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WO2009155634A1 - Procédé de lixiviation atmosphérique à contre-courant - Google Patents

Procédé de lixiviation atmosphérique à contre-courant Download PDF

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Publication number
WO2009155634A1
WO2009155634A1 PCT/AU2009/000600 AU2009000600W WO2009155634A1 WO 2009155634 A1 WO2009155634 A1 WO 2009155634A1 AU 2009000600 W AU2009000600 W AU 2009000600W WO 2009155634 A1 WO2009155634 A1 WO 2009155634A1
Authority
WO
WIPO (PCT)
Prior art keywords
leach
counter current
stage
current atmospheric
discharge
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
Application number
PCT/AU2009/000600
Other languages
English (en)
Inventor
Peter Mason
Jeremy Tape
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
GLADSTONE PACIFIC NICKEL Ltd
Original Assignee
GLADSTONE PACIFIC NICKEL Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from AU2008903258A external-priority patent/AU2008903258A0/en
Application filed by GLADSTONE PACIFIC NICKEL Ltd filed Critical GLADSTONE PACIFIC NICKEL Ltd
Publication of WO2009155634A1 publication Critical patent/WO2009155634A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0407—Leaching 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
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0407—Leaching processes
    • C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
    • C22B23/043—Sulfurated acids or salts thereof
    • 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
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
    • 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 invention relates to the hydrometallurgical processing of nickeliferous ores.
  • the invention relates to the extraction of nickel and/or cobalt from high magnesium, or saprolitic, laterite ores by atmospheric pressure acid leaching in combination with the extraction of nickel and/or cobalt from low magnesium, or limonitic, laterite ores by high pressure acid leaching.
  • a High Pressure Acid Leaching (HPAL) process is commonly used to extract nickel and/or cobalt from limonitic laterite ores.
  • the process comprises adding concentrated sulphuric acid to ore slurry and heating to approximately 25O 0 C at a raised pressure. This enhances nickel and cobalt leaching kinetics and promotes the precipitation of iron as hematite.
  • the solution phase of the leach product typically also contains approximately 50 g/L of "free acid".
  • This free acid is subsequently neutralized (totally or partially) by adding limestone or an equivalent alkali material prior to separation of the solid leach residue from the leach solution.
  • Increasing the pH of the slurry by neutralizing a portion of the free acid precipitates some of the impurities, such as iron and aluminium, from the pregnant solution and thus assists in downstream processing.
  • US Patent 3,991 ,159 (Queneau et al) teaches neutralizing leach slurry from a high pressure and temperature acid leach of low magnesium laterite ore with a high magnesium ore.
  • the neutralization process is carried out at a high temperature (200°C-300°C) and pressure (225psig-1750psig).
  • Queneau alternatively teaches pre-treating the high magnesium ore with a leach solution from the high pressure and temperature leach, at a temperature not exceeding 15O 0 C. Thickened pulp from this low temperature leach is used in the high temperature neutralization described above, whilst metal values are recovered from the separated solution.
  • WO 2006/084335 (Liu & Krebs) teaches a simple acid preleach of saprolitic ore prior to its addition to a primary HPAL slurry. This process also relies on the use of process water that has an ionic composition that substantially avoids the formation of jarosite. That is, the process water has low levels of sodium, potassium and ammonia.
  • the invention resides in a counter current atmospheric leach process comprising:
  • HPAL high pressure acid leach
  • the counter current atmospheric leach process further includes:
  • the counter current atmospheric leach process further includes mixing together for a period of time the HPAL discharge slurry with the further leach discharge resulting from the further leach prior to the step of separating the further leach solution from the combined HPAL discharge slurry and the further leach discharge.
  • a portion of the further leach solution is recycled to the further leach at atmospheric pressure and a portion of the further leach solution is recycled to the first stage leach at atmospheric pressure.
  • FIG. 1 shows a flow diagram of a first embodiment of the counter- current atmospheric leach process
  • FIG. 2 shows a flow diagram of a second embodiment of the counter-current atmospheric leach process
  • FIG. 3 shows a flow diagram of a further embodiment of the counter-current atmospheric leach process.
  • the present invention provides a counter current atmospheric leach process of high magnesium, or saprolitic, fraction of lateritic ore, with improved utilization of sulphuric acid, both freshly added and as byproduct of a parallel high pressure acid leach (HPAL) of low magnesium, or limonite, fraction of lateritic ore.
  • HPAL high pressure acid leach
  • a continuous counter current atmospheric leach process in which saprolite ore is mixed with an aqueous phase (e.g. fresh water, seawater, or process solution) to produce saprolite ore slurry 101.
  • an aqueous phase e.g. fresh water, seawater, or process solution
  • the saprolite ore slurry 101 is mixed with a second stage leach solution 110 and the mixture is subjected to a first stage leach 102 at atmospheric pressure and a temperature close to the boiling point of the slurry, preferably 7O 0 C to 105 0 C.
  • nickel, cobalt and other metals are solubilized from the saprolite ore slurry 101 into a solution phase.
  • Heating of the mixture of saprolite ore slurry 101 and second stage leach solution 110 may be achieved by the addition of steam from an HPAL process, or other conventional method as would be known to a person skilled in the field.
  • a reductant 119 e.g. solid sodium metabisulfite (SMBS) or SO 2 gas
  • SMBS solid sodium metabisulfite
  • SO 2 gas SO 2 gas
  • Retention in the first stage leach 102 is typically 1-6 hours.
  • a first stage leach discharge 103 is directed to a first separation device 104 and separated into a first stage leach solution 105 and a first stage leach residue 106.
  • the first separation device 104 may be a thickener or other conventional separation method either separately or in combination.
  • the residual free acid present in the first stage leach solution 105 is typically less than about 50g/L, preferably less than 10g/L.
  • a second stage leach discharge 108 is directed to a second separation device 109.
  • the second separation device 109 may be a thickener or other conventional separation method either separately or in combination.
  • the residual free acid in the HPAL discharge slurry is typically 25g/L to 75g/L, preferably 50g/L.
  • the HPAL discharge slurry 112 is combined with the second stage leach discharge 108 in the second separation device 109. Operation of the second separation device 109 results in a second stage leach solution 110 and a second stage leach residue 111.
  • the residual free acid present in the second stage leach solution 110 is typically 40g/L to 100g/L, preferably 70 g/L to 80 g/L.
  • the second stage leach solution 110 is then directed to the first stage leach 102.
  • the second stage leach residue 111 and the first stage leach solution 105 are processed, either in combination or separately, for the recovery of dissolved nickel and cobalt.
  • the first stage leach 102 and the second stage leach 107 are carried out as part of a continuous process, each in either one or a series of agitated tanks.
  • FIG. 2 shows a second embodiment of the counter-current atmospheric leach process.
  • the saprolite ore slurry 101 is mixed with a second stage leach solution 110 and the mixture is subjected to a first stage leach 102 at atmospheric pressure.
  • a first stage leach discharge 103 is directed to a first separation device 104 and separated into a first stage leach solution 105 and a first stage leach residue 106.
  • the first stage leach residue 106 with the addition of sulfuric acid 113, preferably concentrated, is then subjected to a second stage leach 107 at atmospheric pressure.
  • a second stage leach discharge 108 is then directed to a discharge slurry mix tank 114.
  • the discharge slurry mix tank 114 may be one or a multiple of tanks equipped with mixing or agitating apparatus.
  • HPAL discharge slurry 112 is directed to and combined with the second stage leach discharge 108 in the discharge slurry mix tank 114 and agitated for an extended time.
  • a mix tank discharge 115 is then directed to a second separation device 109. Operation of the second separation device 109 results in a second stage leach solution 110 and a second stage leach residue 111 , as discussed in the process of FIG. 1 , and the second stage leach solution 110 is then directed to the first stage leach 102.
  • the second stage leach residue 111 and the first stage leach solution 105 are processed, either in combination or separately, for the recovery of dissolved nickel and cobalt.
  • a portion of the second stage leach solution 110 may be diverted 116 to the second stage leach 107 to lower the leach solids concentration.
  • a lower solids concentration in the second stage leach 107 may increase the leach kinetics.
  • the diversion 116 of the second stage leach solution 110 may occur in either of the embodiments shown in FIG. 1 or FIG. 2.
  • the saprolite ore used in any embodiment of the invention may undergo a pre-treatment process.
  • Pre-treatment of the saprolite ore prior to the production of the saprolite ore slurry 101 may increase the efficiency of the counter-current atmospheric leach process.
  • Two examples of pre-treatments are shown as optional features in FIG. 3.
  • the saprolite ore undergoes a calcination process 117. Calcination may increase the reactivity of the saprolite ore slurry 101 and thus increase its acid neutralization capacity.
  • the removal of an ultra-fine size fraction 118 from the saprolite ore slurry 101 may increase the efficiency of the first and second separation devices, thus increasing the efficiency of the process.
  • the embodiments of the invention maximize nickel and/or cobalt extraction from the saprolite ore into a solubilised form in the liquid phase by retaining high acid strength leach conditions, yet simultaneously reduce concentrated sulfuric acid consumption.
  • a further benefit is the reduction in the quantity of limestone required for downstream neutralization and consequently a reduction in carbon dioxide evolution.
  • the example shows laboratory simulated continuous processing of nickeliferous saprolite ore by an embodiment of the counter-current atmospheric leach flowsheet as depicted in FIG. 1.
  • the first stage leaching had a retention time of 6 hours.
  • Low magnesium saprolite ore slurry was mixed with a simulated second stage leach solution to give slurry at 10% solids and heated to 90-95 0 C. Separation of the first stage leach discharge via a thickener gave a first stage leach solution with a free acid content of 35 g/L and a first stage leach residue.
  • the first stage leach residue was directed to a second stage leach, which had a retention time of 6 hours.
  • Concentrated sulphuric acid was added and the temperature maintained at 90-95 0 C.
  • the second stage leach solution contained 89 g/L free acid.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

L'invention porte sur un procédé de lixiviation atmosphérique à contre-courant comprenant les opérations consistant à soumettre une boue de minerai de saprolite à une première étape de lixiviation à pression atmosphérique; soumettre un résidu de première étape de lixiviation résultant de la première étape de lixiviation à une lixiviation supplémentaire à pression atmosphérique; combiner une boue sortant d'une lixiviation acide à haute pression (HPAL) avec un autre effluent de lixiviation résultant de la lixiviation supplémentaire; séparer une solution de lixiviation supplémentaire de la boue sortant de HPAL et de l'effluent de lixiviation supplémentaire combinés; et recycler la solution de lixiviation supplémentaire vers la première étape de lixiviation à pression atmosphérique de la boue de minerai de saprolite.
PCT/AU2009/000600 2008-06-26 2009-05-14 Procédé de lixiviation atmosphérique à contre-courant Ceased WO2009155634A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2008903258A AU2008903258A0 (en) 2008-06-26 Counter current atmospheric leach process
AU2008903258 2008-06-26

Publications (1)

Publication Number Publication Date
WO2009155634A1 true WO2009155634A1 (fr) 2009-12-30

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Family Applications (1)

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PCT/AU2009/000600 Ceased WO2009155634A1 (fr) 2008-06-26 2009-05-14 Procédé de lixiviation atmosphérique à contre-courant

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WO (1) WO2009155634A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011036345A1 (fr) * 2009-09-24 2011-03-31 Norilsk Nickel Finland Oy Procédé de récupération de nickel et de cobalt à partir de latérite
US20250171878A1 (en) * 2023-07-31 2025-05-29 Pt Esg New Energy Material Process and system for recovering manganese from high-pressure leaching system of laterite nickel ore

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3962051A (en) * 1974-12-26 1976-06-08 Amax Inc. Atmospheric leaching of matte containing iron
US4548794A (en) * 1983-07-22 1985-10-22 California Nickel Corporation Method of recovering nickel from laterite ores
WO1997007248A1 (fr) * 1995-08-14 1997-02-27 Outokumpu Technology Oy Procede d'extraction du nickel par hydrometallurgie a partir de deux mattes de nickel differentes
US5628817A (en) * 1994-11-15 1997-05-13 Outokumpu Engineering Contractors Oy Method for leaching nickel-copper matte employing substantially neutral leaching solutions
WO2004090176A1 (fr) * 2003-04-11 2004-10-21 Bhp Billiton Ssm Technology Pty Ltd Lixivation ammoniacale reductrice de materiaux a teneur en nickel et en cobalt
AU2007200975A1 (en) * 2006-03-10 2007-09-27 Bhp Billiton Ssm Development Pty Ltd Process for recovering nickel and cobalt from oversize ore particles

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3962051A (en) * 1974-12-26 1976-06-08 Amax Inc. Atmospheric leaching of matte containing iron
US4548794A (en) * 1983-07-22 1985-10-22 California Nickel Corporation Method of recovering nickel from laterite ores
US5628817A (en) * 1994-11-15 1997-05-13 Outokumpu Engineering Contractors Oy Method for leaching nickel-copper matte employing substantially neutral leaching solutions
WO1997007248A1 (fr) * 1995-08-14 1997-02-27 Outokumpu Technology Oy Procede d'extraction du nickel par hydrometallurgie a partir de deux mattes de nickel differentes
WO2004090176A1 (fr) * 2003-04-11 2004-10-21 Bhp Billiton Ssm Technology Pty Ltd Lixivation ammoniacale reductrice de materiaux a teneur en nickel et en cobalt
AU2007200975A1 (en) * 2006-03-10 2007-09-27 Bhp Billiton Ssm Development Pty Ltd Process for recovering nickel and cobalt from oversize ore particles

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011036345A1 (fr) * 2009-09-24 2011-03-31 Norilsk Nickel Finland Oy Procédé de récupération de nickel et de cobalt à partir de latérite
AU2010299790B2 (en) * 2009-09-24 2016-05-12 Norilsk Nickel Harjavalta Oy Method for recovering nickel and cobalt from laterite
US20250171878A1 (en) * 2023-07-31 2025-05-29 Pt Esg New Energy Material Process and system for recovering manganese from high-pressure leaching system of laterite nickel ore
US12378639B2 (en) * 2023-07-31 2025-08-05 Pt Esg New Energy Material Process and system for recovering manganese from high-pressure leaching system of laterite nickel ore

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