Dortmund Data Bank
Vapor-Liquid Equilibrium Data
The experimental data shown in these pages are freely available and have been published already in the DDB Explorer Edition. The data represent a small sub list of all available data in the Dortmund Data Bank. For more data or any further information please search the DDB or contact DDBST.
Vapor-Liquid Equilibrium Data Set 36204
Components
| No. |
Formula |
Molar Mass |
CAS Registry Number |
Name |
| 1 |
H2O |
18.015 |
7732-18-5 |
Water |
| 2 |
C4H10O |
74.123 |
71-36-3 |
1-Butanol |
| 3 |
C8H10 |
106.167 |
106-42-3 |
p-Xylene |
Search the DDB for all data of this mixture
Constant Value
Data Table
| T [K] |
x1 [mol/mol] |
x2 [mol/mol] |
y1 [mol/mol] |
y2 [mol/mol] |
| 368.02 |
0.31200 |
0.67600 |
0.73700 |
0.24500 |
| 369.39 |
0.26400 |
0.72400 |
0.70400 |
0.27900 |
| 369.92 |
0.25300 |
0.73500 |
0.70800 |
0.27600 |
| 371.26 |
0.23100 |
0.76100 |
0.68400 |
0.30300 |
| 373.42 |
0.18400 |
0.80900 |
0.66700 |
0.32200 |
| 375.18 |
0.15200 |
0.84300 |
0.61200 |
0.37900 |
| 377.07 |
0.12600 |
0.86900 |
0.56000 |
0.43300 |
| 379.28 |
0.10000 |
0.89500 |
0.54400 |
0.45000 |
| 379.73 |
0.10900 |
0.88700 |
0.47600 |
0.51800 |
| 378.00 |
0.10900 |
0.87400 |
0.52400 |
0.45300 |
| 375.83 |
0.13400 |
0.83400 |
0.59700 |
0.36600 |
| 372.21 |
0.17800 |
0.77700 |
0.65200 |
0.30100 |
| 370.44 |
0.20400 |
0.73800 |
0.65900 |
0.28500 |
| 368.14 |
0.25300 |
0.67500 |
0.69300 |
0.23700 |
| 366.56 |
0.28600 |
0.62900 |
0.70700 |
0.21300 |
| 365.23 |
0.31600 |
0.58700 |
0.70300 |
0.20400 |
| 365.05 |
0.41800 |
0.54100 |
0.72600 |
0.21700 |
| 365.13 |
0.44300 |
0.52700 |
0.73300 |
0.22000 |
| 365.43 |
0.42000 |
0.55200 |
0.73400 |
0.22300 |
| 365.86 |
0.39600 |
0.57800 |
0.73500 |
0.22900 |
| 366.09 |
0.38100 |
0.59300 |
0.73600 |
0.22700 |
| 366.40 |
0.35700 |
0.62000 |
0.73700 |
0.22900 |
| 365.75 |
0.24200 |
0.60400 |
0.69500 |
0.19200 |
| 364.71 |
0.27400 |
0.55700 |
0.68700 |
0.18800 |
| 367.16 |
0.23000 |
0.62700 |
0.68500 |
0.21400 |
| 369.18 |
0.19500 |
0.68100 |
0.64900 |
0.25600 |
| 371.49 |
0.17200 |
0.72400 |
0.62700 |
0.28700 |
| 373.95 |
0.13800 |
0.77700 |
0.60400 |
0.32100 |
| 376.87 |
0.10600 |
0.82600 |
0.52000 |
0.41300 |
| 378.99 |
0.09200 |
0.85700 |
0.43500 |
0.51100 |
| 380.55 |
0.08300 |
0.89300 |
0.39900 |
0.57000 |
| 384.65 |
0.04800 |
0.94400 |
0.26700 |
0.72000 |
| 384.04 |
0.04800 |
0.92100 |
0.28300 |
0.67700 |
| 383.20 |
0.04700 |
0.89100 |
0.29500 |
0.63600 |
| 382.13 |
0.05700 |
0.84800 |
0.29900 |
0.60500 |
| 381.41 |
0.05300 |
0.80600 |
0.31800 |
0.55500 |
| 381.95 |
0.04300 |
0.78300 |
0.30100 |
0.55300 |
| 382.20 |
0.03900 |
0.75200 |
0.27600 |
0.55700 |
| 382.91 |
0.03700 |
0.71500 |
0.26100 |
0.55500 |
| 382.49 |
0.03300 |
0.67400 |
0.25500 |
0.54400 |
| 379.96 |
0.04300 |
0.62300 |
0.35900 |
0.44500 |
| 378.12 |
0.05400 |
0.57300 |
0.43600 |
0.37300 |
| 376.45 |
0.05600 |
0.52600 |
0.46800 |
0.33900 |
| 375.26 |
0.05900 |
0.48700 |
0.49600 |
0.31200 |
| 374.66 |
0.05500 |
0.44600 |
0.54800 |
0.27200 |
| 373.80 |
0.06000 |
0.40600 |
0.57400 |
0.24800 |
| 372.87 |
0.06300 |
0.36200 |
0.58500 |
0.23500 |
| 371.08 |
0.05800 |
0.33100 |
0.61800 |
0.20500 |
| 368.21 |
0.14000 |
0.52000 |
0.65500 |
0.20200 |
| 369.19 |
0.13300 |
0.54900 |
0.64100 |
0.21700 |
| 371.55 |
0.10700 |
0.60100 |
0.59700 |
0.26000 |
| 373.58 |
0.09700 |
0.66600 |
0.54500 |
0.31400 |
| 376.41 |
0.08200 |
0.71600 |
0.46500 |
0.39500 |
| 377.94 |
0.08100 |
0.75000 |
0.44800 |
0.42300 |
(T - temperature, x - liquid mole fraction, y - vapor mole fraction)
Reference
| Source |
| Gomis V.; Font A.; Saquete M.D.; Garcia-Cano J.: Isothermal (liquid + liquid) equilibrium data at T = 313.15 K and isobaric (vapor + liquid + liquid) equilibrium data at 101.3 kPa for the ternary system (water + 1-butanol + p-xylene). J.Chem.Thermodyn. 79 (2014) 242-247 |
List of All References
Vapor-Liquid Equilibrium Data Overview
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