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WO2000037690A1 - Procede de lixivation biologique catalysee a l'argent pour l'extraction du cuivre dans la chalcopyrite en tas - Google Patents

Procede de lixivation biologique catalysee a l'argent pour l'extraction du cuivre dans la chalcopyrite en tas Download PDF

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Publication number
WO2000037690A1
WO2000037690A1 PCT/IB1999/002092 IB9902092W WO0037690A1 WO 2000037690 A1 WO2000037690 A1 WO 2000037690A1 IB 9902092 W IB9902092 W IB 9902092W WO 0037690 A1 WO0037690 A1 WO 0037690A1
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Prior art keywords
leaching
ore
silver
copper
thiobacillus
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English (en)
Inventor
Sharon Young
David Bruce Dreisinger
Jesus Munoz
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University of British Columbia
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University of British Columbia
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Priority to AU30684/00A priority Critical patent/AU3068400A/en
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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
    • C22B15/00—Obtaining copper
    • C22B15/0063—Hydrometallurgy
    • C22B15/0065—Leaching or slurrying
    • C22B15/0067—Leaching or slurrying with acids or salts thereof
    • C22B15/0071—Leaching or slurrying with acids or salts thereof containing sulfur
    • 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
    • C22B3/18—Extraction of metal compounds from ores or concentrates by wet processes with the aid of microorganisms or enzymes, e.g. bacteria or algae
    • 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

  • the present invention is in the field of copper sulfide ore refining processes. More particularly, the bacterial leaching (biohydrometallurgy) of copper from chalcopyrite ores.
  • Chalcopyrite(CuFeS 2 ) is generally regarded as the most common copper-bearing mineral, and the primary component of the most economically important copper ores.
  • the copper content of commercial ore deposits varies widely, from low-grade ores of less than 1% copper to high-grade ores of up to 8% copper.
  • Copper sulfide ores are typically treated by crushing, grinding and concentration by flotation to produce a concentrate. The copper concentrate is then treated by pyro-metallurgical smelting and converting followed by hydro-metallurgical refining.
  • Traditional treatment methods may not, however, be economically justifiable for low-grade ores. There is therefore a long-felt need in the art for an economical method of extracting copper in high yield from deposits of low-grade primary copper sulfide ores.
  • microbiological processes might possibly be utilized to commercially extract copper from low-grade copper sulfide ores.
  • These microbiological processes generally involve the oxidative dissolution of copper from a sulfide mineral by iron-oxidizing bacteria, typically including species of Thiobacilli, particularly Thiobacillus ferrooxidans and Thiobacillus thiooxidans.
  • iron-oxidizing bacteria typically including species of Thiobacilli, particularly Thiobacillus ferrooxidans and Thiobacillus thiooxidans.
  • commercial embodiments of this process simply involved the collection of copper from drainage water originating with copper ore heaps in which microbiological leaching occurred naturally. This natural process is however very slow and produces relatively low total copper yields in terms of the percentage of copper in the ore that is solubilized. This is a particularly acute problem with chalcopyrite ores, since chalcopyrite shows limited response towards chemical or microbiological oxidative dissolution.
  • the resultant ferric sulfate may undergo hydrolysis in the leaching medium according to the following formula:
  • ferric iron Fe 3+
  • ferric iron may attack the chalcopyrite directly, producing elemental sulfur:
  • This sulfur may coat the mineral particles and may result in a diffusion barrier on the mineral surface.
  • Sulfur-oxidizing bacteria may have a beneficial effect on the copper leaching rate by oxidizing the sulfur layer to remove the protective sulfur layer and to allow mineral leaching to proceed:
  • U.S. Patent No. 3,856,913 issued to McElroy et al. 24 December 1974 exemplifies the use of a silver catalyst to enhance bacteriological leaching of pulped chalcopyrite concentrates.
  • the McElroy et al. process includes the initial step of forming a chalcopyrite concentrate pulp, comprising 2% to 60% solids.
  • U.S. Patent No. 3,886,257 issued to Snell 27 May 1975 discloses a process for the treatment of a finely divided (100%- 150 mesh) copper bearing ore concentrate using an acidic, aqueous leaching solution, the claimed improvement to such a process being the addition of a catalytic amount of silver.
  • a final example of the importance of pulp formation to such processes is provided by U.S.
  • Pawlek patent discloses a non-biological process for using silver to rapidly leach copper from very finely ground chalcopyrite concentrate at high temperature and pressure.
  • Pawlek includes the step of comminuting the concentrate down to a pulp having a particle size of 3 ⁇ m or less in the presence of a dispersing agent that inhibits agglomeration of the pulp.
  • the amount of silver disclosed for use is 100 to 4,000 mg Ag/kg chalcopyrite, and preferably 500 to 2000 mg Ag/kg chalcopyrite (equivalent to 0.29 - 11.55 g Ag/kg Cu, preferably 1.44 - 5.77 g Ag/kg Cu).
  • the present invention is addressed to the quite different problem of leaching copper from a static, low-grade chalcopyrite ore heap. The methods of the present invention therefore avoid the significant expenses associated with milling, concentrating and further treatments of a copper-enriched ore concentrate, which may not be justified for low-grade ores.
  • the present invention provides a process for using an economically low concentration of silver catalyst to extract a commercially meaningful proportion of copper from recalcitrant chalcopyrite ores.
  • the present invention provides a method of leaching copper from a chalcopyrite ore comprising adding to the ore a catalytic amount of soluble silver.
  • the catalytic amount being from about 0.25 to about 1.5 g Ag/kg Cu.
  • the catalytic amount may be from about 0.5 to about 1.5 g Ag/kg Cu, or from about 0.75 to about 1.5 g Ag/kg Cu, or about 1 g Ag/kg Cu.
  • a biologically compatible, acidic, aqueous leach solution is circulated (i.e. passed) through the ore in the presence of a sulfide-oxidizing bacterial culture, to form a leaching medium having an oxidation potential of at least about 700 mV (all potentials herein are given with respect to the standard hydrogen electrode).
  • the sulfide-oxidizing bacterial culture may comprise Thiobacillus sp. such as Thiobacillus ferrooxidans or Thiobacillus thiooxidans. Such a culture may be established by inoculating the ore one or more times with appropriate bacteria.
  • An acid such as sulfuric acid
  • the acidic leaching pH may be less than about 2 or about 1.8.
  • Circulation of the leaching medium is continued to extract at least about 40%> of the copper from the ore during a leaching period.
  • the step of circulating the leaching medium may further comprise recirculating the leaching medium repetitively through the ore, either in a batch or continuous process.
  • the acidic leaching pH and the oxidation potential may advantageously be maintained at such preferred levels for substantially all of the leaching period.
  • the temperature of the ore body may be adjusted to a selected temperature to improve leaching, such as a temperature of between about 20 and 40 °C.
  • the size of the ore particles may be modified to facilitate leaching, for example by crushing an ore so that the particle size of the ore is generally less than about 2", or less than about 1" or less than about 1/2".
  • U.S. Patent No. 4,571,387 to Bruynesteyn et al. teaches that thiosulfate may be added to the leaching medium, together with dissolved copper, in order to keep the oxidation potential of the leaching medium reduced to between about 540 to 660 mV.
  • thiosulfate is added to the leach medium in accordance with the present invention while maintaining the oxidation potential of the leach medium above 700 mV.
  • the present invention comprises favouring higher oxidation potentials and maintaining those high potentials for a sufficient period of time to achieve copper recoveries that are on the order of 40%> or better.
  • Figure 1 is a graph showing the percentage of copper extraction over time for K ore in examples 1-10 (designated C 1 -C 10).
  • Figure 2 is a graph showing the pH of the leaching medium over time for K ore in examples 1-10 (designated C1-C10).
  • Figure 3 is a graph showing the oxidation potential (Eh) over time for K ore in examples 1-10 (designated C1-C10), showing in C3-C10 the correlation between allowing the oxidation potential to rise above 700 mV and extraction of at least about 40%) of the copper from the ore during a leaching period in accordance with the invention.
  • Figure 4 is a graph of copper extraction over time for examples 32-34, showing the beneficial effect of thiosulfate on the efficiency of copper extraction where silver is added in a solution containing chloride ions. A similar pattern was observed for corresponding PVD ore examples 28-30, data not shown.
  • Figure 5 is a graph of pH over time for examples 32-34, showing the maintenance of the pH below 2 for substantially all of the leaching period (as was the case with examples 28-30, data not shown).
  • Figure 6 is a graph of oxidation potential (Eh) over time for examples 32-34, showing the rise in potential above 700 mV even in the presence of thiosulfate (as was the case with examples 28-30, data not shown). Day 0 on the graph is the date of silver addition to the ore.
  • Eh oxidation potential
  • Figure 7 is a graph of percent copper extraction over time for examples 11-16, showing the catalytic effect of bacterial inoculum and silver ions, even when added after a considerable period of leaching (compare examples 11 and 12 to the others).
  • Figure 8 is a graph of pH over time for examples 11-16, showing the maintenance of pH ⁇ 2 during most of the leaching period.
  • Figure 9 is a graph of oxidation potential (Eh) over time for examples 11-16, showing the rise of oxidation potential above 700 mV for most of the leaching period.
  • Figure 10 is a graph of percent copper extraction over time for examples 13 and 16, showing the effect of silver addition mode on leaching yield and indicating that silver may be pre-mixed with the ore or added to the top of the ore to obtain leaching yields in excess of 40%>.
  • Figure 11 is a graph of percent copper extraction over time for examples 13-15, showing the influence of pH on extraction yield.
  • Figure 12 is a graph of percent copper extraction over time for examples 11-13 showing the influence of bacterial inoculation and silver addition on copper extraction, indicating that silver and bacterial culture may be added after a considerable period of leaching to obtain final copper yields of at lease about 40%>.
  • Figure 13 is a graph of percent copper extraction over time for examples 17-19, showing the effect of varying silver concentrations on copper yield, and indicating that concentrations as low as 0.25 g Ag/kg Cu may give copper yields in excess of 40%o.
  • Figure 14 is a graph of pH overtime for examples 17-19, showing the maintenance of pH below about 2 for substantially all of the leaching period.
  • Figure 15 is a graph of oxidation potential (Eh) over time for examples 17-19 showing the rise in potential above 700 mV for substantially all of the leaching period.
  • Figure 16 is a graph of percent copper extraction over time for examples 1/2", 1" and 2", showing the influence of particle size on copper extraction.
  • Figure 17 is a graph of pH over time for examples 1/2", 1" and 2", showing the maintenance of the pH below about 2 for substantially all of the leaching period.
  • Figure 18 is a graph of oxidation potential (Eh) over time for examples 1/2", 1" and 2", showing the maintenance of the potential above 700 for substantially all of the leaching period.
  • Figure 19 is a graph of percent copper extraction over time for examples 24-27, showing the effect of delayed silver addition on copper yield.
  • Figure 20 is a graph of pH and oxidation potential (Eh) over time for examples 24- 27, showing the maintenance of pH below about 2 and Eh above 700 mV for substantially all of the leaching period.
  • a catalytic amount of soluble silver to the ore may be carried out in a wide variety of ways.
  • a soluble silver salt such as silver sulfate, may be added in solid form to the ore body. Such solid silver salts may be physically mixed with a portion of the ore body.
  • the silver may be dissolved before it is added to the ore, in which case the solution in which the silver is dissolved may be adapted to optimize delivery of a catalytic amount of silver to the ore.
  • a silver complexing agent such as thiosulfate may be provided in the silver solution to inhibit the formation of silver chloride.
  • All or a portion of the ore may be treated in a chemical activation stage in which the ore is contacted with the soluble silver for a period of time.
  • This contacting step may for example be carried out with agitation in order to facilitate contacting of the ore particles with the silver catalyst.
  • the ore may be treated by acid leaching prior to the addition of the soluble silver in accordance with initiating the process of the invention.
  • the methods of the present invention are accordingly useful for treating ore bodies that have previously been leached using known methods.
  • the ore may also be dried before the initiation of leaching using the methods of the present invention.
  • the process of the invention involves circulating a biologically compatible, acidic, aqueous leach solution through the ore in the presence of a sulfide-oxidizing bacterial culture, to form a leaching medium having an oxidation potential of at least about 700 mV.
  • circulating it is meant that the leach solution passes through the ore.
  • the leach solution may also be re-circulated so that it is passed through the ore multiple times in a batch process, or is continuously re-circulated.
  • biologically compatible it is meant the leaching solution is adapted to support the growth of the bacterial culture in the ore.
  • the leaching solution comprises a nutrient for the sulfide-oxidizing bacteria, such as biologically compatible soluble phosphate salts (such as KH 2 PO 4 ), biologically compatible soluble nitrogen salts (such as (NH 4 ) 2 SO 4 ), biologically compatible soluble potassium salts (such as KC1), biologically compatible soluble magnesium salts (such as MgSO 4 .7 H 2 O), or a biologically compatible soluble calcium salt (such as Ca(NO 3 ) 2 .4 H 2 O).
  • Aeration of the ore body, or of the leaching medium may also be advantageous to provide bacterial nutrients such as elevated levels of dissolved carbon dioxide.
  • the sulfur-oxidizing bacterial culture may be adapted for use with a particular ore by cultivating the bacteria, for example a shake-flask culture, in the presence of the ore. This adaptation may be carried out over several bacterial generations (a generation being a period over which the number of bacterial cells approximately doubles).
  • the bacterial culture may be adapted for use with the silver catalyst by culturing the bacteria in the presence of dissolved silver. In this way a bacterial culture optimized for a particular ore and a particular silver concentration may be developed and maintained for inoculation into the ore. Such inoculations may take place at the onset of the process of the invention or at one or more times during the process.
  • the oxidation potential of the leaching medium is allowed to rise to levels of at least about 700 mV.
  • preferred copper recoveries in accordance with the invention are correlated with allowing the oxidation potential of the leaching medium to rise to such levels.
  • such oxidation potentials facilitate copper recoveries of at least about 40%> of the copper from the ore during a leaching period.
  • significantly higher oxidation potentials may also be maintained to improve copper extraction rates and yields, as shown in the Figures.
  • the present invention recognizes that compounds, such as thiosulfate, should not be added to the leaching medium at concentrations that will have the effect of reducing the oxidation potential below about 700 mV.
  • the present invention is therefore adapted to function in a leaching environment in which adjustment of the oxidation to below 700 mV with compounds such as thiosulfate is not practical or may not be possible.
  • any such reduction of oxidation potential is correlated with reduced copper leaching yields and rates, which may preclude to operation of the process of the invention so as to extract at least about 40%> of the copper from the ore.
  • the leaching medium pH is preferably less than
  • the acid is preferably added to the leaching medium directly, but could be added indirectly by for example adding the acid to the ore while the ore is being washed with the leaching medium.
  • Leaching may be conducted on a continuous basis for a leaching period to extract at least about 40%> of the copper from the ore.
  • the leaching period may be intermittent, interrupted with rest cycles. Such rest cycles may beneficially effect the performance of the bacterial culture.
  • Fresh inoculations of bacteria, or additions of soluble silver may be carried out in conjunction with providing such rest periods in order to optimize the process of the invention for particular ore bodies.
  • the copper dissolved in the leach medium may be recovered by suitable processes known in the art.
  • processes of copper recovery that may be selected by those skilled in this art include solvent extraction, electrowinning, cementation of copper or precipitation of copper as an insoluble salt, as are disclosed in standard texts such as Biswas, A.K. and Davenport, W.G., 1994 Extractive Metallurgy of Copper, (3rd ed), Pergamon Press.
  • copper may be extracted from the leaching solution at any time.
  • the raffinate from such a step may be recirculated as the leaching medium.
  • Example 10 was aerated with air + 1% CO 2 introduced at the bottom of the heap. 6. Silver concentration is given in g Ag/kg Cu. Silver was added as a Ag 2 SO 4 solution.
  • Example 20 which was maintained at a room temperature of approximately 25 °C.
  • Example 20 was irrigated with the solution previously used to irrigate example 10.
  • AS Cu is acid-soluble copper and "Al” is acid insoluble material, as determined by hot 15%) sulfuric acid leach at 73 °C for 5 minutes followed by the addition of a flocculant.
  • each of the ores was crushed to less than approximately 1/2" in particle size and screened for particles greater than about 600 m in diameter (producing a course fraction of the ore).
  • the ores were dried prior to leaching.
  • the moisture content of the ores prior to leaching was in some examples on the order of 0.5%>.
  • the ores were first treated in a chemical activation stage in which the ore is contacted with a solution of silver sulfate (AgSO 4 ) for about 1 hour with agitation. Following chemical activation, the ore may be separated from the silver solution and dried to form an agglomerated ore.
  • the ores were first subjected to an acid leaching pre- treatment to stabilize the pH at the desired level. In some case, such equilibration was carried out for about 7 days, to provide a pH of 1.8 or 1.4 in different examples. Following pH stabilization, the ore may be inoculated with bacterial cultures in exponential phase growth.
  • the composition of the nutrient medium, adjusted to pH 1.4 or 1.8, is given in Table 3.
  • Controls which are not examples of the process of the invention (but which may be important for use by those wishing to make modifications or adaptations of the methods of the invention), were treated with a bactericide solution containing 2 g/L thymol in methanol, 225 ml initially and a monthly dose of 25 ml thereafter.
  • the exemplified leaches were carried out in columns. Leaches 1-10, for example, were carried out in columns 25" high and 3" in diameter, containing approximately 4.4kg of ore and approximately 15L of leach solution. In most examples, a constant temperature of 35 °C was maintained using a water jacket connected to a thermostatic bath or a plastic thermal blanket. The leach solution was passed through the ore sample by gravity and recirculated with a peristaltic pump at about 1.5 ml/min. One example was aerated with air + 1%> CO 2 at 250 ml/min. Two kinds of bacterial cultures were maintained for inoculation, one with silver in the growth medium and one without silver.
  • the cultures grown without silver were maintained by successive transfer of 5 ml aliquots of bacterial inoculum to fresh medium containing 95 ml OK medium at pH 2.0 (dilute sulfuric acid medium) + 5 g ore (K ore or PVD ore as appropriate).
  • the culture grown in the presence of silver was treated similarly, with the exception that the medium contained 14.3 g Ag/kg Cu (about 0.1 ppm Ag).
  • the cell density of the cultures used for inoculation was generally from about lxlO 9 cells/ml to about 4xl0 9 cells/ml.
  • the bacterial cultures used in the PVD experiments were initially grown in the presence of the K ore and then adapted to the PVD ore by successive culturing in similar media as given above, with the exception that PVD ore was substituted for K ore.
  • a silver salt such as silver sulfate
  • a solution containing chloride ions may result in the precipitation of silver chloride.
  • the present invention provides a process for using a soluble thiosulfate, such as ammonium thiosulfate, (NH 4 ) 2 S 2 O 3 , to provide a thiosulfate level effective to reduce the formation of AgCl while not preventing the redox potential of the solution from rising to at least about 700 mV, in accordance with another aspect of the invention.
  • a thiosulfate level of 0.005 M may be used in conjunction with silver at a concentration of approximately 1 g Ag/kg Cu.
  • silver as solid Ag 2 SO 4 may be dissolved in approximately 100 ml of solution containing 0.0741 g (NH 4 ) 2 S 2 O 3 .
  • the thiosulfate is first dissolved in the solution at near neutral pH and the silver salt is then added to the solution with vigorous stirring.
  • thiosulfate is unstable in solutions at pH less than 7, and the decomposition of the thiosulfate anion (S 2 O 3 2" ) in acid solutions may result in the production of free sulfur that is then available to react with the added silver to form solid Ag 2 S, thereby reducing the availability of the silver for catalysis of the leaching process.
  • Examples 28-30 (PVD ore) and 32-34 (K ore) demonstrate that addition of thiosulfate to a silver solution can counteract the effect of the presence of chloride ion in the solution, i.e. counteract the precipitation of silver chloride.
  • Table 1 shows that, in the presence of chloride ion, the addition of thiosulfate to the silver solution improved copper recoveries, i.e. example 30 produced a better yield than example 29 and example 34 produced a better yield than example 33.
  • Examples 28-30 and 32-34 were carried out in 3" x 25" acrylic, water-jacketed columns containing 4.0 kg of non-agglomerated ore and 12-15 L of leach solution.
  • Examples 28-30 and 32-34 were pH stabilized with a 1/10 dilution of the OK nutrient solution at pH 1.8. The chloride concentration in this solution is about 0.00475 g/L.
  • Silver solutions were then added to the examples in three kinds of solution: (1) essentially no chloride and no thiosulfate (examples 28 and 32); (2) chloride but no thiosulfate (examples 29 and 33), and; (3) chloride and thiosulfate (examples 30 and 34).
  • silver was added as solid Ag 2 SO 4 dissolved in approximately 100 ml of: (1) 1/10 OK nutrient solution (about 5 ppm Cl"); (2) plant water containing approximately 0.059 g/L chloride ion (about 59 ppm Cl " ); or (3) plant water containing approximately 0.059 g/L chloride ion plus 0.0741 g (NH 4 ) 2 S 2 O 3 .
  • Silver addition to examples 32-34 was the same except that the chloride ion concentration was about 0.081 g/L instead of 0.059 g/L.
  • examples 28-30 were leached with a solution containing approximately 0.059 g/L chloride ion.
  • examples 32- 34 were leached with a solution containing approximately 0.081 g/L chloride ion.
  • Examples 17, 18 and 19 demonstrate the effect of varying silver catalyst concentrations, showing that yields in excess of 40%> may be obtained using silver concentrations of 0.25, 0.5 and 1.0 g Ag/kg Cu, where extractions are carried out a pH 1.8 (1/10 OK medium) and at 35 °C. These results also show that copper yields may be optimized in some embodiments by using silver concentrations up to 1.0 g Ag/kg Cu.
  • Examples 24-27 demonstrate the effect of adding silver at various times after the initiation of bioleaching: silver was added at a level of 1.0 g Ag/kg Cu to example 24 at 30 days, to example 26 at 60 days and to example 27 at 91 days, and at a level of 1.5 g Ag/kg Cu to example 25 at 30 days. The results indicate that copper extraction may be enhanced after the initiation of leaching by the addition of silver. With the addition of silver to example 24 and example 25 at 30 days, there is a distinct increase in the yield of copper compared to examples 26 and 27, with the higher silver concentration of example 25 providing a slightly better yield than example 24. After silver was added to example 26 at 60 days, there is a positive effect on copper extraction as compared to example 27.
  • test methods and adaptations of the examples herein may be used to routinely test variations in the process of the invention, and to routinely optimize parameters such as soluble silver concentration, ore particle size, leaching pH, bacterial nutrient concentrations or the composition of the bacterial culture.
  • process of the invention may be adapted for use on various scales using known bio-hydrometalurigical technologies.

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Abstract

La présente invention concerne un procédé permettant d'utiliser un catalyseur à l'argent économique de par sa faible concentration pour extraire une proportion commercialement intéressante de cuivre à partir de minerais de chalcopyrite peu commodes. Pendant le traitement de lixivation biologique de l'invention, contrairement à l'état antérieur de la technique, la présente invention consiste à favoriser des potentiels d'oxydation plus élevés d'au moins 700 mV et à conserver ces potentiels élevés pendant assez longtemps pour arriver à des taux d'extraction du cuivre de l'ordre d'au moins 40%.
PCT/IB1999/002092 1998-12-18 1999-12-15 Procede de lixivation biologique catalysee a l'argent pour l'extraction du cuivre dans la chalcopyrite en tas Ceased WO2000037690A1 (fr)

Priority Applications (1)

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AU30684/00A AU3068400A (en) 1998-12-18 1999-12-15 Silver-catalyzed bio-leaching process for copper extraction from chalcopyrite heap

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US21597598A 1998-12-18 1998-12-18
US09/215,975 1998-12-18

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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002061155A1 (fr) * 2001-01-30 2002-08-08 Peko Rehabilitation Project Pty Ltd Bio-oxydation in situ de mineraux sulfures refractaires maigres
WO2002066689A1 (fr) * 2001-02-22 2002-08-29 Pacific Ore Technology (Australia) Ltd Adaptation de bactéries pour la lixivation
WO2002070757A1 (fr) * 2001-03-06 2002-09-12 Pacific Ore Technology (Australia) Ltd Procede destine a la lixiviation en tas assistee sur le plan bacterien de chalcopyrite
AU2002233033B2 (en) * 2001-03-06 2006-03-09 Bioheap Limited A method for the bacterially assisted heap leaching of chalcopyrite
AU2007203317B2 (en) * 2006-07-27 2009-05-21 Jx Nippon Mining & Metals Corporation Method of leaching copper sulfide ores containing chalcopyrite
AU2009251040A1 (en) * 2009-06-16 2011-01-06 Jx Nippon Mining & Metals Corporation Method of leaching copper sulfide ore
WO2017070747A1 (fr) * 2015-10-30 2017-05-04 Technological Resources Pty. Limited Lixiviation en tas
US20190127822A1 (en) * 2017-04-06 2019-05-02 Technological Resources Pty. Limited Leaching Copper-Containing Ores
US10526685B2 (en) 2015-10-30 2020-01-07 Technological Resources Pty. Limited Heap leaching
US10563284B2 (en) 2018-05-09 2020-02-18 Technological Resources Pty. Limited Leaching copper-containing ores
CN115261619A (zh) * 2022-08-29 2022-11-01 安徽省地质矿产勘查局321地质队 一种利用石榴石促进黄铜矿微生物浸出的方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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WO2002061155A1 (fr) * 2001-01-30 2002-08-08 Peko Rehabilitation Project Pty Ltd Bio-oxydation in situ de mineraux sulfures refractaires maigres
WO2002066689A1 (fr) * 2001-02-22 2002-08-29 Pacific Ore Technology (Australia) Ltd Adaptation de bactéries pour la lixivation
WO2002070757A1 (fr) * 2001-03-06 2002-09-12 Pacific Ore Technology (Australia) Ltd Procede destine a la lixiviation en tas assistee sur le plan bacterien de chalcopyrite
AU2002233033B2 (en) * 2001-03-06 2006-03-09 Bioheap Limited A method for the bacterially assisted heap leaching of chalcopyrite
US7022504B2 (en) 2001-03-06 2006-04-04 Bioheap Limited Method for the bacterially assisted heap leaching of chalcopyrite
AU2007203317B2 (en) * 2006-07-27 2009-05-21 Jx Nippon Mining & Metals Corporation Method of leaching copper sulfide ores containing chalcopyrite
US8277538B2 (en) 2009-06-16 2012-10-02 Jx Nippon Mining & Metals Corporation Method of leaching copper sulfide ore
AU2009251040B2 (en) * 2009-06-16 2011-02-24 Jx Nippon Mining & Metals Corporation Method of leaching copper sulfide ore
AU2009251040A1 (en) * 2009-06-16 2011-01-06 Jx Nippon Mining & Metals Corporation Method of leaching copper sulfide ore
WO2017070747A1 (fr) * 2015-10-30 2017-05-04 Technological Resources Pty. Limited Lixiviation en tas
US10526685B2 (en) 2015-10-30 2020-01-07 Technological Resources Pty. Limited Heap leaching
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CN114410983A (zh) * 2015-10-30 2022-04-29 技术资源有限公司 堆浸
US20190127822A1 (en) * 2017-04-06 2019-05-02 Technological Resources Pty. Limited Leaching Copper-Containing Ores
US10563287B2 (en) * 2017-04-06 2020-02-18 Technological Resources Pty. Limited Leaching copper-containing ores
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CN115261619A (zh) * 2022-08-29 2022-11-01 安徽省地质矿产勘查局321地质队 一种利用石榴石促进黄铜矿微生物浸出的方法

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