By P Chattopadhyay
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E -1 ] a cf. a + ar + ar2 +....... P. Also, 1 + e a + e; + e! P. Y4 +e! 2) yields: Ls·xn - Ls·xo Gs·yn+1 - Gs·y 1 = or, ~. Gs (xn-xo) =Yn+1- Y l Fig. (e a -1)·y o e - Yn e n + 1 _1 a a Now, ea Yn+l - Y1 en+l_ a Yn+l - Y0 = e an+l - 1 where, Yn+1 - Yl Yn+1 - Yo ... 64) = actual change in gas composition. , ifthe gas leaving the absorber is in equilibrium with entering liquid. Putting n =NT' the total number of trays, the Eqn. 64 yields: YN T +1- Y0 Solving for NT we get: ... 65) Expressed in mole ratio terms, Eqn.
This is because, the liq-film resistance in liq-film-controlled processes reduces the value of overall mass transfer coefficient while it has only a small effect on overall coefficient in gas-film controlled processes. 2. Advantages of High Performance Structured Packing in Absorption Columns The structured packings with well-established performance, viz. Sulzer's Mellapak, Norton's IMTP-T series, Koch's Flexipac. etc. give rise to : 1. Low Pressure Losses: Small fans and compressors with efficient intake stages will be sufficient to ensure appropriate gas loading.
X may be constant. Under these circumstances the pressure driving force is the logarithmic average of the driving forces at the bottom and top of the packed bed: ... Z = - - - - - ... 146) KG,p·a. Pa) liq and gas composition at any point in the packed bed in terms of mol ratios. m 2) This straightforward approach to design as described in Eqn. 146 endows a quick method for specifying industrial absorption columns. However, in practice this is not so, because of the following reasons: • The rate of mass transfer is never constant.