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Membrane Su rfacta ntAqueous solutions 1.65 x surfactant Triton X-100 are Ultrafiltration of a Nonionic 10-4 to 1.10 x 10-2 molar in the nonionic subjected to membrane ultrafiltration over the temperature range of 22 to 506C in a continuous flow, thin channel cell, with channel Reynolds numbers from 50 to 1175. Data for the ultrafiltrate flux through the optimum polyelectrolyte complex membrane (of the three tested) are correlated by an equation involving the in-series resistances of the membrane and of the polarized boundary layer of the surfactant rejected by the membrane, with the latter resistance varied over a wide range. The correlations are used to estimate the required membrane area and resultant ultrafiltrate concentration of surfactant to achieve any specified water recovery using cells-in-series and cells-in-parallel operation. The gelation concentration and surfactant mass transfer coefficient are used to estimate water flux in the gel-polarization region. SCOPEMembrane ultrafiltration has been used successfully to 105 to 106 N/m2 and involves the separation of modest concentrate or purify macromolecular solutes and colloidal molecular weight (500 and greater) solutes, macromoleparticulates and for the treatment of aqueous wastes. In cules, and colloids from aqueous solution, utilizing coma recent series of articles, Porter and Michaels (1971a, b, paratively-open, diffusive (or microporous) anisotropic C, d, 1972) have reviewed the applications of ultrafiltration membranes. However, severe performance limitations are in many processing areas. Ultrafiltration (in contrast to encountered during ultrafiltration due to the high-flux reverse osmosis) is carried out at low pressures of about characteristics of the membranes, which result in the

An experimental investigation of the foam separation of E . coli from distilled water suspension using a cationic surface-active agent, ethylhexadecyldimethylammonium bromide (EHDA-Br) is presented. Results are evaluated in terms of total cell count, using a membrane filtrat,ion t,echnique. Cell concentrations iri the initial suspensions are varied from 5.0 X lo5 to 1 .0 x 108 cells/ml. Surfactant concentrations in the initial cell suspensions are varied from 0.015 t,o 0.040 mg./ml., and foaming times are varied from 2 to 20 min. The residual quantity of cells decreases exponentially with foaming t,ime to about 0.027c of the initial quantit'y after 20 min. The cell enrichment rat,io, varying from 10 t,o 1,000,000, is an inverse power function of the initial stirfactant concentration and an exponential function of foaming time. Foaminess decreases with increasing initial cell concentrations, and for an initial surfactant concentration of 0.030 mg./ml., ()he residual cell concentration is a 1inea.r function of the initial cell concentration.

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