- 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-
- Benzenol
- Carbolic acid
- Carbolsaure
- Fenol
- Fenolo
- Hydroxybenzene
- 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
- Phenyl hydroxide
- Phenylic acid
- Phenylic alcohol
- Rcra waste number U188
- UN 1671
- UN 2312
- UN 2821
- 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,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).
- 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).
- 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).
- Tfus : Normal melting (fusion) point (K).
- Ttriple : Triple Point Temperature (K).
- 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 | 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 | 1.60 | 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 | kJ/mol | KDB |
| Rg | 3.5500 | KDB | |
| ΔfH°gas | [-96.44; -94.20] | kJ/mol |
|
| 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. Sol... | |
| log10WS | 0.00 | Estimat... | |
| 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 | 6130.00 | kPa | KDB |
| Pc | 5670.00 | kPa | Vapor-L... |
| Pc | 5930.00 ± 78.45 | kPa | NIST |
| Pc | 6130.16 ± 81.06 | kPa | NIST |
| 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 | 950.00 | NIST | |
| Inp | 950.20 | NIST | |
| Inp | 943.00 | NIST | |
| Inp | 964.00 | NIST | |
| Inp | 951.00 | NIST | |
| Inp | 933.00 | NIST | |
| Inp | 973.00 | NIST | |
| Inp | Outlier 152.20 | NIST | |
| Inp | 982.00 | NIST | |
| Inp | 980.00 | NIST | |
| Inp | 976.00 | NIST | |
| Inp | 974.00 | NIST | |
| Inp | 1002.00 | 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 | |
| I | [1946.00; 2045.00] |
|
|
| I | 2000.00 | NIST | |
| I | 2000.00 | NIST | |
| I | 1971.00 | NIST | |
| I | 1957.00 | NIST | |
| I | Outlier 1947.00 | NIST | |
| I | Outlier 1947.00 | NIST | |
| I | 2030.00 | NIST | |
| I | 2037.00 | NIST | |
| I | 2008.00 | NIST | |
| I | 2008.00 | NIST | |
| I | 1992.00 | NIST | |
| I | 1962.00 | NIST | |
| I | 2019.00 | NIST | |
| I | 2028.00 | NIST | |
| I | 1956.00 | NIST | |
| I | 1987.00 | NIST | |
| I | 2019.00 | NIST | |
| I | 2014.00 | NIST | |
| I | 2032.00 | NIST | |
| I | 2032.00 | NIST | |
| I | 2014.00 | NIST | |
| I | 2004.00 | NIST | |
| I | 2006.00 | NIST | |
| I | 1987.00 | NIST | |
| I | 2000.00 | NIST | |
| I | 2015.00 | NIST | |
| I | 2000.00 | NIST | |
| I | 2000.00 | NIST | |
| I | 2000.00 | NIST | |
| I | 2015.00 | NIST | |
| I | 2015.00 | NIST | |
| I | 1956.00 | NIST | |
| I | 2010.00 | NIST | |
| I | 2023.76 | NIST | |
| I | 2018.23 | NIST | |
| I | 2024.04 | NIST | |
| I | 2015.92 | NIST | |
| I | 2004.00 | NIST | |
| I | 2015.00 | NIST | |
| I | 2008.00 | NIST | |
| I | 1996.00 | NIST | |
| I | 1965.00 | NIST | |
| I | 1978.00 | NIST | |
| I | 1977.00 | NIST | |
| I | 1965.00 | NIST | |
| I | 1973.00 | NIST | |
| I | 1965.00 | NIST | |
| I | 1973.00 | NIST | |
| I | 1973.00 | NIST | |
| I | 1975.00 | NIST | |
| I | 2012.00 | NIST | |
| I | 2014.00 | NIST | |
| I | 1997.00 | NIST | |
| I | 1984.50 | NIST | |
| I | 1983.40 | NIST | |
| I | 1967.00 | NIST | |
| I | 1962.00 | NIST | |
| I | 1950.00 | NIST | |
| I | 2026.00 | NIST | |
| I | 2015.00 | NIST | |
| I | 1996.00 | NIST | |
| I | 1996.00 | NIST | |
| I | 1984.00 | NIST | |
| I | 2003.00 | NIST | |
| I | 2028.00 | NIST | |
| I | 1990.00 | NIST | |
| I | 2035.00 | NIST | |
| I | 2039.00 | NIST | |
| I | 2039.00 | NIST | |
| I | 2012.00 | NIST | |
| I | 2007.00 | NIST | |
| I | 1995.00 | NIST | |
| I | 1989.00 | NIST | |
| I | 2030.00 | NIST | |
| I | 2008.00 | NIST | |
| I | 2020.00 | NIST | |
| I | 2011.00 | NIST | |
| I | 1994.00 | NIST | |
| I | 2019.00 | NIST | |
| I | 1993.00 | NIST | |
| I | 2007.00 | NIST | |
| I | 2007.00 | NIST | |
| I | 2007.00 | NIST | |
| I | 2015.00 | NIST | |
| I | 2023.00 | NIST | |
| I | 2035.00 | NIST | |
| I | 2017.00 | NIST | |
| I | 2015.00 | NIST | |
| I | 2039.00 | NIST | |
| I | 2020.00 | NIST | |
| I | 1969.00 | NIST | |
| I | 2045.00 | NIST | |
| I | 2012.00 | NIST | |
| I | 2019.00 | NIST | |
| I | 2011.00 | NIST | |
| I | Outlier 1946.00 | NIST | |
| I | 2007.00 | NIST | |
| I | 2009.00 | NIST | |
| I | 1995.00 | NIST | |
| I | 2039.00 | NIST | |
| I | 2039.00 | NIST | |
| I | 2035.00 | NIST | |
| I | 1955.00 | NIST | |
| I | 1949.00 | NIST | |
| I | 1973.00 | NIST | |
| I | 1984.00 | NIST | |
| I | 2015.00 | NIST | |
| I | 1951.00 | NIST | |
| I | 2005.00 | NIST | |
| I | 1950.00 | NIST | |
| I | 1989.00 | NIST | |
| I | 1983.00 | NIST | |
| I | 2000.00 | NIST | |
| I | 1990.00 | NIST | |
| I | 2004.00 | NIST | |
| I | 1958.00 | NIST | |
| I | 2028.00 | NIST | |
| I | 1956.00 | NIST | |
| I | 1957.00 | NIST | |
| I | 1969.00 | NIST | |
| I | 1953.00 | NIST | |
| I | 1988.00 | NIST | |
| I | 1996.00 | NIST | |
| I | 2014.00 | NIST | |
| I | 2004.00 | NIST | |
| I | 1973.00 | NIST | |
| I | 1978.00 | NIST | |
| I | 2002.00 | NIST | |
| I | 2037.00 | NIST | |
| I | 2022.00 | NIST | |
| I | 2020.00 | NIST | |
| I | 1996.00 | NIST | |
| I | 1998.00 | NIST | |
| I | 1978.00 | NIST | |
| I | 2007.00 | NIST | |
| I | 1989.00 | NIST | |
| I | 2004.00 | NIST | |
| I | 2007.00 | NIST | |
| I | 1984.00 | NIST | |
| I | 2000.00 | NIST | |
| I | 2020.00 | NIST | |
| I | 2004.00 | NIST | |
| I | 1993.00 | NIST | |
| I | 1996.00 | NIST | |
| I | 2000.00 | NIST | |
| I | 2014.00 | NIST | |
| I | 1996.00 | NIST | |
| I | 2009.00 | NIST | |
| I | 1979.00 | NIST | |
| I | 1995.00 | NIST | |
| I | 1954.00 | NIST | |
| I | 1955.00 | NIST | |
| I | 1954.00 | NIST | |
| I | 1961.00 | NIST | |
| I | 1967.00 | NIST | |
| I | 1973.00 | NIST | |
| I | 2020.00 | NIST | |
| I | 1989.00 | NIST | |
| I | 2014.00 | NIST | |
| I | 1954.00 | NIST | |
| I | 2000.00 | NIST | |
| I | Outlier 1947.00 | NIST | |
| I | 2035.00 | NIST | |
| I | 1995.00 | NIST | |
| I | 2011.00 | NIST | |
| I | 2007.00 | NIST | |
| I | 2017.00 | NIST | |
| I | 2045.00 | NIST | |
| I | 2015.00 | NIST | |
| I | 1983.00 | NIST | |
| I | 2028.00 | NIST | |
| I | 1988.00 | NIST | |
| I | 2008.00 | NIST | |
| I | 2032.00 | NIST | |
| I | 1987.00 | NIST | |
| I | 2023.76 | NIST | |
| I | 1977.00 | NIST | |
| I | 1984.50 | 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 | 455.02 | 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 | KDB |
| Tc | 694.30 ± 0.40 | K | NIST |
| Tc | 694.25 ± 0.15 | K | NIST |
| Tc | 692.40 ± 2.00 | K | NIST |
| Tfus | [314.00; 314.85] | K |
|
| Tfus | 314.30 | K | Aq. Sol... |
| Tfus | 314.00 | K | KDB |
| Tfus | Outlier 314.85 | K | (Solid ... |
| Tfus | 314.05 | K | Solid-l... |
| Tfus | 314.10 | K | The sol... |
| Tfus | 314.15 | K | Liquid ... |
| Ttriple | 314.06 ± 0.01 | K | NIST |
| Vc | 0.229 | m3/kmol | KDB |
| Zc | 0.2432060 | KDB | |
| Zra | 0.28 | KDB |
Temperature Dependent Properties
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [145.52; 193.78] | J/mol×K | [439.00; 671.01] |
|
|
T(K) Ideal gas heat capacity (J/mol×K) 150 160 170 180 190 500 600 | ||||
| Cp,gas | 145.52 | J/mol×K | 439.00 | Joback Calculated Property |
| Cp,gas | 155.59 | J/mol×K | 477.67 | Joback Calculated Property |
| Cp,gas | 164.73 | J/mol×K | 516.34 | Joback Calculated Property |
| Cp,gas | 173.03 | J/mol×K | 555.01 | Joback Calculated Property |
| Cp,gas | 180.59 | J/mol×K | 593.67 | Joback Calculated Property |
| Cp,gas | 187.47 | J/mol×K | 632.34 | Joback Calculated Property |
| Cp,gas | 193.78 | J/mol×K | 671.01 | Joback Calculated Property |
| Cp,solid | [93.70; 199.80] | J/mol×K | [229.30; 313.00] |
|
|
T(K) Solid phase heat capacity (J/mol×K) 100 120 140 160 180 200 240 260 280 300 | ||||
| Cp,solid | 103.80 | J/mol×K | 229.30 | NIST |
| Cp,solid | 93.70 | J/mol×K | 293.00 | NIST |
| Cp,solid | 133.09 | J/mol×K | 295.80 | NIST |
| Cp,solid | 127.21 | J/mol×K | 298.15 | NIST |
| Cp,solid | 127.44 | J/mol×K | 298.15 | NIST |
| Cp,solid | 199.80 | J/mol×K | 313.00 | NIST |
| η | [0.0001736; 0.0135969] | Pa×s | [283.00; 439.00] |
|
|
T(K) Dynamic viscosity (Pa×s) 0 2.00e-3 4.00e-3 6.00e-3 8.00e-3 0.01 0.01 0.01 300 350 400 | ||||
| η | 0.0135969 | Pa×s | 283.00 | Joback Calculated Property |
| η | 0.0048418 | Pa×s | 309.00 | Joback Calculated Property |
| η | 0.0020238 | Pa×s | 335.00 | Joback Calculated Property |
| η | 0.0009592 | Pa×s | 361.00 | Joback Calculated Property |
| η | 0.0005026 | Pa×s | 387.00 | Joback Calculated Property |
| η | 0.0002857 | Pa×s | 413.00 | Joback Calculated Property |
| η | 0.0001736 | Pa×s | 439.00 | Joback Calculated Property |
| ΔfusH | [10.58; 12.12] | kJ/mol | [312.70; 314.13] |
|
|
T(K) Enthalpy of fusion at a given temperature (kJ/mol) 10.5 11 11.5 12 313 313.5 314 | ||||
| ΔfusH | 10.58 | kJ/mol | 312.70 | NIST |
| ΔfusH | 11.51 | kJ/mol | 314.00 | NIST |
| ΔfusH | 11.51 | kJ/mol | 314.00 | NIST |
| ΔfusH | 11.51 | kJ/mol | 314.06 | NIST |
| ΔfusH | 12.12 | kJ/mol | 314.13 | NIST |
| ΔsubH | [65.30; 68.70] | kJ/mol | [280.50; 297.50] |
|
|
T(K) Enthalpy of sublimation at a given temperature (kJ/mol) 65 66 67 68 69 285 290 295 | ||||
| ΔsubH | 65.30 ± 3.30 | kJ/mol | 280.50 | NIST |
| ΔsubH | 68.10 | kJ/mol | 291.50 | NIST |
| ΔsubH | 67.80 | kJ/mol | 291.50 | NIST |
| ΔsubH | 68.20 | kJ/mol | 293.00 | NIST |
| ΔsubH | 68.70 ± 0.50 | kJ/mol | 297.50 | NIST |
| ΔvapH | [43.80; 57.40] | kJ/mol | [354.50; 572.50] |
|
|
T(K) Enthalpy of vaporization at a given temperature (kJ/mol) 44 46 48 50 52 54 56 58 400 500 | ||||
| ΔvapH | 57.40 | kJ/mol | 354.50 | NIST |
| ΔvapH | 53.20 | kJ/mol | 377.00 | NIST |
| ΔvapH | 51.40 | kJ/mol | 417.50 | NIST |
| ΔvapH | 50.90 | kJ/mol | 421.50 | NIST |
| ΔvapH | 51.30 | kJ/mol | 428.00 | NIST |
| ΔvapH | 48.10 | kJ/mol | 434.00 | NIST |
| ΔvapH | 45.61 | kJ/mol | 454.90 | KDB |
| ΔvapH | 46.80 | kJ/mol | 487.50 | NIST |
| ΔvapH | 49.50 | kJ/mol | 555.00 | NIST |
| ΔvapH | 43.80 | kJ/mol | 572.50 | NIST |
| Pvap | [2.04; 53.23] | kPa | [353.15; 433.15] |
|
|
T(K) Vapor pressure (kPa) 0 10 20 30 40 50 360 380 400 420 | ||||
| Pvap | 2.04 | kPa | 353.15 | Vapor-L... |
| Pvap | 5.51 | kPa | 373.10 | Vapor-L... |
| Pvap | 5.53 | kPa | 373.10 | Vapor-L... |
| Pvap | 5.54 | kPa | 373.15 | Vapor-L... |
| Pvap | 13.15 | kPa | 393.15 | Vapor-L... |
| Pvap | 39.18 | kPa | 423.15 | Vapor-L... |
| Pvap | 53.23 | kPa | 433.15 | Vapor-L... |
| n0 | 1.54050 | 314.15 | Liquid-... | |
| ρl | [1032.40; 1061.00] | kg/m3 | [298.15; 343.15] |
|
|
T(K) Liquid Density (kg/m3) 1030 1035 1040 1045 1050 1055 1060 300 320 340 | ||||
| ρl | 1058.51 | kg/m3 | 298.15 | Ternary... |
| ρl | 1059.00 | kg/m3 | 313.00 | KDB |
| ρl | 1058.30 | kg/m3 | 313.15 | Liquid-... |
| ρl | 1058.30 | kg/m3 | 313.15 | Vapor-L... |
| ρl | 1058.30 | kg/m3 | 313.15 | Liquid-... |
| ρl | 1058.51 | kg/m3 | 313.15 | Liquid ... |
| ρl | 1061.00 | kg/m3 | 314.45 | Liquid ... |
| ρl | 1058.10 | kg/m3 | 314.50 | Ternary... |
| ρl | 1054.10 | kg/m3 | 318.15 | Experim... |
| ρl | 1049.81 | kg/m3 | 323.15 | Experim... |
| ρl | 1045.50 | kg/m3 | 328.15 | Experim... |
| ρl | 1041.16 | kg/m3 | 333.15 | Experim... |
| ρl | 1036.79 | kg/m3 | 338.15 | Experim... |
| ρl | 1032.40 | kg/m3 | 343.15 | Experim... |
| ΔfusS | [33.30; 36.66] | J/mol×K | [312.70; 314.06] |
|
| ΔfusS | 33.80 | J/mol×K | 312.70 | NIST |
| ΔfusS | 33.30 | J/mol×K | 314.00 | NIST |
| ΔfusS | 36.66 | J/mol×K | 314.06 | NIST |
| γ | 0.03 | N/m | 373.20 | KDB |
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [0.14; 202.67] | kPa | [314.06; 481.13] |
The Yaw...
|
| Equation | ln(Pvp) = A + B/(T + C) | |||
| 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 | |||
|
T(K) Vapor pressure (kPa) 0 50 100 150 200 350 400 450 | ||||
| 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 | [0.20; 6095.48] | kPa | [314.06; 694.25] |
KDB Vap...
|
| Equation | ln(Pvp) = A + B/T + C*ln(T) + D*T^2 | |||
| Coefficient A | 9.32745e+01 | |||
| Coefficient B | -1.00030e+04 | |||
| Coefficient C | -1.10400e+01 | |||
| Coefficient D | 4.31995e-06 | |||
| Temperature range, min. | 314.06 | |||
| Temperature range, max. | 694.25 | |||
|
T(K) Vapor pressure (kPa) 0 1000 2000 3000 4000 5000 6000 400 500 600 700 | ||||
| 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 |
Similar Compounds
![3-Hydroxybenz[a]anthracene.](data:image/png;base64,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)
Find more compounds similar to Phenol.
Mixtures
- 2-Pyrrolidinone, 1-methyl- + Phenol
- Carbonic acid, methyl phenyl ester + Phenol
- Methyl Alcohol + Phenol + Water
- Phenol + Water
- Carbonic acid, dimethyl ester + Phenol
- Anisole + Phenol
- Choline chloride + Phenol
- Isopropyl acetate + Phenol + Water
- 1-Octanol + Phenol
- Cyclohexanone + Phenol + Water
- 1-Octanol + Phenol + Water
- 1-Hexanol, 2-ethyl- + Phenol + Water
- Isobutyl acetate + Phenol + Water
- Eucalyptol + Phenol + Water
- 2-Hexanone + Phenol + Water
- Benzene, (1-methylethyl)- + Phenol + Water
- Benzenemethanol, «alpha»-methyl- + Phenol
- Acetophenone + Phenol
- Benzeneacetaldehyde, «alpha»-methyl- + Phenol
- Toluene + Phenol + Water
Find more mixtures with Phenol.
Sources
- KDB Pure (Korean Thermophysical Properties Databank)
- KDB Vapor Pressure Data
- 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
- 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
- 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
- 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
- Joback Method
- KDB
- Aqueous Solubility Prediction Method
- Estimated Solubility Method
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
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