JP2008512569A - Formation of zinc drugs from treatment tributaries. - Google Patents

Formation of zinc drugs from treatment tributaries. Download PDF

Info

Publication number
JP2008512569A
JP2008512569A JP2007530727A JP2007530727A JP2008512569A JP 2008512569 A JP2008512569 A JP 2008512569A JP 2007530727 A JP2007530727 A JP 2007530727A JP 2007530727 A JP2007530727 A JP 2007530727A JP 2008512569 A JP2008512569 A JP 2008512569A
Authority
JP
Japan
Prior art keywords
zinc
leaching
production
extraction
roasting
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.)
Abandoned
Application number
JP2007530727A
Other languages
Japanese (ja)
Other versions
JP2008512569A5 (en
Inventor
ミッコ ルオナラ、
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 Outotec Oyj
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
Priority to FI20041163A priority Critical patent/FI117139B/en
Application filed by Outokumpu Technology Oyj filed Critical Outokumpu Technology Oyj
Priority to PCT/FI2005/000380 priority patent/WO2006027412A1/en
Publication of JP2008512569A publication Critical patent/JP2008512569A/en
Publication of JP2008512569A5 publication Critical patent/JP2008512569A5/ja
Abandoned legal-status Critical Current

Links

Images

Classifications

    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B19/00Obtaining zinc or zinc oxide
    • C22B19/20Obtaining zinc otherwise than by distilling
    • C22B19/26Refining solutions containing zinc values, e.g. obtained by leaching zinc ores
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B19/00Obtaining zinc or zinc oxide
    • C22B19/20Obtaining zinc otherwise than by distilling
    • C22B19/22Obtaining zinc otherwise than by distilling with leaching with acids
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06Extraction 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
    • C22B3/08Sulfuric acid, other sulfurated acids or salts thereof
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/26Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
    • C22B3/38Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds containing phosphorus
    • C22B3/384Pentavalent phosphorus oxyacids, esters thereof
    • C22B3/3846Phosphoric acid, e.g. (O)P(OH)3
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/26Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
    • C22B3/38Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds containing phosphorus
    • C22B3/385Thiophosphoric acids, or esters thereof
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00Technologies related to metal processing
    • Y02P10/20Recycling

Abstract

本発明は、亜鉛の焙焼−浸出−電解型の生成処理の支流から、純粋な亜鉛薬品を生成する新規な処理装置である。本発明は、焙焼−浸出−電解プラントにおける浸出から得られた硫酸亜鉛含有溶液の生産量の一部が亜鉛薬品の生成に割り当てられるという事実に基づいている。硫酸亜鉛の生産量の一部だけが亜鉛薬品の生成に割り当てられるので、電気分解に基づく亜鉛の実際の回収処理は妨げられない。抽出処理は有機的置換リン酸または有機的置換チオホスフィン酸の使用に基づいている。強酸溶液は、亜鉛の抽出処理において副産物として生産され、焙焼−浸出−電解型の亜鉛の生成処理に戻されて再利用される。
The present invention is a novel processing apparatus that generates pure zinc chemicals from a tributary of zinc roasting-leaching-electrolytic generation. The present invention is based on the fact that a portion of the production of zinc sulfate-containing solution obtained from leaching in a roasting-leaching-electrolysis plant is allocated to the production of zinc chemicals. Since only a portion of the zinc sulfate production is allocated to the production of zinc chemicals, the actual recovery process of zinc based on electrolysis is not impeded. The extraction process is based on the use of organic substituted phosphoric acid or organic substituted thiophosphinic acid. The strong acid solution is produced as a by-product in the zinc extraction process, and returned to the roasting-leaching-electrolytic zinc production process for reuse.

Description

詳細な説明Detailed description

本発明は亜鉛および亜鉛薬品の生成処理に関するものである。より詳細には、本発明は、湿式精錬および亜鉛の生成処理に関連した、亜鉛薬品を生成するための処理装置および処理路に関するものである。   The present invention relates to a process for producing zinc and zinc chemicals. More particularly, the present invention relates to a processing apparatus and a processing path for generating zinc chemicals related to wet refining and zinc generation processing.

亜鉛の生成に関連して、たびたび一次生成および二次生成が話題にのぼる。一次生成処理は、亜鉛鉱石、亜鉛精鉱および焼鉱の様々な溶解、および、液液抽出を含む様々な湿式精錬方法によってそこから得られる溶液の処理をいう。二次生成処理は、例えば、原材料としての電気鉱炉の微粒子、ウェルツ酸化物、および導電性の燃え殻などの、より少ない量の様々な原材料を使用することをいう。   In relation to the production of zinc, primary and secondary production are frequently discussed. Primary production treatment refers to treatment of solutions obtained therefrom by various hydrorefining methods including various dissolution of zinc ore, zinc concentrate and sinter and liquid-liquid extraction. Secondary generation processing refers to the use of smaller amounts of various raw materials such as, for example, electric blast furnace particulates, Welts oxides, and conductive husks as raw materials.

亜鉛の一次生成処理では、従来の原材料、例えば硫化亜鉛鉱石などが精鉱、すなわち亜鉛精鉱され、要望があれば、亜鉛焼鉱はまたさらにこれらから生成される。さらに、濃縮硫酸亜鉛溶液は、しばしば亜鉛精鉱および亜鉛焼鉱から生成され、亜鉛金属の電解生成に適している。本発明は、亜鉛の従来の湿式精錬一次生成処理に関するものである。   In the primary production process of zinc, conventional raw materials, such as zinc sulfide ore, are refined, ie zinc concentrate, and if desired, zinc sinter is also produced from them. In addition, concentrated zinc sulfate solutions are often produced from zinc concentrate and zinc sinter and are suitable for the electrolytic production of zinc metal. The present invention relates to a conventional wet refining primary production process of zinc.

従来の亜鉛の湿式精錬処理では、多くの段階から成る浄液が原材料の浸出の後に必要であり、浄液には純粋な亜鉛含有溶液の生成が含まれる。亜鉛の電解生成はある不純物質に対して大変敏感である。それゆえ、亜鉛電気分解のために、十分に純粋な溶液を生成することは重要である。   In conventional hydrometallurgical processing of zinc, a multi-stage clean solution is required after leaching of raw materials, and the clean solution involves the production of a pure zinc-containing solution. Electrolytic production of zinc is very sensitive to certain impurities. It is therefore important to produce a sufficiently pure solution for zinc electrolysis.

亜鉛の生成にはある方式が広く使用されており、その方式では、亜鉛精鉱は焼鉱されて亜鉛酸化物が生成され、亜鉛酸化物はいわゆる中性浸出において希硫酸溶液で浸出され、亜鉛含有溶液が精製され、精製された溶液から電解分離によって、亜鉛が分離される。   A method is widely used for the production of zinc, in which the zinc concentrate is sintered to produce zinc oxide, which is leached with dilute sulfuric acid solution in so-called neutral leaching, and zinc The containing solution is purified, and zinc is separated from the purified solution by electrolytic separation.

亜鉛焼鉱の浸出工程では、亜鉛は溶解され、亜鉛焼鉱に含まれる鉄の大部分を、希酸では溶解されない亜鉛フェライトとして分離することができる。亜鉛の他に、中性浸出から得られる溶液には、二価の鉄、カドミウム、銅、コバルト、ニッケル、カルシウム、マンガン、および塩化物が含まれている。   In the leaching process of zinc sinter, zinc is dissolved, and most of the iron contained in the zinc sinter can be separated as zinc ferrite that is not dissolved by dilute acid. In addition to zinc, the solution obtained from neutral leaching contains divalent iron, cadmium, copper, cobalt, nickel, calcium, manganese, and chloride.

亜鉛の電解回収に適した溶液を得るために、中性浸出から得られた溶液は多工程浄液処理によって精製される。通常は、浄液には三つの工程が含まれ、そこで銅、コバルト、ニッケル、および最終的にはカドミウムが除去される。   In order to obtain a solution suitable for the electrolytic recovery of zinc, the solution obtained from the neutral leaching is purified by a multi-step clarification process. Typically, the clarification process involves three steps where copper, cobalt, nickel, and ultimately cadmium are removed.

中性浸出から得られる硫酸亜鉛含有溶液はまた、亜鉛の抽出方法における供給材料に適している。今日まで、液液抽出は、主に二次的な原材料を用いる小規模の処理における亜鉛生成に用いられてきた。例えば、合衆国特許公報第5,135,652号には、硫酸亜鉛液から選択的に亜鉛を分離するために用いることができる溶媒抽出が記載されている。硫酸亜鉛液は硫酸亜鉛をその飽和濃度まで含んでいてもよく、また、二価の鉄、三価の鉄、カルシウム、マグネシウム、マンガン、ナトリウム、カリウム、ヒ素、アンチモン、銅、カドミウム、ゲルマニウム、およびインジウムを含む一群のなかの一つまたはそれ以上を含んでいてもよい。   The zinc sulfate-containing solution obtained from neutral leaching is also suitable as a feed in the zinc extraction process. To date, liquid-liquid extraction has been used primarily for zinc production in small scale processes using secondary raw materials. For example, US Pat. No. 5,135,652 describes a solvent extraction that can be used to selectively separate zinc from a zinc sulfate solution. Zinc sulfate solution may contain zinc sulfate to its saturation concentration, and also includes divalent iron, trivalent iron, calcium, magnesium, manganese, sodium, potassium, arsenic, antimony, copper, cadmium, germanium, and One or more of the group comprising indium may be included.

本発明の目的は、焙焼−浸出−電解型の亜鉛生成処理の支流から純粋な亜鉛薬品を生成する、新規な処理装置を提供することである。本発明は、焙焼−浸出−電解プラントにおける浸出から得られた硫酸亜鉛含有溶液の生産量の一部が、亜鉛薬品の生成に割り当てられるという事実に基づく。硫酸亜鉛液の生産量の一部だけが亜鉛薬品の生成に割り当てられるので、電解に基づく実際の亜鉛回収処理は妨げられない。本発明による処理装置において、亜鉛薬品の生成処理は、公知の抽出技術を用いた抽出による亜鉛の選択的な分離に基づく。公知の抽出処理は、任意の有機的置換リン酸または有機的置換チオホスフィン酸の使用に基づく。本発明によれば、抽出処理は上述の焙焼−浸出−電解工程と繋がる。   An object of the present invention is to provide a novel processing apparatus for generating pure zinc chemicals from a tributary of roasting-leaching-electrolytic zinc generation processing. The present invention is based on the fact that part of the production of zinc sulfate-containing solution obtained from leaching in a roasting-leaching-electrolysis plant is allocated to the production of zinc chemicals. Since only a part of the production of zinc sulfate solution is allocated to the production of zinc chemicals, the actual zinc recovery process based on electrolysis is not hindered. In the treatment apparatus according to the present invention, the zinc chemical production process is based on selective separation of zinc by extraction using known extraction techniques. Known extraction processes are based on the use of any organic substituted phosphoric acid or organic substituted thiophosphinic acid. According to the present invention, the extraction process is linked to the roasting-leaching-electrolysis process described above.

本発明は、かなりの利点を提供する。従来型の焙焼−浸出−電解工程では、生成の妨げとなるものが電解工程に存在する。それゆえ、支流を亜鉛薬品の生成ラインへ引き込むという本発明による解決策は、実際の亜鉛生成処理の有用性を高める。本発明は、より需要の少ない亜鉛薬品の生成のための有利な処理策を提供する。本発明に用いられる亜鉛抽出処理では、強酸溶液が副産物として生産され、この強酸溶液は、単に再循環させて亜鉛の生成処理で利用させることができる。その場合、酸性溶液の最終処理のための特別な投資は必要ない。   The present invention provides significant advantages. In the conventional roasting-leaching-electrolysis process, what interferes with the production exists in the electrolysis process. Therefore, the solution according to the invention of drawing a tributary into the zinc chemical production line increases the usefulness of the actual zinc production process. The present invention provides an advantageous treatment strategy for the production of less demanding zinc chemicals. In the zinc extraction treatment used in the present invention, a strong acid solution is produced as a by-product, and this strong acid solution can be simply recycled and used in the zinc production treatment. In that case, no special investment is required for the final treatment of the acidic solution.

本発明は、抽出方法によって硫酸亜鉛含有溶液から純粋な亜鉛薬品を生成する処理路および処理装置を含み、この方法によって、抽出の原材料の流れは、中性浸出工程の後、亜鉛一次生成における焙焼−浸出−電解型処理ラインからの支流として分岐される。   The present invention includes a treatment path and a treatment device for producing pure zinc chemicals from a zinc sulfate-containing solution by an extraction method, whereby the raw material flow of extraction is reduced in the primary zinc production after a neutral leaching step. It is branched as a tributary from the firing-leaching-electrolytic treatment line.

以下、本発明の添付図面を参照して詳細に説明する。   Hereinafter, the present invention will be described in detail with reference to the accompanying drawings.

亜鉛生成では、亜鉛酸化物を含有する焼鉱10が、中性浸出において硫酸溶液に溶解する。中性浸出は一般的にいくつかの段階を経て行われる。とりわけ、この浸出で溶解せず、鉄を含む溶液残渣12が、強酸浸出に割り当てられる。亜鉛硫酸塩含有溶液11を多段階の浄液に割り当て、そこでは亜鉛末14が、銅、コバルト、ニッケルおよびカドミウムを沈殿させるため使用される。溶液精錬された硫酸亜鉛溶液15は電気分解プラントへ割り当てられ、そこで亜鉛は陰極16で電気分解によって回収される。亜鉛が回収された電解液17は相当量の硫酸を含み、この液はとりわけ強酸浸出へ割り当てられて再導入される。強酸浸出で、この酸は反応で使い切られる。それゆえ、この再利用された酸に加えて、ある量の純粋な酸が処理に加えられる。中性浸出では、この溶液のpHはあまり高くすべきではない。中性浸出のpHが、初期の酸で調整され、さらに強酸浸出から得られた酸18で調整されることは理にかなっている。   In zinc production, the sinter 10 containing zinc oxide dissolves in the sulfuric acid solution during neutral leaching. Neutral leaching is generally performed in several stages. In particular, solution residues 12 that do not dissolve in this leaching and contain iron are assigned to strong acid leaching. Zinc sulfate containing solution 11 is assigned to a multi-stage purification solution, where zinc dust 14 is used to precipitate copper, cobalt, nickel and cadmium. Solution refined zinc sulfate solution 15 is assigned to an electrolysis plant where zinc is recovered by electrolysis at cathode 16. The electrolyte 17 from which the zinc has been recovered contains a considerable amount of sulfuric acid, which is assigned to strong acid leaching, and is reintroduced. With strong acid leaching, this acid is used up in the reaction. Therefore, in addition to this recycled acid, an amount of pure acid is added to the process. For neutral leaching, the pH of this solution should not be too high. It makes sense that the pH of the neutral leaching is adjusted with the initial acid and further with the acid 18 obtained from the strong acid leaching.

本発明によると、支流13は中性浸出から得られた硫酸亜鉛含有溶液の主流11から分岐され、亜鉛の抽出に割り当てられる。この抽出では、ジエチルヘキシルリン酸(DEHPA)または、ジ-2-エチルヘキシルリン酸(D2EHPA)が用いられる。浸出工程の終盤では、抽出に向かう溶液のpHを、必要であれば、焼鉱を用いて、抽出に適したレベルまで上昇させることができる。亜鉛は、酸含有溶液21を用いて剥離することにより有機相から剥離される。ラフィネート19は、この抽出において生成され、とりわけ硫酸を含み、強酸段階へ割り当てられ、再利用される。   According to the invention, the tributary 13 is branched from the main stream 11 of the zinc sulfate-containing solution obtained from neutral leaching and is assigned to the extraction of zinc. In this extraction, diethylhexyl phosphate (DEHPA) or di-2-ethylhexyl phosphate (D2EHPA) is used. At the end of the leaching process, the pH of the solution towards extraction can be raised to a level suitable for extraction, if necessary, using calcined ore. Zinc is stripped from the organic phase by stripping using the acid-containing solution 21. Raffinate 19 is produced in this extraction and contains, inter alia, sulfuric acid, assigned to the strong acid stage and reused.

剥離では、純粋な酸が用いられ、純粋な亜鉛を、硫酸含有溶液から回収することができ、そこでは亜鉛含有量を150g/lまで高めることができる。この溶液20から、さまざまな純粋亜鉛生産物が、化学的な沈殿または蒸発などの任意の公知の方法によって、生成することができる。   For stripping, pure acid is used, and pure zinc can be recovered from the sulfuric acid-containing solution, where the zinc content can be increased to 150 g / l. From this solution 20, various pure zinc products can be produced by any known method such as chemical precipitation or evaporation.

亜鉛の焙焼−浸出−電解型生成処理、およびこの処理と繋がる亜鉛薬品の生成段階の単純化した処理チャートである。FIG. 4 is a simplified process chart of zinc roasting-leaching-electrolytic generation process and a zinc chemical generation stage linked to this process.

Claims (4)

抽出方法によって硫酸亜鉛含有溶液から純粋な亜鉛薬品を生成するための処理路において、抽出の原材料流れは、中性浸出段階の後、焙焼−浸出−電解型の亜鉛第一段処理の処理ラインから支流として分岐されることを特徴とする処理路。   In a process path for producing pure zinc chemical from a zinc sulfate-containing solution by an extraction method, the raw material stream of the extraction is a neutral leaching stage followed by a roasting-leaching-electrolytic zinc first stage treatment line A processing path that is branched off as a tributary. 請求項1に記載の処理装置において、前記抽出において精製されるラフィネート(19)は、割り当てられて、前記焙焼−浸出−電解型処理の強酸浸出で再利用されることを特徴とする処理装置。   2. The processing apparatus according to claim 1, wherein the raffinate (19) to be purified in the extraction is allocated and reused in the strong acid leaching of the roasting-leaching-electrolytic process. . 請求項1に記載の処理装置において、前記抽出では、ジエチルヘキシルリン酸(DEHPA)またはジ−2−エチルヘキシルリン酸(D2EHPA)が使用されることを特徴とする処理装置。   The processing apparatus according to claim 1, wherein diethylhexyl phosphoric acid (DEHPA) or di-2-ethylhexyl phosphoric acid (D2EHPA) is used in the extraction. 請求項1に記載の処理装置において、前記浸出工程の終盤では、前記抽出に向かう溶液のpHが、焼鉱によって該抽出に適した水準にまで高められることを特徴とする処理装置。   The processing apparatus according to claim 1, wherein at the end of the leaching step, the pH of the solution toward the extraction is increased to a level suitable for the extraction by calcination.
JP2007530727A 2004-09-08 2005-09-06 Formation of zinc drugs from treatment tributaries. Abandoned JP2008512569A (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
FI20041163A FI117139B (en) 2004-09-08 2004-09-08 Production of zinc chemicals from process stream
PCT/FI2005/000380 WO2006027412A1 (en) 2004-09-08 2005-09-06 Preparation of zinc chemicals from the minor flow of a process

Publications (2)

Publication Number Publication Date
JP2008512569A true JP2008512569A (en) 2008-04-24
JP2008512569A5 JP2008512569A5 (en) 2008-09-18

Family

ID=33041502

Family Applications (1)

Application Number Title Priority Date Filing Date
JP2007530727A Abandoned JP2008512569A (en) 2004-09-08 2005-09-06 Formation of zinc drugs from treatment tributaries.

Country Status (11)

Country Link
US (1) US20070253878A1 (en)
EP (1) EP1794334A1 (en)
JP (1) JP2008512569A (en)
CN (1) CN100406593C (en)
AU (1) AU2005281684A1 (en)
CA (1) CA2577863A1 (en)
EA (1) EA010853B1 (en)
FI (1) FI117139B (en)
MX (1) MX2007002750A (en)
PE (1) PE20060757A1 (en)
WO (1) WO2006027412A1 (en)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102102148B (en) * 2010-12-15 2012-10-24 河南豫光锌业有限公司 Recycling method of indium raffinate
CN103160688B (en) * 2013-04-17 2015-08-05 昆明奥赛美科技有限公司 Zinc replacement prepares the method for germanium concentrate from germanic leach liquor

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3989607A (en) * 1975-08-21 1976-11-02 Bush Philip D Solvent extraction and electrowinning of zinc and copper from sulfate solution
US5084180A (en) * 1990-10-25 1992-01-28 Cominco Ltd. Method for treating zinc-containing sulfate solution
US5135652A (en) * 1990-10-25 1992-08-04 Cominco Ltd. Method for the solvent extraction of zinc
US5358700A (en) * 1992-10-05 1994-10-25 Cyprus Power Company Method of extracting zinc from brines
CN1040554C (en) * 1994-03-02 1998-11-04 张振逵 Technology and equipment for coproducing zinc sulfate and lead concentrate

Also Published As

Publication number Publication date
CN100406593C (en) 2008-07-30
CN101014723A (en) 2007-08-08
AU2005281684A1 (en) 2006-03-16
EA200700420A1 (en) 2007-10-26
EP1794334A1 (en) 2007-06-13
FI20041163A0 (en) 2004-09-08
PE20060757A1 (en) 2006-09-14
CA2577863A1 (en) 2006-03-16
FI117139B (en) 2006-06-30
WO2006027412A1 (en) 2006-03-16
MX2007002750A (en) 2007-05-18
EA010853B1 (en) 2008-12-30
FI20041163A (en) 2006-03-09
US20070253878A1 (en) 2007-11-01

Similar Documents

Publication Publication Date Title
CN101351567B (en) Method for recovering rare metals in zinc leaching process
AU2012300756B2 (en) Method for recovering metals from material containing them
JP5541336B2 (en) Method for producing high purity cobalt sulfate aqueous solution
JP5514844B2 (en) Method for separating valuable metals from waste secondary batteries and method for recovering valuable metals using the same
CN106119560B (en) A kind of zinc cobalt separation method
RU2741429C1 (en) Method and system for complete reprocessing of copper-nickel sulphide ore
JP5631948B2 (en) Nickel sludge treatment method
JP5800254B2 (en) Method for producing cobalt sulfate
JP5721213B2 (en) Method for producing pure metal indium from zinc oxide and / or metal-containing solution
CN104726724A (en) Method for extracting scandium from nickel laterite ores
JP6471912B2 (en) Method for producing high purity cobalt sulfate aqueous solution
JP2006265592A (en) Wet treatment method for zinc leaching residue
CN105274352B (en) A kind of method that copper cobalt manganese is separated in the manganese cobalt calcium zinc mixture from copper carbonate
FI125216B (en) Method for recovering metals
JP2008208441A (en) Solvent extraction method for chloride aqueous solution
FI127003B (en) Method and process equipment for the separation of indium and arsenic
CN104862503A (en) Method for extracting scandium from nickel laterite ore
JP2008512569A (en) Formation of zinc drugs from treatment tributaries.
KR20210105406A (en) Method for recovering metal from multimetal nodules
AU2004243344B2 (en) A process for treating dust
US10689732B2 (en) Methods for controlling iron via magnetite formation in hydrometallurgical processes
WO2004106560A1 (en) A process for treating dust
JP5181684B2 (en) Solvent extraction method for aqueous chloride solution
WO2015079116A1 (en) Method and arrangement of separating arsenic from starting materials
CN114207160A (en) Method for recovering metals from oxidized ores

Legal Events

Date Code Title Description
A521 Written amendment

Free format text: JAPANESE INTERMEDIATE CODE: A523

Effective date: 20080801

A621 Written request for application examination

Free format text: JAPANESE INTERMEDIATE CODE: A621

Effective date: 20080801

A762 Written abandonment of application

Free format text: JAPANESE INTERMEDIATE CODE: A762

Effective date: 20091110