- InChI
- InChI=1S/C6H12O2/c1-3-4-5-8-6(2)7/h3-5H2,1-2H3
- InChI Key
- DKPFZGUDAPQIHT-UHFFFAOYSA-N
- Formula
- C6H12O2
- SMILES
- CCCCOC(C)=O
- Molecular Weight1
- 116.16
- CAS
- 123-86-4
- Other Names
-
- 1-Acetoxybutane
- 1-Butanol, acetate
- 1-Butyl acetate
- Acetate de butyle
- Acetic acid butyl ester
- Acetic acid n-butyl ester
- Butile
- Butile(acetati di)
- Butyl ester of acetic acid
- Butyl ester, acetic acid
- Butylacetat
- Butylacetaten
- Butyle
- Butyle (acetate de)
- Butylester kyseliny octove
- CH3COO(CH2)3CH3
- NSC 9298
- UN 1123
- butyl acetate
- butyl ethanoate
- ethanoic acid, butyl ester
- n-Butyl ethanoate
- n-butyl acetate
- ω : Acentric Factor.
- Tig : Autoignition Temperature (K).
- 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).
- εr : Dielectric Constant (Relative permittivity).
- LFL : Lower Flammability Limit (% in Air).
- UFL : Upper Flammability Limit (% in Air).
- Tflash,cc : Flash Point (Closed Cup Method) (K).
- Tflash,oc : Flash Point (Open Cup Method) (K).
- ΔfG° : Standard Gibbs free energy of formation (kJ/mol).
- Rg : Radius of Gyration.
- 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).
- 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.
- NFPA Safety : NFPA Safety Rating.
- Pc : Critical Pressure (kPa).
- Ptriple : Triple Point 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).
- γ : Surface Tension (N/m).
- Tboil : Normal Boiling Point Temperature (K).
- Tc : Critical Temperature (K).
- λ : Gas thermal conductivity (W/m×K).
- λ : Liquid thermal conductivity (W/m×K).
- Tfus : Normal melting (fusion) point (K).
- Ttriple : Triple Point Temperature (K).
- UQi : UNIQUAC Qi Parameter.
- URi : UNIQUAC Ri Parameter.
- Vc : Critical Volume (m3/kmol).
- Zc : Critical Compressibility.
- Zra : Rackett Parameter.
- 1: Molecular weight from the IUPAC atomic weights tables.
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Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ω | [0.4070; 0.4170] |
|
|
| ω | 0.4070 | ChemSep v8.3 pure component data Compiled value | |
| ω | 0.4170 | KDB | |
| Tig | [677.59; 698.15] | K |
|
| Tig | 677.59 | K | KDB |
| Tig | 698.15 | K | NCMS SOLV-DB |
| ΔcH°liquid | [-3543.00; -3467.00] | kJ/mol |
|
| ΔcH°liquid | -3467.00 | kJ/mol | NIST |
| ΔcH°liquid | -3543.00 | kJ/mol | NIST |
| μ | [1.80; 1.84] | debye |
|
| μ | 1.84 | debye | ChemSep v8.3 pure component data Compiled value |
| μ | 1.80 | debye | KDB |
| η | 0.0006680 | Pa×s | Excess Molar Volumes and Viscosity Deviations of Binary Liquid Mixtures of 1,3-Dioxolane and 1,4-Dioxane with Butyl Acetate, Butyric Acid, Butylamine, and 2-Butanone at 298.15 K |
| εr | 5.01 | NCMS SOLV-DB | |
| LFL | 1.70 | % in Air | KDB |
| UFL | 7.60 | % in Air | KDB |
| Tflash,cc | [295.15; 310.37] | K |
|
| Tflash,cc | 310.37 | K | KDB |
| Tflash,cc | 295.15 | K | NCMS SOLV-DB |
| Tflash,oc | 297.04 | K | KDB |
| ΔfG° | -312.30 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| Rg | 4.1700 | KDB | |
| ΔfH°gas | [-566.00; -485.60] | kJ/mol |
|
| ΔfH°gas | -485.60 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | -486.80 | kJ/mol | KDB |
| ΔfH°gas | -566.00 | kJ/mol | NIST |
| ΔfH°liquid | -609.60 | kJ/mol | NIST |
| ΔfusH° | 15.67 | kJ/mol | Joback Calculated Property |
| ΔvapH° | [37.50; 43.89] | kJ/mol |
|
| ΔvapH° | 43.64 | kJ/mol | NCMS SOLV-DB |
| ΔvapH° | 43.89 | kJ/mol | NIST |
| ΔvapH° | 42.40 | kJ/mol | NIST |
| ΔvapH° | 42.70 | kJ/mol | NIST |
| ΔvapH° | 43.10 | kJ/mol | NIST |
| ΔvapH° | 41.00 ± 0.50 | kJ/mol | NIST |
| ΔvapH° | 43.60 ± 0.50 | kJ/mol | NIST |
| ΔvapH° | 43.70 ± 0.20 | kJ/mol | NIST |
| ΔvapH° | 43.60 ± 0.20 | kJ/mol | NIST |
| ΔvapH° | 43.60 ± 0.20 | kJ/mol | NIST |
| ΔvapH° | Outlier 37.50 | kJ/mol | NIST |
| IE | [9.56; 10.17] | eV |
|
| IE | 9.92 ± 0.05 | eV | NIST |
| IE | 10.01 | eV | NIST |
| IE | 9.56 ± 0.03 | eV | NIST |
| IE | 10.02 ± 0.05 | eV | NIST |
| IE | 10.17 | eV | NIST |
| log10WS | -1.24 | Aq. Solubility Prediction | |
| logPoct/wat | 2.060 | NCMS SOLV-DB | |
| McVol | 102.840 | ml/mol | McGowan Calculated Property |
| NFPA Fire | [%!d(float64=3); %!d(float64=3)] |
|
|
| NFPA Fire | 3 | KDB | |
| NFPA Fire | 3 | NCMS SOLV-DB | |
| NFPA Health | [%!d(float64=1); %!d(float64=1)] |
|
|
| NFPA Health | 1 | KDB | |
| NFPA Health | 1 | NCMS SOLV-DB | |
| NFPA Safety | 0 | NCMS SOLV-DB | |
| Pc | [3090.00; 3140.00] | kPa |
|
| Pc | 3090.00 | kPa | ChemSep v8.3 pure component data Compiled value |
| Pc | 3140.00 | kPa | KDB |
| Pc | 3090.00 ± 20.00 | kPa | NIST |
| Pc | 3100.00 ± 101.32 | kPa | NIST |
| Ptriple | 8.17e-05 | kPa | ChemSep v8.3 pure component data Compiled value |
| Inp | [769.00; 830.10] |
|
|
| Inp | 796.20 | NIST | |
| Inp | 784.76 | NIST | |
| Inp | 805.85 | NIST | |
| Inp | 805.20 | NIST | |
| Inp | 801.50 | NIST | |
| Inp | 804.70 | NIST | |
| Inp | 801.60 | NIST | |
| Inp | 799.40 | NIST | |
| Inp | 798.20 | NIST | |
| Inp | 796.80 | NIST | |
| Inp | 797.88 | NIST | |
| Inp | 797.88 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 809.40 | NIST | |
| Inp | 808.30 | NIST | |
| Inp | 806.60 | NIST | |
| Inp | 786.00 | NIST | |
| Inp | Outlier 774.00 | NIST | |
| Inp | 810.00 | NIST | |
| Inp | 786.00 | NIST | |
| Inp | Outlier 774.00 | NIST | |
| Inp | 781.00 | NIST | |
| Inp | 810.00 | NIST | |
| Inp | 790.00 | NIST | |
| Inp | 818.00 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 792.00 | NIST | |
| Inp | Outlier 770.00 | NIST | |
| Inp | 796.40 | NIST | |
| Inp | 784.00 | NIST | |
| Inp | 786.00 | NIST | |
| Inp | 786.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 802.00 | NIST | |
| Inp | 805.00 | NIST | |
| Inp | 787.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 799.00 | NIST | |
| Inp | 804.00 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 802.00 | NIST | |
| Inp | 801.00 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 799.00 | NIST | |
| Inp | 817.00 | NIST | |
| Inp | 800.00 | NIST | |
| Inp | 788.00 | NIST | |
| Inp | 789.00 | NIST | |
| Inp | 805.00 | NIST | |
| Inp | 810.00 | NIST | |
| Inp | 787.00 | NIST | |
| Inp | 800.00 | NIST | |
| Inp | Outlier 775.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 815.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 797.00 | NIST | |
| Inp | 814.00 | NIST | |
| Inp | 804.90 | NIST | |
| Inp | 820.00 | NIST | |
| Inp | 816.00 | NIST | |
| Inp | 791.00 | NIST | |
| Inp | 813.00 | NIST | |
| Inp | 792.30 | NIST | |
| Inp | 795.00 | NIST | |
| Inp | 791.00 | NIST | |
| Inp | 791.00 | NIST | |
| Inp | 811.00 | NIST | |
| Inp | 818.00 | NIST | |
| Inp | Outlier 830.10 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 813.00 | NIST | |
| Inp | 817.00 | NIST | |
| Inp | 797.00 | NIST | |
| Inp | 799.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 819.00 | NIST | |
| Inp | 802.00 | NIST | |
| Inp | 812.80 | NIST | |
| Inp | 802.00 | NIST | |
| Inp | 814.00 | NIST | |
| Inp | 814.00 | NIST | |
| Inp | 820.00 | NIST | |
| Inp | 816.00 | NIST | |
| Inp | 815.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 810.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 813.00 | NIST | |
| Inp | 791.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 792.00 | NIST | |
| Inp | 790.00 | NIST | |
| Inp | 788.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 805.00 | NIST | |
| Inp | Outlier 769.00 | NIST | |
| Inp | 809.00 | NIST | |
| Inp | 786.00 | NIST | |
| Inp | 816.00 | NIST | |
| Inp | 815.00 | NIST | |
| Inp | 817.00 | NIST | |
| Inp | Outlier 828.00 | NIST | |
| Inp | 810.00 | NIST | |
| Inp | 820.00 | NIST | |
| Inp | 819.00 | NIST | |
| Inp | Outlier 829.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 815.00 | NIST | |
| Inp | 817.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 800.00 | NIST | |
| Inp | 810.00 | NIST | |
| Inp | 823.00 | NIST | |
| Inp | 815.00 | NIST | |
| Inp | 795.00 | NIST | |
| Inp | 813.00 | NIST | |
| Inp | 795.00 | NIST | |
| Inp | 808.00 | NIST | |
| Inp | 807.00 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 823.00 | NIST | |
| Inp | 799.00 | NIST | |
| Inp | 798.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 813.00 | NIST | |
| Inp | 789.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 786.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 798.00 | NIST | |
| Inp | 818.00 | NIST | |
| Inp | 800.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 814.00 | NIST | |
| Inp | 798.00 | NIST | |
| Inp | 800.00 | NIST | |
| Inp | 797.00 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 808.00 | NIST | |
| Inp | 800.00 | NIST | |
| Inp | 813.00 | NIST | |
| Inp | 819.00 | NIST | |
| Inp | 811.00 | NIST | |
| Inp | Outlier 776.00 | NIST | |
| Inp | 813.00 | NIST | |
| Inp | 810.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 800.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 813.00 | NIST | |
| Inp | 820.00 | NIST | |
| Inp | 819.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 808.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 810.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 811.00 | NIST | |
| Inp | 814.00 | NIST | |
| Inp | 816.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 804.00 | NIST | |
| Inp | 799.00 | NIST | |
| Inp | 795.00 | NIST | |
| Inp | 802.00 | NIST | |
| Inp | 802.00 | NIST | |
| Inp | 795.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 800.00 | NIST | |
| Inp | 800.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 799.00 | NIST | |
| Inp | 797.00 | NIST | |
| Inp | 791.00 | NIST | |
| Inp | 788.00 | NIST | |
| Inp | 813.00 | NIST | |
| Inp | 810.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 819.00 | NIST | |
| Inp | 794.00 | NIST | |
| Inp | 795.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 799.00 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 789.00 | NIST | |
| Inp | 796.20 | NIST | |
| Inp | 804.70 | NIST | |
| Inp | 797.88 | NIST | |
| Inp | 806.60 | NIST | |
| Inp | Outlier 774.00 | NIST | |
| Inp | 786.00 | NIST | |
| Inp | 805.00 | NIST | |
| I | [1036.00; 1114.00] |
|
|
| I | 1077.00 | NIST | |
| I | 1062.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1082.00 | NIST | |
| I | 1053.00 | NIST | |
| I | 1064.00 | NIST | |
| I | 1080.00 | NIST | |
| I | 1079.00 | NIST | |
| I | 1091.00 | NIST | |
| I | Outlier 1036.00 | NIST | |
| I | 1068.00 | NIST | |
| I | 1085.00 | NIST | |
| I | 1078.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1086.00 | NIST | |
| I | 1095.00 | NIST | |
| I | 1078.00 | NIST | |
| I | 1070.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1070.00 | NIST | |
| I | 1080.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1049.00 | NIST | |
| I | Outlier 1100.00 | NIST | |
| I | Outlier 1105.00 | NIST | |
| I | Outlier 1100.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1057.00 | NIST | |
| I | 1067.00 | NIST | |
| I | 1052.00 | NIST | |
| I | 1086.80 | NIST | |
| I | 1072.00 | NIST | |
| I | 1052.00 | NIST | |
| I | 1056.00 | NIST | |
| I | 1052.00 | NIST | |
| I | 1078.00 | NIST | |
| I | 1086.00 | NIST | |
| I | 1072.00 | NIST | |
| I | 1059.00 | NIST | |
| I | 1072.00 | NIST | |
| I | 1050.00 | NIST | |
| I | 1059.00 | NIST | |
| I | 1064.00 | NIST | |
| I | 1066.00 | NIST | |
| I | 1076.20 | NIST | |
| I | 1075.20 | NIST | |
| I | 1077.40 | NIST | |
| I | 1074.50 | NIST | |
| I | 1074.00 | NIST | |
| I | 1074.40 | NIST | |
| I | 1073.70 | NIST | |
| I | 1074.10 | NIST | |
| I | 1057.00 | NIST | |
| I | 1058.00 | NIST | |
| I | 1065.00 | NIST | |
| I | 1077.00 | NIST | |
| I | 1085.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1080.00 | NIST | |
| I | 1062.00 | NIST | |
| I | 1062.00 | NIST | |
| I | 1074.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1080.00 | NIST | |
| I | 1082.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1067.00 | NIST | |
| I | 1082.00 | NIST | |
| I | 1073.00 | NIST | |
| I | 1065.00 | NIST | |
| I | 1093.00 | NIST | |
| I | 1068.00 | NIST | |
| I | 1046.00 | NIST | |
| I | 1074.00 | NIST | |
| I | 1070.00 | NIST | |
| I | 1077.00 | NIST | |
| I | 1064.00 | NIST | |
| I | 1088.00 | NIST | |
| I | 1059.00 | NIST | |
| I | 1066.00 | NIST | |
| I | 1070.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1092.00 | NIST | |
| I | Outlier 1105.00 | NIST | |
| I | 1072.00 | NIST | |
| I | 1072.00 | NIST | |
| I | Outlier 1100.00 | NIST | |
| I | 1047.00 | NIST | |
| I | 1076.00 | NIST | |
| I | 1072.00 | NIST | |
| I | 1059.00 | NIST | |
| I | 1071.00 | NIST | |
| I | 1071.00 | NIST | |
| I | 1076.00 | NIST | |
| I | 1077.00 | NIST | |
| I | 1070.00 | NIST | |
| I | 1059.00 | NIST | |
| I | 1068.00 | NIST | |
| I | 1070.00 | NIST | |
| I | Outlier 1114.00 | NIST | |
| I | 1063.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1098.00 | NIST | |
| I | Outlier 1040.00 | NIST | |
| I | 1059.00 | NIST | |
| I | 1059.00 | NIST | |
| I | 1088.00 | NIST | |
| I | 1077.00 | NIST | |
| I | 1085.00 | NIST | |
| I | 1082.00 | NIST | |
| I | 1082.00 | NIST | |
| I | 1065.00 | NIST | |
| I | 1070.00 | NIST | |
| I | 1082.00 | NIST | |
| I | 1073.00 | NIST | |
| I | 1074.00 | NIST | |
| I | 1082.00 | NIST | |
| I | 1057.00 | NIST | |
| I | 1082.00 | NIST | |
| I | 1060.00 | NIST | |
| I | 1086.00 | NIST | |
| I | 1068.00 | NIST | |
| I | 1086.00 | NIST | |
| I | 1086.00 | NIST | |
| I | 1075.00 | NIST | |
| I | 1070.00 | NIST | |
| I | 1059.00 | NIST | |
| I | 1091.00 | NIST | |
| I | 1078.00 | NIST | |
| I | 1046.00 | NIST | |
| I | 1088.00 | NIST | |
| I | 1092.00 | NIST | |
| I | 1047.00 | NIST | |
| I | 1071.00 | NIST | |
| I | 1068.00 | NIST | |
| I | 1082.00 | NIST | |
| I | 1091.00 | NIST | |
| I | 1063.00 | NIST | |
| I | 1059.00 | NIST | |
| I | 1073.00 | NIST | |
| I | 1060.00 | NIST | |
| I | 1049.00 | NIST | |
| I | 1057.00 | NIST | |
| I | 1052.00 | NIST | |
| I | 1072.00 | NIST | |
| I | 1064.00 | NIST | |
| I | 1074.50 | NIST | |
| Tboil | [397.15; 399.85] | K |
|
| Tboil | 399.11 | K | Vapor liquid equilibria for the binary mixtures of 2,3-butanediol with n-butanol, n-butyl acetate, and ethyl acetate at 101.3 kPa |
| Tboil | 399.15 | K | Isobaric VLE data for the system of butan-1-ol + butylethanoate + 1-butyl-3-methylimidazoliumbis[(trifluoromethyl)sulfonyl]imide |
| Tboil | 399.07 | K | Isobaric (vapour + liquid) equilibria of binary systems containing butyl acetate for the separation of methoxy aromatic compounds (anisole and guaiacol) from biomass fast pyrolysis oil |
| Tboil | 399.26 | K | Vapour-liquid equilibrium and extractive distillation for separation of azeotrope isopropyl alcohol and diisopropyl ether |
| Tboil | 399.09 | K | Vapor Liquid Equilibria Measurements for the Five Linear C6 Esters with n-Octane |
| Tboil | 399.15 | K | Measurement and Correlation of Isobaric Vapor-Liquid Equilibrium for Binary Systems of Allyl Alcohol with Isobutyl Acetate, Butyl Acetate, and Butyl Propionate at 101.3 kPa |
| Tboil | 398.98 | K | Measurement and Modelization of VLE for Butyl Acetate with Methanol, Ethanol, 1-Propanol, and 1-Butanol. Experimental Data at 0.15 MPa |
| Tboil | 399.18 | K | Vapor-Liquid Equilibria at 101.32 kPa and Excess Properties of Binary Mixtures of Butyl Esters + tert-Butyl Alcohol |
| Tboil | 399.11 | K | Liquid-Liquid Equilibria of Water + Acetoin + Butyl Acetate at several temperatures |
| Tboil | 399.15 | K | Phase Equilibrium (VLE, LLE, and VLLE) Data of the Ternary System: Ionic Liquid [OMIM][PF6] + Butan-1-ol + Butyl Acetate |
| Tboil | 399.11 | K | Liquid Liquid Equilibria of Water + 2,3-Butanediol + Butyl Acetate at T ) 298.15 K, T ) 308.15 K, and T ) 318.15 K |
| Tboil | 399.12 | K | ChemSep v8.3 pure component data Compiled value |
| Tboil | 399.20 | K | KDB |
| Tboil | Outlier 397.15 | K | NCMS SOLV-DB |
| Tboil | 399.10 ± 0.10 | K | NIST |
| Tboil | 399.20 ± 0.40 | K | NIST |
| Tboil | 398.20 | K | NIST |
| Tboil | 399.70 | K | NIST |
| Tboil | 399.00 | K | NIST |
| Tboil | 399.20 | K | NIST |
| Tboil | 399.20 ± 0.60 | K | NIST |
| Tboil | 399.30 ± 0.50 | K | NIST |
| Tboil | 399.00 ± 2.00 | K | NIST |
| Tboil | 399.00 ± 3.00 | K | NIST |
| Tboil | 399.15 | K | NIST |
| Tboil | 399.85 ± 0.30 | K | NIST |
| Tboil | 398.00 ± 3.00 | K | NIST |
| Tboil | 398.15 ± 2.00 | K | NIST |
| Tboil | 399.15 ± 0.60 | K | NIST |
| Tboil | 399.24 ± 0.06 | K | NIST |
| Tboil | 399.26 ± 0.11 | K | NIST |
| Tboil | 398.00 ± 2.00 | K | NIST |
| Tboil | 399.40 ± 0.50 | K | NIST |
| Tboil | 398.00 ± 1.50 | K | NIST |
| Tboil | 399.65 ± 0.25 | K | NIST |
| Tboil | Outlier 397.70 ± 1.50 | K | NIST |
| Tc | [560.20; 579.10] | K |
|
| Tc | 579.00 | K | ChemSep v8.3 pure component data Compiled value |
| Tc | 579.00 | K | KDB |
| Tc | 575.40 ± 0.60 | K | NIST |
| Tc | 579.00 | K | NIST |
| Tc | 560.20 ± 10.00 | K | NIST |
| Tc | 561.00 ± 10.00 | K | NIST |
| Tc | 579.10 ± 3.00 | K | NIST |
| Tfus | [195.00; 199.65] | K |
|
| Tfus | 199.65 | K | ChemSep v8.3 pure component data Compiled value |
| Tfus | 195.00 | K | KDB |
| Tfus | 195.15 | K | NCMS SOLV-DB |
| Tfus | 199.65 | K | NIST |
| Tfus | 196.35 ± 0.30 | K | NIST |
| Ttriple | [196.03; 199.65] | K |
|
| Ttriple | 199.65 | K | ChemSep v8.3 pure component data Compiled value |
| Ttriple | 196.03 ± 0.10 | K | NIST |
| Ttriple | 196.12 ± 0.05 | K | NIST |
| UQi | 4.20 | ChemSep v8.3 pure component data Compiled value | |
| URi | 4.83 | ChemSep v8.3 pure component data Compiled value | |
| Vc | [0.400; 0.413] | m3/kmol |
|
| Vc | 0.413 | m3/kmol | ChemSep v8.3 pure component data Compiled value |
| Vc | 0.400 | m3/kmol | KDB |
| Zc | [0.2530000; 0.2609000] |
|
|
| Zc | 0.2530000 | ChemSep v8.3 pure component data Compiled value | |
| Zc | 0.2609000 | KDB | |
| Zra | [0.25; 0.26] |
|
|
| Zra | 0.25 | ChemSep v8.3 pure component data Compiled value | |
| Zra | 0.26 | KDB |
Temperature Dependent Properties
Datasets
Mass density, kg/m3
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 298.15 | 100.00 | 875.7 |
| 298.15 | 1000.00 | 876.3 |
| 298.15 | 2000.00 | 877.2 |
| 298.15 | 3000.00 | 878.0 |
| 298.15 | 3100.00 | 878.1 |
| 298.15 | 5000.00 | 879.9 |
| 298.15 | 10000.00 | 883.8 |
| 298.15 | 15000.00 | 887.6 |
| 298.15 | 20000.00 | 891.3 |
| 298.15 | 25000.00 | 894.9 |
| 298.15 | 30000.00 | 899.1 |
| 298.15 | 35000.00 | 903.7 |
| 303.15 | 100.00 | 870.4 |
| 303.15 | 1000.00 | 871.1 |
| 303.15 | 2000.00 | 872.0 |
| 303.15 | 3000.00 | 872.9 |
| 303.15 | 3100.00 | 873.0 |
| 303.15 | 5000.00 | 874.7 |
| 303.15 | 10000.00 | 878.8 |
| 303.15 | 15000.00 | 882.8 |
| 303.15 | 20000.00 | 886.5 |
| 303.15 | 25000.00 | 890.2 |
| 303.15 | 30000.00 | 894.4 |
| 303.15 | 35000.00 | 899.1 |
| 308.15 | 100.00 | 865.1 |
| 308.15 | 1000.00 | 865.9 |
| 308.15 | 2000.00 | 866.9 |
| 308.15 | 3000.00 | 867.8 |
| 308.15 | 3100.00 | 867.8 |
| 308.15 | 5000.00 | 869.6 |
| 308.15 | 10000.00 | 873.9 |
| 308.15 | 15000.00 | 878.0 |
| 308.15 | 20000.00 | 881.9 |
| 308.15 | 25000.00 | 885.6 |
| 308.15 | 30000.00 | 890.0 |
| 308.15 | 35000.00 | 894.8 |
| 313.15 | 100.00 | 859.9 |
| 313.15 | 1000.00 | 860.8 |
| 313.15 | 2000.00 | 861.7 |
| 313.15 | 3000.00 | 862.7 |
| 313.15 | 3100.00 | 862.7 |
| 313.15 | 5000.00 | 864.6 |
| 313.15 | 10000.00 | 869.0 |
| 313.15 | 15000.00 | 873.2 |
| 313.15 | 20000.00 | 877.2 |
| 313.15 | 25000.00 | 881.0 |
| 313.15 | 30000.00 | 885.6 |
| 313.15 | 35000.00 | 890.5 |
| 318.15 | 100.00 | 854.9 |
| 318.15 | 1000.00 | 855.7 |
| 318.15 | 2000.00 | 856.7 |
| 318.15 | 3000.00 | 857.8 |
| 318.15 | 3100.00 | 857.9 |
| 318.15 | 5000.00 | 859.6 |
| 318.15 | 10000.00 | 864.2 |
| 318.15 | 15000.00 | 868.5 |
| 318.15 | 20000.00 | 872.6 |
| 318.15 | 25000.00 | 876.5 |
| 318.15 | 30000.00 | 881.3 |
| 318.15 | 35000.00 | 886.3 |
| 323.15 | 100.00 | 849.7 |
| 323.15 | 1000.00 | 851.0 |
| 323.15 | 2000.00 | 852.0 |
| 323.15 | 3000.00 | 853.0 |
| 323.15 | 3100.00 | 853.1 |
| 323.15 | 5000.00 | 854.6 |
| 323.15 | 10000.00 | 859.4 |
| 323.15 | 15000.00 | 863.9 |
| 323.15 | 20000.00 | 868.1 |
| 323.15 | 25000.00 | 872.3 |
| 323.15 | 30000.00 | 877.3 |
| 323.15 | 35000.00 | 882.4 |
| 328.15 | 100.00 | 844.6 |
| 328.15 | 1000.00 | 845.7 |
| 328.15 | 2000.00 | 846.8 |
| 328.15 | 3000.00 | 847.9 |
| 328.15 | 3100.00 | 848.0 |
| 328.15 | 5000.00 | 849.7 |
| 328.15 | 10000.00 | 854.6 |
| 328.15 | 15000.00 | 859.3 |
| 328.15 | 20000.00 | 863.6 |
| 328.15 | 25000.00 | 867.8 |
| 328.15 | 30000.00 | 872.5 |
| 328.15 | 35000.00 | 877.7 |
| 333.15 | 100.00 | 839.6 |
| 333.15 | 1000.00 | 840.7 |
| 333.15 | 2000.00 | 841.8 |
| 333.15 | 3000.00 | 842.9 |
| 333.15 | 3100.00 | 842.9 |
| 333.15 | 5000.00 | 844.9 |
| 333.15 | 10000.00 | 850.0 |
| 333.15 | 15000.00 | 854.8 |
| 333.15 | 20000.00 | 859.3 |
| 333.15 | 25000.00 | 863.6 |
| 333.15 | 30000.00 | 868.6 |
| 333.15 | 35000.00 | 873.9 |
| 338.15 | 100.00 | 834.5 |
| 338.15 | 1000.00 | 835.6 |
| 338.15 | 2000.00 | 836.7 |
| 338.15 | 3000.00 | 837.9 |
| 338.15 | 3100.00 | 838.0 |
| 338.15 | 5000.00 | 840.1 |
| 338.15 | 10000.00 | 845.5 |
| 338.15 | 15000.00 | 850.1 |
| 338.15 | 20000.00 | 855.0 |
| 338.15 | 25000.00 | 859.5 |
| 338.15 | 30000.00 | 864.6 |
| 338.15 | 35000.00 | 870.1 |
| 343.15 | 100.00 | 829.5 |
| 343.15 | 1000.00 | 830.5 |
| 343.15 | 2000.00 | 831.7 |
| 343.15 | 3000.00 | 832.9 |
| 343.15 | 3100.00 | 833.0 |
| 343.15 | 5000.00 | 835.2 |
| 343.15 | 10000.00 | 840.7 |
| 343.15 | 15000.00 | 845.7 |
| 343.15 | 20000.00 | 850.5 |
| 343.15 | 25000.00 | 855.1 |
| 343.15 | 30000.00 | 860.7 |
| 343.15 | 35000.00 | 866.3 |
| 348.15 | 100.00 | 824.4 |
| 348.15 | 1000.00 | 825.4 |
| 348.15 | 2000.00 | 826.7 |
| 348.15 | 3000.00 | 827.9 |
| 348.15 | 3100.00 | 828.0 |
| 348.15 | 5000.00 | 830.5 |
| 348.15 | 10000.00 | 836.1 |
| 348.15 | 15000.00 | 841.3 |
| 348.15 | 20000.00 | 846.2 |
| 348.15 | 25000.00 | 850.9 |
| 348.15 | 30000.00 | 856.6 |
| 348.15 | 35000.00 | 862.4 |
| 353.15 | 100.00 | 819.3 |
| 353.15 | 1000.00 | 820.4 |
| 353.15 | 2000.00 | 821.7 |
| 353.15 | 3000.00 | 822.9 |
| 353.15 | 3100.00 | 823.0 |
| 353.15 | 5000.00 | 825.5 |
| 353.15 | 10000.00 | 831.3 |
| 353.15 | 15000.00 | 836.7 |
| 353.15 | 20000.00 | 841.8 |
| 353.15 | 25000.00 | 846.7 |
| 353.15 | 30000.00 | 852.5 |
| 353.15 | 35000.00 | 858.4 |
| 358.15 | 100.00 | 811.6 |
| 358.15 | 1000.00 | 813.2 |
| 358.15 | 2000.00 | 813.9 |
| 358.15 | 3100.00 | 815.3 |
| 358.15 | 5000.00 | 817.7 |
| 358.15 | 10000.00 | 823.6 |
| 358.15 | 15000.00 | 829.1 |
| 358.15 | 20000.00 | 835.5 |
| 363.15 | 100.00 | 806.1 |
| 363.15 | 1000.00 | 807.5 |
| 363.15 | 2000.00 | 808.8 |
| 363.15 | 3000.00 | 810.1 |
| 363.15 | 3100.00 | 810.3 |
| 363.15 | 5000.00 | 812.8 |
| 363.15 | 10000.00 | 819.2 |
| 363.15 | 15000.00 | 824.9 |
| 363.15 | 20000.00 | 830.4 |
| 368.15 | 100.00 | 800.3 |
| 368.15 | 1000.00 | 802.1 |
| 368.15 | 2000.00 | 803.6 |
| 368.15 | 3000.00 | 804.8 |
| 368.15 | 3100.00 | 805.0 |
| 368.15 | 5000.00 | 807.7 |
| 368.15 | 10000.00 | 814.3 |
| 368.15 | 15000.00 | 820.3 |
| 368.15 | 20000.00 | 825.9 |
| 373.15 | 100.00 | 795.8 |
| 373.15 | 1000.00 | 797.2 |
| 373.15 | 2000.00 | 798.7 |
| 373.15 | 3000.00 | 800.2 |
| 373.15 | 3100.00 | 800.4 |
| 373.15 | 5000.00 | 803.1 |
| 373.15 | 10000.00 | 809.9 |
| 373.15 | 15000.00 | 815.9 |
| 373.15 | 20000.00 | 821.3 |
| 378.15 | 100.00 | 790.4 |
| 378.15 | 1000.00 | 791.9 |
| 378.15 | 2000.00 | 793.7 |
| 378.15 | 3000.00 | 795.2 |
| 378.15 | 3100.00 | 795.4 |
| 378.15 | 5000.00 | 798.0 |
| 378.15 | 10000.00 | 804.7 |
| 378.15 | 15000.00 | 810.8 |
| 378.15 | 20000.00 | 817.1 |
| 383.15 | 100.00 | 785.2 |
| 383.15 | 1000.00 | 786.7 |
| 383.15 | 2000.00 | 788.3 |
| 383.15 | 3000.00 | 789.9 |
| 383.15 | 3100.00 | 790.0 |
| 383.15 | 5000.00 | 792.9 |
| 383.15 | 10000.00 | 800.1 |
| 383.15 | 15000.00 | 806.7 |
| 383.15 | 20000.00 | 812.8 |
| 388.15 | 100.00 | 779.9 |
| 388.15 | 1000.00 | 781.6 |
| 388.15 | 2000.00 | 783.2 |
| 388.15 | 3000.00 | 785.2 |
| 388.15 | 3100.00 | 785.4 |
| 388.15 | 5000.00 | 788.4 |
| 388.15 | 10000.00 | 795.8 |
| 388.15 | 15000.00 | 802.4 |
| 388.15 | 20000.00 | 808.6 |
| 393.15 | 100.00 | 775.2 |
| 393.15 | 1000.00 | 776.4 |
| 393.15 | 2000.00 | 778.1 |
| 393.15 | 3000.00 | 779.5 |
| 393.15 | 3100.00 | 779.7 |
| 393.15 | 5000.00 | 782.8 |
| 393.15 | 10000.00 | 790.6 |
| 393.15 | 15000.00 | 797.7 |
| 393.15 | 20000.00 | 804.2 |
| Reference | ||
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [143.60; 367.96] | J/mol×K | [273.00; 1200.00] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is Cp,gas in J/mol×K, T in K | |||
| Coefficient A | 9.28760e+01 | |||
| Coefficient B | -6.66170e+02 | |||
| Coefficient C | 6.52424e+00 | |||
| Coefficient D | -6.61480e-04 | |||
| Coefficient E | 3.06780e-07 | |||
| Comment | ChemSep eq 16, IdealGasHeatCapacityCp | |||
| Temperature range, min. | 273.00 | |||
| Temperature range, max. | 1200.00 | |||
| Cp,gas | 143.60 | J/mol×K | 273.00 | Calculated Property |
| Cp,gas | 187.24 | J/mol×K | 376.00 | Calculated Property |
| Cp,gas | 225.44 | J/mol×K | 479.00 | Calculated Property |
| Cp,gas | 256.66 | J/mol×K | 582.00 | Calculated Property |
| Cp,gas | 282.03 | J/mol×K | 685.00 | Calculated Property |
| Cp,gas | 303.08 | J/mol×K | 788.00 | Calculated Property |
| Cp,gas | 321.20 | J/mol×K | 891.00 | Calculated Property |
| Cp,gas | 337.48 | J/mol×K | 994.00 | Calculated Property |
| Cp,gas | 352.83 | J/mol×K | 1097.00 | Calculated Property |
| Cp,gas | 367.96 | J/mol×K | 1200.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | [213.92; 312.67] | J/mol×K | [202.70; 461.70] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is Cp,liquid in J/mol×K, T in K | |||
| Coefficient A | 2.01710e+02 | |||
| Coefficient B | -1.90250e+01 | |||
| Coefficient C | 1.11134e+00 | |||
| Coefficient D | 6.88890e-03 | |||
| Coefficient E | 2.15050e-06 | |||
| Comment | ChemSep eq 16, LiquidHeatCapacityCp | |||
| Temperature range, min. | 202.70 | |||
| Temperature range, max. | 461.70 | |||
| Cp,liquid | 213.92 | J/mol×K | 202.70 | Calculated Property |
| Cp,liquid | 217.18 | J/mol×K | 231.48 | Calculated Property |
| Cp,liquid | 221.33 | J/mol×K | 260.26 | Calculated Property |
| Cp,liquid | 226.65 | J/mol×K | 289.03 | Calculated Property |
| Cp,liquid | 233.47 | J/mol×K | 317.81 | Calculated Property |
| Cp,liquid | 242.25 | J/mol×K | 346.59 | Calculated Property |
| Cp,liquid | 253.62 | J/mol×K | 375.37 | Calculated Property |
| Cp,liquid | 268.37 | J/mol×K | 404.14 | Calculated Property |
| Cp,liquid | 287.58 | J/mol×K | 432.92 | Calculated Property |
| Cp,liquid | 312.67 | J/mol×K | 461.70 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [0.0014955; 0.0002523] | Pa×s | [250.00; 399.26] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = exp(A + B/T + C·ln(T) + D·T^E) Y is η in Pa×s, T in K | |||
| Coefficient A | -1.70080e+01 | |||
| Coefficient B | 1.46110e+03 | |||
| Coefficient C | 8.42400e-01 | |||
| Coefficient D | 1.11930e-07 | |||
| Coefficient E | 2.00000e+00 | |||
| Comment | ChemSep eq 101, LiquidViscosity | |||
| Temperature range, min. | 250.00 | |||
| Temperature range, max. | 399.26 | |||
| η | 0.0014955 | Pa×s | 250.00 | Calculated Property |
| η | 0.0010985 | Pa×s | 266.58 | Calculated Property |
| η | 0.0008393 | Pa×s | 283.17 | Calculated Property |
| η | 0.0006625 | Pa×s | 299.75 | Calculated Property |
| η | 0.0005376 | Pa×s | 316.34 | Calculated Property |
| η | 0.0004464 | Pa×s | 332.92 | Calculated Property |
| η | 0.0003781 | Pa×s | 349.51 | Calculated Property |
| η | 0.0003258 | Pa×s | 366.09 | Calculated Property |
| η | 0.0002848 | Pa×s | 382.68 | Calculated Property |
| η | 0.0002523 | Pa×s | 399.26 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | [53.52; 6.58] | kJ/mol | [199.65; 575.40] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A·(1 − Tr)^(B + C·Tr + D·Tr² + E·Tr³), Tr = T/Tc Y is ΔvapH in kJ/mol, T in K | |||
| Coefficient A | 8.19257e+01 | |||
| Coefficient B | 1.15159e+00 | |||
| Coefficient C | 8.89674e-02 | |||
| Coefficient D | -1.85987e+00 | |||
| Coefficient E | 1.11395e+00 | |||
| Critical temperature, Tc (K) | 5.79000e+02 | |||
| Comment | ChemSep eq 106, HeatOfVaporization | |||
| Temperature range, min. | 199.65 | |||
| Temperature range, max. | 575.40 | |||
| ΔvapH | 53.52 | kJ/mol | 199.65 | Calculated Property |
| ΔvapH | 49.18 | kJ/mol | 241.40 | Calculated Property |
| ΔvapH | 45.36 | kJ/mol | 283.15 | Calculated Property |
| ΔvapH | 41.95 | kJ/mol | 324.90 | Calculated Property |
| ΔvapH | 38.80 | kJ/mol | 366.65 | Calculated Property |
| ΔvapH | 35.69 | kJ/mol | 408.40 | Calculated Property |
| ΔvapH | 32.27 | kJ/mol | 450.15 | Calculated Property |
| ΔvapH | 27.94 | kJ/mol | 491.90 | Calculated Property |
| ΔvapH | 21.47 | kJ/mol | 533.65 | Calculated Property |
| ΔvapH | 6.58 | kJ/mol | 575.40 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.66] | kPa | [294.21; 424.78] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.46670e+01 | |||
| Coefficient B | -3.49621e+03 | |||
| Coefficient C | -5.10730e+01 | |||
| Temperature range, min. | 294.21 | |||
| Temperature range, max. | 424.78 | |||
| Pvap | 1.33 | kPa | 294.21 | Calculated Property |
| Pvap | 3.00 | kPa | 308.72 | Calculated Property |
| Pvap | 6.18 | kPa | 323.23 | Calculated Property |
| Pvap | 11.83 | kPa | 337.73 | Calculated Property |
| Pvap | 21.29 | kPa | 352.24 | Calculated Property |
| Pvap | 36.30 | kPa | 366.75 | Calculated Property |
| Pvap | 59.05 | kPa | 381.26 | Calculated Property |
| Pvap | 92.20 | kPa | 395.76 | Calculated Property |
| Pvap | 138.89 | kPa | 410.27 | Calculated Property |
| Pvap | 202.66 | kPa | 424.78 | Calculated Property |
| Pvap | [2.12e-04; 3930.98] | kPa | [199.65; 575.40] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = exp(A + B/T + C·ln(T) + D·T^E) Y is Pvap in kPa, T in K | |||
| Coefficient A | 8.35202e+01 | |||
| Coefficient B | -7.62534e+03 | |||
| Coefficient C | -1.02228e+01 | |||
| Coefficient D | 8.98721e-06 | |||
| Coefficient E | 2.00000e+00 | |||
| Comment | ChemSep eq 101, VaporPressure | |||
| Temperature range, min. | 199.65 | |||
| Temperature range, max. | 575.40 | |||
| Pvap | 2.12e-04 | kPa | 199.65 | Calculated Property |
| Pvap | 0.03 | kPa | 241.40 | Calculated Property |
| Pvap | 0.67 | kPa | 283.15 | Calculated Property |
| Pvap | 6.52 | kPa | 324.90 | Calculated Property |
| Pvap | 35.56 | kPa | 366.65 | Calculated Property |
| Pvap | 132.38 | kPa | 408.40 | Calculated Property |
| Pvap | 381.64 | kPa | 450.15 | Calculated Property |
| Pvap | 924.25 | kPa | 491.90 | Calculated Property |
| Pvap | 1985.77 | kPa | 533.65 | Calculated Property |
| Pvap | 3930.98 | kPa | 575.40 | Calculated Property |
| Pvap | [1.41e-04; 3056.18] | kPa | [199.65; 579.15] |
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 | 8.07098e+01 | |||
| Coefficient B | -7.79009e+03 | |||
| Coefficient C | -9.58507e+00 | |||
| Coefficient D | 5.19348e-06 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 199.65 | |||
| Temperature range, max. | 579.15 | |||
| Pvap | 1.41e-04 | kPa | 199.65 | Calculated Property |
| Pvap | 0.02 | kPa | 241.82 | Calculated Property |
| Pvap | 0.64 | kPa | 283.98 | Calculated Property |
| Pvap | 6.72 | kPa | 326.15 | Calculated Property |
| Pvap | 37.57 | kPa | 368.32 | Calculated Property |
| Pvap | 138.45 | kPa | 410.48 | Calculated Property |
| Pvap | 383.82 | kPa | 452.65 | Calculated Property |
| Pvap | 871.75 | kPa | 494.82 | Calculated Property |
| Pvap | 1717.87 | kPa | 536.98 | Calculated Property |
| Pvap | 3056.18 | kPa | 579.15 | Calculated Property |
| Pvap | [9.20; 101.26] | kPa | [332.89; 399.24] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.44327e+01 | |||
| Coefficient B | -3.31625e+03 | |||
| Coefficient C | -6.13620e+01 | |||
| Reference | Kliment, Fried, et al., 1964 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 332.89 | |||
| Temperature range, max. | 399.24 | |||
| Pvap | 9.20 | kPa | 332.89 | Calculated Property |
| Pvap | 12.71 | kPa | 340.26 | Calculated Property |
| Pvap | 17.26 | kPa | 347.63 | Calculated Property |
| Pvap | 23.09 | kPa | 355.01 | Calculated Property |
| Pvap | 30.44 | kPa | 362.38 | Calculated Property |
| Pvap | 39.61 | kPa | 369.75 | Calculated Property |
| Pvap | 50.92 | kPa | 377.12 | Calculated Property |
| Pvap | 64.71 | kPa | 384.50 | Calculated Property |
| Pvap | 81.35 | kPa | 391.87 | Calculated Property |
| Pvap | 101.26 | kPa | 399.24 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ρl | [962.52; 334.86] | kg/m3 | [199.65; 575.40] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A / B^(1 + (1 − T/C)^D) Y is ρl in kg/m3, T in K | |||
| Coefficient A | 1.57836e+01 | |||
| Coefficient B | 1.19300e-01 | |||
| Coefficient C | 5.79000e+02 | |||
| Coefficient D | 1.63050e-01 | |||
| Comment | ChemSep eq 105, LiquidDensity | |||
| Temperature range, min. | 199.65 | |||
| Temperature range, max. | 575.40 | |||
| ρl | 962.52 | kg/m3 | 199.65 | Calculated Property |
| ρl | 927.21 | kg/m3 | 241.40 | Calculated Property |
| ρl | 889.55 | kg/m3 | 283.15 | Calculated Property |
| ρl | 848.98 | kg/m3 | 324.90 | Calculated Property |
| ρl | 804.66 | kg/m3 | 366.65 | Calculated Property |
| ρl | 755.30 | kg/m3 | 408.40 | Calculated Property |
| ρl | 698.68 | kg/m3 | 450.15 | Calculated Property |
| ρl | 630.34 | kg/m3 | 491.90 | Calculated Property |
| ρl | 538.43 | kg/m3 | 533.65 | Calculated Property |
| ρl | 334.86 | kg/m3 | 575.40 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| γ | [0.04; 8.05e-06] | N/m | [199.65; 574.65] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is γ in N/m, T in K | |||
| Coefficient A | -1.67320e-02 | |||
| Coefficient B | 1.75590e+01 | |||
| Coefficient C | -2.79050e+00 | |||
| Coefficient D | -6.41210e-04 | |||
| Coefficient E | -2.91180e-06 | |||
| Comment | ChemSep eq 16, SurfaceTension, ChemSep Tmax 575.4 K | |||
| Temperature range, min. | 199.65 | |||
| Temperature range, max. | 574.65 | |||
| γ | 0.04 | N/m | 199.65 | Calculated Property |
| γ | 0.03 | N/m | 241.32 | Calculated Property |
| γ | 0.03 | N/m | 282.98 | Calculated Property |
| γ | 0.02 | N/m | 324.65 | Calculated Property |
| γ | 0.02 | N/m | 366.32 | Calculated Property |
| γ | 0.01 | N/m | 407.98 | Calculated Property |
| γ | 0.01 | N/m | 449.65 | Calculated Property |
| γ | 0.01 | N/m | 491.32 | Calculated Property |
| γ | 0.00 | N/m | 532.98 | Calculated Property |
| γ | 8.05e-06 | N/m | 574.65 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λ | [0.00; 0.08] | W/m×K | [199.65; 800.00] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A·T^B / (1 + C/T + D/T²) Y is λ in W/m×K, T in K | |||
| Coefficient A | 5.93640e-09 | |||
| Coefficient B | 2.37390e+00 | |||
| Coefficient C | -4.02220e+02 | |||
| Coefficient D | 6.96060e+04 | |||
| Comment | ChemSep eq 102, VaporThermalConductivity | |||
| Temperature range, min. | 199.65 | |||
| Temperature range, max. | 800.00 | |||
| λ | 0.00 | W/m×K | 199.65 | Calculated Property |
| λ | 0.01 | W/m×K | 266.36 | Calculated Property |
| λ | 0.01 | W/m×K | 333.06 | Calculated Property |
| λ | 0.02 | W/m×K | 399.77 | Calculated Property |
| λ | 0.03 | W/m×K | 466.47 | Calculated Property |
| λ | 0.04 | W/m×K | 533.18 | Calculated Property |
| λ | 0.04 | W/m×K | 599.88 | Calculated Property |
| λ | 0.05 | W/m×K | 666.59 | Calculated Property |
| λ | 0.06 | W/m×K | 733.29 | Calculated Property |
| λ | 0.08 | W/m×K | 800.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λ | [0.16; 0.10] | W/m×K | [199.65; 463.15] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is λ in W/m×K, T in K | |||
| Coefficient A | 4.36600e-02 | |||
| Coefficient B | -1.25650e+02 | |||
| Coefficient C | -4.06860e-01 | |||
| Coefficient D | -5.93050e-03 | |||
| Coefficient E | 2.41670e-06 | |||
| Comment | ChemSep eq 16, LiquidThermalConductivity | |||
| Temperature range, min. | 199.65 | |||
| Temperature range, max. | 463.15 | |||
| λ | 0.16 | W/m×K | 199.65 | Calculated Property |
| λ | 0.16 | W/m×K | 228.93 | Calculated Property |
| λ | 0.15 | W/m×K | 258.21 | Calculated Property |
| λ | 0.14 | W/m×K | 287.48 | Calculated Property |
| λ | 0.13 | W/m×K | 316.76 | Calculated Property |
| λ | 0.12 | W/m×K | 346.04 | Calculated Property |
| λ | 0.12 | W/m×K | 375.32 | Calculated Property |
| λ | 0.11 | W/m×K | 404.59 | Calculated Property |
| λ | 0.10 | W/m×K | 433.87 | Calculated Property |
| λ | 0.10 | W/m×K | 463.15 | Calculated Property |
Similar Compounds
Find more compounds similar to Acetic acid, butyl ester.
Mixtures
- Acetonitrile + Acetic acid, butyl ester
- Acetonitrile + Acetic acid, butyl ester + Water
- Acetic acid, butyl ester + Acetone
- Acetic acid, butyl ester + Acetone + Water
- Ethanol + Acetic acid, butyl ester + Acetone
- 1,2-Ethanediol + Acetic acid, butyl ester
- Ethanol + Acetic acid, butyl ester
- Ethanol + Acetic acid, butyl ester + Water
- Benzene + Ethanol + Acetic acid, butyl ester
- Ethanol + Acetic acid, butyl ester + Cyclohexane + Water
- Ethanol + 1-Butanol + Acetic acid, butyl ester + Ethyl Acetate
- Ethanol + Acetic acid, butyl ester + Ethyl Acetate
- Acetic acid, butyl ester + Ethyl Acetate
- Acetic acid, butyl ester + Ethyl Acetate + Water
- Benzene + Acetic acid, butyl ester + Ethyl Acetate
- Benzene + Acetic acid, butyl ester + Ethyl Acetate + Water
- Benzene + 1-Butanol + Acetic acid, butyl ester
- Benzene + Acetic acid, butyl ester
- Benzene + Acetic acid, butyl ester + Water
- 1-Butanol + Acetic acid, butyl ester
Find more mixtures with Acetic acid, butyl ester.
Sources
- KDB Vapor Pressure Data
- ChemSep v8.3 pure component data Converted from ChemSep v8.3 pure component data, H. Kooijman and R. Taylor (2021, 2022), Artistic License 2.0; see how the values differ.
- Dortmund Data Bank Vapor-Liquid Equilibrium Data
- Effect of Temperature on the Change of Refractive Index on Mixing for Butyl Acetate + Aromatic Hydrocarbons
- Densities, Excess Molar Volumes, Viscosities, and Refractive Indices of Binary Mixtures of n-Butyl Acetate with 1-Chloroalkanes (C4 C8) at 298.15 K
- Excess Volumes and Excess Isentropic Compressibilities of Binary Liquid Mixtures of Trichloroethylene with Esters at 303.15 K
- Topological and thermodynamic investigations of molecular interactions in binary mixtures: Molar excess volumes and molar excess enthalpies
- Experimental isobaric vapour liquid liquid equilibrium data for the quaternary systems water (1) ethanol (2) acetone (3) n-butyl acetate (4) and water (1) ethanol (2) acetone (3) methyl ethyl ketone (4) and their partially miscible-constituent ternaries
- Vapor liquid equilibria for the binary mixtures of 2,3-butanediol with n-butanol, n-butyl acetate, and ethyl acetate at 101.3 kPa
- Solubility and limiting activity coefficient of simvastatin in different organic solvents
- Liquid liquid equilibrium of ternary mixture (propargyl alcohol +water + butyl acetate)
- Solubility of lansoprazole in different solvents
- Isobaric VLE data for the system of butan-1-ol + butylethanoate + 1-butyl-3-methylimidazoliumbis[(trifluoromethyl)sulfonyl]imide
- Liquid-liquid equilibria for ternary systems acetic acid + n-butylacetate + hydrocarbons at 293.15 K
- Temperature dependence of limiting activity coefficients, Henry's law constants, and related infinite dilution properties of C4-C6 isomeric n-alkyl ethanoates/ethyl n-alkanoates in water. Measurement, critical compilation, correlation, and recommended data
- Phase equilibria of (water + butyric acid + butyl acetate) ternary systems at different temperatures
- Liquid-liquid equilibrium for the ternary system water + 2-methyl-1-propanol + butyl acetate and water + 2-methyl-2-propanol + butyl acetate at (298.15 and 323.15) K
- Liquid-liquid equilibrium and critical states for the system acetic acid + n-butanol + n-butyl acetate + water at 308.15 K
- Measurement and correlation of solubility of D-camphor-10-sulfonic acid in pure solvents
- Solution thermodynamics of simvastatin in pure solvents and binary solvent mixtures
- Liquid-liquid equilibrium data for water + formic acid + solvent (butyl acetate, ethyl acetate, and isoamyl alcohol) at T = 291.15 K
- Abraham model linear free energy relationships for describing the partitioning and solubility behavior of nonelectrolyte organic solutes dissolved in pyridine at 298.15 K
- Isothermal vapor-liquid equilibria, excess molar volume and the deviation of refractive indices for binary mixtures of 1-butanol, 1- hexanol, 3-methyl-1-butanol and butyl acetate
- Liquid-liquid equilibrium determination and thermodynamics modeling for extraction of isopropanol from its aqueous solution
- Liquid-liquid equilibria and COSMO-SAC modeling of organic solvent/ ionic liquid - hydroxyacetone - water mixtures
- Liquid-liquid equilibrium data for ternary systems of water + acetic acid + acetate esters at 293.2 K and 303.2 K and ~ 95 kPa
- Quaternary liquid-liquid equilibrium, solubility and critical states: Acetic acid - n-butanol - n-butyl acetate - water at 318.15 K and atmospheric pressure
- Thermodynamic properties of (an ester + an alkane). XVI. Experimental HEm and V Em values and a new correlation method for (an alkyl ethanoate + an n-alkane) at 318.15 K
- Properties of ionic liquid HMIMPF6 with carbonates, ketones and alkyl acetates
- Thermodynamic study of (alkyl esters + a,x-alkyl dihalides)III. HE m and V E m for 20 binary mixtures {xCu-1H2u-1CO2C4H9 + (1 - x)a,x-ClCH2(CH2)v-2CH2Cl}, where u = 1 to 4, a = 1 and v = x = 2 to 6
- Molecular interactions in (2,4,6-trimethyl-1,3,5-trioxane + n-alkyl acetates) at T=(298.15, 303.15, and 308.15) K
- Densities, speeds of sound, and refractive indices of the ternary mixtures (toluene + methyl acetate + butyl acetate) and (toluene + methyl acetate + methyl heptanoate) at 298.15 K
- Densities, surface tensions, and derived surface thermodynamics properties of (trimethylbenzene + propyl acetate, or butyl acetate) from T = 298.15 K to 313.15 K
- Liquid phase equilibria of (water + phosphoric acid + 1-butanol or butyl acetate) ternary systems at T = 308.2 K
- Experimental and theoretical study of surface tension of binary mixtures of (n-alkyl acetates + heptane, benzene, and toluene)
- Thermodynamic study of (alkyl esters + alpha,beta-alkyl dihalides) VI.H and V for 20 binary mixtures {xCu-1H2u-1CO2(CH2)3CH3 + (1 - x)alpha,omega-BrCH2(CH2)v-2CH2Br}, where u = 1 to 5, alpha = 1, and v = omega = 2 to 6
- Application of ERAS-model and Prigogine-Flory-Patterson theory to excess molar volumes for ternary mixtures of (2-chlorobutane + butylacetate + isobutanol) at T = 298.15 K
- Study on thermo physical and excess molar properties of binary systems of ionic liquids. I: [Cnmim][PF6] (n = 6, 8) and alkyl acetates
- Thermodynamics of 4'-bromomethyl-2-cyanobiphenyl in different solvents
- Isobaric (vapour + liquid) equilibria of binary systems containing butyl acetate for the separation of methoxy aromatic compounds (anisole and guaiacol) from biomass fast pyrolysis oil
- Solution thermodynamics of valnemulin hydrogen fumarate in different pure solvents
- Thermodynamic equilibrium of 4-hydroxy-2,5-dimethyl-3(2H)-furanone in different solvent systems
- Binary mixtures of ([C4mim][NTf2] + molecular organic solvents): Thermophysical, acoustic and transport properties at various compositions and temperatures
- Measurement and correlation of solubility and solution thermodynamics of 1,3-dimethylurea in different solvents from T = (288.15 to 328.15) K
- Solid-liquid phase equilibrium and mixing properties of 2-Cyano-4'-methylbiphenyl in pure solvents
- Solubility and thermodynamic properties of vanillyl alcohol in some pure solvents
- Measurement and thermodynamic modelling of ternary liquid-liquid equilibrium for extraction of thioglycolic acid from aqueous solution with different solvents
- Vapour-liquid equilibrium and extractive distillation for separation of azeotrope isopropyl alcohol and diisopropyl ether
- Densities, speeds of sound, isentropic compressibilities, refractive indexes, and viscosities of tetrahydrofuran with haloalkane or alkyl ethanoate at T = 303.15 K
- Studies of viscosities of dilute solutions of alkylamine in non-electrolyte solvents. II. Haloalkanes and other polar solvents
- Studies on liquid liquid interactions of some ternary mixtures by density, viscosity, ultrasonic speed and refractive index measurements
- Examination of hydrogen-bonding interactions between dissolved solutes and alkylbenzene solvents based on Abraham model correlations derived from measured enthalpies of solvation
- Effect of halogen substitution on the enthalpies of solvation and hydrogen bonding of organic solutes in chlorobenzene and 1,2-dichlorobenzene derived using multi-parameter correlations
- Determination and correlation of solubility and mixing properties of isonicotinamide (form II) in some pure solvents
- Enthalpies of solution and enthalpies of solvation of organic solutes in ethylene glycol at 298.15 K: Prediction and analysis of intermolecular interaction contributions
- Solubility and Caloric Properties of Cinnarizine
- Vapor Liquid Equilibria Measurements for the Five Linear C6 Esters with n-Octane
- Liquid Liquid Equilibria for the Ternary System n-Butyl Acetate + Pyrocatechol + Water at Different Temperatures at 101.3 kPa
- Measurement and Correlation of Solubility on Reactive Crystallization of Methyl D-(-)-4-Hydroxy-phenylglycinate
- Phase Equilibrium Measurement and Thermodynamic Modeling of the 4-Methylpentan-2-one/3-Methylphenol, and 4-Methylphenol/Water Ternary Systems at 298.2, 313.2, and 323.2 K and 0.1 MPa
- Isobaric Vapor Liquid Equilibrium for Binary Systems of Thioglycolic Acid with Water, Butyl Acetate, Butyl Formate, and Isobutyl Acetate at 101.3 kPa
- Measurement and Correlation of Solubility of Amorphous Cefmetazole Sodium in Pure Solvents and Binary Solvent Mixtures
- Measurement and Correlation of the Solubility of e-CL-20 in 12 Organic Solvents at Temperatures Ranging from 278.15 to 318.15 K
- Ternary Liquid Liquid Equilibrium of Azeotropes (Ester + Alcohol) with Different Ionic Liquids at T = 298.15 K
- Measurements and Modeling of VLE Data for Butyl Acetate with 2-Propanol or 2-Butanol. Binary Systems at 0.15 and 0.6 MPa
- 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
- Solubility Modeling and Mixing Properties for Benzoin in Different Monosolvents and Solvent Mixtures at the Temperature Range from 273.15 to 313.15 K
- Determination and Thermodynamic Analysis of the Solubility of Limonin in Eight Organic Solvents and Ethyl Acetate + 2-Propanol Binary Solvents from 283.2 to 323.2 K
- Measurement and Correlation of Isobaric Vapor-Liquid Equilibrium for Binary Systems of Allyl Alcohol with Isobutyl Acetate, Butyl Acetate, and Butyl Propionate at 101.3 kPa
- Measurement and Modelization of VLE for Butyl Acetate with Methanol, Ethanol, 1-Propanol, and 1-Butanol. Experimental Data at 0.15 MPa
- Investigation of Molecular Interactions in Binary Mixtures of n-Butyl Acetate and (C6 - C10) 1-Alkanol: PC-SAFT Model
- Solubility Determination of Nicotinamide and Its Application for the Cocrystallization with Benzoic Acid
- Solubility Measurement and Correlation of Probenecid in 12 Pure Organic Solvents and Thermodynamic Properties of Mixing of Solutions
- Volumetric and FT-IR Studies of the Binary Liquid Mixtures of Tributylamine and Alkyl Ester (C1-C5)
- Determination and Modeling of Solubility of 4-Aminobenzamide in Different Pure Solvents
- Liquid-Liquid Equilibrium Measurements and Correlation for Ternary Systems (Butyl Acetate + 1-Butanol + Ethylene Glycol/1,3-Propanediol/Ethanolamine) at 298.15 K
- Solubility and Thermodynamic Modeling of Dimethyl Terephthalate in Pure Solvents and the Evaluation of the Mixing Properties of the Solutions
- 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
- Vapor-Liquid Equilibria at 101.32 kPa and Excess Properties of Binary Mixtures of Butyl Esters + tert-Butyl Alcohol
- Thermodynamics of Phase and Chemical Equilibrium in a Strongly Nonideal Esterification System.
- Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
- Density and Viscosity for a Binary Mixture of cis-3-Hexenyl Formate, Butyl Acetate, trans-2-Hexenyl Acetate, and cis-3-Hexenyl Acetate with Ethanol at Several Temperatures
- Liquid-Liquid Equilibria for Water + Benzonitrile + Ethyl Acetate or + Butyl Acetate
- Solubility of Lovastatin in Acetone, Methanol, Ethanol, Ethyl Acetate, and Butyl Acetate between 283 K and 323 K
- Solubility of Hydroquinone in Different Solvents from 276.65 K to 345.10 K
- Excess Molar Volumes and Viscosity Deviations of Binary Liquid Mixtures of 1,3-Dioxolane and 1,4-Dioxane with Butyl Acetate, Butyric Acid, Butylamine, and 2-Butanone at 298.15 K
- Solubility of o-Phthalic Acid in Methanol + Water and Methanol + Butyl Acetate from (295.87 to 359.75) K
- PVT Property Measurements for Some Aliphatic Esters from (298 to 393) K and up to 35 MPa
- Viscosities and Interfacial Properties of I-Methyl-3-butylimidazolium Hexafluorophosphate and 1-Isobutenyl-3-methylimidazolium Tetrafluoroborate Ionic Liquids
- Solubility of 1H-1,2,4-Triazole in Ethanol, 1-Propanol, 2-Propanol, 1,2-Propanediol, Ethyl Formate, Methyl Acetate, Ethyl Acetate, and Butyl Acetate at (283 to 363) K
- Solubility of 3-Nitrophthalic Acid in Different Solvents between 278 K and 353 K
- Liquid-Liquid Equilibrium in Systems with an Ionic Liquid: Experimental Data for an Example of the Biphasic Acid Scavenging Utilizing Ionic Liquids Process
- Activity Coefficients at Infinite Dilution for Hydrocarbons in Fatty Alcohols Determined by Gas-Liquid Chromatography
- Liquid-Liquid Equilibria of Water + Acetoin + Butyl Acetate at several temperatures
- Solubilities of Phloretin in 12 Solvents at Different Temperatures
- Solubilities of Betulinic Acid in Thirteen Organic Solvents at Different Temperatures
- Activity Coefficients at Infinite Dilution by GLC in Alkanediamines as Stationary Phases
- Density and Viscosity of Binary Mixtures of n-Butyl Acetate with Ketones at (298.15, 303.15, 308.15, and 313.15) K
- Biomass-Derived Platform Chemicals: Thermodynamic Studies on the Extraction of 5-Hydroxymethylfurfural from Ionic Liquids
- Determination and Prediction of Vapor Liquid Equilibria for a System Containing Water + Butyl Acetate + Cyclohexane + Ethanol
- Densities and Speeds of Sound of Binary Liquid Mixtures of Some n-Alkoxypropanols with Methyl Acetate, Ethyl Acetate, and n-Butyl Acetate at T = (288.15, 293.15, 298.15, 303.15, and 308.15) K
- Vapor Liquid Equilibrium at 350 K, Excess Molar Enthalpies at 298 K, and Excess Molar Volumes at 298 K of Binary Mixtures Containing Ethyl Acetate, Butyl Acetate, and 2-Butanol
- Vapor Liquid Equilibrium for Several Compounds Relevant to the Biofuels Industry Modeled with the Wilson Equation
- Phase Equilibrium (VLE, LLE, and VLLE) Data of the Ternary System: Ionic Liquid [OMIM][PF6] + Butan-1-ol + Butyl Acetate
- Solubility Determination and Thermodynamic Models for 2-Methylnaphthalene in Different Solvents from T = (278.15 to 303.15) K
- Liquid-Liquid Equilibria for the Ternary Systems Acetic Acid + Water + Butyl Acetate and Acetic Acid + Water + 2-Methyl Propyl Acetate at 304.15 K, 332.15 K, and 366.15 K
- Solubility of Chlorpheniramine Maleate in Ethanol, 1-Propanol, 1-Butanol, Benzene, Ethyl Acetate, Ethyl Formate, and Butyl Acetate between 283 K and 333 K
- Solubility of 1-H-Tetrazole-1-acetic Acid in Different Solvents between 283 K and 323 K
- Phase Equilibrium for the Esterification Reaction of Acetic Acid + Butan-1-ol at 101.3 kPa
- Henry s Law Constants for Fragrance and Organic Solvent Compounds in Aqueous Industrial Surfactants
- Liquid Liquid Equilibria of Water + 2,3-Butanediol + Butyl Acetate at T ) 298.15 K, T ) 308.15 K, and T ) 318.15 K
- Solubility of Losartan Potassium in Different Pure Solvents from (293.15 to 343.15) K
- Solubility of Lovastatin in Ethyl Acetate, Propyl Acetate, Isopropyl Acetate, Butyl Acetate, sec-Butyl Acetate, Isobutyl Acetate, tert-Butyl Acetate, and 2-Butanone, between (285 and 313) K
- Ternary Liquid-Liquid Equilibria for Systems Containing Alcohol or Acetic Acid + Ester + 1-Ethyl-3-methylimidazolium Hydrogen Sulfate at 313.2 K Using Headspace Gas Chromatography
- Densities, Viscosities, and Speeds of Sound of Binary Liquid Mixtures of Sulfolane with Ethyl Acetate, n-Propyl Acetate, and n-Butyl Acetate at Temperature of (303.15, 308.15, and 313.15) K
- Solubility of Cloxacillin Sodium in Different Binary Solvents
- Solubility of Valsartan in Different Organic Solvents and Ethanol + Water Binary Mixtures from (278.15 to 313.15) K
- Solubility of Tiamulin Hydrogen Fumarate in Acetone, Acetonitrile, Ethyl Acetate, Ethyl Formate, and Butyl Acetate from (288.2 to 318.2) K
- Solubility of 2-Aminopyridine in Ethanol + n-Butyl Acetate from (288.15 to 318.15) K
- Isobaric Vapor-Liquid Equilibria for the Binary Systems Benzene + Methyl Ethanoate, Benzene + Butyl Ethanoate, and Benzene + Methyl Heptanoate at 101.31kPa
- Solubility of 3-Aminopyridine in Acetone + n-Butyl Acetate from (288.15 to 323.15) K
- Surface Tension and Surface Properties of Binary Mixtures of 1,4-Dioxane or N,N-Dimethyl Formamide with n-Alkyl Acetates
- Solubility of Penicillin Sulfoxide in Different Solvents
- Liquid-Liquid Equilibria, Density, Viscosity, and Surface and Interfacial Tension of the System Water + n-Butyl Acetate + 1-Propanol at 323.15 K and Atmospheric Pressure
- Solubility of Captopril in 2-Propanol, Acetone, Acetonitrile, Methyl Acetate, Ethyl Acetate, and Butyl Acetate
- Densities, Sound Speed, and IR Studies of (Methanol + 1-Acetoxybutane) and (Methanol + 1,1-Dimethylethyl Ester) at (298.15, 303.15, 308.15, and 313.15) K
- Study of Ether-, Alcohol-, or Cyano-Functionalized Ionic Liquids Using Inverse Gas Chromatography
- Surface Tension Data of Aqueous Binary Mixtures of Methyl, Ethyl, Propyl, and Butyl Acetates at 298.15 K
- Joback Method
- KDB
- Aqueous Solubility Prediction Method
- McGowan Method
- NIST Webbook
- NCMS SOLV-DB
- The Yaws Handbook of Vapor Pressure
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