final press-rev-linkedin
TRANSCRIPT
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CFD Analysis of Pool Boiling over Microstructures
Final presentation of simulation results
By: Yashar Seyed Vahedein
December 12, 2013
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Pure-Heat conduction model
1.Transient conduction
model
2.Mesh-size is optimized
Pure-Heat conduction model
๐๐จ๐ง๐ฌ๐ญ๐๐ง๐ญ ๐ก๐๐๐ญ ๐๐ฅ๐ฎ๐ฑ=๐๐๐๐๐ /๐ฆ๐
๐ ๐
Insulated Walls
0.1m
0.1
m
3
Transient convection
๐๐จ๐ง๐ฌ๐ญ๐๐ง๐ญ ๐ก๐๐๐ญ ๐๐ฅ๐ฎ๐ฑ=๐๐๐๐๐ /๐ฆ๐
๐ ๐
Insulated Walls
0.1m0.
1 m
Heat convection due to movement of liquid โ(temperature dependent density)
โข Calculation of the heat transfer coefficient (h) Vs. Time
โข Calculation of Nusselt Number from the correlations and simulation
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Natural Convection Results
Temperature over time on the surface
0 500 1000 1500 2000 2500 3000 3500 4000 4500290
300
310
320
330
340
350
360
370
f(x) = 7.76637775931171 ln(x) + 288.925301114463
Temperature over time On heater surface
Logarithmic (Tempera-ture over time On heater surface)
Time/ฮt
Tem
pera
ture
(K)
โ ๐=๐ .๐๐ฌ
Nu(from simulation)
27.94206885
Nusselt Number (from correlation)
66.4535
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Two-phase Flow Simulation Technique- Volume of Fluid
Cavity-Finer Mesh โ 0.715 mm
Rest of the surface โ Taken as Y axis
How volume of fluid explains a cell consisting of two fluids (phases)
In this model , phase 0 is liquid water and phase 1 is vapor water
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Current Problem Definition and Objectives
Cavity size
Vapor Inlet-Type: Mass flow rate
Liquid
Bubble interface โ use of VOF in this modelW/out Phase Change
VOF, By โHirt and Nichols 1982โ.
1. Validating simulationโข Match bubble shape and
diameter with experimental data.
2. Finding influence area caused by bubble departure โข Use shear stress over the surface.
3. Finding influence on heat transfer โข Use heat transfer coefficient of
the surface
1.43 mm
Axis of symmetry
25mm
50mm
Using Axisymmetric model
๐๐๐๐ ๐ก๐๐๐ก๐ โฒ โฒ=10000๐๐2
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Experimental data from the literature
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Time and diameter of the first bubble departure (from simulation)
โข mm
(observed for 8 departures)
Necking
Onset of Departure
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Validation of the Numerical Results
Theoretical Bubble Departure Diameter
(1)
(2)
(3)
Using Cole and Rohsenow 1969
ExperimentBaines and Mori
Simulation
1 ๐ต๐๐๐๐ ๐๐๐๐๐๐๐ ,2000
Max. error = 9%
Comparison of Bubble Shape
Comparison of Bubble Departure Diameter
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Comparing Bubble diameter in t= 40 ms -start of the necking- and t=42.25 ms โ near departure
Comparing the bubble shape and diameter with experimental results over
time
t= 40.0 ms
t= 42.2 ms
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Temperature distribution during bubble departure and growth
During the growth of next bubble t=280.4 ms
On the moment of departure t=253 ms
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Effect of Necking on Shear Stress
โข Direction of shear is coupled with the interface
โข Change in velocity enforce the change in shear stress
Receding interface
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Finding influence area on heated wall using shear stress
t= 40.0 ms
t= 42.5 ms
t= 44.5 ms
Influence region โclose to (Rohsenow, Mikic, Griffith 1969)
Increase in shear stress
2๐ท๐
1.82๐ท๐
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Finding the Local heat transfer coefficient on the surface
t= 40.0 ms
t= 42.5 mst= 44.5 ms
t= 49.5 ms
Increase in heat transfer coefficient near departing bubble (micro convection)
h= ๐ โฒ โฒ
๐ ๐ ๐ข๐๐๐๐๐โ๐ ๐ ๐๐ก
Future work: Introducing embedded boiling codes to the same VOF-
method.
Heat generation will be supplied to cavity
surface
Liquid
Cavity with connected
walls-
Modeling Phase change using
embedded boiling code or FT method
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