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Recovery of Scandium by Crystallization Techniques

Journal of Sustainable Metallurgy volume 5, pages 48–56 (2019)Cite this article

Abstract

Bauxite residues, i.e., red mud, can be processed to recover various valuable end products, while reducing the environmental impact of the waste. Scandium is one of the valuable elements in bauxite residues. It is possible to extract and enrich scandium from red mud by leaching and solvent extraction. Scandium can then be recovered from the pregnant strip liquor by crystallization. Different crystallization techniques can be used to generate the supersaturation required for scandium to crystallize out as a salt. In the present study, the crystallization of an ammonium scandium fluoride phase by cooling and antisolvent crystallization techniques is presented. Cooling crystallization gave a low yield of ammonium scandium hexafluoride, (NH4)3ScF6, below 50% at the lowest temperature of 1 °C investigated. Antisolvent crystallization using ethanol gave almost complete recovery with precipitation efficiency greater than 98% for an ethanol-to-strip liquor volumetric ratio of 0.8. Solubility data of (NH4)3ScF6 under different temperatures and in different ethanol–strip liquor mixtures is herein presented. The product obtained by antisolvent crystallization had very minute crystals (< 2 µm) due to the high supersaturation generated upon adding ethanol to the strip liquor, while it was easier to obtain larger crystals by cooling crystallization. Fe and Ti impurities were detected in the solid product, and an insight into the mechanism of impurity uptake is discussed.

Introduction

Scandium is a precious metal that has increasingly found use in many applications, which include production of high strength aluminum alloys for aircraft parts and use in solid oxide fuel cells (SOFCs) [1]. Scandium, in concentrations not exceeding 0.2 wt%, increases the strength to weight ratio of aluminum alloys and allows welding without loss of strength, and about 90% of scandium production is currently used in SOFCs [2]. Due to these developments, there has been an increasing demand for this metal [3], yet there are limited commercially exploitable reserves [1, 4, 5]. Scandium is widely dispersed in the Earth’s crust [5, 6] at a concentration of about 22 ppm, comparable to that of cobalt and greater than that of lead and other common metals [7]. Currently, there is no scandium production in Europe and production occurs in China (66%), Russia (26%) and Ukraine (7%) [8]. Consequently, scandium has been listed as a critical raw material by the EU and the US government [8, 9].

The commercially viable option is to recover scandium from waste streams of other metallurgical processing industries. These include bauxite residue (60–120 ppm Sc) from the aluminum industry, acid waste from TiO2 pigment industry as well as lateritic Ni–Co processing [1, 10, 11]. A range of integrated separation techniques including leaching and solvent extraction can be employed to recover Sc from these waste streams [5, 7, 10, 11]. A solid Sc phase can then be crystallized from the concentrated strip liquor stream. In crystallization under cooling conditions, supersaturation is achieved by cooling a solution below its saturation temperature, whereas in antisolvent crystallization, supersaturation is induced by adding a suitable soluble solvent to the solution, thereby reducing the solubility of the stable salt in the resultant solvent matrix [12].

The current state-of-the-art in the recovery of scandium from metallurgical waste streams involves leaching to extract scandium from the waste stream, e.g., bauxite residue [13,14,15]. Solvent extraction is then employed to extract Sc from the pregnant leach solution (PLS) using an organic solvent, followed by stripping of Sc back into the aqueous phase [11, 16,17,18]. Sc is then recovered by precipitation as the hydroxide or oxalate salt [19, 20], which are calcined at temperatures of 700–800 °C to obtain scandium oxide [21]. The oxide is then fluorinated using hydrofluoric (HF) acid to obtain ScF3 [22], which is the precursor for the production of Sc and Al–Sc alloys.

In the process considered herein, an NH4F solution is used to strip Sc from the organic phase, and Sc is then recovered as (NH4)3ScF6 by crystallization. This intermediate product can be calcined at temperatures between 340 and 350 °C to obtain ScF3 [23]. ScF3 can be used for the direct production of scandium metal and Sc–Al alloys by metallothermic reduction [24]. This processing route is favorable from sustainability and economic perspectives since it eliminates the direct use of HF acid in the production of ScF3 and calcination of the intermediate product, (NH4)3ScF6, is accomplished at lower temperatures, hence at low-energy and with low-cost benefits. In addition, the processing route has fewer steps since fluoride salts can be directly crystallized from solution. For antisolvent crystallization, the high quantities of the antisolvent required can be offset by the fact that the antisolvent can be recovered in a separate distillation process and reused in the precipitation stage.

Scandium can be precipitated in various phases, e.g., hydroxide, oxalate, phosphate, carbonate, and fluoride. The precipitation method commonly used is the addition of a chemical reagent to a solution containing Sc to precipitate the Sc salt. For instance, addition of oxalic acid results in precipitation of scandium oxalate [19], while (NH4)2HPO4 reagent results in ScPO4 precipitation [25]. Addition of NaF solutions in different concentrations to an NH4HF2 solution containing Sc can result in precipitation of a mixture of salts namely, ScF3, Na3ScF6 and Na(NH4)2ScF6 in different proportions [26]. For antisolvent crystallization, the choice of a suitable solvent is dependent on several factors including ionic speciation in the new solvent matrix [27]. The solubility of metal salts is usually decreased upon the addition of an alcohol (antisolvent) to an aqueous solution. This occurs since most inorganic metal salts have lower solubility in alcohol than in water. However, in a previous study, it was found that formation of chloro-complexes was enhanced in aqueous-alcohol solvent mixtures, and the chloride salts did not precipitate [27].

The stability constants of complexes are mainly available for purely aqueous systems and not for solvent mixtures. The stability constants of Sc fluoride complexes [28] as well as the solubility product of ScF3 [29] in aqueous solutions have been published. In addition, the solubilities of ScF3 and (NH4)3ScF6 have been determined in HF-dosed solutions [30]. Various crystalline phases which include ScF3, NH4ScF4, (NH4)5Sc3F14, NH4Sc3F10, (NH4)2Sc3F11, and the α- and β- polymorphs of (NH4)3ScF6 have been reported for the ScF3-NH4F system [26, 31]. β-(NH4)3ScF6 was identified as the most stable phase in the ScF3-NH4F system at high fluoride concentrations at temperatures below 90 °C [31, 32]. This phase was observed to decompose thermally at temperature ranges of 260–290 °C and 340–350 °C to NH4ScF4 and ScF3, respectively [23, 32].

In the current study, the starting solution is a synthetic pregnant strip liquor stream containing about 0.2 wt% Sc and some metal impurities (Fe, Ti) in an NH4F solution matrix. The solution matrix is basically the stripping solvent employed in the upstream solvent extraction process. This paper reports on the preliminary evaluation of the technical feasibility of recovering Sc from the strip liquor using cooling and antisolvent crystallization. A comparison of the two techniques is drawn with regards to product quality and yield. An investigation into the mechanism of impurity uptake by the solid product obtained by antisolvent crystallization is also presented.

Methodology

Strip Liquor Preparation

Synthetic strip liquors were prepared by MEAB Chemie Technik GmbH laboratory. The starting solution in the preparation of the strip liquors was a scandium sulphate solution containing ca. 2640 mg/L Sc. The solvent extraction conditions were chosen so as to obtain a strip liquor that was undersaturated with respect to ammonium scandium hexafluoride. This scandium enrichment process can be employed to any feed material with a considerable scandium concentration, e.g., bauxite residue, and the final strip liquor composition depends on the initial composition of the feed material as well as the extent of coextraction of impurity metals. Sc2(SO4)3.6H2O of purity ca. 99.9% purchased from Richest Group, China was used for solution preparation. In the second case, TiOSO4 and Fe2(SO4)3 salts of purities ca. 99.7% and 99.9% were added to the starting solution in order to obtain a solution containing Ti and Fe impurities. The synthetic solutions were then subjected to solvent extraction using D2EHPA, purchased from Lanxess, Germany, at an organic to aqueous volumetric ratio of 1. The loaded organic phase was then stripped using a 3 mol/L NH4F solution at an aqueous to organic volumetric ratio of 1 in order to concentrate Sc in the aqueous phase. Coextraction of Fe and Ti impurities occurred and the composition of the strip liquors is shown in Table 1.

Table 1 Strip liquor compositions and pH values
Full size table

Materials

Table 1 shows the pH and average compositions of the strip liquors in a 3 mol/L NH4F solution.

An Orion Star A211 pH meter was used for pH measurements under ambient conditions (ca. 20 °C) and the total metal ion concentrations were determined by ICP-OES (ThermoScientific iCAP 7000 series). The phase of the dried precipitates was determined using a SIEMENS powder X-Ray Diffractometer D5000. A JEOL JSM-6490LV Scanning Electron Microscope (SEM) was used to capture images of the solid precipitates obtained by cooling crystallization. A Phillips SL 30 Environmental Scanning Electron Microscope (ESEM) equipped with EDS was used to capture images of the solid precipitates obtained by antisolvent crystallization and to analyze the surface composition of the solids.

For antisolvent crystallization experiments, reagent grade absolute ethanol (99.94% v/v) was used as the antisolvent (AS). A temperature-controlled water bath circulator was used to maintain the desired temperature for all experiments by means of a PT100 temperature sensor with an accuracy of ± 0.01 °C.

Procedure

A methodology was developed to investigate the crystallization behavior of the strip liquor and to determine which solid phase was most stable under various operating conditions, that is different temperatures and different AS dosages.

Cooling Crystallization

A sample of 100 g (ca. 95 mL) of strip liquor (A) was cooled at a rate of 0.5 °C per minute, and the first solid precipitate was observed at 13 °C. The liquor was maintained at 13 °C under stirring at 600 rpm for a period of 72 h to attain equilibrium. Initially, supernatant samples were collected on a daily basis, and it was predetermined that 72 h was sufficient to achieve equilibration. At the end of the experiment, a 2 mL supernatant sample was obtained by means of a 0.2-μm polypropylene syringe filter, and the remaining suspension was filtered under vacuum using a 0.22 μm PVDF membrane filter. The total concentration of metal ions was determined using ICP-OES. The solid precipitate was subjected to natural evaporation until its weight remained appreciably constant. A solid sample was analyzed by powder XRD. SEM analyses were conducted to obtain crystal morphology. The supernatant obtained after filtration was then maintained at a lower temperature for another 72 h and the above procedure was repeated for each temperature investigated. Operating temperatures investigated were 13, 10, 8, 6, 3, and 1 °C, respectively.

Antisolvent Crystallization

Absolute ethanol was added to 50 mL of strip liquor (B) to achieve ethanol-to-strip liquor volumetric ratios of 0.2 to 1.4 at intervals of 0.2. The resulting suspension was then maintained at 25 °C under stirring at 600 rpm for 72 h to achieve equilibration. The solid precipitate obtained was filtered off and then washed using 10 mL of absolute ethanol and analyzed by SEM to obtain crystal morphology. Sample collection and analyses of the supernatant and solid samples were conducted as outlined above. Strip liquor (C) containing higher levels of Ti was also used under similar conditions at ratios of 0.2 and 1.4 to investigate the behavior of Ti during precipitation. All experiments were conducted in triplicate to ascertain reproducibility. In both cooling and antisolvent crystallization, the total Sc concentration obtained by ICP-OES analyses after 72 h of equilibration was taken to be the solubility determined from the supersaturated state.

A separate set of experiments was conducted by the same method using strip liquor (C) at volumetric ratios of 0.2, 0.8 and 1.4, with a residence time of 1 h, in an attempt to determine the mechanism of impurity uptake in the solid product. The solid precipitates were analyzed by ESEM–EDS to determine the surface elemental composition.

Results and Discussion

Solid Phase

The stable phase obtained at all temperatures in the range 1–13 °C for cooling crystallization and at 25 °C for antisolvent crystallization at different ethanol-to-strip liquor ratios was determined by powder XRD to be ammonium scandium hexafluoride (NH4)3ScF6 of monoclinic structure, PDF card 00-040-0595 [31, 33], see Fig. 1.

Fig. 1
figure 1

XRD pattern obtained for the solid product

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Solubility

The solubility was calculated for the phase (NH4)3ScF6 on the basis of total Sc concentration obtained by ICP-OES. Figure 2a shows the solubility in g/L of (NH4)3ScF6 at different temperatures in the range 1–13 °C in a 3 mol/L NH4F strip liquor (A). Figure 2b shows the solubility data obtained using strip liquors (B) and (C) at varying ethanol-to-strip liquor volumetric ratios for antisolvent crystallization at 25 °C.

Fig. 2
figure 2

Solubility of (NH4)3ScF6 phase: a in 3 mol/L NH4F strip liquor solution at different temperatures, b in different ethanol-to-strip liquor ratios at 25 °C

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As expected and shown in Fig. 2a, the solubility decreased almost linearly with the decreasing temperature. It can be noted that complete recovery of the salt is practically impossible due to the solubility limitation at the lowest temperature of 1 °C investigated. The solubility data obtained is indispensable in conducting controlled cooling crystallization experiments.

Figure 2b shows that the solubility decreased asymptotically with the increasing amount of ethanol added almost approaching zero at ethanol-to-strip liquor volumetric ratios above 1. This means that a high recovery close to 100% of the stable phase can be obtained as depicted in Fig. 3b. The solubilities of (NH4)3ScF6 obtained using strip liquor (C) at ratios 0.2 and 1.4 were similar to the data obtained for strip liquor (B). It was also observed that the pH of the mixtures increased almost linearly between 6.1 and 6.8 with the increasing quantity of ethanol.

Fig. 3
figure 3

Cumulative yield %: a cooling crystallization of SL (A), b antisolvent crystallization of SL (B)

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Yield

Figures 3a and b show the cumulative yield (%) obtained during cooling and antisolvent crystallization, respectively. Equation 1 was used to calculate the yield for cooling crystallization (Yc, %), where, Ci is the initial Sc concentration in the strip liquor and Cs is the solubility at the specific temperature.

$$ Y_{c} ,\% = \frac{{100\left( {C_{i} - C_{s} } \right)}}{{C_{i} }} $$
(1)

For antisolvent crystallization, the concentrations in Eq. 1 were multiplied by the respective solution volumes due to significant changes in volume upon addition of ethanol. It should be noted that the volumes are not additive upon adding ethanol to the strip liquor. The densities of the new solvent mixtures were determined to facilitate a correct mass balance. The yield was also determined by weighing the dry solid samples, Yw. During cooling crystallization, the cumulative yield increased with the decreasing operating temperature due to reduction in solubility, see Fig. 3a. It can be noted that the highest yield obtained at 1 °C was below 50%.

It is recommended to investigate cooling crystallization at subzero temperatures to determine if the yield would increase remarkably or asymptotically. However, employing subzero temperatures to the dilute strip liquor could result in formation of large quantities of ice, which could entrap all the salt precipitate. This could be uneconomical given that the Sc content to be recovered is only a minute quantity. Likewise, Fig. 3b shows the cumulative yield (%) obtained during antisolvent crystallization. High yields above 65% were obtained even at the lowest mixing ratio of 0.2. It can be noted that a ratio of 0.8 is optimal, and any further increase in ratio does not result in significant increase in the yield. Although huge quantities of ethanol are required, the increase in raw material costs is counterbalanced by the fact that the ethanol can be recovered by distillation and reused in the process. The data in Fig. 3 also indicate that combining the two crystallization techniques and conducting antisolvent crystallization at a lower temperature could improve the product yield while reducing the antisolvent required.

In both cases, the yield obtained by weighing the solid (Yw) is lower than the calculated yield (Yc). This can be attributed to dissolution of the solid product during the filtration and washing stages. This difference is more pronounced for antisolvent crystallization probably due to the minute crystals obtained as shown in Fig. 5, hence low filterability and greater dissolution extent. In addition, part of the crystals could have passed through the membrane filter.

Morphology and Crystal Size

Figure 4 shows the morphology of the crystals obtained by cooling crystallization at 13, 6 and 1 °C. The crystals obtained by cooling crystallization had regular prismatic shapes indicating that a highly crystalline (NH4)3ScF6 product can be obtained. The product obtained at 13 °C had numerous fines of sizes approximately 10 μm probably due to primary nucleation. Larger crystals were observed for the lower temperatures possibly due to carry-over of some fine crystals during filtration, which in turn, induced secondary nucleation in subsequent lower temperature experiments.

Fig. 4
figure 4

Morphology of the precipitates obtained by cooling crystallization at 13, 6 and 1 °C

Full size image

The effect of the thermal history of the solution on inducing nucleation at a higher temperature, hence lower supersaturation could also play a role [12]. When a solution is cooled to supersaturation resulting in nucleation, the thermal treatment, that is, the heating temperature and duration that the solution undergoes during dissolution of crystals has an effect on the metastable zone width, induction time, hence nucleation upon cooling the same solution again. In general, it was hypothesized that during the initial dissolution phase of crystals, the solution retains some molecular assemblies that promote nuclei formation at a reduced supersaturation [34, 35]. A similar phenomenon could have occurred upon filtration and washing of the solid product resulting in molecular assemblies passing through the membrane filter into the solution that was cooled to lower temperatures in subsequent experiments. Crystals of sizes approaching 50 μm were observed at 6 and 1 °C. By designing a seeded cooling crystallization process, there is potential to obtain even larger product crystals.

Figure 5 shows the morphology of crystals obtained from strip liquor (C) by antisolvent crystallization at 25 °C at ethanol-to-strip liquor ratios of 0.2 and 1.4, respectively.

Fig. 5
figure 5

Morphology of the precipitates obtained by antisolvent crystallization at 25 °C: a ratio 0.2 and b ratio 1.4

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For antisolvent crystallization, discrete minute crystals of defined shapes and sizes of approximately < 2 μm were observed. The fine crystals were attributed to a very high supersaturation generated upon adding the ethanol to the strip liquor, resulting in dominance of nucleation over crystal growth. The crystals decreased in size with the increasing ethanol content due to the increasing supersaturation. The ethanol was added wholly and it was observed that crystallization was instantaneous throughout the entire solution volume due to high bulk supersaturation. For this reason, it is very imperative to control the rate of supersaturation generation in order to obtain larger crystals. This can be accomplished by controlling the rate of addition of the antisolvent, coupled with adequate agitation to prevent high local supersaturation at the point of mixing. Seeding can also improve the crystal sizes since it promotes crystal growth. If this control is mastered, antisolvent crystallization serves as a better alternative for the recovery of (NH4)3ScF6 from the strip liquor, since higher yields are obtained with possible reuse of the ethanol solvent for a cost effective operation.

Impurity Incorporation

Figure 6 shows the impurity (Ti, Fe) content in the solid product obtained from strip liquor (C) by antisolvent crystallization as determined by ICP-OES after dissolving the solid samples.

Fig. 6
figure 6

Impurity content in the solid product at AS/SL ratios 0.2 and 1.4

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The Fe and Ti contents in the solid product increased upon increasing the AS/SL ratio from 0.2 to 1.4. The solid product purities obtained at ratios 0.2 and 1.4 were 98.9 and 98.7%, respectively. After performing a mass balance, it was observed that the concentration of Fe in the supernatant decreased by more than 90% with the increasing AS concentration, while the concentration of Ti remained fairly constant. The precipitation percentages of Fe were computed by Eq. 2, where P is the precipitation percentage, subscript ‘Me’ refers to the metal impurity (Fe), CMe,i and CMe,f are the initial and final concentrations of the metal in solution, and Vi and Vf are the initial and final volumes, respectively.

$$ P_{Me} = \frac{{C_{Me,i} .V_{i} - C_{Me,f} .V_{f} }}{{C_{Me,i} .V_{i} }} \times 100 $$
(2)

The precipitation percentage of Fe was high (98.4 and 98.2% at an AS/SL ratio of 0.8 and 1.4, respectively), but since the initial concentration in the strip liquor is quite low, this does not translate into very high impurity concentrations in the solid product. The Fe and Ti detected in the solid phase could have either coprecipitated as separate phases (e.g., (NH4)3FeF6 and (NH4)2TiF6) and/or have been incorporated in the (NH4)3ScF6 crystal lattice. The solubilities of the Fe and Ti phases are unknown under the experimental conditions. The only phase detected by Powder XRD was (NH4)3ScF6 (Fig. 1).

Further investigations were conducted to gain an insight into the mechanism of impurity uptake into the solid product. Table 2 shows the average Ti and Fe concentrations in the solid precipitate, in wt%, as determined by EDS analyses at different ratios for two sets of experiments.

Table 2 Impurity concentrations (detected by ESEM-EDS)
Full size table

The results are similar to the ones obtained by ICP-OES (after dissolving the solid sample and analyzing the concentrations in the liquid phase) presented in Fig. 6 except that the Fe content decreased slightly with the increasing ethanol-to-strip liquor ratio. Appendix A shows the EDS analysis for one of the experiments conducted at a ratio of 0.8. The EDS analyses revealed that Fe was homogeneously distributed throughout the solid surface layer, while Ti was only detected in lower concentrations at a few specific regions. The even distribution of Fe in the surface layer could imply that Fe was incorporated into the (NH4)3ScF6 crystal lattice substituting Sc ions proportionately, otherwise if Fe had precipitated as separate crystals homogeneously spread in the solid product, it would have been expected that the Fe content would be much higher than the percentages detected by EDS. The ionic radii of Sc3+ and Fe3+ are 74.5 and 64.5 pm, respectively [36]. The ionic radii of Ti4+ is 60.5 pm [36], and Ti4+ is less likely to compete with Sc3+ ions due to the fact that Ti binds strongly to oxygen exhibiting the characteristic titanyl bond [37]. Ti was detected only at a few points, where it was detected together with Sc and Fe indicating that it could have precipitated as a mixed phase.

In the downstream final refinement stage of Sc by sublimation, impurities that have comparable or higher vapor pressure than Sc (e.g., Fe) are difficult to remove, while it is easier to separate Ti due to its lower vapor pressure at the sublimation temperatures employed (> 2000 °C). Therefore, it would be desirable to further reduce the Fe content in the solid product in order to obtain a purer final scandium metal. There is potential to improve the purity of the product by controlling the rate of ethanol addition and seeding as shown in a preliminary study in our lab [38].

Conclusions and Recommendations

The technical feasibility of recovering Sc from strip liquor as (NH4)3ScF6 using cooling and antisolvent crystallization techniques has been proven. While cooling crystallization produced a precipitate with larger crystal sizes, its applicability is limited by the higher product solubility at the lowest temperature investigated with (NH4)3ScF6 yield less than 50%. On the other hand, antisolvent crystallization produced a very high yield of the solid product, but with very minute crystals (~ 2 µm), which have an undesirable impact on the filtration and washing efficiency. However, a tradeoff has to be considered between better filtration efficiency and high efficiency in downstream processing with respect to crystal size. Through EDS analyses, it was postulated that Fe3+ ions were incorporated in the (NH4)3ScF6 crystal lattice due to almost comparable ionic radii of Sc3+ and Fe3+ ions resulting in homogeneous distribution of Fe in the crystals. Ti was only detected at a few specific regions on the solid surface in minute quantities. It is recommended to conduct seeded and supersaturation-controlled experiments in order to improve crystal size and purity, and also conduct antisolvent crystallization experiments at lower temperatures to improve yield and reduce the quantity of the antisolvent required.

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Acknowledgements

This project has received funding from the European Union’s Horizon 2020 research and innovation program under grant agreement No. 730105-SCALE.

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Authors and Affiliations

  1. Department of Chemical Engineering, KTH Royal Institute of Technology, 100-44, Stockholm, Sweden

    Edward Michael Peters & Kerstin Forsberg

  2. Mining Engineering Department, Middle East Technical University, 06800, Ankara, Turkey

    Şerif Kaya

  3. MEAB Chemie Technik GmbH, 52068, Aachen, Germany

    Carsten Dittrich

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Correspondence to Kerstin Forsberg.

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The contributing editor for this article was Yiannis Pontikes.

Appendix A: EDS Analyses of the Solid Sample Obtained from SL (C) at Ethanol-to-Strip Liquor Volumetric Ratio of 0.8

Appendix A: EDS Analyses of the Solid Sample Obtained from SL (C) at Ethanol-to-Strip Liquor Volumetric Ratio of 0.8

figure a

Processing option: all elements analyzed (Normalized)

Spectrum N F Sc Ti Fe Total
wt%
(1,1) 13.80 49.88 34.91   1.40 99.99
(2,1) 14.82 59.05 25.19   0.95 100.01
(3,1) 14.68 56.68 27.10 0.49 1.05 100.00
(4,1) 15.01 53.87 29.93   1.18 99.99
(1,2) 13.21 45.51 39.76   1.53 100.01
(2,2) 13.26 58.61 27.10   1.04 100.01
(3,2) 11.94 51.26 35.54   1.26 100.00
(4,2) 13.32 50.97 34.36   1.36 100.00
(1,3) 13.80 54.38 30.62   1.20 100.00
(2,3) 12.04 46.54 39.92   1.50 100.00
(3,3) 12.70 53.54 32.48   1.30 100.01
(4,3) 14.42 50.15 33.39 0.52 1.51 99.99
(1,4) 14.65 59.14 25.27   0.94 100.00
(2,4) 13.51 57.36 28.02   1.11 99.99
(3,4) 13.87 55.86 29.30   0.96 99.99
(4,4) 13.89 54.00 30.95   1.15 100.00
(1,5) 16.56 59.89 22.70   0.86 100.01
(2,5) 15.45 61.31 22.39   0.84 99.99
(3,5) 14.04 55.37 29.53   1.05 99.99
(4,5) 13.99 53.07 31.22 0.37 1.35 100.00
Average 13.95 54.32 30.48 0.46 1.18  
Max 16.56 61.31 39.92 0.52 1.53  
Min 11.94 45.51 22.39 0.37 0.84  

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Peters, E.M., Kaya, Ş., Dittrich, C. et al. Recovery of Scandium by Crystallization Techniques. J. Sustain. Metall. 5, 48–56 (2019). https://doi.org/10.1007/s40831-019-00210-4

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Keywords

  • Ammonium scandium hexafluoride
  • Cooling crystallization
  • Antisolvent crystallization
  • Purity
  • Solubility
  • Impurity incorporation