CN101270415A - Method for recycling noble metal from battery slag containing Co, Ni, Mn - Google Patents
Method for recycling noble metal from battery slag containing Co, Ni, Mn Download PDFInfo
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- CN101270415A CN101270415A CNA2007103081547A CN200710308154A CN101270415A CN 101270415 A CN101270415 A CN 101270415A CN A2007103081547 A CNA2007103081547 A CN A2007103081547A CN 200710308154 A CN200710308154 A CN 200710308154A CN 101270415 A CN101270415 A CN 101270415A
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- 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
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/006—Wet processes
- C22B7/007—Wet processes by acid leaching
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- 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
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- 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
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
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- 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
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/10—Hydrochloric acid, other halogenated acids or salts thereof
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- 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
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
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- 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
- C22B47/00—Obtaining manganese
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- 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
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- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/84—Recycling of batteries or fuel cells
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Abstract
A method for recovering Co, Ni, Mn and other valuable metal from lithium battery slag from ternary system Li metallic salt; the method comprises: stirring to dip out the lithium battery slag of lithium acid metallic salt comprising equal Co, Ni and Mn by diluted hydrochloride with hydrochloric acid concentration above 250g/l, or heating to 65-80 DEG C. and stirring to dip out by diluted sulfate with sulfate concentration above 200g/l, extracting the solvent of the leaching solution by acidic extractant to extract about 100% of Mn and Co metal so as to generate the liquid containing the metal and recover the corresponding metal from the liquid.
Description
Technical field
The present invention relates to from the lithium cell slag that contains Co, Ni, Mn, reclaim the method for precious metal.What is called contains the lithium cell slag of Co, Ni, Mn, being meant the slurry like material that the solvent by three component system Li metal-salt and carbon, N-N-methyl-2-2-pyrrolidone N-(N-methyl-2-pyrrolidone), polyvinyl alcohol (polyvinyl alcohol) etc. constitutes, is the dregs that produce in lithium secondary battery manufacturing process.The processing of metal acid lithium that contains precious metal in these battery slags is very important from the viewpoint that precious metal reclaims.
Background technology
Patent documentation 1: the spy opens flat 6-251805 communique, when it is applied for to put down into 5 years lithium secondary batteries also untapped, but before exploitation, prepare with regard to the recirculation to lithium secondary battery.In the method, cut off waste lithium cell, will be divided into battery separator (separator), current collector and anodal material by filtration isolated solid area from liquid with jet (water jet).And illustrate that these have carried out fusion or pulverizing utilizes according to material again.Also have, the metal of the metal oxide that uses as anodal material can be enumerated multiple metals such as Ni, Co, Ti, Fe, V, Mn, Mo, Cr, W, but these metals all do not use, and the most usually metal is Co now.
Patent documentation 2: the spy opens the 2006-331707 communique, the lithium cell recirculation method that proposition was made of a plurality of stages, stage before and after positive electrode material reclaims, mechanically separate coiling body, positive pole, negative pole and battery separator, positive pole is immersed in the aqueous nitric acid, separate anodal base material (aluminium) and positive active material, positive active material is immersed in makes it dissolving in the hydrochloric acid soln, obtain the metallic ion mixed liquor of Li, Ni etc. by filtering solution.Then use the method for ion-exchange, electrolysis, precipitate and separate etc., from this mixing solutions, reclaim each metal.
Patent documentation 3: No. 3450684 communique of patent is that lithium secondary battery is equipped on the application in 9 years put down on the various electronicss, wherein proposes to reclaim from the positive active material of waste lithium cell the method for Mo, Co, Ni, Sn etc.Specifically, waste lithium cell is disintegrated, and be with iron-clad roasting together, to calcining matter implement to pulverize, 1 magnetic separation, and nonmagnetics implemented 2 magnetic separation.
Recently, the exploitation that will contain the technology that the lithium acid metal salt of Co, the Ni of equivalent roughly and Mn uses as positive active material is being carried out.For example, patent documentation 4: the spy opens the 2007-48692 communique, be with Ni: Mn: the Co ratio is 1: 1: 1, Li: (Ni, Mn, Co) is than the mode that is 1.06: 1, weighing Manganse Dioxide, cobalt oxide, nickel oxide and Quilonum Retard, these compounds are mixed with polyvinyl alcohol solution, carry out granulation, drying thereafter, burn till.This is burnt till three component system metal Li composite oxides and caking agent and solvent, modulation pulpous state positive active material.
The positive active material of nickel-Hydrogenized compound battery is hydroxy nickel oxide (NiOOH), is not the lithium acid metal as the positive active material of lithium cell.About reclaiming the method for metal from nickel-Hydrogenized compound battery, patent documentation 5: the flat 10-510878 communique of special table proposes to have following method.That is, (1) with jet with the refuse battery fragmentation; (2) chip that obtains by magnetic separation separates Fe, Ni; (3) use the sulfuric acid dissolution nonmagnetic substance; (4) adjust separation Fe by pH; (5) filtrate of having separated Fe is after filtration carried out organic solvent extraction, extract Zn, Cd, Mn, Al thus.
[patent documentation 1] spy opens flat 6-251805 communique
[patent documentation 2] spy opens the 2006-331707 communique
No. 3450684 communique of [patent documentation 3] special permission
[patent documentation 4] spy opens the 2007-48692 communique
The flat 10-510878 communique of [patent documentation 5] special table
[non-patent literature 1] " resource and material ", 1997,12, Vol.113, the big special collection of recirculation number, the 941st page
The Metallkunde in [non-patent literature 2] lecture modern times, a refining piece of writing 2, non-ferrous metal are smelted, and clear and on July 10th, 57, Metallkunde can be published the 240th～241 page
Summary of the invention
In the recirculation of battery, have such as the method for patent documentation 3 and 5 so direct recirculation batteries with as what patent documentation 1 and 2 proposed battery is decomposed into each structural member or material and the method that reclaimed.The present invention is the recirculation method of the pulpous state battery slag that produces from battery manufacturing process, does not belong to any among them.
The objective of the invention is to, a kind of method that reclaims valuable metal from the battery slag of lithium cell from three component system Li metal-salt is provided.
The present invention proposes a kind of from containing Co, Ni, reclaim the method for precious metal in the refuse battery slag of Mn, it is characterized in that, to comprise and contain the roughly Co of equivalent, the useless lithium cell slag of the lithium acid metal salt of Ni and Mn (hereinafter referred to as " three component system Li metal-salt "), hydrochloric acid soln agitation leach with the concentration more than the 250g/l, perhaps the sulphuric acid soln with the concentration more than the 200g/l carries out heated and stirred leaching processing, carry out solvent extraction with acidic extractant for leach liquor, extraction Mn, among Co and the Ni roughly 100% of these 2 kinds of metals of Mn and Co, generation contains the solution of metal separately, reclaims this metal from these solution.
Below, explain the present invention.
Battery slag is the slurry like material that the solvent by three component system Li metal-salt and carbon, N-N-methyl-2-2-pyrrolidone N-(N-methyl-2-pyrrolidone), polyvinyl alcohol (polyvinyl alcohol) etc. constitutes, and is the dregs that produce after lithium secondary battery manufacturing process.Its metal group becomes 10～12 quality %Co, 10～12 quality %Ni, 10～12 quality %Mn.
Present inventors are by the battery slag of following condition leaching three component system Li metal-salt, and its results verification is effective to whole leaching of three component system metal to sulfuric acid and hydrochloric acid.
(A) battery slag: 200g.
(B) leach liquor: the various acid of the concentration shown in the table 1, capacity 2000mL.
(C) extraction time: 4h～8h
(D) temperature: normal temperature or be heated to 70～80 ℃.
(E) stir: have.
The result of test is presented in the table 1.
[table 1]
Leaching is known as below about three component system Li metal.
(1),, but needs evaporation vitriolic treating plant etc. even temperature also can leach more than 80 ℃ if, then just can make all leachings of 100% of Co, Ni, Mn with the 200g/l aqueous sulfuric acid while heated agitation leach 8 hours with 70～80 ℃.In addition, if use the 300g/l aqueous sulfuric acid, then can obtain leaching the same leaching yield with the sulfuric acid that under 65～75 ℃, carried out 8 hours.
(2) in the leaching of only stirring, if with the aqueous hydrochloric acid of the above concentration of 250g/l, then the leaching yield of Co, Ni, Mn all is 100%.
As above, if the aqueous sulfuric acid of the concentration more than the 200g/l heats leaching, then can access 100% leaching yield.
Secondly, for a leaching of only stirring, if, then can access 100% leaching yield with the aqueous hydrochloric acid of the concentration more than the 250g/l.
Also have, why leaching yield is roughly 100% in the present invention, is the error of adding weighing because of this regulation, and usually in monthly output, recirculation is ± 1% during battery slag more than 100 tons.The leach liquor that the result who leaches generates contains the three component system metal ion, and residue mainly is made of the carbon of organic or inorganic state.This carbon is insoluble in sulfuric acid and hydrochloric acid, can be residual as solids, but because carbon etc. do not have the value of recovery, so the residue after leaching goes out of use.
Stir so that the mode that the pulpous state battery slag is dispersed in the leach liquor is equably undertaken by the arbitrary method of rotating paddle etc.
After Co, the Ni that in reclaiming leaching back liquid, is contained, the Mn, these two kinds of metals of solvent extraction Co, Mn, Ni is separated.As it is carried out solvent-extracted extraction agent, can use for example non-patent literature 1: resource and material, 1997,12, Vol.113, " the big special collection of recirculation number ", and the 941st page, by the acidic extractant of table 1 bulletin.
As the Mn extraction agent, preferably use the system D2EHPA of LANXESS society, in addition as the Co extraction agent, preferably use the big system PC-88A of eight KCCs.D2EHPA is two (2-ethylhexyl) phosphoric acid (di-2-ethylhexyl), the known Mn extraction agent by non-patent literature 1.PC-88A is 2-ethylhexyl phosphoric acid single 2-ethyl polyhexamethylene system [(2-ethylhexyl) 2-ethylhexylphosphonate]], this information from
Http:// www/daihachi-chem.co.jp/sehin/pdf/kinz.pdfCan obtain.
About from extract back solution, reclaiming the method for metal,, can be to sell outward as the auxiliary material of existing or known wet type refining procedure as following.
Co: the electroextraction of chlorination Co.
Mn: the electroextraction of sulfuric acid Mn.
Ni: the Ni electrolytic process of utilizing chlorine to leach.
As the additive method of the recovery of metal, that can also adopt has by at the sulfuric acid solution of solvent extraction post neutralization as counterextraction liquid, makes metal salt precipitate thus, by filtering the method that reclaims metal-salt as solids component.Then, this metal-salt also can be sold to refining of metal enterprise outward as raw metal.Perhaps, make that the concentration in the liquid concentrates several times after the concentration ratio solvent extraction of metal-salt, reclaim by extraction thereafter, so, then the regenerated metal that is recovered to from battery slag can accomplish without any letup and circulate.The electrowinning of Ni, Co, Mn, for example can be with non-patent literature 2: the Metallkunde in lecture modern times, a refining piece of writing 2, non-ferrous metal is smelted, and clear and on July 10th, 57, Metallkunde can be published, and the 240th～241 page of described condition carried out.
Next, specifically describe with reference to Fig. 1 and to utilize D2EHPA and PC-88A, respectively the method for solvent extraction Mn and Co.
The extraction of Mn
Mix with kerosene (kerosene) mixed solution (A solvent) and the Co-Ni-Mn solution (promptly leaching back liquid) of the branch liquid bath of being with pipeline flow visor (sight flow) and stirrer, carry out solvent extraction with reference to Fig. 1 with D2EHPA.Adding caustic soda is 2～3 with pH regulator.
, again utilize the extraction of solvent, thus, only stay Co-Ni in the solution thereafter.The A solvent flows become in the other direction with solution on, extracts 3, extracts 2, extracts 1 (extraction of adverse current multistage), and Co concentration is step-down gradually, then uses 10g/l H
2SO
4Clean Co (cleaning 1).
Then, carry out counterextraction, in aqueous sulfuric acid, make Mn concentrate (" Mn solution ") with the 50g/l aqueous sulfuric acid.Counterextraction divides 2 sections to carry out, and the A solvent utilizes in extraction 3 again.In Mn solution, add caustic soda and neutralize, liquid after the neutralization and precipitation are implemented to filter, with Mn (OH)
2Mode reclaim Mn.Scavenging solution is added in the preceding Co-Ni-Mn solution of extraction.
The extraction of Co
At extraction agent is different with the extraction of Mn on the PC-88A this point, and other treatment schemees are identical with Fig. 1.Therefore, Fig. 1 " Co-Ni-Mn solution ", " Mn solution " reach that " Co-Ni solution " is replaced by " Co-Ni solution " respectively, " Co solution " reaches " Ni solution ".
Co, the Ni, the general scope of Mn concentration and the concentration of embodiment that obtain by above-mentioned solvent extraction are presented in the table 2.Metal is by neutralizing respectively with Mn (OH)
2, Co (OH)
2, NiCO
3Mode reclaim.
[table 2]
| Co concentration (g/l) | Ni concentration (g/l) | Mn concentration (g/l) | |
| Mn contains solution | ＜0.01 | ＜0.01 | 44 |
| Co contains solution | 35 | ＜0.01 | ＜0.01 |
| Ni contains solution | ＜0.01 | 7.8 | ＜0.01 |
Preferred implementation of the present invention from the above is as follows.
(1) method of acid solvent extraction Mn and Co.
(2) pH by the solution behind the adjustment counterextraction makes Mn, Co, Ni precipitation, by filtering the method as the solids component separating metal.
(3) solid metal is dissolved in again the method for (2) of electrolytic solution and electrowinning.
The effect of invention
(1) because can be positive active material, so do not need to be used to make the useless solidified energy of lithium cell slag with slurry condition recirculation three component system metal Li salt.In addition, because the three component system metal Li salt in the slurries is the micropartical state, thus big with the contact area of leach liquor, the leaching efficiency height.
(2) Co, Ni and Mn can all leach respectively.On the other hand, the carbon beyond it etc. becomes residue, with described three kinds of metal separation.Because solvent extraction is only carried out 2 times, so operation can be very not long.
(3) because use dilute sulphuric acid or dilute hydrochloric acid, so little to the burden of environment.
(4) though Li is dissolved in leach liquor, by solid-liquid separation can with metal separation (the Ni post precipitation being remained in the solution) from Ni solution.Separate Mn, Co in solvent extraction after, though Li is present in the Ni solution, make the Ni post precipitation, Li remains in the filtrate and is separated.Perhaps, if make the Ni solution concentration become the electrolytic solution time spent to carry out solvent extraction, then Li is not extracted, but remains in the solution separated.Li is separated in a word.
(5) as the positive active material of the battery of electronics, use the Co based compound, also use new ternary prime system metal Li salt, two aspects all are considered to fully to continue to be in the state of listing.The material that also can comprise in this case, Co system in the lithium cell slag.So, many even the kind of battery becomes, go out but carry out acidleach according to the present invention, carry out solvent extraction thereafter, still can reclaim precious metal.
Description of drawings
Fig. 1 is the schema of the solvent extraction step of expression Mn.
Embodiment
100kg leaches and solvent extraction for the paste that contains three component system metal Li salt (Co 11%, Ni 11%, Mn 11%, below only be called " paste ").In the test of following explanation, the counterextraction time cleaned and was undertaken by stirring 10 minutes for stirring 10 minutes in order to stir 10 minutes the extraction time.
(1) leaches
In 300g/l aqueous sulfuric acid 1000L, drop into paste, Yi Bian with 70～80 ℃ of heating, Yi Bian stirred 4 hours, filter thereafter, so at the residual residue that 10kg is arranged of dried state.Metal concentration in the filtrate of 1000L is as shown in the table, leaching that can 100%.
[table 3]
| Filtrate | Co | Ni | Mn |
| Concentration (g/L) | 11 | 11 | 11 |
| Partition ratio (%) | 100.0 | 100.0 | 100.0 |
(2) Mn extraction
With 25%NaOH solution in the filtrate and after, carry out the solvent extraction of Mn.Solution after the neutralization is 1290L.Solvent extraction agent is with the kerosin 1290L of the system D2EHPA of LANXESS society, with its with neutralization after solution stirring, be adjusted to pH=2.5 (O/A ratio=1/1) with 25%NaOH solution.Solvent-extracted result is to obtain Mn extraction liquid 1290L and Co-Ni solution 1340L.Utilize 10g/lH
2SO
4Clean Mn extraction liquid (containing a little Co), then carry out counterextraction, in aqueous sulfuric acid, make Mn concentrate (Mn solution) with the 50g/l aqueous sulfuric acid.Obtain Co-Ni solution 1290L (metal concentration is presented in the table 4) and Mn solution 250L (metal concentration is presented in the table 5).
[table 4]
| Extraction liquid | Co | Ni | Mn |
| Concentration (g/L) | 8.0 | 8.1 | 0 |
| Partition ratio (%) | 98 | 99 | 0 |
[table 5]
| Solution | Co | Ni | Mn |
| Concentration (g/L) | 0 | 0 | 44 |
| Partition ratio (%) | 0 | 0 | 99 |
Co shown in the his-and-hers watches 4, Ni solution carry out the solvent extraction of Co.Solvent extraction agent adopts the kerosin 1290L of the system PC-88A of big eight KCCs, with its with neutralization after solution stirring, be adjusted to pH=4.2 (O/A compares=1/1) with 25%NaOH solution.Solvent-extracted result is to obtain Co extraction liquid 1340L and Ni solution 1390L.Utilize 10g/l H
2SO
4Clean Co extraction liquid (containing a little Ni), then carry out counterextraction, in aqueous sulfuric acid, make Co concentrate (Co solution) with the 50g/l aqueous sulfuric acid.Obtain Ni solution 1390L (metal concentration is presented in the table 6) and Co solution 250L (metal concentration is presented in the table 7).
[table 6]
| Scavenging solution | Co | Ni | Mn |
| Concentration (g/L) | 0 | 7.8 | 0 |
| Partition ratio (%) | 0 | 98 | 0 |
[table 7]
| Extraction liquid | Co | Ni | Mn |
| Concentration (g/L) | 43 | 0 | 0 |
| Partition ratio (%) | 98 | 0 | 0 |
As implied above, can all separate Mn, Co, Ni.Also have, though the example that leaches for sulfuric acid is illustrated, owing to also can leach whole metals by the hydrochloric acid leaching, therefore solvent extraction thereafter is identical result.
[utilizing on the industry possibility]
Because be existing recirculation method take ternary system metal Li salt as the battery slag of positive active material, so although can in the warehouse, take care of etc., if according to the inventive method, with sulfuric acid or Leaching in Hydrochloric Acid battery slag, then can carry out the recovery of noble metal. In addition, adopting solvent extraction in the inventive method, therefore, is that positive active material is also no problem even for example sneak into Co in battery slag, still can reclaim noble metal, therefore is easy to carrying out of the cause that recycles.
Claims (4)
1. method that from the battery slag that contains Co, Ni, Mn, reclaims precious metal, it is characterized in that, the lithium cell slag of the lithium acid metal salt that comprises the Co, the Ni that contain equivalent roughly and Mn is carried out agitation leach with the hydrochloric acid soln of the concentration more than the 250g/l, perhaps the sulphuric acid soln with the above concentration of 200g/l carries out heated and stirred leaching processing, with acidic extractant leach liquor is carried out solvent extraction, extract roughly 100% of Mn and Co, generation contains the solution of metal separately, reclaims this metal from these solution.
2. the method that reclaims precious metal from the battery slag that contains Co, Ni, Mn according to claim 1 is characterized in that, by acidic extractant solvent extraction Mn and Co.
3. the method that reclaims precious metal from the battery slag that contains Co, Ni, Mn according to claim 2 is characterized in that, adjusts by the pH that carries out after the solvent extraction, makes Mn, Co, Ni precipitation, and filters, and thus, reclaims as solids component.
4. the method that reclaims precious metal from the battery slag that contains Co, Ni, Mn according to claim 3 is characterized in that, described solids component is dissolved in the electrolytic solution again, carries out electrowinning.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2007-074089 | 2007-03-22 | ||
| JP2007074089A JP4388091B2 (en) | 2007-03-22 | 2007-03-22 | Noble metal recovery method from Co, Ni, Mn containing battery |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101270415A true CN101270415A (en) | 2008-09-24 |
Family
ID=39904678
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2007103081547A Pending CN101270415A (en) | 2007-03-22 | 2007-12-29 | Method for recycling noble metal from battery slag containing Co, Ni, Mn |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JP4388091B2 (en) |
| KR (1) | KR100930453B1 (en) |
| CN (1) | CN101270415A (en) |
| TW (1) | TW200840115A (en) |
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| CN101603126B (en) * | 2009-07-08 | 2010-11-10 | 中南大学 | Process for efficiently leaching anode active material of waste lithium battery |
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| CN102347521A (en) * | 2011-10-08 | 2012-02-08 | 佛山市邦普循环科技有限公司 | Method for recycling manganese and lithium from power type lithium manganate battery for electric automobile |
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| CN106684489A (en) * | 2017-03-24 | 2017-05-17 | 赣南师范大学 | Method for recycling valuable metal from waste polybasic lithium ion batteries |
| CN107946688A (en) * | 2017-12-16 | 2018-04-20 | 淄博国利新电源科技有限公司 | The method that lithium is recycled from discarded ternary lithium ion battery |
| CN111293286A (en) * | 2018-12-07 | 2020-06-16 | 湖南杉杉新能源有限公司 | Coating modified lithium ion battery anode material and preparation method thereof |
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| JP4865745B2 (en) * | 2008-02-13 | 2012-02-01 | Ｊｘ日鉱日石金属株式会社 | Method for recovering valuable metals from lithium batteries containing Co, Ni, Mn |
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| DE4445496A1 (en) * | 1994-12-20 | 1996-06-27 | Varta Batterie | Process for the recovery of metals from used nickel-metal hydride accumulators |
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- 2007-12-21 KR KR20070135280A patent/KR100930453B1/en active IP Right Grant
- 2007-12-29 CN CNA2007103081547A patent/CN101270415A/en active Pending
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Also Published As
| Publication number | Publication date |
|---|---|
| KR20080086339A (en) | 2008-09-25 |
| KR100930453B1 (en) | 2009-12-08 |
| TW200840115A (en) | 2008-10-01 |
| JP4388091B2 (en) | 2009-12-24 |
| TWI369800B (en) | 2012-08-01 |
| JP2008231522A (en) | 2008-10-02 |
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