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2016
MODELING FOR SLURRY PIPELINE FLOW HAVING COARSE PARTICLES
1-33
10.1615/MultScienTechn.2016016085
Navneet
Kumar
Department of Mechanical Engineering, Galgotias College of Engineering and Technology, Greater Noida, G.B. Nagar, Uttar Pradesh–201306, India
Manoj Kumar
Gopaliya
Department of Mechanical Engineering, C.V. Raman Global University
(CGU-Odisha), Bhubaneswar, Odisha, India
D. R.
Kaushal
Department of Civil Engineering, IIT Delhi, New Delhi, India
CFD modeling
Eulerian model
concentration distribution
slurry pipeline
pressure drop
slip velocity
This paper shows a numerical simulation of horizontal slurry flow (water-glass bead) of coarse particles suspensions in a Newtonian carrier fluid. Glass bead slurry in water having 440 μ;m mean diameter particles is analyzed through 54.9 mm diameter pipe at volumetric concentrations up to
50% flowing with varying flow velocities up to 5 m/s. A computational fluid dynamics Eulerian model with RNG k–ε turbulence closure is adopted to analyze monodispersed glass bead particles of density 2470 kg/m3. The modeling results are compared with experimental data obtained for concentration profiles at a central vertical plane using a γ-ray densitometer and pressure drop along the pipeline using differential pressure transducers. Qualitative aspects of this analysis have also been presented in this paper.
ON FORMATION AND INSTABILITIES OF A LIQUID BELL
35-52
10.1615/MultScienTechn.2016017590
A.
Kushwaha
Department of Mechanical and Industrial Engineering, IIT Roorkee, Roorkee, 247667, India
Arup Kumar
Das
Department of Mechanical and Industrial Engineering, Indian Institute of
Technology, Roorkee,
Uttarakhand-247667, India
liquid bell
liquid sheets
jet impingement
instability
Formation of liquid bells by jet impingement on a hemispherical solid has been numerically simulated
by implementing axisymmetric finite volume discretization on a quadtree adaptive grid. Piecewise linear interface tracking in the framework of the volume-of-fluid method is used to simulate the thin sheet generated by the aftermath of the jet-solid impact. The limits for the Weber number have been found within which stable bell shapes are obtained. Instabilities leading to bell rupture/shape distortion are examined using local velocity vectors and vorticity contours. An effort has been made to propose a generalized correlation for prediction of size in the case of stable and closed bells at different Reynolds number. The effect of variation in fluid viscosity, densities, and surface tension on the shape of the bell is studied. The bell shape has been found to be very sensitive to the surface tension. The density ratio between the fluid and medium affects the bell length while the effect of the fluid's dynamic viscosity is generally minimal except for very high viscosity liquids, which lead to conical
bells.
PHASE HOLDUPS IN THREE-PHASE FLUIDIZED BEDS WITH TWISTED TAPE INTERNAL
53-70
10.1615/MultScienTechn.2016016549
B. S.
Subramanyam
Department of Mechanical Engineering, VITAM,
Visakhapatnam-531173, India
M. S. N
Murty
Department of Chemical Engineering, GVPCOE(A),
Visakhapatnam-530048, India
B. Surendra
Babu
Department of Industrial Engineering, Gitam University, Visakhapatnam-530045, India
Kasala
Venkata Ramesh
Department of Chemical Engineering, Andhra University, Visakhapatnam-530003, India
holdup
bed porosity
three-phase fluidization
twisted tape
internal
turbulent promoter
The present study comprises of an experimental investigation on the phase holdups of a three-phase fluidized bed in the presence of twisted tapes. Well designed and carefully fabricated equipment was used to study the effect of pertinent dynamic and geometric variables on gas and liquid holdups and bed porosity. Measurement of bed height and pressure drop across the bed facilitated the computation
of bed porosity and individual phase holdups. The bed material consisted of glass spheres of different
diameters. Nitrogen was used as the gas phase. An electrolyte having physical properties close to those
of water was employed as the liquid phase. The gas holdup and liquid holdup data were correlated in terms of particle Reynolds number, Froude number based on gas velocity, and geometric parameters of the promoter. The bed porosity data were analyzed, and the Richardson-Zaki exponent was obtained
as 2.79.
A THREE-PHASE SLUG FLOW INVESTIGATION BY TOMOGRAPHIC DUAL-BEAM X-RAY IMAGING: SLUG FREQUENCY MEASUREMENT AND LESSONS FOR CORRELATION DEVELOPMENT AND APPLICATION
71-98
10.1615/MultScienTechn.2016018538
Jae S.
An
Clean Energy Processes (CEP) Laboratory, Department of Chemical
Engineering, Imperial College London, London SW7 2AZ, UK
Rhys G.
Morgan
Forsys Subsea - An FMC Technologies and Technip Company, One St. Paul's Churchyard, London EC4M 8AP, UK
Colin P.
Hale
Department of Chemical Engineering, Imperial College London, London SW7 2AZ, UK
Ivan
Zadrazil
Clean Energy Processes (CEP) Laboratory, Department of Chemical
Engineering, Imperial College London, London SW7 2AZ, UK
Geoffrey F.
Hewitt
Department of Chemical Engineering & Chemical Technology, Imperial College of Science, Technology & Medicine, Prince Consort Road, London SW7 2B Y, England, UK
Christos N.
Markides
Clean Energy Processes (CEP) Laboratory, Department of Chemical Engineering, Imperial College London, London SW7 2AZ, United Kingdom; Kutateladze Institute of Thermophysics, Siberian Branch of the Russian Academy of Sciences,
Russian Federation
slug flow
slug frequency
three-phase gas-liquid-liquid flow
threephase slug flow
three-phase slug frequency
New measurement data on three-phase (air-oil-water) slug flows are reported in a long (37 m), large-diameter
(3 in nominal, 77.9 mm bore) pipe, generated by using a nonintrusive technique based on a dual-beam X-ray tomography system. Based on this measurement data, the frequency of hydrodynamic slugs is determined at a position 30.6 m (~400 diameters) downstream of the inlet and over a range of inlet flow conditions with superficial velocities: 2–6 m/s (air), 0–0.5 m/s (oil), 0–0.5 m/s (water), from which slug frequency trends specific to this three-phase flow system are identified and reported in the literature for the first time. The slug frequency data are subsequently used to examine the feasibility and reliability of using slightly modified versions of many of the current two-phase
gas-liquid slug frequency correlations in order to predict the measured three-phase slug frequencies observed in the experiments. It is found that, in general, these correlations provide poor slug frequency predictions in the investigated flows; nevertheless, the correlations that tend to perform best are those that include terms that attempt to account for variations in the fluid properties. The approach
presented in this paper provides a method for reasonable three-phase slug frequency prediction as a first approximation, although the accuracy of this prediction can be improved if the apparent liquid-liquid mixture-viscosity can be determined more reliably in situ. The data made available in the present paper are to the best knowledge of the authors not presently available in the literature, and
can be used to develop and validate advanced multiphase flow models, beyond acting as a benchmark database for correlation checks and improvement, as is done here.