[go: up one dir, main page]

WO1993004783A1 - Traitement de minerais - Google Patents

Traitement de minerais Download PDF

Info

Publication number
WO1993004783A1
WO1993004783A1 PCT/AU1992/000450 AU9200450W WO9304783A1 WO 1993004783 A1 WO1993004783 A1 WO 1993004783A1 AU 9200450 W AU9200450 W AU 9200450W WO 9304783 A1 WO9304783 A1 WO 9304783A1
Authority
WO
WIPO (PCT)
Prior art keywords
process according
ore
collector
sulphide
pentlandite
Prior art date
Application number
PCT/AU1992/000450
Other languages
English (en)
Inventor
Geoffrey David Senior
William John Trahar
Leanne Kathleen Smith
Peter John Guy
Original Assignee
Commonwealth Scientific And Industrial Research Organisation
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 Commonwealth Scientific And Industrial Research Organisation filed Critical Commonwealth Scientific And Industrial Research Organisation
Priority to AU24911/92A priority Critical patent/AU661714B2/en
Priority to FI940892A priority patent/FI940892A0/fi
Publication of WO1993004783A1 publication Critical patent/WO1993004783A1/fr

Links

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
    • B03D1/02—Froth-flotation processes
    • B03D1/06—Froth-flotation processes differential
    • 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
    • B03D1/001—Flotation agents
    • B03D1/002—Inorganic compounds
    • 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
    • B03D1/001—Flotation agents
    • B03D1/004—Organic compounds
    • B03D1/012—Organic compounds containing sulfur
    • 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
    • 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
    • B03D2201/00—Specified effects produced by the flotation agents
    • B03D2201/007—Modifying reagents for adjusting pH or conductivity
    • 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
    • B03D2201/00—Specified effects produced by the flotation agents
    • B03D2201/02—Collectors
    • 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

  • This invention relates to the processing of nickel deposits, particularly those deposits where the nickel occurs
  • N-ckel occur, in a variety of minerals of which the most economically important is the sulphide mineral pentlandite (Fe,Ni) 9 ⁇ x S 8 .
  • Deposits containing pentlandite usually also contain other sulphides such as pyrrhotite (Fe 1-X S), chalcopyrite (CuFeS 2 ) and pyrite (FeS 2 ) and various non-sulphides including magnesium bearing silicates such as talc.
  • the processing of sulphide nickel deposits currently involves grinding to liberate the nickel sulphides followed by flotation in which gangue minerals are rejected. It is particularly important to reject nearly all of the minerals that contain magnesium because the more MgO there is in a nickel concentrate the higher the temperature for subsequent smelting, owing to the effect whrch magnesia has on slag viscosity. Any increase in smelt-ng temperature increases energy costs and reduces tne llfe of furnace refractories.
  • the approach usually used in flotation is to arrange the chem-cal conditions to be as favourable as possible for the flotation of nickel sulphides and as unfavourable as possible for recovery of magnesium bearing minerals particularly those minerals such as talc which are naturally strongly floatable.
  • copper suiphate is often used to increase the rate of flotation of nickel minerals while polysaccharides such as starches or guar gums are added to suppress the floatability of talc.
  • This strategy produces a highly efficient separation of nickel from non-sulphide minerals with a minimum concomitant loss of nickel.
  • An object of the present invention is to provide a flotation process for the selective rejection of pyrrhotite and optionally for the selective rejection of magnesium bearing minerals from nickel sulphide ores with minimum concomitant loss of nickel recovery.
  • the present invention provides a method for effecting the concentration of pentlandite from a sulphide ore containing pentlandite and pyrrhotite, the method comprising the steps of:
  • the improvement is not the result of any change in particle size distribution, but rather is a consequence of a change in the grinding chemistry which greatly reduces the floatability of pyrrhotite but not that of pentlandite.
  • Stainless steel is far more resistant to corrosion than is mild steel and conditions in mills made of stainless steel are much more oxidising that those in mild steel mills. As a consequence, it is the sulphides rather than the grinding media that oxidise in a stainless steel mill. Mineral-mineral interactions are therefore greatly enhanced compared to those in a mild steel mill and we presume that some such interaction is the reason pyrrhotite floats less strongly.
  • steels that are not highly reactive may be used.
  • An oxygen containing gas such as air may be supplied during grinding to ensure that conditions are not strongly reducing.
  • a mild steel mill with mild steel grinding media and having ports permitting access of air during grinding may be used.
  • a rubber lined mill charged with corrosion resistant steel grinding media could be used.
  • the pH of most nickel flotation pulps ranges from slightly acidic to slightly alkaline and at such pH values sulphides usually float rapidly with collector alone in the absence of any interference from minerals such as talc.
  • the rate of flotation of the sulphides can be increased still further by adding copper sulphate before the collector but once copper sulphate is added it is not possible to select between pentlandite and pyrrhotite.
  • the present invention provides a process for the concentration of pentlandite from a sulphide ore containing petitlandite and pyrrhotite, the process comprising the steps of:
  • the adjustement of the pH to a value greater than about 9 may occur before or after treating the pulp with the collector.
  • the ground are should have an 80 percent passing size less than about 250 ⁇ m.
  • the relatively coarse fraction has a size greater than about 75 ⁇ m.
  • the pulped ore may contain about 20% to 65% solids.
  • alkalis and collectors While many types of alkalis and collectors may be used, soda ash is particularly preferred as the pH modifier and the preferred collector is n-amyl xanthate. Sodium carbonate or lime may also be used as the pH modifier however lime may lead to some loss of selectivity between the sulphides. A mixture of alkalis and of collectors may be used. The water used in this step should have little dissolved copper.
  • the amount of collector and the proportion of the collector added to the coarse fraction need to be determined for each ore, but generally speaking more than half of the collector should preferably be added to the coarse fraction. In our laboratory tests three quarters of the collector was added to the coarse fraction and the other quarter to the fine fraction. This proportion may be varied but it is important that most of the collector is added to the coarse size.
  • the split size for conditioning and the conditioning time need to determined for each particular ore.
  • pulps were wet screened over a 75 ⁇ m sieve and each size fraction was conditioned with collector for 5 minutes.
  • a cyclone or a cylinder-cyclone could be used to classify the pulp.
  • Two stages of classification might also be used to ensure a precise size split. A few minutes of conditioning would probably be sufficient in most cases.
  • a gangue depressant can also be added either during or after split conditioning but such a reagent must be used judiciously because some nickel can be lost if too much is added.
  • a talc depressant such as guar gum may be used, again judiciously. It has been found that the addition of small amounts of Guartec diminishes the extent to which talc slows down the rate of pentlandite flotation. Preferably most of the talc depressant, if used, is added to the fine fraction
  • frother may be used in the flotation step, for example Propylene Glycol.
  • the rate of pentlandite flotation after split conditioning is not quite as rapid as that in the presence of copper sulphate and collector and a longer time is required for flotation. in laboratory tests, flotation times have been up to 16 minutes.
  • a further rejection of non-sulphides in a second stage may be necessary before the concentrate produced by the process of the second aspect is acceptable for smelting.
  • This can be accomplished readily using a method which is in principle very similar to that used in conventional processing.
  • an activator such as copper sulphate and a collector
  • the sulphides can be floated very rapidly while the floatability of the non-sulphides can be suppressed using a suitable depressant.
  • concentrates assaying only about 2 percent MgO can be produced without much additional loss of nickel. Smelters usually require that concentrates assay less than about 4 percent MgO.
  • the invention provides a process in accordance with the second aspect comprising the further step of treating the concentrate produced by process of the second aspect with a collector for sulphides, an activator and optionally a depressant for non-sulphides and subjecting the treated product to froth flotation to produce a sulphide-containing froth.
  • the activator may be copper sulphate. We emphasise here again that while copper sulphate increases the rate of flotation of pentlandite, once it has been added no further selection between pentlandite and pyrrhotite is possible. This is why copper sulphate is not used until after much of the pyrrhotite has been rejected.
  • the depressent may be a talc depressant such as guargum.
  • the amounts of copper sulphate, collector and talc depressant needed are much the same as for conventional processing. In laboratory tests, we have achieved excellent results using 250 g/t of copper sulphate, 150 g/t of amyl xanthate and 550 g/t of the talc depressant Guartec. Other collectors and gangue depressants may also be used. Lowering the pH for the second stage might be advantageous in some circumstances. Sulphuric acid may be a suitable acid to use.
  • the present invention provides a process for the recovery of pentlandite from a sulphide ore containing pentlandite and pyrrhotite wherein the ore is comminuted and subjected to froth flotation in the absence of a collector to produce a talc-containing froth and a sulphide-containing tailing and thereafter subjecting the tailing to one or more sulphide flotation step.
  • the sulphide-containing tailing produced by the process of the fourth aspect may be used as the feed for the processes of the invention in its first, second and third aspects.
  • a second option for handling the talc concentrate is to recycle it to a final stage which is in accordance with the fourth aspect of the present invention where sulphides are floated from talc. Recycling the concentrate in such a manner would provide an opportunity for any floatable nickel to be removed whilst ensuring that the feed to the pyrrhotite rejection stage contains little fast floating talc.
  • a third option is to reject part of the talc concentrate and recycle the rest in the manner just described.
  • treatment is by reverse flotation of cleaned talc concentrate so as to produce a talc product-unfloated fraction-that can be rejected and a sulphide concentrate that can be recycled to the final stage; reagents, and minerals contacted with reagents must be removed from the pre-float circuit.
  • the activator, collector and depressant for non-sulphides used in the final stage may be added in the reverse cleaner instead of being added to the final stage.
  • a pre-float might not be necessary; the floatability of such minerals might be suppressed readily by adding a suitable depressant during sulphide flotation.
  • the ore subjected to the process in accordance with the invention is ground and/or classified so as to minimise particles of a size less than about 10 ⁇ m.
  • the particle size dependence of flotation should be known for each of the ores to be treated. This size dependence can be established by careful sizing of flotation products. Data from such sizings allow the optimum size range for flotation to be determined (see, for example Figure 5).
  • Figure 1 is a general flowsheet showing one arrangement of steps in a process in accordance with the invention
  • Figure 2 is a general flowsheet showing a second arrangement of steps in a process in accordance with the invention.
  • Figure 3 is a general flowsheet showing a third arrangement of steps in a process in accordance with the invention.
  • Figure 4 is a general flowsheet showing a third arrangement of steps in a process in accordance with the invention.
  • Figure 5 is a graph showing recovery-size dependance for one ore using a flotation method in accordance with the invention.
  • N/P/S is a measure of pyrrhotite behaviour and NSG is a measure of the behaviour of all the non-sulphide gangue minerals including talc.
  • Figure 6 is a graph showing Nickel- N/P/S selectivity curves (ratio of average constants) for flotation of an ore ground in an open mild steel mill (test 1) and in a closed stainless stell mill (test 2 ) .
  • Figure 7 is a graph showing Nickel-MgO selectivity curves (ratio of average rate constants) for flotation of an ore ground in an open mild steel mill (test 1) and in a closed steel mill (test 2).
  • FIG. 1 A scheme including the talc pre-float and the first sulphide flotation stage of the second aspect of the invention is shown in Figure 1.
  • the feed ore which has preferably been ground under substantially non-reducing conditions, is supplied to a talc pre-float rougher which may be, for example, a series of Agitair cells.
  • a talc pre-float rougher which may be, for example, a series of Agitair cells.
  • the talc recovered from the pre-float is discarded whilst the sulphide-containing tailings are subjected to split conditioning, that is, the sulphide-containing tailing is separated into a relatively coarse fraction and relatively fine fraction and both fractions are conditioned with potassium n-amyl xanthate, the major proportion of the xanthate being used to treat the coarse fraction, and then the two conditioned fractions are recombined.
  • the conditioned sulphide concentrate is treated in two stages, stage 1 being the first stage of sulphide flotation and stage 2 the second.
  • stage 1 being the first stage of sulphide flotation and stage 2 the second.
  • the conditioned sulphide concentrate is first treated in a stage 1 rougher at pH 9 in the absence of copper sulphate to selectively reject some of the pyrrhotite and recover a pentlandite-containing concentrate.
  • the pentlandite-containing concentrate is then subjected to conventional sulphide flotation in a second stage rougher-cleaner arrangement in the presence of copper sulphate, potassium n-amyl xanthate and a talc depressant such as guartec to produce a final nickel concentrate and tailing streams which are rejected.
  • the tailings from both sulphide flotation stages would be re-cycled or subject to further treatment so as to maximise nickel recovery.
  • the most appropriate place to recycle such streams and the best methods of further treatment need to be determined on a case-by-case basis. For example, for ores that are difficult to grind or v/hich are finely disseminated much of the pentlandite in the tailings might be locked with other minerals. Regrinding of composite particles would therefore be necessary before a further stage of flotation to recover the nickel.
  • Figure 2 illustrates an alternative arrangement of stages in which the talc-containing concentrate floated in the pre-float rougher is subjected to cleaning in a pre-float cleaner and where the tailings are returned to the pre-float rougher and the talc rejected.
  • Figure 3 illustrates another possible arrangement wherein the talc-containing concentrate from the talc pre-float rougher is combined with the sulphide-containing concentrate floated from the stage 1 rougher.
  • Figure 4 illustrates a further possible arrangement in accordance with the invention wherein part of the talc concentrate is rejected in a "reverse cleaner" and the rest is recyced to the final stage of the process where talc is rejected from the sulphides.
  • the sample used was from a nickel deposit containing 2 .38% Ni , 14.5% MgO, 6. 79% S and 13 . 5% Fe .
  • the principal magnesium bearing minerals were talc, magnesite and silicates of the chlorite group. Microprobe analyses showed that none of the gangue minerals contained more than about 0.5% nickel and that most contained much less.
  • Laboratory ball mills constructed of either stainless steel or of mild steel with media of similar type were used to grind the ore. Changing from one mill to the other produced little change in the particle size distribution after grinding. Products from grinding were 80 percent by weight passing about 75 ⁇ m. The ore was ground in 500 gram lots at 67 percent solids using distilled water.
  • a modified Denver laboratory cell was used for flotation Owing to the presence of talc, tests included a 2 minute pre-float in which the only reagent added was a frother. The tailing from this pre-float was then wet-screened over a 75 ⁇ m sieve and the two size fractions separately conditioned with collector before flotation.
  • KnaX potassium n-amyl xanthate
  • KeX potassium ethyl xanthate
  • the frother was polypropylene glycol (Cyanamid Aerofroth 65) made up as a 0.25 percent solution. An initial dose of 2ml of frother solution was added before the talc pre-float and thereafter 2ml per minute was added from an automatic pump to maintain an active froth column.
  • the flotation gas was bottled air (a synthetic mixture of O 2 and N 2 ) and was supplied at a flow rate of 8 litres/minute.
  • the pH was adjusted to 9 and controlled automatically at this value using a dilute sodium hydroxide solution. All water was distilled. Concentrates and tailings were sampled in a standard manner and assayed for Ni, S and MgO.
  • results from the tests are given in Table 1.
  • a and R refer to the cumulative concentrate assay and to the cumulative recovery of each species named. These values include losses to the talc pre-float.
  • the behaviour of the non-pentlandite sulphur (N/P/S) minerals was calculated assuming that pentlandite contains 33.0 percent nickel and 33.0 percent sulphur.
  • pyrrhotite was the predominant sulphide gangue mineral and it is therefore assumed that non-pentlandite sulphur is mostly pyrrhotitic sulphur although it is known that the ore contains some pyrite.
  • the floatability of coarse nickel at pH 9 can be raised by using split conditioning.
  • the collector was divided between two parallel conditioning stages and flotation carried out for 16 minutes.
  • the split conditioning approach was compared with the conventional process using copper stilphate and ethyl xanthate and the results are shown in table 2.
  • Example 2 The first test of Example 1 was repeated but this time a second stage of sulphide flotation was added to reject non-sulphides from the concentrate. This second stage included both roughing and cleaning. The flotation time for the rougher was 8 minutes and for cleaning the time of flotation was 6 minutes. Pulps were conditioned before both the rougher and the cleaner and the order of addition of reagents was as follows:

Landscapes

  • Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Paper (AREA)

Abstract

L'invention se rapporte à un procédé de traitement d'un minerai sulfuré contenant de la pentlandite, de la pyrrhotite et éventuellement du talc. Le minerai est tout d'abord broyé, de préférence dans des conditions non réductrices, puis le minerai broyé est soumis à une pré-flottation du talc, où du talc à flottation rapide peut être récupéré au cours d'un premier stade de flottation sans qu'il se produise de perte excessive de nickel. Les résidus contenant du sulfure, provenant de la pré-flottation du talc, sont ensuite soumis à un traitement divisé suivi d'une flottation en l'absence de sulfate de cuivre afin de faire flotter sélectivement la pentlandite à partir de la pyrrhotite. Le produit de flottation de pentlandite peut ensuite être soumis à un traitement classique de flottation de sulfure en présence d'un activateur tel que le sulfate de cuivre, afin de faire flotter sélectivement les sulfures dans les concentrés.
PCT/AU1992/000450 1991-08-28 1992-08-25 Traitement de minerais WO1993004783A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AU24911/92A AU661714B2 (en) 1991-08-28 1992-08-25 Processing of ores
FI940892A FI940892A0 (fi) 1991-08-28 1992-08-25 Malmien jalostus

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AUPK800491 1991-08-28
AUPK8004 1991-08-28

Publications (1)

Publication Number Publication Date
WO1993004783A1 true WO1993004783A1 (fr) 1993-03-18

Family

ID=3775651

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/AU1992/000450 WO1993004783A1 (fr) 1991-08-28 1992-08-25 Traitement de minerais

Country Status (3)

Country Link
CA (1) CA2116322A1 (fr)
FI (1) FI940892A0 (fr)
WO (1) WO1993004783A1 (fr)

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5795466A (en) * 1995-06-08 1998-08-18 Falconbridge Limited Process for improved separation of sulphide minerals or middlings associated with pyrrhotite
WO2000015346A1 (fr) * 1998-09-15 2000-03-23 M.I.M. Holdings Limited Flotation sans collecteur
WO2003026801A1 (fr) * 2001-09-27 2003-04-03 Outokumpu Oyj Procede de reglage de variation d'alimentation dans un circuit de flottation de mineraux precieux
EP1370362A4 (fr) * 2001-02-28 2004-09-22 Wmc Resources Ltd Ajustement du ph dans la flottation de mineraux de sulfure
US6945407B2 (en) * 1999-11-30 2005-09-20 Wmc Resources Ltd. Flotation of sulphide minerals
AU2002233051B2 (en) * 2001-02-28 2007-03-29 Bhp Billiton Ssm Indonesia Holdings Pty Ltd PH adjustment in the flotation of sulphide minerals
US7314139B2 (en) * 2001-04-12 2008-01-01 Wmc Resources Limited Process for sulphide concentration
AU2005202587B2 (en) * 1999-11-30 2008-07-10 Bhp Billiton Ssm Indonesia Holdings Pty Ltd Improved flotation of sulphide minerals
WO2009086607A1 (fr) * 2008-01-09 2009-07-16 Bhp Billiton Ssm Development Pty Ltd Traitement de sulfures contenant du nickel
CN101850296A (zh) * 2010-06-03 2010-10-06 广西现代职业技术学院 含滑石等硅质矿物较高的高硫铜矿石选铜工艺
EP1622724B1 (fr) * 2003-03-17 2011-06-01 Outotec Oyj Dispositif de flottation differentielle
CN104138793A (zh) * 2014-08-06 2014-11-12 广西龙胜华美滑石开发有限公司 一种含硫铁滑石矿的重选除杂方法
US9028782B2 (en) 2008-01-09 2015-05-12 Bhp Billiton Ssm Development Pty Ltd. Processing nickel bearing sulphides
US9885095B2 (en) 2014-01-31 2018-02-06 Goldcorp Inc. Process for separation of at least one metal sulfide from a mixed sulfide ore or concentrate
CN107670843A (zh) * 2017-10-20 2018-02-09 中国恩菲工程技术有限公司 处理含磁黄铁矿的镍矿石的方法
CN110624698A (zh) * 2019-08-15 2019-12-31 葫芦岛八家矿业股份有限公司 一种从磁选精矿中回收磁黄铁矿的方法
CN115090426A (zh) * 2022-05-05 2022-09-23 中国矿业大学(北京) 一种基于新型抑制剂的锡铅锌多金属矿浮选分离的方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3309029A (en) * 1963-09-09 1967-03-14 Int Nickel Co Activation of sulfide ores for froth flotation
AU2660371A (en) * 1970-03-03 1972-09-21 Western Mining Corporation Limited Improved method forthe concentration of base metal ores containing water soluble metal values
US4256227A (en) * 1979-04-23 1981-03-17 Vojislav Petrovich Froth flotation method for recovering metal values from their ores by thiourea or substituted thiourea
CA1104274A (fr) * 1978-12-04 1981-06-30 Gordon E. Agar Separation des sulfures par oxydation selective
GB2086768A (en) * 1980-03-21 1982-05-19 Inco Ltd Selective flotation of nickel sulphide ores
WO1986006983A1 (fr) * 1985-05-31 1986-12-04 The Dow Chemical Company Nouveaux collecteurs pour le flottage selectif dans de la mousse de mineraux a base de sulfure
WO1989000457A1 (fr) * 1987-07-14 1989-01-26 The Lubrizol Corporation Procede d'enrichissement de minerais contenant du sulfure par flottation par ecumage

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3309029A (en) * 1963-09-09 1967-03-14 Int Nickel Co Activation of sulfide ores for froth flotation
AU2660371A (en) * 1970-03-03 1972-09-21 Western Mining Corporation Limited Improved method forthe concentration of base metal ores containing water soluble metal values
CA1104274A (fr) * 1978-12-04 1981-06-30 Gordon E. Agar Separation des sulfures par oxydation selective
US4256227A (en) * 1979-04-23 1981-03-17 Vojislav Petrovich Froth flotation method for recovering metal values from their ores by thiourea or substituted thiourea
GB2086768A (en) * 1980-03-21 1982-05-19 Inco Ltd Selective flotation of nickel sulphide ores
WO1986006983A1 (fr) * 1985-05-31 1986-12-04 The Dow Chemical Company Nouveaux collecteurs pour le flottage selectif dans de la mousse de mineraux a base de sulfure
WO1989000457A1 (fr) * 1987-07-14 1989-01-26 The Lubrizol Corporation Procede d'enrichissement de minerais contenant du sulfure par flottation par ecumage

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5795466A (en) * 1995-06-08 1998-08-18 Falconbridge Limited Process for improved separation of sulphide minerals or middlings associated with pyrrhotite
WO2000015346A1 (fr) * 1998-09-15 2000-03-23 M.I.M. Holdings Limited Flotation sans collecteur
US6889844B1 (en) 1998-09-15 2005-05-10 Mim Holdings Limited Collectorless flotation
US6945407B2 (en) * 1999-11-30 2005-09-20 Wmc Resources Ltd. Flotation of sulphide minerals
AU2005202587B2 (en) * 1999-11-30 2008-07-10 Bhp Billiton Ssm Indonesia Holdings Pty Ltd Improved flotation of sulphide minerals
EP1370362A4 (fr) * 2001-02-28 2004-09-22 Wmc Resources Ltd Ajustement du ph dans la flottation de mineraux de sulfure
US7028845B2 (en) * 2001-02-28 2006-04-18 Wmc Resources Limited PH adjustment in the flotation of sulphide minerals
AU2002233051B2 (en) * 2001-02-28 2007-03-29 Bhp Billiton Ssm Indonesia Holdings Pty Ltd PH adjustment in the flotation of sulphide minerals
US7314139B2 (en) * 2001-04-12 2008-01-01 Wmc Resources Limited Process for sulphide concentration
WO2003026801A1 (fr) * 2001-09-27 2003-04-03 Outokumpu Oyj Procede de reglage de variation d'alimentation dans un circuit de flottation de mineraux precieux
EP1622724B1 (fr) * 2003-03-17 2011-06-01 Outotec Oyj Dispositif de flottation differentielle
US9028782B2 (en) 2008-01-09 2015-05-12 Bhp Billiton Ssm Development Pty Ltd. Processing nickel bearing sulphides
AU2009203904B2 (en) * 2008-01-09 2013-06-20 Bhp Billiton Ssm Development Pty Ltd Processing nickel bearing sulphides
EA018909B1 (ru) * 2008-01-09 2013-11-29 БиЭйчПи БИЛЛИТОН ЭсЭсЭм ДИВЕЛОПМЕНТ ПТИ ЛТД. Способ выделения никельсодержащих сульфидов из руд
US8753593B2 (en) 2008-01-09 2014-06-17 Bhp Billiton Ssm Development Pty Ltd. Processing nickel bearing sulphides
WO2009086607A1 (fr) * 2008-01-09 2009-07-16 Bhp Billiton Ssm Development Pty Ltd Traitement de sulfures contenant du nickel
CN101850296A (zh) * 2010-06-03 2010-10-06 广西现代职业技术学院 含滑石等硅质矿物较高的高硫铜矿石选铜工艺
US11124857B2 (en) 2014-01-31 2021-09-21 Goldcorp Inc. Process for separation of antimony and arsenic from a leach solution
US9885095B2 (en) 2014-01-31 2018-02-06 Goldcorp Inc. Process for separation of at least one metal sulfide from a mixed sulfide ore or concentrate
US10370739B2 (en) 2014-01-31 2019-08-06 Goldcorp, Inc. Stabilization process for an arsenic solution
CN104138793A (zh) * 2014-08-06 2014-11-12 广西龙胜华美滑石开发有限公司 一种含硫铁滑石矿的重选除杂方法
CN107670843A (zh) * 2017-10-20 2018-02-09 中国恩菲工程技术有限公司 处理含磁黄铁矿的镍矿石的方法
CN110624698A (zh) * 2019-08-15 2019-12-31 葫芦岛八家矿业股份有限公司 一种从磁选精矿中回收磁黄铁矿的方法
CN115090426A (zh) * 2022-05-05 2022-09-23 中国矿业大学(北京) 一种基于新型抑制剂的锡铅锌多金属矿浮选分离的方法
CN115090426B (zh) * 2022-05-05 2023-08-08 中国矿业大学(北京) 一种基于新型抑制剂的锡铅锌多金属矿浮选分离的方法

Also Published As

Publication number Publication date
FI940892A7 (fi) 1994-02-25
CA2116322A1 (fr) 1993-03-18
FI940892L (fi) 1994-02-25
FI940892A0 (fi) 1994-02-25

Similar Documents

Publication Publication Date Title
CA2151316C (fr) Methode pour ameliorer la separation de mineraux sulfures ou les mixtes associes a la pyrrhotite
US4283017A (en) Selective flotation of cubanite and chalcopyrite from copper/nickel mineralized rock
US9475067B2 (en) Chalcopyrite ore beneficiation process and method
CN105903552B (zh) 一种高效回收微细粒钼矿的选矿方法
AU2012379708B2 (en) Method and apparatus for separation of molybdenite from pyrite containing copper-molybdenum ores
WO1993004783A1 (fr) Traitement de minerais
CN111495788B (zh) X射线智能优先选别含铜蓝硫化铜矿石的方法
US4229287A (en) Tin flotation
Bulatovic et al. Selection and evaluation of different depressants systems for flotation of complex sulphide ores
Agar Flotation of chalcopyrite, pentlandite, pyrrhotite ores
Senior et al. The selective flotation of pentlandite from a nickel ore
US7028845B2 (en) PH adjustment in the flotation of sulphide minerals
US3827557A (en) Method of copper sulfide ore flotation
CN115739386B (zh) 一种多金属矿锡石的选矿方法
CA2725223C (fr) Traitement de sulfures contenant du nickel
CA2107963A1 (fr) Traitement des residus de minerai
AU661714B2 (en) Processing of ores
CN115780069B (zh) 一种低品位钼铋硫多金属矿梯级强化浮选高效回收的选矿方法
US3847357A (en) Separation of copper minerals from pyrite
US4515688A (en) Process for the selective separation of base metal sulfides and oxides contained in an ore
Bulatovic et al. Development and application of new technology for the treatment of complex massive sulphide ores case study—Faro lead/zinc concentrator—Yukon
US4650569A (en) Process for the selective separation of base metal sulfides and oxides contained in an ore
US1951326A (en) Process for recovering manganese from ore
US3780860A (en) Flotation of copper sulfide ores
AU2002233051B2 (en) PH adjustment in the flotation of sulphide minerals

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AU CA FI RU

DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
WWE Wipo information: entry into national phase

Ref document number: 2116322

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: 940892

Country of ref document: FI