Estimation of Heat Transfer Coefficient from Universal Expression of Tangential Velocity at Boundary Layer Edge on Side Wall of a Fully Turbulent Agitated Vessel

Shiobara, Katsumi; Hiraoka, Setsuro; Kato, Yoshihito; Iwata, Shuichi; Tada, Yutaka; Yamaguchi, Takao; Yamamura, Masaaki

doi:10.1252/jcej.07we239

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“…The principles of the heat transfer process in agitated vessels and basic correlations which enable calculation of the heat transfer coefficient for different physical systems agitated in vessels of different geometrical configurations have been discussed in monographs ,, and papers. , Over the last 25 years the development of research in this field concerned mainly such problems as mathematical modeling of the mean , and local heat transfer coefficients; optimization of the agitated vessel geometry for heat transfer process; ,,,,,,,, measurements of the mean heat transfer coefficient for viscous ,,,,, and non-Newtonian fluids, ,,, immiscible liquid mixtures, and nanosuspensions; measurements of local heat transfer coefficient for liquid ,, and gas–liquid systems; ,,,,, testing of different types of the heating/cooling heat transfer surfaces in agitated vessels, i.e. jackets, ,,,, helical coils, ,,, vertical tubular coils; ,, CFD modeling of heat transfer process in agitated vessels. ,,,, …”

Section: Introductionmentioning

confidence: 99%

Local Heat Transfer Process for a Gas–Liquid System in a Wall Region of an Agitated Vessel Equipped with the System of CD6-RT Impellers

Bielka

Cudak

Karcz

2014

Ind. Eng. Chem. Res.

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The results of the experimental studies of local heat process for a gas–liquid system in the region of the cylindrical wall of an agitated vessel equipped with the system of CD 6–RT impellers are presented. A lower CD 6 impeller (Smith turbine) and upper RT impeller (Rushton turbine) were located on the common shaft in a baffled agitated vessel of inner diameter equal to 0.3 m. Liquid height in the agitated vessel was equal to 0.6 m. Newtonian liquids of different physical properties were used as a continuous phase. Air was dispersed in the liquid. Local heat transfer coefficients were measured using both thermal and electrochemical methods. In total, 2280 experimental points were obtained. Distributions of the heat transfer coefficients were described by means of eqs 12–17 and 18–23 as a function of the Re and Pr numbers, dimensionless axial coordinate z/H, and modified Fr g number, separately, for turbulent and transitional ranges of the fluid flow in the agitated vessel. Equations 12–17 and 18–23, concerning both coalescing and noncoalescing gas–liquid systems, have no equivalent in the open literature.

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