Spatiotemporal Patterns in Liquid-Liquid Taylor-Couette-Poiseuille Flow

Campero, Richard John; Vigil, R. Dennis

doi:10.1103/physrevlett.79.3897

Cited by 26 publications

(7 citation statements)

References 11 publications

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“…V d became zero for Re /Re ,c greater than 4.3. Campero and Vigil (1997) observed the same phenomenon in a two-liquid phase system. This may worsen the performance of the VFR, since the vortices become a pseudostagnant region when they stop displacement.…”

Section: Introductionsupporting

confidence: 54%

Estimation of mass transfer parameters in a Taylor-Couette-Poiseuille heterogeneous reactor

Resende

Vieira

Sousa

et al. 2004

Braz. J. Chem. Eng.

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-A bench-scale, continuous vortex flow reactor (VFR), with a radius ratio, , equal to 0.48 and an aspect ratio, , equal to 11.19 was studied. This reactor may be used in the enzymatic hydrolysis of polypeptides obtained from sweet cheese whey with enzymes immobilized on agarose gel. Operational conditions were 2410 < Re < 11793 and 30-min residence time for glycerol-water, 14% w/w, 27 o C (Re ax = 1.1) and for water, 38 o C (Re ax = 1.5). Residence time distributions (RTDs) were obtained after pulse injections of different tracers (including dyed solid particles). Mass transfer coefficients of a lumpedparameter model of the reactor were estimated from these data. Model fitting to experimental data was accurate. Working conditions were selected so that transport properties of the fluids would be similar to the ones in the actual process at the final stages of whey hydrolysis.

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Section: Introductionsupporting

confidence: 54%

Estimation of mass transfer parameters in a Taylor-Couette-Poiseuille heterogeneous reactor

Resende

Vieira

Sousa

et al. 2004

Braz. J. Chem. Eng.

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“…For example, if two immiscible liquids are fed continuously to a horizontally oriented Taylor vortex flow cell, a variety of spatial and spatiotemporal hydrodynamic structures arise [35][36][37][38]. More recently it has been reported that the introduction of even a small amount of gas into a vertically oriented Taylor vortex flow cell results in dramatic drag reduction on the rotating inner cylinder and nontrivial gas bubble spatial distribution [39][40][41][42].…”

Section: Introductionmentioning

confidence: 99%

Experimental measurement of oxygen mass transfer and bubble size distribution in an air–water multiphase Taylor–Couette vortex bioreactor

Ramezani

Kong

Gao

et al. 2015

Chemical Engineering Journal

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h i g h l i g h t sMean bubble size, and size distribution in vertical gas-liquid Taylor vortex flow. Mass transfer coefficients for vertical gas-liquid Taylor vortex flow. Wall-driven shear produces prolate rather than oblate bubble shapes. Bubble size and spatial distribution explains low mass transfer coefficients. High wall area in annular geometry has significant impact on mass transfer. a b s t r a c tExperimental measurements of the volumetric liquid mass transfer and bubble size distribution in a vertically oriented semi-batch gas-liquid Taylor-Couette vortex reactor with radius ratio g = r i /r o = 0.75 and aspect ratio C = h/(r o À r i ) = 40 were performed, and the results are presented for axial and azimuthal Reynolds number ranges of Re a = 11.9-143 and Re H = 0-3.5 Â 10 4 , respectively. Based on these data, power-law correlations are presented for the dimensionless Sauter mean diameter, bubble size distribution, bubble ellipticity, and volumetric mass transfer coefficient in terms of relevant parameters including the axial and azimuthal Reynolds numbers. The interaction between wall-driven Taylor vortices and the axial passage of buoyancy-driven gas bubbles leads to significantly different dependencies of the mass transfer coefficient on important operating parameters such as inner cylinder angular velocity and axial superficial gas velocity than has been observed in horizontally oriented gas-liquid Taylor vortex reactors. In general, the volumetric mass transfer coefficients in vertical Taylor vortex reactors have a weaker dependence upon both the axial and azimuthal Reynolds numbers and are smaller in magnitude than those observed in horizontal Taylor vortex reactors or in stirred tank reactors. These findings can be explained by differences in the size and spatial distribution of gas bubbles in the vertically oriented reactor in comparison with the other systems.

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“…Recently, there has been a significant increase in investigating CT flow for two-phase systems [1][2][3][11][12][13][14][15][16][17][18][19][20][21][22][23], especially for the dispersion of two immiscible liquids and the generation of flow regime maps ( [13][14][15][16][17]). Twophase gas-liquid vertical flow has also been investigated by Shiomi et al [18].…”

Section: Introductionmentioning

confidence: 99%