WO2012140284A1 - Metodo hidrometalúrgico para la recuperación de zinc en medio sulfúrico a partir de concentrados de zinc sulfurados - Google Patents
Metodo hidrometalúrgico para la recuperación de zinc en medio sulfúrico a partir de concentrados de zinc sulfurados Download PDFInfo
- Publication number
- WO2012140284A1 WO2012140284A1 PCT/ES2011/070265 ES2011070265W WO2012140284A1 WO 2012140284 A1 WO2012140284 A1 WO 2012140284A1 ES 2011070265 W ES2011070265 W ES 2011070265W WO 2012140284 A1 WO2012140284 A1 WO 2012140284A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- zinc
- solution
- stage
- jarosite
- leaching
- Prior art date
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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
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/20—Obtaining zinc otherwise than by distilling
-
- 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
- C22B19/20—Obtaining zinc otherwise than by distilling
- C22B19/22—Obtaining zinc otherwise than by distilling with leaching with acids
-
- 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
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/02—Roasting processes
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/02—Preliminary treatment of ores; Preliminary refining of zinc oxide
-
- 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
- C22B19/20—Obtaining zinc otherwise than by distilling
- C22B19/26—Refining solutions containing zinc values, e.g. obtained by leaching zinc ores
-
- 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
-
- 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 describes a hydrometallurgical method for the recovery of zinc and other valuable metals, with high extraction rate, and the generation of clean waste during the production of electrolytic zinc from sulphide zinc concentrates.
- the method is particularly suitable for the treatment of different types of zinc concentrates and adapts very well to those plants that use the processes known as jarosite, goetite or direct leaching, improving the results, both in terms of efficiency in the recovery of metals as to the quality of the waste generated.
- this solution containing the Fe +++ in the form of sulfate and a residual acidity necessary to keep the Fe +++ in solution is treated in the presence of a cation such as Na + , K + , 1 / 2Pb ++ , NH + or H 3 O + with calcine under certain conditions to lower acidity and thus precipitate iron in the form of jarosite, a basic sulfate with the formula Me (SO 4 ) 2Fe3 (OH) 6 , where I can be one of the aforementioned cations.
- a cation such as Na + , K + , 1 / 2Pb ++ , NH + or H 3 O +
- a variant of the jarosite process is the so-called conversion process described in document CA 1094819, which differs from the previous one in that both the leaching of ferrites and the precipitation of iron and jarosite take place simultaneously without it being possible to separate in this case the lead-silver residue, obtaining in the end a unique residue that contains all the iron in the form of jarosite as well as the lead, silver and silica contained in the calcine.
- Another process developed a little later than that of the jarosite is the so-called goetite process described in document CA 873262.
- This process consists, as in the case of the jarosite process, of a stage Neutral leaching and two or more stages of acid leaching that work in countercurrent, and where ferrites are leached at the same time that a lead-silver residue can be separated.
- the solution resulting from acid leaching is treated with zinc concentrate to reduce ferric iron (Fe +++ ) to ferrous iron (Fe ++ ).
- a variant of the Goetite process is that of the paragoetite that is similar to the previous one.
- any new technology that intends to be applied in this field should meet the requirements of achieving, with a competitive cost, the maximum recovery of metals and generating environmentally acceptable waste, which can be used favorably in other industrial processes without requiring permanent storage, something that as we have already said, is not allowed in certain countries and it is expected that this prohibition is transmitted to more countries in the not too distant future.
- intensive research work was carried out in the world of zinc to find a process that avoids the storage of iron waste through an easy to handle process, economically competitive and that has a high yield of recovery of metals, without so far a satisfactory solution had been found.
- the present invention it is an objective of the present invention to have a hydrometallurgical method for the recovery of zinc in sulfuric medium from sulfurized zinc concentrates that allows to achieve high metal recovery rates. It is another objective of the present invention to have a hydrometallurgical method for the recovery of zinc in sulfuric medium from sulfur zinc concentrates in which an environmentally acceptable iron residue is obtained that can be used in other industrial processes, avoiding its storage in security warehouses. Description of the Invention The present invention meets the aforementioned requirements for a new technology that aims to displace existing ones: competitive cost, high metal recovery rate and clean waste generation, capable of being reused in other industrial processes.
- the process is based on the fact that first in the solution resulting from acid leaching, Fe +++ is reduced to Fe ++ and subsequently re-oxidized to Fe +++ before being precipitated as a jarosite.
- This allows neutralizing the acidity that accompanies the Fe in the solution before entering the jarosite stage by separating the solids generated during the neutralization to be recycled to the acid leaching stage, and on the other hand in the iron oxidation stage itself and precipitation of jarosite provides a neutralizing element, oxygen, which oxidizes Fe ++ to Fe +++ consumes enough of the acid generated during the precipitation of jarosite to allow said jarosite stage to work under acceptable acidity conditions, such As shown below.
- a hydrometallurgical method for the recovery of zinc in sulfuric medium from sulfur zinc concentrates comprises the following steps: a. Roasting, where sulphides are transformed into oxides b. Neutral leaching where zinc oxide (calcine) is dissolved with sulfuric acid in the form of spent electrolyte to obtain a zinc sulfate solution that is sent to the purification stage c. Acid leaching where zinc ferrites are leached by means of sulfuric acid in the form of spent electrolyte and concentrated sulfuric acid, generating a residue where the lead, silver and gold contained in the concentrates are concentrated and a solution rich in zinc sulfate and ferric sulfate d.
- This stage can also be applied both to those processes that use pressure autoclaves and those that work at atmospheric pressure for direct leaching of a part of the concentrates Stages (f) and (g) only for concentrates with high arsenic and copper contents. Step (i) only when the RLE process is combined with direct leaching
- the solution resulting from the acidic stages containing most of the iron in a ferric form (normally between 5 and 25 g / l of total Fe, of which only 1 -2 g / l are as Fe ++ and the rest as Fe +++ ), as well as a certain acidity (between 10 and 70 g / l) necessary to keep Fe +++ in solution, it is initially treated with zinc concentrate to transform Fe +++ into Fe ++ .
- the acidity is neutralized with calcine and then the copper is cemented with zinc dust, obtaining a neutral solution and free of contaminating solids that mainly contain zinc sulfate and ferrous sulfate.
- stage (h) the oxidation of Fe ++ to Fe +++ and precipitation of jarosite takes place simultaneously with the injection of oxygen and the addition of the amount of alkali (NaOH, Na 2 Co 3 , NH 3 ) necessary for the formation of jarosite depending on the amount of iron precipitated.
- alkali NaOH, Na 2 Co 3 , NH 3
- Figure 1 shows a flow chart of the process object of the invention.
- Figure 2 shows a flow chart of the process object of the invention when zinc concentrates have low copper contents.
- Figure 3 shows a flow chart of the process object of the invention when zinc concentrates have low copper and arsenic contents.
- the hydrometallurgical method of the invention comprises the following steps. See figure 1. a) Roasting the sulphide zinc concentrate to obtain roasted zinc concentrate (calcine) and sulfur dioxide, which is subsequently transformed into sulfuric acid.
- the main reactions that take place in the roasting oven are:
- iron in solution in the form of Fe ++ produced in step (d) according to reaction (5), does not precipitate and remains in solution, while iron present as Fe +++ precipitates as ferric hydroxide according to the reaction (6).
- the neutralization stage can be divided into two phases: in the first phase the acidity contained in the solution from stage (d) is partially neutralized to a range of 5-15 g / l; Then the solid that returns to the acid leaching stage (c) is separated, while the resulting solution is neutralized again with calcine until a pH between 3.8 and 5.2 is reached.
- the solid is sent to the arsenic separation stage (f), while the solution is sent either directly to the jarosite stage (h) or to the stage (g) in case it is necessary to separate copper from the solution for avoid contamination of the final jarosite residue.
- f) Arsenic separation when concentrates with high As content are treated, the residue from step (e) is treated with electrolyte depleted at low acidity (4-10 g / l) and low temperature (30-70 ° C) and in the resulting solution, Fe +++ is reduced to Fe ++ with zinc concentrate to subsequently, after separating unreacted solids, precipitate arsenic and other related impurities, for example with Ca (OH) 2 , CaCO3, or NaSH
- related impurities are those that have a chemical behavior similar to that of arsenic, such as antimony and germanium that dissolve and precipitate under similar pH conditions.
- the reaction (7) takes place by default, so that there is always a certain presence of copper in solution (of the order of 100-200 mg / l), which is sufficient to favor the oxidation reaction
- the neutralized and solids-free solution from stage (e) or (f) is treated at atmospheric pressure and at a temperature between 80 ° C and the boiling point of the solution, injecting oxygen or oxygen enriched air (the necessary to facilitate the oxidation of Fe ++ to Fe +++ and adding an alkali (NaOH, Na 2 CO3 or NH 3 ) in the proportion required for the formation of jarosite according to the stoichiometry of the reaction (9), maintaining an acidity between pH 2 and 15 g / l, in this way the oxidation of Fe ++ to Fe +++ and the precipitation of Fe +++ as a jarosite take place simultaneously, according to the following reactions:
- I be Na + or NH 4 + .
- a solution containing 5 g / l of Fe ++ at the entrance of this stage would have a maximum of 3 g / l at the end of this stage, whereas, in case of having 25 g / l of Fe ++ upon entry, the resulting final solution would have as maximum 15 g / l of acidity (this in case all Fe +++ precipitated, although it is known that with this acidity at least 1.5 - 2.0 g / l of Fe +++ remain in solution, so that the final acidity will really be between 12 and 13 g / l), both favorable conditions to achieve an efficient precipitation of jarosite.
- reaction (9 ) would be replaced by the following:
- I can be either Na + or NH4 + .
- a solution containing 5 g / l of Fe ++ at the entrance of this stage would have a maximum of 5 g / l at the end of this stage, while, in case of having 20 g / l of Fe ++ upon entry, the resulting final solution would have a maximum of 18 g / l of acidity (this in case all Fe +++ precipitated, although it is known that with this acidity at least 2.0 - 3.0 g remain in solution / l of Fe +++ , so the final acidity will really be between 13 and 15 g / l), both favorable conditions to achieve an efficient jarosite precipitation.
- this invention differs from any other that generates a jarosite residue, since with the present invention no external neutralizing agent containing contaminants (such as calcine) is required, at the same time as The precipitation takes place from a clean solution, free of solids that could contaminate the final jarosite residue.
- no external neutralizing agent containing contaminants such as calcine
- the losses of valuable metals Zn, Pb, Ag and Au
- the losses of valuable metals are significantly reduced, thus increasing their recovery to the levels already mentioned, above 99% in the case of zinc and 100% for lead, silver and gold in the set of leaching stages.
- both oxygen and added alkali in this case NaOH, although it could also be Na2CO3 or NH3 are not polluting products, but components that are incorporated into the jarosite itself, it is clear that the final jarosite residue is a clean product and, as such, it can be used in other industrial processes, such as in cement manufacturing.
- BZS basic zinc sulfate
- said BZS can be incorporated into the stage of iron oxidation and precipitation of jarosite, since the zinc contained in the solid is leached immediately, while the gypsum residue that would be incorporated into the jarosite does not constitute an impurity in case of using this final product in the manufacture of cement.
- the jarosite residue obtained constitutes a clean product that can be separated and reused for other industrial processes.
- the solution resulting from this stage, from which most of the iron has precipitated returns to neutral leaching (b).
- Stages (a), (b) and (c) are common to the vast majority of industrial processes (jarosite, goetite, paragoetite). Stages (d) and (e) are used in the Goetite process but not in the Jarosite process. Stage (f) is new and It is only used when concentrates with high arsenic contents are treated. Stage (g) is also new but only differs from a normal stage of purification in its location within the general process. See Figures 2 and 3 to appreciate the progress of the process when these stages are suppressed.
- Stage (h) is novel and its novelty is based on the fact that the solution entering this stage is a solution of zinc sulfate and ferrous sulfate neutral and free of solids that could contaminate the final precipitate of jarosite; It is also based on the fact that the reagents that are added to this stage (oxygen or oxygen enriched air and an alkali or alkaline salt) are strictly necessary for the reactions (8) and (9) to take place.
- stage (h) could not work in this way without the existence of stages (d) and (e).
- stage (d) and (e) most of the iron that has dissolved as a result of the leaching of zinc ferrites is in the form of Fe +++ .
- Fe +++ is reduced to Fe ++ by adding zinc concentrate so that in the next stage (e) we can proceed to neutralize acidity residual generated in stage (c).
- the present invention also distinguishes itself from direct leaching processes in that: a) it uses a solids-free solution that can contaminate the final jarosite residue, b) it does not use calcine or any other neutralizing agent other than the oxygen-enriched air necessary for the oxidation of Fe ++ to Fe +++ or the alkali necessary for the formation of the jarosite precipitate itself and c) no It uses autoclaves, since all stages of the process take place at atmospheric pressure.
- This invention is also compatible with those processes that, in addition to having a part thereof where zinc concentrates are roasted to produce calcine which is then treated by usual procedures, such as the "process conversion", also have another part of the same, where the zinc concentrate is processed by direct leaching and generally making a combination of both processes as described in WO 98/06879.
- this invention can be used advantageously, since the solution leaving the acid leaching (c) can enter a direct leaching stage [step (i)], where zinc concentrate, electrolyte is added exhausted and oxygen enriched air at a temperature between 80 ° C and the boiling point of the solution, maintaining a sufficiently high acidity (greater than 20 g / l), so that iron precipitation is avoided at this stage. In this way the consumption of oxygen or oxygen enriched air will be lower since the Fe +++ present in the solution from step (c) is capable of leaching a part of the zinc contained in the zinc concentrate, according to reaction (5):
- stage (i) The residue resulting from this stage (i) could be combined with that of stage (c), since it contains the lead, silver and gold contained in the leached zinc concentrate, but also contains the elemental sulfur formed according to the reaction (5) , which could cause some problem for the treatment of this residue, as it is happening today, so it could be subjected to an additional flotation stage to separate the sulfur before mixing both residues.
- stage (c ') in parallel to the existing stage (c) where said waste was treated with spent electrolyte and sulfuric acid to proceed with the dissolution of iron, zinc and copper, while other valuable metals such as lead, silver and gold remain insoluble.
- the residue of this stage joins that of the existing stage (c) while the solution would pass in the same way to stage (d).
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Abstract
Description
Claims
Priority Applications (10)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR1020137008846A KR20130108341A (ko) | 2011-04-15 | 2011-04-15 | 황화아연 정광으로부터 출발하여 황산 매질에서 아연을 회수하기 위한 습식 제련 방법 |
BR112013007502A BR112013007502A2 (pt) | 2011-04-15 | 2011-04-15 | método hidrometalúrgico para a recuperação de zinco em meio sulfúrico a apartr de concentrados de zinco sulfurados |
JP2014504361A JP2014510841A (ja) | 2011-04-15 | 2011-04-15 | 硫化亜鉛精鉱から出発して硫黄媒体内の亜鉛を回収する湿式製錬法 |
AU2011365350A AU2011365350A1 (en) | 2011-04-15 | 2011-04-15 | Hydrometallurgical method for the recovery of zinc in a sulphur medium starting from sulphudic zinc concentrates |
CN2011800467297A CN103210099A (zh) | 2011-04-15 | 2011-04-15 | 从硫化锌精矿开始回收含硫介质中的锌的湿法冶金方法 |
MX2013003380A MX2013003380A (es) | 2011-04-15 | 2011-04-15 | Metodo hidrometalurgico para la recuperacion de zinc en medio sulfurico a partir de concentrados de zinc sulfurados. |
EA201370062A EA201370062A1 (ru) | 2011-04-15 | 2011-04-15 | Гидрометаллургический способ извлечения цинка из сернокислой среды, исходя из сульфидных цинковых концентратов |
CA2813860A CA2813860A1 (en) | 2011-04-15 | 2011-04-15 | Hydrometallurgical method for recovery of zinc in sulphuric medium starting from sulphidic zinc concentrates |
PCT/ES2011/070265 WO2012140284A1 (es) | 2011-04-15 | 2011-04-15 | Metodo hidrometalúrgico para la recuperación de zinc en medio sulfúrico a partir de concentrados de zinc sulfurados |
EP11861327.2A EP2543746A4 (en) | 2011-04-15 | 2011-04-15 | HYDROMETALLURGICAL METHOD FOR OBTAINING ZINC IN A SULFUR MEDIUM OF SWEEPED ZINC CONCENTRATES |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/ES2011/070265 WO2012140284A1 (es) | 2011-04-15 | 2011-04-15 | Metodo hidrometalúrgico para la recuperación de zinc en medio sulfúrico a partir de concentrados de zinc sulfurados |
Publications (2)
Publication Number | Publication Date |
---|---|
WO2012140284A1 true WO2012140284A1 (es) | 2012-10-18 |
WO2012140284A8 WO2012140284A8 (es) | 2013-03-28 |
Family
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/ES2011/070265 WO2012140284A1 (es) | 2011-04-15 | 2011-04-15 | Metodo hidrometalúrgico para la recuperación de zinc en medio sulfúrico a partir de concentrados de zinc sulfurados |
Country Status (10)
Country | Link |
---|---|
EP (1) | EP2543746A4 (es) |
JP (1) | JP2014510841A (es) |
KR (1) | KR20130108341A (es) |
CN (1) | CN103210099A (es) |
AU (1) | AU2011365350A1 (es) |
BR (1) | BR112013007502A2 (es) |
CA (1) | CA2813860A1 (es) |
EA (1) | EA201370062A1 (es) |
MX (1) | MX2013003380A (es) |
WO (1) | WO2012140284A1 (es) |
Cited By (5)
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CN103130282A (zh) * | 2013-03-20 | 2013-06-05 | 江苏理工学院 | 黄钾铁矾的制备方法 |
WO2014013092A1 (es) | 2012-07-16 | 2014-01-23 | Tam 5, S.L. | Metodo hidrometalúrgico para la recuperación de zinc en medio sulfúrico a partir de concentrados de zinc sulfurados con alto contenido en hierro |
CN103643036A (zh) * | 2013-12-20 | 2014-03-19 | 广西冶金研究院 | 一种热压选择性浸出处理含铁铟锌焙砂的方法 |
CN103898336A (zh) * | 2014-03-24 | 2014-07-02 | 中国恩菲工程技术有限公司 | 处理锌焙烧矿的方法 |
CN115478172A (zh) * | 2022-09-30 | 2022-12-16 | 云南金鼎锌业有限公司 | 一种锌湿法冶炼降低浸出氧化剂的方法 |
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CN103160688B (zh) * | 2013-04-17 | 2015-08-05 | 昆明奥赛美科技有限公司 | 锌粉置换法从含锗浸出液中制备锗精矿的方法 |
CN104561527B (zh) * | 2015-02-10 | 2016-08-17 | 四川金广实业(集团)股份有限公司 | 一种红土矿中配加硫化镍精矿生产镍铁方法 |
CN105875799A (zh) * | 2016-04-13 | 2016-08-24 | 石河子大学 | 一种牛肉复合保鲜剂及其应用方法 |
EP3592872B1 (en) * | 2017-03-07 | 2022-05-04 | Outotec (Finland) Oy | Process for roasting of gold bearing sulfide concentrate |
CN111206155B (zh) * | 2020-02-28 | 2021-08-27 | 白银有色集团股份有限公司 | 一种利用再生氧化锌进行回收锌金属的方法 |
CN111394586B (zh) * | 2020-04-24 | 2021-09-24 | 云南罗平锌电股份有限公司 | 一种从铅渣中综合回收锌锗的方法 |
CN112359222B (zh) * | 2020-10-19 | 2022-11-15 | 云南云铜锌业股份有限公司 | 一种亚硫酸锌液连续酸分解的方法及装置 |
CN112458309A (zh) * | 2020-12-14 | 2021-03-09 | 昆明冶金研究院有限公司 | 一种提高硫化锌精矿中锌浸出率的方法 |
CN114737064A (zh) * | 2022-03-17 | 2022-07-12 | 云南云铜锌业股份有限公司 | 一种湿法炼锌黄钾铁矾法 |
CN115874058B (zh) * | 2023-03-02 | 2023-05-12 | 昆明理工大学 | 一种预脱锌协同含锗氧化锌烟尘中和法高效富集锗的方法 |
CN117625956B (zh) * | 2024-01-25 | 2024-03-22 | 昆明理工大学 | 一种锌焙砂的高效提锌方法 |
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EP0451456A1 (en) * | 1990-02-16 | 1991-10-16 | Outokumpu Oy | Hydrometallurgic method for processing raw materials containing zinc sulphide |
WO2002046481A1 (en) * | 2000-12-08 | 2002-06-13 | Outokumpu Oyj | Method for the hydrolytic precitpitation of iron |
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CA1176853A (en) * | 1981-08-05 | 1984-10-30 | Gerald L. Bolton | Process for recovering zinc from zinc ferrite material |
JPH05171310A (ja) * | 1991-12-25 | 1993-07-09 | Mitsubishi Materials Corp | 還元焙焼による亜鉛製錬法 |
FI100806B (fi) * | 1996-08-12 | 1998-02-27 | Outokumpu Base Metals Oy | Menetelmä sinkkirikasteen liuottamiseksi atmosfäärisissä olosuhteissa |
JP4129499B2 (ja) * | 2000-08-08 | 2008-08-06 | Dowaメタルマイン株式会社 | 鉱物からの硫黄の回収方法 |
FI116071B (fi) * | 2003-02-26 | 2005-09-15 | Outokumpu Oy | Menetelmä sinkin talteenottamiseksi vastavirtaliuotuksella |
-
2011
- 2011-04-15 CA CA2813860A patent/CA2813860A1/en not_active Abandoned
- 2011-04-15 EA EA201370062A patent/EA201370062A1/ru unknown
- 2011-04-15 BR BR112013007502A patent/BR112013007502A2/pt not_active IP Right Cessation
- 2011-04-15 WO PCT/ES2011/070265 patent/WO2012140284A1/es active Application Filing
- 2011-04-15 EP EP11861327.2A patent/EP2543746A4/en not_active Withdrawn
- 2011-04-15 KR KR1020137008846A patent/KR20130108341A/ko not_active Application Discontinuation
- 2011-04-15 MX MX2013003380A patent/MX2013003380A/es unknown
- 2011-04-15 CN CN2011800467297A patent/CN103210099A/zh active Pending
- 2011-04-15 JP JP2014504361A patent/JP2014510841A/ja active Pending
- 2011-04-15 AU AU2011365350A patent/AU2011365350A1/en not_active Abandoned
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WO2014013092A1 (es) | 2012-07-16 | 2014-01-23 | Tam 5, S.L. | Metodo hidrometalúrgico para la recuperación de zinc en medio sulfúrico a partir de concentrados de zinc sulfurados con alto contenido en hierro |
US9463986B2 (en) | 2012-07-16 | 2016-10-11 | Tam 5, S.L. | Hydrometallurgical method for recovery of zinc in sulphuric medium starting from sulphidic zinc concentrates with high iron content |
CN103130282A (zh) * | 2013-03-20 | 2013-06-05 | 江苏理工学院 | 黄钾铁矾的制备方法 |
CN103922417A (zh) * | 2013-03-20 | 2014-07-16 | 江苏理工学院 | 制备黄钾铁矾的方法 |
CN103922418A (zh) * | 2013-03-20 | 2014-07-16 | 江苏理工学院 | 一种制备黄钾铁矾的方法 |
CN103936080A (zh) * | 2013-03-20 | 2014-07-23 | 江苏理工学院 | 一种黄钾铁矾的制备方法 |
CN103643036A (zh) * | 2013-12-20 | 2014-03-19 | 广西冶金研究院 | 一种热压选择性浸出处理含铁铟锌焙砂的方法 |
CN103898336A (zh) * | 2014-03-24 | 2014-07-02 | 中国恩菲工程技术有限公司 | 处理锌焙烧矿的方法 |
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Also Published As
Publication number | Publication date |
---|---|
BR112013007502A2 (pt) | 2019-09-24 |
EP2543746A4 (en) | 2014-12-03 |
AU2011365350A1 (en) | 2013-03-14 |
WO2012140284A8 (es) | 2013-03-28 |
KR20130108341A (ko) | 2013-10-02 |
EA201370062A1 (ru) | 2013-11-29 |
JP2014510841A (ja) | 2014-05-01 |
CN103210099A (zh) | 2013-07-17 |
CA2813860A1 (en) | 2012-10-18 |
MX2013003380A (es) | 2013-04-29 |
EP2543746A1 (en) | 2013-01-09 |
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