Measurements of Vapor Pressure and Saturated Liquid Density for

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Measurements of Vapor Pressure and Saturated Liquid Density for HFO−1234ze(E) and HFO−1234ze(Z) Tanaka Katsuyuki* Department of Precision Machinery Engineering, Nihon University, Funabashi, Chiba 274−8501, Japan ABSTRACT: Vapor pressure and saturated liquid density for HFO−1234ze(E) and HFO−1234ze(Z) were measured in the temperature range from 300 to 400 K by using the extraction method. Experimental uncertainties are estimated to be 0.028 K for temperature, 0.4 kPa for pressure, and 0.9 kg·m−3 for density. Vapor pressures were obtained in the pressure range from 526 to 3462 kPa for HFO−1234ze(E) and from 185 to 2309 kPa for HFO−1234ze(Z). Saturated liquid densities were obtained in the density range from 670 to 1158 kg·m−3 for HFO−1234ze(E) and from 843 to 1220 kg·m−3 for HFO− 1234ze(Z). These data are compared with the existing equations of state.

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INTRODUCTION HFO−1234ze(E) (trans-1,3,3,3-tetrafluoropropene) and HFO−1234ze(Z) (cis-1,3,3,3-tetrafluoro-propene) are candidates as low Global Warming Potential (GWP) substances. HFO−1234ze(E), whose normal boiling point is about 254 K, can be substituted for HFC−152a, which is used as a blowing agent. HFO−1234ze(Z), whose normal boiling point is about 283 K, can be substituted for HFC−245fa, which is used as a refrigerant in high-temperature heat pump systems or as working fluids for organic Rankine cycle system. Thermophysical properties of HFO−1234ze(E) and HFO−1234ze(Z) can be calculated by REFProp1 using equations of state developed by Lemmon et al.2 for HFO−1234ze(E) and by Akasaka et al.3 for HFO−1234ze(Z). However, the experimental data used for developing equations of state was few. In this work, to compensate for the lack of data for thermophysical properties of HFO−1234ze(E) and HFO− 1234ze(Z), vapor pressures and saturated liquid densities were measured by the extraction method. These data are compared with the existing equations of state.

Table 1. Sample Information

EXPERIMENTAL SECTION Sample. The sample of HFO−1234ze(E) produced by Honeywell International Inc. was used. The sample of HFO− 1234ze(Z) was supplied by Central Grass Co., Ltd., Japan. The sample information is listed in Table 1. The sample was degassed two or three times by freeze−thaw cycling with liquid nitrogen before it was loaded into the cell of the apparatus. No further purification was done. Apparatus. The apparatus for measuring the vapor pressure and saturated liquid density was developed based on the extraction method and results for HFC-245fa were already obtained in a previous publication.4 The schematic diagram of the apparatus is shown in Figure 1. The apparatus has two cells

Figure 1. Schematic diagram of the apparatus:4 a, main cell; b, subcell; c, pressure sensor; d, platium resistance thermosensor; e, thermometer; f, PID controller; g, vacuum pump; h, recovery cell; i, liquid nitrogen; j, sample bomb; k, main heater; l, subheater; m, stirrer.

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© XXXX American Chemical Society

sample

purity

manufacture

HFO−1234ze(E) HFO−1234ze(Z)

99.5% 99.936%

Honeywell International Inc. Central Glass Co., Ltd.

whose volumes are about 27 cm3 (main cell) and about 3 cm3 (subcell) which are immersed in a thermostat whose temperature was kept constant within ±10 mK. The thermometer (Chino: R900-F25AD) with the uncertainty of 26 mK was Received: December 7, 2015 Accepted: March 8, 2016

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DOI: 10.1021/acs.jced.5b01039 J. Chem. Eng. Data XXXX, XXX, XXX−XXX

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Table 2. Experimental Values of the Vapor Pressure ps, Temperature T, and Saturated Liquid Density ρs for HFO− 1234ze(E)a

used. The valve is equipped between these cells and the pressure sensor is installed in a main cell to measure vapor pressure. The pressure sensor (Kulite: XTEL-190M-70BA) was used and calibrated by the calibrator (Fluke: 717-1000G) with the uncertainty of 0.3 kPa. The principle of the extraction method for measuring vapor pressure and saturated liquid density is shown in Figure 2. The sample is filled in the main

Figure 2. Principle of extraction method for measuring saturated liquid density and vapor pressure:4 (a) Filling sample to main cell; (b) expansion to subcell; (c) recovery sample filled in subcell.

cell as shown in Figure 2a, and then the subcell was vacuumed. As shown in Figure 2b, the saturated liquid is filled in the subcell by opening the valve 1. After closing the valve 1, the sample in the subcell was recovered to the recovery cell using liquid nitrogen as shown in Figure 2c. The mass of the sample in the subcell was determined by measuring the recovery cell before and after recovering the sample. Saturated liquid density can be obtained from the mass of recovered sample and inner volume of the subcell. The volume of the subcell considering its temperature dependence was determined in advance using HFC-134a. The experimental uncertainty of temperature is estimated to be 0.028 K because the uncertainty of the thermometer from the manufacture is 0.026 K and maximum temperature fluctuation is 0.01 K. The experimental uncertainty of pressure is estimated to be 0.4 kPa because the uncertainty of the calibrator from the manufacture is 0.1 kPa and maximum deviation of calibration is 0.3 kPa. The experimental uncertainty of density is calculated using eq 1 and estimated to be 0.9 kg· m−3 because the uncertainty of the sample mass is 1.4 mg against to the maximum sample mass of 3.913 g and the uncertainty of the inner volume of the cell is 0.00024 cm3 against to the maximum inner volume of 3.2254 cm3.

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⎛ ∂ρ ⎞2 2 ⎛ ∂ρ ⎞2 uρ = 2 ⎜ ⎟ uV b + ⎜ ⎟ um2 ⎝ ∂m ⎠ ⎝ ∂Vb ⎠

T/K

ps/kPa

ρs/kg·m−3

300.00 300.00 310.00 310.00 320.00 320.00 330.00 330.00 340.00 340.00 350.00 350.00 360.00 360.00 370.00 370.00 380.00 380.00

526.8 526.6 703.2 702.4 919.6 919.0 1182.6 1182.3 1498.4 1498.6 1874.0 1874.1 2318.0 2319.2 2841.4 2842.7 3460.0 3461.5

1157.7 1158.0 1122.8 1122.8 1085.1 1085.1 1045.3 1044.7 1000.9 1001.5 950.3 950.6 889.8 889.8 810.1 810.1 668.8 670.4

a

Standard uncertainties u are u(T) = 0.028 K, u(ps) = 0.3 kPa, and the combined expanded uncertainty Uc is Uc(ρ) = 0.9 kg·m−3 (0.95 level of confidence).

Table 3. Experimental Values of the Vapor Pressure ps, Temperature T, and Saturated Liquid Density ρs for HFO− 1234ze(Z)a

(1)

RESULTS AND DISCUSSIONS Eighteen data of vapor pressure and saturated liquid density for HFO−1234ze(E) in the temperature range from 300 to 380 K and 22 data of those for HFO−1234ze(Z) in the temperature range from 300 to 400 K were obtained. The experimental values are given in Table 2 for HFO−1234ze(E) and in Table 3 for HFO−1234ze(Z). The temperature dependences are shown in Figure 3 for vapor pressure and in Figure 4 for saturated liquid density. The solid lines are calculations from REFProp.1 Critical points measured by Higashi et al.8,10 are also plotted. Deviations of the vapor pressure data of HFO−1234ze(E) from the equation of state by Lemmon et al.1 is shown in Figure 5. The data by McLinden et al.,5 Nicola et al.,6 and

T/K

ps/kPa

ρs/kg·m−3

300.00 300.00 310.00 310.00 320.00 320.00 330.00 330.00 340.00 340.00 350.00 350.00 360.00 360.00 370.00 370.00 380.00 380.00 390.00 390.00 400.00 400.00

185.9 186.4 260.4 260.6 355.3 355.1 473.3 473.5 619.0 619.2 795.2 794.7 1007.3 1007.3 1258.9 1258.7 1554.1 1556.9 1903.6 1903.7 2308.3 2308.8

1218.6 1219.2 1191.2 1191.2 1162.0 1163.5 1132.5 1131.5 1100.2 1101.7 1066.1 1067.3 1032.6 1032.3 993.0 993.3 951.5 949.7 900.5 901.4 843.9 843.6

a

Standard uncertainties u are u(T) = 0.028 K, u(ps) = 0.3 kPa, and the combined expanded uncertainty Uc is Uc(ρ) = 0.9 kg·m−3 (0.95 level of confidence).

Tanaka et al.7 is also plotted. All data in the temperature range from 300 to 400 K is in good agreement within about 0.1%. Deviations of the saturated liquid density data of HFO− 1234ze(E) from the equation of state by Lemmon et al.1 is shown in Figure 6. The data by Higashi et al.8 and Tanaka et al.7 is also plotted. The data by Higashi et al.,8 Tanaka, and this B

DOI: 10.1021/acs.jced.5b01039 J. Chem. Eng. Data XXXX, XXX, XXX−XXX

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work are in good agreement with the equation of state except for near critical point. Deviations of the vapor pressure data of HFO−1234ze(Z) from the equation of state by Akasaka et al.2 is shown in Figure 7. The data by Fedele et al.,9 Higashi et al.,10 and Kayukawa et

Figure 3. Temperature dependence of the vapor pressure for HFO− 1234ze(E) and HFO−1234ze(Z): ○, HFO−1234ze(E); ×, HFO− 1234ze(Z); ●, critical point of HFO−1234ze(E);8 ◎, critical point of HFO−1234ze(Z);10 Solid line, calculated values from the equations of state.2,3 Figure 7. Deviation plots of the vapor pressure data from the equation of state by Akasaka3 for HFO−1234ze(Z): ●, this work; △, Fedele et al.;9 +, Higashi et al.;10 ◇, Kayukawa et al.11

al.11 are also plotted. The data by Fedele, Higashi, and Kayukawa are in good agreement in the temperature range from 300 to 400 K. The data in this work are in good agreement above 330 K, however their deviations below 320 K become larger to be −1.5% at 300 K. At low temperature, there is only two data sets by Fedel et al. and this work. So additional data at low temperature is expected to be reported. Deviations of the saturated liquid density data of HFO− 1234ze(Z) from the equation of state by Akasaka et al.2 is shown in Figure 8. The data by Higashi et al.10 and Kayukawa

Figure 4. Temperature dependence of the saturated liquid density for HFO−1234ze(E) and HFO−1234ze(Z): ○, HFO−1234ze(E); ×, HFO−1234ze(Z) ; ●, critical point of HFO−1234ze(E);8 ◎, critical point of HFO−1234ze(Z);10 solid line, calculated values from the equations of state.2,3

Figure 8. Deviation plots of the saturated liquid density data from the equation of state by Akasaka3 for HFO−1234ze(Z): ●, this work; △, Higashi et al.;10 ▽, Kayukawa et al.11

Figure 5. Deviation plots of the vapor pressure data from the equation of state by Lemmon2 for HFO−1234ze(E): ●, this work; × , McLinden et al.;5 △, Nicola et al.;6 +, Tanaka et al.7

et al.11 are also plotted. The data by Higashi et al.8 are in good agreement with the equation of state except for near critical point. The data by Kayukawa are in good agreement below 370 K, however their deviations above 380 K become larger to be about 2% at 410 K. The data in this work are in good agreement in the temperature range from 300 to 400 K although the behavior of their deviations linearly changes as the temperature rises.

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CONCLUSION The measurements of the vapor pressure and saturated liquid density for HFO−1234ze(E) and HFO−1234ze(Z) were conducted by the extraction method. As for HFO−1234ze(E), 18 data of vapor pressure and saturated liquid density in the temperature range from 300 to 380 K were obtained and are in

Figure 6. Deviation plots of the saturated liquid density data from the equation of state by Lemmon2 for HFO−1234ze(E): ●, this work; △, Higashi et al.;8 ×, Tanaka et al.7 C

DOI: 10.1021/acs.jced.5b01039 J. Chem. Eng. Data XXXX, XXX, XXX−XXX

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good agreement within about 0.1% to existing equations of state. As for HFO−1234ze(Z), and 22 data in the temperature range from 300 to 400 K were obtained and are in good agreement with remaining improvements of the existing equations of state. These data compensate for the lack of data for HFO−1234ze(E) and HFO−1234ze(Z) and can be used for improvements of the equations of state.

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AUTHOR INFORMATION

Corresponding Author

*E-mail: [email protected]. Tel.: +81-47-4698396. Fax: +81-47-467-9504. Notes

The authors declare no competing financial interest.

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ACKNOWLEDGMENTS The author thanks to Central Glass Co., Ltd., Japan, for supplying sample of HFO−1234ze(Z). REFERENCES

(1) Lemmon, E. W.; Huber, M. L.; McLinden, M. O. NIST reference database 23: reference fluid thermodynamic and transport propertiesREFPROP, version 9.1.; Standard Reference Data Program; National Institute of Standards and Technology: Gaithersburg, MD, 2013. (2) Lemmon, E. W.; Span, R. Short fundamental equations of state for 20 industrial fluids. J. Chem. Eng. Data 2006, 51, 785−850. (3) Akasaka, R.; Higashi, Y.; Miyara, A.; Koyama, S. A fundamental equation of state for cis-1,3,3,3-tetrafluoropropene (R-1234ze (Z)). Int. J. Refrig. 2014, 44, 168−176. (4) Tanaka, K. Measurements of Vapor Pressure and Saturated Liquid Density for R 245fa. Trans. JSRAE (in Japanese) 2014, 31, 11− 17. (5) McLinden, M. J 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; International Refrigeration and Air Conditioning Conference, West Lafayette, Indiana, July 14−19, 2010; Paper 1041. (6) Di Nicola, G.; Brown, J. S.; Fedele, L.; Bobbo, S.; Zilio, C. Saturated pressure measurements of trans-1, 3, 3, 3-tetrafluoroprop-1ene (R1234ze (E)) for reduced temperatures ranging from 0.58 to 0.92. J. Chem. Eng. Data 2012, 57, 2197−2202. (7) 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. (8) 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. (9) Fedele, L.; Di Nicola, G.; Brown, J. S.; Bobbo, S.; Zilio, C. Measurements and correlations of cis-1, 3, 3, 3-tetrafluoroprop-1-ene (R1234ze (Z)) saturation pressure. Int. J. Thermophys. 2014, 35, 1−12. (10) Higashi, Y.; Hayasaka, S.; Shirai, C.; Akasaka, R. Measurements of PρT properties, vapor pressures, saturated densities, and critical parameters for R 1234ze (Z) and R 245fa. Int. J. Refrig. 2015, 52, 100− 108. (11) Kayukawa, Y.; Tanaka, K.; Kano, Y.; Fujita, Y.; Akasaka, R.; Higashi, Y. Experimental evaluation of the fundamental properties of low-GWP refrigerant R-1234ze (Z). Int. J. Refrig. 2012, 35, 1003.

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DOI: 10.1021/acs.jced.5b01039 J. Chem. Eng. Data XXXX, XXX, XXX−XXX