la structure inférieure. Le réservoir de flottation comprend en outre des tubes d'air (4) permettant d'introduire une alimentation de boue (100) dans le réservoir. En outre, l'invention concerne une ligne de flottation et l'utilisation de la ligne de flottation.
PCT/FI2018/050568 2018-08-01 2018-08-01 Cellule de flottation WO2020025853A1 (fr)

Priority Applications (11)

Application Number Priority Date Filing Date Title
PE2021000149A PE20210791A1 (es) 2018-08-01 2018-08-01 Celda de flotacion
PCT/FI2018/050568 WO2020025853A1 (fr) 2018-08-01 2018-08-01 Cellule de flottation
AU2018434575A AU2018434575A1 (en) 2018-08-01 2018-08-01 Flotation cell
MX2021001128A MX2021001128A (es) 2018-08-01 2018-08-01 Celda de flotacion.
EP18928263.5A EP3829773A4 (fr) 2018-08-01 2018-08-01 Cellule de flottation
AU2019100825A AU2019100825A4 (en) 2018-08-01 2019-07-29 Flotation cell
CL2019002141U CL2019002141U1 (es) 2018-08-01 2019-07-30 Celda de flotacion
PE2019001516U PE20191428Z (es) 2018-08-01 2019-07-31 Celda de flotacion
CN201921240866.4U CN210965531U (zh) 2018-08-01 2019-08-01 浮选池和浮选线
CN201910708168.0A CN110787916B (zh) 2018-08-01 2019-08-01 浮选池
ZA2021/01401A ZA202101401B (en) 2018-08-01 2021-03-01 Flotation cell

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/FI2018/050568 WO2020025853A1 (fr) 2018-08-01 2018-08-01 Cellule de flottation

Publications (1)

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WO2020025853A1 true WO2020025853A1 (fr) 2020-02-06

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PCT/FI2018/050568 WO2020025853A1 (fr) 2018-08-01 2018-08-01 Cellule de flottation

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EP (1) EP3829773A4 (fr)
CN (2) CN210965531U (fr)
AU (2) AU2018434575A1 (fr)
CL (1) CL2019002141U1 (fr)
MX (1) MX2021001128A (fr)
PE (2) PE20210791A1 (fr)
WO (1) WO2020025853A1 (fr)
ZA (1) ZA202101401B (fr)

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CN118439684A (zh) * 2024-07-04 2024-08-06 临沂大学 一种水体去除微塑料装置

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PE20210791A1 (es) * 2018-08-01 2021-04-22 Metso Outotec Finland Oy Celda de flotacion
CN112604819A (zh) * 2020-11-27 2021-04-06 郴州天朗金石矿山设备有限公司 尾矿和低度矿再选高效节能装置设备

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ZA979702B (en) * 1996-11-08 1998-05-21 Outokumpu Technology Outokumpu Method and apparatus for producing a finely divideMethod and apparatus for producing a finely divided metal precipitate in a reactor. d metal precipitate in a reactor.
WO2000015343A1 (fr) * 1998-09-11 2000-03-23 Graeme John Jameson Appareil et procede de recyclage interne pour cellules de colonnes de flotation
WO2006081611A1 (fr) * 2005-02-01 2006-08-10 The University Of Newcastle Research Associates Limited Procede et appareil pour la mise en contact de bulles et de particules dans un systeme de separation par flottation
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PE20191428Z (es) 2019-10-10
EP3829773A1 (fr) 2021-06-09
ZA202101401B (en) 2022-07-27
CN210965531U (zh) 2020-07-10
CN110787916A (zh) 2020-02-14
AU2018434575A1 (en) 2021-03-18
CL2019002141U1 (es) 2019-10-18
EP3829773A4 (fr) 2022-04-13
CN110787916B (zh) 2022-08-23
AU2019100825A4 (en) 2019-08-29
MX2021001128A (es) 2021-04-29
PE20210791A1 (es) 2021-04-22

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