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The attached calculates the shell nozzle pressure drop. It does an entrance area calculation.\dale\documents\heat exchanger\shellnozdp.doc

Another good source for Kettle Reboiler design is "Process Heat Transfer" by Serth. He discusses such factors as LMTD, Fouling, Number of nozzles and shell diameter.

The allowable dirt(fouling) factor can be found in TEMA (Tubular Exchanger Manufactures Association)

There is a chapter in the book: Process Heat Transfer by Kern that discusses heating liquid batches.

Based on there being a perfect seal of the long baffle, and two tube passes, I would use a LMTD correction factor of 1.0.

There are tips on reboilers on gulleyassociates.com.

I don't have an practical overall heat transfer but for sludge type materials, the tube velocity should be at least 4 ft/sec.

Equivalent formulas in a reference text can be found in Heat Transfer in Process Engineering by Eduardo Cao. It has simplified equations for different objects,

Heat Exchanger Design Handbook has a section on Helical Coils. Also J.S. Jayakumar has articles on this subject.

If the operating pressure is low enough in order to treat the mixture like an ideal gas, it is simple. The K-values are vapor pressure/ operating pressure. Otherwise the Wilson equation could be used. It depends on the critical pressure, critical temperature and acentric factor.

After John Slagle past away, his wife named Pat ran the company. Back in 1970 -1990, I had a computer service named "Gulley Computer Associates" that had thermal design software that Slagle used. I checked our storage but did not find anything helpful.

Heat Transfer Hand Book published by Begell House, Inc

The stagnant area is the area from the forward front of the impingement plate and the tubesheet. I called it an area but it is actually more of a volume.

The perforations slow the velocities coming off the plate. It is not desirable to slow this velocity going toward the tubesheet. Slowing this velocity can create a stagnant area where there can be corrosion and fouling. Report

I am puzzled by using the term "void fraction" when mixing liquids. Void fraction is for two phase streams and is the fraction that is gas. There are different types of static mixtures. The least expensive type is the twisted ribbon. It is for Reynolds number below 2500.

Ludwig's Applied Process Design for Chemical and Petrochemical Plants, volume 3, fourth edition.

The TEMA quantity is also good for gases. I would not exceed the 6000 by much. On www.gulleyassociates.com in the pressure drop section, there is an equation for the maximum velocity inside tubes. In this case it gives a maximum value of 6400 where velocity is in ft/sec. and density is in lb/ft3.

The heat transfer coefficient for the superheated steam will depend on velocity. I would use the heat transfer coefficient for the condensing steam a value of 2000 Btu/ft2-h-F.

There are equations where you do not need the latent heat of vaporization to size a PSV. Refer to section 5 of the Engineering Data Book of the GPSA.

Any text with the title Process Heat Transfer will answer your question. The calculation of the overall heat transfer depends on three resistances. one of those resistances has the thermal conductivity of the pipe metal.