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WO2000029629A1 - Processus et dispositif de biooxidation - Google Patents

Processus et dispositif de biooxidation Download PDF

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Publication number
WO2000029629A1
WO2000029629A1 PCT/AU1999/000917 AU9900917W WO0029629A1 WO 2000029629 A1 WO2000029629 A1 WO 2000029629A1 AU 9900917 W AU9900917 W AU 9900917W WO 0029629 A1 WO0029629 A1 WO 0029629A1
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WO
WIPO (PCT)
Prior art keywords
reactor
slurry
diffuser
oxidation
concentrate
Prior art date
Application number
PCT/AU1999/000917
Other languages
English (en)
Inventor
Mike Rhodes
Paul Charles Miller
Richard Winby
Original Assignee
Bactech (Australia) Pty. 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
Application filed by Bactech (Australia) Pty. Ltd. filed Critical Bactech (Australia) Pty. Ltd.
Priority to AU11414/00A priority Critical patent/AU1141400A/en
Priority to CA002350476A priority patent/CA2350476A1/fr
Priority to MXPA01005009A priority patent/MXPA01005009A/es
Priority to US09/831,579 priority patent/USH2140H1/en
Publication of WO2000029629A1 publication Critical patent/WO2000029629A1/fr

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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
    • 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
    • C22B3/02—Apparatus therefor
    • 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 bio-oxidation processes and reactors for the liberation of metals from minerals, especially sulphides, containing them.
  • Metal containing minerals may be oxidised using specific types of micro-organism, especially bacteria in a bioextraction, particularly a bio-oxidation process. Oxidation of sulphide minerals may be used to put the metals into solution, from for example iron, copper, zinc, nickel and cobalt sulphides, or to release precious metals, such as gold, silver and platinum, encapsulated in metal sulphides, particularly in refractory ores. The process is known as bacterial oxidation, bioextraction, bio-oxidation, bioleaching, or bacterial leaching.
  • pyrite, an iron sulphide, and arsenopyrite, an iron- arsenic sulphide are the most common minerals occluding gold in the so-called refractory gold ores and treatment of such materials by microorganisms may therefore assist in liberation of precious metals from refractory ores containing them.
  • bacteria used in such processes include the mesophiles, Thiobacillus ferrooxidans, Thiobacillus thiooxidans, Leptospirillum ferrooxidans, moderate thermophiles, and thermophiles such as Sulpholobus.
  • the tanks are typically 9 metres high and 9 metres diameter and agitated with axial flow impellers which are driven by large motors. Compressed air is piped into the tank and sheared by the impellers into a fine dispersion of bubbles to maintain a desired dissolved oxygen concentration in the slurry.
  • a variety of impeller types other than axial flow may be used such as turbines.
  • the present invention provides, in its first aspect, a process for recovering metals from materials containing them by bio-oxidation including treating, in a non-mechanically agitated reactor, a slurry containing a metal containing material with bacteria capable of promoting extraction of metals from said metal containing material; and maintaining said material in suspension and bacterial viability in the reactor by introducing an oxygen-containing gas to the slurry within the reactor by aeration means.
  • the aeration means advantageously introduces gases to the reactor in the form of bubbles of controlled size, generally of small diameter to enhance mass transfer of oxygen to bacteria. It will be understood, in this respect, that the bacterial oxygen demand is extremely high and oxygen diffusion characteristics important. Control of bubble size by shearing is not employed.
  • Suitable aeration/agitation means may particularly and advantageously include diffusers as described hereinbelow.
  • Diffusers are devices that will both introduce air or other gases to the slurry by diffusion mass transfer of gas from fine bubbles- advantageously of controlled size-to the solution or slurry and maintain solids in suspension for bacterial oxidation.
  • Dome, tubular, disc or doughnut type diffusers may appropriately be used in accordance with the invention.
  • Aeration means may include hydraulic shear devices. In such devices, very fine bubbles are formed by dislodgment thereof before full development under the influence of shear forces.
  • Surface aerators such as paddle aerators may be used to break liquid surface and assist in entrainment of gas such as air in the bulk reaction slurry.
  • Reactor configuration may be varied to maximise aeration.
  • a further alternative would be the use of liquid jets where a stream of liquid from a reactor is pumped through a venturi which draws air into the liquid thereby aerating it. The aerated liquid is returned to the reactor.
  • a gas appropriate for maintenance of bacterial viability include oxygen containing gases, such as air, oxygen enriched air or oxygen; optionally, with addition of carbon dioxide, such as air enriched with carbon dioxide, may be introduced to the aqueous solution by aeration means, particularly diffusers.
  • chemolithotrophic bacteria may be employed.
  • Various categories of bacteria may be employed in these processes. These categories are as follows:
  • thermophiles which oxidise from above 50°C to 90°C.
  • the process may be carried out employing any one or more such microorganisms, especially bacterial species, often referred to as a single or mixed culture respectively, which will oxidise sulphides or other minerals or metal containing materials in the required temperature range.
  • Preferred mesophiles for use in bacterial oxidation are Thiobacillus ferrooxidans, Thiobacillus thiooxidans and Leptospirillum ferrooxidans.
  • Most of the moderate thermophiles do not have specific names, but some have been referred to as Sulphobacillus thermooxidans.
  • the thermophilic bacteria will be of the type Sulpholobus brierleyi, Sulpholobus BC, and Sulpholobus acidocaldarius.
  • the process may be employed exclusively for metal liberation, pre- or post- treatment by other metallurgical operations, such as CIP or CIL processes for recovery of precious metals for example, may be employed where desirable.
  • Solid/liquid separation may typically follow bio-oxidation, liquor being further treated for metal recovery.
  • the process may be conducted in any suitable reactor, including those types of reactor already generally known to the art, operating advantageously on a continuous basis.
  • Aeration may be achieved by including, in such reactors, suitable aeration means even in large capacity systems.
  • the metal containing material is, for example, a non-ferrous base metal sulphide ore, such as a copper, nickel, zinc, lead or cobalt containing ore, including mixed or polymetallic ores, or a refractory gold ore incorporating occluding sulphides amenable to dissolution by bacterial action.
  • Other materials in this class may include flotation concentrates, gravity concentrates, tailings, precipitates, mattes and sulphidic fume.
  • the above process is also suitable for carrying out bacterial oxidation and bioleaching of non-sulphide ores and other generally inorganic materials containing metals in economic concentrations, where suitable bacteria are available to carry out the process.
  • bioleaching of rare earth ores, oxidic manganese ores and phosphate rock is possible in accordance with process of the invention.
  • a reactor system for bio-oxidation treatment of metal containing materials including at least one rakeless reactor having a reaction volume provided with aeration means for introducing an oxygen containing gas for maintaining said metal containing material in suspension and bacterial viability.
  • the reactor may take various forms, though incorporates no mechanical means of agitating the reactor volume, and may for example be in the form of tanks or vats.
  • the reactor may be fabricated from suitable materials, steel, metal alloys or concrete optionally lined with an acid resistant medium. Additional materials of construction include wood, plastic, fibre-glass or any suitable aeration means may be as known in the art.
  • a reactor may take a reservoir configuration being formed by excavation above or below ground.
  • the reservoir may be lined with a liquid impermeable barrier, such as clay or plastic membrane, to prevent solution entering the surrounding ground or rock.
  • the reactor may be built from rock or other suitable material above the surrounding ground surface.
  • the reactor is preferably rectangular in plan section.
  • the reactor may be tapered towards either end. When viewed from an end the reactor may also be rectangular in section though other shapes may be employed.
  • the walls of the reactor may be substantially vertical or sloped.
  • the depth of the reactor may typically be between 4 and 8 metres, and the width between 5 and 20 metres though both dimensions could be larger or smaller.
  • Very large reactors possibly having length greater than 100 metres, may be built and a number of reactors may be employed. Such reactor systems may be combined in series or operated in parallel.
  • the base of the reactor may be sloped so that there is a gradient from the feed end at which ore or other metal containing material is fed into the reactor to the discharge end. This slope may be a descending slope.
  • the gradient of the reactor may be variable. This may assist in transfer of particles from feed to discharge. Volume of the reactor is calculated in dependence upon the rate at which the metal containing material or mineral is being treated.
  • Aerating means, or diffusers may be located at even spacings along the base of the reactor.
  • a concentration of diffusers may be determined as a function of oxygen demand in the reactor.
  • Feed may be introduced at one end of the reactor through multiple points located along the width of one end. Distribution of slurry to these points may be via a ring main or splitter of conventional type.
  • Figure 1 is a side sectional view of an aeration means to be used in accordance with a first embodiment of the process of the present invention
  • Figure 2 is a plan view of the aeration means shown in side section in Figure 1 ;
  • Figure 3 is a side sectional view of an aeration means to be used in accordance with a second embodiment of the process of the present invention
  • Figure 4 is a plan view of the aeration means shown in side section in
  • Figure 5 is a schematic diagram showing flow circulation in a reactor, including a tubular aeration means, as operated in accordance with a third embodiment of the process of the present invention
  • Figure 6 is a schematic diagram showing flow circulation in a reactor including disc aeration means, as operated in accordance with a fourth embodiment of the process of the present invention.
  • Figure 7 is a side schematic diagram showing another embodiment of a reactor according to the present invention.
  • Figure 8 is a plan schematic diagram for the reactor of Figure 7.
  • the gas is delivered through diffusers, i.e. a means for diffusing a gas into the liquid portion of a slurry or solution.
  • diffusers i.e. a means for diffusing a gas into the liquid portion of a slurry or solution.
  • compressed air - though other gases as described above may be suitable - is blown through gas supply line 10 to the diffuser unit 1 passing through a perforated wall 11 thereof forming air bubbles which serve to transfer oxygen and carbon dioxide into a slurry 2 in a reactor (not shown) for bacterial respiration and for oxidation of minerals.
  • Gas supply line 10 may service a number of reactors. A slug flow introduction of air or gas to the reactor, that is, without control over bubble size at introduction to the reactor, is not desirable and is, most advantageously, to be avoided.
  • Diameter or size of the perforations 13 in wall 1 1 dictates bubble size, as desired, in a controlled manner.
  • Bubble size is to be maintained at 7.5mm average diameter or less, preferably 5mm average diameter or less.
  • Disc, doughnut or tubular designs may be employed, the first two types being shown in Figures 1 to 4.
  • a disc diffuser as seen in side section in Figure 1 and plan in Figure 2, is manufactured from a flexible membrane 15 that closes when no air is being delivered. This ensures that substantially no slurry enters gas supply line 10 during processing.
  • the membrane 15 may be retained in position by a retaining device such as a clamping ring 16 which fixes the membrane in position 15 about an outlet 20 of the gas supply line 10.
  • the pores 13 may advantageously be microscopic, of the order of 1 to 5 ⁇ in diameter.
  • impeller action is not required to shear air slugs to an appropriate bubble size distribution to optimum transfer of oxygen to the slurry. Further the mass transfer occurs in a readily controllable fashion and the bubble size may be controlled by selecting a membrane or other material (see below) with desired pore or hole size.
  • a doughnut shaped diffuser is shown in side section in Figure 3 and plan in Figure 4.
  • a membrane 15 is employed which has the same characteristics as discussed above.
  • the gas supply line 10 serves further supply lines 23 feeding the doughnut shaped tube 24, the walls of which are formed from membrane 15 thereby providing greater contact area of membrane 15 with solution or slurry.
  • Characteristics of membrane 15 may include flexibility, relatively low cost, durability and easy replacement.
  • the membrane 15 may be formed from acid resistant rubber or other polymers with a pore size distribution as desired for use in the process.
  • the membrane may be manufactured in a known manner in the field of membrane technology.
  • a further type of diffuser is of typically dome shape and manufactured from plastics or ceramics.
  • a particularly effective type of diffuser is tubular with the tubular body perforated with holes for gas exit preferably having a U-shaped configuration.
  • the tubular body may be connected to the gas supply line and may be formed from a membrane or suitable plastic or ceramic material.
  • Diffusers suitable for the application will typically be sized to allow a sufficient volume of gas to be diffused into the slurry to achieve between 0.5 and 15 mg/l dissolved oxygen concentration in the slurry depending upon the oxygen requirement of the bacteria used in the bio-oxidation process.
  • Reactor configuration may be selected to achieve optimal aeration.
  • Diffuser(s) 24 may be placed adjacent, that is at, or just off, the base of the reactor, if applicable, spaced at intervals - possibly with different rates of gas introduction - to give a suitable bubble distribution for the material being treated.
  • the diffusers are fixed in position. Under different circumstances, the number of diffusers required to maintain the solids in suspension may be greater than that required for oxidation, at other times the number required may be lower. A uniform arrangement throughout the reactor base may be preferred. Conveniently, the number of aeration means or diffusers per unit area within the reactor may vary such that there is a greater proportion at the feed end of the reactor where higher rates of bacterial oxidation would be expected than at the discharge end.
  • Figures 5 and 6 show, without intending to limit the invention, likely flow circulation patterns for a number of tubular and disc diffusers located in a reactor 100. It may be understood that each arrangement allows efficient mixing and bacterial/solid contacting though a disc diffuser arrangement may be preferred.
  • Figures 7 and 8 show a reactor 200 of rectangular plan having a sloped base 204.
  • the gradient of base 204 descends from feed end 208 (to which input slurry is introduced) to discharge end 212 (at which the output leached particles are removed).
  • An overflow liquor stream 218 is removed to a metal recovery stage (not shown).
  • a number of diffusers 224 of tubular type are located evenly spaced along the base of the reactor 200.
  • Diffusers 224 are supplied with air by line 232 air is induced to flow through line 232 by induction fan 230. Carbon dioxide supplement is introduced by line 226 to line 232.
  • Suitable diffusers 224 are of tubular fine bubble membrane type available in Australia from MRE, Sydney, the distributor of Enviroquip ® tubular diffusers. Such diffusers are particularly suitable for attachment to PVC pipe which may be conveniently used for line 232.
  • the tubular diffusers 224 are supplied with oxygen containing gas by a main pipe or manifold 225 of which the tubular diffusers 224 form lateral extensions covering the base of the reactor 200 as shown in Figure 8. As the core of each diffuser 224 fills with water they will stay on the base of the reactor 200.
  • Diffusers may also be provided in pipelines communicating with a reactor, for example those connecting the reactor with others in the reactor system.
  • gas may be introduced at these points by other suitable means. This may be especially applicable in the case of a heap or dump leaching process in which ore particles are not placed into suspension in the leach liquor.
  • Materials treated by the process and reactor systems of the invention may include ores, concentrates obtained from ores, tailings, wastes and other materials having sufficient metal values present to economically remove the metal or to remove metals detrimental to the environment or other processes. It is to be understood that the present invention is not limited to the treatment of sulphides.
  • the metal value containing material may require to be pre-treated, for example crushed, to a size sufficiently small to enable it to be ground in conventional comminution equipment such as ball mills.
  • the solids requiring oxidation are ground to a particle size sufficiently fine for the gas to be effectively used in maintaining a suspension thereof and without allowing significant build-up on the floor of the reactor.
  • grinding to a suitable particle size distribution is necessary to meet this criterion.
  • the size of the product after grinding is preferably 90% passing 50 microns or less. It is advantageous for the ore or other metal containing material to be ground in an ultra fine grinding machine to particle size between 80% passing 2 microns and 80% passing 30 microns in accordance with a further embodiment of the invention.
  • the bottom particle size is as small a size as is practically attainable by grinding.
  • the size of the particles should be chosen to be the optimum for maintaining the solids in suspension and carrying out a bacterial oxidation process.
  • the material concentration may occur by gravity, flotation or other beneficiation processes to increase the proportion of the sulphides or other desired minerals in the product.
  • the process is equally applicable to the treatment of concentrates of residue produced by others and comminution pre-treatment is not necessarily required in each case.
  • the ground metal containing ore or concentrate is preferably slurried with an aqueous solution, especially water. Slurries from grinding may be diluted within additional water and pumped into the reaction zone in which the bio- oxidation process is to take place.
  • the pulp density of the slurry introduced to the reactor of the invention may be of great importance to the attainment of the object of the invention, accordingly a range of 5 to 15% or upward may be selected. At lower pulp density, as stated, efficient bacterial activity may be achieved as toxic effects due to high ionic concentration; and/or mechanical grinding of bacteria are avoided. Leaching is enhanced by the very low shear, low ionic concentration environment.
  • Bacteria are ideally previously added to the reactor in the form of a culture with a mineral and grown in sufficient numbers so that there are preferably between 10 and 10 bacteria per millilitre of slurry.
  • the bacteria may be maintained in the reactor according to accepted practice or by a method of immobilisation.
  • the retention time in the reactor is 2 to 8 days.
  • the retention time may be longer to allow treatment of less finely ground material, which requires a longer time to be processed, or to achieve higher levels of mineral oxidation and dissolution of the metal.
  • the amount of gas introduced to the slurry may be changed in accordance with retention time but this is not essential.
  • the bacterial oxidation process is carried out in an acidic solution which is suitable for growth of the specific bacteria, for example thiobacilli, used.
  • an acidic solution which is suitable for growth of the specific bacteria, for example thiobacilli, used.
  • This is expected to be in the range of 0.5 to 3.0.
  • the pH will be in the range 0.8 to 2.5.
  • An initial acid addition may be required at the start of the process to neutralise acid consuming minerals and maintain the pH in the required range.
  • the process of oxidising sulphide minerals produces acidic by-products and it is likely that the pH will decrease during processing.
  • the pH may be maintained in the required range by controlled addition of a base or basic agent such as lime, limestone or any other suitable alkali.
  • reaction may be carried out under alkaline conditions.
  • the pH is to be kept at a level suitable to the specific leaching conditions.
  • Support of the bacteria is likely to acquire the addition of nutrients to maintain growth.
  • Typical nutrients to be introduced to the reaction zone are nitrogen, sulphur and phosphorus containing materials such as ammonium sulphate, potassium dithiophosphate and magnesium sulphate.
  • other nutrients may be required for specific ores and concentrates as is known in the art.
  • the reactors are typically to be provided with cooling systems. Water may be a suitable coolant and the cooling system may be direct, with coolant water introduced at the base of the reactor. Alternatively, indirect cooling may be employed using conventional heat exchanger technology.
  • a cooling tower could produce cold water which feeds cooling coils, tube bundles or like means suitably located in the reactor.
  • Tube bundles and coils may be preferred in the absence of strong currents generated by stirring or agitation by turbine blades.
  • Evaporative cooling may be promoted by reducing depth of a reservoir and increasing the surface area.
  • the coolant may be introduced at sufficient velocity to assist in maintaining solids in suspension and admitted water may counteract evaporation losses.
  • a temperature control system with heating/cooling functions may be employed.
  • the location and nature of temperature control system, internal or external, direct or indirect, may be varied to achieve the required temperature control of the reactor. For example, when thermophilic bacteria are used, heating to above 60°C may be required.
  • the process of the invention is suitable for converting ferrous ions in solution to ferric ions which may attack minerals, for example uranium minerals, to liberate metal values of economic interest.
  • Manganese ores may be treated by mixing with a metal sulphide with the parameters for bacterial oxidation being as above described.
  • manganese ores may be bioleached with the organism Enterobacter at pH controlled between 4 and 8.
  • SULPHUR REMOVAL FROM COAL The mineral pyrite occurs with coal and bacterial oxidation using chemolithotrophic bacteria has been used to remove pyrite and reduce sulphur content.
  • the process of the invention may be employed for sulphur removal with the parameters for bacterial oxidation being as above described.
  • the grade of ore, concentrate or other metal containing material may be lower than that for agitated tanks and like reactor systems because of expected lower capital and operating costs.
  • Air flows of at least 2.4 Nm 3 /h/diffuser was required to prevent settling of solids.
  • the air flow rates required were within the manufacturer's recommended operating range. Solids that settled because of a reduction or disruption in air flow were re- suspended when the air flow was re-established at 2.4 Nm 3 /h/diffuser or higher.
  • a sample of gold concentrate containing arsenopyrite and pyrite was ground to a size such that 80% of the particles were less than 15 micrometers in diameter.
  • the bio-oxidation reactor constructed from conventional acid resistant material, had a volume of 200 litres and was provided, at its base, with a membrane diffuser as described in Example A. Air was supplied to the diffuser at a rate which maintained the ground solids in suspension. No other agitation was used.
  • the ground concentrate was mixed with water to produce a slurry at 10% solids on a weight to volume basis.
  • Sulphuric acid was added to the slurry to obtain an acidity level of pH 1.2.
  • Approximately five litres of an inoculum slurry containing a mixture of mineral concentrate and moderately thermophilic bacteria was added to the slurry in the reactor. Thereafter a mixture of nutrients comprising hydrated magnesium sulphate, potassium orthophosphate, and ammonium sulphate was added to the slurry.
  • the reactor was then heated such that the temperature of the slurry was maintained at 48°C, in the moderate thermophile range.
  • the air flowrate was controlled to allow a steady stream of bubbles to be emitted from the diffuser.
  • the air was used to maintain the particles in suspension and also to supply the oxygen requirement of the bacterial culture. No additional agitation of the reactor volume was employed. Samples of the slurry were taken on a daily basis to determine the extent of oxidation of the arsenopyrite/pyrite concentrate.
  • S is the amount of sulphide sulphur present and determines the amount of total oxidation that has occurred. Based on the analysis of the residue, the oxidation extent was determined.
  • Gold was then extracted from the residue using conventional cyanide leaching.
  • the residue assayed 67 g/t gold of which 99% was extracted by cyanidation.
  • a sample of copper concentrate containing chalcopyrite (and designated "CP1") was ground to a size such that 80% of the particles were less than 10 micrometers in diameter.
  • the bio-oxidation reactor had a maximum volume of 200 litres and a membrane diffuser, as described in Example A, was installed at the base. Air was supplied at a rate to maintain the ground solids in suspension and maintain oxygen requirement of the bacteria. No other agitation was employed.
  • the ground concentrate was mixed with water to produce a slurry at 5% solids on a weight to volume basis.
  • Sulphuric acid was added to the slurry to obtain an acidity level of pH 1.2.
  • Approximately 5 litres of an inoculum slurry containing a mixture of mineral concentrate and moderately thermophilic bacteria was added to the slurry in the reactor. Thereafter, a mixture of nutrients comprising hydrated magnesium sulphate, potassium orthophosphate, and ammonium sulphate was added to the slurry.
  • the reactor was then placed in a heated room such that the temperature of the slurry was maintained at 48°C.
  • Air was introduced to the reactor from a standard compressor, through a flowmeter with a flow valve and thence into a pipe connected to the diffuser.
  • the air flowrate was controlled to allow a steady stream of bubbles to be emitted from the diffuser.
  • the air was used to maintain the particles in suspension and provide the oxygen requirement of the bacteria. No additional agitation of the reactor was employed. Samples of the slurry were taken on a daily basis to determine the extent of oxidation of the arsenopyrite/pyrite concentrate.
  • a sample of mixed polymetallic concentrate (designated "M1") containing a mixture of mineral sulphides was bio-oxidised to extract zinc, nickel, copper and cobalt.
  • the concentrate contained the nickel mineral pentlandite, as well as nickel contained within the structure of the mineral pyrrhotite. Copper was predominately present in the form of chalcopyrite though chalcocite and bornite were also present. Zinc was present as sphalerite.
  • the metal cobalt was associated with the nickel minerals and as the mineral cobalt.
  • the concentrate was ground to a size such that 80% of the particles were less than 15 micrometers in diameter.
  • the ground concentrate was mixed with water to produce a slurry at 10% solids on a weight to volume basis.
  • Sulphuric acid was added to the slurry to obtain an acidity level of pH 1.2.
  • Approximately half a litre of an inoculum slurry containing a mixture of mineral concentrate and mesophilic bacteria (Thiobacillus ferrooxidans and Thiobacillus thiooxidans) was added to the slurry in the reactor. Thereafter, a mixture of nutrients comprising hydrated magnesium sulphate, potassium orthophosphate, and ammonium sulphate was added to the slurry.
  • the reactor was then placed in a heated room such that the slurry temperature was maintained at 35°C.
  • Air was introduced to the reactor from a standard compressor, through a flowmeter with a flow valve and thence into a pipe connected to the diffuser.
  • the air flowrate was controlled to allow a steady stream of bubbles to be emitted from the diffuser.
  • the air was used to maintain the particles in suspension and to supply the oxygen requirement of the bacteria. No additional agitation of the reactor was employed.
  • the concentrate was oxidised with metals being released into solution. The level of extraction of the metals was determined by analysing a portion of the liquid fraction of the slurry. When the reaction was complete, the solid and the liquid phases were separated and the solution and the solids analysed.
  • the reactor used was 125mm diameter and 1.7m high.
  • a diffuser as described in Example A, was installed in the base of the reactor.
  • a sample of mixed polymetallic concentrate (designated "M2") containing a mixture of mineral sulphides was bio-oxidised to extract zinc, nickel, copper and cobalt.
  • the concentrate contained the nickel mineral pentlandite, as well as nickel contained within the mineral pyrrhotite. Copper was predominately present in the form of chalcopyrite though chalcocite and bornite were also present. Zinc was present as sphalerite.
  • the metal cobalt was associated with the nickel minerals and as the mineral cobalt.
  • the concentrate was ground to a size such that 80% of the particles were less than 15 micrometers in diameter.
  • the ground concentrate was mixed with water to produce a slurry at 10% solids on a weight to volume basis.
  • Sulphuric acid was added to the slurry to obtain an acidity level of pH 1.2.
  • Approximately half a litre of an inoculum slurry containing a mixture of mineral concentrate and moderately thermophilic bacteria (Thiobacillus ferrooxidans and Thiobacillus thiooxidans) was added to the slurry in the reactor. Thereafter, a mixture of nutrients comprising hydrated magnesium sulphate, potassium orthophosphate, and ammonium sulphate was added to the slurry.
  • the reactor was then placed in a heated room such that the slurry temperature was maintained at 47°C.
  • Air was introduced to the reactor from a standard compressor, through a flowmeter with a flow valve and thence into a pipe connected to the diffuser.
  • the air flowrate was controlled to allow a steady stream of bubbles to be emitted from the diffuser.
  • the air was used to maintain the particles in suspension and to supply the oxygen requirement of the bacteria. No additional agitation of the reactor was employed.
  • the concentrate was oxidised with metals being released into solution. The level of extraction of the metals was determined by analysing a portion of the liquid fraction of the slurry. When the reaction was complete, the solid and the liquid phases were separated and the solution and the solids analysed.
  • the bio-oxidation reactor was of 40mm diameter and 1.0m height.
  • a commercially available sintered polymer diffuser was installed in the base of the reactor.
  • a sample of mixed polymetallic concentrate (designated "M3") containing a mixture of mineral sulphides was bio-oxidised to extract zinc, nickel, copper and cobalt.
  • the concentrate contained the nickel mineral pentlandite, as well as nickel contained within the mineral pyrrhotite. Copper was predominately present in the form of chalcopyrite though chalcocite and bornite were also present. Zinc was present as sphalerite. The metal cobalt was associated with the nickel minerals and as the mineral cobalt.
  • the concentrate was ground to a size such that 80% of the particles were less than 15 micrometers in diameter.
  • the ground concentrate was mixed with water to produce a slurry at 3% solids on a weight to volume basis.
  • Sulphuric acid was added to the slurry to obtain an acidity level of pH 1.2.
  • Approximately 100ml of an inoculum slurry containing a mixture of mineral concentrate and thermophilic bacteria (Sulpholobus) was added to the slurry in the reactor. Thereafter, a mixture of nutrients comprising hydrated magnesium sulphate, potassium orthophosphate, and ammonium sulphate was added to the slurry.
  • the reactor was then heated such that the slurry temperature was maintained at 70°C.
  • Air was introduced to the reactor from a standard compressor, through a flowmeter with a flow valve and thence into a pipe connected to the diffuser.
  • the air flowrate was controlled to allow a steady stream of bubbles to be emitted from the diffuser.
  • the air was used to maintain the particles in suspension and to supply the oxygen requirement of the bacteria. No additional agitation of the reactor was employed.
  • the concentrate was oxidised with metals being released into solution. The level of extraction of the metals was determined by analysing a portion of the liquid fraction of the slurry. When the reaction was complete, the solid and the liquid phases were separated and the solution and the solids analysed.
  • the bio-oxidation reactor was of 40mm diameter and 1.0m height.
  • a sample of zinc concentrate (designated "Z1") containing a mixture of mineral sulphides was treated to extract zinc.
  • the concentrate contained the zinc as the mineral sphalerite.
  • the sample also contained lead sulphide as galena.
  • the concentrate was ground to a size such that 80% of the particles were less than 15 micrometers in diameter.
  • the ground concentrate was mixed with water to produce a slurry at 5% solids on a weight to volume basis.
  • Sulphuric acid was added to the slurry to obtain an acidity level of pH 1.2.
  • Approximately 100ml of an inoculum slurry containing a mixture of mineral concentrate and moderately thermophilic bacteria (Thiobacillus ferrooxidans and Thiobacillus thiooxidans) was added to the slurry in the reactor. Thereafter, a mixture of nutrients comprising hydrated magnesium sulphate, potassium orthophosphate, and ammonium sulphate was added to the slurry.
  • the reactor was then heated such that the slurry temperature was maintained at 48°C.
  • Air was introduced to the reactor from a standard compressor, through a flowmeter with a flow valve and thence into a pipe connected to the diffuser.
  • the air flowrate was controlled to allow a steady stream of bubbles to be emitted from the diffuser.
  • the air was used to maintain the particles in suspension and to supply the oxygen requirement of the bacteria. No additional agitation of the reactor was employed.
  • the concentrate was oxidised with zinc being released into solution. The level of extraction of the zinc was determined by analysing a portion of the liquid fraction of the slurry.
  • a sample of ferrous sulphate was added to the reactor and diluted with water to obtain a strength of 9 g/l iron.
  • Sulphuric acid was added to the slurry in the reactor to obtain an acidity level of pH 1.2.
  • Extremely thermophilic bacteria (Sulpholobus), extracted onto a filter paper to separate them from other residual solution, were added to the slurry in the reactor. Thereafter, a mixture of nutrients comprising hydrated magnesium sulphate, potassium orthophosphate, and ammonium sulphate was added to the slurry.
  • the reactor was then heated such that the solution temperature was maintained at 70°C.
  • Air was introduced to the reactor from a standard compressor, through a flowmeter with a flow valve and thence into a pipe connected to the diffuser.
  • the air flowrate was controlled to allow a steady stream of bubbles to be emitted from the diffuser.
  • the air was used to maintain the particles in suspension and to supply the oxygen requirement of the bacteria. No additional agitation of the reactor was employed.
  • the ferric solution was oxidised so that the ferrous ion was converted into ferric ion. The level of conversion of the ferrous ion was determined by titration with potassium dichromate.

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  • Engineering & Computer Science (AREA)
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  • Metallurgy (AREA)
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Abstract

L'invention concerne un processus et un dispositif utiles dans des processus de biooxydation pour l'extraction de métaux à partir de matériaux renfermant des métaux. Pour cela, on utilise un élément d'aération, et de préférence des éléments diffuseurs, au sein d'un réacteur de biooxydation en vue de préserver la viabilité des bactéries et la suspension des matériaux renfermant des métaux, et ce par l'introduction d'un gaz renfermant de l'oxygène dans un réacteur agité de manière non mécanique.
PCT/AU1999/000917 1998-11-18 1999-10-22 Processus et dispositif de biooxidation WO2000029629A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
AU11414/00A AU1141400A (en) 1998-11-18 1999-10-22 Bio-oxidation process and apparatus
CA002350476A CA2350476A1 (fr) 1998-11-18 1999-10-22 Processus et dispositif de biooxidation
MXPA01005009A MXPA01005009A (es) 1998-11-18 1999-10-22 Proceso y aparato de bio-oxidacion.
US09/831,579 USH2140H1 (en) 1998-11-18 1999-10-22 Bio-oxidation process and apparatus

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AUPP7180 1998-11-18
AUPP7180A AUPP718098A0 (en) 1998-11-18 1998-11-18 Bioxidation process and apparatus

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WO2000029629A1 true WO2000029629A1 (fr) 2000-05-25

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US (1) USH2140H1 (fr)
CN (1) CN1331759A (fr)
AU (1) AUPP718098A0 (fr)
CA (1) CA2350476A1 (fr)
ES (1) ES2192975B1 (fr)
GT (1) GT200000055A (fr)
MX (1) MXPA01005009A (fr)
WO (1) WO2000029629A1 (fr)
ZA (1) ZA200103916B (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001018268A1 (fr) * 1999-09-07 2001-03-15 Billiton Intellectual Property B.V. Recuperation de nickel a partir de minerais sulfures contenant du nickel, par lixiviation biologique
US6736877B2 (en) 2001-07-13 2004-05-18 Teck Cominco Metals Ltd. Heap bioleaching process for the extraction of zinc
WO2005005672A1 (fr) * 2003-07-15 2005-01-20 Mintek Procede de lixiviation oxydante
US7455715B2 (en) 2001-07-13 2008-11-25 Teck Cominco Metals Ltd. Heap bioleaching process for the extraction of zinc
US9499876B2 (en) 2011-10-21 2016-11-22 Servicios Condumex, S.A. De C.V. Bioleaching bioreactor with a system for injection and diffusion of air

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CN1318618C (zh) * 2002-02-14 2007-05-30 Bhp比尔顿有限公司 向进行生物浸提的堆中输送微生物接种物的方法
WO2009103025A2 (fr) * 2008-02-15 2009-08-20 Biometallix, Llc Réacteur destiné à extraire des métaux de matériaux qui contiennent du sulfure de métal et ses procédés d’utilisation
CN102277490B (zh) * 2011-08-30 2013-05-29 内蒙古科技大学 生物柱浸装置
CN103173614B (zh) * 2011-12-23 2014-07-16 北京有色金属研究总院 一种原生硫化铜矿高温生物堆浸方法
EP2952593A1 (fr) * 2014-06-06 2015-12-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de biolixiviation
CN107641713A (zh) * 2017-09-30 2018-01-30 新疆大学 一种用于难处理金精矿的生物氧化预处理方法的搅拌器

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Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001018268A1 (fr) * 1999-09-07 2001-03-15 Billiton Intellectual Property B.V. Recuperation de nickel a partir de minerais sulfures contenant du nickel, par lixiviation biologique
US6733567B1 (en) 1999-09-07 2004-05-11 Billiton Intellectual Property, B.V. Recovery of nickel from nickel bearing sulphide minerals by bioleaching
AU774254B2 (en) * 1999-09-07 2004-06-24 Billiton Intellectual Property B.V. Recovery of zinc from zinc bearing sulphide minerals by bioleaching and electrowinning
AU775052B2 (en) * 1999-09-07 2004-07-15 Billiton Intellectual Property B.V. Recovery of copper from copper bearing sulphide minerals by bioleaching with controlled oxygen feed
AU775042B2 (en) * 1999-09-07 2004-07-15 Billiton Intellectual Property B.V. Bioleaching of sulphide minerals
AU775044B2 (en) * 1999-09-07 2004-07-15 Billiton Intellectual Property B.V. Recovery of nickel from nickel bearing sulphide minerals by bioleaching
AU778258B2 (en) * 1999-09-07 2004-11-25 Billiton Intellectual Property B.V. Recovery of precious metal from sulphide minerals by bioleaching
US6736877B2 (en) 2001-07-13 2004-05-18 Teck Cominco Metals Ltd. Heap bioleaching process for the extraction of zinc
US7455715B2 (en) 2001-07-13 2008-11-25 Teck Cominco Metals Ltd. Heap bioleaching process for the extraction of zinc
WO2005005672A1 (fr) * 2003-07-15 2005-01-20 Mintek Procede de lixiviation oxydante
CN100417733C (zh) * 2003-07-15 2008-09-10 明特克公司 氧化浸提方法
US9499876B2 (en) 2011-10-21 2016-11-22 Servicios Condumex, S.A. De C.V. Bioleaching bioreactor with a system for injection and diffusion of air

Also Published As

Publication number Publication date
CN1331759A (zh) 2002-01-16
USH2140H1 (en) 2006-01-03
ES2192975B1 (es) 2005-02-01
MXPA01005009A (es) 2004-08-19
GT200000055A (es) 2001-10-18
AUPP718098A0 (en) 1998-12-17
ZA200103916B (en) 2003-01-29
ES2192975A1 (es) 2003-10-16
CA2350476A1 (fr) 2000-05-25

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