Article pubs.acs.org/jced
Measurements of Gaseous Pressure-Volume-Temperature Properties for Ethyl Fluoride Xiaoming Zhao,* Guanghua Zhang, and Yu Liu MOE Key Laboratory of Thermo-Fluid Science and Engineering, Xi’an Jiaotong University, Xi’an, Shaanxi 710049, China ABSTRACT: In this paper, the gaseous pressure-volume-temperature properties of ethyl fluoride (HFC-161) were studied over a temperature range from 278 to 378 K and pressures from 135.08 to 4235.22 kPa. A total of 132 data points were acquired using the Burnett isochoric method. The standard uncertainties for temperature and pressure were estimated to be less than 8 mK and 0.7 kPa, respectively. The experimental data were correlated with a virial-type equation of state. The comparisons were carried out between the present data and literature values. In addition, the saturated vapor densities of HFC-161 were derived on the basis of the experimental data.
1. INTRODUCTION The Montreal Protocol established a schedule to phase out the use of chlorofluorocarbons (CFCs) and hydrochlorofluorocarbons (HCFCs) due to their adverse impact on the Earth’s ozone. Ethyl fluoride (HFC-161) is considered an environmentally friendly alternative refrigerant for its zero ozone depletion potential (ODP) and very low global warming potential (GWP). It is also regarded as a component of some newly proposed mixtures to replace R134a, R410A, and R502A.1−3 The thermodynamic properties for HFC-161 were limited until 1999.4−6 Our research team has determined some thermophysical properties of HFC-161 in recent years.7−12 However, few studies have been published on the pressurevolume-temperature (PVT) properties of HFC-161 in vapor phase in addition to that by Chen.13 Chen et al. obtained PVT properties in vapor phase covering a temperature range from 300 to 370 K at pressures from 642 to 3900 kPa. To the author’s knowledge, gaseous PVT properties of HFC-161 in a wide temperature and pressure range are still insufficient. For this reason, PVT measurements were performed for HFC-161 at temperatures ranging from 278.383 to 378.016 K and pressures from 135.08 to 4235.22 kPa by means of a Burnett isochoric technique.
main container and the expansion one were approximately 600 and 300 mL, respectively, and the wall thickness of two cells was 10 mm. The temperature measurement system consisted of a platinum resistance thermometer and a data acquisition unit (Keithley 2000). The thermometer was powered by a highresolution DC power supply (Keithley 2400 sourcemeter); the temperature measurement system includes a standard platinum resistance thermometer (Model: WRPR-T1, No. 92822, Kunming Dafang Instruments Co. Ltd., China). The thermometer was calibrated by ITS-90. The uncertainty of the thermometer is 5 mK; the temperature fluctuation in the bath was controlled within 5 mK, and the uncertainty in the temperature measurement was estimated to be less than 8 mK. The pressure measurement system included a differential pressure transducer (Rosemount 3051) with an accuracy of 0.075% FS and a high-precision pressure sensor (Paroscientific 31K-101) with an accuracy of 0.01% FS. We used nitrogen gas as the transfer medium in the transducer. The total uncertainty of the pressure measurement was less than 0.7 kPa. After the thermal equilibrium between the sample and the thermostatic bath was reached and the pressure stayed constant, the temperature and pressure of the sample were measured by the thermometer and the pressure measurement system, respectively. 2.2. Experimental Method. The Burnett isochoric method14−17 was used to measure the gaseous PVT properties of HFC-161. By applying this method, gaseous PVT properties can be acquired in a wide temperature range with high precision. The Burnett isochoric method adopted in this study was similar to that in the literature.18 A schematic diagram of the experimental system for gaseous PVT properties is shown
2. EXPERIMENTAL SECTION 2.1. Apparatus. A high-precision experimental system for gaseous PVT properties was developed in this study. It mainly included a Burnett apparatus, a temperature measurement system, a pressure measurement system, a high-accuracy thermostatic bath, and a vacuum system, as illustrated in Figure 1. Silicone oil was used in the thermostatic bath as the bath fluid at temperatures ranging from 210 to 420 K. The Burnett apparatus was composed of two cylindrical cells (A and B) made of 1Cr18Ni9Ti stainless steel: A was the main container and B was the expansion container. Volumes of the © XXXX American Chemical Society
Received: February 20, 2017 Accepted: June 7, 2017
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DOI: 10.1021/acs.jced.7b00195 J. Chem. Eng. Data XXXX, XXX, XXX−XXX
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Figure 1. Experimental system of gaseous PVT properties: A, main container; B, expansion container; C, nitrogen; D, sample; E, small gas storage; F, differential pressure transducer; G, pressure transducer; H, pressure acquisition instrument; HC, heater; PT, high-accuracy thermometer; TS, thermometer; TC, controller; DMM, temperature acquisition instrument; TB, thermostatic oil bath; P, pressure gage; Q, vacuum pump; PC, computer.
in Figure 1. The process is as follows. The whole apparatus was evacuated by the vacuum pump. Then, a target amount of HFC161 was charged into the main cell A. The temperature and pressure of the sample in cell A were measured. This was the first point of the Burnett isochoric P-T plane. We needed to ensure the initial state of HFC-161 charged in the main cell was near the saturated vapor phase. The sample was introduced into the main cell, and the thermostatic bath was controlled at the target temperature. After the thermal equilibrium between the sample fluid and thermostatic bath was reached, the pressure of the sample was measured. Then, the apparatus was cooled to the next object temperature along the isochore, and the pressure was obtained after the thermal equilibrium was established between the sample and the thermostatic bath. The apparatus temperature then increased to the initial temperature. Next, the first Burnett expansion was conducted. Expansion container B was evacuated by the vacuum pump to ensure the system vacuum was better than 0.1 Pa. Then, the fluid was introduced into cell B, and the temperature and pressure measurements of the sample in cell A were obtained when the thermal equilibrium was achieved. This formed the first point of the second isochore. Then, the system was cooled to the next desired temperature along the isochore, and the corresponding pressures were measured. The expansion isochoric procedures mentioned above were repeated, and experimental results were recorded along a series of pressures incrementing at 5 K.
Table 1. Samples Used in This Paper chemical name HFC-161 (ethyl fluoride) helium
initial mass fraction purity
source Zhejiang Lantian Environment Protection Hi-Tech Co. Ltd. Shanghai Youjiali Liquid Helium Co. Ltd.
0.9995 0.99999
purification method to liquefy the sample with liquid nitrogen none
separate Burnett expansions of helium (99.999 wt %) were carried out at 324.5K to obtain the volume constant, and the value of N was determined to be 1.5037 by the least-squares method. The experimental density data of helium were compared with the literature values.19,20 The maximum absolute deviation (MAD) was 0.065%, and the average absolute deviation (AAD) was 0.026%, which indicated the reliability and accuracy of the experimental system. The Burnett expansion results of helium are shown in Table 2. 3.3. Experimental Results of HFC-161. Two Burnett isochoric experiments on HFC-161 were conducted. A total of 132 data points were obtained in the temperature range from 278.383 to 378.016 K and pressures from 135.08 to 4235.22 kPa, as shown in Table 3, where Z represents the Table 2. Burnett Expansion Results of Helium and Its Literature Values19,20
3. RESULTS AND DISCUSSION 3.1. Chemicals. The sample of ethyl fluoride was provided by Zhejiang Lantian Environmental Protection Hi-tech Co. Ltd., and the stated mass fraction purity was better than 99.95%. For the effects of impurities to be eliminated, the sample was purified several times by liquefying the sample with liquid nitrogen. The samples of ethyl fluoride and helium used in this paper are described in Table 1. 3.2. Calibration of Volume Constant N. Volume constant N is indispensable for calculating compressibility factor Z. It is defined as the ratio of the total volume of two containers to the volume of the main container. Because both cells were made of the same material, N is only independent of temperature. The effect of pressure variation on the cell volume can also be neglected when the pressure is below 6 MPa. Two B
T/K
p/kPa
Z
ρexp/ kg m−3
ρcal/ kg m−3
100(ρexp − ρcal)/ρcal
324.570 324.573 324.572 324.578 324.573 324.574 324.571 324.515 324.514 324.517 324.515 324.516 324.512 324.514
4532.90 2993.40 1984.00 1315.80 873.44 579.87 385.32 4675.40 3088.50 2045.50 1356.00 900.13 597.53 397.16
1.0190 1.0119 1.0085 1.0057 1.0039 1.0022 1.0014 1.0201 1.0132 1.0091 1.0059 1.0040 1.0022 1.0017
6.598 4.388 2.918 1.941 1.291 0.858 0.571 6.800 4.522 3.007 2.000 1.330 0.884 0.588
6.598 4.385 2.919 1.941 1.291 0.858 0.571 6.803 4.523 3.009 2.000 1.330 0.884 0.588
0.001 0.065 −0.018 −0.021 −0.023 0.026 0.025 −0.040 −0.026 −0.048 −0.019 −0.023 0.030 0.001
DOI: 10.1021/acs.jced.7b00195 J. Chem. Eng. Data XXXX, XXX, XXX−XXX
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Table 3. Gaseous PVT Experimental Data of HFC-161a T/K
p/kPa
Z
ρexp/kg m−3
T/K
p/kPa
Z
ρexp/kg m−3
378.016 378.015 378.011 378.006 378.006 378.010 378.016 378.014 378.010 373.140 373.141 373.144 373.136 373.138 373.133 373.148 373.143 373.138 368.268 368.264 368.263 368.264 368.260 368.261 368.262 368.260 363.358 363.362 363.367 363.368 363.367 363.359 363.367 363.362 358.614 358.607 358.608 358.619 358.613 358.616 358.609 352.744 352.739 352.741 352.748 352.749 352.736 352.737 352.740 352.751 347.853 347.850 347.855 347.853 347.849 347.859 347.861 347.854 343.016 343.021 343.021
4235.22 3335.39 2481.64 1776.12 1240.02 851.98 579.55 391.92 264.55 4091.85 3250.93 2430.12 1744.06 1219.77 838.52 570.74 386.27 260.73 3165.93 2378.24 1712.22 1199.41 825.10 561.93 380.26 256.54 3082.31 2325.74 1680.00 1178.86 811.80 553.08 374.25 252.39 2274.59 1648.32 1158.96 799.33 544.42 368.40 248.43 3018.69 2347.08 1723.98 1222.33 847.82 579.94 393.24 265.25 178.77 2287.35 1687.63 1199.98 833.34 570.22 386.83 260.96 175.51 2227.47 1651.35 1177.41
0.6055 0.7171 0.8023 0.8634 0.9064 0.9365 0.9579 0.9741 0.9887 0.5939 0.7095 0.7975 0.8607 0.9052 0.9357 0.9577 0.9746 0.9892 0.6987 0.7892 0.8544 0.9000 0.9310 0.9534 0.9702 0.9842 0.6912 0.7842 0.8518 0.8988 0.9307 0.9535 0.9702 0.9838 0.7770 0.8467 0.8951 0.9283 0.9508 0.9674 0.9810 0.6404 0.7488 0.8270 0.8817 0.9196 0.9459 0.9645 0.9782 0.9914 0.7395 0.8205 0.8773 0.9161 0.9426 0.9615 0.9754 0.9864 0.7324 0.8165 0.8754
106.825 71.042 47.245 31.420 20.895 13.896 9.241 6.145 4.087 106.604 70.894 47.146 31.354 20.851 13.867 9.221 6.133 4.078 71.038 47.243 31.418 20.894 13.895 9.240 6.145 4.087 70.859 47.122 31.337 20.840 13.859 9.217 6.129 4.076 47.133 31.345 20.845 13.862 9.219 6.131 4.077 77.150 51.308 34.121 22.691 15.090 10.036 6.674 4.438 2.951 51.336 34.140 22.704 15.099 10.041 6.677 4.441 2.953 51.191 34.043 22.640
338.155 338.158 338.160 338.152 338.155 338.153 338.161 333.300 333.295 333.292 333.297 333.299 333.305 328.424 328.421 328.415 328.424 328.426 328.422 328.426 323.512 323.513 323.516 323.513 323.52 323.517 318.667 318.672 318.663 318.672 318.666 318.665 313.802 313.805 313.811 313.802 313.809 313.803 308.967 308.967 308.959 308.962 308.975 303.307 303.316 303.313 303.315 303.309 298.653 298.656 298.654 298.658 298.659 293.095 293.089 293.093 293.097 288.207 288.207 288.205 283.264
1614.54 1154.55 804.44 551.38 374.30 252.41 169.60 1131.52 789.86 541.96 368.16 248.18 166.70 1539.53 1108.32 775.13 532.98 361.91 243.93 163.80 1084.58 760.32 523.39 355.59 239.62 160.85 1060.94 745.44 513.87 349.39 235.35 158.08 1036.81 730.50 504.31 343.12 231.58 155.20 715.60 494.66 336.88 227.65 152.32 697.80 483.63 329.55 222.77 149.42 682.94 474.30 323.48 218.72 146.61 462.98 316.32 213.69 143.41 452.92 309.96 209.64 442.81
0.8101 0.8711 0.9127 0.9407 0.9602 0.9737 0.9838 0.8673 0.9104 0.9393 0.9595 0.9726 0.9824 0.7996 0.8656 0.9103 0.9412 0.9611 0.9740 0.9835 0.8624 0.9091 0.9410 0.9614 0.9741 0.9833 0.8585 0.9070 0.9402 0.9613 0.9737 0.9834 0.8537 0.9044 0.9389 0.9606 0.9749 0.9824 0.9040 0.9396 0.9623 0.9778 0.9838 0.8978 0.9357 0.9588 0.9746 0.9829 0.8962 0.9360 0.9599 0.9759 0.9837 0.9353 0.9609 0.9761 0.9850 0.9298 0.9569 0.9731 0.9287
34.027 22.629 15.048 10.008 6.655 4.426 2.943 22.599 15.029 9.995 6.647 4.420 2.940 33.847 22.509 14.969 9.955 6.620 4.403 2.928 22.444 14.926 9.926 6.601 4.390 2.919 22.390 14.890 9.903 6.585 4.379 2.912 22.346 14.860 9.882 6.572 4.371 2.907 14.793 9.837 6.542 4.351 2.893 14.795 9.838 6.543 4.351 2.894 14.731 9.797 6.515 4.333 2.881 9.751 6.485 4.313 2.868 9.758 6.489 4.316 9.718
C
DOI: 10.1021/acs.jced.7b00195 J. Chem. Eng. Data XXXX, XXX, XXX−XXX
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Table 3. continued T/K
p/kPa
Z
ρexp/kg m−3
T/K
p/kPa
Z
ρexp/kg m−3
343.014 343.016 343.010 343.013 343.029
818.91 560.82 380.56 256.69 172.53
0.9155 0.9428 0.9620 0.9757 0.9861
15.056 10.013 6.659 4.428 2.945
283.262 283.266 278.383 278.388 278.383
303.56 205.41 432.22 297.17 201.28
0.9573 0.9741 0.9261 0.9575 0.9752
6.463 4.298 9.679 6.437 4.281
a
Standard uncertainty u is u(T) = 8 mK and u(P) = 0.7 kPa, and the combined expanded uncertainty Uc,r(ρ) = 0.007 (0.95 level of confidence, k = 2).
Table 4. Numerical Values of the Parameters in Eq 1a
compressibility factor. The experimental uncertainty of the volume constant N is 0.00025. The uncertainty of the compressibility factor Z is estimated to be within 0.007. The density uncertainty was estimated to be less than 0.007. The distributions of gaseous PVT experimental data of HFC-161 were also illustrated in Figure 2, note that the vapor pressure
HFC-161 B0 B1 B2 B3 B4 B5 C0 C1 D0 D1 a
0.6729577 −2.6208096 3.5994588 −1.8046342 0.1804290 −0.0320959 6.0477880e-5 −5.0226732e-5 9.2081725e-8 −1.0529193e-7
Units of Bi−Di are m3 kg−1, (m3 kg−1)2, and (m3 kg−1)3, respectively.
(EOS) for HFC-161 is available in the temperature range from 278 to 378 K and pressures from 135.08 to 4235.22 kPa. Figure 3 shows the deviation distribution of experimental and calculated pressure by eq 1 of HFC-161; the average absolute
Figure 2. Distribution of gaseous PVT experimental data of HFC-161: ■, Chen et al.;13 ○, this work; solid line, vapor pressures calculated from the equation by Wu et al.21
data of HFC-161 was given by Wu.21 Compared with the experimental data proposed by Chen,13 it can be observed that the present data covered a wider temperature and pressure range. Gaseous PVT properties at temperatures below 300 K were first reported in this work. To represent the experimental PVT data in the gas phase of HFC161, a virial-type equation of state was established on the basis of this study, the equation is expressed as p = 1 + Bρ + Cρ2 + Dρ3 ρRT
Figure 3. Deviation distribution of experimental and calculated pressure by eq 1 of HFC-161: ■, Chen et al.;13 ○, this work; solid line, values calculated from eq 1.
B = B0 + B1Tr −1 + B2 Tr −2 + B3Tr −3 + B4 Tr −6 + B5Tr −8 C = C0Tr −5 + C1Tr −6
deviation of experimental data and eq 1 for pressure is 0.21%. The deviation distribution of experimental and calculated density by eq 1 is illustrated in Figure 4; the average absolute deviation of experimental values from eq 1 for density is 0.23%. It can be concluded that the EOS can reproduce the gaseous PVT properties of HFC-161 well. A comparison was conducted between our experimental values and data measured by Chen et al.13 Density deviations of measured PVT values and Chen et al. data are illustrated in Figure 4. Figures 5 and 6 illustrate virial coefficients calculated from eq 1.
D = D0 + D1Tr (1)
where p represents the pressure (Pa), T refers to the temperature (K), the unit of ρ is kg/m3, R (173.2 J K−1 kg−1) is the gas constant of HFC-161, B−D are the second, third, and fourth virial coefficients, respectively, and Bi−Di are parameters with their values listed in Table 4. Tr (= T/Tc) is the reduced temperature, where the critical temperature Tc is 375.25 K for HFC-161.21 The virial-type equation of state D
DOI: 10.1021/acs.jced.7b00195 J. Chem. Eng. Data XXXX, XXX, XXX−XXX
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Table 5. Saturated Vapor Density of HFC-161a
Figure 4. Deviation distribution of experimental and calculated density by eq 1 of HFC-161: ■, Chen et al.;13 ○, this work; solid line, values calculated from eq 1. a
T/K
p/kPa
ρsat/kg m−3
368.26 363.36 358.61 352.74 347.85 343.02 338.16 333.30 328.42 323.52 318.67 313.81 308.97 303.31 298.66 293.09 288.21 283.26
4391.10 4001.20 3652.10 3255.60 2952.00 2674.10 2415.00 2175.20 1952.70 1746.70 1559.10 1386.40 1228.70 1061.60 937.42 803.17 697.78 601.78
151.253 124.095 107.012 90.580 79.303 69.720 61.322 53.957 47.447 41.677 36.628 32.145 28.185 24.122 21.190 18.099 15.728 13.608
Vapor pressures calculated from equation by Wu et al.21
ρr = a0Tr a1 + a 2Tr a3 + a4
(2)
where Tr = T/Tc, ρ = ρ/ρc, and ρc is the critical density (301.81 kg/m3).21 The parameters of eq 2 are listed in Table 6. Eq 2 Table 6. Coefficients in Eq 2 variable
value
a0 a1 a2 a3 a4
0.2398828 68.6171626 0.5090165 9.0857387 0.0058620
can be used to represent the saturated vapor densities of HFC161 for temperatures from 283 to 368 K. This equation fits the saturated vapor densities well with an average absolute deviation of 0.28% and maximum absolute deviation of 0.69%. Figures 7 and 8 show comparisons between the present saturated vapor densities and those of Chen et al. Because
Figure 5. Second virial coefficient calculated from eq 1.
Figure 6. Third virial coefficient calculated from eq 1.
Saturated vapor densities of HFC161 were also acquired on the basis of the present experimental data and vapor pressures,21 and their values are listed in Table 5. A temperature-dependent function was used to represent the saturated vapor densities. The equation was given by
Figure 7. Saturated vapor densities for HFC-161: ■, Chen et al;13 ○, this work; solid line, values calculated from eq 2. E
DOI: 10.1021/acs.jced.7b00195 J. Chem. Eng. Data XXXX, XXX, XXX−XXX
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as an alternative refrigerant to HFC-410A. Energ Buildings 2012, 44, 33−38. (3) Han, X.; Qiu, Y.; Xu, Y.; Zhao, M.; Wang, Q.; Chen, G. Cycle performance studies on a new HFC-161/125/143a mixture as an alternative refrigerant to R404A. J. Zhejiang Univ., Sci., A 2012, 13, 132−139. (4) Booth, H. S.; Swinehart, C. F. The critical constants and vapor pressures at high pressure of some gaseous fluorides of group IV. J. Am. Chem. Soc. 1935, 57, 1337−1342. (5) Grosse, A. V. Refractive indices at low temperatures. J. Am. Chem. Soc. 1937, 59, 2739−2741. (6) Bignell, C. M.; Dunlop, P. J. Second virial coefficients for seven fluoroethanes and interaction second virial coefficients for their binary mixtures with helium and argon. J. Chem. Phys. 1993, 98, 4889−4891. (7) Lv, S.; Zhao, X.; Liu, Y. Measurements for isobaric specific heat capacity of ethyl fluoride (HFC-161) in liquid and vapor phase. Fluid Phase Equilib. 2016, 427, 429−437. (8) Yao, C.; Zhao, X.; Lv, S.; Guo, Z. Thermal conductivity of ethyl fluoride (HFC161). Fluid Phase Equilib. 2014, 375, 228−235. (9) Lv, S.; Zhao, X.; Yao, C.; Wang, W.; Guo, Z. Viscosity of gaseous ethyl fluoride (HFC-161). Fluid Phase Equilib. 2014, 384, 100−105. (10) Fan, J.; Zhao, X.; Guo, Z.; Liu, Z. Saturated Liquid Viscosity of Ethyl Fluoride (HFC161) from 233 to 373 K. Int. J. Thermophys. 2012, 33, 2243−2250. (11) Fan, J.; Zhao, X.; Guo, Z. Surface tension of ethyl fluoride (HFC161) from (233 to 373)K. Fluid Phase Equilib. 2012, 316, 98− 101. (12) Meng, X.; Gu, X.; Wu, J.; Bi, S. Viscosity Measurements of Ethyl Fluoride (R161) from 243 to 363 K at Pressures up to 30 MPa. Int. J. Thermophys. 2015, 36, 2497−2506. (13) Chen, Q.; Hong, R.; Chen, G. Gaseous PVT properties of ethyl fluoride. Fluid Phase Equilib. 2005, 237, 111−116. (14) Duan, Y.; Meng, L. Gaseous PVT properties of 1,1,1,3,3,3hexafluoropropane (HFC-236fa). Fluid Phase Equilib. 2004, 226, 313− 320. (15) Widiatmo, J. V.; Tsuge, T.; Watanabe, K. Measurements of vapor pressures and pvT properties of pentafluoroethyl methyl ether and 1,1,1-trifluoroethane. J. Chem. Eng. Data 2001, 46, 1442−1447. (16) Di Nicola, G. p-v-T behavior of 1,1,1,2,3,3,3-heptafluoropropane (R227ea). J. Chem. Eng. Data 2003, 48, 1332−1336. (17) Feng, X.; Liu, Q.; Zhou, M.; Duan, Y. Gaseous pvTx properties of mixtures of Carbon dioxide and propane with the Burnett isochoric method. J. Chem. Eng. Data 2010, 55, 3400−3409. (18) Yin, J.; Wu, J. Gas phase pvT properties and second virial coefficients of dimethyl ether. Fluid Phase Equilib. 2010, 298, 298− 302. (19) Lemmon, E. W.; Huber, M. L.; Mclinden, M. O. NIST Standard Reference Database 23, NIST Reference Fluid thermodynamic and Transport Properties-REFPROP, version 9.0; Standard Reference Data Program; National Institute of Standards and Technology: Gaithersburg, MD, 2010. (20) McCarty, R. D.; Arp, V. D. A New Wide Range Equation of State for Helium. Adv. Cryog. Eng. 1990, 35, 1465−1475. (21) Wu, J.; Zhou, Y. An Equation of State for Fluoroethane (R161). Int. J. Thermophys. 2012, 33, 220−234.
Figure 8. Deviation distribution of saturated vapor densities by this work and Chen et al.13 from the EOS by Wu and Zhou:21 ■, Chen et al;13 ○, this work; solid line, values calculated from the EOS by Wu and Zhou.21
saturated vapor densities reported by Chen are applicable in the temperature range from 290 to 360 K, the proposed equation extended the temperature range for calculating the densities of the saturated vapor of HFC161.
4. CONCLUSIONS In this study, a high-accuracy experimental measurement system using the Burnett isochoric method was established to measure the gaseous PVT property measurements of HFC-161. A total of 139 data points in the temperature range from 278 to 378 K and pressure range from 135.08 to 4235.22 kPa were obtained along 21 isotherms. A virial-type equation of state for HFC-161 was correlated to reproduce the experimental data with an average absolute deviation of 0.21% in pressure and 0.23% in density. In addition, the saturated vapor densities were also derived at temperatures ranging from 283 to 368 K, and an empirical equation was used to represent the saturated vapor densities with an average absolute deviation of 0.28%.
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AUTHOR INFORMATION
Corresponding Author
*E-mail:
[email protected]. Tel: +86-29-82665445. Fax: +86-29-82668789. ORCID
Xiaoming Zhao: 0000-0003-2938-8080 Notes
The authors declare no competing financial interest.
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ACKNOWLEDGMENTS We acknowledge the support of the National Natural Science Foundation of China (Grant 51676160) and the 111 Project (B16038).
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REFERENCES
(1) Han, X.; Li, P.; Xu, Y.; Zhang, Y.; Wang, Q.; Chen, G. Cycle performances of the mixture HFC-161 + HFC-134a as the substitution of HFC-134a in automotive air conditioning systems. Int. J. Refrig. 2013, 36, 913−920. (2) Han, X.; Qiu, Y.; Li, P.; Xu, Y.; Wang, Q.; Chen, G. Cycle performance studies on HFC-161 in a small-scale refrigeration system F
DOI: 10.1021/acs.jced.7b00195 J. Chem. Eng. Data XXXX, XXX, XXX−XXX
