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Heat transfer and hydrodynamic performance of three different spirally fluted tubes was determined. The tubes were 5/8-in. in nominal diameter and were made of aluminum. Results were compared to 5/8.in. OD, smooth copper-nickel and aluminum tubes. Data was taken by condensing steam at about 3 psia on the outside surface of a horizontally mounted tube in the center of a tube bank. The center tube was cooled by water on the inside at velocities of 3 to 25 feet per second. The overall heat transfer coefficient was determined directly from experimental data. The inside and outside heat transfer coefficients were determined using the Wilson plot technique. The cooling water pressure drop was measured inside the tube and converted to the friction factor in the enhanced section. The overall heat transfer coefficients of the enhanced tubes were as large as 1.75 times the corresponding smooth tube value for the same mass flow rate of cooling water. The inside heat transfer coefficients increased by about a factor of 3 while the outside heat transfer coefficients decreased by 10 to 20 percent when compared to smooth tube values. The results of this work indicate that the required condenser surface area can be reduced by 50 percent if these enhanced tubes are used in place of smooth tubes. (Author).
A test facility to evaluate the effect of condensate inundation on heat transfer within a horizontal tube bundle was designed, constructed and validated. Five 15.9 mm (5/8 in.) nominal outside diameter, smooth stainless steel tubes were utilized in a vertical row. They were located in an equilateral triangular array with a spacing to diameter ratio of 1.5. Heat transfer performance was determined for each tube in the bundle. Data was taken by condensing steam at about 21 kPa (3 psia) on the outside of each tube. Each tube was cooled by water on the inside at velocities of 0.78 to 7.0 m/sec (2.56 to 23 ft/sec). The overall heat transfer coefficient was determined directly from experimental data. The inside and outside heat transfer coefficients were determined using the Wilson plot technique. Observation of condensate flow showed lateral droplet motion along the tube in portions of the condenser as well as side drainage, particularly over the first three tubes. Outside heat transfer coefficients were lower than expected when compared to Nusselt theory, possibly due to the effects of secondary vapor flow and/or non-condensable gases. Recommendations to improve validation are provided. (Author).
This book presents contributions from renowned experts addressing research and development related to the two important areas of heat exchangers, which are advanced features and applications. This book is intended to be a useful source of information for researchers, postgraduate students, academics, and engineers working in the field of heat exchangers research and development.
Heat transfer and hydrodynamic performance of eight different geometrically enhanced tubes of different metals was determined. Results were compared to a 25.4 mm (1.0 in.) OD, smooth stainless steel tube. Steam at about 21 kPa (3 psia) was condensed on the outside surface of each enhanced tube, horizontally mounted in the center of a dummy tube Bank. Each tube was cooled on the inside by water. The overall heat transfer coefficient was determined directly from experimental data. The inside and outside heat transfer coefficients were determined using the Wilson plot technique. The cooling water pressure drop was measured inside the tube and converted to the friction factor in the enhanced section. The overall heat transfer coefficients of the enhanced tubes were increased as much as 1.9 times, and the corrected pressure drops of the enhanced tubes were as large as 4 times the corresponding smooth tube value for the same cooling water velocity. The helix angle should be 45 deg to 60 deg on the inside surface and 90 deg on the outside surface of the tube to obtain maximum inside and outside heat transfer coefficients. (Author).
A test facility to evaluate the effect of condensate inundation on heat transfer within a horizontal tube bundle was designed, constructed and validated. Five 15.9 mm (5/8 in.) nominal outside diameter, smooth stainless steel tubes were utilized in a vertical row. They were located in an equilateral triangular array with a spacing to diameter ratio of 1.5. Heat transfer performance was determined for each tube in the bundle. Data was taken by condensing steam at about 21 kPa (3 psia) on the outside of each tube. Each tube was cooled by water on the inside at velocities of 0.78 to 7.0 m/sec (2.56 to 23 ft/sec). The overall heat transfer coefficient was determined directly from experimental data. The inside and outside heat transfer coefficients were determined using the Wilson plot technique. Observation of condensate flow showed lateral droplet motion along the tube in portions of the condenser as well as side drainage, particularly over the first three tubes. Outside heat transfer coefficients were lower than expected when compared to Nusselt theory, possibly due to the effects of secondary vapor flow and/or non-condensable gases. Recommendations to improve validation are provided. (Author).
Heat transfer and hydrodynamic performance of eight different geometrically enhanced tubes of different metals was determined. Results were compared to a 25.4 mm (1.0 in.) OD, smooth stainless steel tube. Steam at about 21 kPa (3 psia) was condensed on the outside surface of each enhanced tube, horizontally mounted in the center of a dummy tube Bank. Each tube was cooled on the inside by water. The overall heat transfer coefficient was determined directly from experimental data. The inside and outside heat transfer coefficients were determined using the Wilson plot technique. The cooling water pressure drop was measured inside the tube and converted to the friction factor in the enhanced section. The overall heat transfer coefficients of the enhanced tubes were increased as much as 1.9 times, and the corrected pressure drops of the enhanced tubes were as large as 4 times the corresponding smooth tube value for the same cooling water velocity. The helix angle should be 45 deg to 60 deg on the inside surface and 90 deg on the outside surface of the tube to obtain maximum inside and outside heat transfer coefficients. (Author).
&Quot;This book explores flow through passages with hydraulic diameters from about 1 [mu]m to 3 mm, covering the range of minichannels and microchannels. Design equations along with solved examples and practice problems are also included to serve the needs of practicing engineers and students in a graduate course."--BOOK JACKET.