Saturated Pressure Measurements of trans-1,3,3,3-Tetrafluoroprop-1

Article pubs.acs.org/jced

Saturated Pressure Measurements of trans-1,3,3,3Tetrafluoroprop-1-ene (R1234ze(E)) for Reduced Temperatures Ranging from 0.58 to 0.92 Giovanni Di Nicola,† J. Steven Brown,‡ Laura Fedele,*,§ Sergio Bobbo,§ and Claudio Zilio∥ †

Dipartimento di Energetica, Università Politecnica delle Marche, via Brecce Bianche 12, 60131 Ancona, Italy Department of Mechanical Engineering, The Catholic University, Washington, District of Columbia, United States § Istituto per le Tecnologie della Costruzione, Consiglio Nazionale delle Ricerche, Corso Stati Uniti 4, 35131 Padova, Italy ∥ Dipartimento di Ingegneria Industriale, Università degli Studi di Padova, Padova, I-35131, Italy ‡

ABSTRACT: trans-1,3,3,3-Tetrafluoroprop-1-ene (R1234ze(E)) is a promising alternative foam blowing agent, aerosol propellant, and refrigerant primarily because of its low global warming potential of approximately 6. There are few measured thermodynamic data in the public domain. Herein, 78 vapor-pressure data for temperatures between (223.1 and 353.1) K from two different laboratories are presented, and these results are fitted to Wagner-type and extended Antoine-type equations and compared to literature data. The normal boiling temperature for R1234ze(E) is estimated to be 254.21 K.

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INTRODUCTION Currently there is interest in substances, for example, blowing agents, propellants, and refrigerants, possessing low global warming potential (GWP). One of the primary reasons for this is the increasing amount of taxes, laws, and regulations being proposed and implemented by various government bodies. Recently, fluorinated isomers of propylene have received considerable attention as potential new and replacement refrigerants with low GWPs. The two that are receiving the most focus are R1234ze(E) (trans-1,3,3,3-tetrafluoroprop-1ene; CF3CHCHF), with a GWP of 6 relative to carbon dioxide1 based on a 100-year time frame and R1234yf (2,3,3,3tetrafluoroprop-1-ene; CF3CFCH2), with a GWP of 4 relative to carbon dioxide2 over the same time frame. R1234yf is considered as a potential replacement of R134a in automotive applications.3 For these two isomers, a rather limited set of thermophysical property data and equations of state (EoS) based on them are beginning to appear in the public domain, which has motivated the present authors to begin investigating these two isomers. In particular, they have published vapor-pressure data,4,5 pressure−temperature−volume data in the vapor phase,6 and compressed liquid density data7 for R1234yf and solubility data for PAG/R1234yf mixtures.8 This paper is a continuation of these investigations by presenting vapor-pressure data for R1234ze(E) from two different laboratories. In particular, the two laboratories are the Thermodynamic Properties Laboratory of the Istituto per le Tecnologie della Costruzione del Consiglio Nazionale delle Ricerche (ITC−CNR) and the © 2012 American Chemical Society

Dipartimento di Ingegneria Industriale e Scienze Matematiche of the Università Politecnica delle Marche (UnivPM). While there is already some published data for R1234ze(E), there is need for additional experimental property data. To date, experimental data are reported in the public domain for critical state properties,9 vapor pressure,10−13 liquid density,9−14 vapor density,9,11,12,14,15 isobaric and isochoric specific heats,14,16−18 speed of sound,19,20 surface tension,10 liquid and vapor thermal conductivities,10 and liquid and vapor viscosities.10 Several EoS are presented: extended corresponding states (ECS) EoS,10,21 Peng−Robinson (PR) EoS,22 and FEQ Helmholtz EoS.12,23,24 This paper reports vapor-pressure measurements for R1234ze(E) for temperatures ranging from approximately (223.1 to 353.1) K, presents correlations based on these data, and compares previously existing data to existing correlations and to the ones developed herein.

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EXPERIMENTAL SECTION Materials. R1234ze(E) (trans-1,3,3,3-tetrafluoroprop-1-ene, CF3CHCHF, CAS No. 1645-83-6) was provided by Honeywell with a declared purity higher than 0.995 in mass fraction. Table 1 provides a summary of the sample description. However, to eliminate the presence of any remaining noncondensable gases, the refrigerant was subjected to several cycles of freezing, evacuation, melting, and ultrasonic agitation. Received: January 23, 2012 Accepted: May 31, 2012 Published: July 5, 2012 2197

dx.doi.org/10.1021/je300240k | J. Chem. Eng. Data 2012, 57, 2197−2202

Journal of Chemical & Engineering Data

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Table 1. R1234ze(E) Sample Description

a

chemical name

source

initial mass fraction purity

purification method

final mass fraction purity

analysis method

R1234ze(E)a

Honeywell

0.995

−

−

−

trans-1,3,3,3-Tetrafluoroprop-1-ene.

Figure 1. VLE apparatus. A = equilibrium cell, B = magnetic pump, C = cooler, D = thermal resistance, E = PID control reference thermometer, F = measurement thermometer.

of five readings separated by approximately intervals of 10 min, with deviations lower than 0.1 kPa, was taken as the experimental vapor pressure. After a vapor-pressure measurement was taken at a given temperature, the bath temperature was adjusted to the next desired level. To confirm the reliability of the setup, seven 1,1,1,2tetrafluoroethane (R134a) vapor-pressure data5 plus an additional eight for this paper were measured between (255.16 and 337.15) K. The mean absolute deviation (ΔP/P = (Pcalc − Pexp)/Pcalc) relative to Refprop 9.024 was 100·ΔP/P = 0.02 %, indicating reliability in the measurement methodology. UnivPM. The vapor-pressure data were acquired with a constant volume setup consisting of a stainless steel sphere of approximately (273.5 ± 0.3) cm3 at room temperature. The apparatus has already been described in detail26,27 (Figure 2). Here, only a description in abbreviated form is provided. Two different thermostatic baths in which the test cell and pressure transducer could be immersed allowed for operation from approximately (210 to 290) K and (290 to 360) K. A PID controller maintained the set temperature by means of a calibrated 25 Ω platinum resistance thermometer

Experimental Apparatus and Procedure. ITC−CNR. The saturated pressure measurements were obtained by means of a static vapor−liquid equilibrium (VLE) apparatus in the temperature range between (257.14 and 343.15) K. The VLE apparatus, shown in Figure 1, is already described in detail elsewhere;25 therefore, only a few details are provided here. The sample was maintained at isothermal conditions in a 50 cm3 stainless steel cell, which included a glass window for the visual inspection of the meniscus and a magnetic pump for fluid stirring. A temperature stability of ± 1 mK was maintained by a thermostatic water/ethylene glycol bath of about 100 L in which the cell was immersed. A total experimental temperature uncertainty of 0.03 K was obtained by use of a 100 Ω platinum resistance thermometer (ISOTECH 909/100). A RUSKA 6000 transducer recorded pressure measurements with a total uncertainty of less than 1 kPa. Before charging the sample, the test setup was subjected to vacuum for 24 h. After the desired temperature was reached through means of the thermostatic bath, the magnetic pump was actuated to accelerate achievement of equilibrium. The data were recorded at least two hours after temperature stabilization so as to ensure pressure stabilization had occurred. The average 2198



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in the ITC−CNR laboratory, and twenty-nine R1234ze(E) vapor-pressure data were measured from (223.10 to 353.08) K in the laboratory of UnivPM. These values are provided in Tables 1 and 3 and Figure 3, which also includes comparisons with R134a and R1234yf.

Figure 2. Isochoric apparatus. 1 = constant volume spherical cell, 2 = auxiliary cell, 3 = magnetic pump, 4 = differential pressure transducer, 5 = electronic null indicator, 6 = charging system, 7 = thermostatic baths, 8 = platinum thermoresistances, 9 = thermometric bridge, 10 = stirrer, 11 = heater, 12 = power system, 13 = cooling coil, 14 = connections to auxiliary thermostatic bath, 15 = acquisition system, 16 = Bourdon gauge, 17 = dead weight gauge, 18 = vibrating cylinder pressure gage, 19 = precision pressure controller, 20 = nitrogen reservoir, 21 = vacuum pump system.

Figure 3. Experimental saturated pressure for R1234ze(E): ○, Table 2; ▽, Table 3; for R134a: ■, Fedele et al.5 and new data of ITC− CNR; ●, data of UnivPM. Calculated saturation pressure by means of Refprop 9.024 for , R1234ze(E); ··, R134a;  , R1234yf.

Table 2. Vapor-Pressure Measurements for R1234ze(E) from the ITC−CNR Laboratory for T Ranging from Approximately (257.14 to 343.15) Ka

(Hart Scientific 5680), with a total uncertainty of approximately 0.03 K. A Ruska 7000 transducer recorded pressure measurements with a total uncertainty of less than 1 kPa. Before charging the sample, the cell was evacuated and placed in the appropriate thermostatic bath. After achieving the set temperature, a mixing pump was activated for approximately 15 min after which the sample was allowed to stabilize for approximately 20 min, after which the data was recorded. After a vapor-pressure measurement was taken at a given temperature, the thermostatic bath temperature was adjusted to the next desired level. To confirm the reliability of the setup, seven 1,1,1,2tetrafluoroethane (R134a) vapor-pressure data were measured by UnivPM between (243.10 and 352.93) K. The mean absolute deviation (ΔP/P = (Pcalc − Pexp)/Pcalc) relative to Refprop 9.024 was 100·ΔP/P = 0.03 %, indicating reliability in the measurement methodology.

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RESULTS AND DISCUSSION Prior to discussing the vapor-pressure data and correlations, the critical state properties will be presented as these are needed in the development of vapor-pressure correlations and EoS. Critical State Properties. Experimentally measured values of critical temperature (Tc) = 382.51 ± 0.01 K, critical pressure (Pc) = 3632 kPa ± 3 kPa, and critical density (ρc) = 485 ± 3 kg·m−3 have been reported.9 The critical state properties given by Refprop24 are Tc = 382.52 K, Pc = 3636.3 kPa, and ρc = 489.24 kg·m−3. In this paper, the critical state properties of Higashi et al.9 are used to fit the new data and develop two vapor-pressure correlations. Experimental Saturated Pressure. Forty-nine R1234ze(E) vapor-pressure data were measured from (257.14 to 343.15) K

a

T/K

Pexp/MPa

T/K

Pexp/MPa

257.14 259.15 261.15 263.15 265.15 267.15 269.15 271.15 273.15 275.15 277.15 279.15 281.15 283.15 285.15 287.15 289.15 289.15 291.15 291.15 293.15 293.15 295.15 297.15 299.15

0.115 0.125 0.136 0.147 0.160 0.173 0.186 0.201 0.216 0.233 0.250 0.269 0.288 0.308 0.330 0.352 0.376 0.376 0.401 0.401 0.427 0.427 0.455 0.484 0.514

301.15 303.15 303.15 305.15 305.15 307.15 309.15 311.15 313.15 315.15 317.15 319.15 321.15 323.15 325.15 327.15 329.15 331.15 333.15 335.15 337.15 339.15 341.15 343.15

0.546 0.579 0.579 0.614 0.613 0.649 0.687 0.726 0.767 0.810 0.854 0.900 0.948 0.998 1.050 1.104 1.160 1.218 1.278 1.340 1.405 1.472 1.541 1.613

Standard uncertainties are u(T) = 0.03 K and u(P) < 1 kPa.

Literature Saturated Pressure. There have been a total of 119 experimental vapor-pressure data published thus far in the public domain by four different research groups: 49 data for T 2199



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approximately from (254 to 380) K,10 32 data for T approximately from (283 to 330) K,11 30 data for T approximately from (275 to 330) K,12 and 8 data for T approximately from (310 to 380) K.13 Vapor-Pressure Correlations. Grebenkov et al.10 provide an extended Antoine vapor-pressure correlation, McLinden et al.12,24 provide a FEQ Helmholtz EoS, and Tanaka et al.13 provide a Wagner-type vapor-pressure correlation. Each correlation is based on the particular authors' experimental data set. Tables 2 and 3 data were regressed to develop a Wagner-type correlation (eq 1) and an extended Antoine-type correlation (eq 2).

with the constants specified in Table 4 and where the reduced temperature Tr = T/Tc, the reduced pressure Pr = P/Pc, and τ = 1 − Tr. Table 5 shows the deviations (100·ΔP/P) between the vapor-pressure correlations and the measured data sets. In Figures 4 and 5, deviations of eq 1 from the available vapor

Table 3. Vapor-Pressure Measurements for R1234ze(E) from the Laboratory of UnivPM for T Ranging from Approximately (223.10 to 353.08) Ka

a

T/K

Pexp/MPa

T/K

Pexp/MPa

223.10 228.08 232.99 238.04 243.02 248.04 253.02 258.04 263.10 268.01 273.06 278.01 282.93 287.89 292.85

0.021 0.028 0.036 0.047 0.061 0.077 0.096 0.119 0.147 0.178 0.216 0.258 0.306 0.361 0.423

297.87 297.69 298.77 303.68 308.82 312.85 317.75 323.10 328.12 333.11 338.11 343.10 348.09 353.08

0.495 0.492 0.508 0.588 0.681 0.761 0.868 0.997 1.130 1.276 1.436 1.610 1.799 2.005

Figure 4. Relative differences ΔP/P = (Pcalc − Pexp)/Pexp of eq 1 (Pcalc) from experimental values (Pexp) for R1234ze(E) of ◆, Grebenkov et al.;10 □, Kayukawa and Fujii et al.;11 ▲, McLinden et al.;12 ○, Tanaka et al.;13 gray ●, Table 2; gray ▲, Table 3.

pressure are shown. The data of McLinden et al.12 and Tanaka et al.,13 Tables 2 and 3, are consistent with each other; however, the data of Grebenkov et al.10 and Kayukawa and Fujii11 are inconsistent with the other data sets, which is particularly so for the data of Grebenkov et al.10 It also should be noted that the only data set to contain measurements (seven of them) below T = 254 is the one of UnivPM (Table 3). The correlation of Grebenkov et al.10 is able to only predict its own data set with some accuracy, and the correlation of Tanaka et al.13 is not able to capture the low temperature data of Table 3. Note that the lowest temperature used in developing the correlation of Tanaka et al.13 is 310 K. Therefore, the correlations of Grebenkov et al.10 and Tanaka et al.13 should be used with care.

Standard uncertainties are u(T) = 0.03 K and u(P) < 1 kPa.

Tr ln(Pr) = A1τ + A 2 τ1.5 + A3τ 2.5 + A4 τ 5

ln(Pr) = A1 +

(1)

A2 + A4 Tr + A5Tr 2 + A 6 ln(Tr) A3 + Tr

(2)

Table 4. Constants for Equations 1 and 2 Derived from the Data of Tables 2 and 3 eq 1 eq 2

A1

A2

A3

A4

A5

A6

−7.5046 529.6040

1.5524 2032.27

−2.2353 −4.5000

−4.1018 −16.6908

67.7248

54.1696

Table 5. Relative and Absolute Differences ΔP/P = (Pcalc − Pexp)/Pexp of Five Vapor-Pressure Correlations data set literature data

10

literature data11 literature data12 literature data13 Table 2 Table 3

100·ΔP/P |100·ΔP/P| 100·ΔP/P |100·ΔP/P| 100·ΔP/P |100·ΔP/P| 100·ΔP/P |100·ΔP/P| 100·ΔP/P |100·ΔP/P| 100·ΔP/P |100·ΔP/P|

eq 1

eq 2

eq 9

eq 11

eq 12

1.911 1.814 −0.095 0.744 0.026 0.047 0.053 0.053 −0.013 0.027 0.016 0.054

1.844 1.992 −0.108 0.723 −0.057 0.082 −0.123 0.144 −0.023 0.041 0.004 0.049

−0.004 1.172 −1.964 1.964 −1.620 1.657 −1.249 1.404 −1.936 1.936 −2.702 2.702

1.887 2.007 −0.127 0.723 −0.016 0.024 0.006 0.029 −0.044 0.045 0.063 0.103

3.759 3.862 −0.095 0.744 0.573 0.611 −0.000 0.014 1.153 1.207 6.643 6.656

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reactions with Cl atoms, OH radicals, and O3. Chem. Phys. Lett. 2007, 443, 199−204. (2) Nielsen, O. J.; Javadi, M. S.; Sulback Andersen, M. P.; Hurley, M. D.; Wallington, T. J.; Singh, R. Atmospheric chemistry of CF3CF CH2: Kinetics and mechanisms of gas-phase reactions with Cl atoms, OH radicals, and O3. Chem. Phys. Lett. 2007, 439, 18−22. (3) SAE. Industry evaluation of low global warming potential refrigerant HFO-1234yf. 2009. Retrieved online at: http://www.sae.org/ standardsdev/tsb/cooperative/crp1234-3.pdf (accessed Dec 12, 2011). (4) Di Nicola, G.; Polonara, F.; Santori, G. Saturated pressure measurements of 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf). J. Chem. Eng. Data 2010, 55, 201−204. (5) Fedele, L.; Bobbo, S.; Groppo, F.; Brown, J. S.; Zilio, C. Saturated pressure measurements of 2,3,3,3-tetrafluoroprop-1-ene (R1234yf) for reduced temperatures ranging from 0.67 to 0.93. J. Chem. Eng. Data 2011, 56, 2608−2612. (6) Di Nicola, C.; Di Nicola, G.; Pacetti, M.; Polonara, F.; Santori, G. P-V-T behavior of 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) in the vapor phase from (243 to 373) K. J. Chem. Eng. Data 2010, 55, 3302− 3306. (7) Fedele, L.; Brown, J. S.; Colla, L.; Ferron, A.; Bobbo, S.; Zilio, C. Compressed liquid density measurements for 2,3,3,3-tetrafluoroprop1-ene (R1234yf). J. Chem. Eng. Data 2012, 57, 482−489. (8) Bobbo, S.; Groppo, F.; Scattolini. M.; Fedele, L. R1234yf as a substitute of R134a in air conditioning: Solubility measurements in commercial PAG. Proceedings of the 23rd IIR International Congress of Refrigeration, Prague, Czech Republic, August 21−26, 2011; paper ICR-528. (9) Higashi, Y.; Tanaka, K.; Ichikawa, T. Critical parameters and saturated densities in the critical region for trans-1,3,3,3-tetrafluoropropene (HFO-1234ze(E)). J. Chem. Eng. Data 2010, 55, 1594− 1597. (10) Grebenkov, A. J.; Hulse, R.; Pham, H.; Singh, R., Physical properties and equation of state for trans-1,3,3,3-tetrafluoropropene. Proceedings of the 3rd IIR Conference on Thermophysical Properties and Transfer Processes of Refrigerants, Boulder, CO, USA, June 21−26, 2009; paper IIR-191. (11) Kayukawa, Y.; Fujii, K., Vapor pressures and gas-phase PVT properties for hydrofluorooelfin refrigerant. Proceedings of the 2009 Symposium on Environmental Engineering, Okinawa, Japan, October 20−24, 2009; paper A134. (12) McLinden, M. O.; Thol, M.; Lemmon E. W., Thermodynamic properties of trans-1,3,3,3- tetrafluoropropene [R1234ze(E)]: Measurements of density and vapor pressure and a comprehensive equation of state. Proceedings of the 2010 International Refrigeration and Air Conditioning Conference at Purdue, West Lafayette, IN, USA, July 12− 15, 2010; paper 2189. (13) Tanaka, K.; Takahashi, G.; Higashi, Y. Measurements of the vapor pressures and pρT properties for trans-1,3,3,3-tetrafluoropropene (HFO-1234ze(E)). J. Chem. Eng. Data 2010, 55, 2169−2172. (14) Matsuguchi, A.; Kagawa, N.; Koyama, S., Study on isochoric specific heat capacity of liquid HFO-1234ze(E). Proceedings of the 2010 International Symposium on Next-generation Air Conditioning and Refrigeration Technology, Tokyo, Japan, February 17−19, 2010; paper GS08-1-5. (15) Tanaka, K.; Higashi, Y. PρT Property Measurements for trans1,3,3,3-Tetrafluoropropene (HFO-1234ze(E)) in the Gaseous Phase. J. Chem. Eng. Data 2010, 55, 5164−5168. (16) Kagawa, N.; Matsuguchi, A.; Watanabe, K. Measurement of isobaric heat capacity of gaseous trans-1,3,3,3-tetrafluoropropene (HFO 1234ze). Proceedings of the Fifth Asian Conference on Refrigeration and Air Conditioning, Tokyo, Japan, June 7−9, 2010; Paper D3-025. (17) Tanaka, K.; Takahaski, G.; Higashi, Y. Measurements of the Isobaric Specific Heat Capacities for trans-1,3,3,3-Tetrafluoropropene (HFO-1234ze(E)) in the Liquid Phase. J. Chem. Eng. Data 2010, 55, 2267−2270. (18) Yamaya, K.; Matsuguchi, A.; Kagawa, N.; Koyama, S. Isochoric specific heat capacity of trans-1,3,3,3-tetrafluoropropene (HFO-1234ze(E))

Figure 5. Relative differences ΔP/P = (Pcalc − Pexp)/Pexp of eq 1 (Pcalc) from experimental values (Pexp) for R1234ze(E) of ▲, McLinden et al.;12 ○, Tanaka et al.;13 gray ●, Table 2; gray ▲, Table 3.

The correlation of McLinden12,24 and those of eqs 1 and 2 can accurately predict the consistent data sets of McLinden et al.12 and Tanaka et al.13 and Tables 2 and 3. Normal Boiling-Point Temperature. The correlations of Grebenkov et al.,9 McLinden et al.,11 and Tanaka et al.12 yield normal boiling point (NBP) temperatures of 254.93 K, 254.19 K, and 252.01 K, respectively, and eq 1 yields a NBP temperature of 254.21K.

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CONCLUSIONS Herein, 78 vapor-pressure data of R1234ze(E) (trans-1,3,3,3tetrafluoroprop-1-ene; CF3CHCHF) from two different laboratories for reduced temperatures from 0.67 to 0.93 are provided, which represent approximately 40 % of the publicly available data published thus far from six different research groups. The data from two of these groups (Tables 2 and 3) were used to develop Wagner-type and extended Antoine-type vapor-pressure correlations. The Wagner-type correlation (eq 1) provides the lowest mean absolute deviation (|100·ΔP/P|) of 0.049 when compared to the data of McLinden et al.12 and Tanaka et al.13 and Tables 2 and 3. This is followed by the correlations of McLinden et al.,12,24, eq 2, Grebenkov et al.,10 and Tanaka et al.13, which have mean absolute deviations of 0.053, 0.070, 2.126, and 3.351, respectively, when compared to the same experimental data sets. Finally, eq 1 estimates the normal boiling temperature of R1234ze(E) to be 254.21 K.

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AUTHOR INFORMATION

Corresponding Author

*Tel.: +39 049 8295831. Fax +39 049 8295728. E-mail: laura. [email protected]. Notes

The authors declare no competing financial interest.

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ACKNOWLEDGMENTS The authors thank Mauro Scattolini for his help and Honeywell for the sample. REFERENCES

(1) Søndergaard, R.; Nielsen, O.; Hurley, M.; Wallington, T.; Singh, R. Atmospheric chemistry of trans-CF3CHCHF: Kinetics of the gas-phase 2201



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and the HFO-1234ze(E) + CO2 mixture in the liquid phase. J. Chem. Eng. Data 2011, 56, 1535−1539. (19) Kano, Y.; Kayukawa, Y.; Fujii, K.; Sato, H. Speed-of-sound measurement in gaseous phase for novel refrigerants by using a spherical resonator. Proceedings of the 9th Asian Thermophysical Properties Conference, Beijing, China, October 19−22, 2010; paper 109039. (20) Lago, S.; Albo, P. A. G.; Brignolo, S. Speed of sound results in 2,3,3,3-tetrafluoropropene (R-1234yf) and trans-1,3,3,3-Tetrafluoropropene (R-1234ze(E)) in the temperature range of (260 to 360) K. J. Chem. Eng. Data 2011, 56, 161−163. (21) Akasaka, R. An application of the extended corresponding states model to thermodynamic property calculations for trans-1,3,3,3tetrafluoropropene (HFO-1234ze(E)). Int. J. Refrig. 2010, 33, 907− 914. (22) Brown, J. S.; Zilio, C.; Cavallini, A. Thermodynamic properties of eight fluorinated olefins. Int. J. Refrig. 2010, 33, 235−241. (23) Akasaka, R. New fundamental equations of state with a common functional form for 2,3,3,3-tetrafluoropropene (R-1234yf) and trans1,3,3,3-tetrafluoropropene (R-1234ze(E)). Int. J. Thermophys. 2011, 32, 1125−1147. (24) Lemmon, E. W.; Huber, M. L.; McLinden, M. O. NIST Standard Reference Database 23, Reference Fluid Thermodynamic and Transport Properties (REFPROP), version 9.0; National Institute of Standards and Technology: Gaithersburg, MD, 2010 (R134a.fld file dated November 10, 2010 and R1234yf.fld file dated December 22, 2010). (25) Bobbo, S.; Stryjek, R.; Elvassore, N.; Bertucco, A. A recirculation apparatus for vapor−liquid equilibrium measurements of refrigerants. Binary mixtures of R600a, R134a and R236fa. Fluid Phase Equilib. 1998, 150−151, 343−352. (26) Giuliani, G.; Kumar, S.; Zazzini, P.; Polonara, F. Vapor Pressure and Gas Phase PVT Data and Correlation for 1,1,1-Trifluoroethane (R143a). J. Chem. Eng. Data 1995, 40, 903−908. (27) Di Nicola, G.; Polonara, F.; Ricci, R.; Stryjek, R. PVTx Measurements for the R116 + CO2 and R41 + CO2 Systems. New Isochoric Apparatus. J. Chem. Eng. Data 2005, 50, 312−318.

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Saturated Pressure Measurements of trans-1,3,3,3-Tetrafluoroprop-1

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