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IUPAC-NIST Solubility Database
NIST Standard Reference Database 106
Solubility System:
2-Propanol with Toluene and Water
Components:
(1) Water; H2O; [7732-18-5]
NIST Chemistry WebBook
for detail
(2) 2-Propanol (isopropanol, isopropyl alcohol); C3H8O; [67-63-0]
NIST Chemistry WebBook
for detail
(3) Toluene (methylbenzene); C7H8; [108-88-3]
NIST Chemistry WebBook
for detail
Evaluator:
A. Skrzecz, Institute of Physical Chemistry, Polish Academy of Sciences, Warsaw, Poland (1997.03)
Critical Evaluation:
A survey of reported compositions along the saturation curve (sat), and compositions of coexisting phases in equilibrium (eq.) for the system 2-propanol-toluene-water is given in Table 62.
Saturation curve
The ternary system 2-propanol-toluene-water forms a miscibility gap of type 1. The system was measured at 293 K, 298 K, and at boiling temperatures at 101.3
k
Pa. Only toluene-water binary system forms a miscibility gap. The data of this binary system were compiled and critically evaluated in a previously published SDS volume.
6
The recommended values of mutual solubility of toluene-water system at 298 K are
x
'
2
=0.9972 and
x
"
2
=0.000 104.
6
This critical evaluation is based on the original papers with the exception of data of Liekola,
1
which were taken from the handbook of Kafarov,
7
this data set was also taken into account during evaluation but is not reported as a compilation sheet because it does not contribute further to knowledge of the system. At 293 K the experimental data of Borisova
et al
.
4
present a slightly larger miscibility gap than those of Stankova
et al
.
3
which are very close to the results at 298 K. The data for the saturation curve are consistent within each data set, as well as with one another. The miscibility gap decreases with increasing temperature. A maximum value of 2-propanol concentration on saturation curve observed at 298 K is equal to
x
1
=0.39±0.01 (differences between data sets, Refs. 2.5 are about 0.02 mole fraction). The saturation curve was described by the equation proposed by Hlavaty
8
and used also with success by Letcher
et al
.
9
for the description of saturation curves of ternary systems containing alcohols
x
1
=
a
1
·
z
1
·ln(
z
1
)+
a
2
·
z
2
ln(
z
2
)+
a
3
·
z
1
·
z
2
,
where
z
1
=(
x
2
+0.5·
x
1
–
x
"
20
)/(
x
'
20
–
x
"
20
),
z
2
=(
x
'
20
–
x
2
–0.5·
x
1
)/(
x
'
20
–
x
"
20
),
x
1
,
x
2
–mole fractions of component (1) and (2), respectively,
x
'
20
,
x
"
20
–values of
x
2
on the saturation curve which cuts the
x
1
=0 axis.
All experimental compositions on the saturation curve at 298.2 K (compositions of tie lines were included), Refs. 2 and 5, as well as the “best” mutual solubility values of the binary system, Ref. 6, were used in the calculations. The parameters calculated by the least-squares method are:
a
1
=–0.319 92,
a
2
=–0.005 56,
a
3
=1.107 75. The standard error of estimate was 0.0071. The compositions of the saturation curve calculated by the proposed equation at 298.2 K are presented in Table 63 and in
Fig. 32
.
Phases in equilibrium
The phases in equilibrium were measured also at 293 K, 298 K, and at boiling temperatures at 101.3
k
Pa. The tie lines cover the whole area of miscibility gap. They are consistent within each data set, as well as with one another. However, the tie lines reported at 298.2 K,
2,5
cross slightly as could be noticed if a large scale graph were plotted. The tie lines are treated as tentative.
The plait point of the system changes with temperature. At 293.2 K it was reported to be
x
1
=0.292,
x
2
=0.069, (Ref. 4) at 298.2 K–
x
1
=0.27,
x
2
=0.07 (Ref. 5) while at 101
k
Pa at boiling temperature (348.9±0.1 K) it was estimated by the evaluator to be
x
1
=0.370±0.004,
x
2
=0.209±0.001.
Experimental Data:
(Notes on the Nomenclature)
TABLE 62. Summary of experimental data for the system 2-propanol-toluene-water
Author
T/K
DataType
Reference
Leikola, 1940
293
sat. (4)
1
Washburn and Beguin, 1940
298
sat. (24), eq. (13)
2
Stankova
et al
., 1970
293, 349-352
sat. (52)
3
Borisova
et al
., 1978
293, 349-354
eq. (17)
4
Letcher and Siswana, 1992
298
sat. (14), eq. (6)
5
TABLE 63. Calculated compositions along the saturation curve at 298.2 K
T/K
Mole Fraction x
1
Mole Fraction x
2
298.2
0.0000
0.000 104 Ref. 6
298.2
0.1982
0.0200
298.2
0.2479
0.0400
298.2
0.2828
0.0600
298.2
0.3093
0.0800
298.2
0.3300
0.1000
298.2
0.3464
0.1200
298.2
0.3594
0.1400
298.2
0.3696
0.1600
298.2
0.3774
0.1800
298.2
0.3833
0.2000
298.2
0.3874
0.2200
298.2
0.3900
0.2400
298.2
0.3912
0.2600
298.2
0.3912
0.2800
298.2
0.3901
0.3000
298.2
0.3879
0.3200
298.2
0.3848
0.3400
298.2
0.3809
0.3600
298.2
0.3761
0.3800
298.2
0.3706
0.4000
298.2
0.3645
0.4200
298.2
0.3576
0.4400
298.2
0.3502
0.4600
298.2
0.3421
0.4800
298.2
0.3336
0.5000
298.2
0.3245
0.5200
298.2
0.3149
0.5400
298.2
0.3049
0.5600
298.2
0.2944
0.5800
298.2
0.2835
0.6000
298.2
0.2722
0.6200
298.2
0.2605
0.6400
298.2
0.2484
0.6600
298.2
0.2360
0.6800
298.2
0.2232
0.7000
298.2
0.2101
0.7200
298.2
0.1967
0.7400
298.2
0.1830
0.7600
298.2
0.1689
0.7800
298.2
0.1546
0.8000
298.2
0.1401
0.8200
298.2
0.1252
0.8400
298.2
0.1101
0.8600
298.2
0.0948
0.8800
298.2
0.0792
0.9000
298.2
0.0633
0.9200
298.2
0.0473
0.9400
298.2
0.0310
0.9600
298.2
0.0144
0.9800
298.2
0.0000
0.9972 Ref. 6
View Figure 1 for this Evaluation
Notes:
Table 62
Number of experimental points in parentheses.
References: (Click a link to see its experimental data associated with the reference)
1 Leikola, E., Suomen Kemistil B. 13, 13 (1940).
2
Washburn, E.R., Brockway, C.E.; Graham, C.L.; Deming, P., J. Am. Chem. Soc. 64, 1886 (1942).
3
Stankova, L.; Vesely, F., J. Pick, Collect. Czech. Chem. Commun. 35, 1 (1970).
4
Borisova, I.A.; Vatskova, V.G.; Gorbunov, A.I.; Sokolov, N.M., Khim. Prom-st (Moscow) 347 (1978).
5
Letcher, T.M.; Siswana, P.M., Fluid Phase Equilib. 74, 203 (1992).
6 Shaw, D.G., ed., Solubility Data Series, Vol. 37, Hydrocarbons with Water and Seawater, Part I: Hydrocarbons C5 to C7 (Pergamon, New York, 1989).
7 Kafarov, V.V., ed., Spravochnik po Rastvorimosti Vol. 2, Troinye, Mnogokomponentnye Sistemy, Kniga II (Izd. Akademii Nauk SSSR, Moskva, 1963).
8 Hlavaty, K., Collect. Czech. Chem. Commun. 37, 4005 (1972).
9 Letcher, T.M.; Ravindran, S.; Radloff, S.E., Fluid Phase Equilib, 69, 251 (1991).