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3/7/05ME 2591 ME 259 Heat Transfer Lecture Slides III Dr. Gregory A. Kallio Dept. of Mechanical...
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Transcript of 3/7/05ME 2591 ME 259 Heat Transfer Lecture Slides III Dr. Gregory A. Kallio Dept. of Mechanical...
3/7/05 ME 259 1
ME 259Heat Transfer
Lecture Slides III
Dr. Gregory A. Kallio
Dept. of Mechanical Engineering, Mechatronic Engineering & Manufacturing Technology
California State University, Chico
3/7/05 ME 259 2
Transient Conduction
Reading: Incropera & DeWitt
Chapter 5
3/7/05 ME 259 3
Introduction
Transient = Unsteady (time-dependent ) Examples
– Very short time scale: hot wire anemometry (< 1 ms)
– Short time scale: quenching of metallic parts (seconds)
– Intermediate time scale: baking cookies (minutes)
– Long time scale – daily heating/cooling of atmosphere (hours)
– Very long time scale: seasonal heating/cooling of the earth’s surface (months)
3/7/05 ME 259 4
Governing Heat Conduction Equation
Assuming k = constant,
For 1-D conduction (x) and no internal heat generation,
Solution, T(x,t) , requires two BCs and an initial condition
t
T
k
qT
12
t
T
x
T
1
2
2
3/7/05 ME 259 5
The Biot Number
The Biot number is a dimensionless parameter that indicates the relative importance of of conduction and convection heat transfer processes:
Practical implications of Bi << 1: objects may heat/cool in an isothermal manner if– they are small and metallic– they are cooled/heated by natural
convection in a gas (e.g., air)
convt
condt
R
R
hA
kALk
hLBi
,
, 1
3/7/05 ME 259 6
The Lumped Capacitance Method (LCM)
LCM is a viable approach for solving transient conduction problems when Bi<<1
Treat system as an isothermal, homogeneous mass (V) with uniform specific heat (cp)
For suddenly imposed, uniform convection (h, T) boundary conditions, solution yields:
where
ti
tTT
TtT
exp)(
s
pt hA
c V
3/7/05 ME 259 7
General LCM
LCM can be applied to systems with convection, radiation, and heat flux boundary conditions and internal heat generation (see eqn. 5.15 for ODE)
– Forced convection, h = constant– Natural convection, h = C(T-T)1/4
– Radiation (eqn. 5.18)– Convection and radiation (requires
numerical integration)– Forced convection with constant surface
heat flux or internal heat generation (eqn. 5.25)
(Note that the Biot number must be redefined when effects other than convection are included)
3/7/05 ME 259 8
Spatial Effects (Bi 0.1)
LCM not valid since temperature gradient within solid is significant
Need to solve heat conduction equation with applied boundary conditions
1-D transient conduction “family” of solutions:
– Uniform, symmetric convection applied to plane wall, long cylinder, sphere (sections 5.4-5.6)
– Semi-infinite solid with various BCs (section 5.7)
– Superposition of 1-D solutions for multidimensional conduction (section 5.8)
3/7/05 ME 259 9
Convection Heat Transfer: Fundamentals
Reading: Incropera & DeWitt
Chapter 6
3/7/05 ME 259 10
The Convection Problem
Newton’s law of cooling (convection)
“h” is often the controlling parameter in heat transfer problems involving fluids; knowing its value accurately is important
h can be obtained by– theoretical derivation (difficult)– direct measurement (time-consuming)– empirical correlation (most common)
Theoretical derivation is difficult because– h is dependent upon many parameters– it involves solving several PDEs– it usually involves turbulent fluid flow, for which no
unified modeling approach exists
)( TThq ss
3/7/05 ME 259 11
Average Convection Coefficient
Consider fluid flow over a surface:
Total heat rate:
If h = h(x), then
)(
1)(
)(
TTAh
hdAA
ATT
hdATTdAqq
ss
A
ss
ss
A A
sss
s
s s
Ldxh
Lh
0
1
3/7/05 ME 259 12
The Defining Equation for h
The thermal boundary layer:
From Fourier’s law of conduction:
Setting qconv = qcond and solving for h:0
0
y
fluidfluid
y
solidsolids
y
Tk
y
Tkq
TT
yT
k
hs
y 0
3/7/05 ME 259 13
Determination of
Need to find T(x,y) within fluid boundary layer, then differentiate and evaluate at y = 0
T(x,y) is obtained by solving the following conservation equations:– Mass (continuity) ……. Eqn (6.25)– Momentum (x,y) ……. Eqn (6.26, 6.27)– Thermal Energy …….. Eqn (6.28a,b)
Solution of these four coupled PDEs yields the velocity components (u,v), pressure (p), and temperature (T)
Exact solution is only possible for laminar flow in simple geometries
0
yyT
3/7/05 ME 259 14
Boundary Layer Approximations
Because the velocity and thermal boundary layer thicknesses are typically very small, the following BL approximations apply:
The BL approximations with the additional assumptions of steady-state, incompressible flow, constant properties, negligible body forces, and zero energy generation yield a simpler set of conservation equations given by eqns. (6.31-6.33).
x
T
y
T
x
v
y
v
x
u
y
u
vu
,,
3/7/05 ME 259 15
Boundary Layer Similarity Parameters
BL equations are normalized by defining the following dimensionless parameters:
where L is the characteristic length of the surface and V is the velocity upstream of the surface
The resulting normalized BL equations (Table 6.1) produce the following unique dimensionless groups:
Note: all properties are those of the fluid
2,
/,/
/,/
V
pp
TT
TTT
VvvVuu
LyyLxx
s
s
pc
k
VL
and where
number Prandtl
number Reynolds
(Pr)
(Re)
3/7/05 ME 259 16
Boundary Layer Similarity Parameters, cont.
Recall the defining equation for h:
The normalized temperature gradient at the surface is defined as the Nusselt number, which provides a dimensionless measure of the convection heat transfer:
00
yys y
T
L
k
y
T
TT
kh
k
hLNu
3/7/05 ME 259 17
The Nusselt Number
The normalized BL equations indicate that
Since the Nusselt number is a normalized surface temperature gradient, its functional dependence for a prescribed geometry is
Recalling that the average convection coefficient results from an integration over the entire surface, the x* dependence disappears and we have:
dx
dpyxfT Pr,Re,,,
Pr)Re,,( xfNu
Pr)(Re,fk
LhNu
3/7/05 ME 259 18
Physical Significance of the Reynolds and Prandtl Numbers
Reynolds number (VL/) represents a ratio of fluid inertia forces to fluid viscous shear forces– small Re: low velocity, low density, small
objects, high viscosity– large Re: high velocity, high density, large
objects, low viscosity Prandtl number (cp/k) represents the ratio of
momentum diffusion to heat diffusion in the boundary layer.– small Pr: relatively large thermal boundary
layer thickness (t > )– large Pr: relatively small thermal boundary
layer thickness (t < ) Note that Pr is a (composite) fluid property that
is commonly tabulated in property tables
3/7/05 ME 259 19
The Reynolds Analogy
The BL equations for momentum and energy are similar mathematically and indicate analogous behavior for the transport of momentum and heat
This analogy allows one to determine thermal parameters from velocity parameters and vice-versa (e.g., h-values can be found from viscous drag values)
The heat-momentum analogy is applicable in BLs when dp*/dx* 0 (turbulent flow is less sensitive to this)
The modified Reynolds analogy states
– where Cf is the skin friction coefficient
60Pr6.0PrRe2
1 3/1 for fCNu
3/7/05 ME 259 20
Turbulence
Turbulence represents an unsteady flow, characterized by random velocity, pressure, and temperature fluctuations in the fluid due to small-scale eddies
Turbulence occurs when the Reynolds number reaches some critical value, determined by the particular flow geometry
Turbulence is typically modeled with eddy diffusivities for mass, momentum, and heat
Turbulent flow increases viscous drag, but may actually reduce form drag in some instances
Turbulent flow is advantageous in the sense of providing higher h-values, leading to higher convection heat transfer rates
3/7/05 ME 259 21
Forced Convection Heat Transfer – External Flow
Reading: Incropera & DeWitt
Chapter 7
3/7/05 ME 259 22
The Empirical Approach
Design an experiment to measure h– steady-state heating– transient cooling, Bi<<1
Perform experiment over a wide range of test conditions, varying:– freestream velocity (u )
– type of fluid (, )– object size (L)
Reduce data in terms of Reynolds, Nusselt, and Prandtl
Pr, Nu , Re
k
LhLuLL
3/7/05 ME 259 23
The Empirical Approach, cont.
Plot reduced data, NuL vs. ReL, for each fluid (Pr):
Develop an equation curve-fit to the data; a common form is
typically: < m < 1 < n < 0.01 < C < 1
nmLL C PrReNu
3/7/05 ME 259 24
Flat Plate in Parallel, Laminar Flow (the Blasius Solution)
Assumptions:– steady, incompressible flow– constant fluid properties– negligible viscous dissipation– zero pressure gradient (dp/dx = 0)
Governing equations
(energy)
(momentum)
y)(continuit 0
2
2
2
2
y
T
y
Tv
x
Tu
y
u
y
uv
x
uu
y
v
x
u
3/7/05 ME 259 25
Blasius Solution, cont.
Similarity solution, where a similarity variable () is found which transforms the PDEs to ODEs:
Blasius derived:
x
uy
3/1
3/12/1
2/1,
Pr
PrRe332.0Nu
Re664.0
Re
5
/
0.5
t
xx
x
xxf
x
k
xh
C
x
xu
3/7/05 ME 259 26
Empirical Correlations
Flat Plate in parallel flow: Section 7.2
Cylinder in crossflow: Section 7.4
Sphere: Section 7.5
Flow over banks of tubes: Section 7.6
Impinging jets: Section 7.7
3/7/05 ME 259 27
Forced Convection Heat Transfer – Internal Flow
Reading: Incropera & DeWitt
Chapter 8
3/7/05 ME 259 28
Review of Internal (Pipe) Flow Fluid Mechanics
Flow characteristics Reynolds number Laminar vs. turbulent flow Mean velocity Hydrodynamic entry region Fully-developed conditions Velocity profiles Friction factor and pressure drop
3/7/05 ME 259 29
Pipe Reynolds Number
um is mean velocity, given by
Reynolds number for circular pipes:
Reynolds number determines flow condition:– ReD < 2300 : laminar
– 2300 < ReD < 10,000 : turbulent transition
– ReD > 10,000 : fully turbulent
DumRe
pipescircular for
4
2D
m
A
mu
cm
Dm4
Re
3/7/05 ME 259 30
Pipe Friction Factor
Darcy friction factor, f, is a dimensionless parameter related to the pressure drop:
For laminar flow in smooth pipes,
For turbulent flow in smooth pipes,
– good for 3000 < ReD < 5x106
For rough pipes, use Moody diagram (Figure 8.3) or Colebrook formula (given in most fluid mechanics texts)
2/
)/(2mu
Ddxdpf
Df Re64
264.1)ln(Re790.0 Df
3/7/05 ME 259 31
Pressure Drop and Power
For fully-developed flow, dp/dx is constant; so the pressure drop ( p) in a pipe of length L is
The pump or fan power (Wp) required to overcome this pressure drop is
– where p is the pump or fan efficiency
52
22 8
2
D
fLm
D
fLup m
, p
p
pmW
3/7/05 ME 259 32
Thermal Characteristics of Pipe Flow
Thermal entry region Thermally fully-developed conditions Mean temperature Newton’s law of cooling
3/7/05 ME 259 33
Newton’s Law of Cooling & Mean Temperature
The absence of a fixed freestream temperature necessitates the use of a mean temperature, Tm, in Newton’s law of cooling:
Tm is the average fluid temperature at a particular cross-section based upon the transport of thermal (internal) energy, Et:
Unlike T , Tm is not a constant in the flow direction; it will increase in a heating situation and decrease in a cooling situation.
)( mss TThq
cA
cvmvt uTdAcTcmE
3/7/05 ME 259 34
Fully-Developed Thermal Conditions
While the fluid temperature T(x,r) and mean temperature Tm(x) never reach constant values in internal flows, a dimensionless temperature difference does - and this is used to define the fully-developed condition:
the following must also be true:
therefore, from the defining equation for h:
i.e., h = constant in the fully-developed region
0
ms
s
TT
TT
x
)( xfTT
rT
TT
TT
r msms
s
)( 0 xf
TT
rTkh
ms
r
3/7/05 ME 259 35
Pipe Surface Conditions
There are two special cases of interest, that are used to approximate many real situations:
1) Constant surface temperature (Ts = const)
2) Constant surface heat flux (q”s = const)
)(xqq ss
)( ),( xTTxTT mmss
3/7/05 ME 259 36
Review of Energy Balance Results
For any incompressible fluid or ideal gas pipe flow,
1) For constant surface heat flux,
2) For constant surface temperature,
3) For constant ambient fluid temperature,
)( mimopconv TTcmq
p
smimo cm
PLqTT
pmis
mos
cm
hPL
TT
TT
exp
tottpmi
mo
RcmTT
TT
,
1exp
3/7/05 ME 259 37
Convection Correlations for Laminar Flow in Circular Pipes
Fully-developed conditions with Pr > 0.6:
– Note that these correlations are independent of Reynolds number !
– All properties evaluated at (Tmi+Tmo)/2
Entry region with Ts = const and thermal entry length only (i.e., Pr >> 1 or unheated starting length):
– combined entry length correlation given by eqn. (8.57) in text
constant) ( 66.3
constant) ( 36.4
s
sD
T
qk
hDNu
8.56) (eqn. PrRe)(04.01
PrRe)(0668.0 66.3 3/2
D
DD
LD
LDNu
3/7/05 ME 259 38
Convection Correlations for Turbulent Flow in Circular Pipes
Fully-developed conditions, smooth wall, q”s = const or Ts = const
– Dittus-Boelter equation - fully turbulent flow only (ReD > 10,000) and 0.7 < Pr < 160
– NOTE: should not be used for transitional flow or flows with large property variation
heating) (fluid for 0.4
cooling) (fluid for 0.3
where
8.60) (eqn. PrRe023.0 5/4
ms
ms
nD
TTn
TTn
Nu
3/7/05 ME 259 39
Convection Correlations for Turbulent Flow in Circular Pipes, cont.
– Sieder-Tate equation - fully tubulent flow (ReD > 10,000),very wide range of Pr (0.7 - 16,700), large property variations
– Gnielinski equation - transitional and fully-turbulent flow (3000 < ReD < 5x106), wide range of Pr (0.5 - 2000)
– f given on a previous slide (eqn. 8.21)
8.61) (eqn. PrRe027.0 14.03/15/4sDNu
8.63) (eqn. )1(Pr)8(7.12 1
Pr)1000)(Re8(3/22/1
f
fNu D
D
3/7/05 ME 259 40
Convection Correlations for Turbulent Flow in Circular Pipes, cont.
Entry Region– Recall that the thermal entry region for
turbulent flow is relatively short, I.e.,only 10 to 60D
– Thus, fully-developed correlations are generally valid if L/D > 60
– For 20 < L/D < 60, Molki & Sparrow suggest
Liquid Metals (Pr << 1)– Correlations for fully-developed turbulent
pipe flow are given by eqns. (8.65), (8.66)
DLNu
Nu
fdD
D 6 1
,
3/7/05 ME 259 41
Convection Correlations for Noncircular Pipes
Hydraulic Diameter, Dh
– where: Ac = flow cross-sectional area
P = “wetted” perimeter
Laminar Flows (ReDh < 2300)
– use special NuDh relations– rectangular & triangular pipes: Table 8.1– annuli: Table 8.2, 8.3
Turbulent Flows (ReDh > 2300)
– use regular pipe flow correlations with ReD and NuD based upon Dh
P
AD ch
4
3/7/05 ME 259 42
Heat Transfer Enhancement
A variety of methods can be used to enhance the convection heat transfer in internal flows; this can be achieved by
– increasing h, and/or– increasing the convection surface area
Methods include– surface roughening – coil spring insert– longitudinal fins– twisted tape insert– helical ribs