Mixture of Toluene + Diisopropyl ether

Datasets

1. Mole fraction
2. Excess molar enthalpy (molar enthalpy
3. P_vap - Vapor or sublimation pressure, kPa
4. ρ_l - Mass density, kg/m3

Mole fraction of Diisopropyl ether (2) [ref]

Operational condition: Temperature, K = 333.15 (Gas)

Mole fraction of Diisopropyl ether (2) - Liquid	Mole fraction of Diisopropyl ether (2) - Gas
0.0192	0.1066
0.0399	0.1958
0.0597	0.2703
0.0793	0.3269
0.1194	0.4249
0.1692	0.5232
0.2291	0.6117
0.2888	0.6749
0.3486	0.7221
0.4084	0.7644
0.4681	0.7993
0.5287	0.8284
0.5888	0.8549
0.6484	0.8764
0.7085	0.8960
0.7688	0.9176
0.8293	0.9314
0.8789	0.9529
0.9198	0.9691
0.9393	0.9775
0.9603	0.9850
0.9795	0.9926

Excess molar enthalpy (molar enthalpy of mixing), kJ/mol [ref]

Operational conditions:

• Temperature, K = 303.15 (Liquid)
• Pressure, kPa = 101 (Liquid)

Mole fraction of Diisopropyl ether (2) - Liquid	Excess molar enthalpy (molar enthalpy of mixing), kJ/mol - Liquid
0.0570	0.0273
0.1030	0.0422
0.1400	0.0519
0.2280	0.0593
0.3140	0.0548
0.3970	0.0419
0.4550	0.0323
0.6730	0.0032
0.7520	-0.0091
0.8890	-0.0081

Vapor or sublimation pressure, kPa [ref]

Fixed		Measured
Temperature, K - Liquid	Mole fraction of Diisopropyl ether (2) - Liquid	Vapor or sublimation pressure, kPa - Liquid
263.15	0.0843	0.76
263.15	0.1517	1.22
263.15	0.2846	1.49
263.15	0.4047	1.88
263.15	0.6416	2.07
263.15	0.7718	2.69
263.15	0.8702	2.89
273.15	0.0843	1.42
273.15	0.1517	2.14
273.15	0.2846	2.70
273.15	0.4047	3.37
273.15	0.6416	3.87
273.15	0.7718	4.81
273.15	0.8702	5.18
283.15	0.0843	2.52
283.15	0.1517	3.60
283.15	0.2846	4.65
283.15	0.4047	5.73
283.15	0.6416	6.80
283.15	0.7718	8.17
283.15	0.8702	8.80
293.15	0.0843	4.27
293.15	0.1517	5.86
293.15	0.2846	7.66
293.15	0.4047	9.35
293.15	0.6416	11.33
293.15	0.7718	13.27
293.15	0.8702	14.29
303.15	0.0843	6.95
303.15	0.1517	9.22
303.15	0.2846	12.14
303.15	0.4047	14.68
303.15	0.6416	18.03
303.15	0.7718	20.72
303.15	0.8702	22.31
313.15	0.0843	10.90
313.15	0.1517	14.11
313.15	0.2846	18.57
313.15	0.4047	22.30
313.15	0.6416	27.56
313.15	0.7718	31.25
313.15	0.8702	33.64
323.15	0.0843	16.58
323.15	0.1517	21.02
323.15	0.2846	27.55
323.15	0.4047	32.85
323.15	0.6416	40.69
323.15	0.7718	45.72
323.15	0.8702	49.18
333.15	0.0843	24.50
333.15	0.1517	30.57
333.15	0.2846	39.75
333.15	0.4047	47.12
333.15	0.6416	58.24
333.15	0.7718	65.09
333.15	0.8702	69.95
343.15	0.0843	35.28
343.15	0.1517	43.52
343.15	0.2846	55.93
343.15	0.4047	65.98
343.15	0.6416	81.10
343.15	0.7718	90.41
343.15	0.8702	97.07

Mass density, kg/m3 [ref]

Operational conditions:

• Temperature, K = 298.15 (Liquid)
• Pressure, kPa = 101 (Liquid)

Mole fraction of Diisopropyl ether (2) - Liquid	Mass density, kg/m3 - Liquid
0.0500	853.94
0.0995	845.89
0.2004	829.97
0.2999	814.46
0.4001	799.53
0.5003	784.92
0.6001	770.99
0.7004	757.31
0.8003	744.27
0.9003	731.28
0.9498	725.19

Sources

• Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
• Isothermal vapor liquid equilibrium at 333.15K and excess molar volumes at 298.15K for the ternary system di-isopropyl ether + n-propyl alcohol + toluene and its binary subsystems

Note: These property values are available through the Cheméo API. A free account gives you an access key.