A mathematical model for calculation of equilibrium solution speciations for the FeCl3-FeCl2-CuCl2-CuCl-HCl-NaCl-H2O system at 25 ‡C

Kimura, Richard T.; Haunschild, Peter A.; Liddell, K.C.

doi:10.1007/bf02667323

Cited by 36 publications

(17 citation statements)

References 5 publications

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“…Most of these studies, however, examine the extraction of iron when its concentration in solution is not very high, which will be the condition if pure iron oxide is produced in bulk through solvent extraction techniques. Several solvents such as organophosphorus acid derivatives, [3,7,[15][16][17][18][19][20][21][22] carboxylic acids, [8,11,[23][24][25] amines, [4,6] etc. have been used for iron extraction.…”

Section: Introductionmentioning

confidence: 99%

Synergistic extraction of iron(III) at higher concentrations in D2EHPA-TBP mixed solvent systems

Sahu

Das

1997

Metall Mater Trans B

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The extraction of iron(III) from chloride solutions at macrolevel concentration by different solvents such as tri-n-butyl phosphate (TBP), di(2-ethylhexyl) phosphoric acid (D2EHPA), and their mixture in various proportions has been investigated at different acid concentrations. The synergistic extraction of iron(III) with a mixture of TBP and D2EHPA was studied and the results were compared with that of the extraction by individual solvent alone. An increase in the concentration of the synergist, TBP, in the D2EHPA-TBP solvent system resulted in an increase in the synergistic coefficient value. The experimental data are treated graphically to explain the formation of organic phase extracted species, and the equilibrium extraction constants for the species are determined. It is found that a maximum of two molecules of TBP are adducted to the extracted species of the corresponding nonsynergistic system. Stripping of iron(III) with hydrochloric acid from loaded D2EHPA was found to increase with an increase in acid concentration. In the case of D2EHPA-TBP mixtures, stripping efficiency was increased with an increase in acid concentration up to a certain level and then it was decreased. The experimental results indicate that an iron exchange reaction between loaded D2EHPA and TBP proceeds during stripping at a higher concentration of hydrochloric acid (from mixed loaded solvent system). A plausible mechanism for iron(III) extraction and stripping has been discussed.

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Section: Introductionmentioning

confidence: 99%

Synergistic extraction of iron(III) at higher concentrations in D2EHPA-TBP mixed solvent systems

Sahu

Das

1997

Metall Mater Trans B

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“…2a, the dissolution of MoO 3 has to be conducted at pH<0.5 in order to avoid the precipitation of Cu as copper molybdate species, which would remain in the refined MoO 3 calcine after treatment. There are other issues such as the formation of chloro-complexes at increasing chloride content which affect the solubility of metal ions and kinetics of (Bryce and Berk, 1995;Kimura et al, 1984;Senanayake and Muir, 1988). Using Raman spectroscopy, Marston and Bush (1972) .…”

Section: Review Of Chemical Speciation and Eh-ph Diagrams Of Mo Solutmentioning

confidence: 99%

“…Using Raman spectroscopy, Marston and Bush (1972) . From the speciation modeling and distribution of these species reported in detail by Kimura et al (1984), Awakura et al (1987) Muir, 1988, 2003 using an overhead stirrer. Samples were taken at different time intervals, filtered using a 0.5 micron filter (Advantec 5C) and then analysed for Fe, Cu and Mo using ICP-AES.…”

Section: Review Of Chemical Speciation and Eh-ph Diagrams Of Mo Solutmentioning

confidence: 99%

Purification of molybdenum trioxide calcine by selective leaching of copper with HCl–NH4Cl

Nam

Seo

Kang³

et al. 2011

Hydrometallurgy

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The leaching of Mo, Cu and Fe from MoO 3 calcines (59-61% Mo) containing 1-2% Cu, 1-2% Fe and other impurities produced from roasting molybdenite (MoS 2 ) concentrate was examined using water and a series of chloride lixiviants, including NH 4 Cl (0. Although not required, Fe was removed to <0.6% whereas most other metal impurities were removed to <0.1%. Pilot plant trials over 7 campaigns, each treating 2.0-2.2 tonnes of MoO 3 calcine containing 2.1% Cu using 1.44M NH 4 Cl and 0.97M HCl at an ambient temperature yielded final products containing 0.22% Cu as required. Mass balance calculations (closure to 96-99%) of the pilot plant trials confirm that the Mo loss during leaching is around 0.5%. Research Highlight We determine the process chemistry of leaching Cu from MoO3 calcine to reduce its content to <0.5% A C C E P T E D M A N U S C R I P T ACCEPTED MANUSCRIPT2  The optimum leaching conditions to treat calcines containing 1% Cu (0.6M NH4Cl, 0.7M HCl at ambient temperature) were adopted to remove impurities to <0.5% Cu, <0.6% Fe and <0.1% for other impurities  The dissolution of Mo by acid was minimized by the precipitation of ammonimum molybdate  Stabcal was used to model the speciation of the dissolution process.  Pilot plant trials were conducted to treat 14 tonnes of calcines to confirm the results before plant operations were implemented.

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“…The investigation on the solvent extraction of iron (III) mainly focused on separation of iron from blue dust, iron scrap, waste chloride pickle liquors from steel plants and ilmenite leach liquors. A survey of the literature showed that a large number of reagents had been used for the extraction of iron (III), such as organophosphorus acid derivatives [1][2][3][4][5][6][7] , amines [8][9][10][11] , neutral extractants [12][13][14][15] , carboxylic acid etc. Among them, organophosphorus acid extractants and amines are the leading extractants for iron (III) in acid solutions.…”

Section: Introductionmentioning

confidence: 99%

Solvent extraction of iron (III) from chloride acid solutions by decanol

Mao¹

2015

Proceedings of the 3rd International Conference on Material, Mechanical and Manufacturing Engineering

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The solvent extraction of iron (III) from acidic chloride solutions by decanol in kerosene has been investigated. The solvent extraction results demonstrated that the dissolved iron was present as HFeCl 4 .2Decanol. Extraction of iron (III) increased with increased hydrochloric acid concentration in the aqueous phase. On the other hand, titanium (IV ) aluminum (III), calcium (II) and magnesium (II) were not extracted under these experimental conditions. IR spectral study of the extracted complex was further used to clarify the nature of the extracted complex. The extracted complex was easy to strip. Using 0, 0.5 and 1 mol.dm -3 HCl as the stripping agents the stripping rate of iron (III) was above 90%.

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A mathematical model for calculation of equilibrium solution speciations for the FeCl3-FeCl2-CuCl2-CuCl-HCl-NaCl-H2O system at 25 ‡C

Cited by 36 publications

References 5 publications

Synergistic extraction of iron(III) at higher concentrations in D2EHPA-TBP mixed solvent systems

Synergistic extraction of iron(III) at higher concentrations in D2EHPA-TBP mixed solvent systems

Purification of molybdenum trioxide calcine by selective leaching of copper with HCl–NH4Cl

Solvent extraction of iron (III) from chloride acid solutions by decanol

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