Flow of non-Newtonian fluids in fixed and fluidised beds

Viscoelastic flow past mono- and bidisperse random arrays of cylinders: flow resistance, topology and normal stress distribution

“…As the flow configuration with solid fraction of 0.6 has a much stronger fluid solid interaction, the extent of flow resistance is also higher. Even though the bulk fluid is essentially shear thinning in nature, such an increase in flow resistance is consistent with literature findings, especially on experiments in packed beds 5 and very recent simulations of Liu et al 42 Recently, Minale 43,44 used a generalized Brinkman equation to simulate second order fluid flow through porous media. Up to this point we used the radius of the cylinders as the relevant length scale.…”

Viscoelastic flow past mono- and bidisperse random arrays of cylinders: flow resistance, topology and normal stress distribution

“…As the flow configuration with solid fraction of 0.6 has a much stronger fluid solid interaction, the extent of flow resistance is also higher. Even though the bulk fluid is essentially shear thinning in nature, such an increase in flow resistance is consistent with literature findings, especially on experiments in packed beds 5 and very recent simulations of Liu et al 42 Recently, Minale 43,44 used a generalized Brinkman equation to simulate second order fluid flow through porous media. Up to this point we used the radius of the cylinders as the relevant length scale.…”

Steady forced convection heat transfer from a heated circular cylinder to power-law fluids

“…At low Reynolds and/or Prandtl number, the local values of the Nusselt number show little variation over the surface from h = 0 to h = p. This is due to the fact that at such low Reynolds numbers, the heat transfer occurs primarily by conduction, with a little convection, irrespective of the type of the thermal boundary condition on the surface of the cylinder and power-law index. This finding is also consistent with heat/mass transfer in power-law fluids from beds of spherical particles [43,[54][55][56] and from tube banks [19,47]. As the Prandtl number and/or Reynolds number is gradually increased, the contribution of convection increases and the Nusselt number is seen to vary over the surface of the cylinder.…”

Non-Newtonian power-law fluid’s thermal characteristics across periodic array of circular cylinders

“…It, therefore,does not matter whether the type of fluid is Newtonian or non-Newtonian[23]. This again is similar with the features found to the mass transfer in non-Newtonian fluids for the spherical particles[31] and a bundle of cylinders[34]. Yet, with a gradual increase in Re, the Nu starts to increase steadily.For instance, at Re = 1, Pr = 10, n = 0.4 and ϕ f = 0.70, the Nu value is 3.1265, while the corresponding values of Nu are 4.6045 and 5.2934 at Re = 10 and 40, respectively.…”

Viscoelastic flow past mono- and bidisperse random arrays of cylinders: flow resistance, topology and normal stress distribution

“…As the flow configuration with solid fraction of 0.6 has a much stronger fluid solid interaction, the extent of flow resistance is also higher. Even though the bulk fluid is essentially shear thinning in nature, such an increase in flow resistance is consistent with literature findings, especially on experiments in packed beds 5 and very recent simulations of Liu et al 42 Recently, Minale 43,44 used a generalized Brinkman equation to simulate second order fluid flow through porous media. Up to this point we used the radius of the cylinders as the relevant length scale.…”

Steady forced convection heat transfer from a heated circular cylinder to power-law fluids

“…At low Reynolds and/or Prandtl number, the local values of the Nusselt number show little variation over the surface from h = 0 to h = p. This is due to the fact that at such low Reynolds numbers, the heat transfer occurs primarily by conduction, with a little convection, irrespective of the type of the thermal boundary condition on the surface of the cylinder and power-law index. This finding is also consistent with heat/mass transfer in power-law fluids from beds of spherical particles [43,[54][55][56] and from tube banks [19,47]. As the Prandtl number and/or Reynolds number is gradually increased, the contribution of convection increases and the Nusselt number is seen to vary over the surface of the cylinder.…”

Non-Newtonian power-law fluid’s thermal characteristics across periodic array of circular cylinders

“…It, therefore,does not matter whether the type of fluid is Newtonian or non-Newtonian[23]. This again is similar with the features found to the mass transfer in non-Newtonian fluids for the spherical particles[31] and a bundle of cylinders[34]. Yet, with a gradual increase in Re, the Nu starts to increase steadily.For instance, at Re = 1, Pr = 10, n = 0.4 and ϕ f = 0.70, the Nu value is 3.1265, while the corresponding values of Nu are 4.6045 and 5.2934 at Re = 10 and 40, respectively.…”

Viscoelastic flow past mono- and bidisperse random arrays of cylinders: flow resistance, topology and normal stress distribution

“…As the flow configuration with solid fraction of 0.6 has a much stronger fluid solid interaction, the extent of flow resistance is also higher. Even though the bulk fluid is essentially shear thinning in nature, such an increase in flow resistance is consistent with literature findings, especially on experiments in packed beds 5 and very recent simulations of Liu et al 42 Recently, Minale 43,44 used a generalized Brinkman equation to simulate second order fluid flow through porous media. Up to this point we used the radius of the cylinders as the relevant length scale.…”

Steady forced convection heat transfer from a heated circular cylinder to power-law fluids

“…At low Reynolds and/or Prandtl number, the local values of the Nusselt number show little variation over the surface from h = 0 to h = p. This is due to the fact that at such low Reynolds numbers, the heat transfer occurs primarily by conduction, with a little convection, irrespective of the type of the thermal boundary condition on the surface of the cylinder and power-law index. This finding is also consistent with heat/mass transfer in power-law fluids from beds of spherical particles [43,[54][55][56] and from tube banks [19,47]. As the Prandtl number and/or Reynolds number is gradually increased, the contribution of convection increases and the Nusselt number is seen to vary over the surface of the cylinder.…”

Non-Newtonian power-law fluid’s thermal characteristics across periodic array of circular cylinders

“…It, therefore,does not matter whether the type of fluid is Newtonian or non-Newtonian[23]. This again is similar with the features found to the mass transfer in non-Newtonian fluids for the spherical particles[31] and a bundle of cylinders[34]. Yet, with a gradual increase in Re, the Nu starts to increase steadily.For instance, at Re = 1, Pr = 10, n = 0.4 and ϕ f = 0.70, the Nu value is 3.1265, while the corresponding values of Nu are 4.6045 and 5.2934 at Re = 10 and 40, respectively.…”