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 3665
Components
| No. |
Formula |
Molar Mass |
CAS Registry Number |
Name |
| 1 |
C6H14 |
86.177 |
110-54-3 |
Hexane |
| 2 |
C6H6 |
78.114 |
71-43-2 |
Benzene |
| 3 |
C4H10O |
74.123 |
71-36-3 |
1-Butanol |
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] |
| 367.05 |
0.02330 |
0.19200 |
0.12340 |
0.51340 |
| 365.25 |
0.03000 |
0.20400 |
0.15900 |
0.51500 |
| 360.75 |
0.03750 |
0.30500 |
0.14320 |
0.58700 |
| 358.65 |
0.04340 |
0.36650 |
0.14850 |
0.64200 |
| 357.05 |
0.06000 |
0.34650 |
0.21500 |
0.59680 |
| 354.95 |
0.07000 |
0.39000 |
0.23700 |
0.60330 |
| 353.35 |
0.08330 |
0.37680 |
0.28500 |
0.56200 |
| 353.85 |
0.08680 |
0.40000 |
0.26680 |
0.57000 |
| 352.55 |
0.09430 |
0.41330 |
0.27200 |
0.58000 |
| 351.45 |
0.12000 |
0.41200 |
0.33000 |
0.53330 |
| 350.85 |
0.14330 |
0.39670 |
0.36550 |
0.51200 |
| 350.15 |
0.14670 |
0.41340 |
0.36680 |
0.51670 |
| 349.65 |
0.17200 |
0.38680 |
0.41330 |
0.47000 |
| 349.45 |
0.19000 |
0.34670 |
0.44800 |
0.44000 |
| 352.65 |
0.19000 |
0.19000 |
0.54680 |
0.28670 |
| 351.05 |
0.19340 |
0.19340 |
0.55900 |
0.29340 |
| 348.35 |
0.22680 |
0.35330 |
0.48000 |
0.41700 |
| 349.80 |
0.22800 |
0.20330 |
0.58000 |
0.28000 |
| 347.55 |
0.25000 |
0.34500 |
0.52000 |
0.39330 |
| 347.65 |
0.27000 |
0.26680 |
0.56680 |
0.31000 |
| 346.95 |
0.28000 |
0.32500 |
0.53320 |
0.38320 |
| 346.85 |
0.28340 |
0.27500 |
0.57340 |
0.33000 |
| 348.45 |
0.29000 |
0.15900 |
0.66300 |
0.21850 |
| 346.45 |
0.30680 |
0.26330 |
0.59670 |
0.31000 |
| 346.00 |
0.34000 |
0.25000 |
0.62000 |
0.28000 |
| 345.75 |
0.34000 |
0.36000 |
0.58500 |
0.33330 |
| 345.65 |
0.35200 |
0.24000 |
0.63500 |
0.26670 |
| 345.95 |
0.38670 |
0.15320 |
0.72000 |
0.19680 |
| 345.15 |
0.40280 |
0.22500 |
0.66670 |
0.24680 |
| 344.65 |
0.41000 |
0.29340 |
0.63000 |
0.29500 |
| 344.75 |
0.42200 |
0.21200 |
0.68680 |
0.22670 |
| 345.15 |
0.42330 |
0.18000 |
0.70800 |
0.20500 |
| 344.35 |
0.45500 |
0.20680 |
0.69350 |
0.22000 |
| 344.25 |
0.46670 |
0.20000 |
0.71650 |
0.19400 |
| 343.55 |
0.52000 |
0.24000 |
0.70320 |
0.24330 |
| 343.75 |
0.52330 |
0.19000 |
0.74340 |
0.18330 |
| 343.55 |
0.53330 |
0.15320 |
0.75820 |
0.15820 |
| 343.55 |
0.53670 |
0.16000 |
0.75680 |
0.16500 |
| 343.45 |
0.55750 |
0.16150 |
0.76100 |
0.15670 |
| 343.35 |
0.56900 |
0.15000 |
0.77330 |
0.14680 |
| 342.95 |
0.61500 |
0.14320 |
0.78820 |
0.13500 |
| 342.50 |
0.62000 |
0.20330 |
0.75000 |
0.19300 |
| 342.75 |
0.64000 |
0.12850 |
0.81000 |
0.12340 |
| 342.60 |
0.67000 |
0.11680 |
0.82000 |
0.10700 |
| 342.55 |
0.69330 |
0.09000 |
0.84350 |
0.08150 |
| 341.95 |
0.71670 |
0.14500 |
0.80300 |
0.14320 |
| 342.25 |
0.71900 |
0.11200 |
0.83100 |
0.09100 |
| 342.00 |
0.75670 |
0.10680 |
0.84120 |
0.09000 |
| 341.85 |
0.77330 |
0.08330 |
0.85000 |
0.08330 |
| 341.85 |
0.79330 |
0.08000 |
0.85340 |
0.07340 |
| 341.75 |
0.80500 |
0.12180 |
0.84340 |
0.10330 |
| 341.85 |
0.81000 |
0.07150 |
0.85670 |
0.07000 |
| 341.75 |
0.81000 |
0.11670 |
0.84340 |
0.10000 |
| 341.55 |
0.82000 |
0.10680 |
0.85670 |
0.10000 |
| 341.75 |
0.83200 |
0.06900 |
0.87600 |
0.06340 |
(T - temperature, x - liquid mole fraction, y - vapor mole fraction)
Reference
| Source |
| Govindaswamy S.; Andiappan A.; Lakshmanan S.: Vapor-Liquid Equilibrium Data at Atmospheric Pressure for the Ternary and the Subbinary Systems Containing n-Hexane-Benzene-1-Butanol. J.Chem.Eng.Data 21 (1976) 366-369 |
List of All References
Vapor-Liquid Equilibrium Data Overview
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