WO2015004375A1 - Procédé de purification du niobium et/ou du tantale - Google Patents
Procédé de purification du niobium et/ou du tantale Download PDFInfo
- Publication number
- WO2015004375A1 WO2015004375A1 PCT/FR2014/051741 FR2014051741W WO2015004375A1 WO 2015004375 A1 WO2015004375 A1 WO 2015004375A1 FR 2014051741 W FR2014051741 W FR 2014051741W WO 2015004375 A1 WO2015004375 A1 WO 2015004375A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- niobium
- tantalum
- solid
- concentrate
- ore
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B34/00—Obtaining refractory metals
- C22B34/20—Obtaining niobium, tantalum or vanadium
- C22B34/24—Obtaining niobium or tantalum
Definitions
- the present invention relates to the purification of niobium and / or tantalum contained in an ore or concentrate. It also relates to obtaining niobium and / or tantalum of high purity with a high yield.
- Tantalum and niobium are metals with a very high resistance to heat and corrosion and are used industrially very broadly in metal alloys.
- recently the demand for niobium and / or pure tantalum has increased due to their use inter alia in electrodes or optical components.
- niobium (Nb) and tantalum (Ta) are often associated in complex minerals, such as pyrochlore, colombite, tantalite, colombo-tantalite and loparite. Ores or ore concentrates containing these minerals are likely to also contain uranium and rare earths, but also iron and titanium.
- niobium is mainly carried out by a pyrochlore flotation enrichment process, combined with a pyrometallurgical treatment in an aluminothermic furnace (Minerais Engineering, Volume 14, Number 1, January 2001, pp 99-105 ( 7): "Kinetics of Pyrochlore Flotation from Araxa Ore Deposits" by Oliveira JF, Saraiva SM, Pimenta JS, Oliveira APA, Mining Magazine, February 1982: “Araxa niobium mine”).
- the patent application WO 2012/093170 also describes the leaching of pyrochlore ore, in particular ore from the Mabounié deposit, located in Gabon, by quantitative solution of the valuable elements (Nb, rare earths (TR), Ta and you).
- the leachate obtained contains not only Nb and / or Ta but also iron, in particular ferric iron (Fe III), aluminum (Al), titanium (Ti) and phosphates (P). It is therefore necessary to purify the product obtained.
- patent application FR2075933 describes a method of recovering niobium of high purity from a niobium concentrate cooked with sulfuric acid by treatment with ammonia or an alkali metal hydroxide at a pH greater than 7 and at a temperature above 25 ° C, followed by roasting the mixture thus obtained and its leaching with water to obtain a solution containing the niobium before the precipitation of the niobium compounds.
- a wet mass it is necessary to use a lot of energy. The process is therefore industrially expensive.
- to eliminate titanium it it is necessary to add an additional leaching step under atmospheric pressure under reducing conditions.
- US Pat. No. 2,953,453 discloses a niobium recovery process comprising a soda melting step of colombite ore or treatment with sulfuric acid or with hydrofluoric acid.
- the product thus obtained is subject to various leaching operations in order to eliminate the contaminants: firstly washing with water and then washing with 1M sodium hydroxide solution before reducing acidic leaching (hydrochloric acid or nitric and iron powder). It is this last leaching which makes it possible to remove the titanium.
- the product obtained is then brought into contact with hydrofluoric acid to recover Nb and Ta.
- the method described is therefore long and produces a lot of effluents. In addition it is expensive in energy and it requires the use of HF which is expensive and toxic.
- US3058825 discloses a process for recovering niobium and tantalum from ores or ore concentrate. It uses pressure leaching in concentrated KOH colombite medium to solubilize niobates and tantalates. They are then precipitated by addition of a sodium salt and washed with a sodium solution. The precipitate is optionally hydrolysed with an acidic solution. The problem is that KOH solutions are not recyclable and that KOH is expensive. In addition it is necessary to strictly control the amount of KOH used under penalty of forming an insoluble salt.
- US4182744 discloses a process for extracting niobium and tantalum from bario-pyrochlore ore by treatment with CaCl 2 at about 1000 ° C.
- JP2004224619 discloses a method of purifying tantalum oxide or niobium so as to separate it from aluminum and silicon present by using sodium hydroxide at a concentration of between 2 and 20 mol / L, at a temperature between 100 and 300 ° C, preferably between 150 and 250 ° C, and a pressure between 0.1 and 30 MPa.
- this process does not eliminate titanium or iron if it is present in the original ore.
- the temperature and pressure recommended are very high which is economically expensive.
- the present invention therefore relates to a process for purifying niobium and / or tantalum from a niobium and / or tantalum ore or concentrate containing titanium and / or iron, the process comprising the following steps:
- step b) washing the solid recovered in step b) with an aqueous solution containing at most 30 g / l of NaOH and recovery of the washed solid;
- step e) acidifying the aqueous solution obtained in step e) to a pH of between 1 and 5, advantageously between 3 and 4, in particular 4, so as to precipitate niobium and / or tantalum;
- the ore or concentrate of niobium and / or tantalum treated according to the invention may of course consist of, respectively, a mixture of ores or a mixture of concentrates.
- the treated raw material may also consist of a mixed mixture of ore (s) / concentrate (s), which the skilled person also usually qualifies as ore or concentrate according to its niobium / tantalum contents.
- the invention therefore relates to the treatment of a raw material selected from ores, niobium and / or tantalum concentrates and mixtures thereof, advantageously of the invention relates to the treatment of niobium and / or tantalum concentrate, in particular containing between 6 and 26% by weight of niobium and / or tantalum, more particularly between 6 and 25% by mass niobium, advantageously between 8 and 24% by weight niobium, and between 0 and 1% by weight of tantalum, advantageously between 0.1 and 0.5% by weight of tantalum, more particularly it contains only niobium, in particular it contains a mixture of tantalum and niobium.
- the niobium and / or tantalum concentrate can be of any type. It may in particular be a mineralurgical concentrate resulting from an enrichment or a concentrate resulting from chemical enrichment (such as a leach residue).
- the process of the invention comprises, upstream of step a), enrichment of the ore or concentrate of niobium and / or tantalum to be treated.
- enrichment can be a physical enrichment based on any conventional method of physical enrichment of a solid material, for example it can consist of a low-intensity magnetic separation (to remove the magnetic) or a flotation (of the silica flotation type or flotation apatite).
- the method described above, for the purification of niobium and / or tantalum, is suitable for treating any ore or concentrate containing niobium and / or tantalum.
- Such ores and concentrates contain iron and / or titanium.
- it is ore pyrochlore or colombite or niobium concentrate and / or tantalum from these ores.
- it is pyrochlore ore, in particular ore from the Mabounié deposit located in Gabon, or niobium and / or tantalum concentrate obtained from this ore, and even more advantageously from concentrate of pyrochlore ore. niobium and / or tantalum obtained from this ore.
- this ore or concentrate of niobium and / or tantalum contains iron and / or titanium, more particularly it contains between 2 and 15% by weight of titanium, advantageously between 4 and 13% by weight, and / or between 5 and 10% by weight of iron, more particularly it contains iron and titanium, more particularly between 2 and 15% by weight of titanium, advantageously between 4 and 13% by weight, and between 5 and 10% by weight of iron.
- the concentrate or ore of niobium and / or tantalum of step a) contains between 6 and 26% by weight of niobium and / or tantalum (more particularly between 6 and 25% by mass niobium, advantageously between 8 and 24% by weight).
- niobium mass and between 0 and 1% by weight of tantalum, advantageously between 0.1 and 0.5% by weight of tantalum), between 2 and 15% by weight of titanium, advantageously between 4 and 13% by weight, and between 5 and 10% by weight of iron and its purification yield is at least 55%, advantageously at least 60%, more preferably at least 65%, in particular at least 70%.
- the ore or concentrate of niobium and / or tantalum also contains aluminum, advantageously in a content of less than 2% by weight, of phosphorus, advantageously in a content of between 3 and 12% by weight, advantageously between and 11% by weight of zirconium, advantageously in a content of less than 2% by weight, of sulfur, advantageously in a content of between 1 and 4% by weight, of silicon, advantageously in a content of less than 2% by weight, and / or radioactive elements, in particular U and / or Th, advantageously in a content of less than 1% by weight each.
- the niobium and / or tantalum ore or concentrate has the following composition:
- Niobium (from 6 to 25% by weight, advantageously from 8 to 24%
- Titanium from 2 to 15% by weight, advantageously from 4 to 13% by weight
- Phosphorus from 3 to 12% by weight, advantageously from 4 to 11% by weight
- niobium and / or tantalum is in the form of oxide, hydroxides and or phosphates in the ore or concentrate to be purified.
- Step a) according to the present invention therefore consists in suspending the ore or niobium and / or tantalum concentrate in a concentrated aqueous solution of NaOH under particular temperature conditions to recover a solid in step b).
- Step a) of sodium conversion of the process according to the present invention allows the conversion of niobium and / or tantalum ore or solid ore concentrate in the form of niobate and / or tantalate, also being in solid form.
- niobium and / or tantalum is not soluble at the end of step a) in the concentrated aqueous NaOH solution which will allow Al, P, S and Si to be eliminated. solubilize in the aqueous NaOH solution.
- the concentrated NaOH solution contains at least 200 g / l of NaOH, advantageously between 200 and 500 g / l of NaOH, more advantageously between 300 and 500 g / l of NaOH. and 450 g / L, more particularly between 320 and 400 g / L.
- the duration of step a) according to the present invention is between 2 and 24 hours, advantageously between 2 and 18 hours, more particularly between 2 and 16 hours.
- the L / S ratio of step a) of the process according to the present invention is between 3 and 50 L / kg, in particular between 5 and 50 L / kg, more particularly between 10 and 50 L / kg. and 50 L / kg.
- step a) of the process according to the present invention is carried out with stirring.
- the solid / liquid separation steps b) e) and g) of the process according to the present invention are carried out by filtration, decantation or centrifugation, in particular by filtration or centrifugation.
- Step c) of the process according to the present invention makes it possible to eliminate the impregnant of the solid recovered in step b) and the remainder of the elements soluble in basic medium such as aluminum and phosphorus, if they are present in ore or niobium and / or tantalum concentrate.
- step c) is carried out at a temperature of between room temperature and 80 ° C., advantageously at a L / S ratio of between 5 and 15 L / kg, in particular between 8 and HL. / kg.
- the diluted NaOH solution contains between 3 and 30 g / l of NaOH, advantageously between 10 and 26 g / l of NaOH.
- the washing solution used does not contain NaOH. It is therefore only water.
- the volume of water used is controlled and / or step c) is implemented against the current. The use of water against the current makes it possible to reduce as much as possible the quantity of washing liquid used and therefore the quantity of effluents generated.
- step c) is repeated several times, in particular at least four times.
- Stage d) of the process according to the present invention makes it possible to dissolve niobium and / or tantalum in water and to separate them from insolubles such as titanium, iron, zirconium and radioactive elements if these are present in the ore or niobium concentrate and / or tantalum starting material.
- step d) of the process according to the present invention is carried out at a temperature of between room temperature and 90 ° C, advantageously at 40 ° C.
- the aqueous solution obtained in step d) has a pH of between 11 and 13, advantageously 11.5.
- a pH regulation can be implemented during this step d), for example by adding acid, such as sulfuric acid, in order to keep a pH of between 11 and 13, advantageously a pH of 11, 5.
- the L / S ratio of step d) of the process according to the present invention is ⁇ 200 L / kg, advantageously between 10 and 100 L / kg, advantageously between 10 and 60 L / kg. in particular between 13 and 50 L / kg.
- the solid is only partially dissolved and step d) is repeated, advantageously up to two more times, on the solid recovered in step e) of the process according to the present invention, the aqueous solutions obtained at each step e) being mixed together before the implementation of step f) according to the present invention.
- Step f) of the process according to the present invention makes it possible to precipitate niobium and / or tantalum in the form of niobic acid and / or hydrated oxide of tantalum and / or tantalum in order to recover a purified solid.
- the acid used in step f) is acid chosen from sulfuric acid, hydrochloric acid, nitric acid or their mixture, advantageously it is sulfuric acid.
- the ore or concentrate of niobium and / or tantalum of step a) additionally contains aluminum, phosphorus, zirconium, sulfur, silicon and / or radioactive elements, such as Uranium (U) and / or thorium (Th), and the niobium and / or tantalum precipitate is quantitatively purified from these elements, typically with purification efficiencies greater than 98%.
- the process according to the present invention comprises an additional step h) washing the precipitate, preferably with water, and calcining the washed precipitate. If necessary, an extra step can be added to separate niobium and tantalum. This step uses methods well known to those skilled in the art.
- the concentrate or ore of step a) does not contain tantalum and a purified niobium precipitate is obtained in step g).
- the concentrated NaOH solution obtained after the separation step b) is recycled, advantageously after purification by crystallization of the impurities at a temperature below 50.degree. 30 ° C.
- the crystalline impurities are, for example, sodium phosphate and sodium sulphate.
- This crystallization step consists in cooling the sodium conversion filtrate obtained in step b) to a temperature below 50 ° C., advantageously 30 ° C.
- the solution thus obtained, after crystallization is depleted in pollutant but still relatively rich in soda. It is therefore reused in part in the sodium conversion step a) of the process according to the present invention with a fresh addition of concentrated sodium hydroxide to reduce the concentration to the desired value.
- the process according to the present invention comprises a prior step a), before step a), washing the concentrate or ore with an aqueous solution of NaOH diluted so as to eliminate the phosphorus present in the concentrate or ore and the concentrated NaOH solution obtained after the separation step b) is recycled, advantageously directly without crystallization.
- the sodium hydroxide is reused in the sodium conversion step a) of the process according to the present invention. with a refill of fresh concentrated soda to reduce the concentration to the desired value. Part of it is eliminated to avoid the accumulation of pollutants.
- a niobium / tantalum concentrate of the following mass elemental composition is introduced into a soda solution at 330 g / L at a rate of 10L / kg of solid.
- the suspension is heated at 110 ° C for 18 h and then the solid is separated from the liquid by centrifugation.
- the solid obtained is washed 4 times with sodium hydroxide at 26 g / l at a rate of 10 L / kg of starting solid and then the solid is partially dissolved in water at the rate of 35 L / kg of starting solid.
- the remaining solid is separated from the liquid by centrifugation and the solid is subjected to a new water dissolution step at 35 L / kg of starting solid.
- niobium solutions obtained contain the following elemental contents (in g / L):
- the niobium is recovered at 76% by this process, with an increase in the mass ratio Nb / Ti which goes from 1.2 in the starting concentrate to more than 100 in the solutions of niobium.
- Example 2 A niobium / tantalum concentrate of the following mass elemental composition: is introduced into a 320 g / l sodium hydroxide solution at a rate of 10 L / kg of solid. The suspension is heated at 110 ° C for 18 h and then the solid is separated from the liquid by centrifugation. The solid obtained is washed 4 times with sodium hydroxide at 26 g / l at a rate of 10 L / kg of starting solid and then the solid is partially dissolved in water at a rate of 50 L / kg of starting solid. The remaining solid is separated from the liquid by centrifugation and the solid is subjected to a new water dissolution step at 50 L / kg of starting solid.
- niobium solutions obtained contain the following elemental contents (in g / L):
- the niobium is recovered at 83% by this process, with an increase in the Nb / Ti mass ratio which goes from 5 in the starting concentrate to over 30 in the niobium solutions.
- Example 3 A niobium / tantalum concentrate of the following mass elemental composition:
- niobium solutions obtained contain the following elemental contents (in g / L):
- Niobium is recovered at 80% by this process, with an increase in the Nb / Ti mass ratio from 1.2 in the starting concentrate to greater than 140 in the first niobium solution.
- niobium solutions obtained contain the following elemental contents (in g / L):
- Niobium is 85% recovered by this process, with an increase in the Nb / Ti mass ratio from 1.0 in the starting concentrate to greater than 90 in the first niobium solution.
- the Nb / P ratio goes from 1.0 to 970.
- niobium solutions obtained contain the following elemental contents (in g / L):
- Niobium is recovered at 45% by this process (we would have had more if we had dissolved once more), with an increase in the mass ratio Nb / Ti which goes from 0.85 in the starting concentrate to more than 960 in the first solution of niobium and 110 in the second. Therefore, a very good selectivity towards titanium is maintained.
- niobium solutions obtained contain the following elemental contents (in g / L):
- Niobium is 65% recovered by this process, with an increase in the Nb / Ti mass ratio from 1.0 in the starting concentrate to over 100 in the niobium solutions.
- niobium solutions obtained contain the following elemental contents (in g / L):
- Niobium is 64% recovered by this process, with an increase in the Nb / Ti mass ratio from 1.0 in the starting concentrate to greater than 100 in the first niobium solution.
- niobium solutions obtained contain the following elemental contents (in g / L):
- the niobium is recovered at 57% by this process, with an increase in the Nb / Ti mass ratio from 1.0 in the starting concentrate to over 100 in the first niobium solution.
- the niobium solutions obtained contain the following elemental contents (in g / L):
- Niobium is 66% recovered by this process, with an increase in the Nb / Ti mass ratio from 1.3 in the starting concentrate to greater than 130 in the first niobium solution.
- the solid is then separated from the liquid by filtration.
- the solid obtained is washed 4 times in succession by repulping in 10 g / l sodium hydroxide at a solid content of approximately 100 g / l.
- the resulting solid is then partially dissolved in water at 40 ° C at a solid level of 1.9% for 2 h.
- the liquid is then separated from the solid and the latter is washed with water to remove the impregnant which is recovered with the other liquid phase.
- the solid is then separated from the liquid and the solid is washed with distilled water.
- Example 11 Examples of precipitation according to step ⁇ of the process according to the invention
- the precipitation yield of niobium is under these conditions of 98.5%.
- the precipitation yield of niobium is under these conditions of 99.9%.
- Comparative Example 1 Low Sodium Concentration A niobiu m / tantalum concentrate of the following mass elemental composition:
- a dilute sodium hydroxide solution (from 10 to 100 g / l) at a rate of 80 L / kg of solid.
- the suspension is heated at 90 ° C for 1 h and then the solid is separated from the liquid by centrifugation.
- the resulting solution contains a portion of the niobium, and the solid is washed with water twice.
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Abstract
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Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA2916921A CA2916921A1 (fr) | 2013-07-09 | 2014-07-07 | Procede de purification du niobium et/ou du tantale |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1356738A FR3008425B1 (fr) | 2013-07-09 | 2013-07-09 | Procede de purification du niobium et/ou du tantale |
FR1356738 | 2013-07-09 |
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Publication Number | Publication Date |
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WO2015004375A1 true WO2015004375A1 (fr) | 2015-01-15 |
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Application Number | Title | Priority Date | Filing Date |
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PCT/FR2014/051741 WO2015004375A1 (fr) | 2013-07-09 | 2014-07-07 | Procédé de purification du niobium et/ou du tantale |
Country Status (3)
Country | Link |
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CA (1) | CA2916921A1 (fr) |
FR (1) | FR3008425B1 (fr) |
WO (1) | WO2015004375A1 (fr) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2021014095A1 (fr) | 2019-07-25 | 2021-01-28 | Paris Sciences Et Lettres - Quartier Latin | Procédé d'extraction d'un métal réfractaire à partir d'un minerai, d'un concentré ou d'un déchet |
CN115838872A (zh) * | 2023-02-13 | 2023-03-24 | 锦益创典(天津)科技有限责任公司 | 钽铌浆料分解液的压滤洗涤方法 |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR3043696A1 (fr) | 2015-11-17 | 2017-05-19 | Eramet | Procede hydrometallurgique pour la separation et la purification du tantale et du niobium |
CN107236860B (zh) * | 2017-05-16 | 2019-08-30 | 中国科学院地球化学研究所 | 一种从粘土岩回收铝和硅并富集铌和钛的方法 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2956857A (en) * | 1957-11-25 | 1960-10-18 | Mallinckrodt Chemical Works | Methods of decomposing complex uranium-rare earth tantalo-columbates |
US3058825A (en) * | 1958-09-22 | 1962-10-16 | Paul B Cardon | Process for recovering columbium and tantalum from ores and ore concentrates containing same |
WO2013040694A1 (fr) * | 2011-09-23 | 2013-03-28 | Francois Cardarelli | Procédé de valorisation de minerais et de concentrés de tantale et de niobium avec récupération d'oxydes de manganèse et de terres rares |
-
2013
- 2013-07-09 FR FR1356738A patent/FR3008425B1/fr not_active Expired - Fee Related
-
2014
- 2014-07-07 CA CA2916921A patent/CA2916921A1/fr not_active Abandoned
- 2014-07-07 WO PCT/FR2014/051741 patent/WO2015004375A1/fr active Application Filing
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2956857A (en) * | 1957-11-25 | 1960-10-18 | Mallinckrodt Chemical Works | Methods of decomposing complex uranium-rare earth tantalo-columbates |
US3058825A (en) * | 1958-09-22 | 1962-10-16 | Paul B Cardon | Process for recovering columbium and tantalum from ores and ore concentrates containing same |
WO2013040694A1 (fr) * | 2011-09-23 | 2013-03-28 | Francois Cardarelli | Procédé de valorisation de minerais et de concentrés de tantale et de niobium avec récupération d'oxydes de manganèse et de terres rares |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2021014095A1 (fr) | 2019-07-25 | 2021-01-28 | Paris Sciences Et Lettres - Quartier Latin | Procédé d'extraction d'un métal réfractaire à partir d'un minerai, d'un concentré ou d'un déchet |
FR3099184A1 (fr) | 2019-07-25 | 2021-01-29 | Paris Sciences Et Lettres - Quartier Latin | Procédé d’extraction d’un métal réfractaire à partir d’un minerai, d’un concentré ou d’un déchet |
CN115838872A (zh) * | 2023-02-13 | 2023-03-24 | 锦益创典(天津)科技有限责任公司 | 钽铌浆料分解液的压滤洗涤方法 |
Also Published As
Publication number | Publication date |
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FR3008425B1 (fr) | 2015-08-07 |
CA2916921A1 (fr) | 2015-01-15 |
FR3008425A1 (fr) | 2015-01-16 |
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