By Ismail Tosun
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Additional info for Modelling in Transport Phenomena
This can be calculated by integrating the total energy flux at the wall over the surface area. 2-1) where qyly=o is the molecular (or, conductive) energy flux at the wall. As a result of the no-slip boundary condition at the wall, the fluid in contact with the plate is stagnant and heat is transferred by pure conduction through the fluid layer immediately adjacent to the plate. Therefore, Eq. 2-3) Evaluation of the integral in Eq. 2-3) requires the determination of the temperature gradient at the wall.
It depends on the fluid flow mechanism, fluid properties (density, viscosity, thermal conductivity, heat capacity) and flow geometry. Substitution of Eq. 2-4) into Eq. 2. 2-7) where AH is the heat transfer area and (AT)oh is the characteristic temperature difference. 1 P h y s i c a l i n t e r p r e t a t i o n of h e a t t r a n s f e r coefficient According to Fourier's law of heat conduction, Eq. 2-8) Combination of Eqs. 2-9) y--0 The convection heat transfer coefficient can be determined from Eq.
2-4) The term #/p in Eq. 2-2) is called momentum diffusivity or kinematic viscosity, and the term k/pCp in Eq. 2-3) is called thermal diffusivity. Momentum and thermal diffusivities are designated by u and a, respectively. Note that the terms u, a, and DAS all have the same units, m2/s, and Eqs. 2-5) The quantities that appear in Eqs. 1. Since the terms u, a, and ~DABall have the same units, the ratio of any two of these diffusivities results in a dimensionless number. 2-6) The Prandtl number is a function of temperature and pressure.
Modelling in Transport Phenomena by Ismail Tosun