Boundary conditions heat conduction

Discussion This example demonstrates how steady one-dimensional heat conduction problems in composite media can be solved. We could also solve this problem by determining the heat flux at the interface by dividing the total heat generated in the wire by the surface area of the wire, and then using this value as the specifed heat flux boundary condition for both the wire and the ceramic tayer. This way the two problems are decoupled and can be solved separately. 

We wish here to summarize results for the constant-volume heat capacity, Cy, of the RPM. We have performed NVT and pVT MC simulations on systems confined to cubic cells of side L. The long-range Coulombic interactions were handled using Ewald sums with conducting boundary conditions [39], Cy was computed using the appropriate fluctuation formula [40],... 

In this work, heat and fluid flow in some common micro geometries is analyzed analytically. At first, forced convection is examined for three different geometries microtube, microchannel between two parallel plates and microannulus between two concentric cylinders. Constant wall heat flux boundary condition is assumed. Then mixed convection in a vertical parallel-plate microchannel with symmetric wall heat fluxes is investigated. Steady and laminar internal flow of a Newtonian is analyzed. Steady, laminar flow having constant properties (i.e. the thermal conductivity and the thermal diffusivity of the fluid are considered to be independent of temperature) is considered. The axial heat conduction in the fluid and in the wall is assumed to be negligible. In this study, the usual continuum approach is coupled with the two main characteristics of the microscale phenomena, the velocity slip and the temperature jump. 

In this lecture, the effects of the abovementioned dimensionless parameters, namely, Knudsen, Peclet, and Brinkman numbers representing rarefaction, axial conduction, and viscous dissipation, respectively, will be analyzed on forced convection heat transfer in microchannel gaseous slip flow under constant wall temperature and constant wall heat flux boundary conditions. Nusselt number will be used as the dimensionless convection heat transfer coefficient. A majority of the results will be presented as the variation of Nusselt number along the channel for various Kn, Pe, and Br values. The lecture is divided into three major sections for convective heat transfer in microscale slip flow. First, the principal results for microtubes will be presented. Then, the effect of roughness on the microchannel wall on heat transfer will be explained. Finally, the variation of the thermophysical properties of the fluid will be considered. 

J. H. lienhard, An Improved Approach to Conductive Boundary Conditions for the Rayleigh-Benard Instability, J. Heat Transfer (109) 378-387,1987. 

Conductive boundary condition, denoted by . This boundary condition refers to the axial uniform wall heat flux and finite heat condition along the wall circumference. The same applications can be found as those for the boundary condition except for the existence of heat conduction in the circumferential direction. 

C. N. Sokmen and M. M. Razzaque, Finite Element Analysis of Conduction-Radiation Heat Transfer in an Absorbing-Emitting and Scattering Medium Contained in an Enclosure with Heat Flux Boundary Conditions, ASME HTD-vol. 81, pp. 17-23,1987. 

If a constant heat flux boundary condition is required, an electrical heating element, often a thin, metallic foil, can be stretched over an insulated wall. The uniform heat flux is obtained by Joule heating. If the wall is well insulated, then, under steady-state conditions, all of the energy input to the foil goes to the fluid flowing over the wall. Thermocouples attached to the wall beneath the heater can be used to measure local surface temperature. From the energy dissipation per unit time and area, the local surface temperature, and the fluid temperature, the convective heat transfer coefficient can be determined. Corrections to the total heat flow (e.g., due to radiation heat transfer or wall conduction) may have to be made. 

To solve the nonlinear control equation (1) under the condition (2) approximately using FEM, we need to establish relevant functional. The paper adopts one-dimensional nonlinear FEM to solve the above-mentioned one-dimensional heat conduction problem. Under the condition of assumptions in this paper, the element functional [8] (5.14) of one-dimensional steady heat conduction problem under the convective heat transfer boundary condition is... 

We now consider bar element, and the element length is f. Two nodes are denoted by i,j. The trial function of temperature field is linear distribution. Under the convective heat transfer boundary condition, the finite element basic equation of steady heat conduction in the three-layered composite plate is [8]... 

Equilibrium of a gaseous and a liquid phase in contact (permeable, deformable, and heat-conducting boundary) entails the conditions... 

At low Re and when conjugate effects have to be considered, the temperature distribution along the microchannel is not linear. Under constant heat flux boundary conditions, Nu decreases with decreasing ratio of outer to inner channel diameter, approaching the constant temperature solution. A decrease in Nu is also seen with increasing wall conductivity. For constant temperature boundary conditions, Nu will increase approaching the constant heat flux solution with axial heat conduction in the wall. The values for local Nusselt number for the conjugated problem lie between the values for the two boundary conditions constant heat flux and constant temperature. 

Combined heat transfer boundary condition. In combined mode heat transfer, the heat conducted from the interior point of the medium to the surface must be equal to that dissipated by convection and radiation... 

We note the presence of the reactor scale in the heat transfer boundary condition (3.42b). The formulation in terms of the average solid temperature (7 ) is an approximation, which should be reasonable given that these terms are likely to be subdominant in Equation 3.42b. As in Table 3.2, it is possible to identify the timescales for the different processes in Equations 3.41 and 3.42. The axial conduction term in (3.42b) can be ignored for beds with Rh L. Combination of these scales yields some well-known parameters for the internal reaction-diffusion problem, such as... 

When q is zero, Eq. (5-18) reduces to the famihar Laplace equation. The analytical solution of Eq. (10-18) as well as of Laplaces equation is possible for only a few boundary conditions and geometric shapes. Carslaw and Jaeger Conduction of Heat in Solids, Clarendon Press, Oxford, 1959) have presented a large number of analytical solutions of differential equations apphcable to heat-conduction problems. Generally, graphical or numerical finite-difference methods are most frequently used. Other numerical and relaxation methods may be found in the general references in the Introduction. The methods may also be extended to three-dimensional problems. 

Under steady-state conditions, the temperature distribution in the wall is only spatial and not time dependent. This is the case, e.g., if the boundary conditions on both sides of the wall are kept constant over a longer time period. The time to achieve such a steady-state condition is dependent on the thickness, conductivity, and specific heat of the material. If this time is much shorter than the change in time of the boundary conditions on the wall surface, then this is termed a quasi-steady-state condition. On the contrary, if this time is longer, the temperature distribution and the heat fluxes in the wall are not constant in time, and therefore the dynamic heat transfer must be analyzed (Fig. 11.32). 

In general, the axial heat conduction in the channel wall, for conventional size channels, can be neglected because the wall is usually very thin compared to the diameter. Shah and London (1978) found that the Nusselt number for developed laminar flow in a circular tube fell between 4.36 and 3.66, corresponding to values for constant heat flux and constant temperature boundary conditions, respectively. 

One particular characteristic of conduction heat transfer in micro-channel heat sinks is the strong three-dimensional character of the phenomenon. The smaller the hydraulic diameter, the more important the coupling between wall and bulk fluid temperatures, because the heat transfer coefficient becomes high. Even though the thermal wall boundary conditions at the inlet and outlet of the solid wall are adiabatic, for small Reynolds numbers the heat flux can become strongly non-uniform most of the flux is transferred to the fluid at the entrance of the micro-channel. Maranzana et al. (2004) analyzed this type of problem and proposed the model of channel flow heat transfer between parallel plates. The geometry shown in Fig. 4.15 corresponds to a flow between parallel plates, the uniform heat flux is imposed on the upper face of block 1 the lower face of block 0 and the side faces of both blocks... 

A variety of studies can be found in the literature for the solution of the convection heat transfer problem in micro-channels. Some of the analytical methods are very powerful, computationally very fast, and provide highly accurate results. Usually, their application is shown only for those channels and thermal boundary conditions for which solutions already exist, such as circular tube and parallel plates for constant heat flux or constant temperature thermal boundary conditions. The majority of experimental investigations are carried out under other thermal boundary conditions (e.g., experiments in rectangular and trapezoidal channels were conducted with heating only the bottom and/or the top of the channel). These experiments should be compared to solutions obtained for a given channel geometry at the same thermal boundary conditions. Results obtained in devices that are built up from a number of parallel micro-channels should account for heat flux and temperature distribution not only due to heat conduction in the streamwise direction but also conduction across the experimental set-up, and new computational models should be elaborated to compare the measurements with theory. 

The first approach developed by Hsu (1962) is widely used to determine ONE in conventional size channels and in micro-channels (Sato and Matsumura 1964 Davis and Anderson 1966 Celata et al. 1997 Qu and Mudawar 2002 Ghiaasiaan and Chedester 2002 Li and Cheng 2004 Liu et al. 2005). These models consider the behavior of a single bubble by solving the one-dimensional heat conduction equation with constant wall temperature as a boundary condition. The temperature distribution inside the surrounding liquid is the same as in the undisturbed near-wall flow, and the temperature of the embryo tip corresponds to the saturation temperature in the bubble 7s,b- The vapor temperature in the bubble can be determined from the Young-Laplace equation and the Clausius-Clapeyron equation (assuming a spherical bubble) ... 

The heat transfer model, energy and material balance equations plus boundary condition and initial conditions are shown in Figure 4. The energy balance partial differential equation (PDE) (Equation 10) assumes two dimensional axial conduction. Figure 5 illustrates the rectangular cross-section of the composite part. Convective boundary conditions are implemented at the interface between the walls and the polymer matrix. 

The boundary conditions for engineering problems usually include some surfaces on which values of the problem unknowns are specified, for instance points of known temperature or initial species concentration. Some other surfaces may have constraints on the gradients of these variables, as on convective thermal boundaries where the rate of heat transport by convection away from the surface must match the rate of conductive transport to the surface from within the body. Such a temperature constraint might be written ... 

Figure 3. Finite element simulation of plane Couette flow with thermal dissipation and conductive heat transfer. (f) — fixed temperature condition (c) — convective boundary condition.

A concentrated heat capacity. We now consider the boundary-value problem for the heat conduction equation with some unusual condition placing the concentrated heat capacity Co on the boundary, say at a single point X = 0. The traditional way of covering this is to impose at the point a = 0 an unusual boundary condition such as... 

Bunimovich et al. (1995) lumped the melt and solid phases of the catalyst but still distinguished between this lumped solid phase and the gas. Accumulation of mass and heat in the gas were neglected as were dispersion and conduction in the catalyst bed. This results in the model given in Table V with the radial heat transfer, conduction, and gas phase heat accumulation terms removed. The boundary conditions are different and become identical to those given in Table IX, expanded to provide for inversion of the melt concentrations when the flow direction switches. A dimensionless form of the model is given in Table XI. Parameters used in the model will be found in Bunimovich s paper. 

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