CN102534660A - Method for electrolytically refining crude lead - Google Patents

Method for electrolytically refining crude lead Download PDF

Info

Publication number
CN102534660A
CN102534660A CN201210010362XA CN201210010362A CN102534660A CN 102534660 A CN102534660 A CN 102534660A CN 201210010362X A CN201210010362X A CN 201210010362XA CN 201210010362 A CN201210010362 A CN 201210010362A CN 102534660 A CN102534660 A CN 102534660A
Authority
CN
China
Prior art keywords
lead
sodium hydroxide
electrolytic solution
electrolyte
negative electrode
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.)
Granted
Application number
CN201210010362XA
Other languages
Chinese (zh)
Other versions
CN102534660B (en
Inventor
刘伟
杨天足
周琼华
张杜超
刘伟锋
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.)
Henan University of Science and Technology
Original Assignee
Henan University of Science and Technology
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 Henan University of Science and Technology filed Critical Henan University of Science and Technology
Priority to CN201210010362.XA priority Critical patent/CN102534660B/en
Publication of CN102534660A publication Critical patent/CN102534660A/en
Application granted granted Critical
Publication of CN102534660B publication Critical patent/CN102534660B/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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

The invention discloses a method for electrolytically refining crude lead. The method comprises the following steps of: adding sodium hydroxide and tartaric acid into water in turn, and stirring to dissolve at normal temperature to obtain a mixed solution; adding lead oxide powder into the mixed solution, dissolving and filtering to obtain filtrate, namely electrolyte; and adding the prepared electrolyte into an electrolytic cell, and switching on direct current for electrolysis by taking a stainless steel plate or a pure lead plate as a cathode and crude lead to be refined as an anode. By the method, smoke and middle slag generated in pyro-refining are avoided, the direct recovery rate of lead and comprehensive recovery rate of valued metals in the refining process are improved, volatile smoke or acid mist cannot be generated, and a defect that electrolyte in a silicofluoric acid system pollutes environment is overcome; meanwhile, the sodium hydroxide and the tartaric acid are added into the electrolyte, so that the sodium hydroxide and the tartaric acid can form a complex with the lead oxide, the concentration of lead ions in the electrolyte is greatly increased and the electrolysis efficiency is improved.

Description

A kind of method of electrorefining lead bullion
Technical field
The present invention relates to plumbous purification refining field, a kind of specifically method of electrorefining lead bullion.
Background technology
For remove in the lead bullion detrimental impurity with reclaim precious metal, must carry out refining to it, the method for the refining of lead bullion is divided two kinds of pyrogenic process and electrolytic process.The master operation of fire refining process is: 1. copper removal: first liquate or condensation copper removal add sulphur degree of depth copper removal again; 2. add caustic soda and remove tellurium; 3. with oxidation style or alkali-chloride improving arsenic removal, antimony, tin; 4. zincification reclaims gold and silver; 5. dezincify; 6. add calcium magnesium and remove bismuth; 7. final refining ingot casting obtains lead bullion.The slag of each operation output is handled respectively to reclaim wherein valuable element.The pyrorefining lead bullion produces quite a large amount of leaded (and other metal) flue dust, various middle slag and sulfur dioxide gas, and contaminate environment is serious, and plumbous simultaneously direct yield and comprehensive recovery are lower.
Compare with pyrogenic process, the waste gas that electrolytic process produces is few, and energy consumption is low, and therefore superior product quality has obtained using widely in the refining of lead bullion.It is Bai Zifa that the extensive method that adopts of lead bullion electrorefining is gone up in industry at present, and promptly lead bullion is cast positive plate, is processed into starting sheet with negative electrode lead, is containing PbSiF 6With free H 2SiF 6Carry out electrolysis in the solution.Bai Zifa is widely used in the plumbous smeltery of states such as China, Canada, Italy, Japan, Peru, Russia at present.But there are some shortcomings in Bai Zifa, like H 2SiF 6Volatile, the job site can produce a large amount of acid mists, and the smell is awful, PbSiF 6The preparation process in can emit HF and SiF 4Gas, to human body and environmental hazard very big (volume such as Beijing Nonferrous Metallurgy Design Research Institute, the heavy non-ferrous metal smelting DM: plumbous zinc bismuth volume, Beijing: metallurgical industry press, 1995, P88-106, P119-146).Other acid system of once studying has muriate, nitrate salt, borate salt system etc., but only limits to plumbous electrodeposition, do not see the report that is applied to the refining of lead bullion as yet, and acid electrolyte is volatile, pollutes generally bigger.
Summary of the invention
The present invention for solve prior art when the lead bullion electrorefining to environment and the very big problem of human harm; A kind of method of electrorefining lead bullion is provided; This method is through carrying out the electrorefining of lead bullion in containing tartaric basic soln, can alleviate the environmental pollution of electrolytic process and to the harm of human body.
The present invention solves the problems of the technologies described above the technical scheme of employing to be: a kind of method of electrorefining lead bullion; Add sodium hydroxide, tartrate in the entry successively; Stirring and dissolving makes mixing solutions at normal temperatures, and the add-on of tartrate and sodium hydroxide is to add 100 ~ 160g tartrate, 80 ~ 160g sodium hydroxide in every liter of mixing solutions; In mixing solutions, adding lead oxide powder then, is stirring and dissolving under 40 ~ 98 ℃, the condition of stirring velocity 200 ~ 400r/min in temperature, and time 1 ~ 6h filters then, and gained filtrating is electrolytic solution; The granularity of described lead oxide powder is less than 200 orders, and plumbum ion concentration is 80 ~ 130g/L in the electrolytic solution for preparing;
The electrolytic solution that makes is added in the electrolyzer; Adopt stainless steel plate or pure stereotype as negative electrode, adopt and treat that the purified lead bullion processes anode, feed direct current and carry out electrolysis; Concrete electrolytic process parameter is: 40 ~ 60 ℃ of electrolyte temperatures; The circulation of elecrolyte cycle is 45 ~ 120min, the circulation of elecrolyte mode under go out cathode current density 100 ~ 160A/m on advancing 2, bath voltage 0.25 ~ 1.0V, anodic current density 100 ~ 160A/m 2, with interpole gap 80 ~ 130mm;
Rise to 1.0V when bath voltage in the electrolytic process, when promptly anode passivation taking place, take out positive plate and scrub or the double teeming positive plate, scrub or double teeming after positive plate return the participation electrolysis;
According to the steam output of electrolytic solution, timing make up water in electrolytic solution is to keep plumbum ion concentration 80 ~ 130g/L in the electrolytic solution, sodium hydroxide 80 ~ 160 g/L and tartaric acid concentration 100 ~ 160 g/L;
The dirt settling of collecting on the negative electrode is the lead that obtains after the refining.
Among the present invention, said tartrate, sodium hydroxide and plumbous oxide are analytical pure or technical grade reagent.
The present invention can carry out when scrubbing anode during dirt settling on collecting negative electrode.
Among the present invention; Adding sodium hydroxide and tartaric reason are when preparing electrolyte: sodium hydroxide and tartrate can form a kind of structure that is similar to title complex with plumbous oxide; Can increase the concentration of lead ion in the electrolytic solution greatly; The electrolytic solution of alkalescence is also more stable when electrolysis simultaneously, can not produce the gas to environment and human body harmful.
Among the present invention, in electrolytic process, by the anode of lead bullion cast, under the effect of electric current, lead constantly enters into electrolytic solution and forms title complex, and title complex obtains electron reduction for plumbous at negative electrode then; Anode constantly dissolves, and final anode is remaining to be the anode sludge that anode scrap and precious metal are formed.
The present invention is applicable to the lead bullion of plumbous smelting process output, and its staple scope is: Pb 96% ~ 99%, Sb 0.5% ~ 3%, and Cu 0.05% ~ 3%, and As 0.005% ~ 1.5%, and Sn 0.02% ~ 1%, and Bi 0.1% ~ 1%, and Ag 0.1% ~ 3%; Also be suitable for handling lead antimony alloy, lead bismuth alloy etc.
Beneficial effect: the present invention and traditional plumbous refinery practice compare, and following advantage is arranged: 1, the present invention has avoided various flue dust, the middle slag that pyrorefining produces, and has improved the direct yield of refining process lead and the comprehensive recovery of various valuable metals;
2, the alkaline organic electrolysis system is environmentally friendly, can not produce volatilization flue dust or acid mist, has overcome the shortcoming of silicofluoric acid system electrolyte contamination environment;
3, adding sodium hydroxide and tartrate can form title complex with plumbous oxide in the electrolytic solution, have increased the concentration of lead ion in the electrolytic solution greatly, have improved electrolytic efficiency.
Embodiment
Below in conjunction with specific embodiment the present invention is done further elaboration.
Embodiment 1
Lead content in the lead bullion is 98.30%, and the major impurity composition is tin 0.0008%, antimony 0.8281%, bismuth 0.1363%, arsenic 0.5127%, copper 0.0795%, zinc 0.0006%, silver 0.1406%, iron 0.0013%.Tartrate, sodium hydroxide and plumbous oxide are analytical pure.
Take by weighing lead bullion 500 g, 600 ℃ of fusing 15 min that heat take out in retort furnace, in graphite jig, are cast into positive plate, are of a size of 10cm * 10cm.
Take by weighing 200 g plumbous oxide, 180 g sodium hydroxide, 180 g tartrate add in the 1.5 L water, and 70 ℃ of magnetic agitation 4 h filter, and promptly obtain electrolytic solution, and wherein plumbum ion concentration is 110g/L.55 ℃ of control electrolysis temperatures, current density 140 A/m 2, pole span 4 cm, pole plate area 9.7 cm * 9.9 cm, circulation of elecrolyte speed 30 mL/min when bath voltage is increased to 1.0V, take out positive plate, scrub to put into electrolyzer behind the anode sludge and continue electrolysis, and electrolysis time amounts to 24h.Average cell voltage 0.32V, current efficiency 98.93%, negative electrode energy consumption 83.69 kWh/t Pb.The constituent content of the negative electrode lead and the anode sludge is seen table 1 and table 2 respectively.
The foreign matter content (* 10 that table 1 negative electrode is plumbous -6%)
Element Sn Sb Bi As Cu Zn Fe Ag Ni Cd Summation
Negative electrode is plumbous <8.9 <8.9 2880 15.8 573 <8.9 310 <8.9 <8.9 <8.9 <3832.2
GB (<=) 500 800 4000 500 1000 400 500 800 - - 6000
The constituent content of table 2 anode sludge (%)
Element Sn Sb Bi As Cu Zn Fe Ag Ni Cd
The anode sludge - 12.28 10.84 33.83 7.188 - 0.464 10.66 0.109 -
Can be found out that by table 1 foreign matter content in the negative electrode lead is very low, the purity of negative electrode lead is higher, is higher than 99.99617%, has reached the standard of Pb99.994 lead pig among the GB/T 469-2005.Can find out that by table 2 enrichment of element such as silver, bismuth, antimony are in the anode sludge.
Embodiment 2
The content of the lead in the lead bullion is 98.10%, and the major impurity composition is tin 0.0008%, antimony 0.9106%, bismuth 0.1959%, arsenic 0.5451%, copper 0.0933%, zinc 0.0006%, silver 0.1521%, iron 0.0015%.Tartrate, sodium hydroxide and plumbous oxide are analytical pure.
Take by weighing lead bullion 500g, in retort furnace, heat, take out, in graphite jig, be cast into positive plate, be of a size of 10cm * 10cm to 650 ℃ of fusing 15min.
Get 180 g plumbous oxide, 210 g sodium hydroxide, 210 g tartrate add in the 1.5 L zero(ppm) water, and 80 ℃ of magnetic agitation 4 h promptly obtain electrolytic solution after the filtration, and wherein plumbum ion concentration is 100g/L.45 ℃ of control electrolysis temperatures, current density 160 A/m2, pole span 4 cm, pole plate area 9.7 cm * 9.9 cm, electrolytic solution volume 1.5 L, circulation of elecrolyte speed 30 mL/min.When bath voltage is increased to 1.0V, take out positive plate, scrub and put into electrolyzer behind the anode sludge and continue electrolysis, electrolysis time amounts to 25h.Average cell voltage 0.39V, current efficiency 98.77%, negative electrode energy consumption 102.16 kWh/t Pb.Negative electrode the constituent content plumbous and anode sludge is seen table 3 and table 4 respectively.
The foreign matter content (* 10 that table 3 negative electrode is plumbous -6%)
Element Sn Sb Bi As Cu Zn Fe Ag Ni Cd Summation
Negative electrode is plumbous <9.5 <9.5 3100 19.8 540 <9.5 335 <9.5 <9.5 <9.5 <4042.3
GB (<=) 500 800 4000 500 1000 400 500 800 - - 6000
The constituent content of table 4 anode sludge (%)
Element Sn Sb Bi As Cu Zn Fe Ag Ni Cd
The anode sludge - 14.58 9.431 31.53 6.673 - 0.312 9.85 0.0845 -
Can find out that by table 3 the plumbous purity of negative electrode is 99.99596%, has reached the standard of Pb99.994 lead pig among the GB/T 469-2005.Can find out that by 4 enrichment of element such as silver, bismuth, antimony are in the anode sludge.
Embodiment 3
Lead content in the lead bullion is 98.30%, and the major impurity composition is tin 0.0008%, antimony 0.8281%, bismuth 0.1363%, arsenic 0.5127%, copper 0.0795%, zinc 0.0006%, silver 0.1406%, iron 0.0013%.Tartrate, sodium hydroxide and plumbous oxide are analytical pure.
Take by weighing lead bullion 500 g, 600 ℃ of fusing 15 min that heat take out in retort furnace, in graphite jig, are cast into positive plate, are of a size of 10cm * 10cm.
Take by weighing 100 g plumbous oxide, 120g sodium hydroxide, 150 g tartrate add in the 1.5 L water, and 70 ℃ of magnetic agitation 4 h filter, and promptly obtain electrolytic solution, and wherein plumbum ion concentration is 80g/L.40 ℃ of control electrolysis temperatures, current density 100 A/m 2, pole span 4 cm, pole plate area 9.7 cm * 9.9 cm, circulation of elecrolyte speed 8.5 mL/min when bath voltage is increased to 1.0V, take out positive plate, scrub to put into electrolyzer behind the anode sludge and continue electrolysis, and electrolysis time amounts to 24h.Average cell voltage 0.27V, current efficiency 99.15%, negative electrode energy consumption 70.45 kWh/t Pb.The constituent content of the negative electrode lead and the anode sludge is seen table 5 and table 6 respectively.
The foreign matter content (* 10 that table 5 negative electrode is plumbous -6%)
Element Sn Sb Bi As Cu Zn Fe Ag Ni Cd Summation
Negative electrode is plumbous <8.9 <8.9 1850 12.6 435 <8.9 230 <8.9 <8.9 <8.9 <2581
GB (<=) 500 800 4000 500 1000 400 500 800 - - 6000
The constituent content of table 6 anode sludge (%)
Element Sn Sb Bi As Cu Zn Fe Ag Ni Cd
The anode sludge - 13.44 10.97 35.27 8.322 - 0.489 10.83 0.112 -
Can be found out that by table 5 foreign matter content in the negative electrode lead is very low, the purity of negative electrode lead is higher, is higher than 99.99741%, has reached the standard of Pb99.994 lead pig among the GB/T 469-2005.Can find out that by table 6 enrichment of element such as silver, bismuth, antimony are in the anode sludge.
Embodiment 4
Lead content in the lead bullion is 98.30%, and the major impurity composition is tin 0.0008%, antimony 0.8281%, bismuth 0.1363%, arsenic 0.5127%, copper 0.0795%, zinc 0.0006%, silver 0.1406%, iron 0.0013%.Tartrate, sodium hydroxide and plumbous oxide are analytical pure.
Take by weighing lead bullion 500 g, 600 ℃ of fusing 15 min that heat take out in retort furnace, in graphite jig, are cast into positive plate, are of a size of 10cm * 10cm.
Take by weighing 250 g plumbous oxide, 240 g sodium hydroxide, 240 g tartrate add in the 1.5 L water, and 70 ℃ of magnetic agitation 4 h filter, and promptly obtain electrolytic solution, and wherein plumbum ion concentration is 130g/L.55 ℃ of control electrolysis temperatures, current density 160 A/m 2, pole span 4 cm, pole plate area 9.7 cm * 9.9 cm, circulation of elecrolyte speed 30 mL/min when bath voltage is increased to 1.0V, take out positive plate, scrub to put into electrolyzer behind the anode sludge and continue electrolysis, and electrolysis time amounts to 24h.Average cell voltage 0.38V, current efficiency 98.27%, negative electrode energy consumption 100.05 kWh/t Pb.The constituent content of the negative electrode lead and the anode sludge is seen table 7 and table 8 respectively.
The foreign matter content (* 10 that table 7 negative electrode is plumbous -6%)
Element Sn Sb Bi As Cu Zn Fe Ag Ni Cd Summation
Negative electrode is plumbous <8.9 <8.9 3250 17.4 698 <8.9 421 <8.9 <8.9 <8.9 <4749.8
GB (<=) 500 800 4000 500 1000 400 500 800 - - 6000
The constituent content of table 8 anode sludge (%)
Element Sn Sb Bi As Cu Zn Fe Ag Ni Cd
The anode sludge - 11.13 10.62 31.53 6.205 - 0.375 10.35 0.115 -
Can be found out that by table 7 foreign matter content in the negative electrode lead is very low, the purity of negative electrode lead is higher, is higher than 99.99525%, has reached the standard of Pb99.994 lead pig among the GB/T 469-2005.Can find out that by table 8 enrichment of element such as silver, bismuth, antimony are in the anode sludge.

Claims (1)

1. the method for an electrorefining lead bullion; It is characterized by: add sodium hydroxide, tartrate in the entry successively; Stirring and dissolving makes mixing solutions at normal temperatures, and the add-on of tartrate and sodium hydroxide is to add 100 ~ 160g tartrate, 80 ~ 160g sodium hydroxide in every liter of mixing solutions; In mixing solutions, adding lead oxide powder then, is stirring and dissolving under 40 ~ 98 ℃, the condition of stirring velocity 200 ~ 400r/min in temperature, and time 1 ~ 6h filters then, and gained filtrating is electrolytic solution; The granularity of described lead oxide powder is less than 200 orders, and plumbum ion concentration is 80 ~ 130g/L in the electrolytic solution for preparing;
The electrolytic solution that makes is added in the electrolyzer; Adopt stainless steel plate or pure stereotype as negative electrode, adopt and treat that the purified lead bullion processes anode, feed direct current and carry out electrolysis; Concrete electrolytic process parameter is: 40 ~ 60 ℃ of electrolyte temperatures; The circulation of elecrolyte cycle is 45 ~ 120min, the circulation of elecrolyte mode under go out cathode current density 100 ~ 160A/m on advancing 2, bath voltage 0.25 ~ 1.0V, anodic current density 100 ~ 160A/m 2, with interpole gap 80 ~ 130mm;
Rise to 1.0V when bath voltage in the electrolytic process, when promptly anode passivation taking place, take out positive plate and scrub or the double teeming positive plate, scrub or double teeming after positive plate return the participation electrolysis;
According to the steam output of electrolytic solution, timing make up water in electrolytic solution is to keep plumbum ion concentration 80 ~ 130g/L in the electrolytic solution, sodium hydroxide 80 ~ 160 g/L and tartaric acid concentration 100 ~ 160 g/L;
The dirt settling of collecting on the negative electrode is the lead that obtains after the refining.
CN201210010362.XA 2012-01-13 2012-01-13 Method for electrolytically refining crude lead Expired - Fee Related CN102534660B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201210010362.XA CN102534660B (en) 2012-01-13 2012-01-13 Method for electrolytically refining crude lead

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201210010362.XA CN102534660B (en) 2012-01-13 2012-01-13 Method for electrolytically refining crude lead

Publications (2)

Publication Number Publication Date
CN102534660A true CN102534660A (en) 2012-07-04
CN102534660B CN102534660B (en) 2014-06-18

Family

ID=46342648

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201210010362.XA Expired - Fee Related CN102534660B (en) 2012-01-13 2012-01-13 Method for electrolytically refining crude lead

Country Status (1)

Country Link
CN (1) CN102534660B (en)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103510109A (en) * 2013-10-24 2014-01-15 北京化工大学 Method for recycling lead-containing grid of waste lead-acid battery through self-gravity contact electrolysis
CN104131317A (en) * 2014-08-01 2014-11-05 昆明理工大学 Method for preparation of fine lead powder by electrodeposition
CN105714329A (en) * 2014-12-05 2016-06-29 上海奇谋能源技术开发有限公司 Method for directly electrolyzing metal scraps
CN106011931A (en) * 2016-08-08 2016-10-12 昆明冶金研究院 Large-pole plate long-time cycle lead anode two-step electrolytic refining method
CN107059064A (en) * 2016-12-08 2017-08-18 汤恭年 The electricity growth powder method processed of lead-acid accumulator special-purpose nanometer lead powder
CN109055982A (en) * 2018-09-20 2018-12-21 湖南省桂阳银星有色冶炼有限公司 A kind of lead bullion electrolytic smelting method
CN109778230A (en) * 2019-01-22 2019-05-21 河套学院 A kind of method of high lead copper matte electrolytic separation lead and copper
CN113215619A (en) * 2021-04-26 2021-08-06 太和县大华能源科技有限公司 Electrolytic refining system of lead bullion

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009068988A2 (en) * 2007-11-30 2009-06-04 Engitec Technologies S.P.A. Process for producing metallic lead starting from desulfurized pastel
CN101748432A (en) * 2008-12-15 2010-06-23 汉中八一锌业有限责任公司 Electrolytic lead smelting method

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009068988A2 (en) * 2007-11-30 2009-06-04 Engitec Technologies S.P.A. Process for producing metallic lead starting from desulfurized pastel
CN101748432A (en) * 2008-12-15 2010-06-23 汉中八一锌业有限责任公司 Electrolytic lead smelting method

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
CHEN WEIPING ET.AL: "Cathode electrodeposition of lead in Pb2+-OH-C4H4O62- system", 《TRANS. NONFERROUS MET.SOC.CHINA》, vol. 7, no. 3, 30 September 1997 (1997-09-30), pages 155 - 158 *
沈阳有色冶炼技工学校 编: "《铅电解精炼工教材》", 28 February 1958, article "铅电解精炼工教材", pages: 32-33 - 42 *
陈维平 等: "废铅蓄电池浆料回收技术研究", 《有色金属》, vol. 49, no. 4, 30 November 1997 (1997-11-30), pages 64 - 67 *

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103510109A (en) * 2013-10-24 2014-01-15 北京化工大学 Method for recycling lead-containing grid of waste lead-acid battery through self-gravity contact electrolysis
CN103510109B (en) * 2013-10-24 2016-03-02 北京化工大学 The method of the leaded grid of waste lead acid battery is reclaimed from gravity contact electricity solution
CN104131317A (en) * 2014-08-01 2014-11-05 昆明理工大学 Method for preparation of fine lead powder by electrodeposition
CN104131317B (en) * 2014-08-01 2016-08-24 昆明理工大学 The method of thin lead powder is prepared in a kind of electro-deposition
CN105714329A (en) * 2014-12-05 2016-06-29 上海奇谋能源技术开发有限公司 Method for directly electrolyzing metal scraps
CN105714329B (en) * 2014-12-05 2017-10-20 上海奇谋能源技术开发有限公司 A kind of method of Direct Electrolysis scrap
CN106011931A (en) * 2016-08-08 2016-10-12 昆明冶金研究院 Large-pole plate long-time cycle lead anode two-step electrolytic refining method
CN107059064A (en) * 2016-12-08 2017-08-18 汤恭年 The electricity growth powder method processed of lead-acid accumulator special-purpose nanometer lead powder
CN109055982A (en) * 2018-09-20 2018-12-21 湖南省桂阳银星有色冶炼有限公司 A kind of lead bullion electrolytic smelting method
CN109778230A (en) * 2019-01-22 2019-05-21 河套学院 A kind of method of high lead copper matte electrolytic separation lead and copper
CN113215619A (en) * 2021-04-26 2021-08-06 太和县大华能源科技有限公司 Electrolytic refining system of lead bullion

Also Published As

Publication number Publication date
CN102534660B (en) 2014-06-18

Similar Documents

Publication Publication Date Title
CN102534660B (en) Method for electrolytically refining crude lead
CN102851693B (en) Technology for recovering production of electrolytic copper and zinc from smelting ash
CN102560535B (en) Method for recovering lead in waste lead-acid storage battery filler by using wet process
CN101649396B (en) Methods of removing F and Cl in secondary zinc oxide dust effectively and producing electrolytic zinc
CN104630826B (en) Technique for recovering tin from tin anode sludge
CN101157987A (en) Method for preparing electrolytic zinc by processing complex secondary zinc oxide material
CN103849775B (en) A kind of method reclaiming nickel and cobalt from high-temperature alloy waste material
CN101519727A (en) Processing method of zinc smelting byproducts
CN102433443B (en) The method of copper is reclaimed from electroplating sludge, electroplating effluent
CN102633326B (en) Ion exchange membrane electrolysis method for treating acid waste water containing chloride in copper metallurgy process
CN103924095B (en) In a kind of copper-cadmium slag, reclaim the new method of cadmium
CN103710533B (en) A kind of method of producing electrolytic metal Mn
CN101338365B (en) Synthesizing method for molybdenum-nickel ore
CN102839379A (en) On-line treatment method of acidic etching solution
CN105274563A (en) High-purity cobalt preparation method
CN103938228B (en) Lead electrolytic solution and the purification method of earth of positive pole wash water foreign metal ion
CN103710541A (en) Wet process for producing electrolytic manganese dioxide
CN103205576A (en) Method for treating lead anode slime
CN102851508B (en) Method for producing electrolytic lead powder through alkali immersion rotational flow electrolysis of wet electrolytic zinc acid dipping residues
CN101333605A (en) Technology for extracting indium from indium-rich bottom lead
CN102899687A (en) Separation and extraction process for crude lead containing indium
CN102560130A (en) Selective leaching technology of copper and zinc in scrap copper smelting slag
CN102888624A (en) Method for producing superfine zinc powder by performing cyclone electrolyzing on zinc-containing alkali liquor
CN110607444B (en) Novel treatment method for copper and tin slag removal
CN103397182A (en) Method for efficiently recycling bismuth from monomer bismuth ore

Legal Events

Date Code Title Description
PB01 Publication
C06 Publication
SE01 Entry into force of request for substantive examination
C10 Entry into substantive examination
GR01 Patent grant
C14 Grant of patent or utility model
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20140618

Termination date: 20180113

CF01 Termination of patent right due to non-payment of annual fee