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)

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 = 0.25 log μ - 1.67

Η = 1.66 - 0.25 log μ

Η = 17 - 61.1 log μ

Η = 24.6 (Δp/μ)

Η = 0.25 log μ - 1.67

Η = 1.66 - 0.25 log μ

Η = 17 - 61.1 log μ

Η = 24.6 (Δp/μ)

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Process Equipment and Plant Design
for couplings and unions would be

Negligible

60

200

350

Negligible

60

200

350

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Process Equipment and Plant Design
Pressure drop due to pipe fittings can be estimated by the equation, ΔP/p = 4f.Le/D.V2/2gc, where, Le = equivalent length of straight pipeline which will incur the same frictional loss as the fitting and D = diameter of the fitting. The value of Le/D (dimensionless) for 45° elbow and 180° close return bends would be respectively around

5 and 10

45 and 75

300 and 500

180 and 300

5 and 10

45 and 75

300 and 500

180 and 300

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Process Equipment and Plant Design
The ends of a cylinderical vessel can be closed by a head, which can be one of the four shapes. For the same thickness, choose the one which can withstand the highest pressure.

Flat plate

Torispherical

Hemispherical

Ellipsoidal

Flat plate

Torispherical

Hemispherical

Ellipsoidal

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Process Equipment and Plant Design
Movement of pipeline caused by thermal expansion is taken care by providing

All of these

Changes in its direction

Expansion joint

Change in the shape of pipeline

All of these

Changes in its direction

Expansion joint

Change in the shape of pipeline

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

Need not be provided for non-pressure parts like tie rods, spacers, baffles, supports etc

For internal cover and tube sheet is provided on both the sides

All of these

For carbon steel and cast iron pressure parts is 1.5 mm (except for tubes) and for severe conditions it is 3 mm

Need not be provided for non-pressure parts like tie rods, spacers, baffles, supports etc

For internal cover and tube sheet is provided on both the sides

All of these

For carbon steel and cast iron pressure parts is 1.5 mm (except for tubes) and for severe conditions it is 3 mm

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Process Equipment and Plant Design

Process Equipment and Plant Design for couplings and unions would be

Process Equipment and Plant Design The ends of a cylinderical vessel can be closed by a head, which can be one of the four shapes. For the same thickness, choose the one which can withstand the highest pressure.

Process Equipment and Plant Design Movement of pipeline caused by thermal expansion is taken care by providing

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

Process Equipment and Plant Design
for couplings and unions would be

Process Equipment and Plant Design
The ends of a cylinderical vessel can be closed by a head, which can be one of the four shapes. For the same thickness, choose the one which can withstand the highest pressure.

Process Equipment and Plant Design
Movement of pipeline caused by thermal expansion is taken care by providing

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