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                  3.7 Three-Phase Fixed Beds: Trickle-Bed and Ped Bubble-Bed Reactors ack  185


                    Burghardt   et al  . (1995) studied, among others, the liquid distribution using needle-type
                  distributors in trickle beds and found that the density of the liquid feed points does ha e v
                  an important effect on the value of the liquid holdup, and thus on the performance of the
                  reactor. They concluded that for a density of more than 5000 feeding points per square
                  meter, the liquid holdup was stabilized.
                    Another typical liquid distributor, which is sho essentially consists of wn in Figure 3.50,
                  a single parting box and weir troughs. Liquid loading, gas loading, and the column diam-
                  eter determine the number of parting boxes and weir troughs.


                  3.7.4 External Mass transfer

                  In trickle beds, the gas-to-liquid,  k a  GL  , and liquid-to-particle,  k a f  LS  , coef icients are used f
                                              fg
                  to represent the effect of the external mass transfer resistances. The interfacial areas   a  GL
                  and   a  LS  refer to the efe mass transfer surface per unit volume of empty reactor fecti v  . Due
                  to the fact that the coef f icients   k  fg  and   k  fL  cannot be easily estimated independently from
                  the corresponding interfacial areas   a  GL  and   a  LS  respectively, by simple experimental tech-
                  niques, correlations are normally reported for the products   k a  GL  and   k a f  LS   (Smith, 1981).
                                                                  fg
                  eactor Gas-liquid mass transfer in trickle-bed r s

                  The mass transfer coeficient in the gas-to-gas interf f  ace   k a g  GL  is ealuated using the fol- v
                  lowing correlation (F, 1999): ogler

                                              ka             23                     (3.424)
                                                     2 0.91
                                               gG L
                                                        P  G 
                                                 20.96     Z     u  sG          (3.425)


                   a/m,
                  where the pressure drop of the gas phase is in kP the superficial gas velocity in m/s,
                  and the mass transfer coeficient in s f    1  . As in the agitated three-phase mass transfer the ,
                   f
                  liquid-side mass transfer coeficient is the most significant coeficient in trickle beds,
                     f
                  because the gas phase is often either a nearly pure component, e.g. hydrogenations, or a
                  slightly soluble gas, e.g. oxidations, in these reactors (Smith, 1981).













                           Figure 3.50  Liquid distributors with single parting box and weir troughs.
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