CN101979680B - Method for removing aluminum from rare-earth feed liquid - Google Patents
Method for removing aluminum from rare-earth feed liquid Download PDFInfo
- Publication number
- CN101979680B CN101979680B CN2010105477201A CN201010547720A CN101979680B CN 101979680 B CN101979680 B CN 101979680B CN 2010105477201 A CN2010105477201 A CN 2010105477201A CN 201010547720 A CN201010547720 A CN 201010547720A CN 101979680 B CN101979680 B CN 101979680B
- Authority
- CN
- China
- Prior art keywords
- feed liquid
- rare earth
- earth feed
- rare
- organic phase
- 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.)
- Active
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 discloses a method for removing aluminum from rare-earth feed liquid, belongs to rare-earth feed liquid treatment technology and aims to provide the method for removing the aluminum from the rare-earth feed liquid, of which the aluminum-removing effect is good, the aluminum-removing cost is low, the rare-earth recovery rate is high, the operation and control are convenient, the process is simple and the investment in equipment is small. The key point of the technical scheme mainly comprises the following steps of: (1) preparing an organic phase from 15 to 25 volume percent of naphthenic acid and 15 to 25 volume percent of alcohol-kerosene; (2) adding the prepared organic phase and the rare-earth feed liquid into a stirring tank in a volume ratio of 2-5:1, starting the tank, stirring and uniformly mixing; (3) adding alkaline solution into the mixed liquid obtained in the step (2) with stirring, wherein the total number of moles of the added alkali is 50 to 100 percent of that of rare-earth elements in the rare-earth feed liquid; and (4) after adding the alkaline solution, continuously stirring for a certain time, stopping stirring and standing for a certain time, wherein the solution is separated into an aqueous phase and an organic phase and the aqueous phase is the rare-earth feed liquid from which the aluminum is removed. The method is applied to aluminum removal for the rare-earth feed liquid.
Description
Technical field
The present invention relates to a kind of rare earth feed liquid treatment technology, more particularly, it relates to a kind of method of from rare earth feed liquid, removing aluminium.
Background technology
In the ion adsorption type rare earth ore, REE is to be adsorbed on the clay mineral surface with ionic state.When the leaching ion type rareearth ore, a large amount of aluminum ions get in the leach liquor with rare earth in the clay mineral.When the concentrate of ion adsorption type rare earth ore prepares in early days, adopt the rare earth in the oxalic acid precipitation leach liquor, removed a large amount of non-rare earth impurities that comprise aluminium.Yet ion adsorption type rare earth ore leach liquor oxalic acid precipitation technology is progressively substituted by ammonium bicarbonate precipitation in recent years, though the cost of concentrate preparation is greatly descended, non-rare earth impurities such as the aluminium in the concentrate but do not obtain good pre-separation; Aluminium content is up to 4% (massfraction) in southern ion type rareearth concentrate, and the high hydrolysis easily of aluminium composition causes extraction agent emulsification in the rare earth ore concentrate, has increased difficulty not only for the later separation flow process; And charge capacity is descended, and cause processing power to descend, the separation that also influences rare earth is purified; It extensively distributes in P507-kerosene-hydrochloric acid system segregation section; Quite disperse all has in the outlet of elements such as Pr, Nd, Sm, Eu and to accumulate enrichment in various degree, especially with Nd, Sm for very; Aluminium content accounts for 3% of rare earth weight ratio up to 8g/l in the rare earth feed liquid.Because aluminium is close with rare-earth hydroxide deposition pH, and forms colloid, aluminium has both sexes, so aluminium is difficult to separate with rare earth in the rare earth feed liquid.Produce aluminum removing method upward commonly used at present and mainly contain alkaline process, acid system, hydrolysis method, extraction process etc.(1) alkaline process wherein: because aluminium generates soluble meta-aluminate under the highly basic condition; Rare earth then generates oxyhydroxide; Make aluminium and rare earth reach isolating purpose through leave standstill, filtration etc., but rare earth hydrate be the key in the operation of this method separating of mother liquor.This law is suitable for separating aluminium and rare earth in the rare-earth alkali conversion process, and the baotite alkaline process prepares and promptly comprised this step in the rare earth chloride step, and the effect of removing aluminium is general.(2) acid system: claim oxalate precipitation method again, add in the earth solution, because oxalic acid aluminium solubleness in acidic solution is bigger with oxalic acid; Aluminium is stayed in the solution; It is fine that this method is removed the aluminium effect, is suitable for separating the small amount of aluminum in a large amount of rare earths, and this method generally is used for the final step feed liquid and handles; Owing to need complicated transforming process, process links is many, the removal of impurities cost high, the oxalate solution loss is big, the oxalic acid wastewater treatment is difficult and the shortage practical significance for middle feed liquid.(3) hydrolysis method: the pH value with alkali lye or bicarbonate of ammonia adjustment rare earth feed liquid makes Al
3+Hydrolysis and removing.Because Al
3+With RE
3+The pH value of beginning hydrolysis is just quite approaching, thereby causes aluminium and rare earth hydrolytic precipitation simultaneously, and the gelatinous precipitate subsequent disposal that generates ten minutes difficulty.It is low that this method is removed aluminium efficient, and the rare earth loss is big, therefore can't effectively remove aluminium with hydrolysis method.(4) extraction process: traditional extraction process is that the use volume ratio is that 25% naphthenic acid-20% isooctyl alcohol-kerosene is formed organic phase, adds ammoniacal liquor or sodium hydroxide saponification earlier, and saponification value is 0.35M; Utilize the rare earth feed liquid of single-stage steel basin or multi-stage solvent extraction groove and pH value 3.0 to mix then; It is about 30% that aluminium extracts, but the rare earth extraction loss is greater than 10%, and it is general that this method is removed the aluminium effect; And the necessary strict control of the pH value of rare earth feed liquid, otherwise be prone to cause system emulsification that extraction process can't be carried out.
Summary of the invention
The present invention solves the deficiency that present rare earth feed liquid aluminum removing method exists, and provides a kind of effective except that aluminium, and it is low to remove the aluminium cost, and rare earth yield is high, convenient operation and control, and operation is simple, the rare earth feed liquid aluminum removing method that facility investment is few.
Technical scheme of the present invention is such: a kind of method of from rare earth feed liquid, removing aluminium comprises the steps:
(1) is 15～25% naphthenic acid-15～25% alcohol-kerosene preparation organic phase by volume;
(2) above-mentioned organic phase for preparing and rare earth feed liquid are added in steel basin by volume at 2～5: 1, open and stir, mix;
(3) under agitation condition, in the mixed solution of step (2) gained, add basic soln, the alkali total moles of adding is 50%～100% of a rare earth feed liquid middle-weight rare earths element total moles;
(4) add alkali and finish continued stirring for some time, stop then stirring, leave standstill for some time, solution separating is water and organic phase, and water is except that the rare earth feed liquid behind the aluminium.
Further, above-mentioned a kind ofly from rare earth feed liquid, remove in the method for aluminium, the alcohol described in the step (1) is selected from one of them of octanol or isooctyl alcohol or C8～C10 alcohol mixture; Rare earth feed liquid described in the step (2) is rare earth chloride liquid or sulfuric acid rare earth feed liquid; Basic soln described in the step (3) is one of them of ammoniacal liquor or aqueous sodium hydroxide solution or aqueous sodium carbonate or ammonium bicarbonate aqueous solution, and described basic soln volumetric molar concentration is 3～6mol/L; Churning time described in the step (4) is 10～30 minutes, and time of repose is 10～30 minutes.
Further; Organic phase described in the step (4) is under agitation condition; Regenerate with the acidic solution back extraction; The total moles of acid is 100～150% of a rare earth feed liquid middle-weight rare earths element total moles in the acidic solution that adds, and the regeneration organic phase that obtains recycles, and strip liquor reclaims REE wherein with oxalate precipitation method; Described acidic solution is one of them of hydrochloric acid soln or sulphuric acid soln; Described acidic solution concentration is 3～5mol/L.
The present invention compared with prior art has except that aluminium effectively, and it is low to remove the aluminium cost, and rare earth yield is high, and easy to operate, operation is simple, and facility investment is few, practical advantage.
Embodiment
Below in conjunction with specific embodiment the present invention is described further, but does not constitute any restriction of the present invention.
Embodiment 1
The mishmetal extraction divides into groups to separate post chlorization neodymium feed liquid 2500L, rare earth concentration 1.26mol/L, Al
2O
3Be 8232.2mg/L, containing Neodymium trioxide through calculating Neodymium trichloride feed liquid is 525.63Kg.At first prepare organic phase, organic phase consists of 25% naphthenic acid-25% alcohol mixture-kerosene by volume, and the 5000L organic phase is joined 10M
3In the steel basin; The Neodymium trichloride feed liquid that adds 2500L is opened and is stirred to steel basin, mixes; Under agitation condition, adding 358L concentration is the ammoniacal liquor of 6mol/L; Ammoniacal liquor add finish after, continue to stir and stop after 30 minutes stirring, leave standstill phase-splitting in 30 minutes after, emit water, water is except that the Neodymium trichloride feed liquid behind the aluminium; Under agitation condition, organic phase uses concentration to regenerate as the hydrochloric acid soln back extraction of 716L as 5mol/L, volume, and organic phase recycles, and strip liquor reclaims neodymium with the oxalic acid precipitation method.
Removing and obtaining the Neodymium trichloride material liquid volume behind the aluminium is 2813L, through analyzing and testing: rare earth concentration 1.05 mol/L, Al
2O
3Be 1.2mg/L, containing Neodymium trioxide through calculating Neodymium trichloride feed liquid is 496.8Kg, and promptly rare earth yield is 94.51%, and aluminium clearance 99.98% removes the aluminium cost and is no more than 700 yuan/ton (in Neodymium trioxide).
Embodiment 2
The mishmetal extraction divides into groups to separate post chlorization praseodymium feed liquid 1250L, rare earth concentration 1.22 mol/L, Al
2O
3Be 2453mg/L, containing Praseodymium trioxide through calculating praseodymium chloride feed liquid is 259.56Kg.At first prepare organic phase, organic phase consists of 15% naphthenic acid-15% alcohol mixture-kerosene by volume, and the 5000L organic phase is joined 10M
3In the steel basin; The praseodymium chloride feed liquid that adds 1250L is opened and is stirred to steel basin, mixes; Under agitation condition, adding 280L concentration is the sodium hydroxide solution of 3mol/L; Sodium hydroxide solution add finish after, continue to stir and stop after 30 minutes stirring, leave standstill phase-splitting in 20 minutes after, emit water, water is except that the praseodymium chloride feed liquid behind the aluminium; Under agitation condition, organic phase uses concentration to regenerate as the hydrochloric acid soln back extraction of 400L as 3mol/L, volume, and organic phase recycles, and strip liquor reclaims praseodymium with the oxalic acid precipitation method.
Removing and obtaining the praseodymium chloride material liquid volume behind the aluminium is 1503L, through analyzing and testing: rare earth concentration 0.95mol/L, Al
2O
3＜0.1mg/L, containing Praseodymium trioxide through calculating praseodymium chloride feed liquid is 243.02Kg, and promptly rare earth yield is 93.63%, and aluminium clearance＞99.996% removes the aluminium cost and is no more than 700 yuan/ton (in Praseodymium trioxides).
Embodiment 3
The mishmetal extraction divides into groups to separate post chlorization samarium feed liquid 2000L, rare earth concentration 1.18mol/L, Al
2O
3Be 6723mg/L, containing Samarium trioxide through calculating samarium trichloride feed liquid is 411.58Kg.At first prepare organic phase, organic phase consists of 20% naphthenic acid-20% isooctyl alcohol-kerosene by volume, and the 5000L organic phase is joined 10M
3In the steel basin; The samarium trichloride feed liquid that adds 2000L is opened and is stirred to steel basin, mixes; Under agitation condition, adding 460L concentration is the ammonium bicarbonate aqueous solution of 3mol/L; Ammonium bicarbonate aqueous solution add finish after, continue to stir and stop after 20 minutes stirring, leave standstill phase-splitting in 20 minutes after, emit water, water is except that the samarium trichloride feed liquid behind the aluminium; Under agitation condition, organic phase uses concentration to regenerate as the hydrochloric acid soln back extraction of 700L as 4mol/L, volume, and organic phase recycles, and strip liquor reclaims samarium with the oxalic acid precipitation method.
Removing and obtaining the samarium trichloride material liquid volume behind the aluminium is 2436L, through analyzing and testing: rare earth concentration 0.92 mol/L, Al
2O
3Be 1.1mg/L, containing Samarium trioxide through calculating samarium trichloride feed liquid is 390.85Kg, and promptly rare earth yield is 94.96%, and aluminium clearance 99.98% removes the aluminium cost and is no more than 900 yuan/ton (in Samarium trioxides).
Embodiment 4
Mixed chlorinated rare earth feed liquid 2000L, rare earth concentration 1.52 mol/L, Al
2O
3Be 3533mg/L, through its partition of spectroscopic analysis and calculating, mixed chlorinated rare earth feed liquid include mixed rare earth oxide is 480.32Kg.At first prepare organic phase, organic phase consists of 25% naphthenic acid-25% isooctyl alcohol-kerosene by volume, and the 5000L organic phase is joined 10M
3In the steel basin; The mixed chlorinated rare earth feed liquid that adds 2000L is opened and is stirred to steel basin, mixes; Under agitation condition, adding 380L concentration is the ammoniacal liquor of 6mol/L; Ammoniacal liquor add finish after, continue to stir and stop after 25 minutes stirring, leave standstill phase-splitting in 25 minutes after, emit water, water is except that the mixed chlorinated rare earth feed liquid behind the aluminium; Under agitation condition, organic phase uses concentration to regenerate as the hydrochloric acid soln back extraction of 900L as 5mol/L, volume, and organic phase recycles, and strip liquor reclaims its middle-weight rare earths with the oxalic acid precipitation method.
Removing and obtaining the mixed chlorinated rare earth material liquid volume behind the aluminium is 2351L, through analyzing and testing: rare earth concentration 1.19 mol/L, Al
2O
3＜0.1mg/L is 442.04Kg through calculating mixed chlorinated rare earth feed liquid include mixed rare earth oxide, and promptly rare earth yield is 92.03%, and aluminium clearance＞99.997% removes the aluminium cost and is no more than 900 yuan/ton (in mixed rare-earth oxides).
Embodiment 5
The mishmetal extraction divides into groups to separate back sulfuric acid pr-nd enriched product feed liquid 1500L, rare earth concentration 0.28 mol/L, Al
2O
3Be 3685mg/L, its partition of spectroscopic analysis is Pr
6O
1125.32%, Nd
2O
374.63%, containing the oxidation pr-nd enriched product through calculating sulfuric acid pr-nd enriched product feed liquid is 70.85Kg.At first prepare organic phase, organic phase consists of 18% naphthenic acid-18% isooctyl alcohol-kerosene by volume, and the 5000L organic phase is joined 10M
3In the steel basin; The sulfuric acid pr-nd enriched product feed liquid that adds 1500L is opened and is stirred to steel basin, mixes; Under agitation condition, adding 80L concentration is the sodium hydroxide solution of 5mol/L; Sodium hydroxide solution add finish after, continue to stir and stop after 15 minutes stirring, leave standstill phase-splitting in 15 minutes after, emit water, water is except that the sulfuric acid pr-nd enriched product feed liquid behind the aluminium; Under agitation condition, organic phase uses concentration to regenerate as the sulphuric acid soln back extraction of 150L as 4mol/L, volume, and organic phase recycles, and strip liquor reclaims pr-nd enriched product with the oxalic acid precipitation method.
Removing and obtaining sulfuric acid pr-nd enriched product material liquid volume behind the aluminium is 1562L, through analyzing and testing: rare earth concentration 0.25mol/L, Al
2O
3＜0.1mg/L, containing the oxidation pr-nd enriched product through calculating sulfuric acid pr-nd enriched product feed liquid is 65.88Kg, and promptly rare earth yield is 92.98%, and aluminium clearance＞99.997% removes the aluminium cost and is no more than 700 yuan/ton (in oxidation pr-nd enriched products).
Embodiment 6
Mix sulphur acid rare earth feed liquid 1000L, rare earth concentration 0.32 mol/L, Al
2O
3Be 3826mg/L, through its partition of spectroscopic analysis and calculating, mix sulphur acid rare earth feed liquid include mixed rare earth oxide is 101.12Kg.At first prepare organic phase, organic phase consists of 22% naphthenic acid-22% alcohol mixture-kerosene by volume, and the 3000L organic phase is joined 5M
3In the steel basin; The mix sulphur acid rare earth feed liquid that adds 1000L is opened and is stirred to steel basin, mixes; Under agitation condition, adding 80L concentration is the sodium carbonate solution of 3mol/L; Sodium carbonate solution add finish after, continue to stir and stop after 10 minutes stirring, leave standstill phase-splitting in 10 minutes after, emit water, water is except that the mix sulphur acid rare earth feed liquid behind the aluminium; Under agitation condition, organic phase uses concentration to regenerate as the sulphuric acid soln back extraction of 120L as 4mol/L, volume, and organic phase recycles, and strip liquor reclaims its middle-weight rare earths with the oxalic acid precipitation method.
Removing and obtaining mix sulphur acid rare earth material liquid volume behind the aluminium is 1062L, through analyzing and testing: rare earth concentration 0.28 mol/L, Al
2O
3＜0.1mg/L is 93.97Kg through calculating mix sulphur acid rare earth feed liquid include mixed rare earth oxide, and promptly rare earth yield is 92.93%, and aluminium clearance＞99.997% removes the aluminium cost and is no more than 1000 yuan/ton (in mixed rare-earth oxides).
Show from analytical results: the present invention has except that aluminium effective, and it is low to remove the aluminium cost, and rare earth yield is high, and easy to operate, operation is simple, and facility investment is few, practical characteristics.
Claims (9)
1. a method of from rare earth feed liquid, removing aluminium is characterized in that comprising the steps:
(1) is 15～25% naphthenic acid-15～25% alcohol-kerosene preparation organic phase by volume;
(2) above-mentioned organic phase for preparing and rare earth feed liquid are added in steel basin by volume at 2～5: 1, open and stir, mix;
(3) under agitation condition, in the mixed solution of step (2) gained, add basic soln, the alkali total moles of adding is 50～100% of a rare earth feed liquid middle-weight rare earths element total moles;
(4) add alkali and finish continued stirring for some time, stop then stirring, leave standstill for some time, solution separating is water and organic phase, and water is except that the rare earth feed liquid behind the aluminium.
2. a kind of method of from rare earth feed liquid, removing aluminium according to claim 1 is characterized in that the alcohol described in the step (1) is selected from one of them of octanol or isooctyl alcohol or C8～C10 alcohol mixture.
3. a kind of method of from rare earth feed liquid, removing aluminium according to claim 1 is characterized in that the rare earth feed liquid described in the step (2) is rare earth chloride liquid or sulfuric acid rare earth feed liquid.
4. a kind of method of from rare earth feed liquid, removing aluminium according to claim 1 is characterized in that the basic soln described in the step (3) is one of them of ammoniacal liquor or aqueous sodium hydroxide solution or aqueous sodium carbonate or ammonium bicarbonate aqueous solution.
5. according to claim 1 or 4 described a kind of methods of from rare earth feed liquid, removing aluminium, it is characterized in that described basic soln volumetric molar concentration is 3～6mol/L.
6. a kind of method of from rare earth feed liquid, removing aluminium according to claim 1 is characterized in that the churning time described in the step (4) is 10～30 minutes, and time of repose is 10～30 minutes.
7. a kind of method of from rare earth feed liquid, removing aluminium according to claim 1; It is characterized in that; Organic phase described in the step (4) is under agitation condition, and with acidic solution back extraction regeneration, the total moles of acid is 100～150% of a rare earth feed liquid middle-weight rare earths element total moles in the acidic solution of adding; The regeneration organic phase that obtains recycles, and strip liquor reclaims REE wherein with oxalate precipitation method.
8. a kind of method of from rare earth feed liquid, removing aluminium according to claim 7 is characterized in that described acidic solution is one of them of hydrochloric acid soln or sulphuric acid soln.
9. according to claim 7 or 8 described a kind of methods of from rare earth feed liquid, removing aluminium, it is characterized in that described acidic solution concentration is 3～5mol/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010105477201A CN101979680B (en) | 2010-11-17 | 2010-11-17 | Method for removing aluminum from rare-earth feed liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010105477201A CN101979680B (en) | 2010-11-17 | 2010-11-17 | Method for removing aluminum from rare-earth feed liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101979680A CN101979680A (en) | 2011-02-23 |
| CN101979680B true CN101979680B (en) | 2012-08-15 |
Family
ID=43600219
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010105477201A Active CN101979680B (en) | 2010-11-17 | 2010-11-17 | Method for removing aluminum from rare-earth feed liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101979680B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110438351A (en) * | 2019-08-29 | 2019-11-12 | 中稀(常州)稀土新材料有限公司 | A kind of rare earth impurities separation method |
Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103146921B (en) * | 2013-04-07 | 2014-12-24 | 内蒙古包钢稀土(集团)高科技股份有限公司 | Method for removing aluminum in rare-earth solution |
| CN103343245B (en) * | 2013-07-15 | 2014-05-07 | 福州大学 | Method for removing impurity aluminum in rare earth solution by neutralization-magnetic flocculation-magnetic separation |
| CN103773955B (en) * | 2013-11-04 | 2016-08-31 | 中铝广西有色金源稀土股份有限公司 | A kind of remove the method for aluminium in rare earth feed liquid |
| CN103602812A (en) * | 2013-11-18 | 2014-02-26 | 江西理工大学 | Rare-earth organic extractant and back-extraction process thereof |
| CN103966441A (en) * | 2014-05-08 | 2014-08-06 | 广东省工业技术研究院(广州有色金属研究院) | Method for continuously extracting aluminum from rare earth liquid |
| CN105624440B (en) * | 2016-01-25 | 2017-10-03 | 江西理工大学 | One kind complex-precipitation aluminum removing method from earth solution |
| WO2018147399A1 (en) * | 2017-02-09 | 2018-08-16 | 株式会社Uacj | Method for producing aluminum |
| CN107502762B (en) * | 2017-08-29 | 2022-01-07 | 江西理工大学 | Method for extracting rare earth by one-step precipitation and impurity removal of ionic rare earth leaching mother liquor |
| CN108085493B (en) * | 2017-11-29 | 2019-10-25 | 中铝广西国盛稀土开发有限公司 | A method of impurity in rare earth chloride liquid is removed using batch process |
| CN108642310B (en) * | 2018-05-08 | 2020-02-18 | 江西理工大学 | Method for removing aluminum from rare earth feed liquid by complexing precipitation |
| CN108950251B (en) * | 2018-08-01 | 2021-08-24 | 连云港高品再生资源有限公司 | Method for recovering rare earth elements |
| CN111944998A (en) * | 2020-08-25 | 2020-11-17 | 赣州有色冶金研究所 | Method for removing aluminum from rare earth feed liquid |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1415544A (en) * | 2002-10-31 | 2003-05-07 | 施越群 | Method for producing holmium oxide and erbium oxide |
| CN101168799A (en) * | 2006-10-27 | 2008-04-30 | 胡建康 | Extraction separation method for circularly preparing saponification organic phase rear earth from chloride solvent |
-
2010
- 2010-11-17 CN CN2010105477201A patent/CN101979680B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1415544A (en) * | 2002-10-31 | 2003-05-07 | 施越群 | Method for producing holmium oxide and erbium oxide |
| CN101168799A (en) * | 2006-10-27 | 2008-04-30 | 胡建康 | Extraction separation method for circularly preparing saponification organic phase rear earth from chloride solvent |
Non-Patent Citations (2)
| Title |
|---|
| 李剑虹等.环烷酸萃取体系中稀土和铝分配比及分离系数的研究.《矿冶》.2010,第19卷(第1期),66-69，76. * |
| 贾江涛等.铝在稀土萃取分离流程中的分布及分离方法研究(I).《稀土》.2001,第22卷(第02期),10-13. * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110438351A (en) * | 2019-08-29 | 2019-11-12 | 中稀(常州)稀土新材料有限公司 | A kind of rare earth impurities separation method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101979680A (en) | 2011-02-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101979680B (en) | Method for removing aluminum from rare-earth feed liquid | |
| CN106367622B (en) | It is a kind of using aluminum sulfate as the ion adsorption type re efficient green extracting method of leaching agent | |
| CN101319275B (en) | Process for solvent extraction separation purification of rare earth element | |
| CN102312098B (en) | Method for separation and purification of fluorescent grade yttrium oxide and europium oxide from waste phosphor powder | |
| CN100584967C (en) | Method for separating highly-pure rare-earth oxide from rare earth mine for reinforced baking by sulfuric acid | |
| CN104294063B (en) | The method of low concentration of rare earth solution extraction and recovery rare earth | |
| CN110055423B (en) | Method for enriching platinum group metals and rare earth in spent automobile exhaust purification catalyst | |
| CN106319218A (en) | Method for recovering rare earth, aluminum and silicon from rare earth-containing aluminum and silicon wastes | |
| CN104928475B (en) | A kind of recovery method of the aluminium scrap silicon containing rare earth | |
| CN101886175B (en) | Method for producing diuranate by extracting uranium from rare earth slag containing uranium | |
| CN106282553A (en) | The smelting separation method of Rare Earth Mine | |
| CN108893625B (en) | Process for preparing high-purity lanthanum by extraction method | |
| CN110408777B (en) | Method for extracting metal ions by using fatty acid | |
| BR112019002095B1 (en) | METHOD FOR EXTRACTION, ENRICHMENT AND RECOVERY OF RARE-EARTHS FROM LOW CONCENTRATION OF RARE-EARTH SOLUTIONS | |
| CN109721081B (en) | Method for extracting lithium from lithium-rich fly ash alkaline mother liquor | |
| CN107012342A (en) | A kind of method for extracting low-grade ion type rareearth raw ore rare earth elements | |
| CN111690810B (en) | Red mud recycling-soil treatment method | |
| CN103922383A (en) | Extraction separation method for rare earth and zinc in reverse extraction raffinate obtained in reduction extraction separation of europium | |
| CN116002745A (en) | Method for preparing mixed rare earth oxide from rare earth film enriched liquid | |
| CN103966441A (en) | Method for continuously extracting aluminum from rare earth liquid | |
| CN112662900A (en) | Method for co-recovering rare earth in leaching mother liquor by coprecipitation acid dissolution and selective precipitation | |
| CN108342574B (en) | Countercurrent washing device for rare earth precipitation and method for recycling rare earth oxalic acid precipitation mother liquor and washing liquor by using countercurrent washing device | |
| CN103194627B (en) | Method for removing aluminum in rare earth solution | |
| CN101967558A (en) | Method for preparing saponifier by directly recycling saponification wastewater produced by extraction and separation of rare earth | |
| CN102337405B (en) | Method for applying baotite mixed carbonate-rare earth precipitation wastewater in precipitation of europium (II) sulfate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: 514600 Fuyuan Rare Earth Co., Ltd., Chengxi Village, Dazhe Town, Pingyuan County, Meizhou City, Guangdong Province Patentee after: Guangdong Fuyuan Rare Earth Co.,Ltd. Patentee after: GUANGZHOU Research Institute OF NON FERROUS METALS Address before: 514600 Guangdong Fuyuan Rare Earth New Material Co.,Ltd., Chengxi Village, Dazhe Town, Pingyuan County, Meizhou City, Guangdong Province Patentee before: Guangdong Fuyuan Rare Earth New Material Co.,Ltd. Patentee before: GUANGZHOU Research Institute OF NON FERROUS METALS |
|
| CP03 | Change of name, title or address |