- InChI
- InChI=1S/C7H14O2/c1-6(2)4-5-9-7(3)8/h6H,4-5H2,1-3H3
- InChI Key
- MLFHJEHSLIIPHL-UHFFFAOYSA-N
- Formula
- C7H14O2
- SMILES
- CC(=O)OCCC(C)C
- Molecular Weight1
- 130.18
- CAS
- 123-92-2
- Other Names
-
- 1-Butanol, 3-methyl-, 1-acetate
- 2-Methylbutyl ethanoate
- 3-METHYLBUTYL ESTER ACETIC ACID
- 3-Methyl butyl ester acetic acid
- 3-Methyl-1-butanol acetate
- 3-Methyl-1-butanyl acetate
- 3-Methyl-1-butyl acetate
- 3-Methylbutyl ester of acetic acid
- 3-methyl-1-butyl acetate (isoamyl acetate)
- 3-methyl-but-1-yl acetate
- 3-methylbutyl acetate
- 3-methylbutyl ethanoate
- Acetic acid 3-methylbutyl ester
- Acetic acid, isopentyl ester
- Amyl acetate ester
- Amyl acetate, common
- Banana oil
- CH3C(O)O(CH2)2CH(CH3)2
- Isoamyl ethanoate
- Isoamylester kyseliny octove
- Isopentyl alcohol, acetate
- Isopentyl alcohol, acetate pear oil
- Isopentyl ester acetic acid
- Jargonelle pear essence
- NSC 9260
- Pear oil
- acetic acid, 3-methylbutyl ester
- acetic acid, isoamyl ester
- i-Amyl acetate
- isoamyl acetate
- isopentyl acetate
- isopentyl ethanoate
- «beta»-Methyl butyl acetate
- ω : Acentric Factor.
- Cp,gas : Ideal gas 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).
- 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).
- NFPA Fire : NFPA Fire Rating.
- NFPA Health : NFPA Health Rating.
- 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.
- γ : Surface Tension (N/m).
- Tboil : Normal Boiling Point Temperature (K).
- Tboil(P) : Boiling point at given pressure (K).
- Tboilr : Boiling point at reduced pressure (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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Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ω | 0.4722 | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value | |
| μ | 1.80 | debye | KDB |
| ΔfG° | -304.75 | kJ/mol | Joback Calculated Property |
| ΔfH°gas | -518.76 | kJ/mol | Relay (1.0) Calculated Property |
| ΔfusH° | 14.73 | kJ/mol | Joback Calculated Property |
| ΔvapH° | 46.40 ± 0.20 | kJ/mol | NIST |
| IE | 9.89 | eV | Relay (1.0) Calculated Property |
| log10WS | [-1.92; -1.92] |
|
|
| log10WS | -1.92 | Aq. Solubility Prediction | |
| log10WS | -1.92 | Estimated Solubility | |
| logPoct/wat | 1.596 | Crippen Calculated Property | |
| McVol | 116.930 | ml/mol | McGowan Calculated Property |
| NFPA Fire | 3 | KDB | |
| NFPA Health | 1 | KDB | |
| Pc | [2760.00; 2760.00] | kPa |
|
| Pc | 2760.00 | kPa | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value |
| Pc | 2760.00 | kPa | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Pc | 2760.00 ± 20.00 | kPa | NIST |
| Inp | [836.00; 893.00] |
|
|
| Inp | 861.32 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 857.80 | NIST | |
| Inp | 862.00 | NIST | |
| Inp | 859.70 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 854.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 862.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | Outlier 836.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 883.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 869.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 877.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 862.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 855.50 | NIST | |
| Inp | 851.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 883.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 874.60 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 856.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 885.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 875.70 | NIST | |
| Inp | 874.00 | NIST | |
| Inp | 873.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 881.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 877.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 879.00 | NIST | |
| Inp | 883.00 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 852.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 881.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 877.00 | NIST | |
| Inp | 877.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 882.60 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 880.00 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 886.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 856.00 | NIST | |
| Inp | 850.00 | NIST | |
| Inp | 856.00 | NIST | |
| Inp | 857.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 852.00 | NIST | |
| Inp | 849.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 882.00 | NIST | |
| Inp | 880.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 886.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | Outlier 893.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 851.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 852.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 851.00 | NIST | |
| Inp | 871.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | Outlier 843.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 882.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | Outlier 843.00 | NIST | |
| Inp | Outlier 843.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 882.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 880.00 | NIST | |
| Inp | 877.00 | NIST | |
| Inp | 849.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 880.00 | NIST | |
| Inp | 880.00 | NIST | |
| Inp | 847.00 | NIST | |
| Inp | 854.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 852.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 882.00 | NIST | |
| Inp | 877.00 | NIST | |
| Inp | 847.00 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 875.70 | NIST | |
| Inp | 881.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 882.60 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 856.00 | NIST | |
| Inp | 860.00 | NIST | |
| Ip | [1096.00; 1168.00] |
|
|
| Ip | 1131.00 | NIST | |
| Ip | Outlier 1096.00 | NIST | |
| Ip | 1135.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1126.00 | NIST | |
| Ip | 1126.00 | NIST | |
| Ip | 1124.00 | NIST | |
| Ip | 1126.00 | NIST | |
| Ip | 1130.00 | NIST | |
| Ip | 1120.00 | NIST | |
| Ip | 1102.00 | NIST | |
| Ip | 1105.00 | NIST | |
| Ip | 1117.00 | NIST | |
| Ip | 1121.00 | NIST | |
| Ip | 1126.00 | NIST | |
| Ip | 1111.00 | NIST | |
| Ip | 1130.00 | NIST | |
| Ip | 1131.00 | NIST | |
| Ip | 1101.00 | NIST | |
| Ip | 1115.00 | NIST | |
| Ip | 1121.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1143.00 | NIST | |
| Ip | 1123.00 | NIST | |
| Ip | 1126.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1112.00 | NIST | |
| Ip | 1134.00 | NIST | |
| Ip | 1114.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1139.00 | NIST | |
| Ip | 1121.00 | NIST | |
| Ip | 1117.00 | NIST | |
| Ip | 1118.00 | NIST | |
| Ip | 1115.00 | NIST | |
| Ip | 1107.00 | NIST | |
| Ip | 1116.00 | NIST | |
| Ip | 1126.00 | NIST | |
| Ip | 1126.00 | NIST | |
| Ip | 1118.00 | NIST | |
| Ip | 1119.00 | NIST | |
| Ip | 1123.00 | NIST | |
| Ip | 1127.00 | NIST | |
| Ip | 1123.00 | NIST | |
| Ip | 1120.00 | NIST | |
| Ip | 1120.00 | NIST | |
| Ip | 1115.00 | NIST | |
| Ip | 1115.00 | NIST | |
| Ip | 1117.00 | NIST | |
| Ip | 1117.00 | NIST | |
| Ip | 1116.00 | NIST | |
| Ip | 1127.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1127.00 | NIST | |
| Ip | 1137.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1112.00 | NIST | |
| Ip | 1118.00 | NIST | |
| Ip | 1113.00 | NIST | |
| Ip | 1113.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1129.00 | NIST | |
| Ip | 1115.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1114.00 | NIST | |
| Ip | 1122.00 | NIST | |
| Ip | 1128.00 | NIST | |
| Ip | 1128.00 | NIST | |
| Ip | 1114.00 | NIST | |
| Ip | 1119.00 | NIST | |
| Ip | 1122.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1116.00 | NIST | |
| Ip | 1112.00 | NIST | |
| Ip | 1140.00 | NIST | |
| Ip | 1147.00 | NIST | |
| Ip | 1111.00 | NIST | |
| Ip | 1102.00 | NIST | |
| Ip | 1137.00 | NIST | |
| Ip | 1102.00 | NIST | |
| Ip | 1124.00 | NIST | |
| Ip | 1129.00 | NIST | |
| Ip | 1105.00 | NIST | |
| Ip | 1128.00 | NIST | |
| Ip | 1103.00 | NIST | |
| Ip | 1147.00 | NIST | |
| Ip | 1110.00 | NIST | |
| Ip | 1133.00 | NIST | |
| Ip | 1118.00 | NIST | |
| Ip | 1134.00 | NIST | |
| Ip | 1120.00 | NIST | |
| Ip | 1118.00 | NIST | |
| Ip | 1130.00 | NIST | |
| Ip | 1128.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1112.00 | NIST | |
| Ip | 1108.00 | NIST | |
| Ip | 1143.00 | NIST | |
| Ip | 1128.00 | NIST | |
| Ip | 1142.00 | NIST | |
| Ip | 1128.00 | NIST | |
| Ip | 1128.00 | NIST | |
| Ip | 1101.00 | NIST | |
| Ip | 1101.00 | NIST | |
| Ip | 1130.00 | NIST | |
| Ip | 1140.00 | NIST | |
| Ip | 1110.00 | NIST | |
| Ip | 1110.00 | NIST | |
| Ip | 1118.00 | NIST | |
| Ip | 1118.00 | NIST | |
| Ip | 1122.00 | NIST | |
| Ip | 1122.00 | NIST | |
| Ip | 1114.00 | NIST | |
| Ip | 1110.00 | NIST | |
| Ip | 1127.00 | NIST | |
| Ip | 1127.00 | NIST | |
| Ip | 1127.00 | NIST | |
| Ip | 1127.00 | NIST | |
| Ip | 1129.00 | NIST | |
| Ip | 1124.00 | NIST | |
| Ip | 1124.00 | NIST | |
| Ip | Outlier 1165.00 | NIST | |
| Ip | Outlier 1166.00 | NIST | |
| Ip | Outlier 1167.00 | NIST | |
| Ip | 1113.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1123.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1135.00 | NIST | |
| Ip | 1122.00 | NIST | |
| Ip | 1098.00 | NIST | |
| Ip | 1116.00 | NIST | |
| Ip | 1136.00 | NIST | |
| Ip | 1117.00 | NIST | |
| Ip | 1130.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1136.00 | NIST | |
| Ip | 1110.00 | NIST | |
| Ip | 1111.00 | NIST | |
| Ip | 1131.00 | NIST | |
| Ip | 1115.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1143.00 | NIST | |
| Ip | 1121.00 | NIST | |
| Ip | 1110.00 | NIST | |
| Ip | 1136.00 | NIST | |
| Ip | 1126.00 | NIST | |
| Ip | 1100.00 | NIST | |
| Ip | 1114.00 | NIST | |
| Ip | 1114.00 | NIST | |
| Ip | Outlier 1168.00 | NIST | |
| Ip | 1110.00 | NIST | |
| Ip | 1115.00 | NIST | |
| Ip | 1110.00 | NIST | |
| Ip | 1111.00 | NIST | |
| Ip | 1114.00 | NIST | |
| Ip | 1127.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1128.00 | NIST | |
| Ip | 1130.00 | NIST | |
| Ip | 1121.00 | NIST | |
| Ip | Outlier 1166.00 | NIST | |
| Ip | 1136.00 | NIST | |
| Ip | 1110.00 | NIST | |
| Ip | 1143.00 | NIST | |
| Ip | 1100.00 | NIST | |
| Ip | 1115.00 | NIST | |
| Tboil | [410.40; 415.70] | K |
|
| Tboil | 415.24 | K | Effect of Pressure on the Azeotrope of the Mixture Isoamyl Acetate Isoamyl Alcohol at 50.00, 101.32, 250.00, and 350.00 kPa |
| Tboil | 415.15 | K | Isobaric Vapor-Liquid Equilibrium Measurements for Separation of Azeotrope (Methanol + Methyl Acetate) |
| Tboil | 415.70 | K | KDB |
| Tboil | 415.20 | K | NIST |
| Tboil | 415.00 | K | NIST |
| Tboil | 415.20 ± 0.40 | K | NIST |
| Tboil | 415.00 ± 0.50 | K | NIST |
| Tboil | 415.00 ± 2.00 | K | NIST |
| Tboil | 412.00 ± 3.00 | K | NIST |
| Tboil | 415.25 ± 1.00 | K | NIST |
| Tboil | 412.40 ± 3.00 | K | NIST |
| Tboil | 414.25 ± 2.00 | K | NIST |
| Tboil | 414.00 ± 4.00 | K | NIST |
| Tboil | 414.80 ± 0.40 | K | NIST |
| Tboil | 413.15 ± 1.00 | K | NIST |
| Tboil | 413.00 ± 2.00 | K | NIST |
| Tboil | 413.15 ± 1.00 | K | NIST |
| Tboil | 415.25 ± 0.30 | K | NIST |
| Tboil | 415.15 ± 1.50 | K | NIST |
| Tboil | 415.30 ± 0.50 | K | NIST |
| Tboil | 415.00 ± 1.00 | K | NIST |
| Tboil | 415.00 ± 1.50 | K | NIST |
| Tboil | 415.30 ± 0.50 | K | NIST |
| Tboil | 415.25 ± 1.00 | K | NIST |
| Tboil | 412.95 ± 1.00 | K | NIST |
| Tboil | Outlier 410.40 ± 1.00 | K | NIST |
| Tc | [586.10; 599.33] | K |
|
| Tc | 586.10 | K | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value |
| Tc | 586.10 | K | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Tc | 599.00 | K | KDB |
| Tc | 586.10 ± 0.60 | K | NIST |
| Tc | 599.33 ± 6.00 | K | NIST |
| Tfus | [189.53; 194.90] | K |
|
| Tfus | 194.90 | K | Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value |
| Tfus | 194.60 | K | KDB |
| Tfus | 189.53 | K | Aq. Solubility Prediction |
| Vc | 0.443 | m3/kmol | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
Temperature Dependent Properties
Pressure Dependent Properties
Datasets
Mass density, kg/m3
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 298.15 | 100.00 | 867.3 |
| Reference | ||
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [170.00; 389.11] | 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 | 2.02520e+01 | |||
| Coefficient B | 6.19960e-01 | |||
| Coefficient C | -2.65600e-04 | |||
| Coefficient D | 1.45000e-08 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 273.00 | |||
| Temperature range, max. | 1000.00 | |||
| Cp,gas | 170.00 | J/mol×K | 273.00 | Calculated Property |
| Cp,gas | 206.98 | J/mol×K | 353.78 | Calculated Property |
| Cp,gas | 240.69 | J/mol×K | 434.56 | Calculated Property |
| Cp,gas | 271.19 | J/mol×K | 515.33 | Calculated Property |
| Cp,gas | 298.51 | J/mol×K | 596.11 | Calculated Property |
| Cp,gas | 322.70 | J/mol×K | 676.89 | Calculated Property |
| Cp,gas | 343.81 | J/mol×K | 757.67 | Calculated Property |
| Cp,gas | 361.89 | J/mol×K | 838.44 | Calculated Property |
| Cp,gas | 376.97 | J/mol×K | 919.22 | Calculated Property |
| Cp,gas | 389.11 | J/mol×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.63] | kPa | [311.22; 438.68] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.53486e+01 | |||
| Coefficient B | -3.83541e+03 | |||
| Coefficient C | -5.65620e+01 | |||
| Temperature range, min. | 311.22 | |||
| Temperature range, max. | 438.68 | |||
| Pvap | 1.33 | kPa | 311.22 | Calculated Property |
| Pvap | 2.95 | kPa | 325.38 | Calculated Property |
| Pvap | 6.02 | kPa | 339.54 | Calculated Property |
| Pvap | 11.49 | kPa | 353.71 | Calculated Property |
| Pvap | 20.66 | kPa | 367.87 | Calculated Property |
| Pvap | 35.32 | kPa | 382.03 | Calculated Property |
| Pvap | 57.73 | kPa | 396.19 | Calculated Property |
| Pvap | 90.72 | kPa | 410.36 | Calculated Property |
| Pvap | 137.69 | kPa | 424.52 | Calculated Property |
| Pvap | 202.63 | kPa | 438.68 | Calculated Property |
| Pvap | [2.06e-05; 2676.19] | kPa | [194.65; 599.00] |
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 | 7.60348e+01 | |||
| Coefficient B | -7.92872e+03 | |||
| Coefficient C | -8.76739e+00 | |||
| Coefficient D | 3.24333e-06 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 194.65 | |||
| Temperature range, max. | 599.00 | |||
| Pvap | 2.06e-05 | kPa | 194.65 | Calculated Property |
| Pvap | 7.38e-03 | kPa | 239.58 | Calculated Property |
| Pvap | 0.33 | kPa | 284.51 | Calculated Property |
| Pvap | 4.44 | kPa | 329.43 | Calculated Property |
| Pvap | 28.83 | kPa | 374.36 | Calculated Property |
| Pvap | 115.89 | kPa | 419.29 | Calculated Property |
| Pvap | 336.66 | kPa | 464.22 | Calculated Property |
| Pvap | 779.09 | kPa | 509.14 | Calculated Property |
| Pvap | 1532.08 | kPa | 554.07 | Calculated Property |
| Pvap | 2676.19 | kPa | 599.00 | Calculated Property |
| Pvap | [2.01; 24.06] | kPa | [313.80; 367.70] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.63034e+01 | |||
| Coefficient B | -4.44869e+03 | |||
| Coefficient C | -2.86980e+01 | |||
| Reference | Usanovich and Dembitskii, 1959 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 313.80 | |||
| Temperature range, max. | 367.70 | |||
| Pvap | 2.01 | kPa | 313.80 | Calculated Property |
| Pvap | 2.77 | kPa | 319.79 | Calculated Property |
| Pvap | 3.78 | kPa | 325.78 | Calculated Property |
| Pvap | 5.08 | kPa | 331.77 | Calculated Property |
| Pvap | 6.75 | kPa | 337.76 | Calculated Property |
| Pvap | 8.87 | kPa | 343.74 | Calculated Property |
| Pvap | 11.54 | kPa | 349.73 | Calculated Property |
| Pvap | 14.88 | kPa | 355.72 | Calculated Property |
| Pvap | 19.00 | kPa | 361.71 | Calculated Property |
| Pvap | 24.06 | kPa | 367.70 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| γ | [0.03; 0.01] | N/m | [194.65; 415.15] |
Jasper (1972), surface tension of pure liquid compounds Compiled value
|
| Equation | Y = A + B·T + C·T² + D·T³ + E·T⁴ Y is γ in N/m, T in K | |||
| Coefficient A | 5.37645e-02 | |||
| Coefficient B | -9.89000e-05 | |||
| Coefficient C | 0.00000e+00 | |||
| Coefficient D | 0.00000e+00 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 194.65 | |||
| Temperature range, max. | 415.15 | |||
| γ | 0.03 | N/m | 194.65 | Calculated Property |
| γ | 0.03 | N/m | 219.15 | Calculated Property |
| γ | 0.03 | N/m | 243.65 | Calculated Property |
| γ | 0.03 | N/m | 268.15 | Calculated Property |
| γ | 0.02 | N/m | 292.65 | Calculated Property |
| γ | 0.02 | N/m | 317.15 | Calculated Property |
| γ | 0.02 | N/m | 341.65 | Calculated Property |
| γ | 0.02 | N/m | 366.15 | Calculated Property |
| γ | 0.02 | N/m | 390.65 | Calculated Property |
| γ | 0.01 | N/m | 415.15 | Calculated Property |
Similar Compounds
![PROPAN-1,3-DIOC ACID, DI[3-METHYLBUTYL] ESTER.](data:image/png;base64,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)
Find more compounds similar to 1-Butanol, 3-methyl-, acetate.
Mixtures
- 1-Butanol, 3-methyl-, acetate + Acetic acid + Water
- 1-Butanol, 3-methyl-, acetate + Water
- 1-Butanol, 3-methyl-, acetate + Water + Phosphoric Acid
- Methylene chloride + 1-Butanol, 3-methyl-, acetate
- 1,3-Dioxolane + Methylene chloride + 1-Butanol, 3-methyl-, acetate
- 1-Butanol, 3-methyl-, acetate + Methyl Alcohol
- Ethanol + 1-Butanol, 3-methyl-, acetate
- 1-Propanol + 1-Butanol, 3-methyl-, acetate
- 2-Propanol + 1-Butanol, 3-methyl-, acetate
- 1-Butanol, 3-methyl-, acetate + 1-Butanol
- Carbon dioxide + 1-Butanol, 3-methyl-, acetate
- 1-Butanol, 3-methyl-, acetate + 2-Propenoic acid, butyl ester
- 2-Propenoic acid, ethyl ester + 1-Butanol, 3-methyl-, acetate
- 1-Butanol, 3-methyl-, acetate + Methyl methacrylate
- Styrene + 1-Butanol, 3-methyl-, acetate
- 1-Butanol, 3-methyl-, acetate + o-Xylene
- 1-Butanol, 3-methyl-, acetate + Benzene, 1,3-dimethyl-
- p-Xylene + 1-Butanol, 3-methyl-, acetate
- 1-Butanol, 3-methyl-, acetate + Benzene, ethyl-
- 1-Butanol, 3-methyl-, acetate + Ethyl Acetate
Find more mixtures with 1-Butanol, 3-methyl-, acetate.
Sources
- KDB Vapor Pressure Data
- 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.
- Jasper (1972), surface tension of pure liquid compounds ChEDL chemicals 1.5.2, from Jasper, J. J. The Surface Tension of Pure Liquid Compounds. J. Phys. Chem. Ref. Data 1972, 1, 841-1010 (as transcribed in Lange's Handbook).
- 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
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- Experimental study of phase equilibria in aqueous mixtures of phosphoric acid with isoamyl acetate and methyl isoamyl ketone at T = (298.2, 308.2, and 318.2) K
- Phase behavior of binary mixture for the isoalkyl acetate in supercritical carbon dioxide
- Liquid-liquid equilibrium data for ternary systems of water + acetic acid + acetate esters at 293.2 K and 303.2 K and ~ 95 kPa
- Application of the ERAS model to volumetric properties of binary mixtures of banana oil with primary and secondary alcohols (C1- C4) at different temperatures
- Studies on liquid liquid interactions of some ternary mixtures by density, viscosity, ultrasonic speed and refractive index measurements
- Effect of Pressure on the Azeotrope of the Mixture Isoamyl Acetate Isoamyl Alcohol at 50.00, 101.32, 250.00, and 350.00 kPa
- Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
- Isobaric Vapor Liquid Equilibrium for Binary and Ternary Systems of Isoamyl Alcohol + Isoamyl Acetate + Dimethyl Sulfoxide at 101.33 kPa
- Vapor-Liquid Equilibrium Data for Binary Mixtures of Dimethyl Carbonate with Methyl Acetate, Ethyl Acetate, n-Propyl Acetate, Isopropyl Acetate, n-Butyl Acetate, and Isoamyl Acetate at 93.13 kPa
- Isobaric Vapor-Liquid Equilibrium Measurements for Separation of Azeotrope (Methanol + Methyl Acetate)
- Isobaric Vapor Liquid Equilibria for Binary Mixtures of Isoamyl Acetate + Ethyl Acetate at 50 and 100 kPa
- Effect of Ethanol and Temperature on Partition Coefficients of Ethyl Acetate, Isoamyl Acetate, and Isoamyl Alcohol: Instrumental and Predictive Investigation
- Experimental High-Temperature, High-Pressure Density Measurement and Perturbed-Chain Statistical Associating Fluid Theory Modeling of Dimethyl Sulfoxide, Isoamyl Acetate, and Benzyl Alcohol
- Isobaric Vapor-Liquid Equilibria of Binary Mixtures of Diethyl Carbonate with Isopropyl Acetate, sec-Butyl Acetate, or Isoamyl Acetate at 101.3 kPa
- 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
- Liquid-Liquid Equilibria for the Ternary Systems of (Water + Tetrahydrofuran + Polar Solvent) at 298.15 K
- Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
- Densities, Viscosities, Refractive Indices, and Surface Tensions for 12 Flavor Esters from T ) 288.15 K to T ) 358.15 K
- Densities and Viscosities of Binary Mixtures of Isoamyl Acetate, Ethyl Caproate, Ethyl Benzoate, Isoamyl Butyrate, Ethyl Phenylacetate, and Ethyl Caprylate with Ethanol at T = (288.15, 298.15, 308.15, and 318.15) K
- Refractive Indices and Surface Tensions of Binary Mixtures of Isoamyl Acetate, Ethyl Caproate, Ethyl Benzoate, Isoamyl Butyrate, Ethyl Phenylacetate, and Ethyl Caprylate with Ethanol at (288.15, 298.15, 308.15, and 318.15) K
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- Experimental and Correlational Study of Phase Equilibria in Aqueous Solutions of Formic and Butyric Acids with Isoamyl Acetate and Methyl Isoamyl Ketone at T = 298.15 K
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- Isobaric Vapor-Liquid Equilibrium for Binary Mixtures of 3-Methyl-1-butanol + 3-Methyl-1-butyl Ethanoate and 1-Pentanol + Pentyl Ethanoate at 101.3 kPa
- Joback Method
- KDB
- Aqueous Solubility Prediction Method
- Estimated Solubility Method
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
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