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 3829

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 C3H8O 60.096 67-63-0 2-Propanol
Search the DDB for all data of this mixture

Constant Value

Pressure 101.33 kPa

Data Table

T [K] x1 [mol/mol] x2 [mol/mol] y1 [mol/mol] y2 [mol/mol]
344.65 0.01200 0.37850 0.02850 0.47500
346.40 0.01340 0.20670 0.06340 0.36670
344.20 0.01650 0.37340 0.05200 0.46340
346.20 0.02340 0.19330 0.09000 0.33340
344.45 0.02340 0.38850 0.04000 0.46850
345.85 0.03000 0.19500 0.09700 0.32340
344.00 0.03000 0.37160 0.08000 0.45500
345.05 0.03160 0.18670 0.14000 0.32000
345.15 0.03160 0.19000 0.14000 0.33340
345.40 0.03340 0.19330 0.12670 0.33000
345.05 0.03670 0.19500 0.14000 0.32000
345.15 0.03670 0.19660 0.13000 0.32500
343.55 0.03670 0.36170 0.10840 0.44500
344.40 0.04670 0.20000 0.16340 0.32670
343.25 0.05340 0.35500 0.13340 0.43200
344.00 0.05670 0.21600 0.17000 0.32340
343.85 0.06000 0.22000 0.16670 0.31850
343.70 0.06170 0.22170 0.17000 0.32000
343.35 0.06340 0.22340 0.19110 0.32670
343.80 0.06380 0.21000 0.21000 0.28900
343.35 0.07000 0.21670 0.20340 0.31670
342.75 0.07000 0.34000 0.16670 0.40680
343.00 0.07200 0.23000 0.20000 0.32670
342.70 0.07500 0.24000 0.20500 0.32750
343.00 0.08000 0.15670 0.26000 0.24670
342.45 0.08300 0.24500 0.21340 0.33000
342.60 0.08670 0.13660 0.29000 0.21340
341.85 0.09000 0.32340 0.20340 0.37850
342.50 0.09670 0.11500 0.31340 0.19000
342.00 0.09670 0.24170 0.24500 0.32000
341.55 0.10180 0.30680 0.23650 0.36500
340.90 0.12000 0.28160 0.27670 0.33000
339.95 0.15160 0.26340 0.32340 0.29000
339.25 0.18500 0.23000 0.36680 0.25170
339.30 0.18500 0.24680 0.36000 0.26200
338.85 0.21200 0.25600 0.38500 0.26340
338.60 0.22800 0.27150 0.38680 0.27000
338.30 0.25680 0.29340 0.39680 0.26670
338.15 0.27000 0.31840 0.40160 0.28000
337.80 0.30000 0.31170 0.41070 0.27000
337.65 0.32200 0.30340 0.44170 0.26670
338.00 0.34000 0.29000 0.44670 0.24850
337.00 0.37670 0.37000 0.48500 0.23000
336.75 0.41500 0.24850 0.50850 0.21340
336.45 0.46000 0.23670 0.53000 0.19150
336.15 0.51100 0.20330 0.56170 0.17000
336.00 0.55670 0.17340 0.59000 0.11160
335.80 0.61670 0.14680 0.61670 0.12000
335.65 0.65000 0.11670 0.65330 0.10000
335.65 0.69000 0.09680 0.67680 0.08670
335.50 0.73340 0.07850 0.68680 0.06000
335.60 0.74000 0.07340 0.69680 0.07000
335.65 0.77500 0.07000 0.71160 0.05850
335.45 0.77850 0.06000 0.71000 0.05340
335.85 0.80850 0.04160 0.73000 0.05330
336.35 0.88250 0.03000 0.79000 0.02670

(T - temperature, x - liquid mole fraction, y - vapor mole fraction)

Reference

Source
Govindaswamy S.; Andiappan A.; Lakshmanan S.: Isobaric Vapour-Liquid Equilibrium Data for the Ternary and Sub-Binary Systems Containing n-Hexane(1)-Benzene(2)- Isopropanol(3). J.Chem.Eng.Japan 9 (1976) 345-349

List of All References

Source

Vapor-Liquid Equilibrium Data Overview


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