- InChI
- InChI=1S/C4H8O2/c1-2-3-4(5)6/h2-3H2,1H3,(H,5,6)
- InChI Key
- FERIUCNNQQJTOY-UHFFFAOYSA-N
- Formula
- C4H8O2
- SMILES
- CCCC(=O)O
- Molecular Weight1
- 88.11
- CAS
- 107-92-6
- Other Names
-
- 1-Butanoic acid
- 1-Butyric acid
- 1-propanecarboxylic acid
- Butanic acid
- Buttersaeure
- Ethylacetic acid
- Kyselina maselna
- NSC 8415
- Propanecarboxylic acid
- Propylformic acid
- UN 2820
- butyric acid
- n-C3H7COOH
- n-butanoic acid
- n-butyric acid
- 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).
- 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).
- 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).
- ΔsubH : Enthalpy of sublimation 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).
- NFPA Fire : NFPA Fire Rating.
- NFPA Health : NFPA Health 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.
- 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).
- 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.
- 1: Molecular weight from the IUPAC atomic weights tables.
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Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ω | [0.6830; 0.7200] |
|
|
| ω | 0.7200 | ChemSep v8.3 pure component data | |
| ω | 0.6830 | KDB | |
| Tig | 723.15 | K | KDB |
| ΔcH°liquid | -2183.50 ± 0.59 | kJ/mol | NIST |
| μ | [1.50; 1.65] | debye |
|
| μ | 1.65 | debye | ChemSep v8.3 pure component data |
| μ | 1.50 | debye | KDB |
| η | 0.0013960 | 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 |
| LFL | 2.19 | % in Air | KDB |
| UFL | 13.40 | % in Air | KDB |
| Tflash,cc | 347.59 | K | KDB |
| Tflash,oc | 344.26 | K | KDB |
| ΔfG° | -360.00 | kJ/mol | ChemSep v8.3 pure component data |
| ΔfH°gas | [-476.20; -475.80] | kJ/mol |
|
| ΔfH°gas | -475.80 | kJ/mol | ChemSep v8.3 pure component data |
| ΔfH°gas | -476.20 | kJ/mol | KDB |
| ΔfH°gas | -475.90 ± 4.00 | kJ/mol | NIST |
| ΔfH°gas | -475.90 ± 4.00 | kJ/mol | NIST |
| ΔfH°liquid | -533.92 ± 0.59 | kJ/mol | NIST |
| ΔfusH° | 16.26 | kJ/mol | Joback Calculated Property |
| ΔvapH° | [58.00; 60.70] | kJ/mol |
|
| ΔvapH° | 58.50 | kJ/mol | NIST |
| ΔvapH° | 58.20 ± 0.30 | kJ/mol | NIST |
| ΔvapH° | Outlier 60.70 | kJ/mol | NIST |
| ΔvapH° | 58.00 | kJ/mol | NIST |
| ΔvapH° | 58.00 ± 4.00 | kJ/mol | NIST |
| ΔvapH° | 58.00 ± 4.00 | kJ/mol | NIST |
| IE | [10.16; 10.46] | eV |
|
| IE | 10.17 ± 0.05 | eV | NIST |
| IE | 10.17 ± 0.05 | eV | NIST |
| IE | 10.24 | eV | NIST |
| IE | 10.24 | eV | NIST |
| IE | Outlier 10.46 | eV | NIST |
| IE | 10.16 ± 0.05 | eV | NIST |
| IE | 10.38 | eV | NIST |
| IE | 10.22 | eV | NIST |
| log10WS | -0.19 | Aq. Solubility Prediction | |
| logPoct/wat | 0.871 | Crippen Calculated Property | |
| McVol | 74.660 | ml/mol | McGowan Calculated Property |
| NFPA Fire | 2 | KDB | |
| NFPA Health | 2 | KDB | |
| Pc | [3950.00; 4094.07] | kPa |
|
| Pc | 4030.00 | kPa | ChemSep v8.3 pure component data |
| Pc | 4030.00 | kPa | KDB |
| Pc | 4064.00 ± 60.00 | kPa | NIST |
| Pc | 3950.00 ± 50.00 | kPa | NIST |
| Pc | 4094.07 ± 90.00 | kPa | NIST |
| Ptriple | 0.01 | kPa | ChemSep v8.3 pure component data |
| Inp | [763.00; 856.00] |
|
|
| Inp | 828.00 | NIST | |
| Inp | 834.00 | NIST | |
| Inp | 789.00 | NIST | |
| Inp | 790.00 | NIST | |
| Inp | 823.00 | NIST | |
| Inp | 822.00 | NIST | |
| Inp | Outlier 850.00 | NIST | |
| Inp | 840.00 | NIST | |
| Inp | 824.00 | NIST | |
| Inp | 831.00 | NIST | |
| Inp | Outlier 848.00 | NIST | |
| Inp | 841.00 | NIST | |
| Inp | 790.00 | NIST | |
| Inp | 844.00 | NIST | |
| Inp | 820.00 | NIST | |
| Inp | 823.00 | NIST | |
| Inp | 818.00 | NIST | |
| Inp | 780.00 | NIST | |
| Inp | 804.00 | NIST | |
| Inp | 818.00 | NIST | |
| Inp | 818.00 | NIST | |
| Inp | 780.00 | NIST | |
| Inp | 834.00 | NIST | |
| Inp | 826.00 | NIST | |
| Inp | Outlier 856.00 | NIST | |
| Inp | 820.00 | NIST | |
| Inp | 802.00 | NIST | |
| Inp | 795.00 | NIST | |
| Inp | 778.00 | NIST | |
| Inp | 822.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 815.00 | NIST | |
| Inp | 817.00 | NIST | |
| Inp | 812.00 | NIST | |
| Inp | 808.00 | NIST | |
| Inp | 780.00 | NIST | |
| Inp | 815.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 790.00 | NIST | |
| Inp | 826.00 | NIST | |
| Inp | 830.00 | NIST | |
| Inp | 829.00 | NIST | |
| Inp | 814.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 835.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 820.00 | NIST | |
| Inp | 785.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 823.00 | NIST | |
| Inp | 823.00 | NIST | |
| Inp | 784.00 | NIST | |
| Inp | 803.00 | NIST | |
| Inp | 803.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | Outlier 856.00 | NIST | |
| Inp | Outlier 763.00 | NIST | |
| Inp | 786.00 | NIST | |
| Inp | 791.00 | NIST | |
| Inp | 779.00 | NIST | |
| Inp | 804.00 | NIST | |
| Inp | 795.00 | NIST | |
| Inp | 805.00 | NIST | |
| Inp | 824.00 | NIST | |
| Inp | 769.00 | NIST | |
| Inp | 802.00 | NIST | |
| Inp | 779.00 | NIST | |
| Inp | 775.00 | NIST | |
| Inp | 809.00 | NIST | |
| Inp | 778.00 | NIST | |
| Inp | 825.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 784.00 | NIST | |
| Inp | 829.00 | NIST | |
| Inp | 829.00 | NIST | |
| Inp | 803.00 | NIST | |
| Inp | 796.00 | NIST | |
| Inp | 783.00 | NIST | |
| Inp | 780.00 | NIST | |
| Inp | 779.00 | NIST | |
| Inp | 784.00 | NIST | |
| Inp | 783.00 | NIST | |
| Inp | 803.00 | NIST | |
| Inp | 795.00 | NIST | |
| Inp | 773.00 | NIST | |
| Inp | 777.00 | NIST | |
| Inp | 789.00 | NIST | |
| Inp | 802.00 | NIST | |
| Inp | 790.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 788.00 | NIST | |
| Inp | 781.00 | NIST | |
| Inp | 780.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 804.00 | NIST | |
| Inp | 820.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 823.00 | NIST | |
| Inp | 788.00 | NIST | |
| Inp | 788.00 | NIST | |
| Inp | 800.00 | NIST | |
| Inp | 786.00 | NIST | |
| Inp | 779.00 | NIST | |
| Inp | 814.00 | NIST | |
| Inp | 784.00 | NIST | |
| Inp | 792.00 | NIST | |
| Inp | 784.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 789.00 | NIST | |
| Inp | 791.00 | NIST | |
| Inp | 797.00 | NIST | |
| Inp | 797.00 | NIST | |
| Inp | 793.00 | NIST | |
| Inp | 828.00 | NIST | |
| Inp | 822.00 | NIST | |
| Inp | 808.00 | NIST | |
| Inp | 826.00 | NIST | |
| Inp | 835.00 | NIST | |
| Inp | 823.00 | NIST | |
| Inp | 773.00 | NIST | |
| Inp | 821.00 | NIST | |
| Inp | 820.00 | NIST | |
| Inp | 800.00 | NIST | |
| Inp | 792.00 | NIST | |
| Inp | 797.00 | NIST | |
| I | [1576.00; 1670.00] |
|
|
| I | Outlier 1576.00 | NIST | |
| I | Outlier 1576.00 | NIST | |
| I | Outlier 1581.00 | NIST | |
| I | 1628.00 | NIST | |
| I | 1637.00 | NIST | |
| I | 1644.00 | NIST | |
| I | 1624.00 | NIST | |
| I | 1653.00 | NIST | |
| I | 1625.00 | NIST | |
| I | Outlier 1576.00 | NIST | |
| I | 1637.00 | NIST | |
| I | 1637.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1644.00 | NIST | |
| I | 1614.00 | NIST | |
| I | 1607.00 | NIST | |
| I | 1647.00 | NIST | |
| I | 1613.00 | NIST | |
| I | Outlier 1663.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1661.00 | NIST | |
| I | 1650.00 | NIST | |
| I | Outlier 1576.00 | NIST | |
| I | 1628.00 | NIST | |
| I | 1652.00 | NIST | |
| I | 1647.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1599.00 | NIST | |
| I | 1610.00 | NIST | |
| I | 1652.00 | NIST | |
| I | 1647.00 | NIST | |
| I | 1624.00 | NIST | |
| I | 1624.00 | NIST | |
| I | 1633.00 | NIST | |
| I | 1617.00 | NIST | |
| I | 1616.00 | NIST | |
| I | 1637.00 | NIST | |
| I | 1645.00 | NIST | |
| I | 1607.00 | NIST | |
| I | 1613.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1604.00 | NIST | |
| I | 1616.00 | NIST | |
| I | 1627.00 | NIST | |
| I | 1628.00 | NIST | |
| I | 1624.00 | NIST | |
| I | 1604.00 | NIST | |
| I | 1613.00 | NIST | |
| I | 1606.00 | NIST | |
| I | 1599.00 | NIST | |
| I | 1637.00 | NIST | |
| I | 1623.00 | NIST | |
| I | 1624.00 | NIST | |
| I | Outlier 1666.00 | NIST | |
| I | 1646.00 | NIST | |
| I | 1624.00 | NIST | |
| I | 1623.00 | NIST | |
| I | 1624.00 | NIST | |
| I | 1624.00 | NIST | |
| I | 1623.00 | NIST | |
| I | 1631.00 | NIST | |
| I | 1631.00 | NIST | |
| I | 1635.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1630.00 | NIST | |
| I | 1630.00 | NIST | |
| I | 1598.00 | NIST | |
| I | 1598.00 | NIST | |
| I | 1606.00 | NIST | |
| I | 1600.00 | NIST | |
| I | 1596.00 | NIST | |
| I | 1599.00 | NIST | |
| I | 1598.00 | NIST | |
| I | 1600.00 | NIST | |
| I | 1598.00 | NIST | |
| I | 1602.00 | NIST | |
| I | 1591.00 | NIST | |
| I | 1627.00 | NIST | |
| I | 1630.00 | NIST | |
| I | 1641.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1627.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1622.00 | NIST | |
| I | 1622.00 | NIST | |
| I | 1629.00 | NIST | |
| I | 1657.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1648.00 | NIST | |
| I | Outlier 1663.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1650.00 | NIST | |
| I | 1622.00 | NIST | |
| I | 1635.00 | NIST | |
| I | Outlier 1670.00 | NIST | |
| I | 1618.00 | NIST | |
| I | 1650.00 | NIST | |
| I | 1617.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1618.00 | NIST | |
| I | 1618.00 | NIST | |
| I | 1610.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1629.00 | NIST | |
| I | 1599.00 | NIST | |
| I | 1611.00 | NIST | |
| I | 1618.00 | NIST | |
| I | 1622.00 | NIST | |
| I | 1627.00 | NIST | |
| I | 1597.00 | NIST | |
| I | 1594.00 | NIST | |
| I | 1599.00 | NIST | |
| I | 1600.00 | NIST | |
| I | 1612.00 | NIST | |
| I | 1633.00 | NIST | |
| I | 1622.00 | NIST | |
| I | 1614.00 | NIST | |
| I | 1621.00 | NIST | |
| I | 1612.00 | NIST | |
| I | 1640.00 | NIST | |
| I | 1648.00 | NIST | |
| I | 1612.00 | NIST | |
| I | 1606.00 | NIST | |
| I | 1626.00 | NIST | |
| I | 1621.00 | NIST | |
| I | 1623.00 | NIST | |
| I | 1626.00 | NIST | |
| I | 1619.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1646.00 | NIST | |
| I | 1645.00 | NIST | |
| I | 1629.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1659.00 | NIST | |
| I | 1636.00 | NIST | |
| I | 1634.00 | NIST | |
| I | 1609.00 | NIST | |
| I | 1602.00 | NIST | |
| I | 1602.00 | NIST | |
| I | 1602.00 | NIST | |
| I | 1636.00 | NIST | |
| I | 1614.00 | NIST | |
| I | 1613.00 | NIST | |
| I | 1639.00 | NIST | |
| I | 1650.00 | NIST | |
| I | 1641.00 | NIST | |
| I | 1631.00 | NIST | |
| I | 1616.00 | NIST | |
| I | 1652.00 | NIST | |
| I | 1642.00 | NIST | |
| I | 1631.00 | NIST | |
| I | 1642.00 | NIST | |
| I | 1644.00 | NIST | |
| I | 1647.00 | NIST | |
| I | 1647.00 | NIST | |
| I | 1642.00 | NIST | |
| I | 1647.00 | NIST | |
| I | 1642.00 | NIST | |
| I | 1650.00 | NIST | |
| I | 1622.00 | NIST | |
| I | Outlier 1581.00 | NIST | |
| I | 1646.00 | NIST | |
| I | 1640.00 | NIST | |
| I | 1614.00 | NIST | |
| I | 1646.00 | NIST | |
| I | 1622.00 | NIST | |
| I | 1626.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1648.00 | NIST | |
| I | 1612.00 | NIST | |
| I | 1612.00 | NIST | |
| I | 1646.00 | NIST | |
| I | 1614.00 | NIST | |
| I | 1588.00 | NIST | |
| I | 1588.00 | NIST | |
| I | 1621.00 | NIST | |
| I | 1644.00 | NIST | |
| I | 1630.00 | NIST | |
| I | 1630.00 | NIST | |
| I | 1644.00 | NIST | |
| I | 1628.00 | NIST | |
| I | 1613.00 | NIST | |
| I | 1616.00 | NIST | |
| I | 1615.00 | NIST | |
| I | 1615.00 | NIST | |
| I | 1631.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1623.00 | NIST | |
| I | 1623.00 | NIST | |
| I | 1628.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1661.00 | NIST | |
| I | 1630.00 | NIST | |
| I | 1630.00 | NIST | |
| I | 1598.00 | NIST | |
| I | 1607.00 | NIST | |
| I | 1645.00 | NIST | |
| I | 1628.00 | NIST | |
| I | Outlier 1669.00 | NIST | |
| I | 1628.00 | NIST | |
| I | 1639.00 | NIST | |
| I | 1638.00 | NIST | |
| I | 1616.00 | NIST | |
| I | 1642.00 | NIST | |
| I | 1630.00 | NIST | |
| I | Outlier 1585.00 | NIST | |
| I | 1637.00 | NIST | |
| I | 1636.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1630.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1633.00 | NIST | |
| I | 1630.00 | NIST | |
| I | 1642.00 | NIST | |
| I | 1651.00 | NIST | |
| I | 1636.00 | NIST | |
| I | 1636.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1635.00 | NIST | |
| I | 1652.00 | NIST | |
| I | 1589.00 | NIST | |
| I | 1641.00 | NIST | |
| I | 1627.00 | NIST | |
| I | 1641.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1623.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1605.00 | NIST | |
| I | 1622.00 | NIST | |
| I | 1618.00 | NIST | |
| I | 1618.00 | NIST | |
| I | 1634.00 | NIST | |
| I | 1630.00 | NIST | |
| I | 1619.00 | NIST | |
| I | 1588.00 | NIST | |
| I | 1634.00 | NIST | |
| I | 1611.00 | NIST | |
| I | 1619.00 | NIST | |
| I | 1619.00 | NIST | |
| I | 1627.00 | NIST | |
| I | 1602.00 | NIST | |
| I | 1623.00 | NIST | |
| I | 1659.00 | NIST | |
| I | 1634.00 | NIST | |
| I | 1633.00 | NIST | |
| I | 1599.00 | NIST | |
| I | 1600.00 | NIST | |
| I | 1621.00 | NIST | |
| I | 1610.00 | NIST | |
| I | 1619.00 | NIST | |
| I | 1633.00 | NIST | |
| I | 1646.00 | NIST | |
| I | 1627.00 | NIST | |
| I | 1653.00 | NIST | |
| I | 1627.00 | NIST | |
| I | 1596.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1660.00 | NIST | |
| I | 1639.00 | NIST | |
| I | 1627.00 | NIST | |
| I | 1629.00 | NIST | |
| I | 1628.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1609.00 | NIST | |
| I | 1627.00 | NIST | |
| I | 1613.00 | NIST | |
| I | 1652.00 | NIST | |
| I | 1610.00 | NIST | |
| I | 1610.00 | NIST | |
| I | 1613.00 | NIST | |
| I | 1623.00 | NIST | |
| I | 1613.00 | NIST | |
| I | 1600.00 | NIST | |
| I | 1614.00 | NIST | |
| I | Outlier 1581.00 | NIST | |
| I | Outlier 1576.00 | NIST | |
| I | 1628.00 | NIST | |
| I | 1630.00 | NIST | |
| I | 1651.00 | NIST | |
| I | 1652.00 | NIST | |
| I | 1620.00 | NIST | |
| I | 1618.00 | NIST | |
| I | 1588.00 | NIST | |
| I | 1627.00 | NIST | |
| I | 1633.00 | NIST | |
| I | 1619.00 | NIST | |
| I | 1613.00 | NIST | |
| I | Outlier 1581.00 | NIST | |
| I | 1648.00 | NIST | |
| I | 1623.00 | NIST | |
| I | 1645.00 | NIST | |
| I | 1634.00 | NIST | |
| I | 1636.00 | NIST | |
| I | 1641.00 | NIST | |
| I | 1631.00 | NIST | |
| I | 1642.00 | NIST | |
| I | 1622.00 | NIST | |
| I | 1612.00 | NIST | |
| I | 1621.00 | NIST | |
| I | 1625.00 | NIST | |
| I | 1607.00 | NIST | |
| I | 1639.00 | NIST | |
| I | Outlier 1585.00 | NIST | |
| S°gas | 353.26 | J/mol×K | NIST |
| S°liquid | [225.30; 255.20] | J/mol×K |
|
| S°liquid | 225.30 | J/mol×K | NIST |
| S°liquid | 226.40 | J/mol×K | NIST |
| S°liquid | 255.20 | J/mol×K | NIST |
| Tboil | [391.00; 455.15] | K |
|
| Tboil | 436.95 | K | Determination and correlation of liquid liquid equilibria for the (water + carboxylic acid + dimethyl maleate) ternary systems at T = 298.2K |
| Tboil | 436.70 | K | Liquid-liquid equilibria of (water + butyric acid + diethyl succinate or diethyl glutarate or diethyl adipate) ternary systems |
| Tboil | 436.70 | K | Ternary liquid-liquid phase equilibria of (water-carboxylic acid-1-undecanol) systems at 298.15 K |
| Tboil | 436.80 | K | Ternary phase diagrams for aqueous mixtures of butyric acid with several solvents: experimental and correlated data |
| Tboil | 436.67 | K | (Liquid + liquid) equilibria of (water + butyric acid + isoamyl alcohol) ternary system |
| Tboil | 436.67 | K | Phase equilibria of liquid (water + butyric acid + oleyl alcohol) ternary system |
| Tboil | 436.70 | K | (Liquid + liquid) equilibria of (water + butyric acid + esters) ternary systems |
| Tboil | 436.87 | K | ChemSep v8.3 pure component data |
| Tboil | 436.90 | K | KDB |
| Tboil | 435.20 | K | NIST |
| Tboil | 436.00 | K | NIST |
| Tboil | 436.70 ± 0.20 | K | NIST |
| Tboil | 437.00 ± 2.00 | K | NIST |
| Tboil | 436.45 | K | NIST |
| Tboil | 436.55 ± 0.60 | K | NIST |
| Tboil | 436.00 ± 4.00 | K | NIST |
| Tboil | 436.15 ± 0.20 | K | NIST |
| Tboil | 433.65 ± 2.00 | K | NIST |
| Tboil | 437.25 ± 0.60 | K | NIST |
| Tboil | 437.15 ± 0.50 | K | NIST |
| Tboil | 436.55 ± 0.50 | K | NIST |
| Tboil | 436.85 ± 1.00 | K | NIST |
| Tboil | 436.65 ± 1.00 | K | NIST |
| Tboil | 435.50 ± 1.00 | K | NIST |
| Tboil | 436.55 ± 0.50 | K | NIST |
| Tboil | 436.40 ± 0.30 | K | NIST |
| Tboil | 437.15 ± 0.60 | K | NIST |
| Tboil | 437.15 ± 1.00 | K | NIST |
| Tboil | 434.75 ± 1.00 | K | NIST |
| Tboil | 437.20 ± 0.60 | K | NIST |
| Tboil | 435.65 ± 2.00 | K | NIST |
| Tboil | 437.15 ± 0.30 | K | NIST |
| Tboil | 437.15 ± 0.30 | K | NIST |
| Tboil | 435.15 ± 2.00 | K | NIST |
| Tboil | 435.15 ± 1.00 | K | NIST |
| Tboil | 435.55 ± 0.40 | K | NIST |
| Tboil | 437.00 ± 0.60 | K | NIST |
| Tboil | 437.20 ± 0.50 | K | NIST |
| Tboil | 434.55 ± 1.00 | K | NIST |
| Tboil | 437.15 ± 2.00 | K | NIST |
| Tboil | 433.65 ± 3.00 | K | NIST |
| Tboil | 435.60 ± 0.60 | K | NIST |
| Tboil | 436.70 ± 0.50 | K | NIST |
| Tboil | Outlier 391.00 ± 0.50 | K | NIST |
| Tboil | 435.65 ± 1.00 | K | NIST |
| Tboil | 434.15 ± 2.00 | K | NIST |
| Tboil | 433.25 ± 1.00 | K | NIST |
| Tboil | 434.90 ± 1.00 | K | NIST |
| Tboil | 433.20 ± 2.00 | K | NIST |
| Tboil | 436.35 ± 0.60 | K | NIST |
| Tboil | 433.65 ± 2.00 | K | NIST |
| Tboil | 436.15 ± 0.50 | K | NIST |
| Tboil | 436.25 ± 1.00 | K | NIST |
| Tboil | 436.65 ± 0.50 | K | NIST |
| Tboil | Outlier 455.15 ± 2.00 | K | NIST |
| Tboil | 435.00 ± 3.00 | K | NIST |
| Tboil | 434.65 ± 1.00 | K | NIST |
| Tboil | 435.15 ± 2.00 | K | NIST |
| Tboil | 435.50 ± 0.60 | K | NIST |
| Tboil | 435.65 ± 0.60 | K | NIST |
| Tboil | 436.00 ± 2.00 | K | NIST |
| Tboil | 435.45 ± 1.00 | K | NIST |
| Tboil | 435.50 ± 1.00 | K | NIST |
| Tboil | 435.90 ± 1.00 | K | NIST |
| Tboil | 434.15 ± 2.00 | K | NIST |
| Tboil | 430.15 ± 5.00 | K | NIST |
| Tboil | 430.15 ± 5.00 | K | NIST |
| Tc | [615.20; 631.77] | K |
|
| Tc | 624.00 | K | ChemSep v8.3 pure component data |
| Tc | 624.00 | K | KDB |
| Tc | 615.20 ± 2.00 | K | NIST |
| Tc | 624.00 ± 1.00 | K | NIST |
| Tc | 631.77 ± 2.50 | K | NIST |
| Tc | 627.90 ± 6.00 | K | NIST |
| Tfus | [266.68; 268.65] | K |
|
| Tfus | 268.65 | K | Differential scanning calorimetry determination of phase diagrams and water activities of aqueous carboxylic acid solutions |
| Tfus | 267.95 | K | ChemSep v8.3 pure component data |
| Tfus | 267.40 | K | KDB |
| Tfus | 266.68 | K | Aq. Solubility Prediction |
| Tfus | 267.60 ± 0.20 | K | NIST |
| Tfus | 267.95 | K | NIST |
| Tfus | 267.80 ± 0.50 | K | NIST |
| Tfus | 267.89 ± 0.05 | K | NIST |
| Tfus | 267.00 ± 1.50 | K | NIST |
| Ttriple | [267.40; 268.03] | K |
|
| Ttriple | 267.95 | K | ChemSep v8.3 pure component data |
| Ttriple | 268.03 | K | KDB |
| Ttriple | 267.97 ± 0.05 | K | NIST |
| Ttriple | 268.03 ± 0.05 | K | NIST |
| Ttriple | 267.40 ± 0.20 | K | NIST |
| Ttriple | 268.03 ± 0.05 | K | NIST |
| Ttriple | 267.40 ± 0.20 | K | NIST |
| UQi | 3.15 | ChemSep v8.3 pure component data | |
| URi | 3.55 | ChemSep v8.3 pure component data | |
| Vc | [0.290; 0.292] | m3/kmol |
|
| Vc | 0.292 | m3/kmol | ChemSep v8.3 pure component data |
| Vc | 0.290 | m3/kmol | KDB |
| Zc | [0.2252590; 0.2270000] |
|
|
| Zc | 0.2270000 | ChemSep v8.3 pure component data | |
| Zc | 0.2252590 | KDB |
Temperature Dependent Properties
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [107.29; 258.72] | J/mol×K | [267.95; 1500.00] |
ChemSep v8.3 pure component data
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is Cp,gas in J/mol×K, T in K | |||
| Coefficient A | 7.55650e+01 | |||
| Coefficient B | -6.13250e+02 | |||
| Coefficient C | 5.76324e+00 | |||
| Coefficient D | -5.87730e-05 | |||
| Coefficient E | -2.48450e-08 | |||
| Comment | ChemSep eq 16, IdealGasHeatCapacityCp | |||
| Temperature range, min. | 267.95 | |||
| Temperature range, max. | 1500.00 | |||
| Cp,gas | 107.29 | J/mol×K | 267.95 | Calculated Property |
| Cp,gas | 143.64 | J/mol×K | 404.84 | Calculated Property |
| Cp,gas | 174.27 | J/mol×K | 541.74 | Calculated Property |
| Cp,gas | 198.08 | J/mol×K | 678.63 | Calculated Property |
| Cp,gas | 216.29 | J/mol×K | 815.53 | Calculated Property |
| Cp,gas | 230.17 | J/mol×K | 952.42 | Calculated Property |
| Cp,gas | 240.70 | J/mol×K | 1089.32 | Calculated Property |
| Cp,gas | 248.64 | J/mol×K | 1226.21 | Calculated Property |
| Cp,gas | 254.51 | J/mol×K | 1363.11 | Calculated Property |
| Cp,gas | 258.72 | J/mol×K | 1500.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | [168.87; 260.32] | J/mol×K | [267.89; 436.42] |
ChemSep v8.3 pure component data
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is Cp,liquid in J/mol×K, T in K | |||
| Coefficient A | 1.35560e+02 | |||
| Coefficient B | 6.64700e+02 | |||
| Coefficient C | -4.94856e+00 | |||
| Coefficient D | 2.76850e-02 | |||
| Coefficient E | -2.01110e-05 | |||
| Comment | ChemSep eq 16, LiquidHeatCapacityCp | |||
| Temperature range, min. | 267.89 | |||
| Temperature range, max. | 436.42 | |||
| Cp,liquid | 168.87 | J/mol×K | 267.89 | Calculated Property |
| Cp,liquid | 174.17 | J/mol×K | 286.62 | Calculated Property |
| Cp,liquid | 180.56 | J/mol×K | 305.34 | Calculated Property |
| Cp,liquid | 188.14 | J/mol×K | 324.07 | Calculated Property |
| Cp,liquid | 196.97 | J/mol×K | 342.79 | Calculated Property |
| Cp,liquid | 207.10 | J/mol×K | 361.52 | Calculated Property |
| Cp,liquid | 218.56 | J/mol×K | 380.24 | Calculated Property |
| Cp,liquid | 231.31 | J/mol×K | 398.97 | Calculated Property |
| Cp,liquid | 245.28 | J/mol×K | 417.69 | Calculated Property |
| Cp,liquid | 260.32 | J/mol×K | 436.42 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [0.0025499; 0.0001889] | Pa×s | [267.95; 524.00] |
ChemSep v8.3 pure component data
|
| Equation | Y = exp(A + B/T + C·ln(T) + D·T^E) Y is η in Pa×s, T in K | |||
| Coefficient A | 1.42410e+01 | |||
| Coefficient B | 5.34990e+02 | |||
| Coefficient C | -4.04110e+00 | |||
| Coefficient D | 5.34370e-06 | |||
| Coefficient E | 2.00000e+00 | |||
| Comment | ChemSep eq 101, LiquidViscosity | |||
| Temperature range, min. | 267.95 | |||
| Temperature range, max. | 524.00 | |||
| η | 0.0025499 | Pa×s | 267.95 | Calculated Property |
| η | 0.0015256 | Pa×s | 296.40 | Calculated Property |
| η | 0.0009885 | Pa×s | 324.85 | Calculated Property |
| η | 0.0006836 | Pa×s | 353.30 | Calculated Property |
| η | 0.0004993 | Pa×s | 381.75 | Calculated Property |
| η | 0.0003822 | Pa×s | 410.20 | Calculated Property |
| η | 0.0003048 | Pa×s | 438.65 | Calculated Property |
| η | 0.0002519 | Pa×s | 467.10 | Calculated Property |
| η | 0.0002150 | Pa×s | 495.55 | Calculated Property |
| η | 0.0001889 | Pa×s | 524.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | [41.28; 10.36] | kJ/mol | [250.00; 615.70] |
ChemSep v8.3 pure component data
|
| 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 | 5.13870e+01 | |||
| Coefficient B | 1.15170e+00 | |||
| Coefficient C | -2.76560e+00 | |||
| Coefficient D | 2.66170e+00 | |||
| Coefficient E | -6.69830e-01 | |||
| Critical temperature, Tc (K) | 6.24000e+02 | |||
| Comment | ChemSep eq 106, HeatOfVaporization | |||
| Temperature range, min. | 250.00 | |||
| Temperature range, max. | 615.70 | |||
| ΔvapH | 41.28 | kJ/mol | 250.00 | Calculated Property |
| ΔvapH | 40.66 | kJ/mol | 290.63 | Calculated Property |
| ΔvapH | 39.93 | kJ/mol | 331.27 | Calculated Property |
| ΔvapH | 38.90 | kJ/mol | 371.90 | Calculated Property |
| ΔvapH | 37.42 | kJ/mol | 412.53 | Calculated Property |
| ΔvapH | 35.27 | kJ/mol | 453.17 | Calculated Property |
| ΔvapH | 32.21 | kJ/mol | 493.80 | Calculated Property |
| ΔvapH | 27.90 | kJ/mol | 534.43 | Calculated Property |
| ΔvapH | 21.66 | kJ/mol | 575.07 | Calculated Property |
| ΔvapH | 10.36 | kJ/mol | 615.70 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.62] | kPa | [332.48; 460.54] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.57477e+01 | |||
| Coefficient B | -4.11288e+03 | |||
| Coefficient C | -6.64480e+01 | |||
| Temperature range, min. | 332.48 | |||
| Temperature range, max. | 460.54 | |||
| Pvap | 1.33 | kPa | 332.48 | Calculated Property |
| Pvap | 2.92 | kPa | 346.71 | Calculated Property |
| Pvap | 5.94 | kPa | 360.94 | Calculated Property |
| Pvap | 11.31 | kPa | 375.17 | Calculated Property |
| Pvap | 20.33 | kPa | 389.40 | Calculated Property |
| Pvap | 34.80 | kPa | 403.62 | Calculated Property |
| Pvap | 57.03 | kPa | 417.85 | Calculated Property |
| Pvap | 89.93 | kPa | 432.08 | Calculated Property |
| Pvap | 137.06 | kPa | 446.31 | Calculated Property |
| Pvap | 202.62 | kPa | 460.54 | Calculated Property |
| Pvap | [0.01; 4869.00] | kPa | [267.95; 625.15] |
ChemSep v8.3 pure component data
|
| Equation | Y = exp(A + B/T + C·ln(T) + D·T^E) Y is Pvap in kPa, T in K | |||
| Coefficient A | 4.74027e+01 | |||
| Coefficient B | -7.69265e+03 | |||
| Coefficient C | -4.14871e+00 | |||
| Coefficient D | 2.62432e-07 | |||
| Coefficient E | 2.00000e+00 | |||
| Comment | ChemSep eq 101, VaporPressure | |||
| Temperature range, min. | 267.95 | |||
| Temperature range, max. | 625.15 | |||
| Pvap | 0.01 | kPa | 267.95 | Calculated Property |
| Pvap | 0.26 | kPa | 307.64 | Calculated Property |
| Pvap | 2.76 | kPa | 347.33 | Calculated Property |
| Pvap | 17.21 | kPa | 387.02 | Calculated Property |
| Pvap | 73.52 | kPa | 426.71 | Calculated Property |
| Pvap | 237.93 | kPa | 466.39 | Calculated Property |
| Pvap | 624.41 | kPa | 506.08 | Calculated Property |
| Pvap | 1393.97 | kPa | 545.77 | Calculated Property |
| Pvap | 2740.71 | kPa | 585.46 | Calculated Property |
| Pvap | 4869.00 | kPa | 625.15 | Calculated Property |
| Pvap | [9.65e-03; 4278.67] | kPa | [267.95; 628.00] |
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 | 9.87911e+01 | |||
| Coefficient B | -9.90286e+03 | |||
| Coefficient C | -1.19698e+01 | |||
| Coefficient D | 6.22559e-06 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 267.95 | |||
| Temperature range, max. | 628.00 | |||
| Pvap | 9.65e-03 | kPa | 267.95 | Calculated Property |
| Pvap | 0.26 | kPa | 307.96 | Calculated Property |
| Pvap | 2.82 | kPa | 347.96 | Calculated Property |
| Pvap | 17.32 | kPa | 387.97 | Calculated Property |
| Pvap | 71.27 | kPa | 427.97 | Calculated Property |
| Pvap | 220.97 | kPa | 467.98 | Calculated Property |
| Pvap | 558.77 | kPa | 507.98 | Calculated Property |
| Pvap | 1217.47 | kPa | 547.99 | Calculated Property |
| Pvap | 2376.91 | kPa | 587.99 | Calculated Property |
| Pvap | 4278.67 | kPa | 628.00 | Calculated Property |
| Pvap | [0.10; 67.60] | kPa | [293.00; 423.00] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.86729e+01 | |||
| Coefficient B | -6.06609e+03 | |||
| Coefficient C | -3.47100e+00 | |||
| Reference | Jasper and Miller, 1955 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 293.00 | |||
| Temperature range, max. | 423.00 | |||
| Pvap | 0.10 | kPa | 293.00 | Calculated Property |
| Pvap | 0.28 | kPa | 307.44 | Calculated Property |
| Pvap | 0.69 | kPa | 321.89 | Calculated Property |
| Pvap | 1.57 | kPa | 336.33 | Calculated Property |
| Pvap | 3.34 | kPa | 350.78 | Calculated Property |
| Pvap | 6.71 | kPa | 365.22 | Calculated Property |
| Pvap | 12.78 | kPa | 379.67 | Calculated Property |
| Pvap | 23.20 | kPa | 394.11 | Calculated Property |
| Pvap | 40.37 | kPa | 408.56 | Calculated Property |
| Pvap | 67.60 | kPa | 423.00 | Calculated Property |
| Pvap | [6.27; 101.27] | kPa | [364.07; 436.40] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.59087e+01 | |||
| Coefficient B | -4.13060e+03 | |||
| Coefficient C | -7.05640e+01 | |||
| Reference | Dreisbach and Shrader, 1949 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 364.07 | |||
| Temperature range, max. | 436.40 | |||
| Pvap | 6.27 | kPa | 364.07 | Calculated Property |
| Pvap | 9.12 | kPa | 372.11 | Calculated Property |
| Pvap | 13.01 | kPa | 380.14 | Calculated Property |
| Pvap | 18.24 | kPa | 388.18 | Calculated Property |
| Pvap | 25.14 | kPa | 396.22 | Calculated Property |
| Pvap | 34.13 | kPa | 404.25 | Calculated Property |
| Pvap | 45.66 | kPa | 412.29 | Calculated Property |
| Pvap | 60.28 | kPa | 420.33 | Calculated Property |
| Pvap | 78.59 | kPa | 428.36 | Calculated Property |
| Pvap | 101.27 | kPa | 436.40 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ρl | [978.94; 298.72] | kg/m3 | [267.95; 628.15] |
ChemSep v8.3 pure component data
|
| Equation | Y = A / B^(1 + (1 − T/C)^D) Y is ρl in kg/m3, T in K | |||
| Coefficient A | 6.18498e+01 | |||
| Coefficient B | 2.29020e-01 | |||
| Coefficient C | 6.28160e+02 | |||
| Coefficient D | 2.42750e-01 | |||
| Comment | ChemSep eq 105, LiquidDensity | |||
| Temperature range, min. | 267.95 | |||
| Temperature range, max. | 628.15 | |||
| ρl | 978.94 | kg/m3 | 267.95 | Calculated Property |
| ρl | 944.04 | kg/m3 | 307.97 | Calculated Property |
| ρl | 907.10 | kg/m3 | 347.99 | Calculated Property |
| ρl | 867.62 | kg/m3 | 388.02 | Calculated Property |
| ρl | 824.88 | kg/m3 | 428.04 | Calculated Property |
| ρl | 777.72 | kg/m3 | 468.06 | Calculated Property |
| ρl | 724.17 | kg/m3 | 508.08 | Calculated Property |
| ρl | 660.22 | kg/m3 | 548.11 | Calculated Property |
| ρl | 574.88 | kg/m3 | 588.13 | Calculated Property |
| ρl | 298.72 | kg/m3 | 628.15 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| γ | [0.03; 3.59e-04] | N/m | [267.95; 615.70] |
ChemSep v8.3 pure component data
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is γ in N/m, T in K | |||
| Coefficient A | -7.61270e-03 | |||
| Coefficient B | 3.73930e+02 | |||
| Coefficient C | -6.09150e+00 | |||
| Coefficient D | 8.43490e-03 | |||
| Coefficient E | -1.19790e-05 | |||
| Comment | ChemSep eq 16, SurfaceTension | |||
| Temperature range, min. | 267.95 | |||
| Temperature range, max. | 615.70 | |||
| γ | 0.03 | N/m | 267.95 | Calculated Property |
| γ | 0.03 | N/m | 306.59 | Calculated Property |
| γ | 0.02 | N/m | 345.23 | Calculated Property |
| γ | 0.02 | N/m | 383.87 | Calculated Property |
| γ | 0.02 | N/m | 422.51 | Calculated Property |
| γ | 0.01 | N/m | 461.14 | Calculated Property |
| γ | 0.01 | N/m | 499.78 | Calculated Property |
| γ | 0.01 | N/m | 538.42 | Calculated Property |
| γ | 0.00 | N/m | 577.06 | Calculated Property |
| γ | 3.59e-04 | N/m | 615.70 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λ | [0.01; 0.05] | W/m×K | [267.95; 706.95] |
ChemSep v8.3 pure component data
|
| Equation | Y = A + B·T + C·T² + D·T³ + E·T⁴ Y is λ in W/m×K, T in K | |||
| Coefficient A | -4.09203e-03 | |||
| Coefficient B | 3.12540e-05 | |||
| Coefficient C | 6.38999e-08 | |||
| Coefficient D | 0.00000e+00 | |||
| Coefficient E | 0.00000e+00 | |||
| Comment | ChemSep eq 3, VaporThermalConductivity | |||
| Temperature range, min. | 267.95 | |||
| Temperature range, max. | 706.95 | |||
| λ | 0.01 | W/m×K | 267.95 | Calculated Property |
| λ | 0.01 | W/m×K | 316.73 | Calculated Property |
| λ | 0.02 | W/m×K | 365.51 | Calculated Property |
| λ | 0.02 | W/m×K | 414.28 | Calculated Property |
| λ | 0.02 | W/m×K | 463.06 | Calculated Property |
| λ | 0.03 | W/m×K | 511.84 | Calculated Property |
| λ | 0.03 | W/m×K | 560.62 | Calculated Property |
| λ | 0.04 | W/m×K | 609.39 | Calculated Property |
| λ | 0.04 | W/m×K | 658.17 | Calculated Property |
| λ | 0.05 | W/m×K | 706.95 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λ | [0.15; 0.10] | W/m×K | [259.29; 573.15] |
ChemSep v8.3 pure component data
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is λ in W/m×K, T in K | |||
| Coefficient A | -4.39550e-02 | |||
| Coefficient B | 5.76980e+01 | |||
| Coefficient C | -1.88470e+00 | |||
| Coefficient D | 5.06490e-04 | |||
| Coefficient E | -1.34410e-06 | |||
| Comment | ChemSep eq 16, LiquidThermalConductivity | |||
| Temperature range, min. | 259.29 | |||
| Temperature range, max. | 573.15 | |||
| λ | 0.15 | W/m×K | 259.29 | Calculated Property |
| λ | 0.15 | W/m×K | 294.16 | Calculated Property |
| λ | 0.14 | W/m×K | 329.04 | Calculated Property |
| λ | 0.14 | W/m×K | 363.91 | Calculated Property |
| λ | 0.13 | W/m×K | 398.78 | Calculated Property |
| λ | 0.12 | W/m×K | 433.66 | Calculated Property |
| λ | 0.12 | W/m×K | 468.53 | Calculated Property |
| λ | 0.11 | W/m×K | 503.40 | Calculated Property |
| λ | 0.11 | W/m×K | 538.28 | Calculated Property |
| λ | 0.10 | W/m×K | 573.15 | Calculated Property |
Similar Compounds
Find more compounds similar to Butanoic acid.
Mixtures
- n-Hexane + Butanoic acid + Water
- Butanoic acid + 1-Hexanol + Water
- 1-Butanol, 3-methyl- + Butanoic acid + Water
- Butanoic acid + Acetic acid, cyclohexyl ester + Water
- Heptanoic acid + Butanoic acid
- Butanoic acid + Acetic acid
- Formic acid + Butanoic acid
- Butanoic acid + Pentanoic acid
- Butanoic acid + Propanoic acid
- Butanoic acid + Acetic acid, butyl ester + Water
- Butanoic acid + Water
- Butanoic acid + Butanedioic acid, diethyl ester + Water
- Butanoic acid + Pentanedioic acid, diethyl ester + Water
- Diethyl adipate + Butanoic acid + Water
- 1-Dodecanol + Butanoic acid + Water
- 2-Propanol + Butanoic acid
- Butanoic acid + 1-Propanol, 2-methyl-
- 2-Butenedioic acid (Z)-, dimethyl ester + Butanoic acid + Water
- Butanoic acid + Propane, 2-methoxy-2-methyl- + Water
- Propanoic acid, ethyl ester + Butanoic acid + Water
Find more mixtures with Butanoic acid.
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.
- Crippen Method
- Determination and correlation of liquid liquid equilibria for the (water + carboxylic acid + dimethyl maleate) ternary systems at T = 298.2K
- Liquid-liquid equilibria of (water + butyric acid + diethyl succinate or diethyl glutarate or diethyl adipate) ternary systems
- Phase equilibria of (water + carboxylic acid + diethyl maleate) ternary liquid systems at 298.15 K
- Experiment and correlation of osmotic coefficient for aqueous solution of carboxylic acids using NRTL nonrandom factor model
- Ternary liquid-liquid phase equilibria of (water-carboxylic acid-1-undecanol) systems at 298.15 K
- Experimental determination and correlation of tie line data for the system (water + butyric acid + methylcyclohexane) at four temperatures
- Solubility and tie line data for the aqueous solutions of butyric acid with 1-octanol and 2-ethyl-1-hexanol at various temperatures
- Ternary phase diagrams for aqueous mixtures of butyric acid with several solvents: experimental and correlated data
- Phase equilibria of (water + butyric acid + butyl acetate) ternary systems at different temperatures
- Vapour-liquid equilibrium of carboxylic acid alcohol binary systems:2-Propanol + butyric acid, 2-butanol + butyric acid and 2-methyl-1-propanol + butyric acid
- Modeling extraction equilibria of butyric acid distributed between water and tri-n-butyl amine/diluent or tri-n-butyl phosphate/diluent system: Extension of the LSER approach
- Liquid liquid equilibria measurements of ternary systems (acetonitrile + a carboxylic acid + dodecane) at 303.15 K
- Phase equilibria of (water + propionic acid or butyric acid + 2-methoxy- 2-methylpropane) ternary systems at 298.2 K and 323.2 K
- Phase equilibria measurements of ternary mixtures (sulfolane + a carboxylic acid + pentane) at 303.15 K
- Differential scanning calorimetry determination of Solid-Liquid equilibria phase diagrams for binary monocarboxylic acids solutions
- (Liquid + liquid) equilibria of (water + butyric acid + cyclohexyl acetate) ternary system
- (Liquid + liquid) equilibria of (water + butyric acid + isoamyl alcohol) ternary system
- (Liquid + liquid) equilibria of the (water + butyric acid + dodecanol) ternary system
- Phase equilibria of liquid (water + butyric acid + oleyl alcohol) ternary system
- (Liquid + liquid) equilibria of (water + butyric acid + dibasic esters) ternary systems
- (Liquid + liquid) equilibria of (water + butyric acid + esters) ternary systems
- Measurement and correlation of phase equilibrium data of the mixtures consisting of butyric acid, water, cyclohexanone at different temperatures
- Density, speed of sound, and refractive index measurements for the binary systems (butanoic acid + propanoic acid, or 2-methyl-propanoic acid) at T = (293.15 to 313.15) K
- (Liquid + liquid) equilibria of aqueous solutions of butyric acid with n-heptane and toluene at T = (298.2, 308.2, and 318.2) K
- Ternary liquid liquid equilibrium data for the (water + butyric acid + n-hexane or n-hexanol) systems at T = (298.2, 308.2, and 318.2) K
- Tie line data for the (water + butyric acid + n-butyl alcohol or amyl alcohol) at T = (298.2, 308.2, and 318.2) K and (water + butyric acid + isoamyl alcohol) at T = 298.2 K
- Effect of temperature on density, sound velocity, refractive index and their derived properties for the binary systems (heptanoic acid + propanoic or butanoic acids)
- (Liquid + liquid) equilibria measurements for ternary systems (sulfolane + a carboxylic acid + n-heptane) at T = 303.15 K and at 0.1 MPa
- Liquid-liquid equilibria for ternary mixtures of 1-alkyl-3-methyl imidazolium bis{(trifluoromethyl)sulfonyl}imides, n-hexane and organic compounds at 303.15 K and 0.1 MPa
- Liquid phase equilibrium of the ternary systems, water + propionic or butyric acid + mesityl oxide, at (298.2 and 323.2) K
- Liquid-liquid equilibria and density data for pseudoternary systems of refined soybean oil + (hexanal, or heptanal, or butyric acid, or valeric acid, or caproic acid, or caprylic acid) + dimethyl sulfoxide at 298.15 K
- Effect of temperature on the dilution enthalpies of carboxylic acids in aqueous solutions
- Phase diagrams for the aqueous solutions of butyric acid with cyclohexane at different temperatures: Experimental and correlated data
- Influence of alkyl group and temperature on thermophysical properties of carboxylic acid and their binary mixtures
- Differential scanning calorimetry determination of phase diagrams and water activities of aqueous carboxylic acid solutions
- Liquid Phase Equilibria of the Water + Propionic or Butyric Acid + Methyl tert-Butyl Ketone Ternary Systems at (298.15 and 323.15) K
- Tie-Line Data for Aqueous Mixtures of Butyric Acid with Diisopropyl Ether at Various Temperatures
- Investigation of Ternary Phase Diagrams of (Water + Butyric Acid + Phenyl Acetate) at Different Temperatures
- New Mechanism and Model of Butyric Acid Extraction by Phosphonium Ionic Liquid
- Liquid Phase Equilibria of Aqueous Mixtures of Carboxylic Acids (C1-C4) with Ethylbenzene: Thermodynamic and Mathematical Modeling
- Liquid Liquid Equilibrium Data of Water + Butyric Acid + {Butanal or n-Butanol} Ternary Systems at 293.15, 308.15, and 323.15 K
- Density, Viscosity, and Structure of Equilibrium Solvent Phases in Butyric Acid Extraction by Phosphonium Ionic Liquid
- Liquid-Liquid Equilibria for Ternary Mixtures of gamma-Valerolactone + n-Tetradecane + (Butanoic Acid or Hexanoic Acid or Methyl Myristate) at 298.15 K
- Extraction of Butyric Acid by Phosphonium Decanoate Ionic Liquid
- Subatmospheric Vapor Pressure Curves for Propionic Acid, Butyric Acid, Isobutyric Acid, Valeric Acid, Isovaleric Acid, Hexanoic Acid, and Heptanoic Acid
- Vapor-Liquid Equilibria on Four Binary Systems: 2-Phenylpropionaldehyde + Phenol, Propylene Glycol Monomethyl Ether + Nitroethane, Dimethyl Ether + Propylene, and N-Butyric Acid + Propionic Acid
- 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
- Distribution of Butyric Acid between Water and Several Solvents
- Refractive Index, Surface Tension, and Density of Aqueous Mixtures of Carboxylic Acids at 298.15 K
- Apparent Molar Volume and Surface Tension of Dilute Aqueous Solutions of Carboxylic Acids
- 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
- Solubility of Naphthalene in Isobutyl Acetate, n-Butyric Acid, Ethyl Acetate, N-Methyl Pyrrolidone, N,N-Dimethylformamide, and Tetrahydrofuran
- Isothermal Vapor-Liquid Equilibria and Excess Enthalpy Data for the Binary System (Butyric Acid + Toluene)
- Joback Method
- KDB
- Aqueous Solubility Prediction Method
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
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