# Unsteady Free Convection Boundary Layer Flows of a Bingham Fluid in Cylindrical Porous Cavities

- 157 Downloads

## Abstract

We consider two unsteady free convection flows of a Bingham fluid when it saturates a porous medium contained within a vertical circular cylinder. The cylinder is initially at a uniform temperature, and such flows are then induced by suddenly applying either a new constant temperature or a nonzero heat flux to the exterior surface. As time progresses, heat conducts inwards and this may or may not overcome the yield threshold for flow. For the constant temperature case, flow begins immediately should the parameter, Rb, which is a nondimensional yield parameter, be sufficiently large. The ultimate fate, though, is full immobility as the cylinder eventually tends towards a new constant temperature. For the constant heat flux case, the fluid remains immobile but will begin to flow eventually should Rb be sufficiently large. The two cases have different critical values for Rb.

## Keywords

Porous media Boundary layer Unsteady flow Convection Bingham fluid Yield stress Vertical cylinder## List of Symbols

## Latin Letters

- \(A_n\)
\(n\mathrm{th}\) coefficient in a Fourier–Bessel series

*g*Gravity

*G*Threshold body force

- \(J_0\)
Zero\(\mathrm{th}\) order Bessel function of the first kind

- \(J_1\)
First order Bessel function of the first kind

*k*Thermal conductivity

*K*Permeability

*p*Pressure

- \(p_z\)
Pressure gradient in the vertical direction

*q*Surface rate of heat transfer

*r*Radial coordinate

- \(r_1\)
Inner yield surface

- \(r_2\)
Outer yield surface

*R*Cylinder radius

- \(\mathrm{Ra}\)
Darcy–Rayleigh number

- \(\mathrm{Rb}\)
Rees–Bingham number

*t*Time

*T*Temperature (dimensional)

- \(T_0\)
Ambient (cold) temperature

- \(T_1\)
Temperature of heated surface

*w*Vertical Darcy velocity

## Greek Letters

- \(\alpha \)
Thermal diffusivity

- \(\beta \)
Coefficient of cubical expansion

- \(\lambda _n\)
\(n\mathrm{th}\) zero of \(J_0\)

- \(\theta \)
Temperature (nondimensional)

- \(\mu \)
Dynamic viscosity

- \(\rho \)
Reference density

- \(\varsigma \)
Heat capacity ratio

- \(\sigma _n\)
\(n\mathrm{th}\) zero of \(J_1\)

## Other Symbols

- \(\overline{~~}\)
Dimensional quantities

## 1 Introduction

The topic of the flow of a Bingham fluid when it is not saturating a porous matrix is a well-established field of study, and the literature is now quite mature. Efforts continue to develop different numerical methods which will allow an accurate computation of such flows, the chief difficulty being the presence of a yield surface which needs to be computed as part of the overall problem. In some simplified cases, the analysis can proceed analytically (such as for plane-Poiseuille and Hagen–Poiseuille flows), but in other one dimensional problems the analysis has to be completed by using a simple Newton–Raphson iteration equation on a transcendental equation which then allows the positions of the yield surfaces to be found. Examples of such works include those by Yang and Yeh (1965) and Bayazitoglu et al. (2007) who studied steady free convection in a vertical channel which is heated from the side. Steady convection will only ensue once the Rayleigh number is sufficiently large that the yield stress is overcome by the buoyancy force. For this free convection problem, there are two moving zero-shear regions (i.e. ones which act like solids) and three fluid regions undergoing shear. By contrast, Patel and Ingham (1994) considered mixed convection with the combination of buoyancy and a driving pressure gradient, while Barletta and Magyari (2008) studied a free convection version of vertical Couette flow. In both cases the number, the size and the locations of the plug-flow regions are dependent on further nondimensional parameters. One paper whose topic is closer to that of the present is that of Kleppe and Marner (1972) who considered a sudden change in the temperature of one the sidewalls and who then determined the evolution with time of the resulting velocity profile.

When a Bingham fluid saturates a porous medium there are some changes to the modelling of the equations of motion which are caused by the presence of the porous matrix. Just as the Navier–Stokes equations, which apply for a clear Newtonian fluid, are replaced by Darcy’s law, which applies in a porous medium, so it is that the usual yield-stress form of the Navier–Stokes equations, which gives zero shear when stresses are less than the yield stress, needs to be replaced by a Darcy–Bingham law. The first papers which presented such a law were those by Pascal (1979, 1981). This law appears later, see Eq. (1), but it provides a piecewise-linear dependence of the flux velocity on the applied pressure gradient; thus, there is a yield pressure gradient. When the pressure gradient (or, equivalently, body forces) is less than a threshold value then there is no flow. Further realism is obtained by considering the porous medium as an assembly of identical channels or pores, which gives the well-known Buckingham–Reiner law (1921). In this case the initial rise in the flow is quadratic immediately post-threshold, as opposed to linear in Pascal’s model. We also note that more sedate transitions to flow were found by Nash and Rees (2017) who considered distributions of channels/pores. In the present paper, we will adopt Pascal’s piecewise-linear form.

In this short paper, we will consider the flow of a Bingham fluid in a vertical circular cylinder which is filled with a porous medium. The flow is induced by means of applying a sudden heating to the outer surface, and therefore the paper may be categorised in the same way as the works of Kleppe and Marner (1972) and of Rees and Bassom (2015, 2016). The present paper extends the analyses of Rees and Bassom (2015, 2016) into a cylindrical domain, and therefore the work presented has been made as concise as possible. Therefore, the heating considered here takes two forms: (1) a new temperature and (2) a nonzero heat flux. Using Pascal’s piecewise-linear Darcy–Bingham law, the analysis proceeds analytically and again, a Newton–Raphson scheme has to be used in order to locate both the yield surfaces and, given that the flow domain is finite horizontally, the corresponding change to the initial hydrostatic pressure gradient.

## 2 Governing Equations

*G*is used to denote the threshold pressure gradient above which the fluid is able to flow. Other terms in Eq. (1) are the common ones used for flows in porous media and they are given in the Nomenclature. In the present paper, we shall considering a free convective flow, and therefore buoyancy forces may also to be included in such an equation and we obtain,

The cases which we consider are regarded as being of infinite length in the vertical direction, although practically a long finite cylinder or annulus is highly likely to be essentially equivalent. This means that the thermal boundary layer which arises initially and its subsequent evolution will be unidirectional with the temperature and the vertical velocity being functions solely of the radius and time. In such cases, the equation of continuity is satisfied.

*R*is a chosen radius, and we obtain,

*G*, and, given the presence of

*K*and \(\alpha \), it could also be described as a porous convective Bingham number.

*T*and for the definition of \(\mathrm{Ra}\); these will be introduced in the appropriate place in the text.

## 3 Case 1: Constant Temperature

We consider the development of the temperature field within a vertical porous cylinder the initial temperature of which is \(\theta =0\) and where the temperature of the boundary at \(r=1\) is raised suddenly to \(\theta =1\). The evolution of the temperature field is governed solely by conduction and is unaffected by the induced flow.

The temperature at the origin will also be important in what follows, and therefore Fig. 3 shows this as a function of time. The origin remains at the original temperature until \(t\simeq 0.03\) after which the temperature rises towards 1. By the time \(t=1\) the temperature at the origin is \(\theta =0.9951\). At this point in time, the temperature of the cylinder is almost uniform and therefore there are no buoyancy forces available to drive a flow. That this should be so is evident if the present model problem forms the central portion of a very tall closed cylindrical cavity where the mean flow up the layer be zero. If we consider Eq. (5) in its Newtonian form, i.e. with \(w=\mathrm{Ra}\,\theta -p_z\), then the initial state, \(\theta =w=0\), means that \(p_z=0\). However, once the cylinder has heated up completely to \(\theta =1\), then the velocity field must again be zero, and therefore \(p_z\) has now risen to the value given by \(\mathrm{Ra}\). This simply corresponds to an adjustment in the hydrostatic pressure gradient because the new uniform temperature is different from the reference value. Therefore, the variation of \(p_z\) with time will also need to be computed as part of the solution procedure for *w*; this idea was also used in Rees and Bassom (2015, 2016).

*t*. As with our previous papers Rees and Bassom (2015, 2016), the solutions were obtained using a multi-dimensional Newton–Raphson scheme which utilises numerical differentiation to obtain the iteration matrix.

*t*increases further the magnitude of the downflow and the width of the upflow region both reach a maximum and then decrease once more. The primary reason for this is the heating up of the centre of the cylinder which brings about a decrease in the available buoyancy force. Just before the fluid becomes completely stagnant, the upflow and downflow have both become weak and the regions they occupy have become narrow. At a point in time which depends on the value of \(\mathrm{Rb}/\mathrm{Ra}\) (see below, and Fig. 6) the fluid stops moving.

In Fig. 5, we give a summary of how the yield surfaces vary in time for different values of \(\mathrm{Rb}/\mathrm{Ra}\). For each value of \(\mathrm{Rb}/\mathrm{Ra}\) two curves are presented and the fluid is stagnant in the region between those curves. Our previous comment about the narrowness of the stagnant region and its proximity to \(r=1\) at early times is clearly evident in that Figure. In addition, we also see that the width of the stagnant region increases as \(\mathrm{Rb}/\mathrm{Ra}\) increases; that this should be so is because of the reduced effective buoyancy when \(\mathrm{Rb}\) is large. We also see how, in all cases, the stagnant region eventually expands to fill the cylinder, but stagnation happens earlier for larger values of \(\mathrm{Rb}\).

*t*in terms of \(\mathrm{Rb}/\mathrm{Ra}\) using a single-unknown Newton–Raphson scheme. Figure 6, however, is created easily by finding \(\mathrm{Rb}/\mathrm{Ra}\) as a function

*t*. Given the form of Eqs. (12) and (13), it is clear that it is impossible to have any flow at any time should Open image in new window , and therefore flow cannot be initiated. On the other hand, the behaviour of the curve shown in Fig. 6 as \(\mathrm{Rb}\rightarrow 0\) may be found using Eq. (11). If we assume that \(\mathrm{Rb}/\mathrm{Ra}\) is small and that

*t*is large, then it is sufficient to retain one term in the summation in (11) and therefore, when \(r=0\), Eq. (16) may be manipulated to give,

Finally, Fig. 7 shows that the hydrostatic pressure gradient always increases in time from a value which is identical to \(\mathrm{Rb}\) (i.e. \(p_z/\mathrm{Ra}\) increases from \(\mathrm{Rb}/\mathrm{Ra}\)). It is only in the case of a Newtonian fluid that \(p_z/\mathrm{Ra}\) rises to a unit value.

## 4 Case 2: Constant Heat Flux

*t*asymptotic states, namely

*t*asymptotic solutions cannot be resolved visually once

*t*is as large as 0.4. At this time, the asymptotic solution for the mid-point temperature is in error by roughly 0.001, while that for the circumference is in error by roughly 0.0004. At \(t=0.5\), the respective errors are smaller by a factor of 5.

*t*term in the expression for \(\theta \) in (20), and therefore the second frame in Fig. 13 shows how \(\mathrm{Ra}^{-1}p_z -2t\) varies with time. The beginning point of each curve represents the initiation time for convection. In all cases, this modified hydrostatic pressure gradient adjustment tends to zero as time progresses, suggesting that \(p_z\sim 2\mathrm{Ra}\,t\) for large times. Therefore, it is worth determining if there are any useful mathematical results which may be obtained for large times. A large-time analysis is facilitated by the fact that all of the Bessel function terms in Eqs. (20) and (22) tend exponentially to zero as

*t*increases. It is then quite a short analysis to show that

## 5 Conclusions

In this paper, we have considered where the outer impermeable surface of a porous circular cylinder is subject either to a sudden change in the surface temperature or in the applied heat flux. The porous medium within the cylinder is saturated with a Bingham fluid. In both cases a thin thermal boundary layer is initiated at the outer surface which conducts inwards. When a constant temperature is applied, flow is initiated immediately when \(\mathrm{Rb}/\mathrm{Ra}<{\textstyle \frac{1}{2}}\), but this flow eventually ceases as the fluid at the centre of the cylinder heats up, thereby providing a buoyancy force which is too small to overcome the yield threshold of the Bingham fluid. On the other hand, when the surface is subject to a constant heat flux, there is no flow at early times, again due to have too small a buoyancy force. However, flow eventually initiates if \(\mathrm{Rb}/\mathrm{Ra}<{\textstyle \frac{1}{4}}\), and the flowfield tends towards a steady state. In undertaking this analysis, we have assumed that the flow and temperature fields are independent of *z*, the vertical coordinate, and this is the situation which is likely to pertain when the cylinder is very tall compared with its radius; such a tall but finite height means that the overall flow must satisfy a zero vertical mean value.

The present analysis may now be extended to flows which arise outside a heated cylinder which is embedded within a porous medium, or to cases of vertical annuli where the porous medium is confined between the two surfaces, or even to cases where a volumetric heating is initiated suddenly. We believe that it is extremely unlikely that these flows will undergo a convective instability because the Newtonian counterpart has already been shown to be unconditionally stable in various separate analyses; see Gill (1969), Rees (1988, 2011), Straughan (1988), Lewis et al. (1995) and Scott and Straughan (2013). The effect of the threshold pressure gradient is to reduce the strength of the basic fluid flow, which generally means that flows are less susceptible to unstable disturbances. We note, however, that such channels will admit instability, but only when quite substantial alterations have been made from the configuration considered by Gill (1969). Thus Barletta (2015) found that instability can arise when the impermeable surfaces are replaced by constant pressure surfaces. Shankar and Shivakumara (2017) allowed the porous medium to be saturated by an Oldroyd-B fluid, thereby extending the work of Rees (1988), and found that this situation may also be subject to instabilities. It may be argued that these two respective changes to the Gill’s configuration allow the fluid more freedom to be destabilised, whereas the present configuration represents less freedom.

## Notes

### Acknowledgements

The authors would like to thank the reviewers for their comments which have served to improve the manuscript.

## References

- Barletta, A.: A proof that convection in a porous vertical slab may be unstable. J. Fluid Mech.
**770**, 273–288 (2015)CrossRefGoogle Scholar - Barletta, A., Magyari, E.: Buoyant Couette–Bingham flow between vertical parallel plates. Int. J. Therm. Sci.
**47**, 811–819 (2008)CrossRefGoogle Scholar - Bayazitoglu, Y., Paslay, P.R., Cernocky, P.: Laminar Bingham fluid flow between vertical parallel plates. Int. J. Therm. Sci.
**46**, 349–35 (2007)CrossRefGoogle Scholar - Buckingham, E.: On plastic flow through capillary tubes. Proc. Am. Soc. Test. Mater.
**21**, 1154–1156 (1921)Google Scholar - Gill, A.E.: A proof that convection in a porous vertical slab is stable. J. Fluid Mech.
**35**, 545–547 (1969)CrossRefGoogle Scholar - Kleppe, J., Marner, W.J.: Transient free convection in a Bingham plastic on a vertical flat plate. J. Heat Transf.
**94**(4), 371–376 (1972)CrossRefGoogle Scholar - Lewis, S., Bassom, A.P., Rees, D.A.S.: The stability of vertical thermal boundary layer flow in a porous medium European. J. Mech. B Fluids
**14**, 395–408 (1995)Google Scholar - Nash, S., Rees, D.A.S.: The effect of microstructure on models for the flow of a Bingham fluid in porous media. Transp. Porous Media
**116**, 1073–1092 (2017)CrossRefGoogle Scholar - Pascal, H.: Influence du gradient de seuil sur des essais de remontée de pression et d’écoulement dans les puits. Oil Gas Sci. Technol. (formerly: Revue de l’Institut Francais du Petrole)
**343**, 87–404 (1979)Google Scholar - Pascal, H.: Nonsteady flow through porous media in the presence of a threshold gradient. Acta Mech.
**39**, 207–224 (1981)CrossRefGoogle Scholar - Patel, N., Ingham, D.B.: Analytic solutions for the mixed convection flow of non-Newtonian fluids in parallel plate ducts. Int. Commun. Heat Mass Transf.
**21**(1), 75–84 (1994)CrossRefGoogle Scholar - Rees, D.A.S.: The stability of Prandtl–Darcy convection in a vertical porous slot. Int. J. Heat Mass Transf.
**31**, 1529–1534 (1988)CrossRefGoogle Scholar - Rees, D.A.S.: The effect of local thermal nonequilibrium on the stability of convection in a vertical porous channel. Transp. Porous Media
**87**, 459–464 (2011)CrossRefGoogle Scholar - Rees, D.A.S., Bassom, A.P.: Unsteady thermal boundary layer flows of a Bingham fluid in a porous medium. Int. J. Heat Mass Transf.
**82**, 460–467 (2015)CrossRefGoogle Scholar - Rees, D.A.S., Bassom, A.P.: Unsteady thermal boundary layer flows of a Bingham fluid in a porous medium following a sudden change in surface heat flux. Int. J. Heat Mass Transf.
**93**, 1100–1106 (2016)CrossRefGoogle Scholar - Scott, N.L., Straughan, B.: A nonlinear stability analysis of convection in a porous vertical channel including local thermal nonequilibrium. J. Math. Fluid Mech.
**15**(1), 171–178 (2013)CrossRefGoogle Scholar - Shankar, B.M., Shivakumara, I.S.: Effect of local thermal nonequilibrium on the stability of natural convection in an Oldroyd-B fluid saturated vertical porous layer. J. Heat Transf.
**139**(4), 041001 (2017)CrossRefGoogle Scholar - Straughan, B.: A nonlinear analysis of convection in a porous vertical slab. Geophys. Astrophys. Fluid Dyn.
**42**, 269–275 (1988)CrossRefGoogle Scholar - Yang, W.J., Yeh, H.C.: Free convective flow of Bingham plastic between two vertical plates. J. Heat Transf.
**87**(2), 319–320 (1965)CrossRefGoogle Scholar

## Copyright information

**Open Access**This article is distributed under the terms of the Creative Commons Attribution 4.0 International License (http://creativecommons.org/licenses/by/4.0/), which permits unrestricted use, distribution, and reproduction in any medium, provided you give appropriate credit to the original author(s) and the source, provide a link to the Creative Commons license, and indicate if changes were made.