CN104649320A - Method of preparing vanadate of alkali metal from residue of aluminum powder vanadium removal of crude titanium tetrachloride - Google Patents
Method of preparing vanadate of alkali metal from residue of aluminum powder vanadium removal of crude titanium tetrachloride Download PDFInfo
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- CN104649320A CN104649320A CN201310589810.0A CN201310589810A CN104649320A CN 104649320 A CN104649320 A CN 104649320A CN 201310589810 A CN201310589810 A CN 201310589810A CN 104649320 A CN104649320 A CN 104649320A
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Abstract
The invention relates to a method of preparing vanadate of alkali metals from a residue of aluminum powder vanadium removal of crude titanium tetrachloride. The method includes following steps: (1) performing oxidizing leaching to the residue of the aluminum powder vanadium removal of the crude titanium tetrachloride in an alkaline solution, and performing liquid-solid separation to the leached substance; (2) performing precipitation to remove aluminum and evaporate-crystallization separation of chlorides to the leached liquid to obtain an alkaline solution of the vanadate of alkali metals; and (3) cooling and crystallizing the alkaline solution to prepare a vanadate crystal. The method not only achieves full reuse of waste materials but also can prepare a product of the vanadate of alkali metals being higher than 90% in purity.
Description
Technical field
The present invention relates to a kind of hydrometallurgy or solid waste substance treating method, particularly relate to from crude titanic chloride aluminium powder except reclaiming vanadium in vanadium slag and preparing the method for alkali metal vanadate.
Background technology
Crude titanic chloride aluminium powder, except the crude titanic chloride that vanadium slag is produced for the chlorination process slag produced that uses aluminium powder to remove vanadium, is TiCl
4one of production process typical solid waste.In chloride processes, the V in titanium slag
2o
5be chlorinated and generate VOCl
3.After add aluminium powder in crude titanic chloride, titanium tetrachloride can react with aluminium powder and produce TiCl
3, the aluminum chloride of the wherein oxidized rear generation of aluminium can play the effect of this reaction of catalysis.TiCl
3get final product and VOCl
3react and generate precipitation VOCl
2, thus realize removing of vanadium, primitive reaction formula is as follows:
Aluminum reduction TiCl
4:
TiCl
3except vanadium: VOCl
3(l)+TiCl
3(l) → VOCl
2(s)+TiCl
4(l)
The VOCl generated
2be separated with the form of residue at the bottom of still with the impurity that other distills, rectifying produces, owing to also containing most TiCl in residue
4, evaporating concentrating method need be adopted to recycle, be evaporated TiCl
4rear remaining residue is VOCl
2and other solid impurity, namely this slag is called that crude titanic chloride aluminium powder is except vanadium slag.
Crude titanic chloride aluminium powder is about 3% ~ 6% except elemental vanadium content in vanadium slag, has higher recovery value.Meanwhile, crude titanic chloride aluminium powder contains a large amount of chlorions except in vanadium slag, and in the process of storing up, easily discharge the obnoxious flavoures such as hydrogenchloride, environmental pollution is serious.
At present, for crude titanic chloride aluminium powder except the comprehensive utilization of vanadium slag there is not yet the documentation & info report of laboratory study, industrial test or industrial applications both at home and abroad.
Summary of the invention
A kind of removing in vanadium slag from crude titanic chloride aluminium powder is the object of the present invention is to provide to reclaim vanadium and the method preparing alkali metal vanadate.By crude titanic chloride aluminium powder except vanadium slag carries out Oxidation Leaching in alkaline solution, the tetravalence vanadium wherein in dichloro vanadyl is oxidized to pentavalent vanadium, and forms water miscible vanadate, and the aluminium simultaneously in slag is converted into meta-aluminate, and chlorion forms villaumite after leaching.After material carries out solid-liquor separation after leaching, carry out precipitation except aluminium to leach liquor, employing silicate is precipitation agent, and meta-aluminate and silicate can be made to generate insoluble silico-aluminate, thus realizes the object removing aluminium.Evaporative crystallization is carried out to the leach liquor after aluminium and separates out chlorine salt crystal, achieve being separated of villaumite and alkali metal vanadate simultaneously, the feature then utilizing alkali metal vanadate solubleness to decline to a great extent along with temperature reduction, prepares alkali metal vanadate crystal to evaporative crystallization mother liquor crystallisation by cooling.
For reaching above-mentioned purpose, the present invention adopts following technical scheme:
From crude titanic chloride aluminium powder except the method preparing alkali metal vanadate in vanadium slag, comprise the following steps:
(1) crude titanic chloride aluminium powder is placed in basic solution except vanadium slag, and adds oxygenant and carry out Oxidation Leaching, the slurry after leaching obtains filter cake and leach liquor after filtering respectively;
(2) add silicate in the leach liquor obtained in step (1), reacted slurries filtration obtains sial slag and except aluminium leach liquor;
(3) what evaporative crystallization steps (2) obtained removes aluminium leach liquor, is separated by crystal obtains villaumite and evaporative crystallization mother liquor with mother liquor;
(4) the evaporative crystallization mother liquor that step (3) obtains is carried out crystallisation by cooling, alkali metal vanadate and crystallisation by cooling mother liquor are obtained to crystallisation by cooling pulp separation.
As optimal technical scheme, method of the present invention, comprises the following steps:
(1) crude titanic chloride aluminium powder is placed in basic solution except vanadium slag, and adds oxygenant and carry out Oxidation Leaching, the slurry after leaching obtains filter cake and leach liquor after filtering respectively;
(2) steam condensate that the filter cake step (4) obtained step (1) obtains carries out countercurrent washing, obtains washings and finishing slag respectively after filtering;
(3) add silicate in the leach liquor obtained in step (1), reacted slurries filtration obtains sial slag and except aluminium leach liquor;
(4) washings that obtains of evaporative crystallization steps (2) and step (3) obtain except aluminium leach liquor, be separated with mother liquor by crystal and obtain villaumite and evaporative crystallization mother liquor, the steam condensate wherein produced returns step (2) for filter cake washing;
(5) the evaporative crystallization mother liquor that step (4) obtains is carried out crystallisation by cooling, obtain alkali metal vanadate and crystallisation by cooling mother liquor to crystallisation by cooling pulp separation, crystallisation by cooling mother liquor returns step (1) and carries out Oxidation Leaching as basic solution.The program can make raw material be recycled, and has saved resource, has reduced production cost.
As optimal technical scheme, method of the present invention, the basic solution described in step (1) is sodium hydroxide solution, potassium hydroxide solution, sodium carbonate solution or solution of potassium carbonate;
Preferably, the mass concentration of described basic solution is 10% ~ 50%, such as, be 12%, 16%, 20%, 24%, 28%, 33%, 36%, 39%, 44%, 48% etc., is preferably 15% ~ 40%, more preferably 15% ~ 25%;
Preferably, described basic solution and crude titanic chloride aluminium powder are except the volume mass of vanadium slag is than being 1:1 ~ 10:1L/kg, be such as 1.5:1L/kg, 2.2:1L/kg, 2.5:1L/kg, 3.0:1L/kg, 5.0:1L/kg, 7.0:1L/kg, 9.0:1L/kg etc., be preferably 2:1 ~ 8:1L/kg, more preferably 2:1 ~ 6:1L/kg.
Preferably, the oxygenant described in step (1) is the one kind or two or more mixture in air, oxygen, ozone, sodium peroxide or hydrogen peroxide.
Preferably, the temperature leached described in step (1) is 20 ~ 180 DEG C, be such as 25 DEG C, 30 DEG C, 45 DEG C, 55 DEG C, 66 DEG C, 80 DEG C, 100 DEG C, 110 DEG C, 140 DEG C, 160 DEG C, 175 DEG C etc., preferred normal temperature ~ 150 DEG C, further preferred normal temperature ~ 120 DEG C; The time of described leaching is 0.5 ~ 6h, such as, be 0.8h, 1.2h, 1.5h, 2.2h, 3.1h, 4.5h, 5.5h etc., preferably 0.5 ~ 4h, further preferred 1 ~ 3h.
As optimal technical scheme, method of the present invention, the countercurrent washing progression described in step (2) is 2 ~ 6 grades, such as, be 4 grades, 5 grades, is preferably 3 grades;
Preferably, the liquid-solid volume mass of described washing than being 1.5:1 ~ 8:1L/kg, such as, is 1.7:1L/kg, 2.2:1L/kg, 2.5:1L/kg, 3.0:1L/kg, 7.0:1L/kg, 7.5:1L/kg etc., preferred 2:1 ~ 5:1L/kg, more preferably 2:1 ~ 4:1L/kg.
As optimal technical scheme, method of the present invention, described silicate is water glass and/or potassium silicate, such as, can be water glass or potassium silicate, or be the mixture of water glass and potassium silicate.
As optimal technical scheme, method of the present invention, the temperature of described evaporative crystallization is 60 ~ 120 DEG C, such as, be 63 DEG C, 69 DEG C, 75 DEG C, 81 DEG C, 88 DEG C, 95 DEG C, 100 DEG C, 108 DEG C, 115 DEG C etc., is preferably 80 DEG C.
As optimal technical scheme, method of the present invention, the terminal temperature of described crystallisation by cooling is 10 ~ 40 DEG C, such as, be 12 DEG C, 16 DEG C, 19 DEG C, 22 DEG C, 26 DEG C, 30 DEG C, 33 DEG C, 37 DEG C, 39 DEG C etc., is preferably normal temperature.
As optimal technical scheme, method of the present invention, described is separated into centrifugation.
The present invention can realize the efficiency utilization of multi-component separation and vanadium, and achieves the removing toxic substances of hazardous solid waste, has industrial operability.Both made refuse be fully used, the alkali metal vanadate product of purity more than 90% can have been obtained again.
Accompanying drawing explanation
Fig. 1 is except the process flow sheet preparing alkali metal vanadate in vanadium slag from crude titanic chloride aluminium powder.
Embodiment
For ease of understanding the present invention, it is as follows that the present invention enumerates embodiment.Those skilled in the art should understand, described embodiment only understands the present invention for helping, and should not be considered as concrete restriction of the present invention.
Embodiment 1
Crude titanic chloride aluminium powder used except vanadium slag composition and massfraction as shown in table 1.
Table 1
| V | Al | Cl | Fe | Ti | Ca | Mg |
| 2.7% | 15.1% | 28% | 8.4% | 4.2% | 1.6% | 2.0% |
By the crude titanic chloride aluminium powder of above-mentioned composition except vanadium slag is placed in the sodium hydroxide solution that concentration is 10%, the volume mass ratio (L/kg) removing vanadium slag at sodium hydroxide solution and crude titanic chloride aluminium powder is 2:1, extraction temperature is normal temperature, oxygenant is leach 6h under the condition of ozone, and the leaching yield having leached rear V is 98%.By the slurries filtration after leaching, and carry out 2 stage countercurrent washings with secondary steam water of condensation to filter cake, the liquid-solid volume mass of washing process is than being 5:1L/kg, and obtain washings and finishing slag after filtration, in finishing slag, V content is 0.3%; The precipitin reaction that water glass carries out aluminium is added, to obtaining sial slag after reacted slurries filtration respectively and removing aluminium leach liquor in leach liquor; To except aluminium leach liquor and washings evaporative crystallization at 60 DEG C, and carry out centrifugation to crystal and mother liquor and obtain sodium chloride crystal and the evaporative crystallization mother liquor that purity is 86% respectively, the secondary steam water of condensation that wherein this step produces returns for filter cake washing; Be cooled to 10 DEG C to evaporative crystallization mother liquor, carry out centrifugation and obtain vanadic acid sodium crystal and crystallisation by cooling mother liquor respectively, crystallisation by cooling mother is cycled to used in the leaching of slag, and the purity of vanadic acid sodium crystal is 91%.
Embodiment 2
Crude titanic chloride aluminium powder used except vanadium slag composition and massfraction as shown in table 2.
Table 2
| V | Al | Cl | Fe | Ti | Ca | Mg |
| 2.7% | 15.1% | 28% | 8.4% | 4.2% | 1.6% | 2.0% |
By the crude titanic chloride aluminium powder of above-mentioned composition except vanadium slag is placed in the potassium hydroxide solution that concentration is 15%, the volume mass ratio (L/kg) removing vanadium slag at potassium hydroxide solution and crude titanic chloride aluminium powder is 1:1, extraction temperature is 20 DEG C, oxygenant is leach 4h under the condition of hydrogen peroxide, and the leaching yield having leached rear V is 99%.By the slurries filtration after leaching, and carry out 2 stage countercurrent washings with secondary steam water of condensation to filter cake, the liquid-solid volume mass of washing process is than being 8:1L/kg, and obtain washings and finishing slag after filtration, in finishing slag, V content is 0.3%; The precipitin reaction that potassium silicate carries out aluminium is added, to obtaining sial slag after reacted slurries filtration respectively and removing aluminium leach liquor in leach liquor; To except aluminium leach liquor and washings evaporative crystallization at 120 DEG C, and carry out centrifugation to crystal and mother liquor and obtain potassium chloride and the evaporative crystallization mother liquor that purity is 90% respectively, the secondary steam water of condensation that wherein this step produces returns for filter cake washing; Be cooled to 40 DEG C to evaporative crystallization mother liquor, carry out centrifugation and obtain potassium vanadate crystal and crystallisation by cooling mother liquor respectively, crystallisation by cooling mother is cycled to used in the leaching of slag, and the purity of potassium vanadate crystal is 90%.
Embodiment 3
Crude titanic chloride aluminium powder used except vanadium slag composition and massfraction as shown in table 3.
Table 3
| V | Al | Cl | Fe | Ti | Ca | Mg |
| 2.7% | 15.1% | 28% | 8.4% | 4.2% | 1.6% | 2.0% |
By the crude titanic chloride aluminium powder of above-mentioned composition except vanadium slag is placed in the sodium hydroxide solution that concentration is 25%, the volume mass ratio (L/kg) removing vanadium slag at sodium hydroxide solution and crude titanic chloride aluminium powder is 6:1, extraction temperature is 120 DEG C, oxygenant is leach 0.5h under the condition of sodium peroxide, and the leaching yield having leached rear V is 99%.By the slurries filtration after leaching, and carry out 3 stage countercurrent washings with secondary steam water of condensation to filter cake, the liquid-solid volume mass of washing process is than being 4:1L/kg, and obtain washings and finishing slag after filtration, in finishing slag, V content is 0.2%; The precipitin reaction that water glass carries out aluminium is added, to obtaining sial slag after reacted slurries filtration respectively and removing aluminium leach liquor in leach liquor; To except aluminium leach liquor and washings evaporative crystallization at 80 DEG C, and carry out centrifugation to crystal and mother liquor and obtain sodium chloride crystal and the evaporative crystallization mother liquor that purity is 90% respectively, the secondary steam water of condensation that wherein this step produces returns for filter cake washing; Be cooled to normal temperature to evaporative crystallization mother liquor, carry out centrifugation and obtain vanadic acid sodium crystal and crystallisation by cooling mother liquor respectively, crystallisation by cooling mother is cycled to used in the leaching of slag, and the purity of vanadic acid sodium crystal is 95%.
Embodiment 4
Crude titanic chloride aluminium powder used except vanadium slag composition and massfraction as shown in table 4.
Table 4
| V | Al | Cl | Fe | Ti | Ca | Mg |
| 2.7% | 15.1% | 28% | 8.4% | 4.2% | 1.6% | 2.0% |
By the crude titanic chloride aluminium powder of above-mentioned composition except vanadium slag is placed in the sodium carbonate solution that concentration is 50%, the volume mass ratio (L/kg) removing vanadium slag at sodium carbonate solution and crude titanic chloride aluminium powder is 10:1, extraction temperature is 180 DEG C, oxygenant is leach 3h under the condition of oxygen, and the leaching yield having leached rear V is 96%.By the slurries filtration after leaching, and carry out 6 stage countercurrent washings with secondary steam water of condensation to filter cake, the liquid-solid volume mass of washing process is than being 1.5:1L/kg, and obtain washings and finishing slag after filtration, in finishing slag, V content is 0.4%; The precipitin reaction that water glass carries out aluminium is added, to obtaining sial slag after reacted slurries filtration respectively and removing aluminium leach liquor in leach liquor; To except aluminium leach liquor and washings evaporative crystallization at 80 DEG C, and carry out centrifugation to crystal and mother liquor and obtain sodium chloride crystal and the evaporative crystallization mother liquor that purity is 85% respectively, the secondary steam water of condensation that wherein this step produces returns for filter cake washing; Be cooled to normal temperature to evaporative crystallization mother liquor, carry out centrifugation and obtain vanadic acid sodium crystal and crystallisation by cooling mother liquor respectively, crystallisation by cooling mother is cycled to used in the leaching of slag, and the purity of vanadic acid sodium crystal is 90%.
Embodiment 5
Crude titanic chloride aluminium powder used except vanadium slag composition and massfraction as shown in table 5.
Table 5
| V | Al | Cl | Fe | Ti | Ca | Mg |
| 2.7% | 15.1% | 28% | 8.4% | 4.2% | 1.6% | 2.0% |
By the crude titanic chloride aluminium powder of above-mentioned composition except vanadium slag is placed in the solution of potassium carbonate that concentration is 40%, the volume mass ratio (L/kg) removing vanadium slag at solution of potassium carbonate and crude titanic chloride aluminium powder is 8:1, extraction temperature is 150 DEG C, oxygenant is leach 1h under the condition of air, and the leaching yield having leached rear V is 96%.By the slurries filtration after leaching, and carry out 6 stage countercurrent washings with secondary steam water of condensation to filter cake, the liquid-solid volume mass of washing process is than being 2:1L/kg, and obtain washings and finishing slag after filtration, in finishing slag, V content is 0.4%; The precipitin reaction that potassium silicate carries out aluminium is added, to obtaining sial slag after reacted slurries filtration respectively and removing aluminium leach liquor in leach liquor; To except aluminium leach liquor and washings evaporative crystallization at 80 DEG C, and carry out centrifugation to crystal and mother liquor and obtain potassium chloride and the evaporative crystallization mother liquor that purity is 85% respectively, the secondary steam water of condensation that wherein this step produces returns for filter cake washing; Be cooled to normal temperature to evaporative crystallization mother liquor, carry out centrifugation and obtain potassium vanadate crystal and crystallisation by cooling mother liquor respectively, crystallisation by cooling mother is cycled to used in the leaching of slag, and the purity of potassium vanadate crystal is 95%.
Applicant states, the present invention illustrates detailed process equipment and process flow process of the present invention by above-described embodiment, but the present invention is not limited to above-mentioned detailed process equipment and process flow process, namely do not mean that the present invention must rely on above-mentioned detailed process equipment and process flow process and could implement.Person of ordinary skill in the field should understand, any improvement in the present invention, to equivalence replacement and the interpolation of ancillary component, the concrete way choice etc. of each raw material of product of the present invention, all drops within protection scope of the present invention and open scope.
Claims (10)
1. remove the method preparing alkali metal vanadate in vanadium slag from crude titanic chloride aluminium powder, comprise the following steps:
(1) crude titanic chloride aluminium powder is placed in basic solution except vanadium slag, and adds oxygenant and carry out Oxidation Leaching, the slurry after leaching obtains filter cake and leach liquor after filtering respectively;
(2) add silicate in the leach liquor obtained in step (1), reacted slurries filtration obtains sial slag and except aluminium leach liquor;
(3) what evaporative crystallization steps (2) obtained removes aluminium leach liquor, is separated by crystal obtains villaumite and evaporative crystallization mother liquor with mother liquor;
(4) the evaporative crystallization mother liquor that step (3) obtains is carried out crystallisation by cooling, alkali metal vanadate and crystallisation by cooling mother liquor are obtained to crystallisation by cooling pulp separation.
2. method according to claim 1, is characterized in that, said method comprising the steps of:
(1) crude titanic chloride aluminium powder is placed in basic solution except vanadium slag, and adds oxygenant and carry out Oxidation Leaching, the slurry after leaching obtains filter cake and leach liquor after filtering respectively;
(2) steam condensate that the filter cake step (4) obtained step (1) obtains carries out countercurrent washing, obtains washings and finishing slag respectively after filtering;
(3) add silicate in the leach liquor obtained in step (1), reacted slurries filtration obtains sial slag and except aluminium leach liquor;
(4) washings that obtains of evaporative crystallization steps (2) and step (3) obtain except aluminium leach liquor, be separated with mother liquor by crystal and obtain villaumite and evaporative crystallization mother liquor, the steam condensate wherein produced returns step (2) for filter cake washing;
(5) the evaporative crystallization mother liquor that step (4) obtains is carried out crystallisation by cooling, obtain alkali metal vanadate and crystallisation by cooling mother liquor to crystallisation by cooling pulp separation, crystallisation by cooling mother liquor returns step (1) and carries out Oxidation Leaching as basic solution.
3. method according to claim 1 and 2, is characterized in that, the basic solution described in step (1) is sodium hydroxide solution, potassium hydroxide solution, sodium carbonate solution or solution of potassium carbonate;
Preferably, the mass concentration of described basic solution is 10% ~ 50%, is preferably 15% ~ 40%, more preferably 15% ~ 25%;
Preferably, described basic solution and crude titanic chloride aluminium powder, except the volume mass of vanadium slag is than being 1:1 ~ 10:1L/kg, are preferably 2:1 ~ 8:1L/kg, more preferably 2:1 ~ 6:1L/kg.
4. method according to claim 1 and 2, is characterized in that, the oxygenant described in step (1) is the one kind or two or more mixture in air, oxygen, ozone, sodium peroxide or hydrogen peroxide.
5. method according to claim 1 and 2, is characterized in that, the temperature leached described in step (1) is 20 ~ 180 DEG C, preferred normal temperature ~ 150 DEG C, further preferred normal temperature ~ 120 DEG C; The time of described leaching is 0.5 ~ 6h, preferably 0.5 ~ 4h, further preferred 1 ~ 3h.
6. method according to claim 2, is characterized in that, the countercurrent washing progression described in step (2) is 2 ~ 6 grades, is preferably 3 grades;
Preferably, the liquid-solid volume mass of described washing is than being 1.5:1 ~ 8:1L/kg, preferred 2:1 ~ 5:1L/kg, more preferably 2:1 ~ 4:1L/kg.
7. method according to claim 1 and 2, is characterized in that, described silicate is water glass and/or potassium silicate.
8. method according to claim 1 and 2, is characterized in that, the temperature of described evaporative crystallization is 60 ~ 120 DEG C, is preferably 80 DEG C.
9. method according to claim 1 and 2, is characterized in that, the terminal temperature of described crystallisation by cooling is 10 ~ 40 DEG C, is preferably normal temperature.
10. method according to claim 1 and 2, is characterized in that, described is separated into centrifugation.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310589810.0A CN104649320B (en) | 2013-11-20 | 2013-11-20 | From crude titanic chloride aluminium powder except the method preparing alkali metal vanadate in vanadium slag |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310589810.0A CN104649320B (en) | 2013-11-20 | 2013-11-20 | From crude titanic chloride aluminium powder except the method preparing alkali metal vanadate in vanadium slag |
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| CN104649320A true CN104649320A (en) | 2015-05-27 |
| CN104649320B CN104649320B (en) | 2016-09-28 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107032400A (en) * | 2017-04-27 | 2017-08-11 | 攀钢集团研究院有限公司 | TiCl4Tailings alkali soak is refined for the method for high-purity vanadium oxide |
| WO2023142674A1 (en) * | 2022-01-29 | 2023-08-03 | 广东邦普循环科技有限公司 | Method for removing aluminum from strong alkali solution and application thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1394024A (en) * | 1973-02-13 | 1975-05-14 | Tsnii Chernoj Metallurg | Method of recovering vanadium values from a vanadiumcontaining material |
| CN101113495A (en) * | 2006-07-27 | 2008-01-30 | 张荣禄 | Method for extracting iron titanium vanadium from high-titanium iron concentrate |
| CN102732727A (en) * | 2012-05-23 | 2012-10-17 | 河北钢铁股份有限公司承德分公司 | Method for extracting vanadium from high vanadium-sodium-aluminum-silicon slag |
| CN103276218A (en) * | 2013-06-05 | 2013-09-04 | 周长祥 | Method for recycling vanadium from vanadium-containing electrolysis aluminum slag ash |
-
2013
- 2013-11-20 CN CN201310589810.0A patent/CN104649320B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1394024A (en) * | 1973-02-13 | 1975-05-14 | Tsnii Chernoj Metallurg | Method of recovering vanadium values from a vanadiumcontaining material |
| CN101113495A (en) * | 2006-07-27 | 2008-01-30 | 张荣禄 | Method for extracting iron titanium vanadium from high-titanium iron concentrate |
| CN102732727A (en) * | 2012-05-23 | 2012-10-17 | 河北钢铁股份有限公司承德分公司 | Method for extracting vanadium from high vanadium-sodium-aluminum-silicon slag |
| CN103276218A (en) * | 2013-06-05 | 2013-09-04 | 周长祥 | Method for recycling vanadium from vanadium-containing electrolysis aluminum slag ash |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107032400A (en) * | 2017-04-27 | 2017-08-11 | 攀钢集团研究院有限公司 | TiCl4Tailings alkali soak is refined for the method for high-purity vanadium oxide |
| CN107032400B (en) * | 2017-04-27 | 2019-01-22 | 攀钢集团研究院有限公司 | TiCl4The method that purification tailings alkali is soaked standby high-purity vanadium oxide |
| WO2023142674A1 (en) * | 2022-01-29 | 2023-08-03 | 广东邦普循环科技有限公司 | Method for removing aluminum from strong alkali solution and application thereof |
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| CN104649320B (en) | 2016-09-28 |
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