A. All tanks irrespective of their heights and diameters
C. Small diameter tall tanks
D. Small diameter tanks
A. More than
B. Not greater than
C. Not less than one fifth of
A. Three fourth
C. Half
D. 1.5 times
A. Surface area to volume
B. Surface area to perimeter
D. Perimeter to surface area
A. 8 : 1 to 12 : 1 for both liquid-liquid and gas-gas heat exchangers
B. 4 : 1 to 8 : 1 for liquid-liquid exchanger
C. < 4 : 1 for gas-gas exchangers
A. Nu = 0.023 Re0.8. Pr0.4
B. Nu = 2Gz0.5
D. Nu = (?/2) Gz
A. None of these
B. Are less prone to fouling
C. Are easier to clean
A. Pitch
B. None of these
D. Back pitch
A. Noise
C. Turbulence
D. Temperature
A. 48.25
B. 35.5
C. 43.75
B. Liquid flow rate from the surface
C. Condensation rate
D. Surface configuration
A. Pr and Gr
C. Re and Sc
D. Re and Gr
A. Very large vapour space is necessary
B. Bubbles from heating surface are absorbed by the mass of the liquid
D. Temperature of the heating surface is less than the boiling point of the liquid
A. current
B. Flow outside the tube, when the flow is counter-current and inside the tube when the flow is
C. Preferably flow outside the tube
D. Flow at a very slow velocity
A. Remains constant
C. Increases very rapidly
D. Increases linearly
A. 1/A
B. 1/?
C. t
A. Nucleate
B. Pool
C. Saturated
A. ?
B. 0
C. < 1
B. Purge the condenser
C. Facilitate easy cleaning of tubes
B. Because of its low cost
C. In low range of temperature differences
D. To prevent corrosion of the tube bundles
A. gD2??t?/?2
B. gD3??tP2/?
C. gD2??tP2?
A. Sherwood number
B. Stanton number
C. Nusselt number
B. Liquor is inside the tube while the steam is outside the tube
C. Tube dia of 2.5-7.5 cms, tube length of 75-200 cms and cylindrical drum dia of 1-6 metres are
D. mally used
E. rounding tube
F. Area of central downtake is equal to 40 to 100% of total cross-sectional area of the
A. Viscosity of the gas and inversely as density of the gas
D. Density of the gas, but is independent of the viscosity of the gas
A. Heat flux
D. Temperature difference
A. 0.5
B. 0.4
C. 0.6
C. Wet
D. Supersaturated
B. Form friction
C. Both A. and B.
D. Turbulent flow
A. Temperature difference
B. Thermal conductivity
C. Heat transfer area
A. Corrosive
B. Salty
C. Scaling
A. Pressure
B. Viscosity
C. Corrosiveness & fouling characteristics
A. ?(A1 + A2)
C. 2 ?(A1 . A2)
D. ?(A1 . A2)
A. 970
B. 3.97
C. Data insufficient, cant be predicted
A. Sensible heat differences are small, because the temperature changes from tray to tray is small
B. Liquid/vapor loading across the column remains constant
D. Troutons rule is applicable
A. Decreases
B. May increase or decrease, depends on the vacuum
D. Remain constant
A. Buoyancy of the bubbles produced at active nucleation site
C. Existence of thermal boundary layer
D. Temperature gradient produced due to density difference
A. Tar dolomite bricks followed by asbestos
B. Cotton followed by aluminium foil
C. Fireclay refractory followed by aluminium sheet
B. Multipass fixed tube sheet
C. None of these
D. Single pass fixed tube sheet
B. 2-4 heat exchanger
C. 3-2 heat exchanger
D. 1-2 heat exchanger
B. 894 W/m2.K
C. 287 W/m2.K
D. 1200 W/m2.K
A. Gases to be heated/cooled is normally routed through the shell side, because the corrosion
B. Presence of a non-condensable gas decreases the condensing film co-efficient
C. rosive in nature
D. Gases under high pressure are routed through the tube side, because high pressure gases are
F. sed by the cooling water or steam condensate remain localised to the tubes
A. is more accurate in finding the number of equilibrium stages
B. s method
D. accounts for the enthalpy changes in the process
E. Facilitates direct calculation of heat load on reboiler & condenser from, the diagram used in
A. At a particular temperature
D. For circular bodies
A. 0 and 1
B. 1 and ?
C. 0 and 0.5
A. 0.5 d
B. d
C. 2.5 d
A. Colburn
C. Von-Karman
D. Reynolds
A. J.m-2.K-1
B. J.m-1.K-1
C. W.m-2.K-1
B. 1.2 Aa = 1.2 Sa
C. Aa = 1.5 Sa
D. Sa = 1.5 Aa
A. Absorb or emit
B. Refract
C. Reflect
A. 2
C. 2-Jan
D. 4
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