- InChI
- InChI=1S/C6H6O/c7-6-4-2-1-3-5-6/h1-5,7H
- InChI Key
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N
- Formula
- C6H6O
- SMILES
- Oc1ccccc1
- Molecular Weight1
- 94.11
- CAS
- 108-95-2
- Other Names
-
- Acide carbolique
- Baker's P & S liquid & Ointment
- Baker's P and S Liquid and Ointment
- Benzene, hydroxy-
- Carbolic acid
- Carbolsaure
- Fenol
- Fenolo
- Izal
- Monohydroxybenzene
- Monophenol
- NA 2821
- NCI-C50124
- NSC 36808
- Oxybenzene
- Paoscle
- PhOH
- Phenic acid
- Phenic alcohol
- Phenol alcohol
- Phenol, molten
- Phenole
- Phenyl alcohol
- Phenyl hydrate
- Phenylic acid
- Phenylic alcohol
- Rcra waste number U188
- UN 1671
- UN 2312
- UN 2821
- benzenol
- hydroxybenzene
- phenyl hydroxide
- ω : Acentric Factor.
- PAff : Proton affinity (kJ/mol).
- Tig : Autoignition Temperature (K).
- BasG : Gas basicity (kJ/mol).
- ΔcH°solid : Standard solid enthalpy of combustion (kJ/mol).
- Cp,gas : Ideal gas heat capacity (J/mol×K).
- Cp,liquid : Liquid phase heat capacity (J/mol×K).
- Cp,solid : Solid 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).
- Rg : Radius of Gyration.
- ΔfH°gas : Enthalpy of formation at standard conditions (kJ/mol).
- ΔfH°solid : Solid 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 standard conditions (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.
- Ip : Polar retention indices.
- ΔfusS : Entropy of fusion at a given temperature (J/mol×K).
- γ : Surface Tension (N/m).
- S°solid,1 bar : Solid phase molar entropy at standard conditions (J/mol×K).
- Tboil : Normal Boiling Point Temperature (K).
- Tc : Critical Temperature (K).
- λgas : Gas thermal conductivity (W/m×K).
- λliquid : 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 | [0.4380; 0.4420] |
|
|
| ω | 0.4400 | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value | |
| ω | 0.4420 | ChemSep v8.3 pure component data Compiled value | |
| ω | 0.4380 | KDB | |
| PAff | 817.30 | kJ/mol | NIST |
| Tig | 988.15 | K | KDB |
| BasG | 786.30 | kJ/mol | NIST |
| ΔcH°solid | [-3067.00; -3053.50] | kJ/mol |
|
| ΔcH°solid | -3053.60 ± 0.30 | kJ/mol | NIST |
| ΔcH°solid | -3053.50 ± 0.67 | kJ/mol | NIST |
| ΔcH°solid | -3055.80 | kJ/mol | NIST |
| ΔcH°solid | -3054.70 | kJ/mol | NIST |
| ΔcH°solid | -3066.04 | kJ/mol | NIST |
| ΔcH°solid | -3067.00 | kJ/mol | NIST |
| μ | [1.45; 1.60] | debye |
|
| μ | 1.45 | debye | ChemSep v8.3 pure component data Compiled value |
| μ | 1.60 | debye | KDB |
| LFL | 1.70 | % in Air | KDB |
| UFL | 8.60 | % in Air | KDB |
| Tflash,cc | 358.15 | K | KDB |
| Tflash,oc | 352.59 | K | KDB |
| ΔfG° | [-32.90; -32.64] | kJ/mol |
|
| ΔfG° | -32.64 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfG° | -32.90 | kJ/mol | KDB |
| Rg | 3.5500 | KDB | |
| ΔfH°gas | [-96.44; -94.20] | kJ/mol |
|
| ΔfH°gas | -96.40 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | -96.42 | kJ/mol | KDB |
| ΔfH°gas | -96.36 ± 0.59 | kJ/mol | NIST |
| ΔfH°gas | -96.44 ± 0.63 | kJ/mol | NIST |
| ΔfH°gas | -94.20 | kJ/mol | NIST |
| ΔfH°gas | -95.30 | kJ/mol | NIST |
| ΔfH°solid | [-165.10; -162.80] | kJ/mol |
|
| ΔfH°solid | -165.00 | kJ/mol | NIST |
| ΔfH°solid | -165.10 ± 1.30 | kJ/mol | NIST |
| ΔfH°solid | -162.80 ± 1.00 | kJ/mol | NIST |
| ΔfH°solid | -163.90 | kJ/mol | NIST |
| ΔfusH° | 11.51 | kJ/mol | Joback Calculated Property |
| ΔsubH° | [68.60; 69.70] | kJ/mol |
|
| ΔsubH° | 69.70 ± 0.90 | kJ/mol | NIST |
| ΔsubH° | 68.60 | kJ/mol | NIST |
| ΔsubH° | 68.66 ± 0.50 | kJ/mol | NIST |
| ΔsubH° | 68.70 | kJ/mol | NIST |
| ΔvapH° | 58.80 | kJ/mol | NIST |
| IE | [8.00; 9.10] | eV |
|
| IE | 8.49 ± 0.02 | eV | NIST |
| IE | 8.51 ± 0.00 | eV | NIST |
| IE | 8.51 ± 0.00 | eV | NIST |
| IE | 8.49 | eV | NIST |
| IE | Outlier 8.00 | eV | NIST |
| IE | 8.21 | eV | NIST |
| IE | 8.55 | eV | NIST |
| IE | 8.47 ± 0.02 | eV | NIST |
| IE | Outlier 9.10 ± 0.10 | eV | NIST |
| IE | 8.37 | eV | NIST |
| IE | 8.50 | eV | NIST |
| IE | 8.69 | eV | NIST |
| IE | 8.48 ± 0.05 | eV | NIST |
| IE | 8.52 | eV | NIST |
| IE | 8.50 ± 0.01 | eV | NIST |
| IE | 8.52 ± 0.02 | eV | NIST |
| IE | 8.75 | eV | NIST |
| IE | 8.61 | eV | NIST |
| IE | 8.70 | eV | NIST |
| IE | 8.56 | eV | NIST |
| IE | 8.69 | eV | NIST |
| IE | 8.73 | eV | NIST |
| IE | 8.67 | eV | NIST |
| IE | 8.56 | eV | NIST |
| log10WS | [0.00; 0.00] |
|
|
| log10WS | 0.00 | Aq. Solubility Prediction | |
| log10WS | 0.00 | Estimated Solubility | |
| logPoct/wat | 1.392 | Crippen Calculated Property | |
| McVol | 77.510 | ml/mol | McGowan Calculated Property |
| NFPA Fire | 2 | KDB | |
| NFPA Health | 3 | KDB | |
| Pc | [5670.00; 6130.16] | kPa |
|
| Pc | Outlier 5670.00 | kPa | Vapor-Liquid Critical Properties of Phenol and (C8 to C10) Phenylalkanols |
| Pc | 5930.00 | kPa | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value |
| Pc | 6130.16 | kPa | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Pc | 6130.00 | kPa | ChemSep v8.3 pure component data Compiled value |
| Pc | 6130.00 | kPa | KDB |
| Pc | 5930.00 ± 78.45 | kPa | NIST |
| Pc | 6130.16 ± 81.06 | kPa | NIST |
| Ptriple | 0.19 | kPa | ChemSep v8.3 pure component data Compiled value |
| Inp | [150.40; 1004.10] |
|
|
| Inp | 950.00 | NIST | |
| Inp | 950.00 | NIST | |
| Inp | 950.00 | NIST | |
| Inp | 950.00 | NIST | |
| Inp | 974.00 | NIST | |
| Inp | 950.20 | NIST | |
| Inp | 950.70 | NIST | |
| Inp | 944.70 | NIST | |
| Inp | 945.20 | NIST | |
| Inp | 952.50 | NIST | |
| Inp | 943.00 | NIST | |
| Inp | 944.00 | NIST | |
| Inp | 952.00 | NIST | |
| Inp | 954.00 | NIST | |
| Inp | 929.00 | NIST | |
| Inp | 964.00 | NIST | |
| Inp | 952.00 | NIST | |
| Inp | 953.00 | NIST | |
| Inp | 964.00 | NIST | |
| Inp | 924.00 | NIST | |
| Inp | 943.00 | NIST | |
| Inp | 929.00 | NIST | |
| Inp | 932.00 | NIST | |
| Inp | 965.00 | NIST | |
| Inp | 926.00 | NIST | |
| Inp | 951.00 | NIST | |
| Inp | 954.00 | NIST | |
| Inp | 955.00 | NIST | |
| Inp | 966.00 | NIST | |
| Inp | 942.00 | NIST | |
| Inp | 933.00 | NIST | |
| Inp | 950.00 | NIST | |
| Inp | 960.00 | NIST | |
| Inp | 961.00 | NIST | |
| Inp | 964.00 | NIST | |
| Inp | 973.00 | NIST | |
| Inp | 923.00 | NIST | |
| Inp | 950.00 | NIST | |
| Inp | 970.00 | NIST | |
| Inp | 967.00 | NIST | |
| Inp | 981.40 | NIST | |
| Inp | 992.00 | NIST | |
| Inp | 981.00 | NIST | |
| Inp | 959.60 | NIST | |
| Inp | 978.80 | NIST | |
| Inp | 956.00 | NIST | |
| Inp | 961.00 | NIST | |
| Inp | 954.10 | NIST | |
| Inp | 978.16 | NIST | |
| Inp | 979.62 | NIST | |
| Inp | 977.00 | NIST | |
| Inp | 955.00 | NIST | |
| Inp | 977.00 | NIST | |
| Inp | 954.00 | NIST | |
| Inp | 959.00 | NIST | |
| Inp | 958.50 | NIST | |
| Inp | 954.90 | NIST | |
| Inp | 979.90 | NIST | |
| Inp | 959.00 | NIST | |
| Inp | 957.00 | NIST | |
| Inp | 975.00 | NIST | |
| Inp | 978.00 | NIST | |
| Inp | 959.00 | NIST | |
| Inp | 947.60 | NIST | |
| Inp | 965.40 | NIST | |
| Inp | 952.00 | NIST | |
| Inp | 969.00 | NIST | |
| Inp | 980.80 | NIST | |
| Inp | 980.80 | NIST | |
| Inp | 983.00 | NIST | |
| Inp | 962.00 | NIST | |
| Inp | 966.00 | NIST | |
| Inp | 962.00 | NIST | |
| Inp | 998.00 | NIST | |
| Inp | 962.00 | NIST | |
| Inp | 942.00 | NIST | |
| Inp | 933.00 | NIST | |
| Inp | 933.00 | NIST | |
| Inp | 945.00 | NIST | |
| Inp | 944.00 | NIST | |
| Inp | 946.00 | NIST | |
| Inp | 992.00 | NIST | |
| Inp | 1004.10 | NIST | |
| Inp | 995.50 | NIST | |
| Inp | 986.80 | NIST | |
| Inp | 992.00 | NIST | |
| Inp | 992.00 | NIST | |
| Inp | 955.00 | NIST | |
| Inp | 953.00 | NIST | |
| Inp | 980.00 | NIST | |
| Inp | 962.00 | NIST | |
| Inp | 956.00 | NIST | |
| Inp | 989.00 | NIST | |
| Inp | 983.00 | NIST | |
| Inp | 962.00 | NIST | |
| Inp | 962.00 | NIST | |
| Inp | 994.00 | NIST | |
| Inp | 984.00 | NIST | |
| Inp | 987.00 | NIST | |
| Inp | 989.00 | NIST | |
| Inp | 981.00 | NIST | |
| Inp | 994.00 | NIST | |
| Inp | 978.00 | NIST | |
| Inp | 972.00 | NIST | |
| Inp | 986.00 | NIST | |
| Inp | 979.00 | NIST | |
| Inp | 968.00 | NIST | |
| Inp | 978.00 | NIST | |
| Inp | 983.00 | NIST | |
| Inp | 980.00 | NIST | |
| Inp | 951.00 | NIST | |
| Inp | 954.00 | NIST | |
| Inp | 980.00 | NIST | |
| Inp | 957.00 | NIST | |
| Inp | 963.00 | NIST | |
| Inp | 980.00 | NIST | |
| Inp | 957.00 | NIST | |
| Inp | 961.00 | NIST | |
| Inp | 963.00 | NIST | |
| Inp | 964.00 | NIST | |
| Inp | 992.00 | NIST | |
| Inp | 974.00 | NIST | |
| Inp | 989.00 | NIST | |
| Inp | 961.00 | NIST | |
| Inp | 986.00 | NIST | |
| Inp | 978.00 | NIST | |
| Inp | 951.00 | NIST | |
| Inp | 977.00 | NIST | |
| Inp | 986.00 | NIST | |
| Inp | 973.00 | NIST | |
| Inp | 951.00 | NIST | |
| Inp | 981.00 | NIST | |
| Inp | 964.00 | NIST | |
| Inp | 957.00 | NIST | |
| Inp | 984.00 | NIST | |
| Inp | 988.00 | NIST | |
| Inp | 954.00 | NIST | |
| Inp | 948.00 | NIST | |
| Inp | 969.00 | NIST | |
| Inp | 953.00 | NIST | |
| Inp | 982.00 | NIST | |
| Inp | 982.00 | NIST | |
| Inp | 979.00 | NIST | |
| Inp | 995.00 | NIST | |
| Inp | 987.00 | NIST | |
| Inp | 980.00 | NIST | |
| Inp | 983.00 | NIST | |
| Inp | 969.00 | NIST | |
| Inp | 976.00 | NIST | |
| Inp | 976.00 | NIST | |
| Inp | 976.00 | NIST | |
| Inp | 976.00 | NIST | |
| Inp | 977.00 | NIST | |
| Inp | 986.00 | NIST | |
| Inp | 989.00 | NIST | |
| Inp | 974.00 | NIST | |
| Inp | 976.00 | NIST | |
| Inp | 984.00 | NIST | |
| Inp | 952.00 | NIST | |
| Inp | 980.00 | NIST | |
| Inp | 980.00 | NIST | |
| Inp | 1002.00 | NIST | |
| Inp | 977.00 | NIST | |
| Inp | 961.00 | NIST | |
| Inp | 973.00 | NIST | |
| Inp | 976.00 | NIST | |
| Inp | 995.00 | NIST | |
| Inp | 984.00 | NIST | |
| Inp | 987.00 | NIST | |
| Inp | 956.00 | NIST | |
| Inp | 962.00 | NIST | |
| Inp | 985.00 | NIST | |
| Inp | 982.00 | NIST | |
| Inp | 983.00 | NIST | |
| Inp | 962.00 | NIST | |
| Inp | 1002.00 | NIST | |
| Inp | 964.00 | NIST | |
| Inp | 961.00 | NIST | |
| Inp | 982.00 | NIST | |
| Inp | 961.00 | NIST | |
| Inp | 964.00 | NIST | |
| Inp | 973.00 | NIST | |
| Inp | 987.00 | NIST | |
| Inp | 959.00 | NIST | |
| Inp | 926.00 | NIST | |
| Inp | 981.00 | NIST | |
| Inp | Outlier 151.40 | NIST | |
| Inp | Outlier 151.60 | NIST | |
| Inp | Outlier 156.32 | NIST | |
| Inp | Outlier 154.70 | NIST | |
| Inp | Outlier 156.32 | NIST | |
| Inp | Outlier 152.20 | NIST | |
| Inp | Outlier 150.40 | NIST | |
| Inp | Outlier 156.32 | NIST | |
| Inp | Outlier 158.08 | NIST | |
| Inp | 981.40 | NIST | |
| Inp | 956.00 | NIST | |
| Inp | 977.00 | NIST | |
| Inp | 958.50 | NIST | |
| Inp | 975.00 | NIST | |
| Inp | 952.00 | NIST | |
| Inp | 962.00 | NIST | |
| Inp | 942.00 | NIST | |
| Inp | 946.00 | NIST | |
| Inp | 982.00 | NIST | |
| Inp | 980.00 | NIST | |
| Inp | 976.00 | NIST | |
| Inp | 974.00 | NIST | |
| Inp | 1002.00 | NIST | |
| Inp | 964.00 | NIST | |
| Inp | 981.00 | NIST | |
| Inp | Outlier 151.40 | NIST | |
| Inp | 989.00 | NIST | |
| Inp | 984.00 | NIST | |
| Inp | 978.00 | NIST | |
| Inp | 961.00 | NIST | |
| Inp | 948.00 | NIST | |
| Inp | 992.00 | NIST | |
| Inp | 967.00 | NIST | |
| Inp | 950.00 | NIST | |
| Inp | 950.20 | NIST | |
| Inp | 943.00 | NIST | |
| Inp | 951.00 | NIST | |
| Inp | 933.00 | NIST | |
| Inp | 973.00 | NIST | |
| Inp | Outlier 152.20 | NIST | |
| Ip | [1946.00; 2045.00] |
|
|
| Ip | 2000.00 | NIST | |
| Ip | 2000.00 | NIST | |
| Ip | 1971.00 | NIST | |
| Ip | 1957.00 | NIST | |
| Ip | Outlier 1947.00 | NIST | |
| Ip | Outlier 1947.00 | NIST | |
| Ip | 2030.00 | NIST | |
| Ip | 2037.00 | NIST | |
| Ip | 2008.00 | NIST | |
| Ip | 2008.00 | NIST | |
| Ip | 1992.00 | NIST | |
| Ip | 1962.00 | NIST | |
| Ip | 2019.00 | NIST | |
| Ip | 2028.00 | NIST | |
| Ip | 1956.00 | NIST | |
| Ip | 1987.00 | NIST | |
| Ip | 2019.00 | NIST | |
| Ip | 2014.00 | NIST | |
| Ip | 2032.00 | NIST | |
| Ip | 2032.00 | NIST | |
| Ip | 2014.00 | NIST | |
| Ip | 2004.00 | NIST | |
| Ip | 2006.00 | NIST | |
| Ip | 1987.00 | NIST | |
| Ip | 2000.00 | NIST | |
| Ip | 2015.00 | NIST | |
| Ip | 2000.00 | NIST | |
| Ip | 2000.00 | NIST | |
| Ip | 2000.00 | NIST | |
| Ip | 2015.00 | NIST | |
| Ip | 2015.00 | NIST | |
| Ip | 1956.00 | NIST | |
| Ip | 2010.00 | NIST | |
| Ip | 2023.76 | NIST | |
| Ip | 2018.23 | NIST | |
| Ip | 2024.04 | NIST | |
| Ip | 2015.92 | NIST | |
| Ip | 2004.00 | NIST | |
| Ip | 2015.00 | NIST | |
| Ip | 2008.00 | NIST | |
| Ip | 1996.00 | NIST | |
| Ip | 1965.00 | NIST | |
| Ip | 1978.00 | NIST | |
| Ip | 1977.00 | NIST | |
| Ip | 1965.00 | NIST | |
| Ip | 1973.00 | NIST | |
| Ip | 1965.00 | NIST | |
| Ip | 1973.00 | NIST | |
| Ip | 1973.00 | NIST | |
| Ip | 1975.00 | NIST | |
| Ip | 2012.00 | NIST | |
| Ip | 2014.00 | NIST | |
| Ip | 1997.00 | NIST | |
| Ip | 1984.50 | NIST | |
| Ip | 1983.40 | NIST | |
| Ip | 1967.00 | NIST | |
| Ip | 1962.00 | NIST | |
| Ip | 1950.00 | NIST | |
| Ip | 2026.00 | NIST | |
| Ip | 2015.00 | NIST | |
| Ip | 1996.00 | NIST | |
| Ip | 1996.00 | NIST | |
| Ip | 1984.00 | NIST | |
| Ip | 2003.00 | NIST | |
| Ip | 2028.00 | NIST | |
| Ip | 1990.00 | NIST | |
| Ip | 2035.00 | NIST | |
| Ip | 2039.00 | NIST | |
| Ip | 2039.00 | NIST | |
| Ip | 2012.00 | NIST | |
| Ip | 2007.00 | NIST | |
| Ip | 1995.00 | NIST | |
| Ip | 1989.00 | NIST | |
| Ip | 2030.00 | NIST | |
| Ip | 2008.00 | NIST | |
| Ip | 2020.00 | NIST | |
| Ip | 2011.00 | NIST | |
| Ip | 1994.00 | NIST | |
| Ip | 2019.00 | NIST | |
| Ip | 1993.00 | NIST | |
| Ip | 2007.00 | NIST | |
| Ip | 2007.00 | NIST | |
| Ip | 2007.00 | NIST | |
| Ip | 2015.00 | NIST | |
| Ip | 2023.00 | NIST | |
| Ip | 2035.00 | NIST | |
| Ip | 2017.00 | NIST | |
| Ip | 2015.00 | NIST | |
| Ip | 2039.00 | NIST | |
| Ip | 2020.00 | NIST | |
| Ip | 1969.00 | NIST | |
| Ip | 2045.00 | NIST | |
| Ip | 2012.00 | NIST | |
| Ip | 2019.00 | NIST | |
| Ip | 2011.00 | NIST | |
| Ip | Outlier 1946.00 | NIST | |
| Ip | 2007.00 | NIST | |
| Ip | 2009.00 | NIST | |
| Ip | 1995.00 | NIST | |
| Ip | 2039.00 | NIST | |
| Ip | 2039.00 | NIST | |
| Ip | 2035.00 | NIST | |
| Ip | 1955.00 | NIST | |
| Ip | 1949.00 | NIST | |
| Ip | 1973.00 | NIST | |
| Ip | 1984.00 | NIST | |
| Ip | 2015.00 | NIST | |
| Ip | 1951.00 | NIST | |
| Ip | 2005.00 | NIST | |
| Ip | 1950.00 | NIST | |
| Ip | 1989.00 | NIST | |
| Ip | 1983.00 | NIST | |
| Ip | 2000.00 | NIST | |
| Ip | 1990.00 | NIST | |
| Ip | 2004.00 | NIST | |
| Ip | 1958.00 | NIST | |
| Ip | 2028.00 | NIST | |
| Ip | 1956.00 | NIST | |
| Ip | 1957.00 | NIST | |
| Ip | 1969.00 | NIST | |
| Ip | 1953.00 | NIST | |
| Ip | 1988.00 | NIST | |
| Ip | 1996.00 | NIST | |
| Ip | 2014.00 | NIST | |
| Ip | 2004.00 | NIST | |
| Ip | 1973.00 | NIST | |
| Ip | 1978.00 | NIST | |
| Ip | 2002.00 | NIST | |
| Ip | 2037.00 | NIST | |
| Ip | 2022.00 | NIST | |
| Ip | 2020.00 | NIST | |
| Ip | 1996.00 | NIST | |
| Ip | 1998.00 | NIST | |
| Ip | 1978.00 | NIST | |
| Ip | 2007.00 | NIST | |
| Ip | 1989.00 | NIST | |
| Ip | 2004.00 | NIST | |
| Ip | 2007.00 | NIST | |
| Ip | 1984.00 | NIST | |
| Ip | 2000.00 | NIST | |
| Ip | 2020.00 | NIST | |
| Ip | 2004.00 | NIST | |
| Ip | 1993.00 | NIST | |
| Ip | 1996.00 | NIST | |
| Ip | 2000.00 | NIST | |
| Ip | 2014.00 | NIST | |
| Ip | 1996.00 | NIST | |
| Ip | 2009.00 | NIST | |
| Ip | 1979.00 | NIST | |
| Ip | 1995.00 | NIST | |
| Ip | 1954.00 | NIST | |
| Ip | 1955.00 | NIST | |
| Ip | 1954.00 | NIST | |
| Ip | 1961.00 | NIST | |
| Ip | 1967.00 | NIST | |
| Ip | 2008.00 | NIST | |
| Ip | 2028.00 | NIST | |
| Ip | 2032.00 | NIST | |
| Ip | 1987.00 | NIST | |
| Ip | 2000.00 | NIST | |
| Ip | 2023.76 | NIST | |
| Ip | 2015.00 | NIST | |
| Ip | 1977.00 | NIST | |
| Ip | 1973.00 | NIST | |
| Ip | 1984.50 | NIST | |
| Ip | Outlier 1947.00 | NIST | |
| Ip | 2035.00 | NIST | |
| Ip | 1995.00 | NIST | |
| Ip | 2011.00 | NIST | |
| Ip | 2007.00 | NIST | |
| Ip | 2017.00 | NIST | |
| Ip | 2045.00 | NIST | |
| Ip | 1983.00 | NIST | |
| Ip | 1988.00 | NIST | |
| Ip | 2020.00 | NIST | |
| Ip | 1989.00 | NIST | |
| Ip | 2014.00 | NIST | |
| Ip | 1954.00 | NIST | |
| S°solid,1 bar | [142.70; 144.01] | J/mol×K |
|
| S°solid,1 bar | 144.01 | J/mol×K | NIST |
| S°solid,1 bar | 142.70 | J/mol×K | NIST |
| Tboil | [445.20; 458.00] | K |
|
| Tboil | 455.04 | K | ChemSep v8.3 pure component data Compiled value |
| Tboil | 455.02 | K | KDB |
| Tboil | 454.96 ± 0.30 | K | NIST |
| Tboil | 454.90 | K | NIST |
| Tboil | 454.95 | K | NIST |
| Tboil | 455.30 ± 0.15 | K | NIST |
| Tboil | 454.76 ± 0.05 | K | NIST |
| Tboil | 454.75 ± 0.05 | K | NIST |
| Tboil | 454.95 ± 0.20 | K | NIST |
| Tboil | 454.85 ± 0.30 | K | NIST |
| Tboil | 454.85 ± 0.50 | K | NIST |
| Tboil | 454.95 ± 0.15 | K | NIST |
| Tboil | 454.85 ± 1.00 | K | NIST |
| Tboil | 454.90 ± 0.30 | K | NIST |
| Tboil | 455.35 ± 1.00 | K | NIST |
| Tboil | Outlier 445.20 ± 0.50 | K | NIST |
| Tboil | 455.15 ± 2.00 | K | NIST |
| Tboil | 455.35 ± 0.30 | K | NIST |
| Tboil | 455.35 ± 0.30 | K | NIST |
| Tboil | 455.35 ± 0.30 | K | NIST |
| Tboil | 454.35 ± 0.40 | K | NIST |
| Tboil | 455.05 ± 2.00 | K | NIST |
| Tboil | 454.75 ± 2.00 | K | NIST |
| Tboil | 455.40 ± 0.50 | K | NIST |
| Tboil | 454.60 ± 0.30 | K | NIST |
| Tboil | 454.65 ± 1.50 | K | NIST |
| Tboil | 455.35 ± 1.00 | K | NIST |
| Tboil | 458.00 ± 0.30 | K | NIST |
| Tboil | 455.25 ± 1.00 | K | NIST |
| Tboil | 455.75 ± 0.50 | K | NIST |
| Tc | [692.40; 694.30] | K |
|
| Tc | 694.20 | K | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value |
| Tc | 694.20 | K | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Tc | 694.25 | K | ChemSep v8.3 pure component data Compiled value |
| Tc | 694.20 | K | KDB |
| Tc | 694.30 ± 0.40 | K | NIST |
| Tc | 694.25 ± 0.15 | K | NIST |
| Tc | Outlier 692.40 ± 2.00 | K | NIST |
| Tfus | [312.40; 316.15] | K |
|
| Tfus | 314.85 | K | (Solid + liquid) phase equilibria and solid-compound formation in (N-methyl-2-pyrrolidinone + phenol, or 3,5-dimethylphenol) |
| Tfus | 314.05 | K | Solid-liquid equilibria and the physical properties of binary systems of diphenyl carbonate, dimethyl carbonate, methyl phenyl carbonate, anisole, methanol and phenol |
| Tfus | 314.10 | K | The solid-liquid equilitbrium, excess molar volume and refractive deviation properties of binary systems containing dimethyl carbonate, anisole and phenol |
| Tfus | 314.15 | K | Liquid pharmaceuticals formulation by eutectic formation |
| Tfus | 314.15 | K | Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value |
| Tfus | 314.06 | K | ChemSep v8.3 pure component data Compiled value |
| Tfus | 314.00 | K | KDB |
| Tfus | 314.30 | K | Aq. Solubility Prediction |
| Tfus | 313.85 ± 0.30 | K | NIST |
| Tfus | 314.05 | K | NIST |
| Tfus | 314.15 ± 0.30 | K | NIST |
| Tfus | 314.15 ± 0.50 | K | NIST |
| Tfus | 314.15 ± 0.30 | K | NIST |
| Tfus | 314.05 ± 0.06 | K | NIST |
| Tfus | 313.95 ± 0.50 | K | NIST |
| Tfus | 314.05 ± 0.30 | K | NIST |
| Tfus | 314.20 ± 0.30 | K | NIST |
| Tfus | 314.13 ± 0.02 | K | NIST |
| Tfus | 314.05 ± 0.50 | K | NIST |
| Tfus | 314.15 ± 0.50 | K | NIST |
| Tfus | 314.05 ± 0.10 | K | NIST |
| Tfus | 314.15 ± 0.50 | K | NIST |
| Tfus | 314.15 ± 1.00 | K | NIST |
| Tfus | 314.00 ± 0.20 | K | NIST |
| Tfus | 313.15 ± 0.60 | K | NIST |
| Tfus | 313.90 ± 0.20 | K | NIST |
| Tfus | 313.00 ± 1.50 | K | NIST |
| Tfus | Outlier 315.65 ± 0.50 | K | NIST |
| Tfus | 313.35 ± 0.50 | K | NIST |
| Tfus | 314.05 ± 0.20 | K | NIST |
| Tfus | 314.15 ± 0.30 | K | NIST |
| Tfus | 313.55 ± 0.30 | K | NIST |
| Tfus | 314.05 ± 0.30 | K | NIST |
| Tfus | 314.65 ± 0.30 | K | NIST |
| Tfus | 313.65 ± 0.50 | K | NIST |
| Tfus | 314.00 ± 0.20 | K | NIST |
| Tfus | 314.00 ± 0.20 | K | NIST |
| Tfus | 313.85 ± 0.20 | K | NIST |
| Tfus | 313.30 ± 2.00 | K | NIST |
| Tfus | 312.90 ± 2.00 | K | NIST |
| Tfus | Outlier 315.70 ± 1.00 | K | NIST |
| Tfus | Outlier 312.40 ± 0.50 | K | NIST |
| Tfus | 313.86 ± 0.30 | K | NIST |
| Tfus | 313.95 ± 0.30 | K | NIST |
| Tfus | 314.02 ± 0.20 | K | NIST |
| Tfus | 313.86 ± 0.30 | K | NIST |
| Tfus | 314.07 ± 0.10 | K | NIST |
| Tfus | 313.05 ± 1.00 | K | NIST |
| Tfus | 314.15 ± 1.00 | K | NIST |
| Tfus | 312.85 ± 0.20 | K | NIST |
| Tfus | 313.95 ± 0.10 | K | NIST |
| Tfus | 314.15 ± 1.00 | K | NIST |
| Tfus | 314.15 ± 0.50 | K | NIST |
| Tfus | 313.65 ± 0.50 | K | NIST |
| Tfus | 313.95 ± 0.50 | K | NIST |
| Tfus | Outlier 312.55 ± 0.50 | K | NIST |
| Tfus | 314.15 ± 1.00 | K | NIST |
| Tfus | 314.15 ± 0.30 | K | NIST |
| Tfus | 314.00 ± 0.20 | K | NIST |
| Tfus | 312.85 ± 0.50 | K | NIST |
| Tfus | 313.03 ± 1.00 | K | NIST |
| Tfus | 314.15 ± 1.00 | K | NIST |
| Tfus | 313.15 ± 1.00 | K | NIST |
| Tfus | Outlier 316.15 ± 2.00 | K | NIST |
| Tfus | Outlier 315.65 ± 0.60 | K | NIST |
| Tfus | 313.15 ± 1.50 | K | NIST |
| Tfus | 313.95 ± 0.30 | K | NIST |
| Tfus | 313.95 ± 0.30 | K | NIST |
| Tfus | 314.00 ± 0.40 | K | NIST |
| Tfus | 312.70 ± 1.00 | K | NIST |
| Ttriple | [314.06; 314.06] | K |
|
| Ttriple | 314.06 | K | ChemSep v8.3 pure component data Compiled value |
| Ttriple | 314.06 ± 0.01 | K | NIST |
| Ttriple | 314.06 ± 0.01 | K | NIST |
| UQi | 2.68 | ChemSep v8.3 pure component data Compiled value | |
| URi | 3.55 | ChemSep v8.3 pure component data Compiled value | |
| Vc | [0.229; 0.229] | m3/kmol |
|
| Vc | 0.229 | m3/kmol | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Vc | 0.229 | m3/kmol | ChemSep v8.3 pure component data Compiled value |
| Vc | 0.229 | m3/kmol | KDB |
| Zc | [0.2430000; 0.2432060] |
|
|
| Zc | 0.2430000 | ChemSep v8.3 pure component data Compiled value | |
| Zc | 0.2432060 | KDB | |
| Zra | 0.28 | KDB |
Temperature Dependent Properties
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [42.53; 260.33] | J/mol×K | [100.00; 1500.00] |
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 | 3.97580e+01 | |||
| Coefficient B | -4.70560e+02 | |||
| Coefficient C | 5.71924e+00 | |||
| Coefficient D | 6.83470e-05 | |||
| Coefficient E | -4.97080e-08 | |||
| Temperature range, min. | 100.00 | |||
| Temperature range, max. | 1500.00 | |||
| Cp,gas | 42.53 | J/mol×K | 100.00 | Calculated Property |
| Cp,gas | 88.77 | J/mol×K | 255.56 | Calculated Property |
| Cp,gas | 138.68 | J/mol×K | 411.11 | Calculated Property |
| Cp,gas | 175.62 | J/mol×K | 566.67 | Calculated Property |
| Cp,gas | 202.33 | J/mol×K | 722.22 | Calculated Property |
| Cp,gas | 221.91 | J/mol×K | 877.78 | Calculated Property |
| Cp,gas | 236.41 | J/mol×K | 1033.33 | Calculated Property |
| Cp,gas | 247.12 | J/mol×K | 1188.89 | Calculated Property |
| Cp,gas | 254.90 | J/mol×K | 1344.44 | Calculated Property |
| Cp,gas | 260.33 | J/mol×K | 1500.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | [202.65; 301.75] | J/mol×K | [314.05; 655.37] |
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 | 8.67100e+01 | |||
| Coefficient B | -6.28110e+02 | |||
| Coefficient C | 8.82724e+00 | |||
| Coefficient D | -9.17430e-03 | |||
| Coefficient E | 8.18270e-06 | |||
| Temperature range, min. | 314.05 | |||
| Temperature range, max. | 655.37 | |||
| Cp,liquid | 202.65 | J/mol×K | 314.05 | Calculated Property |
| Cp,liquid | 211.59 | J/mol×K | 351.97 | Calculated Property |
| Cp,liquid | 218.76 | J/mol×K | 389.90 | Calculated Property |
| Cp,liquid | 225.34 | J/mol×K | 427.82 | Calculated Property |
| Cp,liquid | 232.29 | J/mol×K | 465.75 | Calculated Property |
| Cp,liquid | 240.44 | J/mol×K | 503.67 | Calculated Property |
| Cp,liquid | 250.56 | J/mol×K | 541.60 | Calculated Property |
| Cp,liquid | 263.47 | J/mol×K | 579.52 | Calculated Property |
| Cp,liquid | 280.14 | J/mol×K | 617.45 | Calculated Property |
| Cp,liquid | 301.75 | J/mol×K | 655.37 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [0.0112250; 0.0000420] | Pa×s | [291.45; 690.00] |
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 | -2.03001e+02 | |||
| Coefficient B | 1.08842e+04 | |||
| Coefficient C | 2.87361e+01 | |||
| Coefficient D | -2.24564e-05 | |||
| Coefficient E | 2.00000e+00 | |||
| Temperature range, min. | 291.45 | |||
| Temperature range, max. | 690.00 | |||
| η | 0.0112250 | Pa×s | 291.45 | Calculated Property |
| η | 0.0025429 | Pa×s | 335.73 | Calculated Property |
| η | 0.0010041 | Pa×s | 380.02 | Calculated Property |
| η | 0.0005393 | Pa×s | 424.30 | Calculated Property |
| η | 0.0003406 | Pa×s | 468.58 | Calculated Property |
| η | 0.0002314 | Pa×s | 512.87 | Calculated Property |
| η | 0.0001597 | Pa×s | 557.15 | Calculated Property |
| η | 0.0001078 | Pa×s | 601.43 | Calculated Property |
| η | 0.0000694 | Pa×s | 645.72 | Calculated Property |
| η | 0.0000420 | Pa×s | 690.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | [58.14; 21.96] | kJ/mol | [314.06; 674.24] |
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 | 7.27028e+01 | |||
| Coefficient B | -2.65673e-01 | |||
| Coefficient C | 2.24855e+00 | |||
| Coefficient D | -2.01871e+00 | |||
| Coefficient E | 3.53169e-01 | |||
| Critical temperature, Tc (K) | 6.94250e+02 | |||
| Temperature range, min. | 314.06 | |||
| Temperature range, max. | 674.24 | |||
| ΔvapH | 58.14 | kJ/mol | 314.06 | Calculated Property |
| ΔvapH | 54.54 | kJ/mol | 354.08 | Calculated Property |
| ΔvapH | 50.91 | kJ/mol | 394.10 | Calculated Property |
| ΔvapH | 47.32 | kJ/mol | 434.12 | Calculated Property |
| ΔvapH | 43.81 | kJ/mol | 474.14 | Calculated Property |
| ΔvapH | 40.38 | kJ/mol | 514.16 | Calculated Property |
| ΔvapH | 36.97 | kJ/mol | 554.18 | Calculated Property |
| ΔvapH | 33.40 | kJ/mol | 594.20 | Calculated Property |
| ΔvapH | 29.17 | kJ/mol | 634.22 | Calculated Property |
| ΔvapH | 21.96 | kJ/mol | 674.24 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [0.14; 202.67] | kPa | [314.06; 481.13] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.49478e+01 | |||
| Coefficient B | -3.75184e+03 | |||
| Coefficient C | -9.17810e+01 | |||
| Temperature range, min. | 314.06 | |||
| Temperature range, max. | 481.13 | |||
| Pvap | 0.14 | kPa | 314.06 | Calculated Property |
| Pvap | 0.53 | kPa | 332.62 | Calculated Property |
| Pvap | 1.62 | kPa | 351.19 | Calculated Property |
| Pvap | 4.26 | kPa | 369.75 | Calculated Property |
| Pvap | 9.93 | kPa | 388.31 | Calculated Property |
| Pvap | 20.92 | kPa | 406.88 | Calculated Property |
| Pvap | 40.58 | kPa | 425.44 | Calculated Property |
| Pvap | 73.40 | kPa | 444.00 | Calculated Property |
| Pvap | 125.10 | kPa | 462.57 | Calculated Property |
| Pvap | 202.67 | kPa | 481.13 | Calculated Property |
| Pvap | [0.05; 6111.19] | kPa | [310.45; 694.25] |
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 | 2.94062e+02 | |||
| Coefficient B | -2.02690e+04 | |||
| Coefficient C | -4.07430e+01 | |||
| Coefficient D | 2.16310e-05 | |||
| Coefficient E | 2.00000e+00 | |||
| Temperature range, min. | 310.45 | |||
| Temperature range, max. | 694.25 | |||
| Pvap | 0.05 | kPa | 310.45 | Calculated Property |
| Pvap | 1.39 | kPa | 353.09 | Calculated Property |
| Pvap | 12.91 | kPa | 395.74 | Calculated Property |
| Pvap | 62.80 | kPa | 438.38 | Calculated Property |
| Pvap | 201.30 | kPa | 481.03 | Calculated Property |
| Pvap | 493.83 | kPa | 523.67 | Calculated Property |
| Pvap | 1025.12 | kPa | 566.32 | Calculated Property |
| Pvap | 1929.63 | kPa | 608.96 | Calculated Property |
| Pvap | 3458.21 | kPa | 651.61 | Calculated Property |
| Pvap | 6111.19 | kPa | 694.25 | Calculated Property |
| Pvap | [0.20; 6095.48] | kPa | [314.06; 694.25] |
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 | 9.32745e+01 | |||
| Coefficient B | -1.00030e+04 | |||
| Coefficient C | -1.10400e+01 | |||
| Coefficient D | 4.31995e-06 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 314.06 | |||
| Temperature range, max. | 694.25 | |||
| Pvap | 0.20 | kPa | 314.06 | Calculated Property |
| Pvap | 2.41 | kPa | 356.30 | Calculated Property |
| Pvap | 15.74 | kPa | 398.55 | Calculated Property |
| Pvap | 66.86 | kPa | 440.79 | Calculated Property |
| Pvap | 209.65 | kPa | 483.03 | Calculated Property |
| Pvap | 528.09 | kPa | 525.28 | Calculated Property |
| Pvap | 1132.56 | kPa | 567.52 | Calculated Property |
| Pvap | 2155.01 | kPa | 609.76 | Calculated Property |
| Pvap | 3748.72 | kPa | 652.01 | Calculated Property |
| Pvap | 6095.48 | kPa | 694.25 | Calculated Property |
| Pvap | [7.60; 101.30] | kPa | [380.30; 454.90] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.43840e+01 | |||
| Coefficient B | -3.47616e+03 | |||
| Coefficient C | -9.89490e+01 | |||
| Reference | Dreisbach and Shrader, 1949 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 380.30 | |||
| Temperature range, max. | 454.90 | |||
| Pvap | 7.60 | kPa | 380.30 | Calculated Property |
| Pvap | 10.83 | kPa | 388.59 | Calculated Property |
| Pvap | 15.12 | kPa | 396.88 | Calculated Property |
| Pvap | 20.74 | kPa | 405.17 | Calculated Property |
| Pvap | 27.97 | kPa | 413.46 | Calculated Property |
| Pvap | 37.15 | kPa | 421.74 | Calculated Property |
| Pvap | 48.65 | kPa | 430.03 | Calculated Property |
| Pvap | 62.87 | kPa | 438.32 | Calculated Property |
| Pvap | 80.26 | kPa | 446.61 | Calculated Property |
| Pvap | 101.30 | kPa | 454.90 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ρl | [1058.02; 530.05] | kg/m3 | [314.06; 688.71] |
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 | 1.40574e+02 | |||
| Coefficient B | 3.28830e-01 | |||
| Coefficient C | 6.94250e+02 | |||
| Coefficient D | 3.40180e-01 | |||
| Temperature range, min. | 314.06 | |||
| Temperature range, max. | 688.71 | |||
| ρl | 1058.02 | kg/m3 | 314.06 | Calculated Property |
| ρl | 1021.57 | kg/m3 | 355.69 | Calculated Property |
| ρl | 983.46 | kg/m3 | 397.32 | Calculated Property |
| ρl | 943.27 | kg/m3 | 438.94 | Calculated Property |
| ρl | 900.41 | kg/m3 | 480.57 | Calculated Property |
| ρl | 853.99 | kg/m3 | 522.20 | Calculated Property |
| ρl | 802.47 | kg/m3 | 563.83 | Calculated Property |
| ρl | 742.85 | kg/m3 | 605.45 | Calculated Property |
| ρl | 667.48 | kg/m3 | 647.08 | Calculated Property |
| ρl | 530.05 | kg/m3 | 688.71 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| γ | [0.04; 0.02] | N/m | [314.15; 455.15] |
Jasper (1972), surface tension of pure liquid compounds Compiled value
|
| Equation | Y = A + B·T + C·T² + D·T³ + E·T⁴ Y is γ in N/m, T in K | |||
| Coefficient A | 7.27397e-02 | |||
| Coefficient B | -1.06900e-04 | |||
| Coefficient C | 0.00000e+00 | |||
| Coefficient D | 0.00000e+00 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 314.15 | |||
| Temperature range, max. | 455.15 | |||
| γ | 0.04 | N/m | 314.15 | Calculated Property |
| γ | 0.04 | N/m | 329.82 | Calculated Property |
| γ | 0.04 | N/m | 345.48 | Calculated Property |
| γ | 0.03 | N/m | 361.15 | Calculated Property |
| γ | 0.03 | N/m | 376.82 | Calculated Property |
| γ | 0.03 | N/m | 392.48 | Calculated Property |
| γ | 0.03 | N/m | 408.15 | Calculated Property |
| γ | 0.03 | N/m | 423.82 | Calculated Property |
| γ | 0.03 | N/m | 439.48 | Calculated Property |
| γ | 0.02 | N/m | 455.15 | Calculated Property |
| γ | [0.04; 0.00] | N/m | [273.15; 674.24] |
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 | -4.78760e-02 | |||
| Coefficient B | -1.63070e+01 | |||
| Coefficient C | -2.03760e+00 | |||
| Coefficient D | -9.04600e-04 | |||
| Coefficient E | -7.35800e-07 | |||
| Temperature range, min. | 273.15 | |||
| Temperature range, max. | 674.24 | |||
| γ | 0.04 | N/m | 273.15 | Calculated Property |
| γ | 0.04 | N/m | 317.72 | Calculated Property |
| γ | 0.03 | N/m | 362.28 | Calculated Property |
| γ | 0.03 | N/m | 406.85 | Calculated Property |
| γ | 0.02 | N/m | 451.41 | Calculated Property |
| γ | 0.02 | N/m | 495.98 | Calculated Property |
| γ | 0.01 | N/m | 540.54 | Calculated Property |
| γ | 0.01 | N/m | 585.11 | Calculated Property |
| γ | 0.01 | N/m | 629.67 | Calculated Property |
| γ | 0.00 | N/m | 674.24 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λgas | [0.01; 0.07] | W/m×K | [199.82; 1000.00] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A·T^B / (1 + C/T + D/T²) Y is λgas in W/m×K, T in K | |||
| Coefficient A | 3.49500e-02 | |||
| Coefficient B | 2.78450e-01 | |||
| Coefficient C | 1.58520e+03 | |||
| Coefficient D | 8.62070e+05 | |||
| Temperature range, min. | 199.82 | |||
| Temperature range, max. | 1000.00 | |||
| λgas | 0.01 | W/m×K | 199.82 | Calculated Property |
| λgas | 0.01 | W/m×K | 288.73 | Calculated Property |
| λgas | 0.02 | W/m×K | 377.64 | Calculated Property |
| λgas | 0.02 | W/m×K | 466.55 | Calculated Property |
| λgas | 0.03 | W/m×K | 555.46 | Calculated Property |
| λgas | 0.04 | W/m×K | 644.36 | Calculated Property |
| λgas | 0.05 | W/m×K | 733.27 | Calculated Property |
| λgas | 0.05 | W/m×K | 822.18 | Calculated Property |
| λgas | 0.06 | W/m×K | 911.09 | Calculated Property |
| λgas | 0.07 | W/m×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λliquid | [0.16; 0.14] | W/m×K | [314.06; 454.99] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A + exp(B/T + C + D·T + E·T²) Y is λliquid in W/m×K, T in K | |||
| Coefficient A | 1.41090e-01 | |||
| Coefficient B | -9.66500e+02 | |||
| Coefficient C | 1.06590e+01 | |||
| Coefficient D | -4.90950e-02 | |||
| Coefficient E | 3.87030e-05 | |||
| Temperature range, min. | 314.06 | |||
| Temperature range, max. | 454.99 | |||
| λliquid | 0.16 | W/m×K | 314.06 | Calculated Property |
| λliquid | 0.16 | W/m×K | 329.72 | Calculated Property |
| λliquid | 0.15 | W/m×K | 345.38 | Calculated Property |
| λliquid | 0.15 | W/m×K | 361.04 | Calculated Property |
| λliquid | 0.15 | W/m×K | 376.70 | Calculated Property |
| λliquid | 0.15 | W/m×K | 392.35 | Calculated Property |
| λliquid | 0.15 | W/m×K | 408.01 | Calculated Property |
| λliquid | 0.15 | W/m×K | 423.67 | Calculated Property |
| λliquid | 0.14 | W/m×K | 439.33 | Calculated Property |
| λliquid | 0.14 | W/m×K | 454.99 | Calculated Property |
Similar Compounds
![3-Hydroxybenz[a]anthracene.](data:image/png;base64,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)
Find more compounds similar to Phenol.
Mixtures
- 1-Octanol + Phenol
- Choline chloride + Carbon dioxide + Phenol
- Carbon dioxide + TETRAMETHYLAMMONIUM CHLORIDE + Phenol
- Choline chloride + Phenol
- TETRAMETHYLAMMONIUM CHLORIDE + Phenol
- Toluene + Choline chloride + Phenol
- Toluene + TETRAMETHYLAMMONIUM CHLORIDE + Phenol
- Methyl Alcohol + Phenol + Water
- Phenol + Water
- Cyclohexanone + Phenol + Water
- 1-Octanol + Phenol + Water
- 1-Hexanol, 2-ethyl- + Phenol + Water
- Acetic acid, 2-methylpropyl ester + Phenol + Water
- 1,2-Ethanediol + Heptane + Phenol
- p-Xylene + Phenol + Water
- Hexadecanoic acid, methyl ester + Phenol + Water
- Toluene + 1,2-Ethanediol + Phenol
- Ethanol + Phenol
- Carbon dioxide + Phenol + Water
- 2-Butanone, 3-methyl- + Phenol + Water
Find more mixtures with Phenol.
Sources
- KDB Vapor Pressure Data
- Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) ChEDL chemicals 1.5.2, from Bradley, J.-C.; Williams, A.; Lang, A. Jean-Claude Bradley Open Melting Point Dataset. Figshare, 2014 (CC0).
- IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 ChEDL chemicals 1.5.2, from Kudchadker, A. P.; Ambrose, D.; Tsonopoulos, C. Vapor-Liquid Critical Properties of Elements and Compounds. 7. Oxygen Compounds Other Than Alkanols and Cycloalkanols. J. Chem. Eng. Data 2001, 46, 457-479.
- Jasper (1972), surface tension of pure liquid compounds ChEDL chemicals 1.5.2, from Jasper, J. J. The Surface Tension of Pure Liquid Compounds. J. Phys. Chem. Ref. Data 1972, 1, 841-1010 (as transcribed in Lange's Handbook).
- PSRK revision IV (2005), critical constants and acentric factors of 1000 components ChEDL chemicals 1.5.2, from Horstmann, S.; Jabłoniec, A.; Krafczyk, J.; Fischer, K.; Gmehling, J. PSRK Group Contribution Equation of State: Comprehensive Revision and Extension IV, Including Critical Constants and α-Function Parameters for 1000 Components. Fluid Phase Equilib. 2005, 227, 157-164.
- 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
- (Solid + liquid) phase equilibria and solid-compound formation in (N-methyl-2-pyrrolidinone + phenol, or 3,5-dimethylphenol)
- Liquid liquid equilibria for the quaternary system methyl isobutyl ketone water phenol hydroquinone
- Ionic liquid structural effects on solute partitioning in biphasic ionic liquid and supercritical carbon dioxide systems
- Liquid-liquid equilibria of ternary mixtures of dimethyl carbonate, diphenyl carbonate, phenol and water at 358.15 K
- Solid-liquid equilibria and the physical properties of binary systems of diphenyl carbonate, dimethyl carbonate, methyl phenyl carbonate, anisole, methanol and phenol
- Ternary liquid-liquid equilibria and binary excess and deviation properties at constant temperature for mixtures of dimethyl carbonate, anisole, methanol, phenol and water
- An experimental investgation on the solubility of CO2 in aqueous solutions of phenol
- The solid-liquid equilitbrium, excess molar volume and refractive deviation properties of binary systems containing dimethyl carbonate, anisole and phenol
- Liquid-liquid equilibria for the extraction of phenols from alkane using ethylene glycol
- Phase equilibria of phenol + toluene + quaternary ammonium salts for the separation of phenols from oil with forming deep eutectic solvents
- Phase equilibria of high pressure CO2 and deep eutectic solvents formed by quaternary ammonium salts and phenol
- Acoustic, volumetric, transport, optical and rheological properties of benzyltripropylammonium based Deep Eutectic Solvents
- Extraction of phenolic compounds from aqueous solution using choline bis(trifluoromethylsulfonyl)imide
- Ternary phase behavior of phenol + toluene + zwitterionic alkaloids for separating phenols from oil mixtures via forming deep eutectic solvents
- Liquid pharmaceuticals formulation by eutectic formation
- Screening solvents to extract phenol from aqueous solutions by the COSMO-SAC model and extraction process simulation
- Phase equilibria of phenolic compounds in water or ethanol
- Liquid-liquid equilibria of water + solutes (acetic acid/ acetol/furfural/guaiacol/methanol/phenol/propanal) + solvents (isopropyl acetate/toluene) ternary systems for pyrolysis oil fractionation
- Heat capacities of aqueous polar aromatic compounds over a wide range of conditions. Part I: phenol, cresols, aniline, and toluidines
- Partial molar volumes of some drug and pro-drug substances in 1-octanol at T = 298.15 K
- (Liquid + liquid) equilibrium of {water + phenol + (1-butanol, or 2-butanol, or tert-butanol)} systems
- Tar removal from biosyngas in the biomass gasification process. (Liquid + liquid) equilibrium {water + solvent (paraxylene and methyl hexadecanoate) + model molecules of tar (benzene, toluene, phenol)}
- Tie-line data for the aqueous solutions of phenol with organic solvents at T = 298.2 K
- Solubilities and thermodynamic properties of CO2 in choline-chloride based deep eutectic solvents
- Measurements and correlation of liquid-liquid equilibrium data for the ternary (3-heptanone + phenol + water) system
- (Liquid + liquid) extraction of phenols from aqueous solutions with cineole
- Liquid-liquid equilibria for toluene/heptane + phenol/cresols + ethylene glycol system
- Phase equilibrium measurements and thermodynamic modelling of {water + phenol + [Hmim][NTf2]} ionic liquid system at several temperatures
- Solvent screening and liquid-liquid measurement for extraction of phenols from aromatic hydrocarbon mixtures
- Experimental Determination and Correlation of Liquid Liquid Equilibria for Methyl Isopropyl Ketone + Phenol + Water Mixtures at 298.15, 313.15, and 323.15 K
- Ternary and Quaternary Liquid-Liquid Equilibria for Systems of Methyl Butyl Ketone + Water + Hydroquinone + Phenol at 313.2 K and Atmospheric Pressure
- Molar Heat Capacity of Selected Type III Deep Eutectic Solvents
- Liquid-Liquid Equilibria for the Ternary System Mesityl Oxide + Phenol + Water at 298.15, 313.15, and 323.15 K
- Liquid-Liquid Equilibrium Measurements for Model Systems Related to Catalytic Fast Pyrolysis of Biomass
- Liquid-Liquid Equilibrium of the Ternary System of Water + Phenol + (Propan-2-yl) Benzene at Several Temperatures
- Experimental Measurements and Modeling Study of Liquid-Liquid Equilibrium [(Water + Methyl Oleate + Model Molecules of Tar Issued from the Biomass Gasification Process (Benzene, Toluene, Phenol, Thiophene, and Pyridine)]
- Salt Effects on Liquid-Liquid Equilibria of Water + Phenol + (Propan-2-yl) Benzene + Salts Systems
- Experimental Measurement and Thermodynamic Model of Liquid-Liquid Equilibrium for the Ternary System of 1-Dodecanol-Phenol-Water
- Experimental Investigation of Liquid-Liquid Extraction of Toluene + Heptane or Toluene + Hexane Using Deep Eutectic Solvents
- Vapor-Liquid Equilibrium for Phenol + r-Methyl Benzyl Alcohol and 2-Ethoxyethanol + n-Butyl Formate
- Measurement and Correlation of Mutual Solubilities for High Viscosity Binary Systems: Aniline + Methylcyclohexane, Phenol + Heptane, Phenol + Octane, and Glycerol + 1-Pentanol
- Vapor-Liquid Equilibria on Seven Binary Systems: Ethylene Oxide + 2-Methylpropane; Acetophenone + Phenol; cis-1,3-Dichloropropene + 1,2-Dichloropropane; 1,5-Hexadiene + Allyl Chloride; Isopropyl Acetate + Acetonitrile; Vinyl Chloride + Methyl Chloride; and 1,4-Butanediol + c-Butyrolactone
- Vapor-Liquid Equilibria on Four Binary Systems: 2-Phenylpropionaldehyde + Phenol, Propylene Glycol Monomethyl Ether + Nitroethane, Dimethyl Ether + Propylene, and N-Butyric Acid + Propionic Acid
- Liquid-Liquid Equilibrium of (Water + Acetone) with Cumene or r-Methylstyrene or Phenol at Temperatures of (323.15 and 333.15) K
- Ternary and Quaternary Liquid + Liquid Equilibria for Systems of (Water + Toluene + m-Xylene + Phenol)
- Vapor-Liquid Critical Properties of Phenol and (C8 to C10) Phenylalkanols
- Liquid-Liquid Equilibria in Ternary Systems of Aromatic Hydrocarbons (Toluene or Ethylbenzene) + Phenols + Water
- Liquid-Liquid(-Liquid) Equilibria in Ternary Systems of Aliphatic Hydrocarbons (Heptane or Octane) + Phenols + Water
- Vapor-Liquid Equilibria in Ternary Systems of Toluene or Octane + Phenols + Water
- Solid-Liquid Equilibria in Three Binary Mixtures Containing Diphenyl Carbonate
- Solute Partitioning Between 1-n-Butyl-3-methylimidazolium Trifluoromethanesulfonate Ionic Liquid and Supercritical CO2
- Formation of Deep Eutectic Solvents by Phenols and Choline Chloride and Their Physical Properties
- Infinite Dilution Binary Diffusion Coefficients for Compounds Derived from Biomass in Water at 0.1 MPa and Temperatures from (298.2 to 353.2) K
- Liquid Liquid Equilibria for the Ternary System 2-Methoxy-2-methylpropane + Phenol + Water
- Experimental Densities and Speeds of Sound of Substituted Phenols and Their Modeling with the Prigogine Flory Patterson Model
- Liquid Liquid Equilibria for Ternary Mixtures of Methylphenyl Carbonate, Dimethyl Carbonate, Diphenyl Carbonate, Anisole, Methanol, Phenol, and Water at Several Temperatures
- Liquid Liquid Equilibria for Ternary Systems: Methyl Butyl Ketone + Phenol + Water and Methyl Butyl Ketone + Hydroquinone + Water at 298.15 K and 323.15 K
- Diffusion Coefficients of Organic Compounds at Infinite Dilution in Mixtures Involving Associating Compounds. Experimental Determination and Modeling by Group Contribution Methods
- Henry s Law Constants of Some Aromatic Aldehydes and Ketones Measured by an Internal Standard Method
- Joback Method
- KDB
- Aqueous Solubility Prediction Method
- Estimated Solubility Method
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
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