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 = 24.6 (Δp/μ)

Η = 17 - 61.1 log μ

Η = 0.25 log μ - 1.67

Η = 1.66 - 0.25 log μ

Η = 24.6 (Δp/μ)

Η = 17 - 61.1 log μ

Η = 0.25 log μ - 1.67

Η = 1.66 - 0.25 log μ

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Process Equipment and Plant Design
For a cylindrical shell, (subject to the thickness of uppermost course being more than the minimum for diaofthe tank in question), the thickness of the courses of shell

Decreases upwards

Increases upwards

Remains same throughout

May decrease or increase upwards depending upon whether vacuum or positive pressure would be maintained inside the shell

Decreases upwards

Increases upwards

Remains same throughout

May decrease or increase upwards depending upon whether vacuum or positive pressure would be maintained inside the shell

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Process Equipment and Plant Design
In a multipass shell and tube heat exchanger, the shell side cross flow area does not depend upon

Pitch

None of these

Clearance

Baffle spacing

Pitch

None of these

Clearance

Baffle spacing

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Process Equipment and Plant Design
Elastic failure of a material occurs, when the tensile stress equals yield strength, yield point or the elastic limit. Also, the elastic failure occurs according to maximum strain theory, when the maximum tensile strain equals (where, σ = yield strength and E = modulus of elasticity)

E/σ

Σ/E

E

Σ

E/σ

Σ/E

E

Σ

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Process Equipment and Plant Design
The approximate liquid depth in an agitation tank is equal to (where, d = tank diameter)

0.5 d

D

2 d

0.75 d

0.5 d

D

2 d

0.75 d

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Process Equipment and Plant Design
At equal mass velocities, the values of film co-efficients for gases as compared to that for liquids are generally.

Higher

Same

Lower

Unpredictable

Higher

Same

Lower

Unpredictable

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Process Equipment and Plant Design

Process Equipment and Plant Design For a cylindrical shell, (subject to the thickness of uppermost course being more than the minimum for diaofthe tank in question), the thickness of the courses of shell

Process Equipment and Plant Design In a multipass shell and tube heat exchanger, the shell side cross flow area does not depend upon

Process Equipment and Plant Design The approximate liquid depth in an agitation tank is equal to (where, d = tank diameter)

Process Equipment and Plant Design At equal mass velocities, the values of film co-efficients for gases as compared to that for liquids are generally.

Process Equipment and Plant Design
For a cylindrical shell, (subject to the thickness of uppermost course being more than the minimum for diaofthe tank in question), the thickness of the courses of shell

Process Equipment and Plant Design
In a multipass shell and tube heat exchanger, the shell side cross flow area does not depend upon

Process Equipment and Plant Design
The approximate liquid depth in an agitation tank is equal to (where, d = tank diameter)

Process Equipment and Plant Design
At equal mass velocities, the values of film co-efficients for gases as compared to that for liquids are generally.