EP2697401A1 - Procédé de lixiviation - Google Patents

Procédé de lixiviation

Info

Publication number
EP2697401A1
EP2697401A1 EP12771850.0A EP12771850A EP2697401A1 EP 2697401 A1 EP2697401 A1 EP 2697401A1 EP 12771850 A EP12771850 A EP 12771850A EP 2697401 A1 EP2697401 A1 EP 2697401A1
Authority
EP
European Patent Office
Prior art keywords
leach
leach process
process according
passed
pls
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP12771850.0A
Other languages
German (de)
English (en)
Other versions
EP2697401A4 (fr
Inventor
Craig Geoffrey FITZMAURICE
Shawn Ginn Ming SEET
Jason Alexander FEWINGS
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Bioheap Ltd
Original Assignee
Bioheap Ltd
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
Priority claimed from AU2011901390A external-priority patent/AU2011901390A0/en
Application filed by Bioheap Ltd filed Critical Bioheap Ltd
Publication of EP2697401A1 publication Critical patent/EP2697401A1/fr
Publication of EP2697401A4 publication Critical patent/EP2697401A4/fr
Withdrawn legal-status Critical Current

Links

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
    • 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
    • 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
    • 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 relates to a leach process. More particularly, the process of the present invention is intended to allow the processing of tailings, at least in part through the use of biological oxidation, to extract and optionally recover valuable metals.
  • tailings consist of the remainder of the ore, from which the target or valuable metal(s) have been extracted.
  • the tailings are routinely passed to tailings dumps, dams or ponds on site for long term storage.
  • tailings dumps dams or ponds
  • the particular composition of the tailings dumps, dams or ponds will depend upon the particular ore being processed, and the process steps being used in the processing operation. Very often, a level of the target metal(s) remains in the tailings. Most mineral processing operations run on specific economic guidelines by which they are judged to be profitable. That is, reagent costs and other operating expenses are weighed against increased recoveries of target metals. Inevitably, some level of target metal is left in the waste material that is passed to tailings storage.
  • Tailings storage brings with it a variety of risks, amongst which are acid mine or rock drainage, which is particularly relevant for the wastes produced from sulphide mineral processing.
  • Tailings from gold ore processing may contain cyanide, which carries particular concerns from an environmental perspective. Accordingly, there is a high level of regulation covering how such tailings are disposed of and stored. This regulation further impacts on how these tailings may be further treated.
  • Various factors have caused operators not to pursue attempts to recover this remaining target metal from the tailings.
  • this waste material invariably also contains relatively high levels of iron.
  • the high levels of iron present particular issues in terms of how this is handled in any proposed processing route for the tailings. For example, high iron levels in leach solutions can cause significant issues in solvent extraction and in materials handling.
  • One object of the method and apparatus of the present invention is to overcome substantially the above mentioned problems of the prior art, or to at least provide a useful alternative thereto.
  • a leach process comprising the following steps: i) Passing a metal containing waste material from a mineral processing
  • the leach process of the present invention may further comprise a step in which the PLS from step i) is passed to an iron removal step iii) in which a significant proportion of the iron is removed from the PLS.
  • the leach process of the present invention may still further comprise a step in which the PLS from the iron removal step is passed to a solid liquid separation step prior to being passed to downstream metal recovery.
  • the metal containing waste material is a product of a concentration step iv).
  • the concentration step is preferably a froth flotation step.
  • the concentration step is fed with a ground or milled metal containing material.
  • An underflow from the solid liquid separation step iv) is preferably passed to waste.
  • a proportion of the underflow of the solid separation step iv) is directed as seed to the iron removal step iii).
  • the metal containing waste material is the waste product of a concentration step producing a concentrate for downstream processing, whereby metal is recovered from both the concentrate and the waste from the concentration step in the one process.
  • the metal containing waste material is sourced from a tailings storage facility.
  • the tailings storage facility may be a dump or dam.
  • the metal containing waste material may be passed to a size reduction step or steps before being passed to the biological leach step.
  • a biological heap leach process is combined with the process of the present invention such that leach solutions may be fed therebetween.
  • a portion of the PLS from step i) is passed to the biological heap leach process.
  • At least a portion of a PLS produced in the biological heap leach process is returned to the process of the present invention for downstream metal recovery.
  • the portion of PLS passed to the biological heap leach is prior any iron removal and/or solid liquid separation steps.
  • the portion of PLS passed to the biological heap leach is post any iron removal and/or solid liquid separation steps.
  • the portion of the PLS produced in the biological heap leach process that is returned to the process of the present invention for downstream metal recovery is returned prior to any iron removal and/or solid liquid separation steps.
  • Figure 1 is a schematic representation of a flow-sheet for a prior art bacterial leach of a gold ore
  • Figure 2 is a schematic representation of a flow-sheet for a prior art process of concentration of base metal from a base metal containing ore;
  • Figure 3 is a schematic representation of a mineral processing flow- sheet incorporating a leach process in accordance with the present invention.
  • Figure 4 is a schematic representation of a mineral processing flowsheet incorporating a leach process in accordance with a second embodiment of the present invention.
  • Figure 5 is a graph illustrating the percentage of metal leached during amenability testing on a tailings sample, data used being from tracked solution assays factoring final residue assays;
  • Figure 6 is a graph illustrating the percentage of metal leached during amenability testing on a concentrate sample, data used being from tracked solution assays factoring final residue assays. Best ode(s) for Carrying Out the Invention
  • FIG. 1 there is shown prior art flow sheet 10 for the processing of a gold ore in which a biological leach step is provided.
  • the gold ore flow sheet 10 shows the initial crushing 12 of an ore, after which the crushed ore is passed to a milling step 14 for further size reduction.
  • the ore is in turn passed to a concentration step, for example a froth flotation step 16, that produces a concentrate 18 and tailings 20.
  • the tailings are passed to a tailings dam 22.
  • the concentrate 18 is passed to a biological leach step 24 in which the concentrate is exposed, in an acidic environment, to a population of sulphide oxidising bacteria.
  • the biological leach step 24 produces a pregnant leach solution (PLS) that is passed to a neutralisation step 26 and in turn to a carbon in leach (CIL) circuit 28.
  • the carbon and adsorbed gold from the CIL circuit 28 is passed to an elution or stripping step 30, which in turn leads to the passing of a pregnant solution to an electrowinning (EW) step 32, in turn producing a gold metal product 34.
  • the CIL circuit 28 produces a waste product 36 that is also passed to the tailings dam 22.
  • Such prior art processes might replace the CIL circuit 28 with one containing a carbon in pulp (CIP) circuit, or a circuit that combines CIL and CIP.
  • a base metal containing ore is first passed to the crushing step 12 and in turn to the milling step 14.
  • the crushed and milled ore is in turn passed to the concentration step, for example the froth flotation step 16, that produces a concentrate 52 that contains the target base metal(s), and tailings 20.
  • the tailings 20 are passed to the tailings dam 22.
  • the concentrate 52 is passed to a thickening circuit 54, an underflow from which is filtered in a filtration step 56 to reduce moisture content before a resulting filter cake is dispatched to a smelting step 58.
  • FIG. 3 there is shown a flow sheet for a leach process 70 in accordance with a first embodiment of the present invention. Again, elements of the process 70 are substantially similar to elements of the flow sheets 1 and 50, and like numerals denote like elements or parts.
  • a metal containing waste material or tailings 72 sourced from any one of a variety of mineral processing operations, is passed to a biological leach step 74 in which the tailings 72 are exposed, in an acidic environment, to a population of sulphide oxidising bacteria.
  • the physical condition of the tailings is such that the solids component thereof has a P 8 o of between about 75 ⁇ and 150 Mm.
  • the sulphide oxidising bacteria are capable of operating in at least the range of 50 to 55°C.
  • the sulphide oxidising bacteria utilised are initially adapted to the tailings 72 through exposure thereto, as described in the
  • the sulphide oxidising bacteria utilised in the biological leach step 74 may be provided in the form of a culture in accordance with those described in the Applicant's International Patent Applications PCT/AUOO/01022 (WO 01/018264) or PCT/AU2004/001597 (WO 2005/056842).
  • Relevant bacterial species include, but are not limited to, Suffobacillus
  • thermosulfidooxidans Thiobacillus caldus
  • Thiobacillus ferrooxidans the latter now being Acidthiobacillus species
  • Thermoplasma species are thermosulfidooxidans, Thiobacillus caldus, Thiobacillus ferrooxidans (the latter now being Acidthiobacillus species), and Thermoplasma species.
  • the adaptation of the sulphide oxidising bacteria is conducted in a bacterial farm 75, comprising a series of stirred and oxygenated tanks in which the sulphide oxidising bacteria are exposed to a sample of the tailings 72. After the process of adaptation of those bacteria to the sample of tailings 72 the bacteria are fed to the leach step 74.
  • the bacterial farm 75 operates largely in accordance with that described in the Applicant's International Patent Application PCT/AU2006/000343.
  • the leach step 74 is conducted in a series of agitated tanks at a pH of about 1.8 with a residence time of between about 3 to 50 days, for example 4 to 7 days. During the leach step 74 one or more target metals are extracted into solution, producing a pregnant leach solution (PLS) 76 that contains a desired level of the or each target metal.
  • PLS pregnant leach solution
  • the PLS 76 is passed to an iron removal step 78 in which iron that has been co-extracted during the leach step 74 is precipitated.
  • the iron removal step 78 may be undertaken in a series of stirred tanks, for example a series of six such agitated tanks.
  • This iron removal step 78 may incorporate a final solid liquid separation stage, the underflow from which may in part be re-directed to the beginning of the iron removal step 78 as a seed.
  • the PLS is passed to a solid liquid separation step 80, producing an underflow, or solid product 82, that is passed to a tailings dam 84, and an overflow, or liquid product 86, that still contains a significant proportion of the or each target metal.
  • the remainder of the underflow or solid product of the iron removal step 78 is fed to the solid liquid separation step 80 also.
  • the liquid product 86 of the solid liquid separation step 80 is then passed to a metal recovery circuit, one example of which includes a solvent extraction step 88 followed by an electrowinning step 90, which in turn produces a plated metal product 92.
  • metal recovery includes the option to produce an "intermediate" product that incorporates the or each target metal. Examples of such intermediate products include sulphides or hydroxides products.
  • the tailings 72 may be sourced from any one or more of a variety of appropriate sources, governed only by the specific ' composition of the tailings 72 and its amenability for treatment by way of the . leach process 70. Other factors such as transport requirements and costs will play a role in determining whether certain waste materials are appropriate for treatment by way of the leach process 70.
  • the leach process 70 of the present invention may be combined readily with methods or processes that produce process streams that may be fed thereto.
  • Figure 3 it depicts the tailings 72 as being sourced from a froth flotation concentration step 94.
  • This concentration step 94 forms a part of a generally prior art concentration process 96 in which an ore is first crushed 98 and then milled 100 to produce a feed 102 for the concentration step 94.
  • a concentrate 104 produced thereby is passed to a thickening step 106 and in turn to a filtration step 08, after which the concentrate may be transported, for example by truck 110, to a smelter for further processing.
  • the biological heap leach process 120 comprises in part a crushing plant 122, through which ore may be fed in turn to an agglomeration step 124, the agglomerated ore then being stacked in one or more heaps 126.
  • the bacterial product of the bacterial farm 128 is fed, with any necessary additional acid, nutrients and makeup water, first to a recirculation pond (not shown) before application to the or each heap 126.
  • PLS flowing from the or each heap 126 is fed to one or more leach ponds 130, from which PLS, or optionally intermediate leach solution dependent upon the specific arrangement of heaps and ponds, may be fed back to one or more of the or each heap 126, or may be fed to the process 70 by a line 132 as shown in Figure 3, for example to a point immediately prior to the iron removal step 78.
  • all or a part of the PLS 76 produced by the biological leach step 74 may be passed from a point prior to the iron removal step 78 to the biological heap leach process 120, for example to one or more of the or each leach pond 130, by way of a line 134.
  • the PLS 76 may be passed to the recirculation pond described above. This arrangement provides significant flexibility in the handling of leach solutions in the combination of the leach processes 70 and 120.
  • the flows between the leach processes 70 and 120 need not occur at the same point in those processes.
  • the leach process 70 shown in Figure 3 shows PLS being passed from a point immediately after the biological leach 74 to the or each leach pond 130 of the biological heap leach process 120 and back to that same point
  • the PLS may in fact be passed from another point in the leach process 70 and returned thereto, or in fact returned at yet another point, one example of which will be described hereinafter.
  • the bacteria from the bacterial farm 128 may also be fed to the agglomeration step 124 so as to achieve early inoculation and/or acidification of the ore.
  • solution from one or more of the or each leach solution pond 130 may be fed to the agglomeration step 124 should it be considered appropriate for bacterial inoculation and/or acid balance purposes.
  • FIG. 4 there is shown a flow sheet for a leach process 150 in accordance with a second embodiment of the present invention. Again, elements of the process 150 are substantially similar to elements of the flow sheets 10, 50 and 70, and like numerals denote like elements or parts.
  • the PLS 76 is passed directly to the solid liquid separation step 80, rather than first being passed to the iron removal step 78 as it is in the leach process 70 of Figure 3. Further, a portion 152 of the solid product 82 from the solid liquid separation step 80 is directed to the iron removal step 78 as a seed.
  • a portion of the liquid product 86 of the solid liquid separation step 80 may be directed to the or each leach pond 130 of the biological heap leach process 120 by way of line 154.
  • PLS or optionally intermediate leach solution dependent upon the specific arrangement of heaps and ponds in the biological leach process 120, may be fed to the process 150 by a line 156 as shown in Figure 4, to a point immediately prior to the iron removal step 78.
  • the samples were then crushed to 100% passing 25mm and split using a riffle to provide samples for head assay, mineralogy, and grind establishment/size check, nitric acid digest and bacterial adaptation and amenability.
  • the head assays were conducted to establish the mineral proportions of the samples, which were used as a reference for tracking leaching and when calculating final recoveries of the bacterial amenability test.
  • the mineralogy was performed to determine the physical characteristics and composition of the samples.
  • Grind establishments were conducted on the samples in order to verify the time required to grind the ore to a specific sizing, which was used as a reference when preparing feed requirements or otherwise. A size analysis was conducted on the concentrate to confirm that at least 80% was passing 75um. [0063] 1 5kgs of each sample was split into 3 charges of 500g each. The samples were subjected to different grind times and sized. Grind establishments were conducted in a rod mill using tap water.
  • a saline nickel bacterial culture was selected and developed, see discussion hereinafter, for this test work.
  • the raw water analysis supplied indicated that the water contained approximately 25 g/L CI " (50 g/L TDS) so the culture was adapted to a TDS level of 50 g/L.
  • Mineralogy on the tails sample indicates the sample contains -1.5% nickel sulphides with pentlandite being the dominant sulphide in this sample.
  • the sulphides generally occurred as locked mineral grains with pyrite or pyrrhotite.
  • Grind establishments were conducted on the samples in order to verify the time required to grind the ore to a specific sizing.
  • a 75pm sieve was used for the test work and the grinding time was evaluated based on 80% passing.
  • the tailings sample, as received required 5 minutes 47 seconds grinding time to sufficiently pass through a 75 m sieve, while the concentrate sample (being fine grains) required only 1 minute 2 seconds meeting the required size.
  • Table 2 Table summarizing the grind size and time taken to achieve
  • Figure 4 provides a graph of the percentage of Ni, Co and Fe into solution, having been normalized by final residue assays based assays.
  • the culture adapted to the ore within 10 days and was moved into amenability after 11 days. Nickel then proceeded to leach into solution at a rapid rate reaching 91.52% in 13 days. Nickel leaching then slowed and increases slowed with final nickel extraction reaching 87.41 % based on residues. Leaching of cobalt occurred at a relatively steady rate throughout amenability phase occurring quite slowly, reaching only 32.08% leached based on residues. The amount of Fe leached quickly climbing to 38.94% after 12 days in amenability, but then decreased steadily with final figure reaching 4.75%. It is envisaged that this may be due to the saline conditions of the test causing iron to precipitate out of solution.
  • Figure 5 provides a graph of the adaptation and amenability test on the concentrate sample. The test leached 90.52% of available nickel in 11 days of adaptation, signifying that the culture had adapted to the concentrate.
  • Table 5 Microbial star rating (1-5) and the amount of cells during adaptation testing. [Star rating:1 (10 5 -10 e ), 2 (10 e -10 7 ), 3 (10 7 -10 8 ), 4 (10 8 -10 9 ), 5 (>10 9 ) cells/ mL]
  • Bacterial counts at the start of the adaptation phase gave star ratings of 1.5 for tailings, and 2 for concentrate. Low bacterial counts are expected at the start of new tests as the start-up culture is diluted with nutrient solution, and the population will take time to develop. The significance of increases in population numbers throughout the test shows that the culture is well adapted to the ore and able to proliferate on the feed. Increases in bacterial numbers occur as the tests move into each phase. By the end of adaptation phase bacterial numbers had increased to 2-3 stars for both tests. By the end of amenability, the tailings sample test numbers had reached 5 stars, or >10 9 cells/mL and the concentrate test had reached 3.5 stars, or 10 8 to 10 9 cells/mL.
  • Bacterial numbers at the commencement of each test were 1.5 to 2 stars due to the dilution of the culture upon initiation of the tests. Numbers then increased as the test moved into its later stages and showed good growth and development of the populations in the saline environment with this feed. This indicates that the developed culture sufficiently adapted to the ore and leached the target elements under saline conditions similar to those expected at a commercial operation on site.
  • the biological leach step of the present invention may utilise a culture of sulphide oxidising bacteria as described hereinabove.
  • a culture may also be a mixed bacterial culture.
  • the biological leach step may be conducted using, instead of or in combination with the options already envisaged, populations of Archaea, fungi and/or yeast.
  • the metals recovery circuit of the leach process 70 of the present invention may be provided in a number of different forms, of which the solvent extraction/electrowinning option described is only one.
  • the process may alternatively produce an intermediate product that is forwarded to another facility at which metal production may occur.
  • downstream metal recovery as used herein is to be understood to include the production of an intermediate metal bearing product that may be subsequently processed to produce metal therefrom.
  • Such an intermediate product may, for example, be provided in the form of a hydroxide.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Manufacturing & Machinery (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Metallurgy (AREA)
  • Materials Engineering (AREA)
  • Biochemistry (AREA)
  • Biotechnology (AREA)
  • Microbiology (AREA)
  • Inorganic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Extraction Or Liquid Replacement (AREA)

Abstract

La présente invention se rapporte à un procédé de lixiviation (70) qui comprend les étapes suivantes consistant à : i) passer un métal qui contient un matériau résiduaire (72) d'une opération de traitement de minerais (96) à une étape de lixiviation biologique (74) au cours de laquelle une partie du métal est extraite d'une solution de lixiviation mère (76) ; et (ii) passer la solution de lixiviation mère (76) de l'étape i) à une récupération de métaux en aval.
EP12771850.0A 2011-04-13 2012-04-13 Procédé de lixiviation Withdrawn EP2697401A4 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2011901390A AU2011901390A0 (en) 2011-04-13 Leach Process
PCT/AU2012/000379 WO2012139166A1 (fr) 2011-04-13 2012-04-13 Procédé de lixiviation

Publications (2)

Publication Number Publication Date
EP2697401A1 true EP2697401A1 (fr) 2014-02-19
EP2697401A4 EP2697401A4 (fr) 2015-04-08

Family

ID=47008709

Family Applications (1)

Application Number Title Priority Date Filing Date
EP12771850.0A Withdrawn EP2697401A4 (fr) 2011-04-13 2012-04-13 Procédé de lixiviation

Country Status (7)

Country Link
US (1) US20140127789A1 (fr)
EP (1) EP2697401A4 (fr)
AU (1) AU2012243436C1 (fr)
CA (1) CA2832512C (fr)
CL (1) CL2013002968A1 (fr)
PE (1) PE20140641A1 (fr)
WO (1) WO2012139166A1 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11236407B1 (en) 2020-07-31 2022-02-01 Rio Tinto Technological Resources Inc. Metal recovery by leaching agglomerates of metal-containing material/pyrite
US11286540B2 (en) 2020-07-31 2022-03-29 Rio Tinto Technological Resources Inc. Method of processing a pyrite-containing slurry

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3776826A (en) * 1972-07-19 1973-12-04 Du Pont Electrolytic recovery of metal values from ore concentrates
WO1992016667A1 (fr) * 1991-03-22 1992-10-01 Bac Tech (Australia) Pty. Ltd. Oxydation de sulfures de metal a l'aide de bacteries resistantes a la chaleur
CA2176147C (fr) * 1993-12-03 2002-05-07 William J. Kohr Bio-oxydation de pyrites refractaires
WO1996012826A1 (fr) * 1994-10-25 1996-05-02 Geobiotics, Inc. Procede de bio-oxydation d'une halde de minerai
AUPP655998A0 (en) * 1998-10-16 1998-11-05 Bactech (Australia) Pty Limited Process for bioleaching of copper concentrates
US6110253A (en) * 1998-12-14 2000-08-29 Geobiotics, Inc. High temperature heap bioleaching process
AUPQ265199A0 (en) * 1999-09-03 1999-09-30 Pacific Ore Technology Limited Improved bacterial oxidation of sulphide ores and concentrates
AUPQ468999A0 (en) * 1999-12-15 2000-01-20 Pacific Ore Technology (Australia) Ltd A bacterially assisted heap leach
US7219804B2 (en) * 2003-08-26 2007-05-22 Newmont Usa Limited Flotation processing including recovery of soluble nonferrous base metal values
SE0502471L (sv) * 2005-11-09 2007-05-10 Boliden Mineral Ab Förfarande för biolakning av metallinnehållande sulfidiska material
US7691347B2 (en) * 2007-09-19 2010-04-06 Freeport-Mcmoran Corporation Silica removal from pregnant leach solutions
CN102002588B (zh) * 2010-12-30 2013-05-22 南华大学 一种生物浸矿方法——真菌浸铀

Also Published As

Publication number Publication date
CL2013002968A1 (es) 2014-03-28
AU2012243436C1 (en) 2022-02-03
AU2012243436A1 (en) 2013-04-18
PE20140641A1 (es) 2014-06-22
US20140127789A1 (en) 2014-05-08
CA2832512A1 (fr) 2012-10-18
WO2012139166A1 (fr) 2012-10-18
CA2832512C (fr) 2019-07-16
AU2012243436B2 (en) 2015-01-29
EP2697401A4 (fr) 2015-04-08

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