The Flow of a Variable Viscosity Fluid down an Inclined Plane with a Free Surface

Abstract

The effect of a temperature dependent variable viscosity fluid flow down an inclined plane with a free surface is investigated. The fluid film is thin, so that lubrication approximation may be applied. Convective heating effects are included, and the fluid viscosity decreases exponentially with temperature. In general, the flow equations resulting from the variable viscosity model must be solved numerically. However, when the viscosity variation is small, then an asymptotic approximation is possible. The full solutions for the temperature and velocity profiles are derived using the Runge-Kutta numerical method. The flow controlling parameters such as the nondimensional viscosity variation parameter, the Biot and the Brinkman numbers, are found to have a profound effect on the resulting flow profiles.

1. Introduction

The study of the flow of a viscous fluid with temperature dependent properties is of great importance in industries such as food processing, coating, and polymer processing, see Macosko and Oron et al. [1, 2]. In industrial systems fluids can be subjected to extreme conditions such as high temperature, pressure, and shear rates. External heating such as the ambient temperature and high shear rates can lead to a high temperature being generated within the fluid. This may have a significant effect on the fluid properties. It is a well-known fact in fluid dynamics studies that the property which is most sensitive to temperature rise is viscosity, see Myers et al. [3]. Fluids used in industries such as polymer fluids have a viscosity that varies rapidly with temperature and this may give rise to strong feedback effects, which can lead to significant changes in the flow structure of the fluid, see Wyle and Huang [4]. Due to the strong coupling effect between the Navier-Stokes and energy equations, viscous heating also plays an important role in fluids with strong temperature dependence, see Costa and Macedonio [5]. In this paper we focus on the effect of temperature on the viscosity. In particular, we investigate the viscosity variation by Reynolds law [5] or Nahme's law [3], which assumes that the viscosity varies exponentially with temperature. Myers et al. [3] studied the flow of variable viscosity between parallel plates with shear heating. Costa and Macedonio [5] applied the temperature dependent viscosity model to study magma flows. Elbashbeshy and Bazid [6] investigated the effect of temperature dependent viscosity on heat transfer over a moving surface. In their investigation, the fluid viscosity model varies as an inverse linear function of temperature. The work in [6] was extended in [7] to include variable internal heat generation. The solution was obtained using the Runge-Kutta numerical method, and results presented show that when the coefficient of viscosity variation parameter increases, the temperature of the fluid (water) increases slightly, whilst the opposite is true for the velocity profiles. Elbarbary and Elgazery [8] investigated the effects of variable viscosity and variable thermal conductivity on heat transfer from moving surfaces with radiation. In their work the fluid viscosity also varies as an inverse linear function of temperature, and the thermal conductivity varies as a linear function of temperature. The effect of convective heat transfer is extremely important in understanding the flow structure of many fluids used in industrial and natural applications. The present paper is aimed at investigating the effect of convective heat transfer on the flow of a viscous fluid with exponential temperature dependent viscosity, down an inclined plane with a free surface.

2. Problem Formulation

Figure 1 represents a two-dimensional laminar flow with a free surface. The figure depicts an infinitely wide channel of typical length scale 𝐿 in the 𝑥 direction and height 𝐻 in the 𝑦 direction. The fluid flows down a plane inclined at an angle 𝛽, and the dominant driving force for the flow is gravity, denoted 𝑔. The ambient temperature is denoted 𝑇_𝑎, the fluid temperature is denoted 𝑇, and the temperature at the bottom surface is denoted 𝑇_𝑠. The fluid viscosity 𝜇 will not be specified, but the viscosity of the fluid will vary exponentially with temperature.

Figure 1 

The geometry of the problem.

In developing the mathematical model for the fluid flow, the following assumptions will be made:(i)the fluid is incompressible, but the viscosity, 𝜇(𝑇), is temperature dependent;(ii)the governing equations are derived for a thin film flow such that lubrication theory may be applied;(iii)the film height 𝑇 is considered to be constant;(iv)the flow regime is laminar.

Taking into account these assumptions, the continuity, Navier-Stokes, and energy equations are written as follows: 𝜕𝑢+𝜕𝑥𝜕𝑣𝜌𝜕𝑦=0,𝜕𝑢𝜕𝑡+𝑢𝜕𝑢𝜕𝑥+𝑣𝜕𝑢𝜕𝑦=−𝜕𝑝𝜕𝜕𝑥+𝜌𝑔sin𝛽+2𝜇𝜕𝑥𝜕𝑢+𝜕𝜕𝑥𝜇𝜕𝑦𝜕𝑢+𝜕𝑦𝜕𝑣,𝜌𝜕𝑥𝜕𝑢𝜕𝑡+𝑢𝜕𝑣𝜕𝑥+𝑣𝜕𝑣𝜕𝑦=−𝜕𝑝𝜕𝜕𝑦+𝜌𝑔cos𝛽+2𝜇𝜕𝑦𝜕𝑣+𝜕𝜕𝑦𝜇𝜕𝑥𝜕𝑢+𝜕𝑦𝜕𝑣,𝜕𝑥𝜌𝑐_𝑝𝜕𝑇𝜕𝑡+𝑢𝜕𝑇𝜕𝑥+𝑣𝜕𝑇𝜕𝜕𝑦=𝑘²𝑇𝜕𝑥²+𝜕²𝑇𝜕𝑦²+𝜕𝑝𝜕𝑡+𝑢𝜕𝑝𝜕𝑥+𝑣𝜕𝑝2𝜕𝑦+𝜇𝜕𝑢𝜕𝑥²+𝜕𝑢+𝜕𝑥𝜕𝑣𝜕𝑦²+2𝜕𝑣𝜕𝑦², (1) where the notation is defined in the nomenclature showed at the end of the paper. These governing equations are nondimensionalised using the following scales: 𝑥=𝐿𝑥^′,𝑦=𝐻𝑦^′,𝑢=𝑈𝑢^′,𝑣=𝐻𝑈𝐿𝑣^′𝐿,𝑡=𝑈𝑡^′,𝜇=𝜇₀𝜇^′𝑝=𝑃𝑝^′=𝜇_0𝑈𝐿𝐻²𝑝^′,𝑇=𝑇₀+𝑇_𝑎−𝑇₀𝑇^′=𝑇₀+Δ𝑇𝑇^′, (2) where all quantities with prime denote nondimensional parameters. The pressure scale 𝑃=𝜇₀𝑈𝐿/𝐻² is standard for lubrication theory. The reference viscosity and the temperature difference are denoted by 𝜇₀ and Δ𝑇, respectively. To simplify notation, the primes are omitted from now on. Since the film is thin, the aspect ratio 𝜀=𝐻/𝐿≪1. Using the scaled parameters, (1) now becomes 𝜕𝑢+𝜕𝑥𝜕𝑣𝜀𝜕𝑦=0,₂Re𝜕𝑢𝜕𝑡+𝑢𝜕𝑢𝜕𝑥+𝑣𝜕𝑢𝜕𝑦=−𝜕𝑝𝜕𝑥+1+2𝜀²𝜕𝜇𝜕𝑥𝜕𝑢+𝜕𝜕𝑥𝜇𝜕𝑦𝜕𝑢𝜕𝑦+𝜀²𝜕𝑣,𝜀𝜕𝑥₂Re⁴𝜕𝑢𝜕𝑡+𝑢𝜕𝑣𝜕𝑥+𝑣𝜕𝑣𝜕𝑦=−𝜕𝑝𝜕𝑦+𝜀cot𝛽+2𝜀²𝜕𝜇𝜕𝑦𝜕𝑣𝜕𝑦+𝜀²𝜕𝜇𝜕𝑥𝜕𝑢𝜕𝑦+𝜀²𝜕𝑣,𝜀𝜕𝑥₂Pe𝜕𝑇𝜕𝑡+𝑢𝜕𝑇𝜕𝑥+𝑣𝜕𝑇𝜕𝑦=𝜀²𝜕²𝑇𝜕𝑥²+𝜕²𝑇𝜕𝑦²+PrEc𝜕𝑝𝜕𝑡+𝑢𝜕𝑝𝜕𝑥+𝑣𝜕𝑝𝜕𝑦+Φ, (3) where Φ=Br𝜇2𝜀²𝜕𝑢𝜕𝑥²+2𝜀²𝜕𝑣𝜕𝑦²+𝜕𝑢𝜕𝑦+𝜀²𝜕𝑣𝜕𝑥². (4)

The Péclet number Pe=𝜌𝑐_𝑝𝑈𝐿/𝑘 represents the ratio of convective heat transport to the conductive heat transport, and the Brinkman number Br=𝜇₀𝑈²/𝑘Δ𝑇 represents the ratio of heat dissipation to fluid conduction. The Prandtl number Pr=𝜇₀𝑐_𝑝/𝑘 denotes the ratio of diffusivity for momentum to thermal diffusivity. The Eckert number Ec=𝑈²/𝑐_𝑝𝑇₀ denotes the ratio of kinetic energy to thermal mass. The velocity scale is given by 𝑈=𝜌𝑔𝐻²sin𝛽/𝜇₀, which denotes the ratio of gravitational forces to the dynamic viscosity. The parameter values may vary widely depending on the particular industrial application or the models under investigation. The parameter values for a lubricant are 𝜇₀∼10⁻³--0.5kg/ms,𝑐_𝑝∼2000J/kgK,𝐻∼10⁻³𝐾m,𝑘∼0.13W/mK,_𝑐∼10³,𝐿∼0.005,𝜀∼10⁻⁴,𝜌∼880--940kg/m³. (5)

The experimental values listed above are taken from several references, [9, page 4], and [10–13]. Using these values listed above, we obtain 𝜇Br=⁰𝑈²𝑘Δ𝑇∼0.01--0.5,Pe=𝜌𝑐_𝑝𝑈𝐿𝑘∼10⁵,𝜇PrEc=⁰𝑈²𝑘𝑇₀∼5×10⁻⁴,Re=𝜌𝑈𝐿𝜇₀∼40--2000,𝑈=𝜌𝑔𝐻²sin30𝜇₀∼0.4m/s. (6)

Despite the fact that the Péclet number is large, the reduced Péclet number 𝜀²Pe≈10⁻³ is small and may be neglected in the governing equations. The reduced Reynolds number 𝜀²Re≈1.8×10⁻⁵ may also be neglected. The reduced quantity PrEc is also assumed to be small, so it will be neglected from the governing equations. The Brinkman number may be close to unity and so must be retained. Using the above approximations, (3) may now be reduced to their final form: 𝜕𝑢+𝜕𝑥𝜕𝑣−𝜕𝑦=0,𝜕𝑝+𝜕𝜕𝑥𝜇𝜕𝑦𝜕𝑢𝜀𝜕𝑦+1=0+𝒪²,𝜀²,−Re𝜕𝑝𝜀𝜕𝑦+𝜀cot𝛽=0+𝒪²,𝜀⁴,𝜕Re₂𝑇𝜕𝑦²+𝜇Br𝜕𝑢𝜕𝑦²=0+𝒪𝜀²,𝜀²Pe. (7)(8)(9)(10)

The velocity and the temperature profiles may be determined after the boundary conditions associated with (7)–(10) are stated.

3. Boundary Conditions

(i)At 𝑦=0, a no slip boundary condition is applied, and the temperature at the bottom surface is constant: 𝑢(0)=𝑣(0)=0,𝑇(0)=0. (11)(ii)At the free surface, the shear stress is zero and the fluid temperature is imposed by the air and substrate, respectively: 𝜕𝑢𝜕𝑦_𝑦=ℎ=0,𝜕𝑇𝜕𝑦_𝑦=ℎ=Bi(𝑇−1), (12) where Bi=𝐻𝐾_𝑐/𝑘 is the Biot number and denotes the ratio of heat transfer to thermal conductivity, Alhama and Zueco [14] and Makinde [15]. The parameters 𝑘 and 𝐾_𝑐 denote the thermal conductivity and heat transfer coefficient, respectively. The fluid at the free surface is exposed to the ambient temperature. Hence, a cooling condition is applied.

In the following section the variable viscosity model is introduced, and the equations governing the flow are coupled to this model and solved using both analytical and numerical methods.

4. Variable Viscosity Analysis

We now focus on the fluid with an exponential variation of the form: 𝜇=𝜇₀𝑒^{−𝜃(𝑇−𝑇0)}, (13) where 𝜇₀ is the reference viscosity at the reference temperature 𝑇₀ and 𝜃 is the coefficient of viscosity variation with temperature Costa and Macedonio [5]. Equation (13) can be written in nondimensional form, 𝜇=𝑒^∝𝑇, (14) where ∝=𝜃Δ𝑇. Equation (14) is commonly known as Nahme's exponential law [5] or Reynolds law, see Myers et al. [3]. Combining (8) and (14), integrating with respect to 𝑦, and applying the boundary conditions (12) give the velocity gradient, 𝜕𝑢=𝑒𝜕𝑦1−𝑦^∝𝑇, (15) where we have used the fact that 𝜕𝑝/𝜕𝑥=0 to write (15) as a result from (9). Equation (15) cannot be integrated further to determine 𝑢, since it involves the temperature 𝑇 which is unknown, so it must be solved numerically using the Runge-Kutta method. Substituting (14) and (15) into the reduced energy (10) gives 𝜕²𝑇𝜕𝑦²=Br1−𝑦²𝑒^𝛼𝑇. (16)

Equations (15) and (16) form a coupled system of nonlinear partial differential equations which require a numerical technique to obtain a full solution. However, when the viscosity variation is gradual, that is, 𝛼≪1 and 𝑇∼𝒪(1), an asymptotic analysis is possible. The main reason for using an asymptotic analysis is that we can clearly illustrate how the parameters affect the flow by looking into the dominant terms from the governing equations. This approach can be used to validate numerics. The question is how small must the parameter 𝛼 be? Therefore, the key factor in determining the stage at which ∝ is small is the magnitude of Δ𝑇, since 𝜃 is the fluid property. In certain industrial applications for lubricating oil, the experimental values for the temperature may be confined in the region 50^∘C≤𝑇≤300^∘C; see [12, 13, 16], for example. Our interest is on large values Δ𝑇, since ∝∼𝜃Δ𝑇, and usually the fluid property 𝜃 for lubricant is small. Now taking the temperature difference Δ𝑇∼200^∘C and 𝜃∼0.00242 (see [17, page 31]), it can easily be shown that ∝∼0.5 for a lubricating oil. It is important to note that for different values of 𝜃 andΔ𝑇, the results will obviously yield a different value of ∝, depending on the fluid under investigation. The velocity and temperature may then be expanded in a series form, 𝑢=𝑢₀+∝𝑢₁,𝑇=𝑇₀+∝𝑇₁, (17)(18) where 𝑢₀, 𝑇₀, 𝑢₁, and 𝑇₁ represent the leading-order terms and the first-order perturbation terms in ∝. Substituting for 𝑇 into (16) yields 𝜕²𝑇₀𝜕𝑦²𝜕+∝²𝑇₁𝜕𝑦²=−Br1−𝑦²−∝𝑇₀1−𝑦². (19)

The leading order and 𝒪(∝) terms from (19) are 𝜕²𝑇₀𝜕𝑦²=−Br1−𝑦²,𝜕²𝑇₁𝜕𝑦²=−Br1−𝑦². (20)(21)

Equations (20) and (21) are solved subject to 𝑇₀=𝑇₁=0at𝑦=0,𝜕𝑇₀𝜕𝑦_𝑦=1=−Bi𝑇₀−1,𝜕𝑇₁𝜕𝑦_𝑦=1=Bi𝑇₁. (22)

Integrating (21) with respect to 𝑦 and applying the boundary conditions in (22) yield 𝑇₀=−Br121−𝑦⁴−1−Bi()+Bi−1Bi(Bi−1)𝑦. (23)

Integrating Equation (21) and applying the boundary conditions (22), we obtain 𝑇₁=Br²112561−𝑦²−15601−𝑦⁴+Bi(Biℎ=1)10𝑦³−10𝑦⁴+3𝑦⁵+Br²12Bi()1Bi−1()−12Bi−1Bi()𝑦+20Bi−111+168Bi(Bi−1)10𝑦³−10𝑦⁴+3𝑦⁵+Bi(Bi−1)²1−12Bi20𝑦. (24)

The final temperature profile is obtained by combining both (23) and (24) as =𝑇₀+∝𝑇₁. Similarly, a solution for the velocity profile can be derived. Combining (15) and (17) gives 𝜕𝑢₀𝜕𝑦+𝛼𝜕𝑢₁=𝜕𝑦1−𝑦+∝𝑇_𝑎1−𝑦. (25)

The leading order and 𝒪(∝) terms are therefore 𝜕𝑢₀=,𝜕𝑦1−𝑦𝜕𝑢₁𝜕𝑦=𝑇₀1−𝑦. (26)(27)

Equations (26) and (27) are solved subject to 𝑢₀=𝑢₁=0at𝑦=0. (28)

Equation (26) gives the Newtonian velocity profile as 𝑢₀=𝑦22−𝑦. (29)

A similar expression for (29) may be obtained in Myers et al. [3]. To obtain 𝑢₁, (23) and (27) are combined and integrated subject to (28), 𝑢₁=−Br721−𝑦⁶𝑦−622−𝑦−Bi𝑦²6()+Bi−13−2𝑦−1Bi𝑦²6().Bi−13−2𝑦 (30)

The final velocity profile is given by (29) and (32) as 𝑢=𝑢₀+∝𝑢₁. The numerical solution is discussed in the following section.

5. Numerical Solution

The coupled nonlinear partial differential equations (15) and (16) for the velocity and the temperature profiles are solved numerically using the fourth-order Runge-Kutta integration scheme. The solution for the temperature profile must be calculated first and then substituted into the velocity equation to obtain the solution for the velocity profile. Setting 𝑡₁=𝑇 and 𝑡₂=𝜕𝑇/𝜕𝑦, (16) can be written as a system of two first-order equations in 𝑡₁ and 𝑡₂ of the form, 𝜕𝑡𝜕𝑦¹𝑡₂=𝑡₂−Br1−𝑦²𝑒^∝𝑡1. (31)

This system can be written in vector form, 𝜕𝐭,𝜕𝑦=𝐹𝐭,𝑦 (32) where 𝐭=(𝑡₁,𝑡₂). The solutions for this system of differential equations are solved subject to the boundary conditions (11) and (12). The Runge-Kutta method requires an initial value, and the initial value for the temperature 𝑡₁ is taken as the boundary condition at 𝑦=0. The corresponding initial value for 𝑡₂ is randomly chosen. It is important to note that the best numerical results largely depend on a good guess for the initial condition; see [6, 7]. Once this initial value is chosen, we employ the Runge-Kutta method to solve for the temperature. When the solution of the iterative process for the Runge-Kutta scheme terminates, then the derivative for the temperature 𝑡₂ at the free surface is eventually corrected using the given boundary conditions (12). The set of parameters ∝, Bi, and Br are coupled to the system of differential equations, and we solve our equations using a small step size forΔ𝑦. The velocity gradient is given by 𝜕𝑢=𝑒𝜕𝑦1−𝑦^𝛼𝑡1. (33)

Once the temperature profile is calculated, the velocity profile is computed from (32) using the finite difference scheme, 𝑢_𝑛+1=𝑢_𝑛+Δ𝑢_𝑦⋅𝜕𝑢𝜕𝑦_{(𝑦𝑖,𝑡𝑖)}. (34)

In Section 6, we will discuss the results for the asymptotic and numerical methods. We will give account of the findings in this paper. We proceed our analysis for comparison of the asymptotic and numerical solutions.

6. Results and Discussion

Figure 2 depicts a typical application of the temperature dependent model in (16). This illustrates the relations between temperatures of the fluid with the Brinkman number. This also is widely studied by several references, such as Myers et al. [3] who studied the application in a closed channel and Makinde [15, 18, 19] who investigated the application with a free surface flow. In this case, the critical point for the temperature is depicted at 0.53 after which the two solution branches are shown. When the temperature is greater than 0.53, the system has no real solution which is indicative of thermal runaway.

Figure 2 

The channel temperature.

Figure 3 shows the temperature profiles corresponding to (18) where 𝑇₀ and 𝑇₁ are given by (23) and (24) and the numerical solution. In this figure the dotted lines represent the profiles from the asymptotic solution and solid lines for the numerical solution. The results are calculated for the case Bi=Br=0.3, so that the Biot and the Brinkman numbers are of the same magnitude. Different values of ∝ were considered in order to investigate its effect on resulting flow profiles. We start our investigation with a simple case where ∝=0 for a Newtonian fluid to a maximum of ∝=0.5 typically, for a lubricating oil. Curves (a), (b), (c), and (d) display four different values of ∝, namely, ∝=0,0.1,0.3, and 0.5. It is important to note that when ∝ increases, the viscosity of the fluid decreases. The temperature of the fluid in all four curves increases to their maximum temperatures at the free surface. When ∝ increases, the temperature of the fluid increases due to heat generation by the internal friction caused by the collision of the fluid particles. The Newtonian case is retrieved in curve (a) with ∝. The numerical results are in good agreement with the asymptotic as shown in curves (a) through to (d). In Figure 4, four curves representing the velocity profiles for (17) where 𝑢_𝑜 and 𝑢₁ are given by (29) and (32) are plotted together with the numerical solution. These profiles correspond to different values of ∝ as shown in Figure 3. The figure shows that the velocity of the fluid increases when increases. This is a result of the resistance force to the flow which decreases as ∝ increases. Curve (a) displays a Newtonian velocity profile with ∝=0, and this curve increases across the fluid layer to the maximum point at the top due to the effect of the gravitational forces and lack of resistance force to the flow. As shown in the figure, the numerical and asymptotic velocity profiles are in good agreement, particularly for the set of curves (c) and (d).

Figure 3 

The temperature profiles for (18) and numerical solution.

Figure 4 

The velocity profile for (17) and numerical solution.

In Figures 5 and 6 the temperature and the velocity profiles for a numerical solution are displayed. The profiles are plotted to include large values for ∝ as shown in curves (c) through to (h) from ∝=10 to 62 for the temperature profiles in Figure 5. The velocity gradient in (11) increases exponentially with temperature, which eventually feeds back into (12) through the viscous heating term. The Newtonian temperature profile is shown in curve (a) with ∝=0, and curve (b) is plotted with ∝=0.5; these curves are the same as the ones which are shown in Figure 3 curves (a) and (b). It is important to note that the large values of ∝ were randomly chosen to test the reliability of the numerical scheme. The resulting temperature profiles show that the temperature of the fluid increases significantly when ∝ increases. The velocity profiles are displayed in Figure 6. Curves (a) through to (f) correspond to different values of ∝ as displayed in the figure, and other flow controlling parameters are the same as those which are given in Figure 5. The velocity of the fluid for all these curves increases to the maximum velocity occurring at the free surface. In this case, when ∝ increases, the velocity of the fluid increases due to less resistance force to the flow. Curves (a) with ∝=0 and (b) with ∝=0.5 are similar to the ones shown in Figure 4. The resulting velocity profiles show that for values of ∝>50, a change in the flow structure is observed.

Figure 5 

The temperature profiles for varying ∝.

Figure 6 

The velocity profiles for varying ∝.

In Figure 6, curves (g) and (h) show different flow behaviour as compared to curves (a) through to (f). Since the viscosity of the fluid decreases exponentially when ∝ increases, this therefore causes the fluid to behave like a Newtonian fluid when ∝=58 and62. Elbashbeshy and Bazid [6] analysed the effect of temperature dependent viscosity on heat transfer over a continuous moving surface. The full solutions for the velocity and temperature profiles were obtained using the fourth-order Runge-Kutta numerical scheme. Their results indicate that when the viscosity variation parameter increases for water, the temperature of the fluid increases slightly, which is in agreement with our results. However, in their investigation the velocity of the fluid decreases when the viscosity variation parameter increases.

The effect of the Biot number on the resulting temperature and velocity profiles is investigated. The importance of the Biot number is that it helps understand the influence of the ambient temperature on the flow system. When the Biot number tends to infinity (𝑘→∞), then both the ambient temperature and the fluid temperature reache equilibrium and ∼0. However, when the Biot number decreases (𝑘→0), the fluid loses its temperature to the surrounding atmosphere, and this process will have a major influence on the temperature variation of the fluid. An increase in the Biot number indicates that more heat is lost from the fluid to the surrounding atmosphere (hence cooling the fluid). When the Biot number decreases, a reduction in heat transferred to the surrounding atmosphere occurs, and the fluid gets hotter [11]. Because of the strong feedback between the Navier-Stokes and the energy equations, the Biot number will have a major influence on the resulting velocity and temperature profiles. Using the parameters listed in the previous section, we can easily show that Bi=7.692∼8. We again begin with a simple analysis for Bi=0 to a maximum of Bi=8 calculated for lubricating oil. The curves for the temperature profiles are shown in Figure 7 with different values of the Biot numbers, namely, Bi=0,0.01,1,4, and 8. The fluid temperature increases across the fluid layer to its maximum temperatures at the free surface as Bi decreases due to reduction in the heat transferred to the surrounding atmosphere. The figure clearly demonstrates that the fluid temperature rises with decreasing values of the Biot number, and the temperature profiles flatten out at the free surface as $Bi$ decreases, and when Bi=0, the temperature profile shows that the temperature gradient at the free surface is zero. Khaled [11] investigated the rate of heat and entropy transfer to the slab wall, and the results showed that the dimensionless temperature in the slab wall increases as Bi decreases, which is in agreement with our findings. The corresponding velocity profiles are shown in Figure 8 with different values of the Biot numbers. The fluid velocity increases across the layer to its maximum at the free surface as the Biot number decreases. This is a result of the resistance force to the flow which decreases as Bi decreases.

Figure 7 

The temperature profiles for varying Bi.

Figure 8 

The velocity profiles for varying Bi.

The effect of the Brinkman number is displayed in Figures 9 and 10 for the temperature and velocity profiles. Other parameters are given by 𝛼=0.3 and Bi=0.3. Using the values listed in the previous section, the Brinkman numbers are given by Br=0 for the Newtonian case to 0.5 as shown in Figure 9. We have the Newtonian case displayed in curves (a) in each figure with a constant viscosity. Increasing Br results in increased viscous heat dissipation effect. The temperature of the fluid increases significantly when Br increases. In Figure 9, when Br increases, the fluid heats up quickly, the viscosity of the fluid drops, and the flow is faster. As a result, the fluid velocity increases significantly in the direction of the flow.

Figure 9 

The effect of the Brinkman number on temperature profiles.

Figure 10 

The effect of the Brinkman number on the velocity profiles.

7. Conclusion

A steady gravity driven flow of a temperature dependent variable viscosity model was investigated. The results were obtained using an asymptotic technique and the fourth-order Runge-Kutta integration scheme. We used experimental values for lubricating oil to determine the value of 𝛼 for the asymptotic approximation terms. The numerical results were compared with the asymptotics. The Newtonian cases for both the temperature and velocity of the fluid are retrieved when 𝛼 is zero, and the results showed good agreement in all the curves for the temperature and velocity profiles. The effects of large values of 𝛼 on the resulting velocity and temperature profiles were further investigated. When 𝛼 increase, the temperature and the velocity of the fluid increase significantly. However, when 𝛼=58, a change in the flow structure is observed from the velocity profiles. Since the viscosity of the fluid decreases exponentially when 𝛼 increases, the prediction of the velocity profiles shows a different flow structure. This therefore causes the fluid to behave like a Newtonian fluid, in particular when 𝛼≥58. Furthermore, the effect of the flow controlling parameters such as the Biot and the Brinkman numbers was investigated. In the case of the Biot number, the temperature of the fluid increases significantly when the Biot number decreases due to heat lost from the fluid to the surrounding atmosphere, and as a result, the fluid temperature flattens out at the free surface. The velocity of the fluid increases as the Biot number decreases, due to less resistance force to the flow. The Brinkman number Br was also investigated, and the results showed that as Br increases, the temperature of the fluid increases due to heat dissipation, and the velocity of the fluid increased significantly due to the resistance force to the flow, which decreases when the Br increases.

Nomenclature

Bi=𝐻𝐾𝑐/𝑘:	Biot number
Br=𝜇0𝑈2/𝑘Δ𝑇:	Brinkman number
𝐶𝑝:	Heat capacity (J·Kg−1·K−1)
Ec=𝑈2/𝑐𝑝𝑇0:	Eckert number
𝑔:	Acceleration due to gravity (m s2)
𝐻:	Channel height (m)
𝑘:	Thermal conductivity (W·m−1·K−1)
𝐾𝑐:	Heat transfer coefficient (W·m−2·K−1)
𝐿:	Channel length (m)
𝑃:	Pressure scale (Pa)
𝑝:	Pressure (Pa)
Pe=𝜌𝑐𝑝𝐿𝑈/𝑘:	Péclet number
Pr=𝜇0𝑐𝑝/𝑘:	Prandtl number
Re=𝜌𝑈𝐿/𝜇0:	Renolds number
𝑡:	Time (s)
𝑇:	Temperature (°C)
𝑇𝑎:	Ambient temperature (°C)
𝑇𝑠:	Bottom surface temperature (°C)
Δ𝑇:	Temperature drop (°C)
𝑈=𝜌𝑔𝐻2sin𝛽/𝜇0:	Velocity scale (m s1)
(𝑢,𝑣):	Cartesian velocity (m s1)
(𝑥,𝑦):	Cartesian coordinates (m)
𝜀:	Aspect ratio of the flow
𝜇:	Dynamic viscosity (kg·m−1·s−1)
𝜇0:	Dynamic viscosity reference (kg·m−1·s−1)
Φ:	Viscous dissipation function
𝜌:	Fluid density (Kg·m−3)
𝜃:	Coefficient of viscosity variation (K−1).