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| The '''log mean temperature difference''' (also known by its [[Acronym and initialism|initialism]] '''LMTD''') is used to determine the temperature driving force for [[heat transfer]] in flow systems, most notably in [[heat exchanger]]s. The LMTD is a logarithmic average of the temperature difference between the hot and cold streams at each end of the exchanger. The larger the LMTD, the more heat is transferred. The use of the LMTD arises straightforwardly from the analysis of a heat exchanger with constant flow rate and fluid thermal properties.
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| == Definition ==
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| We assume that a generic heat exchanger has two ends (which we call "A" and "B") at which the hot and cold streams enter or exit on either side; then, the LMTD is defined by the [[logarithmic mean]] as follows:
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| :<math>LMTD=\frac{\Delta T_A - \Delta T_B}{\ln \left( \frac{\Delta T_A}{\Delta T_B} \right ) }</math>
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| where ''ΔT<sub>A</sub>'' is the temperature difference between the two streams at end ''A'', and ''ΔT<sub>B</sub>'' is the temperature difference between the two streams at end ''B''. With this definition, the LMTD can be used to find the exchanged heat in a heat exchanger:
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| :<math> Q = U \times Ar \times LMTD</math>
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| Where ''Q'' is the exchanged heat duty (in [[watt]]s), ''U'' is the [[heat transfer coefficient]] (in watts per [[kelvin]] per square meter) and ''Ar'' is the exchange area. Note that estimating the heat transfer coefficient may be quite complicated.
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| This holds both for parallel flow, where the streams enter from the same end, and for [[Countercurrent exchange|counter-current]] flow, where they enter from different ends.
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| In a cross-flow, in which one system, usually the heat sink, has the same nominal temperature at all points on the heat transfer surface, a similar relation between exchanged heat and LMTD holds, but with a correction factor. A correction factor is also required for other more complex geometries, such as a shell and tube exchanger with baffles.
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| ==Derivation==
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| Assume heat transfer is occurring in a heat exchanger along an axis ''z'', from generic coordinate ''A'' to ''B'', between two fluids, identified as ''1'' and ''2'', whose temperatures along ''z'' are T<sub>1</sub>(z) and T<sub>2</sub>(z).
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| The local exchanged heat at ''z'' is proportional to the temperature difference:
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| :<math> q(z) = U (T_2(z)-T_1(z))/D = U (\Delta\;T(z))/D,</math> | |
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| where ''D'' is the distance between the two fluids.
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| The heat that leaves the fluids causes a temperature gradient according to [[Fourier's law]]:
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| ::<math>\frac{\mathrm{d}\,T_1}{\mathrm{d}\,z}=k_a (T_1(z)-T_2(z))=-k_a\,\Delta T(z)</math>
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| ::<math>\frac{\mathrm{d}\,T_2}{\mathrm{d}\,z}=k_b (T_2(z)-T_1(z))=k_b\,\Delta T(z)</math>
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| Summed together, this becomes
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| :<math>\frac{\mathrm{d}\,\Delta T}{\mathrm{d}\,z}=\frac{\mathrm{d}\,(T_2-T_1)}{\mathrm{d}\,z}=\frac{\mathrm{d}\,T_2}{\mathrm{d}\,z}-\frac{\mathrm{d}\,T_1}{\mathrm{d}\,z}=K\Delta T(z)</math>
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| where ''K=k<sub>a</sub>+k<sub>b</sub>''.
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| The total exchanged energy is found by integrating the local heat transfer ''q'' from ''A'' to ''B'':
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| :<math> Q = \int^{B}_{A} q(z) dz = \frac{U}{D} \int^{B}_{A} \Delta T(z) dz = \frac{U}{D} \int^{B}_{A} \Delta T \,dz</math>
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| Use the fact that the heat exchanger area ''Ar'' is the pipe length ''A''-''B'' multiplied by the interpipe distance ''D'':
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| :<math> Q = \frac{U Ar}{(B-A)} \int^{B}_{A} \Delta T \,dz = \frac{U Ar \int^{B}_{A} \Delta T \,dz}{\int^{B}_{A} \,dz} </math>
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| In both integrals, make a change of variables from ''z'' to ''Δ T'':
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| :<math> Q = \frac{U Ar \int^{\Delta T(B)}_{\Delta T(A)} \Delta T \frac{\mathrm{d}\,z}{\mathrm{d}\,\Delta T}\,d(\Delta T)}{\int^{\Delta T(B)}_{\Delta T(A)} \frac{\mathrm{d}\,z}{\mathrm{d}\,\Delta T}\,d(\Delta T)} </math>
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| With the relation for ''Δ T'' found above, this becomes
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| :<math> Q = \frac{U Ar \int^{\Delta T(B)}_{\Delta T(A)} \frac{1}{K}\,d(\Delta T)}{\int^{\Delta T(B)}_{\Delta T(A)} \frac{1}{K \Delta T}\,d(\Delta T)} </math>
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| Integration is at this point trivial, and finally gives:
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| :<math> Q = U \times Ar \times \frac{\Delta T(B)-\Delta T(A)}{\ln [ \Delta T(B) / \Delta T(A) ]} </math>,
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| from which the definition of LMTD follows.
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| == Assumptions and Limitations ==
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| * It has been assumed that the rate of change for the temperature of both fluids is proportional to the temperature difference; this assumption is valid for fluids with a constant [[specific heat]], which is a good description of fluids changing temperature over a relatively small range. However, if the specific heat changes, the LMTD approach will no longer be accurate.
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| * A particular case where the LMTD is not applicable are [[condenser (heat transfer)|condensers]] and [[reboiler]]s, where the [[latent heat]] associated to phase change makes the hypothesis invalid.
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| * It has also been assumed that the heat transfer coefficient (''U'') is constant, and not a function of temperature. If this is not the case, the LMTD approach will again be less valid
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| * The LMTD is a steady-state concept, and cannot be used in dynamic analyses. In particular, if the LMTD were to be applied on a transient in which, for a brief time, the temperature differential had different signs on the two sides of the exchanger, the argument to the logarithm function would be negative, which is not allowable.
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| ==References==
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| * Kay J M & Nedderman R M (1985) ''Fluid Mechanics and Transfer Processes'', Cambridge University Press
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| ==External links==
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| [[Category:Heat transfer]]
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Diving Coach (Open water ) Dominic from Kindersley, loves to spend some time classic cars, property developers in singapore house for rent (Source Webpage) and greeting card collecting. Finds the world an interesting place having spent 8 days at Cidade Velha.