Zbigniew Hubicki

Removal of tartrazine from aqueous solutions by strongly basic polystyrene anion exchange resins.

The removal of tartrazine from aqueous solutions onto the strongly basic polystyrene anion exchangers of type 1 (Amberlite IRA-900) and type 2 (Amberlite IRA-910) was investigated. The experimental data obtained at 100, 200, 300 and 500 mg/dm(3) initial concentrations at 20 degrees C were applied to the pseudo-first order, pseudo-second order and Weber-Morris kinetic models. The calculated sorption capacities (q(e,cal)) and the rate constant of the first order adsorption (k(1)) were determined. The pseudo-second order kinetic constants (k(2)) and capacities were calculated from the plots of t/q(t) vs. t, 1/q(t) vs. 1/t, 1/t vs. 1/q(t) and q(t)/t vs. q(t) for type 1, type 2, type 3 and type 4 of the pseudo-second order expression, respectively. The influence of phase contact time, solution pH and temperature on tartrazine removal was also discussed. The FTIR spectra of pure anion exchangers and those loaded with tartrazine were recorded, too.

Selective Removal of Heavy Metal Ions from Waters and Waste Waters Using Ion Exchange Methods

© 2012 Hubicki and Kolodynska, licensee InTech. This is an open access chapter distributed under the terms of the Creative Commons Attribution License (http://creativecommons.org/licenses/by/3.0), which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited. Selective Removal of Heavy Metal Ions from Waters and Waste Waters Using Ion Exchange Methods

Sorption of SPADNS azo dye on polystyrene anion exchangers: equilibrium and kinetic studies.

The sorption of SPANDS from aqueous solution onto the macroporous polystyrene anion exchangers of weakly basic Amberlyst A-21 and strongly basic Amberlyst A-29 in a batch method was studied. The effect of initial dye concentration and phase contact time was considered to evaluate the sorption capacity of anion exchangers. Equilibrium data were attempted by various adsorption isotherms including the Langmuir, Freundlich and Dubinin-Radushkevich (D-R) models. A comparison of kinetic models applied to the adsorption rate constants and equilibrium sorption capacities was made for the Lagergren first-order, pseudo second-order and Morris-Weber intraparticle diffusion kinetic models. The results showed that the adsorption isotherm is in the good agreement with the Langmuir equation and that the adsorption kinetics of SPADNS on both anion exchangers can be best described by the pseudo second-order model.

Studies of removal of palladium(II) ions from chloride solutions on weakly and strongly basic anion exchangers

Palladium and its compounds find wide application in industry as a catalytic agent in different manufacture processes. Recovery of precious metals from industrial wastes is difficult and time consuming but in spite of these disadvantages it becomes profitable. Palladium(II) ions sorption from various chloride solutions of the composition: 0.1-6.0M HCl-0.00056 M Pd(II), 1.0M ZnCl(2)-0.1M HCl-0.00056 M Pd(II), 1.0M AlCl(3)-0.1M HCl-0.00056 M Pd(II) on the weakly and strongly basic anion exchangers (Varion ATM, Varion ADM and Varion ADAM) was discussed. The sorption research of Pd(II) ions on these resins was carried out by means of static and dynamic methods. The dynamic processes were applied in order to determine the breakthrough curves of Pd(II) ions. Moreover, the working ion-exchange capacities as well as the weight and bed distribution coefficients were determined from the Pd(II) breakthrough curves. The recovery factors of Pd(II) ions (% R) depending on the phase contact time were obtained by means of static methods. The highest ion-exchange capacities for the 0.1-6.0M HCl-0.00056 M Pd(II) systems were obtained for the weakly basic ion-exchange resin Varion ADAM.

Equilibrium and kinetic studies on the adsorption of acidic dye by the gel anion exchanger.

In the present study, the gel anion exchanger Purolite A-850 of N(+)(CH(3))(3) functional groups was used in order to remove the acidic dye (Acid Blue 29) from aqueous solutions. Batch experiments were conducted to study the effect of phase contact time (1-180 min), initial concentration of dye (100-500 mg/L), solution pH (1-8), anion exchanger dosage (0.25-1.0 g) as well as temperature (20-40 degrees C). The contact time necessary to reach equilibrium was 40 min with the exception for the solution of the initial concentration 500 mg/L. The amounts of Acid Blue 29 adsorbed at equilibrium using the strongly basic anion exchanger were equal to 9.97, 19.97, 29.96 and 49.90 mg/g for the dye solutions of the initial concentrations 100, 200, 300 and 500 mg/L, respectively. The equilibrium sorption capacity slightly increased when the temperature of dye solution increased from 20 to 40 degrees C. The experimental data were analyzed by the Langmuir, Freundlich and Temkin models of adsorption. The adsorption isotherm data were fitted well to the Langmuir isotherm and the monolayer adsorption capacity was found to be 83.303 mg/g at 20 degrees C. The value of R(L) was equal to 0.00054 (favourable). The kinetic data obtained at different concentrations were modeled using the pseudo-first order, pseudo-second order and intraparticle diffusion equations. The experimental data were well described by the pseudo-second order kinetic model.

Studies on the extraction process of nickel(II) sulphate purification using Cyanex 272

Extractive purification of macroquantities of NiSO4 from microquantities of Co(II), Zn(II), Cu(II), Mn(II) and Fe(III) using Cyanex 272 was studied. The optimum conditions of Co(II) removal depending on equilibrium pH value, phase ratio and extraction temperature were determined. The most effective results were obtained using a two-stage extractive purification of Ni(II) sulphate from Co(II) at a phase ratio of 1:1, equilibrium pH > 6 and 323 K. Under these conditions the Co(II) content in the purified NiSO4 decreases several hundred times compared to the initial content. Nickel sulphate purified in this way contains <0.001% Co, <0.0001% Zn, <0.00005% Fe, <0.00005% Cu and <0.00005% Mn.

A comparative study of chelating and cationic ion exchange resins for the removal of palladium(II) complexes from acidic chloride media

The increasing demand for palladium for technological application requires the development of ion exchange chromatography. Recently ion exchange chromatography has developed largely as a result of new types of ion exchangers available on the market of which two types are widely applied. One of them are selective (chelating) and modified ion exchangers and the other one are liquid exchangers. Two types of ion exchange resins such as chelating (Lewatit TP 214, Purolite S 920) and cationic (Chelite S, Duolite GT 73) ion exchangers are used for the recovery of palladium(II) complexes from chloride media (0.1-2.0M HCl-1.0M NaCl-0.0011 M Pd(II); 0.1-2.0M HCl-2.0M NaCl-0.0011M Pd(II)). The influence of concentration of hydrochloric acid, sodium chloride as well as the phase contact time on the degree of recovery of palladium(II) complexes was studied. Moreover, the amount of palladium(II) chlorocomplexes sorbed onto ion exchangers, the working ion exchange capacities and the weight and bed distribution coefficients were calculated in order to judge which of two types of resins possesses the best performance towards palladium(II) complexes.

Studies of extractive removal of silver (I) from nitrate solutions by Cyanex 471 X

Abstract Silver(I) extraction from nitrate solutions by Cyanex 471 X (triisobutylphosphine sulphide) was investigated. The optimal conditions of silver(I) removal were determined depending on the concentration of purified salts, concentration of nitric acid, concentration of Cyanex 471X, kind of diluent and modifier, as well as phase contact time. Silver(I) extraction isotherms, using 2.5 and 5% Cyanex 471X and D2EHPA or TBP, were determined depending on nitric acid concentration. In the case of a 6 M HNO3 solution a rapid decomposition of Cyanex 471X was observed. The removal of Ag(I) from solutions containing Cu(II), Zn(II), Bi(III) and Fe(III) was studied. It was found that Cyanex 471X could reduce the silver content in the purified salts to below 10−5%.

Kinetics of adsorption of sulphonated azo dyes on strong basic anion exchangers

The macroporous polystyrene anion exchangers Amberlite IRA‐900 and Amberlite IRA‐910 were used in order to remove sulphonated azo dyes (Allura Red and Sunset Yellow) from aqueous solutions of 100–500 mg/L concentrations. The experimental data obtained at 100, 200, 300 and 500 mg/L initial concentrations at 20 °C were applied to the pseudo‐first‐order, pseudo‐second‐order and Weber–Morris kinetic models. The calculated sorption capacities (qe,cal ) and the rate constant of the first‐order adsorption (k1 ) were determined. The pseudo‐second‐order kinetic constants (k2 ) and capacities were calculated from the plots of t/qt vs t, 1/qt vs 1/t, 1/t vs 1/qt , qt/t vs qt and 1/qe–qt vs t for type 1, type 2, type 3, type 4 and type 5 of the pseudo‐second‐order expression, respectively. The influence of phase contact time, initial dye concentration, solution pH and temperature on Allura Red and Sunset Yellow removal was also discussed.

Remazol Black B removal from aqueous solutions and wastewater using weakly basic anion exchange resins

AbstractIn this study, the use of the weakly basic anion exchange resins of phenol-formaldehyde (Amberlyst A 23), polyacrylate (Amberlite IRA 67) and polystyrene (Lewatit MonoPlus MP 62) matrices for removal of the reactive dye Remazol Black B (RBB) from aqueous solution and wastewater were investigated. RBB sorption on the anion exchangers was a time dependent process. Color reduction percentiles of 75.2, 33.9 and 25.1% in wastewater treatment were found after 216 h of phase contact time with Lewatit MonoPlus MP 62, Amberlyst A 23 and Amberlite IRA 67, respectively. Inorganic salts and anionic surfactant action influenced RBB uptake by the anion exchangers. The amounts of dye retained by the anion exchangers increased with a rise in temperature. The maximum sorption capacities calculated from the Langmuir model were 66.4, 282.1 and 796.1 mg g−1 for Amberlite IRA 67, Amberlyst A 23 and Lewatit MonoPlus MP 62, respectively. Regeneration of phenol-formaldehyde and polystyrene resins were possible using 1 M NaOH, 2 M KSCN, 1M KSCN in 40–60% methanol as well as 1 M NaOH in 60% methanol.