- InChI
- InChI=1S/C4H10O2/c1-2-6-4-3-5/h5H,2-4H2,1H3
- InChI Key
- ZNQVEEAIQZEUHB-UHFFFAOYSA-N
- Formula
- C4H10O2
- SMILES
- CCOCCO
- Molecular Weight1
- 90.12
- CAS
- 110-80-5
- Other Names
-
- 1,2-ethanediol, monoethyl ether
- 2-Ethoxyethanol
- 2-Ethoxyethyl alcohol
- 2-ethoxyethan-1-ol
- 2-ethoxyethanol (cellosolve)
- 2EE
- 3-oxa-1-pentanol
- Bikanol E 1
- Cellosolve
- Cellosolve solvent
- Dowanol EE
- EE solvent
- EGEE
- Ektasolve EE
- Emkanol
- Ether monoethylique de l'ethylene-glycol
- Ethoxyethanol
- Ethyl cellosolve
- Ethyl glycol
- Ethyl icinol
- Ethyl-2-hydroxyethyl ether
- Ethylene glycol ethyl ether
- Ethylene glycol monoethyl ether
- Ethylethylene glycol
- Etoksyetylowy alkohol
- Glycol ether EE
- Glycol ethyl ether
- Glycol monoethyl ether
- HOCH2CH2OC2H5
- Hydroxy ether
- Jeffersol EE
- NCI-C54853
- NSC 8837
- Oxitol
- Plastiazan 60
- Poly-Solv EE
- Solvid
- ethylene glycol, monoethyl ether
- «beta»-Ethoxyethanol
- «beta»-Ethoxyethanol
- 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).
- 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).
- 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.
- csound,fluid : Speed of sound in fluid (m/s).
- Tboil : Normal Boiling Point Temperature (K).
- Tc : Critical Temperature (K).
- Tfus : Normal melting (fusion) point (K).
- Vc : Critical Volume (m3/kmol).
- Vm : Molar Volume (m3/mol).
- 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 |
|---|---|---|---|
| η | 0.0018450 | Pa×s | Conduct... |
| ΔfG° | -259.02 | kJ/mol | Joback Calculated Property |
| ΔfH°gas | -410.34 | kJ/mol | Joback Calculated Property |
| ΔfusH° | 11.39 | kJ/mol | Joback Calculated Property |
| ΔvapH° | [48.20; 50.00] | kJ/mol |
|
| ΔvapH° | 48.23 | kJ/mol | NIST |
| ΔvapH° | 49.40 | kJ/mol | NIST |
| ΔvapH° | 50.00 | kJ/mol | NIST |
| ΔvapH° | 48.20 ± 0.10 | kJ/mol | NIST |
| ΔvapH° | 49.20 | kJ/mol | NIST |
| IE | [9.60; 9.97] | eV |
|
| IE | 9.60 | eV | NIST |
| IE | 9.97 | eV | NIST |
| log10WS | 0.15 | Crippen Calculated Property | |
| logPoct/wat | 0.015 | Crippen Calculated Property | |
| McVol | 78.960 | ml/mol | McGowan Calculated Property |
| Pc | 4288.66 | kPa | Joback Calculated Property |
| Inp | [666.00; 743.50] |
|
|
| Inp | 687.00 | NIST | |
| Inp | 671.00 | NIST | |
| Inp | 694.00 | NIST | |
| Inp | 666.00 | NIST | |
| Inp | 670.00 | NIST | |
| Inp | 718.00 | NIST | |
| Inp | 708.00 | NIST | |
| Inp | 716.00 | NIST | |
| Inp | Outlier 743.50 | NIST | |
| Inp | 702.00 | NIST | |
| Inp | 702.00 | NIST | |
| Inp | 695.00 | NIST | |
| Inp | 702.00 | NIST | |
| Inp | 695.00 | NIST | |
| Inp | 716.50 | NIST | |
| Inp | 694.00 | NIST | |
| Inp | 694.00 | NIST | |
| Inp | 701.00 | NIST | |
| Inp | 701.00 | NIST | |
| Inp | 695.00 | NIST | |
| I | [1218.00; 1266.00] |
|
|
| I | 1231.00 | NIST | |
| I | 1266.00 | NIST | |
| I | 1246.00 | NIST | |
| I | 1239.00 | NIST | |
| I | 1239.00 | NIST | |
| I | 1218.00 | NIST | |
| Tboil | [407.80; 408.62] | K |
|
| Tboil | 408.62 | K | Isobari... |
| Tboil | 408.19 | K | Vapour-... |
| Tboil | 407.80 | K | Vapor L... |
| Tboil | 408.35 | K | Isobari... |
| Tc | 568.04 | K | Joback Calculated Property |
| Tfus | 217.89 | K | Joback Calculated Property |
| Vc | 0.296 | m3/kmol | Joback Calculated Property |
| Vm | 9.74e-05 | m3/mol | Excess ... |
Temperature Dependent Properties
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [154.66; 193.38] | J/mol×K | [405.52; 568.04] |
|
| Cp,gas | 154.66 | J/mol×K | 405.52 | Joback Calculated Property |
| Cp,gas | 161.57 | J/mol×K | 432.61 | Joback Calculated Property |
| Cp,gas | 168.30 | J/mol×K | 459.69 | Joback Calculated Property |
| Cp,gas | 174.85 | J/mol×K | 486.78 | Joback Calculated Property |
| Cp,gas | 181.21 | J/mol×K | 513.87 | Joback Calculated Property |
| Cp,gas | 187.39 | J/mol×K | 540.95 | Joback Calculated Property |
| Cp,gas | 193.38 | J/mol×K | 568.04 | Joback Calculated Property |
| Cp,liquid | [203.30; 226.50] | J/mol×K | [275.15; 339.15] |
|
| Cp,liquid | 203.30 | J/mol×K | 275.15 | Measure... |
| Cp,liquid | 204.00 | J/mol×K | 277.15 | Measure... |
| Cp,liquid | 204.60 | J/mol×K | 279.15 | Measure... |
| Cp,liquid | 205.30 | J/mol×K | 281.15 | Measure... |
| Cp,liquid | 205.90 | J/mol×K | 283.15 | Measure... |
| Cp,liquid | 206.60 | J/mol×K | 285.15 | Measure... |
| Cp,liquid | 207.30 | J/mol×K | 287.15 | Measure... |
| Cp,liquid | 208.00 | J/mol×K | 289.15 | Measure... |
| Cp,liquid | 208.60 | J/mol×K | 291.15 | Measure... |
| Cp,liquid | 209.30 | J/mol×K | 293.15 | Measure... |
| Cp,liquid | 210.00 | J/mol×K | 295.15 | Measure... |
| Cp,liquid | 210.70 | J/mol×K | 297.15 | Measure... |
| Cp,liquid | 211.10 | J/mol×K | 298.15 | Measure... |
| Cp,liquid | 210.50 | J/mol×K | 298.15 | NIST |
| Cp,liquid | 209.82 | J/mol×K | 298.15 | NIST |
| Cp,liquid | 210.80 | J/mol×K | 298.15 | NIST |
| Cp,liquid | 211.40 | J/mol×K | 299.15 | Measure... |
| Cp,liquid | 212.10 | J/mol×K | 301.15 | Measure... |
| Cp,liquid | 212.80 | J/mol×K | 303.15 | Measure... |
| Cp,liquid | 213.60 | J/mol×K | 305.15 | Measure... |
| Cp,liquid | 214.30 | J/mol×K | 307.15 | Measure... |
| Cp,liquid | 215.00 | J/mol×K | 309.15 | Measure... |
| Cp,liquid | 215.70 | J/mol×K | 311.15 | Measure... |
| Cp,liquid | 216.50 | J/mol×K | 313.15 | Measure... |
| Cp,liquid | 217.20 | J/mol×K | 315.15 | Measure... |
| Cp,liquid | 218.00 | J/mol×K | 317.15 | Measure... |
| Cp,liquid | 218.70 | J/mol×K | 319.15 | Measure... |
| Cp,liquid | 219.50 | J/mol×K | 321.15 | Measure... |
| Cp,liquid | 220.20 | J/mol×K | 323.15 | Measure... |
| Cp,liquid | 221.00 | J/mol×K | 325.15 | Measure... |
| Cp,liquid | 221.80 | J/mol×K | 327.15 | Measure... |
| Cp,liquid | 222.60 | J/mol×K | 329.15 | Measure... |
| Cp,liquid | 223.30 | J/mol×K | 331.15 | Measure... |
| Cp,liquid | 224.10 | J/mol×K | 333.15 | Measure... |
| Cp,liquid | 224.90 | J/mol×K | 335.15 | Measure... |
| Cp,liquid | 225.70 | J/mol×K | 337.15 | Measure... |
| Cp,liquid | 226.50 | J/mol×K | 339.15 | Measure... |
| η | [0.0014070; 0.0021420] | Pa×s | [293.15; 308.15] |
|
| η | 0.0021420 | Pa×s | 293.15 | Viscosi... |
| η | 0.0018480 | Pa×s | 298.15 | Viscosi... |
| η | 0.0018500 | Pa×s | 298.15 | Densiti... |
| η | 0.0016460 | Pa×s | 303.15 | Viscosi... |
| η | 0.0014070 | Pa×s | 308.15 | Densiti... |
| ΔvapH | [39.22; 47.40] | kJ/mol | [338.00; 408.10] |
|
| ΔvapH | 45.90 | kJ/mol | 338.00 | NIST |
| ΔvapH | 47.40 | kJ/mol | 347.50 | NIST |
| ΔvapH | 44.70 | kJ/mol | 372.00 | NIST |
| ΔvapH | 39.22 | kJ/mol | 408.10 | NIST |
| Pvap | [1.30; 101.33] | kPa | [308.15; 407.80] |
|
| Pvap | 1.30 | kPa | 308.15 | Total V... |
| Pvap | 1.83 | kPa | 313.15 | Total V... |
| Pvap | 1.80 | kPa | 313.15 | Total V... |
| Pvap | 1.86 | kPa | 313.15 | Total V... |
| Pvap | 5.30 | kPa | 333.15 | Vapor-L... |
| Pvap | 8.65 | kPa | 343.15 | Vapor-L... |
| Pvap | 13.62 | kPa | 353.15 | Vapor-L... |
| Pvap | 28.10 | kPa | 373.48 | Vapor-l... |
| Pvap | 34.20 | kPa | 378.36 | Vapor-l... |
| Pvap | 41.30 | kPa | 383.18 | Vapor-l... |
| Pvap | 47.90 | kPa | 387.06 | Vapor-l... |
| Pvap | 53.33 | kPa | 388.60 | Vapor L... |
| Pvap | 53.70 | kPa | 390.12 | Vapor-l... |
| Pvap | 60.50 | kPa | 393.37 | Vapor-l... |
| Pvap | 69.33 | kPa | 396.10 | Vapor L... |
| Pvap | 68.60 | kPa | 396.86 | Vapor-l... |
| Pvap | 76.40 | kPa | 399.90 | Vapor-l... |
| Pvap | 80.00 | kPa | 400.40 | Vapor L... |
| Pvap | 81.20 | kPa | 401.65 | Vapor-l... |
| Pvap | 85.33 | kPa | 402.30 | Vapor L... |
| Pvap | 90.66 | kPa | 404.20 | Vapor L... |
| Pvap | 88.70 | kPa | 404.22 | Vapor-l... |
| Pvap | 93.30 | kPa | 406.20 | Estimat... |
| Pvap | 95.30 | kPa | 406.33 | Vapor-l... |
| Pvap | 93.30 | kPa | 406.90 | Estimat... |
| Pvap | 100.93 | kPa | 407.50 | Vapor L... |
| Pvap | 93.60 | kPa | 407.80 | Estimat... |
| Pvap | 101.33 | kPa | 407.80 | Vapor L... |
| Pvap | 100.93 | kPa | 407.80 | Vapor L... |
| n0 | [1.40570; 1.40650] | [293.15; 303.15] |
|
|
| n0 | 1.40650 | 293.15 | Solubil... | |
| n0 | 1.40650 | 293.15 | Solubil... | |
| n0 | 1.40650 | 293.15 | Solubil... | |
| n0 | 1.40620 | 298.15 | Phase e... | |
| n0 | 1.40580 | 298.15 | Thermod... | |
| n0 | 1.40570 | 298.15 | Volumet... | |
| n0 | 1.40650 | 303.15 | Densiti... | |
| ρl | [856.30; 941.20] | kg/m3 | [283.15; 373.15] |
|
| ρl | 941.20 | kg/m3 | 283.15 | Thermop... |
| ρl | 936.70 | kg/m3 | 288.15 | Thermop... |
| ρl | 936.80 | kg/m3 | 288.15 | Thermop... |
| ρl | 929.50 | kg/m3 | 293.15 | Density... |
| ρl | 929.70 | kg/m3 | 293.15 | Viscosi... |
| ρl | 932.20 | kg/m3 | 293.15 | Thermop... |
| ρl | 929.70 | kg/m3 | 293.15 | Solubil... |
| ρl | 932.30 | kg/m3 | 293.15 | Thermop... |
| ρl | 925.10 | kg/m3 | 298.10 | Excess ... |
| ρl | 927.60 | kg/m3 | 298.15 | Thermop... |
| ρl | 927.70 | kg/m3 | 298.15 | Thermop... |
| ρl | 925.54 | kg/m3 | 298.15 | Study o... |
| ρl | 926.00 | kg/m3 | 298.15 | An expe... |
| ρl | 925.00 | kg/m3 | 298.15 | Density... |
| ρl | 925.64 | kg/m3 | 298.15 | Thermod... |
| ρl | 924.92 | kg/m3 | 298.15 | Excess ... |
| ρl | 925.36 | kg/m3 | 298.15 | FT-IR s... |
| ρl | 925.20 | kg/m3 | 298.15 | Solubil... |
| ρl | 923.10 | kg/m3 | 303.15 | Thermop... |
| ρl | 923.10 | kg/m3 | 303.15 | Thermop... |
| ρl | 920.70 | kg/m3 | 303.15 | Solubil... |
| ρl | 920.72 | kg/m3 | 303.15 | FT-IR s... |
| ρl | 920.99 | kg/m3 | 303.15 | Study o... |
| ρl | 921.19 | kg/m3 | 303.15 | Intermo... |
| ρl | 920.50 | kg/m3 | 303.15 | Density... |
| ρl | 921.00 | kg/m3 | 303.15 | An expe... |
| ρl | 916.10 | kg/m3 | 308.15 | Solubil... |
| ρl | 916.41 | kg/m3 | 308.15 | Study o... |
| ρl | 917.00 | kg/m3 | 308.15 | An expe... |
| ρl | 918.50 | kg/m3 | 308.15 | Thermop... |
| ρl | 916.43 | kg/m3 | 308.15 | Intermo... |
| ρl | 916.11 | kg/m3 | 308.15 | FT-IR s... |
| ρl | 915.90 | kg/m3 | 308.15 | Density... |
| ρl | 918.50 | kg/m3 | 308.15 | Thermop... |
| ρl | 916.00 | kg/m3 | 308.50 | Excess ... |
| ρl | 911.80 | kg/m3 | 313.15 | Study o... |
| ρl | 911.58 | kg/m3 | 313.15 | Intermo... |
| ρl | 911.47 | kg/m3 | 313.15 | FT-IR s... |
| ρl | 912.00 | kg/m3 | 313.15 | An expe... |
| ρl | 913.90 | kg/m3 | 313.15 | Thermop... |
| ρl | 911.30 | kg/m3 | 313.15 | Density... |
| ρl | 911.50 | kg/m3 | 313.15 | Solubil... |
| ρl | 913.80 | kg/m3 | 313.15 | Thermop... |
| ρl | 909.30 | kg/m3 | 318.15 | Thermop... |
| ρl | 906.60 | kg/m3 | 318.15 | Density... |
| ρl | 907.00 | kg/m3 | 318.15 | An expe... |
| ρl | 907.76 | kg/m3 | 318.15 | Intermo... |
| ρl | 907.15 | kg/m3 | 318.15 | Study o... |
| ρl | 906.80 | kg/m3 | 318.15 | Solubil... |
| ρl | 906.90 | kg/m3 | 318.15 | FT-IR s... |
| ρl | 904.50 | kg/m3 | 323.15 | Thermop... |
| ρl | 902.46 | kg/m3 | 323.15 | Study o... |
| ρl | 901.90 | kg/m3 | 323.15 | Density... |
| ρl | 904.60 | kg/m3 | 323.15 | Thermop... |
| ρl | 902.10 | kg/m3 | 323.15 | Solubil... |
| ρl | 903.45 | kg/m3 | 323.15 | Intermo... |
| ρl | 899.90 | kg/m3 | 328.15 | Thermop... |
| ρl | 897.20 | kg/m3 | 328.15 | Density... |
| ρl | 897.40 | kg/m3 | 328.15 | Solubil... |
| ρl | 892.40 | kg/m3 | 333.15 | Density... |
| ρl | 892.60 | kg/m3 | 333.15 | Solubil... |
| ρl | 895.10 | kg/m3 | 333.15 | Thermop... |
| ρl | 895.00 | kg/m3 | 333.15 | Thermop... |
| ρl | 887.60 | kg/m3 | 338.15 | Density... |
| ρl | 890.40 | kg/m3 | 338.15 | Thermop... |
| ρl | 882.70 | kg/m3 | 343.15 | Density... |
| ρl | 885.20 | kg/m3 | 343.15 | Thermop... |
| ρl | 885.50 | kg/m3 | 343.15 | Thermop... |
| ρl | 880.70 | kg/m3 | 348.15 | Thermop... |
| ρl | 877.80 | kg/m3 | 348.15 | Density... |
| ρl | 875.80 | kg/m3 | 353.15 | Thermop... |
| ρl | 872.80 | kg/m3 | 353.15 | Density... |
| ρl | 871.00 | kg/m3 | 358.15 | Thermop... |
| ρl | 866.10 | kg/m3 | 363.15 | Thermop... |
| ρl | 861.20 | kg/m3 | 368.15 | Thermop... |
| ρl | 856.30 | kg/m3 | 373.15 | Thermop... |
| csound,fluid | [1224.90; 1290.40] | m/s | [303.15; 323.15] |
|
| csound,fluid | 1290.40 | m/s | 303.15 | Acousti... |
| csound,fluid | 1287.10 | m/s | 303.15 | Densiti... |
| csound,fluid | 1268.00 | m/s | 308.15 | Densiti... |
| csound,fluid | 1257.30 | m/s | 313.15 | Acousti... |
| csound,fluid | 1252.00 | m/s | 313.15 | Densiti... |
| csound,fluid | 1235.10 | m/s | 318.15 | Densiti... |
| csound,fluid | 1224.90 | m/s | 323.15 | Acousti... |
Datasets
Viscosity, Pa*s
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Viscosity, Pa*s - Liquid |
| 293.15 | 20000.00 | 0.0024 |
| 293.15 | 40000.00 | 0.0028 |
| 293.15 | 60000.00 | 0.0031 |
| 293.15 | 80000.00 | 0.0035 |
| 293.15 | 100000.00 | 0.0039 |
| 303.15 | 20000.00 | 0.0019 |
| 303.15 | 40000.00 | 0.0022 |
| 303.15 | 60000.00 | 0.0025 |
| 303.15 | 80000.00 | 0.0028 |
| 303.15 | 100000.00 | 0.0031 |
| 313.15 | 20000.00 | 0.0016 |
| 313.15 | 40000.00 | 0.0018 |
| 313.15 | 60000.00 | 0.0021 |
| 313.15 | 80000.00 | 0.0023 |
| 313.15 | 100000.00 | 0.0025 |
| 323.15 | 20000.00 | 0.0013 |
| 323.15 | 40000.00 | 0.0015 |
| 323.15 | 60000.00 | 0.0017 |
| 323.15 | 80000.00 | 0.0019 |
| 323.15 | 100000.00 | 0.0021 |
| 333.15 | 20000.00 | 0.0011 |
| 333.15 | 40000.00 | 0.0012 |
| 333.15 | 60000.00 | 0.0014 |
| 333.15 | 80000.00 | 0.0016 |
| 333.15 | 100000.00 | 0.0018 |
| 343.15 | 20000.00 | 0.0009 |
| 343.15 | 40000.00 | 0.0011 |
| 343.15 | 60000.00 | 0.0012 |
| 343.15 | 80000.00 | 0.0014 |
| 343.15 | 100000.00 | 0.0015 |
| 353.15 | 20000.00 | 0.0008 |
| 353.15 | 40000.00 | 0.0010 |
| 353.15 | 60000.00 | 0.0011 |
| 353.15 | 80000.00 | 0.0012 |
| 353.15 | 100000.00 | 0.0013 |
| Reference | ||
Mass density, kg/m3
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 293.15 | 100.00 | 929.6 |
| 293.15 | 5000.00 | 932.9 |
| 293.15 | 10000.00 | 936.2 |
| 293.15 | 15000.00 | 939.3 |
| 293.15 | 20000.00 | 942.4 |
| 293.15 | 25000.00 | 945.2 |
| 293.15 | 30000.00 | 948.2 |
| 293.15 | 35000.00 | 951.1 |
| 293.15 | 40000.00 | 953.7 |
| 293.15 | 45000.00 | 956.5 |
| 293.15 | 50000.00 | 959.0 |
| 293.15 | 55000.00 | 961.6 |
| 293.15 | 60000.00 | 964.0 |
| 303.15 | 100.00 | 920.7 |
| 303.15 | 5000.00 | 924.0 |
| 303.15 | 10000.00 | 927.4 |
| 303.15 | 15000.00 | 930.7 |
| 303.15 | 20000.00 | 933.9 |
| 303.15 | 25000.00 | 937.0 |
| 303.15 | 30000.00 | 939.9 |
| 303.15 | 35000.00 | 942.9 |
| 303.15 | 40000.00 | 945.8 |
| 303.15 | 45000.00 | 948.6 |
| 303.15 | 50000.00 | 951.3 |
| 303.15 | 55000.00 | 953.8 |
| 303.15 | 60000.00 | 956.3 |
| 313.15 | 100.00 | 911.3 |
| 313.15 | 5000.00 | 914.9 |
| 313.15 | 10000.00 | 918.5 |
| 313.15 | 15000.00 | 922.1 |
| 313.15 | 20000.00 | 925.5 |
| 313.15 | 25000.00 | 928.7 |
| 313.15 | 30000.00 | 931.8 |
| 313.15 | 35000.00 | 934.9 |
| 313.15 | 40000.00 | 937.8 |
| 313.15 | 45000.00 | 940.7 |
| 313.15 | 50000.00 | 943.4 |
| 313.15 | 55000.00 | 946.1 |
| 313.15 | 60000.00 | 948.9 |
| 323.15 | 100.00 | 901.8 |
| 323.15 | 5000.00 | 905.8 |
| 323.15 | 10000.00 | 909.7 |
| 323.15 | 15000.00 | 913.4 |
| 323.15 | 20000.00 | 916.9 |
| 323.15 | 25000.00 | 920.3 |
| 323.15 | 30000.00 | 923.6 |
| 323.15 | 35000.00 | 926.9 |
| 323.15 | 40000.00 | 930.0 |
| 323.15 | 45000.00 | 933.0 |
| 323.15 | 50000.00 | 935.7 |
| 323.15 | 55000.00 | 938.7 |
| 323.15 | 60000.00 | 941.4 |
| 333.15 | 100.00 | 892.3 |
| 333.15 | 5000.00 | 896.5 |
| 333.15 | 10000.00 | 900.5 |
| 333.15 | 15000.00 | 904.5 |
| 333.15 | 20000.00 | 908.2 |
| 333.15 | 25000.00 | 911.8 |
| 333.15 | 30000.00 | 915.4 |
| 333.15 | 35000.00 | 918.7 |
| 333.15 | 40000.00 | 921.8 |
| 333.15 | 45000.00 | 925.0 |
| 333.15 | 50000.00 | 927.9 |
| 333.15 | 55000.00 | 931.1 |
| 333.15 | 60000.00 | 933.9 |
| 343.15 | 100.00 | 882.6 |
| 343.15 | 5000.00 | 887.2 |
| 343.15 | 10000.00 | 891.4 |
| 343.15 | 15000.00 | 895.6 |
| 343.15 | 20000.00 | 899.4 |
| 343.15 | 25000.00 | 903.4 |
| 343.15 | 30000.00 | 906.9 |
| 343.15 | 35000.00 | 910.5 |
| 343.15 | 40000.00 | 913.8 |
| 343.15 | 45000.00 | 917.2 |
| 343.15 | 50000.00 | 920.4 |
| 343.15 | 55000.00 | 923.4 |
| 343.15 | 60000.00 | 926.5 |
| 353.15 | 100.00 | 872.6 |
| 353.15 | 5000.00 | 877.6 |
| 353.15 | 10000.00 | 882.0 |
| 353.15 | 15000.00 | 886.5 |
| 353.15 | 20000.00 | 890.6 |
| 353.15 | 25000.00 | 894.8 |
| 353.15 | 30000.00 | 898.5 |
| 353.15 | 35000.00 | 902.0 |
| 353.15 | 40000.00 | 905.9 |
| 353.15 | 45000.00 | 908.8 |
| 353.15 | 50000.00 | 912.5 |
| 353.15 | 55000.00 | 915.7 |
| 353.15 | 60000.00 | 918.7 |
| Reference | ||
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.63] | kPa | [309.84; 430.65] |
The Yaw...
|
| Equation | ln(Pvp) = A + B/(T + C) | |||
| Coefficient A | 1.73172e+01 | |||
| Coefficient B | -4.91675e+03 | |||
| Coefficient C | -2.11200e+01 | |||
| Temperature range, min. | 309.84 | |||
| Temperature range, max. | 430.65 | |||
| Pvap | 1.33 | kPa | 309.84 | Calculated Property |
| Pvap | 2.84 | kPa | 323.26 | Calculated Property |
| Pvap | 5.68 | kPa | 336.69 | Calculated Property |
| Pvap | 10.72 | kPa | 350.11 | Calculated Property |
| Pvap | 19.26 | kPa | 363.53 | Calculated Property |
| Pvap | 33.11 | kPa | 376.96 | Calculated Property |
| Pvap | 54.71 | kPa | 390.38 | Calculated Property |
| Pvap | 87.28 | kPa | 403.80 | Calculated Property |
| Pvap | 134.90 | kPa | 417.23 | Calculated Property |
| Pvap | 202.63 | kPa | 430.65 | Calculated Property |
Similar Compounds
![Ethanol, 2-[2-(2-ethoxyethoxy)ethoxy]-.](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-[2-[2-[2-[2-(2-Hydroxyethoxy)ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethoxy]ethanol.](data:image/png;base64,iVBORw0KGgoAAAANSUhEUgAAAPoAAAD6CAIAAAAHjs1qAAAN4ElEQVR4nO3Ze0xUB97G8d9BEIY7itRrqSKCirquQcXFrV3jYlDaalWMG1LaooBacGNtKl0v1XXtmO0rpjEGXbcg2uoqWl0vrSDo2tBiK/UC1gs3CRZrHcSiyEV99o+D2g6M2W7q+77J7/n8RfSc84zMd+bMRAOAEOng9H/9AIj+9zB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEeZOijB3UoS5kyLMnRRh7qQIcydFmDspwtxJEWeHf7N4saxeLSKSliYzZ0pmpnh7S+/ekpDwxB/U11/L1q3i6Sl9+0p8/BOf++or+egj8fCQ4GCJi3vic0VFsnOnWCwycKDMmvXE5woLZc8ecXOTsDCJjX3ic//6l+zfL507y69+JdOmPfG5ggL55BNxdpbwcDlxQv7yF5EfpdseHJk7FzU1qKlBcjKSktDaCgDJyWhq6vDwe/fubdy48ejRo5s3b753756jqxYVFe3atWvNmjU2m83hdGIi7t5t+8Hcbefu3bsbNmwoKCjIzMx8zFxhYeGePXusVmtdXZ3DuTlzYF5h9mw4uFRra+v69esLCgq2bNly//59R1c6fvz43r17rVZrfX29w7nZs2FeISEBDi7V2tr6/vvvFxQUbNu27TFzx44d27dvn9VqvXnzpsO5hyuvvebokJaWlnXr1h05cmT79u2PmcvPz9+/f7/Vav3hhx8eN2dyPNfc3Lx27dojR47s3LnT4XWAvLy8gwcPWq3WW7du/Udzycltxc6d6+hwx7knJuKDD/DBB4iPR1JS2x++9RZKS1Fba3fsF198MWrUKBHp2bOniMwaPx7Hj9tf8MqVDYsWGYbh6ekpIn5+funp6a12Nbe04PTpR3NvvIFvvsF339ldqaCgYNiwYQ/nXomKQmGh/VxNzfsLFxqG4eXlJSJdunTpYK65+SdzCxbgwgVcu2Z3pfz8/KFDhz6cS4yORlGR/Vx19f8sWGAYhre3t4h07do1PT39rvmifaipCWfOPJqbPx+XLuH6dbsr5eXlDRkyRER69OghIq8//zy+/NJ+rqpqTUqKiPj4+Dicu3MHZ88+mps7F2VlaPcuk5ubGxYWJiLdu3cXkYVTp+LkSfu5iopV8+aZz5r5wDIyMuznGhtRUvJoLikJZWVo9y6Tm5s7ePDgh3OLp0/HqVP2c2Vly5OSzGfN/LVnZGTYv6ndvo3S0p/Mxce3FZuYaH/BBxznPm9e2w/z5yM9HTk5KCnBa69hyhR4edWvXdvU1ASgqqpqxowZ5o0iMDAwNTW1T58+FyIjYRiYMwfffoutW1FcjB074OlZ3bOnn69vQkLCuHHjzFPCwsLy8vLMnbrDhxESAn9/rFyJjz/GmTOYPRuTJ8PH58a6dc3NzQAqKipeeukl89y+ffumpqb26tWr/De/gWFg3jxcuYLsbHz9NbZtg4dHRZ8+fr6+c+bMGTt2rHnK0KFD8/Pzzbkbn3yCAQMQEIDly7F/P06fRmIioqLg63tj/fqWlhYAZWVlL774onluv379UlJSevbseXnMGBgGUlNRU4PsbJw+jawsuLtfCgz09fVNTEyMjIw0Txk+fPixY8fa5g4cQP/+6NEDS5fi0CGcOoWkJPzud/Dzq9uwwXwdXrx4MSYmxjy3f//+KSkp3bt3rxk9Gk5OeOMNVFcjOxtnzmDzZlgs3/TrZ85FRESYp4wYMeL4g3eZG/v2oV8/9O6Nt9/G4cMoLsbcufjtb9G1qy0jw5w7f/58dHS0ee6AAQNSUlICAgJqR46EkxMWL8bly8jORkkJMjLg5lbSv7+Pj09ycvLIkSPNU8LDwwsfvMvc2LMHzzyDwECkpeHIEXz1FV5/HRER8Pe3bd5svjDOnTsXFRVlnhsaGpqSktKtW7dr4eHo1AlLlqCyEtnZKC3F+vVwdT01YICvr29ycnJ4eLh5yujRo4uKigDcv3+/PicHTz+NoCC89RaOHsWJE0hNxfz59un+jNyLi3/yQ34+tm+HzYbnn4dIwtixQUFBM2fOtFgsIuLu7r5ixYrGxkYAt2/fvr98OSwWrFiB+HhUVMBqxaZNcHbGlCkNFRXmVXfv3h0UFGT+SyZMmPDcc8+N6dULFgtCQnDmDPLysGMHbDZMmgSRlyMjg4ODZ86c6ebmJiIeHh6rVq26c+cOgFu3bmHJEri5YdUqvPIKKiqwahU2bUKnTpg2raGqypzbtWtX3759zbmoqKhnn332uaefhqsrBg5ESQlyc/GPf+D6dUycCJFZY8aEhITExsa6urqKiJeX1+rVq82X962GBixeDDc3WK149VVUVuKdd9rmYmMbqqvNuR07dgQGBppzEydOHDt27O+feQadO2PwYJw7h08/xc6d+P57TJgAkekREaGhobGxsZ07dxYRb2/vNWvWmC/vhps38eabcHXFX/+KhARUVmLpUmzaBCcnzJrVUFNjPv0ffvhhnz59RMQwjOjo6MjIyJigIDg7Y8gQXLiAQ4ewaxeuXcP48RCZMmrUoEGDZsyY4eLiYt4f3nvvPfPl3VBfj4UL0bkz1q7FnDmorERaWttcXFzDlSvmXHZ2dq9evcy5SZMmRURETBswAJ06YdgwlJXh4EHk5ODqVYwbB5HJ4eFhYWHTpk0z58y7etvcjRtYsAAuLli3DklJqKrCm2+2zcXHN9TWmnOZmZnmjc4wjJiYmFGjRs0KDYWTE379a5SXY/9+7N6Nlhb7Yn9e7o7deXC37d27t4hMnjy56kFVj1y+jMOHsX07ADQ24o9/xKVLdoe0tLSkp6d7e3u7uLh06tTJx8enZONGtLTYHXb7008HDRpk3kMNw5g+ffrly5ft56qqcOAAcnIA4OZNLFrUfq65ufnHc35+ft/87W/t5xoOHQoNDf3xXPWDiB+prMTevdi3DwCuX0daWvu5xsbGd99918vLy9XV1cnJqUuXLhf//vf2X0XqDxwIDg4WkaeeesowjLi4uNp2nxVRUYGcHBw6BAC1tVi2zNGcp6enm5ubYRhdu3Ytz8qC3ecNoO6f/zTfZQICApycnOLi4q5evWo/V16OHTtg3nWrq/HnP7efu3379rJlyywWi7u7u2EY3bp1q9yypf3c9x9/bL7L+Pv7m3PftftoirIybN0K8zZYXg6r1dGcm5ubu7u7+buq3rrV0RetxzAAdPwd9rHu3r2blZU1cOBAERkzZkzHB509KwUFkpIilZXy0UeSltbhUbW1tcePH79379748eMDAgI6PKa1tTUrKys0NNTZ2Xn06NEdzxUXS1GRJCfLxYuyd68sWtThUVeuXPn888+bm5ujoqL8/f0dzWVmZoaEhFgsloc3U3tFRXL2rCQkSGmp5ObKggUdHlVTU3PixInGxsbo6Gjzk2h7LS0tWVlZISEhHh4eI0aM6Hjus8+kvFxefllOnZLPPpP58zs8qrq6+uTJkw0NDTExMebn7Paam5u3bNkSHBzs4+MzfPjwjucKCuTbb+UPf5Avv5TiYklM7PCoqqqq06dP19fXv/DCC76+vh0e09TUlJ2dHRQU5O/vb34F6sDhw1JfLzNmSGGhnD8vr77a4VEVFRWlpaU2m23q1Knmd6Sf67/M/T+1cqUYhtTVSVqaOGjrl7R8ubi4iM0mf/qTOGjrl7R0qbi6is0mS5eKgyf7FwPIkiVisUhdnSxbJv/Vk/3z5t5+Wzw9xWaTd94RT88nO3f/vqSlibe32GyycqW4uz+hnSecO9H/J/xfVVKEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmToowd1KEuZMizJ0UYe6kCHMnRZg7KcLcSRHmTor8G0jXJgZVQ8wiAAAAAElFTkSuQmCC)
Find more compounds similar to Ethanol, 2-ethoxy-.
Mixtures
- 1-Butanol, 3-methyl- + Ethanol, 2-ethoxy-
- Ethanol, 2-ethoxy- + Cyclohexane
- Octane + Ethanol, 2-ethoxy-
- n-Hexane + Ethanol, 2-ethoxy-
- Benzene + Ethanol, 2-ethoxy-
- Di-n-propyl ether + Ethanol, 2-ethoxy-
- 1-Propanol + Ethanol, 2-ethoxy-
- 1-Propanol + Di-n-propyl ether + Ethanol, 2-ethoxy-
- 2-Pyrrolidinone, 1-methyl- + Ethanol, 2-ethoxy-
- Benzenamine, 4,4'-oxybis- + Ethanol, 2-ethoxy-
- Ethanol, 2-ethoxy- + Cyclohexane, methyl-
- Ethanol, 2-ethoxy- + Water
- Propane, 2-ethoxy-2-methyl- + Ethanol, 2-ethoxy-
- Ethanol, 2-ethoxy- + Formamide
- Benzyl alcohol + Ethanol, 2-ethoxy-
- Diethyl carbonate + Ethanol, 2-ethoxy-
- Isopropyl Alcohol + Ethanol, 2-ethoxy-
- Diisopropyl ether + Ethanol, 2-ethoxy-
- Monoethanolamine + Ethanol, 2-ethoxy-
- Nitrous oxide + Ethanol, 2-ethoxy-
Find more mixtures with Ethanol, 2-ethoxy-.
Sources
- Crippen Method
- Crippen Method
- Densities, Viscosities, Sound Speeds, Refractive Indices, and Excess Properties of Binary Mixtures of Isoamyl Alcohol with Some Alkoxyethanols
- Influence of the molecular structure on the viscosity of some alkoxyethanols
- Phase Compositions and Saturated Densities for the Binary System of Carbon Dioxide with 2-ethoxyethanol
- Excess enthalpies of binary mixtures of 2-ethoxyethanol with four hydrocarbons at 298.15, 308.15, and 318.15K An experimental and theoretical study
- Phase equilibria involved in extractive distillation of dipropyl ether + 1-propyl alcohol using 2-ethoxyethanol as entrainer
- Selection of entrainers for the separation of the binary azeotropic system methanol + dimethyl carbonate by extractive distillation
- Vapor-liquid equilibria and excess molar volumes of N-methyl-2-pyrrolidone with 2-alkoxyethanols
- Measurement and correlation of the solubility of 4,4'-oxydianiline in different organic solvents
- Isobaric vapor-liquid equilibrium data for methylcyclohexane + 2-methoxyethanol and methylcyclohexane + 2-ethoxyethanol at 50.00 and 101.33 kPa
- Solubility of disodium 4,4'-dinitrobibenzyl-2,2'-disulfonate in aqueous organic solutions and its effects on the oxidation reaction of DSD acid synthesis
- Thermodynamic properties and sPC-SAFT modeling of 2-ethoxyethanol, 2-propoxyethanol and 2-butoxyethanol from T = (293.15-413.15) K and pressure up to 30 MPa
- Viscosity of aqueous solutions of 2-methoxyethanol, 2-ethoxyethanol, and ethanolamine
- Excess molar enthalpies and volumes of binary mixtures of nonafluorobutylmethylether with ethylene glycol ethers at T = 298.15 K
- Viscosities of binary mixtures of some n-ethoxyethanols with ethyl tert-butyl ether at T = (293.15, 298.15, and 303.15) K
- Thermodynamic and optical studies of some ethylene glycol ethers in aqueous solutions at T = 298.15 K
- Volumetric and viscometric study of aqueous binary mixtures of some glycol ethers at T = (275.15 and 283.15) K
- Acoustic, volumetric, and spectroscopic studies of formamide with 2-alkoxyethanols at different temperatures
- Solubility of disodium 4,4'-dinitrostilbene-2,2'-disulfonate and sodium 4-nitrotoluene-2-sulfonate in aqueous organic solutions and its application feasibility in oxidation stage of DSD acid synthesis
- FT-IR spectroscopic study of excess thermodynamic properties of liquid mixtures containing benzylalcohol with alkoxyalkanols
- Study of molecular interactions of binary mixtures DEC with alkoxyalkanols at various temperatures
- Vapour-liquid equilibrium and extractive distillation for separation of azeotrope isopropyl alcohol and diisopropyl ether
- Solubility of N2O and CO2 in non-aqueous systems of monoethanolamine and glycol ethers: Measurements and model representation
- An experimental investigation of molecular interactions between [Emim][triflate] ionic liquid & 2-alkoxyethanols and theoretical comparison by PFP theory
- Intermolecular interactions in Formamide +2-Alkoxyethanols: Viscometric study
- Densities, speed of sound, and IR studies of Ethyl lactate with 2-alkoxyethanols at different temperatures
- Measurement and Prediction of Molar Heat Capacities of Liquid Polyoxyethylene Glycol Monoalkyl Ethers (CnEm)
- Thermophysical properties of glycols and glymes
- Solid-Liquid Equilibrium of Rebaudioside A in Pure and Binary Mixed Solvents at T = (288.15 to 328.15) 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
- Solid-Liquid Equilibrium Solubility, Thermodynamic Properties, and Molecular Simulation of Phenylphosphonic Acid in 15 Pure Solvents at Different Temperatures
- Density, Viscosity, and Excess Properties of Binary Mixtures of 2-(Methylamino)ethanol with 2-Methoxyethanol, 2-Ethoxyethanol, and 2-Butoxyethanol from 293.15 to 353.15 K
- Solubility Determination and Modeling of EGCG Peracetate in 12 Pure Solvents at Temperatures from 278.15 to 318.15 K
- Total Vapor Pressure Measurements for 2-Ethoxyethanol with Methyl Acetate, Ethyl Acetate, Propyl Acetate, and Ethyl Propionate at 313.15 K and for 2-Ethoxyethanol with Methyl Formate at 308.15 K
- Vapor-Liquid Equilibrium for Phenol + r-Methyl Benzyl Alcohol and 2-Ethoxyethanol + n-Butyl Formate
- Densities, Excess Molar Volumes, Viscosities, Speeds of Sound, Excess Isentropic Compressibilities, and Relative Permittivities for CmH2m+1(OCH2CH2)nOH (m ) 1 or 2 or 4 andn ) 1) + Benzene, + Toluene, + (o-, m-, and p-) Xylenes, + Ethylbenzene, and + Cyclohexane
- Total Vapor Pressure Measurements for 2-Ethoxyethanol with Carbon Tetrachloride, Chloroform, and Dichloromethane at 303.15 K
- High-Pressure Volumetric Properties of Three Monoethylene Glycol Alkyl Ethers
- Excess Molar Enthalpies and Hydrogen Bonding in Binary Mixtures Containing Ethers and Benzyl Alcohol at 308.15 K and Atmospheric Pressure
- Solubilities of Phosphorus-Containing Compounds in Selected Solvents
- Excess Gibbs Energies of the Ternary System 2-Methoxyethanol + Tetrahydrofuran + Cyclohexane and Other Relevant Binaries at 298.15 K
- Solubilities of Phenylphosphinic Acid, Methylphenylphosphinic Acid, Hexachlorocyclotriphosphazene, and Hexaphenoxycyclotriphosphazene in Selected Solvents
- Solubility of CO2 in Alcohols, Glycols, Ethers, and Ketones at High Pressures from (288.15 to 318.15) K
- Estimation of Activity Coefficients for the Pairs of the System 2-Ethoxyethanol + 2-Ethoxyethyl Acetate + 2-Butoxyethanol + 2-Butoxyethyl Acetate
- Vapor Liquid Equilibrium for the 2-Ethoxyethanol 2-Ethoxyethyl Acetate System
- Isobaric Vapor Liquid Equilibrium of Binary and Ternary Systems with 2-Ethoxyethanol + Ethylbenzene + Dimethyl Sulfoxide
- Deduction of Physicochemical Properties from Solubilities: 2,4-Dihydroxybenzophenone, Biotin, and Caprolactam as Examples
- Solid-Liquid Equilibria of Dibenzothiophene and Dibenzothiophene Sulfone in Organic Solvents
- Solubilities of 2-(6-Oxido-6H-dibenz[c,e][1,2]oxaphosphorin-6-yl)-1,4-dihydroxy Phenylene in the Selected Solvents
- Solubilities of Diphenylphosphinic Acid in Selected Solvents
- Density, Viscosity, Refractive Index, and Ultrasonic Speed of Binary Mixtures of 1,3-Dioxolane with 2-Methoxyethanol, 2-Ethoxyethanol, 2-Butoxyethanol, 2-Propylamine, and Cyclohexylamine
- Conductance Studies of NaCl, KCl, NaBr, NaI, NaBPh4, and Bu4NI in Water + 2-Ethoxyethanol Mixtures at 298.15 K
- Solubilities of (2,5-Dihydroxyphenyl)diphenyl Phosphine Oxide in Selected Solvents
- Joback Method
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
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