- InChI
- InChI=1S/C5H12O/c1-3-5-6-4-2/h3-5H2,1-2H3
- InChI Key
- NVJUHMXYKCUMQA-UHFFFAOYSA-N
- Formula
- C5H12O
- SMILES
- CCCOCC
- Molecular Weight1
- 88.15
- CAS
- 628-32-0
- Other Names
-
- 1-Ethoxypropane
- Ether, ethyl propyl
- Ethyl n-propyl ether
- Ethyl propyl ether
- Propyl ethyl ether
- UN 2615
- n-C3H7OC2H5
- ω : Acentric Factor.
- 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).
- μ : Dipole Moment (debye).
- 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).
- ΔfusH : Enthalpy of fusion at a given temperature (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).
- ρc : Critical density (kg/m3).
- ρl : Liquid Density (kg/m3).
- Inp : Non-polar retention indices.
- ΔfusS : Entropy of fusion at a given temperature (J/mol×K).
- S°gas : Molar entropy at standard conditions (J/mol×K).
- S°liquid : Liquid phase molar entropy at standard conditions (J/mol×K).
- Tboil : Normal Boiling Point Temperature (K).
- Tc : Critical Temperature (K).
- Tfus : Normal melting (fusion) point (K).
- Ttriple : Triple Point Temperature (K).
- Vc : Critical Volume (m3/kmol).
- Zc : Critical Compressibility.
- 1: Molecular weight from the IUPAC atomic weights tables.
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Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ω | 0.3330 | KDB | |
| ΔcH°liquid | -3378.97 | kJ/mol | NIST |
| μ | 1.20 | debye | KDB |
| ΔfG° | -125.50 | kJ/mol | KDB |
| ΔfH°gas | -272.20 ± 1.20 | kJ/mol | NIST |
| ΔfH°liquid | -303.60 ± 1.20 | kJ/mol | NIST |
| ΔfusH° | 9.89 | kJ/mol | Joback Calculated Property |
| ΔvapH° | [31.39; 31.57] | kJ/mol |
|
| ΔvapH° | Outlier 31.57 | kJ/mol | NIST |
| ΔvapH° | 31.39 | kJ/mol | NIST |
| ΔvapH° | 31.40 | kJ/mol | NIST |
| ΔvapH° | 31.40 | kJ/mol | NIST |
| ΔvapH° | 31.43 ± 0.11 | kJ/mol | NIST |
| ΔvapH° | 31.40 ± 0.10 | kJ/mol | NIST |
| IE | 9.50 ± 0.10 | eV | NIST |
| log10WS | [-0.66; -0.66] |
|
|
| log10WS | -0.66 | Aq. Solubility Prediction | |
| log10WS | -0.66 | Estimated Solubility | |
| logPoct/wat | 1.433 | Crippen Calculated Property | |
| McVol | 87.180 | ml/mol | McGowan Calculated Property |
| Pc | [3250.00; 3370.00] | kPa |
|
| Pc | 3370.00 | kPa | KDB |
| Pc | 3370.00 ± 6.00 | kPa | NIST |
| Pc | 3250.00 ± 40.53 | kPa | NIST |
| ρc | 260.13 ± 1.76 | kg/m3 | NIST |
| Inp | [566.50; 590.00] |
|
|
| Inp | 590.00 | NIST | |
| Inp | 566.50 | NIST | |
| Inp | 572.10 | NIST | |
| Inp | 590.00 | NIST | |
| S°gas | 388.10 | J/mol×K | NIST |
| S°liquid | 295.00 | J/mol×K | NIST |
| Tboil | [336.30; 336.80] | K |
|
| Tboil | 336.36 | K | KDB |
| Tboil | 336.80 | K | NIST |
| Tboil | 336.30 | K | NIST |
| Tboil | 336.40 ± 0.50 | K | NIST |
| Tc | [500.20; 500.60] | K |
|
| Tc | 500.23 | K | KDB |
| Tc | 500.20 | K | NIST |
| Tc | 500.23 ± 0.20 | K | NIST |
| Tc | 500.60 ± 0.50 | K | NIST |
| Tfus | [145.60; 146.45] | K |
|
| Tfus | 145.60 | K | KDB |
| Tfus | 145.90 | K | Aq. Solubility Prediction |
| Tfus | 146.45 ± 0.40 | K | NIST |
| Ttriple | [145.65; 145.65] | K |
|
| Ttriple | 145.65 ± 0.05 | K | NIST |
| Ttriple | 145.65 ± 0.05 | K | NIST |
| Vc | 0.339 | m3/kmol | KDB |
| Zc | 0.2746780 | KDB |
Temperature Dependent Properties
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | [197.20; 197.50] | J/mol×K | [298.15; 298.15] |
|
| Cp,liquid | 197.20 | J/mol×K | 298.15 | NIST |
| Cp,liquid | 197.50 | J/mol×K | 298.15 | NIST |
| ΔfusH | [8.39; 8.39] | kJ/mol | [145.65; 145.70] |
|
| ΔfusH | 8.39 | kJ/mol | 145.65 | NIST |
| ΔfusH | 8.39 | kJ/mol | 145.65 | NIST |
| ΔfusH | 8.39 | kJ/mol | 145.70 | NIST |
| ΔfusH | 8.39 | kJ/mol | 145.70 | NIST |
| ΔvapH | [28.94; 33.00] | kJ/mol | [311.50; 336.30] |
|
| ΔvapH | 33.00 | kJ/mol | 311.50 | NIST |
| ΔvapH | 29.00 | kJ/mol | 311.50 | NIST |
| ΔvapH | 31.60 | kJ/mol | 314.00 | NIST |
| ΔvapH | 28.94 | kJ/mol | 336.30 | NIST |
| ρl | 733.00 | kg/m3 | 293.00 | KDB |
| ΔfusS | [57.64; 57.64] | J/mol×K | [145.65; 145.65] |
|
| ΔfusS | 57.64 | J/mol×K | 145.65 | NIST |
| ΔfusS | 57.64 | J/mol×K | 145.65 | NIST |
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [126.96; 295.78] | 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 | 2.38430e+01 | |||
| Coefficient B | 4.15640e-01 | |||
| Coefficient C | -1.37200e-04 | |||
| Coefficient D | -6.50000e-09 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 273.00 | |||
| Temperature range, max. | 1000.00 | |||
| Cp,gas | 126.96 | J/mol×K | 273.00 | Calculated Property |
| Cp,gas | 153.43 | J/mol×K | 353.78 | Calculated Property |
| Cp,gas | 178.02 | J/mol×K | 434.56 | Calculated Property |
| Cp,gas | 200.71 | J/mol×K | 515.33 | Calculated Property |
| Cp,gas | 221.48 | J/mol×K | 596.11 | Calculated Property |
| Cp,gas | 240.31 | J/mol×K | 676.89 | Calculated Property |
| Cp,gas | 257.17 | J/mol×K | 757.67 | Calculated Property |
| Cp,gas | 272.05 | J/mol×K | 838.44 | Calculated Property |
| Cp,gas | 284.93 | J/mol×K | 919.22 | Calculated Property |
| Cp,gas | 295.78 | J/mol×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [0.0070406; 0.0001907] | Pa×s | [145.98; 350.22] |
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 | -1.11440e+01 | |||
| Coefficient B | 9.03330e+02 | |||
| Coefficient C | 0.00000e+00 | |||
| Coefficient D | 0.00000e+00 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 145.98 | |||
| Temperature range, max. | 350.22 | |||
| η | 0.0070406 | Pa×s | 145.98 | Calculated Property |
| η | 0.0030624 | Pa×s | 168.68 | Calculated Property |
| η | 0.0016228 | Pa×s | 191.37 | Calculated Property |
| η | 0.0009839 | Pa×s | 214.06 | Calculated Property |
| η | 0.0006566 | Pa×s | 236.76 | Calculated Property |
| η | 0.0004703 | Pa×s | 259.45 | Calculated Property |
| η | 0.0003554 | Pa×s | 282.14 | Calculated Property |
| η | 0.0002800 | Pa×s | 304.83 | Calculated Property |
| η | 0.0002281 | Pa×s | 327.53 | Calculated Property |
| η | 0.0001907 | Pa×s | 350.22 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.65] | kPa | [250.01; 357.64] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.53548e+01 | |||
| Coefficient B | -3.24200e+03 | |||
| Coefficient C | -3.48390e+01 | |||
| Temperature range, min. | 250.01 | |||
| Temperature range, max. | 357.64 | |||
| Pvap | 1.33 | kPa | 250.01 | Calculated Property |
| Pvap | 2.95 | kPa | 261.97 | Calculated Property |
| Pvap | 6.02 | kPa | 273.93 | Calculated Property |
| Pvap | 11.48 | kPa | 285.89 | Calculated Property |
| Pvap | 20.66 | kPa | 297.85 | Calculated Property |
| Pvap | 35.31 | kPa | 309.80 | Calculated Property |
| Pvap | 57.72 | kPa | 321.76 | Calculated Property |
| Pvap | 90.72 | kPa | 333.72 | Calculated Property |
| Pvap | 137.70 | kPa | 345.68 | Calculated Property |
| Pvap | 202.65 | kPa | 357.64 | Calculated Property |
| Pvap | [7.50e-07; 3410.31] | kPa | [145.65; 500.23] |
KDB Vapor Pressure Data
|
| Equation | ln(Y) = A + B/T + C·ln(T) + D·T² + E/T² Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.32471e+02 | |||
| Coefficient B | -8.24837e+03 | |||
| Coefficient C | -1.81397e+01 | |||
| Coefficient D | 1.95507e-05 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 145.65 | |||
| Temperature range, max. | 500.23 | |||
| Pvap | 7.50e-07 | kPa | 145.65 | Calculated Property |
| Pvap | 2.17e-03 | kPa | 185.05 | Calculated Property |
| Pvap | 0.22 | kPa | 224.45 | Calculated Property |
| Pvap | 4.20 | kPa | 263.84 | Calculated Property |
| Pvap | 30.21 | kPa | 303.24 | Calculated Property |
| Pvap | 123.68 | kPa | 342.64 | Calculated Property |
| Pvap | 359.27 | kPa | 382.04 | Calculated Property |
| Pvap | 846.38 | kPa | 421.43 | Calculated Property |
| Pvap | 1759.30 | kPa | 460.83 | Calculated Property |
| Pvap | 3410.31 | kPa | 500.23 | Calculated Property |
| Pvap | [19.72; 99.28] | kPa | [293.53; 335.66] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.40950e+01 | |||
| Coefficient B | -2.75076e+03 | |||
| Coefficient C | -4.60150e+01 | |||
| Reference | Cidlinský and Polák, 1969 | |||
| Temperature range, min. | 293.53 | |||
| Temperature range, max. | 335.66 | |||
| Pvap | 19.72 | kPa | 293.53 | Calculated Property |
| Pvap | 24.23 | kPa | 298.21 | Calculated Property |
| Pvap | 29.56 | kPa | 302.89 | Calculated Property |
| Pvap | 35.81 | kPa | 307.57 | Calculated Property |
| Pvap | 43.08 | kPa | 312.25 | Calculated Property |
| Pvap | 51.50 | kPa | 316.94 | Calculated Property |
| Pvap | 61.19 | kPa | 321.62 | Calculated Property |
| Pvap | 72.29 | kPa | 326.30 | Calculated Property |
| Pvap | 84.94 | kPa | 330.98 | Calculated Property |
| Pvap | 99.28 | kPa | 335.66 | Calculated Property |
Similar Compounds
![CH3O[CH2CH2CH2O]3CH3.](data:image/png;base64,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)
Find more compounds similar to Propane, 1-ethoxy-.
Sources
- KDB Vapor Pressure Data
- Crippen Method
- Joback Method
- KDB
- Aqueous Solubility Prediction Method
- Estimated Solubility Method
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
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