- InChI
- InChI=1S/C5H12O2/c1-5(2)7-4-3-6/h5-6H,3-4H2,1-2H3
- InChI Key
- HCGFUIQPSOCUHI-UHFFFAOYSA-N
- Formula
- C5H12O2
- SMILES
- CC(C)OCCO
- Molecular Weight1
- 104.15
- CAS
- 109-59-1
- Other Names
-
- 2-[(1-Methylethyl)oxy]ethanol
- 2-isopropoxyethanol
- 4-Methyl-3-oxa-1-pentanol
- Dowanal EiPAT
- Dowanol EiPAT
- Ethylene glycol monisopropyl ether
- Ethylene glycol monoisopropyl
- Isopropyl Cellosolve
- Isopropyl Oxitol
- Isopropyl glycol
- NSC 1259
- Ucar AC
- ethanol, 2-isopropoxy-
- ethylene glycol isopropyl ether
- ethylene glycol monoisopropyl ether
- monoisopropyl ether of ethylene glycol
- «beta»-Hydroxyethyl isopropyl ether
- Cp,gas : Ideal gas heat capacity (J/mol×K).
- Cp,liquid : Liquid phase heat capacity (J/mol×K).
- η : Dynamic viscosity (Pa×s).
- 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.
- Tboil : Normal Boiling Point Temperature (K).
- Tboilr : Boiling point at reduced pressure (K).
- Tc : Critical Temperature (K).
- Tfus : Normal melting (fusion) point (K).
- 1: Molecular weight from the IUPAC atomic weights tables.
Cheméo is a service of Céondo GmbH, since 2007, we provide simulation, modelling and software development services for the industry.
Do not hesitate to contact us for your projects.
Contents
- Physical Properties
- Temperature Dependent Properties
- Pressure Dependent Properties
- Datasets
- Correlations
- Similar Compounds
- Mixtures
- Sources
Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ΔfH°gas | -458.06 | kJ/mol | Relay (1.0) Calculated Property |
| ΔfusH° | 10.46 | kJ/mol | Joback Calculated Property |
| ΔvapH° | [50.10; 50.14] | kJ/mol |
|
| ΔvapH° | 50.14 | kJ/mol | NIST |
| ΔvapH° | 50.10 ± 0.10 | kJ/mol | NIST |
| IE | 9.74 | eV | Relay (1.0) Calculated Property |
| log10WS | 0.48 | Relay (1.0) Calculated Property | |
| logPoct/wat | 0.404 | Crippen Calculated Property | |
| McVol | 93.050 | ml/mol | McGowan Calculated Property |
| Pc | 3834.03 | kPa | Joback Calculated Property |
| Inp | 768.00 | NIST | |
| Tboil | 414.70 | K | NIST |
| Tc | 589.67 | K | Relay (1.0) Calculated Property |
| Tfus | 213.15 | K | Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value |
Cheméo can also estimate Critical Volume, Standard Gibbs free energy of formation, Acentric Factor for this compound, but they fall outside the models' validated range, so they are not shown here. Open the prediction tool to compute them on demand.
Temperature Dependent Properties
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | 238.80 | J/mol×K | 298.15 | NIST |
| ΔvapH | [40.42; 45.10] | kJ/mol | [377.00; 414.70] |
|
| ΔvapH | 45.10 | kJ/mol | 377.00 | NIST |
| ΔvapH | 40.42 | kJ/mol | 414.70 | NIST |
| Pvap | [60.00; 100.00] | kPa | [398.12; 414.21] |
|
| Pvap | 60.00 | kPa | 398.12 | Isobaric vapor liquid equilibria for the n-hexane + 2-isopropoxyethanol and n-heptane + 2-isopropoxyethanol systems |
| Pvap | 80.00 | kPa | 407.13 | Isobaric vapor liquid equilibria for the n-hexane + 2-isopropoxyethanol and n-heptane + 2-isopropoxyethanol systems |
| Pvap | 100.00 | kPa | 414.21 | Isobaric vapor liquid equilibria for the n-hexane + 2-isopropoxyethanol and n-heptane + 2-isopropoxyethanol systems |
| n0 | 1.40790 | 298.15 | Density, Speed of Sound, and Refractive Index of Aqueous Binary Mixtures of Some Glycol Ethers at T = 298.15 K |
Pressure Dependent Properties
| Property | Value | Unit | Pressure (kPa) | Source |
|---|---|---|---|---|
| Tboilr | [316.20; 417.20] | K | [1.70; 99.10] |
|
| Tboilr | 316.20 | K | 1.70 | NIST |
| Tboilr | 417.20 | K | 99.10 | NIST |
Datasets
Viscosity, Pa*s
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Viscosity, Pa*s - Liquid |
| 293.15 | 20000.00 | 0.0029 |
| 293.15 | 40000.00 | 0.0035 |
| 293.15 | 60000.00 | 0.0041 |
| 293.15 | 80000.00 | 0.0047 |
| 293.15 | 100000.00 | 0.0052 |
| 303.15 | 20000.00 | 0.0023 |
| 303.15 | 40000.00 | 0.0027 |
| 303.15 | 60000.00 | 0.0031 |
| 303.15 | 80000.00 | 0.0036 |
| 303.15 | 100000.00 | 0.0040 |
| 313.15 | 20000.00 | 0.0019 |
| 313.15 | 40000.00 | 0.0022 |
| 313.15 | 60000.00 | 0.0025 |
| 313.15 | 80000.00 | 0.0028 |
| 313.15 | 100000.00 | 0.0032 |
| 323.15 | 20000.00 | 0.0015 |
| 323.15 | 40000.00 | 0.0017 |
| 323.15 | 60000.00 | 0.0020 |
| 323.15 | 80000.00 | 0.0023 |
| 323.15 | 100000.00 | 0.0026 |
| 333.15 | 20000.00 | 0.0013 |
| 333.15 | 40000.00 | 0.0015 |
| 333.15 | 60000.00 | 0.0017 |
| 333.15 | 80000.00 | 0.0020 |
| 333.15 | 100000.00 | 0.0022 |
| 343.15 | 20000.00 | 0.0010 |
| 343.15 | 40000.00 | 0.0012 |
| 343.15 | 60000.00 | 0.0014 |
| 343.15 | 80000.00 | 0.0017 |
| 343.15 | 100000.00 | 0.0019 |
| 353.15 | 20000.00 | 0.0009 |
| 353.15 | 40000.00 | 0.0011 |
| 353.15 | 60000.00 | 0.0012 |
| 353.15 | 80000.00 | 0.0014 |
| 353.15 | 100000.00 | 0.0015 |
| Reference | ||
Mass density, kg/m3
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 293.15 | 100.00 | 904.0 |
| 293.15 | 5000.00 | 907.3 |
| 293.15 | 10000.00 | 910.8 |
| 293.15 | 15000.00 | 914.1 |
| 293.15 | 20000.00 | 917.3 |
| 293.15 | 25000.00 | 920.4 |
| 293.15 | 30000.00 | 923.6 |
| 293.15 | 35000.00 | 926.4 |
| 293.15 | 40000.00 | 929.2 |
| 293.15 | 45000.00 | 932.0 |
| 293.15 | 50000.00 | 934.5 |
| 293.15 | 55000.00 | 937.1 |
| 293.15 | 60000.00 | 939.6 |
| 303.15 | 100.00 | 895.0 |
| 303.15 | 5000.00 | 898.4 |
| 303.15 | 10000.00 | 902.1 |
| 303.15 | 15000.00 | 905.5 |
| 303.15 | 20000.00 | 908.8 |
| 303.15 | 25000.00 | 912.1 |
| 303.15 | 30000.00 | 915.2 |
| 303.15 | 35000.00 | 918.2 |
| 303.15 | 40000.00 | 921.2 |
| 303.15 | 45000.00 | 924.0 |
| 303.15 | 50000.00 | 927.0 |
| 303.15 | 55000.00 | 929.7 |
| 303.15 | 60000.00 | 932.1 |
| 313.15 | 100.00 | 885.5 |
| 313.15 | 5000.00 | 889.2 |
| 313.15 | 10000.00 | 893.2 |
| 313.15 | 15000.00 | 896.9 |
| 313.15 | 20000.00 | 900.4 |
| 313.15 | 25000.00 | 903.7 |
| 313.15 | 30000.00 | 907.2 |
| 313.15 | 35000.00 | 910.2 |
| 313.15 | 40000.00 | 913.3 |
| 313.15 | 45000.00 | 916.2 |
| 313.15 | 50000.00 | 919.1 |
| 313.15 | 55000.00 | 921.9 |
| 313.15 | 60000.00 | 924.8 |
| 323.15 | 100.00 | 875.9 |
| 323.15 | 5000.00 | 880.1 |
| 323.15 | 10000.00 | 884.3 |
| 323.15 | 15000.00 | 888.2 |
| 323.15 | 20000.00 | 891.9 |
| 323.15 | 25000.00 | 895.4 |
| 323.15 | 30000.00 | 899.0 |
| 323.15 | 35000.00 | 902.3 |
| 323.15 | 40000.00 | 905.4 |
| 323.15 | 45000.00 | 908.5 |
| 323.15 | 50000.00 | 911.4 |
| 323.15 | 55000.00 | 914.5 |
| 323.15 | 60000.00 | 917.3 |
| 333.15 | 100.00 | 866.4 |
| 333.15 | 5000.00 | 871.0 |
| 333.15 | 10000.00 | 875.2 |
| 333.15 | 15000.00 | 879.4 |
| 333.15 | 20000.00 | 883.3 |
| 333.15 | 25000.00 | 887.0 |
| 333.15 | 30000.00 | 890.7 |
| 333.15 | 35000.00 | 894.2 |
| 333.15 | 40000.00 | 897.4 |
| 333.15 | 45000.00 | 900.7 |
| 333.15 | 50000.00 | 903.6 |
| 333.15 | 55000.00 | 906.9 |
| 333.15 | 60000.00 | 910.0 |
| 343.15 | 100.00 | 856.8 |
| 343.15 | 5000.00 | 861.5 |
| 343.15 | 10000.00 | 866.1 |
| 343.15 | 15000.00 | 870.5 |
| 343.15 | 20000.00 | 874.7 |
| 343.15 | 25000.00 | 878.6 |
| 343.15 | 30000.00 | 882.5 |
| 343.15 | 35000.00 | 886.1 |
| 343.15 | 40000.00 | 889.5 |
| 343.15 | 45000.00 | 893.1 |
| 343.15 | 50000.00 | 896.4 |
| 343.15 | 55000.00 | 899.4 |
| 343.15 | 60000.00 | 902.5 |
| 353.15 | 100.00 | 846.8 |
| 353.15 | 5000.00 | 851.9 |
| 353.15 | 10000.00 | 856.7 |
| 353.15 | 15000.00 | 861.6 |
| 353.15 | 20000.00 | 865.8 |
| 353.15 | 25000.00 | 870.0 |
| 353.15 | 30000.00 | 874.1 |
| 353.15 | 35000.00 | 877.8 |
| 353.15 | 40000.00 | 881.6 |
| 353.15 | 45000.00 | 885.2 |
| 353.15 | 50000.00 | 888.3 |
| 353.15 | 55000.00 | 891.7 |
| 353.15 | 60000.00 | 894.9 |
| Reference | ||
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [139.14; 314.99] | J/mol×K | [273.00; 1000.00] |
Joback Predicted correlation
|
| Equation | Y = A + B·T + C·T² + D·T³ + E·T⁴ Y is Cp,gas in J/mol×K, T in K | |||
| Coefficient A | 2.74520e+01 | |||
| Coefficient B | 4.55540e-01 | |||
| Coefficient C | -1.70800e-04 | |||
| Coefficient D | 2.80000e-09 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 273.00 | |||
| Temperature range, max. | 1000.00 | |||
| Cp,gas | 139.14 | J/mol×K | 273.00 | Calculated Property |
| Cp,gas | 167.36 | J/mol×K | 353.78 | Calculated Property |
| Cp,gas | 193.39 | J/mol×K | 434.56 | Calculated Property |
| Cp,gas | 217.23 | J/mol×K | 515.33 | Calculated Property |
| Cp,gas | 238.90 | J/mol×K | 596.11 | Calculated Property |
| Cp,gas | 258.41 | J/mol×K | 676.89 | Calculated Property |
| Cp,gas | 275.77 | J/mol×K | 757.67 | Calculated Property |
| Cp,gas | 290.98 | J/mol×K | 838.44 | Calculated Property |
| Cp,gas | 304.05 | J/mol×K | 919.22 | Calculated Property |
| Cp,gas | 314.99 | J/mol×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [0.1147234; 0.0002624] | Pa×s | [213.15; 415.57] |
Joback Predicted correlation
|
| Equation | Y = exp(A + B/T + C·ln(T) + D·T^E) Y is η in Pa×s, T in K | |||
| Coefficient A | -1.46482e+01 | |||
| Coefficient B | 2.66074e+03 | |||
| Coefficient C | 0.00000e+00 | |||
| Coefficient D | 0.00000e+00 | |||
| Coefficient E | 0.00000e+00 | |||
| Comment | Liquid phase. Joback/Reid (1987), valid from Tf to 0.7·Tc. | |||
| Temperature range, min. | 213.15 | |||
| Temperature range, max. | 415.57 | |||
| η | 0.1147234 | Pa×s | 213.15 | Calculated Property |
| η | 0.0348500 | Pa×s | 235.64 | Calculated Property |
| η | 0.0130295 | Pa×s | 258.13 | Calculated Property |
| η | 0.0057035 | Pa×s | 280.62 | Calculated Property |
| η | 0.0028223 | Pa×s | 303.12 | Calculated Property |
| η | 0.0015391 | Pa×s | 325.61 | Calculated Property |
| η | 0.0009077 | Pa×s | 348.10 | Calculated Property |
| η | 0.0005708 | Pa×s | 370.59 | Calculated Property |
| η | 0.0003785 | Pa×s | 393.08 | Calculated Property |
| η | 0.0002624 | Pa×s | 415.57 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.65] | kPa | [320.62; 436.38] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.67352e+01 | |||
| Coefficient B | -4.32941e+03 | |||
| Coefficient C | -5.73960e+01 | |||
| Temperature range, min. | 320.62 | |||
| Temperature range, max. | 436.38 | |||
| Pvap | 1.33 | kPa | 320.62 | Calculated Property |
| Pvap | 2.87 | kPa | 333.48 | Calculated Property |
| Pvap | 5.77 | kPa | 346.34 | Calculated Property |
| Pvap | 10.92 | kPa | 359.21 | Calculated Property |
| Pvap | 19.62 | kPa | 372.07 | Calculated Property |
| Pvap | 33.68 | kPa | 384.93 | Calculated Property |
| Pvap | 55.51 | kPa | 397.79 | Calculated Property |
| Pvap | 88.20 | kPa | 410.66 | Calculated Property |
| Pvap | 135.66 | kPa | 423.52 | Calculated Property |
| Pvap | 202.65 | kPa | 436.38 | Calculated Property |
| Pvap | [5.61; 98.40] | kPa | [338.80; 413.80] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.54398e+01 | |||
| Coefficient B | -3.89658e+03 | |||
| Coefficient C | -5.46960e+01 | |||
| Reference | Dykyj, Seprakova, et al., 1957 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 338.80 | |||
| Temperature range, max. | 413.80 | |||
| Pvap | 5.61 | kPa | 338.80 | Calculated Property |
| Pvap | 8.29 | kPa | 347.13 | Calculated Property |
| Pvap | 12.00 | kPa | 355.47 | Calculated Property |
| Pvap | 17.01 | kPa | 363.80 | Calculated Property |
| Pvap | 23.68 | kPa | 372.13 | Calculated Property |
| Pvap | 32.42 | kPa | 380.47 | Calculated Property |
| Pvap | 43.69 | kPa | 388.80 | Calculated Property |
| Pvap | 58.03 | kPa | 397.13 | Calculated Property |
| Pvap | 76.04 | kPa | 405.47 | Calculated Property |
| Pvap | 98.40 | kPa | 413.80 | Calculated Property |
| Pvap | [5.61; 98.40] | kPa | [338.80; 413.80] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.54398e+01 | |||
| Coefficient B | -3.89658e+03 | |||
| Coefficient C | -5.46960e+01 | |||
| Reference | Dykyj, Seprakova, et al., 1957, 2 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 338.80 | |||
| Temperature range, max. | 413.80 | |||
| Pvap | 5.61 | kPa | 338.80 | Calculated Property |
| Pvap | 8.29 | kPa | 347.13 | Calculated Property |
| Pvap | 12.00 | kPa | 355.47 | Calculated Property |
| Pvap | 17.01 | kPa | 363.80 | Calculated Property |
| Pvap | 23.68 | kPa | 372.13 | Calculated Property |
| Pvap | 32.42 | kPa | 380.47 | Calculated Property |
| Pvap | 43.69 | kPa | 388.80 | Calculated Property |
| Pvap | 58.03 | kPa | 397.13 | Calculated Property |
| Pvap | 76.04 | kPa | 405.47 | Calculated Property |
| Pvap | 98.40 | kPa | 413.80 | Calculated Property |
Similar Compounds
![Ethanol, 2-[2-(2-ethoxyethoxy)ethoxy]-.](data:image/png;base64,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)
Find more compounds similar to Ethanol, 2-(1-methylethoxy)-.
Mixtures
- Carbon dioxide + Ethanol, 2-(1-methylethoxy)-
- n-Hexane + Ethanol, 2-(1-methylethoxy)-
- Heptane + Ethanol, 2-(1-methylethoxy)-
- Ethanol, 2-(1-methylethoxy)- + Water
- Methanone, (2,4-dihydroxyphenyl)phenyl- + Ethanol, 2-(1-methylethoxy)-
Sources
- 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).
- Cheméo Relay (1.0)
- Crippen Method
- Crippen Method
- Influence of the molecular structure on the viscosity of some alkoxyethanols
- Isobaric vapor liquid equilibria for the n-hexane + 2-isopropoxyethanol and n-heptane + 2-isopropoxyethanol systems
- A (vapor + liquid) equilibria of the {carbon dioxide + isopropoxyethanol (iC3E1)} and the {carbon dioxide + isobutoxyethanol (iC4E1)} systems
- High-Pressure Volumetric Properties of Three Monoethylene Glycol Alkyl Ethers
- Deduction of Physicochemical Properties from Solubilities: 2,4-Dihydroxybenzophenone, Biotin, and Caprolactam as Examples
- Density, Speed of Sound, and Refractive Index of Aqueous Binary Mixtures of Some Glycol Ethers at T = 298.15 K
- Joback Method
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
Note: Cheméo is only indexing the data, follow the source links to retrieve the latest data. The source is also providing more information like the publication year, authors and more.
Take the time to validate and double check the source of the data.
Calculated This icon marks a calculated value or equation: a prediction, not a measurement.
Compiled This icon marks a compiled value or equation: taken from a data compilation such as ChemSep, not from an original measurement report.
These property values are available through the Cheméo API. A free account gives you an access key.