US3917519A - Process for the manufacture of electrolytic copper - Google Patents

Process for the manufacture of electrolytic copper Download PDF

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Publication number
US3917519A
US3917519A US44631474A US3917519A US 3917519 A US3917519 A US 3917519A US 44631474 A US44631474 A US 44631474A US 3917519 A US3917519 A US 3917519A
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Prior art keywords
copper
slurry
sulfide
solids
calcium
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Bernard M Fisher
Robert C Hills
Freddie J Touro
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Freeport Minerals Co
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Freeport Minerals Co
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Priority to US44631474 priority Critical patent/US3917519A/en
Priority to CA218,933A priority patent/CA1041037A/fr
Priority to GB384675A priority patent/GB1484976A/en
Priority to AU77919/75A priority patent/AU7791975A/en
Priority to PH16784A priority patent/PH10724A/en
Priority to DE19752505417 priority patent/DE2505417A1/de
Priority to JP50023794A priority patent/JPS5817814B2/ja
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Publication of US3917519A publication Critical patent/US3917519A/en
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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
    • 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
    • C22B15/0086—Treating solutions by physical 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
    • C22B15/0063—Hydrometallurgy
    • C22B15/0084—Treating solutions
    • C22B15/0089—Treating solutions by chemical methods
    • 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

  • ABS CT P A process is described for making electrolytic copper [73] Asslgnee' fi f g rals Company New of high quality from chalcopyrite flotation concen- Or trates, and the like.
  • the concentrates are first slurried [22] Filed: Feb. 27, 1974 and then subjected to a high temperature-high pressure oxidation-leaching operation in an autoclave sys- [21] Appl. No.: 446 314 tem under controlled conditions, The resulting slurry from the oxidation-leaching operation is flashed to at- [52] U.S. Cl.
  • hydrometallurgical processes for the most part, do not involve the generation of sulfur dioxide and the consequent problems of air pollution characteristic of pyrometallurgical process.
  • Another reason for considering hydrometallurgical processes is the extreme flexibility afforded with regard to the virtually infinite sets of unique conditions of temperature, pressure, retention time, specific solvents and additives and procedures that can be resorted to for whatever particular metallurgical separation one is confronted with.
  • the preliminary steps for producing the electrolyte include the best possible solids-liquid separation, reduction ofdissolved iron and arsenic to minimal levels, and concentration of copper, as copper sulfate, to maximum levels in the feed to the electrowinning step. While a variety of methods are available for carrying out each of these steps, in most known processes these individual methods do not always complement each other, i.e., they lack in technological compatibility with regard to making up an efficient, economical, pollution-free process. It is an object of this invention to provide a process wherein each individual step is uniquely suited to the others and to the overall process for manufacturing a high quality metallic copper product efficiently and economically. A sec ondary object is to circumvent the production of sulfur dioxide and thereby negate the possiblity of air pollution.
  • the present invention provides a process wherein a copper sulfide flotation concentrate, at least a portion of which is chalcopyrite, CuFeS is first mixed with water and recycle process liquors and slurries.
  • the concentrate may be slurried with recycle process liquors and slurries only.
  • the resulting slurry is then subjected to a high temperaturehigh pressure operation in an autoclave system, wherein the temperature is closely controlled and an oxygen partial pressure (from industrial oxygen or an oxygen bearing gas) is maintained.
  • the autoclave sys tern may be a single vessel or a series of vessels
  • the oxidation in the high temperature-high pressure operation results in the formation of sulfuric acid and the solubilization of the metal constituents of the concentrate in the form of sulfates.
  • iron and arsenic also are dissolved by the acid, but the latter two are removed from solution, after solubilization of virtually all of the copper, by the neutralization of the greater portion of the sulfuric acid with a neutralizing agent such as limestone.
  • the neutralization of the sol furic acid results in the precipitation of virtually all of the dissolved iron and arsenic.
  • the slurry is flashed to atmospheric pressure and fed to a solids-liquid separation system.
  • the separated liquor from the solids-liquid separation system is then cooled and fed to an electrolytic deposition operation where end-product copper cathodes are produced.
  • the solids from the solids-liquid separation operation are normally washed with water and the return wash water, containing residual copper values, is recycled back to the initial stages of the process.
  • the washed solids composed of the ore gangue and the materials precipitated in the autoclave-Fe O (hematite), iron and calcium arsenates, and CaSO (anhydrite)are sent on for further processing or to waste.
  • the spent electrolyte from the electrolytic deposition operation is then treated with a sulfiding agent, such as hydrogen sulfide, to precipitate, as copper sulfide, the copper values not deposited with the copper cathodes.
  • a sulfiding agent such as hydrogen sulfide
  • the copper sulfide slurry is then thickened to a solids content of between about 3 and l5 percent and recycled back to the initial stages of the process.
  • the various steps required are uniquely compatible with each other and with the overall process.
  • the high-temperature precipitation of iron and calcium as hematite and anhydrite, respectively makes the subsequent solids-liquid separation much easier than if the precipitated materials were ferric hydroxide and gypsum as would be obtained in a low-temperature processv
  • the steps wherein water vapor is removed from the liquor in the process of venting noncondensable gases, or controlling the temperature, or flashing, etc. are compatible with the overall object of the leaching step, that is, providing a liquor with a maximum concentration of copper as copper sulfite and a very low concentration of dissolved iron.
  • a chalcopyrite flotation concentrate 1 containing between about 20 and 30% copper, is fed into a slurry tank and mixed with recycle wash water 16 containing residual amounts of copper sulfate and sulfuric acid, and with a recycle acidic slurry of copper sulfide 22.
  • the resultant slurry 2 is fed continuously to a high temperature-high pressure oxidation-leaching operation which, in a preferred embodiment, is carried out in a multi-compartment, horizontal autoclave system equipped with agitators.
  • the slurry temperature is maintained between 350 and 450F, and preferably between 425 and 450F.
  • the total pressure is maintained at between about 300 and I000 psig, and preferably between about 400 and 600 psig, by the introduction of a high quality oxygen-containing gas 3 so as to provide an oxygen partial pressure of between about 50 and 500 psi, and preferably between about 100 and 200 psi.
  • the oxygencontaining gas used should have an oxygen content of at least about and preferably in the order of 99%.
  • the oxidizing chemical reactions in the autoclave system result in the formation of sulfuric acid and the dissolution of the copper and iron as sulfates. Because the oxidizing reactions are exothermic, heat must be removed to maintain the temperature within the desired range. Water may be removed from the system during the oxidation-leaching operation, resulting in a desirable increase in the concentration of the sulfates in the slurry liquor.
  • the autoclave system may be a single pressurized vessel or may include several pressurized vessels.
  • Removal of water also serves to increase the concentration of the acidity of the slurry, which is desirable, since increased acidity results in increased copper extraction rates when the oxidation-leaching operation is carried out under the preferred temperature conditions of 425450F.
  • Control of the acidity during the oxidation-leaching of chalcopyrite forms the subject matter of another copending application for US. Pat. Ser. No. 446,315, filed Feb. 27, 1974 by Freddie .I. Touro, one of the present inventors.
  • a neutralizing agent such as limestone slurry 4 is added in the autoclave system so as to reduce the acidity to less than about 40 grams per liter H 80 preferably between about IO and 20 grams per liter H 80 and permit the hydrolysis of Fe (SO and precipitation of iron as Fe O- Neutralization of the acidity at a temperature between 425450F in the autoclave is a particularly preferred embodiment of the process because in this temperature range the iron is precipitated as hematite (Fe O and the calcium as anhydrite (CaSO both of which are crystalline in nature and their precipitation in this form results in the satisfactory separation of the solids from the liquid later in the process. In contrast, the precipitates obtained at low temperatures (iron as ferric hydroxide, and calcium as gypsum) are much more difficult to separate from the liquid phase.
  • While limestone i.e., calcium carbonate, has been described as the neutralizing agent used in the preferred embodiment, other neutralizing agents may be utilized.
  • the hydroxides, oxides and carbonates of calcium, strontium and barium, all of which form insoluble sulfate, may be used as the neutralizing agent.
  • the slurry is provided additional retention tim in the autoclave system at the preferred temperature of between 425 and 425F, and at the stated oxygen partial pressure with constant mechanical agitation. During this time, additional iron is precipitated and further oxidation and dissolution of copper may occur.
  • a vaporspace bleed-stream may be vented to atmosphere from the autoclave to purge the gradual buildup of contaminant nitrogen (introduced with the oxygencontaining gas). Some oxygen is lost with this bleedstream as well as some water vapor. The loss of the latter again serves to increase the copper concentration in the leach liquor and to remove some heat.
  • the treated slurry stream 5 leaving the autoclave is made up of a liquid phase composed of a solution of acidic copper sulfate and solids composed of gangue, anhydrite (CaSO and hematite (Fe O Before this liquid phase is separated from these solids, the slurry is subjected to a flashing operation.
  • the flashing operation may optionally be preceded by an indirect cooling operation.
  • the flashing operation is preceded by an indirect cooling operation, as indicated in the drawing.
  • the slurry is first cooled with water 6 in an indirect heat exchanger to approximately 275400F while maintaining the same pressure as used in the autoclave.
  • the heat exchanger may be a waste heat boiler, for example, generating 15 psig steam. This reduction in temperature is provided so that when the cooled slurry 7 is finally flashed to atmospheric pressure, the volume of flashed steam produced 8 is significantly less than that which would be produced if flashing occurred at the original temperature of between 425 and 450F. As a result, the velocity of the slurry -steam mixture through the letdown valve is decreased and the erosion of the valve reduced in severity.
  • a portion of the cooled separated liquor 13 is recycled to cool the slurry, as it leaves the flashing operation, as described above.
  • additional water 11 is removed under vacuum at about 120F to further increase the copper concentration of the leach liquor. Removal of water at this point has the beneficial effect of increasing the wash water-to-tailings ratio that may be used in the washing system.
  • the solids are washed with water 15 to recover the retained copper sulfate solution.
  • the return wash water 16, containing copper values and dilute sulfuric acid, is recycled back to the slurry preparation facilities.
  • the washed solids tailings 17 may be sent to a tailings pond or to further treatment for the recovery of gold or silver, etc.
  • any type of solids-liquid separation techniques such as filtration, centrifuging, etc., may be employed in these operations; however, a thickener or a combination of thickeners is preferred.
  • the portion of the I20F liquor from the barometric condenser that is not recycled 12 is fed to the electrolytic cells. At this point, the concentration of copper in the separated copper sulfate solution has been increased to about grams per liter.
  • copper cathodes 18 of as high as 99.9 percent purity can be produced as final product. Heat is liberated during this or eration and should be removed in order to keep the temperature in the electrolytic cells at about 150F or less. Sulfuric acid is also produced to the stoichiometric extent of the copper deposited so that the spent electrolyte l9 normally contains between about 5 and 15 grams per liter of copper and between about and 170 grams per liter of sulfuric acid.
  • the spent solution 19 is then treated with a sulfiding agent 20 to precipitate the copper as copper sulfide.
  • a sulfiding agent 20 Any one of a number of sulfiding agents which cause the precipitation of the copper from spent electrolyte 19 as copper sulfide, such as hydrogen sulfide (H 8), ammonium sulfide (NH S), sodium sulfide (Na S), ammonium hydrosulfide (NH HS), sodium hydrosulfide (NaI-IS), potassium sulfide (K 5) and potassium hydrosulfide (Kl-IS), may be used.
  • hydrogen sulfide (H 8) is used.
  • the sulfided slurry 21 is processed in a thickener and the thickened acidic copper sulfide (CuS) slurry 22, having a solids content of between about 3 percent and percent and preferably higher than 5 percent, is recycled to the feed slurry tank.
  • CuS copper sulfide
  • About 70-90% of spent electrolyte stream 19 can be bled from the process via stream 23 by this method with minimal loss of copper. This bleed serves to eliminate from the process certain soluble impurities such as calcium, magnesium, nickel and cobalt.
  • the acidic supernatant liquor stream 23 from the thickener may be treated with a limestone slurry 24, as shown in the drawing, and the resultant gypsum slurry 25 pumped to waste, i.e., to holding ponds or land-fill areas, or it may be used in any other process which requires the use of a dilute sulfuric acid solution.
  • Example 1 illustrates the manner in which the process of this invention may be operated.
  • Chalcopyrite concentrate 1 may be fed to the system of the drawing and mixed with recycle streams l6 and 22 as previously indicated.
  • the composition of stream 1 is given below, in Table 1, together with the typical compositions of other pertinent streams of the process.
  • Oxidation-leaching of the slurried concentrate 2 is carried out at 425F and 100 psi of oxygen partial pressure in an autoclave system. Total pressure is 445 psig.
  • Limestone 4 is used to partially neutralize the acidity during oxidation-leaching so that the exiting slurry 5 goin J the indirect cooler has an acidity of about grams per liter H 80
  • the temperature of slurry 5 is decreased in the indirect cooler to about 320F.
  • Partially cooled slurry 7 is then flashed to atmospheric pressure and to a temperature of about 230F, and blended with cooled recycle liquor stream 13 for further cooling to 150F before entering the solids-liquid separation system.
  • the solids-liquid separation is carried out in one thickener, and the bottoms 14 from this thickener are washed with water in a countercurrent fashion using three thickeners. Tailings 17 from the last washing 6 thickener may be sent to waste.
  • the overflow 10 from the solids-liquid separation thickener is further cooled to 120F using a barometric condenser and then divided into stream 13, which is used for blending with the flashed slurry, as described above, and stream 12, which is fed to the electrolytic deposition operation.
  • Copper cathodes 18 of high purity are produced in the electrolytic cells.
  • the temperature in this operation normally tends to rise and so an external cooler (not shown) is provided to maintain it at about I50F.
  • the copper content of the electrolyte is reduced from about -80 grams per liter (in stream 12) to about 5 grams per liter (in stream 19). Depletion of the copper, during electrolysis, to below about 5 grams per liter is not deemed economically attractive in view of the convenience of scavenging the copper values not deposited during electrolysis which is provided by the subsequent sulfiding operation of our process.
  • Spent electrolyte 19 is treated with hydrogen sulfide 20 in an amount sufficient to precipitate as copper sulfide virtually all of the copper present in solution at this point.
  • Sulfided slurry 21 is thickened and recycled as stream 22 to the slurry feed tank.
  • the overflow stream 23 from the sulfide thickener contains most of the impurities not rejected in the oxidation-leaching as precipitated solids and is conveniently treated with limestone 24 and pumped to waste 25. It is significant of the process of this invention that these impurities are rejected from the system in the manner just described and without losing any significant amount of copper values.
  • a process in which the spent electrolyte 19 is sent to waste would lose significant amounts of copper values as dissolved copper in the waste spent electrolyte.
  • the copper values not deposited in the electrolytic deposition operation are conveniently recovered by the recycling of a relatively concentrated copper sulfide slurry 22 to the initial stages of the process without the recycling of impurities or large quantities of undesirable water to the initial stages of the process.
  • a process which chose to recycle the spent electrolyte 19 from the electrolyte deposition operation in order to recover the copper values not deposited during electrolysis would do so at the expense of recycling the impurities associated with the spent electrolyte and, of course, of not being able to remove water from the system at this point.
  • said sulfiding agent is selected from the group consisting of hydrogen sulfide, ammonium sulfide, sodium sulfide, ammonium hydrosulfide, sodium hydrosulfide, potassium sulfide, and potassium hydrosulfide.
  • the oxi dation-leaching operation is carried out using an oxygen partial pressure of between about I00 and 200 wherein a first part of said calcium in said calcium carbonate forms insoluble calcium sulfate, wherein said arsenic, solubilized to a metal sulfate in said oxidationleaching operation, is precipitated with at least a part of said calcium as insoluble iron and calcium arsenates upon the addition of said calcium carbonate, and wherein said iron and calcium arsenates are withdrawn from said autoclave as part of the solids in said treated slurry.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Manufacture And Refinement Of Metals (AREA)
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US44631474 1974-02-27 1974-02-27 Process for the manufacture of electrolytic copper Expired - Lifetime US3917519A (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
US44631474 US3917519A (en) 1974-02-27 1974-02-27 Process for the manufacture of electrolytic copper
CA218,933A CA1041037A (fr) 1974-02-27 1975-01-29 Methode de fabrication du cuivre electrolytique
GB384675A GB1484976A (en) 1974-02-27 1975-01-29 Process for the manufacture of electrolytic copper
AU77919/75A AU7791975A (en) 1974-02-27 1975-02-05 Manufacture of electrolytic copper
PH16784A PH10724A (en) 1974-02-27 1975-02-07 Process for the manufacture of electrolytic copper
DE19752505417 DE2505417A1 (de) 1974-02-27 1975-02-08 Verfahren zur gewinnung von kupfer aus einem kupferfuehrenden sulfidischen erz, das eisen enthaelt
JP50023794A JPS5817814B2 (ja) 1974-02-27 1975-02-26 テツオフクム ドウガンユウリユウカコウヨリドウオ カイシユウスル ホウホウ

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US44631474 US3917519A (en) 1974-02-27 1974-02-27 Process for the manufacture of electrolytic copper

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JP (1) JPS5817814B2 (fr)
AU (1) AU7791975A (fr)
CA (1) CA1041037A (fr)
DE (1) DE2505417A1 (fr)
GB (1) GB1484976A (fr)
PH (1) PH10724A (fr)

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4357261A (en) * 1979-07-16 1982-11-02 Sumitomo Metal Mining Company Limited Method for manufacture of a composite copper-arsenic compound mixture
US4364773A (en) * 1980-12-23 1982-12-21 Marcel Veronneau Waste metal conversion process and products
US4606764A (en) * 1983-08-17 1986-08-19 Resource Technology Associates Method of recovering metals from ores using a formate reducing agent
EP0646185A4 (fr) * 1992-06-26 1995-04-26 Intec Pty Ltd
US5498398A (en) * 1993-11-08 1996-03-12 Lucky Metals Corporation Method of treating spent electrolytic solution from electrolytic copper production
WO1996019593A1 (fr) * 1993-07-29 1996-06-27 Cominco Engineering Services Ltd. Extraction hydrometallurgique de cuivre au moyen de chlorures
US5535992A (en) * 1995-03-07 1996-07-16 Goro Nickel S.A. Apparatus and method for acidic leaching of lateritic ores
US5573739A (en) * 1994-10-28 1996-11-12 Noranda, Inc. Selective bismuth and antimony removal from copper electrolyte
US5783057A (en) * 1996-09-19 1998-07-21 Nippon Mining & Metals Co., Ltd. Method of purifying copper electrolytic solution
US6451089B1 (en) * 2001-07-25 2002-09-17 Phelps Dodge Corporation Process for direct electrowinning of copper
US6497745B2 (en) * 2000-07-25 2002-12-24 Phelps Dodge Corporation Method for processing elemental sulfur-bearing materials using high temperature pressure leaching
US20050109163A1 (en) * 2001-07-25 2005-05-26 Phelps Dodge Corporation Process for multiple stage direct electrowinning of copper
US20050126923A1 (en) * 2001-07-25 2005-06-16 Phelps Dodge Corporation Process for recovery of copper from copper-bearing material using medium temperature pressure leaching, direct electrowinning and solvent/solution extraction
WO2005066378A1 (fr) * 2004-01-07 2005-07-21 Grenvil Marquis Dunn Circuits d'autoclave de lixiviation sous pression exothermique
US20060117908A1 (en) * 2004-12-03 2006-06-08 Virnig Michael J Processes for recovering metals from ores using organic solvent extraction and aqueous stripping at selected temperature differentials
US20060144717A1 (en) * 2004-10-29 2006-07-06 Phelps Dodge Corporation Process for recovery of copper from copper-bearing material using pressure leaching, direct electrowinning and solvent/solution extraction
US20080023342A1 (en) * 2004-10-29 2008-01-31 Phelps Dodge Corporation Process for recovery of copper from copper-bearing material using pressure leaching, direct electrowinning and solution extraction
US20090071839A1 (en) * 2004-10-29 2009-03-19 Phelps Dodge Corporation Process for multiple stage direct electrowinning of copper
WO2014122363A1 (fr) * 2013-02-08 2014-08-14 Outotec Oyj Procédé et agencement permettant de réduire la détente automatique et le transfert de bouillie dans des systèmes de détente d'autoclave
US20170009318A1 (en) * 2015-07-06 2017-01-12 Sherritt International Corporation Recovery of Copper from Arsenic-Containing Process Feed
CN111485118A (zh) * 2020-04-14 2020-08-04 长沙有色冶金设计研究院有限公司 一种硫化铜精矿控温氧压平行浸出回收电积铜的方法
US11118244B2 (en) 2017-04-14 2021-09-14 Sherritt International Corporation Low acidity, low solids pressure oxidative leaching of sulphidic feeds
CN114561542A (zh) * 2022-02-25 2022-05-31 盛隆资源再生（无锡）有限公司 一种提高含铁铜废液中铜回收率的方法

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Publication number Priority date Publication date Assignee Title
US4225571A (en) 1979-03-09 1980-09-30 Berenice Isabelle de Denus Electrowinning of metal from sulphide ores and recovery of water soluble sulphides
DE602007013737D1 (de) * 2006-05-01 2011-05-19 Freeport Mcmoran Corp Verfahren zur kupfergewinnung aus kupferhaltigem material mittels drucklaugung, direkter elektrogewinnung und lösemittel-/lösunsgextraktion
JP5423046B2 (ja) * 2009-02-26 2014-02-19 住友金属鉱山株式会社 硫化銅鉱物を含む銅原料の浸出方法
JP5760954B2 (ja) * 2011-10-31 2015-08-12 住友金属鉱山株式会社 銅及び鉄を含有する硫化鉱物から銅を回収する方法
CN109261346B (zh) * 2018-08-23 2020-12-04 北京矿冶科技集团有限公司 一种含易浮钙镁矿物铜钴矿的选矿方法
KR102703301B1 (ko) * 2023-11-14 2024-09-06 고려아연 주식회사 구리를 회수하는 방법

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US3637371A (en) * 1967-02-10 1972-01-25 Sherritt Gordon Mines Ltd Direct pressure leaching of copper-iron sulphides

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3637371A (en) * 1967-02-10 1972-01-25 Sherritt Gordon Mines Ltd Direct pressure leaching of copper-iron sulphides

Cited By (45)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4357261A (en) * 1979-07-16 1982-11-02 Sumitomo Metal Mining Company Limited Method for manufacture of a composite copper-arsenic compound mixture
US4364773A (en) * 1980-12-23 1982-12-21 Marcel Veronneau Waste metal conversion process and products
US4606764A (en) * 1983-08-17 1986-08-19 Resource Technology Associates Method of recovering metals from ores using a formate reducing agent
EP0646185A4 (fr) * 1992-06-26 1995-04-26 Intec Pty Ltd
WO1996019593A1 (fr) * 1993-07-29 1996-06-27 Cominco Engineering Services Ltd. Extraction hydrometallurgique de cuivre au moyen de chlorures
US5498398A (en) * 1993-11-08 1996-03-12 Lucky Metals Corporation Method of treating spent electrolytic solution from electrolytic copper production
US5573739A (en) * 1994-10-28 1996-11-12 Noranda, Inc. Selective bismuth and antimony removal from copper electrolyte
US5535992A (en) * 1995-03-07 1996-07-16 Goro Nickel S.A. Apparatus and method for acidic leaching of lateritic ores
US5783057A (en) * 1996-09-19 1998-07-21 Nippon Mining & Metals Co., Ltd. Method of purifying copper electrolytic solution
US20060191377A1 (en) * 2000-07-25 2006-08-31 Phelps Dodge Corporation Method for processing elemental sulfur-bearing materials using high temperature pressure leaching
US6497745B2 (en) * 2000-07-25 2002-12-24 Phelps Dodge Corporation Method for processing elemental sulfur-bearing materials using high temperature pressure leaching
EP1303640B1 (fr) * 2000-07-25 2004-10-06 Phelps Dodge Corporation Procede pour traiter des materiaux portant du soufre elementaire, par mise en oeuvre d'une lixiviation sous pression a haute temperature
AU2001278015B2 (en) * 2000-07-25 2004-12-23 Freeport-Mcmoran Corporation Processing elemental sulfur-bearing materials using high temperature pressure leaching for sulfuric acid production and metal recovery
US6663689B2 (en) * 2001-07-25 2003-12-16 Phelps Dodge Corporation Process for direct electrowinning of copper
US20040130076A1 (en) * 2001-07-25 2004-07-08 Phelps Dodge Corporation System for direct electrowinning of copper
US20060196313A1 (en) * 2001-07-25 2006-09-07 Phelps Dodge Corporation Method for recovering copper from copper-containing materials using direct electrowinning
US20050109163A1 (en) * 2001-07-25 2005-05-26 Phelps Dodge Corporation Process for multiple stage direct electrowinning of copper
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AU7791975A (en) 1976-08-05
JPS5817814B2 (ja) 1983-04-09
DE2505417A1 (de) 1975-08-28
PH10724A (en) 1977-08-25
JPS50121112A (fr) 1975-09-22
CA1041037A (fr) 1978-10-24
GB1484976A (en) 1977-09-08

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