Mixture of Benzene + 1-Butanol

Datasets

1. Excess molar enthalpy (molar enthalpy (4)
2. P_vap - Vapor or sublimation pressure, kPa (3)
3. ρ_l - Mass density, kg/m3
4. Vapor Liquid Equilibrium at Constant Pressure
5. Vapor Liquid Equilibrium at Constant Temperature (2)

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

Operational conditions:

• Pressure, kPa = 101 (Liquid)
• Temperature, K = 313.15 (Liquid)

Mole fraction of Benzene (1) - Liquid	Excess molar enthalpy (molar enthalpy of mixing), kJ/mol - Liquid
0.0494	0.1481
0.1007	0.3037
0.1497	0.4510
0.2007	0.5981
0.2495	0.7328
0.3002	0.8622
0.3507	0.9803
0.4010	1.0859
0.4493	1.1714
0.4993	1.2431
0.5492	1.2965
0.6010	1.328
0.6506	1.337
0.7001	1.3216
0.7495	1.2794
0.8007	1.1995
0.8498	1.0836
0.9007	0.9011
0.9495	0.6055

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

Operational conditions:

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

Mole fraction of Benzene (1) - Liquid	Excess molar enthalpy (molar enthalpy of mixing), kJ/mol - Liquid
0.0504	0.1180
0.0997	0.2370
0.1497	0.3562
0.1997	0.4745
0.2505	0.5898
0.3001	0.6967
0.3506	0.7974
0.3999	0.8865
0.4502	0.9634
0.5002	1.0283
0.5501	1.076
0.5998	1.107
0.6505	1.1182
0.7000	1.1066
0.7503	1.0725
0.7996	1.0124
0.8497	0.9190
0.8996	0.7758
0.9504	0.5377

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

Operational conditions:

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

Mole fraction of Benzene (1) - Liquid	Excess molar enthalpy (molar enthalpy of mixing), kJ/mol - Liquid
0.1430	0.3439
0.2530	0.6116
0.3370	0.8004
0.3800	0.8932
0.4250	1.0033
0.4910	1.1132
0.5500	1.1962
0.6020	1.2436
0.6550	1.2576
0.7230	1.16
0.7610	1.0303
0.8210	0.8231

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

Fixed			Measured
Mole fraction of Benzene (1) - Liquid	Pressure, kPa - Liquid	Temperature, K - Liquid	Excess molar enthalpy (molar enthalpy of mixing), kJ/mol - Liquid
0.5000	101.00	303.15	1.1319

Vapor or sublimation pressure, kPa [ref]

Operational condition: Temperature, K = 313.15 (Liquid)

Mole fraction of Benzene (1) - Liquid	Vapor or sublimation pressure, kPa - Liquid
0.0000	2.49
0.0590	6.42
0.1080	9.18
0.1510	11.27
0.1980	13.23
0.2559	15.24
0.3023	16.58
0.3533	17.82
0.4027	18.84
0.4028	18.83
0.4501	19.66
0.4519	19.67
0.4997	20.38
0.5019	20.40
0.5497	21.00
0.5506	21.00
0.5999	21.55
0.6001	21.54
0.6497	22.03
0.7001	22.45
0.7502	22.83
0.8010	23.18
0.8591	23.52
0.9108	23.83
0.9547	24.14
1.0000	24.37

Vapor or sublimation pressure, kPa [ref]

Operational condition: Temperature, K = 313.15 (Liquid)

Mole fraction of 1-Butanol (2) - Liquid	Vapor or sublimation pressure, kPa - Liquid
0.3006	22.45
0.6922	16.79

Vapor or sublimation pressure, kPa [ref]

Operational condition: Temperature, K = 308.15 (Liquid)

Mole fraction of 1-Butanol (2) - Liquid	Vapor or sublimation pressure, kPa - Liquid
0.0802	20.17
0.1690	20.28
0.2561	20.11
0.3150	19.84
0.3896	19.35
0.4603	18.61
0.5294	17.43
0.6035	16.49
0.6755	15.09
0.7565	13.29
0.8052	12.25
0.8465	10.72
0.9238	7.41
0.9789	4.03

Mass density, kg/m3 [ref]

Operational condition: Pressure, kPa = 101 (Liquid)

Fixed		Measured
Temperature, K - Liquid	Mole fraction of 1-Butanol (2) - Liquid	Mass density, kg/m3 - Liquid
288.15	0.0000	884.246
288.15	0.0193	882.483
288.15	0.0534	879.595
288.15	0.1013	875.72
288.15	0.1509	871.829
288.15	0.2016	867.984
288.15	0.2018	867.955
288.15	0.2500	864.382
288.15	0.2997	860.741
288.15	0.3532	856.936
288.15	0.4019	853.504
288.15	0.4525	850.0
288.15	0.4998	846.738
288.15	0.5532	843.129
288.15	0.6004	839.985
288.15	0.6493	836.693
288.15	0.7010	833.239
288.15	0.7502	829.979
288.15	0.7945	827.051
288.15	0.8511	823.296
288.15	0.8961	820.299
288.15	0.9510	816.663
288.15	1.0000	813.373
293.15	0.0000	878.918
293.15	0.0193	877.168
293.15	0.0534	874.309
293.15	0.1013	870.495
293.15	0.1509	866.677
293.15	0.2016	862.908
293.15	0.2018	862.874
293.15	0.2500	859.372
293.15	0.2997	855.806
293.15	0.3532	852.081
293.15	0.4019	848.721
293.15	0.4525	845.3
293.15	0.4998	842.111
293.15	0.5532	838.594
293.15	0.6004	835.529
293.15	0.6493	832.317
293.15	0.7010	828.949
293.15	0.7502	825.772
293.15	0.7945	822.92
293.15	0.8511	819.258
293.15	0.8961	816.336
293.15	0.9510	812.791
293.15	1.0000	809.573
298.15	0.0000	873.582
298.15	0.0193	871.844
298.15	0.0534	869.007
298.15	0.1013	865.255
298.15	0.1509	861.506
298.15	0.2016	857.807
298.15	0.2018	857.776
298.15	0.2500	854.344
298.15	0.2997	850.849
298.15	0.3532	847.201
298.15	0.4019	843.914
298.15	0.4525	840.574
298.15	0.4998	837.46
298.15	0.5532	834.03
298.15	0.6004	831.042
298.15	0.6493	827.91
298.15	0.7010	824.631
298.15	0.7502	821.537
298.15	0.7945	818.759
298.15	0.8511	815.196
298.15	0.8961	812.348
298.15	0.9510	808.897
298.15	1.0000	805.762
303.15	0.0000	868.233
303.15	0.0193	866.507
303.15	0.0534	863.694
303.15	0.1013	859.995
303.15	0.1509	856.309
303.15	0.2016	852.685
303.15	0.2018	852.651
303.15	0.2500	849.285
303.15	0.2997	845.866
303.15	0.3532	842.294
303.15	0.4019	839.08
303.15	0.4525	835.817
303.15	0.4998	832.778
303.15	0.5532	829.436
303.15	0.6004	826.525
303.15	0.6493	823.473
303.15	0.7010	820.282
303.15	0.7502	817.269
303.15	0.7945	814.569
303.15	0.8511	811.102
303.15	0.8961	808.331
303.15	0.9510	804.977
303.15	1.0000	801.923
308.15	0.0000	862.871
308.15	0.0193	861.158
308.15	0.0534	858.36
308.15	0.1013	854.713
308.15	0.1509	851.089
308.15	0.2016	847.536
308.15	0.2018	847.499
308.15	0.2500	844.201
308.15	0.2997	840.854
308.15	0.3532	837.357
308.15	0.4019	834.214
308.15	0.4525	831.029
308.15	0.4998	828.059
308.15	0.5532	824.804
308.15	0.6004	821.974
308.15	0.6493	819.001
308.15	0.7010	815.895
308.15	0.7502	812.965
308.15	0.7945	810.343
308.15	0.8511	806.975
308.15	0.8961	804.274
308.15	0.9510	801.025
308.15	1.0000	798.053
313.15	0.0000	857.498
313.15	0.0193	855.809
313.15	0.0534	853.019
313.15	0.1013	849.433
313.15	0.1509	845.861
313.15	0.2016	842.375
313.15	0.2018	842.342
313.15	0.2500	839.11
313.15	0.2997	835.83
313.15	0.3532	832.4
313.15	0.4019	829.324
313.15	0.4525	826.217
313.15	0.4998	823.32
313.15	0.5532	820.157
313.15	0.6004	817.402
313.15	0.6493	814.449
313.15	0.7010	811.483
313.15	0.7502	808.64
313.15	0.7945	806.094
313.15	0.8511	802.822
313.15	0.8961	800.189
313.15	0.9510	797.051
313.15	1.0000	794.147

Vapor Liquid Equilibrium at Constant Pressure [ref]

Operational condition: Pressure, kPa = 101.33 (VLE)

Fixed	Measured
T [K] - VLE	x1[mol/mol] of Benzene (1) - Liquid	y1[mol/mol] of Benzene (1) - Vapour
390.85	0.0000	0.0000
390.05	0.0040	0.0250
385.15	0.0400	0.2170
380.25	0.0850	0.3800
375.37	0.1340	0.5100
373.37	0.1610	0.5600
371.85	0.1800	0.5900
368.75	0.2340	0.6600
365.4	0.3080	0.7240
362.84	0.3690	0.7790
361.43	0.3970	0.7870
359.54	0.4750	0.8190
357.69	0.5600	0.8470
356.34	0.6310	0.8670
355.13	0.7140	0.8850
354.51	0.7900	0.9040
354.02	0.8480	0.9200
353.82	0.8970	0.9470
353.54	0.9280	0.9520
353.43	0.9420	0.9600
353.36	0.9480	0.9630
353.31	0.9540	0.9660
353.24	1.0000	1.0000

Vapor Liquid Equilibrium at Constant Temperature [ref]

Operational condition: Temperature, K = 298.15 (VLE)

Fixed	Measured
P [kPa] - VLE	x1[mol/mol] of Benzene (1) - Liquid	y1[mol/mol] of Benzene (1) - Vapour
0.8533	0.0000	0.0000
6.879	0.2020	0.8870
8.986	0.3500	0.9190
10.386	0.5000	0.9300
11.439	0.6870	0.9410
11.906	0.8030	0.9550
12.586	1.0000	1.0000

Vapor Liquid Equilibrium at Constant Temperature [ref]

Operational condition: Temperature, K = 318.15 (VLE)

Fixed	Measured
P [kPa] - VLE	x1[mol/mol] of Benzene (1) - Liquid	y1[mol/mol] of Benzene (1) - Vapour
15.204	0.1794	0.8107
19.844	0.2928	0.8689
22.837	0.3997	0.8946
25.014	0.5085	0.9115
26.309	0.5996	0.9221
27.422	0.6993	0.9316
28.371	0.8014	0.9421
29.184	0.9026	0.9568
29.503	0.9462	0.9677

Sources

• Dortmund Data Bank Vapor-Liquid Equilibrium Data
• Temperature Dependence of Densities and Excess Molar Volumes of the Ternary Mixture (1-Butanol + Chloroform + Benzene) and its Binary Constituents (1-Butanol + Chloroform and 1-Butanol + Benzene)
• Excess enthalpies of ether + alcohol + hydrocarbon mixtures: Binary and ternary mixtures containing dibutyl ether (DBE), 1-butanol and benzene at 298.15K and 313.15K
• Experimental and predicted excess molar enthalpies of binary mixtures containing 2,2'-oxybis[propane], benzene, butan-1-ol, 2-methylpropan-1-ol, 2-methyl-2-ene-1-propanol at 303.15 K
• (Vapour + liquid) equilibria of (1-butanol + benzene, or toluene, or o-, or m-, or p-xylene) at T = 308.15 K
• Phase equilibrium properties of binary and ternary systems containing di-isopropyl ether + 1-butanol + benzene at 313.15 K

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