CN102417995A - Process for extracting lithium from lithium pyroxene concentrate by using fluorine chemistry - Google Patents
Process for extracting lithium from lithium pyroxene concentrate by using fluorine chemistry Download PDFInfo
- Publication number
- CN102417995A CN102417995A CN201110358932XA CN201110358932A CN102417995A CN 102417995 A CN102417995 A CN 102417995A CN 201110358932X A CN201110358932X A CN 201110358932XA CN 201110358932 A CN201110358932 A CN 201110358932A CN 102417995 A CN102417995 A CN 102417995A
- Authority
- CN
- China
- Prior art keywords
- lithium
- reaction
- triphane
- fluorine chemistry
- put forward
- 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
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)
Abstract
The invention provides a process for extracting lithium from lithium pyroxene concentrate by using fluorine chemistry. The process comprises the following steps of: firstly, uniformly mixing raw materials, such as alpha-lithium pyroxene concentrate powder, an additive and sulfuric acid according to weight ratio of 1:(0.1-2):(0.5-5); secondly, feeding the uniformly-mixed raw materials into a reactor and finishing the reaction and timely extracting gas generated in the reaction process; thirdly, leaching reaction slag retained in the reactor with water and carrying out solid-liquid separation on the reaction slag to obtain a sulfate solution and remove ionic impurities in the solution, such as potassium, sodium, aluminum, magnesium, calcium, ferrum and the like; and fourthly, after the impurities are filtered, concentrating residual solution to obtain a precipitation containing lithium ions, filtering to obtain a rough lithium salt product and producing refined lithium salt according to the requirement. The process disclosed by the invention has the advantages of low reaction temperature, low production energy consumption and high lithium extraction rate; the lithium can be directly extracted from alpha-lithium pyroxene without crystal form transformation; and various valuable components of the lithium pyroxene can be integrally utilized while the lithium salt is produced.
Description
Technical field
The present invention relates to a kind of ore and put forward the lithium technical field, more specifically put forward lithium technology for a kind of triphane concentrate fluorine chemistry.
Background technology
Lithium and lithium salts expand to high-technology fields such as Al-Li alloy, lithium cell, nucleosynthesis by traditional Application Areas such as glass-ceramic, electrolytic aluminum, railway grease, refrigeration etc.; The particularly new forms of energy explosive type demand growth that possibly exist for efficient store battery; Technical progress to lithium salts industry has proposed urgent challenge, studies new lithium minerals and puies forward the lithium technology development of world's new forms of energy is had crucial meaning.
The main raw material of carrying lithium at present is salt lake brine and solid lithium minerals, and the reserves of Chinese lithionite and triphane are abundant.The method of from lithium minerals, carrying lithium mainly contains sulphate process, chloride process, limestone-based process, sulfuric acid process and gas-solid reaction method.These methods all are that lithium minerals is carried out high-temperature calcination, handle the calcining slag with diverse ways then and further produce lithium salts, exist the production cost height, and energy consumption is big, and the lithium extraction yield is low, and the waste residue amount is big.
Summary of the invention
For solving the problem of above-mentioned existence; The present invention proposes a kind of triphane concentrate fluorine chemistry and put forward lithium technology; Utilize the character of the distinctive destruction silicate minerals of fluorine chemistry crystalline structure; Adopt the α triphane directly to carry lithium, under relatively low temperature of reaction temperature, just can destroy the fine and close layered crystal structure of triphane, reach the purpose of efficiently carrying lithium without the crystal formation conversion; Greatly reduce the energy consumption in the production process, when producing lithium salts, also can fully utilize the various valuable components of α triphane mineral.
For achieving the above object, the technical scheme that the present invention adopted is following:
A kind of triphane concentrate fluorine chemistry is put forward lithium technology, realizes through following steps:
1) raw material α triphane fine ore, additive, sulfuric acid are pressed the weight proportion uniform mixing of 1:0.1-2:0.5-5;
2) raw material after above-mentioned the mixing is sent into completion reaction in the reactor drum, the gas that produces in the reaction process is in time extracted out;
3) the reaction slag that retains in the reactor drum is used water extraction, obtains sulfate liquor through liquid-solid separation, removes potassium, sodium, aluminium, magnesium, calcium, iron plasma impurity in the solution;
4) after the impurity filtering, surplus solution concentrates, and obtains containing the throw out of lithium ion, filters and makes thick lithium salts product, can produce refined lithium salt as required.
Raw material preheating in the said step 1) and mix after send into again in the reactor drum and to accomplish reaction.
The preheating temperature of said raw material is 50-150 ℃, and be 0.1-2 hour warm up time.
Step 2) after raw material gets into reactor drum in, is 150-350 ℃ in temperature and reacted 0.5-4 hour down.
Said additive is one or more of fluorine-containing mineral, salt or acid.
Li in the α triphane fine ore in the raw material
2The weight content of O>=5.0%, the weight content of F>=10% in the additive, H in the sulfuric acid
2SO
4Weight content>=50%.
Adopt into alum crystallization removal of impurities in the step 3) and regulate the pH removal of impurities, remove potassium, sodium, aluminium, magnesium, calcium, iron plasma impurity.
Regulating the PH scope of regulating in the PH removal of impurities process is 5.0-11.0.
After the gas that produces in the reaction process is extracted out, absorb through water or alkaline solution after the cooling dedusting.
Triphane concentrate fluorine chemistry provided by the present invention is put forward lithium technology, and its beneficial effect is:
1, operational path does not need high-temperature calcination; The α triphane is directly carried lithium without the crystal formation conversion; Utilize the characteristic of fluorine chemistry corrosion Si oxide, the employing additive than destroying the lithium minerals crystalline structure under the low reaction temperatures, has been practiced thrift production energy consumption with sulfuric acid greatly;
2, the fluorine in the reaction mass separates with the reaction slag with the form of silicon fluoride, hydrogen fluoride gas; And be absorbed and obtain silicofluoric acid or silicofluoride is used for producing the fluoride salt product; The reaction slag is gone out the sulfate liquor that the back obtains to contain lithium by water logging; Filter residue is mainly calcium sulfate, can be used as the crown filler and is used;
3, the sulfate liquor that contains lithium that obtains is behind impurity such as deposition potassium, sodium, aluminium, iron, magnesium, calcium; Further concentrate, precipitate, separate the acquisition lithium salts; It is high to have the lithium extraction yield; And can fully utilize in the mineral various valuable compositions and realize coproduction, advantage such as comprehensive benefit is good, and production cost is low, production energy consumption is little.
Embodiment
Describe the present invention below in conjunction with specific embodiment:
A kind of triphane concentrate fluorine chemistry provided by the invention is put forward lithium technology, realizes through following steps:
1) take by weighing α triphane fine ore, additive, three kinds of raw materials of sulfuric acid, additive can adopt one or more of fluorine-containing mineral, salt or acid, the weight content of F>=10%, Li in the α triphane fine ore
2The weight content of O>=5.0%, H in the sulfuric acid
2SO
4Weight content>=50%.Above-mentioned raw materials α triphane fine ore, additive, sulfuric acid are mixed by the weight proportion of 1:0.1-2:0.5-5 and stir.
2) raw material after above-mentioned the mixing is sent in the reactor drum accomplished reaction, also can be earlier above-mentioned raw materials is sent in the blender preheating and stirred, send into again and accomplish reaction in the reactor drum, help to improve speed of reaction.The preheating temperature of raw material is 50-150 ℃ in the blender, and be 0.1-2 hour warm up time.After raw material gets into reactor drum, be 150-350 ℃ in temperature and reacted 0.5-4 hour down.The gas that produces in the reaction process is mainly silicon tetrafluoride, water vapour, hydrogen fluoride, in time extracts out and absorbs through water or alkaline solution after the cooling dedusting, obtains silicofluoric acid or silicofluoride and is used for producing the fluoride salt product.
3) the reaction slag that retains in the reactor drum is used water extraction; Obtain sulfate liquor through liquid-solid separation; Adopt into alum crystallization removal of impurities and regulate the pH removal of impurities, regulate the pH scope, remove potassium, sodium, aluminium, magnesium, calcium, iron plasma impurity in the solution at 5.0-11.0; Filter residue is mainly calcium sulfate, can be used as the crown filler and is used.
4) after the impurity filtering, surplus solution concentrates, and obtains containing the throw out of lithium ion, filters and makes thick lithium salts product, can produce refined lithium salt as required.
Embodiment 1:
Raw material weight is than being α triphane fine ore: additive: sulfuric acid=1:0.1:0.5, Li in the α triphane fine ore
2The weight content of O is 5.5%, and said additive is the hydrofluoric acid of weight concentration 30%, and the weight content of F is 10%, and the vitriolic weight concentration is 50%.Preheating temperature in the blender is 50 ℃, and be 0.1 hour warm up time.Mixture gets in the reactor drum, is 350 ℃ in temperature of reaction and reacts 2 hours down.The reaction slag with water extraction after; Liquid-solid separation obtains sulfate liquor, adds the sinker mother liquor that contains sodium sulphate, is cooled to-5 ℃ after concentrating and removes most aluminium in the solution, magnesium, calcium, iron plasma impurity; The pH that regulates this solution is 6.0, to remove aluminium, magnesium, calcium, iron plasma impurity; After the impurity elimination, solution concentrates, and deposition is filtered behind the lithium ion, the lithium carbonate containing weight ratio is 80% thick lithium salts product, need based on purposes, produce corresponding refined lithium salt.
Embodiment 2:
Raw material weight is than being α triphane fine ore: additive: sulfuric acid=1:2:5, Li in the α triphane fine ore
2The weight content of O is 5.5%, and said additive is the Calcium Fluoride (Fluorspan) of weight concentration 70%, and the weight content of F is 15%, and the vitriolic weight concentration is 60%.Preheating temperature in the blender is 150 ℃, and be 1 hour warm up time.Mixture gets in the reactor drum, is 200 ℃ in temperature of reaction and reacts 4 hours down.The reaction slag with water extraction after; Liquid-solid separation obtains sulfate liquor, adds the sinker mother liquor that contains sodium sulphate, is cooled to-5 ℃ after concentrating and removes most aluminium in the solution, magnesium, calcium, iron plasma impurity; The pH that regulates this solution is 5.0, to remove aluminium, magnesium, calcium, iron plasma impurity; After the impurity elimination, solution concentrates, and deposition is filtered behind the lithium ion, the lithium carbonate containing weight ratio is 85% thick lithium salts product, need based on purposes, produce corresponding refined lithium salt.
Embodiment 3:
Raw material weight is than being α triphane fine ore: additive: sulfuric acid=1:1:3, Li in the α triphane fine ore
2The weight content of O is 6.0%, and said additive is the hydrofluoric acid of weight concentration 30%, and the weight content of F is 15%, and the vitriolic weight concentration is 70%.Preheating temperature in the blender is 100 ℃, and be 1 hour warm up time.Mixture gets in the reactor drum, is 250 ℃ in temperature of reaction and reacts 2 hours down.The reaction slag with water extraction after; Liquid-solid separation obtains sulfate liquor, adds the sinker mother liquor that contains sodium sulphate, is cooled to-5 ℃ after concentrating and removes most aluminium in the solution, magnesium, calcium, iron plasma impurity; The pH that regulates this solution is 5.0, to remove aluminium, magnesium, calcium, iron plasma impurity; After the impurity elimination, solution concentrates, and deposition is filtered behind the lithium ion, the lithium carbonate containing weight ratio is 85% thick lithium salts product, need based on purposes, produce corresponding refined lithium salt.
Embodiment 4:
Raw material weight is than being α triphane fine ore: additive: sulfuric acid=1:1:4, Li in the α triphane fine ore
2The weight content of O is 5.5%, and said additive is the hydrofluoric acid of weight concentration 30% and the Calcium Fluoride (Fluorspan) of weight concentration 70%, and the weight content of F is 10%, and the vitriolic weight concentration is 50%.Preheating temperature in the blender is 120 ℃, and be 0.5 hour warm up time.Mixture gets in the reactor drum, is 150 ℃ in temperature of reaction and reacts 4 hours down.The reaction slag with water extraction after; Liquid-solid separation obtains sulfate liquor, adds the sinker mother liquor that contains sodium sulphate, is cooled to-5 ℃ after concentrating and removes most aluminium in the solution, magnesium, calcium, iron plasma impurity; The pH that regulates this solution is 10.0, to remove aluminium, magnesium, calcium, iron plasma impurity; After the impurity elimination, solution concentrates, and deposition is filtered behind the lithium ion, the lithium carbonate containing weight ratio is 85% thick lithium salts product, need based on purposes, produce corresponding refined lithium salt.
Embodiment 5:
Raw material weight is than being α triphane fine ore: additive: sulfuric acid=1:0.5:3, Li in the α triphane fine ore
2The weight content of O is 5.5%, and said additive is the mixture of fluorine-containing mineral, salt and acid, and the weight content of F is 12%, and the vitriolic weight concentration is 50%.Preheating temperature in the blender is 100 ℃, and be 1 hour warm up time.Mixture gets in the reactor drum, is 350 ℃ in temperature of reaction and reacts 0.5 hour down.The reaction slag with water extraction after; Liquid-solid separation obtains sulfate liquor, adds the sinker mother liquor that contains sodium sulphate, is cooled to-5 ℃ after concentrating and removes most aluminium in the solution, magnesium, calcium, iron plasma impurity; The pH that regulates this solution is 11.0, to remove aluminium, magnesium, calcium, iron plasma impurity; After the impurity elimination, solution concentrates, and deposition is filtered behind the lithium ion, the lithium carbonate containing weight ratio is 80% thick lithium salts product, need based on purposes, produce corresponding refined lithium salt.
Embodiment 6:
Raw material weight is than being α triphane fine ore: additive: sulfuric acid=1:0.1:0.5, Li in the α triphane fine ore
2The content of O is 5.0%, and said additive is the hydrofluoric acid of weight concentration 30%, and the weight content of F does, 20%, and the vitriolic weight concentration is 50%.Preheating temperature in the blender is 100 ℃, and be 2 hours warm up time.Mixture gets in the reactor drum, is 300 ℃ in temperature of reaction and reacts 1 hour down.The reaction slag with water extraction after; Liquid-solid separation obtains sulfate liquor, adds the sinker mother liquor that contains sodium sulphate, is cooled to-5 ℃ after concentrating and removes most aluminium in the solution, magnesium, calcium, iron plasma impurity; The pH that regulates this solution is 5.0, to remove aluminium, magnesium, calcium, iron plasma impurity; After the impurity elimination, solution concentrates, and deposition is filtered behind the lithium ion, the lithium carbonate containing weight ratio is 85% thick lithium salts product, need based on purposes, produce corresponding refined lithium salt.
Embodiment 7:
Raw material weight is than being α triphane fine ore: additive: sulfuric acid=1:0.1:0.5, Li in the α triphane fine ore
2The content of O is 5.5%, and said additive is the hydrofluoric acid of weight concentration 30%, and the weight content of F is 25%, and the vitriolic weight concentration is 50%.Preheating temperature in the blender is 150 ℃, and be 0.5 hour warm up time.Mixture gets in the reactor drum, is 300 ℃ in temperature of reaction and reacts 3 hours down.The reaction slag with water extraction after; Liquid-solid separation obtains sulfate liquor, adds the sinker mother liquor that contains sodium sulphate, is cooled to-5 ℃ after concentrating and removes most aluminium in the solution, magnesium, calcium, iron plasma impurity; The pH that regulates this solution is 6.0, to remove aluminium, magnesium, calcium, iron plasma impurity; After the impurity elimination, solution concentrates, and deposition is filtered behind the lithium ion, the lithium carbonate containing weight ratio is 90% thick lithium salts product, need based on purposes, produce corresponding refined lithium salt.
Claims (9)
1. a triphane concentrate fluorine chemistry is put forward lithium technology, it is characterized in that, realizes through following steps:
1) raw material α triphane fine ore, additive, sulfuric acid are pressed the weight proportion uniform mixing of 1:0.1-2:0.5-5;
2) raw material after above-mentioned the mixing is sent into completion reaction in the reactor drum, the gas that produces in the reaction process is in time extracted out;
3) the reaction slag that retains in the reactor drum is used water extraction, obtains sulfate liquor through liquid-solid separation, removes potassium, sodium, aluminium, magnesium, calcium, iron plasma impurity in the solution;
4) after the impurity filtering, surplus solution concentrates, and obtains containing the throw out of lithium ion, filters and makes thick lithium salts product, can produce refined lithium salt as required.
2. triphane concentrate fluorine chemistry according to claim 1 is put forward lithium technology, it is characterized in that, the raw material preheating in the said step 1) and mix after send into again in the reactor drum and to accomplish reaction.
3. triphane concentrate fluorine chemistry according to claim 2 is put forward lithium technology, it is characterized in that, the preheating temperature of said raw material is 50-150 ℃, and be 0.1-2 hour warm up time.
4. triphane concentrate fluorine chemistry according to claim 1 is put forward lithium technology, it is characterized in that step 2) in after raw material gets into reactor drum, be 150-350 ℃ of reaction 0.5-4 hour down in temperature.
5. triphane concentrate fluorine chemistry according to claim 1 is put forward lithium technology, it is characterized in that, said additive is one or more of fluorine-containing mineral, salt or acid.
6. triphane concentrate fluorine chemistry according to claim 1 is put forward lithium technology, it is characterized in that Li in the α triphane fine ore in the raw material
2The weight content of O>=5.0%, the weight content of F>=10% in the additive, H in the sulfuric acid
2SO
4Weight content>=50%.
7. triphane concentrate fluorine chemistry according to claim 1 is put forward lithium technology, it is characterized in that, adopts into alum crystallization removal of impurities in the step 3) and regulates the pH removal of impurities, removes potassium, sodium, aluminium, magnesium, calcium, iron plasma impurity.
8. triphane concentrate fluorine chemistry according to claim 7 is put forward lithium technology, it is characterized in that, regulating the PH scope of regulating in the PH removal of impurities process is 5.0-11.0.
9. triphane concentrate fluorine chemistry according to claim 1 is put forward lithium technology, it is characterized in that, after the gas that produces in the reaction process is extracted out, absorbs through water or alkaline solution after the cooling dedusting.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110358932XA CN102417995A (en) | 2011-11-14 | 2011-11-14 | Process for extracting lithium from lithium pyroxene concentrate by using fluorine chemistry |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110358932XA CN102417995A (en) | 2011-11-14 | 2011-11-14 | Process for extracting lithium from lithium pyroxene concentrate by using fluorine chemistry |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102417995A true CN102417995A (en) | 2012-04-18 |
Family
ID=45942638
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110358932XA Pending CN102417995A (en) | 2011-11-14 | 2011-11-14 | Process for extracting lithium from lithium pyroxene concentrate by using fluorine chemistry |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102417995A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102690961A (en) * | 2012-06-28 | 2012-09-26 | 贵州开磷（集团）有限责任公司 | Method for directly extracting lithium by utilizing low-grade alpha-spodumene as raw material |
| CN106687611A (en) * | 2014-04-09 | 2017-05-17 | Inis生物技术有限责任公司 | Process for obtaining lithium from aluminosilicates and intermediate compounds |
| WO2017136885A1 (en) | 2016-02-09 | 2017-08-17 | Lithium Australia Nl | Processes for extracting and recovering lithium values from lithium bearing materials |
| WO2017181766A1 (en) * | 2016-04-20 | 2017-10-26 | 天齐锂业股份有限公司 | Method for extracting lithium using slag from thermal recycling of lithium battery |
| CN110526264A (en) * | 2019-09-27 | 2019-12-03 | 福州大学 | A kind of method that natural α spodumene directly mentions lithium by-product zeolite |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040028585A1 (en) * | 2000-09-13 | 2004-02-12 | Francois Cardarelli | Method for recycling spent lithium metal polymer rechargeable batteries and related materials |
| CN101974684A (en) * | 2010-11-26 | 2011-02-16 | 福州大学 | Process for removing impurities from lepidolite leaching solution |
| CN101974678A (en) * | 2010-11-24 | 2011-02-16 | 中南大学 | Method for extracting lithium and other alkali metal elements from lepidolite mineral |
| CN102041380A (en) * | 2010-11-17 | 2011-05-04 | 山东瑞福锂业有限公司 | Production process for extracting lithium from ore with low-temperature method |
-
2011
- 2011-11-14 CN CN201110358932XA patent/CN102417995A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040028585A1 (en) * | 2000-09-13 | 2004-02-12 | Francois Cardarelli | Method for recycling spent lithium metal polymer rechargeable batteries and related materials |
| CN102041380A (en) * | 2010-11-17 | 2011-05-04 | 山东瑞福锂业有限公司 | Production process for extracting lithium from ore with low-temperature method |
| CN101974678A (en) * | 2010-11-24 | 2011-02-16 | 中南大学 | Method for extracting lithium and other alkali metal elements from lepidolite mineral |
| CN101974684A (en) * | 2010-11-26 | 2011-02-16 | 福州大学 | Process for removing impurities from lepidolite leaching solution |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102690961A (en) * | 2012-06-28 | 2012-09-26 | 贵州开磷（集团）有限责任公司 | Method for directly extracting lithium by utilizing low-grade alpha-spodumene as raw material |
| CN106687611A (en) * | 2014-04-09 | 2017-05-17 | Inis生物技术有限责任公司 | Process for obtaining lithium from aluminosilicates and intermediate compounds |
| WO2017136885A1 (en) | 2016-02-09 | 2017-08-17 | Lithium Australia Nl | Processes for extracting and recovering lithium values from lithium bearing materials |
| US20190048438A1 (en) * | 2016-02-09 | 2019-02-14 | Lithium Australia Nl | Process for extracting and recovering lithium values from lithium bearing materials |
| EP3414351A4 (en) * | 2016-02-09 | 2019-07-31 | Lithium Australia NL | Processes for extracting and recovering lithium values from lithium bearing materials |
| US10883157B2 (en) | 2016-02-09 | 2021-01-05 | Lithium Australia Nl | Process for extracting and recovering lithium values from lithium bearing materials |
| AU2017218457B2 (en) * | 2016-02-09 | 2021-01-21 | Lithium Australia Nl | Processes for extracting and recovering lithium values from lithium bearing materials |
| WO2017181766A1 (en) * | 2016-04-20 | 2017-10-26 | 天齐锂业股份有限公司 | Method for extracting lithium using slag from thermal recycling of lithium battery |
| CN110526264A (en) * | 2019-09-27 | 2019-12-03 | 福州大学 | A kind of method that natural α spodumene directly mentions lithium by-product zeolite |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101885496B (en) | Process for extracting lithium from lithionite by fluorine chemistry | |
| CN100455512C (en) | Method for preparing battery-stage monohydrate lithium hydroxide | |
| CN102020294B (en) | Lithium hydroxide monohydrate and preparation method thereof | |
| CN102041380B (en) | Production process for extracting lithium from ore with low-temperature method | |
| CN110240182B (en) | Resourceful treatment method of lithium-rich aluminum electrolyte | |
| CN104445311B (en) | Poly-generation clean preparation method of high-content silicon dioxide fly ash | |
| CN103145158A (en) | Method for preparing lithium carbonate from lepidolite through sulfuric acid roasting method | |
| CN101974684A (en) | Process for removing impurities from lepidolite leaching solution | |
| JP2022510998A (en) | Manufacture of Lithium Chemicals and Metallic Lithium | |
| CN113292057B (en) | Recovery method of waste lithium iron phosphate battery | |
| CN102417995A (en) | Process for extracting lithium from lithium pyroxene concentrate by using fluorine chemistry | |
| CN112624161B (en) | Method for preparing lithium carbonate by extracting lithium from mechanically activated lepidolite | |
| WO2014047764A1 (en) | Method for producing high-purity nanometer zinc oxide from steel plant smoke and dust by ammonia decarburization | |
| CN111115665A (en) | Method for recycling lithium-potassium-rich aluminum electrolyte | |
| CN114457237B (en) | Method for recovering lithium from acidic leaching solution of aluminum electrolyte | |
| CN104003428A (en) | Method for producing lithium hydroxide by dissolving spodumene out of pipeline reactor | |
| CN103193253B (en) | Pressurized acid-leaching potassium extracting technology for potassium feldspar | |
| CN108063295A (en) | The method that lithium is extracted in the clinker generated from pyrogenic process recycling lithium battery | |
| CN108118143A (en) | Two sections of chloridising roastings-alkaline leaching method puies forward the method that lithium prepares lithium carbonate from lepidolite | |
| CN114684835B (en) | Method for preparing aluminum fluoride product by combined treatment of aluminum industry solid waste | |
| CN115216630B (en) | Recycling treatment method of waste lithium-containing aluminum electrolyte | |
| CN111592017A (en) | Method for preparing battery-grade lithium chloride by pressing and soaking spodumene | |
| CN116497235A (en) | Method for extracting lithium from low-lithium clay | |
| CN111410215A (en) | Method for extracting lithium sulfate from brine with high magnesium-lithium ratio | |
| CN115505740A (en) | Resource method for treating red mud by adopting nitrate wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20120418 |