Measurements and New Vapor Pressure Correlation for HFO-1234ze

Article pubs.acs.org/jced

Measurements and New Vapor Pressure Correlation for HFO1234ze(E) Baolin An,†,‡ Fufang Yang,† Yuanyuan Duan,*,† and Zhen Yang† †

Key Laboratory for Thermal Science and Power Engineering of Ministry of Education, Beijing Key Laboratory for CO2 Utilization and Reduction Technology, Tsinghua University, Beijing 100084, China ‡ CAS Key Laboratory of Cryogenics, Technical Institute of Physics and Chemistry, Beijing 100190, China ABSTRACT: The vapor pressure of HFO-1234ze(E) (trans1,3,3,3-tetrafluoropropene) was measured from 235 to 381 K for pressures from 40 to 3493 kPa using a Burnett apparatus. The temperature measurement uncertainty was estimated to be 2.3 mK, and the pressure uncertainty was estimated to be 600 Pa. A Wagner-type equation was used to correlate the vapor pressure of HFO-1234ze(E) based on the experimental data. This vapor equation has five coefficients and correlates the vapor pressure data of this work with a maximum relative deviation of 0.00082.

1. INTRODUCTION Organic Rankine cycles (ORCs) make good use of low-grade heat sources and have been extensively researched in reccent years.1−7 Since the 1990s, the global warming impact of refrigerant emissions has received wide attention, so much effort has been made to search for alternative refrigerants with low global warming potential (GWP) and high efficiencies.8−11 The working fluid is very important for both ORCs and refrigeration systems. HFO-1234ze(E) is a promising working fluid for ORCs due to its low GWP, zero ODP (ozone depletion potential), very low flammability, and suitable thermodynamic properties. Thus, HFO-1234ze(E) has recently been frequently selected as the working fluid for ORC systems and refrigeration systems.3,4,10,11 The fluid thermophysical properties must be accurately obtained for proper design and operation of ORC and refrigeration systems. The working fluid vapor pressure is one of the most fundamental thermophysical properties that has been extensively investigated.12−18 For ORC and refrigeration systems, the vapor pressure directly influences the system performance through the evaporation and condensation processes. Thus, accurate system designs using HFO1234ze(E) need reliable vapor pressure data. Di Nicola et al. measured HFO-1234ze(E) vapor pressure from 223 to 353 K, McLinden et al. measured HFO-1234ze(E) vapor pressure from 260 to 380 K, and Tanaka et al. measured HFO1234ze(E) vapor pressure from 310 to 380 K.19−21 However, the data points of Di Nicola et al. show obvious relative differences to calculations by REFPROP 9.1.19,22 McLinden et al. and Tanaka et al. only gave 37 data points.20,21 Therefore, the vapor pressures of HFO-1234ze(E) were measured in this study from 40 to 3493 kPa and from 235 to 381 K using a Burnett apparatus. Then, a Wagner-type equation was used to © 2016 American Chemical Society

correlate the HFO-1234ze(E) vapor pressures from the experimental data.

2. EXPERIMENT Chemicals. HFO-1234ze(E) was supplied by the Beijing Yuji Science & Technology Co., Ltd. The HFO-1234ze(E) sample was measured with an ISQ Trance 1300 to identify the chemical compositions and impurities. The initial temperature was 333.15 K, the final temperature was 553.15 K, and the heating rate was 15 K·min−1. The result shows that the HFO1234ze(E) mole fraction is 0.9996. The main information for the purchased sample is listed in Table 1. Before the vapor pressure measurements, the HFO-1234ze(E) sample was transferred to a stainless steel vessel that was cooled by liquefied nitrogen to remove noncondensable gases (such as air). The procedure was repeated several times to improve the HFO-1234ze(E) purity. Apparatus. The experimental system is shown in Figure 1. The system details were described by Feng et al. and Liu et al.,15,16 with only a brief description given below. The system mainly included a temperature measurement system, a pressure measurement system, two thermostatic baths, a vacuum system, and a data acquisition system. The temperature standard uncertainty was estimated to be 2.3 mK, and the pressure measurements standard uncertainties were listed in Table 2. The differential pressures were measured with two separaters, The two separaters were made of the same material, very close to each other and fixed at the same height in the bath. Because Received: July 27, 2016 Accepted: November 3, 2016 Published: November 15, 2016 328

DOI: 10.1021/acs.jced.6b00673 J. Chem. Eng. Data 2017, 62, 328−332

Journal of Chemical & Engineering Data

Article

Table 1. Fluid Used in This Work name

chemical

source

purity

purification

HFO-1234ze(E)

trans-1,3,3,3-tetrafluoropropene

Beijing Yuji Science & Technology Co., Ltd.

0.9996

none

Figure 1. Vapor pressure measurement apparatus: B, thermostatic bath; H/CP, heater/cooler; MS, mechanical stirrer; DPI, differential pressure detector; MTa, absolute pressure digital manometer; MTgL/MTgH, gauge pressure digital manometer for low and high pressures; PC, personal computer; SC, sample cylinder; ST, super thermometer; T, platinum resistance thermometer; TB, thermometer bridge; VP, vacuum; B1, expansion cell (200 mL) ; B2, sample cell (500 mL); V1−V9, valves.

Table 2. Pressure Measurements Standard Uncertainties manometer type

range/kPa

uncertainty

absolute digital manometer (Yokogawa: MT210) gauge pressure digital manometer (Yokogawa: MT210) Ruska manometer (Ruska: 7050i) differential pressure detector (Rosemount: 3051S)

0−130 up to 3000 up to 10000 0−16

0.0001 of the reading and 0.00005 of the full scale 0.0001 of the reading and 0.00005 of the full scale 0.00005 of the reading 20 Pa

small amount of gaseous HFO-1234ze(E). Then, the valve was closed. The measured vapor pressures before opening the valve were compared with the measured vapor pressures after opening the valve to confirm that there were no noncondensable gases (such as air) in the sample cell and the HFO-1234ze(E) sample was in the two phase vapor−liquid region. Several sets of experimental measurements were carried out to eliminate random and systematic errors.

the unstability and nonuniformity of the thermostatic bath are no more than 2 mK, the influence of temperature on the two separaters can be ignored. Procedure. The Burnett apparatus was composed of two sample cells, and the material of the two sample cells was 316 stainless steel. About 260 g of HFO-1234ze(E) was put into the sample cell. Therefore, the initial density of the measured HFO-1234ze(E) is about 520 kg/m3 which is very close to but a little higher than the critical density, 489 kg/m3. The purpose of this step is to ensure that the vapor pressure measurement can be carried out along more than one isochore to check whether the data are in a two phase vapor−liquid region or not. The temperature and pressure at each state point were measured three times to reduce the experimental error, with the average value of the three measurements used as the final value. When the measurement at one state point was finished, the bath temperature was changed to a new experimental temperature. The sample pressure always changed before equilibrium was achieved. The experimental data at this point were recorded at least 1 h after the sample pressure did not change at the experimental temperature. After the state point data at 313.15 K were recorded, the pressure in the sample was much higher than atmospheric pressure. The valve on the sample cell was then opened at this temperature to release a

3. RESULTS AND DISCUSSION The HFO-1234ze(E) vapor pressures were measured with the temperature range of 235−381 K, and the results were shown in Figure 2 and Table 3. The vapor pressures uncertainties were estimated with the following equation: U (p) = U (pexp ) + (dp /dT ) U (Texp)

(1)

where U(p) is the uncertainty of the vapor pressure, U(pexp) is the uncertainty of the pressure measurement, dp/dT is the vapor pressure first derivative with respect to the temperature, and U(pexp) is the uncertainty of the temperature measurement. The total standard uncertainty of the vapor pressure was 600 Pa 329



Article

Table 3. Experimental Vapor Pressure Data for HFO1234ze(E)

Figure 2. Vapor pressure of HFO-1234ze(E): ,● data points; −, calculated result from eq 2.

A Wagner-type equation was established for the HFO1234ze(E) vapor pressure, based on experimental data in Table 3, with a least-squares fit method:17 5 ⎛ p⎞ T ln⎜⎜ ⎟⎟ = (∑ Ai τ ci) c T ⎝ pc ⎠ i=1

(2)

where pc is the critical pressure, Tc is the critical temperature, T is the temperature, Ai and ci are the fitting coefficients, and τ = 1 − T/Tc. The critical temperature for HFO-1234ze(E) of 382.52 K was used from Di Nicola et al.19 The critical pressure of 3631.81 kPa was extrapolated from eq 2 at the critical temperature. The coefficients in eq 2 are listed in Table 4. The absolute and relative deviations of the measured vapor pressures and calculated results of Thol and Lemmon’ s equation of state for HFO-1234ze(E) from the predictions given by eq 2 are shown in Figures 3 and 4 and listed in Table 5.19−22 The root-mean-square absolute deviation (RMSa) and the root-mean-square relative deviation (RMSb) relative to eq 2 were defined as ⎡ ⎤1/2 N 1 2⎥ ⎢ RMS = ∑ (pj ,exp − pj ,cal ) ⎥ ⎢⎣ N − 1 ⎦ j=1 a

⎡ ⎤1/2 N 1 RMSb = ⎢ ∑ (pj ,exp /pj ,cal − 1)2 ⎥⎥ ⎢⎣ N − 1 ⎦ j=1

(3)

Ta/K

pb/kPa

Ta/K

pb/ kPa

235.009 235.167 239.053 239.070 239.072 242.030 242.044 245.149 245.155 245.157 247.986 248.019 249.380 250.682 250.716 252.236 252.241 252.577 256.245 258.722 258.738 262.014 264.782 268.271 271.723 274.514 277.433 280.734 284.073 287.254 290.507 293.333 296.669 299.734 302.709 303.976 306.419 306.419 308.504 308.505 311.906 311.910 314.303 314.305 316.037

40.19 40.58 49.60 49.60 49.61 57.54 57.54 66.85 66.94 66.90 76.45 76.52 81.49 86.48 86.57 92.69 92.75 94.20 110.47 122.66 122.75 140.52 157.04 179.98 205.14 227.45 252.66 283.77 318.06 353.65 393.03 429.86 476.70 523.05 571.25 592.72 635.82 635.84 674.57 674.57 741.32 741.51 791.29 791.42 829.03

316.040 318.530 319.378 319.379 320.956 323.476 325.227 327.747 329.784 332.091 334.299 336.515 338.428 340.435 342.646 344.942 347.249 349.477 351.211 353.308 355.521 358.516 360.609 362.529 364.709 366.862 367.853 368.951 369.854 371.009 371.913 372.813 374.071 374.899 376.036 377.040 374.071 377.936 378.574 379.161 379.511 379.868 380.023 380.514

829.14 885.61 905.41 905.49 943.34 1006.12 1051.70 1119.92 1177.48 1245.23 1312.84 1383.24 1446.61 1515.02 1593.48 1677.98 1766.38 1855.00 1926.37 2015.30 2112.53 2249.96 2349.94 2444.79 2556.19 2669.59 2724.30 2784.17 2835.52 2900.56 2953.80 3005.54 3082.36 3131.69 3203.11 3265.41 3082.36 3323.47 3364.95 3402.34 3425.95 3450.34 3459.67 3493.46

a

Standard uncertainty for the temperature measurement was estimated to be 2.3 mK. bStandard uncertainty for the pressure measurement was estimated to be 600 Pa.

(4)

where N is the experimental data points number, pj,exp is the experimentally measured vapor pressure, and pj,cal is the vapor pressure predicted from eq 2. The experimental vapor pressures in this work agree well with eq 2. The RMSa is 0.25 kPa with a maximum absolute deviation of 0.81 kPa. On the other hand, RMSb is 0.00021 with a maximum relative deviation of 0.00082.

Table 4. Values of the Coefficients in Equation 2

4. CONCLUSIONS The vapor pressure of HFO-1234ze(E) was measured from 235 to 381 K for pressures from 40 to 3493 kPa using a Burnett apparatus. A Wagner-type vapor pressure equation was used to

i

Ai

ci

1 2 3 4 5

−7.46932 1.32559 −3.52271 2.79659 −20.9931

1.0 1.5 3.0 5.5 7.5

correlate the HFO-1234ze(E) experimental data. The correlation contains five coefficients and correlates the measured vapor 330



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Article

AUTHOR INFORMATION

Corresponding Author

*Tel.: +86 10 6279 6318. E-mail: [email protected]. Funding

This work was supported by the National Natural Science Foundation of China (Grant Nos. 51236004 and 51321002). Notes

The authors declare no competing financial interest.

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Figure 3. Absolute differences of experimental data and calculated results from Thol and Lemmon’ s equation of state to eq 2: □, McLinden et al.;20 ◊, Di Nicola et al.;19 △, Tanaka et al.;21 ●, this work; - -, Thol and Lemmon’ s equation of state.

Figure 4. Relative differences of experimental data points and calculated result from Thol and Lemmon’ s equation of state to eq 2: □, McLinden et al.;20 ◊, Di Nicola et al.;19 △, Tanaka et al.;21 ●, this work; - -, Thol and Lemmon’ s equation of state.

Table 5. Comparisons of Measured HFO-1234ze(E) Vapor Pressure Data to Equation 2a maximum this work Tanaka et al.21 Di Nicola et al.19 McLinden et al.20

absolute diff/kPa

rel diff

RMSa

RMSb

0.81 2.32 1.30 2.20

0.00082 0.00081 0.02225 0.00264

0.25 1.01 0.42 0.61

0.00021 0.00045 0.00375 0.00076

REFERENCES

a

RMSa = root-mean-square absolute deviation. RMSb = root-meansquare relative deviation.

pressures with a maximum relative deviation of 0.00082. The root-mean-square absolute deviation between the equation and the experimental data is 0.25 kPa, and the root-mean-square relative deviation is 0.00021. The measured vapor pressures and the equation provide an accurate basis for predicting the thermophysical properties of HFO-1234ze(E). 331



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(20) 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. International Refrigeration and Air Conditioning Conference, Paper 1041; Purdue University: West Lafayette, IN, USA, 2010. (21) 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. (22) Thol, M.; Lemmon, E. W. Equation of State for the Thermodynamic Properties of trans-1,3,3,3-tetrafluoropropene [R1234ze(E)]. Int. J. Thermophys. 2016, 37, 28−43.

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Measurements and New Vapor Pressure Correlation for HFO-1234ze

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