PROCESS EQUIPMENT AND PLANT DESIGN QUIZ

44055

3.5 to 7.0

0.3 to 0.8

1.25 to 3.125

(d1 + d2)/d1

D2/(d1 + d2)

D1/(d1 + d2)

(d1 + d2)/d2

Smaller reactor should come first

None of these

Larger reactor should come first

Equal sized reactors are the best

About 0.33 times

About 3 times

Same

Less

4(0.86p² - πd²)/πd

4(0.86p² - πd²/4)/πd

(p² - πd²/4)/πd

(4p² - πd²/4)/πd

Minimum recommended downcomer residence time for the disengagement of entrained vapour is the same for both foaming and non-foaming liquids, which is about 20 seconds

An increased weir height improves the tray efficiency at the cost of high plate pressure drop; optimum wear height being 40-90 mm for column pressure above atmospheric and 6-12 mm for vacuum columns

For segmental downcomers, the chord length is 60-80% of the column diameter. An initial value of downcomer area of 12% is taken in the design

Width of the calming section provided at the inlet and outlet sides of the plate is 75 mm for column diameter below 1.5 metres and 100 mm for larger diameter columns

Minimum cleaning lane of 6.5 mm is provided, when tubes are on a square pitch

All of these

Minimum tube sheet thickness (in which tubes are fixed) is equal to the O.D. of the tube upto 15 mm tube diameter; and for > 15 mm tube diameter, tube sheet thickness is smaller than tube diameter

O.D. of the tube is 6 to 40 mm while the tube lengths used are 0.5, 2.5, 3.0, 4.0, 5.0, 6 metres

< 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

Disk and doughnut baffle

75% cut segmental baffle

Orifice baffle

25% cut segmental baffle

Heat transfer between corrosive fluids

Co-current heat transfer systems

Cases where temperature difference between the shell and the tubes is more (>50°C)

Counter-current heat transfer systems