Document Type: Full Lenght Research Article
Authors
Mechanical Engineering Department., Amirkabir University of Technology, Tehran, Iran
Abstract
Keywords
Journal of Heat and Mass Transfer Research
Journal homepage: http://jhmtr.journals.semnan.ac.ir 
History: Received 11 July 2013 Received in revised form 16 September 2013 Accepted 27 October 2013
Keywords: Twoway coupled Gasparticle flow Kinetic theory Turbulent boundary layer 

A B S T R A C T
This study is concerned with the prediction of particles’ velocity in a dilute turbulent gassolid boundary layer flow using a fully Eulerian twofluid model. The closures required for equations describing the particulate phase are derived from the kinetic theory of granular flows. Gas phase turbulence is modeled by oneequation model and solid phase turbulence by MLH theory. Results of oneway and twoway coupled approaches are compared with the available experimental and numerical results. Results show that oneway coupled approach is more efficient for particulate velocity prediction in dilute flows. But, if the gasphase flow characteristics are desired, the twoway coupled approach should be used. Effects of free stream velocity on the coupling are discussed.
© 2014 Published by Semnan University Press. All rights reserved. 
Effects of coupling on turbulent gasparticle boundary layer flows at borderline volume fractions using kinetic theory
Maziar Dehghan, Hassan Basirat Tabrizi^{*}
Mechanical Engineering Departmen., Amirkabir University of Technology, Tehran, Iran


1. Introduction

Gasparticle flows are frequently encountered in the natural environment and industrial processes, such as desert and sand storms, pollutions in industrial or urban regions, fluidized bed and pneumatic conveying of particles [1]. There are many parameters which determine the gasparticle flow characteristics; for example, particle mass loading rate ρp (Tsuji and Morikawa [2]), gravity g (Taniere et al. [3]), interparticle spacing (Sato et al. [4]), particle volume fraction α_{p}(Elghobashi [5]), velocity gradient of the flow (Li et al. [6]).
Elghobashi [5] classified gassolid flows when the solid volume fraction is less (dilute) or greater (dense) than 0.1%. When the flow is dilute, effect of presence of particle on the carrier fluid is negligible. The interaction in this regime is named oneway coupling. Also, a homogeneous model can be used in this regime same as the investigation done by Mirzaei and Dehghan [7]. When the flow is dense, the momentum transfer from particles to the carrier phase is large enough to modify the characteristics of the flow, and the interaction in this regime should be considered. This consideration could be done by using twoway coupling. Interparticle and wallparticle collisions may be important in dense flows and considering the collisions leads the fourway coupling. But, this classification is questionable in borderline values of the solid volume fractions. In this study, it is desired to see which way of coupling is efficient for engineering purposes.
Giacinto et al. [8] studied the coupling effects for the first time. They investigated the behavior of particles based on a oneway model and a twoway model approaches. Also, they proposed a correlation for pressure drop arising from the particulate phase. Nasr and Ahmadi [9] studied the turbulence modulation due to its interaction with dispersed solid particles in a downward fully developed channel flow. They used the Eulerian framework for the gasphase, whereas the Lagrangian approach was used for the particlephase. The effect of turbulence on the flowfield was included via the standard k–ε model. Nasr et al. [10] studied the effects of particle–particle collisions and the twoway coupling on the dispersed and carrier phase turbulence fluctuations in a channel flow based on a DNS solution. They found when the particle collisions were neglected but the particle–fluid twoway coupling effects were accounted for, the twoway coupling and the particle normal fluctuating velocity decreased near the wall causing a decrease in the particle deposition velocity. In the case of the fourway coupling in which both interparticle collisions and twoway coupling effects were present, it was found that the particle deposition velocity increased compared with the oneway coupling case. When the particle aerodynamic interactions were added to the fourway coupled case (termed sixway coupled case), no significant changes in the mean fluid and particle velocities and the fluid and particle fluctuating velocities were obtained.
Researchers investigate particles in particulate flows using two major approaches: Lagrangian and Eulerian. Lagrangian model traces the path of individual particles on their way through the flow field. This needs long computational time in comparison with Eulerian method. Eulerian approach is more efficient for engineering purpose but closure models are the shortcoming of the Eulerian approaches [11]. Closure relations for particulate flow have been derived from kinetic theory of granular flow in this study.
Similarities between nonuniform dense gases and particulate flows were a start point for developing the kinetic theory of granular flows. The kinetic theory of granular flow allows determination of pressure and viscosity of the solid particles by incorporating the flow, gas, and particle characteristics and properties [12, 13]. Lun et al. [14] applied the kinetic theory of granular flow for the first time. This model has been used and developed by researchers such as Sinclair and Jackson [15], Ding and and Gidaspow [16], Huilin et al. [13], Vejahati et al. [17], Dehghan and Basirat Tabrizi [18], and Yusof et al. [19].
Taniere et al. [3], Slater et al. [11], Wang and Levy [20, 21], and Dehghan and Basirat Tabrizi [18, 22] studied the turbulent boundary layer gasparticle flows. Taniere et al. [3] concentrated on the particle response to fluid turbulence in a dilute horizontal boundary layer. Slater et al. [11] used a oneway coupled method to predict the deposition rate of particles in the dilute region. Wang and Levy [20, 21] studied particle motion in a vertical boundary layer experimentally and numerically. They simulated the flow using the commercial ANSYS CFX4 software based on the kinetic theory of granular flow. Dehghan and Basirat Tabrizi [18] studied on the modeling of a dilute turbulent gasparticle flows near the solid flat wall. They introduced a new inlet condition for the granular temperature balance equation. Also, they investigated the self similar profiles of particle velocity in the boundary layer which were independent of location and free stream velocity. Dehghan and Basirat Tabrizi [22] investigated the need of a turbulent model for a turbulent particulate phase and showed that the conventional turbulence models which are based on the conventional fluids are not suitable for particulate flows. However, they indicated that the results of a turbulent model for the particulate flow are more precise in comparison with a laminar model, especially near the wall.
In this study, oneway and twoway coupled approaches have been used to predict the experimental velocities of Wang and Levy [20, 21]. Motion of particles with 60 µm diameter (d_{p}) and 1680 kg/m^{3} material density (ρ_{mp}) at 0.6 and 1.0 kg/m^{3} particulate loading rates (ρ_{p}) and 20 and 30 m/s free stream velocities near a flat solid boundary was simulated numerically. These quantities were used on the basis of experiments of Wang and Levy [20, 21]. So, the volume fraction of particulate phase is in the borderline value. EulerianEulerian twofluid model was used to model the flow. Closure relations for particulate phase have been derived from the kinetic theory of granular flow. Effects of free stream velocity and way of coupling on the velocity of gas and particulate phases are investigated and the numerical simulations are compared with the available numerical and experimental data of Wang and Levy [20, 21].
For twodimensional turbulent gas flow in a boundary layer of a solid flat plate (figure 1), one can write:
(1) 

(2) 

(3) 
U, u, and are instantaneous, mean, and fluctuating values, respectively. “1” is the upstream flow direction (the tangential direction to the plate). τ is the total stress tensor which is defined for incompressible fluids in the boundary layer of flat solid boundaries as:
(4) 
is the turbulent (eddy) viscosity. Oneequation model has been used for the gasphase to model it [20]:
Figure 1. Schematic diagram of the problem 

(5) 


(6) 

Here, k is turbulent kinetic, l denotes characteristic length of eddies which have the maximum portion of turbulent kinetic energy and l_{m} is the mixing length (Mixing Length Hypothesis):
(7) 
Gas phase parameters and variables are written with no subscript for convenience. Subscript ‘p’ denotes particulate phase. Governing equations for the particulate phase are [12]:
(8) 

(9) 
The solid stress tensor (τ_{p}) is expressed in terms of the solid pressure (P_{p}), bulk viscosity (µ_{b}), and shear stress viscosity (µ_{s}) as [12]:
(10) 
where I is unit matrix, µ_{b} is bulk viscosity of particulate phase, µ_{p} is shear viscosity of particulate phase, and B is drag coefficient which is required to couple the interface force for the twoway coupled approach. The interface momentum transfer coefficient will be as following when the porosity is greater than 0.8 [17]:
(11) 
the porosity (α) represents gasphase occupied area per the total area in any crosssection. The granular temperature (θ) is defined as a measure for the energy of the fluctuating velocity of the particles. The conservation equation of granular temperature is [12]:
(12) 

(13) 
Particulate phase pressure and shear viscosity have two important mechanisms in the dilute regimes, collisional and kinetic [24]:
(14) 
Laminar shear viscosity is [25]:
(15) 
“e” is the restitution coefficient of particles and e=1 is fully elastic. In this study, “e” is set to 0.95 [25]. Pressure of the particulate phase is [12]:
(16) 
the first term on the RHS is the kinetic and the second one is the collisional part. “g_{0}” is the radial distribution function [12]:
(17) 

(18) 

(19) 
µ_{b} is bulk viscosity, k_{p} is granular diffusion coefficient, and α_{p,max} is the maximum particle packing limit. Granular temperature dissipation and transfer between gas and particles are expressed as [12]:
(20) 

(21) 
Particles in turbulent flows have two types of motion: a) Random oscillations of individual particles, measured by the classical granular temperature; b) turbulence caused by the motion of clusters of particles. These two kinds of turbulence cause two kinds of mixing, mixing on the level of a particle and mixing on the level of clusters [26]. The expressed granular temperature theory is based on the laminar motion of particles. So, for considering the clusterlike motion of particles and effects of turbulent motion of particles, a model which considers the turbulent phenomena is required [11, 22, 26, 27]. Hence, the MLH (Mixing Length Hypothesis) theory was adopted for particulate phase in which equations are the same as those in the carrier phase and are described in equations 6 and 7.
It is assumed that gas phase had noslip condition and zero turbulent kinetic energy on the solid boundary. Free stream condition at the entrance was considered. At the exit, Neumanntype boundary condition was adopted. Particulate phase had the same boundary conditions, except on the solid wall for tangential velocity and granular temperature which are as following [15]:
(22) 

(23) 
ydirection is normal to solid boundary, e_{w} is the restitution coefficient at the wall and is set to 0.75 [28]. Adopting lm at the solid wall equal to zero is not a realistic assumption for the particulate phase because of slipvelocity of particles. Hence, Neumanntype boundary condition for the mixinglength was adopted for the particulate phase at the wall [22].
These equations (123) describe oneway coupled approach. If one adds “B(uV_{p})” to the RHS of the equations (3), twoway coupled approach will yield. Finitedifference method [18, 22, 29, and 30] was used to solve equations (123). Pseudotransient scheme was used to decouple the equations. Central difference in space and forward in time discretization with the second order of precision was applied to be more accurate. Nonuniform structured gird (figure 2) and artificial viscosity [18, 22] were used to save time with Compaq Visual FORTRAN 6.1 software.
3. Results and Discussion
Simulation is preformed based on a 71x141 grid. Also, a 121x201 grid is used to examine mesh dependency. Figure 2 compares the simulation results in the two grids. The maximum nondimensional difference between results of these two grids is less than 3% for both gas and solidphases. However, computational time of fine mesh increases in several orders.
Singlephase results of the gas phase are compared with the DNS result of Spalart [31] in figure 3. “k^{+}” is the non dimensional kinetic turbulent energy, “δ” is the boundary layer thickness, and “y” is normal direction to the wall.
The numerical result of oneequation turbulence modeling is off at the peak of the kinetic energy curve. This type of error (being out of the peak of the turbulent
a) 
b) 
Figure 2. Used mesh (a) and meshdependency examination (b) (p: particulatephase, g: gasphase, x=0.5, U_{∞}= 30 m/s, d_{p}= 60 µm) 
kinetic energy profile) is usual and originates from the modeling of turbulence phenomena instead of solving a complete and high resolution simulation (DNS). Overall, a good agreement between gasphase simulation and the DNS can be seen.
Figure 4 shows results of oneway coupled approach in comparison with the numerical and experimental results of Wang and Levy [20, 21]. Results of current study are closer to the experiments than the previous simulation of Wang and Levy [21]. It is due to some simplification of commercial ANSYS CFX4 code that has been used by Wang and Levy [21]. As it is discussed by Dehghan and Basirat Tabrizi [18], the accuracy of particulate phase results has a high dependency on the particulate viscosity definition and simulation. Away from the wall, drag term is dominating and velocity gradient vanishes. So, the velocity of particulates is not sensitive to the granular temperature and particulate viscosity values. The accuracy of results of gas and particulate phases has been verified.
Now, effects of coupling on the gas and particulatephase velocities will be discussed. “2W” in the following figures represents the twoway coupled approach.
Figures 5 and 6 show the particulate velocity results of oneway and twoway coupled approaches in comparison with experiments of Wang and Levy [21]. They could show a small discrepancy between the two
Figure 3. Gasphase simulation in comparison with the DNS results of Spalart [27] 
Figure 4. Examination of particulate phase simulation result accuracy (d_{p}=60 μm, particle loading rate ρ_{p}=1.0 kg/m^{3}, U_{∞}=30 m/s) 
approaches. This is due to low volume fraction. Discrepancies between oneway and twoway approaches decrease by increasing the axial location (xdirection). Velocity results of the twoway coupled approach are higher than the oneway one. It is a result of coupling. When the twoway coupled approach is used, the simulated velocity of gas phase would increase since the particles are faster in the boundary layer and the code could consider the momentum enhancement of particles. Figures 7 and 8 are plotted for 20 m/s free stream velocity.
Figure 5. Results of particle velocity of oneway coupled approach in comparison with the twoway at x=0.25 and 0.75 m (ρ_{p}=1.0 kg/m^{3}, U_{∞}=30 m/s) 
Figure 6. Results of particle velocity of oneway coupled approach in comparison with the twoway at x=0.5 and 1.0 m (ρ_{p}=1.0 kg/m^{3}, U_{∞}=30 m/s) 
Figure 7. Results of particle velocity of oneway coupled approach in comparison with the twoway at x=0.25 and 0.75 m (ρ_{p}=1.0 kg/m^{3}, U_{∞}=20 m/s) 
Figure 8. Results of particle velocity of oneway coupled approach in comparison with the twoway at x=0.5 and 1.0 m (ρ_{p}=1.0 kg/m^{3}, U_{∞}=20 m/s) 
Again, it can be seen that twoway coupled approach has still little effects on the results. However, these effects are more sensible than the 30 m/s free stream velocity. By decreasing the free stream velocity, boundary layer will grow. This growth simultaneously occurs with velocity decrease, which decreases the order of viscous term in the NavierStokes equations for the particulate phase. Therefore, importance of viscous term will decrease in comparison with the drag term in the equation of motion. On the other hand, twoway coupled approach has a drag nature. In other words, when drag has a greater order of magnitude, the twoway coupled approach will be more important. Furthermore, as it was expected the results of the twoway coupled approach are closer to the experiments. An important parameter for engineering purposes is the computational time. The cost of the twoway coupled approach is very high in comparison with the achieved accuracy. In this study, simulation of a oneway coupled model lasts less than 72 hours for nondimensional residuals lower than 0.001 on a PC with 3.12 GHz CPU and 4 GB RAM. But, the twoway coupled model needs more than 96 hours to achieve the same residuals of the oneway coupled model. Another matter arising from the twoway coupled approach is the tendency of the code to diverge. So, the code needs finer meshes and further numerical efforts to achieve the same residual of the oneway coupling.
From the presented discussion and results of the oneway and twoway models, one can conclude that the oneway coupled approach is more advantageous for engineering purposes in prediction particles velocity in such dilute conditions. Nevertheless, is it true for the carrying phase?
Figure 9 presents effects of the particulate loading rates (ρ_{p}= 1.0 and 0.6 kg/m^{3}) on the velocity of the carrier gas phase. It shows that particulate loading can modify the gasphase velocity profile. To see effects of particulate phase on carrier phase more obviously, figure 8 has been drawn. Effect of particulate loading rate on the wall friction factor is not negligible even in such dilute conditions as it can be seen in figure 10. Friction factor in 1.0 kg/m^{3} and 0.6 kg/m^{3} loading rates increases 12% and 8% respectively in comparison with the clean gas flow. It is due to some simultaneous effects which affect gasphase flow characteristics. From figure 8 one can see that
Figure 9. Effects of particulate loading rate on the gasphase velocity in the boundary layer (ρ_{p}=0.0, 0.6, and1.0 kg/m^{3}, U_{∞}=30 m/s) 
Figure 10. Effects of particulate loading rate on the wall friction factor (ρ_{p}=0.0, 0.6, and1.0 kg/m^{3}, U_{∞}=30 m/s) 
the gasphase velocity increases due to the particle existence. Simultaneously, boundary layer thickness attenuation occurs. These two simultaneous effects beside the high particle slipvelocity, which can be seen from figures 58, influence the gasphase velocity more considerable. Therefore, the twoway coupled approach could be important in dealing with carrier gasphase; while, it is not efficient for the particulate phase predictions for engineering purposes in such dilute flows.
4. Conclusion
Dilute turbulent gassolid boundary layer flow has been studied numerically. Eulerian twophase model based on the kinetic theory of granular flow has been used to model the flow. Turbulence of gas and solid phases has been modeled by the “kl” and MLH models. Collisions have been considered via restitution coefficients (e and e_{w}). Costs and benefits of the way of coupling (oneway / twoway coupled approach) have been investigated on the simulations. Highlights of this study may be stated as following:
To summarize, twoway coupled approach is not advantageous for such dilute flows, even in borderline volume fraction values (volume fractions near 0.1%). This is due to the computational costs and amount of achieved accuracy in the results. Oneway coupled approach results are accurate enough for engineering purposes. For example in the current simulation, the twoway coupled approach needs up to 50% more computational time than the oneway for a same error limit and mesh size.
Nomenclature 

C 
drag coefficient 
d 
diameter (m) 
e 
Restitution coefficient 
I 
unit matrix

K 
turbulent kinetic energy

l 
length scale

P 
pressure 
Re 
Reynolds number 
t 
time 
u, v 
velocity 
x, y 
coordinate 
Greek symbols 

α 
volume fraction

β 
momentum transfer coefficient 
γ 
granular temperature dissipation

δ 
boundary layer thickness

Θ 
granular temperature

υ 
kinematic viscosity

τ 
stress tensor

µ 
dynamic viscosity (Pa.s) 
ρ 
density (kgm3) 
Φ 
energy transfer between phases 
subscripts 

coll 
collision 
D 
drag 
g 
gas 
i, j 
indices

kin 
kinetic 
m 
mixinglength 
mp 
material density 
p 
particulate phase

t 
turbulent 
w 
wall 
Superscripts


‘ 
fluctuating value 
+ 
nondimension value

T 
transpose 
References
[1]. Li J., H. Wang, Z. Liu, S. Chen, C. Zheng, An experimental study on turbulence modification in the nearwall boundary layer of a dilute gasparticle channel flow, Exp Fluids, 53, 1385–1403 (2012).
[2]. Y. Tsuji, Y. Morikawa, LDV measurements of an airsolid twophase flow in a horizontal pipe, J Fluid Mech., 120, 385–409 (1982).
[3]. A. Taniere, B. Oesterle, J.C. Monnier, On the behavior of solid particles in a horizontal boundary layer with turbulence and saltation effects. Experiments in Fluids, 23, 463471 (1997).
[4]. Y. Sato, U. Fukuichi, K. Hishida, Effect of interparticle spacing on turbulence modulation by Lagrangian PIV, Int J Heat Fluid Flow, 21, 554–561 (2000).
[5]. S.E. Elghobashi, On predicting particleladen turbulent flows. App. Sci. Res., 52, 309329 (1994).
[6]. F. Li, H. Qi, C. You, Phase Doppler anemometry measurements and analysis of turbulence modulation in dilute gas–solid two phase shear flows, J Fluid Mech., 663, 434–455 (2010).
[7]. M. Mirzaei, M. Dehghan, Investigation of flow and heat transfer of nanofluid in microchannel with variable property approach, Heat Mass Transfer, 49, 18031811 (2013).
[8]. M. Di Giacinto, R. Piva, F. Sabetta., Twoway coupling effects in dilute gasparticle flows, ASME Transactions Journal of Fluids Engineering, 104, 304311 (1982).
[9]. H. Nasr, G. Ahmadi, the effect of twoway coupling and inter particle collisions on turbulence modulation in a vertical channel flow, Int. J. Heat Fluid Flow, 28, 15071517 (2007).
[10]. H. Nasr, G. Ahmadi, J.B. McLaughin, A DNS study of effects of particleparticle collisions and twoway coupling on particle deposition and phase fluctuations, J. Fluid Mech., 640, p. 507536 (2009).
[11]. S.A. Slater, A.D. Leeming, J.B. Young, Particle deposition from twodimentional turbulent gas flows. Int. J. Multiphase Flow, 29, 721750 (2003).
[12]. D. Gidaspow, Multiphase flow and fluidization: continuum and kinetic theory descriptions, Boston: Academic press, (1994).
[13]. L. Huilin, D. Gidaspow, J. Bouillard, L. Wenti, Hydrodynamics simulation of gassolid flow in a riser using kinetic theory of granular flow. chemical Engineering Journal, 95, 113 (2003).
[14]. C.K.K. Lun, S.B. Savage, D.J. Jefferey, N. Chepurniy, Kinetic theories for granular flow: inelastic particles in Couette flow and slightly inelastic particles in a general flow field. J. Fluid Mechanics, 140, 223256 (1984).
[15]. J.L Sinclair, R. Jackson, Gasparticle flow in a vertical pipe with particleparticle interactions. AIChE J., 35, 14731486 (1989).
[16]. J. Ding, D. Gidaspow, A bubbling fluidization model using kinetic theory of granular flow. AIChE J., 36, 523538 (1990).
[17]. F. Vejahati, N. Mahinpey, N. Ellis, M.B. Nikoo, CFD simulation of gas–solid bubbling fluidized bed: A new method for adjusting drag law, Canadian J. Chem. Eng., 87 (1), 1930 (2009).
[18]. M. Dehghan, H. Basirat Tabrizi, On nearwall behavior of particles in a dilute turbulent gas–solid flow using kinetic theory of granular flows, Powder Technology, 224, 273–280 (2012).
[19]. R. Yusuf, B. Halvorsen, M.C. Melaaen, Computational fluid dynamic simulation of ethylene hydrogenation in a fluidised bed of porous catalyst particles, Canadian J. Chem. Eng., 90 (3), 544557 (2012).
[20]. J. Wang, E.K. Levy, Particle motions and distributions in turbulent boundary layer of airparticle flow past a vertical flat plate. Experimental Thermal and Fluid science, 27, 845853 (2003).
[21]. J. Wang, E.K. Levy, Particle behavior in the turbulent boundary layer of a dilute gaspartilce flow past a flat plate. Experimental Thermal and Fluid science, 30, 473483 (2006).
[22]. M. Dehghan, H. Basirat Tabrizi, Turbulence effects on the granular model of particle motion in a boundary layer flow, Canadian J. Chem. Eng., 92, 189–195 (2014).
[23]. V.S. Arpaci, P.S. Larsen, Convective heat transfer, PrenticeHall Inc, (1984).
[24]. S. Dartevelle, Numerical and granulometric approaches to geophysical granular flows, PhD thesis, Department of Geological and Mining Engineering, Michigan Technological University: Houghton, (2003).
[25]. V.S. Syamlal, W. Rogers, T.J. O'Brien, MFIX documentation: volume I, theory guide: National Technical information service, Springfield, (1993).
[26]. D. Gidaspow, J. Jung, R.K. Singh, Hydrodynamics of fluidization using kinetic theory: an emerging paradigm 2002 FlourDaniel lecture. Powder Technology, 148, 123141 (2004).
[27]. Y. Cheng, F. Wei , Y. Guo, Y. Jin, CFD simulation of hydrodynamics in the entrance region of a downer. Chemical Engineering Science, 56(4), 16871696 (2001).
[28]. A.H. Govan, G.F. Hewitt, C.F. Ngan, Particle motion in the turbulent pipe flow. Int. J. Multiphase Flow, 15, 471481 (1989).
[29]. M. Dehghan, M. Mirzaei, A. Mohammadzadeh, Numerical formulation and simulation of a nonNewtonian magnetic fluid flow in the boundary layer of a stretching sheet, Journal of Modeling in Engineering 11 (34), 7382 (2013).
[30]. M. Dehghan, M. Mirzaei, M.S. Valipour, S. Saedodin, Flow of a nonNewtonian fluid over a linearly moving sheet at a transient state; new similarity variable and numerical solution scheme, Journal of Modeling in Engineering, (2014) (accepted manuscript).
[31]. P.R. Spalart, Direct numerical simulation of turbulent boundary layer up to Reθ=1410. J. Fluid Mechanics, 187, 6198 (1988).