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HW # 6 /Tutorial # 6
WRF Chapter 20; WWWR Chapters 21 & 22
ID Chapters 10 & 11
• Tutorial # 6
• WRF#20.6; WWWR #21.13, 21.14; WRF#20.7; WWWR# 21.19. 22.3,
• 22.15.• Hint: 21.13: You may neglect the
temperature drop across the tube wall. Suggested initial guess: Tw = 58oC, Ti(out) = 36oC.
• To be discussed during the week 2 - 6 March, 2020.
• By either volunteer or class list.
• Homework # 6 (Self-practice)
• WWWR # 21.17 Correction:
“If eight tubes of the size designated in Problem WRF 20.7.”
• ID # 10.54
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Boiling and Condensation
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Boiling
Two basic types of boiling:
• Pool boiling
– Occurs on heated surface submerged in a liquid pool
which is not agitated
• Flow boiling
– Occurs in flowing stream
– Boiling surface may be a portion of flow passage
– Flow of liquid and vapor important type of 2 phase
flow
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Regimes of Boiling
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Regime 1:
• Wire surface temperature is only a few degrees
higher than the surrounding saturated liquid
• Natural convection currents circulate the
superheated liquid
• Evaporation occurs at the free liquid surface as the
superheated liquid reaches that position
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Regime 2:
• Increase in wire temperature is accompanied by
the formation of vapor bubbles on the wire surface
• These bubbles form at certain surface sites, where
vapor bubble nuclei are present, break off and
condense before reaching the free liquid surface
At a higher surface temperature, as in regime III, larger and more
numerous bubbles form, break away from the wire surface, rise,
and reach the free surface. Regimes II & III are associated with
nucleate boiling.
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Regime IV:
• Beyond the peak of the curve the transition boiling
regime is entered.
• A vapor film forms around the wire, and portions
of this film break off and rise, briefly exposing a
portion of the wire surface
• This film collapse and reformation and this
unstable nature of the film is characteristic of the
transition regime.
• When present, the vapor film provides a
considerable resistance to heat transfer, thus the
heat flux decreases.
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Correlations of Boiling Heat-
Transfer Data
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( )L Vb
gD
Nub = Cfc Rebm PrL
n Refer to Appendix 6 for Detailed Derivation.
surface tension
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As confirmed by Cengel 2007
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Condensation
• Occurs when a vapor contacts a surface
which is at a temperature below the
saturation temperature of the vapor.
• When the liquid condensate forms on the
surface, it will flow under the influence of
gravity.
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• Film Condensation
•Normally the liquid wets the surface, spreads out and forms a
film.
• Dropwise Condensation
•If the surface is not wetted by the liquid, then droplets form and
run down the surface, coalescing as they contact other
condensate droplets.
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Film Condensation:
Turbulent-Flow Analysis
• It is logical to expect the flow of the condensate
film to become turbulent for relatively long
surfaces or for high condensation rates.
• The criterion for turbulent flow is a Reynolds
number for the condensate film.
• In terms of an equivalent diameter, the
applicable Reynolds number is
Re = 4A Lu
P mf
41 ; 1; 4
44Re
L avg L avg
f f
AA P
P
v vA
P
m m
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44Re
L avgc
f f
V
m m
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44Re
L avgc
f f
V
m m
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Dropwise Condensation
Dropwise Condensation
• Associated with higher heat-transfer
coefficients than filmwise condensation
phenomenon.
• Attractive phenomenon for applications
where extremely large heat-transfer rates
are desired.
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Heat Transfer Equipment
• Single-pass heat exchanger – fluid flows through
only once.
• Parallel or Co-current flow – fluids flow in the
same direction.
• Countercurrent flow or Counterflow - fluids flow
in opposite directions.
• Crossflow – two fluids flow at right angles to one
another.
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Double pipe heat exchanger (A) and
crossflow heat exchanger (B)
A B
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Shell-and-tube Arrangement
• E.g. Tube-side fluid makes two passes, shell-side fluid
makes one pass.
• Good mixing of the shell-side fluid makes one pass.
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Log-Mean Temperature Difference
• Temperature profiles for single-pass double-pipe heat
exchanger
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Counterflow analysis
• Temperature vs. contact area
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Log-Mean Temperature Difference (continued)
• First-law-of-thermodynamics
• Energy transfer between the two fluids
. .
p c p H
c H
q mC T mC T
. .
p c c c p H H H
c H
dq mC dT C dT mC dT C dT
( )
( )
H C
H C H C
dq UdA T T
T T T d T dT dT
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Log-Mean Temperature Difference (continued)
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Log-Mean Temperature Difference (continued)
q = U*T*dA
CH* (TH2-TH1) = q
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Log-Mean Temperature Difference (continued)
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Example #1 (continued)
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Shell-and-Tube Heat Exchanger (1)
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Shell-and-Tube Heat Exchanger (2)
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Shell-and-Tube Heat Exchanger (3)
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Shell-and-Tube Heat Exchanger (4)
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Cross Flow Heat Exchanger (1)
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Cross Flow Heat Exchanger (2)
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Cross Flow Heat Exchanger (3)
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Example # 2
350
375
280 375
280 311.1
350 375
S, H, Water 280 -> 311.1
T, C, Oil 375-> 350