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following work [22], the same group evaluated the effect of flow rate and electrolyte viscosity on kmAe, limiting current and pressure drop. An expression for km considering the viscosity of the electrolyte was proposed: ≡ ∙ (2) Where Sh is the Sherwood number, df is the fibre diameter, D is the diffusion coefficient, Daistheso-calledDamköhlernumber,eff istheeffectivesolutionconductivity,Risthe universal gas constant, T is temperature and S is the electrode thickness. Notably, the exchange current density to limiting current density ratio, , an often-unappreciated ratio for electrode processes, is contained in the equation and was plotted as a function of v. The pressure drop over flow fields in cells [23,24,25], has yet to be directly correlated to mass transfer. In some cases (e.g. certain laboratory-scale cell suppliers) flow field designs for proton-exchange fuel cells (PEMFCs) have simply been moved across to RFBs with insufficient thought. PEMFCs employ gases, while most RFBs involve liquids with much higher viscosity. Furthermore, the transport properties of the flow fields depend on their size and shape and do not scale-up linearly [24]. Thus, efforts in this promising area should be directed towards studies which can be readily scaled-up or represent full-size cells, e.g. [26]. Both the local mass transfer at fibre level and the global mass transfer coefficient in utility-scale electrodes experiencing non-homogeneous porous fluid flow can be simulated. For instance, by digitising their geometry from X-ray CT scans, mass transfer coefficients and dimensionless correlations have been calculated for carbon felts using 5PDF Image | Redox flow batteries for energy storage challenges
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