[go: up one dir, main page]

EP1740730A1 - Procede de recuperation d'or - Google Patents

Procede de recuperation d'or

Info

Publication number
EP1740730A1
EP1740730A1 EP20050735875 EP05735875A EP1740730A1 EP 1740730 A1 EP1740730 A1 EP 1740730A1 EP 20050735875 EP20050735875 EP 20050735875 EP 05735875 A EP05735875 A EP 05735875A EP 1740730 A1 EP1740730 A1 EP 1740730A1
Authority
EP
European Patent Office
Prior art keywords
gold
copper
chloride
leaching
solution
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP20050735875
Other languages
German (de)
English (en)
Finnish (fi)
Inventor
Matti Hämäläinen
Olli Hyvärinen
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.)
Metso Corp
Original Assignee
Outokumpu Technology Oyj
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 Outokumpu Technology Oyj filed Critical Outokumpu Technology Oyj
Publication of EP1740730A1 publication Critical patent/EP1740730A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B11/00—Obtaining noble metals
    • C22B11/04—Obtaining noble metals by wet processes
    • C22B11/042—Recovery of noble metals from waste materials
    • C22B11/044—Recovery of noble metals from waste materials from pyrometallurgical residues, e.g. from ashes, dross, flue dust, mud, skim, slag, sludge
    • 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
    • C22B11/00—Obtaining noble metals
    • C22B11/06—Chloridising
    • 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 a method for recovering gold from an intermediate product or residue containing sulphur and iron generated in the leaching of a sulphidic raw material.
  • the recovery of gold and the other valuable metals in the raw material takes place in a chloride environment.
  • the gold contained in the intermediate product or residue is leached with divalent copper and chlorine in a copper (II) chloride - sodium chloride solution in conditions where the oxidation-reduction potential is in the range of 650-750 mV and the pH between 1 and 1.6.
  • the acid generated during the feed of chlorine is neutralized with a suitable alkali. Neutralization avoids the costs of dissolving the iron.
  • US patent 4,551,213 describes a method in which gold can be leached from sulphur-containing material, in particular the residue from hydrometallurgical processes.
  • the preferred starting material for the method is the residue from the CLEAR process.
  • the CLEAR process is a hydrometallurgical copper recovery process, which occurs in a chloride environment and at elevated pressure.
  • the gold-containing residue is elutriated into water and the chloride concentration of the resulting suspension is adjusted so that it is 12 - 38 weight percent.
  • the oxidation-reduction potential is adjusted to the range of 650 - 750 mV and the pH to below 0.
  • Copper (II) chloride or iron (III) chloride are added to the suspension to oxidize the gold contained in the raw material, so that it dissolves.
  • EP patent 646185 relates to the recovery of copper from sulphidic concentrates with chloride leaching in atmospheric conditions.
  • the gold from the leach residue is dissolved into electrolyte, which includes two or more halides, such as sodium chloride and sodium bromide.
  • electrolyte which includes two or more halides, such as sodium chloride and sodium bromide.
  • the purpose is to store oxidising energy in the bromine complex on the copper electrolysis anode, and thereby leach the gold from the residue.
  • WO patent application 03/091463 describes a method for leaching gold from leaching residue or intermediate product containing iron and sulphur, generated in the atmospheric chloride leaching of copper sulphide concentrate.
  • the publication states that gold may be leached from an iron- and sulphur-containing material into an aqueous solution of copper (II) chloride and sodium chloride with copper and oxygen in conditions where the oxidation-reduction potential is below 650 mV and the pH value of the solution in the range 1 - 3. In these conditions iron does not dissolve and the sulphur remains undissolved to a large extent. Thus the costs that arise when iron and sulphur are removed from the solution are avoided.
  • the recovery of gold from the solution is made by one of the methods of the prior art such as electrolysis or active carbon. The method in question is in itself quite good, but in practice however it is somewhat slow.
  • the oxidation-reduction potential of the leaching stage is raised to the range of 650-750 mV by means of chlorine.
  • a high oxidation-reduction potential enables the elemental sulphur in the residue to dissolve and as a consequence, acid is formed in the stage, which is neutralised by some suitable alkali.
  • the simultaneous neutralisation of the acid keeps the pH at a value of 1.0 - 1.6, whereby the dissolution of iron is prevented.
  • the dissolved gold is recovered by some method known as such in the prior art.
  • a gold-bearing intermediate product or residue is leached into sodium chloride solution containing copper(ll) chloride forming a suspension and the oxidation-reduction potential required for gold leaching is obtained particularly by means of divalent copper and chlorine gas. If the feed to gold leaching still contains undissolved copper- or other sulphide, oxygen- containing gas can be fed to the start of the leaching stage in order to dissolve it.
  • the oxidation-reduction potential is measured with Pt- and Ag/AgCI electrodes and the potential is kept at a value of 650-750 mV.
  • the amount of divalent copper, Cu 2+ , in the solution is preferably 20 - 80 g/l and the amount of sodium chloride in the region of 200 - 330 g/l.
  • Gold dissolves as a chloro complex in accordance with the following reaction:
  • Leaching occurs in atmospheric conditions at a temperature, which is between room temperature and the boiling point of the suspension, preferably, however, between 80 °C and the boiling point of the suspension.
  • Reaction (2) shows that a lot of acid is generated (8 mol H+/ mol S°).
  • the acid generated in the solution must however be neutralised, since at pH values under 1 the iron in the solids begins to dissolve.
  • the dissolution of iron causes process costs, as dissolved iron is circulated and consumes reagents.
  • the preferred pH region to keep iron in the residue is between 1.0 and 1.6.
  • Some suitable alkali from the group NaOH, KOH, CaO, CaC0 3 or MgO is used to neutralise the acid. If the process is combined with a chloride-based hydrometallurgical method of producing copper, in which basic copper (II) chloride is generated in the precipitation of divalent copper from leaching, the use of the copper (II) chloride is the best option. When basic copper (II) chloride dissolves, the copper (II) chloride generated can be used for raw material leaching. The neutralization of hydrochloric acid and copper (II) oxychloride leaching occur according to the following reaction:
  • the sulphuric acid generated can be neutralised for example with lime:
  • the recovery of gold from the solution takes place by some method known as such in the prior art, for instance active carbon, electrolysis or chemical precipitation.
  • a sulphidic raw material such as copper sulphide concentrate 2 is fed to the first leaching stage 1 , and solution 3 from a later process stage, which is an aqueous solution of copper (II) chloride and sodium chloride, is also circulated to this stage.
  • the thicker arrows denote solids and the thinner arrows the flow of solution.
  • the stage always includes one or more reactors and thickening.
  • the copper and other valuable metals of the concentrate mainly dissolve into the process solution and the resulting solution 4 includes copper chloride, in which about 70 g/l of copper is mainly monovalent.
  • the further treatment of the copper chloride solution is not presented in more detail here.
  • the leaching of the solids 5 from the first leaching stage is continued in the second leaching stage 6 with solution 7, which is taken from a later process stage. Air is fed into the reactors at this stage in order to enhance leaching of the valuable metals and to precipitate the iron. Thickening is done at the end of this stage.
  • the solution 3 from the second stage is routed to the first leaching stage 1 to leach the concentrate.
  • the leaching of the solids 8 from the second leaching stage is continued in the third stage 9 in order to leach the rest of the copper and the gold.
  • the residue is leached with copper (II) chloride - sodium chloride solution 10, in which the Cu 2+ -content is 20 - 80 g/l and the sodium chloride content 200 - 330 g/l. If the residue entering this leaching stage still contains undissolved sulphide, oxygen, preferably in the form of air, can also be routed to the first reactor at the beginning of the stage.
  • Copper and other sulphides should be leached out of the residue before the gold dissolves.
  • chlorine gas 11 is also fed into the reactor. Because of the high potential, sulphur starts to dissolve and as a result acid is formed in the stage. So that the pH of the stage does not fall below 1.0, some alkali 12 is fed into it such as NaOH, KOH, CaO, CaC0 3 or MgO. If the process is combined with a chloride-based hydrometallurgical method to produce copper, in which basic copper (II) chloride is generated in the precipitation of divalent copper from leaching, the basic copper (II) chloride is used.
  • the gold-chloro complex solution 13 obtained from the leaching stage is routed either as it is or filtered to gold recovery, which in this case occurs in a carbon column 14 by means of active carbon.
  • the gold product 15 is obtained from the column.
  • the solution exiting column 14 is a gold-free solution 16, which is circulated to the second stage of leaching 6 and sodium chloride solution is routed there as required to achieve a suitable copper (II) chloride content for leaching.
  • the residue of the gold recovery stage after normal after-treatment such as filtration and washing (not shown in detail in the diagram), becomes the final leach residue 17, which contains nearly all the sulphur and iron of the concentrate.
  • the residue filtrate and rinse water are returned for example to the concentrate leaching process.
  • the flow chart in Fig. 1 presents a gold leaching method in connection with copper-bearing raw material leaching, but the method of the invention is not limited to the copper-bearing raw material leaching process shown in the chart.
  • the crux of our method is that the leaching of gold-bearing material is performed with divalent copper and chlorine in conditions where the redox potential of the solution is raised to a value of 650-750 mV, and the acid formed during the dissolution of sulphur is neutralized so that the pH is minimum 1 , preferably at least 1.0 - 1.6.

Landscapes

  • 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 récupération d'or à partir d'un produit intermédiaire ou de résidus contenant du soufre et du fer, produits lors de la lixivation d'un matériau brut cuivreux associée à la production hydrométallurgique de cuivre. La récupération du cuivre et de l'or se fait dans un environnent de chlorure. L'or présent dans le produit intermédiaire ou les résidus est lixivé avec le cuivre divalent et le chlore dans une solution de chlorure de cuivre (II) et de chlorure de sodium dans des conditions où le potentiel d'oxydation-réduction est compris entre 650 et 750 mV et le pH entre 1 et 1,6. L'acide résultant de l'apport en chlore est neutralisé par l'oxychlorure de cuivre (II) produit pendant le processus.
EP20050735875 2004-04-30 2005-04-25 Procede de recuperation d'or Withdrawn EP1740730A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FI20040621A FI117709B (fi) 2004-04-30 2004-04-30 Menetelmä kullan talteenottamiseksi
PCT/FI2005/000194 WO2005106052A1 (fr) 2004-04-30 2005-04-25 Procede de recuperation d'or

Publications (1)

Publication Number Publication Date
EP1740730A1 true EP1740730A1 (fr) 2007-01-10

Family

ID=35185129

Family Applications (1)

Application Number Title Priority Date Filing Date
EP20050735875 Withdrawn EP1740730A1 (fr) 2004-04-30 2005-04-25 Procede de recuperation d'or

Country Status (12)

Country Link
US (1) US20070245856A1 (fr)
EP (1) EP1740730A1 (fr)
CN (1) CN1950524A (fr)
AP (1) AP2006003793A0 (fr)
AR (1) AR049633A1 (fr)
AU (1) AU2005238241A1 (fr)
BR (1) BRPI0510505A (fr)
CA (1) CA2564338A1 (fr)
EA (1) EA009726B1 (fr)
FI (1) FI117709B (fr)
PE (1) PE20060226A1 (fr)
WO (1) WO2005106052A1 (fr)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FI118302B (fi) * 2006-02-17 2007-09-28 Outotec Oyj Menetelmä kullan talteenottamiseksi
KR100787205B1 (ko) 2007-06-11 2007-12-21 광해방지사업단 광물찌꺼기 및 정광으로부터 해수를 이용한 유가금속회수방법
CN100582261C (zh) * 2008-04-08 2010-01-20 昆明贵研药业有限公司 一种从含铂碘化银渣回收铂银碘的方法及其装置
FI124954B (fi) * 2013-04-30 2015-04-15 Outotec Oyj Menetelmä kultaa sisältävän liuoksen valmistamiseksi ja prosessijärjestely kullan ja hopean talteenottamiseksi
TR201906828T4 (tr) 2015-10-29 2019-05-21 Outotec Finland Oy Altının geri kazanımına yönelik yöntem.
CN105969990A (zh) * 2016-06-20 2016-09-28 昆山鸿福泰环保科技有限公司 一种利用活性炭法吸附回收金方法
EP3822374B1 (fr) * 2019-11-18 2023-10-04 Heraeus Deutschland GmbH & Co. KG Procédé de récupération de métal précieux
US11319613B2 (en) * 2020-08-18 2022-05-03 Enviro Metals, LLC Metal refinement

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4551213A (en) * 1984-05-07 1985-11-05 Duval Corporation Recovery of gold
AP538A (en) * 1992-06-26 1996-09-18 Intec Pty Ltd Production of metal from minerals
US5542957A (en) * 1995-01-27 1996-08-06 South Dakota School Of Mines And Technology Recovery of platinum group metals and rhenium from materials using halogen reagents
FI113667B (fi) * 2002-04-23 2004-05-31 Outokumpu Oy Menetelmä kullan talteenottamiseksi

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2005106052A1 *

Also Published As

Publication number Publication date
AU2005238241A1 (en) 2005-11-10
FI117709B (fi) 2007-01-31
FI20040621L (fi) 2005-10-31
AR049633A1 (es) 2006-08-23
PE20060226A1 (es) 2006-04-25
EA009726B1 (ru) 2008-02-28
US20070245856A1 (en) 2007-10-25
WO2005106052A1 (fr) 2005-11-10
CN1950524A (zh) 2007-04-18
AP2006003793A0 (en) 2006-10-31
EA200601774A1 (ru) 2007-04-27
CA2564338A1 (fr) 2005-11-10
BRPI0510505A (pt) 2007-10-30

Similar Documents

Publication Publication Date Title
EP1984531B1 (fr) Procédé pour récupérer l'or par lixiviation halogène
AU2011228956B2 (en) Method of processing nickel bearing raw material
PL201418B1 (pl) Sposób odzyskiwania metalicznego cynku z minerału cynkowego
CN101278064A (zh) 以基于氯化物的浸出方式处理含镍原料的方法
AU2003215694B2 (en) Method for the recovery of gold
US4067952A (en) Leaching of copper-nickel concentrates
WO2001083835A2 (fr) Procede de recuperation d'or
US20070245856A1 (en) Method for Recovering Gold
CN100366767C (zh) 用氯化物浸析和萃取回收金属的方法
JP4406745B2 (ja) Ｓｎ，Ｐｂ，Ｃｕ含有物質の処理方法
WO2005106051A1 (fr) Procede de recuperation d'or lie a la production de cuivre
JP4269586B2 (ja) 白金族元素の分離方法
US6861037B1 (en) Method of removal of impurities from gold concentrate containing sulfides
RU2004111286A (ru) Способ извлечения цинка
MX2008010507A (en) Method for recovering gold

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20061019

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LT LU MC NL PL PT RO SE SI SK TR

DAX Request for extension of the european patent (deleted)
RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: OUTOTEC OYJ

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

RIC1 Information provided on ipc code assigned before grant

Ipc: C22B 3/10 20060101AFI20100520BHEP

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20101012