Forced convection heat transfer tube bundles

Whitaker, S., Forced Convection Heat-Transfer Correlations for Flow in Pipes, Past Flat Plated, Single Cylinders, Single Spheres, and Flow in Packed Beds and Tube Bundles , AIChE J.. Vol. 18, pp. 361-371.1972. 

Whitaker, S. Forced convection heat transfer correlations 26. for flow in pipes, past flat plates, single cylinders, single spheres, and for flow in packed beds and tube bundles. 27. AIChE J. 1972, 18, 361-371. 

J. M. McNaught, Two-Phase Forced Convection Heat Transfer During Condensation on Horizontal Tube Bundles, Proc. 7th Int. Heat Transfer Conf, Munich, 5, pp. 125-131,1982. 

JACKSON, J.D. and HALL, W.B., Influences of buoyancy on heat transfer to fluids flowing in vertical tubes under turbulent condition . Turbulent Forced Convection in Channels and Bundles Theory and Applications to Heat Exchangers and Nuclear Reactors, 2, Advanced Study Institute Book (eds. Kakac, S. and Spalding, D.B.), 613-640, (1979). 

Design for Heat Transfer Coefficients by Forced Convection Using Radial Low-Fin tubes in Heat Exchanger Bundles... 

Chen s method was developed from experimental data on forced convective boiling in vertical tubes. It can be applied, with caution, to forced convective boiling in horizontal tubes, and annular conduits (concentric pipes). Butterworth (1977) suggests that, in the absence of more reliable methods, it may be used to estimate the heat-transfer coefficient for forced convective boiling in cross-flow over tube bundles using a suitable cross-flow correlation to predict the forced-convection coefficient. Shah s method was based on data for flow in horizontal and vertical tubes and annuli. 

Caira, M., E. Cipollone, M. Cumo, and A. Naviglio, 1985, Heat Transfer in Forced Convective Boiling in a Tube Bundle, 3rd Int. Topic Meeting on Reactor Thermohydraulics, ANS, Saratoga, New York. (4)... 

Here hNB is the nucleate boiling coefficient (calculated from equations analogous to those given previously) and hFC is the forced convective component, which is related to the heat transfer coefficient h, for the liquid phase flowing alone across the tube bundle by the expression... 

Bell-Delaware Method. Pressure drop and heat transfer calculations (the step 6 of the above thermal design procedure) constitute the key part of design. Tubeside calculations are straightforward and should be executed using available correlations for internal forced convection. The shellside calculations, however, must take into consideration the effect of various leakage streams (A and E streams in Fig. 17.30) and bypass streams (C and F streams in Fig. 17.30) in addition to the main crossflow stream B through the tube bundle. Several methods have been in use over the years, but the most accurate method in the open literature is the above mentioned Bell-Delaware method. This approach is based primarily on limited experimental data. The set of correlations discussed next constitutes the core of the Bell-Delaware method. 

Heat transfer is improved by an increase of the velocity of the liquid. According to natural convection and the buoyancy force of rising bubbles a circulation of the Uq-uid is induced in a short-tube vertical evaporator, see Fig. 7.1-2. In the narrow tubes, liquid is evaporating to a certain degree and recirculated in the central return passage after separation of the vapor. This type is less recommended when a fouling of the heat transfer area by product components takes place. Then it is reasonable to separate the tube bundle and the head space in which the entrainment of hquid is reduced, see Fig. 7.1-3. The cleaning of the tubes can be easily carried out. 

The heat-transfer phenomena for forced convection over exterior surfaces are closely related to the nature of the flow. The heat transfer in flow over tube bundles depends largely on the flow pattern and the degree of turbulence, which in turn are functions of the velocity of the fluid and the size and arrangement of the tubes. The equations available for the calculation of heat transfer coefficients in flow over tube banks are based entirely on experimental data because the flow Is too complex to be treated analytically. Experiments have shown that, in flow over staggered tube banks, the transition from laminar to turbulent flow Is more gradual than in flow through a pipe, whereas for in-line tube bundles the transition phenomena resemble those observed in pipe flow. In either case the transition from laminar to turbulent flow begins at a Reynolds number based on the velocity in the minimum flow area of about 100, and the flow becomes fully turbulent at a Reynolds number of about 3,000. The equation below can be used to predict heat transfer for flow across ideal tube banks. 

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