Purdue University
Purdue e-Pubs
International Refrigeration and Air Conditioning
Conference
School of Mechanical Engineering
1990
Investigation on CFC Diffusivity with an Improved
Double Volume Method
K. Dang
Xi'an Jiaotong University
Y. Wu
Xi'an Jiaotong University
Follow this and additional works at: http://docs.lib.purdue.edu/iracc
Dang, K. and Wu, Y., "Investigation on CFC Diffusivity with an Improved Double Volume Method" (1990). International Refrigeration
and Air Conditioning Conference. Paper 108.
http://docs.lib.purdue.edu/iracc/108
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Program
REFPROP: A Thermo dynamic Proper ties Softwa re
for
Refrig erants and Their Mixtur es
by
Graham Morriso n and J. S. Gallag her
Thermo physics Divisio n
Nation al Institu te of Standa rds and Techno logy
Gaithe rsburg, MD. 20899
ABSTRACT:
re packag e, REFPROP [OSRD. 1990].
This docume nt introdu ces the comput er softwa
describ es the conten ts and
It describ es the origin of the packag e, briefly
have led to the equatio n of state
output of the packag e, lists the data that
correl ation to
summa rizes the precis ion of the fit of the
parame ters, and
the input data for Rl23.
I - INTRODUCTION
designe d to produc e tables of
The softwa re packag e, REFPROP, has been
haloge nated
fully
and
partia lly
15
for
proper ties
thermod ynamic
M more data on
mixtur es.
chloro fluoroc arbon refrige rants and 20 of their
availa ble, these data will be
both pure materi als and mixtur es become
e.
incorp orated into the packag
at NBS (now NIST) in 1982 to
REFPROP has its origin s in a projec t begun
packag e to describ e refrige rant
state
of
n
equatio
produc e an easily- used
st in the use of mixtur es in
intere
an
by
ted
motiva
was
mixtur es. This work
azeotro plc. mixtur es have ever
only
ically,
Histor
[1985].
domest ic heat pumps
ations, such as R502, an
applic
lized
specia
for
then
and
been market ed,
arket open-c ase freeze r
superm
in
used
R115
and
R22
of
e
mixtur
azeotro pic
their phase behavi or is simila r to
that
feature
the
have
opes
Azeotr
s.
system
treated as if they were pure
pure materi als; hence, these mixtur es were
where azeotro py was not a
materi als. The use of mixtur es, partic ularly
from the traditi onal materi als'
consid eration , represe nted a major depart ure
The Montre al Protoc ol, an
y.
applic ations in the refrige ration industr
ally, to elimin ate the use of
interna tional agreem ent to curtai l and, eventu
fluoroc arbons , in partic ular Rll
severa l widely -used, fully-h alogen ated chloro
of thermod ynamic proper ties for
and Rl2, gave furthe r impetus to having tables
es, partic ularly for screen ing
a huge range of pure materi als and their mixtur
nted in the literat ure by
represe
were
als
materi
these
applic ations. Many of
existed for some of the
that
tions
tabula
d
detaile
the
only a few data; hence,
be produc ed despite the
not
could
1975],
[JAR,
R22
as
such
major refrige rants,
tion.
evalua
ance
perform
for
ation
inform
need to have such
proper ty tables for design and
REFPROP was designe d to provid e thermod ynamic
where little experim ental
lary
particu
als
materi
nt
differe
of
compar ison
describ es the equatio n of state
paper
this
of
II
n
Sectio
exist.
ation
inform
Sectio n III presen ts a
flaws.
briefly and discus ses its advant ages and
tables, and additio nal routine s
synops is of the routine s that genera te the
s the data that were used to
include d with the packag e, Sectio n IV review
Finally , Sectio n V review s ability
genera te the equatio n of state parame ters.
as a repres entativ e exampl e of
of REFPROP to repres ent the proper ties of Rl23
the perfom ance of the packag e.
II - THE EQUATION OF STATE
REFPROP are calcul ated using a
The thermod ynamic proper ties tables in
Carnah an and Starlin g
state.
modifi cation of the hard sphere equatio n of
that
cation in a review paper
[1972] reporte d briefly on this modifi
when their repres entatio n far
charac terized the equatio ns of state that arose
the many modifi cations of the van
the hard-sp here fluid was substi tuted into
242
der Waals equatio n
describ e the phase
referre d to as the
in equatio n 1. was
of state. DeSanti s et al. [1976) used this same
form to
behavio r of mixture s of simple fluids. This modific
Carnah an-Star ling-De Santis (CSD) equatio n of state, ation,
given
chosen because it address ed needs in represe
nting the
~
( 1 + y + y2 - y3)
a
R T
( 1 - y)J
R T (V + b)
where y
~
[1]
b I 4 V
propert ies of refrige rants. First, it was founded
on a physica l model, the
fluid of hard spheres , that could be expecte d to
describ e the liquid state
more correct ly than equatio ns using the traditio
nal van der Waals term for the
exclude d molecu lar volume. Second, it was a closed
mathem atical form with few
adjusta ble parame ters. The physica l foundat ion
and this inheren t simplic ity
have several advanta ges. The parame ters are shown
in equatio n 2; althoug h
a
b
(2al
b + b T + b T2
1
Q
[2bl
2
they have a tempera ture depende nce, they retain
a physica l interpr etation .
The equatio n can be used to correla te small sets
of diverse thermod ynamic
informa tion. Finally , the equatio n can be used
with the assuran ce that a
predict ed propert y, while having limited accurac
y because of its origin in a
limited data set, will not be unphysi cal. The simplic
ity of the equatio n also
leads to two other feature s: the retenti on of
a physica l meaning in the
equatio n of state parame ters allows it to be
applied to mixture s in a
straigh tforwar d manner as shown In equatio n 3·
and the simplic ity of its
a
a x 2 + 2 ( 1 - f o ) ( a a J 1/2 x x + a x 2
1
1
b
X
1
b
1
1
+
X
2
1
b
2
2
2
(3a)
[3b]
2 2
topolog y lends a robustn ess to numeric al solutio
ns of its roots. An extende d
discuss ion of the use of this equatio n of state
for refrige rants can be found
!n several publica tions by Morriso n and McLinde
n (1985, 1986a].
The advanta ges of this equatio n of state
lies
shortco mings are also rooted in that same feature ln its simplic ity; its
.
Morriso n and McLinden
[1986bl have shown that saturat ion data aloneliquid and vapor density and
vapor pressur e - produce nearly the optimal functio
n for correla ting all the
thermod ynamic propert ies. They have also shown
that the equatio n does not
represe nt the region near the critica l point well,
a feature of all so-call ed
"classi cal" equatio ns of state, and that the liquid
densiti es deviate in a
system atic way at high pressur es, tending to be
too high at a given pressur e.
Neither of these deficie ncies affects the applica
tion to refrige ration cycles,
however .
Typical ly, one must resort to signifi cantly
more complic ated
functio ns to elimina te these problem s.
The data
materia ls include d in REFPROP do not justify correla sets for many of the
tion with functio ns with
more comple xity than the CSD equatio n of state.
Inevita bly, materia ls, for
which there are large sets of data, will be represe
nted by complex equatio ns
of state. Neverth eless, the signific ance of a
simpler represe ntation , such as
the one found in REFPROP, is that all the materia
ls of interes t, ones hardly
studied as well as ones well-st udied, are represe
nted on an "even footing " and
can be legitim ately compared_
I II - SOFTWARE AND ROUTINES
The equatio n of state and its extensi on to mixture
s describ ed in Section II
has been impleme nted as a FORTRAN program and subrout
ines capable of running
on a persona l compute r. The calcula tion of
the equilib rium thermod ynamic
propert ies of the fluid from the equatio n of state
are made through a series
243
Note 1226, along with the main
of subrou tines as describ ed in NBS Techni cal
user, through a dialog proces s,
program and three subrou tines which allow the
set up the parame ters and calls to
to specify the desired calcul ations and to
are in double precisi on to insure
the proper ty subrou tines. All calcul ations
enough accura cy with a word length of 32 bits.
tines that
A brief descri ption of the interac tive subrou
and their functio ns are as follows :
the
user
encoun ters
The user
desired by the user.
Subrou tine Choice sets up the system of units
a single input from
with
units
of
set
te
comple
a
choose
to
has the opport unity
ng SI, the custom ary engine ering
a selecti on of commonly used system s, includi
The user may also choose the
ts.
chemis
by
often
used
system , and a system
The assume d
separa tely.
amount
and
,
volume
,
energy
units for temper ature,
are chosen for the
units
mass
if
ns
fractio
mass
be
will
units for compo sition
This
chosen for the -volum e.
volume and mole fractio ns if molar units are
proper
shes the
establi
made,
been
have
s
choice
the
subrou tine, after
to be used in the table headin gs,
conver sion factor s and the proper unit names
etc.
fluids for which parame ters are
Subrou tine Dialog presen ts the list of
Calcul ations
) of intere st.
availab le and asks the user to choose the fluid(s in the first version of
mixture
could be made fo< a pure fluid or a binary
g equatio n of state parame ters
REFPROP; the user now has the option of ente<in
library as one compon ent in the
for a materi al not include d in the packag e
ties of mixtur es with as many as
calcul ation and fo< calcul ating the prope<
ter, fa, has been calcul ated
five compon ents. The mixture interac tion parame
experim ental Inform ation; these
for a number of two-com ponent mixtur es from
es on the asserti on that there
combin ations are listed. The program operat
solutio ns to the equatio n of state.
will be only vapcr and single- phase liquid
tered with lubrica nts has not
More comple x phase behavi or that might be encoun
n algorit hm. The user may
solutio
rium
equilib
phase
the
been incorp orated into
when a mixture is chosen
ter
parame
tion
interac
mixture
supply the value of an
value.
stored
usly
previo
a
for which there is not
the user as to the type of
Subrou tine D!alog 2 is now called to query
. The availa ble choice s
desired
be
to
les
variab
dent
indepen
calcul ations and
re, 3) volume , 4) entropy , 5)
pressu
2)
ature,
temper
1)
nt
consta
at
are tables
at increm ents of 6) temper ature
enthalp y, or dew-po int and bubble -point values
s 1 through 5 Is chosen , the user
choice
from
option
an
When
re.
pressu
7)
or
quanti ty and then, as in all the
is asked to enter the value of the consta nt
variab le (tempe rature or pressu re)
option s, the range of the other indepen dent
An additio nal feature ,
ent.
as the initia l and final values and the increm
is to allow pressu re to
re,
offered when the runnin g variab le is pressu
at 1. 2, and 5 times powers of ten
increas e "expon entiall y" with table entrie s
in the region just below the
within the specif ied range. Table entrie s
ties vary rapidly , will be
proper
ynamic
thermod
many
critica l pressu re, where
In all the choice s,
.
chosen
is
mode
ntial
expone
the
when
more closely spaced
ing the values of
contain
d
inserte
is
line
a
,
crossed
is
ry
when a phase bounda
are for a mixture .
ations
calcul
When
ry.
bounda
phase
the
at
the proper ties
at the phase bounda ry is also
the compo sition of the coexis iting phase
variab les specify a state point
dent
indepen
the
of
values
the
Should
printed .
ty and the speed of sound
capaci
heat
ic
isobar
the
,
region
se
within the two~pha
two-ph ase region; instead , the
the
in
ed
undefin
are
they
as
ted
calcula
are not
fluid in the vaper phase, is
value of the quality , the fractio n of the
printed .
subrou tines describ ed above, the
In additio n to the three user interac tive
ns and subrou tines are_ also
FORTRAN source code for the follow ing functio
to implem ent this model as
include d in this packag e for the user who wishes
part of his own design packag e:
BLOCK BDESC contain s the equati on-of- state
refrige rants include d in the library .
parame ters
for
each
ature- depend ent
SUBROUTINE ESPAR (IOPT,T,X,A,Bl calcul ates the temper
n of T and Xfunctio
of "a" and "b" for the desired mixture as a
244
of
the
values
SUBROUTINE BCONST (Il,I2,F O,Fl) accesse s the equatio
n of state parame ters for
refrige rants identif ied by the index numbers Il
and I2, and the value of the
mixture interac tion paramet er, FO, for the chosen
mixture (Fl has not been
impleme nted at present ) and makes them availab le
to other routine s. Referen ce
values for the enthalp y and the entropy are also
calcula ted at this point.
SUBROUTINE CRITX (X,TC,PC,VCl estimat es the value
of the critica l point
predict ed by the equatio n of state for the chosen
mixture and compos ition.
FUNCTION PVT(T,V,X) perform s the basic equatio
n of state calcula tion of
pressur e as a functio
n of T, V, and x.
SUBROUTINE HCVCPS (IOPT,T,V,X,H,CV,CP,SND) calcula
tes values of the enthalp y,
heat capacit ies, and speed of sound as functio ns
of T. V, and x. IOPT allows
the calcula tion of only H if desired .
FUNCTION ENTROP T,V,X) calcula tes the value of the
entropy as a functio n ofT,
V, and x.
SUBROUTINE VIT (T,P,A,B,V,LLIQ,LCON) perform s the
iteratio n to obtain the
volume when the tempera ture and pressur e are
g!ven.
The values of the
equatio n of state parame ters "a," and "b" must be
supplie d. LLIQ and LCON are
logical variabl es: set LLIQ ~ .TRUE. for a liquid
point and~ .FALSE. for a
vapor point. LCON is set~ .TRUE. by the subrout
ine if the iteratio n has
converg
ed_
SUBROUTINE BUBLT (T,XL.XV,PSL,VL,VV,LPHASE,LCR
ITl
and
SUBROUTINE
BUBLP
(P,XL,XV,TSL,VL,VV,LPASE,LCRIT) determi ne, through
an iteratio n to find the
equalit y in chemica l potenti als in each phase, the
dew- and bubble- points of
the specifi ed mixture .
SUBROUTINE
HPIN
(H,P,TSAT,HSAT,VSAT,T,V,LLIQ)
is
conveni ence, perform ing the iteratio n necessa ry
to find
volume corresp onding to a specifi ed enthalp y, pressur
e,
also
include d
the tempera ture
and compos ition.
SUBROUTINE SPIN (S,P,X.TSAT,VSAT,T,V,LLIQ) operate
s in a way similar
with the specifi cation of the·entr opy rather than
enthalp y.
to
for
and
HPIN
IV. DATA SOURCES
This Section reviews the data that were used to
evaluat e the six equatio n of
state parame ters associa ted with the CSD equatio
n of state and the additio nal
three parame ters for the ideal gas heat capacit y.
The heat capacit y data are
necessa ry to generat e a complet e thermod ynamic surface
; without these values,
only states at the same tempera ture can be compare
d with one another .
The minimum set of informa tion necessa ry to evaluat
e the coeffic ients for "a"
and "b" is saturat ion informa tion. As previou sly
mention ed, these data alone
produce nearly the optimal fit for the CSD equatio
n of state.
Since the
locatio n of the saturat ion boundar y is so importa
nt a
even where more extensi ve data exist, the saturat feature in cycle design,
ion data were weighte d
heavily . The parame ters were chosen to optimiz e
the fit to the data.
For
example
. when satur-at ion data alone were used, values
of
nau
and
b
were
determi ned to give the best fit to liquid and vapor
densiti es and the vapor
pressur e. In princip le, only two of these three
necessa ry to satisfy the thermod ynamic requirem ents quantit ies are actuall y
of equatin g the pressur e
and the Gibbs free energy. When larger sets of
data were availab le, values of
"a" and "b" were determi ned that optimiz ed the fit
to the data by means of a
non-lin ear regress ion routine from the IMSL Statist
ical Library [1987).
11
11
The values of the ideal gas heat capacit ies came
from a variety of sources_
In nearly all cases, the values were
calcula ted
from
spectro scopic
informa tion. The ideal gas heat capacit ies
were fit to the followi ng
functio n:
Cp I R
c
0
+ c
!
T + c
2
T
2
[4)
245
Although the value of the heat capacity has
form, the quadratic fit was always found to
prescribed range of applicatio n.
a
be
more
complicate d
accurate
to
functional
0. 01%
in . the
The optimal value of this
Mixtures are characteri zed by the quantity fo.
In most cases,
quantity was chosen to be consistent with the data that exist.
In a few cases,
there were only bubble pressure/l iquid compositio n data.
the
and
there were also other informatio n such as liquid densities,
Morrison and
compositio n and densities of the coexistent vapor phase.
compositio n
McLinden [1986b] have shown the value of fo to be clearly
in REFPROP.
dependent; that feature of the behavior has not been implemente d
for the most
Evidence for variation with temperatur e is sketchy at best, even
to be
extensive sets of mixture data; the values of fo were then assumed
ts for
temperatur e independen t. Other properties , such as virial coefficien
used to
the mixture or the location of an azeotropic compositio n were also
fo.
determine
of those data
The following is a listing of the data sources and the character
that were correlated with the CSD equation of state:
PURE MATERIALS
Rl1: ASHRAE ( 1980) _
Ideal gas heat capacity: JANAF ( 1970).
R12: ASHRAE ( 1980) .
Ideal gas heat capacity: JANAF ( 1970).
R13: ASHRAE ( 1980).
Ideal gas heat capacity: JANAF ( 1970).
R13B1: ASHRAE ( 1980).
Ideal gas heat capacity: JANAF ( !970).
R14: ASHRAE ( 1980 l.
Ideal gas heat capacity: JANAF ( 1870).
s.
R. Kohl en. H. Kratzke. and
R22: Vapor pressure: A. v. Kletskii ( 1964);
Muller- ( 1985).
A.
Liquid and vapor volumes: R. Kohlen, H. Kratzke, and S. Muller (1985);
(1978).
Iwasaki
H.
and
Kumagai
and D.
Enthalpy of vaporizati on and liquid heat capacity: E. F. Neilson
\lhite ( 19S7).
Ernst,
Vapor heat capacity: G .Ernst and J. Busser (1970); K. Bier, G.
and G. Maurer (1974).
Ideal gas heat capacity: JANAF (1970).
R23: ASHRAE ( 1980).
Ideal gas heat capacity: JANAF (1970).
R113: Vapor pressure, liquid densities, vapor phase p-v-T, and critical
temperatur e: H. J. Mastroiann i, R. F. Stahl, and P. N. Sheldon (1978).
Project
Ideal gas heat capacity: Thermodyna mics Research Center Data
( 1986).
Mears et
R114: Saturation densities, liquid and vapor, and pressures: ~- H.
al. (1955).
Project
Ideal gas heat capacity: Thermodyna mics Research Center Data
( 1986).
critical
R123: Saturation densities, liquid and vapor, and pressures,
Levelt
pressure, temperatur e, and density: L. A. ~eber and J. M. H.
Sengers ( 1989) .
Project
Ideal gas heat capacity: Thermodyna mic Research Center Data
( 1986).
et al.
R124o Saturation densities, liquid and vapor, and pressure: H. Kubota
( 1988)Ideal gas heat capacity: R. Bender, K. Bier, and G. Maurer (1980).
critical
pressure,
critical
pressures,
densities,
Saturation
Rl34:
temperatur e, critical density: 0. K. ~ard, G. Morrison 1989).
J. R.
Ideal gas heat capacity from spectrosco pic data: Klabo, P. and
Nielsen (1960).60) .
R134a: saturation densities, liquid and vapor, and pressures: R. S.
D. P. ~ilson (1989); D. K. ~ard and G. Morrison (1989).
246
Basu
and
Satura tion densit ies, vapor, and vapor pressu
re: L. A. ~eber (1989).
Critic al temper ature, pressu re, and density
: D. K. ~ard and G. Morriso n
( 1989).
Ideal gas heat capaci ty: s. S. Chen, A.
S. Rogers , J, Chao, R. C.
~ilhoit, and_B. J. Zwolin ski (1975).
R142b: Satura tion densit ies, liquid and vapor,
and pressu re: ~. H. Mears, et
al. ( 1956).
Ideal gas heat capaci ty: Thermo dynamic Resear
ch Center Data Projec t
( 1986).
R152a: Satura tion densit ies, liquid and vapor,
and pressu re: ~. H. Mears, et
al. (1956). Y. Higash i, et al. (1987).
Compre ssed liquid: A. Iso and M. Uemats u (1989).
Ideal gas heat capaci ty: S. S. Chen, A.
S. Rogers , J. Chao, R. C.
~ilhoit. and 8. J. Zwolin ski (1975).
MIXTURES: for all mixtur es, the
design ation is listed first.
refrige rant
with
the
lower
numeri cal
R11 + R12: bubble point proper ties. N. D- Loi
(1983).
R11 + R22: bubble point proper ties. M. Meskel
-Leavre , D. Richon , and H. Renon
( 1982).
R12 + R13: bubble point proper ties. J. Molleru
p and A.
Freden slund (1976).
R12 + R13B1: vapor- liquid equilib ria. E. G.
~right (1985).
R12 + R22: compo sition and normal boiling
temper ature, B. J. Eisema n (1957).
R12 + R114: bubble point proper ties. M. Kuver
(1983).
R12 + R142b: vapor- liquid equilib ria. V. A.
Nikol' skii, 0. V. Baklan , and N.
I. Arteme nko (1983).
R12 + R152a: azeotro pe compo sition. ~- A.
Pennin gton (1952).
R13 + Rl4: vapor- liquid equilib ria. ~- L. Kubic
and F .P. Stein (1981).
R13 + R23: bubble point proper ties. F. P.
Stein an P. C. Proust (1971).
R13B1 + R22: bubble point proper ties. A. P.
Kuznet zov (1972).
R1381 + Rl14: bubble point proper ties. Kuver
(1986).
R1381 + R152a: bubble point proper ties.
G. Morriso n and M. 0. McLinden
( 1985).
R14 + R23: vapor- liquid equilib ria. A. Piacen
tini and F_ P. Stein (1967).
R22 + R114: bubble point proper ties.
G. Hackst ein (1976); A. Valtz, s.
Laugie r, and H. Richon (1987)_
R22 + R142b: bubble point proper ties. A. Valtz,
S_ Laugie r, and H. Richon
( 1987).
R134 + Rl34a: liquid density and compo sition
and bubble point pressu re. D. K.
~ard and G. Morriso n ( 1989).
Rl34 + Rl52a: liquid density and compo sition
and bubble point pressu re. D. K.
~ard and G. Morriso n ( 1989L
R134a + Rl52a: liquid density and compos iti-on
and bubble point pressu re.
D.
K. ~ard and G. Morriso n ( 1989)-
V - DATA REPRESENTATION
As indicat ed in the previou s section , the extent
and variety of data depend
upon the materi al.
In this section , the proper ties of R123,a s
represe nted by
REFPROP, will be examin ed. The values of the
equatio n of state parame ters
were determ ined exclus ively from the satura
tion proper ties listed in the
bibliog raphy bet~een 273 K and 423 K. The
agreem ent bet~een the satura tion
curve correl ation and the satura tion proper
ties are shown in Figure 1. Since
the determ ination of those quanti ties, a large
collec tion of p-V-T inform ation
on this materi al has become availab le; indeed,
the amount of inform ation is so
large that the thermod ynamic proper ties have
been correla ted to a comple x,
multi-p aramet er equatio n of state [McLin den
et a!., 1989].
Figure 2 shows the differe nce between the
calcula ted densit y at a given
temper ature and pressu re and the experim ental
density . The densit ies in the
liquid phase ~ere measure d by Morriso n and
~ard (1990] from 278 K to 368
K to
a pressu re of 3800 kPa_ The densit ies in the
vapor phase ~ere are derived
from Burnet t measur ements made by ~eber [1990].
Those measur ements range from
358 to 453 K and from 330 to 1960 kPa. The
densit ies in the vapor phase are
system aticall y below the measur ed values;
wherea s the opposi te is true in the
247
1200 kPa the equation of
liquid phase. The figure shows, however, that below
The
than +/- 0.5Y..
better
to
R123
of
es
properti
the
state represen ts
tation of
represen
poor
the
of
result
the
are
s
pressure
higher
deviatio ns at
the systema tic over
the critical point, particu larly for the vapor, and
in the liquid
state
of
equation
CSD
the
by
sibility
compres
the
of
predicti on
CSD equation has,
the
ers
paramet
few
the
with
that
show
does
1
phase. Figure
of operatio n.
it quantita tively repesen ts the properti es in the range
ACKNOIILEDGEMENT
d, in part, by a
Developm ent of the software , REFPROP, package was supporte
National Institut e of
grant from the Office of Standard Referenc e Data,
review was provided , in
Standard s and Technolo gy. The informat ion for this
part, by H. 0. McLinden.
was supporte d, in part, by
The developm ental work that lead finally to REFPROP
National Laborato ry of
the Electric Power Research Institut e, the Oak Ridge
nt Division of the Center
the U. S. Departm ent of Energy, the Building Equipme
Division of the Center
for Building Technolo gy, NIST, and the Therrnop hysics
Chemical
for
Center
for Chemica l Enginee ring and its successo r, the
Technolo gy, NIST.
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249
Densities of 1,1-dichlor o-2,2,2-trif luoroethane ," Fluid Phase Equilibrium
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the
\./right. E. G., "Prediction of Refrigerant Ternary Mixture Properties Using
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( 1985).
0.5 r----,- ------- -,.---- -,---,- -___,
0.4
CIJ
<(
LlJ
::;:
0.3
X
00
0.2
X
0.1
CIJ
<(
LlJ
0
:;:!
X
-0.1
c..
0
c:
c..
-0.2
u..
LlJ
~
-0.3
-0.4
-0.5
L...---....1....-----.1.--------1..-----l
270
400
350
300
420
T/K
Figure l: The deviation ofthe correlated saturation properties from the
Solid line - saturated liquid density; dashed
measured properties for Rl23.
line • vapor pressure; double dashed line - saturated vapor volume.
6000
2000
1000
(?
a..
------======
~2.5
2.0
1.5
1.0
~-5
500
.::t:.
E:
.£
200
100
50
20
270
300
400
350
450 470
T/K
Figure 2: The deviation (in per cent) of the CSD predicted density from the
measured density for Rl23.
250