Article pubs.acs.org/jced
Liquid Density of 2‑Methoxyethyl Acetate, 2‑Ethylhexyl Acetate, and Diethyl Succinate at Temperatures from 283.15 K to 363.15 K and Pressures up to 100 MPa Shengshan Bi,* Tao Jia, Kang Zhao, Xianyang Meng, and Jiangtao Wu Key Laboratory of Thermo-Fluid Science and Engineering, Minister of Education, Xi’an Jiaotong University, Xi’an, Shaanxi 710049, P. R. China S Supporting Information *
ABSTRACT: The density data for 2-ethylhexyl acetate, 2methoxyethyl acetate, and diethyl succinate were reported. The density measurements were conducted with a highpressure vibrating-tube densimeter over 9 isotherms at (283.15 to 363.15) K and 16 isobars at (0.1 to 100) MPa. The uncertainty of each obtained datum was estimated, and the expanded uncertainties of density measurements with a confidence level of 0.95 (k = 2) of density measurement for 2-ethylhexyl acetate, 2-methoxyethyl acetate, and diethyl succinate are 0.1 %. The experimental densities were correlated with the Tait-type equation, and the absolute average percentage deviations were 0.010 %, 0.009 %, and 0.011 % for 2-ethylhexyl acetate, 2-methoxyethyl acetate, and diethyl succinate, respectively. In addition, the isothermal compressibility and the isobaric thermal expansivity were derived from the Tait-type equation. density equipment is estimated to be better than 0.01 kg·m−3. Aminabhavi et al.6 reported the densities of binary mixture (diethylene glycol dimethyl ether + diethyl succinate) measured by a pycnometer at temperatures (298.15 to 318.15 K). The repeatability of the pycnometer is within ±0.2 kg·m−3. In our previous work, the thermal conductivity of 2ethylhexyl acetate, 2-methoxyethyl acetate, and diethyl succinate in liquid phase has already reported.7 The objective of this work is to obtain their liquid densities in the temperature range from (283.15 to 363.15) K and pressures up to 100 MPa. The measured densities have been compared with the published literature data.
1. INTRODUCTION The use of additives in the conventional fossil fuels, represents an excellent way to reduce emissions and improve the efficiency of the vehicles.1 The oxygenated compounds in form of alcohol and ether are common and readily available fuel additives due to their high oxygen content, low greenhouse gas emissions, renewable biomass production, and so on. After the physical and chemical characteristics of some potential oxygenated additives were evaluated, 2-ethylhexyl acetate, 2-methoxyethyl acetate, and diethyl succinate are considered promising candidates in consideration of their higher oxygen content compared to the alcohol. Gong et al.2 found that diesel engine fueled with 2-methoxyethyl acetate can reduce smoke, HC, CO, and NOx emissions. Ramu et al.3 have studied the influence of fuel additives (2-methoxyethyl acetate) plus thermal barrier coating (TBC) on diesel engine performance, combustion, and emission characteristics. Their results showed that NOx emission was further reduced by 10 % in the fuel additive plus thermal-barrier-coated engine. For the industry applications of oxygenated additives, accurate density data are indispensable and required to develop and test the equations of state.4 However, little work has been conducted on the density measurement of the three selected oxygenated additives and then over limited temperature and pressure ranges. Indraswati et al.5 measured the densities of pure liquid and binary mixture(2-ethylhexyl acetate +1pentanol) with a Mettler Toledo density meter (type DE50) at temperatures (293.15 to 323.15) K. And the precision of the © XXXX American Chemical Society
2. EXPERIMENTAL SECTION 2.1. Chemicals. 2-Ethylhexyl acetate, 2-methoxyethyl acetate, and diethyl succinate were provided by Alddin Chemistry Co. Ltd.. The mass purity stated by the manufacturer is better than 0.99. R134a (1,1,1,2-tetrafluoroethane) was obtained from Sinochem Modern Environmental Protection Chemicals with a mass purity of 0.999. R134a was degassed three times with a freeze−pump−thaw cycles by using Special Issue: Memorial Issue in Honor of Anthony R. H. Goodwin Received: May 6, 2015 Accepted: September 14, 2015
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DOI: 10.1021/acs.jced.5b00385 J. Chem. Eng. Data XXXX, XXX, XXX−XXX
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liquid nitrogen and a high vacuum ( 98 %5) E
DOI: 10.1021/acs.jced.5b00385 J. Chem. Eng. Data XXXX, XXX, XXX−XXX
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3.3. Derived Thermodynamics Properties. The temperature and pressure dependence of the isothermal compressibility was calculated with the modified Tait eq 1, which is represented by ⎛ 1 ⎞⎛ ∂ρ ⎞ κT(T , p) = ⎜ ⎟⎜ ⎟ ⎝ ρ ⎠⎝ ∂p ⎠ =
C
(1 − C ln(
B(T ) + p B(T ) + 0.1 MPa
))(B(T) + p)
(8)
According to its definition, the isobaric thermal expansivity data can be obtained analytically by differentiating eq 1, taking into account the temperature dependence of B(T) and ρ0(T). But as Cerdeirina et al.16 and Troncoso et al.17 mention, the estimated isobaric thermal expansivity depends on the form of functions B(T) and ρ0(T). This is the reason why they recommend to derive the isobaric thermal expansivity from the isobaric densities. So at each pressure we suppose that ρp(T) = a0 + a1T + a2T2 + a3T3, and consequently, (∂ρ/∂T)p = a1 + 2a2T + 3a3T2. For each pressure, we get a set (a0, a1, a2, a3). By inserting the determined (∂ρ/∂T)p values and the calculated densities ρp(T) into αp = −(1/ρ)(∂ρ/∂T), the isobaric thermal expansivity at the different T, p conditions has been derived αp = −
a1 + 2a 2T + 3a3T 2 a0 + a1T + a 2T 2 + a3T 3
(9)
As already pointed out, the method used to evaluate the isobaric thermal expansion coefficient may affect the accuracy of the values. It has to be stated (Jacquemin et al.18) that sometimes the values of this coefficient are different from the literature, which is due not only to differences in density values but also to the fitting equations. The isothermal compressibility, κT, and the isobaric thermal expansivity, αp, are reported in Tables S1 to S3 (provided as Supporting Information) and illustrated in Figures S1 to S2 (provided as Supporting Information). As recently indicated on similar high-pressure density study with the same methods,19−22 the estimated relative standard uncertainty is 1 % for the isothermal compressibility, and around 3 % for the isobaric thermal expansivity.
4. CONCLUSIONS In the present work, the experiment was carried out with the high-pressure vibrating tube densimeter system, which was calibrated with vacuum and water. A total of 432 compressed liquid densities of 2-ethylhexyl acetate, 2-methoxyethyl acetate, and diethyl succinate along the nine isotherms between T = (283 and 363) K with pressures up to 100 MPa were presented. The expanded uncertainties with a confidence level of 0.95 (k = 2) for 2-methoxyethyl acetate, 2-ethylhexyl acetate and diethyl succinate are 0.1 %. The experimental densities were fitted with the Tait-type equation with low standard deviations. Moreover, the isobaric thermal expansivity, αp, and the isothermal compressibility, κT, were calculated over the same temperature and pressure ranges.
Figure 2. Comparison of the densities measured for 2-ethylhexyl acetate (a), 2-methoxyethyl acetate (b), and diethyl succinate (c) with the literature values: □, T = 283 K; ■, 293 K; ○, 303 K; ●, 313 K; Δ, 323 K; ▲, 333 K; ▽, 343 K; ▼, 353 K; ◇, 363 K; ★, Indraswati et al.;5 ☆, Aminabhavi et al.6 The baseline is the densities calculated with eqs 1 to 3.
are likely to be one of the reasons for the bigger density values in comparison to our experiment. Aminabhavi et al.6 measured the density of a sample provided by Riedel (Germany, and nominal mole purity of 99.1 %) by a pycnometer with a reported standard uncertainty of 0.2 kg·m−3. It can also be observed from Figure 2c that the densities of the ref 6 are 0.07 %, 0.05 %, 0.04 %, −0.01 %, and 0.02 %, different from those calculated from our correlation at temperatures 298.15 K, 303.15 K, 308.15 K, 313.15 K, and 318.15 K, respectively.
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ASSOCIATED CONTENT
S Supporting Information *
The Supporting Information is available free of charge on the ACS Publications website at DOI: 10.1021/acs.jced.5b00385. F
DOI: 10.1021/acs.jced.5b00385 J. Chem. Eng. Data XXXX, XXX, XXX−XXX
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T. W.; Friend, D. G.; Goodwin, A. R. H.; Hansen, L. D.; Haynes, W. M.; Koga, N.; Mandelis, A.; Marsh, K. N.; Mathias, P. M.; McCabe, C.; O’Connell, J. P.; Pádua, A.; Rives, V.; Schick, C.; Trusler, J. P. M.; Vyazovkin, S.; Weir, R. D.; Wu, J. Improvement of Quality in Publication of Experimental Thermophysical Property Data: Challenges, Assessment Tools, Global Implementation, and Online Support. J. Chem. Eng. Data 2013, 58, 2699−2716. (16) Cerdeirina, C. A.; Tovar, C. A.; Gonzalez-Salgado, D.; Carballo, E.; Romani, L. Isobaric thermal expansivity and thermophysical characterization of liquids and liquid mixtures. Phys. Chem. Chem. Phys. 2001, 3, 5230−5236. (17) Troncoso, J.; Bessieres, D.; Cerdeirina, C. A.; Carballo, E.; Romani, L. Automated measuring device of (p, rho, T) data Application to the 1-hexanol plus n-hexane system. Fluid Phase Equilib. 2003, 208, 141−154. (18) Jacquemin, J.; Husson, P.; Mayer, V.; Cibulka, I. High-pressure volumetric properties of imidazolium-based ionic liquids: Effect of the anion. J. Chem. Eng. Data 2007, 52, 2204−2211. (19) Alaoui, F. E. M.; Montero, E. A.; Bazile, J.-P.; Aguilar, F.; Boned, C. Liquid density of biofuel mixtures: (Dibutyl ether+1-butanol) system at pressures up to 140 MPa and temperatures from (293.15 to 393.15) K. J. Chem. Thermodyn. 2011, 43, 1768−1774. (20) Alaoui, F. E. M.; Montero, E. A.; Bazile, J.-P.; Aguilar, F.; Boned, C. Liquid Density of Biofuel Additives: 1-Butoxybutane at Pressures up to 140 MPa and from (293.15 to 393.15) K. J. Chem. Eng. Data 2011, 56, 595−600. (21) Miyake, Y.; Baylaucq, A.; Plantier, F.; Bessieres, D.; Ushiki, H.; Boned, C. High-pressure (up to 140 MPa) density and derivative properties of some (pentyl-, hexyl-, and heptyl-) amines between (293.15 and 353.15) K. J. Chem. Thermodyn. 2008, 40, 836−845. (22) Milhet, M.; Baylaucq, A.; Boned, C. Volumetric properties of 1phenyldecane and 1-phenylundecane at pressures to 65 MPa and temperature between 293.15 and 353.15 K. J. Chem. Eng. Data 2005, 50, 1430−1433.
Details on the derived thermodynamics properties of 2ethylhexyl acetate, 2-methoxyethyl acetate, and diethyl succinate. (PDF)
AUTHOR INFORMATION
Corresponding Author
*E-mail:
[email protected]. Funding
The authors acknowledge the financial support of the National Natural Science Foundation of China (Grant No. 51276142) and the Fundamental Research Funds for the Central Universities. Notes
The authors declare no competing financial interest.
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DOI: 10.1021/acs.jced.5b00385 J. Chem. Eng. Data XXXX, XXX, XXX−XXX
