Herschel–Bulkley fluid

The Herschel–Bulkley fluid is a generalized model of a non-Newtonian fluid, in which the strain experienced by the fluid is related to the stress in a complicated, non-linear way. Three parameters characterize this relationship: the consistency k, the flow index n, and the yield shear stress $\tau_0$ . The consistency is a simple constant of proportionality, while the flow index measures the degree to which the fluid is shear-thinning or shear-thickening. Ordinary paint is one example of a shear-thinning fluid, while oobleck provides one realization of a shear-thickening fluid. Finally, the yield stress quantifies the amount of stress that the fluid may experience before it yields and begins to flow.

This non-Newtonian fluid model was introduced by Herschel and Bulkley in 1926.^[1] ^[2]

1 Definition
2 Channel flow
3 Pipe flow
4 References
5 External links

Definition

The viscous stress tensor is given, in the usual way, as a viscosity, multiplied by the rate-of-strain tensor:

$\tau_{ij}=2\mu E_{ij}=\mu\left(\frac{\partial u_i}{\partial x_j}%2B\frac{\partial u_j}{\partial x_i}\right),$

where in contrast to the Newtonian fluid, the viscosity is itself a function of the strain tensor. This is constituted through the formula ^[3]

$\mu=\begin{cases}\mu_0,&\Pi\leq\Pi_0\\k\Pi^{n-1}%2B\tau_0\Pi^{-1},&\Pi\geq\Pi_0\end{cases},$

where $\Pi$ is the second invariant of the rate-of-strain tensor:

$\Pi=\sqrt{2E_{ij}E^{ij}}$ .

If n=1 and $\tau_0=0$ , this model reduces to the Newtonian fluid. If $n<1$ the fluid is shear-thinning, while $n>1$ produces a shear-thickening fluid. The limiting viscosity $\mu_0$ is chosen such that $\mu_0=k\Pi_0^{n-1}%2B\tau_0\Pi_0^{-1}$ . A large limiting viscosity means that the fluid will only flow in response to a large applied force. This feature captures the Bingham-type behaviour of the fluid.

This equation is also commonly written as

$\tau = \tau_{0} %2B K \gamma ^ {n}$

where $\tau$ is the shear stress, $\gamma$ the shear rate, $\tau_{0}$ the yield stress, and K and n are regarded as model factors.

Channel flow

A frequently-encountered situation in experiments is pressure-driven channel flow ^[4] (see diagram). This situation exhibits an equilibrium in which there is flow only in the horizontal direction (along the pressure-gradient direction), and the pressure gradient and viscous effects are in balance. Then, the Navier-Stokes equations, together with the rheological model, reduce to a single equation:

$\frac{\partial p}{\partial x}=\frac{\partial}{\partial z}\left(\mu\frac{\partial u}{\partial z}\right)\,\,\, =\begin{cases}\mu_0\frac{\partial^2 u}{\partial{z}^2},&\left|\frac{\partial u}{\partial z}\right|<\gamma_0\\ \\\frac{\partial}{\partial z}\left[\left(k\left|\frac{\partial u}{\partial z}\right|^{n-1}%2B\tau_0\left|\frac{\partial u}{\partial z}\right|^{-1}\right)\frac{\partial u}{\partial z}\right],&\left|\frac{\partial u}{\partial z}\right|\geq\gamma_0\end{cases}$

To solve this equation it is necessary to non-dimensionalize the quantities involved. The channel depth H is chosen as a length scale, the mean velocity V is taken as a velocity scale, and the pressure scale is taken to be $P_0=k\left(V/H\right)^n$ . This analysis introduces the non-dimensional pressure gradient

$\pi_0=\frac{H}{P_0}\frac{\partial p}{\partial x},$

which is negative for flow from left to right, and the Bingham number:

$Bn=\frac{\tau_0}{k}\left(\frac{H}{V}\right)^n.$

Next, the domain of the solution is broken up into three parts, valid for a negative pressure gradient:

A region close to the bottom wall where $\partial u/\partial z>\gamma_0$ ;
A region in the fluid core where $|\partial u/\partial z|<\gamma_0$ ;
A region close to the top wall where $\partial u/\partial z<-\gamma_0$ ,

Solving this equation gives the velocity profile:

$u\left(z\right)=\begin{cases} \frac{n}{n%2B1}\frac{1}{\pi_0}\left[\left(\pi_0\left(z-z_1\right)%2B\gamma_0^n\right)^{1%2B\left(1/n\right)}-\left(-\pi_0z_1%2B\gamma_0^n\right)^{1%2B\left(1/n\right)}\right],&z\in\left[0,z_1\right]\\ \frac{\pi_0}{2\mu_0}\left(z^2-z\right)%2Bk,&z\in\left[z_1,z_2\right],\\ \frac{n}{n%2B1}\frac{1}{\pi_0}\left[\left(-\pi_0\left(z-z_2\right)%2B\gamma_0^n\right)^{1%2B\left(1/n\right)}-\left(-\pi_0\left(1-z_2\right)%2B\gamma_0^n\right)^{1%2B\left(1/n\right)}\right],&z\in\left[z_2,1\right]\\ \end{cases}$

Here k is a matching constant such that $u\left(z_1\right)$ is continuous. The profile respects the no-slip conditions at the channel boundaries,

$u(0)=u(1)=0,$

Using the same continuity arguments, it is shown that $z_{1,2}=\tfrac{1}{2}\pm\delta$ , where

$\delta=\frac{\gamma_0\mu_0}{|\pi_0|}\leq \tfrac{1}{2}.$

Since $\mu_0=\gamma_0^{n-1}%2BBn/\gamma_0$ , for a given $\left(\gamma_0,Bn\right)$ pair, there is a critical pressure gradient

$|\pi_{0,\mathrm{c}}|=2\left(\gamma_0%2BBn\right).$

Apply any pressure gradient smaller in magnitude than this critical value, and the fluid will not flow; its Bingham nature is thus apparent. Any pressure gradient greater in magnitude than this critical value will result in flow. The flow associated with a shear-thickening fluid is retarded relative to that associated with a shear-thinning fluid.

Pipe flow

For laminar flow Chilton and Stainsby ^[5] provide the following equation to calculate the pressure drop. The equation requires an iterative solution to extract the pressure drop, as it is present on both sides of the equation.

$\frac {\Delta P} {L} = \frac {4 K} {D} \left( \frac {8 V} {D} \right) ^ n \left( \frac {3 n %2B 1} {4 n} \right) ^ n \frac {1} {1 - X} \left( \frac {1} {1 - a X - b X^2 - cX^3} \right) ^ n$

$X = \frac {4 L \tau_ y} {D \Delta P}$

$a = \frac {1} {2 n %2B 1}$

$b = \frac {2 n} { \left( n %2B 1 \right) \left( 2 n %2B 1 \right) }$

$c = \frac {2 n ^ 2} { \left( n %2B 1 \right) \left( 2 n %2B 1 \right) }$

For turbulent flow the authors propose a method that requires knowledge of the wall shear stress, but do not provide a method to calculate the wall shear stress. Their procedure is expanded in Hathoot ^[6]

$R = \frac {4 n \rho V D \left( 1 - a X - b X^2 - cX^3 \right)} {\mu_{Wall} \left(3 n %2B 1 \right) }$

$\mu_{Wall} = \tau_{Wall}^{1 - 1/n} \left( \frac {K} {1 - X} \right) ^ {1/n}$

$\tau_{Wall} = \frac {D \Delta P} {4 L}$

All units are SI

$\Delta P$ Pressure drop, Pa.

$L$ Pipe length, m

$D$ Pipe diameter, m

$V$ Fluid velocity, $m/s$

Chilton and Stainsby state that defining the Reynolds number as

$Re = \frac {R} {n ^ 2 \left( 1 - X \right) ^ 4}$

allows standard Newtonian friction factor correlations to be used.

References

^ Herschel, W.H.; Bulkley, R. (1926), "Konsistenzmessungen von Gummi-Benzollösungen", Kolloid Zeitschrift 39: 291–300, doi:10.1007/BF01432034
^ Tang, Hansong S.; Kalyon, Dilhan M. (2004), "Estimation of the parameters of Herschel–Bulkley fluid under wall slip using a combination of capillary and squeeze flow viscometers", Rheologica Acta 43 (1): 80–88, doi:10.1007/s00397-003-0322-y
^ K. C. Sahu, P. Valluri, P. D. M. Spelt, and O. K. Matar (2007) 'Linear instability of pressure-driven channel flow of a Newtonian and a Herschel–Bulkley fluid' Phys. Fluids 19, 122101
^ D. J. Acheson 'Elementary Fluid Mechanics' (1990), Oxford, p. 51
^ Chilton, RA and R Stainsby, 1998, "Pressure loss equations for laminar and turbulent non-Newtonian pipe flow", Journal of Hydraulic Engineering 124(5) pp. 522 ff.
^ Hathoot, HM, 2004, "Minimum-cost design of pipelines transporting non-Newtonian fluids", Alexandrian Engineering Journal, 43(3) 375 - 382

External links

Description of Herschel–Bulkley fluid; graphical comparison between rheological models