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WO2001031072A1 - Technique permettant de proceder a une lixiviation biologique avec maitrise du potentiel d'oxydo-reduction - Google Patents

Technique permettant de proceder a une lixiviation biologique avec maitrise du potentiel d'oxydo-reduction Download PDF

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Publication number
WO2001031072A1
WO2001031072A1 PCT/ZA2000/000196 ZA0000196W WO0131072A1 WO 2001031072 A1 WO2001031072 A1 WO 2001031072A1 ZA 0000196 W ZA0000196 W ZA 0000196W WO 0131072 A1 WO0131072 A1 WO 0131072A1
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WO
WIPO (PCT)
Prior art keywords
bioleach
carbon dioxide
slurry
redox potential
concentration
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.)
Ceased
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PCT/ZA2000/000196
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English (en)
Inventor
Anthony Pinches
Mariekie Gericke
Johan Vincent Van Rooyen
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Mintek
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Mintek
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Filing date
Publication date
Application filed by Mintek filed Critical Mintek
Priority to CA002388990A priority Critical patent/CA2388990C/fr
Priority to BR0015071-1A priority patent/BR0015071A/pt
Priority to AU11078/01A priority patent/AU773999B2/en
Priority to MXPA02004178A priority patent/MXPA02004178A/es
Priority to APAP/P/2002/002491A priority patent/AP1479A/en
Publication of WO2001031072A1 publication Critical patent/WO2001031072A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • 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
    • C22B15/00—Obtaining copper
    • C22B15/0063—Hydrometallurgy
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • THIS INVENTION relates to a method of operating a bioleach process
  • it relates to a method of operating a bioleach process for the leaching of a sulfide bearing ore or concentrate slurry.
  • Bioleaching processes employ mixed cultures of microorganisms or bacteria These microorganisms may include low temperature (mesophilic) types which prefer temperatures in the range 30-45 °C, moderately thermophilic types which prefer temperatures in the range 45-60 °C and extreme thermophilic types which prefer temperatures in the range 60-90 °C.
  • Low temperature bacterial cultures are composed of Thiobacillus ferro-oxidans, Thiobacillus thio-oxidans and Leptospirillum ferro-oxidans. These individual bacteria also exhibit optimum activity at different redox potentials. Thus, Leptospirillum exhibits optimum activity at redox potentials of 600-650 mV, while Thiobacillus ferro-oxidans exhibits optimum activity at redox potentials around 450-500 mV.
  • bioleaching bacteria live and grow using solely inorganic nutrients.
  • the bacteria use the oxidation of ferrous iron and sulphur (or sulphide) by oxygen as the energy sources that allow them to grow and survive.
  • other essential nutrients required by the bacteria are carbon dioxide, nitrogen and phosphorus. When all of these individual nutrients are present (in solution) in excess the bacteria are capable of growing at a maximum rate and exhibiting the maximum rates of oxidation of ferrous iron and sulphur.
  • a method of operating a bioleach process for the leaching of a sulfide bearing ore or concentrate including subjecting a bioleach slurry which includes dissolved oxygen, dissolved carbon dioxide, sulphide and microorganisms to a bioleach stage; and controlling the redox potential of the bioleach slurry within a predetermined range.
  • the method may include ensuring that both the dissolved oxygen concentration and the dissolved carbon dioxide concentration in the bioleach slurry remains above respective lower concentration limits, the respective lower concentration limits being selected to ensure that the growth of the microorganisms is not limited by a too low concentration of either the dissolved oxygen or the dissolved carbon dioxide in the bioleach slurry.
  • the redox potential of the bioleach slurry may be controlled within the predetermined range by controlling the concentration of at least one of the dissolved oxygen and the dissolved carbon dioxide in the bioleach slurry.
  • the redox potential of the bioleach slurry is controlled within the predetermined range by controlling the concentration of the dissolved carbon dioxide in the bioleach slurry.
  • the method may also include supplying carbon dioxide and oxygen to the bioleach slurry in the form of carbon dioxide- enriched air. Instead, the carbon dioxide may be supplied as a separate gas stream.
  • the bioleach slurry may be acidic and the method may include supplying carbon dioxide to the bioleach slurry in the form of limestone.
  • the bioleach slurry may include microorganism with enzymes in their cells which are capable of reacting with urea to release carbon dioxide, the method then including supplying carbon dioxide to the bioleach slurry in the form of urea.
  • the dissolved oxygen concentration may be controlled by controlling the rate of air supply to the bioleach slurry, or by controlling the rate of supply of a separate oxygen gas stream.
  • the dissolved carbon dioxide or dissolved oxygen concentration in the bioleach slurry is controlled by maintaining a constant feed rate of carbon dioxide or oxygen to the bioleach slurry, and manipulating the mean pulp residence time in the bioleach stage.
  • the dissolved carbon dioxide or dissolved oxygen concentration in the bioleach slurry is controlled by maintaining a constant feed rate of carbon dioxide or oxygen to the bioleach slurry, and a constant mean pulp residence time in the bioleach stage, and adding ore or concentrate, in a dry solids form, to the bioleach slurry.
  • the supply of additional sulphide solids acts to create an increased demand for oxygen and carbon dioxide, thereby providing a means of controlling the concentration of carbon dioxide or oxygen in the bioleach slurry.
  • the bioleach slurry may be agitated .
  • the dissolved carbon dioxide or dissolved oxygen concentration in the bioleach slurry is controlled by maintaining a constant feed rate of carbon dioxide or oxygen to the bioleach slurry, and by manipulating the agitation of the bioleach slurry, thereby controlling the rate of dissolution of carbon dioxide or oxygen in the slurry.
  • the gas-liquid mass transfer coefficient for carbon dioxide or oxygen is primarily dependent on stirrer speed.
  • the ore or ore concentrate may include pyrite as an undesirable component, in which case the redox potential may be controlled in the range of 380 mV to 450 mV relative to a Ag/AgCI reference electrode, thereby inhibiting leaching of the pyrite while selectively leaching desirable sulphide minerals present in the ore or ore concentrate with a rest potential which is lower than the rest potential of pyrite.
  • the ore or ore concentrate may include chalcopy ⁇ te as a predominant sulphide component, in which case the redox potential may be controlled in the range of 380 mV to 480 mV relative to a Ag/AgCI reference electrode thereby to promote the rate and extent of chalcopy ⁇ te oxidation.
  • the microorganisms may be selected from mesophiies such as
  • Leptospirillum ferro-oxidans moderate thermophiles such as Sulfobacillus and
  • Acidimicrobium species extreme thermophiles such as Sulfolobus and Acidianus species, and mixtures thereof.
  • the lower limit of the concentration of the dissolved carbon dioxide in the bioleach slurry may be at least 0, 1 5 ppm. Typically, the concentration of the dissolved carbon dioxide in the bioleach slurry is maintained at or above at least 0,2 ppm for a moderately thermophilic bacterial culture. The lower limit of the concentration of the dissolved oxygen in the bioleach slurry may be at least
  • the lower limit of the concentration of the dissolved carbon dioxide in the bioleach slurry may be at least 0,6 ppm, typiclly at least 0,7 ppm, for an extremely thermophilic bacterial culture.
  • the lower limit of the dissolved oxygen in the bioleach slurry may be at least 0,5 ppm, typically at least 0,7 ppm, for an extremely thermophilic bacterial culture. It is however to be appreciated that the lower limits for the concentration of the dissolved oxygen and the dissolved carbon dioxide are dependent on factors such as the microorganisms used and the conditions of the bioleach slurry (pH, temperature), and that the appropriate lower limits can be established for each bioleach process by means of routine experimentation.
  • Figure 1 shows a graph of carbon dioxide consumption (i " co2' against bulk concentration of dissolved carbon dioxide ⁇ Q02) ' n a D ' 0,eacn slu rrv of a first sulphide minerals concentrate, resulting from test work as set out in Example 1 below;
  • Figure 2 shows a graph of carbon dioxide consumption ( ⁇ Q ⁇ ⁇ against bulk concentration of dissolved carbon dioxide (C Q2) in a bioleach slurry of a second sulphide minerals concentrate, resulting from test work as set out in Example 1 below;
  • Figure 3 shows a graph of oxygen consumption (r 02 ) against bulk concentration of dissolved oxygen (CQ 2 ) m the bioleach slurry of the second sulphide minerals concentrate, resulting from test work as set out in Example 1 below;
  • Figure 4a shows a graph of redox potential and air flow against time resulting from test work as set out in Example 2 below;
  • Figure 4b shows a graph of redox potential and bulk concentration of dissolved carbon dioxide against time resulting from test work as set out in Example 2 below;
  • Figure 4c shows a graph of redox potential and bulk concentration of dissolved oxygen against time resulting from test work as set out in Example
  • Figure 4d shows a graph of redox potential and oxygen uptake against time resulting from test work as set out in Example 2 below;
  • Figure 4e shows a graph of redox potential and copper concentration against time resulting from test work as set out in Example 2 below;
  • Figure 5a shows a graph of redox potential and oxygen uptake against time resulting from test work as set out in Example 2 below;
  • Figure 5b shows a graph of bulk dissolved oxygen concentration and bulk dissolved carbon dioxide concentration against time resulting from test work as set out in Example 3 below;
  • Figure 5c shows a graph of leached copper concentration and leached iron concentration against time resulting from test work as set out in Example 3 below;
  • Figure 6 shows a graph of oxygen consumption ( ⁇ Q2> against bulk concentration of dissolved oxygen (CQ2> m a bioleach slurry of the second sulphide minerals concentrate, resulting from test work as set out in Example 4 below, and
  • Figure 7 shows a graph of carbon dioxide consumption (r C Q2* against bulk concentration of dissolved carbon dioxide (CQQ 2 ) in a bioleach slurry of the second sulphide minerals concentrate, resulting from test work as set out in Example 4 below.
  • the 2 litre reactor is similar, but with a single 6-blade flat-blade Rushton turbine at the bottom of the stirrer shaft. Aeration was via a sparge pipe situated below the Rushton turbine. The tank was fully baffled. Control of the operating temperature in the reactor was achieved using a temperature controller via a temperature probe and immersion heater in the reactor. For continuous operation, a slurry of fine milled concentrate was fed to the reactor from a feed make-up tank via a peristaltic pump Pulp overflow from the 25 litre reactor was via a gravity overflow to a collection tank. For the 2 litre reactor, the pulp overflow was pumped from the reactor at the same flow rate as the feed slurry via a peristaltic pump.
  • the air supplied to the tank was supplemented, if necessary, with additional carbon dioxide gas.
  • Inlet gas to the reactor and exit gas above the pulp in the reactor were analysed for oxygen and carbon dioxide contents using gas analysers. This allowed the rate at which these gases were consumed in the reactor to be calculated from simple mass balances.
  • the dissolved oxygen content in the pulp was measured using a dissolved oxygen probe.
  • the redox potential and pH of the pulp was determined using probes immersed in the pulp. Copper (and iron) concentrations were obtained by analysis of liquor samples removed from the reactor.
  • the first concentrate was a polymetallic sulphide concentrate containing (by mass) 42% chalcopyrite, 24.5% sphalerite (ZnS) , 1 6% galena (PbS) , 4% pyrite, 2% bornite (Cu 5 FeS 4 ), 2% covelhte (CuS) , the remaining mass comprising predominantly gangue minerals.
  • the second concentrate (concentrate 2) was a predominantly chalcopyrite concentrate containing (by mass) 60% chalcopyrite (CuFeS2> and 20% pyrite (FeS2>. the remaining mass comprising predominantly gangue minerals.
  • the 25 litre reactor was used in this series of tests.
  • the concentrate slurry fed to the bioleach reactor from the feed make-up tank contained 1 0 % (mass basis) of concentrate in an inorganic nutrient solution.
  • This nutrient solution contained (NH 4 ) 2 S0 4 , 3 g/l, K 2 HP0 4 , 0.5 g/l, MgSO 4 ,0.2 g/l and Ca(NO 3 ) 2 , 0.05 g/l.
  • the bioleach reactor was operated under conditions where it was estimated that both oxygen and carbon dioxide would be present at excess concentrations, in other words, that the sulphide oxidation and bacterial growth rates would not be limited by the concentrations of these components.
  • the supply of oxygen and carbon dioxide from the air supply to the reactors into the leach solution occurs by the process of gas-liquid mass transfer. Under steady operating conditions, the rates of oxygen and carbon dioxide gas-liquid mass transfer will be equal to the rates at which these components are consumed by the bacteria to drive the oxidation and growth reactions occurring in the reactor.
  • Equation ( 1 ) represents a concentration difference driving force, where the magnitude of this driving force can be increased by increasing the partial pressure of oxygen in the gas supplied to the reactor, since this will, in turn, increase the value of C Q2*
  • Equations ( 1 ), (2) and (3) can thus be combined to give:
  • the preferred method of control is that based on the control of the carbon dioxide supply, where the process exhibits a higher level of stability.
  • Example 2 a test was carried out using concentrate 1 described in Example 1 above.
  • the feed slurry concentration was 1 0 % and the mean residence time of the pulp in the reactor was 2 days
  • the moderately thermophilic bacterial culture was used at a temperature of 45 °C, and the inorganic nutrient solution used was the same as in Example 1 .
  • the 25 litre reactor was used in this test.
  • FIG. 4A-E The data for this test over a period of 25 days is shown in Figures 4A-E.
  • the data for days 20 to 28 represent the initial period of steady operation where the redox potential is high (575 - 625 mV) .
  • Figures 4B, 4C 4D and 4E show the corresponding data for and copper concentration over the initial high redox potential period.
  • the air flow rate was maintained at 200-230 litres/hour with the inlet air carbon dioxide content fixed at 1 800 ppm. During this period the dissolved oxygen was high with concentrations greater than 2 ppm.
  • the dissolved carbon dioxide concentration was also generally high within the range 0.1 5 to 0.44 ppm.
  • the 2 litre reactor was used in this test.
  • the feed slurry concentration was 1 0 % and the mean residence time of the pulp in the reactor was 1 .25 days.
  • the inorganic nutrient solution used was as described in Example 1 .
  • the objective of this test was to control the redox potential at different set values by mass transfer control on the carbon dioxide supply, while at the same time maintaining the maximum rate of bioleaching possible at the specific redox potential.
  • a platinum and Ag/AgCI reference electrode was immersed permanently in the reactor and connected to a meter and controller.
  • the output from the controller adjusted the impeller stirrer speed to control the mass transfer supply of carbon dioxide thereby maintaining the redox potential at the set point. Where large changes in bioleaching rate were obtained, changes in the airflow rate were also made, but this was done manually. The inlet carbon dioxide content in the air was maintained constant at 2000 ppm.
  • FIG. 5A shows that the rate of bioleaching (oxygen consumption or uptake rate) changed as the redox potential changes within this range.
  • the maximum rate of bioleaching was achieved over the redox potential range 460 to 470 mV, as indicated by the rate of oxygen consumption (Figure 5A) and the concentrations of copper and iron leached (Figure 5C) .
  • the oxidation (oxygen consumption) rate observed under these leaching conditions was very high.
  • the C Q2 and CQ2 values shown in Figure 5B are daily spot measurements. However, more detailed analyses showed that the values of Q and CQ2 exhibited large cyclical (over several hours) changes despite the nominal steady state operating conditions.
  • Example 2 a test was carried out using an extremely thermophilic bacterial culture at 70 °C.
  • a 25 litre reactor was used with the same nutrient solution as described for Test 1 .
  • the mean pulp residence in the reactor was 1 8 days.
  • the feed solids concentration was 5 % .
  • the Examples described above show how the gas-mass transfer control of carbon dioxide advantageously can be used to maintain the dissolved carbon dioxide concentration at or above a critical lower limit as a means of controlling the slurry redox potential at a chosen value.
  • this can be done while simultaneously maintaining the rate of bioleaching at its maximum.
  • the method of the invention allows effective manipulation of a bioleaching process to achieve a desired level of redox potential.
  • the method of the invention provides a mass transfer control strategy that maintains the disolved carbon dioxide concentration at all times at or above its critical lower limit, thereby reducing the redox potential from its normally high level (600 mV) to a low level (430 mV), advantageously achieving stable operation. It is also to be appreciated that, since the leaching rate of chalcopyrite improved significantly at lower redox potential levels, the final control level for mass transfer supply of carbon dioxide that needed to be sustained is significantly higher than that required at the high redox potential levels.
  • Copper sulphide concentrates often contain significant quantities of pyrite (FeS 2 ) - At high redox potentials O 500 mV) the pyrite component will leach rapidly and will significantly contribute to the overall level of oxidation

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Abstract

Cette technique de lixiviation biologique permettant de procéder à la lixiviation de minerai ou de concentrat renfermant un sulfure, consiste à soumettre à une lixiviation biologique une bouillie renfermant de l'oxygène et du dioxyde de carbone dissous, un sulfure et des micro-organismes, ainsi qu'à agir sur le potentiel d'oxydo-réduction de la bouillie pour maintenir cette oxydo-réduction dans une plage prédéterminée.
PCT/ZA2000/000196 1999-10-28 2000-10-23 Technique permettant de proceder a une lixiviation biologique avec maitrise du potentiel d'oxydo-reduction Ceased WO2001031072A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
CA002388990A CA2388990C (fr) 1999-10-28 2000-10-23 Technique permettant de proceder a une lixiviation biologique avec maitrise du potentiel d'oxydo-reduction
BR0015071-1A BR0015071A (pt) 1999-10-28 2000-10-23 Método para operar um processo de biolixiviação com controle de potencial redox
AU11078/01A AU773999B2 (en) 1999-10-28 2000-10-23 A method of operating a bioleach process with control of redox potential
MXPA02004178A MXPA02004178A (es) 1999-10-28 2000-10-23 Procedimiento para operar un proceso de biolixivacion con control del potencial redox.
APAP/P/2002/002491A AP1479A (en) 1999-10-28 2000-10-23 A Method Of Operating A Bioleach Process With Control Of Redox Potential

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
ZA996790 1999-10-28
ZA99/6790 1999-10-28
ZA99/7057 1999-11-11
ZA997057 1999-11-11

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AP (1) AP1479A (fr)
AU (1) AU773999B2 (fr)
BR (1) BR0015071A (fr)
CA (1) CA2388990C (fr)
ES (1) ES2204340B1 (fr)
MX (1) MXPA02004178A (fr)
PE (1) PE20010875A1 (fr)
WO (1) WO2001031072A1 (fr)

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
WO2002070758A1 (fr) * 2001-03-06 2002-09-12 Bhp Billiton Innovation Pty Ltd Lessivage ameliore et a haut rendement de tas biologiques de minerais de cuivre chalcopyrite
WO2003038137A1 (fr) * 2001-10-29 2003-05-08 Technological Resources Pty Ltd Recuperation de cuivre provenant de la chalcopyrite
WO2004072636A1 (fr) * 2003-02-11 2004-08-26 Australian Nuclear Science & Technology Organisation Mesure de la vitesse de variation de la concentration d'oxygene et de la vitesse d'oxydation intrinseque dans un amas de materiaux
WO2005118894A1 (fr) * 2004-06-03 2005-12-15 The University Of British Columbia Processus de lixiviation de concentres de cuivre
AU2002233033B2 (en) * 2001-03-06 2006-03-09 Bioheap Limited A method for the bacterially assisted heap leaching of chalcopyrite
WO2009135291A1 (fr) * 2008-05-06 2009-11-12 The University Of British Columbia Procédé de lixiviation pour concentrés de cuivre contenant des composés d’arsenic et d’antimoine
GB2461743A (en) * 2008-07-11 2010-01-20 Smith & Nephew Medical device or composition comprising at least two inorganic components
RU2467081C1 (ru) * 2011-07-01 2012-11-20 Сергей Юрьевич Абрамовский Колонна для регенерации железоокисляющими микроорганизмами растворов выщелачивания минерального сырья
WO2018202691A1 (fr) * 2017-05-02 2018-11-08 Linnaeus University Procédé de conduite d'un processus de biolixiviation de chalcopyrite
WO2021186376A1 (fr) * 2020-03-18 2021-09-23 Bhp Chile Inc Biolixiviation oxydative de métaux de base
CN119824237A (zh) * 2024-12-31 2025-04-15 中南大学 一种基于氧气环境调控氧化还原电位和自由基效应强化黄铜矿生物浸出的方法
US12503746B2 (en) 2020-03-18 2025-12-23 Bhp Chile Inc. Oxidative heap leaching of base metals

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CN112280980B (zh) * 2020-11-09 2021-08-20 紫金矿业集团股份有限公司 生物堆浸系统调控电位的方法

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Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AP1573A (en) * 2001-03-06 2006-02-15 Bioheap Ltd A method for the bacterially assisted heap leaching of chalcopyrite
WO2002070758A1 (fr) * 2001-03-06 2002-09-12 Bhp Billiton Innovation Pty Ltd Lessivage ameliore et a haut rendement de tas biologiques de minerais de cuivre chalcopyrite
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
US7022504B2 (en) 2001-03-06 2006-04-04 Bioheap Limited Method for the bacterially assisted heap leaching of chalcopyrite
AU2002233033B2 (en) * 2001-03-06 2006-03-09 Bioheap Limited A method for the bacterially assisted heap leaching of chalcopyrite
CN100345985C (zh) * 2001-10-29 2007-10-31 技术资源有限公司 从黄铜矿中回收铜
WO2003038137A1 (fr) * 2001-10-29 2003-05-08 Technological Resources Pty Ltd Recuperation de cuivre provenant de la chalcopyrite
AU2009200400B2 (en) * 2001-10-29 2012-03-01 University Of South Australia Recovery of copper from chalcopyrite
WO2004072636A1 (fr) * 2003-02-11 2004-08-26 Australian Nuclear Science & Technology Organisation Mesure de la vitesse de variation de la concentration d'oxygene et de la vitesse d'oxydation intrinseque dans un amas de materiaux
WO2005118894A1 (fr) * 2004-06-03 2005-12-15 The University Of British Columbia Processus de lixiviation de concentres de cuivre
AP2057A (en) * 2004-06-03 2009-10-21 Univ British Columbia Leaching process for copper concentrates
RU2373298C2 (ru) * 2004-06-03 2009-11-20 Дзе Юниверсити Оф Бритиш Коламбиа Способ выщелачивания медных концентратов
AU2005250064B2 (en) * 2004-06-03 2010-09-09 The University Of British Columbia Leaching process for copper concentrates
US7846233B2 (en) 2004-06-03 2010-12-07 The University Of British Columbia Leaching process for copper concentrates
US8277539B2 (en) 2008-05-06 2012-10-02 The University Of British Columbia Leaching process for copper concentrates containing arsenic and antimony compounds
WO2009135291A1 (fr) * 2008-05-06 2009-11-12 The University Of British Columbia Procédé de lixiviation pour concentrés de cuivre contenant des composés d’arsenic et d’antimoine
GB2461743A (en) * 2008-07-11 2010-01-20 Smith & Nephew Medical device or composition comprising at least two inorganic components
RU2467081C1 (ru) * 2011-07-01 2012-11-20 Сергей Юрьевич Абрамовский Колонна для регенерации железоокисляющими микроорганизмами растворов выщелачивания минерального сырья
WO2018202691A1 (fr) * 2017-05-02 2018-11-08 Linnaeus University Procédé de conduite d'un processus de biolixiviation de chalcopyrite
WO2021186376A1 (fr) * 2020-03-18 2021-09-23 Bhp Chile Inc Biolixiviation oxydative de métaux de base
US20230407435A1 (en) * 2020-03-18 2023-12-21 Bhp Chile Inc Oxidative bioleaching of base metals
US12492449B2 (en) * 2020-03-18 2025-12-09 Bhp Chile Inc. Oxidative bioleaching of base metals
US12503746B2 (en) 2020-03-18 2025-12-23 Bhp Chile Inc. Oxidative heap leaching of base metals
CN119824237A (zh) * 2024-12-31 2025-04-15 中南大学 一种基于氧气环境调控氧化还原电位和自由基效应强化黄铜矿生物浸出的方法

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BR0015071A (pt) 2002-11-26
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ES2204340B1 (es) 2005-01-01
CA2388990A1 (fr) 2001-05-03
AU1107801A (en) 2001-05-08
MXPA02004178A (es) 2003-08-20
AP1479A (en) 2005-10-21
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