- InChI
- InChI=1S/C3H8O2/c1-3(5)2-4/h3-5H,2H2,1H3
- InChI Key
- DNIAPMSPPWPWGF-UHFFFAOYSA-N
- Formula
- C3H8O2
- SMILES
- CC(O)CO
- Molecular Weight1
- 76.09
- CAS
- 4254-16-4
- Other Names
-
- (.+-.)-1,2-propanediol
- (.+/-.)-1,2-Propanediol
- (R,S)-1,2-propanediol
- (RS)-1,2-Propanediol
- 1,2-Propandiol
- 1,2-Propylenglykol
- 1,2-dihydroxypropane
- 1,2-propanediol
- 1,2-propanediol (propylene glycol)
- 1,2-propylene glycol
- 2,3-Propanediol
- 2-hydroxypropanol
- DL-1,2-Propanediol
- DL-Propylene glycol
- Dowfrost
- Ilexan P
- Isopropylene glycol
- Methylethyl glycol
- Methylethylene glycol
- Monopropylene glycol
- NSC 69860
- PG 12
- Prolugen
- Propylene glycol USP
- Propylenglycol
- Sentry Propylene Glycol
- Sirlene
- Solar winter ban
- Solargard P
- Trimethyl glycol
- Ucar 35
- propane-1,2-diol
- propanediol
- propylene glycol (1,2-propanediol)
- «alpha»-Propylene glycol
- ω : Acentric Factor.
- Tig : Autoignition Temperature (K).
- Cp,gas : Ideal gas heat capacity (J/mol×K).
- Cp,liquid : Liquid phase heat capacity (J/mol×K).
- μ : Dipole Moment (debye).
- η : Dynamic viscosity (Pa×s).
- εr : Dielectric Constant (Relative permittivity).
- Tflash,cc : Flash Point (Closed Cup Method) (K).
- ΔfG° : Standard Gibbs free energy of formation (kJ/mol).
- ΔfH°gas : Enthalpy of formation at standard conditions (kJ/mol).
- ΔfusH° : Enthalpy of fusion at standard conditions (kJ/mol).
- ΔvapH° : Enthalpy of vaporization at standard conditions (kJ/mol).
- ΔvapH : Enthalpy of vaporization at a given temperature (kJ/mol).
- IE : Ionization energy (eV).
- log10WS : Log10 of Water solubility in mol/l.
- logPoct/wat : Octanol/Water partition coefficient.
- McVol : McGowan's characteristic volume (ml/mol).
- NFPA Fire : NFPA Fire Rating.
- NFPA Health : NFPA Health Rating.
- NFPA Safety : NFPA Safety Rating.
- Pc : Critical Pressure (kPa).
- Ptriple : Triple Point Pressure (kPa).
- Pvap : Vapor pressure (kPa).
- n0 : Refractive Index.
- ρl : Liquid Density (kg/m3).
- csound,fluid : Speed of sound in fluid (m/s).
- γ : Surface Tension (N/m).
- Tboil : Normal Boiling Point Temperature (K).
- Tc : Critical Temperature (K).
- λgas : Gas thermal conductivity (W/m×K).
- λliquid : Liquid thermal conductivity (W/m×K).
- Tfus : Normal melting (fusion) point (K).
- Ttriple : Triple Point Temperature (K).
- UQi : UNIQUAC Qi Parameter.
- URi : UNIQUAC Ri Parameter.
- Vc : Critical Volume (m3/kmol).
- vspec : Specific Volume (m3/kg).
- Zc : Critical Compressibility.
- 1: Molecular weight from the IUPAC atomic weights tables.
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Contents
- Physical Properties
- Temperature Dependent Properties
- Datasets
- Correlations
- Similar Compounds
- Mixtures
- Sources
Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ω | [0.5928; 1.1272] |
|
|
| ω | 0.5928 | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value | |
| ω | 1.1272 | ChemSep v8.3 pure component data Compiled value | |
| Tig | 644.15 | K | NCMS SOLV-DB |
| μ | [3.60; 3.63] | debye |
|
| μ | 3.63 | debye | ChemSep v8.3 pure component data Compiled value |
| μ | 3.60 | debye | KDB |
| εr | 32.00 | NCMS SOLV-DB | |
| Tflash,cc | 372.15 | K | NCMS SOLV-DB |
| ΔfG° | -304.00 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | [-424.20; -421.50] | kJ/mol |
|
| ΔfH°gas | -421.50 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | -424.20 | kJ/mol | KDB |
| ΔfusH° | 8.18 | kJ/mol | Joback Calculated Property |
| ΔvapH° | 54.43 | kJ/mol | NCMS SOLV-DB |
| IE | 10.24 | eV | Relay (1.0) Calculated Property |
| log10WS | 0.96 | Relay (1.0) Calculated Property | |
| logPoct/wat | -0.920 | NCMS SOLV-DB | |
| McVol | 64.870 | ml/mol | McGowan Calculated Property |
| NFPA Fire | [%!d(float64=1); %!d(float64=1)] |
|
|
| NFPA Fire | 1 | KDB | |
| NFPA Fire | 1 | NCMS SOLV-DB | |
| NFPA Health | [%!d(float64=0); %!d(float64=1)] |
|
|
| NFPA Health | 1 | KDB | |
| NFPA Health | 0 | NCMS SOLV-DB | |
| NFPA Safety | 0 | NCMS SOLV-DB | |
| Pc | [5900.00; 6090.00] | kPa |
|
| Pc | 5900.00 | kPa | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value |
| Pc | 5941.00 | kPa | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Pc | 6090.00 | kPa | ChemSep v8.3 pure component data Compiled value |
| Pc | 6070.00 | kPa | KDB |
| Ptriple | 9.29e-08 | kPa | ChemSep v8.3 pure component data Compiled value |
| Tboil | [460.50; 461.35] | K |
|
| Tboil | 460.75 | K | ChemSep v8.3 pure component data Compiled value |
| Tboil | 460.50 | K | KDB |
| Tboil | 461.35 | K | NCMS SOLV-DB |
| Tc | [624.15; 676.40] | K |
|
| Tc | 676.00 | K | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value |
| Tc | 676.40 | K | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Tc | 624.15 | K | ChemSep v8.3 pure component data Compiled value |
| Tc | 625.00 | K | KDB |
| Tfus | [213.00; 213.15] | K |
|
| Tfus | 213.15 | K | Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value |
| Tfus | 213.15 | K | ChemSep v8.3 pure component data Compiled value |
| Tfus | 213.00 | K | KDB |
| Tfus | 213.15 | K | NCMS SOLV-DB |
| Ttriple | 213.15 | K | ChemSep v8.3 pure component data Compiled value |
| UQi | 4.02 | ChemSep v8.3 pure component data Compiled value | |
| URi | 4.02 | ChemSep v8.3 pure component data Compiled value | |
| Vc | [0.237; 0.237] | m3/kmol |
|
| Vc | 0.237 | m3/kmol | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Vc | 0.237 | m3/kmol | ChemSep v8.3 pure component data Compiled value |
| Vc | 0.237 | m3/kmol | KDB |
| Zc | [0.2768350; 0.2800000] |
|
|
| Zc | 0.2800000 | ChemSep v8.3 pure component data Compiled value | |
| Zc | 0.2768350 | KDB |
Temperature Dependent Properties
Datasets
Mass density, kg/m3
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 298.15 | 98.00 | 1032.56 |
| 303.15 | 98.00 | 1028.87 |
| 312.98 | 98.00 | 1022.16 |
| 335.78 | 98.00 | 1005.31 |
| 364.39 | 98.00 | 981.63 |
| 394.95 | 98.00 | 953.22 |
| 423.51 | 98.00 | 926.76 |
| 452.17 | 98.00 | 900.36 |
| 298.15 | 49030.00 | 1055.29 |
| 303.15 | 49030.00 | 1052.03 |
| 313.00 | 49030.00 | 1046.22 |
| 335.80 | 49030.00 | 1029.3 |
| 364.66 | 49030.00 | 1007.36 |
| 395.11 | 49030.00 | 982.98 |
| 423.62 | 49030.00 | 959.18 |
| 452.10 | 49030.00 | 934.51 |
| 298.15 | 98060.00 | 1072.94 |
| 303.15 | 98060.00 | 1070.79 |
| 313.05 | 98060.00 | 1065.24 |
| 335.76 | 98060.00 | 1050.34 |
| 364.83 | 98060.00 | 1031.15 |
| 395.17 | 98060.00 | 1010.62 |
| 423.90 | 98060.00 | 989.94 |
| 452.14 | 98060.00 | 965.53 |
| 298.15 | 147100.00 | 1088.48 |
| 303.15 | 147100.00 | 1086.25 |
| 313.03 | 147100.00 | 1081.67 |
| 335.78 | 147100.00 | 1068.19 |
| 364.87 | 147100.00 | 1051.61 |
| 395.38 | 147100.00 | 1033.92 |
| 423.97 | 147100.00 | 1016.34 |
| 452.19 | 147100.00 | 996.01 |
| 298.15 | 196130.00 | 1104.32 |
| 303.15 | 196130.00 | 1101.4 |
| 313.04 | 196130.00 | 1095.69 |
| 335.80 | 196130.00 | 1082.92 |
| 365.00 | 196130.00 | 1067.32 |
| 395.57 | 196130.00 | 1051.9 |
| 424.05 | 196130.00 | 1038.38 |
| 452.18 | 196130.00 | 1022.83 |
| 298.15 | 245160.00 | 1115.28 |
| 303.15 | 245160.00 | 1112.65 |
| 313.03 | 245160.00 | 1107.51 |
| 336.01 | 245160.00 | 1095.8 |
| 364.99 | 245160.00 | 1081.56 |
| 395.68 | 245160.00 | 1067.12 |
| 424.30 | 245160.00 | 1054.25 |
| 452.07 | 245160.00 | 1042.31 |
| Reference | ||
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 278.15 | 100.00 | 1047.1 |
| 278.15 | 1000.00 | 1047.3 |
| 278.15 | 5000.00 | 1049.2 |
| 278.15 | 10000.00 | 1051.2 |
| 278.15 | 15000.00 | 1053.4 |
| 278.15 | 20000.00 | 1055.5 |
| 278.15 | 25000.00 | 1057.6 |
| 278.15 | 30000.00 | 1059.6 |
| 278.15 | 35000.00 | 1061.6 |
| 278.15 | 40000.00 | 1063.6 |
| 278.15 | 45000.00 | 1065.6 |
| 278.15 | 50000.00 | 1067.5 |
| 278.15 | 55000.00 | 1069.3 |
| 278.15 | 60000.00 | 1071.4 |
| 288.15 | 100.00 | 1039.9 |
| 288.15 | 1000.00 | 1040.2 |
| 288.15 | 5000.00 | 1042.1 |
| 288.15 | 10000.00 | 1044.4 |
| 288.15 | 15000.00 | 1046.7 |
| 288.15 | 20000.00 | 1048.9 |
| 288.15 | 25000.00 | 1051.1 |
| 288.15 | 30000.00 | 1053.2 |
| 288.15 | 35000.00 | 1055.4 |
| 288.15 | 40000.00 | 1057.4 |
| 288.15 | 45000.00 | 1059.4 |
| 288.15 | 50000.00 | 1061.4 |
| 288.15 | 55000.00 | 1063.4 |
| 288.15 | 60000.00 | 1065.3 |
| 298.15 | 100.00 | 1032.5 |
| 298.15 | 1000.00 | 1032.9 |
| 298.15 | 5000.00 | 1034.8 |
| 298.15 | 10000.00 | 1037.2 |
| 298.15 | 15000.00 | 1039.6 |
| 298.15 | 20000.00 | 1041.9 |
| 298.15 | 25000.00 | 1044.1 |
| 298.15 | 30000.00 | 1046.3 |
| 298.15 | 35000.00 | 1048.4 |
| 298.15 | 40000.00 | 1050.6 |
| 298.15 | 45000.00 | 1052.5 |
| 298.15 | 50000.00 | 1054.6 |
| 298.15 | 55000.00 | 1056.6 |
| 298.15 | 60000.00 | 1058.5 |
| 308.15 | 100.00 | 1025.3 |
| 308.15 | 1000.00 | 1025.5 |
| 308.15 | 5000.00 | 1027.5 |
| 308.15 | 10000.00 | 1030.1 |
| 308.15 | 15000.00 | 1032.5 |
| 308.15 | 20000.00 | 1034.9 |
| 308.15 | 25000.00 | 1037.2 |
| 308.15 | 30000.00 | 1039.5 |
| 308.15 | 35000.00 | 1041.6 |
| 308.15 | 40000.00 | 1043.8 |
| 308.15 | 45000.00 | 1046.0 |
| 308.15 | 50000.00 | 1048.1 |
| 308.15 | 55000.00 | 1050.1 |
| 308.15 | 60000.00 | 1052.2 |
| 318.15 | 100.00 | 1017.7 |
| 318.15 | 1000.00 | 1018.0 |
| 318.15 | 5000.00 | 1020.2 |
| 318.15 | 10000.00 | 1022.8 |
| 318.15 | 15000.00 | 1025.4 |
| 318.15 | 20000.00 | 1027.9 |
| 318.15 | 25000.00 | 1030.3 |
| 318.15 | 30000.00 | 1032.7 |
| 318.15 | 35000.00 | 1035.0 |
| 318.15 | 40000.00 | 1037.2 |
| 318.15 | 45000.00 | 1039.4 |
| 318.15 | 50000.00 | 1041.5 |
| 318.15 | 55000.00 | 1043.6 |
| 318.15 | 60000.00 | 1045.7 |
| 328.15 | 100.00 | 1010.0 |
| 328.15 | 1000.00 | 1010.3 |
| 328.15 | 5000.00 | 1012.7 |
| 328.15 | 10000.00 | 1015.4 |
| 328.15 | 15000.00 | 1018.0 |
| 328.15 | 20000.00 | 1020.6 |
| 328.15 | 25000.00 | 1023.1 |
| 328.15 | 30000.00 | 1025.6 |
| 328.15 | 35000.00 | 1027.9 |
| 328.15 | 40000.00 | 1030.3 |
| 328.15 | 45000.00 | 1032.5 |
| 328.15 | 50000.00 | 1034.7 |
| 328.15 | 55000.00 | 1036.9 |
| 328.15 | 60000.00 | 1039.0 |
| 338.15 | 100.00 | 1002.2 |
| 338.15 | 1000.00 | 1002.4 |
| 338.15 | 5000.00 | 1004.8 |
| 338.15 | 10000.00 | 1007.6 |
| 338.15 | 15000.00 | 1010.4 |
| 338.15 | 20000.00 | 1013.0 |
| 338.15 | 25000.00 | 1015.6 |
| 338.15 | 30000.00 | 1018.2 |
| 338.15 | 35000.00 | 1020.7 |
| 338.15 | 40000.00 | 1023.2 |
| 338.15 | 45000.00 | 1025.5 |
| 338.15 | 50000.00 | 1027.9 |
| 338.15 | 55000.00 | 1030.2 |
| 338.15 | 60000.00 | 1032.4 |
| 348.15 | 100.00 | 994.1 |
| 348.15 | 1000.00 | 994.5 |
| 348.15 | 5000.00 | 996.9 |
| 348.15 | 10000.00 | 999.9 |
| 348.15 | 15000.00 | 1002.8 |
| 348.15 | 20000.00 | 1005.5 |
| 348.15 | 25000.00 | 1008.2 |
| 348.15 | 30000.00 | 1010.9 |
| 348.15 | 35000.00 | 1013.4 |
| 348.15 | 40000.00 | 1016.0 |
| 348.15 | 45000.00 | 1018.4 |
| 348.15 | 50000.00 | 1020.9 |
| 348.15 | 55000.00 | 1023.2 |
| 348.15 | 60000.00 | 1025.6 |
| 358.15 | 100.00 | 985.8 |
| 358.15 | 1000.00 | 986.2 |
| 358.15 | 5000.00 | 988.8 |
| 358.15 | 10000.00 | 991.9 |
| 358.15 | 15000.00 | 995.0 |
| 358.15 | 20000.00 | 997.8 |
| 358.15 | 25000.00 | 1000.6 |
| 358.15 | 30000.00 | 1003.4 |
| 358.15 | 35000.00 | 1006.0 |
| 358.15 | 40000.00 | 1008.5 |
| 358.15 | 45000.00 | 1011.2 |
| 358.15 | 50000.00 | 1013.6 |
| 358.15 | 55000.00 | 1016.1 |
| 358.15 | 60000.00 | 1018.5 |
| Reference | ||
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 272.69 | 5240.00 | 1054.19 |
| 272.68 | 10290.00 | 1056.38 |
| 272.68 | 15270.00 | 1058.53 |
| 272.72 | 20360.00 | 1060.64 |
| 272.73 | 30580.00 | 1064.73 |
| 272.73 | 50680.00 | 1072.45 |
| 272.77 | 71000.00 | 1079.68 |
| 272.74 | 91400.00 | 1086.61 |
| 272.76 | 50810.00 | 1072.51 |
| 272.78 | 15370.00 | 1058.52 |
| 293.18 | 5180.00 | 1039.1 |
| 293.18 | 10100.00 | 1041.39 |
| 293.18 | 15210.00 | 1043.73 |
| 293.18 | 20190.00 | 1045.96 |
| 293.18 | 30240.00 | 1050.35 |
| 293.18 | 50550.00 | 1058.66 |
| 293.18 | 70760.00 | 1066.35 |
| 293.18 | 90990.00 | 1073.55 |
| 293.18 | 50680.00 | 1058.72 |
| 293.18 | 15310.00 | 1043.77 |
| 313.12 | 5120.00 | 1024.21 |
| 313.13 | 10070.00 | 1026.73 |
| 313.13 | 15110.00 | 1029.21 |
| 313.12 | 20290.00 | 1031.71 |
| 313.13 | 30290.00 | 1036.38 |
| 313.12 | 50710.00 | 1045.31 |
| 313.12 | 71030.00 | 1053.5 |
| 313.12 | 91240.00 | 1061.08 |
| 313.12 | 50990.00 | 1045.42 |
| 313.12 | 15580.00 | 1029.43 |
| 352.99 | 5010.00 | 993.23 |
| 353.00 | 10100.00 | 996.26 |
| 353.00 | 15280.00 | 999.29 |
| 352.99 | 20210.00 | 1002.06 |
| 352.99 | 30360.00 | 1007.57 |
| 353.00 | 50610.00 | 1017.74 |
| 352.99 | 70750.00 | 1027.01 |
| 352.99 | 91060.00 | 1035.61 |
| 352.99 | 50620.00 | 1017.76 |
| 352.99 | 15390.00 | 999.36 |
| 392.94 | 5080.00 | 959.54 |
| 392.94 | 10090.00 | 963.15 |
| 392.95 | 15190.00 | 966.67 |
| 392.96 | 20230.00 | 970.02 |
| 392.97 | 30430.00 | 976.54 |
| 392.95 | 50730.00 | 988.44 |
| 392.94 | 70890.00 | 999.07 |
| 392.94 | 90950.00 | 1008.71 |
| 392.95 | 50820.00 | 988.49 |
| 392.96 | 15180.00 | 966.75 |
| 283.21 | 5190.00 | 1046.44 |
| 283.19 | 10060.00 | 1048.67 |
| 283.17 | 15100.00 | 1050.92 |
| 283.17 | 20200.00 | 1053.13 |
| 283.17 | 30530.00 | 1057.48 |
| 283.18 | 50550.00 | 1065.43 |
| 283.19 | 70990.00 | 1072.96 |
| 283.18 | 91270.00 | 1079.99 |
| 283.18 | 50490.00 | 1065.4 |
| 283.17 | 15140.00 | 1050.94 |
| 298.12 | 5090.00 | 1035.37 |
| 298.12 | 10070.00 | 1037.74 |
| 298.12 | 15240.00 | 1040.15 |
| 298.12 | 20170.00 | 1042.4 |
| 298.12 | 30300.00 | 1046.89 |
| 298.12 | 50590.00 | 1055.32 |
| 298.11 | 70930.00 | 1063.17 |
| 298.12 | 91050.00 | 1070.41 |
| 298.12 | 50650.00 | 1055.35 |
| 298.12 | 15160.00 | 1040.11 |
| 333.05 | 5260.00 | 1009.12 |
| 333.05 | 10050.00 | 1011.76 |
| 333.05 | 15120.00 | 1014.46 |
| 333.05 | 20250.00 | 1017.1 |
| 333.05 | 30400.00 | 1022.19 |
| 333.05 | 50610.00 | 1031.67 |
| 333.06 | 70910.00 | 1040.39 |
| 333.06 | 91130.00 | 1048.43 |
| 333.06 | 51080.00 | 1031.87 |
| 333.06 | 15210.00 | 1014.48 |
| 373.34 | 10320.00 | 980.11 |
| 373.34 | 15330.00 | 983.26 |
| 373.34 | 20360.00 | 986.4 |
| 373.34 | 30530.00 | 992.32 |
| 373.34 | 50610.00 | 1003.25 |
| 373.34 | 70990.00 | 1013.23 |
| 373.35 | 91190.00 | 1022.41 |
| 373.35 | 50860.00 | 1003.34 |
| 373.35 | 15540.00 | 983.34 |
| 373.35 | 5160.00 | 976.65 |
| 313.03 | 5190.00 | 1024.2 |
| 313.03 | 10100.00 | 1026.69 |
| 313.03 | 15280.00 | 1029.25 |
| 313.03 | 20240.00 | 1031.64 |
| 313.03 | 30440.00 | 1036.4 |
| 313.03 | 50660.00 | 1045.24 |
| 313.03 | 70960.00 | 1053.42 |
| 313.03 | 91090.00 | 1061.0 |
| 313.03 | 50710.00 | 1045.28 |
| 313.03 | 15210.00 | 1029.23 |
| Reference | ||
Speed of sound, m/s
Operational condition: Frequency, MHz = 8 (Liquid)
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Speed of sound, m/s - Liquid |
| 303.15 | 99.00 | 1494.429 |
| 303.15 | 5091.00 | 1513.504 |
| 303.15 | 10060.00 | 1532.024 |
| 303.15 | 15098.00 | 1550.199 |
| 303.15 | 20084.00 | 1567.713 |
| 303.15 | 25068.00 | 1584.711 |
| 303.15 | 30167.00 | 1601.587 |
| 313.15 | 99.00 | 1465.858 |
| 313.15 | 5014.00 | 1485.499 |
| 313.15 | 10053.00 | 1504.824 |
| 313.15 | 15011.00 | 1523.212 |
| 313.15 | 20095.00 | 1541.536 |
| 313.15 | 25202.00 | 1559.357 |
| 313.15 | 30222.00 | 1576.498 |
| 333.15 | 100.00 | 1408.863 |
| 333.15 | 5039.00 | 1429.721 |
| 333.15 | 10054.00 | 1450.066 |
| 333.15 | 15107.00 | 1469.848 |
| 333.15 | 20131.00 | 1488.963 |
| 333.15 | 25131.00 | 1507.384 |
| 333.15 | 30024.00 | 1524.874 |
| 353.15 | 99.00 | 1350.887 |
| 353.15 | 5042.00 | 1373.03 |
| 353.15 | 10055.00 | 1394.56 |
| 353.15 | 15135.00 | 1415.607 |
| 353.15 | 20093.00 | 1435.461 |
| 353.15 | 25086.00 | 1454.828 |
| 353.15 | 30207.00 | 1474.064 |
| Reference | ||
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [94.12; 210.58] | J/mol×K | [213.15; 1000.15] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is Cp,gas in J/mol×K, T in K | |||
| Coefficient A | 9.00000e+01 | |||
| Coefficient B | -1.00000e+03 | |||
| Coefficient C | 6.19224e+00 | |||
| Coefficient D | -4.00000e-04 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 213.15 | |||
| Temperature range, max. | 1000.15 | |||
| Cp,gas | 94.12 | J/mol×K | 213.15 | Calculated Property |
| Cp,gas | 105.57 | J/mol×K | 300.59 | Calculated Property |
| Cp,gas | 121.82 | J/mol×K | 388.04 | Calculated Property |
| Cp,gas | 139.35 | J/mol×K | 475.48 | Calculated Property |
| Cp,gas | 156.07 | J/mol×K | 562.93 | Calculated Property |
| Cp,gas | 171.01 | J/mol×K | 650.37 | Calculated Property |
| Cp,gas | 183.86 | J/mol×K | 737.82 | Calculated Property |
| Cp,gas | 194.63 | J/mol×K | 825.26 | Calculated Property |
| Cp,gas | 203.47 | J/mol×K | 912.71 | Calculated Property |
| Cp,gas | 210.58 | J/mol×K | 1000.15 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | [154.19; 263.13] | J/mol×K | [213.15; 460.75] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A + B·T + C·T² + D·T³ + E·T⁴ Y is Cp,liquid in J/mol×K, T in K | |||
| Coefficient A | 6.04000e+01 | |||
| Coefficient B | 4.40000e-01 | |||
| Coefficient C | 0.00000e+00 | |||
| Coefficient D | 0.00000e+00 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 213.15 | |||
| Temperature range, max. | 460.75 | |||
| Cp,liquid | 154.19 | J/mol×K | 213.15 | Calculated Property |
| Cp,liquid | 166.29 | J/mol×K | 240.66 | Calculated Property |
| Cp,liquid | 178.40 | J/mol×K | 268.17 | Calculated Property |
| Cp,liquid | 190.50 | J/mol×K | 295.68 | Calculated Property |
| Cp,liquid | 202.61 | J/mol×K | 323.19 | Calculated Property |
| Cp,liquid | 214.71 | J/mol×K | 350.71 | Calculated Property |
| Cp,liquid | 226.82 | J/mol×K | 378.22 | Calculated Property |
| Cp,liquid | 238.92 | J/mol×K | 405.73 | Calculated Property |
| Cp,liquid | 251.03 | J/mol×K | 433.24 | Calculated Property |
| Cp,liquid | 263.13 | J/mol×K | 460.75 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [950.1896572; 0.0003307] | Pa×s | [213.15; 500.80] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = exp(A + B/T + C·ln(T) + D·T^E) Y is η in Pa×s, T in K | |||
| Coefficient A | -8.04540e+02 | |||
| Coefficient B | 3.04870e+04 | |||
| Coefficient C | 1.30790e+02 | |||
| Coefficient D | -1.54490e-01 | |||
| Coefficient E | 1.00000e+00 | |||
| Temperature range, min. | 213.15 | |||
| Temperature range, max. | 500.80 | |||
| η | 950.1896572 | Pa×s | 213.15 | Calculated Property |
| η | 4.6738069 | Pa×s | 245.11 | Calculated Property |
| η | 0.1803495 | Pa×s | 277.07 | Calculated Property |
| η | 0.0234718 | Pa×s | 309.03 | Calculated Property |
| η | 0.0063183 | Pa×s | 340.99 | Calculated Property |
| η | 0.0026165 | Pa×s | 372.96 | Calculated Property |
| η | 0.0013850 | Pa×s | 404.92 | Calculated Property |
| η | 0.0008321 | Pa×s | 436.88 | Calculated Property |
| η | 0.0005251 | Pa×s | 468.84 | Calculated Property |
| η | 0.0003307 | Pa×s | 500.80 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | [71.30; 0.00] | kJ/mol | [213.15; 624.15] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A·(1 − Tr)^(B + C·Tr + D·Tr² + E·Tr³), Tr = T/Tc Y is ΔvapH in kJ/mol, T in K | |||
| Coefficient A | 8.02000e+01 | |||
| Coefficient B | 3.30000e-01 | |||
| Coefficient C | -1.95000e-01 | |||
| Coefficient D | 1.20000e-01 | |||
| Coefficient E | 1.00000e-01 | |||
| Critical temperature, Tc (K) | 6.24150e+02 | |||
| Comment | Range stopped at Tc; ChemSep gives it to 626 K. | |||
| Temperature range, min. | 213.15 | |||
| Temperature range, max. | 624.15 | |||
| ΔvapH | 71.30 | kJ/mol | 213.15 | Calculated Property |
| ΔvapH | 69.15 | kJ/mol | 258.82 | Calculated Property |
| ΔvapH | 66.72 | kJ/mol | 304.48 | Calculated Property |
| ΔvapH | 63.90 | kJ/mol | 350.15 | Calculated Property |
| ΔvapH | 60.51 | kJ/mol | 395.82 | Calculated Property |
| ΔvapH | 56.33 | kJ/mol | 441.48 | Calculated Property |
| ΔvapH | 51.01 | kJ/mol | 487.15 | Calculated Property |
| ΔvapH | 43.93 | kJ/mol | 532.82 | Calculated Property |
| ΔvapH | 33.66 | kJ/mol | 578.48 | Calculated Property |
| ΔvapH | 0.00 | kJ/mol | 624.15 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [0.40; 208.10] | kPa | [335.73; 485.20] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.64972e+01 | |||
| Coefficient B | -4.64181e+03 | |||
| Coefficient C | -6.92380e+01 | |||
| Temperature range, min. | 335.73 | |||
| Temperature range, max. | 485.20 | |||
| Pvap | 0.40 | kPa | 335.73 | Calculated Property |
| Pvap | 1.11 | kPa | 352.34 | Calculated Property |
| Pvap | 2.74 | kPa | 368.95 | Calculated Property |
| Pvap | 6.19 | kPa | 385.55 | Calculated Property |
| Pvap | 12.87 | kPa | 402.16 | Calculated Property |
| Pvap | 24.96 | kPa | 418.77 | Calculated Property |
| Pvap | 45.58 | kPa | 435.38 | Calculated Property |
| Pvap | 79.01 | kPa | 451.98 | Calculated Property |
| Pvap | 130.83 | kPa | 468.59 | Calculated Property |
| Pvap | 208.10 | kPa | 485.20 | Calculated Property |
| Pvap | [7.31e-08; 6090.00] | kPa | [213.15; 604.05] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is Pvap in kPa, T in K | |||
| Coefficient A | 0.00000e+00 | |||
| Coefficient B | -1.33127e+04 | |||
| Coefficient C | 6.46694e+01 | |||
| Coefficient D | -1.04550e-01 | |||
| Coefficient E | 8.01298e-05 | |||
| Comment | Range stopped where the equation exceeds Pc; ChemSep gives it to 624.15 K. | |||
| Temperature range, min. | 213.15 | |||
| Temperature range, max. | 604.05 | |||
| Pvap | 7.31e-08 | kPa | 213.15 | Calculated Property |
| Pvap | 1.56e-04 | kPa | 256.58 | Calculated Property |
| Pvap | 0.02 | kPa | 300.02 | Calculated Property |
| Pvap | 0.58 | kPa | 343.45 | Calculated Property |
| Pvap | 6.08 | kPa | 386.88 | Calculated Property |
| Pvap | 35.90 | kPa | 430.32 | Calculated Property |
| Pvap | 151.78 | kPa | 473.75 | Calculated Property |
| Pvap | 539.24 | kPa | 517.18 | Calculated Property |
| Pvap | 1798.15 | kPa | 560.62 | Calculated Property |
| Pvap | 6090.00 | kPa | 604.05 | Calculated Property |
| Pvap | [8.87e-08; 6165.74] | kPa | [213.15; 626.00] |
KDB Vapor Pressure Data
|
| Equation | ln(Y) = A + B/T + C·ln(T) + D·T² + E/T² Y is Pvap in kPa, T in K | |||
| Coefficient A | 2.23565e+02 | |||
| Coefficient B | -1.60975e+04 | |||
| Coefficient C | -3.08431e+01 | |||
| Coefficient D | 2.42067e-05 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 213.15 | |||
| Temperature range, max. | 626.00 | |||
| Pvap | 8.87e-08 | kPa | 213.15 | Calculated Property |
| Pvap | 2.36e-04 | kPa | 259.02 | Calculated Property |
| Pvap | 0.03 | kPa | 304.89 | Calculated Property |
| Pvap | 0.91 | kPa | 350.77 | Calculated Property |
| Pvap | 9.52 | kPa | 396.64 | Calculated Property |
| Pvap | 55.54 | kPa | 442.51 | Calculated Property |
| Pvap | 227.08 | kPa | 488.38 | Calculated Property |
| Pvap | 751.49 | kPa | 534.26 | Calculated Property |
| Pvap | 2211.30 | kPa | 580.13 | Calculated Property |
| Pvap | 6165.74 | kPa | 626.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ρl | [1092.94; 478.76] | kg/m3 | [213.15; 624.15] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A / B^(1 + (1 − T/C)^D) Y is ρl in kg/m3, T in K | |||
| Coefficient A | 8.31179e+01 | |||
| Coefficient B | 2.61060e-01 | |||
| Coefficient C | 6.26000e+02 | |||
| Coefficient D | 2.04590e-01 | |||
| Temperature range, min. | 213.15 | |||
| Temperature range, max. | 624.15 | |||
| ρl | 1092.94 | kg/m3 | 213.15 | Calculated Property |
| ρl | 1061.46 | kg/m3 | 258.82 | Calculated Property |
| ρl | 1027.75 | kg/m3 | 304.48 | Calculated Property |
| ρl | 991.25 | kg/m3 | 350.15 | Calculated Property |
| ρl | 951.16 | kg/m3 | 395.82 | Calculated Property |
| ρl | 906.21 | kg/m3 | 441.48 | Calculated Property |
| ρl | 854.19 | kg/m3 | 487.15 | Calculated Property |
| ρl | 790.63 | kg/m3 | 532.82 | Calculated Property |
| ρl | 703.28 | kg/m3 | 578.48 | Calculated Property |
| ρl | 478.76 | kg/m3 | 624.15 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| γ | [0.04; 0.00] | N/m | [213.15; 624.15] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is γ in N/m, T in K | |||
| Coefficient A | -4.17292e-02 | |||
| Coefficient B | 2.71421e+01 | |||
| Coefficient C | -2.52268e+00 | |||
| Coefficient D | 1.34846e-04 | |||
| Coefficient E | -1.90155e-06 | |||
| Temperature range, min. | 213.15 | |||
| Temperature range, max. | 624.15 | |||
| γ | 0.04 | N/m | 213.15 | Calculated Property |
| γ | 0.04 | N/m | 258.82 | Calculated Property |
| γ | 0.03 | N/m | 304.48 | Calculated Property |
| γ | 0.03 | N/m | 350.15 | Calculated Property |
| γ | 0.03 | N/m | 395.82 | Calculated Property |
| γ | 0.02 | N/m | 441.48 | Calculated Property |
| γ | 0.02 | N/m | 487.15 | Calculated Property |
| γ | 0.01 | N/m | 532.82 | Calculated Property |
| γ | 0.01 | N/m | 578.48 | Calculated Property |
| γ | 0.00 | N/m | 624.15 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λgas | [0.03; 0.08] | W/m×K | [460.75; 1000.00] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A·T^B / (1 + C/T + D/T²) Y is λgas in W/m×K, T in K | |||
| Coefficient A | 1.66600e-04 | |||
| Coefficient B | 9.76500e-01 | |||
| Coefficient C | 7.06000e+02 | |||
| Coefficient D | 0.00000e+00 | |||
| Temperature range, min. | 460.75 | |||
| Temperature range, max. | 1000.00 | |||
| λgas | 0.03 | W/m×K | 460.75 | Calculated Property |
| λgas | 0.03 | W/m×K | 520.67 | Calculated Property |
| λgas | 0.04 | W/m×K | 580.58 | Calculated Property |
| λgas | 0.04 | W/m×K | 640.50 | Calculated Property |
| λgas | 0.05 | W/m×K | 700.42 | Calculated Property |
| λgas | 0.06 | W/m×K | 760.33 | Calculated Property |
| λgas | 0.06 | W/m×K | 820.25 | Calculated Property |
| λgas | 0.07 | W/m×K | 880.17 | Calculated Property |
| λgas | 0.08 | W/m×K | 940.08 | Calculated Property |
| λgas | 0.08 | W/m×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λliquid | [0.20; 0.19] | W/m×K | [213.15; 460.75] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A + B·T + C·T² + D·T³ + E·T⁴ Y is λliquid in W/m×K, T in K | |||
| Coefficient A | 2.11000e-01 | |||
| Coefficient B | -3.70000e-05 | |||
| Coefficient C | 0.00000e+00 | |||
| Coefficient D | 0.00000e+00 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 213.15 | |||
| Temperature range, max. | 460.75 | |||
| λliquid | 0.20 | W/m×K | 213.15 | Calculated Property |
| λliquid | 0.20 | W/m×K | 240.66 | Calculated Property |
| λliquid | 0.20 | W/m×K | 268.17 | Calculated Property |
| λliquid | 0.20 | W/m×K | 295.68 | Calculated Property |
| λliquid | 0.20 | W/m×K | 323.19 | Calculated Property |
| λliquid | 0.20 | W/m×K | 350.71 | Calculated Property |
| λliquid | 0.20 | W/m×K | 378.22 | Calculated Property |
| λliquid | 0.20 | W/m×K | 405.73 | Calculated Property |
| λliquid | 0.19 | W/m×K | 433.24 | Calculated Property |
| λliquid | 0.19 | W/m×K | 460.75 | Calculated Property |
Similar Compounds
![2,3-Butanediol, [S-(R*,R*)]-.](data:image/png;base64,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)
![2,3-Butanediol, [R-(R*,R*)]-.](data:image/png;base64,iVBORw0KGgoAAAANSUhEUgAAAPoAAAD6CAIAAAAHjs1qAAAaiUlEQVR4nO3de1xUZf4H8A8XEUJAEUVFbF1EUTRCGEVA84airSaZa6bxM0mszUJQgjRBV5OQbMW0TVdbXS9LaXnZ1fWyyYaiQmJYgG6KhYIX1EGQO8PM74+ZHYnbzOjMec6Z5/t+9ccBzsjH+PB45sw537FQqVQghA+WrAMQIhyqO+EI1Z1whOpOOEJ1JxyhuhOOUN0JR6juhCNUd8IRqjvhCNWdcITqTjhCdSccoboTjlDdCUeo7oQjVHfCEao74QjVnXCE6k44QnUnHKG6E45Q3QlHqO6EI1R3whGqO+EI1Z1whOpOOEJ1JxyhuhOOUN0JR6juhCNUd8IRqjvhCNWdcITqTjhCdSccoboTjlDdCUeo7oQjVHfCEao74Yg46v7wIW7eRG0t6xzEzOlX9w0b4OEBDw+sXKl756lTNTufPt3ebpcvY+lS+PvD1haOjnBzg50dnJwQGor16/HggV7BCDGEtV57yeW4dg0A7t7VvfONG5qdq6tb3+HhQ8TEYPt2KBTNv1RRgWPHcOwYVq1CYiLeeUeveIToR7+6G9GdO5g8GRcuaD7s2hUhIejXD5064e5d5OYiIwMNDZDLERWFggJs2gQrK6FDEjMlbN0bGzF9uqbrdnZYvRoLF8LG5lf7lJQgJgZffgkAmzejVy8kJAgakpgvYZ+qfvQRMjMBwNYWR44gJqZ51wG4uSEtDYsWaT5ctQrffy9kRmLGBKx7XR0+/liznZiI0aPb3NPCAikp8PcHAIUCKSkCpCM8ELDuX3+N0lIA6NwZUVE6dra2RmKiZvurr/R6ikyILgLWPT1dszFtGuzsdO8fGopu3QCgvl5zCETIkxGw7mfPajaGD9drf2trzfEMgHPnTBKJmMz48eM/+ugjpVLJOsivGHhmprQU332nY5+2TrcXFWk2Bg7U99sNGoR//etXjyVScODAgaysrIyMjN27dyclJYWGhrJOpGFg3ffuxd69j/N9FApUVmq2O3fW91Fdumg25PLH+aaEkZSUlMrKSgC5ubmzZ8/28fHZunXrb3/7W9a5BDuYqa6GSqXZtrXV91H29pqNqirjRyKmkZ6enp+fr/1QLpenp6ePGTMmMjKyUrvkMWLg6h4SgvBwHfu8/34rxx6dOsHSEuojubaOdlqqqNBsODnpn5GwtWLFivLy8mafvH79+tatW0+dOrVgwYKoqCgLCwsm2Qyse//+mDNHxz7r1rVSd0tLODhA/X+hrEzfb6fdU//jH8JUVlbWjz/+2OqXVCrV5cuX33vvvbS0tOTk5Oeee07gbBD0zIz20K2gQN+HaP9N7NfP+HmICSQkJJS1u5zV1tZmZWXNnj37xo0bgqXSErDuAQGajawsvfZvaEBOTvPHEhHLy8vLzc3VuZuVldWLL77o7u5u+kTNCVj3sWM1GwcP6nX4fvSo5oSMnR0CA00YjBhJXFxcqfqF83YNHTp03bp1AuRpScC6v/AC3NwA4OFDrF+vY2elEklJmu3Zs+mpqvhdvXr1ez0u5uvVq9dnn33WoUMHASK1JGDdO3R4dJ3j6tU67nVKTNS8CtuxI6KjTR2NPLm4uLhbt261v0+HDh3Cw8OHDh0qTKSWhL0AODpac1hSU4PQUGzZgpYvMsvliIzE6tWaD1euxKBBgoYkhisuLs7Ozta5m0wmW639ybIg7O0dVlbYtw+hofjhB1RVYcECrFmD55+Hpyfs7SGXIycHR4/i4UPN/m+8gdhYQROSxxIbG1tcXNz+Pu7u7tu2bbNiem+a4Dfv9eyJjAy89Rb27IFKhaIifPppK7s5OWHlSt3XCRMRKC0tPau9/q8Ntra2CxYs8PLyEiZSW/Sre9eu8PQEgO7dde/89NOa1/y1lwA04+SEXbsQE4Nt23D0qOY+bjUrK8hkmDwZb74JFxe9shHW4uPji3RdwxcQELB06VJh8rTDQqW9lIWVqiqUlqKiAi4u6Natldv5iIiVl5f7+fkVFha2s0/fvn3T09OffvppwVK1RfCDmZbs7dG3L+sQ5DEtW7as/a7b29tHRUWJoesQyxSxdty9i82bWYcgrauqqjpx4kT7+wQHB0eJ5jmYCFb3dtTVwdcXJSUYMKC9W7kJIytWrLhy5Uo7O/Tr12/Hjh2C5dFJ3Kt7x4544w0AWLiwlZFjhKna2trDhw+389zP0dExPj7e1dVVyFTtE3fdASxZgr59kZ+PbdtYRyG/snbt2p9++qmdHcaOHRsRESFYHn2I4MyMTvv2YcYMODvjyhU4O7NOQwCgoaHBz8+vrUvbAXh5eWVmZjqL7Ocl+tUdwEsvYfRoyOVg+vozaSo1NfXy5cttfbVLly4rVqwQW9chjdUdwMWL8PODhQVyc+HtzToN7xobG/39/du5tH3WrFl79uwRMJG+pLC6A/DxweuvQ6F4dE0lYWfLli2XLl1q66tDhgzZLNZzxxJZ3QHI5fD0hFyOw4cxeTLrNPxSqVQymSxHe6PZr7m4uOzYsWOyWH9AElndATg74/33ASAqCnV1rNPwa9euXQVt3G1saWk5depU0XYdUlrdASgUePZZ5Odj3TrExLBOw6lhw4Z918YkOV9f38zMTDt9BoAyIp3VHYC1Nf70JwBYuRK3b7NOw6MDBw60ddTu6uq6YcMGMXcdEqs7gJAQTJ6MiopH47CJgLTT8JqxsrL6/e9/HxwcLHwkg0jqYEbt6lUMHoyGBmRlPRoRTEwvPT09LCys5YQwADKZLDMzk9UN1/qT2uoOoF8/vPUWlEosWgTJ/a5KWavT8MB6uIBBJFh3AImJ6NEDmZnYt491FF60NQ2P+XABg0jwYEZt82a88Qbc3XH5Mp56inUa8zdhwoRWL20PDAzMyMhge8O1/qS5ugOYPx9+frhxA4zmUXElLy/v4sWLLT8vhuECBpFs3S0tkZoKCwskJeH6ddZpzFyr0/BEMlzAIJKtO4CgILz0EmpqIIJb3M1YW9PwRDJcwCCSPXZXu3EDXl6oqUFGBkR/0leipk+f/vXXXzf7pHiGCxhEyqs7AHd3xMRApUJUVCvz98gTa3UanqiGCxhGJXVVVao+fVSA6q9/ZR3FDL388sstOzNx4kTWuR6TxFd3AE89hQ8+AID4+Efv5USModVpeGIbLmAQ6dcdwOzZCA7GnTuPRsITY2g5DU+EwwUMIvGnqloXLkAmg7U18vI04yzJk2l1Gt60adP279/PKtKTM4vVHcDQoQgPR3093n2XdRQz0XIanpeX1zaJjz8xl7oDWLMGDg44cKD+5EnWUSSv5TQ80Q4XMIgZ1b1nz5oVK3aMHDk8OlpBI8eeTMtpeKGhoTNnzmSVx2hYnxoyprq6Ok9PTwAbN25knUXCampqBg4c2LQkQ4YMqaioYJ3LCMxodQdsbGySk5MBLF++/P79+6zjSFWzaXguLi4ffvihg4MDw0jGYlZ1BxAWFjZhwoSysrKVK1eyziJJDQ0N+/bta2xsVH8o/uEChmH9z4vx5efnW1tbW1tb//DDD6yzSE9KSkrT+5J8fX2rq6tZhzIac1vdAQwaNCgyMlKhUETTG7IaqLGxcffu3Q0NDeoPJTFcwCBmWHcAq1at6tq16zfffHPo0CHWWaSk6TQ8qQwXMAzrf15MJTU1FYCHh0dtbS3rLNKgVCr9/Py0xZDJZPX19axDGZl5ru4A/vCHPwwZMqSwsFDde6JT02l4EhouYBjWv28m9O9//xuAg4PDzZs3WWeRAJlMpq5Ehw4d4uPjWccxCXOuu0qlmjJlCoCIiAjWQcRu//79nTp1Utc9MDBQoVCwTmQS5nJFZBsKCwu9vb0bGhrOnTunXb1IS0FBQWfOnAHg7u5+/Phxad1wrT+zPXZX8/DweOedd5RKZVRUlHn/Yj+J9PT0/Px8SHO4gGEY/+tiehUVFT179gSwZ88e1llEatSoUeoyjB49WqlUso5jQma+ugNwcHBYtWoVgHfffbeqqop1HNHRTsPr27fv9u3bLSwsWCcyIfOvO4DXXntNJpMVFxenpKSwziI6y5cvLysrk/BwAUOY+VNVrTNnzgQHB9va2l66dMnsf6j6y8vLGzduXGlp6cSJE48ePco6jslxsboDCAwMnDlzZk1NTXx8POssIqKehifp4QIG4aXuAFJSUuzt7dPS0jIyMlhnEQX1NDypDxcwCEd1792795IlSwAsWrRISSPHgLi4uFu3bo0dOzYiIoJ1FoHwcuyupr4traioaOvWrfz8jFtVXFw8YsSITp06ZWZmSv2Ga/1xtLoDsLOzS0pKArB06dJW33eFH7GxsZWVlWYwXMAgfNUdwKxZs0aNGlVaWvqBetQel0pLS0+dOjVp0iRzGC5gCL4OZtS+//57f39/a2vrH3/8sX///qzjMDBv3rzTp0/n5OSYxw3X+uNudQfg6+v72muv1dfXq5+58qasrOyrr75KTU3lrevgc3UHUFpa2r9///Ly8iNHjkyaNIl1HEFFRkaWl5d/8cUXrIMwwGndASQlJS1dutTW1lb7Zlrdu3d3cXFhncv4ysvLS0pK1NsdOnRYvnz5+fPnzemGa/3xW/fKykpnZ2ftXff8GDRokPpyXw7xW3cAb775ZlpaWl1dnfpDZ2fnLl26sI1kCpWVlXfu3AGgUqlqa2sB7N+/f9q0aYxjscBv3e/duyeTyQoKCrj6Z/13v/vd4cOH/fz8srOzLS25O1HB3V9Ya8qUKdOnT+eq6wDS0tJ69eqVk5Oze/du1llYYHZjCVMbN250cXF5+PAh6yAMbN++HUCPHj3Ky8tZZxEaj6t7SUlJcnLyrFmztPfecyU8PHz48OG3b99eu3Yt6yxC4/HYfcyYMb/88suFCxfM8ompPs6dOxcYGGhjY5OXl9evXz/WcYTD3eqenJyclZUVEhLCbdcBBAQEzJ49u66u7r333mOdRVB8re7Xrl0bP358Y2Pjd9991717d9ZxWCopKfHy8qqsrDx+/HhISAjrOALhaHVXKpVz5sz5+eefn3vuOc67DsDNzS0uLg5ANFdvZcX6ubJwli1bZmNj4+bm9ssvv7DOIgo1NTV9+/YF8Oc//5l1FoHwsrrn5+fv3Lmzvr4+MDCQJhGo2draqk/OLFu2TC6Xs44jCNa/b0JoaGjw9/cH4Orq+t///pd1HHEZPXo0gOjoaNZBhMDF6r5kyZLc3FwAw4YN4/N+jnZs3LjR2tr6k08+4eG6MfOve3Z29t69exUKhYuLi3p6HmnK29s7IiJCoVAsWrSIdRaTM/MTkXV1dQEBAeqlfdKkSUeOHGGdSIzkcrmnp6dcLj98+LD5vKdka8x8dV+4cKF63qezs3NCQgLrOCLl7Oz8/vvvA4iKitJeDm2WzLnuJ0+ePHTokPodcX19fQMCAlgnEq+3337b29v76tWrmzZtYp3FlFg/VzaVqqoqb29v9d/RycnpxIkTrBOJ3fHjxwE4OjreunWLdRZTMdvVff78+dr3kfPx8Rk/fjzbPOIXEhIyefLkioqKxMRE1llMhvXvm0kcPHiwa9eu6r+gvb39wYMHWSeShitXrnTs2NHS0vL8+fOss5iEGdb9wYMHTd9daMSIEawTSUl0dDSAoKAgs3zXGjOse1hYmLbrtra2u3btYp1ISsrLy3v06AHgyy+/ZJ3F+Myt7jt37uzcubO27v7+/ma5SpnUZ599BsDd3b2qqop1FiMzq6eq9+7d++CDDx48eKD+0MbG5vXXXzfv99Yyhfnz5/v5+d24cePjjz9mncXIzOpV1dDQ0GPHjmk/9PHxycnJUU8IIwbJzMwcOXKknZ3dpUuX+vTpwzqO0ZjP6r5p06bMzEzth9bW1uHh4dT1xxMUFDR9+vTq6uply5axzmJMZrK6l5SUjBkz5sqVK9rPDBky5Pz58zY2NgxTSdqNGze8vLxqamoyMjKCg4NZxzEOM1nd58yZ07TrVlZWL730EnX9Sbi7u8cvWZI2duzwhASYzVtZsX6ubARJSUnNhoENGjSourqadS7pq6pS9emjAlTbt7OOYhySX92vXbu2ZcuWmpoa7WcsLCymTp3K2zQ8k3jqKajf0icuDhUVrNMYgbSP3ZVKZXBw8NmzZ5t+csCAAefPn+dzQpjxqVQYNQqnT+O997BmDes0T0raq3tCQkJOTk6zT4aGhlLXjcbCAuvXw9IS69ahybMjqWJ9NPX48vLyWp4S9vDwKCsrYx3N7Pzf/6kAVVgY6xxPSqqru0KhmDt37vXr15t9fuzYsU0vIiDGkZwMR0fs34/jx1lHeSJSrfvixYvVd6A21adPn9WrV7OIY+5cXREfDwDR0ZDyyDFJ1j07O3vfvn0tR73RNDwTWrwYnp4oKMCWLayjPD7pnZmpq6sbPnz4xYsXm33ezc3t3LlzvXv3ZpKKC19/jenT4eyMn37C/+6ekRbpre4LFy7My8tr+fnAwEDqumm9+CImTIBcjj/+kXWUxySx1f3kyZOzZs0qLS1t9nlXV9eMjAyaEGZyBQXw8QGACxcwZAjrNAaT0upeXV0dFRXVsusAhg8fTl0XwqBBiIyEQoHoaNZRHoeUVvdXXnklLS2tZWAXF5dvvvnmmWeeYZKKO3I5+vfH/fs4dAhTprBOYxjJrO4HDx48fvx4q7+cMpmMui4cZ2eo57FFR0NyI8eYvsilr2bDBZpydnY+e/Ys64CcaWhQDR6sAlRr17KOYhhprO5z5869fPlyq18aOnQoTcMTmrU11q8HgFWrcOsW4zCGkEDdd+7c+Z///KfVLzk5OcWrX+0jAhs3DlOm4OFDLF/OOooBxP5U9d69eyNHjmxraR81atS3334rcCSiUVgIb280NODcOchkrNPoReyr+5w5c9rqur29/eLFiwXOQx7x8MA770CpRFQUxL1oaom67s2GCzTzzDPPTJ06Vcg8pLnly9GzJ86exRdfsI6iF/HWvaSkZP369ZWVla1+1dbWduHChQJHIs05OGguKIiNRVUV6zS6ibTuKpVq9uzZV69ebWuHwYMHz5o1S8hIpHXz5kEmQ3ExUlJYR9FNpHX/8MMPs7Oz2/qqjY3N/PnzaRqeKFhaYv16WFhg7VoUFbFOo4MY615YWPiXv/yl6XCBZgYOHBgRESFkJNKewEDMnImaGoj+pLDo6q5UKl999dWff/65rR1oGp4YpaTA3h5pacjIYB2lPaKr+/Lly1sOF2hq4MCB9CRVdHr3xpIlALBokZhHjomr7vn5+bt27aqvr29rBysrqxkzZtA0PDF69124uyM3V8wLvIheVVUoFAEBATqX9pycHJoQJlInTsDREcOHs87RJmvWAR5ZvHhxyztQm7KwsHjhhReo6+IVEsI6gQ5iWd2zs7PDwsJu3rzZzj79+/fPycmhCWESU1eH+/dx7x5sbdGtG7p0YZhFFMfudXV1kZGR7XcdwKRJk6jrkiGXY80aBAejUye4ucHHBwMGwNkZPXrg1Vdx9GibDzx5Eo6OcHTEyJG6v0tsrGbnpCS9UrG93F4tIiJC54lFmoYnJampqs6dVUB7/40apSosbOWxx45pdnj2Wd3f6K23NDsnJuqTi/2x+8mTJ//5z382Nja2v9u4ceNoGp4EqFSIisInn2g+tLfHhAkYNgxdu6K2FkVFOHIEly4BQEYGAgNx5AiGDhUyHktVVVVD9Jjf0KdPnzt37rCNSvSSmvpo/Q4PV7X6U/vqK1X37pp9evdW3b//q6+acnVnfOweGRnZ6oykZmganjQUFiIuTrMdE4MdO9DqT+3FF/Htt3BxAYDiYiFneLCs+8GDB48eParSdWrIzc1tjfQH6XNhwwbU1gKAry+Sk9vb08sLGzZotvfsQXGxybMBYFj38vLypUuX3r9/X+eeQUFBNA1PAurrsWOHZjs2Fta6nha+/DLUk7AUCnz+uWmz/Q+zus+bN6+goEDnbq6urqtWrRIgD3lSubkoLweAjh0xbZru/S0s8Mormm2hrjtgU/fKysrbt2/r8/ooTcOTjHPnNBuDB0PPV76HDdNsZGcLc2EZmxORnTp1yszM/Nvf/paSklJQUKBs46/arVs3WtolQ3v8PWCAvg/Rjsp6+BDl5c1fcK2owJEjOv4EA28oYXnePTw8fMaMGQkJCXv37i1qLbefnx9Nw5OMsjLNhpOTvg9p+kJKWVnzul+7huefN0KwJhifiLSzs0tJSTl9+vS0adNc1Gem/sfZ2TkxMZFVMGIw7d1nHTvq+5CmxzzV1UbO0xr2r6oC6N279/79+0+dOhUbG5ubm1tXVweahic5jo6aDf1HEjR9a+KWL5l7eGDTJh1/wqef4tAhfb+dSOquNnLkyDNnzqSmpn7++edFRUXLli1jnYgYQttXuVzfhzTds2XdHRwwcaKOP+Ef/9D3ewFgfjDTjKWlZXR0dGZmZkJCwujRo1nHIYbw9NRs6PEyucYPP2g2evWCINe6iqvuao6OjkvUNz4SCdEeeV65gnv39HrI2bOajREjTBKpBTHWnUiSlxfUb2KuVCItTff+DQ34+9812zoPWoyE6k6MxMICkZGa7aQkzSus7diwAXfuAEDnzo9eXjUxqjsxngUL0K0bANy8ifnz23t/7cxMaM8yx8TA3l6IeFR3YkwuLti8WbO9dy8mTkTLYeUKBTZuRGio5nylv7+Qs8dEdCKSmIOwMGzYoBmudPIkvL0hk2HECHTrhtpaFBbixAncvavZ2ccHBw+iQwfB0lHdibG9/TZ+8xssWoRr16BUIisLWVnN97Gywty5WLfOgCsOjIHqTkxgyhRMnIg9e3DkCDIyNE9JAXTsiIEDERqKOXPg7d36Y7t0QVAQAOhzJayHh2Zn9UkhXcQyZ4aYs4YG3LsHe/tHFxowQnUnHKEzM4QjVHfCEao74QjVnXCE6k44QnUnHKG6E45Q3QlHqO6EI1R3whGqO+EI1Z1whOpOOEJ1JxyhuhOOUN0JR6juhCNUd8IRqjvhCNWdcITqTjhCdSccoboTjlDdCUeo7oQjVHfCEao74QjVnXCE6k44QnUnHKG6E45Q3QlHqO6EI1R3whGqO+EI1Z1whOpOOEJ1JxyhuhOOUN0JR6juhCNUd8KR/wdqmxvVwH9WDgAAAABJRU5ErkJggg==)
Find more compounds similar to Propylene Glycol.
Mixtures
- Magnesium chloride + Propylene Glycol + Water
- Propylene Glycol + Water
- Propylene Glycol + Lithium chloride + Water
- lithium bromide + Propylene Glycol + Water
- Propylene Glycol + Carbon dioxide
- Propylene Glycol + sodium iodide + Methyl Alcohol
- Propylene Glycol + Methyl Alcohol
- Propylene Glycol + Methane
- Propylene Glycol + sodium chloride + Water
- Propylene Glycol + Propylamine
- Propylene Glycol + 2-Propanamine
- Propylene Glycol + Formamide
- Propylene Glycol + Butyl lactate
- Propylene Glycol + Threonine + Water
- Propylene Glycol + 1,2-Ethanediol
- 1,3-Propanediol + Propylene Glycol
- Propylene Glycol + Water + daidzein
- Propylene Glycol + daidzein
- 1-Propanol + Propylene Glycol
- Propylene Glycol + 1-Hexanol
Find more mixtures with Propylene Glycol.
Sources
- KDB Vapor Pressure Data
- Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) ChEDL chemicals 1.5.2, from Bradley, J.-C.; Williams, A.; Lang, A. Jean-Claude Bradley Open Melting Point Dataset. Figshare, 2014 (CC0).
- IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 ChEDL chemicals 1.5.2, from Kudchadker, A. P.; Ambrose, D.; Tsonopoulos, C. Vapor-Liquid Critical Properties of Elements and Compounds. 7. Oxygen Compounds Other Than Alkanols and Cycloalkanols. J. Chem. Eng. Data 2001, 46, 457-479.
- PSRK revision IV (2005), critical constants and acentric factors of 1000 components ChEDL chemicals 1.5.2, from Horstmann, S.; Jabłoniec, A.; Krafczyk, J.; Fischer, K.; Gmehling, J. PSRK Group Contribution Equation of State: Comprehensive Revision and Extension IV, Including Critical Constants and α-Function Parameters for 1000 Components. Fluid Phase Equilib. 2005, 227, 157-164.
- Cheméo Relay (1.0)
- ChemSep v8.3 pure component data Converted from ChemSep v8.3 pure component data, H. Kooijman and R. Taylor (2021, 2022), Artistic License 2.0; see how the values differ.
- Crippen Method
- Vapor liquid equilibrium in systems (water + organic solvent + salt) at low water concentrations but high ratios of salt to water: experimental results and modeling
- Thermodynamic study of the solubility of ibuprofen and naproxen in some ethanol + propylene glycol mixtures
- Methane and carbon dioxide solubility in 1,2-propylene glycol at temperatures ranging from 303 to 423 K and pressures up to 12 MPa
- Thermodynamic analysis of the solubility of ketoprofen in some propylene glycol + water cosolvent mixtures
- Thermodynamic studies of fluphenazine decanoate solubility in propylene glycol + water mixtures and correlation with the Jouyban Acree model
- Solution thermodynamics of indomethacin in propylene glycol + water mixtures
- Liquid phase behavior of hexafluorophosphate ionic liquids with polyhydric alcohols
- Solubility of sulfamethizole in some propylene glycol + water mixtures at several temperatures
- Solubility of sulfapyridine in propylene glycol + water mixtures and correlation with the Jouyban Acree model
- Excess volumes and excess heat capacities for alkanediol + water systems in the temperature interval (283.15-313.15) K
- Measurement and correlation of the solubility of florfenicol in binary 1,2-propanediol + water mixtures from 293.15 K to 316.25 K
- Solubility of daidzein in propylene glycol plus water cosolvent mixtures
- Volumetric and viscometric behavior of the binary systems ethyl lactate + 1,2- propanediol, + 1,3-propanediol, + tetrahydrofuran and + tetraethylene glycol dimethyl ether. New UNIFAC-VISCO and ASOG-VISCO parameters determination
- Phase behavior of imidazolium and phosphonium tetrafluoroborates with dihydroxy alcohols
- tert-Butyl chloride as a probe of the solvophobic effects
- Vapor-liquid equilibrium for propylene glycols binary systems: Experimental data and regression
- Liquid-liquid equilibrium data for binary systems containing o-dichlorobenzene and nitrobenzene
- Densities, surface tensions, and isobaric vapor-liquid equilibria for the mixtures of 2-propanol, water, and 1,2-propanediol
- Excess volumes and excess heat capacities of {1,2- alkanediol + methanol} mixtures and ionic volumes in these systems
- Volumetric, ultrasonic and spectroscopic (FT-IR) studies for the binary mixtures of imidazolium based ILs with 1,2-propanediol
- Density and viscosity of propylene glycol at high temperatures and high pressures
- Solubility evaluation and thermodynamic modeling of beta-lapachone in water and ten organic solvents at different temperatures
- Measurement and correlation of excess molar enthalpy for(1,2-propanediol, or 1,3-propanediol, or 1,4-butanediol + water) at the temperatures (298.15, 323.15, and 343.15) K
- Partial molar volumes of organic solutes in water. XIV. Polyhydric alcohols derived from ethane and propane at temperatures T = 298 K to T = 573 K and at pressures up to 30 MPa
- Densities and derived thermodynamic properties of (2-methoxyethanol + 1-propanol, or 2-propanol, or 1,2-propandiol) at temperatures from T = (293.15 to 343.15) K
- Densities and volumetric properties of (formamide + ethanol, or 1-propanol, or 1,2-ethanediol, or 1,2-propanediol) mixtures at temperatures between 293.15 K and 318.15 K
- Volumetric and compressibility properties of liquid water as a solute in glycolic, propylene carbonate, and tetramethylurea solutions at T = 298.15 K
- Excess molar volume and viscosity deviation for binary mixtures of polyethylene glycol dimethyl ether 250 with 1,2-alkanediols (C3 C6) at T = (293.15 to 323.15) K
- Vapour pressures, densities, and viscosities of the aqueous solutions containing (triethylene glycol or propylene glycol) and (LiCl or LiBr)
- Experimental study of the excess molar volume of ternary mixtures containing {water + (1,2-propanediol, or 1,3-propanediol, or 1,2-butanediol, or 1,3-butanediol, or 1,4-butanediol, or 2,3-butanediol) + electrolytes} at a temperature of 298.15 K and atmospheric pressure
- Molar heat capacities of some aqueous 2-amino-2-hydroxymethyl-1,3-propanediol + glycol systems
- (Liquid + liquid) equilibrium data for the system (propylene glycol + water + tetraoctyl ammonium 2-methyl-1-naphthoate)
- Phase diagrams for (water + 1, 2-butanediol or 1, 2-propanediol + 2-ethyl-1-hexanol) systems: Experimental data and UNIQUAC
- Experimental determination and modeling of excess molar volumes, viscosities and refractive indices of the binary systems (pyridine + 1-propanol, + 1,2-propanediol, + 1,3-propanediol, and + glycerol). New UNIFAC-VISCO parameters determination
- Densities, viscosities, and refractive indices of the binary systems (PEG200 + 1,2-propanediol, +1,3-propanediol) and (PEG400 + 1,2-propanediol, +1,3-propanediol) at (288.15 to 333.15) K and atmospheric pressure: Measurements and modeling
- PqT measurements and derived properties of liquid 1,2-alkanediols
- Volume effects for binary mixtures of propane-1,2-diol with methanol, propan-1-ol, hexan-1-ol, octan-1-ol, or nonan-1-ol at temperatures (293.15 to 318.15) K
- Thermophysical characterization of aqueous ternary system containing n-tris-[hydroxymethyl]methyl-3-amino propanesulfonic acid and glycol (PG or DPG or TPG)
- Isobaric specific heat capacity of typical lithium chloride liquid desiccants using scanning calorimetry
- Thermodynamics and activity coefficients at infinite dilution for organic solutes, water and diols in the ionic liquid choline bis(trifluoromethylsulfonyl)imide
- Thermodynamics of solvation in propylene glycol and methyl cellosolve
- Density and vapour pressure of mixed-solvent desiccant systems (propylene glycol or dipropylene glycol or tripropylene glycol + magnesium chloride + water)
- Thermal conductivity of dry anatase and rutile nano-powders and ethylene and propylene glycol-based TiO2 nanofluids
- Liquid extraction of polyhydric alcohols from water using [A336][SCN] as a solvent
- Solubility of rosuvastatin calcium in different neat solvents at different temperatures
- Excess properties and isobaric (vapor + liquid) equilibrium at sub-atmospheric pressures of binary (1,2-propanediol + 1,3-propanediol) system: Measurement and modelling
- Equilibrium solubility of sodium 2,4-diaminobenzene sulfonate in liquid mixtures (methanol + water, isopropanol + water, and 1,2-propanediol + water) from 273.15 K to 323.15 K
- Solubility and thermodynamic function of a bioactive compound bergenin in various pharmaceutically acceptable neat solvents at different temperatures
- Speed of sound in saturated aliphatic alcohols (propan-2-ol, butan-2-ol, and 2-methylpropan-1-ol) and alkanediols (ethane-1,2-diol, propane-1,2- and -1,3-diol) at temperature between 253.15 K and 353.15 K and pressures up to 30 MPa
- Thermodynamic and spectroscopic interpretation of molecular interactions of nicotine + alcohol binary mixtures
- Determination and correlation of solubility and thermodynamics of mixing of 4-aminobutyric acid in mono-solvents and binary solvent mixtures
- Densities, ultrasonic speeds, excess and partial molar properties of binary mixtures of 2-pyrrolidone with isomeric propanediols at temperatures from 303.15 K to 323.15 K
- Thermodynamic and transport properties of acetonitrile + alkanediols liquid mixtures at different temperatures, experimental measurements and modeling
- Equilibrium solubility, dissolution thermodynamics and preferential solvation of adenosine in aqueous solutions of N,N-dimethylformamide, N-methyl-2-pyrrolidone, dimethylsulfoxide and propylene glycol
- Potential heat transfer enhancement of functionalized graphene nanoplatelet dispersions in a propylene glycol-water mixture. Thermophysical profile
- Solubility modelling and preferential solvation of adenine in solvent mixtures of (N,N-dimethylformamide, N-methyl pyrrolidone, propylene glycol and dimethyl sulfoxide) plus water
- Measurement and correlation of the (p, rho, T) behavior of liquid propylene glycol at temperatures from (272.7 to 393.0) K and pressures up to 91.4 MPa
- Thermodynamic solubility modeling, solvent effect and preferential solvation of curcumin in aqueous co-solvent mixtures of ethanol, n-propanol, isopropanol and propylene glycol
- Solubility of CO2 in methanol, ethanol, 1,2-propanediol and glycerol from 283.15 K to 373.15 K and up to 6.0 MPa
- Enthalpies of solution of l-threonine in aqueous alcohol solutions
- Excess enthalpies of binary mixtures of some propylamines + some propanols at 298.15K
- Enthalpies of dilution of formamide in aqueous alcohol solutions at 298.15K
- Heat capacities of the mixed-solvents desiccants (glycols +water + salts)
- DSC determination of partial ternary phase diagrams of methanol/sodium chloride/water and propylene glycol/sodium chloride/water and their applications for synthesized diagrams
- Heat Capacity of Several Mixed-Solvent Desiccants Containing Glycol + Water + MgCl2
- Molar heat capacity of several aqueous solutions of n-[tris(hydroxymethyl)methyl-3-amino]- propanesulfonic acid (TAPS) + glycol
- Thermodynamic study on some alkanediol solutions: measurement and molecular modeling
- Experimental measurements and modelling of volumetric properties, refractive index and viscosity of selected binary systems with butyl lactate at 288.15 to 323.15 K and atmospheric pressure. New UNIFAC-VISCO interaction parameters.
- Calorimetric study of solvation of low polar solutes in propylene glycol and methyl cellosolve at 298 K
- Solubility and dissolution thermodynamics of N-(4-chlorophenyl)-2-(pyridin-4-ylcarbonyl)hydrazinecarbothioamide in PG + water cosolvent mixtures at (298.15 to 338.15) K
- Isobaric Vapor Liquid Equilibria for Binary Systems of Diethyl Carbonate + Propylene Carbonate, Diethyl Carbonate + Propylene Glycol, and Ethanol + Propylene Carbonate at 101.3 kPa
- Solubility and Saturation Apparent Volume of Propranolol Hydrochloride in Some Binary Aqueous Cosolvent Mixtures at 298.15 K
- Solubility and Thermodynamic Analysis of Tenoxicam in Different Pure Solvents at Different Temperatures
- Solubility of Hydrogen Sulfide in Ethanediol, 1,2-Propanediol, 1-Propanol, and 2-Propanol: Experimental Measurement and Modeling
- Apparent Molar Volumes and Isentropic Compressibilities of Tetraalkylammonium Bromides in Aqueous Propane-1,2-diol. An Attempt to Design Hydraulic Liquids
- Densities and Viscosities for Binary Liquid Mixtures of Butan-1-ol + Propane-1,2-diol, + Butane-1,2-diol and 2-Methylpropan-1-ol + Propane-1,2-diol, + Butane-1,2-diol from 298.15 to 333.15 K at 0.1 MPa
- Solubility of Etoricoxib in Aqueous Solutions of Glycerin, Methanol, Polyethylene Glycols 200, 400, 600, and Propylene Glycol at 298.2 K
- Solubility and Modeling of Hesperidin in Cosolvent Mixtures of Ethanol, Isopropanol, Propylene Glycol, and n-Propanol + Water
- Density of Working Liquids for Diffusion Vacuum Pumps
- Viscosities, Densities, and Refractive Indices of Aqueous Propane-1,3-diol
- Thermophysical Properties of Ternary Systems Potassium Formate + Propylene Glycol/Glycerol + Water
- Solubility Determination and Modeling for Artesunate in Binary Solvent Mixtures of Methanol, Ethanol, Isopropanol, and Propylene Glycol + Water
- Experimental Solubility and Density Functional Theory Studies of Deferasirox in Binary Solvent Mixtures: Performance of Polarizable Continuum Model and Jouyban-Acree Model
- Measurement and Correlation of the Solubility of Palmatine Chloride in Four Different Binary Solvent Systems at (283.15-328.15) K
- Phase Equilibrium Involving Xylose, Water, and Ethylene Glycol or 1,2-Propylene Glycol at Different Temperatures
- Solubility of Bifonazole in Four Binary Solvent Mixtures: Experimental Measurement and Thermodynamic Modeling
- Excess Molar Enthalpies of Binary Mixtures Containing Glycols or Polyglycols + Dimethyl Sulfoxide at 308.15 K
- Densities, Excess Molar Volumes, Viscosities, Speeds of Sound, Excess Isentropic Compressibilities, and Relative Permittivities for Alkyl (Methyl, Ethyl, Butyl, and Isoamyl) Acetates + Glycols at Different Temperatures
- Densities, Dynamic Viscosities, Speeds of Sound, and Relative Permittivities for Water + Alkanediols (Propane-1,2- and -1,3-diol and Butane-1,2-, -1,3-, -1,4-, and -2,3-Diol) at Different Temperatures
- Vapor-Liquid Equilibrium for Propylene Glycol + 2-(2-Hexyloxyethoxy)ethanol and 1-Methyl-2-pyrrolidone + 1-Methoxypropan-2-ol
- Excess Molar Enthalpies and Hydrogen Bonding in Binary Mixtures Containing Glycols or Poly(Ethylene Glycols) and 2-Phenylethyl Alcohol at 308.15 K and Atmospheric Pressure
- Density, Viscosity and Thermal Conductivity of Aqueous Solutions of Propylene Glycol, Dipropylene Glycol, and Tripropylene Glycol between 290 K and 460 K
- Solubility of Valdecoxib in the Presence of Glycerol, Propylene Glycol, and Poly(ethylene glycol) 400 at (298.15, 303.15, and 308.15) K
- Static Relative Permittivities of Water + Propane-1,2-diol and Water + Propane-1,3-diol under Pressures up to 300 MPa at 298.15 K
- Solubility of Rofecoxib in the Presence of Aqueous Solutions of Glycerol, Propylene Glycol, Ethanol, Span 20, Tween 80, and Sodium Lauryl Sulfate at (298.15, 303.15, and 308.15) K
- Excess Molar Enthalpies of 1,2-Propanediol + Alkan-1-ols (C1-C6) and Their Correlations at 298.15 K and Ambient Pressure (81.5 kPa)
- Solubility of 1H-1,2,4-Triazole in Ethanol, 1-Propanol, 2-Propanol, 1,2-Propanediol, Ethyl Formate, Methyl Acetate, Ethyl Acetate, and Butyl Acetate at (283 to 363) K
- Densities and Excess Molar Volumes for Binary Glycerol + 1-Propanol, + 2-Propanol, + 1,2-Propanediol, and + 1,3-Propanediol Mixtures at Different Temperatures
- Phase Equilibrium and Physical Properties for the Purification of Propylene Carbonate (PC) and y-Butyrolactone (GBL)
- Solubility of Dimethyl Fumarate in Methanol, Ethanol, 1-Propanol, 2-Propanol, 1,2-Propanediol, and Water from (289.95 to 347.15) K
- Solubility of CO2 in Alcohols, Glycols, Ethers, and Ketones at High Pressures from (288.15 to 318.15) K
- Solubility of Phenothiazine in Water, Ethanol, and Propylene Glycol at (298.2 to 338.2) K and Their Binary and Ternary Mixtures at 298.2 K
- Partial Molar Volumes and Partial Molar Isentropic Compressions of Three Polyhydric Alcohols Derived from Propane at Infinite Dilution in Water at Temperatures T = (278 to 318) K and Atmospheric Pressure
- Solubility of 3-Ethyl-5-methyl-(4RS)-2-((2-aminoethoxy)methyl)-4-(2-chlorophenyl)-1,4-dihydro-6-methyl-3,5-pyridinedicarboxylate Monobenzenesulfonate (Amlodipine Besylate) in Ethanol + Water and Propane-1,2-diol + Water Mixtures at Various Temperatures
- Solubility of Clonazepam and Diazepam in Polyethylene Glycol 200, Propylene Glycol, N-Methyl Pyrrolidone, Ethanol, and Water at (298.2 to 318.2) K and in Binary and Ternary Mixtures of Polyethylene Glycol 200, Propylene Glycol, and Water at 298.2 K
- Solubility, Density, Refractive Index, and Viscosity for the Polyhydric Alcohol + CsBr + H2O Ternary Systems at Different Temperatures
- Solid Liquid Equilibria of 1-Ethyl-3-methylimidazolium Hexafluorophosphate + Polyols
- Isobaric Vapor Liquid Equilibria for the Binary Mixtures Composed of Ethylene Glycol, 1,2-Propylene Glycol, 1,2-Butanediol, and 1,3-Butanediol at 10.00 kPa
- Vapor Liquid Equilibrium for Ternary and Binary Mixtures of Tetrahydrofuran, Cyclohexane, and 1,2-Propanediol at 101.3 kPa
- Heat Capacities of Four Promising Alternatives to Lithium Bromide Aqueous Solution in Absorption Refrigerators
- Solubilities of Carbon Dioxide in Eutectic Mixtures of Choline Chloride and Dihydric Alcohols
- Vapor Liquid Equilibria for Water + Propylene Glycols Binary Systems: Experimental Data and Regression
- Measurement and Correlation of Tadalafil Solubility in Five Pure Solvents at (298.15 to 333.15) K
- Solubility of Metoclopramide Hydrochloride in Six Green Solvents at (298.15 to 338.15) K
- Solubility of Bioactive Compound Hesperidin in Six Pure Solvents at (298.15 to 333.15) K
- Solubility of (2Z)-N-Cyclohexyl-2-(3-hydroxybenzylidine) Hydrazine Carbothioamide in Different Pure Solvents at (298.15 to 338.15) K
- Solubility of N-(4-Chlorophenyl)-2-(pyridin-4-ylcarbonyl)hydrazinecarbothioamide (Isoniazid Analogue) in Five Pure Solvents at (298.15 to 338.15) K
- Correlation of Solubility of Bioactive Compound Reserpine in Eight Green Solvents at (298.15 to 338.15) K
- Measurement, Correlation, and Thermodynamics of Solubility of Isatin in Nine Different Green Solvents at (298.15 to 338.15) K
- Isobaric Vapor Liquid Equilibrium for Two Binary Systems{Propane-1,2-diol + Ethane-1,2-diol and Propane-1,2-diol + Butane-1,2-diol} at p = (10.0, 20.0, and 40.0) kPa
- Dielectric Constants of Aqueous Diisopropanolamine, Diethanolamine, N-Methyldiethanolamine, Triethanolamine, and 2-Amino-2-methyl-1-propanol Solutions
- Solubilities of 2-Methyl-1,4-naphthoquinone in Water + (Methanol, Ethanol, 1-Propanol, 2-Propanol, 1,2-Propanediol, and Glycerin, Respectively) from (293.15 to 337.92) K
- Study of the Acoustic and Thermodynamic Properties of 1,2- and 1,3-Propanediol by Means of High-Pressure Speed of Sound Measurements at Temperatures from (293 to 318) K and Pressures up to 101 MPa
- Densities and Excess Molar Volumes for Binary Mixtures of 1,4-Butanediol + 1,2-Propanediol, + 1,3-Propanediol, and + Ethane-1,2-diol from (293.15 to 328.15) K
- Solubility of Acetylsalicylic Acid in Ethanol, Acetone, Propylene Glycol, and 2-Propanol
- Liquid-Liquid Equilibria of (Limonene + Linalool + Ethylene Glycol or Diethylene Glycol or Triethylene Glycol or 1,2-Propylene Glycol) Ternary Systems
- Solubilities of Menadione Sodium Bisulfite in Water + (Methanol, Ethanol, 1-Propanol, 2-Propanol, 1,2-Propanediol, and Glycerin, Respectively) from (297.67 to 337.76) K
- Densities, Excess Molar Volumes, Viscosity, and Refractive Indices of Binary and Ternary Liquid Mixtures of Methanol (1) + Ethanol (2) + 1,2-Propanediol (3) at P = 81.5 kPa
- Solubilities of Isonicotinic Acid in (Methanol, Ethanol, 1-Propanol, 2-Propanol, and 1,2-Propanediol, Respectively) from (289.65 to 358.75) K
- Solubility of Lamotrigine, Diazepam, Clonazepam, and Phenobarbital in Propylene Glycol + Water Mixtures at 298.15 K
- Solubility of 7-Chloro-2-methylamino-5-phenyl-3H-1,4-benzodiazepine-4-oxide, 7-Chloro-1,3-dihydro-1-methyl-5-phenyl-2H-1,4-benzodiazepin-2-one, and 7-Chloro-5-(2-chlorophenyl)-3-hydroxy-1,3-dihydro-1,4-benzodiazepin-2-one in (Propane-1,2-diol + Water) at a Temperature of 303.2 K
- Densities, Viscosities, and Volumetric Properties of Binary Mixtures of 1,2-Propanediol + 1-Heptanol or 1-Hexanol and 1,2-Ethanediol + 2-Butanol or 2-Propanol at T = (298.15, 303.15, and 308.15) K
- Volumetric Properties of Pressure-Transmitting Fluids up to 350 MPa: Water, Ethanol, Ethylene Glycol, Propylene Glycol, Castor Oil, Silicon Oil, and Some of Their Binary Mixture
- Joback Method
- KDB
- McGowan Method
- NIST Webbook
- NCMS SOLV-DB
- The Yaws Handbook of Vapor Pressure
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