US3730341A - Flotation of coarse particles - Google Patents

Flotation of coarse particles Download PDF

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Publication number
US3730341A
US3730341A US00087611A US3730341DA US3730341A US 3730341 A US3730341 A US 3730341A US 00087611 A US00087611 A US 00087611A US 3730341D A US3730341D A US 3730341DA US 3730341 A US3730341 A US 3730341A
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United States
Prior art keywords
cell
pulp
carrier fluid
flotation
particles
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Expired - Lifetime
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US00087611A
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English (en)
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M Mames
R Berthon
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ALSACE MINES POTASSE
MINES DE POTASSE D ALSACE FR
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ALSACE MINES POTASSE
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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
    • B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
    • B03B5/00—Washing granular, powdered or lumpy materials; Wet separating
    • B03B5/62—Washing granular, powdered or lumpy materials; Wet separating by hydraulic classifiers, e.g. of launder, tank, spiral or helical chute concentrator type
    • B03B5/623—Upward current classifiers
    • 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
    • B03D1/1412—Flotation machines with baffles, e.g. at the wall for redirecting settling solids
    • 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

Definitions

  • ABSTRACT Continuation of Ser. NO. 640,670, Ma 23, 1967, R of particles of i 'f i abandoned. vlnite ore, by passing concentrated condltioned pulp (about 60-7O percent sol1ds)to top of cell JUSt below overflow level, and assing a mixture of air and liquid [30] Foreign Apphcatlon Pmmty p into bottom of celi to float coarse particles, there May 24, 1966 France ..66/62664 ing minimal turbulence but sufficient air bubbles for I I efficient flotation. Suitable apparatus is also provided [52] US.
  • This invention relates to the selective flotation of coarsely ground ores, particularly ores having a particle size larger than about 28 mesh (Tyler sieve).
  • Froth flotation a conventional technique for the separation of solids, is generally performed in the fol- 1O lowing manner.
  • the ore is first comminuted to sufficiently liberate the desired components; and this step often also separates out substances normally deleterious to flotation, such as finely divided insoluble claylike impurities.
  • the thus prepared ore is then suspended in either water or an aqueous solution saturated with respect to the soluble constituents of the ore, thereby forming a pulp.
  • the latter is conditioned by the successive or simultaneous addition of reagents comprising: collectors which selectively film particles enriched in certain components of the ore; depressants which'prevent or considerably reduce the detrimental effects of various factors, particularly those effects arising from clay-like impurities; and frothing agents which facilitate the dispersion of the air bubbles and the formation of froths which elevate particles selectively filmed by the collector.
  • reagents comprising: collectors which selectively film particles enriched in certain components of the ore; depressants which'prevent or considerably reduce the detrimental effects of various factors, particularly those effects arising from clay-like impurities; and frothing agents which facilitate the dispersion of the air bubbles and the formation of froths which elevate particles selectively filmed by the collector.
  • the flotation is performed with a pulp which flows in a substantially horizontal direction in a plurality of series-connected cells.
  • the conditioned pulp is fed continuously into the first cell and the non-floated particles are continuously withdrawn from the last cell of the series.
  • Each cell has the shape of a tank open at the top and is provided in its center with a device'which functions as an agitator and as an air injector. This device provides thorough contact between the air bubbles and the ore particles and, in addition, promotes the circulation of the pulp from one cell to the next.
  • the ore ordinarily treated in these cells is usually ground to a particle size lower than 28-20 mesh.
  • agitation is caused by introducing the mixture of air and pulp by various means such as: suction of air by the pulp in an injector working as a water aspirator pump; aeration under pressure wherein coarsely ground ore, i.e., a particle size of larger than about 28 mesh.
  • suction of air by the pulp in an injector working as a water aspirator pump aeration under pressure wherein coarsely ground ore, i.e., a particle size of larger than about 28 mesh.
  • a principal object of this invention is to provide an improved system for the flotation of coarse particles.
  • the conditioned pulp is fed to the upper portion of a cell and is allowed to flow by gravity countercurrently to an ascending stream of carrier fluid introduced at the lower portion of the cell, the floated particles suspended in the carrier fluid being collected at the overflow level and the non-floated product being withdrawn at the bottom of the cell.
  • the carrier fluid employed in this invention is introduced at least partly as a quasi-homogeneous dispersion of very fine air bubbles in a liquid.
  • this can be described as a discontinuous air phase surrounded by a continuous liquid phase.
  • It can be prepared, for example, by means of a pump, a device similar to a water aspirator pump or, still better, by a mechanical emulsifier such as those used in chemical industry to beat together two fluids in order to produce a state of extremely fine division.
  • the carrier fluid will be called hereunder an emulsion, of air and liquid, it being understood that there is meant a quasi-homogeneous dispersion of air bubbles in a liquid, the physical aspect of which is analogous to that of an emulsion of two liquids.
  • the ideal requirements for the flotation of coarse particles are substantially met. There is little agitation of the pulp flowing slowly downwards by gravity,- being decelerated by the rising stream of carrier fluid. At the same time, aeration is adjustable over a wide range and can be made as strong as desired. Each individual particle of ore can thus move upwards carried by as many air bubbles as necessary in this type of flotation.
  • this process in its more favorable aspect, is not a conventional froth flotation because there is no stable formation of a mineralized froth in which the air bubbles are collectively stabilized by the fine mineral particles. Accordingly, the structure of the coarse particles supported by bubbles, though very fragile and easily destroyed by the slightest impact, can rise quietly and easily with the help of the upward stream of carrier liquid.
  • the suitably comminuted sylvinite ore (the grinding being of the wet or dry type) consisting predominantly of particles larger than 28 mesh and preferably larger than 20-16 mesh is formed into a pulp with a brine saturated with respect to the soluble components of the sylvinite. This pulp is conditioned with conventional flotation reagents.
  • the conditioned pulp is introduced at the upper region of a cell, and generally at the vertical axis thereof.
  • the introduction of pulp should be conducted so as to prevent or considerably reduce turbulence at the upper zone of the cell.
  • the pulp feeding device discharges preferably at a short distance under the overflow level, for example, about 1 to 50, preferably l to cm. This distance is an important factor in the efficiency of separation. It has been observed that for a cell of a given height, the yield increases when this distance decreases. Obviously, though, this increase in yield is obtained at the expense of a less pure concentrate.
  • the pulp introduced in the cell should preferably contain a large quantity of solids, for example, about 45-85 percent by weight and preferably about 60-70 percent. It has been found that an excess of brine creates too many Whirlpools at the surface and modifies the upward velocity of the ascending stream of brine. If the conditioning of the ore should take place in the presence of a larger quantity of brine, the pulp should be thickened before it is introduced in the cell by using a thickener or the like.
  • the emulsion of brine and air is introduced by a fixed distributor which is designed to avoid turbulence as much as possible, particularly to avoid eddy currents at the overflow level of the cell.
  • This brine-air emulsion can be introduced anywhere in the cross-sectional plane of the cell, preferably near the vertical axis of the cell or at its periphery. It is preferred that the vertical distance between the brine-air distributor and the overflow level be higher than cm, preferably higher than cm in a cell in which there is treated an ore consisting predominantly of particles larger than 28 mesh.
  • This supplementary brine helps to create an ascending stream so that it overflows at the top of the cell.
  • the upward linear velocity of this stream depends mostly on the nature and on the particle size of the treated ore. Thus, for instance, there has been found that for a sylvinite having a particle size not larger than 8 mesh, an upward velocity of 1-1.5 cm/sec. is perfectly suitable; for a larger particle size up to 6 and even 5 mesh, the velocity must be higher, ranging about 2 cm/sec.
  • this supplementary brine is generally performed in the vicinity of the brine-air distributor, i.e., at the lower part of the cell and, preferably, near its axis or at its periphery.
  • the device for distributing supplementary brine must create as little agitation as possible in the cell so that no eddy currents should reach the overflow level.
  • the amount of supplementary brine fed to the cell can represent about 0 to 70 percent by volume of the total carrier fluid.
  • the introduction of brine and air-brine can be conducted with distribution nozzles which discharge into the cell at the same or different levels.
  • the nozzles are directed towards the lower part of the cell so as to prevent the formation of any turbulence which might be propagated to the surface.
  • the nozzles are placed all around the cell or at a plurality of points preferably disposed symmetrically on the periphery of the cell in order to provide as uniform a feed as possible.
  • the supplementary brine is introduced all around the cell by a distributing device which prevents or reduces the Whirlpools, and the emulsion is fed at a slightly higher level.
  • the distributing device preferably comprises a distributing sheath placed around the cell and communicating with the latter through openings provided in the wall, these openings being optionally provided with baffle elements or deflectors. which prevent excessive agitation at the brine feed.
  • Another distributing system comprises, for example, discharge pipe (or pipes) carrying the brine under a deflector which is tied by its higher portion to the wall of the cell and which forms a kind of skirt inside the cell.
  • the air bubbles brought by the air-brine emulsion attach themselves to the particles of potassium chloride which have been selectively filmed by the collector and, with the help of the ascending stream of brine, carry these particles to the top of the cell in a continuous movement without any shock which might destroy the fragile structure of particles and bubbles.
  • the tailings which contain substantially all the sodium chloride, are withdrawn at the bottom of the cell. The separation is such that a single pass through one cell gives tailings which are substantially free of liberated potassium chloride.
  • tailings or their coarser fractions often contain an important quantity of non-liberated KCl in the form of middlings which must be reground before being introduced into a standard flotation.
  • the potassium chloride remaining in these tailings can also be recovered by a dissolving-crystallizing technique.
  • Another preferred embodiment of this invention comprises the use of a cell having the shape of a vertical tank with a horizontal cross-section of any form but preferably of a simple form such as circular, rectangular or square.
  • This tank terminates at the lower portion by a narrower part, for example, of conical or pyramidal shape.
  • the obstacle which reduces the free cross-sectional area for flow of carrier for a specific height.
  • this obstacle has an enlarged portion between two portions which become thinner towards the extremities so that the velocity of the ascending stream increases first progressively to a maximum value, then decreases progressively without creating any substantial agitationfThus, the obstacle may be constructed as two in- .verted cones joined either directly by their base or by cylindrical part; it may also have an ovoid shape or any analogous form.
  • the pulp feeding rate and, therefore, the output of the cell is proportional to the horizontal cross-sectional area of the cell at the overflow level and does not substantially depend on the height of the cell.
  • the effective height of the cell i.e., the height in which the particle separation takes place, is relatively low and, for a given ore, varies but little with the output of the cell.
  • the distance between the point of introduction of the emulsion and the overflow level should preferably be at least 1.5 times the effective height to reduce the risks of turbulence at the surface due to the feeding of emulsion and/or make-up brine.
  • the upper part 1 of the cell is cylindrical.
  • the bottom 2 is in the shape of a. cone being terminated at the lowermost portion thereof by a .I-shaped pipe 3.
  • a frustoconical hopper 4 affixed at the narrow portion thereof by pipe 5 is used to introduce pulp below the overflow level 6 of the cell.
  • a nozzle 7 for distributing the air-brine is provided at the bottom of the cylindrical portion 1, and at a slightly lower level is placed a distributing device 8 for supplementary brine.
  • the experimental cell has a diameter of 0.30 m., and the cylindrical part is 1.50 m. high. This cell was used to treat 3.5 tons of sylvinite with an average K 0 content of 20.1 percent, and having the following average particle size:
  • the rate of introduction of brine was adjusted to such a value that the linear upward velocity of the stream was 1.5 cm/sec.
  • the potassium chloride concentrate collected at the overflow level was separated from the accompanying brine and dried. It contained 59.6% K 0 and had the following average particle size:
  • the mesh size openings correspond to Tyler sieve sizes.
  • the K 0 yield of the operation (calculated as K 0 in the concentrate versus K 0 present in the treated ore) was 85 percent and the tailings withdrawn at the bottom of the cell contained only 4.0 percent of K 0.
  • the ore was treated with following flotation reagents 100 g/t of starch as depressant, 200 g/t of stearylamine acetate as collector and 200 g/t of fine oil as frothing agent.
  • flotation reagents 100 g/t of starch as depressant, 200 g/t of stearylamine acetate as collector and 200 g/t of fine oil as frothing agent.
  • the rate of introduction of the pulp has been adjusted to 270 kg/h and there has been withdrawn 9O kg/h of concentrate.
  • FIG. 2 of the accompanying drawing is a plan view of a cell according to the invention.
  • the sin brine emulsion is introduced by four nozzles 9 distributed symmetrically at the periphery of the cell and supplementary brine is fed through nozzles 10.
  • the tailings are with-drawn through pipe 11, the pulp introduction and withdrawal systems not being shown on this simplified drawing.
  • FIG. 3 of the accompanying drawing is a schematic elevation of another cell according to the invention.
  • On this figure 12 represents a deflector-skirt. Brine is fed through line 14 behind this element and emulsion is fed close to this element, but over it, through line 13.
  • An obstacle 15 having the shape of two inverted cones joined by a cylindrical part is used to vary the upward velocity of the carrier stream. The tailings are withdrawn through pipe 16.
  • a coarse flotation process comprising the steps of:
  • a carrier fluid consisting essentially of an emulsion of air and liquid to a bottom zone only of said cell at a rate and in such a manner as to substantially avoid turbulence, whereby the very fragile and easily destroyed structure of the coarse particles supported by bubbles can rise;
  • a process as defined by claim 1 further comprising feeding a supplementary quantity of the carrier liquid in a separate stream adjacent to the feeding of said carrier fluid.
  • a process as defined by claim 1 wherein the pulp comprises a saturated suspension of 60-70 percent by weight of solid sylvinite ore having a major portion of larger than 20-16 mesh particles.
  • a process as defined by claim 11 further comprising feeding a supplementary quantity of brine in a separate stream adjacent to the feeding of said carrier fluid.
  • a coarse flotation process comprising the steps of:
  • a carrier fluid consisting essentially of an emulsion of air and liquid to a bottom zone only of said cell at a rate and in such a manner as to subd. withdrawing floated particles as overflow from the stantially avoid turbulence, whereby the very fragile and easily destroyed structure of the coarse particles supported by bubbles can rise;
  • said floated particles comprising a fraction of said major portion; and e. withdrawing tailings from the bottom of Said cell.

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US00087611A 1966-05-24 1970-11-06 Flotation of coarse particles Expired - Lifetime US3730341A (en)

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FR62664A FR1499990A (fr) 1966-05-24 1966-05-24 Procédé de flottation de particules de granulométrie grossiere

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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4436617A (en) 1982-07-22 1984-03-13 Cocal, Inc. Froth flotation ore beneficiation process utilizing enhanced gasification and flow techniques
US4472271A (en) * 1982-08-25 1984-09-18 Freeport Kaolin Company Froth flotation apparatus and process
US4483624A (en) * 1982-08-25 1984-11-20 Freeport Kaolin Company High intensity conditioning mill and method
US4822493A (en) * 1987-11-27 1989-04-18 Universite Laval, Cite Universitaire Method for separation of coarse particules
US5456362A (en) * 1994-05-26 1995-10-10 The University Of British Columbia Flutation process for the flutation of coarse fractions of potash ores
US5542546A (en) * 1994-05-07 1996-08-06 Kali Und Salz Gmbh Process and apparatus for non-agitated flotation of substances with a low degree of hydrophoby and/or low stability in the foam structure, in particular of salt mixtures
US6425485B1 (en) * 1998-03-26 2002-07-30 Eriez Magnetics Air-assisted density separator device and method
US20100167339A1 (en) * 2007-06-19 2010-07-01 Eastman Chemical Company Process for microalgae conditioning and concentration
CN109414708A (zh) * 2016-04-26 2019-03-01 纽卡斯尔创新有限公司 用于颗粒分离器的进料装置、颗粒分离器和颗粒分离方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114377846B (zh) * 2021-12-28 2023-07-04 湖南鑫恒环境科技有限公司 铁矿尾矿资源化综合利用处理装置

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB189422217A (en) * 1894-11-17 1895-11-16 William Alexander Improvements in Coin-freed Apparatus for the Supply of Gas, Liquids, or Electricity.
US1167835A (en) * 1915-04-05 1916-01-11 Dudley H Norris Apparatus for separating the metallic and rocky constituents of ores.
US1223033A (en) * 1915-08-03 1917-04-17 Metals Recovery Co Apparatus for separating or concentrating ores.
US1410152A (en) * 1919-02-06 1922-03-21 Allen Charles Hydraulic classifier
US2758714A (en) * 1954-08-25 1956-08-14 Smith Douglas Company Inc Concentration of minerals
US2783884A (en) * 1950-12-06 1957-03-05 Ruhrchemie Ag Process and apparatus for the contacting of granular materials with liquids and gases
US2931502A (en) * 1956-07-02 1960-04-05 Saskatchewan Potash Method for flotation concentration in coarse size range
US3016143A (en) * 1958-12-19 1962-01-09 Int Minerals & Chem Corp Flotation of granular ores
US3254762A (en) * 1962-02-19 1966-06-07 Saskatchewan Potash Conditioning of granular potash
US3298519A (en) * 1963-10-23 1967-01-17 Borden Co Concentration of minerals

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB189422217A (en) * 1894-11-17 1895-11-16 William Alexander Improvements in Coin-freed Apparatus for the Supply of Gas, Liquids, or Electricity.
US1167835A (en) * 1915-04-05 1916-01-11 Dudley H Norris Apparatus for separating the metallic and rocky constituents of ores.
US1223033A (en) * 1915-08-03 1917-04-17 Metals Recovery Co Apparatus for separating or concentrating ores.
US1410152A (en) * 1919-02-06 1922-03-21 Allen Charles Hydraulic classifier
US2783884A (en) * 1950-12-06 1957-03-05 Ruhrchemie Ag Process and apparatus for the contacting of granular materials with liquids and gases
US2758714A (en) * 1954-08-25 1956-08-14 Smith Douglas Company Inc Concentration of minerals
US2931502A (en) * 1956-07-02 1960-04-05 Saskatchewan Potash Method for flotation concentration in coarse size range
US3016143A (en) * 1958-12-19 1962-01-09 Int Minerals & Chem Corp Flotation of granular ores
US3254762A (en) * 1962-02-19 1966-06-07 Saskatchewan Potash Conditioning of granular potash
US3298519A (en) * 1963-10-23 1967-01-17 Borden Co Concentration of minerals

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4436617A (en) 1982-07-22 1984-03-13 Cocal, Inc. Froth flotation ore beneficiation process utilizing enhanced gasification and flow techniques
US4472271A (en) * 1982-08-25 1984-09-18 Freeport Kaolin Company Froth flotation apparatus and process
US4483624A (en) * 1982-08-25 1984-11-20 Freeport Kaolin Company High intensity conditioning mill and method
US4822493A (en) * 1987-11-27 1989-04-18 Universite Laval, Cite Universitaire Method for separation of coarse particules
US5542546A (en) * 1994-05-07 1996-08-06 Kali Und Salz Gmbh Process and apparatus for non-agitated flotation of substances with a low degree of hydrophoby and/or low stability in the foam structure, in particular of salt mixtures
US5456362A (en) * 1994-05-26 1995-10-10 The University Of British Columbia Flutation process for the flutation of coarse fractions of potash ores
US6425485B1 (en) * 1998-03-26 2002-07-30 Eriez Magnetics Air-assisted density separator device and method
US20100167339A1 (en) * 2007-06-19 2010-07-01 Eastman Chemical Company Process for microalgae conditioning and concentration
US20100181234A1 (en) * 2007-06-19 2010-07-22 Eastman Chemical Company Process and apparatus for adsorptive bubble separation
US8251228B2 (en) * 2007-06-19 2012-08-28 Renewable Algal Energy, Llc Process and apparatus for adsorptive bubble separation
US8512998B2 (en) 2007-06-19 2013-08-20 Renewable Algal Energy, Llc Process for microalgae conditioning and concentration
US9358553B2 (en) 2007-06-19 2016-06-07 Renewable Algal Energy, Llc Process for microalgae conditioning and concentration
CN109414708A (zh) * 2016-04-26 2019-03-01 纽卡斯尔创新有限公司 用于颗粒分离器的进料装置、颗粒分离器和颗粒分离方法
US20190126287A1 (en) * 2016-04-26 2019-05-02 Newcastle Innovation Limited A feed apparatus for a particle separator, particle separator and method of particle separation
US11117137B2 (en) * 2016-04-26 2021-09-14 Newcastle Innovation Limited Feed apparatus for a particle separator, particle separator and method of particle separation

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Publication number Publication date
OA02438A (fr) 1970-05-05
FR1499990A (fr) 1967-11-03
ES340902A1 (es) 1968-06-16

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