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Hydrometallurgical process for the separation and recovery of nickel from sulphate heap leach liquor of nickeliferrous laterite ores / S. Agatzini-Leonardou in Minerals engineering, Vol. 22 N° 14 (Novembre 2009) 

Public ISBD [article]  in Minerals engineering > Vol. 22 N° 14 (Novembre 2009) . - pp. 1181–1192 Titre : Hydrometallurgical process for the separation and recovery of nickel from sulphate heap leach liquor of nickeliferrous laterite ores Type de document : texte imprimé Auteurs : S. Agatzini-Leonardou, Auteur ; P.E. Tsakiridis, Auteur ; P. Oustadakis, Auteur Année de publication : 2009 Article en page(s) : pp. 1181–1192 Note générale : Génie Minier Langues : Anglais (eng) Mots-clés : Laterite  leach  liquor  Hydrometallurgical  process  Nickel  recovery Résumé : The Laboratory of Metallurgy of the National Technical University of Athens has developed and patented a novel integrated hydrometallurgical method, suitable to treat low-grade nickel oxide ores efficiently and economically. It involves heap leaching of the ore by dilute sulphuric acid at ambient temperature, purification of the leach liquor and recovery of nickel and cobalt by electrowinning. A typical composition of the pregnant solution produced from heap leaching is the following: Ni2+ = 5 g/L, Co2+ = 0.3 g/L, Fe3+ = 23.0 g/L, Al3+ = 6.0 g/L, Cr3+ = 1.0 g/L, Mn2+ = 1 g/L and Mg2+ = 8 g/L. The proposed hydrometallurgical process for nickel recovery from real sulphate heap leach liquors consists of the following six (6) unit operations: (1)Removal of iron, aluminium and chromium, as easily filterable crystalline basic sulphate salts of the jarosite–alunite type, at atmospheric pressure, by chemical precipitation at pH: 3.5 and 95 °C. (2)Cobalt, manganese and magnesium extraction over nickel by Cyanex 272 at pH: 5.5, T: 40 °C, with 20% extractant concentration and stripping of the loaded organic phase at T: 40 °C with diluted H2SO4 (4 M). (3)Nickel concentration by solvent extraction using Cyanex 272 at pH: 7.5, T: 40 °C, with 10% extractant concentration and stripping of the loaded organic phase by nickel spent electrolyte (55.45 g/L Ni) at T: 40 °C with diluted H2SO4 (2 M). (4)Nickel electrowinning from sulphate solutions, using stainless steel as cathode and Pb–8%Sb as anode. The pH of the electrolyte (10 g/L H3BO3, 75.95 g/L Ni2+ and 130 g/L Na2SO4) was adjusted at 3.5 and at 60 °C, while the current density was kept constant at 20 mA/cm2. (5)Cobalt and manganese extraction over magnesium by Cyanex 302 at pH: (5.0), T: 40 °C, with 20% extractant concentration and stripping of the loaded organic phase at T: 40 °C with diluted H2SO4 (1 M). (6)Removal of magnesium by chemical precipitation (as brucite), using Ca(OH)2 as neutralizing agent, at atmospheric pressure, pH = 10 and 25 °C. DEWEY : 622 ISSN : 0892-6875 En ligne : http://www.sciencedirect.com/science/article/pii/S0892687509001514 [article] Hydrometallurgical process for the separation and recovery of nickel from sulphate heap leach liquor of nickeliferrous laterite ores [texte imprimé] / S. Agatzini-Leonardou, Auteur ; P.E. Tsakiridis, Auteur ; P. Oustadakis, Auteur . - 2009 . - pp. 1181–1192. Génie Minier Langues : Anglais (eng) in Minerals engineering > Vol. 22 N° 14 (Novembre 2009) . - pp. 1181–1192 Mots-clés : Laterite  leach  liquor  Hydrometallurgical  process  Nickel  recovery Résumé : The Laboratory of Metallurgy of the National Technical University of Athens has developed and patented a novel integrated hydrometallurgical method, suitable to treat low-grade nickel oxide ores efficiently and economically. It involves heap leaching of the ore by dilute sulphuric acid at ambient temperature, purification of the leach liquor and recovery of nickel and cobalt by electrowinning. A typical composition of the pregnant solution produced from heap leaching is the following: Ni2+ = 5 g/L, Co2+ = 0.3 g/L, Fe3+ = 23.0 g/L, Al3+ = 6.0 g/L, Cr3+ = 1.0 g/L, Mn2+ = 1 g/L and Mg2+ = 8 g/L. The proposed hydrometallurgical process for nickel recovery from real sulphate heap leach liquors consists of the following six (6) unit operations: (1)Removal of iron, aluminium and chromium, as easily filterable crystalline basic sulphate salts of the jarosite–alunite type, at atmospheric pressure, by chemical precipitation at pH: 3.5 and 95 °C. (2)Cobalt, manganese and magnesium extraction over nickel by Cyanex 272 at pH: 5.5, T: 40 °C, with 20% extractant concentration and stripping of the loaded organic phase at T: 40 °C with diluted H2SO4 (4 M). (3)Nickel concentration by solvent extraction using Cyanex 272 at pH: 7.5, T: 40 °C, with 10% extractant concentration and stripping of the loaded organic phase by nickel spent electrolyte (55.45 g/L Ni) at T: 40 °C with diluted H2SO4 (2 M). (4)Nickel electrowinning from sulphate solutions, using stainless steel as cathode and Pb–8%Sb as anode. The pH of the electrolyte (10 g/L H3BO3, 75.95 g/L Ni2+ and 130 g/L Na2SO4) was adjusted at 3.5 and at 60 °C, while the current density was kept constant at 20 mA/cm2. (5)Cobalt and manganese extraction over magnesium by Cyanex 302 at pH: (5.0), T: 40 °C, with 20% extractant concentration and stripping of the loaded organic phase at T: 40 °C with diluted H2SO4 (1 M). (6)Removal of magnesium by chemical precipitation (as brucite), using Ca(OH)2 as neutralizing agent, at atmospheric pressure, pH = 10 and 25 °C. DEWEY : 622 ISSN : 0892-6875 En ligne : http://www.sciencedirect.com/science/article/pii/S0892687509001514