- InChI
- InChI=1S/C4H10O3/c5-1-3-7-4-2-6/h5-6H,1-4H2
- InChI Key
- MTHSVFCYNBDYFN-UHFFFAOYSA-N
- Formula
- C4H10O3
- SMILES
- OCCOCCO
- Molecular Weight1
- 106.12
- CAS
- 111-46-6
- Other Names
-
- 1,1'-oxybis[1-methoxy]methane
- 1,5-Dihydroxy-3-oxapentane
- 2,2'-Dihydroxyethyl ether
- 2,2'-OXYBIS ETHANOL
- 2,2'-Oxybis[Ethanol]
- 2,2'-Oxydiethanol
- 2,2'-Oxyethanol
- 2,2'-oxybis(ethan-1-ol)
- 2,2'-oxybis-ethanol
- 2,2-Di(hydroxyethyl) ether
- 2,4,6-trioxaheptane
- 2-(2-Hydroxyethoxy)ethanol
- 2-Hydroxyethyl ether
- 3-Oxa-1,5-pentanediol
- 3-Oxapentamethylene-1,5-diol
- 3-Oxapentane-1,5-diol
- 3-oxapentan-1,5-diol
- BETA,BETA'-DIHYDROXYDIETHYL ETHER
- Bis(2-hydroxyethyl) ether
- Bis(«beta»-hydroxyethyl) ether
- Bis(«beta»-hydroxyethyl) ether
- Brecolane NDG
- Carbitol
- D.E.H. 20
- D.E.H. 52
- DEG
- Deactivator E
- Deactivator H
- Dicol
- Diethylene glycol
- Diethylenglykol
- Digenos
- Diglycol
- Digol
- Dihydroxydiethyl ether
- Dissolvant APV
- ETHYLENE DIGLYCOL
- Ethanol, 2,2'-oxydi-
- Glycol ether
- Glycol hydroxyethyl ether
- Her
- NSC 36391
- TL4N
- «beta»,«beta»'-Dihydroxydiethyl ether
- «beta»,«beta»'-Dihydroxyethyl ether
- «beta»,«beta»'-Dihydroxydiethyl ether
- «beta»,«beta»'-Dihydroxyethyl ether
- ΔcH°liquid : Standard liquid enthalpy of combustion (kJ/mol).
- Cp,gas : Ideal gas heat capacity (J/mol×K).
- Cp,liquid : Liquid phase heat capacity (J/mol×K).
- η : Dynamic viscosity (Pa×s).
- ΔfG° : Standard Gibbs free energy of formation (kJ/mol).
- ΔfH°gas : Enthalpy of formation at standard conditions (kJ/mol).
- ΔfH°liquid : Liquid phase 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).
- log10WS : Log10 of Water solubility in mol/l.
- logPoct/wat : Octanol/Water partition coefficient.
- McVol : McGowan's characteristic volume (ml/mol).
- Pc : Critical Pressure (kPa).
- Pvap : Vapor pressure (kPa).
- n0 : Refractive Index.
- ρl : Liquid Density (kg/m3).
- Inp : Non-polar retention indices.
- I : Polar retention indices.
- Tboil : Normal Boiling Point Temperature (K).
- Tboilr : Boiling point at reduced pressure (K).
- Tc : Critical Temperature (K).
- λ : Liquid thermal conductivity (W/m×K).
- Tfus : Normal melting (fusion) point (K).
- Vc : Critical Volume (m3/kmol).
- Zra : Rackett Parameter.
- 1: Molecular weight from the IUPAC atomic weights tables.
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Contents
- Physical Properties
- Temperature Dependent Properties
- Pressure Dependent Properties
- Datasets
- Correlations
- Similar Compounds
- Mixtures
- Sources
Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ΔcH°liquid | [-2374.70; -2372.90] | kJ/mol |
|
| ΔcH°liquid | -2374.70 ± 2.40 | kJ/mol | NIST |
| ΔcH°liquid | -2372.90 | kJ/mol | NIST |
| ΔfG° | -395.84 | kJ/mol | Joback Calculated Property |
| ΔfH°gas | -571.50 | kJ/mol | KDB |
| ΔfH°liquid | -628.50 ± 2.40 | kJ/mol | NIST |
| ΔfusH° | 15.48 | kJ/mol | Joback Calculated Property |
| ΔvapH° | 60.27 | kJ/mol | Joback Calculated Property |
| log10WS | 0.89 | Crippen Calculated Property | |
| logPoct/wat | -1.012 | Crippen Calculated Property | |
| McVol | 84.830 | ml/mol | McGowan Calculated Property |
| Pc | [4700.00; 4770.00] | kPa |
|
| Pc | 4700.00 | kPa | KDB |
| Pc | 4770.00 ± 50.00 | kPa | NIST |
| Inp | [925.00; 967.00] |
|
|
| Inp | 927.00 | NIST | |
| Inp | 925.00 | NIST | |
| Inp | 967.00 | NIST | |
| Inp | 941.00 | NIST | |
| I | [1953.00; 1989.00] |
|
|
| I | 1989.00 | NIST | |
| I | 1975.00 | NIST | |
| I | 1968.00 | NIST | |
| I | 1953.00 | NIST | |
| I | 1975.00 | NIST | |
| Tboil | 519.00 | K | KDB |
| Tc | [680.00; 753.00] | K |
|
| Tc | 681.00 | K | KDB |
| Tc | 753.00 | K | Critica... |
| Tc | 753.00 ± 4.00 | K | NIST |
| Tc | 723.50 ± 50.00 | K | NIST |
| Tc | 680.00 ± 20.00 | K | NIST |
| Tfus | [262.80; 265.40] | K |
|
| Tfus | 265.00 | K | KDB |
| Tfus | 265.35 | K | NIST |
| Tfus | 265.40 ± 0.60 | K | NIST |
| Tfus | 263.05 ± 0.50 | K | NIST |
| Tfus | 262.80 ± 0.10 | K | NIST |
| Vc | 0.316 | m3/kmol | Joback Calculated Property |
| Zra | 0.25 | KDB |
Temperature Dependent Properties
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [193.32; 228.87] | J/mol×K | [497.70; 656.34] |
|
|
T(K) Ideal gas heat capacity (J/mol×K) 190 200 210 220 230 500 550 600 650 | ||||
| Cp,gas | 193.32 | J/mol×K | 497.70 | Joback Calculated Property |
| Cp,gas | 199.74 | J/mol×K | 524.14 | Joback Calculated Property |
| Cp,gas | 205.96 | J/mol×K | 550.58 | Joback Calculated Property |
| Cp,gas | 211.98 | J/mol×K | 577.02 | Joback Calculated Property |
| Cp,gas | 217.81 | J/mol×K | 603.46 | Joback Calculated Property |
| Cp,gas | 223.44 | J/mol×K | 629.90 | Joback Calculated Property |
| Cp,gas | 228.87 | J/mol×K | 656.34 | Joback Calculated Property |
| Cp,liquid | [243.90; 287.00] | J/mol×K | [298.00; 353.15] |
|
|
T(K) Liquid phase heat capacity (J/mol×K) 240 250 260 270 280 290 300 320 340 | ||||
| Cp,liquid | 243.90 | J/mol×K | 298.00 | NIST |
| Cp,liquid | 287.00 | J/mol×K | 298.00 | NIST |
| Cp,liquid | 248.20 | J/mol×K | 303.15 | Heat ca... |
| Cp,liquid | 251.30 | J/mol×K | 313.15 | Heat ca... |
| Cp,liquid | 255.00 | J/mol×K | 323.15 | Heat ca... |
| Cp,liquid | 259.20 | J/mol×K | 333.15 | Heat ca... |
| Cp,liquid | 263.80 | J/mol×K | 343.15 | Heat ca... |
| Cp,liquid | 266.80 | J/mol×K | 353.15 | Heat ca... |
| η | [0.0007890; 0.0381100] | Pa×s | [293.15; 464.05] |
|
|
T(K) Dynamic viscosity (Pa×s) 0 5.00e-3 0.01 0.02 0.02 0.03 0.03 0.04 0.04 300 350 400 450 | ||||
| η | 0.0364330 | Pa×s | 293.15 | Supplem... |
| η | 0.0365200 | Pa×s | 293.15 | Experim... |
| η | 0.0381100 | Pa×s | 293.20 | Phase e... |
| η | 0.0351000 | Pa×s | 294.20 | Density... |
| η | 0.0283600 | Pa×s | 298.15 | Experim... |
| η | 0.0300120 | Pa×s | 298.15 | Densiti... |
| η | 0.0300120 | Pa×s | 298.15 | Thermop... |
| η | 0.0298200 | Pa×s | 298.20 | Phase e... |
| η | 0.0220910 | Pa×s | 303.15 | Supplem... |
| η | 0.0221560 | Pa×s | 303.15 | Densiti... |
| η | 0.0236400 | Pa×s | 303.20 | Phase e... |
| η | 0.0179340 | Pa×s | 308.15 | Densiti... |
| η | 0.0169720 | Pa×s | 308.15 | Densiti... |
| η | 0.0169720 | Pa×s | 308.15 | Thermop... |
| η | 0.0190200 | Pa×s | 308.20 | Phase e... |
| η | 0.0152500 | Pa×s | 312.60 | Experim... |
| η | 0.0151000 | Pa×s | 313.05 | Density... |
| η | 0.0147060 | Pa×s | 313.15 | Densiti... |
| η | 0.0145630 | Pa×s | 313.15 | Supplem... |
| η | 0.0156000 | Pa×s | 313.20 | Phase e... |
| η | 0.0121910 | Pa×s | 318.15 | Densiti... |
| η | 0.0126900 | Pa×s | 318.20 | Phase e... |
| η | 0.0100290 | Pa×s | 323.15 | Supplem... |
| η | 0.0101950 | Pa×s | 323.15 | Densiti... |
| η | 0.0106200 | Pa×s | 323.20 | Phase e... |
| η | 0.0088530 | Pa×s | 328.20 | Phase e... |
| η | 0.0084580 | Pa×s | 329.28 | Experim... |
| η | 0.0076400 | Pa×s | 333.05 | Density... |
| η | 0.0072200 | Pa×s | 333.15 | Supplem... |
| η | 0.0073620 | Pa×s | 333.20 | Phase e... |
| η | 0.0062080 | Pa×s | 338.20 | Phase e... |
| η | 0.0053690 | Pa×s | 343.15 | Supplem... |
| η | 0.0053240 | Pa×s | 343.20 | Phase e... |
| η | 0.0053400 | Pa×s | 344.99 | Experim... |
| η | 0.0048090 | Pa×s | 349.77 | Experim... |
| η | 0.0044100 | Pa×s | 353.05 | Density... |
| η | 0.0041390 | Pa×s | 353.15 | Supplem... |
| η | 0.0032310 | Pa×s | 366.77 | Experim... |
| η | 0.0027600 | Pa×s | 373.60 | Density... |
| η | 0.0019200 | Pa×s | 393.40 | Density... |
| η | 0.0014100 | Pa×s | 413.25 | Density... |
| η | 0.0014090 | Pa×s | 413.65 | Experim... |
| η | 0.0011500 | Pa×s | 428.15 | Density... |
| η | 0.0007890 | Pa×s | 464.05 | Experim... |
| ΔvapH | [55.10; 69.20] | kJ/mol | [273.00; 523.00] |
|
|
T(K) Enthalpy of vaporization at a given temperature (kJ/mol) 55 60 65 70 300 400 500 | ||||
| ΔvapH | 57.30 ± 5.90 | kJ/mol | 273.00 | NIST |
| ΔvapH | 66.50 | kJ/mol | 413.00 | NIST |
| ΔvapH | 59.80 | kJ/mol | 441.00 | NIST |
| ΔvapH | 69.20 | kJ/mol | 458.00 | NIST |
| ΔvapH | 66.80 | kJ/mol | 462.50 | NIST |
| ΔvapH | 63.10 ± 0.30 | kJ/mol | 474.50 | NIST |
| ΔvapH | 55.10 ± 0.50 | kJ/mol | 474.50 | NIST |
| ΔvapH | 66.90 ± 0.30 | kJ/mol | 474.50 | NIST |
| ΔvapH | 59.20 ± 0.30 | kJ/mol | 474.50 | NIST |
| ΔvapH | 66.57 | kJ/mol | 523.00 | NIST |
| n0 | 1.44724 | 293.15 | Liquid-... | |
| ρl | [1059.00; 1123.30] | kg/m3 | [283.15; 373.15] |
|
|
T(K) Liquid Density (kg/m3) 1060 1070 1080 1090 1100 1110 1120 300 320 340 360 | ||||
| ρl | 1123.30 | kg/m3 | 283.15 | Thermop... |
| ρl | 1121.40 | kg/m3 | 288.15 | Thermop... |
| ρl | 1120.30 | kg/m3 | 288.15 | Activit... |
| ρl | 1120.05 | kg/m3 | 288.15 | Activit... |
| ρl | 1119.80 | kg/m3 | 288.15 | Thermop... |
| ρl | 1116.00 | kg/m3 | 293.00 | KDB |
| ρl | 1116.50 | kg/m3 | 293.15 | Measure... |
| ρl | 1117.80 | kg/m3 | 293.15 | Thermop... |
| ρl | 1116.73 | kg/m3 | 293.15 | Thermod... |
| ρl | 1116.20 | kg/m3 | 293.15 | Thermop... |
| ρl | 1109.16 | kg/m3 | 298.00 | Removal... |
| ρl | 1112.38 | kg/m3 | 298.15 | Thermod... |
| ρl | 1114.20 | kg/m3 | 298.15 | Thermop... |
| ρl | 1113.00 | kg/m3 | 298.15 | Solubil... |
| ρl | 1112.70 | kg/m3 | 298.15 | Thermop... |
| ρl | 1112.80 | kg/m3 | 298.15 | Density... |
| ρl | 1112.38 | kg/m3 | 298.15 | Excess ... |
| ρl | 1112.56 | kg/m3 | 298.15 | Isobari... |
| ρl | 1112.70 | kg/m3 | 298.15 | Densiti... |
| ρl | 1113.00 | kg/m3 | 298.15 | Measure... |
| ρl | 1113.17 | kg/m3 | 298.15 | Thermod... |
| ρl | 1109.40 | kg/m3 | 303.15 | Measure... |
| ρl | 1110.00 | kg/m3 | 303.15 | Density... |
| ρl | 1109.30 | kg/m3 | 303.15 | Densiti... |
| ρl | 1109.10 | kg/m3 | 303.15 | Thermop... |
| ρl | 1109.60 | kg/m3 | 303.15 | Thermod... |
| ρl | 1109.20 | kg/m3 | 303.15 | Solubil... |
| ρl | 1110.60 | kg/m3 | 303.15 | Thermop... |
| ρl | 1109.20 | kg/m3 | 303.15 | Density... |
| ρl | 1109.00 | kg/m3 | 303.15 | Vapour ... |
| ρl | 1105.65 | kg/m3 | 308.15 | Excess ... |
| ρl | 1105.90 | kg/m3 | 308.15 | Densiti... |
| ρl | 1106.01 | kg/m3 | 308.15 | Thermod... |
| ρl | 1105.65 | kg/m3 | 308.15 | Excess ... |
| ρl | 1105.88 | kg/m3 | 308.15 | Excess ... |
| ρl | 1106.10 | kg/m3 | 308.15 | Solubil... |
| ρl | 1105.60 | kg/m3 | 308.15 | Density... |
| ρl | 1107.00 | kg/m3 | 308.15 | Thermop... |
| ρl | 1105.50 | kg/m3 | 308.15 | Thermop... |
| ρl | 1105.80 | kg/m3 | 308.15 | Measure... |
| ρl | 1105.88 | kg/m3 | 308.15 | Thermod... |
| ρl | 1105.86 | kg/m3 | 308.50 | Excess ... |
| ρl | 1103.00 | kg/m3 | 313.15 | Vapour ... |
| ρl | 1101.90 | kg/m3 | 313.15 | Thermop... |
| ρl | 1102.50 | kg/m3 | 313.15 | Densiti... |
| ρl | 1103.40 | kg/m3 | 313.15 | Thermop... |
| ρl | 1102.30 | kg/m3 | 313.15 | Density... |
| ρl | 1103.00 | kg/m3 | 313.15 | Density... |
| ρl | 1102.20 | kg/m3 | 313.15 | Measure... |
| ρl | 1103.00 | kg/m3 | 313.15 | Solubil... |
| ρl | 1099.30 | kg/m3 | 318.15 | Solubil... |
| ρl | 1099.70 | kg/m3 | 318.15 | Thermop... |
| ρl | 1099.20 | kg/m3 | 318.15 | Density... |
| ρl | 1098.60 | kg/m3 | 318.15 | Measure... |
| ρl | 1095.00 | kg/m3 | 323.15 | Measure... |
| ρl | 1094.70 | kg/m3 | 323.15 | Thermop... |
| ρl | 1095.90 | kg/m3 | 323.15 | Density... |
| ρl | 1096.10 | kg/m3 | 323.15 | Thermop... |
| ρl | 1095.00 | kg/m3 | 323.15 | Vapour ... |
| ρl | 1091.40 | kg/m3 | 328.15 | Measure... |
| ρl | 1092.50 | kg/m3 | 328.15 | Thermop... |
| ρl | 1087.40 | kg/m3 | 333.15 | Thermop... |
| ρl | 1087.70 | kg/m3 | 333.15 | Measure... |
| ρl | 1088.50 | kg/m3 | 333.15 | Density... |
| ρl | 1088.00 | kg/m3 | 333.15 | Vapour ... |
| ρl | 1088.80 | kg/m3 | 333.15 | Thermop... |
| ρl | 1084.00 | kg/m3 | 338.15 | Measure... |
| ρl | 1085.20 | kg/m3 | 338.15 | Thermop... |
| ρl | 1080.00 | kg/m3 | 343.15 | Thermop... |
| ρl | 1081.00 | kg/m3 | 343.15 | Vapour ... |
| ρl | 1081.50 | kg/m3 | 343.15 | Thermop... |
| ρl | 1081.10 | kg/m3 | 343.15 | Density... |
| ρl | 1080.30 | kg/m3 | 343.15 | Measure... |
| ρl | 1077.80 | kg/m3 | 348.15 | Thermop... |
| ρl | 1074.10 | kg/m3 | 353.15 | Thermop... |
| ρl | 1070.30 | kg/m3 | 358.15 | Thermop... |
| ρl | 1066.60 | kg/m3 | 363.15 | Thermop... |
| ρl | 1062.80 | kg/m3 | 368.15 | Thermop... |
| ρl | 1059.00 | kg/m3 | 373.15 | Thermop... |
| λ | [0.20; 0.21] | W/m×K | [298.10; 338.20] |
|
|
T(K) Liquid thermal conductivity (W/m×K) 0.2 0.2 0.2 0.21 300 310 320 330 | ||||
| λ | 0.20 | W/m×K | 298.10 | Applica... |
| λ | 0.20 | W/m×K | 308.00 | Applica... |
| λ | 0.20 | W/m×K | 318.20 | Applica... |
| λ | 0.20 | W/m×K | 328.40 | Applica... |
| λ | 0.21 | W/m×K | 338.20 | Applica... |
Pressure Dependent Properties
| Property | Value | Unit | Pressure (kPa) | Source |
|---|---|---|---|---|
| Tboilr | 406.20 | K | 1.90 | NIST |
Datasets
Viscosity, Pa*s
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Viscosity, Pa*s - Liquid |
| 293.15 | 98.00 | 0.0365 |
| 293.15 | 49030.00 | 0.0527 |
| 293.15 | 98060.00 | 0.0742 |
| 293.15 | 147100.00 | 0.1026 |
| 293.15 | 196130.00 | 0.1399 |
| 293.15 | 245160.00 | 0.1873 |
| 298.15 | 98.00 | 0.0284 |
| 298.15 | 49030.00 | 0.0404 |
| 298.15 | 98060.00 | 0.0565 |
| 298.15 | 147100.00 | 0.0772 |
| 298.15 | 196130.00 | 0.1038 |
| 298.15 | 245160.00 | 0.1383 |
| 312.60 | 98.00 | 0.0152 |
| 312.62 | 49030.00 | 0.0210 |
| 312.63 | 98060.00 | 0.0282 |
| 312.67 | 147100.00 | 0.0371 |
| 312.71 | 196130.00 | 0.0483 |
| 312.75 | 245160.00 | 0.0621 |
| 329.28 | 98.00 | 0.0085 |
| 329.33 | 98060.00 | 0.0147 |
| 329.33 | 196130.00 | 0.0238 |
| 329.33 | 245160.00 | 0.0296 |
| 329.38 | 49030.00 | 0.0113 |
| 329.38 | 147100.00 | 0.0188 |
| 344.99 | 98.00 | 0.0053 |
| 345.20 | 49030.00 | 0.0071 |
| 345.38 | 98060.00 | 0.0090 |
| 345.47 | 147100.00 | 0.0112 |
| 345.61 | 196130.00 | 0.0138 |
| 345.78 | 245160.00 | 0.0168 |
| 349.77 | 98.00 | 0.0048 |
| 350.06 | 49030.00 | 0.0063 |
| 350.13 | 147100.00 | 0.0099 |
| 350.16 | 98060.00 | 0.0079 |
| 350.40 | 196130.00 | 0.0120 |
| 366.77 | 98.00 | 0.0032 |
| 367.13 | 49030.00 | 0.0041 |
| 367.26 | 147100.00 | 0.0063 |
| 367.30 | 98060.00 | 0.0051 |
| 367.37 | 196130.00 | 0.0076 |
| 367.61 | 245160.00 | 0.0091 |
| 413.65 | 98.00 | 0.0014 |
| 413.80 | 49030.00 | 0.0018 |
| 413.93 | 98060.00 | 0.0022 |
| 414.01 | 147100.00 | 0.0026 |
| 414.09 | 196130.00 | 0.0030 |
| 414.29 | 245160.00 | 0.0035 |
| 463.94 | 98060.00 | 0.0012 |
| 463.99 | 49030.00 | 0.0010 |
| 464.05 | 98.00 | 0.0008 |
| 464.09 | 147100.00 | 0.0014 |
| 464.20 | 196130.00 | 0.0017 |
| 464.37 | 245160.00 | 0.0019 |
| Reference | ||
| Fixed | Measured | |
|---|---|---|
| Pressure, kPa - Liquid | Temperature, K - Liquid | Viscosity, Pa*s - Liquid |
| 101.30 | 308.15 | 0.0176 |
| Reference | ||
Mass density, kg/m3
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 283.15 | 100.00 | 1124.3 |
| 283.15 | 1000.00 | 1124.7 |
| 283.15 | 2000.00 | 1125.3 |
| 283.15 | 5000.00 | 1126.5 |
| 283.15 | 7000.00 | 1127.4 |
| 283.15 | 10000.00 | 1128.8 |
| 283.15 | 12000.00 | 1129.6 |
| 283.15 | 16000.00 | 1131.3 |
| 283.15 | 20000.00 | 1133.0 |
| 283.15 | 25000.00 | 1135.1 |
| 283.15 | 30000.00 | 1137.2 |
| 283.15 | 35000.00 | 1139.2 |
| 283.15 | 40000.00 | 1141.2 |
| 283.15 | 45000.00 | 1143.0 |
| 283.15 | 50000.00 | 1145.1 |
| 283.15 | 55000.00 | 1146.9 |
| 283.15 | 60000.00 | 1148.8 |
| 283.15 | 65000.00 | 1150.7 |
| 283.15 | 70000.00 | 1152.4 |
| 283.15 | 75000.00 | 1154.2 |
| 283.15 | 80000.00 | 1155.8 |
| 283.15 | 85000.00 | 1157.5 |
| 283.15 | 90000.00 | 1159.2 |
| 283.15 | 95000.00 | 1160.9 |
| 293.15 | 100.00 | 1117.1 |
| 293.15 | 1000.00 | 1117.5 |
| 293.15 | 2000.00 | 1118.0 |
| 293.15 | 5000.00 | 1119.3 |
| 293.15 | 7000.00 | 1120.2 |
| 293.15 | 10000.00 | 1121.6 |
| 293.15 | 12000.00 | 1122.5 |
| 293.15 | 16000.00 | 1124.3 |
| 293.15 | 20000.00 | 1126.0 |
| 293.15 | 25000.00 | 1128.2 |
| 293.15 | 30000.00 | 1130.3 |
| 293.15 | 35000.00 | 1132.4 |
| 293.15 | 40000.00 | 1134.3 |
| 293.15 | 45000.00 | 1136.4 |
| 293.15 | 50000.00 | 1138.4 |
| 293.15 | 55000.00 | 1140.4 |
| 293.15 | 60000.00 | 1142.2 |
| 293.15 | 65000.00 | 1144.1 |
| 293.15 | 70000.00 | 1145.8 |
| 293.15 | 75000.00 | 1147.7 |
| 293.15 | 80000.00 | 1149.4 |
| 293.15 | 85000.00 | 1151.2 |
| 293.15 | 90000.00 | 1152.9 |
| 293.15 | 95000.00 | 1154.6 |
| 303.14 | 100.00 | 1109.9 |
| 303.14 | 1000.00 | 1110.3 |
| 303.14 | 2000.00 | 1110.7 |
| 303.14 | 5000.00 | 1112.2 |
| 303.14 | 7000.00 | 1113.1 |
| 303.14 | 10000.00 | 1114.5 |
| 303.14 | 12000.00 | 1115.4 |
| 303.14 | 16000.00 | 1117.3 |
| 303.14 | 20000.00 | 1119.0 |
| 303.14 | 25000.00 | 1121.2 |
| 303.14 | 30000.00 | 1123.4 |
| 303.14 | 35000.00 | 1125.5 |
| 303.14 | 40000.00 | 1127.5 |
| 303.14 | 45000.00 | 1129.6 |
| 303.14 | 50000.00 | 1131.6 |
| 303.14 | 55000.00 | 1133.6 |
| 303.14 | 60000.00 | 1135.5 |
| 303.14 | 65000.00 | 1137.4 |
| 303.14 | 70000.00 | 1139.3 |
| 303.14 | 75000.00 | 1141.1 |
| 303.14 | 80000.00 | 1142.9 |
| 303.14 | 85000.00 | 1144.6 |
| 303.14 | 90000.00 | 1146.4 |
| 303.14 | 95000.00 | 1148.2 |
| 313.15 | 100.00 | 1102.7 |
| 313.15 | 1000.00 | 1103.2 |
| 313.15 | 2000.00 | 1103.6 |
| 313.15 | 5000.00 | 1105.2 |
| 313.15 | 7000.00 | 1106.2 |
| 313.15 | 10000.00 | 1107.7 |
| 313.15 | 12000.00 | 1108.6 |
| 313.15 | 16000.00 | 1110.4 |
| 313.15 | 20000.00 | 1112.3 |
| 313.15 | 25000.00 | 1114.5 |
| 313.15 | 30000.00 | 1116.7 |
| 313.15 | 35000.00 | 1118.9 |
| 313.15 | 40000.00 | 1121.0 |
| 313.15 | 45000.00 | 1123.1 |
| 313.15 | 50000.00 | 1125.1 |
| 313.15 | 55000.00 | 1127.1 |
| 313.15 | 60000.00 | 1129.1 |
| 313.15 | 65000.00 | 1131.1 |
| 313.15 | 70000.00 | 1132.9 |
| 313.15 | 75000.00 | 1134.8 |
| 313.15 | 80000.00 | 1136.6 |
| 313.15 | 85000.00 | 1138.4 |
| 313.15 | 90000.00 | 1140.2 |
| 313.15 | 95000.00 | 1141.9 |
| 323.20 | 100.00 | 1095.4 |
| 323.20 | 1000.00 | 1095.8 |
| 323.20 | 2000.00 | 1096.3 |
| 323.20 | 5000.00 | 1097.8 |
| 323.20 | 7000.00 | 1098.8 |
| 323.20 | 10000.00 | 1100.3 |
| 323.20 | 12000.00 | 1101.3 |
| 323.20 | 16000.00 | 1103.3 |
| 323.20 | 20000.00 | 1105.2 |
| 323.20 | 25000.00 | 1107.5 |
| 323.20 | 30000.00 | 1109.9 |
| 323.20 | 35000.00 | 1112.0 |
| 323.20 | 40000.00 | 1114.2 |
| 323.20 | 45000.00 | 1116.3 |
| 323.20 | 50000.00 | 1118.4 |
| 323.20 | 55000.00 | 1120.5 |
| 323.20 | 60000.00 | 1122.5 |
| 323.20 | 65000.00 | 1124.5 |
| 323.20 | 70000.00 | 1126.5 |
| 323.20 | 75000.00 | 1128.3 |
| 323.20 | 80000.00 | 1130.3 |
| 323.20 | 85000.00 | 1132.2 |
| 323.20 | 90000.00 | 1133.9 |
| 323.20 | 95000.00 | 1135.7 |
| 333.20 | 100.00 | 1088.1 |
| 333.20 | 1000.00 | 1088.7 |
| 333.20 | 2000.00 | 1089.2 |
| 333.20 | 5000.00 | 1090.8 |
| 333.20 | 7000.00 | 1091.8 |
| 333.20 | 10000.00 | 1093.3 |
| 333.20 | 12000.00 | 1094.4 |
| 333.20 | 16000.00 | 1096.4 |
| 333.20 | 20000.00 | 1098.3 |
| 333.20 | 25000.00 | 1100.7 |
| 333.20 | 30000.00 | 1103.0 |
| 333.20 | 35000.00 | 1105.3 |
| 333.20 | 40000.00 | 1107.6 |
| 333.20 | 45000.00 | 1109.7 |
| 333.20 | 50000.00 | 1111.9 |
| 333.20 | 55000.00 | 1113.9 |
| 333.20 | 60000.00 | 1116.0 |
| 333.20 | 65000.00 | 1118.0 |
| 333.20 | 70000.00 | 1120.1 |
| 333.20 | 75000.00 | 1121.9 |
| 333.20 | 80000.00 | 1123.8 |
| 333.20 | 85000.00 | 1125.9 |
| 333.20 | 90000.00 | 1127.7 |
| 333.20 | 95000.00 | 1129.5 |
| 343.20 | 100.00 | 1080.7 |
| 343.20 | 1000.00 | 1081.2 |
| 343.20 | 2000.00 | 1081.7 |
| 343.20 | 5000.00 | 1083.4 |
| 343.20 | 7000.00 | 1084.5 |
| 343.20 | 10000.00 | 1086.1 |
| 343.20 | 12000.00 | 1087.1 |
| 343.20 | 16000.00 | 1089.1 |
| 343.20 | 20000.00 | 1091.2 |
| 343.20 | 25000.00 | 1093.7 |
| 343.20 | 30000.00 | 1096.1 |
| 343.20 | 35000.00 | 1098.5 |
| 343.20 | 40000.00 | 1100.8 |
| 343.20 | 45000.00 | 1103.1 |
| 343.20 | 50000.00 | 1105.2 |
| 343.20 | 55000.00 | 1107.4 |
| 343.20 | 60000.00 | 1109.5 |
| 343.20 | 65000.00 | 1111.6 |
| 343.20 | 70000.00 | 1113.7 |
| 343.20 | 75000.00 | 1115.7 |
| 343.20 | 80000.00 | 1117.6 |
| 343.20 | 85000.00 | 1119.5 |
| 343.20 | 90000.00 | 1121.4 |
| 343.20 | 95000.00 | 1123.3 |
| 353.19 | 100.00 | 1073.2 |
| 353.19 | 1000.00 | 1073.8 |
| 353.19 | 2000.00 | 1074.3 |
| 353.19 | 5000.00 | 1076.0 |
| 353.19 | 7000.00 | 1077.1 |
| 353.19 | 10000.00 | 1078.7 |
| 353.19 | 12000.00 | 1079.8 |
| 353.19 | 16000.00 | 1081.9 |
| 353.19 | 20000.00 | 1084.0 |
| 353.19 | 25000.00 | 1086.6 |
| 353.19 | 30000.00 | 1089.1 |
| 353.19 | 35000.00 | 1091.6 |
| 353.19 | 40000.00 | 1093.9 |
| 353.19 | 45000.00 | 1096.3 |
| 353.19 | 50000.00 | 1098.5 |
| 353.19 | 55000.00 | 1100.8 |
| 353.19 | 60000.00 | 1102.9 |
| 353.19 | 65000.00 | 1105.0 |
| 353.19 | 70000.00 | 1107.2 |
| 353.19 | 75000.00 | 1109.2 |
| 353.19 | 80000.00 | 1111.2 |
| 353.19 | 85000.00 | 1113.2 |
| 353.19 | 90000.00 | 1115.1 |
| 353.19 | 95000.00 | 1117.0 |
| 363.17 | 100.00 | 1065.6 |
| 363.17 | 1000.00 | 1066.2 |
| 363.17 | 2000.00 | 1066.8 |
| 363.17 | 5000.00 | 1068.5 |
| 363.17 | 7000.00 | 1069.6 |
| 363.17 | 10000.00 | 1071.4 |
| 363.17 | 12000.00 | 1072.5 |
| 363.17 | 16000.00 | 1074.6 |
| 363.17 | 20000.00 | 1076.9 |
| 363.17 | 25000.00 | 1079.4 |
| 363.17 | 30000.00 | 1082.0 |
| 363.17 | 35000.00 | 1084.6 |
| 363.17 | 40000.00 | 1087.0 |
| 363.17 | 45000.00 | 1089.4 |
| 363.17 | 50000.00 | 1091.8 |
| 363.17 | 55000.00 | 1094.1 |
| 363.17 | 60000.00 | 1096.3 |
| 363.17 | 65000.00 | 1098.5 |
| 363.17 | 70000.00 | 1100.5 |
| 363.17 | 75000.00 | 1102.6 |
| 363.17 | 80000.00 | 1104.8 |
| 363.17 | 85000.00 | 1106.8 |
| 363.17 | 90000.00 | 1108.8 |
| 363.17 | 95000.00 | 1110.7 |
| Reference | ||
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 283.15 | 100.00 | 1123.1 |
| 283.15 | 100.00 | 1123.1 |
| 283.15 | 640.00 | 1123.3 |
| 283.15 | 1080.00 | 1123.5 |
| 283.15 | 1590.00 | 1123.7 |
| 283.15 | 2140.00 | 1124.0 |
| 283.15 | 3050.00 | 1124.3 |
| 283.15 | 5050.00 | 1125.2 |
| 283.15 | 6930.00 | 1126.0 |
| 283.15 | 9930.00 | 1127.2 |
| 283.15 | 14810.00 | 1129.3 |
| 283.15 | 19760.00 | 1131.3 |
| 283.15 | 24610.00 | 1133.3 |
| 283.15 | 29600.00 | 1135.2 |
| 283.15 | 34500.00 | 1137.1 |
| 283.15 | 39420.00 | 1139.0 |
| 283.15 | 44300.00 | 1140.8 |
| 283.15 | 49180.00 | 1142.6 |
| 283.15 | 54060.00 | 1144.4 |
| 283.15 | 59030.00 | 1146.1 |
| 283.15 | 63810.00 | 1147.8 |
| 283.15 | 68760.00 | 1149.5 |
| 293.15 | 100.00 | 1115.9 |
| 293.15 | 100.00 | 1115.9 |
| 293.15 | 570.00 | 1116.1 |
| 293.15 | 1080.00 | 1116.3 |
| 293.15 | 1530.00 | 1116.6 |
| 293.15 | 2110.00 | 1116.8 |
| 293.15 | 3080.00 | 1117.2 |
| 293.15 | 5040.00 | 1118.1 |
| 293.15 | 6990.00 | 1118.9 |
| 293.15 | 9940.00 | 1120.2 |
| 293.15 | 14840.00 | 1122.3 |
| 293.15 | 19740.00 | 1124.3 |
| 293.15 | 24680.00 | 1126.4 |
| 293.15 | 29600.00 | 1128.4 |
| 293.15 | 34530.00 | 1130.3 |
| 293.15 | 39360.00 | 1132.2 |
| 293.15 | 44320.00 | 1134.1 |
| 293.15 | 49120.00 | 1136.0 |
| 293.15 | 54090.00 | 1137.8 |
| 293.15 | 58990.00 | 1139.6 |
| 293.15 | 63820.00 | 1141.3 |
| 293.15 | 68750.00 | 1143.0 |
| 303.15 | 100.00 | 1108.8 |
| 303.15 | 100.00 | 1108.8 |
| 303.15 | 680.00 | 1109.0 |
| 303.15 | 1130.00 | 1109.2 |
| 303.15 | 1580.00 | 1109.4 |
| 303.15 | 2120.00 | 1109.7 |
| 303.15 | 3030.00 | 1110.1 |
| 303.15 | 5040.00 | 1111.0 |
| 303.15 | 6950.00 | 1111.9 |
| 303.15 | 9960.00 | 1113.2 |
| 303.15 | 14840.00 | 1115.4 |
| 303.15 | 19740.00 | 1117.5 |
| 303.15 | 24680.00 | 1119.6 |
| 303.15 | 29610.00 | 1121.6 |
| 303.15 | 34520.00 | 1123.6 |
| 303.15 | 39380.00 | 1125.6 |
| 303.15 | 44350.00 | 1127.5 |
| 303.15 | 49140.00 | 1129.4 |
| 303.15 | 54090.00 | 1131.3 |
| 303.15 | 58990.00 | 1133.1 |
| 303.15 | 63850.00 | 1134.9 |
| 303.15 | 68760.00 | 1136.6 |
| 313.15 | 100.00 | 1101.7 |
| 313.15 | 100.00 | 1101.6 |
| 313.15 | 640.00 | 1101.8 |
| 313.15 | 1140.00 | 1102.1 |
| 313.15 | 1640.00 | 1102.3 |
| 313.15 | 2100.00 | 1102.5 |
| 313.15 | 3090.00 | 1103.0 |
| 313.15 | 5130.00 | 1103.9 |
| 313.15 | 6960.00 | 1104.8 |
| 313.15 | 9960.00 | 1106.1 |
| 313.15 | 14940.00 | 1108.4 |
| 313.15 | 19750.00 | 1110.6 |
| 313.15 | 24640.00 | 1112.7 |
| 313.15 | 29640.00 | 1114.8 |
| 313.15 | 34510.00 | 1116.9 |
| 313.15 | 39340.00 | 1118.9 |
| 313.15 | 44340.00 | 1120.9 |
| 313.15 | 49190.00 | 1123.2 |
| 313.15 | 54020.00 | 1124.7 |
| 313.15 | 59030.00 | 1126.7 |
| 313.15 | 63880.00 | 1128.5 |
| 313.15 | 68820.00 | 1130.3 |
| 323.15 | 100.00 | 1094.3 |
| 323.15 | 100.00 | 1094.3 |
| 323.15 | 680.00 | 1094.6 |
| 323.15 | 1130.00 | 1094.8 |
| 323.15 | 1570.00 | 1095.0 |
| 323.15 | 2100.00 | 1095.2 |
| 323.15 | 3080.00 | 1095.7 |
| 323.15 | 5080.00 | 1096.7 |
| 323.15 | 7000.00 | 1097.6 |
| 323.15 | 9950.00 | 1099.0 |
| 323.15 | 14890.00 | 1101.4 |
| 323.15 | 19770.00 | 1103.6 |
| 323.15 | 24680.00 | 1105.8 |
| 323.15 | 29600.00 | 1108.0 |
| 323.15 | 34530.00 | 1110.1 |
| 323.15 | 39360.00 | 1112.2 |
| 323.15 | 44290.00 | 1114.3 |
| 323.15 | 49260.00 | 1116.3 |
| 323.15 | 54100.00 | 1118.2 |
| 323.15 | 59060.00 | 1120.2 |
| 323.15 | 63880.00 | 1122.0 |
| 323.15 | 68770.00 | 1123.8 |
| 333.15 | 100.00 | 1087.0 |
| 333.15 | 100.00 | 1087.0 |
| 333.15 | 660.00 | 1087.3 |
| 333.15 | 1120.00 | 1087.5 |
| 333.15 | 1630.00 | 1087.8 |
| 333.15 | 2100.00 | 1088.0 |
| 333.15 | 3070.00 | 1088.5 |
| 333.15 | 5060.00 | 1089.5 |
| 333.15 | 7050.00 | 1090.5 |
| 333.15 | 9930.00 | 1091.9 |
| 333.15 | 14780.00 | 1094.3 |
| 333.15 | 19770.00 | 1096.7 |
| 333.15 | 24660.00 | 1099.0 |
| 333.15 | 29540.00 | 1101.2 |
| 333.15 | 34500.00 | 1103.4 |
| 333.15 | 39330.00 | 1105.5 |
| 333.15 | 44230.00 | 1107.6 |
| 333.15 | 49130.00 | 1109.7 |
| 333.15 | 54060.00 | 1111.7 |
| 333.15 | 59020.00 | 1113.7 |
| 333.15 | 63840.00 | 1115.7 |
| 333.15 | 68830.00 | 1117.5 |
| 343.15 | 100.00 | 1079.7 |
| 343.15 | 100.00 | 1079.7 |
| 343.15 | 670.00 | 1080.0 |
| 343.15 | 1100.00 | 1080.2 |
| 343.15 | 1520.00 | 1080.4 |
| 343.15 | 2120.00 | 1080.7 |
| 343.15 | 3060.00 | 1081.2 |
| 343.15 | 5040.00 | 1082.3 |
| 343.15 | 6970.00 | 1083.3 |
| 343.15 | 9950.00 | 1084.8 |
| 343.15 | 14870.00 | 1087.3 |
| 343.15 | 19740.00 | 1089.6 |
| 343.15 | 24710.00 | 1092.1 |
| 343.15 | 29560.00 | 1094.4 |
| 343.15 | 34490.00 | 1096.6 |
| 343.15 | 39350.00 | 1098.8 |
| 343.15 | 44290.00 | 1101.0 |
| 343.15 | 49180.00 | 1103.1 |
| 343.15 | 54070.00 | 1105.2 |
| 343.15 | 58980.00 | 1107.3 |
| 343.15 | 63910.00 | 1109.3 |
| 343.15 | 68720.00 | 1111.2 |
| 353.15 | 100.00 | 1072.2 |
| 353.15 | 100.00 | 1072.2 |
| 353.15 | 560.00 | 1072.5 |
| 353.15 | 1090.00 | 1072.8 |
| 353.15 | 1550.00 | 1073.0 |
| 353.15 | 2080.00 | 1073.3 |
| 353.15 | 3040.00 | 1073.8 |
| 353.15 | 5060.00 | 1074.9 |
| 353.15 | 7020.00 | 1076.0 |
| 353.15 | 9970.00 | 1077.5 |
| 353.15 | 14830.00 | 1080.1 |
| 353.15 | 19740.00 | 1082.6 |
| 353.15 | 24680.00 | 1085.1 |
| 353.15 | 29560.00 | 1087.5 |
| 353.15 | 34550.00 | 1089.8 |
| 353.15 | 39420.00 | 1092.1 |
| 353.15 | 44280.00 | 1094.3 |
| 353.15 | 49230.00 | 1096.5 |
| 353.15 | 54110.00 | 1098.7 |
| 353.15 | 59020.00 | 1100.8 |
| 353.15 | 64010.00 | 1102.9 |
| 353.15 | 68770.00 | 1104.8 |
| 363.08 | 100.00 | 1064.5 |
| 363.08 | 100.00 | 1064.4 |
| 363.08 | 620.00 | 1064.7 |
| 363.08 | 1110.00 | 1065.0 |
| 363.08 | 1570.00 | 1065.2 |
| 363.08 | 2100.00 | 1065.5 |
| 363.08 | 3020.00 | 1066.0 |
| 363.08 | 5070.00 | 1067.2 |
| 363.08 | 7000.00 | 1068.3 |
| 363.08 | 9970.00 | 1069.9 |
| 363.08 | 14840.00 | 1072.6 |
| 363.08 | 19750.00 | 1075.1 |
| 363.08 | 24660.00 | 1077.7 |
| 363.08 | 29610.00 | 1080.2 |
| 363.08 | 34480.00 | 1082.6 |
| 363.08 | 39400.00 | 1084.9 |
| 363.08 | 44290.00 | 1087.2 |
| 363.08 | 49160.00 | 1089.5 |
| 363.08 | 54110.00 | 1091.7 |
| 363.08 | 58990.00 | 1093.9 |
| 363.08 | 63880.00 | 1096.0 |
| 363.08 | 68760.00 | 1098.0 |
| Reference | ||
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 298.15 | 100.00 | 989.2 |
| Reference | ||
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.64] | kPa | [396.81; 548.09] |
The Yaw...
|
| Equation | ln(Pvp) = A + B/(T + C) | |||
| Coefficient A | 1.56166e+01 | |||
| Coefficient B | -4.75686e+03 | |||
| Coefficient C | -8.64930e+01 | |||
| Temperature range, min. | 396.81 | |||
| Temperature range, max. | 548.09 | |||
|
T(K) Vapor pressure (kPa) 0 50 100 150 200 400 450 500 550 | ||||
| Pvap | 1.33 | kPa | 396.81 | Calculated Property |
| Pvap | 2.93 | kPa | 413.62 | Calculated Property |
| Pvap | 5.97 | kPa | 430.43 | Calculated Property |
| Pvap | 11.36 | kPa | 447.24 | Calculated Property |
| Pvap | 20.44 | kPa | 464.05 | Calculated Property |
| Pvap | 34.97 | kPa | 480.85 | Calculated Property |
| Pvap | 57.26 | kPa | 497.66 | Calculated Property |
| Pvap | 90.19 | kPa | 514.47 | Calculated Property |
| Pvap | 137.28 | kPa | 531.28 | Calculated Property |
| Pvap | 202.64 | kPa | 548.09 | Calculated Property |
| Pvap | [1.07e-05; 4415.80] | kPa | [262.70; 744.60] |
KDB Vap...
|
| Equation | ln(Pvp) = A + B/T + C*ln(T) + D*T^2 | |||
| Coefficient A | 1.08791e+02 | |||
| Coefficient B | -1.28556e+04 | |||
| Coefficient C | -1.28373e+01 | |||
| Coefficient D | 3.16995e-06 | |||
| Temperature range, min. | 262.70 | |||
| Temperature range, max. | 744.60 | |||
|
T(K) Vapor pressure (kPa) 0 1000 2000 3000 4000 400 600 | ||||
| Pvap | 1.07e-05 | kPa | 262.70 | Calculated Property |
| Pvap | 4.34e-03 | kPa | 316.24 | Calculated Property |
| Pvap | 0.24 | kPa | 369.79 | Calculated Property |
| Pvap | 3.86 | kPa | 423.33 | Calculated Property |
| Pvap | 29.48 | kPa | 476.88 | Calculated Property |
| Pvap | 135.63 | kPa | 530.42 | Calculated Property |
| Pvap | 439.99 | kPa | 583.97 | Calculated Property |
| Pvap | 1115.30 | kPa | 637.51 | Calculated Property |
| Pvap | 2367.36 | kPa | 691.06 | Calculated Property |
| Pvap | 4415.80 | kPa | 744.60 | Calculated Property |
Similar Compounds
![2-[2-[2-[2-[2-[2-[2-[2-[2-[2-[2-(2-Hydroxyethoxy)ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethanol.](data:image/png;base64,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)
![2-[2-[2-[2-[2-[2-[2-(2-Hydroxyethoxy)ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethanol.](data:image/png;base64,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)
![2-[2-[2-[2-[2-[2-(2-Methoxyethoxy)ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethanol.](data:image/png;base64,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)
![2-[2-[2-[2-[2-[2-[2-[2-[2-[2-(2-Methoxyethoxy)ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethanol.](data:image/png;base64,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)
Find more compounds similar to Ethanol, 2,2'-oxybis-.
Mixtures
- Benzene, nitro- + Ethanol, 2,2'-oxybis-
- 1-Butanol + Ethanol, 2,2'-oxybis-
- 1,4-Butanediol + Ethanol, 2,2'-oxybis-
- Ethanol, 2,2'-oxybis- + Thiophene, tetrahydro-, 1,1-dioxide
- 1,2-Ethanediol + Ethanol, 2,2'-oxybis-
- Triethylene glycol + Ethanol, 2,2'-oxybis-
- 1,2-Ethanediol + Triethylene glycol + Ethanol, 2,2'-oxybis-
- Nitrogen + Sulfur dioxide + Ethanol, 2,2'-oxybis-
- Formamide, N,N-dimethyl- + Ethanol, 2,2'-oxybis-
- Sulfur dioxide + Ethanol, 2,2'-oxybis-
- Formamide, N,N-dimethyl- + Sulfur dioxide + Ethanol, 2,2'-oxybis-
- Toluene + Decane + Ethanol, 2,2'-oxybis-
- Ethanol, 2,2'-oxybis- + lithium chloride + Water
- lithium bromide + Ethanol, 2,2'-oxybis- + Water
- Ethanol, 2,2'-oxybis- + Tromethamine + Water
- Ethanol, 2,2'-oxybis- + Pentane
- n-Hexane + Ethanol, 2,2'-oxybis-
- Heptane + Ethanol, 2,2'-oxybis-
- Octane + Ethanol, 2,2'-oxybis-
- Ethanol, 2,2'-oxybis- + Nonane
Find more mixtures with Ethanol, 2,2'-oxybis-.
Sources
- KDB Vapor Pressure Data
- Crippen Method
- Crippen Method
- Application of the Multi-Current Transient Hot-Wire Technique for Absolute Measurements of the Thermal Conductivity of Glycols
- Thermophysical Properties For Diethylene Glycol + Nitrobenzene and Triethylene Glycol + (Chloro-, Bromo-, Nitro-) Benzene Systems at Different Temperatures
- Densities, Ultrasonic Speeds, and Excess Properties of Binary Mixtures of Diethylene Glycol with 1-Butanol, 2-Butanol, and 1,4-Butanediol at Different Temperatures
- Mutual diffusion coefficients of aqueous solutions of some glycols
- Experimental study of the density and viscosity of polyethylene glycols and their mixtures at temperatures from 293 K to 465 K and at high pressures up to 245 MPa
- The effect of the end group, molecular weight and size on the solubility of compounds in supercritical carbon dioxide
- Experimental study and phase equilibrium modeling of systems containing acid gas and glycol
- Solubility for dilute sulfur dioxide, viscosities, excess properties, and viscous flow thermodynamics of binary system N, N-dimethylformamide + diethylene glycol
- Removal of aromatic hydrocarbons from hydrocarbon mixture using glycols at 303.15 K and 333.15 K and atmospheric pressure: Experimental and calculated data by NRTL and UNIQUAC models
- Thermodynamic properties and spectral investigation of dilute sulfur dioxide in binary system N,N-dimethylformamide + diethylene glycol
- Determination and modeling of binary and ternary solid-liquid phase equilibrium for the systems formed by adipic acid, urea and diethylene glycol
- Separation of methane/ethylene gas mixtures efficiently by using ZIF- 67/water-ethylene glycol slurry
- Liquid-liquid equilibrium in binary and ternary mixtures containing formaldehyde, water, methanol, methylal, and poly(oxymethylene) dimethyl ethers
- New measurements and modeling of high pressure thermodynamic properties of glycols
- Critical temperatures and pressures of ethylene glycols
- Viscosity of liquid diethylene, triethylene and tetraethylene glycols at moderately high pressures using a vibrating wire instrument
- Separation of thiophene, or benzothiophene from model fuel using glycols. Liquid-liquid phase equilibria and oxidative desulfurization study
- Effective extraction of benzene and thiophene by novel deep eutectic solvents from hexane / aromatic mixture at different temperatures
- The experimental study on the influence of crown ethers and glycols on the mutual solubility of lithium bromide in water
- Vapour pressures and densities of the mixed-solvent desiccants (glycols + water + salts)
- Densities and vapor pressures of mixed-solvent desiccant systems containing {glycol (diethylene, or triethylene, or tetraethylene glycol) + salt (magnesium chloride) + water}
- Experimental and predicted refractive index properties in ternary mixtures of associated liquids
- Experimental study of the density and viscosity of polyethylene glycols and their mixtures at temperatures from 293 K to 473 K and at atmospheric pressure
- Molar heat capacities of some aqueous 2-amino-2-hydroxymethyl-1,3-propanediol + glycol systems
- Thermophysical property characterization of ternary system containing {glycol (DEG/TEG/T4EG) + 2-amino-2-hydroxymethyl-1,3-propanediol + water}
- Activity coefficients at infinite dilution of organic solutes in diethylene glycol and triethylene glycol from gas-liquid chromatography
- Solubilities and thermodynamic properties of CO2 in choline-chloride based deep eutectic solvents
- Liquid-liquid equilibria for ternary systems polyoxymethylene dimethyl ethers + para-xylene + water
- Activity coefficients at infinite dilution of hydrocarbons in glycols: Experimental data and thermodynamic modeling with the GCA-EoS
- Binary and ternary solid-liquid phase equilibrium for the systems formed by succinic acid, urea and diethylene glycol: Determination and modelling
- Measurement and correlation of physicochemical properties of phosphonium-based deep eutectic solvents at several temperatures (293.15 K - 343.15 K) for CO2 capture
- Densities and viscosities for binary mixtures of polyoxymethylene dimethyl ethers with different CH2O chain length n = 2, 3, 4 at different temperatures
- Thermal stability analysis, experimental conductivity and pH of phosphonium-based deep eutectic solvents and their prediction by a new empirical equation
- Thermodynamics properties of binary mixtures of aqueous solutions of glycols at several temperatures and atmospheric pressure
- Phase equilibria study on bromide-based ionic liquids with glycols and sulfolane. Experimental data and correlation
- Volumetric and ultrasonic studies on interactions of ethylene glycol, diethylene glycol and triethylene glycol in aqueous solutions of glycerol at temperatures T = (293.15 K - 308.15) K
- Acoustic and thermodynamic study of D-Panthenol in aqueous solutions of glycol at different temperatures
- Solubility of dibenzothiophene in nine organic solvents: Experimental measurement and thermodynamic modelling
- Excess molar enthalpies of binary mixtures containing ethylene glycols or poly(ethylene glycols) + ethyl alcohol at 308.15K and atmospheric pressure
- Heat capacities of the mixed-solvents desiccants (glycols +water + salts)
- Experimental and predicted excess molar enthalpies of some working pairs for absorption cycles
- 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
- Density, viscosity, surface tension, and spectroscopic properties for binary system of 1,2-ethanediamine + diethylene glycol
- Partial Molar Volumes and Partial Molar Isentropic Compressions of Four Poly(Ethylene Glycols) at Infinite Dilution in Water at Temperatures T = (278 to 343) K and Atmospheric Pressure
- Thermophysical properties of glycols and glymes
- Solubility of 2-Ethylanthraquinone in Binary Mixtures of Oligooxymethylene Dimethyl Ethers with Different Number of CH2O Groups of n = 2, 3, and 4 from 293.15 to 343.15 K
- Investigation on Temperature-Dependent Volumetric and Acoustical Properties of Homologous Series of Glycols in Aqueous Sorbitol Solutions
- Solubility of Carbon Dioxide in Poly(oxymethylene) Dimethyl Ethers
- Measurement and Modeling of Isobaric Vapor-Liquid Equilibrium of Water + Glycols
- Thermodynamic and Kinetic Studies of CO2 Capture by Glycol and Amine-Based Deep Eutectic Solvents
- Thermodynamic Interactions Study of Some Ethylene Glycols in Aqueous Aniline Solutions at Different Temperatures: An Acoustical and Volumetric Approach
- Solubility of Acetylene in Alcohols and Ketones
- Effect of Ethylene, Diethylene, and Triethylene Glycols and Glycerol on the Physicochemical Properties and Phase Behavior of Benzyltrimethyl and Benzyltributylammonium Chloride Based Deep Eutectic Solvents at 283.15-343.15 K
- Measurement and Thermodynamic Models for Ternary Liquid-Liquid Equilibrium Systems {Water + Polyoxymethylene Dimethyl Ethers +4-Methyl-2-pentanol} at Different Temperatures
- Experimental Isobaric Vapor Liquid Equilibrium for Binary Systems Diethylene Glycol Dibenzoate + Diethylene Glycol, Diethylene Glycol Dibenzoate + Octyl Benzoate, and Ternary System Diethylene Glycol Dibenzoate + Diethylene Glycol + Octyl Benzoate at 1.0152 kPa
- Liquid-Liquid Equilibrium for Ternary Systems of Polyoxymethylene Dimethyl Ethers + o-Xylene + Water at 293.15 K
- Solubility of 4-Chloro-2,5-dimethoxynitrobenzene, 4-Chloro-2,5-dimethoxyaniline, and 2,5-Dimethoxyaniline in Binary and Pure Solvents: Determination and Modeling
- Salting Effect of Sodium Hydroxide and Sodium Formate on the Liquid-Liquid Equilibrium of Polyoxymethylene Dimethyl Ethers in Aqueous Solution
- Liquid-Liquid Equilibria for Benzene/Thiophene + Cyclohexane/Hexadecane + Deep Eutectic Solvents: Data and Correlation
- Experimental and Correlated Liquid-Liquid Equilibrium Data for Ternary Systems (Water + Poly(oxymethylene) Dimethyl Ethers + Toluene) at T = 293.15 and 303.15 K and p = 101.3 kPa
- Densities, Viscosities, and Excess Properties for Binary Mixtures of Some Glycols and Polyglycols in N-Methylacetamide at 308.15 K
- Density, Viscosity and Thermal Conductivity of Aqueous Ethylene, Diethylene and Triethylene Glycol Mixtures between 290 K and 450 K
- 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
- Thermodynamic Study of Binary Mixtures Containing Glycols or Polyethylene Glycols + Benzyl Alcohol at 308.15 K
- Liquid-Liquid Equilibrium for the System Heptane + o-Xylene + Diethylene Glycol over the Temperature Range of 288.15 K to 318.15 K
- 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
- Solubility of Ethane in Diethylene Glycol
- Excess Molar Enthalpies and Hydrogen Bonding in Binary Mixtures Containing Ethers and Benzyl Alcohol at 308.15 K and Atmospheric Pressure
- Densities, Viscosities, and Surface Tensions of the System Water + Diethylene Glycol
- Densities and Viscosities of Binary Mixtures Containing Diethylene Glycol and 2-Alkanol
- Measurement and Correlation of the Solubility of Disodium 4,4?-Dinitrostilbene-2,2?-disulfonate in Aqueous Organic Solutions
- Measurement and Prediction of Excess Enthalpies for Ternary Solutions 1-Ethyl-3-methylimidazolium Dimethylphosphate + Methanol or Ethanol + Water at 298.15 K and at Normal Atmospheric Pressure
- Isobaric Vapor-Liquid Equilibrium for Four Binary Systems of Ethane-1,2-diol, Butane-1,4-diol, 2-(2- Hydroxyethoxy)ethan-1-ol and 2-[2-(2- Hydroxyethoxy)ethoxy]ethanol at 10.0 kPa, 20.0 kPa and 40.0 kPa
- Solubility of CO2 in Nonaqueous Absorption System of 2-(2-Aminoethylamine)ethanol + Benzyl Alcohol
- Density, Viscosities, and Excess Properties for Binary Mixtures of Sulfolane + Alcohols and Sulfolane + Glycols at Different Temperatures
- Liquid-Liquid Equilibria of (Limonene + Linalool + Ethylene Glycol or Diethylene Glycol or Triethylene Glycol or 1,2-Propylene Glycol) Ternary Systems
- Supplementary Densities and Viscosities of Aqueous Solutions of Diethylene Glycol from (283.15 to 353.15) K
- Solubility Comparison of Bis(2-hydroxyethyl) Ether and Tetraethylene Glycol before and after End-Group Modification by Ethyl Oxalyl Chloride in Supercritical Carbon Dioxide
- Joback Method
- KDB
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
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