2
0
2011
has
pen
1
journal
Original
Hasan, S. M. N.[S M Nazmul]
Peng, D.-Y.[Ding-Yu]
J. Chem. Eng. Data
2011
2020-09-29
Excess Molar Enthalpies of Dipropyl Ether + Dibutyl Ether + (1-Hexene or Tetrahydrofuran) at 298.15 K
Excess molar enthalpies, measured at the temperature 298.15 K and atmospheric pressure conditions by means of a flow microcalorimeter, are reported for the ternary mixtures {x1 dipropyl ether + x2 dibutyl ether + (1 - x1 - x2) (1-hexene or tetrahydrofuran)}. A smooth representation of the results is described and used to construct constant-enthalpy contours on a Roozeboom diagram. It is shown that good estimates of the excess molar enthalpies of the ternary systems can be obtained from the Liebermann-Fried model by using the physical properties of the pure components and the parameters determined from their binary mixtures.
10.1021/je100897y
4
56
946-950
1
InChI=1S/C6H14O/c1-3-5-7-6-4-2/h3-6H2,1-2H3
POLCUAVZOMRGSN-UHFFFAOYSA-N
dipropyl ether
1-propoxypropane
4-oxaheptane
propyl ether
C6H14O
1
Commercial source
1
De-gassed by evacuation
2
99
2
Gas chromatography
2
InChI=1S/C8H18O/c1-3-5-7-9-8-6-4-2/h3-8H2,1-2H3
DURPTKYDGMDSBL-UHFFFAOYSA-N
dibutyl ether
1,1'-oxybisbutane
1-butoxybutane
5-oxanonane
butyl ether
butyl oxide
di-n-butyl ether
dibutyl oxide
n-butyl ether
C8H18O
1
Commercial source
1
De-gassed by evacuation
2
99.9
3
Gas chromatography
3
InChI=1S/C6H12/c1-3-5-6-4-2/h3H,1,4-6H2,2H3
LIKMAJRDDDTEIG-UHFFFAOYSA-N
hex-1-ene
1-hexene
C6H12
1
Commercial source
1
De-gassed by evacuation
2
99
2
Gas chromatography
4
InChI=1S/C4H8O/c1-2-4-5-3-1/h1-4H2
WYURNTSHIVDZCO-UHFFFAOYSA-N
tetrahydrofuran
1,4-epoxybutane
THF
oxacyclopentane
oxolane
tetramethylene oxide
C4H8O
1
Commercial source
1
De-gassed by evacuation
2
99.9
3
Gas chromatography
1
1
1
Principal objective of the work
KNA
TRC
5/13/2011
1
Mass density, kg/m3
VIBTUB:UFactor:4
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
1
Temperature, K
Liquid
2
Pressure, kPa
Liquid
1
298.15
5
2
101.325
6
1
741.997
6
1
0.833
2
2
1
Principal objective of the work
KNA
TRC
5/13/2011
1
Mass density, kg/m3
VIBTUB:UFactor:2
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
1
Temperature, K
Liquid
2
Pressure, kPa
Liquid
1
298.15
5
2
101.325
6
1
763.806
6
1
0.327
3
3
1
Principal objective of the work
KNA
TRC
5/13/2011
1
Mass density, kg/m3
VIBTUB:UFactor:4
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
1
Temperature, K
Liquid
2
Pressure, kPa
Liquid
1
298.15
5
2
101.325
6
1
668.762
6
1
0.957
4
4
1
Principal objective of the work
KNA
TRC
5/13/2011
1
Mass density, kg/m3
VIBTUB:UFactor:2
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
1
Temperature, K
Liquid
2
Pressure, kPa
Liquid
1
298.15
5
2
101.325
6
1
882.078
6
1
0.209
5
1
1
2
1
Principal objective of the work
KNA
TRC
5/13/2011
1
Excess molar enthalpy (molar enthalpy of mixing), kJ/mol
Flow calorimetry
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
1
Pressure, kPa
Liquid
101
3
2
Temperature, K
Liquid
298.15
5
1
Mole fraction
1
Liquid
1
0.05
3
1
0.00223
3
1
0.00079
1
0.1
4
1
0.00427
3
1
0.00081
1
0.15
4
1
0.00586
3
1
0.00082
1
0.2001
4
1
0.00732
3
1
0.00083
1
0.25
4
1
0.00856
3
1
0.00084
1
0.3
4
1
0.00957
3
1
0.00085
1
0.35
4
1
0.01031
4
1
0.00086
1
0.3998
4
1
0.01094
4
1
0.00086
1
0.4497
4
1
0.01152
4
1
0.00087
1
0.4998
4
1
0.01185
4
1
0.00087
1
0.5004
4
1
0.01185
4
1
0.00087
1
0.55
4
1
0.01188
4
1
0.00087
1
0.6001
4
1
0.01176
4
1
0.00087
1
0.65
4
1
0.01132
4
1
0.00087
1
0.6999
4
1
0.01057
4
1
0.00086
1
0.75
4
1
0.00955
3
1
0.00085
1
0.8
4
1
0.00818
3
1
0.00084
1
0.8503
4
1
0.00666
3
1
0.00083
1
0.9
4
1
0.00463
3
1
0.00082
1
0.95
4
1
0.00256
3
1
0.0008
6
1
1
3
1
Principal objective of the work
KNA
TRC
5/13/2011
1
Excess molar enthalpy (molar enthalpy of mixing), kJ/mol
Flow calorimetry
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
1
Pressure, kPa
Liquid
101
3
2
Temperature, K
Liquid
298.15
5
1
Mole fraction
1
Liquid
1
0.0529
3
1
0.0066
3
1
0.00084
1
0.1001
4
1
0.01208
4
1
0.00088
1
0.15
4
1
0.01649
4
1
0.00091
1
0.2001
4
1
0.0201
4
1
0.00094
1
0.25
4
1
0.02282
4
1
0.00096
1
0.3002
4
1
0.02491
4
1
0.00097
1
0.3499
4
1
0.02645
4
1
0.00098
1
0.4001
4
1
0.02735
4
1
0.00099
1
0.4501
4
1
0.02809
4
1
0.001
1
0.5001
4
1
0.028
4
1
0.001
1
0.5001
4
1
0.028
4
1
0.001
1
0.55
4
1
0.02765
4
1
0.00099
1
0.5998
4
1
0.02683
4
1
0.00099
1
0.6499
4
1
0.02548
4
1
0.00098
1
0.6996
4
1
0.02385
4
1
0.00097
1
0.75
4
1
0.02154
4
1
0.00095
1
0.8003
4
1
0.01883
4
1
0.00093
1
0.85
4
1
0.01538
4
1
0.0009
1
0.9
4
1
0.01133
4
1
0.00087
1
0.95
4
1
0.0061
3
1
0.00083
7
4
1
1
1
Principal objective of the work
KNA
TRC
5/13/2011
1
Excess molar enthalpy (molar enthalpy of mixing), kJ/mol
Flow calorimetry
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
1
Pressure, kPa
Liquid
101
3
2
Temperature, K
Liquid
298.15
5
1
Mole fraction
1
Liquid
1
0.05
3
1
0.05228
4
1
0.00149
1
0.1
4
1
0.09688
4
1
0.00189
1
0.1501
4
1
0.1361
4
1
0.0023
1
0.2
4
1
0.1682
4
1
0.0026
1
0.2498
4
1
0.1959
4
1
0.0029
1
0.2998
4
1
0.2169
4
1
0.0031
1
0.3503
4
1
0.2328
4
1
0.0033
1
0.3998
4
1
0.2426
4
1
0.0034
1
0.45
4
1
0.2473
4
1
0.0035
1
0.4998
4
1
0.2483
4
1
0.0035
1
0.4998
4
1
0.2486
4
1
0.0035
1
0.5499
4
1
0.2446
4
1
0.0035
1
0.5999
4
1
0.2363
4
1
0.0034
1
0.6502
4
1
0.2237
4
1
0.0032
1
0.7003
4
1
0.2062
4
1
0.003
1
0.7499
4
1
0.1845
4
1
0.0028
1
0.7999
4
1
0.1594
4
1
0.0025
1
0.85
4
1
0.1277
4
1
0.0022
1
0.9
4
1
0.09047
4
1
0.00181
1
0.95
4
1
0.04808
4
1
0.00143
8
4
1
2
1
Principal objective of the work
KNA
TRC
5/13/2011
1
Excess molar enthalpy (molar enthalpy of mixing), kJ/mol
Flow calorimetry
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
1
Pressure, kPa
Liquid
101
3
2
Temperature, K
Liquid
298.15
5
1
Mole fraction
2
Liquid
1
0.05
3
1
0.07875
4
1
0.00198
1
0.0998
3
1
0.1436
4
1
0.0025
1
0.1502
4
1
0.1984
4
1
0.0031
1
0.2
4
1
0.2434
4
1
0.0035
1
0.2
4
1
0.2434
4
1
0.0035
1
0.25
4
1
0.2787
4
1
0.0039
1
0.3
4
1
0.3058
4
1
0.0042
1
0.3499
4
1
0.3249
4
1
0.0044
1
0.4
4
1
0.3368
4
1
0.0046
1
0.4502
4
1
0.3415
4
1
0.0046
1
0.4998
4
1
0.339
4
1
0.0046
1
0.4998
4
1
0.3393
4
1
0.0046
1
0.5498
4
1
0.3319
4
1
0.0045
1
0.6002
4
1
0.3182
4
1
0.0044
1
0.6499
4
1
0.2979
4
1
0.0041
1
0.7
4
1
0.2727
4
1
0.0038
1
0.7501
4
1
0.2404
4
1
0.0035
1
0.8
4
1
0.2041
4
1
0.0031
1
0.85
4
1
0.1622
4
1
0.0026
1
0.9
4
1
0.1121
4
1
0.0021
1
0.95
4
1
0.05948
4
1
0.00165
9
1
1
2
1
3
1
Principal objective of the work
KNA
TRC
5/13/2011
1
Excess molar enthalpy (molar enthalpy of mixing), kJ/mol
Flow calorimetry
Liquid
Direct value, X
2
3
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
1
Temperature, K
Liquid
298.15
5
2
Pressure, kPa
Liquid
101
3
1
Mole fraction
1
Liquid
2
Solvent: Amount ratio of component to other component of binary solvent
2
Liquid
1
0.05
3
2
0.3333
4
1
0.00517
3
1
0.00082
1
0.05
3
2
0.9996
4
1
0.00431
3
1
0.00081
1
0.05
3
2
3
5
1
0.00303
3
1
0.0008
1
0.1
4
2
0.3333
4
1
0.00958
3
1
0.00086
1
0.1
4
2
0.9996
4
1
0.00818
3
1
0.00084
1
0.1
4
2
3
5
1
0.00583
3
1
0.00082
1
0.1499
4
2
0.9996
4
1
0.01167
4
1
0.00087
1
0.15
4
2
0.3333
4
1
0.01358
4
1
0.00089
1
0.15
4
2
3
5
1
0.00845
3
1
0.00084
1
0.1998
4
2
0.3333
4
1
0.017
4
1
0.00091
1
0.1999
4
2
3
5
1
0.01066
4
1
0.00086
1
0.2001
4
2
0.9996
4
1
0.01473
4
1
0.00089
1
0.2499
4
2
0.9996
4
1
0.01733
4
1
0.00091
1
0.2501
4
2
0.3333
4
1
0.02003
4
1
0.00093
1
0.2501
4
2
3
5
1
0.01275
4
1
0.00088
1
0.2999
4
2
0.9996
4
1
0.0195
4
1
0.00093
1
0.3001
4
2
0.3333
4
1
0.02234
4
1
0.00095
1
0.3001
4
2
3
5
1
0.01443
4
1
0.00089
1
0.3499
4
2
3
5
1
0.01585
4
1
0.0009
1
0.3501
4
2
0.3333
4
1
0.02431
4
1
0.00097
1
0.3502
4
2
0.9996
4
1
0.02117
4
1
0.00094
1
0.4
4
2
3
5
1
0.01689
4
1
0.00091
1
0.4001
4
2
0.3333
4
1
0.02556
4
1
0.00098
1
0.4001
4
2
0.9996
4
1
0.02265
4
1
0.00095
1
0.4496
4
2
0.3333
4
1
0.02642
4
1
0.00098
1
0.4501
4
2
3
5
1
0.01762
4
1
0.00091
1
0.4502
4
2
0.9996
4
1
0.0234
4
1
0.00096
1
0.4996
4
2
3
5
1
0.01812
4
1
0.00092
1
0.4997
4
2
3
5
1
0.01816
4
1
0.00092
1
0.5
4
2
0.9996
4
1
0.02387
4
1
0.00096
1
0.5
4
2
0.9996
4
1
0.02392
4
1
0.00096
1
0.5002
4
2
0.3333
4
1
0.02674
4
1
0.00098
1
0.5002
4
2
0.3333
4
1
0.02676
4
1
0.00098
1
0.5497
4
2
3
5
1
0.01828
4
1
0.00092
1
0.55
4
2
0.9996
4
1
0.02394
4
1
0.00096
1
0.5503
4
2
0.3333
4
1
0.02663
4
1
0.00098
1
0.5999
4
2
0.3333
4
1
0.02601
4
1
0.00098
1
0.6001
4
2
3
5
1
0.01808
4
1
0.00092
1
0.6003
4
2
0.9996
4
1
0.02352
4
1
0.00096
1
0.6497
4
2
3
5
1
0.01751
4
1
0.00091
1
0.65
4
2
0.9996
4
1
0.02251
4
1
0.00095
1
0.6501
4
2
0.3333
4
1
0.02491
4
1
0.00097
1
0.6997
4
2
3
5
1
0.01676
4
1
0.00091
1
0.7001
4
2
0.9996
4
1
0.02129
4
1
0.00094
1
0.7003
4
2
0.3333
4
1
0.02337
4
1
0.00096
1
0.7497
4
2
3
5
1
0.01543
4
1
0.0009
1
0.7499
4
2
0.9996
4
1
0.01961
4
1
0.00093
1
0.75
4
2
0.3333
4
1
0.02138
4
1
0.00094
1
0.7998
4
2
0.3333
4
1
0.01898
4
1
0.00093
1
0.7998
4
2
3
5
1
0.01394
4
1
0.00089
1
0.8001
4
2
0.9996
4
1
0.01729
4
1
0.00091
1
0.8497
4
2
3
5
1
0.01206
4
1
0.00087
1
0.85
4
2
0.3333
4
1
0.01579
4
1
0.0009
1
0.85
4
2
0.9996
4
1
0.01471
4
1
0.00089
1
0.9
4
2
0.3333
4
1
0.01219
4
1
0.00088
1
0.9
4
2
0.9996
4
1
0.01165
4
1
0.00087
1
0.9
4
2
3
5
1
0.00972
3
1
0.00085
1
0.95
4
2
0.3333
4
1
0.00712
3
1
0.00084
1
0.95
4
2
0.9996
4
1
0.00781
3
1
0.00084
1
0.95
4
2
3
5
1
0.00639
3
1
0.00083
10
4
1
1
1
2
1
Principal objective of the work
KNA
TRC
5/13/2011
1
Excess molar enthalpy (molar enthalpy of mixing), kJ/mol
Flow calorimetry
Liquid
Direct value, X
4
2
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
1
Temperature, K
Liquid
298.15
5
2
Pressure, kPa
Liquid
101
3
1
Mole fraction
1
Liquid
2
Solvent: Amount ratio of component to other component of binary solvent
2
Liquid
1
0.05
3
2
0.3333
4
1
0.02123
4
1
0.001
1
0.05
3
2
1.0004
5
1
0.00653
3
1
0.00083
1
0.05
3
2
3
5
1
0.00193
3
1
0.00079
1
0.1
4
2
0.3333
4
1
0.03877
4
1
0.00113
1
0.1
4
2
1.0004
5
1
0.01261
4
1
0.00088
1
0.1
4
2
3
5
1
0.00352
3
1
0.0008
1
0.15
4
2
0.3333
4
1
0.05528
4
1
0.00127
1
0.15
4
2
1.0004
5
1
0.01785
4
1
0.00092
1
0.1555
4
2
3
5
1
0.00501
3
1
0.00081
1
0.2
4
2
1.0004
5
1
0.02278
4
1
0.00096
1
0.2
4
2
3
5
1
0.00595
3
1
0.00082
1
0.2002
4
2
0.3333
4
1
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