By Ernest E. Ludwig
Just like the different volumes during this 3-volume set, quantity three emphasizes how one can follow options of technique layout and the way to interpret effects into mechanical gear info. It specializes in the utilized features of chemical engineering layout to assist layout and/or venture engineers in score technique specifications, specifying for buying reasons, and examining and choosing the mechanical apparatus had to fulfill the method services. technique chemical engineering and mechanical hydraulics are integrated within the layout procedures.
Provides prepared layout approaches, apparatus compatible for software choice, and charts in conveniently usable form
Covers warmth move, refrigeration structures, compression surge drums, and mechanical drivers
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Extra info for Applied Process Design for Chemical and Petrochemical Plants, Vol. 3
The number of tie rods used depends upon the size and construction of the exchanger bundle. The material of the rods and spacers must be the same or equivalent to that of the baffles or bundle tubes. Provision must be made in the tubesheet layout for these rods, which is usually accomplished by omitting a tube (or more) at selected locations on the outer periphery of the tube bundle. The rod is usually threaded into the back of only one of the tubesheets, being free at the other end, terminating with the last baffle or support by means of lock washers or similar fool-proof fastening.
66131_Ludwig_CH10A 5/30/2001 4:08 PM Page 33 Heat Transfer Figure 10-22C. Longitudinal shell-pass baffle. , Patent No. ) Figure 10-22D. Longitudinal baffle, sliding slot detail. Figure 10-23. Tube-to-double tubesheet assembly detail. 33 66131_Ludwig_CH10A 5/30/2001 4:08 PM 34 Page 34 Applied Process Design for Chemical and Petrochemical Plants 8. Tube Joints in Tubesheets The quality of the connection between the tube and tubesheet is extremely important. A poor joint here means leakage of shell-side fluid into the tube side or vice versa.
Values read from the chart are not more than 1% lower than those obtained by calculations, except where the curve is extrapolated to lower tube counts. Such extrapolations result in errors of 3%, 4%, and higher, giving larger values than those calculated. This does not apply to higher tube count extrapolations. The chart is limited to 3/4 -in. B. Area Ft2 Act. Area % Error 66 3 /4 in. D. ᮀ 2 in. 43 88 3 /4 in. D. ᮀ 2 in. 19 54 1 in. D. ᮀ 3 in. B. ϭ Radius of bend. *The calculated areas were based on Figure 10-27B using only the respective tube size and number of tubes.
Applied Process Design for Chemical and Petrochemical Plants, Vol. 3 by Ernest E. Ludwig