Recovery Of Vanadium Research Articles

Recovery of vanadium and nickel from heavy oil fly ash (HOFA): a critical review.

Heavy oil fly ash "HOFA" is the fly ash generated in power stations using heavy oil as fuel. HOFA is considered a hazardous waste because it contains considerable amounts of heavy metals. However, it contains significant amounts of vanadium "V" and nickel "Ni", which are precious metals for manufacturing processes. This paper presents a critical review of various approaches described in the literature for the recovery of V and Ni from HOFA, including processes of leaching, chemical precipitation, solvent extraction, and ion exchange. The optimum operational parameters and their effects on recovery efficiency are discussed. The digestion mixtures of strong mineral acids used for dissolving all metals present in HOFA are also highlighted. The leaching processes of V and Ni use mainly acidic and alkaline solutions. Bioleaching is a promising environmentally friendly approach for the recovery of V and Ni through using appropriate bacteria and fungi. After leaching, V and Ni compounds are recovered and purified using various techniques, including chemical precipitation, solvent extraction, and ion exchange. In most cases, V and Ni are recovered as thermally decomposable compounds that undergo calcination to produce V2O5 and NiO. Eventually, V and Ni are recovered as pure oxides in most approaches, but pure metals are obtained in exceptional procedures.

Vanadium (V) Adsorption from Aqueous Solutions Using Xerogel on the Basis of Silica and Iron Oxide Matrix.

Vanadium is considered a strategic metal with wide applications in various industries due to its unique chemical and physical properties. On the basis of these considerations, the recovery of vanadium (V) is mandatory because of the lack of raw materials. Various methods are used to recover vanadium (V) from used aqueous solutions. This study develops a clean and effective process for the recovery of vanadium (V) by using the adsorption method. At the same time, this study synthesizes a material starting from silica matrices and iron oxides, which is used as an adsorbent material. To show the phase composition, the obtained material is characterized by X-ray diffraction showing that the material is present in the amorphous phase, with a crystal size of 20 nm. However, the morphological texture of the material is determined by the N2 adsorption-desorption method, proving that the adsorbent material has a high surface area of 305 m2/g with a total pore volume of 1.55 cm3/g. To determine the efficiency of the SiO2FexOy material for the recovery of vanadium through the adsorption process, the role of specific parameters, such as the L-to-V ratio, pH, contact time, temperature, and initial vanadium concentration, must be evaluated. The adsorption process mechanism was established through kinetic, thermodynamic, and equilibrium studies. In our case, the process is physical, endothermic, spontaneous, and takes place at the interface of SiO2FexOy with V2O5. Following equilibrium studies, the maximum adsorption capacity of the SiO2FexOy material was 58.8 mg (V)/g of material.

Synthesis of nickel powder with good hydrogen evolution performance from spent Fluid Catalytic Cracking catalysts

The strategic metals in spent Fluid Catalytic Cracking (FCC) catalysts have attracted worldwide attention. In this work, the recovery of rare earths (lanthanum and cerium), nickel and vanadium have been achieved by acid leaching, extraction and precipitation, while the high-purity nickel powder with pretty hydrogen evolution performance has been synthesized for value-added utilization. Secondary leaching has been used for insoluble Ni power, and the total leaching rates of Ce, La, V and Ni are 96.17%, 85.86%, 99.99% and 74.62%, respectively. Rare earths have been recovered by the precipitation in primary leaching solution. The recovery rate of La is 97.11% and Ce is 99.96%. In secondary leaching solution, the impurity removal has been conducted, and the removal rate of Al and Fe is above 99.9%. Then the V and Ni are separated by solvent extraction, the extraction rate of V by N235 is 97.57%, the separation factor of Ni and V is 634.61. Finally, the high-purity NiSO4 solution(99.62%)is reduced to nickel power by the reducing agent N2H4·H2O, which was made for the hydrogen evolution reaction catalyst. When the current density is 10 mA/cm2, the overpotential is 308 mV, and the slope of Tafel is 128 mV·dec−1. This process provides a comprehensive recovery route of valuable metals from spent FCC catalysts for new energy industry.

Separation and Recovery of Vanadium, Nickel, and Aluminum from Acid Leaching Solution of Spent Hydrodesulfurization Catalyst by a Solvent Extraction-Oxalic Acid Precipitation Process

Separation and Recovery of Vanadium, Nickel, and Aluminum from Acid Leaching Solution of Spent Hydrodesulfurization Catalyst by a Solvent Extraction-Oxalic Acid Precipitation Process

Ecological treatment of El Kriymat boiler ash for recovering vanadium, nickel and zinc from sulfate leach liquor

The primary goal of this work is to develop a technology that allows for the recovery of metal values from waste products, thereby promoting the wise and efficient use of our nation's resources. To achieve this goal, an industrial waste of El Kriymat boiler fly Ash was used for recovering its content of vanadium, nickel and zinc. About 97, 95 and 99% respectively of these economic elements were first dissolved from boiler fly ash magnetic concentrate (after physical concentration). Leaching experiments using optimum conditions include: 180 g/L sulfuric acid concentration and 4% solid/solid proportion manganese dioxide acts as an oxidant at 80 °C. The recovery of vanadium (V) metal ions was carried out using 3% Alamine 336 in kerosene at an equilibrium pH value of 0.9. Subsequently, 15% sodium sulfide solution was used for co-precipitation of nickel and zinc metal ions in the raffinate solution at pH value of 3.5.Graphical

Recovery of Vanadium, Titanium, and Iron from Vanadium Titanomagnetite Concentrate Through Ammonium Sulfate Cascade Roasting with Potassium Pyrosulfate

Recovery of Vanadium, Titanium, and Iron from Vanadium Titanomagnetite Concentrate Through Ammonium Sulfate Cascade Roasting with Potassium Pyrosulfate

Fusion–Extraction Technique of Vanadium(III) Using Ammonium Phosphate Salt as Flux

This study presents an alternative fusion method for sample dissolution and extraction of vanadium from an inorganic (V2O3) compound and mineral ore sample (AMIS 0501) using phosphate salts as flux. Complete sample dissolution was achieved at 800 °C within ±20 min using both the sodium and ammonium phosphate flux. The precipitation of vanadium was subsequently achieved after the fusion of the sample using ammonium phosphate flux, and no precipitate was obtained using sodium phosphate flux. The differences in cations between the two fluxes (NH4+ and Na+) influenced the precipitation of vanadium. The XRD analysis of the precipitate from V2O3 using ammonium phosphate showed a monoclinic structure of vanadium (III) tris(metaphosphate) (V(PO3)3) compound, which belonged to the Ic space group with lattice parameters a = 10.6071, b = 19.0871 and c = 9.4230. A remarkable vanadium recovery of 98% was obtained from inorganic compounds, V2O3, and up to 70% from the AMIS mineral ore sample using the ammonium phosphate flux method. The vanadium precipitates from AMIS contained Fe (20.97%) and Ti (44.97%), which occurred as impurities in the recovery of vanadium using the ammonium phosphate flux method.

Heterotrophic Bioleaching of Vanadium from Low-Grade Stone Coal by Aerobic Microbial Consortium.

Bioleaching is a viable method that assists in increasing the vanadium output in an economical and environmentally friendly manner. Most bioleaching is conducted by pure cultures under autotrophic conditions, which frequently require strong acidity and produce acid wastewater. However, little is known about heterotrophic bioleaching of vanadium by mixed culture. This study investigated the bioleaching of vanadium from low-grade stone coal by heterotrophic microbial consortium. According to the results, vanadium was efficiently extracted by the employed culture, with the vanadium recovery percentage in the biosystem being 7.24 times greater than that in the control group without inoculum. The average vanadium leaching concentration reached 680.7 μg/L in the first three cycles. The kinetic equation indicated that the main leaching process of vanadium was modulated by a diffusion process. Scanning electron microscopy revealed traces of bacterial erosion with fluffy structures on the surface of the treated stone coal. X-ray photoelectron spectroscopy confirmed the reduction of the vanadium content in the stone coal after leaching. Analysis of high-throughput 16S rRNA gene sequencing revealed that the metal-oxidizing bacteria, Acidovorax and Delftia, and the heterotrophic-metal-resistant Pseudomonas, were significantly enriched in the bioleaching system. Our findings advance the understanding of bioleaching by aerobic heterotrophic microbial consortium and offer a promising technique for vanadium extraction from low-grade stone coals.

Separation of vanadium and tungsten in roasting‐acid leaching solutions of the spent selective catalytic reducing denitration catalyst by co‐extraction using hydroxyoxime extractant‐quaternary ammonium salt extractant LIX984–N263 extractant

AbstractThis study presents a synergistic extraction and recovery of vanadium and tungsten by mixed extractants (LIX984 and N263) from an acid leaching solution which was obtained from spent denitrification catalysts by chlorination heat treatment and acid leaching. Through thrice counter‐flow extraction, 99.5% V and 99.7% W were extracted, while 3.0% Fe, 2.9% Ti, 2.1% P, and 3.3% Mg were co‐extracted at a LIX984:N263 volume content of 22.0%, the phase ratio of 2.5 and the mother liquor's pH of 2.5. Then, at 0.80 mol/l NaOH and a phase ratio of 1, 99.9% tungsten and 99.1% vanadium were stripped from the organic phase to the aqueous phase. Subsequently, the aqueous phase's tungsten of 99.3% and vanadium of 98.1% were separated as calcium tungstate and ammonium metavanadate, respectively. In contrast, the residual solutions containing tungsten and vanadium can be returned to the following purification separation process to recover the valuable metals from the solution. Roasting converts the precipitated calcium tungstate and ammonium metavanadate to V2O5 and WO3 products. In addition, the thermodynamic analysis found the separation and recovery of tungsten and vanadium from the acid leach solution with LIX984:N263 to be an exothermic process. This method can be effectively extended for the separation of vanadium and tungsten from spent denitrification catalysts by the proposed process and validates the conclusion that metals with similar properties can be extracted using a mixture of extractants.

Recovery of V2O5 from spent SCR catalyst by H2SO4-ascorbic acid leaching and chemical precipitation

Large amounts of spent selective catalytic reduction (SCR) catalysts were produced in industry after losing their activity. This study developed a clean and effective route of leaching and recovery of vanadium (V) from spent SCR catalyst. First, ascorbic acid (C6H8O6) as the adjuvant can enhance vanadium leaching in H2SO4 solution. The effect parameters of acid concentration, leaching temperature, leaching time and liquid-solid (L/S) ratio on the leaching efficiency of vanadium were investigated. Then, the enrichment of vanadium in the leachate to obtain the black cake was carried out through adjusting pH value. The effects of vanadium concentration and pH on the precipitation efficiency of vanadium were studied. Finally, after alkaline dissolution and oxidation of the black cake, ammonium chloride (NH4Cl) was selected and used as the precipitant to obtain the ammonium poly-vanadate (APV). The final product vanadium pentoxide (V2O5) was obtained through roasting APV at 550 ℃ for 1.0 h. The black cake, APV and V2O5 were analyzed by the characterization of XRD or XRF. This study may introduce a new perspective for the effective usage of vanadium from spent SCR catalyst.

Recovery and kinetics of gold and vanadium from vanadium-bearing carbonaceous gold by chlorination roasting-acid leaching

ABSTRACT The idle mining or flotation decarburization of vanadium-bearing carbonaceous gold ores polluted the environment and wasted resources. In this paper, the volatilization behavior of calcined gold and the extraction kinetics of vanadium from calcined slag were analyzed to increase the high-value utilization efficiency of double refractory gold deposits. The results showed that the high-temperature chlorination efficiency of gold increased with the increase of calcium chloride dosage. At the same time, the oxidation effect of vanadium in roasting slag is also improved, which reduces the cost of extracting vanadium from roasting slag by acid. the vanadium leaching ratio of 83.3% when the calcium chloride amount of 10%, the roasting temperature of 1000℃, the roasting time of 240min, and the airflow rate of 1L/min, and the gold volatilization rate of 89.9%. The high-temperature chlorination reaction of gold and the acid leaching reaction of vanadium from calcined slag were also controlled by the interfacial chemical reaction. The apparent activation energy of the high-temperature chlorination of gold and the acid leaching of vanadium from calcined slag is calculated to be E = 71.61kJ/mol and 40.82kJ/mol, respectively. Suggested that gold recovery from vanadium-bearing carbonaceous gold ores was achieved using chlorination heat treatment. Also, the possibility of recovering vanadium from the roasting slag was verified by acid leaching experiments.

Efficient removal and recovery of vanadium (IV and V) from high acidic waste water with resins D851 and D201: A comparative study

Vanadium in acid waste water poses a potential environmental hazard due to its mobility and toxicity. A chelating resin D851 was used to remove and recover the vanadium from the acid solution system in contrast to resin D201. The adsorption efficiency of vanadium was >98 % with resin D851 at pH value of 1.5 for 60 min, while the adsorption efficiency of vanadium (IV and V) with resin D201 was <40 % and 60 %, respectively. Furthermore, the equilibrium adsorption capacity of vanadium (IV) was 162 mg/g with D851 and 104 mg/g with D201, respectively. The adsorption selectivity of vanadium with resin D851 was also better than that of resin D201 from titanium dioxide waste liquid (TDWL), in which the adsorption efficiency of V, Fe, Al, K, and Na was 88 %, 17 %, 14 %, 1 % & 2 % with D851, and 46 %, 33 %, 23 %, 5 % & 6 % with D201, respectively. The adsorption efficiency of vanadium remained >97 % within 10 times with the used resin D851 after regeneration. The adsorption process was accorded with the Freundlich model belonging to chemical adsorption. The vanadium could be adsorbed with resin D201 by ion exchange between OH of the N(CH3)3OH and the anions of V(IV) and V(V). The COOH of CH2N(CH2COOH)2 in resin D851 played a key role, in which the OH could be loosed to adsorb vanadium anions, and the H atom could also be loosed to form the stable conjugate structure of OCO adsorbing the cations of V(IV) and V(V).

Recovery of Tungsten and Vanadium from Spent Selective Catalytic Reduction Catalysts by Soda Roasting: A Mechanistic Study

This research investigated how soda roasting, which alters the roasting temperature and sodium carbonate concentration, recovers tungsten and vanadium from used selective catalytic reduction (SCR) catalysts. The ideal sodium carbonate content and roasting temperature were determined to be 800 °C and 30 wt%, respectively. Under these circumstances, tungsten and vanadium recoveries were 82.63% and 90.07%, respectively. In order to understand the roasting process, the compositions and morphologies of the original catalyst and specimens after roasting were examined by X-ray diffraction, scanning electron microscopy, and energy dispersive spectroscopy. In addition, the thermodynamic parameters associated with this process were calculated using the HSC 6.0 program to confirm compositional changes during roasting, the result shows that the chemical reactions among vanadium, tungsten, titanium and sulfur with sodium carbonate have priority in this system, as V2O5= SO3&gt; WO3&gt; TiO2; And the phases formation of vanadium and titanium are different at different temperatures and the amount of sodium carbonate, such as Na2V2O6, NaVO3, Na3VO4, VO2, Na2O* TiO2, Na2O* 3TiO2, 4Na2O* 5TiO2, and so on. Therefore, the recovery of vanadium and tungsten is significantly influenced by the other catalyst components as well as the reaction conditions. Based on this combination of experimental study and theoretical calculations, a technique for recovering tungsten and vanadium from spent SCR catalysts by soda roasting is suggested.

Selectively stepwise separation and recovery of molybdenum and vanadium from simulated leaching solution of spent hydrodesulfurization catalysts

Selective separation of molybdenum(Mo) and vanadium(V) from hazardous secondary resources containing Mo and V has become a technical bottleneck of its resource utilization. In this work, the selective separation of Mo and efficient recovery of V from simulated leaching solutions of spent hydrodesulfurization (HDS) catalysts were investigated via solvent extraction and chemical precipitation. The result indicates that the D2EHPA(P204) exhibits higher selectivity for Mo in strongly acidic conditions. Under optimum experimental conditions of hydrochloric acid of 1 mol/L, extractant concentration of 20 % (v/v), O/A ratio of 1:3 and contact time of 50 min, the single-stage extraction ratio of Mo reached 98.63 %, meanwhile, the co-extraction ratio of vanadium was less than 5 %. Additionally, over 97 % of Mo could be stripped from loaded organic phase at O/A ratio of 1 with 50 g/L NH4HCO3. The mechanism analysis revealed that selective extraction of Mo was mainly through the cation exchange mechanism. Moreover, the enthalpy changes in the molybdenum extraction were 44.1 kJ mol−1, which demonstrated that was an endothermic reaction. Furthermore, the Fe(III) was adopted to fabricate FeVO4 by precipitating vanadium from raffinate, and the precipitation efficiency of vanadium reached 97.71 % at a Fe/V molar ratio of 5/2, meanwhile, the precipitation product was further confirmed by XRD, XPS and SEM-EDS. Ultimately, a conceptual flowsheet for recovering completely Mo and V from simulated leaching solutions of spent HDS catalysts was proposed, which provides theoretical guidance for the resource utilization of containing molybdenum and vanadium secondary resources.

A novel complexation method for separation and recovery of low valence vanadium, iron and chromium from sulfuric acid solution

Traditional methods of vanadium recovery from vanadium slag suffer from serious environmental pollution due to the residue and wastewater containing highly toxic V(V) and Cr(VI). To avoid this, a complexation method based on sodium diethyldithiocarbamate (DDTC) complexing agent was proposed to separate and recover V(IV), Fe(II), Cr(III) in the leaching solution directly prepared from vanadium slag. Firstly, the recovery effect of DDTC on metal ions was studied in the imitated solution containing V (IV), Fe (II) and Cr (III), 97.67% vanadium, 99.51% iron and 98.99% chromium were recovered, respectively. In addition, DDTC was recycled in the complexation process. After four cycles, the regeneration rate of DDTC remained above 86%. Then, this method was applied to the leaching solution of vanadium slag, and 97.38% Cr, 97.69% V, 99.66% Fe and 97.64% Mn were recovered, respectively. Chromium was recovered as Cr2O3 with purity of 97.1%. Most iron was recovered as (NH4)2Fe(SO4)2·6H2O with purity of 99.23%. Manganese and a small amount of iron were enriched in the slag, which could be used to produce manganese alloy. Vanadium was recovered as calcium salt, which could be used to produce VOSO4 electrolyte with purity greater than 99.8%. Without waste water and residue containing highly toxic V(V) and Cr(VI) produced in this new method, which provides a new strategy for cleaner comprehensive utilization of vanadium slag.

Internal coordination of vanadium industrial waste—Preparation of hydroxyapatite and fluorine wastewater purification

In the vanadium industry, raffinate poses potential environmental risks due to the presence of corrosive fluoride and toxic heavy metals, and waste neutralizing slag (NS) was largely stockpiled given the low economic value, resulting in extensive land occupation and secondary pollution risks. Hydroxyapatite (HAP) was synthesized uniformly from the NS using the hydrothermal method, with no surfactants or additives used except for the three inexpensive reactants required. It was discovered that the pH of the raw material, the temperature, and the length of the hydrothermal reaction all had a significant effect on the adsorption characteristics of the produced HAP. When the conditions for synthesizing HAP were set with a pH of 11.5, a hydrothermal reaction temperature of 120 °C, and a reaction time of 1.5 h, the HAP had the optimum impact on raffinate treatment. The products' characterization by XRD, FTIR, SEM-EDS, and BET corroborated the successful synthesis of homogeneous HAP under the process conditions. The waste stream from the hydrothermal synthesis of HAP was recovered and crystallized to obtain a sodium sulfate by-product which was determined for purity. Adsorbed at room temperature for 1 h, the HAP synthesized by NS has a maximum percentage adsorption of 99.66 % and a saturation adsorption capacity of 43.64 mg/L for F ions in the raffinate. Additionally, the HAP removed over 95 % of the trace heavy metal ions Cr, As, and Cd from the raffinate. The saturated HAP was treated using a hydrothermal regeneration process, and the regenerated HAP retained a fluoride percentage adsorption still reaching 99.28 %. The thermodynamic and leaching experiments reveal that the desorption solution for the regeneration of HAP has the performance to increase the efficiency of vanadium recovery. This technique recycles waste NS to produce high-value HAP, which purification treatment of the raffinate with a high fluorine and contaminants content, solves the problem of treating two types waste of vanadium industry waste (NS and raffinate), and allows for the recycling of valuable element fluorine in vanadium industrial effluent.

The development of a techno-economic model for the assessment of vanadium recovery from bitumen upgrading spent catalyst

Spent catalyst from bitumen upgrading contains a substantial amount of vanadium. Recovering this vanadium can contribute to meeting the global demand. However, there are no studies on the economic feasibility of vanadium recovery plants, which is critical for decision makers. In this research, a techno-economic assessment of a vanadium recovery process was performed to bridge that gap. Data intensive process models were developed to understand the mass and energy balances of the vanadium recovery process. Capital and operating costs were estimated from material and energy balances. The recovery cost of vanadium was estimated using the developed techno-economic models, including the revenue for selling the co-products and by-products of the process. The economies of the scale and the effect of co-product and by-product selling price on the vanadium recovery cost were also studied. We found that for a plant capacity of 30,000 tonnes of spent catalyst per year, the vanadium recovery cost is $9.89/kg V2O5. For a market price of $12.00/kg V2O5, the minimum profitable capacity is about 22,400 tonnes of spent catalyst per year, and molybdenum trioxide is the co-product whose selling price has the most influence on the vanadium recovery cost. The results show that for spent catalyst generated in bitumen upgrading operations, the recovery of vanadium is potentially profitable considering the current vanadium market price. The developed information is useful for the decision makers in making investment decisions and policy formulation.

Efficient recovery of vanadium using lysine

This study presents an environmental-friendly technique for vanadium precipitation using lysine. Experimental results indicate that 99.4 % of the vanadium is precipitated under the select reaction conditions within the lysine. During the precipitation process, the vanadium exists as negatively charged polyoxometalates, while the lysine is positively charged. The negative vanadium polyoxometalates precipitate out through electrostatic interactions. The results shown in this study introduce a new way to utilize lysine and a new treatment for polyoxometalates.

Chromatographic Purification of Lithium, Vanadium, and Uranium from Seawater Using Organic Composite Adsorbents Composed of Benzo-18-Crown-6 and Benzo-15-Crown-5 Embedded in Highly Porous Silica Beads

The use of the composite adsorbents composed of benzo-15-crown-5 (abbreviated as BC15) and benzo-18-crown-6 (BC18) for the simultaneous recovery of vanadium (V), uranium (U), and lithium (Li) from seawater has been proposed for industrial applications. The adsorption and desorption behavior of these elements on BC15 and BC18 has been examined in various types of aqueous solutions over a wide temperature range. As a result, it was shown that BC15 and BC18 have sufficient adsorption ability for the simultaneous recovery of V, U, and Li from seawater. Moreover, it was seen that the distribution coefficients (Kd) of V decrease with an increase in [HCl]T (subscript T: total concentration), indicating that the anionic V species such as H2V4O134– are exponentially changed into the cationic V species such as V3+, VO2+, and VO2+ under the condition [HCl]T = 1.0 M, and the complexation reactions between BC15 (or BC18) and the initial V structures are inhibited. Besides, it was reasonably shown that the adsorption mechanism is the path through the electrostatic interaction between the anionic V species such as H2V4O134–, and the −C–O–C– single bond that the electron density is eccentrically located in ether functional groups in crown ether rings in BC15 and BC18 (or the −C–OH single bond that the electron density is eccentrically located in bisphenol A in BC15 and BC18). Then, the chromatography experiment of V, U, and Li on BC15 (or BC18) at 298 K was carried out by flowing seawater, 1.0 × 10–2 M HCl, and 1.0 M HCl in sequence. The first peak of V can be separated from the plateau of Li and the first and second peaks of U in the case of the BC15 system. The recovery ratios of V and U were more than 80%. On the other hand, entirely overlapping chromatograms were obtained in the case of the BC18 system, and accordingly, the recovery ratios of V and U were much lower. In short, the separation efficiency of V with BC15 is more pre-eminent than that with BC18. Judging from these results, the durability of BC15 was finally assessed for industrial applications, that is, the aforementioned chromatography experiment was repeatedly carried out to check whether V, U, and Li were stably and mutually separated from seawater or not. The evidence that the recovery performances of V, U, and Li from seawater do not decrease at all after at least five cycle tests was provided. This indicates that this information will be valuable for the development of a practical chromatographic technology to simultaneously recover V, U, and Li from seawater.

Kinetic modeling of adsorption of vanadium and iron from acid solution through ion exchange resins

This study assessed the adsorption process and the reaction kinetics involved in the selective recovery of vanadium from an acid solution containing iron as an impurity. Four commercial resins were studied: Lewatit® MonoPlus TP 209 XL, Lewatit® TP 207, Dowex™ M4195 (chelating resin) and Lewatit® MonoPlus S 200 H (strong cationic exchange resin). To investigate the effect of time on the adsorption process, batch experiments were carried out using the following initial conditions: pH 2.0, 298 K, and a proportion of 1 g of resin to 50 mL of solution. The variation of pH over time was analyzed. Chelating resin released less H+ ions as the adsorption occurred, resulting in a lower drop of pH when compared to S 200 H resin. Ion adsorption by the resins was also evaluated through FT-IR and SEM−EDS before and after the experiments. Among the evaluated kinetic models (pseudo-first order, pseudo-second order, Elovich and intraparticle diffusion models), the pseudo-second order model best fits the experimental data of the adsorption of vanadium and iron by all of the four resins. M4195 resin showed the highest recovery of vanadium and the lowest adsorption of iron. Kinetic data, which are fundamental to industrial processes applications, are provided.