Recovery Of Vanadium Research Articles

Reduction Roasting of a Titanomagnetite Concentrate with the Formation of a Titanium–Vanadium Slag Suitable for the Subsequent Recovery of Vanadium and Titanium

Reduction Roasting of a Titanomagnetite Concentrate with the Formation of a Titanium–Vanadium Slag Suitable for the Subsequent Recovery of Vanadium and Titanium

Full-process analysis on volatilizing gold, zinc by chlorination roasting and synchronous recovery vanadium by water leaching of carbonaceous gold ore

This paper describes the chlorination roasting-water leaching process for the volatilization separation of gold, zinc and simultaneous vanadium recovery from carbonaceous gold ore. Chlorination roasting was conducted on carbonaceous gold ore. The chlorination residue and volatile precipitates were examined for textural and chemical properties. The results, and the thermodynamic calculations performed using HSC, showed that gold reacts directly with NaCl to produce AuCl for volatilization, promoting associated mineral FeS2 or C. Also, ZnS can be chlorinated to produce ZnCl for volatilization directly or indirectly. FeS2 is mainly converted into Fe2O3 and retained in the chlorination residue. Low-valent vanadium (V(III), V(IV)) primarily reacts with NaCl to form NaVO3. Under optimized conditions, roasting carbonaceous gold ore with 10 wt% NaCl at 800 ℃ yielded to 92.05% gold, 92.56% zinc and ＜5% iron volatilization, respectively. After grinding the chlorination residue to < 0.074 mm particle sizes, 85.34% vanadium was recovered by water leaching extraction at 80 ℃, 10:1 liquid–solid ratio, 500 r/min stirring speed, and 4 h extraction time. The present approach may efficiently volatilize gold, zinc, recover vanadium, and separate iron from carbonaceous gold ore.

Comparison and evaluation of vanadium extraction from the calcification roasted vanadium slag with carbonation leaching and sulfuric acid leaching

Calcification roasting process for vanadium extraction has advantages in environmental protection, low cost of roasting additives, easy reutilization of the tailings. During the calcification roasting process, the vanadium spinel contained in the converter vanadium slag transforms into calcium vanadate. Carbonation leaching and sulfuric acid leaching used for extracting vanadium from the calcification roasted slag were compared and evaluated in detail, and effects of leaching parameters and the leaching kinetics were investigated. It was found that grinding the roasted slag particles below 94 μm can ensure a higher vanadium recovery. Leaching temperature, concentration of the ammonium carbonate, solid to liquid ratio all impacted the recovery of vanadium significantly. Under the conditions of temperature of 353 K, ammonium carbonate concentration of 200 g/L and solid to liquid ratio of 1:20 g/mL, 73.67% of the vanadium was extracted in 60 min. In the sulfuric acid leaching process, the aqueous pH value played a vital role and it was better to conduct the leaching at temperatures below 323 K. The sulfuric acid leaching reactions progressed fast and under a solid to liquid ratio of 1:10 the leaching efficiency of vanadium reached around 84% at 313 K and pH 2.50 in less than 30 min. Both leaching processes can be well described by the kinetic equation of 1/5(1 − α)−5/3 − 1/4(1 − α)-4/3 + 1/20 = kt, which represents the leaching process is controlled by diffusion of the two reactants in both directions. The difference lies in that the solid layer which the reactants pass through is mainly composed of silicate phases and Fe-rich phases in the ammonium carbonate leaching process, while in the sulfuric acid leaching process, calcium sulfate which instantaneously generates and tightly wraps the unreacted core, plays a dominant role in limiting the diffusion of the reactants. The ammonium carbonate leaching performs better in selectivity over the vanadium than the sulfuric acid leaching, but collection of ammonia and enrichment of vanadium-bearing solution should be considered..

Vanadium recovery by electrodialysis using polymer inclusion membranes

Industrial applications and environmental awareness recently prompted vanadium recovery spell from secondary resources. In this work, a polymer inclusion membrane containing trioctylmethylammonium chloride as carrier was successfully employed in electrodialysis for vanadium recovery from acidic sulfate solutions. The permeability coefficient of V(V) increased from 0.29 µm·s-1 (without electric field) to 4.10 µm·s-1 (with the 20 mA·cm-2 current density). The transport performance of VO2SO4-, which was the predominant species containing V(V) in the acidic region (pH <3), was influenced by the aqueous pH value and sulfate concentration. Under an electric field, a low concentrated H2SO4 solution (0.2 M) effectively stripped V(V) from the membranes, avoiding the requirement of a highly concentrated H2SO4 without electric field. Under the optimum conditions, the permeability coefficient and flux reached 6.80 µm·s-1 and 13.34 µmol·m-2·s-1, respectively. High selectivity was observed for the separation of V(V) and Mo(VI) from mixed solutions of Co (II), Ni (II), Mn (II), and Al (III). Additionally, the separation between Mo(VI) and V(V) was further improved by adjusting the acidity of the stripping solution. The V(V) selectivity for the resulting membrane was higher than that of commercial anion exchange membranes.

Recovery of vanadium from direct acid leaching solutions of weathered crust vanadium‐titanium magnetite via solvent extraction with N235

In this study, we developed a new method for the efficient extraction and separation of V from direct acid leaching solutions of weathered crust VTi magnetite using N235/TBP, sodium sulfate (Na2SO4), and sodium carbonate (Na2CO3) as the extraction system and washing and stripping agents, respectively. The effects of various experimental conditions on the extraction results were investigated, and the extraction efficiency of V was approximately 70% with <4% Fe co-extraction under optimal conditions. A four-stage countercurrent extraction method was used to extract >96% of V and <4.5% of Fe, and the separation factor of V/Fe was 541. Upon washing the V-loaded organic phase with a 0.70 mol/L Na2SO4 solution, >96% of Fe and ~1% of V were removed. Moreover, upon stripping the purified organic phase with a 0.70 mol/L Na2CO3 solution, >98% of V was recovered. The effects of other impurities on the separation of V were negligible. Moreover, the stripped organic phase can be recycled sustainably during extraction. In this study, we selectively separated V and provided a new method for accelerating the purification and enrichment of V, which is present at low concentrations in acid leaching solutions.

Stepwise separation and recovery of molybdenum, vanadium, and nickel from spent hydrogenation catalyst

Recovering metal values in hazardous spent hydrogenation catalysts is of vital economic and environmental importance. Herein, the selective recovery of valuable molybdenum (Mo), vanadium (V), and nickel (Ni) from spent hydroprocessing catalysts are achieved by using a sulfuric acid leaching-stepwise extraction process. After roasting in the air at 400 °C, the valuable metals are effectively leached within 20 min by 1 mol/L sulfuric acid at 75 °C. The leaching efficiency of Al, Ni, Mo, and V is 22.16%, 99.44%, 98.59%, and 100%, respectively. Based on the species analysis of the leachate, a stepwise extraction separation route was established for selective recovery of Mo, Ni, and V from the acidic leachate. Mo and V are preferentially co-extracted by the mixed TOA/Cyanex272 with a molar ratio of 7:3, which exhibits an excellent extraction selectivity over Ni and Al. Increasing the concentration of Cyanex272 in the mixed system can effectively improve the selective stripping of vanadium but slightly inhibit its extraction. Residual Ni in the raffinate can be selectively separated by 50%(V/V) commercial HBL110 with an extraction efficiency of 98.5%. Especially, the reductive sodium sulfite can greatly enhance the selective stripping of vanadium from the loaded organic phase. Residual Mo in the organic phase can be well stripped with an alkaline solution. The selective stripping mechanism of vanadium is revealed by the FT-IR and Raman spectra. This work proposes a sustainable stepwise separation route for recovering valuable metals in the spent hydroprocessing catalyst.

Vanadium recovery from Na2SO4-added V-Ti magnetite concentrate via grate-kiln process

Pilot experiments on Na2SO4-roasting of V-Ti magnetite (VTM) concentrate pellets were performed to activate vanadium with simulated grate-kiln machines. Combined with thermodynamic calculation, X-ray diffraction (XRD), scanning electron microscopy with energy-dispersive X-ray spectroscopy (SEM-EDS), and inductively coupled plasma-atomic emission spectrometry (ICP-AES) analyses, process parameters of pellet making were optimized, and the enhancement of vanadium oxidation and conversion was realized. The results show that, in balling stage, adding Na2SO4 can promote the thermal decrepitation resistance of green pellets; in the drying stage, higher wind temperature can improve the dispersion of sodium salt in pellets; in preheating stage, using O2-rich hot gas can promote more thorough oxidation of vanadium; in roasting stage, the effect of vanadium conversion to sodium vanadate is better when the liquid amount is 15.5%-22.5%. Based on the above measures, the vanadium conversion rate achieved in the roasted pellets is 85.6%, proving the feasibility of vanadium recovery using an existing pellet production line.

Will Vanadium-Based Electrode Materials Become the Future Choice for Metal-Ion Batteries?

Metal-ion batteries have emerged as promising candidates for energy storage system due to their unlimited resources and competitive price/performance ratio. Vanadium-based compounds have diverse oxidation states rendering various open-frameworks for ions storage. To date, some vanadium-based polyanionic compounds have shown great potential as high-performance electrode materials. However, there has been a growing concern regarding the cost and environmental risk of vanadium. In this Review, all links in the industry chain of vanadium-based electrodes were comprehensively summarized, starting with an analysis of the resources, applications, and price fluctuation of vanadium. The manufacturing processes of the vanadium extraction and recovery technologies were discussed. Moreover, the commercial potentials of some typical electrode materials were critically appraised. Finally, the environmental impact and sustainability of the industry chain were evaluated. This critical Review will provide a clear vision of the prospects and challenges of developing vanadium-based electrode materials.

Separation of vanadium and iron from the steelmaking slag convertor using Aliquat 336 and D2EHPA: Effect of the aqueous species and the extractant type

• For efficient separation of V and Fe, transformation of ferric to ferrous was found essential. • V +4 and V +5 species were both extracted through cation exchange reactions. • Through anion exchange reactions, only V +5 species were extracted. • Proper aqueous species of V/Fe were prepared prior to SX, through leaching and cementation operations. • Flow diagram of vanadium recovery from convertor slag was proposed. In this study, a selective process for separation of vanadium and iron from the steelmaking slag was proposed. The proposed process has a potential to be considered industrially due to its relative simplicity. The process for the separation of vanadium and iron is consisted of three main stages: leaching, cementation, and solvent extraction. The leaching and cementation stage, were designed such that the proper aqueous species of vanadium and iron for the solvent extraction stage got generated. In the solvent extraction experiments, the effect of vanadium and iron aqueous species and the extractant type (extraction through anion and cation exchange reactions) on the separation of these elements were studied. In the solvent extraction stage, D2EHPA (cationic exchange) and Aliquat 336 (anionic exchange) were used. The results, for both extractants, showed that for selective separation of vanadium and iron, conversion of ferric to ferrous is essential. By converting ferrous to ferric ion, almost no iron was extracted through the anion exchange. Through cation exchange, however, ferrous extraction was started at significantly higher pH values comparing to ferric ion. D2EHPA was shown to have the ability to extract vanadium with both oxidation states of +4 and +5. Aliquat 336, however, showed no extraction toward V +4 , and only extracted V +5 species. This was found due to the absence of anionic complexes of V +4 in a sulfuric acid solution. The extraction mechanism of vanadium through both anion and cation exchange reactions were studied. The results showed the formation of VO 2 R(RH) through cationic extraction and VO 2 SO 4 R 4 N for the anionic extraction. Finally, 90% vanadium stripping efficiency from D2EHPA and Aliquat 336 loaded organics were obtained using 2 M H 2 SO 4 and 3 M HCl solutions, respectively.

Development of Vanadium Recovery Process Using Reduction Pre-treatment from Vanadium Titanium-Magnetite (VTM) Ore

Development of Vanadium Recovery Process Using Reduction Pre-treatment from Vanadium Titanium-Magnetite (VTM) Ore

Thermochemical Modeling Factors in Roasting Pre-treatment using a Rotary Kiln for Efficient Vanadium Recovery

본 연구에서는 Rotary kiln(RK)을 이용하여 바나듐 염배소 전처리시 적정온도를 유지하기 위한 열화학적 모델링 관련 인자에 대해 논의하였다. 관련 모델 메카니즘은 열화학 관련 반응속도모델, 열수지 및 열전달 등이며 이를 통해 rotary kiln내 온도분포를 직관적으로 추정할 수 있다. 이러한 작업을 통해 최적 염배소 온도인 1000 °C(또는 약 1273 K) 근방을 kiln내에서 장기간 유지하는 것이 관건이다. 본 연구에서는 탄화수소(천연가스) 연료연소 및 광석 산화반응으로부터의 발열과 광석으로의 복사열전달 등을 산정하였다. 또한 열화학 측면에서 Rotary kiln내 적정 배소온도구역에서의 온도구배 완화를 위한 방안을 제시하였다.

Hydrogen reduction behaviors and mechanisms of vanadium titanomagnetite ore under fluidized bed conditions

Vanadium titanomagnetite ore has prominent latent applications in the recovery of iron, vanadium and titanium. In this study, the reduction effect and product characteristics of vanadium titanomagnetite ore using hydrogen as reductant under fluidized bed conditions were investigated by X-ray diffraction, scanning electron microscopy and energy dispersive spectrometer. Under the optimal condition of gas flow rate of 1000 mL·min−1, reduction temperature of 850 °C, reduction time of 30 min and H2 concentration of 80%, the reduced product with a metallization degree of 90.22% was obtained. The titanium-bearing maghemite in raw ore was reduced to titanomagnetite, the massive generated rutile and minor hardly reducible Fe3-xMxO4(M = Mg/Al/Si/) hindered the further aggregation of metallic iron grains, and there was no FeO detected during the whole reduction process. Thus,the phase transformation process of vanadium titanomagnetite is suggested as follows: γ-(Fe,Ti)2O3 → Fe3-xTixO4 → FeTi5O8 → Fe2TiO5 → Fe2TiO4 → Fe + FeTiO3 → Fe + TiO2.

Vanadium recovery from spent iron sorbent used for the treatment of mining-influenced water

Vanadium was recovered successfully from spent iron sorbent (ferric oxyhydroxide, CFH-12) using a two-step process including alkaline leaching and precipitation with CaCl2. The spent CFH-12 was collected from a field study in which a filter system was used to remove vanadium from mining-influenced water (referred to as MIW-treated CFH-12). Fresh CFH-12 was treated with synthetic vanadium solution (SVS-treated CFH-12) to compare the recovery process with the field study. First, a full factorial design was performed to optimize the precipitation process using synthetic leaching solution. The optimal conditions were found to be two times the theoretical dosage of CaCl2, a precipitation temperature of 60°C, and a precipitation pH of 12.7. Vanadium desorption from the spent sorbents was conducted using 1 M NaOH, a contact time of 30 minutes and a CFH-12 solid-to-liquid ratio of 0.15 kg/L. The results revealed that vanadium could be efficiently precipitated from the leaching solution of MIW-treated CFH-12 and SVS-treated CFH-12. A higher dosage of CaCl2 was required to recover vanadium from MIW-treated CFH-12 due to the complexity of the leaching solution, which resulted in a lower vanadium content in the product. XRD analysis showed that the product recovered from SVS-treated CFH-12 mainly contained Ca5(VO4)3OH and a small amount of CaCO3. TEM images revealed that the calcium vanadate hydroxide particles were round in shape, about 0.2–0.4 µm in size and formed aggregates. The product recovered from MIW-treated CFH-12 contained amorphous calcium vanadate and crystalline Ca(OH)2. XPS analysis confirmed that vanadium existed as V5+ in all of the recovered products.

Selective separation and recovery of vanadium from acid leaching solution of polymetallic black shale as function of aminophosphonic acid

AbstractBACKGROUNDAcid leaching is an effective method to extract vanadium from polymetallic black shale. However, a large amount of metal impurities, especially iron and aluminum, which accompany V, are released during this process.RESULTSIn this study, a aminophosphonic acid chelating resin was used for the differential adsorption and desorption of vanadium, iron and aluminum ions to achieve deep separation and concentration of vanadium ions present in the acid leaching solution of polymetallic black shale. Results showed that vanadium adsorption efficiency reached 90.17% at a pH of 1.8. After differential adsorption and desorption, the V:Fe and V:Al concentration ratios increased from 1.84 to 64.53 and from 0.24 to 37.92, respectively. When a 2.5 mol L−1 NaOH solution was used as desorbent, the separation factors β(V/Fe) and β(V/Al) reached values of 694.22 and 452.29, realizing the selective separation and concentration of vanadium.CONCLUSIONIt was found that the vanadium, iron and aluminum ions were selectively adsorbed onto the phosphonic acid functional groups (PO(OH)2) and amino functional groups (NH). The vanadium ions existed in the form of the polyvanadate (), which can be directionally adsorbed onto PO(OH)2 under POH bond cleavage and coordination of to the unsaturated phosphorus atom and then desorbed through the exchange between hydroxide anions OH− and . The iron and aluminum ions cannot be desorbed by OH− because the iron and aluminum sulfate moieties and were capable of coordinating to the nitrogen atom of the NH group via its lone electron pair. © 2022 Society of Chemical Industry (SCI).

A cleaner and sustainable method to recover vanadium and chromium from the leaching solution based on solvent extraction

In the work, a cleaner and sustainable method to recover vanadium (V) and chromium (VI) from the leaching solution based on solvent extraction using amide as extractant was developed. In the method, V(V) and Cr(VI) in the chlorinated system were co-extracted in extraction section and then separated in stripping section. Different parameters were explored to determine the optimum conditions of co-extracting V and Cr. The final V and Cr extraction efficiency could reach above 99.5% and 99.9%, respectively. Vanadium and chromium in the loaded organic phase could be stepwise stripped selectively using 1.5 mol/L HCl and 0.5 mol/L NaOH, and final V and Cr stripping efficiency could reach above 99.8% and 99%, respectively. The purity of the V2O5 product was 99.22% and the total recovery of vanadium was about 95%. The purity of the Cr2O3 product was 98.66% and the total recovery of chromium was about 97%. The slope analysis method confirmed that V(V)-amide extraction complex in chlorinated system was H2VO2Cl3R2. ESI-MS and FT-IR spectrums further confirmed extraction mechanism. The reduction phenomenon of V(V) and Cr(VI) was investigated and internal mechanism was proposed. The work provided a cleaner and sustainable method to recover V and Cr from the leaching solution and to produce vanadium and chromium products. The cleaner and sustainable method process has potential application for treating other solution containing vanadium and chromium such as leaching solution of chromite, stone coal and vanadium containing waste catalyst.

Vanadium recovery by glycine precipitation

Vanadium recovery by glycine precipitation

Efficient Separation and Recovery of Vanadium(V) from Hydrochloric Acid Solution Using N1923 as an Extractant.

Hydrochloric acid leaching has been widely used in the recovery process of vanadium due to its efficient selectivity. It was necessary to further separate vanadium from hydrochloric acid leaching solution. Four extractants of P204, P507, Cyanex272, and N1923 were compared for extraction of vanadium from a simulated hydrochloric acid solution, and it is concluded that N1923 was an effective extractant suitable for the extraction and separation of V (V) in the medium. The single-stage extraction efficiency of vanadium reached more than 90% with a pH value of 2.0, extraction time of 5 min, and XN1923 of 0.2 at 30 °C. The functional group characteristics of the extraction complex were analyzed by means of an extraction slope method, FT-IR, and 1H NMR to judge the extraction mechanism of vanadium with N1923 as an extractant. The extraction of V (V) by using N1923 was in the coordination form of a molar ratio of 2:1, and the extraction process was an endothermic reaction. The N–H vibrational absorption peak in the −NH2 group still appeared in the loaded N1923, in which the chemical shift of 1H in the primary amine and secondary carbon still existed. This technology was a more efficient process for extraction of vanadium from hydrochloric acid solution.

Removal and recovery of vanadium from waste by chemical precipitation, adsorption, solvent extraction, remediation, photo-catalyst reduction and membrane filtration. A review

Removal and recovery of vanadium from waste by chemical precipitation, adsorption, solvent extraction, remediation, photo-catalyst reduction and membrane filtration. A review

Efficient Recovery of Vanadium from High-Chromium Vanadium Slag with Calcium-Roasting Acidic Leaching

High-chromium vanadium slag (HCVS) is an important by-product generated during the smelting process of high-chromium-vanadium-titanium-magnetite. Direct acid leaching and calcium-roasting acid leaching technology were applied to recover vanadium and chromium from HCVS. The effects of experimental parameters on the leaching process, including concentration of H2SO4, reaction temperature, reaction time, and liquid-to-solid ratio, were investigated. The XRD and UV-Vis DRS results showed that vanadium and chromium existed in low valence with a spinel structure in the HCVS. The Cr-spinel was too stable to leach out; no more than 8% of the chromium could be leached out both in the direct acid leaching process and calcium-roasting acid-leaching process. Most low valence vanadium could be oxidized to high valence with calcium-roasting technology, and the leaching efficiency could be increased from 33.89% to 89.12% at the selected reaction conditions: concentration of H2SO4 at 40 vt.%, reaction temperature of 90 °C, reaction time of 3 h, liquid-to-solid ratio of 4:1 mL/g, and stirring rate of 500 rpm. The kinetics analysis indicated that the leaching behavior of vanadium followed the shrinking core model well, and the leaching process was controlled by the surface chemical reaction, with an Ea of 58.95 kJ/mol and 62.98 kJ/mol for direct acid leaching and roasting acid leaching, respectively.

Efficient Separation and Recovery of Vanadium, Titanium, Iron, Magnesium, and Synthesizing Anhydrite from Steel Slag

Efficient Separation and Recovery of Vanadium, Titanium, Iron, Magnesium, and Synthesizing Anhydrite from Steel Slag