EPA/600/A 93/062
PHYSICAL PROPERTIES OF FLUORINATED PROPANE AND
BUTANE DERIVATIVES AS ALTERNATIVE REFRIGERANTS
A. L Beyerlein, Ph. D. D. D. DesMarteau, Ph. D. S. -H. Hwang, Ph. D.
N. D. Smith, Ph. D. P. Joyner, Ph. D.
ABSTRACT
Physical property measurements are presented for 24 fluorinated propane and
butane derivatives and one fluorinated ether. These measurements include melting
point, boiling point, vapor pressure below the boiling point, heat of vaporization at the
boiling point, critical properties (temperature and density), and liquid-phase heat
capacities at 40°C (104°F). Measured vapor pressures are obtained up to the critical
/ 'J
temperature for four of the compounds: HFC-227ea, HFC-245cb, HFC-236ea, and HFE-
125a. These measured data, combined with estimated vapor-phase densities, heat
capacities, and vapor pressures, may be used to evaluate the chemicals as alternative
refrigerants. Modified corresponding states methods, using HFC-134a as a reference
fluid, are presented as a means of obtaining the needed estimated data, and the accuracy
of these methods is judged by comparisons with measured data.
KEYWORDS
Refrigerant chlorofluorocarbons chlorofluorohydrocarbons
Thermodynamic measurement
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INTRODUCTION
Twenty-four fluorinated propane and butane derivatives and one fluorinated ether
(see Table 1) have been investigated as second generation alternatives for currently
used CFCs (chlorofluorocarbons) and HCFCs (hydrochlorofluorocarbons). These
investigations included both syntheses and physical property measurements. Synthetic
routes were emphasized that used inexpensive commercially available starting materials
and basic synthetic procedures [chlorination, hydrogenation, and addition of hydrogen
fluoride (Hudlicky, 1976, and Lovelace et al., 1958)] which are carried out
industrially. However further details regarding the synthetic procedures are left for a
separate publication, and in this paper only the results of the physical property
investigations are presented. The emphasis is on hydrogen containing compounds that
are expected to have finite atmospheric lifetimes which reduce their greenhouse
warming potential. Sixteen of the chemicals investigated contain no chlorine and
therefore have zero ozone depletion potential. The remaining nine chlorine containing
chemicals were selected for investigation before the current calls for the complete
phaseout of chlorine containing refrigerants (US,1990, and UNEP, 1990).
Nevertheless the low chlorine content of these chemicals combined with a finite
atmospheric lifetime may in some cases yield an alternative with a sufficiently low
ozone depletion potential. Therefore it is possible that some of the chlorine containing
chemicals studied in this work may eventually prove to be valuable as we gain more
knowledge about the ozone depletion problem.
The physical property investigations included measurement of the melting point,
boiling point, vapor pressure below the boiling point, heat of vaporization at the boiling
point, critical properties (temperature and density), liquid densities, and liquid-phase
* Adolph L. Beyerlein is a Professor of Chemistry, Darryl D. DesMarteau is the
Tobey-Beaudrot Professor of Chemistry, and Sun-Hee Hwang is a Research Associate at
Clemson University, Chemistry Department, Clemson, SC 29634-1905. N. Dean
Smith is a Project Officer in the Stratospheric Ozone Protection Branch, EPA Air and
Energy Engineering Research Laboratory, Research Triangle Park, NC 27711, and
Powell Joyner is Director of Residential Projects at the Electric Power Research
Institute at 3412 Hillview Avenue, Palo Alto, CA 94303.
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heat capacities at 40°C (104°F). Measured vapor pressures are reported from the
boiling point, Tb, to the critical temperature, Tc, for four of the compounds: HFE-125a
(Tb=-34.6°C [-30.3°F] and Tc= 80.7°C [177.3°F]), HFC-227ea (Tb = -18.3°C
[-0.9°F] and TC=102.8°C [217°F]), HFC-245cb (Tb = -18.3°C [-0.9°F], and Tc=
108.5°C [227.3°F]), and HFC-236ea (Tb = 6.5°C [43.7°F] and TC=141.1°C
[286.0°F]) where the chemical formula equivalents for each compound are given in
Table 1. The purpose of these measurements was to provide data for judging these
compounds as alternative refrigerants. Portions of the data have already been used to
estimate the performance of these chemicals as refrigerants by modeling the
refrigeration operation (Sand and Fischer, 1992).
The screening of the compounds as alternative refrigerants requires, in addition to
the measured data: the vapor-phase heat capacities, vapor densities, and vapor
pressures up to the critical point for all the compounds. For the initial screening
purposes these may be estimated from the measured data obtained in this work, ideal gas
heat capacities, and various equations of state. The ideal gas heat capacities may be
estimated by a functional group method and the extensive database of S. W. Benson, et al.
(1969). In order to demonstrate the accuracy that one can expect from estimates for
the saturated vapor density and the vapor pressure between the boiling point and the
critical point, these were estimated by a modified corresponding states technique (Reid
et al., 1984) and compared with measured values for CFC-12, HFC-227ea, HFC-
245cb, HFC-236ea, and HFE-125a. The measured liquid-phase heat capacity at 40°C
(104°F) is useful for judging the accuracy of caloric data (liquid and vapor heat
capacities) estimated from equations of state and the ideal gas heat capacity.
EXPERIMENTAL METHODS
The compounds were synthesized to 99.5% purity. The vapor pressure was
measured over about a 30°C (54°F) temperature range from temperatures below the
boiling point up to the boiling point with a mercury isoteniscope to within ±0.5 kPa
(±0.1 psia). From these measurements the boiling point was obtained to within ±0.2°C
(±0.4°F) and heat of vaporization at the boiling point to within ±0.1 kJ/mole (±0.1
Btu/lb). The vapor pressure above the boiling point was measured to about ±3 kPa
(±0.4 psia) using a precision Baratron MKS 315 pressure sensor with a vacuum on its
reference side. The pressure sensor is connected to a stainless steel sample cell
- 2 -
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immersed in a bath with the temperature controlled to within ±0.1 °C (0.2°F). The total
volume of the pressure sensor and cell combination is 50 ml (3 in3). Thus to measure
pressures near the critical point at least 20 g {0.7 oz) of sample is required. Since the
pressure sensor is external to the temperature bath both the sensor and its connection to
the sample cell are heated to a temperature well above the critical temperature of the
sample. The electronic readout via a MKS 272C power supply automatically
compensates for the temperature effect on the pressure sensor.
The melting point was determined to within ±0.2°C (±0.4°F) as the thermocouple
temperature at which a solidified ring of the compound disappeared from the surface of a
sample tube. The critical temperature was measured by slowly raising the temperature
of the sample in a sealed tube until the meniscus disappears.
The liquid density in the liquid-vapor coexistence region was determined by
enclosing a sample in a 1.5 mL (0.09 in3) tube (about 12 cm [4.7 in] long) and
measuring the displacement of the meniscus to within 0.05 mm (0.002 in) from the
bottom of the tube with a Gaertner cathetometer. The mass of the sample was
determined gravimetrically and the cathetometer readings are converted to the volumes
of the saturated liquid and vapor phases by a calibration procedure with weighed amounts
of water in the tube. The sample temperature was controlled to within ±0.1 °C (±0.2°F)
and was measured to the same accuracy. The experiment is performed for several
samples of differing mass. In order to show that the average density (or diameter), p =
(Pi + pg)/2 (p| and pg being the liquid and vapor densities) is most accurately obtained
by this technique, the sample mass to volume ratio is expressed in terms of p by,
m _ V|- Vg
=
where Ap is given by,
A
Ap •
P| ' PO
AP = '2 H , (2)
V is the sample volume, and V| and Vg are the liquid and vapor volumes, respectively.
The Ap is obtained to within 2% by comparing samples with widely differing weights,
i.e.,
- 3 -
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(v \ - (v 1
^r y\ I \ / \ x\ / \ / v V *^ /
where the subscripts 1 and 2 indicate that the data are obtained from measurements on
two separate samples. The diameter, p, is then accurately obtained (to within 0.5%)
from measurements on samples where V| and Vg are comparable in value. For such cases
the second term in Eq. (1) is small and the measured p is sensitive only to m and V both
of which are precisely measured. Normally measurements are obtained to within 20%
of the critical point and the critical density is calculated to within about 2% accuracy by
extrapolating the diameters to the critical temperature. The liquid densities are
obtained to within 2% from p and Ap with the relation,
PI = p + Ap . {4 )
The vapor densities can also be obtained from measured p and Ap as pg = p - Ap.
However, our experiments were not precise enough to obtain accurate saturated vapor
densities. Therefore no measured vapor densities are reported although the reader may
calculate them from the measured diameters and liquid densities which are presented in
Table A-1 of the Appendix (Table A-1a is in SI units, and Table A-1b is in IP units).
The liquid-phase heat capacity was measured using a Perkin-Elmer DSC-4
differential scanning calorimeter (DSC) and sapphire reference standards. The samples
were contained in stainless steel sample capsules of 75 u.L (0.0046 in3) capacity with
an 0-ring seal. The sample capsules are manufactured by Perkin-Elmer and the leakage
during a calorimeter experiment is negligible. The capsules were filled using a
microliter syringe in a cold room with a temperature below the boiling point of the
sample (as low as -40°C [-40°F]). The DSC measurement was corrected for vapor
volume and heat of vaporization effects due to changes in the relative sizes of the liquid
and vapor phases as the temperature is scanned (Hwang et al., 1992). The data were
also corrected to the constant pressure heat capacity, Cp, using formulas given in Reid et
al. (1984). The vapor volume was kept at a minimum by using sample sizes of 60 mg
(0.002 oz) or larger. For these sample sizes the corrections (1%) were less than the
estimated experimental error of 3% or 0.04 kJ/°C-g (0.01Btu/°F-lb).
- 4 -
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MODIFIED CORRESPONDING STATES ESTIMATION OF VAPOR DENSITY AND
VAPOR PRESSURE
In order to evaluate these compounds as refrigerants, vapor pressures and vapor
densities are needed to temperatures approaching the critical point. It has already been
noted that these may be estimated from the boiling point and measured critical
parameters using various equations of state. In this section we demonstrate how the
modified corresponding states method combined with the Benedict-Webb-Rubin
equations of state (1940) may be used for this evaluation. The modified corresponding
states method is based on the following expression for the compressibility Z (Reid et al.,
1984),
Z = Z + (oZ , (6)
(7)
where w is the Pitzer acentric factor for the system of interest and COR is the same factor
for a reference fluid which was selected to be HFC-134a. The quantity p is the density,
P is the pressure, and T is the temperature. The quantity 2^°) is the compressibility of
a simple fluid which is defined to be the Benedict-Webb-Rubin equations with the
simple fluid constants of Lee and Kesler (1975). The Modified Benedict- Webb- Rubin
equation of state (Jacobsen and Stewart, 1973) with constants obtained by McLinden, et
al. (1989) was used to obtain the reference fluid compressibility Z(R). The acentric
factor is calculated from the equations of Lee and Kesler (1975),
In Pc + f(°)(Tbr)
a = - !•> \ . ( 8 )
f(1)(Tbr)
where Pc is the critical pressure in units of atmospheres (101.325 kPa) and,
f(°)(Tr) = 5.92714 - 6-°3648 - 1.28862 ln(Tr) + 0.16934 Tr6 , (9)
f(1>(Tr) = 15.2518 - 15'^875 - 13.4721 ln(Tr) + 0.43577 Tr6 . (10)
The quantity Tr(= T/TC) is the reduced temperature, and Tt>r is the reduced boiling
point.
- 5 -
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The refrigerant HFC-134a was picked as a reference fluid because excellent
equation of state data (McLinden et al,, 1989} have been obtained for this compound, and
its acentric factor is comparable in value to the acentric factor for most of the
fluorinated propane and butane derivatives. The latter fact increases the accuracy of the
modified corresponding state methods because the correction from the reference fluid
equation of state to that for the compounds being investigated is small. The latter fact
becomes evident if one rewrites Eq. (6) so that the reference fluid compressibility is
the primary zero order term,
Z = Z
-------
these were calculated from the measured critical temperature and critical density using
modified corresponding states equations.
In order to judge the accuracy of the measured liquid densities and vapor
pressures these were measured for CFC-12 for comparison with literature data
(Stoecker and Jones, 1982). However after completing this work a search of the
literature revealed very precise data for HFC-245cb, which were obtained by Shank
(1967). Also during the course of this work, data were reported for HFE-125a (Wang
et al., 1991, and Adcock et al., 1991) and HFC-227ea (Hoechst Chemicals, 1991).
Comparisons are made with these literature data in Tables 3 and 4. The liquid densities
measured in this work are well within 1% of the literature values for CFC-12
(Stoecker and Jones, 1982) and HFC-245cb (Shank, 1967) presented in Table 3. For
HFC-227ea the discrepancy between our liquid densities and those reported by Hoechst
Chemicals (1991) is somewhat larger, being 2.0% below 50°C (122°F). This
discrepancy may be related to the fact that our boiling point of -18.3°C (-0.9°F)
differs from the value of -17.3°C (0.9°F) reported by Hoechst Chemicals. Nevertheless
this still represents excellent agreement and it verifies the estimated accuracy for the
measured liquid densities. The measured liquid densities of this work, given in Table 3,
for HFE-125a are within 1% of the values (Wang et al., 1991, and Adcock et al.,
1991), which were measured in van Hook's laboratory. Observations for the
comparisons of vapor pressures of this work with literature values in Table 4 are
similar to those made for liquid densities.
The critical temperature, pressure, and density of this work [108.5°C
(227.3°F), 499 kg/m3 (31.2 Ib/ft3), 3264 kPa (473.4 psia)] and [102.8°C
(217.0°F), 580 kg/m3 (36.2 Ib/ft3), 2943 kPa (426.9 psia)] for HFC-245cb and
HFC227ea, respectively, are in very good agreement with the values of Shank (1967)
[107.0°C (224.6°F), 490 kg/m3 (30.6 Ib/ft3), 3137 kPa (455.0 psia)] and Hoechst
Chemicals (1991) [101.9°C (215.4°F), 592 kg/m3 (36.9 Ib/ft3), 2952 kPa (428.2
psia)]. The measured critical density for CFC-12, 567 kg/m3 (35.4 Ib/ft3), which is
obtained by extrapolation of density data ranging from temperatures of 20°C (68°F) to
85°C (185°F), is within 2% of the literature value (CRC, 1989), 558 kg/m3 (34.8
Ib/ft3).
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Since no vapor densities were measured and a complete set of vapor pressures up
to the critical point were measured for only four compounds, the accuracy of modified
corresponding states methods using HFC-134a as a reference fluid was checked for
estimating these properties by comparisons of the estimates with experimental data.
Vapor densities estimated using this method and measured critical properties (density
and temperature) and the boiling point are compared with the literature data for CFC-
12 (Stoecker and Jones, 1982), HFC-227ea (Hoechst Chemicals, 1991), and HFC-
245cb (Shank, 1967) in Table 3. The vapor densities estimated by modified
corresponding states methods agree with the experimental literature values within 1%.
We believe that the excellent agreement is the result of a good choice of reference fluid,
HFC-134a (has an acentric factor comparable to those of compounds being investigated)
for the modified corresponding states method. These comparisons provide confidence for
the modified corresponding states method as a means of estimating vapor densities.
The modified corresponding states method was used to estimate the critical
pressure for most of the compounds investigated. In order to demonstrate the accuracy
of the method for estimates of the critical pressure and vapor pressure between the
boiling point and critical point, these are compared with experimental vapor pressures
in Tables A-2 to A-5 of the Appendix. The estimated vapor pressures for HFC-236ea,
HFC-245cb, and HFE-125a are within 4% of the measured values. The deviations are
somewhat larger (about 5%) for HFC-227ea but nevertheless still confirm that
modified corresponding states methods are useful for estimating vapor pressures up to
the critical point.
SUMMARY AND CONCLUSIONS
Data have been presented which can be used to evaluate fluorinated propane and
butane derivatives as alternative refrigerants. Estimation methods for the vapor density
and vapor pressure that are based on boiling point and critical property measurements
can provide a useful complement to the measured data. These conclusions are based on
comparisons of the results of modified corresponding states estimation methods with
measured data.
Qualitative judgements regarding the potential of the various chemicals as
alternative refrigerants can be made by examining the physical property data in Table 2.
The lowest boiling point propane chemicals HFC-245cb [ Tb=-18.3°C (-0.9°F)], HFC-
- 8 -
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227ea [ Tb= -18.3°C (-0.9°F)], and HFC-227ca [ Tb = -16.3°C (2.7°F)] may be
alternatives for CFC-12 [ Tb=-29.8°C (-21.6°F)] and HFC-134a [Tb=-26.5°C
(-15.7°F)] for some applications. The critical temperatures of these alternatives
which range from 102.8°C (217°F) to 108.5°C (227.3°F) compare well with the
critical temperatures, 112.1°C (233.8°F) and 101.1°C (214.0°F) of CFC-12 and
HFC-134a, respectively. The ether compound HFE-125a [ Tb= -34.6°C (-30.3°F)]
may in some instances also be an alternative for CFC-12 or HFC-134a, but its low
critical temperature [80.7°C (177.3°F)] means that it is only marginally suitable for
air conditioning applications.
The compound HFC-245ca with a boiling point of 25.0°C (77°F) and a critical
temperature of 178.4°C (353.1°F) appears to be a very likely alternative for CFC-11
[Tb= 23.8°C (74.8°F) and TC=198°C (388.4°F)]. The chemical HCFC-235ca with a
boiling point of 28.1°C (82.6°F) and critical temperature of 170.3°C (338.5°F) also
appears to be an alternative for CFC-11. However since the latter chemical contains
chlorine, it is a much less desirable alternative than HFC-245ca. The butanes, HFC-
338ccb [Tb= 27.8°C (82.0°F)] and HFC-338eea [Tb=25.4°C (77.7°F)], have boiling
points that match the boiling point of CFC-11 very well; but their critical
temperatures, 160.5°C (320.9°F) and 148.5°C (299.3°F), respectively, are
significantly lower than that of CFC-11.
The compounds, HFC-236ea [Tb= 6.5°C (43.7°F) and Tc= 141.1°C (286.0°F)],
and HFC-236fa [Tb= -1.1°C (30.0°F) and TC=130.6°C (267.1°F)] are potential
alternatives for CFC-114 [Tb= 3.77°C (38.8°F) and Tc= 145.7°C (294.3°F)]. Other
compounds, such as HFC-245fa, HFC-236ca, and HFC-329ccb which have boiling
points in the range 12°C (54°F) to 16°C (61°F), also may have applications as
refrigerants. Chlorinated propane derivatives containing one chlorine atom per
molecule have boiling points less that 30°C (86°F) and therefore would have potential
refrigerant applications. The hydrogen containing dichloropropane derivatives
investigated in this work all have boiling points above 50°C (122°F), which are
probably too high for refrigerant applications.
APPENDIX
This Appendix contains tabulations of the measured saturated liquid densities and
vapor pressures between the boiling point and critical point for HFC-227ea,
- 9 -
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HFC-245cb, HFC-236ea, and HFE-125a in Tables A-1 to A-5. Since the presentation
of measured vapor pressures below the boiling point would require extensive
tabulations, only parameters for empirical representations of these data are given in
Table A-6. The parameters are based on,
InP = A - | -ClnT , (A-1)
where for SI units the pressure P is in kPa and T is the Kelvin temperature and in IP
units P is in psia and T is the Rankine temperature. The parameters are calculated by
least squares methods from vapor pressures, measured at about 2°C (3.6°F) intervals
over about a 30°C (54°F) temperature range from below the boiling point up to the
boiling point. The RMS deviations of the measured vapor pressures from Eq. (A-1) are
about 0.7 kPa (0.1 psia). The exception to the above are the chemicals, HFC-338eea
and HCFC-225da, for which data were obtained over a smaller 20°C (36°F)
temperature range and for these data only the parameters A and B were included in the
empirical representation. For the latter chemicals the RMS deviation obtained from the
least squares calculation is 0.7 kPa (0.1 psia).
ACKNOWLEDGEMENTS
The authors are grateful to the U. S. Environmental Protection Agency's
Stratospheric Ozone Protection Branch, Research Triangle Park, NC, and the Electric
Power Research Institute, Palo Alto, CA, for supporting this research.
REFERENCES
Adcock, J. L; S. B. Mathur; W. A. van Hook; H. Q. Huang; M. Narkhede; and B.-H. Wang.
1991. "Fluorinated ethers a new new series of CFC substitutes." Proceedings of
the International CFC and Halon Alternatives Conference, Baltimore, Maryland
(December 3-5). pp. 386 to 395.
Benedict, M.; G. B. Webb; and G. B. Rubin. 1940. Journal of Chemical Physics. Vol. 8,
pp. 334-345.
Benson, S. W.; F. R. Cruickshank; D. M. Golden; G. R. Haugen; H. E. O1 Neal; A. S. Rodgers;
R. Shaw; and R. Walsh. 1969. "Additivity rules for the estimation of
thermochemical properties." Chemical Reviews. Vol. 69, No. 3, pp. 279-324.
CRC. 1989. CRC Handbook of Chemistry and Phvsics. 69th ed. Boca Raton, Florida:
CRC Press.
Hoechst Chemicals. 1991. Hoechst Refrigerant R 227. Technical Report (January).
-10-
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Hudlicky, M. 1976. Chemistry of Organic Fluorine Compounds. 2nd Ed. New York:
John Wiley.
Hwang, S.-H.; D. D. DesMarteau; A. L Beyerlein; N. D. Smith; and P. Joyner. 1992.
"The heat capacity of fluorinated propane and butane derivatives by differential
scanning calorimetry." Submitted to the Journal of Thermal Analysis.
Jacobsen, R. T. and R. B. Stewart. 1973. "Thermodynamic properties of nitrogen
including liquid and vapor phases from 63 K to 2000 K with pressures to 10000
bar." Journal of Physical and Chemical Reference Data. Vol. 2, pp. 757-922.
Lee, B. I. and M. G. Kesler. 1975. "A generalized thermodynamic correlation based on
three-parameter corresponding states." AlChE. Journal. Vol. 21, No. 3, pp 510-
527.
Lovelace, A. M.; D. A. Rausch; and William Postelnek. 1958. Aliphatic Fluorine
Compounds. No. 138. New York: John Wiley.
McLinden, M. O.; J. S. Gallagher; L. A. Weber; G. Morrison; D. Ward; A. R. H.
Goodwin; M. R. Moldover; J. W. Schmidt; H. B. Chae; T. J. Bruno; J. F. Ely; and M. L
Huber. 1989. "Measurement and formulation of the thermodynamic properties of
refrigerants 134a (1,1,1,2-tetrafluoroethane) and 123 (1,1-dichloro-2,2,2-
trifluoroethane}." ASHRAE Transactions. Vol. 95, No. 2, pp. 263 -283.
Reid, R. C.; J. M. Prausnitz; and Bruce E. Poling. 1984. The Properties of Gases and
Liquids. 4th ed. New York: McGraw-Hill.
Sand, J. R. and S. K. Fischer. 1992. "Modeled performance of non-chlorinated
substitutes for CFC-11 and CFC-12 in centrifugal chillers." To be published in
The International Journal of Refrigeration.
Shank, R. L. 1967. "Thermodynamic properties of 1,1,1,2,2-pentafluoropropane
(refrigerant 245)." Journal of Chemical and Engineering Data. Vol. 12, No. 4,
pp. 474 -480.
Stoecker, W. F. and J. W. Jones. 1982. Refrigeration and Air Conditioning. 2nd Ed. New
York: McGraw-Hill.
UNEP. 1990. United Nations Environment Programme Meeting, London.
US. 1990. United States Clean Air Act. Title Vl-Stratospheric Ozone Protection, Public
Law 101-549 (November 15).
Wang, B.-H.; J. L. Adcock; S. B. Mathur; and W. A. van Hook. 1991. "Vapor pressures,
liquid molar volumes, vapor nonideality, and critical properties of some
fluorinated ethers (CF30CF2OCF3, CF3CF20CF2H, cyclo-CF2CF2CF2-, CF3OCF2H,
and CFsOCHa), and of CCIsF and CF2CIH." Journal of Chemical Thermodynamics.
Vol. 23, No. 7, pp. 699-710.
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TABLE 1
The ASHRAE code for each compound along with its chemical formula
Code
HFE-125a
HFC-227ea
HFC-227ca
HFC-236fa
HFC-236ea
HFC-236cb
HFC-236ca
HFC-245fa
HFC-245ca
HFC-245cb
HFC-254cb
HFC-329ccb
HFC-338eea
Formula
CF3OCF2H
CF3CHFCF3
CF3CF2CF2H
CFsCH^Fs
CF3CHFCF2H
CF3CF2CFH2
HCF2CF2CF2H
CF3CH2QF2H
HCF2CF2CFH2
CF3CF2CH3
HCF2CF2CH3
CF3CF2CF2CF2H
CF3CFHCFHCF3
Code
HFC-338cca
HFC-338ccb
HFC-347ccd
HCFC-226da
HCFC-226ea
HCFC-235ca
HCFC-244ca
HCFC-225da
HCFC-225ba
HCFC-234da
HCFC-243da
C-326d
Formula
HCF2CF2CF2CF2H
CF3CF2CF2CFH2
CF3CF2CF2CH3
CF3CHCICF3
CFsCHFCF^I
HCF2QF2CH2CI
CF3CHCICF2CI
CF3CFCICFHCI
CF3CHCICFHCI
CFsCHCICH^I
cyclic-(CF2)3CHCI
-1 2-
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TABLE 2a
Boiling point, melting point, heat of vaporization at the boiling point, critical
properties, and liquid-phase heat capacity (SI units).
Compound
Code
HFE-125a
HFC-227ea
HFC-227C3
HFC-236fa
HFC-236ea
HFC-236cb
HFC-236C3
HFC-245fa
HFC-245ca
HFC-245cb
HFC-254cb
HFC-329ccb
HFC-338eea
HFC-338cca
HFC-338ccb
HFC-347ccd
HCFC-226da
HCFC-226ea
HCFC-235ca
HCFC-244ca
HCFC-225da
HCFC-225ba
HCFC-234da
HCFC-243da
C-326d
Tb(°C)
-34.6
-18.3
-16.3
-1 .1
6.5
-1.4
12.6
15.3
25.0
-18.3
-0.8
15.1
25.4
42.5
27.8
15.1
14.1
17.6
28.1
54.8
50.8
51.9
70.1
76.7
38.1
Tmelt
(°C)
-156.1
-126.8
-140.3
-94.2
-146.1
-105.4
-123.3
-102.1
-73.4
-81 .1
-121.1
-122.3
-91.5
-91.0
-119.4
-124.9
-119.6
-134.0
-85.0
-101.8
-130.3
-132.7
-98.0
-71.6
-94.8
AHvap
(kj/mof)
21.92
22.29
23.69
25.66
26.83
25.25
26.59
27.96
29.21
23.59
24.86
26.71
27.79
31.13
26.36
25.82
24.64
26.26
27.57
31.07
25.89
29.38
31.70
30.86
28.69
TC(°C)
80.7
102.8
106.3
130.6
141.1
130.1
155.2
157.5
178.4
108.5
146.1
140.2
148.5
186.4
160.5
144.2
158.2
158.3
170.3
221.0
206.2
212.9
242.5
251.9
196.9
Pc
(kPa)
3253
2943
2870
3180
3533
3120
3410
3640
3860
3264
3750
2390
2470
2830
2550
2570
3020
2950
3080
3710
3010
3070
. . .
. . .
PC
kg/rn3
584
580
594
556
571
545
558
529
529
499
467
600
581
578
562
532
591
584
550
525
589
586
. . .
- - -
. . .
Cp(liq.)
at 40°C
( kJ 1
lkg-°cj
1.33
1.26
1.25
1.37
1.30
1.44
. . .
1.42
1.45
1.46
1.59
1.22
...
1.33
1.34
1.38
1.21
1.20
1.28
1.16
1.09
1.09
1.17
1.23
1.16
-1 3-
-------
TABLE 2b
Boiling point, melting point, heat of vaporization at the boiling point, critical
properties, and liquid-phase heat capacity (IP units).
Compound
Oxte
HFE-125a
HFC-227ea
HFC-227ca
HFC-236fa
HFC-236ea
HCFC-236cb
HFC-236ca
HFC-245fa
HFC-245ca
HFC-245cb
HFC-254cb
HFC-329ccb
HFC-338eea
HFC-338cca
HFC-338ccb
HFC-347ccd
HCFC-226da
HCFC-226ea
HCFC-235ca
HCFC-244ca
HCFC-225da
HCFC-225ba
HCFC-234da
HCFC-243da
C-326d
Tb(°F)
-30.3
-0,9
2.7
30.0
43.7
29.4
54.7
59.5
77.0
-0.9
30.6
59.2
77.7
108.5
82.0
59.2
57.4
63.7
82.6
130.6
123.4
125.4
158.2
170.1
100.6
Tmelt
(°F)
-249.0
-196.2.
-220.5
-137.6
-231.0
-157.7
-189.9
-151.8
-100.1
-114.0
-186.0
-188.1
-132.7
-131.8
-182.9
-192.8
-183.3
-209.2
-121.0
-151.2
-202.5
-206.7
-144.4
-96.9
-136.6
AHygp
(Btu/lb)
69.32
56.39
59.93
72.61
75.90
71.44
75.25
89.74
93.75
75.72
92.16
52.23
59.16
66.28
56.12
60.36
56.84
60.59
70.40
88.80
54.89
62.27
73.74
79.52
62.18
TC(°F)
177.3
217.0
223.3
267.1
286.0
266.2
311.4
315.5
353.1
227.3
295.0
284.4
299.3
367.5
320.9
291.6
316.8
316.9
338.5
429.8
403.2
415.2
468.5
485.4
386.4
PC
(psia)
471.8
426.9
416
461
512.4
452
494
528
560
473.4
544
347
358
410
370
373
438
428
447
538
436
445
- - -
. - .
. . .
PC
Ib/ft3
36.4
36.2
37.1
34.7
35.6
34.0
34.8
33.0
33.0
31.2
29.2
37.4
36.2
36.1
35.1
33.2
36.9
36.4
34.3
32.7
36.8
36.6
. .. .
. . .
Cp(liq.)
at 104°F
( BtU 1
ljb-0Fj
0.318
0.301
0.300
0.328
0.312
0.344
. . .
0.340
0.348
0.348
0.380
0.292
. , .
0.319
0.321
0.331
0.289
0.288
0,305
0.277
0.260
0.260
0.281
0.295
0.277
-1 4-
-------
TABLE 3a
Comparison of measured liquid densities and modified corresponding states
vapor densities with literature values (SI units).
Temp
(°C)
20
30
40
50
60
70
80
Liquid
This
Work
1313.
1286.
1250.
1207.
1156.
1097.
1030.
Density (kg/m3)
Litera-
ture*
1329.0
1292.2
1253.1
1211.0
1165.3
1114.6
1056.9
% Dev
CFC-12
-1 .21
-0.48
-0.25
-0.33
-0.83
-1 .62
-2.50
Vapor
Corre-
ponding
states
32.6
42.6
55.0
70.3
89.7
114.2
146.2
Density (kg/m3)
Litera-
ture*
32.49
42.54
55.03
70.57
90.00
114.61
146.66
% Dev
0.34
0.15
-0.06
-0.39
-0.33
-0.36
-0.27
HFC-245cb
23.0
34.4
43.3
52.6
61.5
71.2
81.2
1185
1142
1 109
1074
1034
986
924
1185.0
1145.0
1111.5
1073.2
1033.1
984.3
925.4
0.00
-0.22
-0.19
0.04
0.08
0.17
-0.13
27.6
38.3
48.8
62.4
79.0
102.0
134.1
27.34
38.10
48.68
62.78
79.49
102.71
135.32
0.97
0.48
0.21
-0.50
-0.63
-0.59
-0.86
HFC-227ea
23.0
35.0
45.0
55.0
65.0
75.0
85.0
9.7
22.4
32.1
42.2
51.4
60.8
1380
1314
1268
1215
1 161
1096
1013
1362
1298
1255
1196
1133
1051
1404
1347
1294
1234
1 168
1094
1006
1345. 1a
1283.5b
1238.7b
1184.9b
1133.4b
1064.03
-1.74
-2.50
-2.05
-1 .54
-0.60
0.18
0.69
HFE-125a
1.26
1.13
1.37
0.93
0.00
-1 .22
35.3
49.8
65.7
86.1
112.9
149.2
201.7
35.19
50.07
66.24
86.97
113.99
150.42
203.01
0.30
-0.60
-0.75
-1 .03
-0.96
-0..80
-0.64
* The literature data are taken from Stoecker and Jones (1982) for CFC-
12, data of Shank (1967) for HFC-245cb, and Hoechst Chemicals data
[1991] for HFC-227ea. The literature values for HFE-125a labeled, a,
are obtained from Adcock, et al. (1991) and data labeled, b, are obtained
from Wanq et al. (1991).
-15-
-------
TABLE 3b
Comparison of measured liquid densities and modified corresponding slates
vapor densities with literature values (IP units).
Temp
(°F)
68
86
104
122
140
158
176
Liquid
This
Work
82.0
80.3
78.0
75.4
72.1
68.5
64.3
Density (Ib/ft3)
Litera-
ture*
82.97
80.67
78.23
75.60
72.75
69.58
65.98
% Dev
CFC-12
-1.21
-0.48
-0.25
-0.33
-0.83
-1 .62
-2.50
Vapor
Corre-
ponding
states
2.04
2.66
3.43
4.39
5.60
7.13
9.13
Density (Ib/ft3)
Litera-
ture*
2.028
2.655
3.436
4.406
5.618
7.155
9.152
% Dev
0.34
0.15
-0.06
-0.39
-0.33
-0.36
-0.27
HFC-245cb
73.4
93,9
109.9
126.7
142.7
160.2
178.2
74.0
71.3
69.2
67.1
64.6
61.6
57.7
73.98
71.48
69.39
66.99
64.49
61.45
57.77
0.00
-0.22
-0.19
0.04
0.08
0.17
-0.13
1.72
2.39
3.05
3.90
4.93
6.37
8.37
1.707
2.379
3.039
3.919
4.962
6.412
8.448
0.97
0.48
0.21
-0.50
-0.63
-0.59
-0.86
HFC-227ea
73.4
95.0
113.0
131.0
149.0
167.0
185.0
48.6
72.3
89.8
108.0
124.5
141.4
86.2
82.0
79.2
75.9
72.5
68.4
63,2
85.0
81.0
78.4
74.7
70.7
65.6
87.6
84.1
80.8
77.0
72.9
68.3
62.8
83.97a
8Q.12b
77.33b
73.97b
70.73b
66.42b
-1.74
-2.50
-2.05
-1.54
-0.60
0.18
0.69
HFE-125a
1.3
1.2
1.3
0.9
0.0
-1 .2
2.20
3.11
4.10
5.38
7.05
9.31
12.59
2.197
3.125
4.135
5.429
7.116
9.390
12.674
0.30
-0.60
-0.75
-1.03
-0.96
-0..80
-0.64
* The literature data are taken from Stoecker and Jones (1982) for CFC-
12, data of Shank (1967) for HFC-245eb, and Hoechst Chemicals data
[1991] for HFC-227ea. The literature values for HFE-125a labeled, a,
are obtained from Adcoek, et al. (1991) and data labeled, b, are obtained
from Wang et al. (1991).
-16-
-------
TABLE 4
Comparison of measured vapor pressures with literature values.
SI Units
Temp
<°C)
20,0
40.0
60.0
80.0
95.0
10.1
20.0
40,1
60.1
80.3
106.9
108.5
4.8
20.2
40.9
60.0
80.2
101.9
102.8
5.4
20.0
40.0
59.9
80.6
80.7
Measured
This
Work
(kPa)
571
965
1529
2291
3004
293
402
715
1176
1839
...
3264
252
416
747
1201
1883
2943
500
777
1327
2101
. . .
3253
Litera-
ture*
(kPa)
IP Units
Temp
(OF)
CFC-12
567.3
960.7
1525.9
2304.6
3056.9
68.0
104.0
140.0
176.0
203.0
HFC-245cb
289.2
398.5
711.0
1169.1
1837.9
3137.2
. . .
50.2
68.0
104.3
140.2
176.5
224.5
227.3
HFC-227ea
241.1
401.8
728.5
1176.7
1858.9
2952
. . .'
40.6
68.4
105.6
140.0
176.4
215.4
217.0
HFE-1253
491.5
772.4
1324.0
2123.2
3326.1
...
41.7
68.0
104.0
139.8
177.1
177.3
Measured
This
Work
(psia)
82.8
140.0
221.8
332.3
435.8
42.4
58.3
103.7
170.6
266.8
...
473.4
36.6
60.3
108.4
174.2
273.1
. . .
426.8
72.5
1 1 2.7
192.5
304.7
. . .
471.8
Litera-
ture*
(psia)
%
Dev.
82.28
139.33
221.31
334.25
443.36
0.7
0.4
0.2
-0.6
-1 .8
41.95
57.80
103.12
169.57
266.57
455.02
. . .
1.2
0.8
0.6
0,6
0.1
3.9
35.00
58.28
105.66
170.66
269.61
428.2
. . .
4.6
3.5
2.6
2.0
1.3
-0.3
71.29
112.03
192.08
307.95
482.42
...
1.7
0.6
0.2
-1 .1
-2.2
* The literature data are taken from Stoecker and Jones (1982) for
CFC-12, data of Shank (1967) for HFC-245cb, Hoechst Chemicals data
(1991) for HFC227ea, and data of Wanq et al. (1991) for HFE-125a.
-17-
-------
The
TABLE A-1a
measured diameters and saturated liquid densities (SI units).
Temp.
(°C)
9.7
22.4
32.1
42.2
51.4
60.8
24.5
37.6
42.0
60.7
71.6
86.8
1.6
11.9
22.7
32.4
44.6
64.4
75.2
94.6
Diameter
-------
The
TABLE A-1a (Continued)
measured diameters and saturated liquid densities (SI units).
Temp.
22.0
40.0
60.0
80.0
100.0
110.0
120.0
22.0
60.0
80.0
100.0
120.0
140.0
23.5
43.5
63.5
73.5
93.5
100.5
110.5
Diameter
(P|+Pg)/2
(kq/m3)
HFC-236ca
743
718
690
662
635
621
607
HFC-245ca
688
650
629
609
589
568
HFC-254cb
593
573
552
542
522
515
505
Liquid
Density
1484
1420
1339
1268
1 189
1148
1084
1344
1252
1208
1 152
1076
987
1171
1 169
1083
1041
960
929
890
Temp.
11.3
30.6
44.1
57.3
75.0
84.5
23.0
34.4
43.3
52.6
61.5
71.2
81.2
25.0
52.5
66.6
75.0
95^0
100.5
110.0
Diameter
(p,+ pg)/2
HFC-245fa
688
667
652
638
618
608
HFC-245cb
611
596
585
572
561
548
535
HFC-329ccb
766
726
706
694
665
657
643
Liquid
Density
(kg/m3)
1342
1318
1282
1238
1187
1 151
1185
1 142
1109
1074
1034
986
924
1518
1413
1360
1333
1230
1208
1143
(Continued)
-19-
-------
The
TABLE A-1a
measured diameters and
(Continued )
saturated liquid densities (SI units).
Temp.
(°C)
26.0
46.0
56.0
66.0
86.0
100.0
110.0
22.0
42.0
62.0
82.0
102.0
114.0
124.0
25.6
36.3
53.7
69.5
78.2
89.6
Diameter Liquid
(p|+pg)/2 Density
(ka/m3) (kg/m3)
HFC-338eea
761
732
717
702
673
652
637
HFC-338ccb
763
734
705
676
647
629
615
HCFC-226da
741
729
709
691
681
669
1510
1455
1404
1360
1281
1216
1179
1514
1470
1399
1322
1214
1139
1079
1467
1438
1397
1342
131 1
1267
Temp.
22.0
40.0
60.0
80.0
100.0
120.0
140.0
22.5
42.5
70.5
82.5
92.5
102.5
112.5
25.5
49.9
67.7
77.7
89.4
104.9
121.0
Diameter
(p|+Pg)/2
(kq/m3)
HFC-338cca
766
754
729
707
683
656
628
HFC-347ccd
668
645
614
601
590
578
567
HCFC-226ea
747
717
695
683
668
649
630
Liquid
Density
1510
1486
1440
1398
1312
1236
1148
1324
1271
1183
1145
1 105
1057
1004
1478
1417
1357
1316
1268
1212
1124
(Continued)
-20-
-------
The
TABLE A-1a (Continued)
measured diameters and saturated liquid densities (SI units).
Temp.
(°C)
24.0
34.0
46.0
56.0
66.0
79.0
95.5
24.3
34.7
59.3
73.6
88.0
102.6
Diameter Liquid
(p|+pg)/2 Density
(kg/m3) (kg/m3)
HCFC-235ca
698
688
676
666
656
642
626
HCFC-225da
783
772
746
731
715
700
1382
1371
1344
1317
1289
1250
1199
1558
1541
1486
1447
1406
1364
Temp.
(°C)
21.0
41.5
61.0
84.5
104.2
113.5
133.5
24.5
38.1
49.8
66.0
77.8
96.7
Diameter
(P|+Pg)/2
(kq/m3)
HCFC-244ca
719
699
680
657
638
629
609
HFC-225ba
789
775
762
745
732
712
Liquid
Density
(kg/m3)
1433
1392
1354
1308
1253
1227
1 170
1559
1547
1528
1487
1459
1377
-2 1 -
-------
The
TABLE A-1b
measured diameters and saturated liquid densities (IP units).
Temp.
(OF)
49.5
72.3
89.8
108.0
124.4
141.5
76.1
99.7
107.6
141.3
161.9
188.2
34.8
53.4
72.8
90.4
112.3
148.0
167.3
202.2
Diameter
(P|+Pg)/2
(Ib/ft3)
HFE-1258
43.7
42.4
41.4
40.4
39.5
38.5
HFC-227ca
44.8
43.5
43.1
41.3
40.3
38.9
HFC-236ea
46.8
46.0
45.1
44.4
43.4
41.8
41.0
39.4
Liquid
Density
(Ib/ft3)
85.0
81.0
78.4
74.7
70.7
65.6
86.7
84.0
81.7
76.1
72.4
66.5
91.9
88.7
87.1
85.9
82.8
76.6
76.0
69.1
Temp.
(°F)
73.4
95.0
113.0
131.0
149.0
167.0
185.0
33.1
42.5
97.7
124.5
151.3
182.3
207.4
72.5
108.5
126.5
162.5
180.5
212.9
Diameter
(P|+Pg)/2
(Ib/ft3)
HFC-227ea
44.0
42.8
41.8
40.8
39.8
38.8
37.8
HFC-236fa
45.6
45.2
42.6
41.4
40.1
38.7
37.5
HFC-236cb
42.5
41.7
40.8
39.1
38.1
36.6
Liquid
Density
(Ib/ft3)
86.2
82.0
79.2
75.9
72.5
68.4
63.2
90.5
89.1
83.0
79.2
75.8
69.9
65,8
83.1
81.7
78.9
74.4
71.7
64.0
(Continued)
-22-
-------
The
TABLE A-1b (Continued)
measured diameters and saturated liquid densities (IP units).
Temp.
(OF)
71.6
104.0
140.0
176.0
212.0
230.0
248.0
71.6
140.0
176.0
212.0
248.0
284.0
74.3
110.3
146.3
164.3
200.3
212.9
230.9
Diameter
(p,+ pg)/2
(lb/ft3)
HFC-236ca
46.4
44.8
43.1
41.3
39.6
38.8
37.9
HFC-245C3
42.9
40.6
39.3
38.0
36.8
35.5
HFC-254cb
37.0
35.8
34.5
33.8
32.6
32.2
31.5
Liquid
Density
(lb/ft3)
92.6
88.7
83.6
79.2
74.2
71.6
67.7
83.9
78.2
75.4
71.9
67.2
61.6
73.1
73.0
67.6
65,0
59.9
58.0
55.6
Temp.
52.3
87.1
111.4
135.1
167.0
184.1
73.3
93.9
109.9
126.7
142.7
160.2
178.2
77.0
126.5
151.9
167.0
203.0
212.9
230.0
Diameter
(P|+Pg)/2
(lb/ft3)
HFC-245fa
43.0
41.6
40,7
39.8
38.6
38.0
HFC-245cb
38.1
37.2
36.5
35.7
35.0
34.2
33.4
HFC-329ccb
47.8
45.3
44.1
43.3
41.5
41.0
40.1
Liquid
Density
(lb/ft3)
83.8
82.3
80.1
77.3
74.1
71.8
74.0
71.3
69.2
67.1
64.6
61.6
57.7
94.8
88.2
84.9
83.2
76.8
75.4
71.4
(Continued)
-23-
-------
The
TABLE A-1b (Continued)
measured diameters and saturated liquid densities (IP units).
Temp.
(°F)
78.8
114.8
132.8
150.8
186.8
212.0
230.0
71.6
107.6
143.6
179.6
215.6
237.2
255.2
78.1
97.3
128.7
157.1
172.8
193.3
Diameter Liquid
(p|+Pg)/2 Density
(Ib/lt3) Ob/ft3)
HFC-338eea
47.5
45.7
44.8
43.8
42.0
40.7
39.8
HFC-338ccb
47.6
45.8
44.0
42.2
40.4
39.3
38.4
HCFC-226da
46.3
45.5
44.3
43.1
42.5
41.8
94.3
90.8
87.6
84.9
80.0
75.9
73.6
94.5
91.8
87,4
82.5
75.8
71.1
67.4
91.6
89.8
87.2
83.8
81.8
79.1
Temp.
71.6
104.0
140.0
176.0
212.0
248.0
284.0
72.5
108.5
158.9
180.5
198.5
216.5
234.5
77.8
121.8
153.9
171.9
192.9
220.8
249.8
Diameter
(p|+Pg)/2
(ib/ft3)
HFC-338cca
47.8
47.1
45.5
44.1
42.6
41.0
39.2
HFC-347ccd
41.7
40.3
38.3
37.5
36.8
36.1
35.4
HCFC-226ea
46.6
44.8
43.4
42.6
41.7
40.5
39.3
Liquid
Density
(Ib/ft3)
94.2
92.8
89.9
87.3
81.9
77.2
71.7
82.6
79.4
73.8
71.5
69.0
66.0
62.7
92.3
88.5
84.7
82.1
79.2
75.6
70.2
(Continued)
-24-
-------
The
TABLE A-1b (Continued)
measured diameters and saturated liquid densities (IP units).
Temp.
(°F)
75.2
93.2
114.8
132.8
150.8
174.2
203.9
75.7
94.5
138.7
164.5
190.5
216.7
Diameter Liquid
(p|+pg)/2 Density
(Ib/ft3) Ob/ft*)
HCFC-235ca
43.6
43.0
42.2
41.6
40.9
40.1
39.1
HCFC-225da
48.9
48.2
46.6
45.6
44.6
43.7
86.3
85.6
83.9
82.2
80.5
78.0
74.9
97.3
96.2
92.7
90.3
87.8
85.1
Temp.
(°F)
69.8
106.7
141.8
184.1
219.5
236.3
272.3
76.1
100.6
121.6
150.8
172.0
206.1
Diameter
{p,+ pg}/2
(Ib/ft3)
HCFC-244ca
44.9
43.6
42.5
41.0
39.8
39.3
38.0
HFC-225ba
49.3
48.4
47.6
46.5
45.7
44.4
Liquid
Density
(Ib/ft3)
89.5
86.9
84.5
81.6
78.2
76.6
73.1
97.3
96.6
95.4
92.8
91.1
86.0
-25-
-------
TABLE A-2
Measured vapor pressures for HFE-125a compared with vapor
pressures estimated by modified corresponding states methods.
SI Units
Temp
(°C)
5.4
10.1
14.8
20.0
24.8
30.4
34.7
40.0
45.3
50.4
54.9
59.9
65.9
70.0
74.8
78.0
80.0
80.7
Measured
This
Work
(kPa)
500.
581
669
777
889
1034
1160
1327
1509
1703
1881
2100
2393
2610
2892
3087
3203
3253
Corres.
States
(kPa)
482
560
645
754
864
1008
1130
1295
1478
1671
1858
2084
2383
2608
2892
3098
3229
3242
IP Units
Temp
(OF)
41.7
50.2
58.6
68.0
76.6
86.7
94.5
104.0
113.5
122.7
130.8
139.8
150.6
158.0
166.6
172.4
176.0
177.3
Measured
This
Work
(psia)
72.5
84.2
97.0
112.6
129.0
150.0
168.2
192.4
218.8
247.0
272.8
304.7
347.1
378.6
419.5
447.8
464.6
471.8
Corres.
States
(psia)
70.0
81.3
93.6
109.4
125.3
146.2
163.8
187.9
214.4
242.4
269.5
302.3
345.6
378.2
419.4
449.3
468.3
470.2
%
Dev.
3.5
3.5
3.5
2.9
2.9
2.5
2.6
2.3
2.0
1.9
1.2
0.8
0.4
0.1
0.01
-0.4
-0.8
0.3
-26-
-------
TABLE A-3
Measured vapor pressures for HFC-227ea compared with vapor
pressures estimated by modified corresponding states methods.
SI Units
Temp
(°C)
3.4
4.8
9.9
15.0
20.2
25.2
30.2
35.3
40.9
45.2
50.1
55.8
60.0
65.4
70.0
74.9
80.2
84.7
90.0
95.4
99.8
102.8
Measured
This
Work
(kPa)
240
252
300
353
416
481
558
642
747
838
952
1091
1201
1361
1510
1680
1883
2067
2297
2525
2752
2943
Corres.
States
(kPa)
233
244
289
341
400
464
535
616
715
798
901
1034
1141
1290
1428
1587
1776
1949
2170
2416
2632
2787
IP Units
Temp
(°F)
38.1
40.6
49.8
59.0
68.4
77.4
86.4
95.5
105.6
113.4
122.2
132.4
140.0
149.7
158.0
166.8
176.4
184.5
194.0
203.7
211.6
217.0
Measured
This
Work
(psia)
34.9
36.6
43.5
51.2
60.3
69.8
80.9
93.1
108.4
121.5
138.0
158.2
174.2
197.2
219.1
243.7
273.1
299.7
333.1
366.2
399.1
426.8
Corres.
States
(psia)
33.7
35.4
41.9
49.4
58.0
67.3
77.6
89.3
103.6
115.8
130.7
150.0
165.4
187.1
207.2
230.2
257.6
282.7
314.8
350.4
381.8
404.2
%
Dev.
3.2
3.3
3.5
3.6
3.8
3.6
4.1
4.1
4.4
4.8
5.3
5.2
5.0
5.2
5.5
5.6
5.7
5.7
5.5
4.3
4.4
5.3
-27-
-------
TABLE A-4
Measured vapor pressures for HFC-245cb compared with vapor
pressures estimated by modified corresponding states methods.
SI Units
Temp
(°C)
7.1
10.1
15.1
20.0
25.0
30.0
35.1
40.1
45.4
50.2
55.2
60.1
65.1
70.3
75.2
80.3
85.5
86.3
90.2
95.6
96.1
97.6
102.1
104.2
108.5
Measured
This
Work
(kPa)
264
293
344
402
468
541
624
716
820
925
1047
1176
1320
1483
1651
1839
2044
2099
2244
2497
2557
2610
2877
2995
3264
Corres.
States
(k.Pa)
264
293
343
400
465
536
617
706
807
909
1026
1 151
1290
1446
1608
1793
1992
2023
2187
2416
2457
2529
2759
2870
3113
IP Units
Temp
<°F)
44.7
50.2
59.1
68.1
77.1
86.1
95.2
104.3
113.7
122.7
131.3
140.1
149.1
158.4
167.3
176.6
185.9
187.3
194.3
204.0
204.9
207.6
215.7
219.5
227.3
Measured
This
Work
(psia)
38.2
42.4
49.9
58.3
67.8
78.4
90.5
103.7
119.0
134.2
151.8
170.6
191.4
215.1
239.4
266.8
296.5
304.5
325.5
362.2
370.8
378.6
417.3
434.4
473.4
Corres.
States
(psia)
38.3
42.5
49.8
58.0
67.4
77.8
89.5
102.3
117.0
131.8
148.8
166.9
187.0
209.8
233.3
260.0
289.0
293.4
317.3
350.4
356.4
366.8
400.1
416.2
451.5
%
Dev.
-0,1
-0.2
0.3
0.4
0.6
0.8
1.1
1.4
1.6
1.8
2.0
2.1
2.3
2.5
2.6
2.5
2.5
3.7
2.5
3.2
3.9
3.1
4.1
4.2
4.6
-28-
-------
TABLE A-5
Measured vapor pressures for HFC-236ea compared with vapor
pressures estimated by modified corresponding states methods.
SI Units
Temp
(°C)
10,3
14.1
19.0
24.8
30.0
35.2
40.0
45.6
49.8
54.8
59.8
65.2
69.9
74.9
79.7
85.6
90.0
93.3
94.7
97.0
101.8
106.9
115.5
119.9
125.3
130.3
135.2
138.1
141.1
Measured
This
Work
(kPa)
121
141
169
207
247
291
338
403
456
523
598
690
777
878
979
1124
1227
1325
1359
1463
1626
1808
2158
2350
2609
2870
3146
3313
3533
Corres.
States
(kPa)
118
137
164
202
239
285
331
392
443
509
584
673
757
859
963
1104
1219
1310
1352
1420
1572
1746
2072
2259
2502
2751
3010
3281
3354
IP Units
Temp
(OF)
50.5
57.4
66.2
76.6
86.0
95.4
104.0
114.1
121.6
130.6
139.6
149.4
157.8
166.8
175.5
186.1
194.0
199.9
202.5
206.6
215.2
224.4
239.9
247.8
257.5
266.5
275.4
280.6
286.0
Measured
This
Work
(psia)
17.5
20.5
24.5
30.0
35.8
42.2
49.0
58.5
66.1
75.9
86.7
100.1
112.7
127.3
142.0
163.0
178.0
192.2
197.1
212.2
235.8
262.2
313.0
340.8
378.4
416.3
456.3
480.5
512.4
Corres.
States
(psia)
17.1
19.9
23.8
29.3
34.7
41.3
48.0
56.9
64.3
73.8
84.7
97.6
109.8
124.6
139.7
160.1
176.8
190.0
196.1
206.0
228.0
253.2
300.5
327.6
362.9
399.0
436.6
475.9
486.5
%
Dev.
2.6
3.0
3.1
2.7
3.1
2.3
2.1
2.6
2.8
2.5
2.3
2.5
2.5
2.2
1.6
1.7
0.6
1.1
0.6
2.9
3.4
3.4
4.0
3.9
4.1
4.1
4.3
1.0
5.0
-29-
-------
TABLE A-6
Parameters of Eq. (A-1) obtained by a least squares calculation
of vapor pressures measured below the boiling point.
Compound
HFE-125a
HFC-227ea
HFC-227ca
HFC-236fa
HFC-236ea
HFC-236cb
HFC-236ca
HFC-245fa
HFC-245ca
HFC-245cb
HFC-254cb
HFC-329ccb
HFC-338eea
HFC-338cca
HFC-338ccb
HFC-347ccd
HCFC-226da
HCFC-226ea
HCFC-235ca
HCFC-244ca
HCFC-225da
HCFC-225ba
HCFC-234da
HCFC-243da
cy-HCFC-326d
A
SI units (IP units)
48.950 (50,040)
40.725 (41.112)
38.971 (39.128)
46.023 (46.767)
45.842 (46.542)
40.036 (40.262)
44.047 (44.610)
47.161 (47.954)
7.970 (5.299)
18.204 (16.493)
29.555 (28.866)
46.138 (46.886)
15.809 (13.878)
50.452 (51.478)
76.357 (79.790)
33.917 (33.620)
11.604 (9.967)
50.716 (51.889)
59.410 (61.316)
44.209 (44.718)
14.224 (12.293)
31.554 (31.016)
70.182 (72.932)
78.912 (82.443)
43.515 (44.009)
B
SI units (IP units)
3862.2 (6952.0)
3613.1 (6503.6)
3761.3 (6770.3)
4324.3 (7783.8)
4478.1 (8060.7)
4034.0 (7261.1)
4410.9 (7939.6)
4700.0 (8460.0)
3138.1 (5648.5)
2933.3 (5279.9
3565.6 (6418.0)
4526.6 (8147.9)
3342.0 (6015.7)
5331.9 (9597.4)
5916.5 (10649.7)
3907.3 (7033.2)
2819.6 (5075.3)
4691.9 (8445.4)
5282.9 (9509.2)
5098.1 (9176.5)
3313.8 (5604.8)
4303.1 (7745.6)
6546.3 (11783.4)
6962.6 (12532.6)
4735.1 (8523.1)
C
SI or IP
units
5.1395
3.9579
3.5521
4.5497
4.4756
3.6704
4.2424
4.6342
-1.2597
0.3749
2.1126
4.5579
. . -
5.0297
9.1255
2.7798
0.4999
5.2817
6.5274
4.1512
- - -
2.3681
7.9628
9.2916
4.1260
-30-
-------
AEERL-P-909
TECHNICAL REPORT DATA
/Please read Instructions on the reverse before completi
1. REPORT NO
EPA/600/A-93/062
2.
3.
4. TITLE AND SUBTITLE
Physical Properties of Fluorinated Propane and
Butane Derivatives as Alternative Refrigerants
5. REPORT DATE
6. PERFORMING ORGANIZATION CODE
7.AUTHOR
------- |