Conjugate heat transfer in thermally developing laminar flow with viscous dissipation effects

In this study, thermally developing laminar forced convection in a pipe including viscous dissipation and wall conductance is investigated numerically. The constant heat flux is assumed to be imposed at the outer surface of the pipe wall. The finite volume method is used. The distributions for the developing temperature and local Nusselt number in the entrance region are obtained. The dependence of the results on the Brinkman number and the dimensionless thermal conductivity are shown. The viscous heating effect on the wall is shown. Significant viscous dissipation effects have been observed for large Br.     

Forced convection heat transfer of Giesekus viscoelastic fluid in pipes and channels

A theoretical solution is presented for the convective heat transfer of Giesekus viscoelastic fluid in pipes and channels, under fully developed thermal and hydrodynamic flow conditions, for an imposed constant heat flux at the wall. The fluid properties are taken as constant and axial conduction is negligible. The effect of Weissenberg number (We), mobility parameter (α) and Brinkman number (Br) on the temperature profile and Nusselt number are investigated. The results emphasize the significant effect of viscous dissipation and fluid elasticity on the Nusselt number in all circumstances. For wall cooling and the Brinkman number exceeds a critical value (Br ₁), the heat generated by viscous dissipation overcomes the heat removed at the wall and fluid heats up longitudinally. Fluid elasticity shifts this critical Brinkman number to higher values.     

Slip-flow heat transfer in a microchannel with viscous dissipation

Forced convection flow in a microchannel with constant wall temperature is studied, including viscous dissipation effect. The slip-flow regime is considered by incorporating both the velocity-slip and the temperature-jump conditions at the surface. The energy equation is solved for the developing temperature field using finite integral transform. To increase β_v Kn is to increase the slip velocity at the wall surface, and hence to decrease the friction factor. Effects of the parameters β_v Kn, β, and Br on the heat transfer results are illustrated and discussed in detail. For a fixed Br, the Nusselt number may be either higher or lower than those of the continuum regime, depending on the competition between the effects of β_v Kn and β. At a given β_v Kn the variation of local Nusselt number becomes more even when β becomes larger, accompanied by a shorter thermal entrance length. The fully developed Nusselt number decreases with increasing β irrelevant to β_v Kn. The increase in Nusselt number due to viscous heating is found to be more pronounced at small β_v Kn.     

The effects of viscous dissipation on heat transfer to power law fluids in arbitrary cross-sectional ducts

In this paper, the analytical study of forced convection heat transfer to power-law fluids in arbitrary cross-sectional ducts with finite viscous dissipation is undertaken. Both the flow and heat transfer develop simultaneously from the entrance of the duct the walls of which are maintained at a constant temperature different from the entering fluid temperature. The governing conservation equations written in curvilinear coordinates are solved using the Line-Successive-Over relaxation (LSOR) method. Numerical results of dimensionless heat transfer coefficients and temperature profiles are presented for the trapezoidal, triangular, circular and square ducts. For cooling, viscous dissipation generally augments heat transfer. At low values of Brinkman number (Br0.1), the cooling effect dominates over viscous heating in the entrance region. AsBr is increased, the location where viscous dissipation becomes important shifts closer to the entrance until a value is reached for which the effect of viscous dissipation is always predominant irrespective of the axial location. When the walls are heated, for a non-zero Brinkman number, theNu _X* distribution exhibits a singularity from the negative side of theNu _X* axis. As the power-law index increases, the position of this singularity shifts closer to the entrance of the duct. Far downstream of the duct, for a fixedn, Nu _X* attains an asymptotic value which is independent ofBr and is at least thrice that for forced convection without viscous dissipation.Es wird die analytische Studie des Wärmeübergangs (freie Konvektion, begrenzte viskose Dissipation) bei mit Potenzansatz beschriebenen Fluiden in Rohrleitungen mit verschiedenen Querschnitten durchgeführt. Die Strömung und der Wärmeübergang entwickeln sich gleichzeitig ab dem Eingang der Leitungen. Die Wände der Rohrleitungen werden auf konstanter Temperatur gehalten, welche ungleich der Temperatur der einströmenden Flüssigkeiten ist. Die in Gaußschen Koordinaten geschriebenen Erhaltungsgleichungen werden mit der LSOR-(Line-Successive-Over-Relaxation-) Methode gelöst. Die numerischen Ergebnisse der dimensionslosen Wärmeübergangskoeffizienten und der Temperaturprofile werden für trapezförmige, dreieckige und runde Querschnitte vorgelegt. Beim Kühlen erhöht die viskose Dissipation in der Regel den Wärmeübergang. Bei kleinen Brinkman-Zahlen (Br0,1) dominieren die Kühlungseffekte über das viskose Aufheizen im Einlaufbereich. Wenn die Br-Zahlen erhöht werden, verschiebt sich die Gegend, in der die viskosen Effekte überwiegen, in Richtung Einlauf solange, bis eine Br-Zahl erreicht wird, bei der die Dissipation, unabhängig von der axialen Entfernung, immer dominant ist.Wenn die Wände bei Br-Zahlen ungleich Null beheizt werden, weist dieNu _X*-Verteilung eine Singularität auf der negativen Seite derNu _X*-Achse auf. Wenn der Index des Potenzansatzes steigt, nähert sich die Singularität dem Einlauf der Rohrleitung. Weit strömungsabwärts, für ein festesn, nimmtNu _X*, unabhängig von der Br-Zahl, asymptotische Werte an. Diese Werte erreichen das Dreifache derjenigen für erzwungene Konvektion ohne viskose Dissipation.     

Non-Darcian Forced Convection Flow of Viscous Dissipating Fluid over a Flat Plate Embedded in a Porous Medium

In this study, laminar boundary layer flow over a flat plate embedded in a fluid-saturated porous medium in the presence of viscous dissipation, inertia effect and suction/injection is analyzed using the Keller box finite difference method. The flat plate is assumed to be held at constant temperature. The non-Darcian effects of convection, boundary and inertia are considered. Results for the local heat transfer parameter and the local skin friction parameter as well as the velocity and temperature profiles are presented for various values of the governing parameters. The non-Darcian effects are shown to decrease the velocity and to increase the temperature. It is also shown that the local heat transfer parameter and the local skin friction parameter increase due to suction of fluid while injection reverses this trend. It is disclosed that the effect of the viscous dissipation for negative values of Ec (T _w < T _∞) is to enhance the heat transfer coefficient while the opposite is true for positive values of Ec (T _w > T _∞). The results are compared with those available in the existing literature and an excellent agreement is obtained.     

The developing heat transfer and fluid flow in micro-channel heat sink with viscous heating effect

The numerical modeling of the conjugate heat transfer and fluid flow through the micro-heat sink was presented in the paper, considering the viscous dissipation effect. Three different fluids with temperature dependent fluid viscosity are considered: water, dielectric fluid HFE-7600 and isopropanol. The square shape of the cross-section is considered with D _h  = 50 μm with a channel length L = 50 mm. As most of the reported researches dealt with fully developed fluid flow and constant fluid properties in this paper the thermal and hydro-dynamic developing laminar fluid flow is analyzed. Two different heat transfer conditions are considered: heating and cooling at various Br. The influence of the viscous heating on local Nu and Po is analyzed. It was shown that for a given geometry the local Po and Nu numbers are strongly affected by the viscous heating. Moreover the Po number attains the fully developed value as the external heating is equal with the internal viscous heating.     

Heat transfer in the flow of a viscoelastic fluid over a stretching surface

An analysis is made of heat transfer in the boundary layer of a viscoelastic fluid flowing over a stretching surface. The velocity of the surface varies linearly with the distance x from a fixed point and the surface is held at a uniform temperature T _w higher than the temperature T _∞ of the ambient fluid. An exact analytical solution for the temperature distribution is found by solving the energy equation after taking into account strain energy stored in the fluid (due to its elastic property) and viscous dissipation. It is shown that the temperature profiles are nonsimilar in marked contrast with the case when these profiles are found to be similar in the absence of viscous dissipation and strain energy. It is also found that temperature at a point increases due to the combined influence of these two effects in comparison with its corresponding value in the absence of these two effects. A novel result of this analysis is that for small values of x, heat flows from the surface to the fluid while for moderate and large values of x, heat flows from the fluid to the surface even when T _w >T _∞. Temperature distribution and the surface heat flux are determined for various values of the Prandtl number P, the elastic parameter K ₁ and the viscous dissipation parameter a. Numerical solutions are also obtained through a fourth-order accurate compact finite difference scheme. Received on 14 October 1997     

On the laminar forced convection with axial conduction in a circular tube with exponential wall heat flux

The values of the fully developed Nusselt number for laminar forced convection in a circular tube with axial conduction in the fluid and exponential wall heat flux are determined analytically. Moreover, the distinction between the concepts of bulk temperature and mixing-cup temperature, at low values of the Peclet number, is pointed out. Finally it is shown that, if the Nusselt number is defined with respect to the mixing-cup temperature, then the boundary condition of exponentially varying wall heat flux includes as particular cases the boundary conditions of uniform wall temperature and of convection with an external fluid.

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Über laminare Zwangskonvektion mit Längswärmeleitung in einem Kreisrohr mit exponentiell veränderlichem Wandwärmefluß

Zusammenfassung Es werden die Endwerte der Nusselt-Zahlen für vollausgebildete laminare Zwangskonvektion in einem Kreisrohr mit Längswärmeleitung und exponentiell veränderlichem Wandwärmefluß analytisch ermittelt. Besondere Betonung liegt auf dem Unterschied zwischen den Konzepten für die Mittel- und die Mischtemperatur bei niedrigen Peclet-Zahlen. Schließlich wird gezeigt, daß bei Definition der Nusselt-Zahl bezüglich der Mischtemperatur die Randbedingung exponentiell veränderlichen Randwärmeflusses die Spezialfälle konstanter Wandtemperatur und konvektiven Wärmeaustausches mit einem umgebenden Fluid einschließt.

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Nomenclature A _n dimensionless coefficients employed in the Appendix - Bi Biot numberBi=h _e r ₀/ - c _n dimensionless coefficients defined in Eq. (17) - c _p specific heat at constant pressure of the fluid within the tube, [J kg^–1 K^–1] - f solution of Eq. (15) - h ₁,h ₂ specific enthalpies employed in Eqs. (2) and (4), [J kg^–1] - h _e convection coefficient with a fluid outside the tube, [W m^–2 K^–1] - rate of mass flow, [kg s^–1] - Nu bulk Nusselt number,2r ₀ q _w /[(T _w –T _b )] - Nu _H fully developed value of the bulk Nusselt number for the boundary condition of uniform wall heat flux - Nu _T fully developed value of the bulk Nusselt number for the boundary condition of uniform wall temperature - Nu ^* mixing Nusselt number,2r ₀ q _w /[(T _w –T _m )] - Nu _C ^* fully developed value of the mixing Nusselt number for the boundary condition of convection with an external fluid - Nu _H ^* fully developed value of the mixing Nusselt number for the boundary condition of uniform wall heat flux - Nu _T ^* fully developed value of the mixing Nusselt number for the boundary condition of uniform wall temperature - Pe Peclet number, 2r ₀/ - q ₀ wall heat flux atx=0, [W m^–2] - q _w wall heat flux, [W m^–2] - r radial coordinate, [m] - r ₀ radius of the tube, [m] - s dimensionless radius,s=r/r ₀ - T temperature, [K] - T ₀ temperature constant employed in Eq. (14), [K] - T reference temperature of the fluid external to the tube, [K] - T _b bulk temperature, [K] - T _m mixing or mixing-cup temperature, [K] - T _w wall temperature, [K] - u velocity component in the axial direction, [m s^–1] - mean value ofu, [m s^–1] - x axial coordinate, [m] Greek symbols thermal diffusivity of the fluid within the tube, [m² s^–1] - exponent in wall heat flux variation, [m^–1] - dimensionless parameter - dimensionless temperature =(T _w –T)/(T _w –T _b ) - ^* dimensionless temperature ^*=(T _w –T)/(T _w –T _m ) - thermal conductivity of the fluid within the tube, [W m^–1 K^–1] - density of the fluid within the tube, [kg m^–3]     

Transient heat transfer in the laminar thermal entry region of a pipe: an analytical solution

Attention is directed toward the problem of unsteady convective heat transfer to a fluid flowing inside a pipe in a laminar, fully developed fashion when suddenly, an ambient fluid outside the pipe undergoes a step change in temperature. For the fastest portion of the resultant transient, time domain I, an analytical solution of the governing partial differential thermal energy equation is effected via the Laplace transformation. From this solution, response functions are found for the pipe wall temperature, surface heat flux, and fluid bulk mean temperature as a function of non-dimensional time for a range of values of a parameter which characterizes the heat transfer between the ambient and the pipe.Comparison of results is made with a recent finite difference solution in the literature and with the standard quasi-steady type of analysis. It is found that the analytical solution presented herein extends and complements the finite difference solution and that the quasi-steady solution can be severely in error in this part of the transient.Nomenclature â c _p R/_wc_pwb Ratio of thermal energy storage capacity of fluid to wall material - b pipe wall thickness - C _n defined by equation (24) - c _p , c _pw specific heat capacity of fluid and pipe wall, respectively - D _n functions defined by equation (23) - erf, erfc error function and complimentary error function, respectively - F t/R ² Fourier number - g 1–2S - h local surface coefficient of heat transfer between inside of pipe wall and inside flowing fluid - i ⁿ erfc n ^th repeated integral of the error function - k thermal conductivity of the inside fluid - N h(2R)/k Nusselt number - p Laplace transform parameter - q _w local, instantaneous surface heat flux at inside of pipe wall - Q _w 2Rq _w /k(T _L –T _i ) nondimensional surface heat flux - R pipe inside radius - S UR/k - t time - T local instantaneous fluid temperature - T _B , T _L , T _i bulk mean, ambient, and initial, as well as inlet, temperature, respectively - u, u _m local and mass average, fluid velocity, respectively - U overall heat transmission coefficient between ambient fluid outside of pipe and inside pipe wall - X, Y x/R, y/R nondimensional space coordinates along, and radially inward from, the pipe wall, respectively - k/c _p thermal diffusivity of inside fluid - , _w mass density of inside fluid and wall, respectively - (T(x, y, t)–T _i )/(T _L –T _i ) - _w , _B wall, bulk mean value of , respectively     

Viscous dissipation effect on heat transfer characteristics of rectangular microchannels under slip flow regime and H1 boundary conditions

Viscous dissipation effect on heat transfer characteristics of a rectangular microchannel is studied. Flow is governed by the Navier–Stokes equations with the slip flow and temperature jump boundary conditions. Integral transform technique is applied to derive the temperature distribution and Nusselt number. The velocity distribution is taken from literature. The solution method is verified for the case where viscous dissipation is neglected. It is found that, the viscous dissipation is negligible for gas flows in microchannels, since the contribution of this effect on Nu number is about 1%. However, this effect should be taken into account for much more viscous flows, such as liquid flows. Neglecting this effect for a flat microchannel with an aspect ratio of 0.1 for Br=0.04 underestimates the Nu number about 5%.     

Combined effect of viscous dissipation and thermal radiation on fluid flows over a non-linearly stretched permeable wall

An analysis is presented for the steady non-linear viscous flow of an incompressible viscous fluid over a horizontal surface of variable temperature with a power-law velocity under the influences of suction/blowing, viscous dissipation and thermal radiation. Numerical results are illustrated by means of tables and graphs. The governing partial differential equations are converted into nonlinear ordinary differential equations by a similarity transformation. The effects of the stretching parameter n, suction/blowing parameter b, Prandtl number σ, Eckert number E_c(E_c ^* )E_{c}(E_{c}^{ *} ) and radiation parameter N _R are discussed. Two cases are studied, namely, (i) Prescribed surface temperature (PST case) and, (ii) Prescribed heat flux at the sheet (PHF case).     

Analysis of viscous dissipation effect on thermal entrance heat transfer in laminar pipe flows with convective boundary conditions

Consideration is given to the influence of viscous dissipation on the thermal entrance region laminar pipe flow heat transfer with convective boundary condition. The Eigenfunction series expansion technique is employed to solve the governing energy equation. The results for axial distributions of dimensionless bulk and wall temperatures, local Nusselt number as well as modified local Nusselt number are presented graphically forNu ₀ =0.1, 2, and 100. The complicated variations of conventional local Nusselt number is due to the inappropriate definition of conventional heat transfer coefficient in this problem. A modified local heat transfer coefficient, based on the difference of bulk fluid temperature and wall temperature, is introduced. Its value can clearly indicate the extent and the direction of heat exchange between the fluid in the pipe and the ambient. The effects of outside Nusselt number are also investigated. Significant viscous dissipation effects have been observed for large Br.     

Predictions on momentum,heat and mass transfer in turbulent channel flow with the aid of a boundary layer growth-breakdown model

This paper deals with theoretical aspects of momentum, heat and mass transfer in turbulent channel flow and in particular with phenomena occurring close to the wall. The analysis presented involves the use of a boundary-layer growth-breakdown model. Theoretical expressions have been derived predicting heat and mass transfer at smooth surfaces in the fully developed and entrance region and at surfaces provided with ideal two-dimensional roughness elements. The analysis is restricted to fluids having Prandtl and Schmidt numbers larger than one. Good agreement appears to exist between theoretical predictions and experimental observations.

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Zusammenfassung Diese Arbeit behandelt die Theorie der Übertragungsvorgänge von Impuls, Wärme und Stoff in turbulenter Kanalströmung unter besonderer Berücksichtigung der Vorgänge in Wandnähe. Das verwendete Modell beruht auf dem Zusammenbruch der anwachsenden Grenzschicht. Für die ausgebildete Strömung und für den Einlaufbereich bei glatter Wand und bei Oberflächen mit idealen zweidimensionalen Rauhigkeitselementen werden theoretische Ausdrücke abgeleitet bei Beschränkung auf Prandtl- und Schmidt-Zahlen über Eins. Zwischen den theoretischen Voraussagen und den Versuchsergebnissen scheint gute Übereinstimmung zu herrschen.

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Nomenclature a thermal diffusivity [m²/s] - c concentration [kg/m³] - c _p specific heat [J/kg °C] - D molecular diffusivity [m²/s] - G relative increase in friction factor due to surface roughening - d pipe diameter [m] - e height (depth) of roughness element [m] - e ^p+ dimensionless roughness height (depth) - F parameter denoting the ratio - f friction factor for smooth surface and isothermal conditions - f _h friction factor for heating conditions - f _r friction factor for artificially roughened surface - n _av average frequency of fluctuations at the wall [s^–1] - q heat flux [W/m₂] - q _w heat flux at the wall [W/m²] - q _wr heat flux at roughened wall [W/m²] - q _wx wall heat flux to growing laminar boundary layer at positionx [W/m²] - R _ma longitudinal correlation coefficient for mass transfer - R _mo longitudinal correlation coefficient for momentum transfer - T temperature [°C] - T _b bulk temperature of fluid [°C] - T ₀ fluid temperature at edge of viscous boundary layer (edge of viscous region) [°C] - T _w wall temperature [°C] - T _wx wall temperature at positionx for growing laminar boundary layer [°C] - t time [s] - t ₀ characteristic time period associated with boundary layer growth [s] - u local axial fluid velocity, at wall distancey, for turbulent flow also denoting the mean velocity at that distance [m/s] - u _b bulk fluid velocity [m/s] - u ₀ fluid velocity at edge of viscous boundary layer (edge of viscous region) [m/s] - u _0r fluid velocity at edge of viscous region for the case of an artificially roughened wall [m/s] - u axial fluid velocity fluctuation [m/s] - u ⁺ dimengionless fluid velocity,u/(_w/)^1/2 - u _i ⁺ instantaneous value ofu ⁺ - u _min ⁺ minimum value ofu _i ⁺ - u _r ⁺ root mean square value of dimensionless axial velocity - u ₀ ⁺ value ofu ⁺ at edge of viscous region - v fluid velocity normal to flow direction and normal to wall [m/s] - v fluctuation of the velocityv [m/s] - x coordinate in flow direction [m] - x axial distance interval [m] - x ⁺ dimensionless distance interval - x ₀ viscous boundary layer growth length [m] - x ₀ ⁺ dimensionless boundary growth length - x _r axial dixtance between roughness elements [m] - x _r ⁺ dimensionless distance between roughness elements - x _h value of viscous boundary growth length for heating conditions [m] - y distance from wall [m] - y ⁺ dimensionless wall distance - y _v thickness of viscous region [m] - y _v ⁺ dimensionless form ofy _v - z _u unheated (zero mass transfer) part of elementary viscous boundary layer in entrance region [m] - z _h heated (mass transfer) part of elementary viscous boundary layer [m] - z _v lateral extent of elementary viscous boundary layer [m] Greek symbols heat transfer coefficient defined with respect to bulk fluid temperature [W/m² °C] - ₀ viscous region heat transfer coefficient [W/m² °C] - _0h viscous boundary layer heat transfer coefficient averaged over lengthx ₀ for conditions of heating [W/m² °C] - _0hh viscous region heat transfer coefficient averaged over lengthx _h for conditions of heating [W/m² °C] - entrance region heat transfer coefficient at position [W/m² °C - _,t viscous boundary layer heat transfer coefficient at position and timet [W/m² °C] - mass transfer coefficient [m/s] - _av average value of mass transfer coefficient [m/s] - _x mass transfer coefficient for viscous boundary layer at positionx [m/s] - entrance region mass transfer coefficient at position [m/s] - thickness of laminar (viscous) boundary layer evaluated atu=1/2u ₀ [m] - _max maximum value of boundary layer thickness [m] - _i turbulent diffusivity for momentum transfer [m²/s] - _h turbulent diffusivity for heat transfer [m²/s] - _m turbulent diffusivity for mass transfer [m²/s] - turbulent intensity - thermal conductivity [W/m °C] - kinematic viscosity [m²/s] - ₀ value ofv at edge of viscous region [m²/s] - _w value ofv at the wall [m²/s] - density [kg/m³] - shear stress [N/m²] - _tx local value of wall shear stress associated with viscous boundary layer growth [N/m²] - ₀ value of wall shear stress averaged over lengthx ₀ [N/m²] - _0r value of ₀ for the case of an artificially roughened wall [N/m²] - _0h value of ₀ for heating conditions [N/m²] - _h value of wall shear stress for heating conditions, averaged over lengthx _h [N/m²] - _w wall shear stress for conditions of turbulent flow [N/m²] - _wh value of _w for heating conditions [N/m²] - dimensionless axial distancex/x ₀ in extrance region Dimensionless numbers Nu Nusselt number (d/) - Nu _x Entrance region Nusselt number at axial positionx - Nu _h Nusselt number for heating conditions - Nu _r Nusselt number for the case of artificially roughened surface - Pr Prandtl number (v/a) - Re Reynolds number (d u _b/v) - Re _b Boundary layer Reynolds number (1/2 u ₀/v) - Re _ber Critical value ofRe _b - Sh Sherwood number (d/D) - Sh _x entrance region Sherwood number at axial positionx - Sc Schmidt number (v/D)     

Investigations on viscous dissipation effect of liquid flow in microtubes

The experimental and numerical investigations are carried out to explore the viscous dissipation effect during de-ionized ultra pure water flowing through smooth quartz glass microtubes with inner diameters of 25 and 50 m, and the Reynolds number varies in the range from 0 to 680. The viscous dissipation characteristic in microtubes is numerically calculated by a 2-D model and the Electrical Double Layer (EDL) effect on the flow is considered. A new criterion V _c demonstrating the law of the viscous dissipation effect in microtubes is summed up with the numerical simulation results. By applying the micro-area thermal-imaging technology and a series of correction tests, the viscous heating temperature increment in the microtube can be exactly measured by an IR camera with a special magnifying lens. Furthermore, the temperature increment of the working fluid due to the heat generated by the pump is also considered in the experimental investigation. The comparisons among the experimental results, the numerical predictions and the new theoretical correlations are made in the present research, which indicates the experimental data are in rough accordance with the numerical and the theoretical results.     

The effect of a nonlinear temperature dependent Prandtl-number on heat transfer of fully developed flow of liquids in a straight tube

If Nu_o is the Nusselt Number for a temperature-independent Prandtl number Pr, and Nu the Nusselt number for a temperature dependent Prandtl number, it is usual to define the correction factor Nu/Nu_o=C. A correction factor which has been defined in this form has, up to now, only been expressed as a function of two characteristic Pr numbers. Thus it was simply assumed that the Pr number was a linear function of the temperature. Fluids with very large Pr numbers show a (T;Pr) relationship which deviates considerably from a linear one. This leads to a very large difference (up to 70%) between the calculated and the measured values of the Nusselt number. In the following study we shall determine a so-called curvature parameter of the (T;Pr) curve and obtain a semi-empirical formula for C. This formula has a deviation from the actual relationship many times smaller than that of the formulae for a linear (T;Pr) relationship.

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Zusammenfassung Ist Nu_o die Nusseltzahl bei temperaturunabhangiger und Nu die Nusseltzahl bei temperaturabhangiger Prandtlzahl Pr, so ist es üblich, mit Nu/Nu_o=C den Korrekturfaktor zu bezeichnen. Ein in dieser Form definierter Faktor C ist bisher als Funktion nur zweier charakteristischer Pr-Zahlen ausgedrückt worden. Es wurde somit nur eine lineare Abhängigkeit von der Pr-Zahl von der Temperatur T vorausgesetzt. Flüssigkeiten mit großen Pr-Zahlen weisen eine (T;Pr)-Charakteristik auf, die sehr stark von der linearen abweicht. Sehr große Abweichungen (bis — 70%) der gerechneten von den gemessenen Nu-Zahlen sind eine Folge davon. In vorliegender Arbeit bilden wir mit einer dritten charakteristischen Pr-Zahl einen sogenannten Krümmungsparameter der Kurve (T;Pr) und leiten eine semiempirische Formel für C ab, die um ein großes Vielfaches kleinere Fehler aufweist, als die Formeln für den linearen (T;Pr)-Verlauf.

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Nomenclature

Material constants c_p specific heat at constant pressure [J/kgK] - k heat conductivity [W/mK] - density [kg/m³] - a temperature diffusivity, a=k/c_p [m²/s] - dynamic viscosity [Ns/m²] - kinematic viscosity [m²/s] Fluid dynamics D inner diameter of the tube [m] - L length of tube [m] - w mean speed of fluid [m/s] Heat transfer h coefficient of heat transfer [W/m²K] - T absolute temperature [K] - T_b bulk temperature (corresponding to the adiabatic mixing temperature) [K] - T_w tube wall temperature [K] - T_f=(T_b+T_w)/2 film temperature [K] - T=T_b-T_w temperature forcing difference of heat transfer [K] Characteristic quantities without dimensions Re=wD/ Reynolds number - Pr=/a Prandtl number - Nu=hD/k Nusselt number - related temperature - related Prandtl number - curvature parameter of the Prandtl number Various - C=Nu_b/Nu_o correction factor according to Eq.(5) - p exponent in Eq.(6), (a), (8) and (16) Indices o corresponding to the quasi-isothermal heat transfer - b,w,f with reference to quantities, including physical properties which correspond to the temperatures T_b, T_wor T_f - Pr,k,, for quantities calculated corresponding to the Prandtl number, the thermal conductivity coefficient, the density or the dynamic viscosity - H,C for heating or cooling exp for quantities calculated from experimental data     

The laminar hole pressure for Newtonian fluids

For flows with wall turbulence the hole pressure, P _H , was shown empirically by Franklin and Wallace (J Fluid Mech, 42, 33–48, 1970) to depend solely on R ₊, the Reynolds number constructed from the friction velocity and the hole diameter b. Here this dependence is extended to the laminar regime by numerical simulation of a Newtonian fluid flowing in a plane channel (gap H) with a deep tap hole on one wall. Calculated hole pressures are in good agreement with experimental values, and for two hole sizes are well represented by: (P _H −P _HS )/τ _w = √(k ² + c ² R ₊²)−k, where the Stokes hole pressure P _HS /τ _w = s (b/H)³, k, c, s are fitted constants, and τ _w is the wall shear stress.     

Heat transfer characteristics of boundary-layer flows induced by continuous surfaces stretched with prescribed skin friction

A continuous surface stretched with velocity u _w=u _w (x) and having the temperature distribution T _w=T _w (x) interacts with the viscous fluid in which it is immersed both mechanically and thermally. The thermal interaction is characterized by the surface heat flux q _w=q _w (x) and the mechanical one by the skin friction τ _w=τ _w (x). In the whole previous theoretical research concerned with such processes, either (u _w and T _w) or (u _w and q _w) have been prescribed as known boundary conditions. The goal of the present paper is to initiate the investigation of the boundary layer flows induced by stretching processes for which either (τ _w and T _w ) or (τ _w and q _w) are the prescribed quantities. The case of an isothermal surface stretched with constant skin friction, (τ _w=const., T _w=const. ≠ T _∞) is worked out in detail. The corresponding flow and heat transfer characteristics are compared to those obtained for the (well known) case of a uniformly moving isothermal surface (u _w=const., T _w=const. ≠ T _∞).     

Mixed convection cooling of a heated, continuously stretching surface

 An numerical study of the flow and heat transfer characteristics associated with a heated, continuously stretching surface being cooled by a mixed convection flow has been carried out. The relevant heat transfer mechanisms are of interest in a wide variety of practical applications, such as hot rolling, continuous casting, extrusion, and drawing. The surface velocity of the continuously stretching sheet was assumed to vary according to a power-law form, that is, u _w (x)=Cx ^p . Two conditions of surface heating were considered, a variable wall temperature (VWT) in the form T _w (x)−T _∞=Ax ⁿ and a variable surface heat flux (VHF) in the form q _w (x)=Bx ^m . The governing differential equations are transformed by introducing proper nonsimilarity variables and solved numerically using a procedure based on finite difference approximations. Results for the local Nusselt number and the local friction coefficient are obtained for a wide range of governing parameters, such as the surface velocity parameter p, the wall temperature exponent n, the surface heat flux exponent m, the buoyancy force parameters (ξ for the VWT case and χ for the VHF case), and Prandtl number of the fluid. It is found that the local Nusselt number is increased with increasing the velocity exponent parameter p for the VWT case, while the opposite trend is observed for the VHF case. The local friction coefficient is increased for a decelerated stretching surface, while it is decreased for an accelerated stretching surface. Also, appreciable effects of the buoyancy force on the local Nusselt number and the local friction coefficient are observed for both VWT and VHF cases, as expected. Received on 11 January 1999     

Dependence of the critical heat flux over a cylinder in a cross flow on the thermal resistances of tube wall and heating medium

This investigation has been carried out to determine experimentally the influence of the thermal resistances of the tube wall and the heating medium (inside flow) on the critical heat flux over a cylinder of large diameter placed horizontally in a cross flow. The cross flow was normal to earth gravity. The parameters varied were the tube material, tube thickness, flow rate of heating medium, undisturbed cross velocity of the coolant and coolant subcooling. The experimental results are discussed and a qualitative explanation for the experimental findings is given.

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Abhängigkeit der kritischen Wärmestromdichte an einem quer angeströmten Zylinder von dem thermischen Widerstand der Rohrwand und des heizenden Mediums

Zusammenfassung Diese Untersuchung wurde durchgeführt um experimentell den Einfluß des thermischen Widerstandes der Rohrwand und des heizenden Mediums (innen) auf die kritische Wärmestromdichte über einen horizontalen Zylinder großen Durchmessers, der quer angeströmt wird, zu bestimmen. Die Anströmrichtung wurde senkrecht zur Erdgravitation gewählt. Die variierten Parameter waren das Rohrmaterial, die Rohrdicke, der Durchsatz des heizenden Mediums, die ungestörte Anströmgeschwindigkeit und Unterkühlung des Kühlmittels. Die experimentellen Ergebnisse wurden diskutiert und eine qualitative Erklärung für die experimentellen Befunde wurde gegeben.

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Abbrevations

Nomenklature d outside diameter of test cylinder - g acceleration due to gravity - k thermal conductivity of material of test cylinder - q_crit critical heat flux over the test cylinder - R_h thermal resistance of the heating mediumR _h=1/_h - t wall thickness of test cylinder - T _h bulk temperature of heating medium - T _s saturation temperature of coolant - T _w wall temperature - T _sub coolant subcooling - w _h mean velocity of heating medium - w undisturbed coolant velocity - w _.crit critical undisturbed coolant velocity (velocity at which the critical heat flux is a minimum, [6]) Greek symbols _h heat transfer coefficient of the heating medium (inside flow) - _nb nucleate boiling heat transfer coefficient     

Unsteady free convection on a vertical cylinder with variable heat and mass flux

The unsteady natural convection boundary layer flow over a semi-infinite vertical cylinder is considered with combined buoyancy force effects, for the situation in which the surface temperature T ^′ _w(x) and C ^′ _w(x) are subjected to the power-law surface heat and mass flux as K(T ^′/r) = −ax ⁿ and D(C ^′/r) = −bx ^m . The governing equations are solved by an implicit finite difference scheme of Crank-Nicolson method. Numerical results are obtained for different values of Prandtl number, Schmidt number ‘n’ and ‘m’. The velocity, temperature and concentration profiles, local and average skin-friction, Nusselt and Sherwood numbers are shown graphically. The local Nusselt and Sherwood number of the present study are compared with the available result and a good agreement is found to exist. Received on 7 July 1998