- InChI
- InChI=1S/C8H10/c1-7-3-5-8(2)6-4-7/h3-6H,1-2H3
- InChI Key
- URLKBWYHVLBVBO-UHFFFAOYSA-N
- Formula
- C8H10
- SMILES
- Cc1ccc(C)cc1
- Molecular Weight1
- 106.17
- CAS
- 106-42-3
- Other Names
-
- 1,4-dimethyl-benzene ( p-xylene)
- 1,4-dimethylbenzene
- 1,4-xylene
- 4-Methyltoluene
- Benzene, 1,4-dimethyl-
- Chromar
- NSC 72419
- Scintillar
- p-Dimethylbenzene
- p-Methyltoluene
- p-Xylol
- para-xylene
- ω : Acentric Factor.
- PAff : Proton affinity (kJ/mol).
- Tig : Autoignition Temperature (K).
- BasG : Gas basicity (kJ/mol).
- 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).
- EA : Electron affinity (eV).
- SProt : Protonation entropy at 298K (J/mol×K).
- εr : Dielectric Constant (Relative permittivity).
- LFL : Lower Flammability Limit (% in Air).
- UFL : Upper Flammability Limit (% in Air).
- Tflash,cc : Flash Point (Closed Cup Method) (K).
- Tflash,oc : Flash Point (Open Cup Method) (K).
- ΔfG° : Standard Gibbs free energy of formation (kJ/mol).
- Rg : Radius of Gyration.
- Δc,grossH : Heat of Combustion, Gross form (kJ/mol).
- Δc,netH : Heat of Combustion, Net Form (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.
- NFPA Safety : NFPA Safety Rating.
- Pc : Critical Pressure (kPa).
- Ptriple : Triple Point Pressure (kPa).
- Pvap : Vapor pressure (kPa).
- n0 : Refractive Index.
- ρc : Critical density (kg/m3).
- 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).
- S°liquid : Liquid phase molar entropy at standard conditions (J/mol×K).
- csound,fluid : Speed of sound in fluid (m/s).
- γ : Surface Tension (N/m).
- 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).
- Tfus(P) : Melting point (K).
- Ttriple : Triple Point Temperature (K).
- UQi : UNIQUAC Qi Parameter.
- URi : UNIQUAC Ri Parameter.
- Vc : Critical Volume (m3/kmol).
- VCOSTALD : COSTALD Characteristic Volume (m3/kmol).
- ωSRK : SRK acentric factor.
- Zc : Critical Compressibility.
- Zra : Rackett Parameter.
- 1: Molecular weight from the IUPAC atomic weights tables.
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Contents
- Physical Properties
- Temperature Dependent Properties
- Pressure Dependent Properties
- Datasets
- Correlations
- Similar Compounds
- Mixtures
- Sources
Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ω | [0.3200; 0.3243] |
|
|
| ω | 0.3240 | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value | |
| ω | 0.3243 | Passut and Danner (1973), critical constants and acentric factors Compiled value | |
| ω | 0.3220 | ChemSep v8.3 pure component data Compiled value | |
| ω | 0.3200 | KDB | |
| PAff | [790.50; 794.40] | kJ/mol |
|
| PAff | 794.40 | kJ/mol | NIST |
| PAff | 793.70 | kJ/mol | NIST |
| PAff | 790.50 ± 1.10 | kJ/mol | NIST |
| Tig | [738.71; 801.15] | K |
|
| Tig | 738.71 | K | KDB |
| Tig | 801.15 | K | NCMS SOLV-DB |
| BasG | [766.80; 771.30] | kJ/mol |
|
| BasG | 766.80 | kJ/mol | NIST |
| BasG | 766.90 | kJ/mol | NIST |
| BasG | 771.30 ± 1.40 | kJ/mol | NIST |
| ΔcH°liquid | [-4565.90; -4551.44] | kJ/mol |
|
| ΔcH°liquid | -4551.44 ± 0.50 | kJ/mol | NIST |
| ΔcH°liquid | -4552.86 ± 0.92 | kJ/mol | NIST |
| ΔcH°liquid | -4551.70 | kJ/mol | NIST |
| ΔcH°liquid | -4565.90 | kJ/mol | NIST |
| Cp,liquid | 181.73 | J/mol×K | Thermodynamics of mixtures involving some (benzene derivatives + benzonitrile) |
| μ | [0.00; 0.10] | debye |
|
| μ | 0.00 | debye | ChemSep v8.3 pure component data Compiled value |
| μ | 0.10 | debye | KDB |
| η | [0.0006090; 0.0006090] | Pa×s |
|
| η | 0.0006090 | Pa×s | Viscosities, Densities, and Speeds of Sound of Binary Mixtures of o-Xylene, m-Xylene, p-Xylene, and Isopropylbenzene with 2-Butanone at 298.15 K |
| η | 0.0006090 | Pa×s | Viscosities, Densities, and Speeds of Sound of Binary Mixtures of o-Xylene, m-Xylene, p-Xylene, and Isopropylbenzene with 4-Methylpentan-2-one at 298.15 K |
| EA | 0.00 ± 0.00 | eV | NIST |
| SProt | 44.20 | J/mol×K | NIST |
| εr | 2.27 | NCMS SOLV-DB | |
| LFL | 1.10 | % in Air | KDB |
| UFL | 6.60 | % in Air | KDB |
| Tflash,cc | 298.15 | K | NCMS SOLV-DB |
| Tflash,oc | 300.37 | K | KDB |
| ΔfG° | [121.20; 121.40] | kJ/mol |
|
| ΔfG° | 121.40 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfG° | 121.20 | kJ/mol | KDB |
| Rg | 3.7960 | KDB | |
| Δc,grossH | 4552.86 | kJ/mol | KDB |
| Δc,netH | 4332.784 | kJ/mol | KDB |
| ΔfH°gas | [17.90; 18.03] | kJ/mol |
|
| ΔfH°gas | 18.03 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | 17.96 | kJ/mol | KDB |
| ΔfH°gas | 17.90 ± 1.00 | kJ/mol | NIST |
| ΔfH°liquid | -24.40 ± 1.00 | kJ/mol | NIST |
| ΔfusH° | 10.13 | kJ/mol | Joback Calculated Property |
| ΔvapH° | [35.90; 43.00] | kJ/mol |
|
| ΔvapH° | 42.38 | kJ/mol | NCMS SOLV-DB |
| ΔvapH° | 42.42 | kJ/mol | NIST |
| ΔvapH° | 42.30 | kJ/mol | NIST |
| ΔvapH° | 43.00 ± 0.10 | kJ/mol | NIST |
| ΔvapH° | 42.35 ± 0.10 | kJ/mol | NIST |
| ΔvapH° | 42.30 ± 0.01 | kJ/mol | NIST |
| ΔvapH° | 42.30 ± 0.10 | kJ/mol | NIST |
| ΔvapH° | 42.60 | kJ/mol | NIST |
| ΔvapH° | 42.40 | kJ/mol | NIST |
| ΔvapH° | 42.72 | kJ/mol | NIST |
| ΔvapH° | Outlier 35.90 | kJ/mol | NIST |
| ΔvapH° | 42.40 ± 0.10 | kJ/mol | NIST |
| ΔvapH° | 42.37 | kJ/mol | NIST |
| ΔvapH° | 42.30 | kJ/mol | NIST |
| ΔvapH° | Outlier 36.00 ± 0.08 | kJ/mol | NIST |
| IE | [8.37; 8.80] | eV |
|
| IE | 8.44 ± 0.05 | eV | NIST |
| IE | 8.52 ± 0.01 | eV | NIST |
| IE | 8.44 | eV | NIST |
| IE | Outlier 8.80 ± 0.05 | eV | NIST |
| IE | 8.37 ± 0.02 | eV | NIST |
| IE | 8.52 | eV | NIST |
| IE | 8.45 | eV | NIST |
| IE | 8.44 ± 0.02 | eV | NIST |
| IE | 8.45 ± 0.01 | eV | NIST |
| IE | 8.48 | eV | NIST |
| IE | 8.44 | eV | NIST |
| IE | 8.43 | eV | NIST |
| IE | 8.60 ± 0.03 | eV | NIST |
| log10WS | [-2.77; -2.77] |
|
|
| log10WS | -2.77 | Aq. Solubility Prediction | |
| log10WS | -2.77 | Estimated Solubility | |
| logPoct/wat | 3.150 | NCMS SOLV-DB | |
| McVol | 99.820 | ml/mol | McGowan Calculated Property |
| NFPA Fire | [%!d(float64=3); %!d(float64=3)] |
|
|
| NFPA Fire | 3 | KDB | |
| NFPA Fire | 3 | NCMS SOLV-DB | |
| NFPA Health | [%!d(float64=2); %!d(float64=2)] |
|
|
| NFPA Health | 2 | KDB | |
| NFPA Health | 2 | NCMS SOLV-DB | |
| NFPA Safety | 0 | NCMS SOLV-DB | |
| Pc | [3343.73; 3617.50] | kPa |
|
| Pc | 3511.00 | kPa | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 3 Compiled value |
| Pc | 3515.98 | kPa | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Pc | 3510.81 | kPa | Passut and Danner (1973), critical constants and acentric factors Compiled value |
| Pc | 3511.00 | kPa | ChemSep v8.3 pure component data Compiled value |
| Pc | 3511.00 | kPa | KDB |
| Pc | 3510.00 ± 20.00 | kPa | NIST |
| Pc | 3510.70 ± 5.00 | kPa | NIST |
| Pc | 3617.50 ± 100.00 | kPa | NIST |
| Pc | 3511.00 ± 0.01 | kPa | NIST |
| Pc | Outlier 3343.73 ± 151.99 | kPa | NIST |
| Pc | 3430.00 ± 7.84 | kPa | NIST |
| Ptriple | 0.58 | kPa | ChemSep v8.3 pure component data Compiled value |
| ρc | [280.70; 282.51] | kg/m3 |
|
| ρc | 281.34 ± 2.12 | kg/m3 | NIST |
| ρc | 282.51 ± 5.31 | kg/m3 | NIST |
| ρc | 280.70 ± 4.25 | kg/m3 | NIST |
| Inp | [120.40; 908.00] |
|
|
| Inp | 859.00 | NIST | |
| Inp | 848.40 | NIST | |
| Inp | 855.20 | NIST | |
| Inp | 852.10 | NIST | |
| Inp | 850.50 | NIST | |
| Inp | 852.30 | NIST | |
| Inp | 856.70 | NIST | |
| Inp | 883.20 | NIST | |
| Inp | 888.10 | NIST | |
| Inp | 874.28 | NIST | |
| Inp | 847.60 | NIST | |
| Inp | 850.20 | NIST | |
| Inp | 852.70 | NIST | |
| Inp | 855.30 | NIST | |
| Inp | 857.80 | NIST | |
| Inp | 860.90 | NIST | |
| Inp | 863.50 | NIST | |
| Inp | 857.70 | NIST | |
| Inp | 867.50 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 863.30 | NIST | |
| Inp | 871.20 | NIST | |
| Inp | 857.10 | NIST | |
| Inp | 857.00 | NIST | |
| Inp | 857.40 | NIST | |
| Inp | 857.60 | NIST | |
| Inp | 856.90 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 857.00 | NIST | |
| Inp | 857.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 856.00 | NIST | |
| Inp | 866.80 | NIST | |
| Inp | 871.30 | NIST | |
| Inp | 866.70 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 854.20 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 849.10 | NIST | |
| Inp | 854.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 856.00 | NIST | |
| Inp | 879.00 | NIST | |
| Inp | 881.00 | NIST | |
| Inp | 848.00 | NIST | |
| Inp | 853.10 | NIST | |
| Inp | 871.00 | NIST | |
| Inp | 890.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 862.00 | NIST | |
| Inp | 886.00 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 848.00 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 880.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 862.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 857.10 | NIST | |
| Inp | 857.60 | NIST | |
| Inp | 860.80 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 861.20 | NIST | |
| Inp | 867.70 | NIST | |
| Inp | 872.50 | NIST | |
| Inp | 878.30 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 860.30 | NIST | |
| Inp | 854.20 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 848.30 | NIST | |
| Inp | 853.40 | NIST | |
| Inp | 858.40 | NIST | |
| Inp | 858.60 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 859.30 | NIST | |
| Inp | 854.10 | NIST | |
| Inp | 854.60 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 861.20 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 855.73 | NIST | |
| Inp | 882.00 | NIST | |
| Inp | 886.00 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 849.00 | NIST | |
| Inp | 854.00 | NIST | |
| Inp | 857.80 | NIST | |
| Inp | 861.80 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 850.00 | NIST | |
| Inp | 908.00 | NIST | |
| Inp | 858.10 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 865.50 | NIST | |
| Inp | 864.90 | NIST | |
| Inp | 858.10 | NIST | |
| Inp | 894.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 850.00 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 894.00 | NIST | |
| Inp | 901.00 | NIST | |
| Inp | 907.00 | NIST | |
| Inp | 888.00 | NIST | |
| Inp | 862.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 885.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 889.20 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 877.00 | NIST | |
| Inp | 874.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 862.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 860.40 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 847.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 861.70 | NIST | |
| Inp | 864.40 | NIST | |
| Inp | 866.50 | NIST | |
| Inp | 849.30 | NIST | |
| Inp | 877.80 | NIST | |
| Inp | 869.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 852.00 | NIST | |
| Inp | 856.30 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 873.00 | NIST | |
| Inp | 845.70 | NIST | |
| Inp | 851.30 | NIST | |
| Inp | 855.50 | NIST | |
| Inp | 855.40 | NIST | |
| Inp | 869.30 | NIST | |
| Inp | 861.70 | NIST | |
| Inp | 864.40 | NIST | |
| Inp | 866.50 | NIST | |
| Inp | 853.96 | NIST | |
| Inp | 854.41 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 854.75 | NIST | |
| Inp | 854.85 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 855.12 | NIST | |
| Inp | 859.70 | NIST | |
| Inp | 856.00 | NIST | |
| Inp | 854.30 | NIST | |
| Inp | 861.80 | NIST | |
| Inp | 853.70 | NIST | |
| Inp | 859.80 | NIST | |
| Inp | 864.70 | NIST | |
| Inp | 855.90 | NIST | |
| Inp | 860.80 | NIST | |
| Inp | 866.94 | NIST | |
| Inp | 842.00 | NIST | |
| Inp | 851.35 | NIST | |
| Inp | 854.04 | NIST | |
| Inp | 855.80 | NIST | |
| Inp | 865.82 | NIST | |
| Inp | 868.78 | NIST | |
| Inp | 870.79 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 871.00 | NIST | |
| Inp | 862.00 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 888.00 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 879.49 | NIST | |
| Inp | 854.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 856.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 852.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 845.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 854.00 | NIST | |
| Inp | 857.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 850.00 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 890.00 | NIST | |
| Inp | 874.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 862.00 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 899.00 | NIST | |
| Inp | 856.00 | NIST | |
| Inp | 874.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 854.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 856.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 849.00 | NIST | |
| Inp | 848.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 883.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 857.41 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 857.00 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 875.80 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 854.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 849.00 | NIST | |
| Inp | 852.00 | NIST | |
| Inp | 851.00 | NIST | |
| Inp | 848.00 | NIST | |
| Inp | 859.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 853.80 | NIST | |
| Inp | 847.70 | NIST | |
| Inp | 854.00 | NIST | |
| Inp | 855.10 | NIST | |
| Inp | 854.90 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 849.30 | NIST | |
| Inp | 851.50 | NIST | |
| Inp | 854.70 | NIST | |
| Inp | 857.10 | NIST | |
| Inp | 859.10 | NIST | |
| Inp | 848.00 | NIST | |
| Inp | 851.00 | NIST | |
| Inp | 854.00 | NIST | |
| Inp | 856.00 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 851.00 | NIST | |
| Inp | 852.00 | NIST | |
| Inp | 854.00 | NIST | |
| Inp | 832.00 | NIST | |
| Inp | 862.00 | NIST | |
| Inp | 881.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 889.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 888.00 | NIST | |
| Inp | 848.46 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 857.00 | NIST | |
| Inp | 878.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 844.00 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 904.00 | NIST | |
| Inp | 873.00 | NIST | |
| Inp | 875.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 867.00 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 865.60 | NIST | |
| Inp | 871.80 | NIST | |
| Inp | 871.30 | NIST | |
| Inp | 870.70 | NIST | |
| Inp | 861.90 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 846.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 860.00 | NIST | |
| Inp | 874.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | Outlier 120.40 | NIST | |
| Inp | Outlier 120.40 | NIST | |
| Inp | Outlier 121.20 | NIST | |
| Inp | Outlier 136.39 | NIST | |
| Inp | 862.00 | NIST | |
| Inp | 872.00 | NIST | |
| Inp | 876.00 | NIST | |
| Inp | 884.00 | NIST | |
| Inp | 849.00 | NIST | |
| Inp | 865.00 | NIST | |
| Inp | 852.00 | NIST | |
| Inp | 853.00 | NIST | |
| Inp | 854.90 | NIST | |
| Inp | 851.50 | NIST | |
| Inp | 851.00 | NIST | |
| Inp | 863.00 | NIST | |
| Inp | 861.00 | NIST | |
| Inp | 885.00 | NIST | |
| Inp | 868.00 | NIST | |
| Inp | 845.00 | NIST | |
| Inp | 864.00 | NIST | |
| Inp | 870.00 | NIST | |
| Inp | 877.00 | NIST | |
| Inp | 877.80 | NIST | |
| Inp | 856.30 | NIST | |
| Inp | 855.50 | NIST | |
| Inp | 866.50 | NIST | |
| Inp | 854.75 | NIST | |
| Inp | 859.70 | NIST | |
| Inp | 859.80 | NIST | |
| Inp | 842.00 | NIST | |
| Inp | 868.78 | NIST | |
| Inp | 889.00 | NIST | |
| Inp | 866.00 | NIST | |
| Inp | 857.00 | NIST | |
| Inp | 855.00 | NIST | |
| Inp | 871.30 | NIST | |
| Inp | 858.00 | NIST | |
| Inp | 879.49 | NIST | |
| Inp | Outlier 120.40 | NIST | |
| Ip | [1101.00; 1189.00] |
|
|
| Ip | 1169.50 | NIST | |
| Ip | Outlier 1180.40 | NIST | |
| Ip | 1123.00 | NIST | |
| Ip | 1123.00 | NIST | |
| Ip | 1145.00 | NIST | |
| Ip | 1159.94 | NIST | |
| Ip | 1165.00 | NIST | |
| Ip | 1169.77 | NIST | |
| Ip | 1145.24 | NIST | |
| Ip | 1149.89 | NIST | |
| Ip | 1152.22 | NIST | |
| Ip | 1138.90 | NIST | |
| Ip | 1143.00 | NIST | |
| Ip | 1169.20 | NIST | |
| Ip | 1134.80 | NIST | |
| Ip | 1118.60 | NIST | |
| Ip | Outlier 1189.00 | NIST | |
| Ip | Outlier 1182.00 | NIST | |
| Ip | 1163.00 | NIST | |
| Ip | 1170.00 | NIST | |
| Ip | Outlier 1178.00 | NIST | |
| Ip | 1156.00 | NIST | |
| Ip | 1136.00 | NIST | |
| Ip | 1142.00 | NIST | |
| Ip | Outlier 1180.00 | NIST | |
| Ip | 1129.00 | NIST | |
| Ip | 1134.00 | NIST | |
| Ip | 1142.00 | NIST | |
| Ip | 1154.20 | NIST | |
| Ip | 1117.00 | NIST | |
| Ip | 1137.00 | NIST | |
| Ip | 1137.00 | NIST | |
| Ip | 1117.00 | NIST | |
| Ip | 1164.00 | NIST | |
| Ip | 1139.00 | NIST | |
| Ip | 1123.00 | NIST | |
| Ip | 1123.00 | NIST | |
| Ip | 1137.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1136.00 | NIST | |
| Ip | 1130.00 | NIST | |
| Ip | 1130.00 | NIST | |
| Ip | 1156.00 | NIST | |
| Ip | 1134.00 | NIST | |
| Ip | 1136.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1135.00 | NIST | |
| Ip | 1140.00 | NIST | |
| Ip | 1119.00 | NIST | |
| Ip | 1136.00 | NIST | |
| Ip | 1119.00 | NIST | |
| Ip | 1119.00 | NIST | |
| Ip | 1137.00 | NIST | |
| Ip | 1140.00 | NIST | |
| Ip | 1126.00 | NIST | |
| Ip | 1129.00 | NIST | |
| Ip | 1156.50 | NIST | |
| Ip | 1141.30 | NIST | |
| Ip | 1150.60 | NIST | |
| Ip | 1117.00 | NIST | |
| Ip | 1153.20 | NIST | |
| Ip | 1143.40 | NIST | |
| Ip | 1146.00 | NIST | |
| Ip | 1143.90 | NIST | |
| Ip | 1148.70 | NIST | |
| Ip | 1130.00 | NIST | |
| Ip | 1127.00 | NIST | |
| Ip | 1129.00 | NIST | |
| Ip | 1130.00 | NIST | |
| Ip | 1130.00 | NIST | |
| Ip | 1125.00 | NIST | |
| Ip | 1120.00 | NIST | |
| Ip | 1152.00 | NIST | |
| Ip | 1137.00 | NIST | |
| Ip | 1140.00 | NIST | |
| Ip | 1140.00 | NIST | |
| Ip | 1165.00 | NIST | |
| Ip | Outlier 1176.00 | NIST | |
| Ip | 1142.00 | NIST | |
| Ip | 1153.00 | NIST | |
| Ip | 1155.00 | NIST | |
| Ip | 1150.00 | NIST | |
| Ip | 1154.00 | NIST | |
| Ip | 1168.00 | NIST | |
| Ip | Outlier 1178.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1141.00 | NIST | |
| Ip | 1119.00 | NIST | |
| Ip | 1136.00 | NIST | |
| Ip | Outlier 1101.00 | NIST | |
| Ip | 1154.00 | NIST | |
| Ip | 1114.00 | NIST | |
| Ip | 1137.00 | NIST | |
| Ip | 1149.00 | NIST | |
| Ip | 1111.00 | NIST | |
| Ip | 1140.00 | NIST | |
| Ip | 1113.00 | NIST | |
| Ip | 1149.00 | NIST | |
| Ip | 1129.00 | NIST | |
| Ip | 1129.00 | NIST | |
| Ip | 1133.00 | NIST | |
| Ip | 1129.00 | NIST | |
| Ip | 1164.00 | NIST | |
| Ip | 1146.00 | NIST | |
| Ip | 1142.00 | NIST | |
| Ip | 1131.00 | NIST | |
| Ip | 1138.00 | NIST | |
| Ip | 1133.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1115.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1140.00 | NIST | |
| Ip | 1153.00 | NIST | |
| Ip | 1164.00 | NIST | |
| Ip | 1138.00 | NIST | |
| Ip | 1142.00 | NIST | |
| Ip | 1173.00 | NIST | |
| Ip | 1137.00 | NIST | |
| Ip | 1127.00 | NIST | |
| Ip | 1129.00 | NIST | |
| Ip | 1120.00 | NIST | |
| Ip | 1120.00 | NIST | |
| Ip | 1142.00 | NIST | |
| Ip | 1123.00 | NIST | |
| Ip | 1140.00 | NIST | |
| Ip | 1139.00 | NIST | |
| Ip | 1137.00 | NIST | |
| Ip | 1119.00 | NIST | |
| Ip | 1145.00 | NIST | |
| Ip | 1155.00 | NIST | |
| Ip | 1139.00 | NIST | |
| Ip | 1132.00 | NIST | |
| Ip | 1138.00 | NIST | |
| Ip | 1155.00 | NIST | |
| Ip | 1110.00 | NIST | |
| Ip | 1126.00 | NIST | |
| Ip | 1140.00 | NIST | |
| Ip | 1140.00 | NIST | |
| Ip | 1150.00 | NIST | |
| Ip | 1136.00 | NIST | |
| Ip | 1169.50 | NIST | |
| Ip | 1159.94 | NIST | |
| Ip | 1152.22 | NIST | |
| Ip | 1118.60 | NIST | |
| Ip | Outlier 1178.00 | NIST | |
| Ip | 1165.00 | NIST | |
| Ip | 1150.00 | NIST | |
| Ip | 1141.00 | NIST | |
| S°liquid | [243.51; 253.10] | J/mol×K |
|
| S°liquid | 247.15 | J/mol×K | NIST |
| S°liquid | 243.51 | J/mol×K | NIST |
| S°liquid | 253.10 | J/mol×K | NIST |
| Tboil | [409.00; 412.70] | K |
|
| Tboil | 411.40 | K | Isobaric vapor-liquid equilibrium for the binary mixtures of nonane with cyclohexane, toluene, m-xylene, or p-xylene at 101.3 kPa |
| Tboil | 411.45 | K | Separation of azeotrope (2,2,3,3-tetrafluoro-1-propanol + water): Isobaric vapour-liquid phase equilibrium measurements and azeotropic distillation |
| Tboil | 411.45 | K | Vapour-liquid equilibrium measurements and extractive distillation process design for separation of azeotropic mixture (dimethyl carbonate + ethanol) |
| Tboil | 411.21 | K | Investigation on Thermodynamics in Separation for Ethylene Glycol + Neopentyl Glycol System by Azeotropic Distillation |
| Tboil | 411.49 | K | Isobaric Vapor-Liquid Equilibrium Measurements for Separation of Azeotrope (Methanol + Methyl Acetate) |
| Tboil | 411.23 | K | Isobaric Vapor-Liquid Equilibria for Binary and Ternary Mixtures of Ethanol, Methylcyclohexane and p-Xylene |
| Tboil | 411.37 | K | Isobaric Vapor-Liquid Equilibium for the Binary Systems of Methyl Formate with o-Xylene, m-Xylene, p-Xylene, and Ethylbenzene at 101.33 kPa |
| Tboil | 411.53 | K | ChemSep v8.3 pure component data Compiled value |
| Tboil | 411.52 | K | KDB |
| Tboil | 411.51 | K | NCMS SOLV-DB |
| Tboil | 411.15 ± 0.20 | K | NIST |
| Tboil | 411.35 ± 0.20 | K | NIST |
| Tboil | 411.50 | K | NIST |
| Tboil | 411.35 ± 0.20 | K | NIST |
| Tboil | 410.65 ± 0.50 | K | NIST |
| Tboil | 411.55 ± 0.30 | K | NIST |
| Tboil | 410.65 ± 0.40 | K | NIST |
| Tboil | 411.50 | K | NIST |
| Tboil | 411.45 ± 0.20 | K | NIST |
| Tboil | 411.45 ± 0.20 | K | NIST |
| Tboil | 411.60 ± 0.30 | K | NIST |
| Tboil | 411.35 ± 0.15 | K | NIST |
| Tboil | 411.36 ± 0.30 | K | NIST |
| Tboil | 411.52 ± 0.20 | K | NIST |
| Tboil | 411.60 ± 0.20 | K | NIST |
| Tboil | 411.53 ± 0.15 | K | NIST |
| Tboil | 411.60 ± 0.10 | K | NIST |
| Tboil | 411.69 ± 0.01 | K | NIST |
| Tboil | 411.30 ± 0.80 | K | NIST |
| Tboil | 411.50 ± 0.30 | K | NIST |
| Tboil | 411.50 ± 0.30 | K | NIST |
| Tboil | Outlier 409.00 ± 1.50 | K | NIST |
| Tboil | 412.00 ± 3.00 | K | NIST |
| Tboil | Outlier 412.70 ± 2.00 | K | NIST |
| Tboil | 411.00 ± 2.00 | K | NIST |
| Tboil | Outlier 409.90 ± 2.00 | K | NIST |
| Tboil | 411.20 ± 0.50 | K | NIST |
| Tboil | 411.50 ± 0.20 | K | NIST |
| Tboil | 411.60 ± 0.50 | K | NIST |
| Tboil | 411.50 ± 0.02 | K | NIST |
| Tboil | 411.00 ± 0.50 | K | NIST |
| Tboil | 411.00 ± 2.00 | K | NIST |
| Tboil | 411.55 ± 0.30 | K | NIST |
| Tboil | 411.50 ± 0.20 | K | NIST |
| Tboil | 411.50 ± 0.20 | K | NIST |
| Tboil | 411.49 ± 0.01 | K | NIST |
| Tboil | 412.01 ± 0.20 | K | NIST |
| Tboil | 411.20 ± 0.50 | K | NIST |
| Tboil | 411.55 ± 1.00 | K | NIST |
| Tboil | 411.50 ± 0.20 | K | NIST |
| Tboil | 411.15 ± 0.50 | K | NIST |
| Tboil | 411.50 ± 0.05 | K | NIST |
| Tboil | 411.50 ± 0.02 | K | NIST |
| Tboil | 411.70 ± 0.30 | K | NIST |
| Tboil | 411.70 ± 0.50 | K | NIST |
| Tboil | 411.65 ± 0.10 | K | NIST |
| Tboil | 411.50 ± 0.10 | K | NIST |
| Tboil | 411.59 ± 0.20 | K | NIST |
| Tboil | 411.47 ± 0.30 | K | NIST |
| Tboil | 411.55 ± 0.50 | K | NIST |
| Tboil | 411.30 ± 0.40 | K | NIST |
| Tboil | 411.60 ± 0.40 | K | NIST |
| Tboil | 411.55 ± 0.20 | K | NIST |
| Tboil | 411.55 ± 0.30 | K | NIST |
| Tboil | 411.55 ± 0.30 | K | NIST |
| Tboil | Outlier 410.00 ± 5.00 | K | NIST |
| Tboil | Outlier 410.15 ± 2.00 | K | NIST |
| Tboil | 411.50 ± 0.25 | K | NIST |
| Tboil | Outlier 409.00 ± 3.00 | K | NIST |
| Tboil | 411.55 ± 0.30 | K | NIST |
| Tboil | 411.00 ± 3.00 | K | NIST |
| Tboil | 411.00 ± 2.00 | K | NIST |
| Tboil | 410.65 ± 0.50 | K | NIST |
| Tboil | 411.00 ± 2.00 | K | NIST |
| Tboil | 411.30 ± 1.50 | K | NIST |
| Tc | [615.90; 621.70] | K |
|
| Tc | 616.20 | K | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 3 Compiled value |
| Tc | 616.20 | K | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Tc | 616.26 | K | Passut and Danner (1973), critical constants and acentric factors Compiled value |
| Tc | 616.20 | K | ChemSep v8.3 pure component data Compiled value |
| Tc | 616.20 | K | KDB |
| Tc | 616.20 ± 0.20 | K | NIST |
| Tc | 616.23 ± 0.10 | K | NIST |
| Tc | 616.20 | K | NIST |
| Tc | 618.20 ± 2.00 | K | NIST |
| Tc | 616.20 ± 0.61 | K | NIST |
| Tc | 616.20 ± 0.15 | K | NIST |
| Tc | 619.00 ± 3.00 | K | NIST |
| Tc | 617.45 ± 2.00 | K | NIST |
| Tc | 615.90 ± 0.50 | K | NIST |
| Tc | 618.20 ± 2.00 | K | NIST |
| Tc | Outlier 621.70 ± 6.00 | K | NIST |
| Tc | 617.60 ± 1.50 | K | NIST |
| Tfus | [260.15; 288.00] | K |
|
| Tfus | 286.15 | K | Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value |
| Tfus | 286.41 | K | ChemSep v8.3 pure component data Compiled value |
| Tfus | 286.30 | K | KDB |
| Tfus | 285.90 | K | Aq. Solubility Prediction |
| Tfus | 286.41 | K | NCMS SOLV-DB |
| Tfus | 286.36 ± 0.05 | K | NIST |
| Tfus | 286.45 ± 0.15 | K | NIST |
| Tfus | 286.41 ± 0.03 | K | NIST |
| Tfus | 286.38 ± 0.10 | K | NIST |
| Tfus | 286.20 ± 2.00 | K | NIST |
| Tfus | 286.20 ± 2.00 | K | NIST |
| Tfus | 286.53 ± 0.20 | K | NIST |
| Tfus | 286.38 ± 0.30 | K | NIST |
| Tfus | 287.00 ± 3.00 | K | NIST |
| Tfus | 286.30 ± 0.50 | K | NIST |
| Tfus | 286.45 ± 0.20 | K | NIST |
| Tfus | 286.37 ± 0.01 | K | NIST |
| Tfus | 286.43 ± 0.10 | K | NIST |
| Tfus | 286.36 ± 0.05 | K | NIST |
| Tfus | 286.22 ± 0.15 | K | NIST |
| Tfus | 288.00 ± 2.00 | K | NIST |
| Tfus | Outlier 260.15 ± 2.00 | K | NIST |
| Tfus | 286.10 ± 0.60 | K | NIST |
| Tfus | 286.40 ± 0.40 | K | NIST |
| Tfus | 286.35 ± 0.40 | K | NIST |
| Tfus | 286.50 ± 0.20 | K | NIST |
| Tfus | 286.40 ± 0.50 | K | NIST |
| Ttriple | [286.30; 286.41] | K |
|
| Ttriple | 286.41 | K | ChemSep v8.3 pure component data Compiled value |
| Ttriple | 286.40 ± 0.01 | K | NIST |
| Ttriple | 286.30 ± 0.30 | K | NIST |
| Ttriple | 286.40 ± 0.01 | K | NIST |
| Ttriple | 286.30 ± 0.30 | K | NIST |
| UQi | 3.54 | ChemSep v8.3 pure component data Compiled value | |
| URi | 4.66 | ChemSep v8.3 pure component data Compiled value | |
| Vc | [0.378; 0.379] | m3/kmol |
|
| Vc | 0.378 | m3/kmol | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 3 Compiled value |
| Vc | 0.379 | m3/kmol | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Vc | 0.378 | m3/kmol | ChemSep v8.3 pure component data Compiled value |
| Vc | 0.378 | m3/kmol | KDB |
| Vc | 0.378 | m3/kmol | NIST |
| VCOSTALD | 0.37 | m3/kmol | Hankinson and Thomson (1979), COSTALD parameters Compiled value |
| ωSRK | 0.32 | Hankinson and Thomson (1979), COSTALD parameters Compiled value | |
| Zc | [0.2590000; 0.2590380] |
|
|
| Zc | 0.2590000 | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 3 Compiled value | |
| Zc | 0.2590000 | ChemSep v8.3 pure component data Compiled value | |
| Zc | 0.2590380 | KDB | |
| Zra | [0.26; 0.26] |
|
|
| Zra | 0.26 | Hankinson and Thomson (1979), COSTALD parameters Compiled value | |
| Zra | 0.26 | ChemSep v8.3 pure component data Compiled value | |
| Zra | 0.26 | KDB |
Temperature Dependent Properties
Pressure Dependent Properties
| Property | Value | Unit | Pressure (kPa) | Source |
|---|---|---|---|---|
| Tfus(P) | 286.45 | K | 100.00 | Activity coefficient at infinite dilution, azeotropic data, excess enthalpies and solid liquid-equilibria for binary systems of alkanes and aromatics with esters |
Datasets
- Viscosity, Pa*s (2)
- Refractive index (Na D-line) (1)
- Mass density, kg/m3 (2)
- Speed of sound, m/s (1)
Viscosity, Pa*s
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Viscosity, Pa*s - Liquid |
| 293.04 | 100.00 | 0.0006 |
| 293.04 | 1000.00 | 0.0006 |
| 293.04 | 5000.00 | 0.0007 |
| 293.04 | 10000.00 | 0.0007 |
| 293.03 | 15000.00 | 0.0007 |
| 293.03 | 20000.00 | 0.0008 |
| 293.03 | 25000.00 | 0.0008 |
| 293.03 | 30000.00 | 0.0008 |
| 302.86 | 100.00 | 0.0006 |
| 302.86 | 1000.00 | 0.0006 |
| 302.87 | 5000.00 | 0.0006 |
| 302.87 | 10000.00 | 0.0006 |
| 302.88 | 15000.00 | 0.0006 |
| 302.88 | 20000.00 | 0.0007 |
| 302.88 | 25000.00 | 0.0007 |
| 302.89 | 30000.00 | 0.0007 |
| 312.76 | 100.00 | 0.0005 |
| 312.76 | 1000.00 | 0.0005 |
| 312.77 | 5000.00 | 0.0005 |
| 312.77 | 10000.00 | 0.0006 |
| 312.76 | 15000.00 | 0.0006 |
| 312.76 | 20000.00 | 0.0006 |
| 312.76 | 25000.00 | 0.0006 |
| 312.76 | 30000.00 | 0.0006 |
| 322.62 | 100.00 | 0.0005 |
| 322.63 | 1000.00 | 0.0005 |
| 322.64 | 5000.00 | 0.0005 |
| 322.64 | 10000.00 | 0.0005 |
| 322.64 | 15000.00 | 0.0005 |
| 322.64 | 20000.00 | 0.0005 |
| 322.64 | 25000.00 | 0.0006 |
| 322.65 | 30000.00 | 0.0006 |
| 332.58 | 100.00 | 0.0004 |
| 332.58 | 1000.00 | 0.0004 |
| 332.58 | 5000.00 | 0.0004 |
| 332.58 | 10000.00 | 0.0005 |
| 332.58 | 15000.00 | 0.0005 |
| 332.58 | 20000.00 | 0.0005 |
| 332.58 | 25000.00 | 0.0005 |
| 332.57 | 30000.00 | 0.0005 |
| 342.27 | 100.00 | 0.0004 |
| 342.27 | 1000.00 | 0.0004 |
| 342.28 | 5000.00 | 0.0004 |
| 342.28 | 10000.00 | 0.0004 |
| 342.29 | 15000.00 | 0.0004 |
| 342.28 | 20000.00 | 0.0004 |
| 342.29 | 25000.00 | 0.0005 |
| 342.29 | 30000.00 | 0.0005 |
| 352.21 | 100.00 | 0.0003 |
| 352.21 | 1000.00 | 0.0004 |
| 352.20 | 5000.00 | 0.0004 |
| 352.20 | 10000.00 | 0.0004 |
| 352.20 | 15000.00 | 0.0004 |
| 352.20 | 20000.00 | 0.0004 |
| 352.20 | 25000.00 | 0.0004 |
| 352.20 | 30000.00 | 0.0004 |
| 362.73 | 100.00 | 0.0003 |
| 362.74 | 1000.00 | 0.0003 |
| 362.75 | 5000.00 | 0.0003 |
| 362.76 | 10000.00 | 0.0003 |
| 362.76 | 15000.00 | 0.0004 |
| 362.77 | 20000.00 | 0.0004 |
| 362.81 | 25000.00 | 0.0004 |
| 362.82 | 30000.00 | 0.0004 |
| 372.71 | 100.00 | 0.0003 |
| 372.71 | 1000.00 | 0.0003 |
| 372.71 | 5000.00 | 0.0003 |
| 372.70 | 10000.00 | 0.0003 |
| 372.70 | 15000.00 | 0.0003 |
| 372.69 | 20000.00 | 0.0003 |
| 372.69 | 25000.00 | 0.0004 |
| 372.69 | 30000.00 | 0.0004 |
| Reference | ||
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Viscosity, Pa*s - Liquid |
| 313.15 | 100.00 | 0.0005 |
| 313.15 | 800.00 | 0.0005 |
| 313.15 | 1600.00 | 0.0005 |
| 313.15 | 2400.00 | 0.0005 |
| 313.15 | 3200.00 | 0.0005 |
| 333.15 | 100.00 | 0.0004 |
| 333.15 | 800.00 | 0.0004 |
| 333.15 | 1600.00 | 0.0004 |
| 333.15 | 2400.00 | 0.0004 |
| 333.15 | 3200.00 | 0.0004 |
| 353.15 | 100.00 | 0.0003 |
| 353.15 | 800.00 | 0.0003 |
| 353.15 | 1600.00 | 0.0003 |
| 353.15 | 2400.00 | 0.0004 |
| 353.15 | 3200.00 | 0.0004 |
| 373.15 | 100.00 | 0.0003 |
| 373.15 | 800.00 | 0.0003 |
| 373.15 | 1600.00 | 0.0003 |
| 373.15 | 2400.00 | 0.0003 |
| 373.15 | 3200.00 | 0.0003 |
| 393.15 | 800.00 | 0.0003 |
| 393.15 | 1600.00 | 0.0003 |
| 393.15 | 2400.00 | 0.0003 |
| 393.15 | 3200.00 | 0.0003 |
| 413.15 | 800.00 | 0.0002 |
| 413.15 | 1600.00 | 0.0002 |
| 413.15 | 2400.00 | 0.0002 |
| 413.15 | 3200.00 | 0.0002 |
| 433.15 | 800.00 | 0.0002 |
| 433.15 | 1600.00 | 0.0002 |
| 433.15 | 2400.00 | 0.0002 |
| 433.15 | 3200.00 | 0.0002 |
| 453.15 | 800.00 | 0.0002 |
| 453.15 | 1600.00 | 0.0002 |
| 453.15 | 2400.00 | 0.0002 |
| 453.15 | 3200.00 | 0.0002 |
| 473.15 | 1600.00 | 0.0002 |
| 473.15 | 2400.00 | 0.0002 |
| 473.15 | 3200.00 | 0.0002 |
| Reference | ||
Refractive index (Na D-line)
| Fixed | Measured | |
|---|---|---|
| Pressure, kPa - Liquid | Temperature, K - Liquid | Refractive index (Na D-line) - Liquid |
| 93.00 | 298.15 | 1.4929 |
| Reference | ||
Mass density, kg/m3
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 293.15 | 100.00 | 862.7 |
| 293.15 | 1000.00 | 863.3 |
| 293.15 | 3000.00 | 864.7 |
| 293.15 | 5000.00 | 865.9 |
| 293.15 | 10000.00 | 869.6 |
| 293.15 | 15000.00 | 873.0 |
| 293.15 | 20000.00 | 876.3 |
| 293.15 | 25000.00 | 879.6 |
| 303.15 | 100.00 | 852.9 |
| 303.15 | 1000.00 | 853.8 |
| 303.15 | 3000.00 | 855.3 |
| 303.15 | 5000.00 | 856.9 |
| 303.15 | 10000.00 | 860.6 |
| 303.15 | 15000.00 | 864.3 |
| 303.15 | 20000.00 | 867.6 |
| 303.15 | 25000.00 | 871.0 |
| 303.15 | 30000.00 | 874.3 |
| 303.15 | 35000.00 | 877.4 |
| 303.15 | 40000.00 | 880.3 |
| 303.15 | 50000.00 | 886.3 |
| 303.15 | 60000.00 | 892.5 |
| 313.15 | 100.00 | 843.6 |
| 313.15 | 1000.00 | 844.7 |
| 313.15 | 3000.00 | 846.5 |
| 313.15 | 5000.00 | 848.1 |
| 313.15 | 10000.00 | 852.0 |
| 313.15 | 15000.00 | 855.8 |
| 313.15 | 20000.00 | 859.5 |
| 313.15 | 25000.00 | 863.0 |
| 313.15 | 30000.00 | 866.4 |
| 313.15 | 35000.00 | 869.6 |
| 313.15 | 40000.00 | 872.8 |
| 313.15 | 50000.00 | 879.1 |
| 313.15 | 60000.00 | 884.5 |
| 323.15 | 100.00 | 835.7 |
| 323.15 | 1000.00 | 836.7 |
| 323.15 | 3000.00 | 838.5 |
| 323.15 | 5000.00 | 840.2 |
| 323.15 | 10000.00 | 844.5 |
| 323.15 | 15000.00 | 848.4 |
| 323.15 | 20000.00 | 852.3 |
| 323.15 | 25000.00 | 855.7 |
| 323.15 | 30000.00 | 859.2 |
| 323.15 | 35000.00 | 862.6 |
| 323.15 | 40000.00 | 866.1 |
| 323.15 | 50000.00 | 872.8 |
| 323.15 | 60000.00 | 878.1 |
| 333.15 | 100.00 | 827.0 |
| 333.15 | 1000.00 | 827.8 |
| 333.15 | 3000.00 | 829.7 |
| 333.15 | 5000.00 | 831.5 |
| 333.15 | 10000.00 | 835.9 |
| 333.15 | 15000.00 | 840.0 |
| 333.15 | 20000.00 | 844.1 |
| 333.15 | 25000.00 | 847.9 |
| 333.15 | 30000.00 | 851.6 |
| 333.15 | 35000.00 | 855.0 |
| 333.15 | 40000.00 | 858.8 |
| 333.15 | 50000.00 | 865.1 |
| 333.15 | 60000.00 | 871.1 |
| 343.15 | 100.00 | 817.8 |
| 343.15 | 1000.00 | 818.8 |
| 343.15 | 3000.00 | 820.6 |
| 343.15 | 5000.00 | 823.0 |
| 343.15 | 10000.00 | 827.2 |
| 343.15 | 15000.00 | 831.7 |
| 343.15 | 20000.00 | 836.3 |
| 343.15 | 25000.00 | 840.0 |
| 343.15 | 30000.00 | 843.9 |
| 343.15 | 35000.00 | 847.6 |
| 343.15 | 40000.00 | 851.0 |
| 343.15 | 50000.00 | 858.0 |
| 343.15 | 60000.00 | 864.1 |
| 353.15 | 100.00 | 808.7 |
| 353.15 | 1000.00 | 809.6 |
| 353.15 | 3000.00 | 811.5 |
| 353.15 | 5000.00 | 813.6 |
| 353.15 | 10000.00 | 818.1 |
| 353.15 | 15000.00 | 822.8 |
| 353.15 | 20000.00 | 827.6 |
| 353.15 | 25000.00 | 831.5 |
| 353.15 | 30000.00 | 835.8 |
| 353.15 | 35000.00 | 839.8 |
| 353.15 | 40000.00 | 843.4 |
| 353.15 | 50000.00 | 850.6 |
| 353.15 | 60000.00 | 856.9 |
| 363.15 | 100.00 | 799.5 |
| 363.15 | 1000.00 | 800.7 |
| 363.15 | 3000.00 | 802.9 |
| 363.15 | 5000.00 | 805.3 |
| 363.15 | 10000.00 | 810.2 |
| 363.15 | 15000.00 | 815.5 |
| 363.15 | 20000.00 | 819.9 |
| 363.15 | 25000.00 | 824.1 |
| 363.15 | 30000.00 | 828.5 |
| 363.15 | 35000.00 | 832.7 |
| 363.15 | 40000.00 | 836.7 |
| 363.15 | 50000.00 | 844.0 |
| 363.15 | 60000.00 | 850.8 |
| Reference | ||
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 288.15 | 100.00 | 864.9 |
| 298.15 | 100.00 | 856.2 |
| 308.15 | 100.00 | 847.5 |
| 288.15 | 5000.00 | 868.3 |
| 298.15 | 5000.00 | 860.2 |
| 308.15 | 5000.00 | 851.4 |
| 288.15 | 10000.00 | 871.8 |
| 298.15 | 10000.00 | 863.5 |
| 308.15 | 10000.00 | 855.2 |
| 288.15 | 20000.00 | 878.1 |
| 298.15 | 20000.00 | 870.1 |
| 308.15 | 20000.00 | 862.1 |
| 288.15 | 30000.00 | 884.0 |
| 298.15 | 30000.00 | 876.5 |
| 308.15 | 30000.00 | 868.6 |
| 288.15 | 40000.00 | 889.7 |
| 298.15 | 40000.00 | 882.2 |
| 308.15 | 40000.00 | 874.8 |
| Reference | ||
Speed of sound, m/s
Operational condition: Frequency, MHz = 5 (Liquid)
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Speed of sound, m/s - Liquid |
| 305.99 | 1000.00 | 1281.77 |
| 306.07 | 2050.00 | 1287.1 |
| 306.02 | 2050.00 | 1287.22 |
| 305.93 | 3690.00 | 1296.49 |
| 306.00 | 4900.00 | 1302.49 |
| 305.98 | 5250.00 | 1304.38 |
| 306.05 | 6960.00 | 1312.94 |
| 306.03 | 9400.00 | 1325.57 |
| 306.00 | 13840.00 | 1347.72 |
| 306.07 | 16500.00 | 1360.11 |
| 306.06 | 19900.00 | 1376.19 |
| 306.07 | 24630.00 | 1397.78 |
| 306.14 | 26930.00 | 1407.8 |
| 306.18 | 28370.00 | 1413.93 |
| 306.10 | 29650.00 | 1419.72 |
| 306.00 | 30490.00 | 1423.77 |
| 305.99 | 35160.00 | 1443.56 |
| 305.97 | 40270.00 | 1464.54 |
| 305.98 | 45030.00 | 1483.47 |
| 305.98 | 50870.00 | 1505.99 |
| 323.56 | 210.00 | 1206.43 |
| 323.57 | 490.00 | 1208.1 |
| 323.54 | 1060.00 | 1211.51 |
| 323.57 | 2600.00 | 1220.4 |
| 323.58 | 5070.00 | 1234.53 |
| 323.54 | 6060.00 | 1240.28 |
| 323.58 | 6090.00 | 1240.29 |
| 323.59 | 7490.00 | 1248.03 |
| 323.57 | 10070.00 | 1262.13 |
| 323.58 | 11110.00 | 1267.65 |
| 323.53 | 11470.00 | 1269.76 |
| 323.60 | 15130.00 | 1288.59 |
| 323.59 | 17890.00 | 1302.54 |
| 323.55 | 18570.00 | 1306.1 |
| 323.57 | 20900.00 | 1317.51 |
| 323.59 | 25130.00 | 1337.71 |
| 323.59 | 30210.00 | 1361.29 |
| 323.52 | 30290.00 | 1361.83 |
| 323.48 | 34540.00 | 1381.14 |
| 323.58 | 34830.00 | 1382.01 |
| 323.57 | 39580.00 | 1402.7 |
| 323.47 | 41260.00 | 1410.19 |
| 323.54 | 44230.00 | 1422.37 |
| 323.57 | 44830.00 | 1424.72 |
| 323.54 | 45010.00 | 1425.56 |
| 323.49 | 46870.00 | 1433.42 |
| 323.51 | 49380.00 | 1443.5 |
| 323.47 | 49810.00 | 1445.32 |
| 323.48 | 54770.00 | 1464.84 |
| 323.48 | 55430.00 | 1467.39 |
| 323.47 | 59650.00 | 1483.53 |
| 323.51 | 65910.00 | 1506.74 |
| 335.99 | 280.00 | 1158.02 |
| 335.99 | 570.00 | 1159.79 |
| 335.98 | 1230.00 | 1163.95 |
| 335.98 | 2630.00 | 1172.56 |
| 335.98 | 5600.00 | 1190.42 |
| 336.00 | 10270.00 | 1217.21 |
| 335.99 | 10300.00 | 1217.47 |
| 336.01 | 14980.00 | 1243.1 |
| 335.99 | 20370.00 | 1271.42 |
| 336.01 | 20750.00 | 1273.3 |
| 336.00 | 24830.00 | 1293.84 |
| 336.00 | 30890.00 | 1322.99 |
| 336.06 | 31080.00 | 1323.64 |
| 336.00 | 34840.00 | 1341.19 |
| 336.02 | 40670.00 | 1367.23 |
| 336.05 | 41270.00 | 1369.78 |
| 336.03 | 41380.00 | 1370.31 |
| 335.98 | 45230.00 | 1387.08 |
| 335.97 | 50590.00 | 1409.56 |
| 335.95 | 55000.00 | 1427.54 |
| 335.96 | 61040.00 | 1451.3 |
| 335.95 | 65380.00 | 1467.88 |
| 348.25 | 40.00 | 1108.83 |
| 348.32 | 1270.00 | 1116.85 |
| 348.30 | 2110.00 | 1122.26 |
| 348.27 | 2120.00 | 1122.47 |
| 348.29 | 2590.00 | 1125.51 |
| 348.28 | 4090.00 | 1135.15 |
| 348.32 | 8600.00 | 1162.9 |
| 348.32 | 8900.00 | 1164.69 |
| 348.35 | 10880.00 | 1176.32 |
| 348.37 | 14620.00 | 1197.72 |
| 348.36 | 15220.00 | 1201.14 |
| 348.36 | 20050.00 | 1227.6 |
| 348.45 | 24930.00 | 1252.9 |
| 348.43 | 29340.00 | 1275.02 |
| 348.43 | 33900.00 | 1297.21 |
| 348.43 | 39830.00 | 1324.82 |
| 348.42 | 45170.00 | 1348.71 |
| 348.42 | 49930.00 | 1369.38 |
| 348.42 | 54750.00 | 1389.61 |
| 348.39 | 59820.00 | 1410.34 |
| 348.41 | 59890.00 | 1410.6 |
| 348.37 | 60580.00 | 1413.43 |
| 348.39 | 64180.00 | 1427.64 |
| 348.40 | 64670.00 | 1429.6 |
| 355.98 | 270.00 | 1081.04 |
| 355.95 | 490.00 | 1082.63 |
| 355.94 | 920.00 | 1085.65 |
| 355.95 | 2620.00 | 1097.05 |
| 355.98 | 5370.00 | 1115.13 |
| 355.96 | 10930.00 | 1149.89 |
| 355.89 | 12280.00 | 1158.25 |
| 355.92 | 15640.00 | 1177.67 |
| 355.94 | 20950.00 | 1207.26 |
| 355.95 | 25050.00 | 1229.15 |
| 355.95 | 31130.00 | 1260.21 |
| 356.05 | 34600.00 | 1276.89 |
| 356.02 | 41360.00 | 1308.87 |
| 356.02 | 45060.00 | 1325.7 |
| 356.08 | 50520.00 | 1349.51 |
| 356.04 | 54960.00 | 1368.53 |
| 356.00 | 59390.00 | 1387.08 |
| 355.98 | 65160.00 | 1410.32 |
| 373.59 | 240.00 | 1014.61 |
| 373.58 | 570.00 | 1017.06 |
| 373.55 | 950.00 | 1020.07 |
| 373.53 | 2520.00 | 1031.71 |
| 373.54 | 2530.00 | 1031.73 |
| 373.53 | 5450.00 | 1052.49 |
| 373.60 | 10260.00 | 1084.6 |
| 373.61 | 14920.00 | 1114.21 |
| 373.60 | 19750.00 | 1143.36 |
| 373.62 | 20290.00 | 1146.4 |
| 373.63 | 24920.00 | 1172.65 |
| 373.60 | 29800.00 | 1199.11 |
| 373.60 | 29850.00 | 1199.31 |
| 373.60 | 35000.00 | 1226.08 |
| 373.62 | 39790.00 | 1249.82 |
| 373.62 | 40800.00 | 1254.88 |
| 373.57 | 44340.00 | 1271.77 |
| 373.58 | 49640.00 | 1296.23 |
| 373.63 | 54980.00 | 1319.83 |
| 373.62 | 58970.00 | 1337.14 |
| 373.61 | 59070.00 | 1337.54 |
| 373.64 | 64880.00 | 1361.68 |
| 398.20 | 220.00 | 923.76 |
| 398.21 | 500.00 | 926.17 |
| 398.22 | 1040.00 | 930.76 |
| 398.25 | 2490.00 | 942.77 |
| 398.24 | 5190.00 | 964.55 |
| 398.25 | 10300.00 | 1002.89 |
| 398.26 | 12650.00 | 1019.53 |
| 398.24 | 15110.00 | 1036.53 |
| 398.25 | 19720.00 | 1066.63 |
| 398.22 | 20010.00 | 1068.47 |
| 398.22 | 24890.00 | 1098.56 |
| 398.20 | 29920.00 | 1127.9 |
| 398.25 | 31220.00 | 1135.23 |
| 398.24 | 31220.00 | 1135.21 |
| 398.21 | 34890.00 | 1155.44 |
| 398.19 | 37260.00 | 1168.3 |
| 398.20 | 37270.00 | 1168.29 |
| 398.20 | 40070.00 | 1182.91 |
| 398.21 | 44950.00 | 1207.53 |
| 398.23 | 50040.00 | 1232.26 |
| 398.20 | 54810.00 | 1254.71 |
| 398.20 | 60130.00 | 1278.81 |
| 398.21 | 64730.00 | 1298.96 |
| 422.73 | 190.00 | 834.7 |
| 422.72 | 550.00 | 838.3 |
| 422.75 | 780.00 | 840.37 |
| 422.74 | 1230.00 | 844.88 |
| 422.65 | 2630.00 | 858.44 |
| 422.57 | 5690.00 | 886.27 |
| 422.74 | 9190.00 | 915.48 |
| 422.75 | 10020.00 | 922.14 |
| 422.70 | 14830.00 | 959.38 |
| 422.75 | 19940.00 | 995.75 |
| 422.75 | 24810.00 | 1028.16 |
| 422.73 | 28590.00 | 1052.11 |
| 422.75 | 29890.00 | 1060.03 |
| 422.77 | 34850.00 | 1089.33 |
| 422.77 | 40720.00 | 1122.29 |
| 422.74 | 44830.00 | 1144.36 |
| 422.72 | 50170.00 | 1171.8 |
| 422.73 | 54780.00 | 1194.57 |
| 422.76 | 59900.00 | 1218.69 |
| 422.75 | 64580.00 | 1240.21 |
| 447.07 | 300.00 | 748.43 |
| 447.07 | 580.00 | 751.73 |
| 447.02 | 1020.00 | 756.94 |
| 446.94 | 5130.00 | 800.91 |
| 447.01 | 7300.00 | 821.88 |
| 446.99 | 10180.00 | 848.37 |
| 446.99 | 14830.00 | 887.97 |
| 447.00 | 19890.00 | 927.32 |
| 447.03 | 22500.00 | 946.32 |
| 447.02 | 24900.00 | 963.22 |
| 447.09 | 30510.00 | 1000.66 |
| 447.13 | 35270.00 | 1030.41 |
| 447.12 | 40150.00 | 1059.45 |
| 447.13 | 45010.00 | 1086.93 |
| 447.08 | 49880.00 | 1113.32 |
| 447.11 | 54450.00 | 1136.99 |
| 447.13 | 59760.00 | 1163.32 |
| 447.08 | 64750.00 | 1187.32 |
| Reference | ||
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [86.67; 359.53] | J/mol×K | [200.00; 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 | 6.23970e+01 | |||
| Coefficient B | -5.85600e+02 | |||
| Coefficient C | 6.11724e+00 | |||
| Coefficient D | 3.79210e-06 | |||
| Coefficient E | -1.70440e-08 | |||
| Temperature range, min. | 200.00 | |||
| Temperature range, max. | 1500.00 | |||
| Cp,gas | 86.67 | J/mol×K | 200.00 | Calculated Property |
| Cp,gas | 145.19 | J/mol×K | 344.44 | Calculated Property |
| Cp,gas | 199.02 | J/mol×K | 488.89 | Calculated Property |
| Cp,gas | 241.54 | J/mol×K | 633.33 | Calculated Property |
| Cp,gas | 274.48 | J/mol×K | 777.78 | Calculated Property |
| Cp,gas | 300.16 | J/mol×K | 922.22 | Calculated Property |
| Cp,gas | 320.38 | J/mol×K | 1066.67 | Calculated Property |
| Cp,gas | 336.45 | J/mol×K | 1211.11 | Calculated Property |
| Cp,gas | 349.28 | J/mol×K | 1355.56 | Calculated Property |
| Cp,gas | 359.53 | J/mol×K | 1500.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | [177.03; 325.05] | J/mol×K | [286.40; 600.00] |
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 | 6.30840e+01 | |||
| Coefficient B | -3.43380e+02 | |||
| Coefficient C | 6.53024e+00 | |||
| Coefficient D | -3.38510e-03 | |||
| Coefficient E | 4.55920e-06 | |||
| Temperature range, min. | 286.40 | |||
| Temperature range, max. | 600.00 | |||
| Cp,liquid | 177.03 | J/mol×K | 286.40 | Calculated Property |
| Cp,liquid | 190.11 | J/mol×K | 321.24 | Calculated Property |
| Cp,liquid | 202.66 | J/mol×K | 356.09 | Calculated Property |
| Cp,liquid | 215.30 | J/mol×K | 390.93 | Calculated Property |
| Cp,liquid | 228.59 | J/mol×K | 425.78 | Calculated Property |
| Cp,liquid | 243.07 | J/mol×K | 460.62 | Calculated Property |
| Cp,liquid | 259.30 | J/mol×K | 495.47 | Calculated Property |
| Cp,liquid | 277.90 | J/mol×K | 530.31 | Calculated Property |
| Cp,liquid | 299.54 | J/mol×K | 565.16 | Calculated Property |
| Cp,liquid | 325.05 | J/mol×K | 600.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [0.0007018; 0.0001322] | Pa×s | [286.41; 493.60] |
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 | -2.39160e+01 | |||
| Coefficient B | 1.49980e+03 | |||
| Coefficient C | 2.07190e+00 | |||
| Coefficient D | -3.70650e-06 | |||
| Coefficient E | 2.00000e+00 | |||
| Temperature range, min. | 286.41 | |||
| Temperature range, max. | 493.60 | |||
| η | 0.0007018 | Pa×s | 286.41 | Calculated Property |
| η | 0.0005303 | Pa×s | 309.43 | Calculated Property |
| η | 0.0004164 | Pa×s | 332.45 | Calculated Property |
| η | 0.0003368 | Pa×s | 355.47 | Calculated Property |
| η | 0.0002787 | Pa×s | 378.49 | Calculated Property |
| η | 0.0002348 | Pa×s | 401.52 | Calculated Property |
| η | 0.0002006 | Pa×s | 424.54 | Calculated Property |
| η | 0.0001732 | Pa×s | 447.56 | Calculated Property |
| η | 0.0001508 | Pa×s | 470.58 | Calculated Property |
| η | 0.0001322 | Pa×s | 493.60 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | [42.91; 0.00] | kJ/mol | [286.41; 616.20] |
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 | 5.63320e+01 | |||
| Coefficient B | 3.79650e-01 | |||
| Coefficient C | 4.23950e-01 | |||
| Coefficient D | -8.56830e-01 | |||
| Coefficient E | 4.37040e-01 | |||
| Critical temperature, Tc (K) | 6.16200e+02 | |||
| Temperature range, min. | 286.41 | |||
| Temperature range, max. | 616.20 | |||
| ΔvapH | 42.91 | kJ/mol | 286.41 | Calculated Property |
| ΔvapH | 40.95 | kJ/mol | 323.05 | Calculated Property |
| ΔvapH | 38.91 | kJ/mol | 359.70 | Calculated Property |
| ΔvapH | 36.76 | kJ/mol | 396.34 | Calculated Property |
| ΔvapH | 34.42 | kJ/mol | 432.98 | Calculated Property |
| ΔvapH | 31.78 | kJ/mol | 469.63 | Calculated Property |
| ΔvapH | 28.66 | kJ/mol | 506.27 | Calculated Property |
| ΔvapH | 24.71 | kJ/mol | 542.91 | Calculated Property |
| ΔvapH | 19.06 | kJ/mol | 579.56 | Calculated Property |
| ΔvapH | 0.00 | kJ/mol | 616.20 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [0.58; 202.65] | kPa | [286.41; 439.06] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.44593e+01 | |||
| Coefficient B | -3.57809e+03 | |||
| Coefficient C | -4.79200e+01 | |||
| Temperature range, min. | 286.41 | |||
| Temperature range, max. | 439.06 | |||
| Pvap | 0.58 | kPa | 286.41 | Calculated Property |
| Pvap | 1.57 | kPa | 303.37 | Calculated Property |
| Pvap | 3.76 | kPa | 320.33 | Calculated Property |
| Pvap | 8.12 | kPa | 337.29 | Calculated Property |
| Pvap | 16.10 | kPa | 354.25 | Calculated Property |
| Pvap | 29.72 | kPa | 371.22 | Calculated Property |
| Pvap | 51.60 | kPa | 388.18 | Calculated Property |
| Pvap | 85.01 | kPa | 405.14 | Calculated Property |
| Pvap | 133.86 | kPa | 422.10 | Calculated Property |
| Pvap | 202.65 | kPa | 439.06 | Calculated Property |
| Pvap | [0.47; 3499.27] | kPa | [282.99; 616.20] |
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 | 9.04442e+01 | |||
| Coefficient B | -8.08210e+03 | |||
| Coefficient C | -1.11970e+01 | |||
| Coefficient D | 7.26050e-06 | |||
| Coefficient E | 2.00000e+00 | |||
| Comment | Range stopped at Tc; ChemSep gives it to 616.23 K. | |||
| Temperature range, min. | 282.99 | |||
| Temperature range, max. | 616.20 | |||
| Pvap | 0.47 | kPa | 282.99 | Calculated Property |
| Pvap | 3.83 | kPa | 320.01 | Calculated Property |
| Pvap | 18.52 | kPa | 357.04 | Calculated Property |
| Pvap | 62.99 | kPa | 394.06 | Calculated Property |
| Pvap | 167.46 | kPa | 431.08 | Calculated Property |
| Pvap | 373.43 | kPa | 468.11 | Calculated Property |
| Pvap | 733.26 | kPa | 505.13 | Calculated Property |
| Pvap | 1312.46 | kPa | 542.15 | Calculated Property |
| Pvap | 2195.94 | kPa | 579.18 | Calculated Property |
| Pvap | 3499.27 | kPa | 616.20 | Calculated Property |
| Pvap | [0.58; 3449.39] | kPa | [286.41; 616.26] |
KDB Vapor Pressure Data
|
| Equation | ln(Y) = A + B/T + C·ln(T) + D·T² + E/T² Y is Pvap in kPa, T in K | |||
| Coefficient A | 7.95572e+01 | |||
| Coefficient B | -7.63795e+03 | |||
| Coefficient C | -9.52735e+00 | |||
| Coefficient D | 5.74897e-06 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 286.41 | |||
| Temperature range, max. | 616.26 | |||
| Pvap | 0.58 | kPa | 286.41 | Calculated Property |
| Pvap | 4.34 | kPa | 323.06 | Calculated Property |
| Pvap | 20.01 | kPa | 359.71 | Calculated Property |
| Pvap | 66.32 | kPa | 396.36 | Calculated Property |
| Pvap | 173.76 | kPa | 433.01 | Calculated Property |
| Pvap | 383.85 | kPa | 469.66 | Calculated Property |
| Pvap | 747.85 | kPa | 506.31 | Calculated Property |
| Pvap | 1327.08 | kPa | 542.96 | Calculated Property |
| Pvap | 2196.10 | kPa | 579.61 | Calculated Property |
| Pvap | 3449.39 | kPa | 616.26 | Calculated Property |
| Pvap | [0.58; 270.21] | kPa | [286.43; 452.38] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.41506e+01 | |||
| Coefficient B | -3.39494e+03 | |||
| Coefficient C | -5.53770e+01 | |||
| Reference | Osborn and Douslin, 1974 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 286.43 | |||
| Temperature range, max. | 452.38 | |||
| Pvap | 0.58 | kPa | 286.43 | Calculated Property |
| Pvap | 1.72 | kPa | 304.87 | Calculated Property |
| Pvap | 4.39 | kPa | 323.31 | Calculated Property |
| Pvap | 9.93 | kPa | 341.75 | Calculated Property |
| Pvap | 20.34 | kPa | 360.19 | Calculated Property |
| Pvap | 38.40 | kPa | 378.62 | Calculated Property |
| Pvap | 67.68 | kPa | 397.06 | Calculated Property |
| Pvap | 112.56 | kPa | 415.50 | Calculated Property |
| Pvap | 178.16 | kPa | 433.94 | Calculated Property |
| Pvap | 270.21 | kPa | 452.38 | Calculated Property |
| Pvap | [127.15; 2865.52] | kPa | [420.00; 600.00] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.49885e+01 | |||
| Coefficient B | -4.11912e+03 | |||
| Coefficient C | -1.39020e+01 | |||
| Reference | Ambrose, Broderick, et al., 1967 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 420.00 | |||
| Temperature range, max. | 600.00 | |||
| Pvap | 127.15 | kPa | 420.00 | Calculated Property |
| Pvap | 204.69 | kPa | 440.00 | Calculated Property |
| Pvap | 315.73 | kPa | 460.00 | Calculated Property |
| Pvap | 469.23 | kPa | 480.00 | Calculated Property |
| Pvap | 674.99 | kPa | 500.00 | Calculated Property |
| Pvap | 943.47 | kPa | 520.00 | Calculated Property |
| Pvap | 1285.59 | kPa | 540.00 | Calculated Property |
| Pvap | 1712.52 | kPa | 560.00 | Calculated Property |
| Pvap | 2235.47 | kPa | 580.00 | Calculated Property |
| Pvap | 2865.52 | kPa | 600.00 | Calculated Property |
| Pvap | [6.35; 103.90] | kPa | [331.44; 412.44] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.40720e+01 | |||
| Coefficient B | -3.34033e+03 | |||
| Coefficient C | -5.81600e+01 | |||
| Reference | Williamham, Taylor, et al., 1945 | |||
| Temperature range, min. | 331.44 | |||
| Temperature range, max. | 412.44 | |||
| Pvap | 6.35 | kPa | 331.44 | Calculated Property |
| Pvap | 9.38 | kPa | 340.44 | Calculated Property |
| Pvap | 13.52 | kPa | 349.44 | Calculated Property |
| Pvap | 19.07 | kPa | 358.44 | Calculated Property |
| Pvap | 26.35 | kPa | 367.44 | Calculated Property |
| Pvap | 35.77 | kPa | 376.44 | Calculated Property |
| Pvap | 47.73 | kPa | 385.44 | Calculated Property |
| Pvap | 62.73 | kPa | 394.44 | Calculated Property |
| Pvap | 81.26 | kPa | 403.44 | Calculated Property |
| Pvap | 103.90 | kPa | 412.44 | Calculated Property |
| Pvap | [1.18; 6.81] | kPa | [298.00; 333.00] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.48491e+01 | |||
| Coefficient B | -3.78594e+03 | |||
| Coefficient C | -4.02290e+01 | |||
| Reference | Pitzer and Scott, 1943 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 298.00 | |||
| Temperature range, max. | 333.00 | |||
| Pvap | 1.18 | kPa | 298.00 | Calculated Property |
| Pvap | 1.46 | kPa | 301.89 | Calculated Property |
| Pvap | 1.81 | kPa | 305.78 | Calculated Property |
| Pvap | 2.22 | kPa | 309.67 | Calculated Property |
| Pvap | 2.71 | kPa | 313.56 | Calculated Property |
| Pvap | 3.29 | kPa | 317.44 | Calculated Property |
| Pvap | 3.98 | kPa | 321.33 | Calculated Property |
| Pvap | 4.78 | kPa | 325.22 | Calculated Property |
| Pvap | 5.72 | kPa | 329.11 | Calculated Property |
| Pvap | 6.81 | kPa | 333.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ρl | [866.45; 277.86] | kg/m3 | [286.41; 616.20] |
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 | 7.19289e+01 | |||
| Coefficient B | 2.58870e-01 | |||
| Coefficient C | 6.16200e+02 | |||
| Coefficient D | 2.75960e-01 | |||
| Temperature range, min. | 286.41 | |||
| Temperature range, max. | 616.20 | |||
| ρl | 866.45 | kg/m3 | 286.41 | Calculated Property |
| ρl | 835.50 | kg/m3 | 323.05 | Calculated Property |
| ρl | 802.88 | kg/m3 | 359.70 | Calculated Property |
| ρl | 768.17 | kg/m3 | 396.34 | Calculated Property |
| ρl | 730.78 | kg/m3 | 432.98 | Calculated Property |
| ρl | 689.77 | kg/m3 | 469.63 | Calculated Property |
| ρl | 643.53 | kg/m3 | 506.27 | Calculated Property |
| ρl | 588.79 | kg/m3 | 542.91 | Calculated Property |
| ρl | 516.63 | kg/m3 | 579.56 | Calculated Property |
| ρl | 277.86 | kg/m3 | 616.20 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| γ | [0.03; 0.02] | N/m | [286.15; 411.15] |
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 | 6.00263e-02 | |||
| Coefficient B | -1.07400e-04 | |||
| Coefficient C | 0.00000e+00 | |||
| Coefficient D | 0.00000e+00 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 286.15 | |||
| Temperature range, max. | 411.15 | |||
| γ | 0.03 | N/m | 286.15 | Calculated Property |
| γ | 0.03 | N/m | 300.04 | Calculated Property |
| γ | 0.03 | N/m | 313.93 | Calculated Property |
| γ | 0.02 | N/m | 327.82 | Calculated Property |
| γ | 0.02 | N/m | 341.71 | Calculated Property |
| γ | 0.02 | N/m | 355.59 | Calculated Property |
| γ | 0.02 | N/m | 369.48 | Calculated Property |
| γ | 0.02 | N/m | 383.37 | Calculated Property |
| γ | 0.02 | N/m | 397.26 | Calculated Property |
| γ | 0.02 | N/m | 411.15 | Calculated Property |
| γ | [0.03; 2.24e-06] | N/m | [273.10; 612.43] |
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 | -8.01880e-03 | |||
| Coefficient B | 6.60970e+01 | |||
| Coefficient C | -3.48780e+00 | |||
| Coefficient D | 1.83530e-03 | |||
| Coefficient E | -6.85160e-06 | |||
| Comment | Range stopped where the equation turns negative; ChemSep gives it to 616.2 K. | |||
| Temperature range, min. | 273.10 | |||
| Temperature range, max. | 612.43 | |||
| γ | 0.03 | N/m | 273.10 | Calculated Property |
| γ | 0.03 | N/m | 310.80 | Calculated Property |
| γ | 0.02 | N/m | 348.51 | Calculated Property |
| γ | 0.02 | N/m | 386.21 | Calculated Property |
| γ | 0.01 | N/m | 423.91 | Calculated Property |
| γ | 0.01 | N/m | 461.61 | Calculated Property |
| γ | 0.01 | N/m | 499.32 | Calculated Property |
| γ | 0.00 | N/m | 537.02 | Calculated Property |
| γ | 0.00 | N/m | 574.72 | Calculated Property |
| γ | 2.24e-06 | N/m | 612.43 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λgas | [0.01; 0.09] | W/m×K | [286.41; 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 | 1.26100e-07 | |||
| Coefficient B | 1.89160e+00 | |||
| Coefficient C | -4.53430e+02 | |||
| Coefficient D | 1.11720e+05 | |||
| Temperature range, min. | 286.41 | |||
| Temperature range, max. | 1000.00 | |||
| λgas | 0.01 | W/m×K | 286.41 | Calculated Property |
| λgas | 0.01 | W/m×K | 365.70 | Calculated Property |
| λgas | 0.02 | W/m×K | 444.99 | Calculated Property |
| λgas | 0.03 | W/m×K | 524.27 | Calculated Property |
| λgas | 0.04 | W/m×K | 603.56 | Calculated Property |
| λgas | 0.05 | W/m×K | 682.85 | Calculated Property |
| λgas | 0.06 | W/m×K | 762.14 | Calculated Property |
| λgas | 0.07 | W/m×K | 841.42 | Calculated Property |
| λgas | 0.08 | W/m×K | 920.71 | Calculated Property |
| λgas | 0.09 | W/m×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λliquid | [0.13; 0.10] | W/m×K | [286.41; 413.10] |
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 | 6.68810e-04 | |||
| Coefficient B | -1.22940e+02 | |||
| Coefficient C | -6.08750e-01 | |||
| Coefficient D | -3.73220e-03 | |||
| Coefficient E | 9.74460e-07 | |||
| Temperature range, min. | 286.41 | |||
| Temperature range, max. | 413.10 | |||
| λliquid | 0.13 | W/m×K | 286.41 | Calculated Property |
| λliquid | 0.13 | W/m×K | 300.49 | Calculated Property |
| λliquid | 0.13 | W/m×K | 314.56 | Calculated Property |
| λliquid | 0.12 | W/m×K | 328.64 | Calculated Property |
| λliquid | 0.12 | W/m×K | 342.72 | Calculated Property |
| λliquid | 0.12 | W/m×K | 356.79 | Calculated Property |
| λliquid | 0.11 | W/m×K | 370.87 | Calculated Property |
| λliquid | 0.11 | W/m×K | 384.95 | Calculated Property |
| λliquid | 0.11 | W/m×K | 399.02 | Calculated Property |
| λliquid | 0.10 | W/m×K | 413.10 | Calculated Property |
Similar Compounds
![[2H9]-1-(Chloromethyl)-4-methylbenzene.](data:image/png;base64,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)
Find more compounds similar to p-Xylene.
Mixtures
- Acetonitrile + p-Xylene
- p-Xylene + Acetone
- p-Xylene + Ethanol + Water
- p-Xylene + Ethanol
- p-Xylene + Ethyl Acetate
- Benzene + n-Hexane + p-Xylene
- Benzene + p-Xylene
- p-Xylene + 1-Butanol + Water
- p-Xylene + 1-Butanol
- p-Xylene + Cyclohexane
- p-Xylene + Acetic acid + Water
- p-Xylene + Acetic acid
- n-Hexane + p-Xylene
- 2-Propanol + p-Xylene
- 1-Hexene + p-Xylene
- p-Xylene + Methyl Alcohol
- p-Xylene + Tetrahydrofuran
- p-Xylene + Water
- p-Xylene + Benzene, 1,3-dimethyl-
- p-Xylene + 2-Pyrrolidinone, 1-methyl-
Find more mixtures with p-Xylene.
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).
- Hankinson and Thomson (1979), COSTALD parameters ChEDL chemicals 1.5.2, from Hankinson, R. W.; Thomson, G. H. A New Correlation for Saturated Densities of Liquids and Their Mixtures. AIChE J. 1979, 25, 653-663.
- IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 3 ChEDL chemicals 1.5.2, from Tsonopoulos, C.; Ambrose, D. Vapor-Liquid Critical Properties of Elements and Compounds. 3. Aromatic Hydrocarbons. J. Chem. Eng. Data 1995, 40, 547-558.
- 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).
- Passut and Danner (1973), critical constants and acentric factors ChEDL chemicals 1.5.2, from Passut, C. A.; Danner, R. P. Acentric Factor. A Valuable Correlating Parameter for the Properties of Hydrocarbons. Ind. Eng. Chem. Process Des. Dev. 1973, 12, 365-368.
- 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.
- Dortmund Data Bank Vapor-Liquid Equilibrium Data
- Effect of Temperature on the Change of Refractive Index on Mixing for Butyl Acetate + Aromatic Hydrocarbons
- Isobaric Vapor Liquid Equilibria of 1-Butanol p-Xylene System1
- Experimental Study of the Dynamic Viscosity Deviations in the Binary Systems: Hexane + Ethylbenzene, + o-Xylene, + m-Xylene, + p-Xylene at 298.15 K
- Thermodynamic Properties of Ternary Liquid Mixtures of 2-Pyrrolidinone with Aromatic Hydrocarbons
- Densities and Volumetric Properties of Binary Mixtures of Butyl Acrylate with Benzene, Toluene, o-Xylene, m-Xylene, p-Xylene, and Mesitylene at Temperatures from 288.15 K to 318.15 K
- Isentropic Compressibilities Changes of Mixing of Tetrahydropyran and Aromatic Hydrocarbons Ternary Mixtures at 308.15 K
- Bubble temperature measurements on the binary mixtures formed by decane with a variety of compounds at 95.8 kPa
- Activity coefficient at infinite dilution, azeotropic data, excess enthalpies and solid liquid-equilibria for binary systems of alkanes and aromatics with esters
- Experimental and theoretical surface tension deviations in the binary systems propyl propanoate + o-, m- and p-xylene at 298.15K
- Isobaric molar heat capacities of the ternary system dimethyl carbonate + p-xylene + n-decane
- Topological and thermodynamic investigations of molecular interactions in binary mixtures: Molar excess volumes and molar excess enthalpies
- Bubble points of some binary mixtures formed by o-cresol at 95.75 kPa
- Separation of aromatic hydrocarbons from alkanes using ammonium ionic liquid C2NTf2 at T = 298.15K
- Ultrasonic and viscometric study of molecular interactions in binary mixtures of aniline with 1-propanol, 2-propanol, 2-methyl-1-propanol, and 2-methyl-2-propanol at different temperatures
- Measurement and prediction of pyrene solubility in pure, binary, ternary and quaternary solvent systems
- Excess Gibbs' energies of the binary mixtures formed by N,N-dimethylformamide with xylenes and cresols at 95.1 kPa
- Influence of temperature on thermodynamics of ethers + xylenes
- Activity coefficients at infinite dilution measurements for organic solutes and water in the ionic liquid 1-butyl-1-methylpyrrolidinium trifluoromethanesulfonate using GLC
- Isobaric vapor liquid liquid equilibrium and vapor liquid equilibrium for the system water ethanol-1,4-dimethylbenzene at 101.3 kPa
- Activity coefficients at infinite dilution measurements for organic solutes and water in the 1-hexyloxymethyl-3-methyl-imidazolium and 1,3-dihexyloxymethyl-imidazolium bis(trifluoromethylsulfonyl)-imide ionic liquids The cation influence
- Vapor liquid equilibria and density measurement for binary mixtures of o-xylene + NMF, m-xylene +NMF and p-xylene +NMF at 333.15 K, 343.15 K and 353.15 K from 0 kPa to 101.3 kPa
- Isomer effect in the separation of octane and xylenes using the ionic liquid 1-ethyl-3-methylimidazolium bis{(trifluoromethyl)sulfonyl}amide
- Application of [EMpy][ESO4] ionic liquid as solvent for the liquid extraction of xylenes from hexane
- Gas-liquid chromatography measurements of activity coefficients at infinite dilution of hydrocarbons and alkanols in 1-alkyl-3-methylimidazolium bis(oxalato)borate
- Study of [EMim][ESO4] ionic liquid as solvent in the liquid-liquid extraction of xylenes from their mixtures with hexane
- Physical properties of 3-methyl-N-butylpyridinium tricyanomethanide and ternary LLE data with an aromatic and an aliphatic hydrocarbon at T = (303.2 and 328.2) K and p = 0.1 MPa
- Solubility of elemental sulfur in pure organic solvents and organic solvent-ionic liquid mixtures from 293.15 to 353.15 K
- Isobaric vapor-liquid equilibrium for the binary mixtures of nonane with cyclohexane, toluene, m-xylene, or p-xylene at 101.3 kPa
- Activity coefficients at infinite dilution of organic solutes in the ionic liquid ethyl(2-hydroxyethyl)dimethyl-ammonium diethylphosphate using gas liquid chromatography
- Activity coefficients at infinite dilution of organic solutes in 1-octyl-3-methylimidazolium nitrate using gas-liquid chromatography
- Liquid-liquid equilibrium (LLE) data for ternary mixtures of {aliphatic + p-xylene + [EMpy][ESO4]} at T = 313.15 K
- Isobaric vapor-liquid equilibrium of binary systems of decane with p-, o-, m-xylene at 20 kPa
- Liquid-liquid equilibria of imidazolium ionic liquids having bistriflamide or triflate anions with aromatic non-polar and polar compounds
- Solubility and partition coefficient of p-toluic acid in p-xylene and water
- Isobaric vapor-liquid equilibrium data of the binary systems of octane with p, o, m-xylene at 20 kPa
- Enthalpies and Gibbs free energies of solvation in ethylene glycol at298 K: Influence of the solvophobic effect
- Phase equilibria of binary mixtures (ionic liquid + aromatic hydrocarbon): Effect of the structure of the components on the solubility
- Isobaric vapor-liquid equilibrium for n-undecane + p-, o-, m-xylene at 10 kPa
- Vapor-liquid equilibrium for the binary mixtures of dipropylene glycol with aromatic hydrocarbons: Experimental and regression
- Experimental and theoretical study of interaction between organic compounds and 1- (4-sulfobutyl)-3-methylimidazolium based ionic liquids
- Extraction of benzene, ethylbenzene, and xylenes from n-heptane using binary mixtures of [4empy][Tf2N] and [emim][DCA] ionic liquids
- Study of interaction between organic compounds and mono or dicationic oxygenated ionic liquids using gas chromatography
- Liquid liquid equilibria in the ternary systems {hexadecane + BTX aromatics + 2-methoxyethanol or acetonitrile} at 298.15 K
- Isobaric vapor-liquid equilibrium of the binary system sec-butyl acetate + para-xylene and the quaternary system methyl acetate + para-xylene + sec-butyl acetate + acetic acid at 101.3 kPa
- Liquid-liquid phase diagrams of poly(ethylene glycol) and aromatic hydrocarbons
- Experimental study on liquid - liquid equilibria of ionic liquids + alkane + ethyl benzene or p-xylene at 298.15 K
- Measurement of infinite dilution partition coefficients of isomeric benzene derivatives in [bmim][Tf2N]-CO2 biphasic system and correlation with the ePC-SAFT equation of state
- Liquid-liquid extraction of p-xylene from their mixtures with alkanes using 1-butyl-1-methylmorpholinium tricyanomethanide and 1- butyl-3-methylimidazolium tricyanomethanide ionic liquids
- Activity coefficients at infinite dilution of organic solvents and water in 1-butyl-3-methylimidazolium dicyanamide. A literature review of hexane/hex-1-ene separation
- Vapor-liquid equilibria for n-heptane + (benzene, toluene, pxylene, or ethylbenzene) + {[4empy][Tf2N] (0.3) + [emim][DCA] (0.7)} binary ionic liquid mixture
- Vapour-liquid equilibrium for tripropylene glycol + aromatic hydrocarbons binary systems: Experimental data and regression
- Liquid-liquid equilibria for the extraction of furfural from aqueous solution using different solvents
- Abraham model linear free energy relationships for describing the partitioning and solubility behavior of nonelectrolyte organic solutes dissolved in pyridine at 298.15 K
- High selective water/butan-1-ol separation on investigation of limiting activity coefficients with [P8,8,8,8][[NTf2] ionic liquid
- Liquid densities for n-decane + p-xylene mixtures from 293.15 K to 363.15 K at pressures up to 60 MPa
- Separation of binary mixtures based on limiting activity coefficients data using specific ammonium-based ionic liquid and modelling of thermodynamic functions
- Determination and correlation of solubility of 2,2',4,4',6,6 '-hexanitro-1,1'-biphenyl and 2,2',2" ,4,4',4" ,6,6',6" -Nonanitro-1,1 ':3',1"-terphenyl in six pure solvents
- Thermodynamics and activity coefficients at infinite dilution for organic solutes in the ionic liquid 1-butyl-1-methylpyrrolidinium dicyanamide
- New ionic liquid [P4,4,4,4][NTf2] in bio-butanol extraction on investigation of limiting activity coefficients
- Ammonium ionic liquids in extraction of bio-butan-1-ol from water phase using activity coefficients at infinite dilution
- Application of trihexyltetradecylphosphonium dicyanamide ionic liquid for various types of separations problems: Activity coefficients at infinite dilution measurements utilizing GLC method
- (Vapour + liquid) equilibria of (1-butanol + benzene, or toluene, or o-, or m-, or p-xylene) at T = 308.15 K
- Volumetric properties of (cyclohexanone + a xylene) at temperature between (293.15 and 353.15) K
- Densities and volumetric properties of a (xylene + dimethyl sulfoxide) at temperature from (293.15 to 353.15) K
- A study of densities and volumetric properties of binary mixtures containing nitrobenzene at T = (293.15 to 353.15) K
- Excess volumes and partial molar volumes of binary mixtures of 1,2-propanediol carbonate with xylene in the temperature range of (293.15 to 353.15) K
- Liquid phase behaviour of 1-hexyloxymethyl-3-methyl-imidazolium-based ionic liquids with hydrocarbons: The influence of anion
- (Vapor + liquid) equilibria of binary mixtures formed by iso-octane with a variety of compounds at 95.8 kPa
- Systems with ionic liquids: Measurement of VLE and c1 data and prediction of their thermodynamic behavior using original UNIFAC, mod. UNIFAC(Do) and COSMO-RS(Ol)
- Excess and deviation properties for the binary mixtures of methylcyclohexane with benzene, toluene, p-xylene, mesitylene, and anisole at T = (298.15, 303.15, and 308.15) K
- Excess molar volumes and refractive indices of (methoxybenzene + benzene, or toluene, or o-xylene, or m-xylene, or p-xylene, or mesitylene) binary mixtures between T = (288.15 to 303.15) K
- Densities and volumetric properties of binary mixtures of xylene with N,N-dimethylformamide at different temperatures
- Thermodynamics of mixtures involving some (benzene derivatives + benzonitrile)
- A study of densities and volumetric properties of binary mixtures of N-methyl-2-pyrrolidone with xylene at different temperatures and atmospheric pressure
- Activity coefficients and excess Gibbs free energy of some binary mixtures formed by p-cresol at 95.23 kPa
- Measurement of activity coefficients at infinite dilution in 1-hexadecyl-3-methylimidazolium tetrafluoroborate ionic liquid
- Measurements of activity coefficients at infinite dilution of aromatic and aliphatic hydrocarbons, alcohols, and water in the new ionic liquid [EMIM][SCN] using GLC
- Activity coefficients at infinite dilution measurements for organic solutes and water in the ionic liquid triethylsulphonium bis(trifluoromethylsulfonyl)imide
- Surface tension, density, and speed of sound for the ternary mixture {diethyl carbonate + p-xylene + decane}
- Measurements of activity coefficients at infinite dilution of aliphatic and aromatic hydrocarbons, alcohols, thiophene, tetrahydrofuran, MTBE, and water in ionic liquid [BMIM][SCN] using GLC
- Excess thermodynamic functions derived from densities and surface tensions of (p- or o-xylene + ethylene glycol dimethyl ether) between the temperatures (298.15 and 308.15) K
- Activity coefficients at infinite dilution measurements for organic solutes and water in the ionic liquid 4-methyl-N-butyl-pyridinium bis(trifluoromethylsulfonyl)-imide
- (Liquid + liquid) equilibria in the binary systems (aliphatic, or aromatic hydrocarbons + 1-ethyl-3-methylimidazolium ethylsulfate, or 1-butyl-3-methylimidazolium methylsulfate ionic liquids)
- LLE data for the ionic liquid 3-methyl-N-butyl pyridinium dicyanamide with several aromatic and aliphatic hydrocarbons
- Gas liquid chromatography measurements of activity coefficients at infinite dilution of various organic solutes and water in tri-iso-butylmethylphosphonium tosylate ionic liquid
- Activity coefficients at infinite dilution of organic solutes in the ionic liquid 1-ethyl-3-methylimidazolium tetracyanoborate [EMIM][TCB] using gas liquid chromatography
- Measurements of activity coefficients at infinite dilution of organic solutes and water in 1-propyl-1-methylpiperidinium bis{(trifluoromethyl)sulfonyl}imide ionic liquid using g.l.c.
- Activity coefficients at infinite dilution of organic solutes in N-alkylpyridinium bis(trifluoromethylsulfonyl)imide ([CnPY][NTf2], n = 2, 4, 5) using gas liquid chromatography
- Excess molar volumes, excess molar enthalpies, and excess isentropic compressibilities of tetrahydropyran with aromatic hydrocarbons
- Measurements of activity coefficients at infinite dilution of organic compounds and water in isoquinolinium-based ionic liquid [C8iQuin][NTf2] using GLC
- Activity coefficients at infinite dilution measurements for organic solutes and water in the ionic liquid 1-ethyl-3-methylimidazolium tetracyanoborate
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(3-hydroxypropyl)pyridinium bis(trifluoromethylsulfonyl)-amide
- Physical properties of 3-methyl-N-butylpyridinium tetracyanoborate and 1-butyl-1-methylpyrrolidinium tetracyanoborate and ternary LLE data of [3-mebupy]B(CN)4 with an aromatic and an aliphatic hydrocarbon at T = 303.2 K and 328.2 K and p = 0.1 MPa
- Thermodynamics and activity coefficients at infinite dilution measurements for organic solutes and water in the ionic liquid 1-butyl-1-methylpyrrolidinium tetracyanoborate
- Thermophysical properties for (diethyl carbonate + p-xylene + octane) ternary system
- Volumetric properties of binary mixtures of tributylamine with benzene derivatives and comparison with ERAS model results at temperatures from (293.15 to 333.15) K
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 4-(2-methoxyethyl)-4-methylmorpholinium bis(trifluoromethylsulfonyl)-amide
- Measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-hexyl-3-methylimidazolium tetracyanoborate
- 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)}
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)-1-methylpiperidinium bis(trifluoromethylsulfonyl)-amide
- Measurement and correlation of phase equilibria for (water + aromatic hydrocarbon) binary mixtures at T = (573 to 623) K using microfluidic mixing
- Measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-ethyl-3-methylimidazolium methanesulfonate
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)-1-methylpyrrolidinium bis(trifluoromethylsulfonyl)-amide
- Liquid-liquid extraction of aromatics from their mixtures with alkanes using 1-methyl 3-octylimidazolium thiocyanate ionic liquid
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 4-(2-methoxyethyl)-4-methylmorpholinium trifluorotris(perfluoroethyl)phosphate
- Effect of temperature and composition on the density, refractive index, and excess quantities of binary mixtures of 2,4,6,8-tetramethyl-2,4,6,8- tetraethenylcyclotetrasiloxane with aromatic hydrocarbons
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)- 1-methylpiperidinium trifluorotris(perfluoroethyl)phosphate
- Physicochemical properties and activity coefficients at infinite dilution for organic solutes and water in a novel bicyclic guanidinium superbase-derived protic ionic liquid
- Acoustic and thermodynamic properties of binary mixtures of 1-nonanol with o-xylene, m-xylene, p-xylene, ethylbenzene and mesitylene at T = (298.15 and 308.15) K
- Experimental and theoretical study on infinite dilution activity coefficients of various solutes in piperidinium ionic liquids
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)- 1-methylpyrrolidinium trifluorotris(perfluoroethyl)phosphate
- Phase equilibria for the [{water + 1-methylnaphthalene + p-xylene}] system at T = (573, 623 and 653) K
- Measurements of activity coefficients at infinite dilution for organic solutes and water in N-hexylisoquinolinium thiocyanate, [HiQuin][SCN] using GLC
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-hydroxyethyl)- 3-methylimidazolium trifluorotris(perfluoroethyl)phosphate
- Measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-butyl-1-methylpyrrolidinium tricyanomethanide
- Phase behaviour of aqueous mixtures of acetic acid with isomers of xylene
- Thermodynamics and activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-butyl-1-methylmorpholinium tricyanomethanide
- The study of activity coefficients at infinite dilution for organic solutes and water in 1-butyl-4-methylpyridinium dicyanamide, [B4MPy][DCA] using GLC
- Experimental and Nitta-Chao model prediction of high pressure density of p-xylene with dialkyl carbonates or n-alkanes
- Measurement of activity coefficients at infinite dilution of organic solutes in the ionic liquid 1-hexyl-1,4-diaza[2.2.2]bicyclooctanium bis(trifluoromethylsulfonyl)imide using gas-liquid chromatography
- Activity coefficients at infinite dilution of organic solutes in 1-hexyl-3- methylimidazolium trifluoroacetate and influence of interfacial adsorption using gas liquid chromatography
- Activity coefficients at infinite dilution of organic solutes in the ionic liquid 1-butyl-3-methylimidazolium methyl sulfate
- Thermodynamics and activity coefficients at infinite dilution for organic solutes, water and diols in the ionic liquid choline bis(trifluoromethylsulfonyl)imide
- Thermodynamics of solvation in propylene glycol and methyl cellosolve
- Isothermal (liquid + liquid) equilibrium data at T = 313.15 K and isobaric (vapor + liquid + liquid) equilibrium data at 101.3 kPa for the ternary system (water + 1-butanol + p-xylene)
- Measurement and correlation of solubility of 4-chloro-2,5-dimethoxynitrobenzene and 4-chloro-2,5- dimethoxyaniline in methanol, ethanol, xylene and toluene
- Solvation parameter model and thermodynamic parameters in a dicationic ionic liquid based on pyrrolidinium
- Experimental and theoretically study of interaction between organic compounds and tricyanomethanide based ionic liquids
- Activity coefficients at infinite dilution of organic solutes in methylphosphonate based ionic liquids using gas-liquid chromatography
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 4-(3-hydroxypropyl)-4-methylmorpholinium bis(trifluoromethylsulfonyl)-amide
- Activity coefficients at infinite dilution for organic solutes and water in 1-ethyl-1-methylpyrrolidinium lactate
- Activity coefficients at infinite dilution, physicochemical and thermodynamic properties for organic solutes and water in the ionic liquid ethyl-dimethyl-(2-methoxyethyl)ammonium trifluorotris-(perfluoroethyl)phosphate
- Activity coefficients at infinite dilution of alkanes, alkenes, alkyl benzenes in dimethylphosphate based ionic liquids using gas liquid chromatography
- Viscosity measurements of ortho-xylene, meta-xylene, para-xylene and ethylbenzene
- Selective recovery of aliphatics from aromatics in the presence of the {[4empy][Tf2N] + [emim][DCA]} ionic liquid mixture
- A 1-alkylcyanopyridinium-based ionic liquid in the separation processes
- Liquid-liquid equilibria for ternary systems polyoxymethylene dimethyl ethers + para-xylene + water
- Thermodynamics and selectivity of separation based on activity coefficients at infinite dilution of various solutes in 1-allyl-3-methylimidazolium bis{(trifluoromethyl)sulfonyl}imide ionic liquid
- Separation of aliphatic from aromatic hydrocarbons and sulphur compounds from fuel based on measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid N,N-diethyl-N-methyl-N-(2-methoxy-ethyl)ammonium bis(trifluoromethylsulfonyl)imide
- Thermodynamics and activity coefficients at infinite dilution for organic solutes in the ionic liquid 1-hexyl-2,3-dimethylimidazolium bis(trifluoromethylsulfonyl)imide
- Thermodynamics and limiting activity coefficients measurements for organic solutes and water in the ionic liquid 1-dodecyl-3-methylimidzolium bis(trifluoromethylsulfonyl) imide
- Determination of melting temperatures in hydrocarbon mixtures by differential scanning calorimetry
- Physicochemical study of intermolecular interactions in 1,4-dioxane + aromatic hydrocarbons binary mixtures at different temperatures by using ultrasonic and viscometric methods
- Separation of binary mixtures hexane/hex-1-ene, cyclohexane/cyclohexene and ethylbenzene/styrene based on limiting activity coefficients
- Thermodynamics and activity coefficients at infinite dilution for organic compounds and water in the ionic liquid 1-butyl-3-methylimidazolium perchlorate
- Separation of azeotrope (2,2,3,3-tetrafluoro-1-propanol + water): Isobaric vapour-liquid phase equilibrium measurements and azeotropic distillation
- New aspects of relationship between the enthalpies of fusion of aromatic compounds at the melting temperatures and the enthalpies of solution in benzene at 298.15 K. Part I
- Separation of water/butan-1-ol based on activity coefficients at infinite dilution in 1,3-didecyl-2-methylimidazolium dicyanamide ionic liquid
- Separation of binary mixtures hexane/hex-1-ene, cyclohexane/cyclohexene and ethylbenzene/styrene based on gamma infinity data measurements
- Separation of binary mixtures based on gamma infinity data using [OMMIM][NTf2] ionic liquid and modelling of thermodynamic functions
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid trihexyl-tetradecyl-phosphonium tricyanomethanide
- Thermodynamic study of molecular interaction-selectivity in separation processes based on limiting activity coefficients
- Abraham model correlations for describing the thermodynamic properties of solute transfer into pentyl acetate based on headspace chromatographic and solubility measurements
- Thermodynamics and selectivity of separation based on activity coefficients at infinite dilution of various solutes in ionic liquid [HMMIM][BF4]
- The use of ionic liquids for separation of binary hydrocarbons mixtures based on gamma infinity data measurements
- Thermodynamics and activity coefficients at infinite dilution for organic compounds in the ionic liquid 1-hexyl-3-methylimidazolium chloride
- Separation of binary mixtures based on gamma infinity data using [OMMIM][BF4] ionic liquid and modelling of thermodynamic functions
- Determination of the thermodynamic parameters of ionic liquid 1-propyl-3-methylimidazolium bromide by gas-liquid chromatography
- Thermodynamic characterization of binary mixtures of poly(propylene glycol) 425 with toluene and o-, m- and p-xylenes
- Vapour-liquid equilibrium measurements and extractive distillation process design for separation of azeotropic mixture (dimethyl carbonate + ethanol)
- Speed of sound and derived thermodynamic properties of para-xylene at temperatures between (306 and 448) K and at pressures up to 66 MPa
- Separation of (water/butan-1-ol) binary systems based on activity coefficients at infinite dilution with phosphonium ionic liquid
- Molecular interactions in binary mixtures containing o-toluidine
- Excess molar volumes and excess isentropic compressibilities of 2-pyrrolidinone at 308.15K
- Excess Molar Enthalpies for Binary and Ternary Mixtures containing Cyclic Ether, 2-Methylaniline and Aromatic Hydrocarbons
- Calorimetric study of solvation of low polar solutes in propylene glycol and methyl cellosolve at 298 K
- Examination of hydrogen-bonding interactions between dissolved solutes and alkylbenzene solvents based on Abraham model correlations derived from measured enthalpies of solvation
- Effect of halogen substitution on the enthalpies of solvation and hydrogen bonding of organic solutes in chlorobenzene and 1,2-dichlorobenzene derived using multi-parameter correlations
- Standard molar Gibbs free energy and enthalpy of solvation of lowpolar solutes in formamide derivatives at 298 K
- Relative Permittivity and Apparent Dipole Moments of Nitromethane, Nitroethane, 1-Nitropropane and 2- Nitropropane in Several Nonpolar Solvents.
- Activity Coefficients at Infinite Dilution of Organic Solutes and Water in Tributylethylphosphonium Diethylphosphate Using Gas Liquid Chromatography: Thermodynamic Properties of Mixtures Containing Ionic Liquids
- Investigation on Thermodynamics in Separation for Ethylene Glycol + Neopentyl Glycol System by Azeotropic Distillation
- Liquid Liquid Equilibria, Equilibrium Phase Densities, and Refractive Indices for the Quaternary Mixtures Containing 2-Propanol or 2-Methyl-2-Propanol of Fuel Oxygenate at T = 298.15 and 318.15 K
- Isobaric Vapor Liquid Equilibrium for the Binary Systems of Diethyl Carbonate with Xylene Isomers and Ethylbenzene at 101.33 kPa
- Mutual solubility of aromatic hydrocarbons in pyrrolidinium and ammonium-based ionic liquids and its modeling using the Cubic-Plus-Association (CPA) Equation of State
- Elimination of Tar in Biomass Gasification Process: Liquid Liquid Equilibrium of Ternary Systems {Water + Solvent (p-Xylene and Methyl Hexadecanoate) + Model Molecules of Tar (Thiophene, Pyridine, Naphthalene, Phenathrene, and Anthracene)}
- Isobaric Vapor Liquid Equilibrium for Binary Systems of Cyclohexanone + Benzene, Cyclohexanone + Toluene, and Cyclohexanone + p-Xylene at 101.3 kPa
- Liquid Liquid Equilibria Data for Ethylbenzene or p-Xylene with Alkane and 1-Butylpyridinium Nitrate Ionic Liquid at 298.15 K
- Liquid Liquid Equilibria of Binary, Ternary, and Quaternary Systems Involving Monoethylene Glycol, Water, Toluene, p-Xylene, Hexane, and Octane
- Experimental Determination and Correlation of Liquid Liquid Equilibria for Water + Cyclohexanone + Solvents (Toluene or p-Xylene) Ternary Systems at 303.15 and 323.15 K under 101.3 kPa
- Isobaric Vapor Liquid Equilibrium Data for the Binary Systems of Dimethyl Carbonate with Xylene Isomers at 93.13 kPa
- Determination and Correlation of Liquid-Liquid Equilibria Data for Water + Cyclohexanol + (Mesityl Oxide, Toluene, and p-Xylene) Ternary Systems at Different Temperatures
- Viscometric Studies of Molecular Interactions in Binary Liquid Mixtures of Isomeric Xylenes with Methanol
- Determination of Activity Coefficients at Infinite Dilution of Organic Solutes in the Ionic Liquid 1-(2-Hydroxyethyl)-3-methylimidazolium Nonafluoro-1-butanesulfonate Using Gas-Liquid Chromatography
- Refractive Index and Vapor-Liquid Equilibrium Data for the Binary Systems of Anisole with Xylene Isomers at 93.13 kPa
- Thermodynamic Parameters of a New Synthesized Tricationic Ionic Liquid Stationary Phase by Inverse Gas Chromatography
- Determination of Activity Coefficients at Infinite Dilution of Solutes in N,N'-Di(2-ethylhexyl)isobutyramide Using Inverse Gas-Liquid Chromatography
- Isobaric Vapor-Liquid Equilibrium Measurements for Separation of Azeotrope (Methanol + Methyl Acetate)
- Separation of Alkylbenzenes from n-Heptane Using Binary Mixtures of Ionic Solvents
- Determination and Correlation of Solubility of Borneol, Camphor, and Isoborneol in Different Solvents
- Assessment of Pyrrolidinium-Based Ionic Liquid for the Separation of Binary Mixtures Based on Activity Coefficients at Infinite Dilution
- Liquid-liquid equilibria for mixtures of (Furfural + an Aromatic hydrocarbon + an alkane) at T=298.15 K
- Excess Molar Entalpies of Dimethyl Carbonate with o-Xylene, m-Xylene, p-Xylene, Ethylbenzene, or Ethyl Benzoate at 298.15 K
- Solubility of 1-Alkyl-3-methylimidazolium Hexafluorophosphate in Hydrocarbons
- Excess Molar Enthalpies for Dimethyl Carbonate with o-Xylene, m-Xylene, p-Xylene, Ethylbenzene or Ethyl Benzoate at 298.15 K and 10.2 MPa
- Excess Molar Volumes and Surface Tensions of Xylene with 2-propanol or 2-methyl-2-propanol at 298.15 K
- Densities, Excess Molar Volumes, Viscosities, Speeds of Sound, Excess Isentropic Compressibilities, and Relative Permittivities for CmH2m+1(OCH2CH2)nOH (m ) 1 or 2 or 4 andn ) 1) + Benzene, + Toluene, + (o-, m-, and p-) Xylenes, + Ethylbenzene, and + Cyclohexane
- Densities, Excess Molar Volumes at T = (298.15 to 313.15) K, Speeds of Sound, Excess Isentropic Compressibilities, Relative Permittivities and Deviations in Molar Polarizations at T = (298.15 and 308.15) K for Methyl Methacrylate + 2-Butoxyethanol or + Dibutyl Ether + Benzene, + Toluene and + p-Xylene
- Liquid-Liquid Equilibria for Binary Mixtures of Water + Benzene, + Toluene, and + p-Xylene from 273 K to 458 K
- Thermal Conductivity and Thermal Diffusivity of Twenty-Nine Liquids: Alkenes, Cyclic (Alkanes, Alkenes, Alkadienes, Aromatics), and Deuterated Hydrocarbons
- Excess Molar Volumes and Surface Tensions of Xylene with Acetone or 2-Butanone at 298.15 K
- Excess Molar Volumes and Viscosities of Binary Mixtures of Sulfolane with Benzene, Toluene, Ethylbenzene, p-Xylene, o-Xylene, and m-Xylene at 303.15 and 323.15 K and Atmospheric Pressure
- Isobaric Vapor-Liquid Equilibria for Binary and Ternary Mixtures of Ethanol, Methylcyclohexane and p-Xylene
- Excess Molar Volumes and Surface Tensions of Xylene with Isopropyl Ether or Methyl tert-Butyl Ether at 298.15 K
- Viscosity, Density, and Refractive Index of Some (Ester + Hydrocarbon) Binary Mixtures at 303.15 K and 313.15 K
- Vapor-Liquid Equilibria Data for Binary Systems of Ethylbenzene + Xylene Isomers at 100.65 kPa
- Thermodynamic Properties of Binary Mixtures of p-Xylene with Cyclohexane, Heptane, Octane, and N-Methyl-2-pyrrolidone at Several Temperatures
- Viscosities, Densities, and Speeds of Sound of Binary Mixtures of o-Xylene, m-Xylene, p-Xylene, and Isopropylbenzene with 2-Butanone at 298.15 K
- Viscosities, Densities, and Speeds of Sound of Binary Mixtures of o-Xylene, m-Xylene, p-Xylene, and Isopropylbenzene with 4-Methylpentan-2-one at 298.15 K
- Isobaric Vapor-Liquid Equilibria at 97.3 kPa and Excess Properties at (303.15, 308.15, and 313.15) K of Binary Mixture of p-Xylene + Decane
- Vapor-Liquid Equilibria and Excess Properties of the Binary System Vinyl Acetate + p-Xylene
- Determination of Partitioning Coefficients of Numerous Organic Solutes between a Long-Chain Aliphatic Alcohol and the Gas Phase as a Function of Temperature
- Solubilities of 2-(6-Oxido-6H-dibenz[c,e][1,2]oxaphosphorin-6-yl)-methanol in the Selected Solvents
- Isobaric Vapor-Liquid Equilibria for the Binary Mixtures of Styrene with Ethylbenzene, o-Xylene, m-Xylene, and p-Xylene
- Solubilities of Benzene, Toluene, and Xylene Isomers in 1-Butyl-3-methylimidazolium Tetrafluoroborate
- Activity Coefficients at Infinite Dilution of Alkanes, Alkenes, and Alkyl Benzenes in 1-Butyl-3-methylimidazolium Tetrafluoroborate Using Gas-Liquid Chromatography
- Viscosities, Densities, and Speeds of Sound of Binary Mixtures of Benzene, Toluene, o-Xylene, m-Xylene, p-Xylene, and Mesitylene with Anisole at (288.15, 293.15, 298.15, and 303.15) K
- Henry's Law Constants and Infinite Dilution Activity Coefficients of Propane, Propene, Butane, 2-Methylpropane, 1-Butene, 2-Methylpropene, trans-2-Butene, cis-2-Butene, 1,3-Butadiene, Dimethyl Ether, Chloroethane, and 1,1-Difluoroethane in Benzene, Toluene, o-Xylene, m-Xylene, p-Xylene, and Styrene
- Densities and Surface Tensions of Propyl Acetate + Xylenes or + Ethylbenzene from (298.15 to 308.15) K
- Activity Coefficients at Infinite Dilution Measurements for Organic Solutes and Water in the Ionic Liquid 1-Butyl-3-methyl-pyridinium Trifluoromethanesulfonate
- Volumetric and Viscometric Behavior of the Binary System: (Hexan-1-ol + p-Xylene)
- Determination of Activity Coefficients at Infinite Dilution of 35 Solutes in the Ionic Liquid, 1-Butyl-3-methylimidazolium Tosylate, Using Gas-Liquid Chromatography
- Vapor-Liquid Equilibria and Density Measurement for Binary Mixtures of Benzene + Nonane, Methylbenzene + 1,2-Dimethylbenzene, 1,3-Dimethylbenzene + 2,3,4,5-Tetrahydrothiophene-1,1-dioxide (Sulfolane), 1,2-Dimethylbenzene + Sulfolane, 1,2-Dimethylbenzene + N-Methylformamide (NMF), 1,3-Dimethylbenzene + NMF, and 1,4-Dimethylbenzene + NMF from (333.15 to 353.15) K at Vacuum Conditions
- Densities, Speeds of Sound, Excess Molar Volumes, and Excess Isentropic Compressibilities at T = (298.15 and 308.15) K for Methyl Methacrylate + 1-Alkanols (1-Butanol, 1-Pentanol, and 1-Heptanol) + Cyclohexane, + Benzene, + Toluene, + p-Xylene, and + Ethylbenzene
- Densities, Speeds of Sound, and Isentropic Compressibilities of Binary Mixtures of {Alkan-1-ols + 1,2-Dimethylbenzene, or 1,3-Dimethylbenzene, or 1,4-Dimethylbenzene, or Ethylbenzene} at (293.15, 303.15, and 313.15) K
- Density and Viscosity of the Binary Mixtures of Hexan-1-ol with Isomeric Xylenes at T = (308.15 and 318.15) K and Atmospheric Pressure
- Activity Coefficients at Infinite Dilution of Organic Solutes in 1-Decyl-3-methylimidazolium Tetrafluoroborate Using Gas-Liquid Chromatography
- Measurements of Activity Coefficients at Infinite Dilution for Organic Solutes and Water in the Ionic Liquid 1-Butyl-1-methylpiperydinium Thiocyanate
- Activity Coefficients at Infinite Dilution of Organic Solutes in 1-Butyl-3-methylimidazolium Nitrate Using Gas-Liquid Chromatography
- Solubilities of 1-Hexyl-3-methylimidazole Nitrate and 1-Octyl-3-methylimidazole Nitrate in Selected Solvents
- Activity Coefficients at Infinite Dilution of Organic Compounds in Four New Imidazolium-Based Ionic Liquids
- Activity Coefficients at Infinite Dilution of Alkanes, Alkenes, and Alkyl Benzenes in 1-Ethyl-3-methylimidazolium Diethylphosphate Using Gas Liquid Chromatography
- Partition Coefficients of Organic Compounds in Four New Tetraalkylammonium Bis(trifluoromethylsulfonyl)imide Ionic Liquids Using Inverse Gas Chromatography
- Ebulliometric Determination and Prediction of Vapor Liquid Equilibria for Binary Mixtures of Ethanol and Ethyl Hexanoate
- Excess Molar Volumes of 2,4,6,8-Tetramethylcyclotetrasiloxane with Benzene, Toluene, and Xylene at T = (288.15, 298.15, and 308.15) K
- Isobaric Vapor-Liquid Equilibium for the Binary Systems of Methyl Formate with o-Xylene, m-Xylene, p-Xylene, and Ethylbenzene at 101.33 kPa
- Isobaric vapor liquid equilibium for the binary systerms of 1-butanol with o-xylene, m-xylene, p-xylene, and ethylbenzene at 101.33 kPa
- Evaluation of the Performance of Trigeminal Tricationic Ionic Liquids for Separation Problems
- Evaluation of the Performance of Four Solvents for the Liquid Liquid Extraction of Acrylic Acid from Water
- Densities, Excess Molar Volumes, Viscosity, and Refractive Indices of Binary Mixtures of Ethanoic Acid and Trichloroethylene with Dimethylbenzenes at Different Temperatures
- Activity Coefficients at Infinite Dilution of Alkanes, Alkenes, and Alkyl Benzenes in 1-Butyl-3-methylimidazolium Dibutylphosphate Using Gas Liquid Chromatography
- Activity Coefficients at Infinite Dilution for Organic Compounds Dissolved in 1-Alkyl-1-methylpyrrolidinium Bis(trifluoromethylsulfonyl)imide Ionic Liquids Having Six-, Eight-, and Ten-Carbon Alkyl Chains
- Isobaric Vapor Liquid Equilibria for Binary Systems Comprising 1-Chloro-2-ethylhexane, 2-Ethyl-1-hexanol, p-Xylene, and N-Methylpyrrolidone (NMP) at 40.0 kPa
- Determination of Henry's Law Constants Using Internal Standards with Benchmark Values
- Vapor Liquid Equilibrium for 2-Methyl-1-butanol + Ethylbenzene + Xylene Isomers at 101.33 kPa
- Surface Tension of Dialkyl Carbonates + (Alkanes or 1,4-Dimethylbenzene) and 1,4-Dimethylbenzene + Alkanes Binary Mixtures at T = 308.15 K
- Activity Coefficients at Infinite Dilution for Organic Solutes Dissolved in Three 1-Alkyl-1-methylpyrrolidinium Bis(trifluoromethylsulfonyl)imide Ionic Liquids Bearing Short Linear Alkyl Side Chains of Three to Five Carbons
- Liquid Liquid Equilibria for the Ternary Systems of 4-Methyl-1,3-dioxolan-2-one + 1,4-Dimethylbenzene + Octane, Decane, or Dodecane and the Ternary Systems of Acetonitrile + Morpholine + Octane, Decane, or Dodecane at 313.15 K or 298.15 K
- Isobaric Vapor Liquid Equilibrium for Binary Systems of 2,2,4-Trimethylpentane with o-Xylene, m-Xylene, p-Xylene, and Ethylbenzene at 250 kPa
- Infinite Dilution Activity Coefficients of Solutes Dissolved in Two Trihexyl(tetradecyl)phosphonium Ionic Liquids
- Liquid Liquid Equilibria at Three Temperatures (between 280.15 K and 333.15 K) of Binary, Ternary, and Quaternary Systems Involving Monoethylene Glycol, Water, Cyclohexane, para-Xylene, trans- and cis-Dimethylcyclohexane, and trans- and cis-Decahydronaphthalene
- Deduction of Physicochemical Properties from Solubilities: 2,4-Dihydroxybenzophenone, Biotin, and Caprolactam as Examples
- Activity Coefficients at Infinite Dilution of Alkanes, Alkenes, and Alkyl Benzenes in 1-Propyl-2,3-dimethylimidazolium Tetrafluoroborate Using Gas-Liquid Chromatography
- Measurement of Activity Coefficient at Infinite Dilution of Hydrocarbons in Sulfolane Using Gas-Liquid Chromatography
- Densities and Viscosities of N-Formylmorpholine (NFM) + p-Xylene, + o-Xylene, + m-Xylene at Different Temperatures and Atmospheric Pressure
- Activity Coefficients at Infinite Dilution of Alkanes, Alkenes, and Alkyl Benzenes in 1-Butyl-3-methylimidazolium Trifluoromethanesulfonate Using Gas-Liquid Chromatography
- Molar Excess Volume of sec- and tert-Butyl Chloride with Aromatic Hydrocarbons at T = 298.15 K
- Effect of an Ionic Liquid (IL) Cation on the Ternary System (IL + p-Xylene + Hexane) at T= 298.15 K
- Solubilities of Vitamin K3 in Benzene, Toluene, Ethylbenzene, o-Xylene, m-Xylene, and p-Xylene between (299.44 and 344.24) K
- Excess Enthalpies of (N-Methylformamide or N-Methylacetamide) + Aromatic Compounds at 303.15 K
- Refractive Indices of Binary Mixtures of Tetrahydrofuran with Aromatic Hydrocarbon at Temperatures from (288.15 to 318.15) K
- Vapor Liquid Equilibrium of N-Formylmorpholine with Toluene and Xylene at 101.33 kPa
- Measuring Surface Tension of Liquids at High Temperature and Elevated Pressure
- Densities and Viscosities of Binary Mixtures of Vitamin K3 with Benzene, Toluene, Ethylbenzene, o-Xylene, m-Xylene, and p-Xylene from (303.15 to 333.15) K
- Activity Coefficients at Infinite Dilution of Alkanes, Alkenes, and Alkyl Benzenes in 1-Hexyl-3-methylimidazolium Trifluoromethanesulfonate Using Gas-Liquid Chromatography
- Enthalpies of Vaporization and Vapor Pressures of Some Deuterated Hydrocarbons. Liquid-Vapor Pressure Isotope Effects
- Molar Excess Volumes and Excess Isentropic Compressibilities of Ternary Mixtures of o-Toluidine
- Activity Coefficients at Infinite Dilution of Organic Solutes in 1-Ethyl-3-methylimidazolium Tetrafluoroborate Using Gas-Liquid Chromatography
- Measurement of Infinite Dilution Activity Coefficients of Alcohols, Ketones, and Aromatic Hydrocarbons in 4-Methyl-N-butylpyridinium Tetrafluoroborate and 1-Butyl-3-methylimidazolium Hexafluorophosphate by Gas-Liquid Chromatography
- Thermophysical Properties of Isoamyl Acetate or Methyl Benzoate + Hydrocarbon Binary Mixtures, at (303.15 and 313.15) K
- Densities, Refractive Indices, and Excess Properties of Binary Mixtures of 1,4-Dioxane with Benzene, Toluene, o-Xylene, m-Xylene, p-Xylene, and Mesitylene at Temperatures from (288.15 to 318.15) K
- Analysis of Surface Tension, Density, and Speed of Sound for the Ternary Mixture Dimethyl Carbonate + p-Xylene + n-Octane
- Viscosities of p-Xylene, Acetic Acid, and p-Xylene + Acetic Acid at (313.15 to 473.15) K and (0.10 to 3.20) MPa: Determined by the Rolling-Ball Method
- Activity Coefficients at Infinite Dilution of Organic Compounds in 1-Butyl-3-methylimidazolium Tetrafluoroborate Using Inverse Gas Chromatography
- Densities and Viscosities of Binary Mixtures of Methyl 4-Chlorobutyrate with Aromatic Hydrocarbons at T ) (298.15 to 318.15) K
- Molar Excess Volumes and Excess Isentropic Compressibilities of {2-Methylaniline (i) + Benzene (j) + Methylbenzene}, {2-Methylaniline (i) + Benzene (j) + 1,2-Dimethylbenzene (k)}, and {2-Methylaniline (i) + Benzene (j) + 1,4-Dimethylbenzene (k)} at T = 308.15 K
- Activity Coefficients at Infinite Dilution of Alkanes, Alkenes, and Alkyl Benzenes in 1-(2-Hydroxyethyl)-3-methylimidazolium Tetrafluoroborate Using Gas-Liquid Chromatography
- Solubilities of Methyldiphenylphosphine Oxide in Selected Solvents
- Partition Coefficients of Organic Compounds in New Imidazolium and Tetralkylammonium Based Ionic Liquids Using Inverse Gas Chromatography
- Surface Tension Deviations and Excess Molar Volumes on the Ternary System Propyl Propanoate + Hexane + p-Xylene at 298.15 K
- Activity Coefficients at Infinite Dilution of Alkanes, Alkenes, and Alkyl Benzenes in Glycerol Using Gas-Liquid Chromatography
- Study of Ether-, Alcohol-, or Cyano-Functionalized Ionic Liquids Using Inverse Gas Chromatography
- Activity Coefficients at Infinite Dilution of Organic Solutes in 1-Ethyl-3-methylimidazolium Tris(pentafluoroethyl)trifluorophosphate [EMIM][FAP] Using Gas-Liquid Chromatography
- Activity Coefficients at Infinite Dilution Measurements for Organic Solutes and Water in the Ionic Liquid 1-Hexyl-3-methylimidazolium Thiocyanate
- Density, Speed of Sound, and Refractive Index for Binary Mixtures Containing Cycloalkanes with o-Xylene, m-Xylene, p-Xylene, and Mesitylene at T = (298.15 and 313.15) K
- Solubility of Triadimefon in Organic Solvents at Temperatures between (288.15 and 333.15) K
- Joback Method
- KDB
- Aqueous Solubility Prediction Method
- Estimated Solubility Method
- McGowan Method
- NIST Webbook
- NCMS SOLV-DB
- The Yaws Handbook of Vapor Pressure
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