To design fixed-bed adsorbers, kinetic parameters such as the fluid-film mass transfer coefficient and intraparticle diffusivity are required. The fluid-film mass transfer coefficient is usually estimated by theoretical and/or empirical equations. Most of the equations were derived from experimental data obtained through techniques other than adsorption. Thus, values estimated from empirical equations are unreliable to use for adsorption systems. The fluid-film mass transfer coefficients (k(F)) were determined experimentally from adsorption uptake curves measured under conditions of low Reynolds numbers. The experimental k(F) values were compared with several empirical equations, such as Carberry equation. The experimental values were found to be always 4/3 of the Carberry and Yoshida et al. equation. The experimental k(F) values were converted into modified k(F) values (=k(F)Delta a(v) = k(F)epsilon(p)/phi(s)). and compared with these equations. The particle void (epsilon(p)) and shape factor (phi(s)) were introduced into the particle surface area (a(V)) for experimental values to modify the area where mass transfer at the fluid-film boundary surrounding adsorbent particles affects. Those k(F) values were nearly identical, suggesting that only mass transfer around particle pores contributes to the k(F) value for adsorbent particles. To represent the mass transfer at fluid film appropriately, k(F)a(V) should be employed, since the error of a(V) is included in k(F) value. (C) 2011 Elsevier B.V. All rights reserved.