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AME2H0D OF CORIMAZDII1G HE&T TRANSF)
30A BURFACE
RAfINO.
tUI
by
Warren m. Robsenovu
A method based an a logical uxplanation of the meani
of beat trans-
fer associated with the boiling process is presented for correlating heat
transfer data for nucleate boiling of liquids for the case of pool boiling.
Tbe suggested relation is
1/As
-
I.7
iere the various fluid properties awe evaluated at the saturation tempera-
Stre correspondinag to the local pressure and C5g is a function of the particu3w eatn
sranfeat for
cbatonetinfov witbout boiling is correrd
Lated by the nomal baselt umaber, Rsynolds umber based on pipe diameter and
Pwaudtl umber.
For pool boiling with essentially saturated liquids, Jakob (1)
rg; dasacusets nstt1 t o
e ocx
a tProessr
shovs that the heat transfew from the surfae is for the most part transferred
directly to the liquid, the increased heat transfew rate assaoiated with boillug being accounted for by the resulting agitation of the fluid by motian ofthe liquid
flowlan
behind the wak. of te bubble departing from the surface.
Ilohsenov and Clark (2) showed a siinrlar result in studying notion piotteres e
M~o~dama (3) for subco.le4 liguldsi
heili
but
?lowicg in luacised convection withi suface
o uet gention of 'eaer-,
Kurtther and greith (4) and Gunther(5)
-2presented photographic evidence that in highly subcooled liquids in pool
boiling and in forced ocnvection with surface boiling, the bubbles oould fona
at the surfaoe pow, and then collapse ile
remaining attached to the sur-
eovertheless the increased heat transfer in boiling we attributed to
face.
The agitation of the liquid by the bubble notion.
As the rate of heat transfer s increased and bubble agitation beemes
more vigorous the effect of forced convoction fluid velocity and hence Reaolds
maber based on pipe diameter becomes less and less.
This effect is showm
by the data of rohsenow and Clark (6) reproduosd here in figures 1 and 2.
Wis data is representative of data of others for surface boiling with forced
convection. In these figures the curves for various fluid velocities are seen
to merge into one curve, showing that as the boiling becaes more vigorous,
the effect of fluid vel<eity disappears.
It seen reasccable then to seek.a
correlation of the heat transfer data by meas of a bubble Reynolds umaber
based on bubble diameter and velocity.
For purposes of analysis one can visualse a number of streams of bubble
receding from the heating surfaoe and a bubble Raynolds nmber defined by
-tlhe mass velocity of the bubbles and their diameter as they leave
111
at
4
numbow *U-16 *
Mis quantity is a measure of the local agitation of the fluid
s0~g
urfaee and hence is analogous to the ordinary pipe Reynolds
s aeasure of the turbulence in the stream.
To eam&$ate te bubble REynolds number, characteristics of bubbles in
pool boiling will be employed since there is more detailed visual evidence
available for this case than there is for forced convection surface boel .
w
3
04
Results of these bubble characterics are ompi4ed by Jakob. (1).
The heat
transfer to the babbles while attached to the surface can be written with
good appradaation (2) as
(2)
f
Ir
Frita (8) presents a relation for the diameter of the bubble as it leaves
the surface, mhich may be written in the fom
Fgi~~awhere
- -o- -m(3)
is the angle of centact of the bubble as sheen in figure 3.
Jakob (9) has shoun for vapor bubbles of water and of carbon tetrachloride
a relation
sdts btmen te frequency of bubble formation at a favored
point ca the smfae and the diter
faco.
of the bubble when it leaves the sur-
Tis relation an be aprcated by the equation
f~c
UC
Coge~mftn
.. amma
W
ithout serious error.
Inspecting the terms of equation (2) in the light of equations (3) and
(4) @hows that (q/A)b is proportonal to a for a given operating pressure, it
-
sin* all other quantities are functions
of saturation pressure alcm. or are oconstant.
Experiments have shown that
bubbles forM at selective points on surface forming swaying cols
of bubbles.
Jakob (7) found that the nmber of celvme or points of origin of bubbles mas
very nearly directly proportional to the rate of heat transfer from the heating
surface for a given operating pressure.
Terefore q/A ~ (q/A)b and cn be
written as
where Cq may be a function of pressure.
The mass velocity of the vapor bubbles leaving the surface may be written as
-
rquettions (3),
-(6)
-
(5) and (6) may be substituted into equation (1) to obtain an
expression for the bubble Reynolds number as
- - - where
Caw
, Gb and n have been eliminated, and CR
5/y$---
is dimensionless and
(7)
The term
.
has the dimensions
radians of angle.
In applying this reasoning to attempt to correlate heat transfer data
in the boiling regime it would seem that a bubble Nusselt number would be
useful, defined as
-I --W
This quantity has been defined and utilised by Jakob (1)(16).
-
-
(8)
Substituting
equation (3) into equation (8) results in
- - - -J(9)
A~-
hre
= ECd
ere, too,, the term
///y
*
f.f)
is.
Sta:e the postalated aechanism of heat transfer indicates that most of'
-
5
-
the heat transfer goes directly from the wall to the liquid, and since the
Prandtl umber is significant in relatiJufor heat transfer to a non-boiling
fluid, it abould probably be included in the oorrelation for beat transfer
to a boiling fluid.
then the correlation suggested is
Nxq
w Np,(10)
jP
where
-/iS1 t, are aln evaluated at the saturation tempers-
C
ture corresponding to the local pressure.
The above relation applieS to the
region of vigorous boiling ihere the fluid velocity or pipe Reynolds number
does not influence the heat transfer rate.
of pool boiling.
It would also apply to the case
In the case of surface boiling with forced convection and
not very vigorous boiling
bere the fluid velocity does influence the heat
transfer rate, some form of a pipe Reynolds number might be added to the right
side of equation (10).
There is some doubt that the ordinary pipe Reynolds
number would be significant because the notdon of the bubbles might tend to
destroy the norml relationship between viscous and inertia forces.
CtStat AnGE.
The bubble contact angles
values of C*
T.
n4 0;
, shown in figure 3, is determined by the
hence it is
fluid and the kind ofheatng suface.
detemined both by the kind of
All of
e other properties in the
expressions- for bubble Reynolds muber and bubble Musselt numbers are fumctions
of the fluid alone.
he angle 9 from 'fire
3 iseen
to be related to the
various surface tensions by the relata
Cos
qv
ioa........
w()
-o - -o -
For lack of available inforimation th" effec-t of pressure on
$
was
*
-
--
disregarded in applying equation (10) to existing data.
This assumption
is equivalent to assuming that the effect of pressure on the values of
and
of figure 3 is such that the angle
a4
pressure.
In applying equation (10) to the correlation of experimental data
the terms CR' Cn and j
Ef- L
remains independent of
will be omitted.
Liauid SubgolUn
In pool boiling the primary region of interest is the case in which
the liquid temperature is essentially at the saturation temperature.
However,
In forced convection with surface boiling the liquid temperature may be greatly
subcooled.
It has been shown by many experimenters that the effect of sub-
cooling of the liquid may be eliminated if the data is pintted as q/A vs T
Hence defining the film coefficient in the
as shown in figures 1 and 2.
bubble Nusselt number ash 1
*
((/A)-i Tx eliminates the necessity of includ-
ing liquid subooling as a variable in a correlation.
OTHER FO3t
F7THE P1DPOSED 00RE1L&TION LUATIMN
Since both the bubble Reynolds number and the bubble Nusselt number
embody a (q/A) term, it will be desirable to employ the tezu
'to
Ce
(12)
This dimer sionless group is the ratio of liquid superheat enthalpy at the
surface temperature to the latent enthalpy of evaporation.
The equation (10) may be replaced by
Pool Boiling:
The proposed correlation equation (13) has been applied to the data of
ni'ous experimenters.
It vll hof
in treat so observi in som deital) ik
application to the data of Addes (10) for pool boiling of water because of
the wide range of pressures covered -- 14.7 psia to 246 5 psia.
In these
experiments degasssed, distilled water was boiled by an electrically heated
Data for a wire diameter of 0.024 inches is shown in
horisontal platima wire.
figure 4a.
A plot of
(q/A)/4
1g q0" 1
vs C
(-,
On this plot the position of the lines rises to a axi-
isshown in figure 4b.
am. with pressure and then falls again.
At the pressure corresponding to the
highest line on this plot, the Prandtl amber is very nearly at its minim
value according to the data tabulated by Welum=
Hence this effect
(11).
appears to be a Prandtl naber effect, which was anticipated in the analysis.
A cross-plot of
/
,
N,,
for constant values of bubble Reynolds
aumber shows the slope of the line on a log-log plot to be approximately 1.7;
hence the final correlation as shown in figure 4c results in an equation of
the form
a~)
'
C
where the value of C
7
-- -----
- (14)
is 0.013 with a spread of data of approximately - 20%.
This process was repeated for some of the data of Cichelli and Bonailla (12)
who boiled various fluids on a polished chroniu :.plated, hortsontal pleate
which was electrically heated.
shown in figures 5 through 7.
form of equation (14).
The results of the preposed correls tion e,e
In each came the resulting equatione are (- tf
Only the data for sing.
component fluids on alcn
surfaces were correlated,
The data of Cryder and Finalborgo (15) i
In every case the correlation equation (14)
of C ,ire
listed in. Table I.
snown correlated in figure 8.
ra6 applietd and the resulting- valuvet
[Eai
Flui an
urface
28f
Water - PlatiM a
Addems(10)
Ciabelli-Banilla(12) Bensene
-
0.013
Crit
0.010
Cichelli-Bonilla(12) Ethyl Alchol - Chromite
0.0027
Cichelli-Bonilla(12) n-Pentane-Cromium
0.015
Cryder-Finalborgo(15) water - Brass
0.0060
&ArgAd
Comeon~wt
Buf
Soilina:
In order to show the effect of forced convection flow on the boiling
process plots of
vs (sifT)
C
t
were
u, made for the sur-
)
face boiling data of Robsenow and Clark (6)(13) for degassed distilled water
flowing in a vertical nickel tube 0.180' diameter 9.4N long and for the data
of Kreith and Suimerfield (4)
for degassed distilled water flowing in a
stainless steel tube 0.587' diameter 17.5' long.
Superimposed on these plots,
figures 9 and 10, is the correlation line for the pooling boiling data for
water from figure 4c.
Lines of constant forced convetion velocity and pressure are seen to
merge toward a single line whicb would probably be parallel to this line for
pool boiling from figure 4a.
When the boiling tecomes more vigorous at the
bigher values of T, the effect of forcd eiuwction fluid velocity apparently
disappears.
In this region the motian o' th- bubbles seem
to control th
mechaniam of heat tasmfer due to fluid egitat.ion.
In these correlations the fluid properties have been evaluated as properties of liquid at the saturation temperature.
This was done both for the case
of pool boiling with saturated liquid and for the case of surface boiling in
forced convection of a subcooled liquid.
Ir. each case the liquid near the
heating surface is very nearly at saturation temperature or possib.; even at
a nestastable superheated temperature. Properties of the liquid were used for
tbe C./
,
and k values in the bubble Nusselt number, the Pr' dti numbor,
ad te new ters
because the heat transfer wa found to occur
imarily by transfer of heat directly from the heating surface to the liquid.
The value of
4
of the bubble Reynolds mabhr was evaluated as a property of
liquid because viscous forces acting to retard the notion of the bubble are
those of the liquid.
The results shown in figures 4 through 10 are essentially plots of q/A
'
'' each muliplied by a judious oabination of fluid properties thus
effecting the correlation.
.mall
changes in T.
It is readily observed that q/A rises rapidly with
FNrthes, the magnitude of Tz is rather mall, being of
the order of 50 ? for water at atMospher
10 F for water at 2000 psia.
pressure and of the order of 5 or
Inallof the data
oorrelated
here the energy
was suplied by electricityj hence T became the dependent variable in each
case.
It is difficult to measure the heating surface temperature directly when
electric heating is employed.
It must be calculated from other measured values
such as outer tube surface temperature or resistance of the heating wire.
The
value of TZ is obtained by subtracting the saturation temperature from this
determined heating surface temperature.
Since the agnitude of T. is s=m1
any errors in the determined value of heating surface temperature will be greaz
magnified in the resulting value of Ty. This can. possibly account for some or'
the cifference in the value of C of equation (14) as obtained by variou
experienters.
It ia, of course, evssntial in obteining a correlation of data that the
p f the fjald employ-ed be n;recZ.
a
error
:n the vaues
i
:
- 10 -
properties is directly reflected in the data correlation.
Probably the most significant cause of the difference in the values of C
is the result of emittiag, for lack of currently available information, the
ters
frm the bubble Reynolds number and the, bubble Nusselt number in
arriving at the oorrelation as applied.
be a fwnotian of P *ih
The effect of this is to cause C to
is deterained by the character of and the kind of
heating surface and by the properties of the fluid as shown by equation (11).
There is then good reason to expect a different value of C to result for every
cimnation of kind of surface and kind of fluid.
Additional infomtion regard-
ing the values of f for various combinations of surfaces and fluids should
clarify this matter and produce a valid correlation for all such combinations.
In arriving at tquation (5) and hence equations (7) and (9), the expressions for bubble Reynolds nmber and bubble lusselt number, it was assumed that
did not vary with pressure for a particular ombination of fluid and
heating surface.
This assption
y account for same of the small spread of
the final correlation for each surface.-fluid combination.
The assumption
appears to be fairly good, nevertheless, since Vie data for a particular fnwidheating surface ocabination is correlated within about t 20% by equation (14).a
It is not suggested that the exponents 0.33 and 1.7 of equation (14) are
the tme values nor that the form of equation (14) is the best one.
Rather i
in suggested that the dimensionless groups -if equation (14) are significant in
correlation boiling heat transfer data,
presented here.
Much more data was correlated than 14n
Only the data for single omponent fluids on clean surface*
are presented here.
They semed to be correlated quite adequately by equation,
(14) with the exponents of 0.33 and 1.7.
The 0.33 expopent of the bubble
Reynolds number appeared to be adequate for most of the data whether the heat,ing surface was clean or not, but the 1.7 exponent appearel to be valid on.ly
for clean surfaces.
With dirty surfaces the
vAlue of thia exponent wat at
-.
-~
-
-
-
-
-
-
-
-
-
___
11 -
erratic, varying between 0.8 and 2.0.
For purposes of comparison the oorrelation equation (4) may be re-written
in the form
a=IA
IVA-
N
NR,
nayhbe owtpared
C41
-
(15)
Npe
the non-boiling fomed ocavection exression
C, NkRe NN
.
..
,
qwere tht is in the range of 0.5 to 0.7 men the flow area varies along the
direction of flw, e.g., for flow across tubes, around spheres or cylinders,
or across interrupted tins.
Data for pool boiling of a liquid on a clean surface an be correlated
by an equation of the forms
CCAA
Further eaperimental work is needed to study the variation of bubble contact angle
and coefficient C
with pressure ad with type of heating su-
face fluid combination.
Further experimental work is needed to study the validity of equations
(3), (4) and (5)
uhich were used in obtainin
tbe terma
bubble Reynolds number and bable Nuaetlt vumtr.
j T;
- 12-
Ths3ka are due to Dr. J. N. Addmcs for permia=w"u
to us his data shoun
in figure 4 and to Mr. Fakhri Rahmatasah for perfoming most of the calcuiations required in preparing this report.
-
Cd,Cfd, Cq,
13
-
Coefficients in equatians (3),(4),(5),(9),(7),
respectively.
Cnf CR
C
Coefficient of equation (14),
a&ih depends upon the nature
of the heating surfacefluid ccibination.
Db
Dameter of the bubble as it leaves the heating surface, ft.
Mass velocity of bubbles at their departure from the heating
e@,
Nush
4
ftp.
Bubble Rusiselt niuber, defined by equations (8) and (9).
NPR
0
NRe,b
T
Bubble Reiynoads nmber, defined by equations (1) and (7).
Heag surface temperature minus saturation temperature, F.
Specific heat of saturated liquid, Btu/lb *O
f
Frequency of bubble foimation, lAr.
g
Acceleration of gravity.
Ccnversion factor, 4.17 a 10
f
(lb mas)(ft)/(hr)(potwso force.)
Latent heat of evaporation, Btu/lba
q/A + !,, flm coefficient of heat transfer, BtA/hr ftayo
Thermal oceductivity of saturated liquid, Stu/hr ft F.
Nuaber of points of origin of bubble columns per fta of heating
surface.
(VA)b
Beat transfer rate to bubble per unit heating surface area
wAhol bubble remains attacbed to the surface, Btu/hr fte
q/A
Beat transfer rate per unit heating surface area, BtuAr ft 3 .
Bubble contact angle, defined in figure 3.
Qh
ry'4
VnV.
Surface tension of liquid-vapor interface, lb/ft
Surface tension of vapor-solid interface, lbf/ft
Surface tension of solid-liquid interface, lb./ft
Density of aaturated liquid Iba/ft3
Density of saturated vapor lb./ft$
Viscosity of saturated liquid, lblft hr.
1. Jakob, M., 'Heat Transfer,' Vol. I, Chap. 29, Wiley, 1949.
2. Rohsenow, W. M. and Clark, J. A., "A Study of the Hochanim of Boiling
Heat Transfer," ASME Trans., July, 1951.
3.
Kennel, Minden, Rudoff, Picornell, Dew, 'Heat Transfer
at High Rates to Water with Surface Boiling,' Ind. Eg. Chem.
MeAdans, W. H.
Vol. 37, No. 10, Oct., 1945, pp 1010-1016
4. Gunther, F. C. and Lreith, F., 'Photographia Study of Bubble Formation in
Heat Transfer to Subooled Water," Beat Transfer and Fluid Mech. Inst.
1949, Berkeley, California, p. 113.
5.
Gunther, F. C., "Pbotograho Study of Surface-Boiling Heat Transfer to
Water with Fored Convection," AM Trans., Vol. 73, No. 2, Feb., 1951,
p. 115.
6.
Robsenow, W. N., and Clark, J. A., 'Heat Transfer and Pressure Drop Data
for High Heat Flux Densities to Water at High Sub-Critical Pressures,'
Heat Transfer and Fluid Medh. Inst., 1951, Stanford, California.
7. Jakob, M., 'Local Temperature Differences Occurring in Evaporation,
Condensation, and Cats~ytto Reaction,' Temperature, its Measurement
and Control in Scienc and Industry, Reinhold, New York, 1941, p. 834.
8. Frity, W., Physik. Zeitshr., Vol. 36, 1935, p. 37'.
9, Jakob, M., Zeitabr. d. Ver. deutsch. Ing. Vol. 76, 1932, p. 1161.
10. Addmma, J. N., "eat Transfer at Nig Rates to Water Boiling Outside
Cylinders,' D.Sc. hesis, Chen. kgrg. Dept., Mass. Inst. of Tech.,
Jum, 1948.
11.
Vel2aan, E. J., "Survey of Thermodync and Physical Properties of Water,'
.8. Thesis, Jan., 1950, Purdue University, Lafayette, Indiana.
12. Ciaelli, M. T. and Boni1a, C. Y., 'Heat Transfer to Liquids Boiling
under Pressure,' Trans. As. Inst. Chm. Engre., Vol 41, 755-787, 1945.
13. Clark, J. A., Malherbe, P., Mullin, F., and Robsenow, W. M., 'Heat Transfer
Data for Low Velocity Forced Convection Flow of Water with Surface
Boiling,' Tech. Rpt. #4, DIC Project 6627, M.I.T., July 1, 1951.
4. Kreith, F, and Sumierfield, M. J., 'Heat Transfer to Water at High Flux
Densities,' Trans. ASME, Vol. 71, No. 7, Oct., 1949.
15. Cryder, D. 8., and Finalborgo, A. C., 'Heat Transmission From Metal
Suf aces to Boiling Liquids: Effect of Temperature of the Liquid an
Fila Coefficient,' As. Inst. Chem. Engrs. Vol. 33, 1937, p. 346.
16. Jakob, N., Proc. 5th Internat. Coqgr. Appl.
echo., 1938, p. 561.
Figure No*
1
Title
Effect of Fluid Velocity an Heat Trafer Pat, in Nucleate
Boiling (Data of Rohsenov and Clark,( ).
Effect of Fluid Velocity oa Heat Transfer Rate In Nucleate
Boiling. Data of Rohseuoo and Clark (6).
Surface TeAsion forces Acting at Point of Bubble Contact.
Correlation of hata of Addm (10) for latinum-Vater
Interfaos for Pool Boiling.
Correlation of Data of Ciel-Bsilla (12) for ChromiumBansene Interfacebr Pool Boiling.
Cornlation of Data of Cihelli-Bnilla (12) for ChrominuMthl Alohol Interface for Pool Boiling.
Correlation of Data of Ciohelli-Bcnilla (12) for Chraiu.n-pmntne Interfaee for Pool Boiling.
Correlation of Data of Cryderinalborgo (15) for Brass-Water
Interface for Pool Boiling.
Data of Robsenow-Clark (6) (13) for Nickel-Water Interface
for Forced Convetion Surface Boiling.
Data of Kreith-4tmerfield (14) for Stainless Steel-Water
interface for Forced Convection Surface Boiling.
5.0
4.0
3.0
2.0
1.0
0
x
0.5
cr
0.4
0.3 g
0.21-
60
100
200
WALL TEMP. - LIQUID TEMP. (*F)
FIGURE
I
4.0
IO
3.0
A
A
P =2000 PSIA
Vi= 30 FT /SEC
G
I
0
A
5.7 x 106 LB / HR FT 2
2.0 --
0
O0
20 FT/
HVi=
c
A.
--
GG5.7xI
p 2000
x
1.5 -p = 2000
PSIA
PSIA
6
p=2000
PSIA
LB/HR FT 2
p =150
PSIA
Vi= 0 FT /
SE Vj= 0 FT SECVi2O
FT/ SEC
G = .2 106 2
= .96x 10 LBHR T?-G =4.2x 10 6
LB/HR FT 2
LBFT2 FTI
G9OLB/HR
1.0
3
Tx
89
7
4 5 6
=
5.7
106 L
10
20
15
R
FIGURE
2
LIQUID
VAPOR
a'tv
o'v s
HEATING
SURFACE
FIGURE
107
100
100
xx
A
ox
A
14.7
383
PSIA
P S IA
e
770
PSIA
A
1205
1602
2465
PSIA
0
10
10
x
0
0
b
PSIA
PSIA
A
b
0
x.
0'
Nn
0
A
1.0
0
gf
x =0.0
x
/A
=0
y3
h fg
g0 c
g(Pe-Pv)
0-
33
(c
/
kt
0./
0/
0.1
104
0.01
C
ADDOMS (10)
POOL BOILING
PLATINUM WIRE-WATER
0.024" DI AM.
I
1111111
0.1
T
hfg T
hfg
Npr''
FIGURE
p
4
+^-
1O
+
o
465
+ 645
0oD
0
b
00
x .0
0
0'0
x
CICHELLI-BONILLA (12)
POOL BOILING BENZENE
ON
POLISHED PLATED CHROMIUM
x
1.0
3
C
Tx
g 0 0o.
q/A
h fg
At h fg
.3
c.
g (p -pv)
0.1
0.01
hf
TX
N p'
FI GUR E
10 -
+
A
L
/
-it3A
Z
o
11 5
+
265
5 15
765
b0)
CICHELLI - BONILLA (12
POOL BOILING
ETHYL
ALCOHOL
ON POLISHED PLATED CHRC
1.00:>
q/A
a0
hg Tx =0.0027
.001
hg
90~
g(P-P )
0-33C
/
0.01
111 Tx
1.0
N
1pr'
FIGURE
6
22 PSIA
o
A60
o
+
10
A
*
115
2 15
3 1 5
4 15
'I
CICHELL I -BON ILLA (12)
BOILI NG
n- PENTANE
ON POLISHED PLATED CHROMI
POOL
cT
1.0-
£LTx =
hfgg
goa,-
q/A
.
h fg
gT(pt -pv )
033 cIp
)I.7
k.1
0.1
0.01
hfg
X
Npr'' 7
FIGURE
7
I
I
I
0.10
*
0
I
11111
I
o
22.4 PSIA
A
14.1
03
8.76
e
o
4.31
2.05
b
Q_
0.
CRYDER-FINALBORGO (15)
0'
1.
2
Ct
0.011
.0 01
POOL BOILING
BRASS TUBE-WATER
T. =0.0060
I
I
I
I
hfg
(q/A
hf
ILL
I
I
op;p))
g
gpi~p-v)
O.33
cl gA.
kg
II Iliii I I I
,01
pr
FIGURE
8
CORRELATION LINE FOF
ADDOMS DATA, FIG.4
~5O
V
100
'>'
ob0
b
2000 PSI
V=30
20
10
T-0
1.4
/
/
(b
V
0.8
0.5
0.2
A
0.1
*
0.05
1500 PSIA
+ V=30
20
0
10
1000 PSIA
v V =30
10
/
/
0?
0
/
ROHSENOW - CLARK (6)(13)
FORCED CONVECTION
SURFACE BOILING
NICKEL - WATER
1.0
0.1
0.01
I
h fg
N '.
FIGURE
9
100
I
CORRELATION
_
ADDOMS
I /I I I
LINE FOR
DATA,
/
FIG. 4
p=157-168 PSIA
o V = 6-7 FT/SEC
a
12
100-110
o
6-7
12
60- 66
v
6-7
*
12
45.5
v
6-7
40.5
10
U
36
0
36
*
(
6-7
6-7
22.5-25
6-7
A
'4-
/
/
/
12
0
KREITH -SUMMERFIELD
(14)
FORCED CONVECTION
SURFACE BOILING
STAINLESS STEEL-WATER
I
I
I I I I I
0.1
I
0.01
I
hfg
N 'r7
FIGURE
10
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