CN1986849A - No-saponifying pre-grouped extraction and separation process of ion adsorbing RE mineral - Google Patents
No-saponifying pre-grouped extraction and separation process of ion adsorbing RE mineral Download PDFInfo
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- CN1986849A CN1986849A CNA2005101347674A CN200510134767A CN1986849A CN 1986849 A CN1986849 A CN 1986849A CN A2005101347674 A CNA2005101347674 A CN A2005101347674A CN 200510134767 A CN200510134767 A CN 200510134767A CN 1986849 A CN1986849 A CN 1986849A
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- 238000000605 extraction Methods 0.000 title claims abstract description 88
- 238000000926 separation method Methods 0.000 title claims abstract description 22
- 229910052500 inorganic mineral Inorganic materials 0.000 title description 4
- 239000011707 mineral Substances 0.000 title description 4
- 239000007788 liquid Substances 0.000 claims abstract description 41
- 238000000034 method Methods 0.000 claims abstract description 15
- 239000000463 material Substances 0.000 claims abstract 4
- 229910052761 rare earth metal Inorganic materials 0.000 claims description 43
- 150000002910 rare earth metals Chemical class 0.000 claims description 35
- 239000003795 chemical substances by application Substances 0.000 claims description 25
- 238000005516 engineering process Methods 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 230000007935 neutral effect Effects 0.000 claims description 8
- -1 2-ethyl Chemical group 0.000 claims description 7
- 239000008346 aqueous phase Substances 0.000 claims description 6
- 229910001404 rare earth metal oxide Inorganic materials 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- LJKDOMVGKKPJBH-UHFFFAOYSA-N 2-ethylhexyl dihydrogen phosphate Chemical compound CCCCC(CC)COP(O)(O)=O LJKDOMVGKKPJBH-UHFFFAOYSA-N 0.000 claims description 2
- 150000002148 esters Chemical class 0.000 claims description 2
- 238000006386 neutralization reaction Methods 0.000 claims 1
- 239000012071 phase Substances 0.000 claims 1
- 239000002253 acid Substances 0.000 abstract description 25
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 abstract description 17
- 239000012074 organic phase Substances 0.000 abstract description 16
- 239000003513 alkali Substances 0.000 abstract description 15
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 7
- 239000012141 concentrate Substances 0.000 abstract description 6
- 229910052688 Gadolinium Inorganic materials 0.000 abstract description 5
- 229910052689 Holmium Inorganic materials 0.000 abstract description 4
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 abstract description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 3
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 3
- 239000011574 phosphorus Substances 0.000 abstract description 3
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 239000002351 wastewater Substances 0.000 abstract 1
- 150000002500 ions Chemical class 0.000 description 10
- 238000007127 saponification reaction Methods 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- 229910052727 yttrium Inorganic materials 0.000 description 6
- 229910052693 Europium Inorganic materials 0.000 description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 description 4
- VWQVUPCCIRVNHF-UHFFFAOYSA-N yttrium atom Chemical compound [Y] VWQVUPCCIRVNHF-UHFFFAOYSA-N 0.000 description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 235000010755 mineral Nutrition 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- HNNQYHFROJDYHQ-UHFFFAOYSA-N 3-(4-ethylcyclohexyl)propanoic acid 3-(3-ethylcyclopentyl)propanoic acid Chemical compound CCC1CCC(CCC(O)=O)C1.CCC1CCC(CCC(O)=O)CC1 HNNQYHFROJDYHQ-UHFFFAOYSA-N 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 description 2
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 description 2
- 229910052691 Erbium Inorganic materials 0.000 description 2
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 235000012538 ammonium bicarbonate Nutrition 0.000 description 2
- 239000001099 ammonium carbonate Substances 0.000 description 2
- OGPBJKLSAFTDLK-UHFFFAOYSA-N europium atom Chemical compound [Eu] OGPBJKLSAFTDLK-UHFFFAOYSA-N 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000012452 mother liquor Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 229910052684 Cerium Inorganic materials 0.000 description 1
- 229910052692 Dysprosium Inorganic materials 0.000 description 1
- 229910052765 Lutetium Inorganic materials 0.000 description 1
- 229910052779 Neodymium Inorganic materials 0.000 description 1
- 229910052777 Praseodymium Inorganic materials 0.000 description 1
- 206010067171 Regurgitation Diseases 0.000 description 1
- 229910052772 Samarium Inorganic materials 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 229910052771 Terbium Inorganic materials 0.000 description 1
- 101000898914 Tetrahymena thermophila (strain SB210) Histone H2A.1 Proteins 0.000 description 1
- 229910052775 Thulium Inorganic materials 0.000 description 1
- 229910052769 Ytterbium Inorganic materials 0.000 description 1
- JJEJDZONIFQNHG-UHFFFAOYSA-N [C+4].N Chemical compound [C+4].N JJEJDZONIFQNHG-UHFFFAOYSA-N 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- SEGLCEQVOFDUPX-UHFFFAOYSA-N di-(2-ethylhexyl)phosphoric acid Chemical compound CCCCC(CC)COP(O)(=O)OCC(CC)CCCC SEGLCEQVOFDUPX-UHFFFAOYSA-N 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 229910052746 lanthanum Inorganic materials 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000012768 molten material Substances 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
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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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- Manufacture And Refinement Of Metals (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The present invention is process of dissolving ion adsorbing RE ore concentrate with the after acid produced in the exchange course of the hydrogen ion of acid phosphorus extractant, such as P507, etc and the RE material liquid. In the separation process, the material liquid is used circularly and Dy/Ho or Gd/Tb pre-separated, so as to reach the aims of reducing hydrochloric acid for dissolving material and extraction separating and liquid ammonia or liquid alkali for saponifying the organic phase, lowering the extracting and separating cost and decreasing waste water exhaust.
Description
Technical field
The invention belongs to field of metallurgy and chemical engineering, relate to southern ore deposit lucium raw material at the technology extraction separating method of the own ester of 2-ethylhexyl phosphoric acid single 2-ethyl (hereinafter to be referred as P507) for extraction agent fractionation extraction grouping separation of rare earth elements.Be particularly useful for adopting extraction agents such as P507 to separate southern ion ore deposit carbonated rare earth or rare earth oxide raw material.
Background technology
China's rare earth resources occupies first place in the world, and wherein southern ion-adsorption type ore is rich in middle heavy rare earths, has higher exploitation and using value.The south ion-adsorption type ore generally adopts solution such as ammonium sulfate, ammonium chloride, after ore deposit or dump leaching are soaked in the original place, adopt ammonium bicarbonate precipitation to obtain the carbonated rare earth concentrate, (related content is consulted patent 01125180.8 to obtain the oxide compound concentrate after calcination, 94110881.3,94102455.5).
In order to carry out extracting and separating, before the art of this patent, the general practice be carbonated rare earth or rare earth oxide concentrate with dissolving with hydrochloric acid after, enter in the extraction tank, use extraction agent to extract, extraction agent at first carries out saponification with ammoniacal liquor or liquid caustic soda, exchange with rare earth feed liquid after the saponification, the organic and rare earth feed liquid of supported rare earth reaches easy collection component and the isolating effect of difficult collection component through multistage exchange, easily the collection component carries out back extraction with hydrochloric acid, easily come together component aqueous phase liquid and blank organic phase.Acid and alkali consumption in the extraction separation process is mainly employed alkali of organic phase saponification (ammonia) and the employed acid of back extraction.The main extraction agent that rare earth grouping is at present used is except that P507, also has di-(2-ethylhexyl)phosphoric acid extraction agents such as (hereinafter to be referred as P204), compare with P204, the P507 extraction agent has higher separation factor, and be easy to back extraction relatively, the separation in the southern ore deposit of difficult back extraction elements such as heavy rare earths in being suitable for containing.The content relevant with P507 separation system isolating ions type ore deposit can be consulted patent documentation 85102210.
In the ionic ore deposit, contain whole 15 kinds of rare earth elements, they in P507 and P204 by the extraction of being come together by difficulty to easy collection are in proper order: La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, Ho, Y, Er, Tm, Yb, Lu.For realizing extracting and separating, need enter organic phase to easy collection component extraction, and the difficulty collection component that collection is gone in the organic phase adopts the mode of washing to stay aqueous phase.For realizing the separation of raw material, back extraction obtained product after each component that easily comes together all needed the process extraction to enter organic phase, the main raw material consumption of extraction process is needed alkali of organic phase saponification or ammoniacal liquor, the hydrochloric acid of dissolved carbon acid rare earth or rare earth oxide concentrate and load organic phases washing, the needed acid of back extraction.Common mineral have rich europium ore deposit of middle yttrium and high yttrium ore deposit, its heavy rare earths (Ho, Y, Er in the ion ore deposit
-Lu) content is all higher, and the heavy rare earths mol ratio accounts for about 40% in the rich europium of the middle yttrium ore deposit, and the heavy rare earths mol ratio is especially up to more than 70% in the high yttrium ore deposit, and the needed acid and alkali consumption of heavy rare earths in the extracting and separating is one of major portion of ion ore deposit extracting and separating consumption.
Patent 92106000.9 has been announced the pre-grouping of way take to(for) the ionic ore deposit, carrying out Dy/Ho earlier separates, after separating most of easily collection component, can increase the treatment capacity of back segment operation, reduce the acid and alkali consumption of last part technology, but because saponification system is adopted in pre-grouping, need equally to consume soda acid, whole acid and alkali consumption can't be starkly lower than traditional technology.
Patent 90107128.5 has been announced the technology that adopts the direct extracting rare-earth mother liquor of naphthenic acid, directly obtain spissated rare earth chloride liquid by back extraction, compare with dissolving rare earth chloride behind the ammonium bicarbonate precipitation, this technology is equivalent to the carbon ammonium that precipitation is used is replaced to the ammoniacal liquor that saponification naphthenic acid organic phase is used, the hydrochloric acid of the use of dissolved carbon acid rare earth replaces to the hydrochloric acid that back extraction is used, and does not therefore have clear superiority with present technical comparing on acid and alkali consumption.
Patent 86105043 has been announced the hydrogen ion that utilizes P204 extraction agent self, and northern ore deposit sulfuric acid rare earth mother liquor is carried out extracting and separating and is the method for rare earth chloride transition.For southern ore deposit, owing to wherein be rich in middle heavy rare earths, and the back extraction of middle heavy rare earths in the P204 system is very difficult, thereby the P204 system can not be applicable to the separation of southern ion type rareearth ore.The middle heavy rare earths back extraction balance acidity of P507 system is lower with respect to the P204 system, can be applicable to the extracting and separating of southern ion type rareearth ore preferably.But the problem that balance acidity is lower is exactly an extraction agent need be added alkaline solution or ammoniacal liquor and carry out can reaching after the saponification and be fit to industrial organic charge capacity, therefore, simply adopt non-saponifying P507 can not effectively separate to southern ion ore deposit rare earth chloride liquid.
Summary of the invention
The objective of the invention is to reduce effectively the acid and alkali consumption cost in the extraction separation process of ion ore deposit.In the extraction separation process of ion ore deposit, acid and alkali consumption is mainly reflected on dissolving raw material and needed acid of extraction agent back extraction and the needed alkali of organic phase saponification.Find suitable method to utilize the contained hydrogen ion of extraction agent to realize that the target of dissolving raw material is a main task of the present invention.
The technical scheme that the present invention solves its technical problem is as follows: when P507 extraction agent and aqueous phase liquid carry out extraction process, following reaction: H takes place
2A
2+ RECl
3=RE (HA
2)+HCl, wherein, H
2A
2Be the molecular formula of writing a Chinese character in simplified form of extraction agent P507 or P204, this reaction is a reversible reaction, in the rare earth extraction process, utilizes forward reaction to make the extraction agent extracting rare-earth, obtains the required load organic phases of extraction process.Get in the collection process counter, utilize backward reaction with the rare earth back extraction in the aqueous solution, obtain reusable blank organic phase.For different rare earth elements, the equilibrium constant of reaction difference, thereby the balance acidity of water is also different.When extraction agent (H2A2) total concn is 0.75mol/L, when the rare earth loaded amount of extraction agent was 0.1mol/L, concentration was the balance acidity in the different earth solutions of 1mol/L, and Gd is about 0.5mol/L, and Dy is about 0.8mol/L, and Y is about 1.2mol/L.In the extraction separation process of routine, in order to make the rare earth loaded of extraction agent, extraction agent need so just increase acid and alkali consumption with exchanging with rare earth after the alkali soapization.In the present invention, use and contain sour water feed liquid dissolved carbon acid rare earth and rare earth oxide mutually after extraction agent carries out extractive reaction, the part feed liquid enters the back segment extraction process, other feed liquid circulation enters this section extraction process and continues to carry out rare earth exchanged with extraction agent, makes extraction agent reach the needed rare earth loaded amount of extracting and separating.Extracting and separating can be carried out the pre-grouping of Dy/Ho or Gd/Tb divides into groups in advance, and after the separation of having carried out most of easy collection component, whole separating technology acid and alkali consumption is minimized.
The invention has the beneficial effects as follows: first, the present invention has effectively utilized the hydrogen ion in the acidic phosphorus extractants such as P507, use it that ionic ore deposit raw material is dissolved, finish the extracting and separating work of most of easily collection component with the required acid consumption of dissolving raw material, thereby saved a large amount of acid and alkali consumptions.The second, the way that adopts the feed liquid circulation to add can be controlled the rare earth loaded of extraction agent, effectively to satisfy the processing requirement of extracting and separating.The 3rd, the present invention utilizes the acidic phosphorus extractants such as P507 that generally use in the extraction and separation technology of southern ore deposit, extraction system is identical with existing extraction system, and extraction and support equipment are not had particular requirement, adopts the existing extraction and stripping apparatus required production line of improvement cost patent at an easy rate.
Description of drawings
Below in conjunction with drawings and Examples this patent is further specified.
Fig. 1 is a process flow sheet of the present invention
1. extraction tanks among the figure, 2. blank organic phase, the multistage inlet of 3. neutral feed liquid, 4. back extraction acid 5. contains the multistage outlet of sour feed liquid, 6. carbonate or oxide dissolution reactor, 7. stripping section outlet 8. enters the difficulty collection component outlet of hypomere operation, 9. washing section three outlets.
Embodiment
In Fig. 1, front end at extraction tank [1] adds blank organic phase [2], the nearly neutral feed liquid of the multistage adding of extraction section [3], back segment adds sour regurgitation [4], the multistage extraction section of drawing of leading portion goes out to suck sour feed liquid [5], contain sour feed liquid [5] and react with carbonated rare earth or rare earth oxide concentrate in molten material equipment [6], nearly neutral feed liquid [3] circulation adds in the extraction tank behind the dissolving raw material.In the washing section outlet [7] is the easy collection component that back extraction obtains, and chooses suitable progression output aqueous phase liquid [8] in the extraction section, enters follow-up extracting and separating operating process.According to the needs of technology, can also open three outlets [9] at washing section, obtain the middle rare earth component of enrichment.
Claims (5)
1. non-saponifying pre-grouped extraction and separation process of ion type rareearth ore is characterized by:
A. extraction process uses non-saponifying extraction agent to carry out the ion type rareearth ore separation, and extraction agent includes but not limited to the own ester of 2-ethylhexyl phosphoric acid single 2-ethyl (P507);
B. use a part in extraction process with extraction agent contacted contain sour water mutually feed liquid carry out the dissolving of carbonated rare earth or rare earth oxide raw material, the acidity scope that contains sour water phase feed liquid is 0.1
-4.0mol/L.
2. the extraction separating method described in claim 1, it is characterized by acidity behind the dissolving rare earths material and add in the extraction process less than the near neutral feed liquid part circulation of 0.3mol/L and carry out extractive reaction, another part contains sour feed liquid and outputs to the back segment separating technology further separate after neutralization.
3. as extraction separating method as described in claim 1 and 2, it is characterized by extraction process and comprise three sections of extraction section, washing section and stripping sections.
4. as extraction separating method as described in claim 1 and 2, it is characterized by the mode that extraction process adds aqueous phase liquid and output aqueous phase liquid is multistage charging, and multistage output can increase the input and output mouth according to the actual process needs.
5. as extraction separating method as described in claim 1 and 2, it is characterized by the separation of being carried out and include but not limited to that Gd/TbDy/Ho separates or Dy/Ho separates.
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| CNB2005101347674A CN100417734C (en) | 2005-12-21 | 2005-12-21 | No-saponifying pre-grouped extraction and separation process of ion adsorbing RE mineral |
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|---|---|---|---|
| CNB2005101347674A CN100417734C (en) | 2005-12-21 | 2005-12-21 | No-saponifying pre-grouped extraction and separation process of ion adsorbing RE mineral |
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| Publication Number | Publication Date |
|---|---|
| CN1986849A true CN1986849A (en) | 2007-06-27 |
| CN100417734C CN100417734C (en) | 2008-09-10 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102191381A (en) * | 2010-03-19 | 2011-09-21 | 上海健达化工有限公司 | Method for removing calcium and manganese from nickel sulfate solution without saponification extraction |
| CN103526055A (en) * | 2013-10-09 | 2014-01-22 | 南昌航空大学 | Process for grouping quasi-fractionated extraction of neodymium/samarium through bastnaesite |
| CN104451191A (en) * | 2014-12-03 | 2015-03-25 | 紫金矿业集团股份有限公司 | Dilution extraction process capable of improving copper recovery rate |
| CN105256155A (en) * | 2015-10-20 | 2016-01-20 | 江西农业大学 | Method for extraction separation of ion rare earth ore through load organic phase of extraction separation light rare earth ore |
| CN112126802A (en) * | 2020-08-14 | 2020-12-25 | 南昌大学 | Rare earth alkaline precipitation, conversion, decomposition and separation method |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1060876A (en) * | 1991-11-05 | 1992-05-06 | 冶金工业部包头稀土研究院 | The preparation method of Samarium trioxide |
| CN1099072A (en) * | 1993-08-20 | 1995-02-22 | 清华大学 | Extraction process extracts the method for rare earth from the rare-earth mineral leach liquor |
| CN1131326C (en) * | 1999-02-12 | 2003-12-17 | 通用电气公司 | Technological process for directly producing mixed rare earth oxide |
-
2005
- 2005-12-21 CN CNB2005101347674A patent/CN100417734C/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102191381A (en) * | 2010-03-19 | 2011-09-21 | 上海健达化工有限公司 | Method for removing calcium and manganese from nickel sulfate solution without saponification extraction |
| CN102191381B (en) * | 2010-03-19 | 2013-01-02 | 启东市北新无机化工有限公司 | Method for removing calcium and manganese from nickel sulfate solution without saponification extraction |
| CN103526055A (en) * | 2013-10-09 | 2014-01-22 | 南昌航空大学 | Process for grouping quasi-fractionated extraction of neodymium/samarium through bastnaesite |
| CN103526055B (en) * | 2013-10-09 | 2014-12-03 | 南昌航空大学 | Process for grouping quasi-fractionated extraction of neodymium/samarium through bastnaesite |
| CN104451191A (en) * | 2014-12-03 | 2015-03-25 | 紫金矿业集团股份有限公司 | Dilution extraction process capable of improving copper recovery rate |
| CN105256155A (en) * | 2015-10-20 | 2016-01-20 | 江西农业大学 | Method for extraction separation of ion rare earth ore through load organic phase of extraction separation light rare earth ore |
| CN105256155B (en) * | 2015-10-20 | 2017-10-10 | 江西农业大学 | The load organic phases of extract and separate light rare earth ore deposit are used for the method for ion Rare Earth Mine extract and separate |
| CN112126802A (en) * | 2020-08-14 | 2020-12-25 | 南昌大学 | Rare earth alkaline precipitation, conversion, decomposition and separation method |
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| CN100417734C (en) | 2008-09-10 |
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