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Investigation on Vapor–Liquid Equilibrium for 2-Propanol+1

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Investigation on Vapor–Liquid Equilibrium for 2-Propanol+1 Fluid Phase Equilibria 341 (2013) 30–34 Contents lists available at SciVerse ScienceDirect Fluid Phase Equilibria j ournal homepage: www.elsevier.com/locate/fluid Investigation on vapor–liquid equilibrium for 2-propanol + 1-butanol + 1-pentanol at 101.3 kPa ∗ Juan Wang, Zonghong Bao College of Chemistry and Chemical Engineering, Nanjing University of Technology, Nanjing 210009, PR China a r t i c l e i n f o a b s t r a c t Article history: Isobaric vapor–liquid equilibrium (VLE) data for 2-propanol + 1-butanol, 2-propanol + 1-pentanol, 1- Received 26 September 2012 butanol + 1-pentanol and 2-propanol + 1-butanol + 1-pentanol were measured at 101.3 kPa by using an Received in revised form 5 December 2012 improved Rose still. All the binary VLE data have passed the traditional area test proposed by Herington. Accepted 18 December 2012 The interaction parameters for the Wilson, NRTL and UNIQUAC equations were determined by regress- Available online 7 January 2013 ing the binary VLE data. The prediction for ternary system was given by using the three pairs of binary parameters correlated. And the ternary data predicted agreed well with the experiment data. Keywords: © 2013 Elsevier B.V. All rights reserved. 2-Propanol 1-Butanol 1-Pentanol Vapor–liquid equilibrium 1. Introduction 1-pentanol and ternary mixture of 2-propanol + 1-butanol + 1- pentanol were obtained at 101.3 kPa. The experimental values were Currently the international oil price has been rising, and the correlated by the Wilson, NRTL and UNIQUAC equations, in which domestic oil resources are increasingly scarce. All these lead to a the binary parameters were obtained through the maximum like- trend about producing mixed alcohols by using coal. The C1–C8 lihood. The quality of the experimental binary values was verified mixed alcohols were produced at the same time by a new coal by the Herington method [5]. chemical synthesis technology in a set of device. This production has already begun to accelerate the domestic industrial process [1]. 2. Experimental Mixed alcohols can continue to conduct multi-fractionations and result in a series of single alcohol include methanol, ethanol, 2.1. Chemicals propanol, etc. But the vapor–liquid equilibrium (VLE) data play an important role in the design and optimized operations of The physical properties of chemical reagents used are given distillation processes. So far many useful VLE data among the in Table 1. Methanol and 1-pentanol were supplied by Shanghai mixed alcohols have been presented. However, for 2-propanol + 1- Lingfeng Chemical Co. Ltd. 2-Propanol and 1-butanol were supplied pentanol system, there is only one report about VLE data in 313.15 K by Shanghai Shenbo Chemical Co. Ltd. Methanol and 2-propanol [2], and no report is in isobaric condition. To 1-butanol + 1-pentanol were used without further purification. 1-Butanol and 1-pentanol system, data in low pressure are available [3], but they may not were further purified by distillation in a column. All the reagents meet the requirement of design calculations. As for 2-propanol + 1- were dried on 0.4 nm molecular sieves and degassed by ultrasound butanol system, Wang et al. [4] determined temperature and before use. The purity of chemicals used was checked by the gas liquid phase mole fraction in 101.3 kPa without giving vapor- chromatography equipped with a thermal conductivity detector phase mole fraction. Therefore, it is necessary to measure the VLE and a stainless steel column. The refractive indices and normal boil- data for 2-propanol + 1-butanol, 2-propanol + 1-pentanol, and 1- ing points were measured by the WYA Abbe refractometer and the butanol + 1-pentanol at atmospheric pressure condition. improved Rose still, respectively. In this paper, isobaric VLE results for binary mixture of 2-propanol + 1-butanol, 2-propanol + 1-pentanol and 1-butanol + 2.2. Apparatus and procedures In this study, the VLE data were obtained with a glass recircula- ∗ tion apparatus called improved Rose still described by Zhang et al. Corresponding author. Tel.: +86 025 83587190. E-mail address: [email protected] (Z. Bao). [7]. A mercury thermometer was used to measure the equilibrium 0378-3812/$ – see front matter © 2013 Elsevier B.V. All rights reserved. http://dx.doi.org/10.1016/j.fluid.2012.12.020 J. Wang, Z. Bao / Fluid Phase Equilibria 341 (2013) 30–34 31 Table 1 Physical properties of experimental materials. Compound Purity (mass %) Water (mass %) nD (298.15 K) Tb/K (101.3 kPa) Experiment Literature [6] Experiment Literature [6] Methanol >99.5 <0.1% 1.3288 1.3286 337.69 337.66 2-Propanol >99.7 <0.1% 1.3776 1.3775 355.50 355.55 1-Butanol >99.6 0.1% 1.3995 1.3993 390.86 390.85 1-Pentanol >99.6 0.1% 1.4097 1.4099 411.10 411.15 Note: u(w) = ±0.001, u(nD) = ±0.0001, u(Tb) = ±0.01 K. Table 2 temperature with an accuracy of temperature of 0.1 K, and con- VLE data for 2-propanol (1) + 1-butanol (2), 2-propanol (1) + 1-pentanol (2), and 1- ducted exposed neck correction to obtain the true temperature. The butanol (1) + 1-pentanol (2) system at 101.3 kPa. experiment pressure was controlled by a constant pressure system T/K x y T/K x y (a vacuum pump, a U-tube, and a buffer tank), and the precision 1 1 1 1 ± was within 133 Pa. 2-Propanol (1) + 1-butanol (2) In the experiments, all the analytical work was carried out by 390.86 0 0 370.75 0.4002 0.7221 389.12 0.0227 0.0672 369.13 0.4471 0.7615 a gas chromatograph (GC6890, supplied by Shandong Lunan Rui- 387.53 0.0474 0.1362 367.77 0.4938 0.7954 hong instruments company), which was equipped with a flame 385.95 0.0744 0.2067 366.51 0.5341 0.8218 ionization detector (FID). The composition of vapor phase and liq- 384.15 0.1062 0.2825 364.99 0.5840 0.8526 uid phase was calculated by the area normalization method, which 382.96 0.1299 0.3357 363.60 0.6307 0.8768 381.80 0.1465 0.3750 362.17 0.6836 0.9015 can accurate to 0.001. The GC column was 30 m long and 0.32 mm 379.00 0.2023 0.4759 360.67 0.7333 0.9221 in diameter silica capillary column packed with OV-1701. The car- 376.05 0.2693 0.5731 359.27 0.7957 0.9448 rier gas was high purity nitrogen, and head pressure was 400 kPa. 374.00 0.3170 0.6373 357.16 0.9052 0.9775 The injector and detector temperature of column were 473.15 K 373.65 0.3255 0.6480 355.50 1 1 and 493.15 K, respectively. 2-propanol (1) + 1-pentanol (2) Methanol + 2-propanol system as a checking system was mea- 411.10 0 0 380.36 0.3302 0.7905 sured first. The VLE data at 101.3 kPa and comparisons to literature 408.68 0.0156 0.0741 379.45 0.3494 0.8072 406.51 0.0315 0.1499 377.00 0.3956 0.8405 are shown in Fig. 1. The results matched very well with previous 404.91 0.0495 0.2355 374.75 0.4364 0.8644 literature and this result gives us a confidence of our instruments 402.10 0.0682 0.2973 372.45 0.4821 0.8861 and analysis method. 400.42 0.0854 0.3565 371.03 0.5105 0.8990 398.32 0.1016 0.4056 367.88 0.5908 0.9275 395.97 0.1250 0.4684 366.57 0.628 0.9385 3. Results and discussion 392.48 0.1615 0.5509 363.69 0.7059 0.9573 390.25 0.1895 0.6088 361.67 0.7645 0.9685 3.1. VLE model and experiment data 388.14 0.2141 0.6498 359.47 0.8324 0.9798 385.00 0.2579 0.7155 357.45 0.9032 0.9895 383.55 0.2794 0.7398 355.50 1 1 The VLE results of binary system (2-propanol + 1-butanol, 2-propanol + 1-pentanol, and 1-butanol + 1-pentanol) and ternary 1-butanol (1) + 1-pentanol (2) 411.10 0 0 400.17 0.4836 0.6405 system (2-propanol + 1-butanol + 1-pentanol) are shown in 410.00 0.0440 0.0741 398.60 0.5369 0.6895 Tables 2 and 3. The activity coefficient of pure component was 409.70 0.0537 0.0900 397.88 0.5796 0.7297 calculated by: 408.00 0.1046 0.1725 396.57 0.6488 0.7920 407.50 0.1383 0.2245 395.93 0.6913 0.8250 p V L 406.04 0.1906 0.3065 395.13 0.7336 0.8604 v sat s i 404.96 0.2408 0.3763 393.83 0.8022 0.8997 = pyiϕi xiipi ϕi exp dp (1) RT 404.31 0.2936 0.4378 393.13 0.8579 0.9290 s p 403.20 0.3394 0.4950 392.02 0.9115 0.9599 i 401.74 0.3833 0.5366 390.86 1 1 400.90 0.4308 0.5875 356 Note: u(T) = ±0.01 K, u(x) = ±0.001, u(y) = ±0.001. 354 352 Table 3 VLE data for 2-propanol (1) + 1-butanol (2) + 1-pentanol (3) ternary system at 350 101.3 kPa. 348 T/K x1 x2 y1 y2 1 2 3 /K T 346 375.71 0.3031 0.6489 0.5264 0.3045 1.0056 1.0199 1.0343 378.07 0.2648 0.6172 0.4775 0.3047 1.0099 1.0259 1.0383 344 381.30 0.2184 0.5675 0.4341 0.3125 1.0102 1.0227 1.0354 342 383.30 0.1911 0.5321 0.4084 0.3174 1.0136 1.0240 1.0390 385.91 0.1595 0.4855 0.3722 0.3189 1.0183 1.0249 1.0408 340 388.36 0.1341 0.4399 0.3396 0.3179 1.0152 1.0243 1.0419 338 391.37 0.1068 0.3818 0.3002 0.3132 1.0072 1.0253 1.0374 395.79 0.0428 0.1755 0.3980 0.4846 1.0100 1.0259 1.0393 336 397.46 0.0373 0.1599 0.3404 0.4378 1.0047 1.0236 1.0398 0.0 0.2 0.4 0.6 0.8 1.0 399.49 0.0281 0.1285 0.2881 0.3973 1.0097 1.0250 1.0365 x , y 1 1 401.17 0.0216 0.1036 0.2429 0.3547 1.0086 1.0263 1.0367 403.04 0.0151 0.0759 0.1974 0.3060 1.0018 1.0244 1.0343 ± ± ± Fig.
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