- InChI
- InChI=1S/C8H18O3/c1-2-3-5-10-7-8-11-6-4-9/h9H,2-8H2,1H3
- InChI Key
- OAYXUHPQHDHDDZ-UHFFFAOYSA-N
- Formula
- C8H18O3
- SMILES
- CCCCOCCOCCO
- Molecular Weight1
- 162.23
- CAS
- 112-34-5
- Other Names
-
- 2-(2-butoxyethoxy)ethanol
- 2-(2-n-Butoxyethoxy)ethanol
- 2-2-Butoxyethoxy;ethanol
- 3,6-Dioxadecanol
- 3,6-dioxa-1-decanol
- BuCb
- Butoxydiethylene glycol
- Butoxydiglycol
- Butyl di-icinol
- Diethylene DB
- Diethylene glycol butyl ester
- Diethylene gylcol monobutyl ether
- Dowanol OR
- Ektasolve DB
- Ethanol 2-butoxyethoxy
- Ethylene glycol monobutyl ether
- Glycol ether DB
- Glycol, monobutyl ether
- Jeffersol DB
- NSC 407762
- O-butyl diethylene glycol
- Poly-Solv DB
- butadigol
- butoxyethoxyethanol
- butyl carbitol
- butyl diglycol
- butyl digol
- butyl dioxitol
- butyl oxitol glycol ether
- diethylene glycol butyl ether
- diethylene glycol mono-n-butyl ether
- diethylene glycol monobutyl ether
- diethylene glycol n-butyl ether
- diethylene glycol, n-butyl ether
- diglycol monobutyl ether
- dowanol DB
- ethanol, 2,2'-oxybis-, monobutyl ether
- n-Butyl carbitol
- ω : Acentric Factor.
- 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.
- Ip : 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).
- 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 | 0.6471 | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value | |
| ΔfG° | -330.34 | kJ/mol | Joback Calculated Property |
| ΔfH°gas | -629.63 | kJ/mol | Relay (1.0) Calculated Property |
| ΔfusH° | 22.94 | kJ/mol | Joback Calculated Property |
| ΔvapH° | 69.60 | kJ/mol | Relay (1.0) Calculated Property |
| IE | 9.83 | eV | Relay (1.0) Calculated Property |
| log10WS | -0.36 | Relay (1.0) Calculated Property | |
| logPoct/wat | 0.290 | NCMS SOLV-DB | |
| McVol | 141.190 | ml/mol | McGowan Calculated Property |
| Pc | [2789.48; 2790.00] | kPa |
|
| Pc | 2790.00 | kPa | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value |
| Pc | 2789.48 | kPa | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Pc | 2790.00 ± 70.00 | kPa | NIST |
| Inp | [1169.00; 1211.00] |
|
|
| Inp | 1193.00 | NIST | |
| Inp | 1192.00 | NIST | |
| Inp | 1188.00 | NIST | |
| Inp | 1196.00 | NIST | |
| Inp | 1194.50 | NIST | |
| Inp | 1189.00 | NIST | |
| Inp | 1198.00 | NIST | |
| Inp | Outlier 1169.00 | NIST | |
| Inp | Outlier 1169.00 | NIST | |
| Inp | 1174.00 | NIST | |
| Inp | 1188.00 | NIST | |
| Inp | 1195.00 | NIST | |
| Inp | 1184.00 | NIST | |
| Inp | 1196.20 | NIST | |
| Inp | 1192.00 | NIST | |
| Inp | Outlier 1211.00 | NIST | |
| Inp | 1186.00 | NIST | |
| Inp | 1186.00 | NIST | |
| Inp | 1188.00 | NIST | |
| Ip | [1749.00; 1827.00] |
|
|
| Ip | 1760.00 | NIST | |
| Ip | 1749.00 | NIST | |
| Ip | 1827.00 | NIST | |
| Ip | 1796.00 | NIST | |
| Ip | 1786.00 | NIST | |
| Ip | 1786.00 | NIST | |
| Ip | 1796.00 | NIST | |
| Ip | 1797.00 | NIST | |
| Ip | 1823.00 | NIST | |
| Ip | 1823.00 | NIST | |
| Ip | 1791.00 | NIST | |
| Ip | 1781.00 | NIST | |
| Ip | 1797.00 | NIST | |
| Ip | 1823.00 | NIST | |
| Ip | 1760.00 | NIST | |
| Tboil | [503.75; 504.35] | K |
|
| Tboil | 503.75 | K | NCMS SOLV-DB |
| Tboil | 504.20 | K | NIST |
| Tboil | 504.35 ± 0.50 | K | NIST |
| Tc | [692.00; 692.30] | K |
|
| Tc | 692.00 | K | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value |
| Tc | 692.30 | K | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Tc | 692.30 ± 1.50 | K | NIST |
| Tfus | [205.05; 205.15] | K |
|
| Tfus | 205.15 | K | Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value |
| Tfus | 205.05 | K | NCMS SOLV-DB |
| Vc | 0.536 | m3/kmol | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
Temperature Dependent Properties
Datasets
Mass density, kg/m3
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 283.15 | 100.00 | 960.4 |
| 283.15 | 1000.00 | 961.3 |
| 283.15 | 3000.00 | 962.6 |
| 283.15 | 5000.00 | 963.4 |
| 283.15 | 10000.00 | 966.5 |
| 283.15 | 15000.00 | 969.4 |
| 283.15 | 20000.00 | 971.9 |
| 283.15 | 25000.00 | 974.5 |
| 283.15 | 30000.00 | 977.1 |
| 283.15 | 35000.00 | 979.1 |
| 283.15 | 40000.00 | 981.4 |
| 283.15 | 50000.00 | 986.9 |
| 283.15 | 60000.00 | 990.4 |
| 293.15 | 100.00 | 952.4 |
| 293.15 | 1000.00 | 952.9 |
| 293.15 | 3000.00 | 954.3 |
| 293.15 | 5000.00 | 955.2 |
| 293.15 | 10000.00 | 958.4 |
| 293.15 | 15000.00 | 961.2 |
| 293.15 | 20000.00 | 964.0 |
| 293.15 | 25000.00 | 966.9 |
| 293.15 | 30000.00 | 969.6 |
| 293.15 | 35000.00 | 972.0 |
| 293.15 | 40000.00 | 974.4 |
| 293.15 | 50000.00 | 979.7 |
| 293.15 | 60000.00 | 983.9 |
| 303.15 | 100.00 | 943.8 |
| 303.15 | 1000.00 | 944.2 |
| 303.15 | 3000.00 | 946.0 |
| 303.15 | 5000.00 | 947.0 |
| 303.15 | 10000.00 | 950.3 |
| 303.15 | 15000.00 | 953.0 |
| 303.15 | 20000.00 | 956.0 |
| 303.15 | 25000.00 | 959.1 |
| 303.15 | 30000.00 | 962.0 |
| 303.15 | 35000.00 | 964.7 |
| 303.15 | 40000.00 | 967.1 |
| 303.15 | 50000.00 | 972.2 |
| 303.15 | 60000.00 | 977.1 |
| 313.15 | 100.00 | 935.5 |
| 313.15 | 1000.00 | 935.9 |
| 313.15 | 3000.00 | 937.2 |
| 313.15 | 5000.00 | 938.8 |
| 313.15 | 10000.00 | 942.0 |
| 313.15 | 15000.00 | 945.2 |
| 313.15 | 20000.00 | 948.4 |
| 313.15 | 25000.00 | 951.2 |
| 313.15 | 30000.00 | 953.8 |
| 313.15 | 35000.00 | 956.9 |
| 313.15 | 40000.00 | 959.7 |
| 313.15 | 50000.00 | 965.0 |
| 313.15 | 60000.00 | 969.7 |
| 323.15 | 100.00 | 927.0 |
| 323.15 | 1000.00 | 927.3 |
| 323.15 | 3000.00 | 928.8 |
| 323.15 | 5000.00 | 930.3 |
| 323.15 | 10000.00 | 933.8 |
| 323.15 | 15000.00 | 937.2 |
| 323.15 | 20000.00 | 940.4 |
| 323.15 | 25000.00 | 943.5 |
| 323.15 | 30000.00 | 946.4 |
| 323.15 | 35000.00 | 949.5 |
| 323.15 | 40000.00 | 952.5 |
| 323.15 | 50000.00 | 958.2 |
| 323.15 | 60000.00 | 963.4 |
| 333.15 | 100.00 | 917.8 |
| 333.15 | 1000.00 | 918.7 |
| 333.15 | 3000.00 | 920.7 |
| 333.15 | 5000.00 | 922.2 |
| 333.15 | 10000.00 | 925.7 |
| 333.15 | 15000.00 | 929.2 |
| 333.15 | 20000.00 | 932.5 |
| 333.15 | 25000.00 | 935.5 |
| 333.15 | 30000.00 | 939.0 |
| 333.15 | 35000.00 | 942.0 |
| 333.15 | 40000.00 | 945.2 |
| 333.15 | 50000.00 | 950.6 |
| 333.15 | 60000.00 | 956.0 |
| 343.15 | 100.00 | 909.1 |
| 343.15 | 1000.00 | 910.5 |
| 343.15 | 3000.00 | 912.35 |
| 343.15 | 5000.00 | 913.6 |
| 343.15 | 10000.00 | 917.6 |
| 343.15 | 15000.00 | 921.3 |
| 343.15 | 20000.00 | 924.7 |
| 343.15 | 25000.00 | 928.1 |
| 343.15 | 30000.00 | 931.3 |
| 343.15 | 35000.00 | 934.4 |
| 343.15 | 40000.00 | 937.3 |
| 343.15 | 50000.00 | 943.2 |
| 343.15 | 60000.00 | 948.8 |
| 353.15 | 100.00 | 901.1 |
| 353.15 | 1000.00 | 902.1 |
| 353.15 | 3000.00 | 903.9 |
| 353.15 | 5000.00 | 905.3 |
| 353.15 | 10000.00 | 909.3 |
| 353.15 | 15000.00 | 913.1 |
| 353.15 | 20000.00 | 916.8 |
| 353.15 | 25000.00 | 920.3 |
| 353.15 | 30000.00 | 923.7 |
| 353.15 | 35000.00 | 927.1 |
| 353.15 | 40000.00 | 930.3 |
| 353.15 | 50000.00 | 936.3 |
| 353.15 | 60000.00 | 942.2 |
| 363.15 | 100.00 | 892.6 |
| 363.15 | 1000.00 | 893.2 |
| 363.15 | 3000.00 | 894.9 |
| 363.15 | 5000.00 | 896.7 |
| 363.15 | 10000.00 | 900.4 |
| 363.15 | 15000.00 | 904.8 |
| 363.15 | 20000.00 | 908.5 |
| 363.15 | 25000.00 | 912.1 |
| 363.15 | 30000.00 | 915.7 |
| 363.15 | 35000.00 | 919.2 |
| 363.15 | 40000.00 | 922.7 |
| 363.15 | 50000.00 | 929.1 |
| 363.15 | 60000.00 | 935.2 |
| Reference | ||
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 283.15 | 100.00 | 960.5 |
| 283.15 | 1000.00 | 961.0 |
| 283.15 | 2500.00 | 961.9 |
| 283.15 | 5000.00 | 963.4 |
| 283.15 | 7500.00 | 964.9 |
| 283.15 | 10000.00 | 966.3 |
| 283.15 | 15000.00 | 969.1 |
| 283.15 | 20000.00 | 971.8 |
| 283.15 | 25000.00 | 974.4 |
| 293.15 | 100.00 | 952.2 |
| 293.15 | 1000.00 | 952.7 |
| 293.15 | 2500.00 | 953.7 |
| 293.15 | 5000.00 | 955.2 |
| 293.15 | 7500.00 | 956.7 |
| 293.15 | 10000.00 | 958.2 |
| 293.15 | 15000.00 | 961.1 |
| 293.15 | 20000.00 | 963.9 |
| 293.15 | 25000.00 | 966.7 |
| 303.15 | 100.00 | 943.8 |
| 303.15 | 1000.00 | 944.3 |
| 303.15 | 2500.00 | 945.3 |
| 303.15 | 5000.00 | 946.9 |
| 303.15 | 7500.00 | 948.5 |
| 303.15 | 10000.00 | 950.1 |
| 303.15 | 15000.00 | 953.1 |
| 303.15 | 20000.00 | 956.1 |
| 303.15 | 25000.00 | 959.0 |
| 313.15 | 100.00 | 935.3 |
| 313.15 | 1000.00 | 935.9 |
| 313.15 | 2500.00 | 936.9 |
| 313.15 | 5000.00 | 938.6 |
| 313.15 | 7500.00 | 940.3 |
| 313.15 | 10000.00 | 941.9 |
| 313.15 | 15000.00 | 945.1 |
| 313.15 | 20000.00 | 948.2 |
| 313.15 | 25000.00 | 951.2 |
| 323.15 | 100.00 | 926.6 |
| 323.15 | 1000.00 | 927.2 |
| 323.15 | 2500.00 | 928.3 |
| 323.15 | 5000.00 | 930.1 |
| 323.15 | 7500.00 | 931.8 |
| 323.15 | 10000.00 | 933.5 |
| 323.15 | 15000.00 | 936.9 |
| 323.15 | 20000.00 | 940.1 |
| 323.15 | 25000.00 | 943.2 |
| 333.15 | 100.00 | 917.8 |
| 333.15 | 1000.00 | 918.5 |
| 333.15 | 2500.00 | 919.7 |
| 333.15 | 5000.00 | 921.6 |
| 333.15 | 7500.00 | 923.4 |
| 333.15 | 10000.00 | 925.2 |
| 333.15 | 15000.00 | 928.7 |
| 333.15 | 20000.00 | 932.0 |
| 333.15 | 25000.00 | 935.2 |
| 343.15 | 100.00 | 909.7 |
| 343.15 | 1000.00 | 910.4 |
| 343.15 | 2500.00 | 911.6 |
| 343.15 | 5000.00 | 913.6 |
| 343.15 | 7500.00 | 915.5 |
| 343.15 | 10000.00 | 917.4 |
| 343.15 | 15000.00 | 921.1 |
| 343.15 | 20000.00 | 924.6 |
| 343.15 | 25000.00 | 928.0 |
| 353.15 | 100.00 | 900.9 |
| 353.15 | 1000.00 | 901.7 |
| 353.15 | 2500.00 | 903.0 |
| 353.15 | 5000.00 | 905.0 |
| 353.15 | 7500.00 | 907.1 |
| 353.15 | 10000.00 | 909.1 |
| 353.15 | 15000.00 | 912.9 |
| 353.15 | 20000.00 | 916.6 |
| 353.15 | 25000.00 | 920.1 |
| Reference | ||
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [218.50; 487.73] | 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 | 5.19070e+01 | |||
| Coefficient B | 6.71420e-01 | |||
| Coefficient C | -2.19800e-04 | |||
| Coefficient D | -1.58000e-08 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 273.00 | |||
| Temperature range, max. | 1000.00 | |||
| Cp,gas | 218.50 | J/mol×K | 273.00 | Calculated Property |
| Cp,gas | 261.23 | J/mol×K | 353.78 | Calculated Property |
| Cp,gas | 300.87 | J/mol×K | 434.56 | Calculated Property |
| Cp,gas | 337.38 | J/mol×K | 515.33 | Calculated Property |
| Cp,gas | 370.70 | J/mol×K | 596.11 | Calculated Property |
| Cp,gas | 400.78 | J/mol×K | 676.89 | Calculated Property |
| Cp,gas | 427.57 | J/mol×K | 757.67 | Calculated Property |
| Cp,gas | 451.03 | J/mol×K | 838.44 | Calculated Property |
| Cp,gas | 471.09 | J/mol×K | 919.22 | Calculated Property |
| Cp,gas | 487.73 | J/mol×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.64] | kPa | [383.54; 533.16] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.53016e+01 | |||
| Coefficient B | -4.46698e+03 | |||
| Coefficient C | -8.60200e+01 | |||
| Temperature range, min. | 383.54 | |||
| Temperature range, max. | 533.16 | |||
| Pvap | 1.33 | kPa | 383.54 | Calculated Property |
| Pvap | 2.95 | kPa | 400.16 | Calculated Property |
| Pvap | 6.03 | kPa | 416.79 | Calculated Property |
| Pvap | 11.51 | kPa | 433.41 | Calculated Property |
| Pvap | 20.70 | kPa | 450.04 | Calculated Property |
| Pvap | 35.38 | kPa | 466.66 | Calculated Property |
| Pvap | 57.82 | kPa | 483.29 | Calculated Property |
| Pvap | 90.82 | kPa | 499.91 | Calculated Property |
| Pvap | 137.78 | kPa | 516.54 | Calculated Property |
| Pvap | 202.64 | kPa | 533.16 | Calculated Property |
| Pvap | [0.03; 9.05] | kPa | [323.40; 426.10] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.30680e+01 | |||
| Coefficient B | -3.17546e+03 | |||
| Coefficient C | -1.33841e+02 | |||
| Reference | Gardner and Brewer, 1937 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 323.40 | |||
| Temperature range, max. | 426.10 | |||
| Pvap | 0.03 | kPa | 323.40 | Calculated Property |
| Pvap | 0.07 | kPa | 334.81 | Calculated Property |
| Pvap | 0.15 | kPa | 346.22 | Calculated Property |
| Pvap | 0.33 | kPa | 357.63 | Calculated Property |
| Pvap | 0.65 | kPa | 369.04 | Calculated Property |
| Pvap | 1.21 | kPa | 380.46 | Calculated Property |
| Pvap | 2.14 | kPa | 391.87 | Calculated Property |
| Pvap | 3.61 | kPa | 403.28 | Calculated Property |
| Pvap | 5.82 | kPa | 414.69 | Calculated Property |
| Pvap | 9.05 | kPa | 426.10 | Calculated Property |
Similar Compounds
![Ethanol, 2-[2-(2-butoxyethoxy)ethoxy]-.](data:image/png;base64,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)
![Butane, 1,1'-[oxybis(2,1-ethanediyloxy)]bis-.](data:image/png;base64,iVBORw0KGgoAAAANSUhEUgAAAPoAAAD6CAIAAAAHjs1qAAAL5ElEQVR4nO3ae0yV9R/A8e8REBFMCUHES4u0oouZ1uY9l6QtGfs1AXe2Dk0Xbi45Lf8Q99viiPzDPzlc/ZwuL2Okc2z6B92ciGs4XUPJLLWA2gInaoQkN5PL+fz++J7OULmcA8dsfd6vv87w8XOe8/D+Pud5HnWIiAF0GPOwdwD4+5A7FCF3KELuUITcoQi5QxFyhyLkDkXIHYqQOxQhdyhC7lCE3KEIuUMRcoci5A5FyB2KkDsUIXcoQu5QhNyhCLlDEXKHIuQORcgdipA7FCF3KELuUITcoQi5QxFyhyLkDkXIHYqQOxQhdyhC7lCE3KEIuUMRcoci5A5FyB2KkDsUIXcoQu5QhNyhCLlDEXKHIuQORcgdipA7FCF3KELuUITcoQi5QxFyhyLkDkXIHYqQOxQhdyhC7lCE3KEIuUMRcoci5A5FyB2KkDsUIXcoQu5QhNyhCLlDEXKHIuQORcgdipA7FCF3KELuUITcoQi5QxFyhyLkDkXIHYqQOxQhdyhC7lCE3KEIuUMRcoci5A5FyB2KkDsUIXcoQu5QhNyhCLlDEXKHIuQORcgdipA7FCF3KELuUITcoQi5QxFyhyLkDkXIHYqQOxQhdyhC7lCE3KEIuUMRcoci5A5FyB2KkDsUIXcoQu5QJPxh74A+3d3m9GljjFm82Iwd+7D3RhfO7n+vnh6TkWGuXDGNjWbNGtPb+7B3SJfQ575///7U1NSCgoKQT7aOHz++cuXK7du3e73eBzG/qakpIyMjOzu7o6Mj9NMrKszSpSY727z9tlmyxFRUhPwdOjo6srOzMzIympqaQj7cGOP1erdv375y5crjx48/iPnGmIKCgtTU1P3794d+tITO1atXN2zY4HA47OQVK1Z8//33IZzf2tqal5cXERFh58+bN6+qqiqE8+/cuVNcXPzII4+MGzfOGPPEE0+UlZWFcL6IyIEDUlrqe11aKgcOhHZ8RUVFSkqKMSYqKmr8+PEej+f27dshnF9dXb1w4UJ7/MPDwzds2NDc3BzC+bW1tatXr7bzHQ5HZmbmr7/+GsL5ocm9q6ursLAwOjraGDNu3Ljk5ORJkyYZYyIiItxu982bN0c5v7e3d/fu3fHx8caYsLCwlJSUpKQke0ScTmdjY+PoP8KRI0eSk5PtgZ47d+7MmTPt69TU1IsXL45+vlRViccj587Je+/5fpKbKzU14vFIKBbtxYsXU1NT7T7PnDlz7ty59nVycvKRI0dGP7+xsdHpdNpzWVJSUkpKSlhYmDEmPj5+9+7dvb29o5x/8+ZNt9ttz2WTJk1KTk62J53o6OjCwsKurq7RfwQJSe7l5eWPP/64PbhpaWm//PKLiLS0tLjd7vDwcGPMo48+Wlxc3NPTM7L5X3/9tf+X98orr5w/f15EOjs7i4qKYmJi7JksLy+vvb19ZPN//PHH119/3c5/+umnv/rqKxHp6enZs2ePXWBjxoxxuVy//fbbyOZLQ4OsXSsOhzgccuaMfPCBrF8v69dLfr6cOeP7+dq10tAwsvE2FHuoY2Nji4qK7ty5IyInT5584YUX7Odavnz5d999N7L5XV1d9xzqtrY2Ebl8+fKqVavs/JSUlGPHjo1sfl9fX0lJSUJCgv9Q37hxQ0SuXLnicrnsAps+fXpJSYnX6x3ZW/iNKvdhP/A9JX355ZdBzR/2Azc0NGRlZdkNytLT5fBhCeqINDffzs2NnzzZGBMXF7dr1657zlKDlRSozk4pKpKYGDFGxo+XvDyxa7KvT/r6RES6uqSoSCZMEGMkKkry8qStLfDxw67J3t7eXbt2xcXFGWOenDy5JzdXgrr28Hrl8OH/pqfbL9KsrKyG+9bkgCe7wJ08eXLOnDlDrMkBT3YjNsLc7cnbfp3Zk/cQX2fl5eX+64S0tLSff/552PmdnZ0ejycqKsoYY69Bh/g6q6qq+s+yZd7YWDFGli6VmprhP0B3txQXS2ysGPO/5cuHvuL66aef3njjDbv/Tz311BdffDH8fK9XDh2SGTPEGHE4xOmUIa64GhvF6RSHQ4yRGTPk0KFAFm1lZeXzzz9v9+rVV1+9cOHCYFvaRXth+XIxRmJjpbhYuruH/wg1NbJ0qRjTEhu7YtmyIW6T7D3PhAkTjDFjx451u91tASzaxsZGl8tl93/GjBklJSWDbWlP/1OmTPGv6uvXrw+//wMJOvfu7u7i4mL/pXmANyv+u0D/Bf2tW7cG3NLr9ZaVlT322GPB3az09UlJiUyZ4svL5ZJr1wbd+MQJee45MUaMkRUr5Icfhp/f7y7QXtBfunRpsC1ramqWLFny+/z5YozMmxfopXl1tSxcKMZUvvjiyy+/fObMmcE2rK+vz8zMtHsya9asQO+na2tl9Wrfp37ySfn880G3/P13cbslLEyMkbg4KS6WAC7N7YOKMWPG2Iv7PXv29NlvsPt0dHR4PB7/pXmA99P2QUVkZKQxJiYmxuPx/Pnnn8P+rXsEl3tFRcWzzz474nu4pqYm/xGZOnXq/Ufk3LlzixcvtvPnz59/6tSpoOZLR4d4PBIZKcZIdLR4PGKPiP9kVlcnmZm+X/msWRLkgxe71Psv2j/++KP/BteuXVu3bp39gO8sWCD79skgv/KB9fXJvn2pCxbY09i6deuu3b1oRxbKXSoq5JlnfEcgNVX8v0F7iOyX3sSJYoxERIjbLXd/wGGdPXt20aJF9jf40ksvnT59uv+f2nOZfQxgz2X3Xx0Nra6uzr/UZ8+eHeyjs0Bzr62tTUtL87/NZ599FtTb9Ddg08OuhCDU1/uaTkiQ69fF5ZJNmyQzUw4elE8+uXclBK+5udl/IRcXF2cv5IZdCYEbsGmv11tSUpKYmGhDcblc14b4+hpa/6b37pVPP5WsLHn3XXnrLblxQ6ZO9a2Ewb++hjZY09XV1UOshKDcc9r9IbDvZwkw9y1btvifEO3YsaM7kCu/IXm93tLS0mnTptkjkpCQYB9iRkZGbt26dcTPWO5y7JgcPSoffSSHD/t+8tpr0t4u27bJSK/8+ut/GktMTLQPRo0x6enp9fX1o59fX1+fnp5uZyYlJdnQjTGLFi06e/bs6OfL9euybZu0tcmqVb6fHDwoH38sR4/KSJ+x9Nfe3r5161Z77REdHZ2QkGCfKEybNq20tHT0z1i6u7t37Njhv6jesmVLIH8roNzff//9Ud4iDMjej4796/+NBHgXG5yNG6Wuzvd60ya5fDm048vLy6dPn+5wOCIiIgK9iw1GZWXlnDlzwsPDHQ5HYmJiSB7G3eXSJcnN9b2urZWNG0M5/O770fDw8ADvYgPnf2SyefPmQLYPKPfW1tZRPgAawqlTp5xO586dOx/I9IICqaz0vX7zTWlpCfk7NDc35+Tk5Ofnj/gfFobW09OTn5+fk5MT2n+/9GlpkTVrfK9PnJDCwtC/hcjOnTudTmfQd2IBO3/+fGtrayBbOkTE/ItdvWpycsw775i6OtPcbD788GHv0D/P5s1myhQze7bZu9fs3Wv+uir7V/q3526MuXXLfPONiY838+Y97F35p/r2W9PcbBYsMBMnPuxdebAU5A78hf/vDkXIHYqQOxQhdyhC7lCE3KEIuUMRcoci5A5FyB2KkDsUIXcoQu5QhNyhCLlDEXKHIuQORcgdipA7FCF3KELuUITcoQi5QxFyhyLkDkXIHYqQOxQhdyhC7lCE3KEIuUMRcoci5A5FyB2KkDsUIXcoQu5QhNyhCLlDEXKHIuQORcgdipA7FCF3KELuUITcoQi5QxFyhyLkDkXIHYqQOxQhdyhC7lCE3KEIuUMRcoci5A5FyB2KkDsUIXcoQu5QhNyhCLlDEXKHIuQORcgdipA7FCF3KELuUITcoQi5QxFyhyLkDkXIHYqQOxQhdyhC7lCE3KEIuUMRcoci5A5FyB2KkDsUIXcoQu5QhNyhCLlDEXKHIuQORcgdipA7FCF3KELuUITcoQi5QxFyhyLkDkXIHYqQOxQhdyhC7lCE3KEIuUMRcoci5A5FyB2KkDsUIXcoQu5QhNyhCLlDEXKHIuQORcgdipA7FCF3KPJ/BT0mnoJFlzsAAAAASUVORK5CYII=)
![2-[2-(2-Pentoxyethoxy)ethoxy]ethanol.](data:image/png;base64,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)
Find more compounds similar to Ethanol, 2-(2-butoxyethoxy)-.
Mixtures
- Ethanol, 2-(2-butoxyethoxy)- + Dibenzothiophene
- 1-Hexanol + Ethanol, 2-(2-butoxyethoxy)-
- 1-Octanol + Ethanol, 2-(2-butoxyethoxy)-
- 1-Decanol + Ethanol, 2-(2-butoxyethoxy)-
- Propane, 1,2-dichloro- + Ethanol, 2-(2-butoxyethoxy)-
- Propylamine + Ethanol, 2-(2-butoxyethoxy)-
- Ethanol, 2-(2-butoxyethoxy)- + Water
- sodium chloride + Ethanol, 2-(2-butoxyethoxy)- + Water
- 1-Butanol + Ethanol, 2-(2-butoxyethoxy)-
- Nitrogen + Ethanol, 2-(2-butoxyethoxy)-
- Decane + Ethanol, 2-(2-butoxyethoxy)- + Water
- Monoethanolamine + Ethanol, 2-(2-butoxyethoxy)-
- ETHANOL, 2,2'-IMINOBIS- + Ethanol, 2-(2-butoxyethoxy)-
- Ethanol, 2-(2-butoxyethoxy)- + Triethanolamine
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).
- 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)
- Crippen Method
- Speeds of Sound and Isentropic Compressibilities of n-Alkoxyethanols and Polyethers with Propylamine at 298.15K
- Excess molar volumes and excess molar enthalpies of the binary mixtures of 1,2-dichloropropane with di- and triethylene glycol mono-alkyl ethers at T=298.15K
- FT-IR studies and excess thermodynamic properties of binary liquid mixtures 2-(2-butoxyethoxy) ethanol with 1-hexanol, 1-octanol and 1-decanol at different temperatures
- Solubility of dibenzothiophene in nine organic solvents: Experimental measurement and thermodynamic modelling
- Partial molar volumes of organic solutes in water. XXX. Two poly(ethylene glycol) monoalkyl ethers, C4E2 and C1E3, at temperatures T = 298 K to 573 K and pressures up to 30 MPa
- Measurement and Prediction of Molar Heat Capacities of Liquid Polyoxyethylene Glycol Monoalkyl Ethers (CnEm)
- Densities of Diethylene Glycol, Monobutyl Ether, Diethylene Glycol Dibutyl Ether, and Ethylene Glycol Monobutyl Ether from (283.15 to 363.15) K at Pressures up to 60 MPa
- Liquid-liquid equilibria for the ternary system water + decane + diethylene glycol monobutyl ether at 20 C, 30 C, and 40 C
- PpT Measurements and EoS Predictions of Glycol Ethers from (283.15 to 353.15) K at Pressures up to 25 MPa
- Phase Behavior and Spectroscopic Properties for Ternary Systems Water + Sodium Chloride + Diethylene Glycol Monobutyl Ether at 303.15 K and Atmospheric Pressure
- Density and Viscosity for Binary Mixtures of Diethylene Glycol Monobutyl Ether with Monoethanolamine, Diethanolamine, and Triethanolamine from (293.15 to 333.15) K
- Isothermal Vapor-Liquid Equilibria of Binary Mixtures of Nitrogen with Dimethyl Sulfoxide, N-Methyl-2-pyrrolidone, and Diethylene Glycol Monobutyl Ether at Elevated Pressures
- Thermodynamics of Mixtures Containing Alkoxyethanols. XXIV. Densities, Excess Molar Volumes, and Speeds of Sound at (293.15, 298.15, and 303.15) K and Isothermal Compressibilities at 298.15 K for 2-(2-Alkoxyethoxy)ethanol + 1-Butanol Systems
- Excess Molar Volume and Viscosity Deviation for the Binary Mixture of Diethylene Glycol Monobutyl Ether + Water from (293.15 to 333.15) K at Atmospheric Pressure
- Density, Viscosity, and Refractive Index for Water + 2-Butoxyethanol and + 2-(2-Butoxyethoxy)ethanol at Various Temperatures
- 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
- NCMS SOLV-DB
- The Yaws Handbook of Vapor Pressure
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