2
0
2009
tre
0
journal
Original
Trejbal, J.[Jiri]
Int. J. Thermophys.
2009
2020-09-29
Vapor Liquid Equilibrium for Binary Mixtures of 1,4-Diazabicyclo[2.2.2]octane with Ethylenediamine, Ethanolamine, and Ethylene Glycol
Vapor-liquid equilibria ofmixtures of 1,4-diazabicyclo[2.2.2]octane with ethylenediamine, ethanolamine, and ethylene glycol were studied. Ideal behavior in the ethylenediamine and 1,4-diazabicyclo[2.2.2]octane mixture was observed. Ethanolamine and 1,4-diazabicyclo[2.2.2]octane form an azeotrope with a minimum boiling point whereas ethylene glycol and 1,4-diazabicyclo[2.2.2]octane form an azeotrope with a maximum boiling point. Non-ideal behavior of the mixtures was described by the NRTL equation, and the corresponding constants were calculated.
Amine
Azeotrope
NRTL
vapor liquid equilibrium
10.1007/s10765-009-0570-x
2
30
490-498
1
InChI=1S/C6H12N2/c1-2-8-5-3-7(1)4-6-8/h1-6H2
IMNIMPAHZVJRPE-UHFFFAOYSA-N
1,4-diazabicyclo[2.2.2]octane
triethylenediamine
C6H12N2
1
Commercial source
1
Crystallization from solution
2
99
2
Estimated by the compiler
2
InChI=1S/C2H8N2/c3-1-2-4/h1-4H2
PIICEJLVQHRZGT-UHFFFAOYSA-N
ethane-1,2-diamine
1,2-diaminoethane
1,2-ethanediamine
dimethylenediamine
ethylenediamine
C2H8N2
1
Commercial source
3
InChI=1S/C2H7NO/c3-1-2-4/h4H,1-3H2
HZAXFHJVJLSVMW-UHFFFAOYSA-N
2-aminoethan-1-ol
2-aminoethanol
MEA
ethanolamine
monoethanolamine
C2H7NO
1
Commercial source
4
InChI=1S/C2H6O2/c3-1-2-4/h3-4H,1-2H2
LYCAIKOWRPUZTN-UHFFFAOYSA-N
1,2-ethanediol
1,2-dihydroxyethane
ethane-1,2-diol
ethylene glycol
C2H6O2
1
Commercial source
1
Fractional distillation
2
99
2
Estimated by the compiler
1
2
1
1
1
Principal objective of the work
KNA
TRC
4/6/2009
1
Boiling temperature at pressure P, K
EBULLIO:UFactor:8
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
Gas
1
Pressure, kPa
Liquid
99.6
3
1
Mole fraction
2
Gas
1
0.505
3
1
425.65
4
1
0.9
1
0.614
3
1
415.75
4
1
0.9
1
0.677
3
1
412.25
4
1
0.9
1
0.706
3
1
409.05
4
1
0.9
1
0.759
3
1
407.35
4
1
0.9
1
0.8
1
1
405.45
4
1
0.9
1
0.825
3
1
403.25
4
1
0.9
1
0.843
3
1
400.65
4
1
0.9
1
0.846
3
1
401.65
4
1
0.9
1
0.876
3
1
399.85
4
1
0.9
1
0.902
3
1
398.75
4
1
0.9
1
0.914
3
1
398.25
4
1
0.9
1
0.927
3
1
397.65
4
1
0.9
1
0.934
3
1
397.15
4
1
0.9
1
0.94
2
1
396.65
4
1
0.9
1
0.958
3
1
396.05
4
1
0.9
1
0.967
3
1
395.55
4
1
0.9
1
0.974
3
1
395.25
4
1
0.9
1
0.982
3
1
394.85
4
1
0.9
1
0.987
3
1
394.45
4
1
0.9
1
0.991
3
1
394.15
4
1
0.9
2
2
1
1
1
Principal objective of the work
KNA
TRC
4/6/2009
1
Mole fraction
Chromatography
2
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
Gas
1
Pressure, kPa
Liquid
99.6
3
1
Mole fraction
2
Gas
1
0.505
3
1
0.122
3
1
0.04
1
0.614
3
1
0.215
3
1
0.04
1
0.677
3
1
0.278
3
1
0.04
1
0.706
3
1
0.332
3
1
0.04
1
0.759
3
1
0.357
3
1
0.04
1
0.8
1
1
0.447
3
1
0.04
1
0.825
3
1
0.49
2
1
0.04
1
0.843
3
1
0.568
3
1
0.041
1
0.846
3
1
0.511
3
1
0.041
1
0.876
3
1
0.595
3
1
0.041
1
0.902
3
1
0.646
3
1
0.04
1
0.914
3
1
0.676
3
1
0.04
1
0.927
3
1
0.693
3
1
0.04
1
0.934
3
1
0.735
3
1
0.04
1
0.94
2
1
0.76
2
1
0.04
1
0.958
3
1
0.797
3
1
0.04
1
0.967
3
1
0.821
3
1
0.04
1
0.974
3
1
0.848
3
1
0.04
1
0.982
3
1
0.868
3
1
0.04
1
0.987
3
1
0.884
3
1
0.04
1
0.991
3
1
0.902
3
1
0.04
3
3
1
1
1
Principal objective of the work
KNA
TRC
4/6/2009
1
Boiling temperature at pressure P, K
EBULLIO:UFactor:8
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
Gas
1
Pressure, kPa
Liquid
98.9
3
1
Mole fraction
3
Gas
1
0.207
3
1
442.65
4
1
0.9
1
0.288
3
1
440.75
4
1
0.9
1
0.338
3
1
439.65
4
1
0.9
1
0.369
3
1
439.05
4
1
0.9
1
0.472
3
1
438.95
4
1
0.9
1
0.55
2
1
439.05
4
1
0.9
1
0.616
3
1
439.65
4
1
0.9
1
0.669
3
1
439.75
4
1
0.9
1
0.719
3
1
440.35
4
1
0.9
1
0.764
3
1
440.65
4
1
0.9
1
0.791
3
1
440.85
4
1
0.9
4
3
1
1
1
Principal objective of the work
KNA
TRC
4/6/2009
1
Mole fraction
Chromatography
3
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
Gas
1
Pressure, kPa
Liquid
98.9
3
1
Mole fraction
3
Gas
1
0.207
3
1
0.134
3
1
0.04
1
0.288
3
1
0.213
3
1
0.04
1
0.338
3
1
0.286
3
1
0.04
1
0.369
3
1
0.352
3
1
0.04
1
0.472
3
1
0.482
3
1
0.04
1
0.55
2
1
0.569
3
1
0.041
1
0.616
3
1
0.655
3
1
0.04
1
0.669
3
1
0.703
3
1
0.04
1
0.719
3
1
0.751
3
1
0.04
1
0.764
3
1
0.796
3
1
0.04
1
0.791
3
1
0.817
3
1
0.04
5
4
1
1
1
Principal objective of the work
KNA
TRC
4/6/2009
1
Boiling temperature at pressure P, K
EBULLIO:UFactor:8
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
Gas
1
Pressure, kPa
Liquid
98.9
3
1
Mole fraction
4
Gas
1
0.042
2
1
451.75
4
1
0.9
1
0.07
1
1
453.15
2
1
1
1
0.127
3
1
456.25
4
1
0.9
1
0.154
3
1
459.75
4
1
0.9
1
0.178
3
1
457.25
4
1
0.9
1
0.25
2
1
463.25
4
1
0.9
1
0.349
3
1
465.25
4
1
0.9
1
0.434
3
1
466.75
4
1
0.9
1
0.531
3
1
468.25
4
1
0.9
1
0.611
3
1
469.25
4
1
0.9
1
0.624
3
1
469.75
4
1
0.9
1
0.64
2
1
469.75
4
1
0.9
1
0.71
2
1
470.25
4
1
0.9
1
0.748
3
1
470.25
4
1
0.9
1
0.787
3
1
469.25
4
1
0.9
1
0.799
3
1
470.25
4
1
0.9
1
0.82
2
1
470.25
4
1
0.9
1
0.847
3
1
470.25
4
1
0.9
1
0.871
3
1
470.25
4
1
0.9
1
0.9
1
1
470.75
4
1
0.9
1
0.912
3
1
470.75
4
1
0.9
1
0.938
3
1
470.25
4
1
0.9
1
0.953
3
1
469.75
4
1
0.9
1
0.961
3
1
469.75
4
1
0.9
6
4
1
1
1
Principal objective of the work
KNA
TRC
4/6/2009
1
Mole fraction
Chromatography
4
Liquid
Direct value, X
1
Data file compiler
Propagation of evaluated standard uncertainties
95
Liquid
Gas
1
Pressure, kPa
Liquid
98.9
3
1
Mole fraction
4
Gas
1
0.042
2
1
0.142
3
1
0.04
1
0.07
1
1
0.191
3
1
0.04
1
0.127
3
1
0.289
3
1
0.04
1
0.154
3
1
0.349
3
1
0.04
1
0.178
3
1
0.338
3
1
0.04
1
0.25
2
1
0.431
3
1
0.04
1
0.349
3
1
0.509
3
1
0.04
1
0.434
3
1
0.577
3
1
0.04
1
0.531
3
1
0.62
2
1
0.04
1
0.611
3
1
0.69
2
1
0.04
1
0.624
3
1
0.699
3
1
0.04
1
0.64
2
1
0.719
3
1
0.04
1
0.71
2
1
0.759
3
1
0.04
1
0.748
3
1
0.78
2
1
0.04
1
0.787
3
1
0.805
3
1
0.04
1
0.799
3
1
0.815
3
1
0.04
1
0.82
2
1
0.832
3
1
0.04
1
0.847
3
1
0.854
3
1
0.04
1
0.871
3
1
0.87
2
1
0.04
1
0.9
1
1
0.898
3
1
0.04
1
0.912
3
1
0.912
3
1
0.04
1
0.938
3
1
0.929
3
1
0.04
1
0.953
3
1
0.945
3
1
0.04
1
0.961
3
1
0.953
3
1
0.04