content material: the answer concept modeling of gasoline adsorption on zeolites / Arthur W. Woltman and William H. Hartwig --
Mathematical modeling of adsorption in multicomponent structures / Alexander P. Mathews and Walter J. Weber, Jr. --
research of combination equilibria of methane and krypton on 5A zeolite / K.F. Loughlin and G.D. Roberts --
obvious floor diffusion results for carbon dioxide/air and carbon dioxide/nitrogen combos with pelleted zeolite beds / Richard T. Maurer --
impact of presorbed water at the sorption of nitrogen by means of zeolites at ambient temperatures / Donald Peterson --
Selective sorption homes of zeolites / R.M. Dessau --
4 crystal buildings of BaxNa₁₂₂x-A (1[less than or equivalent to] x [less than or equivalent to] 6) when it comes to the instability of barium-exchanged zeolite A towards dehydration / Yang Kim, V. Subramanian, Roger L. Firor, and Karl Seff --
The influence of oxygen of photoluminescence and resonance strength move in copper (I) Y zeolite / D.H. Strome and ok. Klier --
education of copper(II)-exchanged Y zeolites from sodium and ammonium Y zeolites / Richard G. Herman and John B. Bulko --
Lead and cadmium ion alternate of zeolite NaA / Elliot P. Hertzenberg and Howard S. Sherry --
Liquid section drying purposes of zeolites / George W. younger, Joseph R. Kiovsky, and Pramod B. Koradia --
Separation of n-paraffins from wax distillate with supercritical fluids and molecular sieves / Paul Barton and David F. Hajnik --
Polybed pressure-swing adsorption hydrogen processing / R.T. Cassidy --
Separation of hydrogen sulfide-hydrogen combinations by means of heatless adsorption / M.D. Whitley and C.E. Hamrin, Jr. / a brand new method for adsorption separation of gasoline streams --
George E. Keller, II and Russell L. Jones.
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Additional info for Adsorption and Ion Exchange with Synthetic Zeolites. Principles and Practice
At 271 and 255K the t o t a l amount adsorbed increases continuously with increasing mole fraction of methane, whereas at 238K the t o t a l amount adsorbed passes through a maximum at 60% methane i n the adsorbed phase. ; ACS Symposium Series; American Chemical Society: Washington, DC, 1980. LOUGHLIN AND ROBERTS CHj & Kr Mixture Equilibria Figure 1. Schematic of apparatus: A, calibrated variable-volume mercury burette; B reference volume; C, main chamber; D, mixing pump; E, adsorption chamber; F, reference chamber; G, constant temperature baths; H, mercury manometer; J, cold-cathode gauge; P, Pirani vacuum gauge; R, mercury reservoir t Figure 2.
J . , 1974, 20, 915. 4. Gariepy, R. ; AIChE Symp. , 1971, 67 (117), 17. 5. Usinowicz, P. J . ; Weber, W. ; Paper presented at the 46th Annual Conference of the Water Pollution Control Federation, October 1972. 6. de Boer, J. ; "The Dynamical Character of Physical Ad sorption," Oxford University Press, London, 1953. 7. ; Olivier, J. , New York, 1964. 8. Ruthven, D. , 1976, 22, 753. 9. Butler, J. Α. ; J. Phys. , 1930, 34, 2841. 10. Jain, J. ; Snoeyink, V. ; J. Water Poll. , 1972, 45, 2463. ; ACS Symposium Series; American Chemical Society: Washington, DC, 1980.
The Langmuir equation i s derived by considering the adsorbed phase as a two-dimensional mobile monolayer, and a correction term analogous to the Van-der Waal's term in the threedimensional gas phase i s applied to correct for the surface area occupied by the adsorbed molecules. The resulting expres sion for the Langmuir isotherm i s given by the following equation: q i - Σ (i+b ' (c /n )) 1 i ± The η. are interaction terms, one for each solute, and are ob tained by correlating the mixture equilibrium data.