Parameters Effect on Heat Transfer Augmentation in a Cavity with Moving Horizontal Walls

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1. Introduction

Mixed convection, takes place when natural convection and forced convection mechanisms perform simultaneously to exchange heat due to temperature differences. This is likewise characterized as circumstances where both pressure and buoyancy forces interface. The heat transfer behavior of the fluid as convection is mostly depended on the flow, temperature, geometry and inclination. In recent years, the natural and mixed convection flow has gained interest from their hypothetical and practical perspectives.

“The double lid-driven cavity problem has been gained extensive interest among the scientists and researchers because of its simplest geometrical settings with all fluid mechanical structure and applications such as cooling of electronic gadgets, drying instrument, softening procedures and so forth. Additionally, movement of side walls is also responsible for the fluid convective behavior within the enclosed square cavity” [1] . Furthermore, many numerical investigations are examined on double lid driven square cavities [2] - [15] .

In recent past, Pal et al. [1] performed a numerical experiment on a lid driven cavity for low $\mathrm{Re}$ flow using Finite Difference Method (FDM). Therefore, we observe that no investigation has been done on the behaviors of heat transfer filled with air/water inside a square enclosure where the upper and lower walls are moving at constant speed and side walls are adiabatic. In this study, we have considered low and high Reynolds number flow to examine heat transfer properties. In such manner, the goal of this investigation is to review the behavior of fluid and temperature fields for various $\mathrm{Re},Ri\text{and}\mathrm{Pr}$ in a double lid driven square domain. Moreover, average Nusselt number $\left(Nu\right)$ is investigated in order to see the performance of the heat transfer inside the chamber.

2. Governing Equation

In the present experiment, a steady state, incompressible flow inside a cavity has been studied. The physical model along with boundary conditions is shown in Figure 1. To continue study, we have considered the case where the horizontal upper hot wall is moving towards and lower cold lid is moving backwards at a constant velocity. However, left and right side vertical wall are kept adiabatic in each case.

The following governing equation has been presented for 2D and incompressible flow in non-dimensional form:

$\frac{\partial U}{\partial X}+\frac{\partial V}{\partial Y}=0$ (1)

$U\frac{\partial U}{\partial X}+V\frac{\partial U}{\partial Y}=-\frac{\partial P}{\partial X}+\frac{1}{\mathrm{Re}}\left(\frac{{\partial}^{2}U}{\partial {X}^{2}}+\frac{{\partial}^{2}U}{\partial {Y}^{2}}\right)$ (2)

$U\frac{\partial V}{\partial X}+V\frac{\partial V}{\partial Y}=-\frac{\partial P}{\partial Y}+\frac{1}{\mathrm{Re}}\left(\frac{{\partial}^{2}V}{\partial {X}^{2}}+\frac{{\partial}^{2}V}{\partial {Y}^{2}}\right)+Ri\theta $ (3)

$U\frac{\partial \theta}{\partial X}+V\frac{\partial \theta}{\partial Y}=\frac{1}{Pr\text{}Re}\left(\frac{{\partial}^{2}\theta}{\partial {X}^{2}}+\frac{{\partial}^{2}\theta}{\partial {Y}^{2}}\right)$ (4)

Figure 1. Simplified diagram of the physical geometry.

where U and V are the velocity components along X and Y directions, θ is the non-dimensional temperature and P is the non-dimensional pressure component. Here, the dimensionless parameters in Equations (1)-(4) are: Ri is the Richardson number, Re is the Reynolds number, Gr is the Grashof number,

$X=\frac{x}{L};Y=\frac{y}{L};U=\frac{u}{{V}_{L}};V=\frac{v}{{V}_{L}};P=\frac{p}{\rho {V}_{L}^{2}};\theta =\frac{T-{T}_{C}}{{T}_{H}-{T}_{C}};$

$Ri=\frac{Gr}{R{e}^{2}};Re=\frac{{V}_{L}L}{\nu};Gr=\frac{g\beta \Delta T{L}^{3}}{{\nu}^{3}};Pr=\frac{\nu}{\alpha};$

where $\rho ,g,\alpha ,\beta \text{and}\nu $ are the fluid density, gravitational acceleration, thermal diffusivity, the coefficient of thermal expansion and kinematic viscosity, respectively. The velocity and temperature flow fields boundary conditions are shown in Figure 1 and have the following dimensionless form:

$\begin{array}{l}U=V=0,\frac{\partial \theta}{\partial x}=0\text{at}X=0\text{and}X=1\\ U=-1,V=0,\theta =0\text{at}Y=0\\ U=1,V=0,\theta =1\text{at}Y=1\end{array}\}$ (5)

Also, the definition of local and average Nusselt number is described in Pal et al. [1] .

3. Numerical Procedure and Validation

We have used finite difference method to deal with the governing equations (1)-(4) along with the boundary situation (5). Then an in house code (DGK) has been implemented to represent the flow and thermal behaviors. However, grid independent test has been done to verify the code which is also presented in Pal et al. [1] . Furthermore, numerical approximation and comparison has been examined graphically for centerlines velocity profiles with Adair et al. [16] , Ghia et al. [9] and found good harmony. Another study has been presented for average Nusselt number by using Simpson’s 1/3 rule to approve the code and validate result with Abu-Nada et al. [7] , Waheed et al. [5] and Sharif et al. [17] . Aspects of these studies have been discussed in Pal et al. [1] .

4. Result and Discussion

In this research, variation of velocity and temperature profiles with different Re, Ri and Pr inside the square cavity with the given boundary conditions (5) are studied and explained graphically in Figures 2-4. Additionally, variation of average Nusselt number has been studied and presented in tabular form in Table 1. The dimensionless parameters considered here are 100 ≤ Re ≤ 1000, 0.1 ≤ Ri ≤ 3.0 and 0.71 ≤ Pr ≤ 10.

The flow and thermal fields within the double lid driven cavity for Ri = 1.5 and Pr = 10.0 are represented in Figure 2 for numerous values of Reynolds number. This profiles shows that for Re = 500 fluid flow develops a high speed velocity region near the moving lid. For the moving lids, there appear two large secondary vortices in the two opposite corner and two tiny secondary vortices in the center of the cavity. The flow is dominated by the forced convection and due to high temperature difference along the moving lids, the flow field becomes more turbulent. Furthermore, the size of the secondary vortices increases with the increase of Re to 1000. Moreover, two tiny secondary eddies as it is located at the center of the cavity form another convective cell inside it which seems to be chaotic. From temperature profiles in Figure 2, there occurs high temperature

Table 1. Variation of average Nusselt number for different Re, Pr and Ri.

Figure 2. Variation of velocity and temperature profiles with different Reynolds number for Ri = 1.5, Pr = 10.0.

Figure 3. Variation of velocity and temperature profiles with different Richardson number for Re = 100, Pr = 10.0.

Figure 4. Variation of velocity and temperature with different Prandtl number for Re = 100, Ri = 0.1.

difference region near the moving lid for Re = 500. Additionally, the center thermal region separate into two parts. One part moving towards the hot region and another part moving towards the cold region. These all makes a steep temperature gradient along the adiabatic wall. This is due to the presence of shear stress. As an increase of Reynolds number Re = 1000, shows hot fluid mixes up with the cold fluid very well and the thermal boundary layer diminishes.

Figure 3 represents the variation of velocity and isothermal profiles for miscellaneous values of 𝑅𝑖 with fixed Re = 100 and Pr = 10.0. Usually, the flow seems to be dominated by the mixed convection for 0.1 < Ri < 10. From velocity profiles for Ri = 1.0, it is observed that the upper and lower secondary cells are moving in the clockwise pattern due to the movement of the upper and lower walls. Moreover, it creates high speed velocity region near the velocity boundary layer and it covers most of the cavity. However, two small eddies have been visible near the vertical walls. Besides, the tiny secondary vortices tend to merge and finally form a large secondary vortex for Ri = 1.5, 3.0 in the core of the cavity which may control the flow field with further increment of Ri. As a result, dominant secondary vortices are decreased in size. In this regard, buoyancy effect is clearly seen in velocity profiles. From Figure 3, it is seen that shear powers are prevailing in the cavity and, subsequently, the isotherms are generally assemble to the region close to the top and bottom surfaces of the square cavity for Ri = 1.0. The high temperature inclination close to the upper and lower walls is because of these high shear stress created due to moving lids. Also, a thin thermal boundary layer has developed on the top of the hot lid. Besides, mid temperature zone is visible in the center of the domain. Now if we look forward, expanding 𝑅𝑖 up to 1.5, the shear forces and buoyancy forces are a similar extent. In this way, coarse isotherms existed close to the top and base walls. Therefore, a direct temperature difference in the vertical direction can be seen. Additionally, increments in Ri (Ri = 3.0) prompt more extensive development of isotherms covering the entire cavity. This leads a further abatement of the heat exchange strength the along moving lid because of a dynamically stable free convection impact. Along these lines, the buoyancy force characterizes the shaped fluid stream and heat exchange inside the domain.

Figure 4 represents the isothermal profiles for various Pr such as Pr = 0.71, 2.0, 5.0, 10.0 and taking the other dimensionless numbers such as Re = 100 and Ri = 0.10 as constant. If we consider the velocity profiles in Figure 4 for various Prandtl number then it is observed that velocity profiles is independent of Prandtl number. There exists a primary eddy for Pr = 0.71 and when Pr increases for the next three cases, there is no significant differences on the flow field. Because for Ri < 1.0 the flow is commanded by the shear force inside cavity and determines the temperature and buoyancy variations in the cavity. It shows strong dependency on Pr. From Figure 4, it is seen that there is a development of higher temperature difference zones located near the two opposite corners due to the adiabatic walls. As we increase the Prandtl number (Pr = 2.0), the temperature patterns are trying to twist due to the forced convection. Moreover, the thermal boundary layer thickness decreases so the average Nu increases with the higher values of Pr. In addition there exists a large isotherm region in the core of the cavity and tend to increase if Pr increases more.

Table 1 represent the average Nu for wide range of different dimensionless parameters such as Re, Pr and Ri. Further, it is seen that percentage enhancements of avg. Nu are 45%, 65% and 73% respectively for Re = 100 and Pr = 2, 5, 10. Moreover, such percentage enhancements of avg. Nu are 74%, 80% 88% respectively for Re = 500 and Pr = 2, 5, 10. Also increment in percentage of the rate of heat transfer are 76% 80% 87% where Re = 1000 and Pr = 2, 5, 10, in all these cases keeping Ri = 0.1. More precisely, the maximum heat transfer difference almost 10% occurs when we consider Re = 100 and Re = 500. After that, it reduces to almost 2% to 3% between Re = 500 to Re = 1000. Thus we can conclude that if 𝑃𝑟 increase then the heat transfer rate increases. Also, highest heat transfer rate occurs for small values of Ri. Highest heat exchange attribute occurs for Ri = 0.1 which is fallen by almost 40% for Ri = 1.0. Finally, the heat transfer rate slightly decreases with the increase of Ri.

5. Conclusion

The flow phenomena and heat transfer are observed inside a bounded domain where the upper wall is moving in the positive direction and lower wall is moving in the negative direction. The geometrical characteristics have been set to the Equations (1)-(5) and then solved by 4th order FDM. The effects of dimensionless parameters Re, and Pr have been presented graphically and in tabular form. It is noticed that there is no effect of Pr on the velocity profiles but strong effect on temperature profiles. Also, it is found that for increasing of Ri, rate of heat exchange decreases. Besides, for low Richardson number flow is dynamically unstable and for higher values of Ri, the flow is stable. Furthermore, as Re increases, the augmentation of average Nu increases for all cases. Overall, higher intensification of average Nu is pragmatic when flow becomes turbulent and deterioration of average Nu can be realistic when flow becomes laminar.

Acknowledgements

This work has been fully supported by University Grant Commission (UGC), Bangladesh via grant number Reg./Admin-3/76338 (Year: 2017-2018).

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