Heat Transfer in FullyDeveloped Internal Turbulent Flow
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  Heat transfer in fullydeveloped turbulent flow in a circular tube subject to constant heat flux (<math>{{{q}''}_{w}}=</math> const) will be considered in this  +  Heat transfer in fullydeveloped turbulent flow in a circular tube subject to constant heat flux (<math>{{{q}''}_{w}}=</math> const) will be considered in this article <ref name="ON1999">Oosthuizen, P.H., and Naylor, D., 1999, Introduction to Convective Heat Transfer Analysis, WCB/McGrawHill, New York.</ref><ref>Faghri, A., Zhang, Y., and Howell, J. R., 2010, Advanced Heat and Mass Transfer, Global Digital Press, Columbia, MO.</ref>. When the turbulent flow in the tube is fully developed, we have <math>\bar{v}=0</math> and the energy equation becomes 
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{{EquationRef(2)}}  {{EquationRef(2)}}  
}  }  
  where <math>{{\bar{T}}_{c}}</math> is the timeaveraged temperature at the centerline of the tube, and  +  where <math>{{\bar{T}}_{c}}</math> is the timeaveraged temperature at the centerline of the tube, and ''T<sub>w</sub>'' is the wall temperature. Thus, <math>({{T}_{w}}\bar{T})/({{T}_{w}}{{\bar{T}}_{c}})</math> is a function of ''r'' only, i.e., 
  <math>({{T}_{w}}\bar{T})/({{T}_{w}}{{\bar{T}}_{c}})</math>  +  
  +  
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{{EquationRef(3)}}  {{EquationRef(3)}}  
}  }  
  where f is independent from x. Differentiating  +  where ''f'' is independent from ''x''. Differentiating eq. (2) yields 
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{{EquationRef(5)}}  {{EquationRef(5)}}  
}  }  
  Substituting eq. (  +  Substituting eq. (3) into eq. (5), one obtains: 
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{{EquationRef(6)}}  {{EquationRef(6)}}  
}  }  
  Since the heat flux is constant, <math>{{{q}''}_{w}}=</math> const, it follows that  +  Since the heat flux is constant, <math>{{{q}''}_{w}}=</math> const, it follows that <math>({{T}_{w}}{{\bar{T}}_{c}})= Const</math>, i.e., 
  <math>({{T}_{w}}{{\bar{T}}_{c}})=</math>  +  
  +  
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{{EquationRef(7)}}  {{EquationRef(7)}}  
}  }  
  Therefore, eq. (  +  Therefore, eq. (4) becomes: 
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{{EquationRef(10)}}  {{EquationRef(10)}}  
}  }  
  Since <math>{{{q}''}_{w}}=</math> const, it follows from eq. (  +  Since <math>{{{q}''}_{w}}=</math> const, it follows from eq. (9) that <math>({{T}_{w}}{{\bar{T}}_{m}})= Const</math>, i.e., 
  <math>({{T}_{w}}{{\bar{T}}_{m}})=</math>  +  
  +  
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{{EquationRef(11)}}  {{EquationRef(11)}}  
}  }  
  Combining eqs. (  +  Combining eqs. (7), (8) and (11), the following relationships are obtained: 
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{{EquationRef(12)}}  {{EquationRef(12)}}  
}  }  
  The timeaveraged mean temperature,  +  The timeaveraged mean temperature, <math>{{\bar{T}}_{m}}</math>, changes with ''x'' as the result of heat transfer from the tube wall. The rate of mean temperature change can be obtained as follows: 
  <math>{{\bar{T}}_{m}}</math>  +  
  , changes with x as the result of heat transfer from the tube wall.  +  
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{{EquationRef(13)}}  {{EquationRef(13)}}  
}  }  
  Substituting eq. (  +  Substituting eq. (12) into eq. (1), the energy equation becomes: 
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{{EquationRef(14)}}  {{EquationRef(14)}}  
}  }  
  where <math>y={{r}_{0}}r</math> is the distance measured from the tube wall. Equation (  +  where <math>y={{r}_{0}}r</math> is the distance measured from the tube wall. Equation (14) is subject to the following two boundary conditions: 
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{{EquationRef(16)}}  {{EquationRef(16)}}  
}  }  
  Integrating eq. (  +  Integrating eq. (14) in the interval of (''r<sub>0</sub>'', ''r'') and considering eq. (15), we have: 
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{{EquationRef(19)}}  {{EquationRef(19)}}  
}  }  
  Integrating eq. (  +  Integrating eq. (18) in the interval of (0, ''y'') and considering eq. (16), one obtains: 
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{{EquationRef(20)}}  {{EquationRef(20)}}  
}  }  
  If the profiles of axial velocity and the thermal eddy diffusivity are known, eq. (  +  If the profiles of axial velocity and the thermal eddy diffusivity are known, eq. (20) can be used to obtain the correlation for internal forced convection heat transfer. With the exception of the very thin viscous sublayer, the velocity profile in the most part of the tube is fairly flat. Therefore, it is assumed that the timeaveraged velocity, <math>\bar{u}</math>, in eq. (19) can be replaced by <math>{{\bar{u}}_{m}}</math>, and ''I''(''y'') becomes: 
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{{EquationRef(21)}}  {{EquationRef(21)}}  
}  }  
  Substituting eqs. (  +  Substituting eqs. (21) and (13) into eq. (20) yields: 
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{{EquationRef(23)}}  {{EquationRef(23)}}  
}  }  
  where y+ is defined  +  where ''y''+ is defined as <math>{{y}^{+}}=\frac{y{{u}_{\tau }}}{\nu }</math>. 
  To consider heat transfer in an internal turbulent flow, the entire turbulent boundary layer is divided into three regions: (1) inner region (<math>{{y}^{+}}<5</math>), (2) buffer region (<math>5\le {{y}^{+}}\le 30</math>), and (3) outer region (<math>{{y}^{+}}>30</math>). In the inner region  +  
  <math>{{\varepsilon }_{M}}={{\varepsilon }_{H}}=0</math>  +  To consider heat transfer in an internal turbulent flow, the entire turbulent boundary layer is divided into three regions: (1) inner region (<math>{{y}^{+}}<5</math>), (2) buffer region (<math>5\le {{y}^{+}}\le 30</math>), and (3) outer region (<math>{{y}^{+}}>30</math>). In the inner region <math>{{\varepsilon }_{M}}={{\varepsilon }_{H}}=0</math> and eq. (23) becomes 
  +  
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{{EquationRef(24)}}  {{EquationRef(24)}}  
}  }  
  Since the inner region is very thin,  +  Since the inner region is very thin, <math>y/{{r}_{0}}\ll 1</math> and <math>1y/{{r}_{0}}</math> is effectively equal to 1. Therefore, the temperature profile in the inner region becomes: 
  <math>y/{{r}_{0}}\ll 1</math>  +  
  +  
  <math>1y/{{r}_{0}}</math>  +  
  +  
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{{EquationRef(25)}}  {{EquationRef(25)}}  
}  }  
  The temperature at the boundary between the inner and buffer regions (<math>{{y}^{+}}=5</math>),  +  The temperature at the boundary between the inner and buffer regions (<math>{{y}^{+}}=5</math>), <math>{{\bar{T}}_{s}}</math>, can be obtained from eq. (25) as 
  <math>{{\bar{T}}_{s}}</math>  +  
  +  
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{{EquationRef(27)}}  {{EquationRef(27)}}  
}  }  
  Substituting eq. (  +  Substituting eq. (27) into eq. (23) and assuming the turbulent Prandtl number <math>{{\Pr }^{t}}=1</math>, the following expression is obtained: 
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{{EquationRef(28)}}  {{EquationRef(28)}}  
}  }  
  Since the buffer region is also very thin,  +  
  <math>1y/{{r}_{0}}</math>  +  Since the buffer region is also very thin, <math>1y/{{r}_{0}}</math> in eq. (28) is effectively equal to 1. Defining <math>{{T}^{+}}={(\bar{T}{{T}_{w}})}/{\left( \frac{{{{{q}''}}_{w}}}{\rho {{c}_{p}}}\sqrt{\frac{\rho }{{{\tau }_{w}}}} \right)}\;</math> and Integrating eq. (28) yields 
  +  
  <math>{{T}^{+}}={(\bar{T}{{T}_{w}})}/{\left( \frac{{{{{q}''}}_{w}}}{\rho {{c}_{p}}}\sqrt{\frac{\rho }{{{\tau }_{w}}}} \right)}\;</math>  +  
  +  
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{{EquationRef(30)}}  {{EquationRef(30)}}  
}  }  
  The temperature at the top of the buffer region where <math>{{y}^{+}}=30</math>,  +  The temperature at the top of the buffer region where <math>{{y}^{+}}=30</math>, <math>{{\bar{T}}_{b}}</math>, becomes 
  <math>{{\bar{T}}_{b}}</math>  +  
  , becomes  +  
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{{EquationRef(31)}}  {{EquationRef(31)}}  
}  }  
  For the outer region where <math>{{\varepsilon }_{M}}\gg \nu \text{ and }{{\varepsilon }_{H}}\gg \alpha </math>, eq. (  +  For the outer region where <math>{{\varepsilon }_{M}}\gg \nu \text{ and }{{\varepsilon }_{H}}\gg \alpha </math>, eq. (23) becomes 
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}  }  
where the turbulent Prandtl number is assumed to be equal to 1.  where the turbulent Prandtl number is assumed to be equal to 1.  
  It is assumed that the Nikuradse equation  +  
+  It is assumed that the Nikuradse equation is valid in the outer region and the velocity gradient in this region becomes:  
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{{EquationRef(33)}}  {{EquationRef(33)}}  
}  }  
  The expression of apparent shear stress in this region  +  The expression of apparent shear stress in this region, can be nondimensionalized as: 
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{{EquationRef(34)}}  {{EquationRef(34)}}  
}  }  
  Substituting  +  Substituting 
+  <center><math>{{\tau }_{app}}={{\tau }_{w}}\cdot \left( \frac{r}{{{r}_{o}}} \right)={{\tau }_{w}}\cdot \left( 1\frac{y}{{{r}_{o}}} \right)</math></center>  
+  
+  and eq. (33) into eq. (34), the eddy diffusivity in the outer region is obtained as:  
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{{EquationRef(35)}}  {{EquationRef(35)}}  
}  }  
  Substituting eq. (  +  Substituting eq. (35) into eq. (32), the temperature distribution in this region becomes: 
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{{EquationRef(37)}}  {{EquationRef(37)}}  
}  }  
  The temperature at the center of the tube, <math>{{\bar{T}}_{c}}</math>, can be obtained by letting  +  The temperature at the center of the tube, <math>{{\bar{T}}_{c}}</math>, can be obtained by letting <math>{{y}^{+}}=y_{c}^{+}</math> in eq. (36), i.e. 
  <math>{{y}^{+}}=y_{c}^{+}</math>  +  
  +  
  +  
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{{EquationRef(38)}}  {{EquationRef(38)}}  
}  }  
  The overall temperature change from the wall to the center of the tube can be obtained by adding eqs. (  +  The overall temperature change from the wall to the center of the tube can be obtained by adding eqs. (26), (31) and (38): 
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{{EquationRef(39)}}  {{EquationRef(39)}}  
}  }  
  It follows from the definition of friction factor,  +  It follows from the definition of friction factor, <math>{{c}_{f}}=\frac{{{\tau }_{w}}}{\rho \bar{u}_{m}^{2}/2}</math>, that 
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{{EquationRef(40)}}  {{EquationRef(40)}}  
}  }  
  Substituting eq. (  +  Substituting eq. (40) into eq. (39) and considering the definition of Reynolds number, <math>{{\operatorname{Re}}_{D}}={{\bar{u}}_{m}}D/\nu </math>, eq. (39) becomes: 
  +  
+  { class="wikitable" border="0"  
+    
+   width="100%" <center>  
<math>{{T}_{w}}{{\bar{T}}_{c}}=\left( \frac{{{{{q}''}}_{w}}}{\rho {{c}_{p}}{{{\bar{u}}}_{m}}} \right)\sqrt{\frac{2}{{{c}_{f}}}}\left[ 2.5\ln \left( \frac{{{\operatorname{Re}}_{D}}}{60}\sqrt{\frac{{{c}_{f}}}{2}} \right)+5\ln (5\Pr +1)+5\Pr \right]</math>  <math>{{T}_{w}}{{\bar{T}}_{c}}=\left( \frac{{{{{q}''}}_{w}}}{\rho {{c}_{p}}{{{\bar{u}}}_{m}}} \right)\sqrt{\frac{2}{{{c}_{f}}}}\left[ 2.5\ln \left( \frac{{{\operatorname{Re}}_{D}}}{60}\sqrt{\frac{{{c}_{f}}}{2}} \right)+5\ln (5\Pr +1)+5\Pr \right]</math>  
  +  </center>  
  In order to obtain the heat transfer coefficient, <math>h={{{q}''}_{w}}/({{T}_{w}}{{\bar{T}}_{m}})</math>, the temperature difference <math>{{T}_{w}}{{\bar{T}}_{m}}</math> must be obtained. If the velocity profile can be approximated by  +  {{EquationRef(41)}} 
+  }  
+  
+  In order to obtain the heat transfer coefficient, <math>h={{{q}''}_{w}}/({{T}_{w}}{{\bar{T}}_{m}})</math>, the temperature difference <math>{{T}_{w}}{{\bar{T}}_{m}}</math> must be obtained. If the velocity profile can be approximated by <math>\frac{{\bar{u}}}{{{{\bar{u}}}_{c}}}={{\left( \frac{y}{{{r}_{o}}} \right)}^{1/7}}</math>, and the temperature and velocity can also be approximated by the oneseventh law, i.e.,  
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<math>\frac{{{T}_{w}}\bar{T}}{{{T}_{w}}{{{\bar{T}}}_{c}}}={{\left( \frac{y}{{{r}_{o}}} \right)}^{1/7}}{{,}_{_{\text{ }}}}\frac{{\bar{u}}}{{{{\bar{u}}}_{c}}}={{\left( \frac{y}{{{r}_{o}}} \right)}^{1/7}}</math>  <math>\frac{{{T}_{w}}\bar{T}}{{{T}_{w}}{{{\bar{T}}}_{c}}}={{\left( \frac{y}{{{r}_{o}}} \right)}^{1/7}}{{,}_{_{\text{ }}}}\frac{{\bar{u}}}{{{{\bar{u}}}_{c}}}={{\left( \frac{y}{{{r}_{o}}} \right)}^{1/7}}</math>  
</center>  </center>  
  {{EquationRef(  +  {{EquationRef(42)}} 
}  }  
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<math>{{T}_{w}}{{\bar{T}}_{m}}=\frac{\int_{0}^{{{r}_{o}}}{\bar{u}({{T}_{w}}\bar{T})2\pi rdr}}{\int_{0}^{{{r}_{o}}}{\bar{u}2\pi rdr}}=\frac{5}{6}({{T}_{w}}{{\bar{T}}_{c}})</math>  <math>{{T}_{w}}{{\bar{T}}_{m}}=\frac{\int_{0}^{{{r}_{o}}}{\bar{u}({{T}_{w}}\bar{T})2\pi rdr}}{\int_{0}^{{{r}_{o}}}{\bar{u}2\pi rdr}}=\frac{5}{6}({{T}_{w}}{{\bar{T}}_{c}})</math>  
</center>  </center>  
  {{EquationRef(  +  {{EquationRef(43)}} 
}  }  
  Substituting eq. (  +  Substituting eq. (41) into eq. (43) results in: 
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<math>{{T}_{w}}{{\bar{T}}_{m}}=\frac{5}{6}\left( \frac{{{{{q}''}}_{w}}}{\rho {{c}_{p}}{{{\bar{u}}}_{m}}} \right)\sqrt{\frac{2}{{{c}_{f}}}}\left[ 2.5\ln \left( \frac{{{\operatorname{Re}}_{D}}}{60}\sqrt{\frac{{{c}_{f}}}{2}} \right)+5\ln (5\Pr +1)+5\Pr \right]</math>  <math>{{T}_{w}}{{\bar{T}}_{m}}=\frac{5}{6}\left( \frac{{{{{q}''}}_{w}}}{\rho {{c}_{p}}{{{\bar{u}}}_{m}}} \right)\sqrt{\frac{2}{{{c}_{f}}}}\left[ 2.5\ln \left( \frac{{{\operatorname{Re}}_{D}}}{60}\sqrt{\frac{{{c}_{f}}}{2}} \right)+5\ln (5\Pr +1)+5\Pr \right]</math>  
</center>  </center>  
  {{EquationRef(  +  {{EquationRef(44)}} 
}  }  
which can be rearranged to the following empirical correlation  which can be rearranged to the following empirical correlation  
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<math>\text{N}{{\text{u}}_{D}}=\frac{{{\operatorname{Re}}_{D}}\Pr \sqrt{\frac{{{c}_{f}}}{2}}}{\frac{5}{6}\left[ 2.5\ln \left( \frac{{{\operatorname{Re}}_{D}}}{60}\sqrt{\frac{{{c}_{f}}}{2}} \right)+5\ln (5\Pr +1)+5\Pr \right]}</math>  <math>\text{N}{{\text{u}}_{D}}=\frac{{{\operatorname{Re}}_{D}}\Pr \sqrt{\frac{{{c}_{f}}}{2}}}{\frac{5}{6}\left[ 2.5\ln \left( \frac{{{\operatorname{Re}}_{D}}}{60}\sqrt{\frac{{{c}_{f}}}{2}} \right)+5\ln (5\Pr +1)+5\Pr \right]}</math>  
</center>  </center>  
  {{EquationRef(  +  {{EquationRef(45)}} 
}  }  
  which can be used together with appropriate friction coefficient  +  which can be used together with appropriate friction coefficient to obtain the Nusselt number. 
+  
+  ==References==  
+  {{Reflist}} 
Current revision as of 20:21, 23 July 2010
Heat transfer in fullydeveloped turbulent flow in a circular tube subject to constant heat flux (q''_{w} = const) will be considered in this article ^{[1]}^{[2]}. When the turbulent flow in the tube is fully developed, we have and the energy equation becomes

After the turbulent flow is hydrodynamically and thermally fully developed, the timeaveraged temperature profile is no longer a function of axial distance from the inlet, i.e.,

where is the timeaveraged temperature at the centerline of the tube, and T_{w} is the wall temperature. Thus, is a function of r only, i.e.,

where f is independent from x. Differentiating eq. (2) yields

At the wall, the contribution of eddy diffusivity on the heat transfer is negligible, and the heat flux at the wall becomes

Substituting eq. (3) into eq. (5), one obtains:

Since the heat flux is constant, q''_{w} = const, it follows that , i.e.,

Therefore, eq. (4) becomes:

For fully developed flow, the local heat transfer coefficient is:

where is the timeaveraged mean temperature defined as:

Since q''_{w} = const, it follows from eq. (9) that , i.e.,

Combining eqs. (7), (8) and (11), the following relationships are obtained:

The timeaveraged mean temperature, , changes with x as the result of heat transfer from the tube wall. The rate of mean temperature change can be obtained as follows:

Substituting eq. (12) into eq. (1), the energy equation becomes:

where y = r_{0} − r is the distance measured from the tube wall. Equation (14) is subject to the following two boundary conditions:
(axisymmetric condition) 

Integrating eq. (14) in the interval of (r_{0}, r) and considering eq. (15), we have:

which can be rearranged to

where

Integrating eq. (18) in the interval of (0, y) and considering eq. (16), one obtains:

If the profiles of axial velocity and the thermal eddy diffusivity are known, eq. (20) can be used to obtain the correlation for internal forced convection heat transfer. With the exception of the very thin viscous sublayer, the velocity profile in the most part of the tube is fairly flat. Therefore, it is assumed that the timeaveraged velocity, , in eq. (19) can be replaced by , and I(y) becomes:

Substituting eqs. (21) and (13) into eq. (20) yields:

which can be rewritten in terms of wall coordinate

where y+ is defined as .
To consider heat transfer in an internal turbulent flow, the entire turbulent boundary layer is divided into three regions: (1) inner region (y^{ + } < 5), (2) buffer region (), and (3) outer region (y^{ + } > 30). In the inner region and eq. (23) becomes

Since the inner region is very thin, and 1 − y / r_{0} is effectively equal to 1. Therefore, the temperature profile in the inner region becomes:

The temperature at the boundary between the inner and buffer regions (y^{ + } = 5), , can be obtained from eq. (25) as

In the buffer region where , the eddy diffusivity in the buffer region is:

Substituting eq. (27) into eq. (23) and assuming the turbulent Prandtl number , the following expression is obtained:

Since the buffer region is also very thin, 1 − y / r_{0} in eq. (28) is effectively equal to 1. Defining and Integrating eq. (28) yields

i.e.,

The temperature at the top of the buffer region where y^{ + } = 30, , becomes

For the outer region where , eq. (23) becomes

where the turbulent Prandtl number is assumed to be equal to 1.
It is assumed that the Nikuradse equation is valid in the outer region and the velocity gradient in this region becomes:

The expression of apparent shear stress in this region, can be nondimensionalized as:

Substituting
and eq. (33) into eq. (34), the eddy diffusivity in the outer region is obtained as:

Substituting eq. (35) into eq. (32), the temperature distribution in this region becomes:

which is valid from y^{ + } = 30 to the center of the tube where y_{c} = r_{0} or

The temperature at the center of the tube, , can be obtained by letting in eq. (36), i.e.

The overall temperature change from the wall to the center of the tube can be obtained by adding eqs. (26), (31) and (38):

It follows from the definition of friction factor, , that

Substituting eq. (40) into eq. (39) and considering the definition of Reynolds number, , eq. (39) becomes:

In order to obtain the heat transfer coefficient, , the temperature difference must be obtained. If the velocity profile can be approximated by , and the temperature and velocity can also be approximated by the oneseventh law, i.e.,

it follows that

Substituting eq. (41) into eq. (43) results in:

which can be rearranged to the following empirical correlation

which can be used together with appropriate friction coefficient to obtain the Nusselt number.