The complete thermodynamic model implemented in FreeStanMix is documented in the following references:
Colonna, P., June 1995. Properties of Fluid Mixtures for Thermodynamic Cycles Applications.Tech. rep., Stanford University, Stanford, CA.
Angelino, G. and Colonna, P., 1998. ''Multicomponent Working fluids for Organic Rankine Cycles (ORCs).'' Energy , 23, pp. 449-463.
The PRSV cubic equation of state, which is a modified Peng Robinson equation of state particularly suited for the accurate estimation of saturation properties, is described in
Stryjeck, R. and Vera, J. H., 1986. ``PRSV: An Improved Peng-Robinson Equation Of State For Pure Compounds And Mixtures.'' Can. J. Chem. Eng. , 64, pp. 323-333.
The Wong and Sandler mixing rules which are suitable for the modeling of highly non-ideal mixtures are documented e.g. in:
Wong, D. S. H., Sandler, S. I., and Orbey, H., 1992. ``Equation Of State Mixing Rule For Nonideal Mixtures Using Available Activity Coefficient Model Parameters And That Allows Extrapolation Over Large Ranges Of Temperature And Pressure.'' Ind. Eng. Chem. Res. , 31, pp. 2033-2039.
Wong, D. S. H. and Sandler, S. I., 1992. ``A Theoretically Correct Mixing Rule for Cubic Equations of State.'' AIChE Journal , 38, pp. 671-680.
Huang, H. and Sandler, S. I., 1993. ``Prediction of Vapor-Liquid Equilibria at High Pressures Using Activity Coefficient Parameters Obtained from Low Pressure Data: A comparison of Two Equation of State Mixing Rules.'' Ind. Eng. Chem. Res. , 32, pp. 1498-1503.
Orbey, H. and Sandler, S. I., 1993. ``Accurate Equation of State Predictions at high temperatures and pressures using the existing UNIFAC model.'' Fluid Phase Equilib. , 85, pp. 41-54.
Sandler, S. I. et al. , 1994. Models For Thermodynamic And Phase Equilibria Calculations . Marcel Dekker, New York.
Orbey, H. and Sandler, S. I., 1995. ``On the Combination of Equation of State and Excess Free Energy Models.'' Fluid Phase Equilib. , 111, pp. 53-70.
Orbey, H. and Sandler, S. I., 1995. ``Reformulation of Wong-Sandler Mixing Rules for Cubic Equations of State.'' AIChE J. , 41.
Orbey, H. and Sandler, S. I., 1995. ``Equation of State modeling of Refrigerant Mixtures.'' Ind. Eng. Chem. Res. , 34, pp. 2520-2525.
Orbey, H. and Sandler, S. I., 1997. ``A Comparison of Huron-Vidal Type Mixing Rules of Mixtures of Compounds with Large Size Differences, and a New Mixing Rule.'' Fluid Phase Equilib. , 132, pp. 1-14.
Shiflett, M. B. and Sandler, S. I., June 1998. ``Modeling Fluorocarbon Vapor Liquid Equilibria using the Wong-Sandler model.'' Fluid Phase Equilib. , 147, pp. 145-162.
IMPORTANT NOTE: FreeStanMix implements a simple Successive Substitution Model for the solution of saturation calculations that is known to fail for close-to-critical states and performs worse for highly non-ideal mixtures. The critical point calculation for a mixture is implemented as the pseudo-critical point calculation if the user specifies the composition, therefore the result is highly inaccurate, but an estimate is necessary for all other type of calculations. For predefined mixtures the critical point is calculated with a "climbing" method, that is the bubble point calculation is repeated by increasing the temperature in ever-small steps until it does not converge anymore. This is also an inaccurate estimate even if much better than the pseudo-critical point calculation. Refer to StanMix for improved versions of these algorithms.
The critical point calculation for a mixture is implemented as the pseudo-critical point calculation if the composition is specified by the user, therefore the result is highly inaccurate, but an estimate is necessary for all other type of calculations. For predefined mixtures the critical point is calculated with a "climbing" method, that is the bubble point calculation is repeated by increasing the temperature in ever small steps until it does not converge anymore. This is also an inaccurate estimate even if much better than the pseudo-critical point calculation. We plan to improve these calculations.
FreeStanMix provides thermodynamic properties for the pure fluids listed in Table 1 and 2. The listed FluidProp names (either short or long) must be used to specify the fluid name the SetFluid method. For a given fluid, the FluidProp name is the same in all thermodynamic libraries in which the fluid is available.
Table 1
FluidProp Name (short) | FluidProp Name (long) | Tc [°C] | Pc [bar] | MW [g/mol] | Tmin[°C] | Tmax[°C] |
1-C4H10O |
1-butanol |
74.1200 |
289.83 |
44.13 |
-50.00 |
1226.85 |
1-C8018O |
1-octanol |
130.2279 |
411.65 |
28.60 |
0.00 |
400.00 |
1-C3H8O |
1-propanol |
60.0960 |
263.56 |
51.70 |
59.85 |
350.00 |
2-C4H10O |
2-butanol |
74.1200 |
289.90 |
44.23 |
-73.15 |
1226.85 |
2-C3H8O |
2-propanol |
60.0960 |
235.25 |
47.64 |
-75.00 |
350.00 |
C3H6O |
acetone |
58.0800 |
234.95 |
46.96 |
-94.95 |
1500.00 |
NH3 |
ammonia |
17.0305 |
132.45 |
112.98 |
-78.15 |
350.00 |
Ar |
argon |
39.9480 |
-122.29 |
48.98 |
-190.00 |
1226.85 |
C6H6 |
benzene |
78.1140 |
289.01 |
48.98 |
5.85 |
350.00 |
C12H10 |
biphenyl |
154.2100 |
496.00 |
31.21 |
19.85 |
350.00 |
C4H10 |
butane |
58.1240 |
152.01 |
37.97 |
-91.15 |
400.00 |
C10H14 |
butylbenzene |
134.2182 |
387.35 |
28.90 |
-87.85 |
1226.85 |
CO2 |
carbon dioxide |
44.0100 |
31.06 |
73.82 |
-57.15 |
400.00 |
C6H12 |
cyclohexane |
84.1620 |
280.49 |
40.75 |
6.85 |
400.00 |
D3 |
D3 |
222.4640 |
281.05 |
16.63 |
64.00 |
400.00 |
D4 |
D4 |
296.6180 |
313.35 |
13.32 |
17.65 |
400.00 |
D5 |
D5 |
370.7697 |
346.00 |
11.60 |
-4.65 |
400.00 |
D6 |
D6 |
444.9270 |
372.65 |
9.61 |
-1.15 |
400.00 |
CH3OCH3 |
dimethylether |
46.0680 |
126.95 |
52.40 |
-141.50 |
700.00 |
C12H10O |
diphenyl ether |
170.2072 |
503.65 |
30.80 |
15.00 |
600.00 |
C12H26 |
dodecane |
170.3348 |
295.61 |
24.86 |
-9.55 |
700.00 |
diethylbenzene |
Dowtherm J |
170.3348 |
295.61 |
24.86 |
-9.55 |
700.00 |
C2H6 |
ethane |
30.0700 |
29.28 |
48.80 |
-153.15 |
350.00 |
C2H5OH |
ethanol |
46.0690 |
240.77 |
61.48 |
-114.15 |
700.00 |
C8H10 |
ethylbenzene |
106.1680 |
344.05 |
36.06 |
32.85 |
329.85 |
C2H6O2 |
ethylene glycol |
62.0678 |
446.85 |
82.00 |
-13.00 |
1000.00 |
C5H4O2 |
furfural |
96.1000 |
396.85 |
58.90 |
-50.00 |
160.00 |
C7H16 |
heptane |
100.2019 |
267.05 |
27.40 |
-73.15 |
1226.85 |
C6F6 |
hexafluoro benzene |
186.0000 |
243.52 |
33.38 |
0.00 |
400.00 |
C6H14 |
hexane |
86.1780 |
234.15 |
30.12 |
-41.15 |
400.00 |
H2 |
hydrogen |
2.0160 |
-229.55 |
20.47 |
-259.15 |
350.00 |
i-C4H10 |
isobutane |
58.1240 |
135.05 |
36.50 |
-108.15 |
135.05 |
i-C5H12 |
isopentane |
72.1510 |
187.25 |
33.90 |
-53.15 |
187.25 |
MD2M |
MD2M |
310.6900 |
326.25 |
11.79 |
-10.15 |
400.00 |
MD3M |
MD3M |
384.8430 |
355.25 |
9.96 |
2.85 |
400.00 |
MD4M |
MD4M |
458.9933 |
380.05 |
8.77 |
13.85 |
400.00 |
MD5M |
MD5M |
533.1500 |
398.65 |
7.63 |
21.85 |
400.00 |
MD6M |
MD6M |
607.3100 |
415.75 |
6.77 |
29.85 |
400.00 |
MDM |
MDM |
236.5315 |
290.94 |
14.15 |
-25.15 |
400.00 |
CH4 |
methane |
16.0425 |
-82.59 |
45.99 |
-182.46 |
351.85 |
CH4O |
methanol |
32.0420 |
239.43 |
80.96 |
-85.00 |
700.00 |
MM |
MM |
162.3790 |
245.60 |
19.39 |
-45.15 |
400.00 |
C10H8 |
naphthalene |
128.1740 |
475.20 |
40.51 |
86.85 |
249.85 |
N2 |
nitrogen |
28.0130 |
-146.95 |
34.00 |
-209.15 |
350.00 |
C8H18 |
octane |
114.2200 |
295.61 |
24.86 |
0.00 |
400.00 |
O2 |
oxygen |
31.9990 |
-118.38 |
50.90 |
-217.15 |
350.00 |
C5H12 |
pentane |
72.1510 |
196.55 |
33.68 |
-77.15 |
400.00 |
C6F12 |
PFCH |
79.1645 |
217.20 |
32.32 |
-41.15 |
400.00 |
C7F14 |
PP2 |
350.0000 |
211.85 |
20.60 |
0.00 |
600.00 |
C10F18 |
PP5 |
462.0000 |
291.85 |
17.88 |
0.00 |
400.00 |
C3H8 |
propane |
44.0970 |
96.67 |
42.50 |
-187.62 |
400.00 |
C8H10 |
p-xylene |
106.1680 |
344.05 |
36.06 |
32.85 |
329.85 |
R113 |
R113 |
187.3800 |
214.15 |
34.10 |
-34.95 |
400.00 |
R114 |
R114 |
170.9400 |
145.75 |
32.70 |
-94.00 |
400.00 |
R116 |
R116 |
138.0120 |
19.85 |
30.18 |
-100.75 |
400.00 |
R12 |
R12 |
120.9140 |
111.85 |
40.70 |
-140.00 |
273.15 |
R125 |
R125 |
120.0200 |
66.25 |
36.31 |
-40.15 |
400.00 |
R134a |
R134a |
102.0300 |
101.06 |
40.56 |
-63.15 |
400.00 |
R14 |
R14 |
88.0050 |
-45.55 |
37.40 |
-183.15 |
400.00 |
R142b |
R142b |
100.4960 |
136.45 |
43.30 |
-130.15 |
136.45 |
R22 |
R22 |
86.4800 |
96.05 |
49.80 |
-73.15 |
400.00 |
R23 |
R23 |
70.0130 |
25.91 |
48.41 |
-163.15 |
400.00 |
R245fa |
R245fa |
134.0488 |
154.05 |
36.40 |
-73.15 |
226.85 |
R32 |
R32 |
52.0240 |
78.41 |
58.30 |
-124.15 |
78.41 |
silox 1 |
silox 1 |
199.4554 |
266.49 |
17.37 |
-10.15 |
400.00 |
silox 2 |
silox 2 |
192.0394 |
245.60 |
19.39 |
-25.15 |
400.00 |
silox 3 |
silox 3 |
206.8723 |
280.54 |
17.09 |
-10.15 |
400.00 |
C7H8 |
toluene |
92.1410 |
318.65 |
41.06 |
12.85 |
399.85 |
C9H12 |
trimethylbenzene |
120.1900 |
364.10 |
31.27 |
56.85 |
359.85 |
C4H6O2 |
vinyl acetate |
86.0900 |
246.05 |
41.40 |
-73.15 |
1226.85 |
H2O |
water |
18.0150 |
374.14 |
220.90 |
0.00 |
750.00 |
xx |
xxxxxx |
16.0425 |
-82.59 |
45.99 |
-182.46 |
351.85 |
More fluids can easily be added. The necessary data are the critical temperature, the critical pressure, the saturation curve and the specific heat in the ideal gas state.
Moreover the mixtures listed in Table 2 are available as predefined mixtures. The listed FluidProp names (either short or long) must be used to specify the fluid name the SetFluid method. Other mixtures can be added if pure and binary interaction data are available.
A large collection of binary interaction parameters data is available, for example, on:
Various authors. DECHEMA Chemistry Data Series, Frankfurt am Main (1977 and thereafter).
DETHERM: Thermophysical properties of pure substances & mixtures
Infotherm: Experimental thermodynamic and physical properties of mixtures and pure substances
DIPPR: Evaluated Process Design Data of the AIChE Design Institute of Physical Properties
Please contact us if you need to add a fluid or a mixture.
Table 2
FluidProp Name (short) | FluidProp Name (long) | Tc [°C] | Pc [bar] | MW [g/mol] | Tmin[°C] | Tmax[°C] |
1-C3H8O/C6H14 |
1-propanol/hexane |
60.0960 |
263.56 |
51.70 |
59.85 |
350.00 |
C3H6O/CH4O |
acetone/methanol |
58.0800 |
234.95 |
46.96 |
-94.95 |
1500.00 |
C3H6O/H2O |
acetone/water |
38.0475 |
275.30 |
97.40 |
0.00 |
750.00 |
air |
air |
28.8501 |
-142.14 |
35.89 |
-209.15 |
350.00 |
NH3/H2O |
ammonia/water |
17.5235 |
278.09 |
156.67 |
0.00 |
350.00 |
Ar/CH4 |
argon/methane |
39.9480 |
-122.29 |
48.98 |
-190.00 |
1226.85 |
C6H6/C6H12 |
benzene/cyclohexane |
81.1380 |
284.72 |
45.89 |
6.85 |
350.00 |
C6H6/C6H12/C6H14 |
benzene/cyclohexane/hexane |
83.1540 |
254.73 |
36.91 |
6.85 |
350.00 |
C6H6/C8H10 |
benzene/ethylbenzene |
92.1410 |
321.63 |
43.77 |
32.85 |
329.85 |
C6H6/C6H14 |
benzene/hexane |
82.1460 |
260.72 |
40.03 |
5.85 |
350.00 |
C6H6/C7H8 |
benzene/toluene |
85.1275 |
305.36 |
45.52 |
12.85 |
350.00 |
C6H6/H2O |
benzene/water |
48.0645 |
341.16 |
146.89 |
5.85 |
350.00 |
C4H10/C6H14 |
butane/hexane |
72.1510 |
202.08 |
36.84 |
-41.15 |
400.00 |
C4H10/C5H12 |
butane/pentane |
65.1375 |
177.02 |
37.67 |
-77.15 |
400.00 |
C4H10/C5H12/C6H14 |
butane/pentane/hexane |
65.1375 |
177.02 |
37.67 |
-77.15 |
400.00 |
CO2/1-C4H10O |
carbon dioxide/1-butanol |
44.0100 |
31.06 |
73.82 |
-57.15 |
400.00 |
CO2/C6H6 |
carbon dioxide/benzene |
44.0100 |
31.06 |
73.82 |
-57.15 |
400.00 |
CO2/C4H10 |
carbon dioxide/butane |
44.0100 |
31.06 |
73.82 |
-57.15 |
400.00 |
CO2/furfural |
carbon dioxide/furfural |
44.0100 |
31.06 |
73.82 |
-57.15 |
400.00 |
CO2/C6H14 |
carbon dioxide/hexane |
44.0100 |
31.06 |
73.82 |
-57.15 |
400.00 |
CO2/C5H12 |
carbon dioxide/pentane |
44.0100 |
31.06 |
73.82 |
-57.15 |
400.00 |
CO2/C3H8 |
carbon dioxide/propane |
44.0100 |
31.06 |
73.82 |
-57.15 |
400.00 |
CO2/C7H8 |
carbon dioxide/toluene |
44.0100 |
31.06 |
73.82 |
-57.15 |
400.00 |
CO2/C4H6O2/2-C4H10O |
carbon diox/vinyl ace/2-butanol |
44.0100 |
31.06 |
73.82 |
-57.15 |
400.00 |
D3/D4/D5/D6 |
D3/D4/D5/D6 |
222.4640 |
281.05 |
16.63 |
64.00 |
400.00 |
D4/D3 |
D4/D3 |
259.5410 |
297.00 |
15.00 |
64.00 |
400.00 |
D4/D5 |
D4/D5 |
333.6955 |
330.00 |
12.50 |
17.65 |
400.00 |
D4/D6 |
D4/D6 |
370.7725 |
342.00 |
11.50 |
17.65 |
400.00 |
D4/CP28 |
D4/CP28 |
241.3363 |
295.17 |
24.97 |
17.65 |
400.00 |
D4/PFCH |
D4/PFCH |
298.3325 |
0.00 |
0.00 |
17.65 |
400.00 |
D5/D3 |
D5/D3 |
296.6185 |
314.00 |
14.10 |
64.00 |
400.00 |
D5/D6 |
D5/D6 |
407.8500 |
360.00 |
10.60 |
-1.15 |
400.00 |
D6/D3 |
D6/D3 |
333.6955 |
327.00 |
13.10 |
64.00 |
400.00 |
C2H5OH/H2O |
ethanol/water |
32.0420 |
304.64 |
135.01 |
19.85 |
350.00 |
C8H10/C7H8 |
ethylbenzene/toluene |
99.1545 |
332.28 |
38.84 |
32.85 |
329.85 |
C7H16/C2H5OH |
heptane/ethanol |
100.2019 |
267.05 |
27.40 |
-73.15 |
1226.85 |
C6H14/C6H12 |
hexane/cyclohexane |
85.1700 |
256.70 |
35.50 |
6.85 |
400.00 |
i-C4H10/i-C5H12 |
isobutane/isopentane |
65.1375 |
164.99 |
36.39 |
-53.15 |
135.05 |
MD2M/MD3M |
MD2M/MD3M |
347.7665 |
340.00 |
10.00 |
2.85 |
400.00 |
MD2M/MD4M |
MD2M/MD4M |
384.8450 |
353.00 |
10.30 |
13.85 |
400.00 |
MD2M/MD5M |
MD2M/MD5M |
421.9200 |
362.00 |
9.70 |
21.85 |
400.00 |
MD2M/MD6M |
MD2M/MD6M |
459.0000 |
371.00 |
9.30 |
29.85 |
400.00 |
MD2M/PP2 |
MD2M/PP2 |
330.3713 |
0.00 |
0.00 |
29.85 |
400.00 |
MD3M/MD4M |
MD3M/MD4M |
421.9215 |
368.00 |
9.30 |
13.85 |
400.00 |
MD3M/MD5M |
MD3M/MD5M |
458.9965 |
377.00 |
8.80 |
21.85 |
400.00 |
MD3M/MD6M |
MD3M/MD6M |
496.0765 |
386.00 |
8.40 |
29.85 |
400.00 |
MD3M/PP2 |
MD3M/PP2 |
367.4478 |
0.00 |
0.00 |
29.85 |
400.00 |
MD4M/MD5M |
MD4M/MD5M |
496.0750 |
389.00 |
8.20 |
21.85 |
400.00 |
MD4M/MD6M |
MD4M/MD6M |
533.1550 |
398.00 |
7.80 |
29.85 |
400.00 |
MD4M/PP2 |
MD4M/PP2 |
404.5229 |
0.00 |
0.00 |
29.85 |
400.00 |
MD5M/MD6M |
MD5M/MD6M |
570.2300 |
407.00 |
7.20 |
29.85 |
400.00 |
MDM/MD2M |
MDM/MD2M |
273.6100 |
309.00 |
13.10 |
-10.15 |
400.00 |
MDM/MD3M |
MDM/MD3M |
310.6865 |
323.00 |
12.20 |
2.85 |
400.00 |
MDM/MD4M |
MDM/MD4M |
347.7650 |
336.00 |
11.60 |
13.85 |
400.00 |
MDM/MD5M |
MDM/MD5M |
384.8400 |
345.00 |
11.00 |
21.85 |
400.00 |
MDM/MD6M |
MDM/MD6M |
421.9200 |
354.00 |
10.60 |
29.85 |
400.00 |
MDM/PP2 |
MDM/PP2 |
293.2920 |
0.00 |
0.00 |
29.85 |
400.00 |
CH4/CO2 |
methane/carbon dioxide |
16.0425 |
-82.59 |
45.99 |
-182.46 |
351.85 |
CH4O/C6H6 |
methanol/benzene |
55.0780 |
269.75 |
76.23 |
14.85 |
350.00 |
CH4O/C7H8 |
methanol/toluene |
55.0780 |
269.75 |
76.23 |
14.85 |
350.00 |
CH4O/H2O |
methanol/water |
25.0285 |
308.12 |
149.91 |
14.85 |
350.00 |
MM/PP2 |
MM/PP2 |
256.2158 |
0.00 |
0.00 |
-45.15 |
400.00 |
MM/CP28 |
MM/CP28 |
174.2168 |
0.00 |
0.00 |
-45.15 |
400.00 |
MM/D3 |
MM/D3 |
192.4215 |
263.00 |
18.00 |
64.00 |
400.00 |
MM/MD2M |
MM/MD2M |
236.5345 |
286.00 |
15.60 |
-10.15 |
400.00 |
MM/MD3M |
MM/MD3M |
273.6110 |
300.00 |
14.70 |
2.85 |
400.00 |
MM/MD4M |
MM/MD4M |
310.6895 |
313.00 |
14.10 |
13.85 |
400.00 |
MM/MD5M |
MM/MD5M |
347.7645 |
322.00 |
13.50 |
21.85 |
400.00 |
MM/MD6M |
MM/MD6M |
384.8445 |
331.00 |
13.10 |
29.85 |
400.00 |
MM/MDM |
MM/MDM |
199.4545 |
268.00 |
16.90 |
-25.15 |
400.00 |
MM/MDM/MD2M |
MM/MDM/MD2M |
199.4554 |
266.49 |
17.37 |
-10.15 |
400.00 |
MM/MDM/MD3M |
MM/MDM/MD3M |
251.3635 |
306.00 |
16.00 |
2.85 |
400.00 |
MM/MDM/MD4M |
MM/MDM/MD4M |
273.6106 |
306.00 |
16.00 |
13.85 |
400.00 |
MM/MDM/MD2M/MD3M |
MM/MDM/MD2M/MD3M |
273.6106 |
306.00 |
16.00 |
13.85 |
400.00 |
MM/MDM/MD2M/MD3M/MD4M/MD5M/MD6M |
MM/MDM/MD2M/MD3M/MD4M/MD5M/MD6M |
273.6106 |
306.00 |
16.00 |
13.85 |
400.00 |
N2/O2 |
nitrogen/oxygen |
28.8102 |
-140.72 |
37.94 |
-209.15 |
350.00 |
C5H12/C6H14 |
pentane/hexane |
79.1645 |
217.20 |
32.32 |
-41.15 |
400.00 |
C3H8/C4H10 |
propane/butane |
44.0970 |
96.67 |
42.50 |
-187.62 |
400.00 |
C3H8/C5H12 |
propane/pentane |
58.1205 |
160.08 |
44.82 |
-77.15 |
400.00 |
c8H10/c6H14 |
p-xylene/hexane |
106.1680 |
344.05 |
36.06 |
32.85 |
329.85 |
R113/C2H5OH |
R113/ethanol |
116.7245 |
229.85 |
60.56 |
19.85 |
350.00 |
R114/C2H5OH |
R114/ethanol |
108.5045 |
204.18 |
59.05 |
19.85 |
350.00 |
R125/R134a |
R125/R134a |
120.0200 |
66.25 |
36.31 |
-40.15 |
400.00 |
R134a/R116 |
R134a/R116 |
120.0210 |
65.92 |
31.53 |
-63.15 |
101.06 |
R134a/R142b |
R134a/R142b |
101.2630 |
119.27 |
43.19 |
-63.15 |
101.06 |
R14/R23 |
R14/R23 |
79.0090 |
-1.65 |
57.24 |
-163.15 |
400.00 |
R32/R125 |
R32/R125 |
52.0240 |
78.41 |
58.30 |
-124.15 |
78.41 |
R32/R134a |
R32/R134a |
52.0240 |
78.41 |
58.30 |
-124.15 |
78.41 |
R407a |
R407A |
90.1095 |
75.78 |
41.83 |
-40.15 |
78.41 |
R410a |
R410A |
72.5853 |
74.83 |
51.42 |
-40.15 |
78.41 |
R410b |
R410B |
75.5717 |
74.31 |
50.42 |
-40.15 |
78.41 |
H2O/2-C3H8O |
water/2-propanol |
34.8474 |
292.45 |
98.70 |
51.85 |
350.00 |
H2O/2-C4H10O |
water/2-butanol |
34.8474 |
292.45 |
98.70 |
51.85 |
350.00 |
The limits for the calculation of properties are as follows:
For a pure fluid:
Pmin = Psat at freezing temperature, i.e. P(Tmin, q=1)
Pmax = P(Tmax, v = 1/2 vc)
For a mixture:
Tmin = Max[Tmin (i)]; i = 1,2,..., ncomponents
Tmax = Min[Tmax(i)]; i = 1,2,..., ncomponents
Pmin = P(Tmin, q = 0)
Pmax = P(Tmax, v = 1/2 vc,min),
vc,min = Max[vc (i)] ; i = 1,2,..., ncomponents