The experimental volumetric liquid-phase mass transfer coefficients k(L)a measured in a slurry bubble column (0.095 in in ID) operated with several three-phase systems (air-ligroin-polyvinylchloride (PVC), air-ligroin-polyethylene (PE) and air-water-activated carbon) were predicted successfully based on a correction of Higbie's (1935) penetration theory. A correction factor (which is a single function of the Eotvos number) developed earlier (Nedeltchev et al., 2007) in gas liquid bubble columns was found applicable to slurry bubble columns. It varied from 0.22 to 1.91 in the above mentioned three-phase systems. As the bubble size becomes bigger, the correction factor increases and vice versa. The two major changes in the algorithm (applied to slurry bubble columns) are associated with the calculation of the Sauter-mean bubble diameter (Lemoine et al., 2008) and the gas liquid interfacial area. In the case of a slurry bubble column, both the slurry density and effective viscosity were used in the model correlations. It was found that the model yielded good results not only in the homogeneous regime but also in the heterogeneous regime (up to gas velocities of 0.08 m/s). It worked also well at relatively high solids concentrations (up to 15%). When the bubble Reynolds number is higher than 700 and when the superficial gas velocity is beyond 0.04 m/s, then the penetration theory based on the new definition of the contact time can be applied straightforwardly (without any correction factor). The developed model is applicable to ellipsoidal bubbles and it demonstrates the important effect of the geometrical characteristics (length and height) of these bubbles on the mass transfer coefficients. (C) 2013 Elsevier Ltd. All rights reserved