Selective removal of calcium from sulfate solutions containing magnesium and nickel using aqueous two phase systems (ATPS)

Santos, Leandro José dos; Carvalho, Pablo Luis Gutierrez; Rodrigues, Guilherme Dias; Mansur, Marcelo Borges

doi:10.1016/j.hydromet.2015.06.010

Cited by 29 publications

(7 citation statements)

References 22 publications

Supporting

Mentioning

Contrasting

Unclassified

Order By: Relevance

“…At present, many researchers have successfully applied this technology to bioengineering [21,22], fermentation engineering [23], separation of organic matter [24] and other fields. There are also many studies on the application of this technology to extraction and separation of metal ions, for example the separation of Hg(II), Zn(II) and Co(II) by Dehghani [25], the separation of Ca(II), Mg(II) and Ni(II) by Rodrigues [26] and the extraction of Bi(III) subsalicylate by Sen [27]. The extraction and separation performance and the extraction mechanism of molybdenum and tungsten with the aqueous twophase system were reported by our early research work [28,29], and we also used the same system to investigate the extraction and separation of vanadium.…”

Section: Introductionmentioning

confidence: 99%

Separation of vanadium and molybdenum from aqueous solution using PEG2000 + sodium sulfate + water aqueous two-phase system

2019

View full text Add to dashboard Cite

The separation of vanadium (V) and molybdenum (VI) was studied by co-extraction with an aqueous two-phase system formed by PEG2000 + sodium sulfate + water and by selective stripping with another aqueous two-phase system formed by ammonium sulfate solution and PEG2000 phase loaded vanadium and molybdenum. The effect of aqueous pH, concentration of vanadium and molybdenum, temperature on the co-extraction and concentration of ammonium sulfate, temperature and phase ratio on selective stripping separation of vanadium and molybdenum was investigated. The experimental results on co-extraction of vanadium and molybdenum indicated that the co-extraction rate of both metals is sensitive to aqueous pH, and their extraction rate can achieve above 97.54% and 99.49%, respectively, when the pH value of aqueous solution is at 2.0, the molar ratio of vanadium to molybdenum is about 1.5, the concentration of PEG2000 is 20%, and the temperature is 313.15 K, respectively. The co-extraction rate of both metals decreases slightly with an increase in temperature from 313.15 to 343.15 K. The extraction isotherm and McCabe-Thiele method showed that two theoretical stages are needed when concentration of vanadium and molybdenum decreases from initial 12 g/L and 10 g/L to 0.1 g/L under the optimal conditions. The results on selective stripping of both metals from loaded PEG2000 phase to aqueous phase indicated that the stripping rate and precipitation rate of vanadium are evidently impacted by aqueous pH within 8.0 ~ 11.0 and then a little influenced by other parameters. The stripping rate of molybdenum is relatively lower than that of vanadium and is influenced by all kinds of stripping conditions. The stripping rate and precipitation rate of vanadium achieve 99.88% and 98.84%, respectively, and stripping rate of molybdenum achieves 81.99% under the optimal stripping conditions of O/A = 2:1, stripping temperature 343.15 K, (NH 4 ) 2 SO 4 (w/w) 40% and the pH of aqueous solution at 10.0.

show abstract

Section: Introductionmentioning

confidence: 99%

Separation of vanadium and molybdenum from aqueous solution using PEG2000 + sodium sulfate + water aqueous two-phase system

2019

View full text Add to dashboard Cite

show abstract

“…According to the results shown in the previous sections, a comparison of organic (MANSUR et al, 2022;SANTOS et al, 2015). A conceptual flowsheet presenting the systematic recovery of metals in the loaded organic solution using the extractive systems investigated in this work capable of simultaneously extract Ni and Co over Ca, Mg, Mn, and/or Zn is shown in Figure 3.9.…”

Section: Comparison Of Organic Systems and Possible Applicationsmentioning

confidence: 94%

Separação Níquel-Cobalto de PLS (Pregnant Leaching Solution) por extração por solvente

Santos,

Mansur

2023

View full text Add to dashboard Cite

Sulfuric acid leaching of lateritic nickel ores results in a PLS (Pregnant Leaching Solution) containing Ni, Co, and impurities (Al, Ca, Cr, Cu, Fe, Mg, Mn, Zn, etc.). This project was developed based on the results obtained by Ribeiro et al. (2021) and Silva et al. (2022), who obtained a PLS from the sulfation-thermal treatment of lateritic nickel ore, followed by pretreatment of the PLS for Fe, Al, and Cr removal by the jarosite/goethite method. Based on these results, this work aimed to separate Ni, Co, and impurities (Ca, Cu, Zn, Mg, and Mn) from the purified PLS. Different mixtures of extractants were investigated. The organic systems that performed well were: (i) versatic acid (pH 6.5), (ii) Cyanex 301 + versatic acid (pH 1.5), (iii) LIX 84-I + versatic acid (pH 5) e, (iv) LIX 860N-IC + versatic acid (pH 4). As a disadvantage, all organic systems extract 100% Cu, although this is the lowest contaminant in purified PLS. Systems (i) and (ii) extract 100% Zn. Therefore, systems (iii) and (iv) are the most selective for Ni and Co. Other disadvantages include system (i) presents partial extraction of Mn, systems (ii), (iii), and (iv) require operation in an inert atmosphere, and system (ii) uses only Cyanex 301, which is already applied industrially (Goro). For system (ii), effectively Ni stripping is challenged. In system (iii), the phase separation is slow at pH > 3.5. Two conceptual routes were developed in this work using two of the organic systems investigated. Both produced concentrated solutions of Ni and Co (purity greater than 99.9% Ni and 99.8% Co) suitable for feeding the electrowinning step. Route 1 (Chapter 4) employed typical commercial reagents to treat Ni sulfuric liquors, versatic acid, Cyanex 272, D2EHPA + TBP. The main disadvantage is the partial extraction of Mn in the first circuit because Mn is a contaminant in high contents, resulting in greater base consumption for neutralization and the risk of cross-contamination. Route 2 (Chapter 5) used an unprecedented combination of reagents, LIX 860N-IC + versatic acid and Cyanex 272. Removing Cu (pH 2-2.5) contained in the liquor can avoid contamination. The main disadvantage would be operating in an inert atmosphere. However, the Goro plant (with Cyanex 301 extractant) also uses an inert atmosphere industrially. Reuse of refined products containing Mg and Mn from Route 2, usually present in high levels in PLS can result in economic/environmental advantages. Ca rejection is advantageous because it avoids the formation of gypsum in the process. Therefore, although new, route 2 seemed to be more promising for future industrial applications.

show abstract

“…Катионы Ca(II) и Mg(II), а также хлорид-ионы, отрицательно влияющие на качество сульфата никеля, также необходимо удалять с целью обеспечения стабильного состава технологических растворов для гарантированного получения кондиционных солей никеля [10,11].…”

Section: Introductionunclassified

Using liquid extraction to clean JSC «Kola MMC» nickel production solutions from impurities

Dyakova¹,

Kasikov

Jeleznova

2022

Izv.VUZ. Tsvet. Met.

View full text Add to dashboard Cite

Studies of the extractive recovery of Ca(II), Mg(II) и B(III) impurities from nickel production solutions at JSC «Kola Mining and Smelting Company» were conducted. As extraction agents, we used di-(2-ethylhexyl)phosphoric acid (D2EHPA), di-(2,4,4-trime-thylpentyl)phosphinic acid (Cyanex 272), trialkylamine (TAA), tributyl phosphate (TBP), aliphatic alcohols: octanol-1, 2-ethylhexanol and a by-product of its production – heavy product of 2-ethylhexanol distillation (TPRD). In order to assess the effect of conditions used to extract impurities from solutions, laboratory studies on the effect of aqueous phase acidity, extraction agent concentration, composition of organic impurities on their extractability were conducted. According to the research results, it was found that the optimal concentration of individual extraction agents is 20 vol.% each in the Escaid 100 solvent, and the mixture composition is 15 vol.% D2EHPA + 5 vol.% Cyanex 272 at Ca(II) and Mg(II) extraction. Individual D2EHPA predominantly extracts calcium (II): extraction of 62 % Ca(II) and 15 % Mg(II). When using Cyanex 272, the extraction of magnesium (II) predominates: extraction of 59 % Mg(II) and 20 % Ca(II). It was found that the extraction mixture has higher performance than individual extraction agents for Ca(II) and Mg(II) extraction from nickel solutions in the pH range of 3.0÷3.5, at which Ni(II) coextraction is negligible. With increasing pH values, Ca(II) extraction decreases due to the increasing extraction of nickel and the displacement of calcium by it from the organic phase. It was established that a mixture of 40 % TAA + + 60 % 2-octanone and heavy product of 2-ethylhexanol distillation exhibits high extraction ability with respect to B(III): the degree of boron extraction is 60.7 and 74.5 %, respectively. The paper provides the results of the extraction purification of the nickel electrolyte from JSC «Kola Mining and Smelting Company» with an extraction mixture in the Ni-form to exclude pH adjustment at each stage of the process. Based on the results of the studies conducted, a flowchart is recommended for obtaining pure NiSO4 solutions with a residual total B(III), Ca(II), Mg(II) and Cl– content of £0.010 g/dm3 .

show abstract

Selective removal of calcium from sulfate solutions containing magnesium and nickel using aqueous two phase systems (ATPS)

Cited by 29 publications

References 22 publications

Separation of vanadium and molybdenum from aqueous solution using PEG2000 + sodium sulfate + water aqueous two-phase system

Separation of vanadium and molybdenum from aqueous solution using PEG2000 + sodium sulfate + water aqueous two-phase system

Separação Níquel-Cobalto de PLS (Pregnant Leaching Solution) por extração por solvente

Using liquid extraction to clean JSC «Kola MMC» nickel production solutions from impurities

Contact Info

Product

Resources

About