WO2009003240A1 - Lixiviation maîtrisée du fer - Google Patents

Lixiviation maîtrisée du fer Download PDF

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Publication number
WO2009003240A1
WO2009003240A1 PCT/AU2008/000979 AU2008000979W WO2009003240A1 WO 2009003240 A1 WO2009003240 A1 WO 2009003240A1 AU 2008000979 W AU2008000979 W AU 2008000979W WO 2009003240 A1 WO2009003240 A1 WO 2009003240A1
Authority
WO
WIPO (PCT)
Prior art keywords
ferric
basic sulphate
controlling iron
precipitation
jarosite
Prior art date
Application number
PCT/AU2008/000979
Other languages
English (en)
Inventor
Craig Klauber
Machiel David Maree
Original Assignee
Commonwealth Scientific And Industrial Research Organisation
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 AU2007903594A external-priority patent/AU2007903594A0/en
Application filed by Commonwealth Scientific And Industrial Research Organisation filed Critical Commonwealth Scientific And Industrial Research Organisation
Publication of WO2009003240A1 publication Critical patent/WO2009003240A1/fr

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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
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00—Obtaining copper
    • C22B15/0063—Hydrometallurgy
    • C22B15/0065—Leaching or slurrying
    • C22B15/0067—Leaching or slurrying with acids or salts thereof
    • C22B15/0071—Leaching or slurrying with acids or salts thereof containing sulfur
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00—Obtaining copper
    • C22B15/0063—Hydrometallurgy
    • C22B15/0084—Treating solutions
    • C22B15/0089—Treating solutions by chemical methods
    • 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
    • C22B15/0095—Process control or regulation methods
    • 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
    • C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
    • 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 method for controlling iron concentrations in leaching processes. More particularly, the present invention relates to a process for inducing iron precipitation from an acidic ferric sulphate leach solution.
  • Acidic ferric ion leaching is commonly practiced in the minerals industry. When acid contacts for example, an iron-containing sulphidic ore in an oxidising environment, acidic ferric sulphate leach solutions invariably form.
  • the ferric ion plays an important role in the leaching process by oxidising the sulphidic ore and concomitantly being reduced to ferrous ion (Equation 1 ).
  • Ferrous ion may then be re-oxidised to ferric ion by, for example, atmospheric oxygen (Equation 2). Such re-oxidation may be biologically-assisted by, for example, iron-oxidising bacteria.
  • the equations below demonstrate such a process for chalcopyrite (CuFeS 2 ) leaching.
  • jarosite refers to any iron-hydroxy- sulphate species of the general formula M a Fe b (SO 4 ) c (OH)d, where M is a metal ion such as Na + or K + , an ammonium ion (NH 4 + ) or a hydronium ion (H + or H 3 O + ).
  • jarosite formation can be induced and accelerated by nucleation and / or seeding (e.g. with the provision of a high-surface-area, jarosite-like substrate).
  • the rate of jarosite precipitation is enhanced by the addition of jarosite seed as shown in Figure 2 (Note that the activation energy of the process is unaltered.) (Dutrizac, J. E., 1996. The effect of seeding on the rate of precipitation of ammonium jarosite and sodium jarosite. Hydrometallurgy, 42, 293-312). This kinetic enhancement is important, as in the absence of seed, the conditions for jarosite formation could exist without it apparently forming. Jarosite might thus appear a benign issue until massive precipitation occurred resulting in coated leaching surfaces.
  • jarosite formation on leaching surfaces may be inhibited by providing conditions unfavourable to jarosite formation.
  • preventing jarosite precipitation and still maintaining an ideal environment for oxidative dissolution is problematic.
  • a low pH ( ⁇ 2) is required for jarosite formation
  • a very low pH ( ⁇ 1) is known to inhibit formation as shown in Figure 1.
  • Possible alternatives would be to operate the process at either pH ⁇ 1 or pH>3. In a biologically-assisted leach, this would necessitate the development of alternate microbial strains that are active away from the present ideal of just below a pH of 2.
  • an operating pH of ⁇ 1 is unlikely to be economically attainable in practice in the presence of large amounts of acid-consuming gangue minerals, as for example in heap leach operations.
  • controlling the leaching conditions in a heap is difficult compared to control in a reactor. Even if an average pH and temperature were targeted in a heap, local variations could occur that favoured jarosite formation.
  • a method for controlling iron precipitation from acidic ferric sulphate leach solutions in leaching of chalcopyrite and/or pyrite comprising the steps of:
  • the method of the present invention advantageously confers the ability to control the location in a leaching process where the ferric basic sulphate is precipitated.
  • the method of the present invention confers the ability to control iron levels in the leach solutions such that co-precipitation of the ferric basic sulphate with the chalcopyrite and/or pyrite is reduced.
  • the method of the present invention becomes particularly advantageous where the ore grade is low and/or the gangue contains considerable undesirable but reactive gangue material such as pyrite (FeS 2 )
  • the method of the present invention enables higher valuable metal recovery and reduced reagent demand.
  • the ferric basic sulphate is jarosite.
  • the method comprises the steps of: increasing the rate of formation of a ferric basic sulphate;
  • the step of increasing the rate of formation of a ferric basic sulphate comprises the step of:
  • the step of increasing the temperature of the leach solution comprises the step of:
  • the temperature of the leach solution is increased at the location of precipitation of the ferric basic sulphate.
  • the step of increasing the temperature of the leach solution may be achieved by any method known in the art including the use of solar power, ultrasonic or microwave sources.
  • the temperature at the location of precipitation of the ferric basic sulphate is between about 40 0 C and about 80 0 C.
  • the pH at the location of precipitation of the ferric basic sulphate is about 2.
  • the step of promoting precipitation of a ferric basic sulphate comprises the step of:
  • the seed comprises jarosite-like properties and in a preferred form of the invention, the seed is jarosite. Without being limited by theory, it is believed that precipitation of a ferric basic sulphate may forego the need for further seeding.
  • the step of adding seed to the leach solution comprises the step of:
  • the seed is added to the leach solution at the location of precipitation of the iron-containing compound.
  • the step of promoting precipitation of a ferric basic sulphate comprises the step of:
  • first location and the second location may be the same.
  • the step of in situ generation of seed in the leach solution comprises the step of:
  • the step of precipitating the ferric basic sulphate at a desired location comprises the step of:
  • the third location may be the same as either the first location or the second location or the first location and the second location.
  • the method comprises the further step of:
  • the ferric basic sulphate may be removed from the leach solution by any means known in the art including the use of filters, screens, settlers and thickeners.
  • the method of the present invention may be applicable to any known method of leaching including heap leaching, dump leaching and vat leaching.
  • the method of the present invention may be performed as a batch process or a continuous process.
  • reactor volume shall be taken to include a specific vessel or a pond or an ore or concentrate heap or an in situ ore body.
  • the method comprises the further steps of:
  • the method comprises the further steps of:
  • the method comprises the further step of: winning a desired material from the leach solution.
  • the desired material is preferably copper.
  • the rate of formation of jarosite and the rate of precipitation of jarosite may be enhanced by, but is not limited to, pH and sulphate adjustment.
  • Figure 1 is a Eh-pH diagram for the Fe-S-K-O-H system at a temperature of
  • Figure 2 is an illustration of the significant enhancement of the rate of jarosite precipitation found in the presence of jarosite seed
  • FIG. 3 is a schematic illustration of the solar pond of the present invention.
  • Figure 4a is a flow diagram showing how a first embodiment of the present invention may be implemented in a typical heap circuit
  • Figure 4b is a flow diagram showing how a second embodiment of the present invention may be implemented in a typical heap circuit
  • Figure 4c is a flow diagram showing how a third embodiment of the present invention may be implemented in a typical heap circuit.
  • Figure 5 is the predicted relative jarosite precipitation rate over a 40-60 0 C solar pond range.
  • the method of the present invention is described in the context of the control of jarosite precipitation on chalcopyrite in a leaching process, although such should not be seen as limiting the generality of the foregoing description.
  • the invention describes the control of jarosite precipitation in a leaching process by careful control of the conditions amenable to jarosite formation and precipitation.
  • the fate and transport of jarosite in the leaching process may be controlled.
  • the process involves the combined or individual steps of increasing the leach solution temperature to accelerate jarosite formation, and/or the provision of seed material to promote jarosite formation away from the surface of the chalcopyrite.
  • leach solution emanating from a chalcopyrite-containing heap is passed through a solar heated jarosite- precipitation pond for the purpose of lowering the iron content of the leach solution, thereby reducing iron precipitation and coating of the chalcopyrite in the heap.
  • This preferred embodiment has been found to be particularly useful in mitigating hindered dissolution (reduced leaching rates) or "passivation" attributable to jarosite coating of chalcopyrite surfaces in heap leaching.
  • the leachate is continually re-cycled and tapped off for copper recovery in a conventional fashion such as by solvent extraction, electrowinning or cementation.
  • reducing background iron concentration can improve purity and recovery of the copper.
  • the solar-heated, jarosite precipitation circuit is provided in the form of a black plastic lined pond of a calculable area with a solar blanket and can be operated in batch or continuous mode.
  • continuous operation it would optionally be fitted with a staged weir design for concentration control.
  • batch mode the jarosite may remain in place and for the continuous weir design periodic jarosite removal may be required.
  • the pond would normally operate at a temperature elevated above the average core temperature of the heap and the leachate may only require a residence time of a few hours in the pond. Without being limited by theory, it is believed that residence time is governed by leachate chemistry and pond temperature. It will be appreciated that temperature, existing jarosite and/or other seed material surface area, mass flow rates compared to pond or reactor volume will all affect the residence time of the leachate in the pond. Part or all of the leachate emanating from the heap may be passed through the pond. It will be appreciated that both the heap and pond temperatures will be seasonally dependent. However, as the core temperature of the heap is also due to the sulphide oxidation process it would be expected that the pond-to-heap temperature advantage would be at a maximum in summer.
  • Jarosite precipitation outside the heap provides advantages in addition to the ability to control jarosite precipitation.
  • Jarosite precipitation generates substantial extra acid (see equation 4) which is particularly advantageous if the heap gangue is acid-consuming.
  • the removal of the jarosite may present easier remediation/disposal options.
  • AMD acid mine drainage
  • jarosite removal improves copper recovery and lowers iron levels in copper recovery circuits. It will be appreciated that jarosite precipitation prior to copper recovery may result in a small copper loss via jarosite incorporation.
  • FIG. 3 schematically illustrates the solar pond cross-section for non-weir batch operation.
  • the anticipated pond construction is below ground, for reasons of lower capital cost and reduced thermal losses, however the system can be constructed above ground.
  • the primary elements of the pond are (i) carefully levelled base (for example, within 20 mm over entire pond bottom), (ii) black plastic lining (colours other than black will work but will reduce performance until jarosite bed is consolidated), (iii) high R-value solar blanket.
  • the vertical dimensions A, B, C and D are dictated by issues of heap leach operation (e.g. heap size, ore type and grade), solar radiation and ambient weather.
  • the overall height D is governed by the total expected jarosite recovery during the lifetime of the pond and is likely to be in the order of one to a few metres. It is believed that based on mineralogy and grade, the total maximum jarosite recovery is calculable.
  • Initial operation can commence with seeding of the jarosite bed. Over heap and pond life the jarosite bed thickness C will continue to increase, eventually approaching D.
  • the air gap A may range from zero through to a few 10's of millimetres.
  • the air gap adds to the effective R-value of the blanket by reducing thermal conduction losses and prevents jarosite precipitation onto the blanket that would reduce solar transmission.
  • the air-gap may be achieved by spaced plastic floats under the blanket (not shown).
  • leachate depth B is largely dependent upon available solar radiation, leachate composition and the preferred rate of jarosite and acid production. Lower values for B will result in higher leachate temperatures. For typical operations B would be expected to be, but not limited to, a value range of 100-200 mm.
  • High R-value solar blankets are a commercial product with R-values ranging typically from 0.067 to 0.13.
  • a secondary adjunct to the solar pond (not illustrated), advantageous in cooler climates, is the fitting of a light-weight clear UV-stabilized plastic film cover over the entire pond. This is conventional technology and can be fabricated, installed and supported in a number of ways (such as single skin, twin skin, fan inflated).
  • volumetric size and depth D are both operationally restrained and thus dictate the actual pond surface area.
  • the pond might typically be in the order of 5000 m 2 , with shape, aspect ratio and orientation to maximize solar performance. Side and bottom insulation would initially be advantageous, but with operation and jarosite deposition the jarosites' characteristics would dominate.
  • the extent to which the leachate's temperature can be elevated is decided essentially by the energy gain from solar radiation and the energy losses back to the environment. Characteristically, this is typically 10% to ground, 20% via radiation to sky and 70% via evaporation. Use of a solar blanket significantly reduces the evaporative loss and converts that fraction to a smaller amount via conductive transfer. Both the solar transmission and the R-value of the blanket then become important. Energy loss as watts/m 2 is determined by K/R where K is the gradient temperature difference ( 0 C or K) and R is the insulation value. Low K and high R minimizes this energy loss.
  • the most preferable configuration would have the pond gravity fed, but pump drained.
  • Pump inlet for leachate removal suitably guarded to not damage or entrain the pool blanket, is anticipated to be flexible, moored and fixed with floats to adjust to leachate level. End of batch pump operation would be dictated by the inlet resting on the jarosite bed.
  • FIGS 4a to 4c schematically illustrate simplified flow diagrams showing how three embodiments of the present invention may be implemented in a typical heap circuit.
  • the circuit incorporation could use any one of the three ways individually or in combination.
  • Figure 4a shows a schematic flow sheet comprising the steps of:
  • Figure 4b shows a schematic flow sheet comprising the steps of:
  • Figure 4c shows a schematic flow sheet comprising the steps of:
  • the invention may be operated in either continuous or batch mode, although batch mode may offer a number of advantages.
  • the intent is batch operation.
  • the aim of the batch process is not to specifically maximize individual jarosite or acid production per batch period, but rather to increase the rate at which this is achieved as increasing rate lowers the general cost.
  • Investigations of batch jarosite production specifically display an initial maximum rate that then tapers off; the rate being driven by the higher initial ferric and sulphate concentrations.
  • the batch cycle may be any convenient time period, although the maximum solar benefit is gained by a leachate fill in early morning and then decant in late afternoon with the pond having low leachate levels at night.
  • the optimum mode of operation is dependent not only upon the leachate chemistry and heap leach management but also the prevailing weather conditions.
  • 24 hour rainfall periods with, for example, 20 mm of rain represents only a minor perturbation on return leachate chemistry, both in terms of dilution and depression of temperature.
  • Diagnostic choices for batch operation are relatively simple and require no sophisticated control methodology.
  • Optimum depth B can be estimated by modelling and verified by practice; for a float defined air gap and known jarosite bed depth this is a simple periodic measurement.
  • Monitoring pond leachate temperature with time gives a guide as to optimum return time for purposes of returning the low-grade heat.
  • Monitoring pond leachate pH enables the progress of the precipitation reaction to be followed as it directly gives sulphuric acid production and indirectly both jarosite production and iron removal values. Simple T and pH indicators thus control residence time.
  • the gross design features of the solar pond can be determined in advance; the key parameters of B plus the T and pH for residence time can be optimised at operation commencement and changed as the heap changes behaviour, so the Invention represents a versatile and low capital cost solution to iron control.
  • the Invention represents a versatile and low capital cost solution to iron control.
  • the solar pond footprint of 5000 m 2 would be only about 10% the footprint of the actual heap.
  • the pond envelope (in this example it would have a total volume of 6000 m 3 ) could store the entire jarosite output of the heap over the two years estimated lifetime based on 50% iron removal from the pond leachate for 8 hours batch operation and in the process returning over 16 tonnes of sulphuric acid per day.
  • Table 1 shows the sensitivity of iron removal both to temperature and to residence time for solar pond leachate conditions for iron levels at the lower end of the concentration range that would typically be expected for heap leachate. At higher iron levels the rate of iron removal would be expected to be higher.
  • solar pond temperatures are environmentally dependent but can be manipulated by adjustment of B. Under most summer or dry season conditions an operational solar pond range of 50-60 0 C would be expected and for temperate winter or wet season conditions an operational range of 40-50 0 C. The lower end cool season temperature may have an impact on performance so the B value may need to be reduced to maintain the leachate temperature toward 5O 0 C.
  • Table 1 Iron removal in relation to temperature and residence time Based on the known behaviour that Arrhenius activation energy for jarosite precipitation is preserved; though rate is dramatically enhanced in the presence of seed the typical results shown in Table 1 can be generalized with some confidence over other temperatures relative to a fixed value. This predicted relationship based on preserved activation energy is shown in Figure 5 and shows that over the 45-5O 0 C range the precipitation efficiency is 17-31 % compared to that at 6O 0 C. From Table 1 it can be seen that doubling residence time at the higher iron concentration end more than doubles the jarosite precipitation as a consequence of the lower turbulence. It is known that at sufficient seed concentration the initial behaviour is at least linear with time so that for an 8 hour residence time the worse case scenario for the cool season low end 45-5O 0 C range is at least 15-27% removal, though the reality is that it is likely to be much higher.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Metallurgy (AREA)
  • Manufacturing & Machinery (AREA)
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Abstract

L'invention concerne un procédé permettant de maîtriser la précipitation de fer dans des solutions de lixiviation de sulfate ferrique acide pour la lixiviation de chalcopyrite et/ou de pyrite. Le procédé consiste à augmenter la vitesse de formation d'un sulfate basique ferrique et/ou favoriser la précipitation d'un sulfate basique ferrique; et faire précipiter le sulfate basique ferrique à un emplacement désiré.
PCT/AU2008/000979 2007-07-03 2008-07-03 Lixiviation maîtrisée du fer WO2009003240A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2007903594A AU2007903594A0 (en) 2007-07-03 Iron Control in Leaching
AU2007903594 2007-07-03

Publications (1)

Publication Number Publication Date
WO2009003240A1 true WO2009003240A1 (fr) 2009-01-08

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PCT/AU2008/000979 WO2009003240A1 (fr) 2007-07-03 2008-07-03 Lixiviation maîtrisée du fer

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9340503B2 (en) 2009-01-28 2016-05-17 Karus Therapeutics, Limited Scriptaid isosteres and their use in therapy
WO2019175838A1 (fr) * 2018-03-14 2019-09-19 Flsmidth A/S Régulation du fer dans des solutions de traitement contenant du cuivre et du zinc

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3817743A (en) * 1972-09-18 1974-06-18 Pennzoil Co Treatment of copper iron sulfides to form x-bornite
US3876537A (en) * 1973-10-31 1975-04-08 Industrial Resources Method of insolubilizing demineralizer and cooling tower blowdown wastes
US3912330A (en) * 1974-03-04 1975-10-14 Us Interior Chemical mining of copper porphyry ores
US4333736A (en) * 1979-01-26 1982-06-08 Solmat Systems Ltd. Method of utilizing solar ponds for effecting controlled temperature changes of solutions particularly in processes involving the dissolution and/or precipitation of salts
US5091160A (en) * 1990-11-05 1992-02-25 Her Majesty The Queen In Right Of Canada, As Represented By The Minister Of Energy Use of microwave radiation to eliminate foam in ore leaching
US5232490A (en) * 1985-11-27 1993-08-03 Leadville Silver And Gold Oxidation/reduction process for recovery of precious metals from MnO2 ores, sulfidic ores and carbonaceous materials

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3817743A (en) * 1972-09-18 1974-06-18 Pennzoil Co Treatment of copper iron sulfides to form x-bornite
US3876537A (en) * 1973-10-31 1975-04-08 Industrial Resources Method of insolubilizing demineralizer and cooling tower blowdown wastes
US3912330A (en) * 1974-03-04 1975-10-14 Us Interior Chemical mining of copper porphyry ores
US4333736A (en) * 1979-01-26 1982-06-08 Solmat Systems Ltd. Method of utilizing solar ponds for effecting controlled temperature changes of solutions particularly in processes involving the dissolution and/or precipitation of salts
US5232490A (en) * 1985-11-27 1993-08-03 Leadville Silver And Gold Oxidation/reduction process for recovery of precious metals from MnO2 ores, sulfidic ores and carbonaceous materials
US5091160A (en) * 1990-11-05 1992-02-25 Her Majesty The Queen In Right Of Canada, As Represented By The Minister Of Energy Use of microwave radiation to eliminate foam in ore leaching

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9340503B2 (en) 2009-01-28 2016-05-17 Karus Therapeutics, Limited Scriptaid isosteres and their use in therapy
WO2019175838A1 (fr) * 2018-03-14 2019-09-19 Flsmidth A/S Régulation du fer dans des solutions de traitement contenant du cuivre et du zinc

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