[go: up one dir, main page]

WO2004081242A1 - Recuperation de metaux a partir de poussieres industrielles - Google Patents

Recuperation de metaux a partir de poussieres industrielles Download PDF

Info

Publication number
WO2004081242A1
WO2004081242A1 PCT/AU2004/000267 AU2004000267W WO2004081242A1 WO 2004081242 A1 WO2004081242 A1 WO 2004081242A1 AU 2004000267 W AU2004000267 W AU 2004000267W WO 2004081242 A1 WO2004081242 A1 WO 2004081242A1
Authority
WO
WIPO (PCT)
Prior art keywords
leaching
solution
stage
solids
acid
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/AU2004/000267
Other languages
English (en)
Inventor
John Moyes
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.)
Intec Ltd
Original Assignee
Intec Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Intec Ltd filed Critical Intec Ltd
Publication of WO2004081242A1 publication Critical patent/WO2004081242A1/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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/02—Apparatus therefor
    • 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
    • C22B19/00—Obtaining zinc or zinc oxide
    • C22B19/30—Obtaining zinc or zinc oxide from metallic residues or scraps
    • 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
    • C22B3/10—Hydrochloric acid, other halogenated 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
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/006—Wet processes
    • C22B7/007—Wet processes by acid leaching
    • 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
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/02—Working-up flue dust
    • 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 process and apparatus for leaching metal contaminant (s) from industrial dusts, in particular electric arc furnace dusts (in various parts of the specification these dusts will be denominated by the nomenclature EAF for brevity) .
  • the present applicant has previously developed a number of combined leaching/electrolysis processes for the electro-recovery of metals including copper, zinc, nickel and lead. Examples of such processes are shown in the applicant's Australian patent 669906 and the applicant's Australian patent application 2002328671 (WO 03/023077) .
  • the present invention provides a process for leaching metal contaminant (s) from an EAF dust, the process replacing a leaching stage in a combined leaching/electrolysis circuit wherein, in the leaching stage, a metal-containing material is leached in a solution and, in an electrolysis stage, one or more metals are recovered from the solution and an oxidising agent is produced, with the resultant solution and oxidising agent being recycled to the leaching stage for further leaching, the process comprising the steps of: feeding the EAF dust to a first leaching stage to form a mixture of EAF solids with a solution of relatively low acidity such that at least some of the metal contaminant (s) are leached into the solution; passing solids from the first leaching stage to a second leaching stage to form a mixture of the solids with a solution of relatively high acidity such that at least some of any remaining metal contaminant (s) are leached into the solution; passing at least a portion of the solution from the first leaching stage
  • the leaching process of the present ⁇ invention provides two leaching stages, one of relatively low acidity and one of relatively high acidity.
  • This enables metals that are leached in the first leaching stage to be withdrawn from the process, typically in a clarified solution, and fed to the electrolysis stage.
  • More difficult to leach components of the EAF dust can then be passed with the solids to the second leaching stage having a higher acidity, and can be leached in that stage without affecting the leaching conditions in the first leaching stage.
  • the solution employed in the combined leaching/electrolysis circuit, incorporating the leaching process of the present invention includes a halide or a mixture of different halides.
  • an oxidising agent is produced in an anode compartment of the or each electrolysis cell employed in that circuit.
  • the oxidising agent produced is a halogen gas (when the solution includes a single halide) or is a soluble complex halide species (when the solution includes two or more different halides - eg. BrCl 2 " when the solution includes both chloride and bromide) .
  • halogen gas when the solution includes a single halide
  • a soluble complex halide species when the solution includes two or more different halides - eg. BrCl 2 " when the solution includes both chloride and bromide
  • Other complex halide species may also be produced, including dissolved metal halide complexes.
  • Halide based oxidising agents have the advantage that they have a high oxidising potential, and thus can be used to generate strong acids for feeding to the second leaching stage.
  • the acid generating substance reacts with the halogen gas or the soluble halide species to produce acid in the solution that is recycled to the second leaching stage of the leaching process.
  • the acid produced is a halide-based acid such as hydrochloric acid, although other halide- based acids may be produced depending on the solution chemistry (eg. hydrobromic acid etc.).
  • the acid generating substance employed is sulphur so that two acids are formed, eg. hydrochloric acid (when the solution halide is chloride) and sulphuric acid.
  • sulphur as the acid generating substance, including the fact that sulphiric acid is produced, and the resultant sulphate ion can be used to precipitate out undesirable metals (eg. calcium) in the first leaching stage, for subsequent removal and disposal (calcium sulphate being environmentaly friendly and readily disposable) .
  • the acid generating substance can be for example, a gas (eg. hydrogen gas) which can be reacted with a halogen gas produced in the electrolysis circuit (eg. chlorine or bromine gas) to then produce an acid for feeding into the second leaching stage.
  • a gas eg. hydrogen gas
  • a halogen gas produced in the electrolysis circuit eg. chlorine or bromine gas
  • the solution of relatively high acidity has a sufficiently high acidity (sufficiently low pH) to leach and dissolve difficult to leach/react substances in the dust and/or residue such as spinnels (ie. ZnO.Fe 2 0 3 ) .
  • a low pH can be employed in the second leaching stage and a relatively high pH can be employed in the first leaching stage.
  • those metal contaminants which are leached at relatively high pH can be leached in one stage in optimal conditions. Then, the more refractory (ie. difficult to leach) compounds can be leached in the higher acidity, lower pH stage.
  • ferric ion can advantageously be produced which can then be recycled from the second leaching stage to the first leaching stage to participate in further leaching (oxidation) of the EAF dust fed to the process.
  • the first leaching stage has a relatively higher pH, (typically greater than pH 1.5) hematite is not preferentially formed with the ferric ion recycled from the second to the first leaching stage, thus freeing the ferric ion to participate in EAF solids leaching.
  • the solution recycled to the leaching process is reacted with the acid generating substance in a separate reaction stage to thereby separately generate the acid.
  • the resultant acidic solution is then recycled to the leaching process.
  • Producing the acid in a separate stage enables the solution parameters to be controlled and optimised, typically the pH and Eh
  • a separate reaction stage may not necessarily be required and, for example, the acid can be formed in the solution as it is recycled to the second leaching stage, or may even be formed in the second leaching stage itself.
  • a portion of the mixture from the first leaching stage is passed to a thickening stage.
  • this portion represents the entire out flow from the first leaching stage to match the mass inflow into the first leaching stage (ie. feed of EAF dust together with recycled solution from the second leaching stage) .
  • an overflow therefrom defines the solution passed to the electrolysis stage and an underflow therefrom defines the solids passed to the second leaching stage.
  • the underflow is typically a slurry incorporating a small portion of the solution withdrawn from the first leaching stage (but in an idealised model would be entirely solids) .
  • the solution recycled from the second to the first leaching stage is first passed through a solid- liquid separation stage.
  • the separation stage is used to separate out solids present in that solution prior to recycling a clarified (typically filtered) solution to the first leaching stage.
  • a filtration process comprises the solid-liquid separation stage (eg. using one or a multiple number of plate filters) .
  • the solids removed from the separation stage can then be disposed of or re-used elsewhere.
  • At least one of the metal contaminants in the EAF dust is electrolytically recovered in the electrolysis stage.
  • EAF dust usually comprises zinc oxide so that at least zinc is electrolytically recovered in the electrolysis stage.
  • lead may also be electrolytically recovered.
  • contaminants such as cadmium, copper, manganese, silver and mercury are converted to by-products.
  • these contaminants may be precipitated out of solution in a separate purification stage, prior to electrolytic recovery, for subsequent processing or disposal.
  • a number of them may be electrolytically or otherwise recovered in a parallel or series processing circuit.
  • EAF dusts include high levels of iron and, to a lesser extent, calcium.
  • iron typically a ferric oxide precipitate (eg. hematite) is formed in the first leaching stage, which is passed with the solids fed to the second leaching stage for subsequent removal therefrom (typically in the solid-liquid separation stage) .
  • the EAF dust typically includes calcium, typically the acid generating substance employed is sulphur, so that a calcium sulphate precipitate is formed in the first leaching stage (ie. as a result of sulphate ion present in the solution recycled from the second to the first leaching stage) . Again, this calcium sulphate precipitate can be passed with the solids fed to the second leaching stage for subsequent removal therefrom (typically in the solid-liquid separation stage) .
  • the present invention provides a combined leaching/electrolysis process for the recovery of one or more metals from an EAF dust, wherein the leaching process of the combined process is as defined in the first aspect .
  • the present invention provides apparatus for leaching metal contaminant (s) from an EAF dust, the apparatus for use in a leaching stage in a combined leaching/electrolysis circuit wherein, in the leaching stage, a metal-containing material is leached in a solution and, in an electrolysis stage, one or more metals are recovered from the solution and an oxidising agent is produced, with the resultant solution and oxidising agent being recyclable to the leaching stage for further leaching, the apparatus comprising: a first leaching vessel into which the EAF dust is fed to form a mixture of EAF solids with a solution of relatively low acidity so that at least some of the metal contaminant (s) can be leached into the solution; a second leaching vessel into which solids from the first leaching stage are passed to form a mixture of the solids with a solution of relatively high acidity so that at least some of any remaining metal contaminant (s) can be leached into the solution; and acid generating means for producing the solution of relatively high acid
  • the acid generating means is a reactor, typically a continuously stirred tank reactor, into which the recycled solution with oxidising agent and acid generating substance are fed and reacted.
  • the reactor is typically operated such that the solution of relatively high acidity is optimally produced which is then passed to the second leaching vessel .
  • each of the first and second leaching vessels is a continuously stirred tank reactor and typically the vessels are operated in a countercurrent leaching configuration.
  • a single vessel is employed in each stage, however, multiple vessels may also constitute each of the first and second leaching stages.
  • the apparatus further comprises a thickener into which is fed a mixture of EAF solids and the solution of relatively low acidity withdrawn from the first leaching vessel .
  • a clarified overflow solution is withdrawn from the thickener for passing to the electrolysis stage whilst a solids underflow is withdrawn from the thickener for passing to the second leaching vessel .
  • the apparatus further comprises a solid- liquid separator, typically a filtration apparatus, into which is passed a solution to be recycled from the second to the first leaching vessel .
  • the separator separates and removes solids present in that recycled solution so that a filtered (clarified) solution is returned to the first leaching vessel.
  • the solids can then be disposed of or re-used elsewhere.
  • a fourth aspect the present invention relates to any metal produced by the processes of the first and second aspects or recovered in the apparatus of the third aspect .
  • Figure 2 shows a process flow diagram for a preferred leaching process in accordance with the present invention.
  • the present invention will first be described with reference to its incorporation into a known zinc electrolytic recovery process, however, it should be appreciated that it is not in any way limited to use in this process.
  • ZRP zinc recovery process
  • This process is set forth in detail in WO 03/023077 (Australian patent application number 2002328671) , the entire contents of which are incorporated herein by reference .
  • This zinc recovery process is schematically depicted in Figure 1.
  • the present invention was advantageously and surprisingly able to be combined with the applicant's ZRP to allow the processing of secondary zinc-bearing materials such as electric arc furnace (EAF) dusts.
  • EAF electric arc furnace
  • Non-limiting examples according to the present invention will now be described. Examples Processing of EAF Dust
  • a modification was made to the applicant's ZRP to enable processing of EAF dusts. This modification related to the leach circuit only. The purification and electrowinning circuits of the ZRP remained unaltered and thus were able to be used for the recovery of zinc from the EAF dust.
  • Figure 1 schematically depicts the applicants ZRP.
  • the leach circuit is shown bounded by dotted outline.
  • FIG. 2 schematically depicts modifications made to the leach circuit of Figure 1 in accordance with the present invention.
  • the modified leach circuit had three primary reaction stages (or zones) labelled in Figure 2 as (1) , (2) and (3) .
  • the chemical reactions which took place in these three primary stages were as follows:
  • the modified leach circuit was based on a two-stage counter-current configuration with the EAF dust added to stage (1) and the leach liquor added to stage (2) .
  • the third stage (3) was included for the purpose of generating acid used in the leaching stages, making use of an oxidant generated in and supplied by the zinc electrowinning circuit.
  • HalexTM oxidising agent was typically recycled to the leaching stage in the ZRP to oxidise sulfide mineral concentrates fed to the process .
  • EAF dust was a fully oxidised material and could only be leached with acid.
  • stage (1) located in stage (1) (the thickener was used to separate the Stage (1) slurry into clear liquor and solids (described below) ) .
  • Stage (1) the EAF dust had been depleted of all easily leachable components leaving only the relatively refractory components, such as zinc ferrite (ZnO.Fe 2 0 3 ), to be leached in Stage (2) .
  • Stage (2) the relatively refractory components were contacted with the highly acidic Stage (3) liquor. Leaching occurred according to reaction (2), repeated as follows:
  • Stage (1) As described above, the acidic ferric liquor from Stage (2) was fed to Stage (1) along with fresh EAF dust where the residual acid was utilised to directly to leach zinc and other minor metals such as lead, copper, cadmium, silver, mercury, etc. This leaching is represented by reactions 1 (a), (b) and (d) above.
  • additives to the process could include additional acid.
  • sulphuric acid was not generated
  • sulphate ion was also able to be added to the process to precipitate out eg. calcium sulphate.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Metallurgy (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Manufacturing & Machinery (AREA)
  • Environmental & Geological Engineering (AREA)
  • Geology (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Inorganic Chemistry (AREA)
  • Electrolytic Production Of Metals (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

La présente invention a trait à un procédé de lixiviation de contaminant(s) métallique(s) à partir d'une poussière de four à arc électrique se substituant à un étage de lixiviation dans un circuit combiné de lixiviation/électrolyse. Dans l'étage de lixiviation un matériau contenant du métal est soumis à une lixiviation dans une solution et dans l'étage d'électrolyse un ou des métaux sont récupérés à partir de la solution et un oxydant est produit. La solution obtenue et l'oxydant sont recyclés vers l'étage de lixiviation pour une lixiviation supplémentaire. Le procédé comprend les étapes suivantes : l'alimentation de poussière de four à arc électrique à un premier étage de lixiviation pour la formation d'un mélange de matières solides de four à arc électrique avec une solution d'acidité relativement faible de sorte qu'au moins certains des contaminants métalliques soient soumis à un lixiviation dans la solution ; le passage des matières solides depuis le premier étage de lixiviation vers un deuxième étage de lixiviation pour la formation d'un mélange de matières solides avec une solution d'acidité relativement élevée de sorte que certains des contaminants métallique(s) restants soient soumis à une lixiviation dans la solution ; le passage d'au moins une portion de la solution depuis le premier étage de lixiviation vers le stage d'électrolyse pour la récupération de métaux ; et le recyclage de la solution depuis le deuxième étage de lixiviation vers le premier étage de lixiviation. La solution d'acidité relativement élevée est produite par la réaction de l'oxydant avec une substance de génération d'acide.
PCT/AU2004/000267 2003-03-10 2004-03-03 Recuperation de metaux a partir de poussieres industrielles Ceased WO2004081242A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2003901066 2003-03-10
AU2003901066A AU2003901066A0 (en) 2003-03-10 2003-03-10 Recovery of metals from industrial dusts

Publications (1)

Publication Number Publication Date
WO2004081242A1 true WO2004081242A1 (fr) 2004-09-23

Family

ID=31500111

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/AU2004/000267 Ceased WO2004081242A1 (fr) 2003-03-10 2004-03-03 Recuperation de metaux a partir de poussieres industrielles

Country Status (2)

Country Link
AU (1) AU2003901066A0 (fr)
WO (1) WO2004081242A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006119611A1 (fr) * 2005-05-10 2006-11-16 George Puvvada Procede de traitement de poussieres electriques et autres poussieres de four et residus contenant des oxydes et ferrites de zinc
RU2346065C1 (ru) * 2007-06-13 2009-02-10 Институт химии и технологии редких элементов и минерального сырья им. И.В. Тананаева Кольского научного центра Российской академии наук (ИХТРЭМС КНЦ РАН) Способ переработки пыли медного производства
RU2348714C1 (ru) * 2007-06-13 2009-03-10 Институт химии и технологии редких элементов и минерального сырья им. И.В. Тананаева Кольского научного центра Российской академии наук Способ извлечения меди из сульфатсодержащей пыли медного производства
CN107604180A (zh) * 2017-09-07 2018-01-19 湖南三立集团股份有限公司 一种湿法炼锌净化除杂方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4272341A (en) * 1980-01-09 1981-06-09 Duval Corporation Process for recovery of metal values from lead-zinc ores, even those having a high carbonate content
WO1994000606A1 (fr) * 1992-06-26 1994-01-06 Intec Pty. Ltd. Production de metaux a partir de mineraux
WO2003023077A1 (fr) * 2001-09-13 2003-03-20 Intec Ltd Procede d'extraction de zinc

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4272341A (en) * 1980-01-09 1981-06-09 Duval Corporation Process for recovery of metal values from lead-zinc ores, even those having a high carbonate content
WO1994000606A1 (fr) * 1992-06-26 1994-01-06 Intec Pty. Ltd. Production de metaux a partir de mineraux
WO2003023077A1 (fr) * 2001-09-13 2003-03-20 Intec Ltd Procede d'extraction de zinc

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006119611A1 (fr) * 2005-05-10 2006-11-16 George Puvvada Procede de traitement de poussieres electriques et autres poussieres de four et residus contenant des oxydes et ferrites de zinc
RU2346065C1 (ru) * 2007-06-13 2009-02-10 Институт химии и технологии редких элементов и минерального сырья им. И.В. Тананаева Кольского научного центра Российской академии наук (ИХТРЭМС КНЦ РАН) Способ переработки пыли медного производства
RU2348714C1 (ru) * 2007-06-13 2009-03-10 Институт химии и технологии редких элементов и минерального сырья им. И.В. Тананаева Кольского научного центра Российской академии наук Способ извлечения меди из сульфатсодержащей пыли медного производства
CN107604180A (zh) * 2017-09-07 2018-01-19 湖南三立集团股份有限公司 一种湿法炼锌净化除杂方法

Also Published As

Publication number Publication date
AU2003901066A0 (en) 2003-03-20

Similar Documents

Publication Publication Date Title
Jha et al. Review of hydrometallurgical recovery of zinc from industrial wastes
CN1252293C (zh) 利用氯化物处理从复合硫化物精矿中制备氧化锌
CN101278064B (zh) 以基于氯化物的浸出方式处理含镍原料的方法
CN1210417C (zh) 从硫化物浮选精矿中回收镍、钴和铜的湿法冶金方法
US7465334B2 (en) Zinc recovery process
CN102859012B (zh) 处理含镍原料的方法
Antuñano et al. Hydrometallurgical processes for Waelz oxide valorisation–An overview
WO2001023627A1 (fr) Procede de recuperation selective de metaux dans les dechets a l'etat de poussieres, boues et minerais
JP5721213B2 (ja) 酸化亜鉛及び／又は金属含有溶液からの純金属インジウムの製造方法
BG62180B1 (bg) Хидрометалургично извличане на никел и кобалт от сулфиднируди с помощта на хлорид
US8323377B2 (en) Recovery of metals from oxidised metalliferous materials
WO1998036102A1 (fr) Raffinage de minerais contenant du sulfure de zinc
JP2011021219A (ja) 含銅鉄物からの銅回収方法
JP5370777B2 (ja) 銅硫化物からの銅の回収方法
WO2015192234A1 (fr) Récupération de zinc et de manganèse à partir de résidus ou de boues de pyrométallurgie
US20110283831A1 (en) Process for the Recovery of Nickel and/or Cobalt from a Leach Solution
JP4710034B2 (ja) 砒素含有物質の処理方法
JP2010059035A (ja) 脱銅スライムからの高純度亜砒酸水溶液の製造方法
WO2020107122A1 (fr) Procédé de récupération de métaux de valeur à partir de minerais, de concentrats, d'intermédiaires et de déchets contenant du zinc
CN113354164B (zh) 酸性湿法炼锑溶液的综合处理方法
US4384890A (en) Cupric chloride leaching of copper sulfides
WO2004081242A1 (fr) Recuperation de metaux a partir de poussieres industrielles
WO2011120093A1 (fr) Récupération de métaux à partir d'une liqueur de décapage
CN105765090A (zh) 从起始材料中分离砷的方法和布置
AU769984B2 (en) Process for recovering metal values

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): BW GH GM KE LS MW MZ SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IT LU MC NL PL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
DPEN Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed from 20040101)
122 Ep: pct application non-entry in european phase