Rajinder Kumar

Flow through a plateau border of cellular foam

Experimentally measured average velocities through plateau borders of stationary cellular foam, when compared with those calculated with the assumption of rigid Plateau Border walls, show that the assumption of rigid walls severely underestimates the velocities. n nAn analysis of the situation wherein plateau border walls have velocities, as decided by the surface viscosity of the system, is presented here. The plateau border is idealized as a pipe of equilateral triangular cross-section with vertices of the triangle having zero velocity. The pertinent form of Navier-Stokes equations with inhomogeneous boundary conditions and its solution through a procedure of successive approximations is presented in dimensionless form. The solution reduces to the known solution of slow steady flow through a triangular pipe, when surface viscosity is infinite. n nResults indicate that the assumption of rigid plateau border walls is valid only when value of the inverse of dimensionless surface viscosity is less than 0.044. Beyond that the assumption severely underestimates the flow and the effect of nonrigidity of the wall must be considered.

Studies in bubble formation — III

Bubble formation from single horizontal orifices submerged in Newtonian liquids has been investigated for such chamber volumes that both the pressure inside the chamber and flow rate into the bubble are time dependent. The data collected show that under these conditions the bubble volume decreases exponentially with increase in orifice submergence. The equations for the generalized two stage model of bubble formation, taking the variation of gas flow rate with time into account, have been derived. These equations reduce to the cases of constant gas flow rate and constant pressure when adequate constraints are imposed. The results obtained under intermediate conditions have been quantitatively explained on the basis of these equations.

Liquid holdup in semi-batch cellular foams

Abstract This paper presents a new model to predict liquid holdup profiles in serni-batch cellular foams. The model is based on two basic processes of film thinning and flow through Plateau borders. It takes into account the mobility of Plateau border walls, as decided by the surface viscosity; and the mobility of the film surface, as dictated by the surfactant concentration gradient on the film surface. The cellular foam is idealized to consist of three components; namely, the film, the “nearly horizontal Plateau border” and the “nearly vertical Experimental investigation on the overall liquid holdup profiles in the semi-batch foams is reported. The experimental parameters varied were the super The theoretically predicted liquid holdup profiles compare reasonably well with those determined experimentally.

Coalescence of drops in stirred dispersion. A white noise model for coalescence

Coalescence between two droplets in a turbulent liquid-liquid dispersion is generally viewed as a consequence of forces exerted on the drop-pair squeezing out the intervening continuous phase to a critical thickness. A new synthesis is proposed herein which models the film drainage as a stochastic process driven by a suitably idealized random process for the fluctuating force. While the true test of the model lies in detailed parameter estimations with measurement of drop-size distributions in coalescing dispersions, experimental measurements on average coalescence frequencies lend preliminary support to the model.

Liquid overflow from vertical co-current foam columns

Abstract A new criterion to predict the liquid overflow rate from vertical co-current foam column has been suggested. This criterion is combined with a recent model for liquid holdup in semi-batch foams to generate an analysis for co-current foam columns. The paper also presents experimental investigations on liquid overflow rate in the hitherto unexplored ranges of parameters. The variables studied are The suggested model is compared with both the published as well as present experimental data on the liquid overflow rate. The agreement between the two

Mass transfer with chemical reaction in a foam bed contactor

On the basis of dodecahedral structure of a foam bed, a model to predict conversion in a foam bed contactor with mass transfer with chemical reaction has been developed. To verify the proposed model, experiments have been carried out in a semi-batch apparatus for the absorption of lean CO2 gas in a foam of sodium hydroxide solution. The proposed model predicts fairly well the experimentally found absorption values.

Coalescence of rigid droplets in a stirred dispersion—II. Band-limited force fluctuations

The coalescence of nearly rigid liquid droplets in a turbulent flow field is viewed as the drainage of a thin film of liquid under the action of a stochastic force representing the effect of turbulence. The force squeezing the drop pair is modelled as a correlated random function of time. The drops are assumed to coalesce once the film thickness becomes smaller than a critical thickness while they are regarded as separated if their distance of separation is larger than a prescribed distance. A semi-analytical solution is derived to determine the coalescence efficiency. The veracity of the solution procedure is established via a Monte-Carlo solution scheme. The model predicts a reversing trend of the dependence of the coalescence efficiency on the drop radii, the film liquid viscosity and the turbulence energy dissipation per unit mass, as the relative fluctuation increases. However, the dependence on physical parameters is weak (especially at high relative fluctuation) so that for the smallest droplets (which are nearly rigid) the coalescence efficiency may be treated as an empirical constant. The predictions of this model are compared with those of a white-noise force model. The results of this paper and those in Muralidhar and Ramkrishna (1986, Ind. Engng Chem. Fundam. 25, 554-56) suggest that dynamic drop deformation is the key factor that influences the coalescence efficiency.

Breakage of viscoelastic drops in turbulent stirred dispersions

The existing models of drop breakage in stirred turbulent dispersions are applicable only to purely viscous dispersed phases. In their present form, they are found to underpredict the diameters of the largest stable drops formed when a viscoelastic fluid is dispersed into a Newtonian liquid. In purely viscous fluids, the turbulent stresses are opposed both by the stresses due to interfacial tension and the viscous stresses generated as the drop deforms. In viscoelastic fluids, drop deformation produces additional retractive elastic stresses which also oppose turbulent stresses. As the deformation rates are large, the retractive stresses can be large in magnitude. Assuming that these additional stresses decay with time, a model of viscoelastic drop breakage in turbulent stirred dispersions has been developed. The new model quantitatively predicts the dmax of viscoelastic fluids. The model, however, does not predict the observation that when the time constant of the fluid becomes large (λ > 0.5 s), the fluid can not be dispersed into droplets up to agitator speeds of about 10 rps in our equipment.

Prediction of bubble growth rates and departure volumes in nucleate boiling at isolated sites

A model has been developed to predict heat transfer rates and sizes of bubbles generated during nucleate pool boiling. This model assumes conduction and a natural convective heat transfer mechanism through the liquid layer under the bubble and transient conduction from the bulk liquid. The temperature of the bulk liquid in the vicinity of the bubble is obtained by assuming a turbulent natural convection process from the hot plate to the liquid bulk. The shape of the bubble is obtained by equilibrium analysis. The bubble departure condition is predicted by a force balance equation. Good agreement has been found between the bubble radii predicted by the present theory and the ones obtained experimentally.

An elongational flow model for drop breakage in stirred turbulent dispersions

The value of the average drop size in a stirred liquid-liquid dispersion is required for the analysis of rate processes occurring in it. This is normally achieved through the determination of the maximum diameter of stable drops,