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The drop diameter was independent from the applied pressure difference.
The first model requires as input the average drop diameter and the residence time while the second model uses the measured drop diameter distribution.
An empirical correlation is proposed for the estimation of the Sauter mean drop diameter.
Parameters varied are the drop diameter, the initial solute concentration and the mass transfer direction.
From these measurements, Sauter mean drop diameter (d3,2) has been estimated.
The maximum stable drop diameter ds derived from the model, shows a dependence of NWe−0.6.
The mean drop diameter decreases all along with increasing jet flow rate.
An optimum drop diameter of 0.20 0.25 cm is indicated for the toluene-acetone-water system.
The effects of liquid flow rate, drop diameter, inlet baffle position and organic phase density were investigated.
The drop diameter increased with a decrease in the ratio of the dispersed-phase viscosity to the continuous-phase viscosity.
The simplified correlation of Kumar and Hartland could be used for estimating the Sauter-mean drop diameter.
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