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A new theoretical formula for turbulent heat and mass transfer with gases or liquids in tube flow
Author(s) -
Sandall O. C.,
Hanna O. T.,
Mazet P. R.
Publication year - 1980
Publication title -
the canadian journal of chemical engineering
Language(s) - English
Resource type - Journals
SCImago Journal Rank - 0.404
H-Index - 67
eISSN - 1939-019X
pISSN - 0008-4034
DOI - 10.1002/cjce.5450580404
Subject(s) - prandtl number , thermodynamics , turbulence , churchill–bernstein equation , heat transfer , convective heat transfer , heat transfer coefficient , mass transfer , schmidt number , mechanics , chemistry , nusselt number , physics , reynolds number
A new theoretically‐based formula is presented for fully developed steady‐state forced convection heat or mass transfer in turbulent tube flow. This relationship, which is proposed for the frill range range of Prandtl or Schmidt numbers between 0.7 (gases) and 100 000 (liquids), is as follows:\documentclass{article}\pagestyle{empty}\begin{document}$$ \frac{{St}}{{\sqrt {f/2} }} = \left\{ {C_1\,Pr ^{2/3} + C_2\,Pr ^{1/3} + C_3 \ln Pr + C_4 + 2.78\ln \left( {\frac{{Re\sqrt {f/2} }}{{90}}} \right)} \right\}_{(heat\,transfer)}^{ - 1} $$\end{document}Coniparisons a with widely quotcd sets of data show very good agreement IFriend and metzner (heat transfer in liquids), Dcisser and Eian (heat transfer in air), Allen aid Eckert (heat transfer in water), Malina and Sparrow (heat trniisfcr in liquids), Harrott and Hamilton (mass transfcr in liquids)]. Absolute mean deviations vary from 3.6 to 8.1% over the range 0.73 + Pr or Sr ≤ 97 600.