Local heat-transfer coefficients for condensation of steam ...
BOLING AND CONDENSATION HEAT TRANSFER
Transcript of BOLING AND CONDENSATION HEAT TRANSFER
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BOILING AND
CONDENSATION
Boiling – The change from the liquid to the vapor state is sustained by heat
transfer from the solid surface.
Condensation – The change from the vapor to the liquid state results in heat
transfer to the solid surface.
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CONVECTION PROCESSES OF BOILING ANDCONDENSATION
Boiling Modes
• When evaporation occurs at a solid-liquid interface, it is termed boiling• Heat is transferred from the solid surface to the liquid
q”s = h (Ts – Tsat) = h ΔTe , ΔTe = excess temp.
• The process is characterized by the formation of vapor bubbles
• Boiling may occur under various conditions:
i) Pool boiling- process in which the heating surface is submerged in a large
body of stagnant liquid
ii) Forced convection boiling
- fluid motion is induced by external means as well as by free
convection and bubble induced mixing
iii) Subcooled boiling
- the temp.of the liquid is below the saturation temp. and
bubbles formed at the surface may condensed in liquid
iv) Saturated boiling
- the temp. of the liquid slightly exceeds the saturation temp.
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Homeworks
Describe briefly the boiling regimes as shown above
(Figure 10.4)
Explain briefly the forced convection boiling flow
regimes as shown above (Figure 10.8)
Submit: 23rd of September 2010
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Pool Boiling Correlations
Nucleate Pool Boiling Correlation:
– The coefficient Cs,f and the exponent n depend on the solid-liquid combination and representative
experimentally determined values are presented in Table 10.1
• Critical Heat Flux
– For horizontal plates (C = 0.149)
– For sphere, large horizontal cylinders and large finite heated surfaces (C = 0.131)
• Minimum Heat Flux
C = 0.09
All properties are evaluated at the saturation temperature.
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Pool Boiling Correlations
• Film Pool Boiling Correlation:
– For horizontal cylinders (C = 0.62)
–For spheres (C = 0.67)
Vapor properties are evaluated at the film temperature, Tf = (Ts + Tsat)/2 and the liquid density is evaluated
at the saturation temperature (Tsat).
At Ts ≥ 300°C, radiation across the vapor film becomes significant. To calculate total heat transfer
coefficient:
The effective radiation coefficient is expressed as
( )sats
4sat
4s
rad TT
TTεσ
=h
ε = emissivity of the solid (Table A.11)
σ = Stefan-Boltzman constant
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PROBLEM 10.10 – Nucleate Boiling
PROBLEM 10.27 – Film Boiling
EXAMPLES:
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CONDENSATION : PHYSICAL MECHANISMS
• Condensation occurs when the temperature of a vapor is reduced below its saturation temperature
• The latent energy of the vapor is released, heat is transferred to thesurface and the condensate is formed
• Modes of Condensation :
i) Film condensation (Figure 10.9 a)
- occurs in clean and uncontaminated surfaceii) Dropwise condensation (Figure 10.9 b)
- occurs in coated surface with a substance that inhibits wetting
- the drops form in crack, pits and cavities on the surface
iii) homogenous condensation (Figure 10.9 c)- vapor condenses out as droplets suspended in a gas phase to
form a fog
iv) direct contact condensation (Figure 10.9 d)
- occurs when vapor is brought into contact with a cold liquid
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LAMINAR CONDENSATION ON A VERTICALPLATE
• For laminar film condensation, the total condensation rate may bedetermined from the relation :
m = q q = total heat transfer to the surface
h’fg • The total heat transfer to the surface is
q = hL A (Tsat – Ts)
• The average Nusselt number :NuL = hL L = 0.943 ρℓ g (ρℓ - ρ v ) h’fg L3 1/4
k μℓk ℓ (Tsat – Ts)
• Heat of vaporization, h’fg
h’fg = hfg (1 + 0.68Ja)Ja = CPℓ (Tsat – Ts)
hfg
* All liquid properties (ρℓ , μℓ , CPℓ , k ℓ) should be evaluated at the filmtemperature, Tf = (Tsat – Ts)/2 and ρ v and hfg should be evaluated at Tsat *
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TURBULENT FILM CONDENSATION• To check the flow conditions, Reynolds number may be expressed as
Reδ = 4m = 4ρℓ Um δ
μℓ b μ ℓ
• For Laminar Wave – free Region:hL (υℓ
2/g)1/3 = 1.47 Reδ-1/3 , Reδ ≤ 30
k ℓ • For Laminar Wavy Region :
hL
(υℓ
2/g)1/3 = Reδ
, 30 ≤ Reδ ≤ 1800
k ℓ 1.08 Reδ1.22 – 5.2
• For Turbulent Region :
hL (υℓ2/g)1/3 = Reδ
, Reδ ≥ 1800
k ℓ 8750 + 58Pr-0.5 (Reδ
0.75 – 253)
L
b
Laminar wave-free region (Re ≤ 30)
Laminar wavy region (30 ≤ Re ≤ 1800)
Turbulent region (Re ≥ 1800)
υℓ = μℓ /ρℓ g = 9.81 m/s2
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• To determine the value of Reynolds number,
Reδ :
( )
( )
( )
( )
( )( )1800 ≥Re 253+Pr 151Pr +
g/υhμ
TTLk069.0=Re
1800 ≤Re ≤30 8.4+g/υhμ
TTLk70.3=Re
30 ≤Re g/υhμ
TTLk78.3=Re
δ345.05.0
312'fg
ssatδ
δ
82.0
312'fg
ssatδ
δ
43
312'fg
ssatδ
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FILM CONDENSATION ON RADIAL SYSTEMS
• Laminar film condensation on the outer surface of a sphere may be
expressed as :hD = 0.826 g ρℓ (ρℓ - ρ v ) k ℓ
3 h’fg ¼
μℓ (Tsat – Ts) D
• Laminar film condensation on the outer surface of a horizontal tube:
hD = 0.729 g ρℓ (ρℓ - ρ v ) k ℓ3 h’fg
¼
μℓ (Tsat – Ts) D
• For N horizontal tubes :
hD,N = 0.729 g ρℓ (ρℓ - ρ v ) k ℓ3 hfg
¼
Nμℓ (Tsat – Ts) D
hD,N = hDN-1/4 , hD = heat transfer coefficient for thefirst (upper) tube
h’fg = hfg [1 + 0.68 Ja] , Ja = CPℓ (Tsat – Ts)
hfg
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FILM CONDENSATION IN HORIZONTAL TUBES
• For low vapor velocities :Reυ,i = ρυ um,υ D < 35,000
μυ i
• Laminar film condensation in the inner surface of a horizontal tubemay be expressed as :
hD = 0.555 g ρℓ (ρℓ - ρ v ) k ℓ3 h’fg ¼
μℓ (Tsat – Ts) D
h’fg = hfg + 3 CPℓ (Tsat – Ts)
8
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DROPWISE CONDENSATION
• For drop wise condensation :hdc = 51104 + 2044 Tsat (°c) , 22°c ≤ Tsat ≤ 100°c
hdc = 255510 , Tsat ≥ 100°c
• All liquid properties are evaluated at the film temperature
Tf = (Tsat + Ts)/2
• ρυ and hfg are evaluated at Tsat
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PROBLEM 10.47
Saturated ethylene glycol vapor at 1 atm is exposed to a vertical plate
300 mm high and 100 mm wide having a uniform temperature of 420 K.Estimate the heat transfer rate to the plate and the condensation rate. Approximate the liquid properties as those corresponding to saturated
conditions at 373 K (Table A.5)
Example – Film condensation on vertical plate
Example – Film condensation on radial system
PROBLEM 10.55
A horizontal tube of 50mm diameter with a surface temperature of 34°c isexposed to steam at 0.2 bar. Estimate the condensation rate and heat transferrate per unit length of the tube?