CN104271781A - Processing of lithium containing material - Google Patents
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- CN104271781A CN104271781A CN201380003136.1A CN201380003136A CN104271781A CN 104271781 A CN104271781 A CN 104271781A CN 201380003136 A CN201380003136 A CN 201380003136A CN 104271781 A CN104271781 A CN 104271781A
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/14—Alkali metal compounds
- C25B1/16—Hydroxides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D15/00—Lithium compounds
- C01D15/02—Oxides; Hydroxides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D15/00—Lithium compounds
- C01D15/04—Halides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D15/00—Lithium compounds
- C01D15/08—Carbonates; Bicarbonates
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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
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/16—Sintering; Agglomerating
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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
- C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
- C22B26/10—Obtaining alkali metals
- C22B26/12—Obtaining lithium
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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
- C22B3/42—Treatment or purification of solutions, e.g. obtained by leaching by ion-exchange extraction
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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
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical 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
- C22B4/00—Electrothermal treatment of ores or metallurgical products for obtaining metals or alloys
- C22B4/02—Light metals
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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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Abstract
A process (10) for the treatment of a lithium containing material, the process comprising the steps of: (i) Preparing a process solution from the lithium containing material (12); (ii) Passing the process solution from step (i) to a series of impurity removal steps (36) thereby providing a substantially purified lithium chloride solution; and (iii) Passing the purified lithium chloride solution of step (ii) to an electrolysis step (70) thereby producing a lithium hydroxide solution.
Description
Technical field
The present invention relates to the process of lithium-containing materials.
More specifically, the present invention relates to the technique that lithium-containing materials process and lithium hydroxide and Quilonum Retard are produced.This technique is to by triphane ore deposit or concentrate, or the lithium chloride solution that bittern obtains carries out electrolysis.On the whole, technique of the present invention its objective is the lithium hydroxide and Quilonum Retard product that provide a kind of high purity or cell-grade.
Technique of the present invention can provide a kind of hydrochloric acid product further.Further, on the whole, technique of the present invention have employed mixed metal oxide (MMO) electrode containing precious metal, thus improves the efficiency of the electrochemistry link of this technique.
Background technology
Generally α-triphane ore deposit or concentrate are heat-treated from containing the existing technique of producing Quilonum Retard lithium ore deposit or concentrate.This thermal treatment can be referred to as decrepitation method and α-triphane can be converted into β-triphane, β-triphane and then can by acid fluid dissolves.The step that β-triphane dissolves in acid solution is carried out and is generated dissolubility lithium salts in kiln.This lithium salts is transported to one or more container, and in these containers, described lithium salts is purified.The thick lithium salts leached then enters into the step of pH value regulating slurry, thus makes specific impurity ,-comprise iron and magnesium-by precipitated precipitation.Like this, the lithium salts after purification can carry out processing to produce Quilonum Retard with sodium carbonate.This Quilonum Retard can and then carry out processing to generate lithium hydroxide with slaked lime.
The technique of producing Quilonum Retard and lithium hydroxide from bittern generally comprises and adopts evaporation tank to the concentration of the salt increasing it and comprise, and then reduces foreign matter content by series of steps again.
Above-mentioned technique of the prior art efficiency in removing the impurity existed in leach liquor is relatively low, and this can produce the lower lithium hydroxide of purity and Quilonum Retard product by causing.
Thus, the target of technique of the present invention overcomes problem existing in one or more prior aries mentioned above, or at least provides a kind of useful prior art replacement scheme.
The object be above introduced background technology is only conveniently to understand the present invention.Above-mentioned introduction and do not mean that show or admit above any material of mentioning when the priority date of the application, belong to the part of common practise.
In the specification sheets and claims of the application, the meaning that term " comprises " should be understood to contain a listed things or one group of things, but do not get rid of other one or one group of things any, but based on context separately do except other explains to " comprising " needs.
Term " battery-level lithium carbonate " refers to the product of the purity with about 99.5% or higher.Similar, term " cell-grade lithium hydroxide " refers to the product of the purity with about 99% or higher.
Summary of the invention
According to the present invention, provide a kind of technique for lithium-containing materials process, this technique comprises the following steps:
(1) with described lithium-containing materials preparation technology liquid;
(2) process liquor making step (1) generate enters a series of removal of impurity step, thus generates the lithium chloride solution of purifying substantially; And
(3) lithium chloride solution of the purifying making step (2) generate enters electrolysis step, thus generates lithium hydroxide solution.
As a scheme of the present invention, with the process liquor of the form preparation process (1) of leach liquor.Preferably, enter leaching step by making lithium-containing materials and form described leach liquor, described in this leaching step, material is leached by hydrochloric acid.
Preferably, comprise further as the removal of impurity step of step (2) and make leach liquor be concentrated to lithium chloride close to saturated enrichment step.
The lithium hydroxide solution generated in step (3) can by water evaporates thickening to generate Lithium Hydroxide Monohydrate crystal.
And then the lithium hydroxide solution generated in step (3) can be carbonized by making compression arbon dioxide enter this solution, thus generate Quilonum Retard precipitation.
As a scheme of the present invention, described lithium-containing materials is α-triphane ore deposit or concentrate, and described technique comprises further: first α described in calcination-triphane ore deposit or concentrate are to generate the step of β-triphane.In another scheme of the present invention, described lithium-containing materials is containing lithium bittern.
As another scheme of the present invention, a part for the lithium hydroxide solution generated in step (3) carrys out thickening to generate Lithium Hydroxide Monohydrate crystal by evaporation/crystallization, and its another part is carbonized by making compression arbon dioxide enter this solution, thus generate Quilonum Retard precipitation.
Preferably, the removal of impurity step of step (2) comprises the muriatic one or many pyrohydrolysis of Al and Fe, increases pH value to make Al, the precipitation of hydroxide of Fe, Mg and Mn, and precipitation Quilonum Retard is to remove Ca, and fractional crystallization is to remove Na and K.
Further preferably, the described fractional crystallization of removing Na and K is carried out immediately after described enrichment step.
Described removal of impurity step preferably further comprises ion-exchange step.Preferably, the calcium existed in leach liquor, magnesium and other polyvalent cation are removed all by described ion-exchange step substantially.Further preferably, described polyvalent cation is removed to the level lower than about 10 ppm.
Preferred further, the moisture content be evaporated from solution in evaporation/crystallization is recompressed slightly, with supply vapor mixing and for evaporation/crystallization.Described evaporation/crystallization step preferably adopts vacuum evaporation crystallizer.
Preferably, described β-triphane was first cooled and grinds before described leaching step.Preferably described β-triphane is milled to lower than about 300 μm.Further preferably, described β-triphane is milled to the granularity of about 75 μm is P
80.
Preferably, described leaching step is at high temperature carried out.
Preferably, the hydrochloric acid soln adopted in described leaching step is about 20% HCl w/w.
Further preferably, the described high temperature leaching step is approximately the boiling point of the hydrochloric acid soln adopted in this leaching step.
Described leaching step is preferably carried out at ambient pressure.
In a scheme of the present invention, the time stopped in the chlorination kiln of about 108 DEG C about 6 to 10 hours performs described leaching step.Preferably, this residence time is about 8 hours.
Accompanying drawing explanation
For exemplary object, below with reference to an embodiment and accompanying drawing, technique of the present invention is described, wherein
Fig. 1 is the schematic flow sheet describing lithium-containing materials treatment process according to an embodiment of the invention, and wherein said lithium-containing materials is α-triphane concentrate.
Embodiment
Fig. 1 shows lithium-containing materials treatment process 10 according to an embodiment of the invention, and described lithium-containing materials provides with the form of α-triphane concentrate in this embodiment.
The whole flow elements existed in this technique 10 all perform under the condition with whole process Instrumentation and Control.
α-triphane concentrate 12 enters calcining step, in this step described concentrate 12 in incinerator 14 about 1050 DEG C to 1100 DEG C between temperature under be converted into by calcination so that by α-triphane can for the β-triphane leached.Waste gas from incinerator is conducted through swirler (not shown) and electrostatic precipitator (not shown) meets known environmental emission standard to make it.The hot calcine obtained enters water cooler 16 and is directly cooled to about 80 DEG C.Then, in shredder, such as dry grinded in closed-circuit ball mill 18 (dry-milled), to being less than 300 μm, the granularity such as reaching about 75 μm is P80.
After being stored in surge bunker (not shown), polished β-triphane mixes mutually with the 20% hydrochloric acid w/w 20 with at least 40-300% stoichiometric excess amount (stoichiometric excess) in pulping stage.Described pulping stage such as, for leaching step, leach circuit 22 feed, and described leach circuit comprises the first leaching level 24 and second and leaches level 26.
Described leaching step performs the duration of about 6 to 12 hours in consecutive batch extractor at about 108 DEG C, and such as about 8 hours, this temperature was the boiling point of the hydrochloric acid leachate added in pulping stage.In described leach circuit 22, have employed the pulp density of about 40% thus maximize leaching concentration and the solid solubility ensureing not exceed Quilonum Retard in leaching process.Waste gas can be purified in wet scrubber (not shown).Described leaching step 22 generates slag slurry and process liquor, such as leach liquor.Lithium in β-triphane and silico-aluminate are leached in the solution with other impurity, thus the sub-saturated forming Quilonum Retard in leach liquor concentrates.
Make the leach liquor from leach circuit 22 enter thickening loop 28, described thickening loop preferably includes two-stage 28a and 28b, connects with the two-stage 24 and 26 of leach circuit 22.Overflow from thickening loop 28 is directed to pyrohydrolysis step 30, and this step performs at about 300 DEG C, and the muriate of Al and Fe existed in leach liquor described in this step is converted into their respective insolubility oxide compounds 32.All residual HCl are also being separated in HCl step 34 again.
Except Al with Fe being separated again in the employing pyrohydrolysis step 30 described in the preceding paragraph, major part in residual soluble iron, aluminium and magnesium will be removed from leach liquor by a series of removal of impurity step, and these steps are collectively referred to as removal of impurity step 36 in FIG.Described removal of impurity step 36 and then comprise pH set-up procedure 38, pH value is increased to 9 by adding LiOH 40 by this step.The product of step 38 enters belt filter 42, by this strainer, the precipitation containing Al, Fe, Mn and Mg is separated again.Described removal of impurity step 36 and then also comprise calcium deposit step 44, adds sodium carbonate (i.e. soda powder) or Quilonum Retard 46 in this step to generate containing calcium deposit 48 in another belt filter 50.
The thicker underflow product 52 that second stage thickening step 28b produces enters drying step 54, becomes waste material 56 afterwards and then by disposal 58.
The liquid product of belt filter 50, it is LiCl solution mainly, enters enrichment step 60 and and then enter fractional crystallization step 62.In described enrichment step 60, this LiCl solution is concentrated into close to saturation point, such as 35-40% LiCl w/w, and is cooled to subzero.At follow-up fractional crystallization step 62, major part is removed by substep respectively containing the impurity 64 of Na and K, such as NaCl and KCl crystal.
As described above, eliminating substantially after all dirt, lithium chloride solution enters ion-exchange step 66, and this step comprises all to be removed residual calcium, magnesium and other polyvalent cation to the level lower than about 10ppm substantially by ion-exchange (IX) post 68, such as 1ppm.
Lithium chloride solution through being further purified then is heated to 90 DEG C and pumps to electrolysis step 70, and this step adopts several electrolyzers, such as 6 to 20 electrolyzers, produces lithium hydroxide, chlorine and hydrogen in a cell by consumption lithium chloride and water.
After passing through above-mentioned electrolyzer, thin or after being consumed lithium chloride solution contains the chlorine of dissolving.Before being circulated at this thin lithium chloride solution the pulping stage being positioned at the previous link of described leach circuit 22, a point two-stage is removed by the chlorine dissolved by this.In a first stage, hydrochloric acid is added described lithium chloride solution thus pH value is reduced to <5, this numerical value can force part chlorine to discharge solution.Then, remaining is removed by carrying out stripping (not shown) to solution by the chlorine dissolved.
The hydrochloric acid HCl that can use in pulping stage and leach circuit 22 is mixed to produce as the chlorine of by product and hydrogen.
First the lithium hydroxide solution obtained by electrolysis step 70 enters insulation can 72, as clearly illustrated in FIG, in insulation can, lithium hydroxide can by (1) evaporation and crystallization to generate Lithium Hydroxide Monohydrate crystal, or (2) are sent to carburising step thus are converted into Quilonum Retard.
In the first option in above-mentioned option, the described lithium hydroxide in solution is such as working in about 80 DEG C and about 45kPa(a) pressure under vacuum crystallization vaporizer 80(Oslo-type Oslo type) in by crystallization.Its residence time is about 60 minutes to obtain coarse crystallization product.The water vapor produced is recompressed, with supply vapor mixing and as hot media for this crystallizer 80.
Lithium hydroxide xln is with the cleaning efficiency of cold water (not shown) cleaning acquisition 99%.As noted, the washings obtained gets back to leach circuit 22 by recirculation.Solid from whizzer is fed to and works in about 120 DEG C of indirect firings or moisture eliminator 82 with dried crystals.The crystalline product obtained is cell-grade LiOH.H2O, and it is pneumatically sent to product storehouse 84, and is finally transmitted to pack station (not shown) along with it in shell-type screw conveyer 86 and is cooled to 50 DEG C.
In the second option in above-mentioned option, generate Quilonum Retard by carbonization lithium hydroxide solution, described carbonization makes Quilonum Retard precipitate by compression arbon dioxide gas 88 being passed into lithium hydroxide solution in carbonization container 90.The slurry formed is fed to cleaning machine/whizzer 92 through strainer 94, and washings and any residual lithium hydroxide solution or mother liquor are recirculated to electrolysis step 70 after this.Wet Quilonum Retard crystal is fed to moisture eliminator 96, adopts this crystal of hot-air dry in this moisture eliminator.Adopt the air heating warm air of middle pressure.After the drying, the granular size of battery-level lithium carbonate required for micronize to human consumer, is sent to storage silo and following packaged (not shown) afterwards.
In whole technique, adopt condensation to form supplementary feed as thermal treatment water, deepfreeze water and water coolant.Because this technique does not return condensation, thus there is water balance positive on the whole, and the process water of about 1/10 is switched to sink drainage (not shown).
Can expect, tantalum and aluminium also can adopt technique of the present invention to decompose again.Filter residue from thickening step can be exchanged to tantalum recovery process (not shown).Discharge from this lithium recovery process can be fed to belt filter to remove moisture content, and removed moisture content returns tantalum recovery process.Filter and do not adopt cleaning and the filtrating area with 19 m2.From the filter residue of belt filter at direct firing inner drying.Dry pure aluminium silicate is cooled to 50 DEG C and is then pneumatically sent to storage silo in shell-type screw conveyer, is then distributed.
According to another embodiment of the present invention, described lithium-containing materials is provided by with the form containing lithium bittern.Bittern does not need to carry out calcining in the present invention described by an embodiment, cooling, grinding and leaching step, and substantially identical with described by a upper embodiment of all the other steps of this technique.
In sum, the invention provides from α-triphane ore deposit or concentrate, or from containing the technique obtaining high purity or cell-grade lithium hydroxide and Quilonum Retard product lithium bittern, also can produce HCl gas product simultaneously.
The change can expected easily to those skilled in the art or replacement, all should be encompassed within protection scope of the present invention.Such as, described leach circuit 22 only can comprise a leaching level/operation and not deviate from scope of the present invention.
Claims (26)
1., for a technique for lithium-containing materials process, described technique comprises the following steps:
(1) with described lithium-containing materials preparation technology liquid;
(2) process liquor making step (1) generate enters a series of removal of impurity step, thus generates the lithium chloride solution of purifying substantially; And
(3) lithium chloride solution of the purifying making step (2) generate enters electrolysis step, thus generates lithium hydroxide solution.
2. technique according to claim 1, wherein with the process liquor of the form preparation process (1) of leach liquor.
3. technique according to claim 2, wherein form described leach liquor by making lithium-containing materials enter leaching step, described in this leaching step, material is leached by hydrochloric acid.
4., according to the technique in the claims described in any one, wherein comprise further as the removal of impurity step of step (2) and make leach liquor be concentrated to lithium chloride close to saturated enrichment step.
5., according to the technique in the claims described in any one, the lithium hydroxide solution wherein generated in step (3) can by water evaporates thickening to generate Lithium Hydroxide Monohydrate crystal.
6. according to the technique in the claims described in any one, the lithium hydroxide solution wherein generated in step (3) can be carbonized by making compression arbon dioxide enter this solution, thus generates Quilonum Retard precipitation.
7. according to the technique in the claims described in any one, wherein said lithium-containing materials is α-triphane ore deposit or concentrate, and described technique comprises further: first α described in calcination-triphane ore deposit or concentrate are to generate the step of β-triphane.
8., according to the technique in claim 1-6 described in any one, wherein said lithium-containing materials is containing lithium bittern.
9. technique according to claim 6, a part for the lithium hydroxide solution wherein generated in step (3) carrys out thickening to generate Lithium Hydroxide Monohydrate crystal by evaporation/crystallization, and its another part is carbonized by making compression arbon dioxide enter this solution, thus generate Quilonum Retard precipitation.
10. according to the technique in the claims described in any one, wherein the removal of impurity step of step (2) comprises the muriatic one or many pyrohydrolysis of Al and Fe, increase pH value to make Al, Fe, the precipitation of hydroxide of Mg and Mn, precipitation Quilonum Retard is to remove Ca, and fractional crystallization is to remove Na and K.
11. techniques according to claim 10, the described fractional crystallization of wherein removing Na and K is carried out immediately after described enrichment step.
12. techniques according to claim 10 or 11, wherein said removal of impurity step preferably further comprises ion-exchange step.
13. techniques according to claim 12, the calcium existed in leach liquor, magnesium and other polyvalent cation are removed all by wherein said ion-exchange step substantially.
14. techniques according to claim 13, wherein said polyvalent cation is removed to the level lower than about 10ppm.
15. techniques according to claim 13 or 14, wherein said polyvalent cation is removed to the level of about 1ppm.
16. according to the technique in claim 9 to 15 described in any one, and the moisture content be wherein evaporated from solution in evaporation/crystallization is recompressed slightly, with supply vapor mixing and for evaporation/crystallization.
17. according to the technique in claim 9 to 16 described in any one, and wherein said evaporation/crystallization step preferably adopts vacuum evaporation crystallizer.
18. according to the technique in claim 7 to 17 described in any one, and wherein said β-triphane was first cooled and grinds before described leaching step.
19. techniques according to claim 18, wherein said β-triphane is milled to lower than about 300 μm.
20. techniques according to claim 18 or 19, the granularity that wherein said β-triphane is milled to about 75 μm is P
80.
21. according to the technique in claim 3 to 20 described in any one, and wherein said leaching step is at high temperature carried out.
22. according to the technique in claim 3 to 21 described in any one, and the hydrochloric acid soln wherein adopted in described leaching step is about 20%HCl w/w.
23. techniques according to claim 22, the described high temperature wherein leaching step is approximately the boiling point of the hydrochloric acid soln adopted in this leaching step.
24. according to the technique in claim 3 to 23 described in any one, and wherein said leaching step is preferably carried out at ambient pressure.
25. according to the technique in claim 3 to 24 described in any one, and the time wherein stopped about 6 to 10 hours in the chlorination kiln of about 108 DEG C performs described leaching step.
26. techniques according to claim 25, wherein said leaching step is performed on the residence time of about 8 hours.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010274898.7A CN111519042A (en) | 2012-08-13 | 2013-08-01 | Process for treating lithium-containing materials |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2012903483A AU2012903483A0 (en) | 2012-08-13 | Processing of Lithium Containing Ore | |
| AU2012903483 | 2012-08-13 | ||
| PCT/AU2013/000857 WO2014026217A1 (en) | 2012-08-13 | 2013-08-01 | Processing of lithium containing material |
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| CN202010274898.7A Division CN111519042A (en) | 2012-08-13 | 2013-08-01 | Process for treating lithium-containing materials |
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| CN202010274898.7A Pending CN111519042A (en) | 2012-08-13 | 2013-08-01 | Process for treating lithium-containing materials |
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| JP (1) | JP6275138B2 (en) |
| KR (1) | KR101857458B1 (en) |
| CN (2) | CN104271781A (en) |
| AU (1) | AU2013201833B2 (en) |
| CA (1) | CA2851786C (en) |
| CL (1) | CL2014001656A1 (en) |
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| CN107454916A (en) * | 2015-01-27 | 2017-12-08 | 里德先进材料有限公司 | The processing of lithium-containing materials including HCl injections |
| CN108367933A (en) * | 2015-08-27 | 2018-08-03 | 内玛斯卡锂公司 | Method for handling lithium-containing materials |
| CN108660476A (en) * | 2017-08-10 | 2018-10-16 | 青海盐湖工业股份有限公司 | A kind of new process of salt lake bittern production high-purity hydrogen lithia |
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| CN110494574A (en) * | 2017-02-28 | 2019-11-22 | Sms集团有限公司 | The method that lithium hydroxide is prepared by the ore containing lithium by chlorination and chloralkali process |
| CN111826531A (en) * | 2020-07-07 | 2020-10-27 | 浙江衢州明德新材料有限公司 | Method for extracting lithium from brine by using powdery adsorbent |
| CN113453788A (en) * | 2019-02-20 | 2021-09-28 | 笹仓机械工程有限公司 | Lithium recovery method |
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| CN108367933A (en) * | 2015-08-27 | 2018-08-03 | 内玛斯卡锂公司 | Method for handling lithium-containing materials |
| CN106148730A (en) * | 2016-07-05 | 2016-11-23 | 广东道氏技术股份有限公司 | One extracts alkali-metal method from lepidolite |
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| CN110494573A (en) * | 2017-02-28 | 2019-11-22 | Sms集团有限公司 | Method for preparing lithium hydroxide by the ore containing lithium |
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| CN108660476A (en) * | 2017-08-10 | 2018-10-16 | 青海盐湖工业股份有限公司 | A kind of new process of salt lake bittern production high-purity hydrogen lithia |
| CN108660476B (en) * | 2017-08-10 | 2019-04-02 | 青海盐湖工业股份有限公司 | A kind of new process of salt lake bittern production high-purity hydrogen lithia |
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| CN111826531A (en) * | 2020-07-07 | 2020-10-27 | 浙江衢州明德新材料有限公司 | Method for extracting lithium from brine by using powdery adsorbent |
Also Published As
| Publication number | Publication date |
|---|---|
| JP6275138B2 (en) | 2018-02-07 |
| CA2851786A1 (en) | 2014-02-20 |
| CL2014001656A1 (en) | 2014-10-10 |
| KR101857458B1 (en) | 2018-05-14 |
| CA2851786C (en) | 2016-04-12 |
| WO2014026217A1 (en) | 2014-02-20 |
| US20150152523A1 (en) | 2015-06-04 |
| JP2015531826A (en) | 2015-11-05 |
| AU2013201833B2 (en) | 2014-07-17 |
| AU2013201833A1 (en) | 2014-02-27 |
| MY163075A (en) | 2017-08-15 |
| CN111519042A (en) | 2020-08-11 |
| KR20150041661A (en) | 2015-04-16 |
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