scholarly journals Solvent Extraction of Sc(III) by D2EHPA/TBP from the Leaching Solution of Vanadium Slag

Metals ◽  
2020 ◽  
Vol 10 (6) ◽  
pp. 790
Author(s):  
Xuejiao Cao ◽  
Ting-an Zhang ◽  
Weiguang Zhang ◽  
Guozhi Lv
Keyword(s):  
Solvent Extraction ◽  
Thermodynamic Analysis ◽  
Organic Phase ◽  
Species Distribution ◽  
Extraction Process ◽  
Optimal Conditions ◽  
Vanadium Slag ◽  
Extractant Concentration ◽  
Leaching Solution ◽  
Loaded Organic Phase

The solvent extraction of scandium by the mixture of di-(2-ethylhexyl) phosphate (D2EHPA) and tri-n-butyl phosphate (TBP) has been investigated in the acidic leaching solution of vanadium slag. Thermodynamic analysis of the species distribution diagrams on the Sc-S-H2O system showed that scandium mainly exists as Sc3+ and Sc(SO4)+, and sulfur mainly exists as HSO4− in the actual leaching solution of vanadium slag (pH = −0.75). The extraction process was studied to optimize various parameters such as the extractant concentration, dosage of TBP, phase ratio, and stirring speed. The results indicated that 83.64% of scandium and less than 2% of co-extracted elements were extracted under optimal conditions. Then, over 95% of the co-extracted elements and less than 1.1% of scandium were scrubbed from the loaded organic phase by 4.0 mol/L of HCl. Finally, 87.20% of scandium was stripped with 2 mol/L of NaOH and 1 mol/L of NaCl at a stripping O/A of 1:1.

Solvent Extraction and Stripping of Tetravalent Titanium from Acidic Chloride Solutions by Trioctylphosphine Oxide

2012 ◽  
Vol 550-553 ◽  
pp. 616-621
Author(s):  
Xue Hua Mao ◽  
Dai Jun Liu
Keyword(s):  
Solvent Extraction ◽  
Organic Phase ◽  
Chloride Concentration ◽  
Extraction Process ◽  
Trioctylphosphine Oxide ◽  
Extractant Concentration ◽  
Total Chloride ◽  
Chloride Solutions ◽  
Acidic Chloride ◽  
Kinetics Of

The solvent extraction and stripping of titanium(Ⅳ) from acidic chloride solutions by trioctylphosphine oxide（TOPO） in kerosene has been investigated. The solvent extraction results demonstrate that the extracted titanium is present as TiCl4.2TOPO. The kinetics of the extraction process is very fast, since the equilibrium is reached in 5 min. In addition, the extraction of titanium (Ⅳ) increases with the total chloride concentration in the aqueous phase, as well as with the extractant concentration in the organic phase. The loading capacity of TOPO for titanium (Ⅳ) is 4.60g/100g TOPO. The stripping results show that when the O/A phase radio changing from 1 to 10, titanium (Ⅳ) is completely stripped from the mental loaded organic phase of TOPO with 1 mol dm-3 hydrochloric acid. Thus titanium (Ⅳ) can be enriched to tenfold concentration by the stripping.

scholarly journals Study on the Effect and Mechanism of Impurity Aluminum on the Solvent Extraction of Rare Earth Elements (Nd, Pr, La) by P204-P350 in Chloride Solution

Minerals ◽  
2021 ◽  
Vol 11 (1) ◽  
pp. 61
Author(s):  
Wenjie Zhang ◽  
Xian Xie ◽  
Xiong Tong ◽  
Yunpeng Du ◽  
Qiang Song ◽  
...  
Keyword(s):  
Rare Earth ◽  
Solvent Extraction ◽  
Rare Earth Elements ◽  
Organic Phase ◽  
Extraction Process ◽  
Industrial Applications ◽  
Separation And Purification ◽  
Aluminum Ion ◽  
Hydrochloric Acid Medium ◽  
Impurity Ion

Solvent extraction is the most widely used method for separation and purification of rare earth elements, and organic extractants such as di(2-ethylhexyl) phosphoric acid (P204) and di(1-methyl-heptyl) methyl phosphonate (P350) are most commonly used for industrial applications. However, the presence of impurity ions in the feed liquid during extraction can easily emulsify the extractant and affect the quality of rare earth products. Aluminum ion is the most common impurity ion in the feed liquid, and it is an important cause of emulsification of the extractant. In this study, the influence of aluminum ion was investigated on the extraction of light rare earth elements by the P204-P350 system in hydrochloric acid medium. The results show that Al3+ competes with light rare earths in the extraction process, reducing the overall extraction rate. In addition, the Al3+ stripping rate is low and there is continuous accumulation of Al3+ in the organic phase during the stripping process, affecting the extraction efficiency and even causing emulsification. The slope method and infrared detection were utilized to explore the formation of an extraction compound of Al3+ and the extractant P204-P350 that entered the organic phase as AlCl[(HA)2]2P350(o).

scholarly journals Modelling and Optimizing the Solvent Extraction of Cadmium from Phosphoric Acid using Experimental Design

2021 ◽  
Vol 33 (3) ◽  
pp. 637-643
Author(s):  
K. Berkalou ◽  
A. Nounah ◽  
H. Chaair ◽  
M. Khamar ◽  
R. Boussen ◽  
...  
Keyword(s):  
Solvent Extraction ◽  
Experimental Design ◽  
Phosphoric Acid ◽  
Graphical Representation ◽  
Extraction Process ◽  
Optimal Conditions ◽  
Anova Analysis ◽  
Stirring Rate ◽  
Stirring Time ◽  
Variable Space

The removal of cadmium from phosphoric acid was carried out using the solvent extraction process, taking into account factors such as pH, concentration of the extracting agent [EA], organic phase/aqueous phase (O/A) ratio, stirring time and stirring rate. In order to study the effect of these involved factors and their interactions on the extraction percentage of cadmium, a composite central design (CCD) of 24 experiments was adopted. An empirical model was developed and validated by applying ANOVA analysis. The graphical representation of this model in the variable space allowed to determine the optimal conditions of these factors. The extraction of cadmium from phosphoric acid reached a percentage of the order of 98%, under the following conditions: pH = 3, [EA] = 10-2 M, O/A = 1.1, stirring time 90 min, stirring rate 800 rpm.

scholarly journals The Manufacture of Synthetic Rutile by Solvent Extraction of Tri-Alkyl Phosphine Oxide from HCl Leaching Solution of Soda-Roasted Ilmenite Ore

Metals ◽  
2020 ◽  
Vol 10 (5) ◽  
pp. 588
Author(s):  
Sung-Ho Joo ◽  
Dong Ju Shin ◽  
Dongseok Lee ◽  
Jungshin Kang ◽  
Min-seuk Kim ◽  
...  
Keyword(s):  
Solvent Extraction ◽  
Organic Phase ◽  
Phosphine Oxide ◽  
Inductively Coupled Plasma ◽  
Spherical Shape ◽  
Feed Solution ◽  
Synthetic Rutile ◽  
Inductively Coupled ◽  
Leaching Solution ◽  
Series Of Experiments

To manufacture TiO2, a high-purity synthetic rutile, the recovery of Ti was investigated using a hydro-metallurgical process. Using a feed solution containing 32050 mg/L Ti, 110 mg/L Si, 88 mg/L Nb, 2614 mg/L Fe, and 130 mg/L Zr, solvent-extraction experiments were conducted with alkyl phosphine oxide in conjunction with diluents such as kerosene and xylene. The results showed that the extraction mechanism of both diluents was very similar to slope analysis, which had a value of 1.9; however, the extraction equilibrium constant value of organic–metallic species in xylene as a diluent was lower than in kerosene as a diluent. This result affected the stripping efficiency of Ti in particular; therefore, xylene was selected as a diluent. To recover Ti ion from a leaching solution, a series of experiments was conducted, such as the McCabe–Thiele method and countercurrent simulation test for extraction and stripping of Ti. As a result, Ti and impurities such as Fe and Zr were extracted to 99.9% from Si and Nb under optimal conditions using countercurrent four-stage extraction, with 1 M Cyanex 923 at a ratio of organic phase/ aqueous phase=3. In the stripping test, Ti was selectively stripped to 90.1% from Fe and Zr in the organic phase by 1 M HCl. The obtained powder, which was hydrolyzed from an impurity-free solution, was analyzed to a purity of 99.9% by inductively coupled plasma. The TiO2, which has a spherical shape and a diameter of approximately 2 µm according to SEM, was evident by XRD.

scholarly journals Selective Recovery of Molybdenum over Rhenium from Molybdenite Flue Dust Leaching Solution Using PC88A Extractant

Metals ◽  
2020 ◽  
Vol 10 (11) ◽  
pp. 1423
Author(s):  
Ali Entezari-Zarandi ◽  
Dariush Azizi ◽  
Pavel Anatolyevich Nikolaychuk ◽  
Faïçal Larachi ◽  
Louis-César Pasquier
Keyword(s):  
Dft Calculations ◽  
Organic Phase ◽  
Density Functional ◽  
Leach Solution ◽  
Interaction Energies ◽  
Extractant Concentration ◽  
Flue Dust ◽  
Calculation Results ◽  
Leaching Solution ◽  
Experimental Findings

Selective solvent extraction of molybdenum over rhenium from molybdenite (MoS2) flue dust leaching solution was studied. In the present work, thermodynamic calculations of the chemical equilibria in aqueous solution were first performed, and the potential–pH diagram for the Mo–Re–SO42−–H2O system was constructed. With the gained insight on the system, 2-ethylhexyl phosphonic acid mono-(2-ethylhexyl)-ester (PC88A) diluted in kerosene was used as the extractant agent. Keeping constant the reaction temperature and aqueous-to-organic phase ratio (1:1), organic phase concentration and pH were the studied experimental variables. It was observed that by increasing the acidity of the solution and extractant concentration, selectivity towards Mo extraction increased, while the opposite was true for Re extraction. Selective Mo removal (+95%) from leach solution containing ca. 9 g/L Mo and 0.5 g/L Re was achieved when using an organic phase of 5% PC88A at pH = 0. No rhenium was coextracted during 10 min of extraction time at room temperature. Density functional theory (DFT) calculations were performed in order to study the interactions of organic extractants with Mo and Re ions, permitting a direct comparison of calculation results with the experimental data to estimate selectivity factors in Mo–Re separation. For this aim, PC88A and D2EHPA (di-(2-ethylhexyl) phosphoric acid) were simulated. The interaction energies of D2EHPA were shown to be higher than those of PC88A, which could be due to its stronger capability for complex formation. Besides, it was found that the interaction energies of both extractants follow this trend considering Mo species: MoO22+ > MoO42−. It was also demonstrated through DFT calculations that the interaction energies of D2EHPA and PC88A with species are based on these trends, respectively: MoO22+ > MoO42− > ReO4− and MoO22+ > ReO4− > MoO42−, in qualitative agreement with the experimental findings.

The Saponification Extraction Process and Result Analysis of Rare Earth Organic Phase

2013 ◽  
Vol 668 ◽  
pp. 132-135
Author(s):  
Yan Mei ◽  
Zuo Ren Nie
Keyword(s):  
Rare Earth ◽  
Organic Phase ◽  
Extraction Process ◽  
Rare Earth Ions ◽  
Ir Absorption ◽  
Absorption Frequency ◽  
Naoh Solution ◽  
Loaded Organic Phase ◽  
Result Analysis ◽  
The Rare Earth

10mol/L NaOH solution was used to saponify P507 (2-ethylhexylphosphonic acid mono-2-ethylhexyl ester) and then to extract and strip the rare earth cerium solution. The experimental procedure and results of the saponified organic phase and loaded organic phase were analyzed using IR spectrum and electrical conductivity meter. The results suggested the conductance value achieved highest when the saponified degree of alkaline solution was 60-80%, and the saponified organic phase formed a single-phase stable and uniform microemulsion. While the rare earth were extracted by P507, the IR absorption frequency of P=O decreased while the absorption intensity increased, suggesting that P=O group had been coordinated with the rare earth ions. More colloidal agglomerates in the loaded organic phase appeared when more rare earth was loaded.

Experimental Study on Extraction of Scandium from Complex Silicate Ore

2013 ◽  
Vol 734-737 ◽  
pp. 1037-1040
Author(s):  
Qing Rong Yang ◽  
Gui Fang Zhang ◽  
Peng Yan
Keyword(s):  
Experimental Study ◽  
Organic Phase ◽  
Mixing Time ◽  
Extraction Rate ◽  
Impact Factors ◽  
Optimal Conditions ◽  
Extractant Concentration ◽  
Leaching Experiments ◽  
The Impact ◽  
Extraction Agent

Based on leaching experiments of complex silicate ore contenting scandium, the research has adopted extraction to concentrate scandium and separate impurity. The emphasis of this reaserch is the impact factors, so the experiments including extractant concentration, organic aqueous ratio, mixing time, organic phase washing, organic phase reextraction, have been conducted. The optimal conditions are that the concentration of extraction is 25%, the O/A is 1:10, the mixing time is 3min, the washing time is 3, the O/A of reextraction is 1:2.3, and the extraction rate of exceeding 98% and reextracion rate of 99.01% were obtained when adopting P501 as the extraction agent.

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