Smoker's equation for the calculation of number of equilibrium stages in a continuous binary distillation column is used, when the

Process Equipment and Plant Design
Smoker's equation for the calculation of number of equilibrium stages in a continuous binary distillation column is used, when the

Number of equilibrium stages in only stripping section is to be calculated

Number of equilibrium stages required is likely to be very small

Feed is not at its bubble point

Relative volatility is close to one (e.g., separation of close boiling isomers)

Number of equilibrium stages in only stripping section is to be calculated

Number of equilibrium stages required is likely to be very small

Feed is not at its bubble point

Relative volatility is close to one (e.g., separation of close boiling isomers)

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Process Equipment and Plant Design
Apex angle of conical heads used in the bottom heads of chemical process equipments is usually

60°

30°

45°

75°

60°

30°

45°

75°

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Process Equipment and Plant Design
Factor of safety (i.e., overdesign factor) in heat transfer equipments is about __________ percent more than the actual/theoretical design factor.

35-40

43961

30-35

15-20

35-40

43961

30-35

15-20

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Process Equipment and Plant Design
Mc Cable Thiele method used for finding theoretical stages in a distillation column assumes that the

All of these

Sensible heat differences are small, because the temperature changes from tray to tray is small

Liquid/vapor loading across the column remains constant

Trouton's rule is applicable

All of these

Sensible heat differences are small, because the temperature changes from tray to tray is small

Liquid/vapor loading across the column remains constant

Trouton's rule is applicable

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Process Equipment and Plant Design
__________ closure is the weakest enclosure for cylindrical vessels.

Elliptical

Hemispherical

Conical or flat plate

Torispherical

Elliptical

Hemispherical

Conical or flat plate

Torispherical

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Process Equipment and Plant Design
Ratio of tube length to shell diameter for a shell and tube heat exchanger is

4 : 1 to 8 : 1 for liquid-liquid exchanger

Both B & C

8 : 1 to 12 : 1 for both liquid-liquid and gas-gas heat exchangers

< 4 : 1 for gas-gas exchangers

4 : 1 to 8 : 1 for liquid-liquid exchanger

Both B & C

8 : 1 to 12 : 1 for both liquid-liquid and gas-gas heat exchangers

< 4 : 1 for gas-gas exchangers

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Process Equipment and Plant Design

Process Equipment and Plant Design Smoker's equation for the calculation of number of equilibrium stages in a continuous binary distillation column is used, when the

Process Equipment and Plant Design Apex angle of conical heads used in the bottom heads of chemical process equipments is usually

Process Equipment and Plant Design Factor of safety (i.e., overdesign factor) in heat transfer equipments is about __________ percent more than the actual/theoretical design factor.

Process Equipment and Plant Design Mc Cable Thiele method used for finding theoretical stages in a distillation column assumes that the

Process Equipment and Plant Design __________ closure is the weakest enclosure for cylindrical vessels.

Process Equipment and Plant Design Ratio of tube length to shell diameter for a shell and tube heat exchanger is

Process Equipment and Plant Design
Smoker's equation for the calculation of number of equilibrium stages in a continuous binary distillation column is used, when the

Process Equipment and Plant Design
Apex angle of conical heads used in the bottom heads of chemical process equipments is usually

Process Equipment and Plant Design
Factor of safety (i.e., overdesign factor) in heat transfer equipments is about __________ percent more than the actual/theoretical design factor.

Process Equipment and Plant Design
Mc Cable Thiele method used for finding theoretical stages in a distillation column assumes that the

Process Equipment and Plant Design
__________ closure is the weakest enclosure for cylindrical vessels.

Process Equipment and Plant Design
Ratio of tube length to shell diameter for a shell and tube heat exchanger is