WO1988001654A1 - Procede de traitement de minerais, de concentres ou de residus de plomb-zinc - Google Patents
Procede de traitement de minerais, de concentres ou de residus de plomb-zinc Download PDFInfo
- Publication number
- WO1988001654A1 WO1988001654A1 PCT/AU1987/000287 AU8700287W WO8801654A1 WO 1988001654 A1 WO1988001654 A1 WO 1988001654A1 AU 8700287 W AU8700287 W AU 8700287W WO 8801654 A1 WO8801654 A1 WO 8801654A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- zinc
- lead
- bath
- fume
- concentrate
- Prior art date
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Classifications
-
- 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
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/04—Obtaining zinc by distilling
-
- 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
- C22B13/00—Obtaining lead
- C22B13/02—Obtaining lead by dry processes
Definitions
- This invention relates to a process for the treatment of lead-zinc complex sulphide ores and concentrates.
- the invention is concerned with a process wriich involves both pyrometallurgical and hydrometallurgical treatments.
- One aspect of the present invention relates to the recovery of zinc, lead and other metal values such as silver, gold and copper from complex sulphide ores or concentrates.
- zinc, lead and other metal values such as silver, gold and copper from complex sulphide ores or concentrates.
- a bath smelting process in which the contents are vigorously agitated by the injection of gas.
- a high-iron matte is produced and the operating conditions are selected to obtain an efficient separation of the lead and zinc from the iron in the feed.
- a process for the treatment of a lead-zinc complex sulphide ore or concentrate which comprises:
- the resulting leachate (principally a zinc sulphate solution) is further processed to recover the zinc, for example by electrowinning to obtain pure zinc metal, or precipitation of basic zinc sulphate, or spray drying to produce zinc oxide.
- the leaching conditions are generally but not always such that the bulk of the sulphide sulphur associated with the zinc is converted to elemental sulphur, the remainder being oxidized to sulphate.
- the Q leaching reaction is carried out in a pressurized reaction vessel so that the oxygen partial pressure is substantially greater than atmospheric pressure.
- Oxygen partial pressures in the range 300-2000 kPa are normally used. Although air can be used as the source of oxygen, it is preferable to use compressed oxygen itself.
- An elevated temperature is also used to increase reaction kinetics. Temperatures in the range 90-230°C can be used.
- the conversion of zinc sulphide to zinc sulphate by reaction with aqueous sulphuric acid in the presence of an oxygen-bearing gas is commonly termed the "oxygen pressure leach process".
- oxygen pressure leaching process it may be preferable to carry out the oxygen pressure leaching process under more aggressive conditions than those noted above so that all the sulphide sulphur is oxidized to sulphate. This normally involves leaching at temperatures in the range 170-230°C. Under these conditions much of the pyrite in the concentrate will be leached.
- the feeds generally used for the oxygen pressure leach process are derived from orebodies that contain zinc sulphide that can be readily recovered in a substantially 0pure form by physical beneficiation techniques such as flotation.
- the zinc sulphide concentrate will typically contain 45-55% zinc with less than a total of 10% of other non-ferrous metals such as lead and copper.
- the residue will also contain any gangue minerals such as silicates in the bulk concentrate and any unreacted sulphide minerals.
- the pyrite in the bulk concentrate is generally unreactive under the conditions used and so reports in the leach residue.
- Another disadvantage of most of the proposed methods for treating the anglesite/plumbojarosite residue is that they do not allow the recovery of the small amount of gold that is often found in bulk concentrates.
- the gold in the bulk concentrate is usually associated with the pyrite in the concentrate.
- the gold is not solubilized during the oxygen pressue leaching process so that it also reports with the anglesite/plumbojarosite residue.
- the bath smelting technique can be applied to leach residues that are produced under a wide variety of leaching conditions.
- the bath smelting technique can be applied to residue that contain varrying amounts of elemental sulphur and sulphate. It is not essential to remove any elemental sulphur from the residue prior to bath smelting, neither is it essential that the residue contain a specified amount of elemental sulphur. This means that the conditions used to leach the bulk lead-zinc concentrate are essentially those that give maximum zinc dissolution under minimum capital and operating cost conditions.
- a process for the treatment of a leach residue obtained from a lead-zinc complex sulphide ore or concentrate said residue containing at least 20% by weight of sulphur and not more than 35% of lead comprising:
- the leach residue is preferably obtained by:
- the lead-zinc fume from the smeljing operation (in either aspect of this invention) can be collected by conventional means and treated to separate the zinc and lead. We have found that leaching with acid results in selective dissolution of the zinc which can then be recovered by electrowinning or other known methods. The lead-rich residue which remains after leaching can be treated to recover the lead, again by known methods.
- the high-iron matte from the smelting operation can be subsequently treated, if desired, to recover the gold, silver and copper values in it.
- FIG. 1 A simplified flowsheet of the first embodiment of the process is shown in Fig. 1 and described below.
- the sulphide ore or concentrate containing zinc and lead, and possibly other metal values such as gold, silver and copper is added to a molten matte bath which is contained in a refractory lined vessel.
- the matte bath is agitated vigorously by means of one or more submerged lances through which fuel and air are introduced in the correct proportion.
- a reductant may be added either separately onto the bath or through the lance.
- the reductant may be the fuel or another material.
- the use of the "SIROSMELT" lance, as described in U.S. Patent No.4,251,271, is particularly preferred in the smelting operation.
- the temperature of the operation depends on the composition of the feed ore or concentrate and is selected to ensure high recoveries of zinc and lead in the fume and to maintain the bath in a molten state. Typically this temperature is 1350-1400°C.
- the gangue can be conveniently separated into a slag phase with the addition of flux if required.
- the quantity of fuel e.g., coal, oil or other hydrocarbon source, injected through the lance is controlled so that the combustion of the fuel provides sufficient heat to allow for the heat requirements of the smelting reactions, melting of the feed, sensible heat of the products and heat losses from the reactor.
- the ratio of air to fuel fed to the lance is also controlled such that the oxygen potential of the gas phase in equilibrium with the matte is at the optimum value.
- the selected combination of air, fuel and reductant feed rates for a specified feed rate of concentrate of ore ensures the simultaneous, high recoveries of lead and zinc in the fume.
- a high-iron matte is produced from the reductive fuming operation.
- the distributions of silver ° and copper between matte, slag and gas are dependent on the feed composition and the operating conditions and their recoveries in the matte increase with the amount of matte formed which in turn increases with the reducing potential of the gas.
- the recoveries of zinc and lead into the fume are high and 89.4% of the silver was recovered in the matte.
- This example illustrates the results for a bulk concentrate containing 31% Zn, 13%Pb, 17.3% Fe, 36.6% S, 0.6% Cu, 0.5% Si02, 280 g/t Ag.
- the concentrate with 10% moisture addition is fed into a matte bath held at 1350°C.
- Fuel plus reductant are injected into the bath through the lance at the rate of 0.328% kg per kg of the wet feed together with air at 3.025 cubic meters per kg of concentrate.
- the reductant could be added directly to the matte bath with the fuel and air being supplied through the lance. 0.26 kg of matte and 0.014 kg of slag are formed per kg of the wet feed. 95% of the zinc and >99% of the lead in the feed are fumed under these conditions.
- Silver 5.0 95.0 94% of the zinc and all of the lead in the feed concentrate were fumed while 99.4% of the copper and 95% of the silver were recovered in the matte.
- Example 3 In another test the concentrate in Example 3 above was mixed with char in the ratio 30.7 g char/100 g of concentrate and dry pellets were prepared. These pellets were continuously charged into the bath of molten matte
- T ⁇ O and 313.7 1 of air 100/g of concentrate were injected into the bath through a lance during a period of 60 minutes.
- the char and air rates were selected to provide the required heat for the smelting reactions and to maintain an oxygen potential of 10 atmospheres in the
- T e mixed fume of zinc and lead is recovered using conventional means, such as a bag house.
- the composition of the fume from the smelting operation depends on the composition of the feed and the operating conditions but typically would contain 25-30% lead and 50-55% zinc assuming 100% collection efficiency.
- the preferred method of processing the lead-zinc fume is by leaching in aqueous sulphuric acid.
- the selective dissolution of the zinc from the lead-zinc fume is typically carried out at 75-95 c C in a conventional agitated leach tank.
- the reaction is generally exothermic and is carried out under controlled pH conditions such that the pH of the resultant leach liquor is typically in the range 3.0-3.5.
- the -pulp density of the slurry being leached depends on the composition of the lead-zinc fume and will usually be such that the resultant zinc sulphate solution will contain 120-170g/litre zinc.
- the solution of zinc sulphate formed by the leaching reaction is separated from the leach residue by conventional solid-liquid separation techniques such as thickening and filtration.
- the leach residue remaining after removal of the zince sulphate solution consists of lead sulphate and other lead-containing solids and any unreacted sulphides that are carried over in the fume.
- the residue can be processed by conventional pyrometallurgical methods for the recovery of lead.
- the zinc sulphate solution produced by leaching the lead-zinc fume can be used to produce various zinc-containing products.
- the solution can be subjected to various purification procedures to remove impurities such as copper, nickel, cobalt, manganese, chloride, cadmium, germanium, etc., prior to zinc recovery by electrowinning.
- a hydrated zinc sulphate can be crystallized from the zinc sulphate solution, basic zinc sulphate can be precipitated by controlled addition of a suitable alkaline reagent, or zinc oxide can be produced by spray drying/roasting techniques.
- Figure 2 is a flowsheet that demonstrates the overall integrated route.
- a bulk concentrate is reground to 80% minus 45 micron, preferably 80% minus 33 micron, if necessary.
- the bulk concentrate is repulped in spent electrolyte from the zinc
- -, c electrowinning circuit which will typically contain 40-60 g/litre zinc and 120-160 g/litre sulphuric acid, while at the same time the free acidity is adjusted such that the total sulphate concentration in solution is equivalent to
- the pulp density of the mixture to be added to the oxygen pressure leach autoclave will typically be in the range 40-70% solids and will typically yield a final leach solution that contains 120-170 g/litre soluble zinc and 10-50 g/litre free sulphuric acid. 5
- lead-zinc fume and bulk concentrate in the appropriate proportions are mixed while being pulped in the spent electrolyte.
- the amounts of lead-zinc fume, bulk concentrate, spent electrolyte, sulphuric acid and process water are adjusted such that composition of the resultant leach solution typically contains 120-170 g/litre zinc and 10-50 g/litre free sulphuric acid.
- Surface active agents may be added.
- bulk concentrate is slurried in recycled process liquor from the alternative zinc recovery circuit and sufficient sulphuric acid added so that the resultant leach liquor will contain the desired amount of excess acid.
- the necessary amount of surface active agents is added to the leach slurry.
- the lead-rich fume produced in the bath smelting of the leach residue is led to a separate leaching circuit where it is reacted on its own with a 5-10% excess of sulphuric acid to produce a zinc sulphate solution.
- Leaching is carried out at atmospheric pressure at a temperature generally in the range 75-95°C such that the pH of the resultant leach liquor is generally in the range 3.0-3.5.
- the leach residue remaining after removal of the zinc sulphate solution consists predominantly of lead sulphate. This can be processed by conventional means.
- the zinc sulphate solution can be processed separately or, preferably, combined with that produced in the initial pressure leaching stage.
- the leach pulp is added to a suitable well-agitated autoclave that is pressurized such that the oxygen partial pressure is maintained in the range 300-1500 kPa and heated to 90-230°C.
- the preferred oxygen partial pressure and temperatures are 500-1000kPa and 140-230°C, respectively. These conditions are maintained for 60-150 minutes, typically 90-120 minutes. During this period more than 90% of the zinc sulphide in the bulk concentrate is converted into soluble zinc sulphate.
- the reacted pulp When leaching is complete the reacted pulp is discharged from the autoclave and the leach residue separated from the zinc sulphate solution by known solid-liquid separation techniques. Alternatively, the reacted pulp may be treated in an appropriate manner such that it is separated into three components, comprising of the bulk of the elemental sulphur formed by the leaching reactions, the lead- and silver-rich leach residue, which also contains unreacted sulphide minerals and other gangue in' the leach pulp, and the zinc sulphate solution. The elemental sulphur is removed from reacted pulp by known methods such as flotation and/or crystallization/filtration and/or dissolution in a suitable organic solvent.
- the zinc sulphate solution is subjected to a range of known purification procedures to remove soluble impurities such as iron, arsenic, copper, cobalt, nickel, chloride, fluoride, antimony, manganese, etc.
- the purified zinc sulphate solution is then subjected to known electrowinning procedures to produce metallic zinc.
- the spent electrolyte is returned to the bulk concentrate leaching circuit where it is used to repulp fresh bulk concentrate.
- the purified zinc sulphate solution is treated in such a manner that a solid zinc-containing product is obtained.
- the zinc sulphate solution may be passed through a spray drier/roaster whereby solid zinc oxide is formed, or the zinc sulphate solution subjected to an evaporation process so that a hydrated zinc sulphate crystallizes out of the mother liquor, or a suitable alkaline reagent, for example, lime, is added to the zinc sulphate solution to precipitate a basic zinc sulphate.
- a spray drier/roaster whereby solid zinc oxide is formed
- the zinc sulphate solution subjected to an evaporation process so that a hydrated zinc sulphate crystallizes out of the mother liquor, or a suitable alkaline reagent, for example, lime, is added to the zinc sulphate solution to precipitate a basic zinc sulphate.
- a suitable alkaline reagent for example, lime
- the leach residue consisting predominantly of anglesite, plumbojarosite, unreacted sulphides, other gangue minerals, as well as elemental sulphur if this has not been removed, is subjected to a bath smelting process, 5 as described above.
- the operating conditions are dependent on the composition of the leach residue, but in general, with high-sulphur residues (20% S or more), reductive fuming at 1250-1300°C gives a good separation between the lead and zinc.
- With the correct choice of the 0 air/fuel reductant ratio 85-98% of the lead in the leach residue feed is removed in the fume while the iron is collected in the matte phase.
- the lead content of the fume is high, typically 60-75%.
- the fume is recovered by conventional means such as a baghouse. The recovery of 5 silver in the matte increases with the weight of matte produced, which in turn increases with the reducing potential of the system.
- This example illustrates the recovery of lead and silver from a leach residue assaying 12.8% Pb, 2.3% Zn, 0.41% Cu, 30.2% Fe, 33% S, 340 g/t Ag, 6.0% silica. Dry
Abstract
Des minerais ou des concentrés complexes de sulfure de plomb-zinc sont traités par un procédé qui consiste: a) à ajouter le minerai ou le concentré à un bain de matte en fusion qui est recouvert d'une couche de scories; b) à agiter et à chauffer le bain par injection submergée d'un combustible et d'air (ou d'un autre mélange de gaz porteur d'oxygène); c) à ajouter au bain un agent réducteur; puis à convertir au moins une proportion substantielle de la teneur en plomb et en zinc du minerai ou du concentré en des vapeurs mélangées de plomb et de zinc et à former une matte à haute teneur en fer dans le bain; et d) à recueillir les vapeurs de plomb-zinc. Ledit procédé peut également s'appliquer au traitement de résidus de lessivage contenant au moins 20 % en poids de soufre et pas plus de 35 % en poids de plomb, par modification du bain à l'étape a) de façon à ce qu'il se compose essentiellement de scories en fusion.
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AUPH7693 | 1986-08-27 | ||
AUPH7694 | 1986-08-27 | ||
AU769486 | 1986-08-27 | ||
AU769386 | 1986-08-27 |
Publications (1)
Publication Number | Publication Date |
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WO1988001654A1 true WO1988001654A1 (fr) | 1988-03-10 |
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Application Number | Title | Priority Date | Filing Date |
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PCT/AU1987/000287 WO1988001654A1 (fr) | 1986-08-27 | 1987-08-25 | Procede de traitement de minerais, de concentres ou de residus de plomb-zinc |
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WO (1) | WO1988001654A1 (fr) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2251252A (en) * | 1990-10-09 | 1992-07-01 | Sumitomo Metal Mining Co | Pyrometallurgical process for refining zinc sulfide concentrates |
EP0557312A1 (fr) * | 1990-11-14 | 1993-09-01 | Minproc Tech | Distillation par sulfidisation directe de zinc. |
WO1998036102A1 (fr) * | 1997-02-17 | 1998-08-20 | Buka Technologies Pty. Ltd. | Raffinage de minerais contenant du sulfure de zinc |
WO2006133777A1 (fr) * | 2005-06-13 | 2006-12-21 | Umicore | Separation des valeurs metalliques dans les residus d'extraction du zinc |
US20150232961A1 (en) * | 2012-09-21 | 2015-08-20 | Matej Imris | Plasma Induced Fuming |
CN114438323A (zh) * | 2022-01-25 | 2022-05-06 | 呼伦贝尔驰宏矿业有限公司 | 一种铁渣、钴渣、铅渣、硫尾矿环保无害化处理方法 |
Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
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AU1819670A (en) * | 1969-09-18 | 1972-02-03 | Bechtel International Corporation | A process fop the submerged smelting of mineral products |
AU5605873A (en) * | 1972-06-26 | 1974-11-28 | Borax Consolidated Limited | Improvements in or relating to zinc and lead smelting |
AU2757677A (en) * | 1977-08-03 | 1979-02-08 | Enaf Empresa Nacional De Fundiciones | Recovery of zinc andother valuable metals from oxide zinc ores and concentrates |
AU3496878A (en) * | 1977-04-12 | 1979-10-18 | Metallgesellschaft Aktiengesellschaft And St. Joe Minerals Corporation | Process for volatising zinc and when present lead |
US4252563A (en) * | 1975-08-25 | 1981-02-24 | Boiden Aktiebolag | Process for the fuming treatment of metallurgical slag |
US4372780A (en) * | 1978-07-13 | 1983-02-08 | Bertrand Madelin | Process for recovery of metals contained in plombiferous and/or zinciferous oxide compounds |
US4612041A (en) * | 1984-09-11 | 1986-09-16 | Sumitomo Heavy Industries, Ltd. | Process for recovering valuable metals from an iron dust containing a higher content of zinc |
AU6152786A (en) * | 1985-08-16 | 1987-02-19 | Ausmelt Pty Ltd | Recovery of zinc, plus silver and lead, as a fume by lancing |
-
1987
- 1987-08-25 WO PCT/AU1987/000287 patent/WO1988001654A1/fr unknown
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AU1819670A (en) * | 1969-09-18 | 1972-02-03 | Bechtel International Corporation | A process fop the submerged smelting of mineral products |
AU5605873A (en) * | 1972-06-26 | 1974-11-28 | Borax Consolidated Limited | Improvements in or relating to zinc and lead smelting |
US4252563A (en) * | 1975-08-25 | 1981-02-24 | Boiden Aktiebolag | Process for the fuming treatment of metallurgical slag |
AU3496878A (en) * | 1977-04-12 | 1979-10-18 | Metallgesellschaft Aktiengesellschaft And St. Joe Minerals Corporation | Process for volatising zinc and when present lead |
AU2757677A (en) * | 1977-08-03 | 1979-02-08 | Enaf Empresa Nacional De Fundiciones | Recovery of zinc andother valuable metals from oxide zinc ores and concentrates |
US4372780A (en) * | 1978-07-13 | 1983-02-08 | Bertrand Madelin | Process for recovery of metals contained in plombiferous and/or zinciferous oxide compounds |
US4612041A (en) * | 1984-09-11 | 1986-09-16 | Sumitomo Heavy Industries, Ltd. | Process for recovering valuable metals from an iron dust containing a higher content of zinc |
AU6152786A (en) * | 1985-08-16 | 1987-02-19 | Ausmelt Pty Ltd | Recovery of zinc, plus silver and lead, as a fume by lancing |
Cited By (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2251252A (en) * | 1990-10-09 | 1992-07-01 | Sumitomo Metal Mining Co | Pyrometallurgical process for refining zinc sulfide concentrates |
US5178667A (en) * | 1990-10-09 | 1993-01-12 | Sumitomo Metal Mining Company Limited | Dry process for refining zinc sulfide concentrates |
GB2251252B (en) * | 1990-10-09 | 1995-01-25 | Sumitomo Metal Mining Co | Pyrometallurgical process for refining mixtures of zinc sulfide and lead sulfide concentrates |
EP0557312A1 (fr) * | 1990-11-14 | 1993-09-01 | Minproc Tech | Distillation par sulfidisation directe de zinc. |
EP0557312A4 (fr) * | 1990-11-14 | 1994-03-30 | Minproc Technology Inc. | |
WO1998036102A1 (fr) * | 1997-02-17 | 1998-08-20 | Buka Technologies Pty. Ltd. | Raffinage de minerais contenant du sulfure de zinc |
WO2006133777A1 (fr) * | 2005-06-13 | 2006-12-21 | Umicore | Separation des valeurs metalliques dans les residus d'extraction du zinc |
EA013690B1 (ru) * | 2005-06-13 | 2010-06-30 | Юмикор | Извлечение ценных металлов из отходов выщелачивания цинка |
US20150232961A1 (en) * | 2012-09-21 | 2015-08-20 | Matej Imris | Plasma Induced Fuming |
US10006100B2 (en) * | 2012-09-21 | 2018-06-26 | Val'eas Recycling Solutions Ab | Plasma induced fuming |
CN114438323A (zh) * | 2022-01-25 | 2022-05-06 | 呼伦贝尔驰宏矿业有限公司 | 一种铁渣、钴渣、铅渣、硫尾矿环保无害化处理方法 |
CN114438323B (zh) * | 2022-01-25 | 2023-09-12 | 呼伦贝尔驰宏矿业有限公司 | 一种铁渣、钴渣、铅渣、硫尾矿环保无害化处理方法 |
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