The overall heat transfer co-efficient for a shell and tube heat exchanger for clean surfaces is U0 = 400 W/m².K. The fouling factor after one year of operation is found to be hd0 = 2000 W/m².K. The overall heat transfer co-efficient at this time is

Heat Transfer
The overall heat transfer co-efficient for a shell and tube heat exchanger for clean surfaces is U0 = 400 W/m².K. The fouling factor after one year of operation is found to be hd0 = 2000 W/m².K. The overall heat transfer co-efficient at this time is

894W/m².K

1200W/m².K

333W/m².K

287 W/m².K

894W/m².K

1200W/m².K

333W/m².K

287 W/m².K

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Heat Transfer
Dietus-Boelter equation cannot be used for molten metals mainly due to its very low

Grashoff number

Prandtl number

viscosity

thermal conductivity

Grashoff number

Prandtl number

viscosity

thermal conductivity

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Heat Transfer
Grashhoff number is given by

gD2βΔtP²μ

gD³.β.Δtρ²/μ²

gD³βΔtP²/μ

gD2βΔtρ/μ²

gD2βΔtP²μ

gD³.β.Δtρ²/μ²

gD³βΔtP²/μ

gD2βΔtρ/μ²

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Heat Transfer
The thermal boundary layer at NPr > 1

Is thinner than hydrodynamic boundary layer

And the hydrodynamic boundary layer are identical

Disappears

Is thicker than hydrodynamic boundary layer

Is thinner than hydrodynamic boundary layer

And the hydrodynamic boundary layer are identical

Disappears

Is thicker than hydrodynamic boundary layer

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Heat Transfer
The average heat transfer co-efficient for laminar film condensation on vertical surface is inversely proportional to (where, ΔT = Temperature drop across condensate film )

ΔT

(ΔT)1/4

None of the listed here

(ΔT)2

ΔT

(ΔT)1/4

None of the listed here

(ΔT)2

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Heat Transfer
Tubes are held between top and bottom tube sheets in Calenderia type evaporator by keeping

Both the tube sheets fixed

Both the tube sheets floating

The top tube sheet fixed and the bottom tube-sheet floating

The top tube sheet floating and bottom tube sheet fixed

Both the tube sheets fixed

Both the tube sheets floating

The top tube sheet fixed and the bottom tube-sheet floating

The top tube sheet floating and bottom tube sheet fixed

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Heat Transfer

Heat Transfer The overall heat transfer co-efficient for a shell and tube heat exchanger for clean surfaces is U0 = 400 W/m².K. The fouling factor after one year of operation is found to be hd0 = 2000 W/m².K. The overall heat transfer co-efficient at this time is

Heat Transfer Dietus-Boelter equation cannot be used for molten metals mainly due to its very low

Heat Transfer Grashhoff number is given by

Heat Transfer The thermal boundary layer at NPr > 1

Heat Transfer The average heat transfer co-efficient for laminar film condensation on vertical surface is inversely proportional to (where, ΔT = Temperature drop across condensate film )

Heat Transfer Tubes are held between top and bottom tube sheets in Calenderia type evaporator by keeping

Heat Transfer
The overall heat transfer co-efficient for a shell and tube heat exchanger for clean surfaces is U0 = 400 W/m².K. The fouling factor after one year of operation is found to be hd0 = 2000 W/m².K. The overall heat transfer co-efficient at this time is

Heat Transfer
Dietus-Boelter equation cannot be used for molten metals mainly due to its very low

Heat Transfer
Grashhoff number is given by

Heat Transfer
The thermal boundary layer at NPr > 1

Heat Transfer
The average heat transfer co-efficient for laminar film condensation on vertical surface is inversely proportional to (where, ΔT = Temperature drop across condensate film )

Heat Transfer
Tubes are held between top and bottom tube sheets in Calenderia type evaporator by keeping