Preparation and separation properties of polyamide nanofiltration membrane

Utilizing an interfacial polymerization technique for the preparation of a polymeric composite nanofiltration membrane, both high permeation flux of water and high salt rejection can be achieved. Synthesis conditions, such as concentration of monomer, reaction time, and swelling agent, significantly affected the separation performance of composite membranes. The composite polyamide membrane had a permeation rate of ∼2–5 gallon/ft2/day (gfd) and a salt rejection rate of ∼94–99% when 2000 ppm aqueous salt solution was fed at 200 psi and 25°C. Also, a higher performance nanofiltration membrane could be prepared by suitably swelling the support matrix in the period of polymerization. The results of various feed concentrations showed that permeate flux decreased with increasing salt concentration in the feed solution. This result may be due to concentration polarization on the surface of polyamide membranes. The separation performance of polyamide membranes showed an almost independent relationship with operation pressure until it was up to 200 psi. © 2002 Wiley Periodicals, Inc. J Appl Polym Sci 83: 1112–1118, 2002

[1]  Ashish Kulkarni,et al.  Chemical treatment for improved performance of reverse osmosis membranes , 1996 .

[2]  C. Vandecasteele,et al.  Removal of hardness from groundwater by nanofiltration , 1998 .

[3]  S. Chellam Effects of Nanofiltration on Trihalomethane and Haloacetic Acid Precursor Removal and Speciation in Waters Containing Low Concentrations of Bromide Ion , 2000 .

[4]  J. S. Campbell,et al.  High-temperature reverse osmosis membrane element , 1988 .

[5]  R. Rangarajan,et al.  Interfacially synthesized thin film composite RO membranes for seawater desalination , 1997 .

[6]  E. Chian,et al.  Reverse osmosis separation of polar organic compounds in aqueous solution , 1976 .

[7]  W. Pusch Comparison of transport of alkali halides and nitrates across asymmetric cellulose acetate and polyamide, composite poly(etherurea), and cation exchange membranes , 1991 .

[8]  D. J. Forgach,et al.  Characterization of composite membranes by their non-equilibrium thermodynamic transport parameters , 1991 .

[9]  A. B. Riedinger,et al.  Desalination of non-chlorinated surface seawater using TFCR membrane elements , 1988 .

[10]  K. Ahn,et al.  Removal of ions in nickel electroplating rinse water using low-pressure nanofiltration , 1999 .

[11]  R. H. Forester,et al.  Nanofiltration membranes broaden the use of membrane separation technology , 1988 .

[12]  Takeshi Matsuura,et al.  Low pressure reverse osmosis performances of sulfonated poly(2,6-dimethyl-1,4-phenylene oxide) thin film composite membranes: effect of coating conditions and molecular weight of polymer , 2000 .

[13]  N. Gondrexon,et al.  Influence of operating conditions on the retention of copper and cadmium in aqueous solutions by nanofiltration: experimental results and modelling , 1999 .

[14]  E. Chian,et al.  Optimization of NS-100 membrane for reverse osmosis , 1976 .

[15]  C. Vandecasteele,et al.  Influence of ion size and charge in nanofiltration , 1998 .

[16]  G. R. Groves,et al.  Treatment of pulp/paper bleach effluents by reverse osmosis , 1983 .

[17]  X. Xing,et al.  Effect of ion adsorption on its permeation through a nanofiltration membrane , 1997 .

[18]  R. J. Petersen,et al.  Composite reverse osmosis and nanofiltration membranes , 1993 .

[19]  N. Gondrexon,et al.  Ion transport modelling through nanofiltration membranes , 1999 .

[20]  Javier Fernandez,et al.  Degradation of membrane concentrates of the textile industry by Fenton like reactions in iron-free solutions at biocompatible pH values (pH ≈ 7–8) , 1999 .

[21]  J. J. Porter,et al.  Recovery of hot water, dyes and auxiliary chemicals from textile wastestreams☆ , 1984 .

[22]  D. Bhattacharyya,et al.  Reverse‐osmosis membrane for treating coal‐liquefaction wastewater , 1984 .