Process Equipment and Plant Design
Overall distillation column efficiency for most of the refinery columns can be given by (for μ = 0.07 - 1.4 cp and relative volatility < 4) (where η = overall column efficiency, % μ = molal average viscosity of feed at average column temperature and pressure, cp Δp = pressure drop per tray, psi)

Η = 1.66 - 0.25 log μ
Η = 0.25 log μ - 1.67
Η = 17 - 61.1 log μ
Η = 24.6 (Δp/μ)

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Process Equipment and Plant Design
In the design of a shell and tube heat exchanger, the corrosion allowance

For internal cover and tube sheet is provided on both the sides
For carbon steel and cast iron pressure parts is 1.5 mm (except for tubes) and for severe conditions it is 3 mm
All of these
Need not be provided for non-pressure parts like tie rods, spacers, baffles, supports etc

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Process Equipment and Plant Design
Triangular pitch tube layout as compared to square pitch in a shell and tube heat exchanger

Permits the use of less tubes in a given shell diameter
Both B and C
Permits the use of more tubes in a given shell diameter
Facilitates comparatively easier external cleaning because of large clearance

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