CN101974682A - Method for extracting electrolytic zinc from oxide material containing less than 20% of zinc by using waste acid in titanium white plant - Google Patents
Method for extracting electrolytic zinc from oxide material containing less than 20% of zinc by using waste acid in titanium white plant Download PDFInfo
- Publication number
- CN101974682A CN101974682A CN2010105213190A CN201010521319A CN101974682A CN 101974682 A CN101974682 A CN 101974682A CN 2010105213190 A CN2010105213190 A CN 2010105213190A CN 201010521319 A CN201010521319 A CN 201010521319A CN 101974682 A CN101974682 A CN 101974682A
- Authority
- CN
- China
- Prior art keywords
- zinc
- solution
- iron
- cadmium
- precipitate
- 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.)
- Pending
Links
Images
Classifications
-
- 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
Landscapes
- Manufacture And Refinement Of Metals (AREA)
- Electrolytic Production Of Metals (AREA)
Abstract
The invention discloses a method for producing electrolytic zinc, which comprises the following steps: (1) producing the electrolytic zinc from oxide material containing less than 20% of zinc serving as a raw material and by taking waste acid in a titanium white plant as a leaching agent, namely by using two wastes; (2) grinding the oxide material to obtain 80 to 100-mesh material and leaching zinc in the material by using the waste acid for about 3 to 4 h so as to obtain soluble zinc sulfate; (3) filtering and adding lime milk to regulate the pH value to 5.4 and hydrolyze impurities and rare metals in the solution to be separated out in the form of precipitate; (4) adding zinc powder into the solution without the impurities so that copper and cadmium in the solution perform replacement reaction to generate cooper and cadmium-containing precipitates which are commonly called 'copper and cadmium slag'; (5) separating the zinc from ferrous iron in the solution without cobalt, namely, hydrolyzing zinc sulfate in the solution by using lime milk as a precipitant to generate white zinc hydroxide precipitate; (6) filtering the zinc hydroxide precipitate, heating the obtained solution to about 70 DEG C and introducing air to oxidize the ferrous iron to ferric iron; and adding a proper amount of oxidant so as to oxidize the ferrous iron in the solution to the ferric iron and separate out the ferric iron in the form of precipitate, namely, removing iron by a 'goethite process'; (7) dissolving the precipitate by the electrolyzed solution and filtering, wherein the filter residue is used for preparing 'gypsum', the solution is subjected to impurity removal, evaporation, concentration and crystallization, the crystallization mother solution is returned to the leaching process, and the crystal is dissolved by water and used for preparing electrolyte; and (8) electrolyzing, stripping, melting and casting into a zinc ingot.
Description
Technical field:
The present invention is relevant with the method for producing electrolytic zinc from zinc content the oxidation class material below 20% with the spent acid of titanium powder plant.
Technical background:
Because the spent acid of titanium powder plant can not effectively be utilized, the method for handling mainly is to take spissated mode at present, and being about to sulfuric acid content and being about 20% spent acid, to be condensed into content be 80% the vitriol oil, returns as the leaching of ilmenite concentrate with acid again.Because content is low, the thermal value when leaching does not reach the temperature required of dissolving ilmenite concentrate, and contain the harmful element calcium and the magnesium of titanium dioxide quality product higher, thereby influence quality product.Spissated cost is higher, needs four tons of spent acid could concentrate one ton the vitriol oil, and labor condition is comparatively abominable.
At the oxidation class material below 20%,, can't use technical grade sulfuric acid to produce electrolytic zinc, as zinc content so go out of use basically owing to the restriction of production cost.And the spent acid that uses titanium powder plant is used as leaching with sulfuric acid the production of restriction titanium powder plant and the environmental issue of development is solved up hill and dale, also make zinc content obtain effective development and utilization, thereby " treatment of wastes with processes of wastes against one another, recycle " that country is advocated obtained real utilization at the oxidation class material below 20%.Make production cost reduce, under condition of market economy, manufacturing enterprise has also strengthened competitive capacity.
The content of invention:
The production technique that the purpose of this invention is to provide the environment-friendly type of a kind of " treatment of wastes with processes of wastes against one another, recycle ", promptly utilize spent acid and zinc content production technique at the oxidation class material production electrolytic zinc below 20%, reduce production costs significantly, good product quality, the production method of environmentally safe.
The present invention is achieved in that
The present invention produces the method for electrolytic zinc, comprises the steps:
1. with the spent acid of titanium powder plant as leaching agent, zinc content as raw material, promptly utilizes two useless electrolytic zincs of producing at the oxidation class material below 20%.
2. oxidation class material is levigate between 80～100 orders, with the zinc in the spent acid leaching material, the time is about 3～4 hours, makes it generate zinc sulfate soluble in water then.
3. after filtering, add milk of lime and regulate pH value to 5.4, impurity thing and rare metal hydrolysis generation precipitation in the solution are separated out.
4. will remove in the solution of impurity and add zinc powder, make copper and cadmium generation replacement(metathesis)reaction in its solution, generate the throw out of cupric, cadmium, " copper, the cadmium slag " that promptly is commonly called as.
5. need zinc is separated with ferrous iron except that the solution behind the cobalt, promptly make precipitation agent, make the zinc sulfate hydrolysis in the solution, generate the zinc hydroxide precipitation of white with milk of lime.
6. filter out the solution behind the zinc hydroxide throw out, be heated to about 70 ℃ and bubbling air, oxidation of divalent to ferric iron, is added proper amount of oxidant again, make the oxidation of divalent in the solution become ferric iron, generate precipitation and separates out i.e. " goethite process " deironing.
7. with the solution after the electrolysis throw out is dissolved, after the filtration, filter residue is used to produce " gypsum ".Evaporation concentration, crystallization are carried out in dissolving after removal of impurities, crystalline mother solution returns the leaching operation, and xln is mixed with the electrolytic solution that is fit to the electrolysis requirement with water dissolution.
8. by peeling off after the electrolysis and melting, cast zinc ingot metal.
The 1. middle zinc content of step is at the oxidation class material below 20%.
Step in 2. every 1000mL leach liquor add milk of lime (CaO dry basis) 8～20g, pH value is 5.4.
Behind 3. middle adding milk of lime of step and the sodium hydroxide, the control pH value is not more than 6.5.
The 6. middle Zinc Sulphate Heptahydrate water dissolution of step, zinc content is suitable for electrolytic zinc content at 130～150g among every 1000mL.
The present invention mainly is the production extractive technique that spent acid (content is 18%～22%) at titanium powder plant and zinc content carry out at the oxidation class material below 20%.
Technical characterstic of the present invention and advantage are as follows:
1. utilize the spent acid of titanium powder plant to use sulfuric acid, leach the zinc oxide of zinc content in the depleted oxidation class material below 20%, make it generate zinc sulfate soluble in water as leaching.Because contain more ferrous iron (being about 25%～32%) in the spent acid, ferrous iron can be used as oxygenant, has improved the leaching amount of zinc in the material, its leaching yield is about about 96%.When raw meal particle size was about 80～100 orders, about four tons with spent acid of leachings can be leached one ton of oxidation class material, and solid-to-liquid ratio is 1: 6, and extraction time is about 3～4 hours, makes leaching agent than technical grade sulfuric acid, and leaching yield has improved 1.5%.Because spent acid is to belong to source of pollution, when obtaining spent acid, need not to buy, corresponding titanium powder plant need go out the spent acid processing costs, and the high raw materials cost of corresponding also ratio content that obtains of raw material hangs down two, three times, promptly the cost of the zinc of a metal tonnage is 2500～3000 yuan/ton, make the production cost of last electrolytic zinc reduce about about 2000～2500 yuan, the utilization that has fundamentally solved the handling problem of spent acid and developed low levels oxidation material simultaneously.
Just to make so that spent acid, this pair of waste material are useless obtained effectively utilizing and developing, thereby reached the mode of production of " treatment of wastes with processes of wastes against one another, recycle " that present national industrial policies advocate.
2. adopting milk of lime to adjust pH value, remove the impurity in the leach liquor and the enrichment and the extraction of rare elements germanium and indium created advantageous conditions, is 80g/T by the germanium in the original material promptly, and indium is 100g/T.Being enriched to germanium is 500g/T, and indium is 900g/T.After enrichment repeatedly, germanium can reach 21% in the solution, and indium can reach about 44%.
Through removal of impurities, solution behind heavy germanium, the heavy indium behind zinc dust precipitation copper, cadmium, makes it generate the precipitation slag of cupric, cadmium, " copper, the cadmium slag " that promptly is commonly called as, solution through removing cobalt, is used the milk of lime depositing zinc after filtering more then, the zinc hydroxide that makes the zinc hydrolysis generate white is separated out from solution, by this sedimentary enrichment mode, just make the content of zinc use the raw material zinc content below 20% by original production, be enriched to the zinc mixed sediment of the sulfur acid calcium more than 50%.
Adopt at last " goethite process " with the oxidation of divalent in the solution to ferric iron, generation hydrated ferric oxide precipitation, after the filtration, filtrate can be returned and make to leach water, filter residue is a ferric oxide, the oven dry back promptly generates " red iron oxide " after 600～800 ℃ of temperature condition are calcined down, and the content of its ferric oxide can reach about 95%.
3. the environmental protection of whole process flow follow through is first production factors, so process using " substep complexometry ", the various metal goods and materials and the nonmetal goods and materials of leach liquor are extracted from solution step by step, use milk of lime, it is the adjustment of calcium oxide carrying out hydrolyzing and precipitating and pH value, its purpose is exactly in order to reduce the existence of water-soluble compound in the solution, to use up the meltage that increases to greatest extent in the aqueous solution and be beneficial to recycle.
Its heavy germanium, indium slag and contain the zinc mixed sediment through the acidleach after-filtration, the major ingredient of filter cake is a calcium sulfate, after the calcium sulfate oven dry, in the calcining down of 700～900 ℃ of temperature condition.Can obtain the powder calcium sulfate of iron-free, white, " terra alba " that promptly is commonly called as can be used for structure material, and this just makes the waste material that self produces change valuable a kind of commodity into, reduced to produce and used cost.
4. contain the zinc hydroxide dissolving that the solution of zinc mixed sediment after with electrolysis will be wherein at last, the solution zinc content of this moment is about 150～180g/L, through evaporation concentration, reaches about 223g/L, and crystallisation by cooling, xln are Zinc Sulphate Heptahydrate.Mother liquor after the crystallization is after whizzer filters, and mother liquor returns the leaching program, reclaims wherein zinc and rare metal, as: metallic elements such as germanium, indium, copper, cadmium.The crystalline crystal is under 5.4～5.6 the condition at pH value, dezincify can crystallization outside, other metallics especially can crystallization for the material that can damage the yin, yang pole plate when the electrolysis, still stays in the solution, promptly in " mother liquor ".After a removal of impurities and extracting various metallicses, adopt the crystalline mode to carry out the secondary removal of impurities once more, its total impurities removing efficiency can reach more than 99.8%.Zinc Sulphate Heptahydrate adds entry in proportion it is dissolved, and control is fit to electrolytic zinc amount, i.e. 130～150g/L.Carry out electrolysis, peel the electrolysis zinc metal sheet from negative plate, zinc ingot metal is cast in fusing, and the product matter of its zinc ingot metal can reach the target level of product quality of No. zero zinc ingot metal more than 98%.
Comprehensive above-mentioned said, the present invention not only makes the environmental issue of long-term puzzlement titanium powder plant spent acid obtain solving the most completely.Simultaneously, also make zinc content, obtained the most effective development and utilization at the oxidation class material below 20%.And make each ton electrolysis zinc ingot metal reduce by 2000～2500 yuan production cost, accomplished the optimum production technique pattern of " treatment of wastes with processes of wastes against one another, recycle ".Thereby make the sharp contradiction of interests problem of environmental protection problem and manufacturing enterprise obtain the most perfect solution, i.e. " environmental protection come from enterprise produce, company interest derives from environmental protection ".
The present invention has simplified production process, makes it easy handling.
Description of drawings:
Fig. 1 is a process flow sheet of the present invention.
Embodiment:
The spent acid (vitriolic content is 18～22%) that utilizes sulfuric acid method titanium pigment factory is as leaching agent, leaches metallicses such as the zinc oxide of zinc content in the oxidation class material below 20%, indium, germanium, copper, cadmium, iron.
At normal temperatures, under the velocity conditions with per minute 60～80 commentaries on classics, agitation leach.Churning time 2～3 hours is 1: 4 with the spent acid amount.Promptly containing zinc oxidation class material is 1 part, and spent acid is 4 parts, and solid-to-liquid ratio is 1: 6, is stabilized in less than below 1.0 to the pH value of infusion solution, and after prolonging time of 1 hour, just can stops to stir.Chemical equation is:
ZnO+H
2SO
4→ZnSO
4+H
2O
In
2O
3+3H
2SO
4→In
2(SO
4)
3+3H
2O
GeO+H
2SO
4→GeSO
4+H
2O
CdO+H
2SO
4→CdSO
4+H
2O
CuO+H
2SO
4→CuSO
4+H
2O
Iron mainly comes from the spent acid, contains the iron about about 15～30g in every 1000ml spent acid, and next comes from ferrous about 40% in the zinciferous oxidation class material can be by sulfuric acid dissolution.Chemical equation is:
FeO+H
2SO
4→FeSO
4+H
2O
One, heavy germanium indium and removal of impurities
Leaching is filtered after finishing, and after solid-liquid separation, adds milk of lime in through the solution after filtering, and the calcium oxide dry basis that adds in promptly every 1000m1 solution is 8～20% white lime.At normal temperatures, add milk of lime while stirring, the pH value that makes solution is by less than 1.0.After adjusting to 5.4, to solution remain on 5.4 o'clock constant, continue to stir time of 2 hours.Germanium≤0.4mg/L, indium≤5mg/L in the solution after testing, the impurity overwhelming majority of other metal object and nonmetal thing is hydrolyzed postprecipitation and comes out in the solution simultaneously, can stop to stir.
Solid-liquid separation after filtration, solids it is germanic, indium are retained and are used to extract germanium, indium or other metallic element.Chemical equation is:
GeSO
4+Ca(OH)
2→CaSO
4+Ge(OH)
2↓
In
2(SO
4)
3+3Ca(OH)
2→3CaSO
4+2In(OH)
3↓
Two, zinc powder copper removal, cadmium
The copper in the solution behind germanium, indium and the impurity, the content of cadmium are removed in detection.And 1.5 times the zinc powder that adds copper, cadmium total amount in solution is used for replacing copper, the cadmium of zinc-containing solution.Under the stirring at normal temperature condition, about 2～3 hours of time, make on copper in the solution, the system that cadmium is replaced zinc powder, form zinciferous hydration copper cadmic compound precipitation.Chemical equation is:
2ZnO+CuSO
4+H
2O→ZnSO
4+ZnO·Cu(OH)
2↓
2ZnO+CdSO
4+H
2O→ZnSO
4+ZnO·Cd(OH)
2↓
When Cu≤the 2mg/L of back in the solution after testing, Cd≤3mg/L, just can filter, throw out eliminating, " copper-cadmium slag " that the throw out of gained promptly is commonly called as.Copper in the copper-cadmium slag shared ratio in copper-cadmium slag is 1.26%, cadmium is 56.66%, zinc is 24.92%, slag is 17.14%.Have approximately in the zinc powder in 63.66% the solution in copper, cadmium and the solution exchange of free sulfate ion and in conjunction with and generated zinc sulfate soluble in water.
Copper-cadmium slag is retained, and is used for separating and extracting copper and cadmium.
Three, remove cobalt
Adopt 2-Naphthol-Sodium Nitrite mixture to remove cobalt.Take by weighing 2-Naphthol and Sodium Nitrite by the cobalt amount that contains in the leach liquor, press leach liquor 1000ml and calculate, the sodium hydroxide solution stirring and dissolving of preparation 8ml 3% is under 5.4 the situation, to remove the cobalt rate more than 90% at pH value, removes about 1～3 hour of cobalt time.
Four, the heavy zinc of milk of lime
Remove in the solution behind the cobalt, the content of zinc is about 15～30g/L, also has the above iron of 30g/L simultaneously.So need zinc is separated with iron, and zinc carried out enrichment, make the zinc content of producing in the electrolytic solution reach 130～150g/L at last.Common mode is to adopt the mode of extraction, promptly uses P
2O
4Add sulfonated kerosene zinc is extracted from solution, carry out back extraction then.But because the process of extraction is comparatively complicated, and cost is also corresponding higher, particularly in the process of Fan Cuiquing, can increase compound soluble in water in the solution, increases electrolytic kwh loss when electrolysis.So present method adopts the method for the heavy zinc of milk of lime in the precipitation enrichment process, under pH value is no more than 6.5 situation, the zinc hydrolysis in the solution is generated the zinc hydroxide throw out, and separate with iron phase in the solution.Milk of lime is calculated as 0.8～1.5 of zinc amount with dry basis CaO, and adds a certain amount of NaOH, makes the zinc in the solution generate zinc hydroxide as much as possible, and the zinc that promptly remains in the solution should not surpass 0.4g/L.Chemical equation is:
ZnSO
4+Ca(OH)
2→CaSO
4+Zn(OH)
2↓
After filtration after the oven dry, the content of depositing zinc is about 50%, and separates with the iron of the overwhelming majority, and iron-containing liquor can adopt goethite process or directly iron is precipitated out with NaOH solution, produce content in the ferric oxide powder more than 90%, i.e. " red iron oxide " by calcining process then.
Five, electrolytic solution produces
With the solution behind the intact zinc of electrolysis (the about 30～50g/L of zinc content in the liquid after its electrolysis, sulfuric acid are about 200～300g/L), and dissolving mixed precipitation zinc makes it to be separated with calcium sulfate, and chemical equation is:
CaSO
4·Zn(OH)
2+H
2SO
4→CaSO
4↓+ZnSO
4+H
2O
After solid-liquid separation, filter residue calcium sulfate can be used for producing " terra alba ", is applicable in the material of construction.Zinc content is about about 150～180g in the 1000ml solution at this moment.Because zinc is an enrichment process, thus the harmful element in the solution as: germanium, cadmium, cobalt etc. also can increase thereupon exponentially, must carry out one time the removal of impurities process again, promptly add a certain amount of milk of lime adjustment pH value in solution about 5.4.
In solution, add a spot of oxygenant---hydrogen peroxide, i.e. " hydrogen peroxide ".After wherein oxidation of divalent become ferric iron, hydrolysis was separated out.Produce post precipitation at ferric iron and can discharge the sulfate ion that equates with the iron amount, thereby reduce the pH value of solution, the pH value of solution is about about 2.0～2.5 generally speaking.So need add the milk of lime of doses again pH value is transferred to about 5.4, and is continued to stir two hours, filter then.Because the harmful element in the solution of this moment is less relatively, adopt the meaning of displacement or generation complex precipitate little again.But be not removed and can have influence on electrowinning process and cathode-anode plate is caused damage.We's rule in the favourable condition of 150～180g/L, adopts the mode of condensing crystal to make the zinc sulfate content in the solution reach the weight that every 1000ml is 1600g according to zinc content in the solution.Promptly; Zinc content is about about 223g, and calcium in the solution and magnesium also can form throw out naturally thereupon and separate out from solution.After the filtration, make the zinc sulfate crystallization generate the Zinc Sulphate Heptahydrate xln by the refrigerative mode.Other metallic elements then can be left in the mother liquor after the crystallization, can be discharged from after the whizzer high speed rotating filters.The clearance of its impurity element is 99%, and mother liquor can return to leach in the flow process and go, and reworking extracts wherein each kind of metallic element, and resulting Zinc Sulphate Heptahydrate solids can be used as the intermediate raw material use.
1. can be to dry under 40～60 ℃ of temperature condition in temperature, produce content, be used for the Zinc Sulphate Heptahydrate of feed, food, medicine and fine chemistry industry at the zinc sulfate more than 98.5%.
2. produce content at 99.7% zinc oxide by the mode of hydrolysis, be used for other chemical industries and use.
3. the solid Zinc Sulphate Heptahydrate is added a certain amount of water it is dissolved, send into electrolytic tank electrolysis behind control zinc content 130～150g/L, to produce metal zinc ingot.By the crystalline mode, the quality product of the electrolysis zinc ingot metal of producing is about more than 98% to be No. zero zinc.
Claims (6)
1. utilize spent acid to leach zinc content at the oxidation class material below 20%.
2. adopt milk of lime to calculate with the dry basis calcium oxide, the add-on of every 1000mL leach liquor is 8～20g, and the pH value of adjusting zinc lixiviating solution is 5.4, and removal of impurities also precipitates germanium, indium and impurity.
3. adopt milk of lime and add a certain amount of sodium hydroxide, be not more than at 6.5 o'clock at pH value, make the zinc hydrolysis of leach liquor produce throw out, and separate with iron in the solution, throw out is the mixed sediment of calcium sulfate and zinc hydroxide.
4. with solution after the electrolysis, the zinc hydroxide in the dissolving mixed sediment reaches the purpose that zinc and calcium sulfate are separated.
By evaporation concentration, crystalline mode with the leach liquor of zinc concentrate, crystallization, the crystalline mother solution behind the crystallisation by cooling filters with whizzer and makes itself and zinc sulfate crystal separation, thereby removes poisonous metal element and non-metallic element, mother liquor returns the leaching operation.
6. the Zinc Sulphate Heptahydrate water is dissolved to that zinc content promptly is suitable for electrolytic electrolytic zinc liquid in every 1000mL solution about 130～150g.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010105213190A CN101974682A (en) | 2010-10-27 | 2010-10-27 | Method for extracting electrolytic zinc from oxide material containing less than 20% of zinc by using waste acid in titanium white plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010105213190A CN101974682A (en) | 2010-10-27 | 2010-10-27 | Method for extracting electrolytic zinc from oxide material containing less than 20% of zinc by using waste acid in titanium white plant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101974682A true CN101974682A (en) | 2011-02-16 |
Family
ID=43574589
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010105213190A Pending CN101974682A (en) | 2010-10-27 | 2010-10-27 | Method for extracting electrolytic zinc from oxide material containing less than 20% of zinc by using waste acid in titanium white plant |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101974682A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102776384A (en) * | 2012-08-08 | 2012-11-14 | 汉源县广超有色金属综合回收有限责任公司 | Method for extracting zinc from non-ferrous metal waste residue |
| CN103588240A (en) * | 2013-11-27 | 2014-02-19 | 郴州市金贵银业股份有限公司 | Green utilization method of waste acid |
| CN106745151A (en) * | 2016-12-19 | 2017-05-31 | 唐山市斯瑞尔化工有限公司 | Waste acid containing the zinc comprehensive treatment utilization method high |
| CN107986321A (en) * | 2017-12-18 | 2018-05-04 | 东北大学 | A kind of waste water extraction zinc of iron content containing zinc and the method for preparing zinc hydroxide |
| CN108034838A (en) * | 2017-12-04 | 2018-05-15 | 中国恩菲工程技术有限公司 | Zincky waste liquor treatment process |
| CN109292831A (en) * | 2018-11-23 | 2019-02-01 | 湖南中伟新能源科技有限公司 | A kind of processing method of cobaltosic oxide production waste water |
| CN114622094A (en) * | 2022-01-18 | 2022-06-14 | 云锡文山锌铟冶炼有限公司 | Method for separating magnesium ions in zinc hydrometallurgy system |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1298037A (en) * | 1999-12-02 | 2001-06-06 | 重庆钢铁(集团)有限责任公司 | Method of preparing zinc plating solvent by utilizing waste liquid |
| CN101824542A (en) * | 2010-04-29 | 2010-09-08 | 钟超 | Comprehensive utilization method of titanium dioxide waste acid by sulfuric acid process |
-
2010
- 2010-10-27 CN CN2010105213190A patent/CN101974682A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1298037A (en) * | 1999-12-02 | 2001-06-06 | 重庆钢铁(集团)有限责任公司 | Method of preparing zinc plating solvent by utilizing waste liquid |
| CN101824542A (en) * | 2010-04-29 | 2010-09-08 | 钟超 | Comprehensive utilization method of titanium dioxide waste acid by sulfuric acid process |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102776384A (en) * | 2012-08-08 | 2012-11-14 | 汉源县广超有色金属综合回收有限责任公司 | Method for extracting zinc from non-ferrous metal waste residue |
| CN103588240A (en) * | 2013-11-27 | 2014-02-19 | 郴州市金贵银业股份有限公司 | Green utilization method of waste acid |
| CN103588240B (en) * | 2013-11-27 | 2016-02-10 | 郴州市金贵银业股份有限公司 | A kind of green utilization method of dirty acid |
| CN106745151A (en) * | 2016-12-19 | 2017-05-31 | 唐山市斯瑞尔化工有限公司 | Waste acid containing the zinc comprehensive treatment utilization method high |
| CN106745151B (en) * | 2016-12-19 | 2019-01-29 | 唐山市斯瑞尔化工有限公司 | High waste acid containing the zinc comprehensive treatment utilization method |
| CN108034838A (en) * | 2017-12-04 | 2018-05-15 | 中国恩菲工程技术有限公司 | Zincky waste liquor treatment process |
| CN107986321A (en) * | 2017-12-18 | 2018-05-04 | 东北大学 | A kind of waste water extraction zinc of iron content containing zinc and the method for preparing zinc hydroxide |
| CN109292831A (en) * | 2018-11-23 | 2019-02-01 | 湖南中伟新能源科技有限公司 | A kind of processing method of cobaltosic oxide production waste water |
| CN114622094A (en) * | 2022-01-18 | 2022-06-14 | 云锡文山锌铟冶炼有限公司 | Method for separating magnesium ions in zinc hydrometallurgy system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101643243B (en) | Method for recycling copper, nickel, chromium, zinc and iron from plating sludge | |
| CN106893877B (en) | A method of extracting vanadium chromium from vanadium chromic acid mixed salt solution | |
| CN100402676C (en) | Method for recovering valuable metals from electroplating sludge | |
| CN101974682A (en) | Method for extracting electrolytic zinc from oxide material containing less than 20% of zinc by using waste acid in titanium white plant | |
| CN101209853B (en) | Method for preparing cupric sulfate from spongy copper and copper-containing acid pickle | |
| CN107324303B (en) | Method for separating refined iron and chromium from multi-metal hazardous waste | |
| CN108570557B (en) | Method for separating iron, chromium, nickel, copper and zinc from high-iron high-chromium electroplating sludge leachate | |
| CN102851693A (en) | Technology for recovering production of electrolytic copper and zinc from smelting ash | |
| CN102876887B (en) | Method for comprehensively recycling metal from laterite-nickel ore leaching agent | |
| CN104593598A (en) | Method for resource utilization of multiple metals in electroplating sludge | |
| CN104480325A (en) | Method for extracting cobalt from cobalt-containing raw material | |
| CN112708777B (en) | Method for recovering zinc sulfate from zinc-containing waste | |
| CN115140777B (en) | Method for producing ferromanganese composite material for soft magnetic by utilizing ocean manganese nodule | |
| CN108570555A (en) | A method of directly producing LITHIUM BATTERY nickel sulfate from nickel cobalt enriched substance | |
| CN105567983A (en) | Soot treatment process in copper smelting process | |
| CN103757260B (en) | Treatment method of nickel-containing eluvial ores | |
| CN102925701A (en) | Method using wet alkaline process of cobalt-nickel (Co-Ni) residue containing arsenic to prepare arsenate | |
| CN106521555B (en) | A kind of method of antimony electrolyte selectivity iron removaling | |
| CN108754158A (en) | A kind of method of copper-contained sludge production cupric sulfate purified | |
| CN113955775B (en) | Method for extracting lithium carbonate from lithium-rich clay by acid-base combined method | |
| CN103484694A (en) | Method for extracting bismuth from copper-bismuth concentrate | |
| CN103014346A (en) | Process method for separating zinc, iron and cobalt and nickel ore concentrates from cobalt and nickel slag | |
| CN101987733B (en) | Method for separating potassium and rubidium from lepidolite processing fluid | |
| CN112853101B (en) | Electroplating sludge recycling treatment method | |
| CN101693554A (en) | Method for extracting vanadium pentoxide from stone coal ores |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| DD01 | Delivery of document by public notice |
Addressee: Xu Luecheng Document name: the First Notification of an Office Action |
|
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20110216 |