WO2015095054A2 - Procédé de lixiviation par flottaison de minéraux de sulfure de cuivre - Google Patents

Procédé de lixiviation par flottaison de minéraux de sulfure de cuivre Download PDF

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Publication number
WO2015095054A2
WO2015095054A2 PCT/US2014/070354 US2014070354W WO2015095054A2 WO 2015095054 A2 WO2015095054 A2 WO 2015095054A2 US 2014070354 W US2014070354 W US 2014070354W WO 2015095054 A2 WO2015095054 A2 WO 2015095054A2
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WIPO (PCT)
Prior art keywords
flotation
concentrate
subjecting
leaching
slurry
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Application number
PCT/US2014/070354
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English (en)
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WO2015095054A9 (fr
WO2015095054A3 (fr
Inventor
David J. Chaiko
Sara ROCKS (Sally)
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Flsmidth A/S
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Publication of WO2015095054A2 publication Critical patent/WO2015095054A2/fr
Publication of WO2015095054A3 publication Critical patent/WO2015095054A3/fr
Publication of WO2015095054A9 publication Critical patent/WO2015095054A9/fr

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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00—Obtaining copper
    • C22B15/0063—Hydrometallurgy
    • C22B15/0065—Leaching or slurrying
    • C22B15/0067—Leaching or slurrying with acids or salts thereof
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • This invention relates to systems and methods for leaching metals from ores such as metal sulfide ores and concentrates thereof, and more particularly to systems and methods for separating gangue minerals during or prior to primary leaching of metal values from sulfide ores and concentrates and after primary flotation.
  • the invention further relates to the leaching of copper-containing, zinc-containing and/or molybdenum-containing sulfide concentrates produced from a typical primary flotation process.
  • Chalcopyrite is the primary copper-containing mineral found in the majority of the copper sulfide ores of commercial interest.
  • Other copper-containing ore minerals of commercial interest include chalcocite (Cu 2 S), bornite (Cu 5 FeS 4 ), covellite (CuS), digenite (Cu 2 S), enargite (Cu 3 AsS 4 ), tennantite (Cu 12 As 4 S 13 ), and tetrahedrite (Cu 12 Sb 4 S 13 ).
  • Copper sulfide ores aside from containing a variety of copper-containing minerals, will typically also contain a wide variety of gangue minerals including, but not limited to, silicates, pyrite (FeS 2 ), pyrrhotite (FeS), and arsenopyrite (FeAsS).
  • gangue minerals including, but not limited to, silicates, pyrite (FeS 2 ), pyrrhotite (FeS), and arsenopyrite (FeAsS).
  • flotation In the processing of metal sulfide ores, flotation is commonly and successfully used to effect separations of metal values (i.e., metalliferous minerals) from gangue minerals found in comminuted ore. Unlike acidic leaching, flotation is generally performed under high pH (e.g., greater than 10) to suppress the recovery of gangue minerals.
  • high pH e.g., greater than 10
  • certain types of gangue/mineral separations are difficult to achieve - a non-limiting example is the separation of primary copper sulfides from pyrite. Therefore, it is fairly common for materials containing a target mineral/metal value to be floated and removed from collection launders in the flotation circuit, along with large amounts of lesser or non- valued gangue.
  • This frothing causes difficulties in controlling solution redox potentials within the leach reactors and requires excessive reactor heights to contain the froth.
  • the gangue minerals reduce the efficiency of post-flotation processing, such as ultra-fine grinding, and occupy valuable space within the leach reactors.
  • Separation of individual metal sulfides from each other can be a challenge, and the separation of copper-bearing sulfide minerals from pyrite, pyrrhotite, arsenopyrite, quartz, layered silicates, and/or other gangue by selective flotation remains a technical problem.
  • a target metal concentrate e.g., copper concentrate
  • an object of the present invention to control redox potential in at least a first reaction vessel of a leaching process, or a conditioning tank wherein leaching and flotation may occur simultaneously and advantageously;
  • a further object of the present invention is to reduce the amount of unnecessary solids (by volume or by weight) which are processed by a leach circuit.
  • a further object of the present invention is to reduce the amount of acid-generating waste, such as pyrite, that must be stored and monitored indefinitely in waste impoundments.
  • a method of leaching a metal sulfide ore is disclosed.
  • the method may comprise the steps of providing slurry having metal sulfide ore particles therein: subjecting the slurry to a flotation step at a pH level above nine to obtain a first concentrate; subjecting the first concentrate to an acidic leach solution; subjecting the first concentrate to a flotation step at a pH level below five to obtain a second concentrate; and, chemically leaching a metal into the acidic leach solution.
  • the flotation step which takes place at a pH level above nine may be accomplished in a different vessel than the flotation step which takes place at a pH level below five.
  • the flotation step at a pH level above nine may be accomplished at a different temperature than the flotation at a pH level below five, in some embodiments, the flotation in step at a pH level above nine may be accomplished at a different pressure than the flotation at a pH level below five. In some embodiments, the flotation in step at a pH level above nine may be accomplished at a different redox potential than the flotation at a pH level below five, in some embodiments, the step of subjecting the first concentrate to a flotation step at a pH level belo five to obtain a second concentrate may occur after the step of subjecting the slurry to a flotation step at a pH level above nine to obtain a first concentrate.
  • the step of subjecting the first concentrate to a flotation step at a pH level below five to obtain a second concentrate may occur prior to the step of chemically leaching a metal into the acidic leach solution.
  • the flotation step at a pH level below five may occur simultaneously with the step of chemically leaching a metal into the acidic leach solution.
  • the flotation step at a pH level below five may occur in a flotation leach reactor having an agitator, gas sparging system, and a launder.
  • the flotation step at a pH level below five may occur in a flotation-- leach reactor having means for introducing a gas or reagent.
  • the step of subjecting the first concentrate to a flotation step at a pH level below five to obtain a second concentrate may involve separating a first product containing a gangue material from the first concentrate to form the second concentrate, in some embodiments, the first product containing a gangue material may be obtained from froth generated during the chemical leaching step.
  • the method may further comprise the step of fine-grinding the second concentrate prior to introducing the second concentrate into a leach circuit.
  • the method may further comprise the step of applying steam directly or indirectly to the first concentrate.
  • the method may comprise the step of forming a cake from the first concentrate with filtration means.
  • steam may be applied to the cake.
  • the cake may be re-pulped with a lo pH solution in a re-pulp tank.
  • a system for leaching a metal-sulfide ore may comprise means for providing slurry having metal sulfide ore particles therein, means for subjecting the slurry to a flotation step at a pH level above nine to obtain a first concentrate, means (e.g., a flotation leach reactor) for subjecting the first concentrate to an acidic leach solution, and means for simultaneously subjecting the first concentrate to a flotation step at a pH level below five to obtain a second concentrate and chemically leaching a metal into the acidic leach solution,
  • the means for subjecting the slurry to a flotation step at a pH level above nine may be separate from the means for subjecting the first concentrate to a flotation step at a pH level below five.
  • the means for subjecting the first concentrate to a flotation step at a pH level below five may be configured to operate at or otherwise be held at a different temperature than the means for subjecting the slurry to a flotation step at a pH level above nine.
  • the means for subjecting the first concentrate to a flotation step at a pH level below five may be configured to operate at or otherwise be held at a different pressure than the means for subjecting the slurry to a flotation step at a pH level above nine.
  • the means for subjecting the first concentrate to a flotation step at a pH level below five is configured to operate at or otherwise be held at a different redox potential than the means for subjecting the slurry to a flotation step at a pH level above nine.
  • the means for subjecting the first concentrate to a flotation step at a pH below five may comprise means for controlling redox potential which includes adjusting and maintaining redox potential.
  • the means for subjecting the first concentrate to a flotation step at a pH level below five comprises an agitator and a launder.
  • the means for subjecting the first concentrate to a flotation step at a pH level below five may comprise means for introducing a gas or reagent.
  • the means for subjecting the first concentrate to a flotation step at a pH level below five may be configured to produce a first product containing a gangue material and the second concentrate from the first concentrate.
  • the first product containing a gangue material may be obtained from froth.
  • the system may further comprise a fine- grinding mill configured to receive the second concentrate prior to solvent extraction.
  • the system may comprise means for applying steam directly or indirectly to the first concentrate.
  • the system may comprise filtration means for forming a cake from the first concentrate.
  • the means for applying steam may be configured to apply steam to the cake.
  • the system may comprise a re- pulp tank which is configured for re-pulping the cake in a low pH solution.
  • FIG. 1 is a process flowsheet showing a combined flotation/leaching step after primary flotation according to some embodiments.
  • FIG. 2 is a process flowsheet showing a combined flotation/leaching step after primary flotation according to some embodiments.
  • FIG. 3 is a process flowsheet showing a more detailed depiction of certain downstream portions of the flowsheets shown in FIGS. 2 and 3.
  • Froth produced in a metal leach reaction may be rich in or contain amounts of gangue minerals.
  • a flotation-leach reactor 40 comprising an agitator 44 and launder 46 may be provided and utilized to facilitate the post-flotation preliminary leaching and gangue separations.
  • the reactor 40 may be purposely built in accordance with special design, it may be provided as a leach reactor (e.g., modified to remove froth), or it may be provided as a flotation cell or (whether modified to hold pressure or low pH, or left unmodified).
  • flotation leach reactor 40 By removing gangue minerals via a flotation-leach reactor 40, metal value leaching may progress more efficiently, and at higher solids density in downstream leach reactors 91, 95, 97 of a conventional leach reactor circuit 90.
  • One or more flotation leach reactors 40 may be provided between traditional primary flotation 2 and primary leaching 90 steps for provisional leaching and simultaneous separation of gangue by flotation.
  • Flotation leach reactors 40 may be open to the atmosphere or covered/sealed so as to control gas composition and/or consumption.
  • Flotation leach reactors 40 discussed herein may be heated by heat transfer lines or direct steam injection. Flotation-leach reactors 40 discussed herein may be temperature-adjustable or configured to be held at a flotation-leach temperature which is different (e.g., greater) than the temperature of an upstream conventional flotation step 2. Flotation reagents 45 may be used within one or more flotation leach reactors 40. The reagents 45 may be of the same type or may differ from flotation reagents 1 added to feed 3 in the primary flotation circuit 2. The reagents 45 may be added to a flotation leach reactor 40 to promote the flotation of certain gangue minerals during preliminary leaching.
  • Redox potential within a flotation leach reactor 40 may be controlled by controlling the solution composition (such as the concentration and ratio of Fe(II)/Fe(III)), the sparging of air, the sparging of oxygen-enriched air, the sparging of pure oxygen, or alternatively and/or sparging an inert gas such as nitrogen..
  • the flotation reagents 1 used in the upstream primary flotation process 2 may be removed from value metal-bearing particles in the first concentrate 15.
  • Such reagent-stripping measures render the value metal- bearing particles non-floatable.
  • impurities in the first concentrate 15, such as pyrite and pyrrhotite remain naturally floatable.
  • Such impurities may be selectively removed from the first concentrate 15 by capturing froth within the flotation leach reactor 40, thereby forming a second concentrate 49.
  • Acid leaching conditions may be employed, adjusted, maintained, or otherwise managed to promote the stripping of the flotation reagents 1 from the value metal-bearing minerals within the first concentrate 15, while simultaneously allowing the flotation of gangue fractions within the first concentrate 15.
  • ferric-assisted/catalyzed leaching in sulfuric acid may alone be effective in stripping flotation reagents 1 added during primary flotation 2.
  • Gangue, (in particular, pyrite) which is recovered in launder 60 of the flotation leach reactor 40 during preliminary acid leaching, may be sold as a first product 50, such as a fuel for a roasting operation. If amounts of the first product 50 contain precious metals (such as gold or silver), the precious metals in the first product 50 may be recovered from one or more cyanidation processes used to treat precious metal ores and/or concentrates thereof.
  • a value metal-containing first concentrate 15 is treated by a multi-stage leaching process 90 wherein simultaneous flotation of gangue minerals and oxidative leaching of the value metal-containing minerals takes place simultaneously in the first or otherwise earliest stage of the multi-stage leaching process 90.
  • Selective flotation reagents 47 may also be used to enhance the selective removal of problem gangue minerals like quartz and layered silicates. The selective flotation reagents 47 may be added during the first steps of, or just prior to leaching. Flotation of the first concentrate 15 may occur under leaching conditions to separate the other gangue fraction 48 from the rest of the first concentrate 15 to form a second concentrate 49 having higher content of value mineral(s).
  • the flotation leaching circuit 100 may comprise a typical flotation circuit 2 which receives feed 3 and an amount of flotation reagent 1.
  • the typical flotation circuit 2 may comprise one or more rougher cells 5a-c, one or more cleaner cells 5d, and one or more scavenger cells 5e-f.
  • the typical flotation circuit 2 may comprise slurry delivery means 4 such as a high pH slurrying device or slurry container which feeds a first rougher cell 5a.
  • a first rougher cell 5a may deliver first rougher tails 6a to a second rougher cell 5b and first rougher froth 8a to a cleaner cell 5d.
  • a second rougher cell 5b may deliver second rougher tails 6b to a third rougher cell 5c and second rougher froth 8b to the cleaner cell 5d.
  • a third rougher cell 5c may deliver third rougher tails 6c to a first scavenger cell 5e and third rougher froth 8c to a cleaner cell 5d.
  • Cleaner froth 8d from the cleaner cell 5d may be steam-stripped and/or advance to a filtration step as will be described hereinafter. Cleaner tails 6d from the cleaner cell 5d may be reground and delivered as return/recycle feed 12 to the slurry delivery means 4.
  • a first scavenger cell 5e may send first scavenger tails 6e to a second scavenger cell 5f and first scavenger froth 8e to the return/recycle feed 12.
  • Second scavenger tails 6f from the second scavenger cell 5f may be moved to a tailings 9 disposal.
  • Second scavenger froth 8f may also be delivered as return/recycle feed 12 to the slurry delivery means 4. Regrinding of the first 8e and second 8f scavenger froth may be accomplished with an optional regrind device 10.
  • the cleaner froth 8d may be sent to an optional holding tank 14 which feeds a filter 16, such as a belt filter, with first concentrate 15.
  • Steam delivery means 18 such as a pressurized water tank having a heating element and nozzle may be provided locally to the filter 16.
  • Steam delivery means 18 may provide steam 19 in various amounts, flow rates, temperatures, pressures, and at one or more locations along filter 16 to steam- strip residual high pH flotation reagents from the first concentrate 15.
  • the filter 16 may be configured to produce a steam- stripped, value mineral-laden cake 21, which is dewatered of filtrate 23 containing residual high pH solutions, flotation reagents, and/or residual water from steam 19.
  • the cleaned cake 21 may be added to a re-pulp tank 30 and reconstituted with a low pH solution 27 to form a re-pulped slurry 32.
  • the low pH solution 27 may be stored in a low pH solution tank 25.
  • re-pulping may occur in a flotation leach reactor 40.
  • Re-pulped slurry 32 leaving the re-pulp tank 30 may be sent to one or more flotation leach reactors 40 each having a launder 46 and an agitator 44.
  • flotation leach reactor 40 may be maintained at a pH level below five, for example, between about 0.1 and 4, and preferably under 3.
  • the leach reaction within the flotation leach reactor is a ferric-catalyzed leach reaction.
  • flotation leach reactor 40 may be maintained at a temperature below the boiling point of the slurry for example, between approximately 20°C and 100°C and preferably between approximately 60°C and 80°C.
  • One or more gases 41 such as air, oxygen enriched air, pure oxygen, and/or inert gas or gasses, such as nitrogen, oxygen depleted air, carbon dioxide may be added to a flotation leach reactor 40 at pressures between atmospheric and pressures equal to or above the hydrostatic pressure within the flotation-leach reactor, via gas delivery means 43 such as one or more gas-holding tanks.
  • a flotation-leach reactor 40 may be open to the atmosphere, and in some embodiments, a flotation-leach reactor 40 may be enclosed or otherwise sealed to prevent unnecessary escape or consumption of gas and facilitate gas recycle back to the flotation-leach reactor or recycle to downstream leach reactor(s). If more than one flotation leach reactor 40 is used (e.g., in series), then one or more of the operating conditions described herein may be similar or dissimilar between reactors 40.
  • One or more reagents 45 commonly used in the reverse flotation of gangue minerals may be added to the flotation leach reactor 40, e.g., via one or more reagent tanks 47.
  • pyrite, pyrrhotite, arsenopyrite, , and other gangue such as may be floated and caught in launder 46 during leaching.
  • Overflow froth 48 from the reactor 40 may form a first product 50 which may be sent to a smelter to recover target minerals contained therein (e.g., copper, gold, silver).
  • Overflow froth 48 may also be sent to a grinding circuit (not shown) for further downstream processing, or prepared for tailings disposal.
  • low gangue-containing underflow i.e., second concentrate 49
  • low gangue-containing underflow i.e., second concentrate 49
  • Effluent finely-ground slurry 63 exiting the fine grinding mill may then be sent to a leach reactor circuit 90 and then to an SX/EW circuit 70.
  • Leaching of second concentrate 49 within the leach reactor circuit 90 may efficiently take place without negative side-effects of residual float reagents 1 on solids and/or negative side- effects of surplus gangue.
  • a second product 72 obtained from the SX/EW circuit 70 may comprise more highly-concentrated target minerals (e.g., >95 cathode copper obtained through electrowinning 78) and may be sent to a second product storage tank 80.
  • first product 50 and second product 72 may be combined and sent to the same smelter together. In some instances, first product 50 and second product 72 may be sent to the same smelter independently. In some instances, first product 50 and second product 72 may be sent to different smelters in different product streams altogether.
  • fine-grinding may take place prior to flotation-leaching in flotation leach reactor 40.
  • a fine-grinding mill 60 may receive re-pulped slurry 32 leaving a re-pulp tank 30. Residual flotation reagent 1 remaining with first concentrate 15 particles in the re -pulped slurry 32 may be removed during fine-grinding of said particles.
  • flotation leaching may take place in the flotation reactor 40.
  • Effluent from the flotation reactor 40 may form a second concentrate 49 having a lower gangue content than the first concentrate 15.
  • the second concentrate 49 may be re ground again in another fine-grinding mill 60 (not shown), or sent downstream to a leach reactor circuit 90 and ultimately to a SX/EW plant 70 in a manner similar to FIG. 1.
  • a leach reactor circuit 90 may comprise one or more leach reactors 91, 95, 97.
  • a first leach reactor 91, a second leach reactor 95, and a third leach reactor 97 may be provided in a leach reactor circuit 90.
  • Any one or more of the leach reactors 91, 95, 97 may comprise means 43 for introducing a gas 41, or means 47 for introducing a leach catalyst or reagent 45.
  • the leach reactors 91, 95, 97 may be of the conventional type having agitation means as shown.
  • leach reactors 91, 95, 97 in the circuit 90 may change depending on particle sizes within the second concentrate 49, desired residence time, and nature or method of leaching.
  • the leach circuit 90 may comprise one or more counter-current recycle/feedback streams.
  • flotation leach reactors described herein may also contain one or more froth-removal mechanisms (e.g., a movable rake device or air blow nozzle) in order to aid in the transfer of the froth to the froth collection launder by sweeping the froth outward to the launder 46.
  • froth-removal mechanisms e.g., a movable rake device or air blow nozzle
  • Examples of such froth removal mechanisms may be found in any one or more of US Patent No. 6,926,154, US Patent No. 5,174,973, US Patent No.
  • re-pulp tank 30 may be used to float pyrite or other gangue materials at a low pH and may be provided with a launder or froth removal mechanism. Alternatively, re-pulp tank 30 may be completely replaced or combined with one or more flotation leach reactors 40 described herein. In such instances, cake 21 and low pH solution 27 may be added directly or indirectly to the one or more flotation leach reactors 40.
  • Second product e.g., cathode copper

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Abstract

L'invention concerne un procédé [100] de lixiviation d'un minerai de sulfure de cuivre. Le procédé [100] peut comprendre les étapes consistant à : fournir une suspension épaisse [3] contenant des particules de minerai de sulfure de cuivre ; soumettre la suspension épaisse [3] à une étape de flottaison [2] à un pH supérieur à neuf pour obtenir un premier concentré [15] ; soumettre le premier concentré [15] à une solution de lixiviation acide [27] ; soumettre le premier concentré [15] à une étape de flottaison à un pH inférieur à cinq pour obtenir un second concentré [49] ; et lixivier par voie chimique un métal dans une solution de lixiviation acide [27]. L'invention concerne également un système [100] permettant de lixivier un minerai de sulfure de cuivre. Le système [100] peut comprendre : un moyen [4] permettant d'obtenir une suspension épaisse [3] contenant des particules de minerai de sulfure de cuivre ; un moyen [2] soumettant la suspension épaisse [3] à une étape de flottaison à un pH supérieur à neuf pour obtenir un premier concentré [15] ; un moyen soumettant le premier concentré [15] à une solution de lixiviation acide [27] ; et un moyen soumettant simultanément le premier concentré [15] à une étape de flottaison à un pH inférieur à cinq pour obtenir un second concentré [49] et à lixivier par voie chimique un métal dans la solution de lixiviation acide [27].
PCT/US2014/070354 2013-12-17 2014-12-15 Procédé de lixiviation par flottaison de minéraux de sulfure de cuivre WO2015095054A2 (fr)

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WO2017087498A1 (fr) * 2015-11-16 2017-05-26 Cidra Corporate Services Inc. Utilisation de milieu modifié pour la récupération de minéraux dans un flux de résidus à la fin d'un processus de séparation par flottation
WO2018150093A1 (fr) * 2017-02-15 2018-08-23 Outotec (Finland) Oy Agencement de flottation
US12005460B2 (en) 2022-08-29 2024-06-11 Cidra Corporate Services Llc Utilizing engineered media for recovery of minerals in tailings stream at the end of a flotation separation process

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WO2017066752A1 (fr) * 2015-10-16 2017-04-20 Cidra Corporate Services Inc. Enrichissement de minéraux utilisant des matériaux modifiés pour la séparation des minéraux et la récupération de grosses particules
US10981181B2 (en) 2015-10-16 2021-04-20 Cidra Corporate Services Inc. Mineral beneficiation utilizing engineered materials for mineral separation and coarse particle recovery
WO2017087498A1 (fr) * 2015-11-16 2017-05-26 Cidra Corporate Services Inc. Utilisation de milieu modifié pour la récupération de minéraux dans un flux de résidus à la fin d'un processus de séparation par flottation
US11517918B2 (en) 2015-11-16 2022-12-06 Cidra Corporate Services Llc Utilizing engineered media for recovery of minerals in tailings stream at the end of a flotation separation process
US10913075B2 (en) 2017-02-15 2021-02-09 Outotec (Finland) Oy Flotation arrangement
AU2018221279C1 (en) * 2017-02-15 2020-08-13 Outotec (Finland) Oy Flotation arrangement
AU2018221279B2 (en) * 2017-02-15 2020-05-07 Outotec (Finland) Oy Flotation arrangement
US10960408B2 (en) 2017-02-15 2021-03-30 Outotec (Finland) Oy Flotation arrangement
WO2018150094A1 (fr) * 2017-02-15 2018-08-23 Outotec (Finland) Oy Agencement de flottaison
EA038566B1 (ru) * 2017-02-15 2021-09-15 Оутотек (Финлэнд) Ой Флотационное устройство
EA039726B1 (ru) * 2017-02-15 2022-03-04 Оутотек (Финлэнд) Ой Флотационное устройство
AU2020213386B2 (en) * 2017-02-15 2022-07-14 Outotec (Finland) Oy Flotation arrangement
WO2018150093A1 (fr) * 2017-02-15 2018-08-23 Outotec (Finland) Oy Agencement de flottation
US12005460B2 (en) 2022-08-29 2024-06-11 Cidra Corporate Services Llc Utilizing engineered media for recovery of minerals in tailings stream at the end of a flotation separation process

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