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For flow over a flat plate of length \(L\), the local heat transfer coefficient \(h_{x}\) is known to vary as \(x^{-1 / 2}\), where \(x\) is the distance from the leading edge of the plate. What is the ratio of the average Nusselt number for the entire plate \(\left(\overline{N u}_{L}\right)\) to the local Nusselt number at \(x=L\left(N u_{L}\right)\) ?

Short Answer

Expert verified
The ratio of the average Nusselt number for the entire plate \(\overline{Nu}_L\) to the local Nusselt number at \(x=L\) (\(Nu_L\)) is \(\frac{2}{3} L\).

Step by step solution

01

Write the equation for the local heat transfer coefficient

According to the given information, we know that the local heat transfer coefficient \(h_x\) varies with the distance from the leading edge of the plate, as: \[h_x = cx^{-1/2}\] Where \(c\) is a constant.
02

Write the expressions of local Nusselt numbers

The relation between the local heat transfer coefficient and local Nusselt number at a position \(x\) along the plate can be expressed as: \[Nu_x = \frac{h_xx}{k}\] By substituting the expression for \(h_x\), we can rewrite the expression as: \[Nu_x = \frac{c}{k} \cdot x^{1/2}\] At \(x=L\), the local Nusselt number (\(Nu_L\)) can be expressed as: \[Nu_L = \frac{c}{k} \cdot L^{1/2}\]
03

Find the average Nusselt number \(\overline{Nu}_L\)

It is given that the local heat transfer coefficient varies along the length of the plate. Therefore, to find the average Nusselt number over the entire plate, we need to calculate the average of the local Nusselt number along the plate: \[\overline{Nu}_L = \frac{1}{L} \int_{0}^L Nu_x dx\] Substitute the expression for \(Nu_x\) into the integration: \[\overline{Nu}_L = \frac{1}{L} \int_{0}^L \frac{c}{k} \cdot x^{1/2} dx\]
04

Perform the integration

Let's perform the integration in the expression for \(\overline{Nu}_L\): \[\overline{Nu}_L = \frac{1}{L} \cdot \frac{c}{k} \int_{0}^L x^{1/2} dx\] \[\overline{Nu}_L = \frac{c}{Lk} \left[\frac{2}{3} x^{3/2} \right]_0^L\] \[\overline{Nu}_L = \frac{2c}{3Lk} \cdot L^{3/2}\]
05

Calculate the ratio between \(\overline{Nu}_L\) and \(Nu_L\)

Now that we have both expressions, let's find the ratio between the average Nusselt number \(\overline{Nu}_L\) and the local Nusselt number at \(x = L\) (\(Nu_L\)): \[\frac{\overline{Nu}_L}{Nu_L} = \frac{\frac{2c}{3Lk} \cdot L^{3/2}}{\frac{c}{k} \cdot L^{1/2}}\] Simplify the ratio expression: \[\frac{\overline{Nu}_L}{Nu_L} = \frac{2c}{3Lk} \cdot L \cdot \frac{k}{c}\] The constant terms \(c\) and \(k\) cancel out: \[\frac{\overline{Nu}_L}{Nu_L} = \frac{2}{3} L\] The ratio of the average Nusselt number for the entire plate \(\overline{Nu}_L\) to the local Nusselt number at \(x=L\) (\(Nu_L\)) is \(\frac{2}{3} L\).

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Key Concepts

These are the key concepts you need to understand to accurately answer the question.

heat transfer coefficient
The heat transfer coefficient, denoted by \( h \), is a measure of the heat transfer rate through a fluid for each unit area of a surface. It provides insight into the thermal interaction between a solid surface and adjacent fluid.
When dealing with a flat plate, this coefficient allows us to evaluate the heat dissipation from the plate into the fluid. In the problem scenario, the local heat transfer coefficient \( h_x \) varies as \( x^{-1/2} \), showcasing how the heat transfer efficiency diminishes as we move along the plate from the leading edge \( x = 0 \).
Understanding the dependence of the heat transfer coefficient on distance helps in designing efficient thermal systems, such as cooling fins or heat exchangers. This information is crucial for predicting temperature distributions and ensuring effective thermal management.
flat plate
A flat plate in fluid dynamics typically serves as a model for understanding simplified flow patterns and heat transfer behaviors. Such models are used extensively in engineering to analyze convection heat transfer over surfaces.
This concept is crucial because it provides a reference scenario where the boundary layer develops along the plate. The boundary layer is a thin region near the plate where fluid velocity changes from zero (due to the no-slip condition at the plate surface) up to the free stream velocity.
By studying heat transfer over a flat plate, engineers can evaluate and design various practical applications like aerofoils in aircraft, or even flat solar collectors. A flat plate model makes it computationally easier to calculate different parameters, which can be applied to scale up to more complex shapes in real-world scenarios.
integration in heat transfer
The integration step is pivotal when calculating average values over a surface, such as determining the average Nusselt number. This process involves integrating the local heat transfer characteristics to account for variations along the length of the flat plate.
In this exercise, integration is used to average the local Nusselt numbers, which are initially calculated using a differential model, reflecting how the heat transfer varies as the fluid moves over the plate.
Mathematically, this involves the integration of the local Nusselt number expression \( Nu_x = \frac{c}{k} \cdot x^{1/2} \) over the interval from \( 0 \) to \( L \), representing the entire length of the plate. The integration effectively smoothens out variations and provides a single representative value for the heat transfer efficiency for the whole plate, allowing us to make comparisons or optimization decisions inherently valuable in design and analysis.
fluid dynamics over surfaces
Fluid dynamics over surfaces such as a flat plate is essential for understanding how fluids behave when interacting with solid boundaries. Key phenomena to consider include boundary layer formation, laminar to turbulent transitions, and velocity profiles.
Depending on conditions, the characteristics of fluid flow, like velocity and pressure distribution, change significantly over the surface which, in turn, affect the heat transfer rates.
By analyzing fluid dynamics, engineers can predict how efficiently heat is transferred from solid surfaces to the fluid flow, which is critical for designing industrial processes, chemical reactors, and environmental systems. As shown in this problem, knowing how the heat transfer coefficient varies over the length of the plate allows for optimizing designs, ensuring better thermal management performance, and avoiding thermal stresses.

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Most popular questions from this chapter

Consider cross flow of gas \(\mathrm{X}\) over an object having a characteristic length of \(L=0.1 \mathrm{~m}\). For a Reynolds number of \(1 \times 10^{4}\), the average heat transfer coefficient is \(25 \mathrm{~W} / \mathrm{m}^{2} \cdot \mathrm{K}\). The same object is then impregnated with liquid \(Y\) and subjected to the same flow conditions. Given the following thermophysical properties, what is the average convection mass transfer coefficient?

Experiments have shown that the transition from laminar to turbulent conditions for flow normal to the axis of a long cylinder occurs at a critical Reynolds number of \(R e_{D,} \approx 2 \times 10^{5}\), where \(D\) is the cylinder diameter. Moreover, the transition from incompressible to compressible flow occurs at a critical Mach number of \(M a_{e}=0.3\). For air at a pressure of \(p=1 \mathrm{~atm}\) and temperature \(T=27^{\circ} \mathrm{C}\), determine the critical cylinder diameter \(D_{c}\) below which, if the flow is turbulent, compressibility effects are likely to be important.

An expression for the actual water vapor partial pressure in terms of wet-bulb and dry-bulb temperatures, referred to as the Carrier equation, is given as $$ p_{v}=p_{g w}-\frac{\left(p-p_{g w}\right)\left(T_{d b}-T_{\mathrm{wb}}\right)}{1810-T_{\mathrm{wb}}} $$ where \(p_{v}, p_{g w}\) and \(p\) are the actual partial pressure, the saturation pressure at the wet-bulb temperature, and the total pressure (all in bars), while \(T_{\mathrm{db}}\) and \(T_{\mathrm{wb}}\) are the dry- and wet-bulb temperatures in kelvins. Consider air at \(1 \mathrm{~atm}\) and \(37.8^{\circ} \mathrm{C}\) flowing over a wet-bulb thermometer that indicates \(21.1^{\circ} \mathrm{C}\). (a) Using Carrier's equation, calculate the partial pressure of the water vapor in the free stream. What is the relative humidity? (b) Refer to a psychrometric chart and obtain the relative humidity directly for the conditions indicated. Compare the result with part (a). (c) Use Equation \(6.65\) to determine the relative humidity. Compare the result to parts (a) and (b).

A disk of 20-mm diameter is covered with a water film. Under steady-state conditions, a heater power of \(200 \mathrm{~mW}\) is required to maintain the disk-water film at \(305 \mathrm{~K}\) in dry air at \(295 \mathrm{~K}\) and the observed evaporation rate is \(2.55 \times 10^{-4} \mathrm{~kg} / \mathrm{h}\). (a) Calculate the average mass transfer convection coefficient \(\bar{h}_{s}\) for the evaporation process. (b) Calculate the average heat transfer convection coefficient \(\bar{h}\). (c) Do the values of \(\bar{h}_{\mathrm{m}}\) and \(\bar{h}\) satisfy the heat- mass analogy? (d) If the relative humidity of the ambient air at \(295 \mathrm{~K}\) were increased from 0 (dry) to \(0.50\), but the power supplied to the heater was maintained at \(200 \mathrm{~mW}\), would the evaporation rate increase or decrease? Would the disk temperature increase or decrease?

An object of irregular shape has a characteristic length of \(L=1 \mathrm{~m}\) and is maintained at a uniform surface temperature of \(T_{s}=325 \mathrm{~K}\). It is suspended in an airstream that is at atmospheric pressure \((p=1 \mathrm{~atm})\) and has a velocity of \(V=100 \mathrm{~m} / \mathrm{s}\) and a temperature of \(T_{x}=275 \mathrm{~K}\). The average heat flux from the surface to the air is \(12,000 \mathrm{~W} / \mathrm{m}^{2}\). Referring to the foregoing situation as case 1 , consider the following cases and determine whether conditions are analogous to those of case 1. Each case involves an object of the same shape, which is suspended in an airstream in the same manner. Where analogous behavior does exist, determine the corresponding value of the average convection coefficient. (a) The values of \(T_{s}, T_{x}\), and \(p\) remain the same, but \(L=2 \mathrm{~m}\) and \(V=50 \mathrm{~m} / \mathrm{s}\). (b) The values of \(T_{x}\) and \(T_{\infty}\) remain the same, but \(L=2 \mathrm{~m}, V=50 \mathrm{~m} / \mathrm{s}\), and \(p=0.2 \mathrm{~atm}\). (c) The surface is coated with a liquid film that evaporates into the air. The entire system is at \(300 \mathrm{~K}\), and the diffusion coefficient for the air-vapor mixture is \(D_{\mathrm{AB}}=1.12 \times 10^{-4} \mathrm{~m}^{2} / \mathrm{s}\). Also, \(L=2 \mathrm{~m}\), \(V=50 \mathrm{~m} / \mathrm{s}\), and \(p=1 \mathrm{~atm}\). (d) The surface is coated with another liquid film for which \(D_{\mathrm{AB}}=1.12 \times 10^{-4} \mathrm{~m}^{2} / \mathrm{s}\), and the system is at \(300 \mathrm{~K}\). In this case \(L=2 \mathrm{~m}, V=250 \mathrm{~m} / \mathrm{s}\), and \(p=0.2\) atm.

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