EP0364654A2 - Procédé et dispositif de production de microbulles dans les systèmes de concentration de minerais par flottation avec écumage - Google Patents

Procédé et dispositif de production de microbulles dans les systèmes de concentration de minerais par flottation avec écumage Download PDF

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Publication number
EP0364654A2
EP0364654A2 EP89103088A EP89103088A EP0364654A2 EP 0364654 A2 EP0364654 A2 EP 0364654A2 EP 89103088 A EP89103088 A EP 89103088A EP 89103088 A EP89103088 A EP 89103088A EP 0364654 A2 EP0364654 A2 EP 0364654A2
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EP
European Patent Office
Prior art keywords
porous
sleeve
housing
liquid
porous sleeve
Prior art date
Legal status (The legal status 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 status listed.)
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Application number
EP89103088A
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German (de)
English (en)
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EP0364654A3 (fr
Inventor
Donald E. Zipperian
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Deister Concentrator Co Inc
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Deister Concentrator Co Inc
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Publication of EP0364654A2 publication Critical patent/EP0364654A2/fr
Publication of EP0364654A3 publication Critical patent/EP0364654A3/fr
Withdrawn legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/24—Pneumatic
    • 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
    • B01F23/231—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids by bubbling
    • B01F23/23105—Arrangement or manipulation of the gas bubbling devices
    • B01F23/2312—Diffusers
    • B01F23/23126—Diffusers characterised by the shape of the diffuser element
    • B01F23/231265—Diffusers characterised by the shape of the diffuser element being tubes, tubular elements, cylindrical elements or set of tubes
    • 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
    • B01F23/2321—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 moving liquid and gas in counter current
    • B01F23/23211—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 moving liquid and gas in counter current the liquid flowing in a thin film to absorb the gas
    • 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
    • B01F23/237—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media
    • B01F23/2373—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids characterised by the physical or chemical properties of gases or vapours introduced in the liquid media for obtaining fine bubbles, i.e. bubbles with a size below 100 µm
    • 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
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/314—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced at the circumference of the conduit
    • B01F25/3142—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced at the circumference of the conduit the conduit having a plurality of openings in the axial direction or in the circumferential direction
    • B01F25/31421—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced at the circumference of the conduit the conduit having a plurality of openings in the axial direction or in the circumferential direction the conduit being porous
    • 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
    • B03D1/1431—Dissolved air flotation machines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F2215/00—Auxiliary or complementary information in relation with mixing
    • B01F2215/04—Technical information in relation with mixing
    • B01F2215/0413—Numerical information
    • B01F2215/0418—Geometrical information
    • B01F2215/0431—Numerical size values, e.g. diameter of a hole or conduit, area, volume, length, width, or ratios thereof
    • 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
    • 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
    • B01F23/231—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids by bubbling
    • B01F23/23105—Arrangement or manipulation of the gas bubbling devices
    • B01F23/2312—Diffusers
    • B01F23/23123—Diffusers consisting of rigid porous or perforated material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/02—Froth-flotation processes
    • B03D1/028—Control and monitoring of flotation processes; computer models therefor
    • 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

Definitions

  • This invention relates to the separation of minerals in finely comminuted form from an aqueous pulp by froth flotation process, and especially to a froth flota­tion system with an improved means for introducing the gaseous medium in the form of minute bubbles into the liquid flotation column. More particularly, the invention relates to a device for generating gas bubbles in a flowing stream of aqueous liquid and delivering the bubble contain­ing stream to the flotation column.
  • Froth flotation involves conditioning an aqueous slurry or pulp of the mixture of mineral and gangue par­ticles with one or more flotation reagents which will promote flotation of either the mineral or the gangue constituents of the pulp when the pulp is aerated.
  • the conditioned pulp is aerated by introducing into the pulp minute gas bubbles which tend to become attached either to the mineral particles of the gangue particles of the pulp, thereby causing one category of these particles, a float fraction, to rise to the surface and form a froth which overflows or is withdrawn from the flotation apparatus.
  • the other category of particles tends to gravitate downwardly through the aqueous pulp and may be withdrawn at an underflow outlet from the flotation vessel.
  • Examples of flotation apparatus of this type are disclosed in U.S. patents Nos. 2,753,045; 2,758,714; 3,298,519; 3,371,779; 4,287,054; 4,394,258; 4,431,531; 4,617,113; 4,639,313; and 4,735,709.
  • the conditioned pulp is introduced into a vessel to form a column of aqueous pulp, and aerated water is introduced into the lower portion of the column.
  • An overflow fraction containing floated par­ticles of the pulp is withdrawn from the top of the body of aqueous pulp and an underflow or non-float fraction con­taining non-floated particles of the pulp is withdrawn from the column in the lower portion.
  • the aerated water is produced by first introducing a frother or surfac­tant into the water and passing the mixture through an inductor wherein air is aspirated into the resulting liquid.
  • a high flow rate for the water must be maintained through the inductor. While recirculation systems have been de­vised to minimize the amount of "new" water added to the system, a significant expenditure in energy is required to move such large quantities of water.
  • aqueous slurry or pulp fed to the flotation apparatus typically consists of approximately seventy-five percent (75%) solids and twenty-five percent (25%) water.
  • Another method for introducing minute air bubbles into the flotation vessel comprises a sparging system such as that disclosed in U.S. patent No. 4,735,709.
  • Spargers or microdiffusers are normally tubular members formed of porous material such as sintered stainless steel, porous plastic, ceramic or the like, with a porous wall having a typical average pore size of about 50 microns.
  • the sparger is placed within the flotation vessel and air under pressure is introduced into its inter­ior.
  • the pressurized gas or air within the interior cham­ber is forced through the pores and into the aqueous pulp in the flotation chamber.
  • spargers are used with considerable suc­cess, they do have certain disadvantages, including the tendency of the small pores to become clogged with contami­nants. Also, the spargers typically used, because they are inserted within the flotation column, do not themselves supply water to the vessel and the replacement water must be provided with another system.
  • Another object is to achieve the above result with a minimal amount of water inflow.
  • Still another object of the invention is to provide a flotation apparatus for the concentration of minerals requiring a significantly reduced energy condi­tion, thereby providing more economic operation.
  • a further object of the invention is to provide a bubble generator adapted for use with a flotation column, which bubble generator is external of the flotation column and thus easily accessible for maintenance.
  • a still further object of the invention is to produce bubbles for a froth flotation column wherein the bubbles are finer in size than those that can be produced by conventional spargers and with a minimum amount of supply liquid.
  • minute bubbles or microbubbles are first generated in a flowing stream of aqueous liquid and then introduced into the flotation column.
  • the system utilizes a microbubble gener­ator having a tubular housing with an inlet end and an outlet end. Located coaxially within the housing is an inner member with an elongated exterior cylindrical sur­face.
  • a porous tubular sleeve is mounted between the housing and the inner member coaxially therewith to define with the cylindrical interior surface of the housing an elongated air chamber of annular cross section.
  • the porous sleeve also has a cylindrical inner surface that defines, with the exterior surface of the inner member, an elongated liquid flow chamber of thin, annular cross section.
  • aqueous liquid is supplied through a fitting on the housing to the liquid flow chamber and is forced through the flow chamber at a relatively high flow rate and in a thin, annular space to minimize the contact between the liquid and the inner surface of the porous sleeve.
  • Air or other gas under pressure is supplied through another fitting on the housing to the air chamber so that air is forced radially inwardly through the porous sleeve and is diffused in the form of microbubbles in the flowing stream.
  • an aqueous liquid infused with minute gaseous bubbles is discharged from the outlet end of the housing and piped to the flotation vessel.
  • the resulting product is introduced into the flotation column through distribution pipes with openings of a size calculated to maintain a pressure condition that prevents coalescence of the bubbles.
  • a fluid vessel or cylinder 10 for use in the separation of minerals in finely comminuted form from an aqueous pulp by the froth flotation process and which utilizes an improved means in accordance with the invention for introducing gas in the form of minute bubbles into the liquid flotation column.
  • the vessel includes a feed well 11 for feeding the aqueous pulp into the upper end of the flotation column, the pulp being received through a feed tube 12 from an external source of aqueous slurry to deliver a controlled quantity of the slurry to the feed well 11.
  • the feed well 11 may include baffles (not shown) so that the aqueous slurry fed into the feed well becomes distributed throughout the flotation column.
  • the introduction of aerated water into the fluid vessel 10 is accomplished by means of an air system 20.
  • the aerated water that is introduced tends to flow upwardly through the aqueous slurry and the particulate matter sus­pended therein so that either the particles of the desired valuable mineral or the particles of the gangue suspended in the aqueous slurry adhere to the rising bubbles and collect at the upper end of the flotation column in the form of a froth.
  • a launder 13 is provided at the upper end of the vessel and is adapted to receive the froth which overflows from the top of the vessel.
  • An output conduit 14 is provided to convey the overflowing froth from the laun­der 13 to further processing or storage apparatus.
  • the system for introducing an aqueous mixture containing minute gas bubbles includes an upper system 21 and a lower system 22, each of which has a pair of micro­bubble generators 50 formed in accordance with the inven­tion. In the preferred arrangement, only one of the gener­ators 50 of each pair is used at a time, the other gener­ator being used as a spare, such as during repair and replacement.
  • Gas under pressure is supplied to one of the lower system microbubble generators 50 through a branched air inlet 23 that communicates with a compressor 24.
  • An aqueous liquid is supplied to each of the lower microbubble generators 50 through a branched water inlet 25 which is connected to a pump 26 to provide the desired pressure and flow rate.
  • the resulting aerated liquid is exhausted from the generators through a branched water outlet 27 and then conveyed through a pipe 28 to a manifold 30 located on the vessel.
  • the manifold has four outlet pipes 31, 32, 33, and 34 which connect to four distributor tubes 36, 37, 38, and 39, which extend through pipe hous­ings 41, 42, 43, and 44, respectively, into the interior of the vessel.
  • the distributor tubes are provided with a predetermined pattern of small openings through which the aerated water is discharged into the flotation column.
  • the upper air system 21 is essentially identical to the lower system 22 and, accordingly, like numerals are used to indicate like parts in the system components.
  • the most effective arrangement comprises supplying about one-half or more of the aerated water through the lower system 22 and one-half or more through the upper system 21. Also, it is desirable that the pipe sizes be selected to retain a uniform flow cross section through the length of the flow so as to maintain a uniform velocity.
  • the four microbubble generators 50 are all iden­tical and provide a new and improved means for aerating the aqueous liquid flowing into the flotation column, while at the same time minimizing the amount of water or aqueous liquid required to introduce an optimum volume of gas.
  • the generators 50 are each in the form of an elongated tube, typically about 48 inches long (24 inches for some small cells), and most of the components are fabricated of stain­less steel to eliminate the effects of corrosion and scale.
  • Each of the generators includes an upper end member 51 and a lower end member 52 separated by an elon­gated, cylindrical, tubular housing 53.
  • the upper end of the tubular housing 53 seats in an annular groove 54 formed in the adjacent face of the upper end member 51 and the lower end of the tubular housing 53 seats in an annular groove 55 formed in the adjoining face of the lower end member 52.
  • the resulting assembly is held in place by an elongated, threaded rod 56 which extends through a central bore 57 in the upper end member 51 and axially through the entire length of the tubular housing 53.
  • the axial bore 57 has a narrowed throat portion 58.
  • the lower or inner end of the threaded rod 56 screws into a threaded bore 59 in the lower end member 52.
  • a cap nut 60 with an associated cap centering washer 60a, is tightened down on the upper end of the threaded rod 56 and seats in the throat portion 58 to secure the assembly.
  • the upper end member 51 has an air inlet port 61 that extends in an axial direction and a radial water inlet port 62. Both ports 61 and 62 are adapted to receive fittings that connect to air and water inlet lines, respec­tively.
  • the upper end member 51 has an inner fitting 63 associated therewith that seats against an annular axial extension 64 formed on the upper end member so that it does not block the air inlet port 61.
  • An axially extending locater pin 65 that extends into mating bores in the upper end member 51 and in the inner fitting 63 prevents relative rotation between the two parts.
  • An axially extending neck portion 66 of the inner fitting 63 extends upwardly into the axial bore 57.
  • the lower portion of the neck 66 has a pair of spaced, annular grooves 67 and 68 which receive seal rings 69 and 70.
  • a central axial bore 71 is formed in the inner fitting 63, the bore being provided with a lower tapered portion 72.
  • a tangential slot 73 is milled in the neck portion 66 adjacent the radial water inlet port 62 to provide a passage for water through the neck portion and into the central bore 71.
  • the locater pin 65 assures that the tangential slot is correctly aligned so that the water passage is not blocked.
  • the lower end of the lower end member 52 has an axial threaded outlet bore 75 formed therein that receives a fitting for the outlet line 27 for the aerated aqueous liquid.
  • the outlet bore 27 communicates with a tapered passage 76, which in turn communicates with a plurality of axially extending, parallel ports 77 formed in a circular pattern in the lower end member 52.
  • a porous, tubular sleeve 80 that extends axially between the lower end member 52 and the inner fitting 63.
  • the upper end of the sleeve 80 seats in an annular groove 81 formed in the inner fitting 63 and bears against an annular gasket 83 positioned in the groove 81.
  • the lower end of the porous sleeve seats in an annular groove 82 formed in the lower end member 52 and bears against an annular gasket 84 that is seated in the bottom of the groove 82.
  • the porous sleeve 80 is formed of a porous plastic material manufactured by Porex Technologies, of Fairburn, Georgia.
  • the material is a porous polypropylene and has a typical pore size of about 75 microns.
  • the designation used by the manufacturer is POREX XM-1339. Other materials may be used, however, such as sintered stainless steel, porous ceramics, etc.
  • the sleeve 80 is 2.925 inches O.D., and has a wall thickness of about .375 inch.
  • the exterior surface of the porous sleeve 80 and the interior surface of the tubular housing 53 define an elongated, annular air chamber 85 that communicates with the air inlet port 61.
  • the lower end member 52 has a drain port 87 formed therein communicating with the air chamber 85 and an associated drain valve 88 to drain off accumu­lated oil and particles when necessary.
  • an axially extending filler tube 90 that extends between an upper tip member 91 and a lower tip member 95.
  • the tip members 91 and 95 both have a frustoconical shape, the upper member 91 tapering in an upward direction and the lower tip member 95 tapering in a downward direction to encourage laminar flow.
  • the upper tip member 91 has an annular rabbet 92 formed in its base that receives the upper end of the filler tube 90 and also has a central axial bore 93 with a threaded upper end portion 94 adapted to be threadedly received on the threaded rod 56.
  • the lower tip member 95 has an annular rabbet 96 formed in its base portion and adapted to receive the lower end of the filler tube 90.
  • the lower tip member also has a central axial bore 97 with a threaded portion 98 at its lower end adapted to be threaded onto the threaded rod 56.
  • the exterior surface of the filler tube 90 together with the tapered exterior surfaces of the two tip members 91 and 95, define with the interior surface of the porous sleeve 80, a thin, annular fluid passage 99 for the aqueous fluid that is supplied through the inlet port 62. It is desir­able that the fluid passage 99 be relatively thin in its cross section perpendicular to the direction of flow and in the embodiment shown, the passage is about .094 inch in radial thickness.
  • the aqueous liquid entering through the port 62 passes through the slot 73 into the central bore 71 within the inner fitting 63.
  • the flow proceeds downwardly through the lower tapered portion 72 adjacent the central bore 71 and then outward into the annular flow passage 99, as shown in FIG. 3.
  • gas passing through the porous sleeve 80 becomes en­trained in the flow so that the resulting aqueous fluid that exits through the outlet 75 has a volume of gas en­trained therein in the form of minute bubbles.
  • the radial thickness of the water flow passage 99 is relatively small, e.g., .094 inch, the sur­face area of the flowing mass of water that contacts the interior surface of the porous sleeve 80 is relatively large with respect to the cross-sectional area of the flow passage. This assures that a maximum amount of gas is entrained in the flowing liquid in the form of minute bubbles.
  • the small ports or holes 100 formed in the distributor tubes must be of a proper size to assure that a substantial pressure drop does not occur within the distributor tubes.
  • a preferable arrangement is to provide openings located on the bottom of the tube and spaced between about 2.5 to 7.5 inches apart.
  • the openings preferably have a diameter of between about one-sixteenth inch and one-eighth inch. These spacings and hole sizes may vary, of course, depending upon the size of the vessel and the length of the particular distributor tube.
  • the tubes may extend into the flotation column from opposite sides of the vessel from separate manifolds. Preferably, tube lengths are kept substantially equal.
  • Some typical hole sizes and spacings are shown in Table I below, together with dimensions for respective microbubble generators 50. TABLE I Microbubble Generator 50 Distributor Tubes (.5 inch O.D.) Cell Dia. (ft.) Housing 53 (Inches) O.D. /I.D. Porous Tube 80 (Inches) O.D. / I.D. Inner Tube 90 (Inches) O.D. Passage 99 Area (Sq.Inch) Hole Dia.
  • the aqueous pulp will be fed at a controlled rate through the feed pipe 12 into the feed well 11.
  • Aerated water will be fed at a controlled rate through both the upper and lower distribution systems 21 and 22, the flow rate being about twice as great in the lower system as in the upper or intermediate system.
  • the process begins with the infusion of an aque­ous liquid with microbubbles by means of the microbubble generators 50.
  • Gas is supplied to the generators by the compressor 24 and water is supplied by means of the water pump 26 or head pressure, which pumps the water at a de­sired predetermined pressure.
  • Recommended flow rates for various sizes of flotation cells are shown in tabular form in Table II below, it being understood that these are variable. For example, satisfactory operation has been achieved using less water and air at lower pressure, rang­ing as low as 40 psi. TABLE II CELL DIA.
  • GENERATOR PSI AIR
  • WATER WATER SUPPLY GPM 8" 70 2 70 .05 2.0' 70 15 70 4 2.5' 70 20 70 5 3.0' 70 30 70 8 5.5' 70 100 70 25 6.5' 70 140 70 35 8.0' 70 200 70 50 10.0' 70 320 70 80 12.0' 70 450 70 115
  • the gas enters each of the microbubble generators 50 through the inlet port 61 and fills the annular space 85 surrounding the exterior surface of the porous sleeve 80.
  • the aqueous liquid which is preferably water mixed with a typical surfactant of the type well known in the art, is supplied through the radial port 62 and flows through the central passage 71 into the annular water flow passage 99, where it flows along the interior surface of the porous sleeve 80.
  • the gas pressure in the gas chamber 85 forces air through the small pores (i.e., about 75 microns in pore size), so that it emerges at the cylindrical interior surface of the sleeve, where it contacts the flowing aque­ous liquid. Due to the relatively high velocity of the liquid flow, the bubbles are sheared from the surface as they emerge and become entrained in the form of minute bubbles in the flowing stream.
  • the resulting liquid is then introduced into the flotation column through the small holes 100 in the respec­tive tubes.
  • the minute gas bubbles then levitate through the aqueous slurry in the flotation column and the par­ticles of the desired valuable mineral adhere to the bub­bles and collect at the upper end of the flotation vessel in the form of froth.
  • the froth overflows into the launder 13, where it is collected and delivered to the output conduit 14, which conveys it away for further processing.
  • the apparatus herein disclosed provides for greater efficiency in mater­ial recovery. Since bubble size is small, retention time within the water column is correspondingly large. The finer bubbles provide maximum surface area for attachment to descending particles. Turbulence within the water column is minimized whereby bubbles tend to follow only substantially vertical paths. Larger bubbles tend to be erratic and to create voids therebelow which result in descending particles moving somewhat laterally rather than downwardly.
  • the distributor pipes 36, 37, 38, 39 extend horizontally across the cross section of the cell (as shown in FIG. 1), have evenly spaced openings 100, and are evenly spaced apart so as to provide a substantially uniform cross section of bubbles thereabove in the column 10.
  • Two levels or elevations of distributor pipes are used, thereby creating two recovery zones within the column 10, one between the two pipe sets and the other above the upper set.
  • the lower set is two to four feet above the tailings discharge port (not shown) in the bottom of the column 10, while the upper set is disposed midway between the lower set and the upper end of the column 10.
  • Bubbles from both pipe sets will obtain.
  • the lower zone the only bubbles will be those from the lower set.
  • bubble density is correspondingly different in the two zones. Bubbles in the upper zone, being more concentrated, attach to and im­mediately float off that particle fraction most susceptible to float separation. The remaining particles descend through the lower zone where the fine bubbles are ascending relatively slowly, the slow ascent creating more time during which attachment to descending particles may occur. Primary recovery, therefore, may be said to occur in the upper zone, and scavenging in the lower zone.
  • bubble generation and sizing are external to column 10 and that the same size bubbles are fed to both of the upper and lower sets of pipes. Since rising bubbles progressively expand in size, those bubbles introduced at the lower level will enlarge by the time they reach the upper level. Thus, some of the desired qualities of tiny bubbles will there be lost. However, tiny bubbles are introduced at the upper level and will rise vertically, providing maximum surface area for particle attachment. Thus, by means of multilevel bubble introduction of externally generated bubbles, bubble size is maintained optimally small, thereby enhancing the proba­bility of particle attachment.
  • Tiny bubble introduction at the different levels also minimizes turbulence within the column water. Smaller bubbles tend to create less disturbance and to follow vertical paths. Thus, there will be minimal turbulence in the lower zone, as bubble size is small. In the upper zone where bubble concentration is greater, the distance to the water surface is relatively short and the introduction of small bubbles tends to infiltrate smaller bubbles with the enlarged ones and ascendancy remains substantially ver­tical. Turbulence in the form of circular motion or boil­ing action is thereby minimized, contributing further to the efficiency of material pick-up. The two sets of dis­tributor pipes at the two levels, receiving and emitting the same size bubbles, inhibit development of turbulence, thereby enhancing column efficiency.
  • air and water are preferred in the working embodiments of this invention, gases other than air, such as nitrogen, and liquids other than water may be used.
  • gases other than air such as nitrogen
  • liquids other than water may be used.
  • air and water and the term “aerated water” are intended to include these equivalents.
  • micro-­sized bubbles enhances the efficiency of the flotation mechanism through increased surface area of the bubbles while reducing the air volume requirements typical of present flotation mechanisms.
  • the system requires lower air and water pressures (40-70 psi) and lower water volume (0.5 GPM/CFM) than other microbubble sparger systems, which require minimum 80 psi air and water pressure and water requirements of 1 - 1.5 GPM/CFM.

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  • Biotechnology (AREA)
  • Nanotechnology (AREA)
  • Physical Water Treatments (AREA)
EP19890103088 1988-10-21 1989-02-22 Procédé et dispositif de production de microbulles dans les systèmes de concentration de minerais par flottation avec écumage Withdrawn EP0364654A3 (fr)

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EP0364654A3 EP0364654A3 (fr) 1991-01-23

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AU (1) AU2830689A (fr)
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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SG83220A1 (en) * 1999-08-06 2001-09-18 Sumitomo Seika Chemicals Apparatus for generating minute gas foams under self-suction
WO2012168084A1 (fr) * 2011-06-07 2012-12-13 Siemens Aktiengesellschaft Procédé d'extraction de matériaux contenant du métal dans un flux massique de type suspension contenant des matériaux contenant du métal
CN103120986A (zh) * 2013-02-04 2013-05-29 中国矿业大学 浮选池
EP3057712A4 (fr) * 2013-10-17 2017-06-14 Eriez Manufacturing Co. Système de séparation à assistance pneumatique amélioré
CN107096646A (zh) * 2017-06-28 2017-08-29 贵州大学 一种粗颗粒浮选柱浮选的方法及装置
CN108607692A (zh) * 2018-05-25 2018-10-02 河南东大科技股份有限公司 一种低品位铝土矿选矿浮选气泡发生器
CN108854616A (zh) * 2018-05-08 2018-11-23 李常德 一种微气泡发生系统
CN114700182A (zh) * 2021-07-22 2022-07-05 中国矿业大学 一种梯度进气的粗颗粒流态化浮选装置及方法

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU617977B2 (en) * 1989-06-26 1991-12-05 Carroll International Corporation Method and apparatus for generating microbubbles in froth flotation mineral concentration systems

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US2758714A (en) * 1954-08-25 1956-08-14 Smith Douglas Company Inc Concentration of minerals
DE2046254A1 (fr) * 1969-09-18 1971-04-01 Atomic Energy Of Canada Ltd
US4735709A (en) * 1985-07-05 1988-04-05 Deister Concentrator Company, Inc. Method and apparatus for concentration of minerals by froth flotation using dual aeration

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GB694918A (en) * 1951-02-23 1953-07-29 F S Gibbs Inc Diffusion of gases in liquids
US2758714A (en) * 1954-08-25 1956-08-14 Smith Douglas Company Inc Concentration of minerals
DE2046254A1 (fr) * 1969-09-18 1971-04-01 Atomic Energy Of Canada Ltd
US4735709A (en) * 1985-07-05 1988-04-05 Deister Concentrator Company, Inc. Method and apparatus for concentration of minerals by froth flotation using dual aeration

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Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SG83220A1 (en) * 1999-08-06 2001-09-18 Sumitomo Seika Chemicals Apparatus for generating minute gas foams under self-suction
WO2012168084A1 (fr) * 2011-06-07 2012-12-13 Siemens Aktiengesellschaft Procédé d'extraction de matériaux contenant du métal dans un flux massique de type suspension contenant des matériaux contenant du métal
CN103596696A (zh) * 2011-06-07 2014-02-19 西门子公司 用于从含有含金属的有价值矿物的悬浮液中获得含金属的有价值矿物的方法
RU2594916C2 (ru) * 2011-06-07 2016-08-20 Прайметалз Текнолоджиз Джермани Гмбх Способ получения металлосодержащих ценных веществ из содержащего металлосодержащие ценные вещества суспензионного массового потока
CN103120986A (zh) * 2013-02-04 2013-05-29 中国矿业大学 浮选池
CN103120986B (zh) * 2013-02-04 2014-03-05 中国矿业大学 浮选池
EP3057712A4 (fr) * 2013-10-17 2017-06-14 Eriez Manufacturing Co. Système de séparation à assistance pneumatique amélioré
RU2639340C2 (ru) * 2013-10-17 2017-12-21 Эриез Мануфэкчуринг Ко. Улучшенная система разделения с подачей воздуха
CN107096646A (zh) * 2017-06-28 2017-08-29 贵州大学 一种粗颗粒浮选柱浮选的方法及装置
CN108854616A (zh) * 2018-05-08 2018-11-23 李常德 一种微气泡发生系统
CN108607692A (zh) * 2018-05-25 2018-10-02 河南东大科技股份有限公司 一种低品位铝土矿选矿浮选气泡发生器
CN114700182A (zh) * 2021-07-22 2022-07-05 中国矿业大学 一种梯度进气的粗颗粒流态化浮选装置及方法

Also Published As

Publication number Publication date
EP0364654A3 (fr) 1991-01-23
ZA891489B (en) 1989-11-29
AU2830689A (en) 1990-04-26
FI894972A0 (fi) 1989-10-19

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