RU2247788C1 - Method for preparation of scandium oxide from red mud - Google Patents

Method for preparation of scandium oxide from red mud Download PDF

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RU2247788C1
RU2247788C1 RU2003119050/02A RU2003119050A RU2247788C1 RU 2247788 C1 RU2247788 C1 RU 2247788C1 RU 2003119050/02 A RU2003119050/02 A RU 2003119050/02A RU 2003119050 A RU2003119050 A RU 2003119050A RU 2247788 C1 RU2247788 C1 RU 2247788C1
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solution
precipitate
sodium hydroxide
mixture
scandium oxide
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RU2003119050A (en
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С.П. Яценко (RU)
С.П. Яценко
нов Н.А. Сабирз (RU)
Н.А. Сабирзянов
Л.А. Пасечник (RU)
Л.А. Пасечник
Г.М. Рубинштейн (RU)
Г.М. Рубинштейн
В.Н. Диев (RU)
В.Н. Диев
бнева Л.М. Скр (RU)
Л.М. Скрябнева
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Институт химии твердого тела Уральского отделения Российской Академии наук
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Abstract

FIELD: non-iron metallurgy, in particular scandium oxide recovery from industrial waste.
SUBSTANCE: method for preparation of scandium oxide from red mud being waste of alumina production includes: multiple subsequent leaching of red mud with mixture of sodium carbonate and hydrocarbonate solutions; washing and precipitate separation; addition into obtained solution zinc oxide, dissolved in sodium hydroxide; solution holding at elevated temperature under agitation; precipitate separation and treatment with sodium hydroxide solution at boiling temperature; separation, washing, and drying of obtained product followed by scandium oxide recovery using known methods. Leaching is carried out by passing through mixture of sodium carbonate and hydrocarbonate solutions gas-air mixture containing 10-17 vol.% of carbon dioxide, and repeated up to scandium oxide concentration not less than 50 g/m3; solid sodium hydroxide is introduced into solution to adjust concentration up to 2-3.5 g/m3 as calculated to Na2O (caustic); and mixture is hold at >=800C followed by flocculating agent addition, holding, and separation of precipitate being a titanium concentrate. Obtained mixture is electrolyzed with solid electrode, cathode current density of 2-4 A/dm3, at 50-750C for 1-2 h to purify from impurities. Zinc oxide solution in sodium hydroxide is added into purified after electrolysis solution up to ratio ZnO/Sc2O3 = (10-25):1, and flocculating agent is introduced. Solution is hold at 100-1020C for 4-8 h. Separated precipitate is treated with 5-12 % sodium hydroxide solution, flocculating agent is introduced again in amount of 2-3 g/m3, mixture is hold, and precipitate is separated. Method of present invention is useful in bauxite reprocessing to obtain alumina.
EFFECT: improved recovery ratio of finished product into concentrate; decreased impurity concentration in concentrate, reduced sodium hydrocarbonate consumption, as well as reduced process time due to decreased time of fine-dispersed precipitate.
2 cl, 2 ex

Description

The invention relates to ferrous metallurgy, and in particular to the extraction of scandium oxide from industrial wastes during the processing of bauxite into alumina.
There is a method of extracting scandium oxide from waste from the production of alumina - red mud, including leaching with sulfuric acid, sorption on anion exchangers treated with sulfuric acid based on polyethylene polyamines, sorption of scandium with phosphorus-containing ion exchanger, subsequent washing of the ion exchanger, desorption of scandium and processing of the obtained eluate with extraction 2196184, C 22B 59/00, 2003).
But the known method has several disadvantages: the complex technology of using ion exchangers during extraction and sorption, an unfavorable environmental situation due to the use of organics.
Closest to the technical nature of the claimed is a method for the extraction of scandium during the processing of bauxite into alumina, for example, from red mud, a by-product of the processing, including leaching with water and / or 5-12% sodium carbonate or sodium bicarbonate solution or their mixture, which is carried out at least 3 times at a temperature not exceeding 50 ° C for at least 2 hours at a ratio of T: W = 1: 2.5-5.0 using each time new portions of the bauxite processing product as a feedstock, separating the solution from sediment, administration to the resulting solution aluminum oxide or zinc dissolved in sodium hydroxide, extract at a temperature not lower than 80 ° C for at least 2 hours. The precipitate obtained is separated, washed and treated with a 10-25% sodium hydroxide solution while heating to a boil, filtered and washed with a 1-5% sodium hydroxide solution, then the precipitate is dissolved in 1-5% hydrochloric acid, filtered and the filtrate treated with 10-25% ammonia solution or 2-10% hydrofluoric acid with an excess of 1-3% of stoichiometry to obtain primary scandium concentrate (RF patent No. 2201988, IPC C 22 V 59/00, 2003).
The disadvantages of this method are:
- a significant consumption of sodium bicarbonate and reduced extraction of scandium during leaching, a limited number of cycles of leaching of red mud from one portion of the solution, since the content of sodium carbonate increases beyond its solubility in the sodium bicarbonate solution;
- obtaining a poor scandium concentrate enriched with a number of harmful impurities;
- significant settling time of the precipitated fine precipitate of scandium oxide.
Thus, the authors were faced with the task of developing a method for producing scandium oxide from red mud, a waste from alumina production, which would have high processability along with high extraction of scandium into the final product.
The proposed method provides a technical result, which consists in a high technological process along with high extraction of scandium.
The technical result is achieved in the proposed method for producing scandium oxide from red mud, waste from alumina production, including multiple sequential leaching of red mud from a mixture of sodium carbonate and sodium bicarbonate solutions, washing and separating the precipitate, introducing zinc oxide dissolved in sodium hydroxide into the resulting solution, holding the solution at elevated temperature and stirring, separation of the precipitate and its processing with a solution of sodium hydroxide at boiling point, separation, washing and drying the resultant product followed by extraction of scandium oxide by known methods, wherein the leaching through the mixture of sodium carbonate and sodium bicarbonate solutions passed the gas-air mixture containing 10-17% CO 2 (by volume), leaching is repeated until a solution with a concentration of scandium oxide is not less than 50 g / m 3 are introduced into a solid sodium hydroxide solution to a concentration of 2-3.5 kg / m 3 to Na 2 O caustic and maintained at a temperature not higher than 80 ° C, followed by the introduction of flocculant, exposure and separation of the precipitate is schegosya titanium concentrate and the resulting solution is electrolysed with solid electrodes at a cathodic density of 2-4 A / dm 2 and a temperature of 50-75 ° C for 1-2 hours for the removal of impurities, zinc oxide solution in sodium hydroxide is added after electrolysis in the purified the solution to a ratio of ZnO: Sс 2 O 3 = (10-25): 1 and a flocculant is introduced, the solution is aged at 100-102 ° C for 4-8 hours, the separated precipitate is treated with a 5-12% sodium hydroxide solution at a temperature boiling, the flocculant is again introduced, the sediment is kept and separated.
Moreover, as a flocculant can be used flocculant brand "Nalko" in an amount of 2-3 g / m 3 .
Currently, from the patent and scientific and technical literature there is no known method for producing scandium oxide from alumina production wastes, including the proposed sequence of technological operations with the parameters of the modes in the proposed value ranges.
The proposed technological modes and parameters are explained by the following reasons.
Obtaining bicarbonate from sodium carbonate directly in the apparatus by passing through a pulp of red mud a CO 2 -containing air-gas mixture obtained, for example, from cleaned and cooled furnace gases (from sintering furnaces, calcining limestone, etc.), allows the use of cheaper and less the amount of product, as well as secondary sodium carbonate, which is formed as a result of neutralization of Na 2 O ku contained in the red mud, sodium bicarbonate, and reduces the consumption of soda products.
The use of CO 2 -containing gases makes it possible to adjust the content of sodium carbonate accumulating in the solution, preventing it from precipitating upon repeated use of a portion of the enriched solution, which makes it possible to increase the content of scandium in the solution. In the temperature range used, there is an increased resistance of the scandium hydrocarbonate complex and, accordingly, its maximum recovery.
The proposed method uses the effect of increasing the activity of sodium bicarbonate at the time of its formation, due to which the extraction of scandium oxide into a soluble bicarbonate complex increases by more than 3%.
The introduction of a solution of solid sodium hydroxide in a scandium-enriched solution in a certain amount and under certain conditions makes it possible to partially separate the soluble compounds of titanium, iron, zirconium, etc., whose complexes are destroyed when a slightly alkaline medium is created. These oxide compounds precipitate, while more strongly bound to the bicarbonate ion, scandium remains in solution, which allows to obtain an increased purity of the final product. The electrolysis under the proposed conditions is also aimed at increasing the purity of the final product, providing a several-fold reduction in the content of iron, lead, copper, and other impurities.
The introduction of a solution of zinc oxide in sodium hydroxide in the proposed ratio, followed by the introduction of a flocculant and high-temperature hydrolysis under the proposed conditions, contributes to the release of fine precipitate, further processing of which provides a high percentage of extraction of scandium oxide.
The proposed method is as follows.
The filtered red mud, water, carbonate (30-100 g / dm 3 ) and sodium bicarbonate (50-100 g / dm 3 ) are placed in the carbonizer, the ratio T: W = 1: (2-5). The pulp is treated at a temperature of 50-60 ° C with a gas-air mixture containing 10-17% (volume) of CO 2 . In the process of carbonization, a part of scandium oxide, sodium oxide contained in the liquid and solid phase of the sludge (20%), a certain amount of titanium, iron, zirconium compounds, etc., as well as a fine suspension consisting of silicon oxides, iron are transferred into a soda hydrocarbonate solution etc. The use of CO 2 from a gas-air mixture is on average close to 30%. After the operation, the solution is defended, separated from the precipitate. The latter is washed with water, which is used to compensate for water losses during carbonization. Due to the return of industrial products, the losses of scandium and soda products with sediment moisture are insignificant. The required concentration of sodium bicarbonate is supported by the interaction of the source and secondary sodium carbonate with carbon dioxide. The temperature range is due to the fact that at a temperature below 50 ° C the rate of leaching of the sludge decreases, and at a temperature above 60 ° C, the loss of solvent, sodium bicarbonate, increases. The use of carbonate instead of sodium bicarbonate allows you to spend 1.68 times less soda products, in addition, secondary sodium carbonate is used, the amount of which per 1 carbonization operation is 15-19% (mass.) Of the primary sodium carbonate. The use of carbon dioxide increases by 3% the extraction of scandium in solution, since the resulting sodium bicarbonate at the time of formation has a greater reactivity.
One portion of the soda-hydrocarbonate enriched solution is used up to 10 times, accumulating at least 50 g / m 3 of scandium oxide in it. The number of operations is limited by the concentration of sodium bicarbonate and sodium carbonate in the solution, since when the solubility limit is exceeded, precipitation of solid phases begins.
After carbonation and clarification, a scandium-rich soda hydrocarbonate solution is made alkaline with sodium hydroxide to a concentration of 2-3.5 g / dm 3 for Na 2 O caustic. and subjected to hydrolysis at a temperature of 80 ° C for at least 2 hours. The precipitated precipitate of titanium, iron, zirconium, silicon oxides is a rich titanium concentrate [(56% TiO 2 and 3.5% ZrO 2 (mass.)]. The obtained alkaline solution is subjected to electrolysis at a cathodic current density of 2-4 A / dm 2 , temperature 50 -75 ° C for 1-2 hours. During electrolysis, the concentration of electropositive impurities — iron, copper, lead — decreases several times. At the same time, the concentration of titanium and silicon oxides in colloidal form decreases, which can be explained by the electrophoretic transfer of micelles to the cathode and their discharge due to which the oxides of titanium and silicon also partially precipitate.
A zincate solution is introduced into the purified co-alkaline solution based on the dosage of ZnO: Sc 2 O 3 = (10-25): 1, a flocculant is introduced and the mixture is stirred at 100-102 ° C for 4-8 hours. Under conditions of high-temperature hydrolysis, a precipitate precipitates from the solution in which zinc oxide is a collector for scandium oxide. With a smaller declared excess of zinc, scandium oxide extraction decreases, a larger excess does not affect the process, but a poorer concentrate is obtained, which creates additional difficulties in the subsequent operation - removal of zinc oxide from the precipitate. The wet cake is leached with a 5-12% sodium hydroxide solution at 100 ° C and with stirring.
At a concentration of less than 5% sodium hydroxide, the rate and completeness of leaching of zinc oxide deteriorate; at a concentration of more than 12%, the loss of scandium oxide increases.
In the known method, when leaching sediments obtained from industrial solutions, the extraction of zinc oxide into a sodium hydroxide solution usually stops after 92-94% is removed; in the proposed method, due to the removal of impurities during electrolytic cleaning, the percentage of leachability of zinc oxide increases, as a result of which 95-98% of zinc oxide is removed.
The mother liquor after alkali extraction is transferred to alumina production or partially used in the head of the process. The zincate solution after leaching the precipitate of oxides is used repeatedly.
The scandium oxide precipitate is filtered off from the zincate solution, washed and dried at 250 ° C. It is a rich concentrate containing up to 32% scandium oxide. To separate a fine precipitate of scandium oxide, a flocculant is introduced and a sufficient exposure time is given - up to 6 hours for precipitation. As a flocculant can be used flocculant "Nalko" No. 7864 in the form of a solution at the rate of 2-3 g / m 3 .
The total recovery of scandium oxide from red mud to concentrate averages 12.8% (mass.).
The proposed method is illustrated by the following examples.
Example 1. In a steel glass with a capacity of 3.5 dm 3 (⌀150 mm, height 200 mm), a carbonizer equipped with a stirrer, a lid, a bubbler and a water jacket was placed with 150 g of Na 2 CO 3 and 30 g of NaHCO 3 , 1.6 dm 3 water and 1 kg of waste red mud with a moisture content of 25%. Sludge composition: solid phase, mass%: Fe 2 O 3 39-40, FeO 6-7, Al 2 O 3 12-14, SiO 2 8-9, CaO 12-13, TiO 2 3.5-4.0, Na 2 O 3-3.5, ZrO 2 0.16, Cu 0.08, Pb 0.05, Sc 2 O 3 0.0125, nnn 14.0; liquid phase, g / dm 3 : Na 2 O ku 8.0, Na 2 O kb 0.4, Al 2 O 3 1.6.
Through a pulp consisting of 1.85 dm 3 liquid and 0.75 kg of solid phase (ratio W: T = 1: 2.5), for 6 hours of carbonization at a temperature of 60 ° C, 290 ndm 3 of a gas mixture containing 17% CO 2 are passed. During carbonization, a constant volume of pulp is maintained, compensating for the loss of water by the addition of a slurry obtained by washing the leached sludge. Due to washing, the loss of soda products is reduced by 3.3 g of Na 2 O in one operation.
Part of NaHCO 3 - 19.8 g - is spent on the neutralization of Na 2 O ku contained in the liquid and solid phases of red mud: 2.1 and 5.2 g, respectively, only 7.3 g Na 2 O ku . In this case, 25.0 g of Na 2 CO 3 are formed in the solution. The absorption of CO 2 by solution during carbonization averages 30%.
The mass of the obtained precipitate in the first and subsequent operations is ~ 1.0 kg at a moisture content of 25%.
The volume of the filtrate after separation and washing of the precipitate is 1.60 dm 3 and has a composition, kg / m 3 : Na 2 CO 3 71.9, NaHCO 3 60.1, Fe 2 O 3 0.14, Al 2 O 3 0.1, TiO 2 0.7, ZrO 2 0.02, Sc 2 O 3 8.13 · 10 -3 (total in the entire volume of the solution 13.0 mg). The resulting solution is used to carbonize a second portion of red mud in the above conditions. For carbonization in a second portion of the slurry for 2 hours, the pulp was fed 65 3 BAT-gas mixture containing 17% (by volume) of CO 2 to compensate for losses during the neutralization NaNSO 3 Na 2 O ku slurry and washing the precipitate. As a result of the second operation get 1.6 DM 3 filtrate composition, kg / m 3 : Na 2 CO 3 72.9; NaHCO 3 65.1; Fe 2 O 3 0.22; Al 2 O 3 0.12; TiO 2 1.38; ZrO 2 0.058 and Sc 2 O 3 15.3 g / m 3 (24.5 mg).
In subsequent operations, carbonization is carried out in such a way that in 3-5 operations the hydrocarbonate content is in the range of 65-68 kg / m 3 , and in 6-10 it is in the range of 70-75 kg / m 3 . Correction of the composition by the addition of Na 2 CO 3 in this case is not carried out. After performing 5 carbonization operations, 1.63 dm 3 of the filtrate of the composition is obtained, kg / m 3 : Na 2 CO 3 81.9, NaHCO 3 68.3, Fe 2 O 3 0.27, Al 2 O 3 0.14, TiO 2 1.40, ZrO 2 0.059 and Sc 2 O 3 38.6 g / m 3 (62.9 mg). The extraction from the sludge into the solution in all operations for Na 2 O and Sc 2 O 3 remains approximately constant; the content of iron, titanium, aluminum, silicon, and other oxides in the solution changes insignificantly.
Sludge carbonization operations with one portion of the solution continue up to 10 operations, after which 1.68 dm 3 of filtrate of the composition, kg / m 3 , is obtained: Na 2 CO 3 98.5, NaHCO 3 74.9, Fe 2 O 3 0.62, Al 2 O 3 0.17, TiO 2 1.69, ZrO 2 0.06, SiO 2 0.23, Cu 0.046, Pb 0.056 and Sс 2 O 3 79 g / m 3 (132.0 mg).
In the solution obtained after filtration, a significant amount of suspension is observed, consisting of finely dispersed and colloidal particles of iron, titanium, silicon and other compounds. For the precipitation of a number of hydroxides (Fe, Ti, Zr, etc.) soluble in bicarbonate, as well as part of the suspension 65.3 g of solid sodium hydroxide are added to the filtrate with stirring to obtain a slightly alkaline solution, which corresponds to 2.5 kg / m 3 in Na 2 O caustic . After 2 hours of exposure at 75-80 ° C, 1% Nalko flocculant solution No. 7864 is added to the solution at a rate of 2 g / m 3 , then after 6 hours of settling, the precipitate formed is filtered off and washed.
The dried and calcined precipitate weighing 5.2 g contains, wt.%: TiO 2 56.0; ZrO 2 3.5; Fe 2 O 3 25.9; SiO 2 6.0; others (SiO 2 , Fe 2 O 3 , Na 2 O, etc.) 8.2; Sc 2 O 3 5.1 mg or 0.16% by weight of the precipitate.
The resulting co-alkaline solution with a volume of 1.7 dm 3 of the composition, kg / m 3 : Na 2 CO 3 176.9, Na 2 O ku 2.5, Al 2 O 3 0.1, Fe 2 O 3 0.04, TiO 2 0.04, ZrO 2 0.01, SiO 2 0.05, Cu 0.036, Pb 0.05 and Sс 2 O 3 74.20 g / m 3 (126.0 mg), are subjected to electrolysis at a current density of: cathodic 2.0 A / dm 2 , bulk 5 A / dm 3 , temperature 75 ° C with electrodes made of acid-resistant steel. After 2 hours of electrolysis, the concentration of a number of harmful impurities decreases and amounts to, kg / m 3 : Fe 2 O 3 0.003, TiO 2 0.01, SiO 2 0.03, Pb 0.005, Cu 0.004. Visually, the solution after settling is more transparent. Then, 0.05 dm 3 of a zincate solution (1.05 g of Zn) with a concentration of Na 2 O ku of 180 kg / m 3 and Zn 21 kg / m 3 (ZnO: Sс 2 O 3 = 10: 1 ratio) is added to the solution, 3.2 mg of flocculant is added “Nalko” and incubated at a temperature of about 100 ° C and stirring for 4 hours. After 6 hours of settling, the precipitated fine crystalline precipitate is filtered off. After washing and drying at 250 ° C, the mass of the precipitate is 1.61 g, the content of components,% mass .: Sс 2 O 3 - 7.60 (0.122 g); ZnO - 81.80; Al 2 O 3 - 4.16; Fe 2 O 3 - 0.31; TiO 2 - 1.05; ZrO 2 0.37; SiO 2 - 3.10; Cu - 0.006; Pb - 0.1; etc. - 1.53.
The filtered alkaline solution is used to leach the next batch of red mud.
A wet oxide precipitate is treated at 100 ° C for 2 hours with stirring with a 12% sodium hydroxide solution. At the end of the operation, 3.2 mg of Nalko flocculant is administered and after 6 hours of sedimentation, the precipitate of scandium concentrate is filtered. After washing and drying at 250 ° C, the mass of the precipitate is 0.41 g, composition,% (mass.): Sс 2 O 3 - 29.70; ZnO - 11.82; Al 2 O 3 - 20.30; TiO 2 - 5.15; Fe 2 O 3 - 1.52; Cu - 0.30; Pb - 0.60; etc. - 6.98.
Next, the scandium concentrate is processed according to known technology.
As a result, the average recovery of scandium oxide from the sludge into a soda-hydrocarbonate solution in 10 operations is (taking into account losses with moisture from the dump cake) 13.90%. Losses of scandium oxide during operations are,% (mass.): Separation of the precipitate of titanium, zirconium hydroxides, etc. - 3.8; from contained in solution; mechanical - 0.5%; the precipitation of a mixture of scandium and zinc oxides is 3%, and when zinc oxide is leached from the precipitate, 2%. The total recovery of scandium oxide in the primary concentrate containing 29.70% S 2 O 3 is 12.8%.
In the known method, the calcined sludge contains only 5-20% S 2 O 3 , that is, 1.5-5.9 times less, and the extraction of S 2 O 3 from the sludge is 3.0% lower. The duration of clarification of solutions before filtration in the known method is also 2-3 times longer than the duration of this operation in the proposed method.
Example 2. Carry out 10 carbonization operations, as described in example 1, but using a gas-air mixture with a content of 10% (vol.) CO 2 at a temperature of 50 °. The remaining conditions correspond to example 1. In the first operation, the volume of the gas mixture is 437 nm 3 , the duration is 8.5 hours. In the second operation, the volume of the gas mixture is equal to 100 ndm 3 with a duration of 3 hours; in subsequent operations, the supply of the gas mixture is carried out based on the calculation of the hydrocarbonate content in the solution of 65-75 g / dm 3 . After 10 operations, the content of Сc 2 O 3 is 77.4 g / m 3 (127.4 mg), which is 96.5% of the result in Example 1. For precipitation of a number of hydroxides (Fe, Ti, Zr, etc.) soluble in hydrocarbonate compounds solid sodium hydroxide is added to the filtrate with stirring, at a rate of 2.5 kg / m 3 according to Na 2 O caustic, to obtain a slightly alkaline solution. After 2 hours of exposure, 1% Nalko flocculant solution No. 7864 is added to the solution at 75-80 ° C at a rate of 3 g / m 3 , then after 6 hours of settling, the precipitate formed is filtered off, washed and calcined. The content of Sc 2 O 3 in the precipitate after calcination is 0.08% (4.5 mg) or 3.2% of the initial in solution. The resulting co-alkaline solution is subjected to electrolysis at a cathodic current density of 4.0 A / dm 2 , at a temperature of 50 ° C with electrodes made of acid-resistant steel. Visually, the solution after settling is more transparent. Next, 2.5 g of zinc is introduced into the solution, based on the ratio of ZnO: S 2 O 3 = 25: 1, the process is carried out at 102 ° C for 8 hours. A wet oxide precipitate is treated at 100 ° C for 2 hours with stirring with a 5% sodium hydroxide solution. At the end of the operation, Nalko flocculant No. 7864 is introduced at a rate of 3 g / m 3 and after 6 hours of settling, the precipitate of scandium concentrate is filtered off, washed and dried at 250 ° C.
The extraction of Sс 2 O 3 from the sludge into the soda-hydrocarbonate solution is 13.6%. Losses of Сс 2 O 3 upon receipt of the concentrate from the soda-hydrocarbonate solution in operations,%: when separating the precipitate of hydroxide impurities - 3.2; precipitation of ZnO and Sc 2 O 3 - 3.1; leaching of ZnO - 2.5; mechanical - 0.5; total - 9.6.
The total recovery (wt.) From the sludge to the concentrate is 11.4% with a content of 30.6 wt.% Sc 2 O 3 .
Thus, the proposed method for producing scandium oxide from red mud, alumina production waste, allows to increase the percentage of the target product in the concentrate, reduce the content of impurities in the concentrate, as well as significantly reduce the consumption of sodium bicarbonate, shorten the process by settling fine sediment.

Claims (2)

1. A method of producing scandium oxide from red mud - a waste product from alumina production, including multiple sequential leaching of red mud from a mixture of sodium carbonate and sodium bicarbonate solutions, washing and separating the precipitate, introducing zinc oxide dissolved in sodium hydroxide into the resulting solution, holding the solution at elevated temperature and stirring, separating the precipitate and treating it with sodium hydroxide solution at boiling point, separating, washing and drying the resulting product, followed by extraction scandium oxide known methods, characterized in that the leaching solution through a mixture of sodium carbonate and sodium hydrogencarbonate passed the gas-air mixture containing 10-17% CO 2 (by volume), leaching is repeated until a solution with a concentration of scandium oxide at least 50 g / m 3 , solid sodium hydroxide is introduced into the solution to a concentration of 2-3.5 kg / m 3 in Na 2 O caustic and kept at a temperature not exceeding 80 ° C, followed by the introduction of a flocculant, exposure and separation of the precipitate, which is a titanium concentrate, this solution is subjected to electrolysis with solid electrodes at a cathode density of 2-4 A / dm 2 and a temperature of 50-75 ° C for 1-2 hours to remove impurities; a solution of zinc oxide in sodium hydroxide is added to the solution purified after electrolysis to the ZnO ratio : Sc 2 O 3 = (10 ÷ 25): 1 and a flocculant is introduced, the solution is kept at 100-102 ° С for 4-8 hours, the separated precipitate is treated with a 5-12% sodium hydroxide solution at boiling point, flocculant is introduced again, the sediment is kept and separated.
2. The method according to claim 1, characterized in that as a flocculant use a flocculant brand "Nalko" in an amount of 2-3 g / m 3 .
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RU2480412C1 (en) * 2012-02-10 2013-04-27 Общество с ограниченной ответственностью "Научно-производственная компания "СКАНТЕХ" Processing method of red muds of alumina industry
RU2483131C1 (en) * 2011-12-26 2013-05-27 Учреждение Российской академии наук Институт химии твердого тела Уральского отделения РАН Method of making scandium oxide from red slag
RU2484164C1 (en) * 2011-12-27 2013-06-10 Общество с ограниченной ответственностью "Научно-производственная компания "СКАНТЕХ" Method of producing scandium-bearing concentrate from red mud
US20140314639A1 (en) * 2013-04-22 2014-10-23 Vale S.A. Method for recovering scandium from intermediate products formed in the hydrometallurgical processing of laterite ores
RU2536714C1 (en) * 2013-08-06 2014-12-27 Общество с ограниченной ответственностью "Объдиненная Копания РУСАЛ Инженерно-технологический центр" Method of producing scandium-bearing concentrate from red mud
RU2562183C1 (en) * 2014-05-29 2015-09-10 Общество с ограниченной ответственностью "Объединенная Кoмпания РУСАЛ Инженерно-технологический центр" Method of producing of scandium concentrate from red slime
RU2582425C1 (en) * 2014-12-10 2016-04-27 Общество с ограниченной ответственностью "Объединенная Компания РУСАЛ Инженерно-технологический центр" Method of extracting scandium from scandium-bearing material
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