Triethanolamine–cyclohexanone supported liquid membranes study for extraction and removal of nickel ions from nickel plating wastes

Performance Evaluation of Nickel Separation and Extraction Process from Simulated Spent Cr/Ni Electroplating Bath Solutions by ELM Process Using LIX63 and PC88A

“…However, the transport phenomena is governed by kinetic rather than chemical equilibrium such as non-equilibrated mass transfer. [30][31][32] The process provides maximum yield of the extracted solute with the use of minimum extractant and organic solvent. Two different aqueous phases, called the donor (feed) phase and the acceptor (stripping) phase, are in contact with the membrane phase in LM processes.…”

Extraction of Lead through Supported Liquid Membrane Using Triethanolamine/Cyclohexanone Carrier and Na2SO4strippant

“…Fig.3 indicates the Pb +2 ion transport with 1.0 M acid concentration in the feed phase. Amount of protons and the pH value in feed phase is fundamental factor onto which the trasportation course of Pb +2 ions in the feed phase of the liquid membrane depends.This can be attributed to the increased pH values of the feed side as noted after regular time intrevals ( Bukhari et al,2004) Since H + ions are responsible for formation of a metal complex with carrier molecule so these three protons are consumed from the feed side thereby increasing the pH of feed side. As the acid concentration decreases on the feed side the amount of acid decreases with time when initial concentration of acid in feed is taken 0.1M i.e.…”

“…This technique is also useful for gas separation process (Abedini and Nezhadmoghadam, 2010).Previously the removal of Cr (III), Co (II), and Ni (II) has been studied in a similar system. The prime aim of this effort was to optimize the conditions for the removal Pb (II) using the TEA-cyclohexanone support (Bukhari et al, 2004(Bukhari et al, , 2006(Bukhari et al, , 2007.…”

Separation of Eu(III) with supported dispersion liquid membrane system containing D2EHPA as carrier and HNO3 solution as stripping solution

“…In this mechanism, the separation of Eu(III) across SDLM will be described by considering only diffusion coefficient of Eu(III), because the complex reaction between the Eu(III) and D2EHPA at the interfaces is much faster compared with the diffusion in the feed phase and membrane phase [32][33][34] . To formulate the model, the following assumptions were made: (1) the Eu(III) diffuses in the organic medium only as the EuR 3 (HR) 3 complex; (2) there is no net flow due to convection within the liquid membrane; (3) the metal ions react only with D2EHPA at the membrane interfaces; (4) the D2EHPA monomer and dimer are in equilibrium at all times throughout the organic phase; (5) the solubility of D2EHPA in the aqueous acid solution has been found to be negligible and, therefore, its concentration in the SDLM is assumed to remain constant [35] .…”