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CN100368571C - Method for separating Fe-Mn and Mn-Zn - Google Patents

Method for separating Fe-Mn and Mn-Zn Download PDF

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CN100368571C
CN100368571C CNB2005100324177A CN200510032417A CN100368571C CN 100368571 C CN100368571 C CN 100368571C CN B2005100324177 A CNB2005100324177 A CN B2005100324177A CN 200510032417 A CN200510032417 A CN 200510032417A CN 100368571 C CN100368571 C CN 100368571C
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zinc
manganese
iron
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CN1970801A (en
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何静
杨声海
唐朝波
唐谟堂
李仕庆
鲁君乐
姚维义
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Central South University
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Abstract

一种硫酸盐中铁-锌和锰-锌的分离以及电解制取高纯锌或高纯锌粉的方法，本发明包括硫酸盐溶液还原、沉复盐、复盐转化与氨浸液净化、电解等过程，较好地解决了硫酸盐中铁-锌和锰-锌的分离问题，在制备锰锌软磁用共沉粉的同时，开路和回收多余的锌，并将这部分锌制成高纯锌或高纯锌粉，它的纯度≥99.995%，有毒元素镉、铅、砷、汞的含量≤0.0005%。还可为铁、锰精细产品的制备及锌回收提供技术支撑。

Figure 200510032417

A method for separating iron-zinc and manganese-zinc in sulfate and electrolytically producing high-purity zinc or high-purity zinc powder. The invention includes reduction of sulfate solution, precipitation of double salt, conversion of double salt, purification of ammonia immersion solution, and electrolysis and other processes have better solved the separation problem of iron-zinc and manganese-zinc in sulfate. While preparing the co-precipitated powder for manganese-zinc soft magnetism, the excess zinc is opened and recovered, and this part of zinc is made into high-purity Zinc or high-purity zinc powder, its purity ≥ 99.995%, the content of toxic elements cadmium, lead, arsenic, mercury ≤ 0.0005%. It can also provide technical support for the preparation of iron and manganese fine products and zinc recovery.

Figure 200510032417

Description

The separation method of a kind of iron-zinc and manganese-zinc
[technical field] the invention belongs to field of metallurgy and chemical engineering, relate to iron and zinc and manganese and zinc in the vitriol separate and the method for high purity zinc or high-purity zinc powder is produced in electrolysis.
Iron carries out in acidic solution with zinc and separating generally of manganese and zinc in [background technology] vitriol, it is the iron removal of full zinc hydrometallurgy that typical zinc-iron separates, jarosite process, goethite process and hematite process are arranged on method for removing iron, but these method for removing iron all produce the scum of a large amount of contaminate environment; Industrial, realize that with the neutralization precipitation method manganese-zinc separates, when the vitriol acidic solution that is about to contain zinc and manganese neutralized the PH=6 left and right sides, zinc was with Zn (OH) 2Precipitation, if contain iron in the solution, then it is than the first precipitation of zinc.Cancelled iron removal in the patent application 03118199.2 " a kind of slag-free zinc hydrometallurgy method ", increase substantially metal recovery rate and comprehensive utilization of resources degree, reduce environmental pollution, particularly iron is directly produced Mn-Zn soft magnetic ferrite. but the very low iron of the impurity content of this method output, manganese, zinc content in the mixing double salt of zinc substantially exceeds the ratio requirement of soft magnetism powder, necessary and the iron of unnecessary zinc, manganese separates, reclaim separately behind the open circuit. once from the vitriol acidic solution, extracted unnecessary zinc with P204, also once adopted pure water repeatedly to wash this double salt, attempt realizes unnecessary zinc and iron, the separation of manganese, but, on engineering, all can't realize because of separation factor is all little.
[summary of the invention] the present invention changes into the mixing double salt of iron, manganese, zinc with ammonium hydrogencarbonate-ammonia solution the coprecipitated powder of carbonate of soft magnetism iron, manganese, zinc, and leach unnecessary zinc, thereby realize the separation of iron-zinc and manganese-zinc, produce high-purity electric zinc or zinc powder through purifying electrolysis then.
The present invention adopts the raw mineral materials of iron, manganese, zinc, as in soak slag and pyrolusite, zinc sulfide concentrates high temperature peracid reduction leach liquor be raw material, its composition is: H 2SO 420～40g/L, Fe 3+1～5g/L, Fe 2+30～65g/L, Zn 2+45～80g/L, In 3+0.2～0.6g/L, Mn 2+9～40g/L.
The present invention is earlier with the high valence ion Fe in iron, manganese, the zinc sulfate liquor + 3And Cu + 2Reduction with the indium in the extraction process extraction reduced liquid, is reclaimed germanium with the precipitator method then; Primary purification promptly removes with sulfurization-precipitation method earlier and removes Zn + 2All heavy metal ion are in addition tentatively removed impurity element aluminium, silicon, arsenic, antimony with neutralisation then; Secondary-cleaned is promptly further removed detrimental impurity elemental silicon, aluminium, calcium, magnesium, potassium, sodium and is removed Zn with the double salt precipitation method + 2All heavy metal ion in addition, the mixing double salt of the iron that the acquisition impurity content is very low, manganese, zinc, it is FeSO 4(NH 4) 2SO 46H 2O, ZnSO 4(NH 4) 2SO 46H 2O and MnSO 4(NH 4) 2SO 46H 2The mixture of O, the Fe/Mn weight percent is 2.8～4.5 in this double salt, and manganese meets the ratio requirement of soft magnet powder material substantially, and the weight percent of Fe/Zn is 0.6～1.5, and zinc surpasses the ratio requirement of soft magnetism powder in a large number; To mix iron in the double salt, manganese and part zinc with ammonium hydrogencarbonate-ammonia solution and change into the carbonate coprecipitated powder of soft magnetism with iron, manganese, zinc, the control proportioning makes it to reach substantially the ratio of magneticsubstance principal constituent, and leaches and the unnecessary zinc of opening a way; At last ammonia leaching solution purification, electrolysis are produced its purity 〉=99.995%, the content of poisonous element cadmium, lead, arsenic, the mercury high-purity electric zinc or the high-purity zinc powder that can be used as medicine or feed grade zinc product raw material respectively≤0.0005%. details are as follows for specific embodiment and condition.
1. reduction, collection indium and rough purification
Press general technology reduction, collection indium and rough purification, obtain primary purification liquid and secondary-cleaned liquid, as the method for patent application 03118199.2 introduction.
2. heavy double salt and secondary-cleaned
With the double salt precipitation method one clean liquid is carried out secondary-cleaned, make most of Fe, Mn and whole Zn with double salt precipitation, and impurity elemental silicon, aluminium, calcium, magnesium, potassium, sodium and remove Zn + 2All heavy metal ion are in addition mostly stayed in the double salt mother liquor:
MeSO 4+(NH 4) 2SO 4+6H 2O＝MeSO 4·(NH 4) 2SO 4·6H 2O↓(1)
In the formula: Me represents Fe, Mn, Zn.The technology condition of heavy double salt and secondary-cleaned is: temperature is 0～50 ℃; Time is 0.5～10h; PH value=1～3; Free (NH 4) 2SO 4Concentration is 0.2～3.5mol/L.
3. double salt transforms and open circuit zinc
To mix iron in the double salt, manganese and part zinc with ammonium hydrogencarbonate-ammonia solution and change into the coprecipitated powder of soft magnetism, the control proportioning makes it to reach substantially the ratio of magneticsubstance principal constituent, and leaches and the unnecessary zinc of opening a way:
MeSO 4·(NH 4) 2SO 4·6H 2O+2NH 4HCO 3＝MeCO 3↓+2(NH 4) 2SO 4+CO 2+7H 2O (2)
In the formula: Me represents Fe, Mn, Zn.
ZnSO 4·(NH 4) 2SO 4·6H 2O+(i+2)NH 3＝Zn(NH 3) i 2++2(NH 4) 2SO 4+2OH -+4H 2O?(3)
The technology condition that double salt transforms with open circuit zinc is: 1. the ammonium hydrogencarbonate consumption is 1.2～2.5 times of theoretical consumption; Ammonia concentration is 1.5～3.5molL -1, 2.. and liquid-solid ratio=1.0～3.0/1,3.. temperature is 293～323K; 4.. churning time is 30～120min; 5.. digestion time 8～24h; 6.. filter residue with 40～80 ℃ ± pure water repeatedly wash, can't check SO up to barium chloride solution 4 2-Till.
4. the purification of ammonia leaching solution and electrolysis
Remove de-iron and the electropositive impurity element of heavy metal geometric ratio zinc with the zinc replacement degree of depth:
2Me n++nZn＝2Me+nZn 2+ (4)
n?Zn 2++inNH 3＝n?Zn(NH 3) i 2+ (5)
Purification condition is: 1. the zinc powder consumption is 1～4g/L reduced liquid, and zinc powder is crossed 120 mesh sieves; 2. open to stir in the 10～60min of back and add zinc powder; 3. the clarification time is 15～90min; 4. purify and finish back filtration at once;
The scavenging solution of ammonia leaching solution obtains high-purity electric zinc or zinc powder under the direct current effect, emit oxygen simultaneously:
Negative electrode: Zn (NH 3) i 2++ 2e=Zn+iNH 3(6)
Anode: 4OH-=O 2+ 2H 2O+4e (7)
Electrolytic condition is: 1. the titanium plate is made pole plate, and spread of electrodes is 10～18cm; 2. bath composition: (NH 4) 2SO 41.2～3.5mol/L, NH 31.5～3.5mol/L, Zn 2+10～60g/L; 3.. temperature is 293～333K; 4.. current density 200～1000A/m 25.. bath voltage 2～5v.
The present invention has realized the separation of iron-zinc and manganese-zinc in the vitriol, when the preparation soft magnetism is with coprecipitated powder, reclaim unnecessary zinc, raw material---the high-purity electric zinc or the zinc powder of preparation medicine or feed grade zinc product, make the iron resources in the zinc ore concentrate fully obtain utilizing, the preparation and the zinc recovery that also can be iron, manganese fine product provide technical support, thereby bring remarkable economic efficiency and social benefit.
[description of drawings]
Fig. 1 is a process flow sheet of the present invention.
[specific embodiment mode]
Embodiment 1
A: reduction, collection indium and rough purification
With composition is Zn54.22g/L, Fe 3+1.7g/L, Fe 2+42.1g/L, Mn 2+10.36g/L, In0.312g/L, H 2SO 425.74g/L high temperature peracid reduction leach liquor 8L by the technology condition of No. 03118199.2 patent application specification reduce, come together indium and rough purification, obtaining composition at last is Zn48.48g/L, Fe 2+41.22g/L, Mn 2+12.80g/L and the primary purification liquid 8.5L of pH=5.
B: heavy double salt and secondary-cleaned
(1). get above-mentioned one clean liquid 8.4L, with Cp sulfuric acid adjust pH to 2; (2). add industrial top grade ammonium sulfate 5265g down at 30 ℃, stir 1h; (3). the double salt of centrifuging at once slip, get double salt mother liquor 8.0L, composition is: Zn0.05g/L, Fe6.92g/L, Mn4.84g/L, (NH 4) 2SO 4330g/L; Liquid meter double salt precipitation rate (%) is respectively: Zn99.90, Fe84.01, Mn63.99; Must mix double salt 4538g in addition, Fe/Mn=4.228 in the double salt meets the requirement of high μ magnetic, and Fe/Zn=0.715 differs bigger with 3.86 of high μ magnetic requirement.
C: double salt transforms and open circuit zinc
1.. take by weighing ammonium hydrogencarbonate 849.83g, measure strong aqua 1688ml and pure water and be mixed with 6.75L ammonia and soak transforming agent; 2.. add above-mentioned mixing double salt 4500g, 3.. under 40～45 ℃ temperature, stir 60min; 4.. ageing 10h; 5.. filter, filter residue repeatedly washs with 60 ℃ pure water, can't check SO up to barium chloride solution 4 2-Till.Get coprecipitated powder 695.39g, composition (%) is: Fe41.83, Mn9.89, Zn10.28, Si0.0011, Al0.053, Mg0.0577, Cd0.101, Pb0.0085, K0.008, Na0.0022, Cl0.021, SO 4 2-0.028; Coprecipitated powder foreign matter content is low, and particularly Si, K, Na equal size are very low, and proportioning meets the requirement of high magnetic permeability soft magnetism: Fe: Mn: Zn=67.47: 15.95: 16.58 (wt.); Obtain ammonia leaching solution 7.965L in addition, its composition is: Zn41.67g/L, Fe0.05g/L, Mn0.03g/L, Pb0.01g/L, Cd0.025g/L, As0.008g/L, (NH 4) 2SO 4250.38g/L, (HN 4) 2CO 341.73g/L, NH 32.06molL -1
D: the purification of ammonia leaching solution and electrolysis
1. purify: 1.. measure above-mentioned ammonia leaching solution 6.000L; 2.. open and stir, in 20min, add-120 purpose zinc powder 18g; 3.. continue to stir 30min; 4.. purify and finish back filtration at once; Get scavenging solution 6.05L, its composition is: Zn42.32.g/L, Fe0.0005g/L, Mn0.002g/L, Pb0.0005g/L, Cd0.001g/L, As0.0002g/L, (NH 4) 2SO 4250g/L, NH 32.1molL -1
2. electrolysis: 1.. get above-mentioned scavenging solution 5.0L and place and have in the square electrolyzer of 8L volumetrical, and add electrolysis additive; 2.. make negative electrode with 3 blocks of pure titanium plates, every area 2 * 60cm 2, plating ruthenium titanium plate is made anode, and spread of electrodes is 12cm; 3.. under the temperature of 313K, current density is 200A/m 2And bath voltage is electrolysis 18h under the condition of 3v; Obtain impurity element Cu, Cd, Ni, Co, As, Sb, Hg, Fe all＜0.0001%, Pb＜0.0003%, the high purity zinc 150g of Zn＞99.996%, current efficiency 95%; Waste electrolyte 4.6L contains Zn13.39g/L, (NH 4) 2SO 4271.14g/L, NH 32.05molL -1
Embodiment 2:
A: reduction, collection indium and rough purification
With composition is Zn55.01g/L, Fe 3+3.71g/L, Fe 2+49.75g/L, Mn 2+17.94g/L, In0.349g/L, H 2SO 424.57g/L high temperature peracid reduction leach liquor 10L by the technology condition of No. 03118199.2 patent application specification reduce, come together indium and rough purification, obtaining composition at last is Zn48.39g/L, Fe 2+48.66g/L, Mn 2+21.63g/L and the primary purification liquid 10.8L of PH=5.
B: heavy double salt and secondary-cleaned
Get above-mentioned one clean liquid 10L, technology condition and operation steps are with embodiment 1, obtain to mix double salt 5402g, the double salt precipitation rate is respectively Zn:99.95%, Fe:84.82%, Mn:64.04%, Fe/Mn=2.94 in the double salt, meet the requirement of reduce power consumption magnetic, Fe/Zn=0.853 differs greatly with 9.13 of reduce power consumption magnetic requirement.
C: double salt transforms and open circuit zinc
1.. take by weighing ammonium hydrogencarbonate 1102.44g, measure strong aqua 2625ml and pure water and be mixed with 7.5L ammonia and soak transforming agent; 2.. add above-mentioned mixing double salt 5000g; 3.. under 40～45 ℃ temperature, stir 60min; 4.. ageing 12h; 5.. filter, filter residue repeatedly washs with 60 ℃ pure water, can't check SO up to barium chloride solution 4 2-Till.Get coprecipitated powder 944.08g, composition (%) is: Fe40.465, Mn13.58, Zn4.33, Si0.0019, Al0.032, Mg0.034, Cd0.029, Pb0.003, K0.004, Na0.002, Cl0.02, SO 4 2-0.048; Coprecipitated powder foreign matter content is low, and particularly Si, K, Na equal size are very low, and proportioning meets the requirement of reduce power consumption magnetic: Fe: Mn: Zn=69.32: 23.26: 7.42 (wt.); Obtain ammonia leaching solution 9.16L in addition, its composition is: Zn44.41g/L, Fe0.04g/L, Mn0.035g/L, Pb0.015g/L, Cd0.020g/L, As0.006g/L, (NH 4) 2SO 4282.43g/L, (HN 4) 2CO 347.07g/L, NH 32.33molL -1
D: the purification of ammonia leaching solution and electrolysis
1. purify: step gets scavenging solution 8.10L with embodiment 1, and its composition is: Zn43.86g/L, Fe0.0003g/L, Mn0.0008g/L, Pb0.0004g/L, Cd0.00075g/L, As0.00018g/L, (NH 4) 2SO 4278.94g/L, NH 32.3mo lL -1
2. electrolysis: 1.. get above-mentioned scavenging solution 5.0L and place and have in the square electrolyzer of 8L volumetrical, and add electrolysis additive; 2.. make negative electrode with 3 blocks of pure titanium plates, every area 2 * 60cm 2, plating ruthenium titanium plate is made anode, and spread of electrodes is 10cm; 3.. under the temperature of 323K, current density is 800A/m 2And bath voltage is electrolysis 5h under the condition of 5v; Obtain impurity element Cu, Cd, Ni, Co, As, Sb, Hg, Fe all＜0.0001%, Pb＜0.00023%, the high-purity zinc powder 163.32g of Zn＞99.998%, current efficiency 93%; Waste electrolyte 4.2L contains Zn 13.33g/L, (NH 4) 2SO 4332.07g/L, NH 32.40mo1L -1

Claims (4)

1.一种铁-锌和锰-锌的分离方法，先将铁、锰、锌的硫酸盐溶液还原、萃铟和初步净化制取一净液，然后对一净液进行铁-锌和锰-锌分离，其特征在于下述步骤：1. A method for separating iron-zinc and manganese-zinc, first reducing iron, manganese, zinc sulfate solution, extracting indium and preliminary purification to prepare a clean solution, and then carrying out iron-zinc and manganese to a clean solution - Zinc separation, characterized by the following steps: (1).沉复盐与二次净化(1). Heavy salt and secondary purification 用复盐沉淀法对一净液进行二次净化，二次净化的条件为温度：0～50℃，时间：0.5～10h，PH值：1～3，游离(NH4)2SO4浓度：0.2～3.5mol/L，二次净化使大部分Fe、Mn及全部Zn以复盐沉淀，杂质元素硅、铝、钙、镁、钾、钠及除Zn+2以外的所有重金属离子大都留于复盐母液中，反应方程如下：Use the double salt precipitation method to perform secondary purification on a clean liquid. The conditions for the secondary purification are temperature: 0-50°C, time: 0.5-10h, pH value: 1-3, free (NH 4 ) 2 SO 4 concentration: 0.2～3.5mol/L, secondary purification makes most of Fe, Mn and all Zn precipitated as double salt, impurity elements silicon, aluminum, calcium, magnesium, potassium, sodium and all heavy metal ions except Zn +2 mostly remain in In the double salt mother liquor, the reaction equation is as follows: MeSO4+(NH4)2SO4+6H2O＝MeSO4·(NH4)2SO4·6H2O↓式中Me代表Fe、Mn、Zn；MeSO 4 +(NH 4 ) 2 SO 4 +6H 2 O＝MeSO 4 ·(NH 4 ) 2 SO 4 ·6H 2 O↓ where Me represents Fe, Mn, Zn; (2).复盐转化与开路锌(2). Double salt conversion and open-circuit zinc 用碳酸氢氨-氨溶液将混合复盐中铁、锰和部分锌转化成软磁用共沉粉，工艺条件为：碳酸氢氨用量为理论用量的1.2～2.5倍；氨浓度为1.5～3.5mol·L-1；液固比＝1.0～3.0/1；温度为293～323K；搅拌时间为30～120min；陈化时间8～24h；滤渣用40～80℃的纯水多次洗涤，直到氯化钡溶液检不出SO4 2-为止；得到铁、锰、锌的碳酸盐共沉粉，并浸出和开路多余的锌，主要反应如下：Use ammonium bicarbonate-ammonia solution to convert iron, manganese and part of zinc in the mixed double salt into co-precipitated powder for soft magnetic. The process conditions are: the amount of ammonium bicarbonate is 1.2 to 2.5 times the theoretical amount; the ammonia concentration is 1.5 to 3.5 mol ·L -1 ; liquid-solid ratio=1.0～3.0/1; temperature 293～323K; stirring time 30～120min; aging time 8～24h; Barium solution until SO 4 2- cannot be detected; obtain iron, manganese, zinc carbonate co-precipitation powder, and leaching and opening excess zinc, the main reaction is as follows: MeSO4·(NH4)2SO4·6H2O+2NH4HCO3＝Me CO3↓+2(NH4)2SO4+CO2+7H2O式中Me代表Fe、Mn、Zn；MeSO 4 ·(NH 4 ) 2 SO 4 ·6H 2 O+2NH 4 HCO 3 ＝Me CO 3 ↓+2(NH 4 ) 2 SO 4 +CO 2 +7H 2 O, where Me represents Fe, Mn, Zn; Zn SO4·(NH4)2SO4·6H2O+(i+2)NH3＝Zn(NH3)i 2++2(NH4)2SO4+2OH-+4H2OZn SO 4 ·(NH 4 ) 2 SO 4 ·6H 2 O+(i+2)NH 3 ＝Zn(NH 3 ) i 2+ +2(NH 4 ) 2 SO 4 +2OH - +4H 2 O (3).氨浸液的净化和电解(3). Purification and electrolysis of ammonia immersion solution 用锌粉置换法深度除去铁与重金属比锌正电性的杂质元素，净化条件为：锌粉用量为1～4g/L还原液，锌粉过120目筛；开启搅拌后10～60min内加入锌粉；净化时间为15～90min；净化结束后马上过滤，反应方程如下：Use the zinc powder replacement method to deeply remove impurity elements that are more electropositive than iron and heavy metals than zinc. The purification conditions are: the amount of zinc powder is 1-4g/L reducing solution, and the zinc powder passes through a 120-mesh sieve; add it within 10-60 minutes after starting the stirring Zinc powder; purification time is 15-90 minutes; filter immediately after purification, the reaction equation is as follows: 2Men++n Zn＝2Me+n Zn2+ 2Me n+ +n Zn＝2Me+n Zn 2+ n Zn2++inNH3＝n Zn(NH3)i 2+ n Zn 2+ +inNH 3 ＝n Zn(NH 3 ) i 2+ 将氨浸液的净化液在直流电作用下获得高纯电锌或锌粉，电解条件为：电极距：10～18cm；电解液成分：(NH4)2SO4 1.2～3.5mol/L，NH31.5～3.5mol/L，Zn2+10～60g/L；温度为293～333K；电流密度200～1000A/m2；槽电压2～5v；反应同时放出氧气，反应方程如下：The purification solution of ammonia immersion solution is subjected to direct current to obtain high-purity electrolytic zinc or zinc powder. The electrolysis conditions are: electrode distance: 10-18cm; electrolyte composition: (NH 4 ) 2 SO 4 1.2-3.5mol/L, NH 3 1.5～3.5mol/L, Zn 2+ 10～60g/L; temperature 293～333K; current density 200～1000A/m 2 ; cell voltage 2～5v; the reaction releases oxygen at the same time, the reaction equation is as follows: 阴极：Zn(NH3)i 2++2e＝Zn+iNH3 Cathode: Zn(NH 3 ) i 2+ +2e＝Zn+iNH 3 阳极：40H-＝O2+2H2O+4eAnode: 40H - ＝O 2 +2H 2 O+4e 2.根据权利要求1所述的铁-锌和锰-锌的分离方法，其特征在于：所述的铁、锰、锌的硫酸盐溶液指含铁、锰、锌的矿物原料的硫酸浸出液，其成分为：H2SO420～40g/L，Fe3+1～5g/L，Fe2+30～65g/L，Zn2+45～80g/L，In3+0.2～0.6g/L，Mn2+9～40g/L。2. the separation method of iron-zinc and manganese-zinc according to claim 1 is characterized in that: the vitriol solution of described iron, manganese, zinc refers to the sulfuric acid leachate of the mineral raw material containing iron, manganese, zinc, Its composition is: H 2 SO 4 20～40g/L, Fe 3+ 1～5g/L, Fe 2+ 30～65g/L, Zn 2+ 45～80g/L, In 3+ 0.2～0.6g/L , Mn 2+ 9～40g/L. 3.根据权利要求1所述的铁-锌和锰-锌的分离方法，其特征在于，步骤(2)所述的铁、锰、锌的混合复盐是FeSO4·(NH4)2SO4·6H2O、ZnSO4·(NH4)2SO4·6H2O与MnSO4·(NH4)2SO4·6H2O的混合物，其中Fe/Mn的重量百分比为2.8～4.5，锰符合软磁粉料的配比要求，Fe/Zn的重量百分比为0.6～1.5。3. The separation method of iron-zinc and manganese-zinc according to claim 1, characterized in that the mixed double salt of iron, manganese and zinc in step (2) is FeSO 4 ·(NH 4 ) 2 SO 4 · 6H 2 O, ZnSO 4 · (NH 4 ) 2 SO 4 · 6H 2 O and MnSO 4 · (NH 4 ) 2 SO 4 · 6H 2 O mixture, wherein the weight percentage of Fe/Mn is 2.8-4.5, The manganese complies with the proportion requirement of the soft magnetic powder, and the weight percentage of Fe/Zn is 0.6-1.5. 4.根据权利要求1所述的铁-锌和锰-锌的分离方法，其特征在于：步骤(3)直流电解得到的高纯电锌或锌粉的纯度≥99.995％，其中有毒元素镉、铅、砷、汞的含量≤0.0005％。4. the separation method of iron-zinc and manganese-zinc according to claim 1 is characterized in that: the purity of the high-purity electric zinc or zinc powder obtained by step (3) direct current electrolysis ≥ 99.995%, wherein toxic elements cadmium, The content of lead, arsenic and mercury ≤0.0005%.
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WO1994008057A1 (en) * 1992-09-29 1994-04-14 Metals Recycling Technologies Corp. Method for the enhanced recovery of zinc oxide
CN1101680A (en) * 1994-03-09 1995-04-19 本溪钢铁公司 Process for producing zinc oxide by ammonia immersion method
US5464596A (en) * 1992-01-15 1995-11-07 Metals Recycling Technologies Corp. Method for treating waste streams containing zinc

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