- InChI
- InChI=1S/C10H14/c1-3-9-5-7-10(4-2)8-6-9/h5-8H,3-4H2,1-2H3
- InChI Key
- DSNHSQKRULAAEI-UHFFFAOYSA-N
- Formula
- C10H14
- SMILES
- CCc1ccc(CC)cc1
- Molecular Weight1
- 134.22
- CAS
- 105-05-5
- Other Names
-
- 1,4-diethylbenzene
- Benzene, p-diethyl-
- l,.l-diethylbenzene
- p-Ethylethylbenzene
- p-diethylbenzene
- para-Diethylbenzene
- ω : Acentric Factor.
- 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).
- ΔfG° : Standard Gibbs free energy of formation (kJ/mol).
- ΔfH°gas : Enthalpy of formation at standard conditions (kJ/mol).
- ΔfH°liquid : Liquid phase enthalpy of formation at standard conditions (kJ/mol).
- ΔfusH° : Enthalpy of fusion at standard conditions (kJ/mol).
- 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).
- Pc : Critical Pressure (kPa).
- Ptriple : Triple Point Pressure (kPa).
- Pvap : Vapor pressure (kPa).
- n0 : Refractive Index.
- ρl : Liquid Density (kg/m3).
- Inp : Non-polar retention indices.
- Ip : Polar retention indices.
- 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).
- Ttriple : Triple Point Temperature (K).
- UQi : UNIQUAC Qi Parameter.
- URi : UNIQUAC Ri Parameter.
- Vc : Critical Volume (m3/kmol).
- Zc : Critical Compressibility.
- Zra : Rackett Parameter.
- 1: Molecular weight from the IUPAC atomic weights tables.
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Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ω | [0.4030; 0.4090] |
|
|
| ω | 0.4090 | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value | |
| ω | 0.4031 | Passut and Danner (1973), critical constants and acentric factors Compiled value | |
| ω | 0.4030 | ChemSep v8.3 pure component data Compiled value | |
| ω | 0.4040 | KDB | |
| ΔcH°liquid | [-5863.08; -5862.90] | kJ/mol |
|
| ΔcH°liquid | -5863.08 ± 0.79 | kJ/mol | NIST |
| ΔcH°liquid | -5862.90 ± 1.80 | kJ/mol | NIST |
| μ | 0.00 | debye | ChemSep v8.3 pure component data Compiled value |
| ΔfG° | 138.50 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | -22.30 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°liquid | [-73.10; -72.84] | kJ/mol |
|
| ΔfH°liquid | -72.84 ± 0.96 | kJ/mol | NIST |
| ΔfH°liquid | -73.10 ± 1.80 | kJ/mol | NIST |
| ΔfusH° | 15.31 | kJ/mol | Joback Calculated Property |
| ΔvapH° | 52.50 | kJ/mol | NIST |
| IE | [8.40; 8.43] | eV |
|
| IE | 8.40 | eV | NIST |
| IE | 8.40 | eV | NIST |
| IE | 8.43 | eV | NIST |
| log10WS | [-3.75; -3.75] |
|
|
| log10WS | -3.75 | Aq. Solubility Prediction | |
| log10WS | -3.75 | Estimated Solubility | |
| logPoct/wat | 2.811 | Crippen Calculated Property | |
| McVol | 128.000 | ml/mol | McGowan Calculated Property |
| Pc | [2800.00; 2803.00] | kPa |
|
| Pc | 2803.00 | kPa | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 3 Compiled value |
| Pc | 2802.65 | kPa | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Pc | 2802.72 | kPa | Passut and Danner (1973), critical constants and acentric factors Compiled value |
| Pc | 2803.00 | kPa | ChemSep v8.3 pure component data Compiled value |
| Pc | 2803.00 | kPa | KDB |
| Pc | Outlier 2800.00 ± 40.00 | kPa | NIST |
| Pc | 2803.00 ± 7.00 | kPa | NIST |
| Ptriple | 2.13e-04 | kPa | ChemSep v8.3 pure component data Compiled value |
| Inp | [1029.00; 1084.00] |
|
|
| Inp | 1045.00 | NIST | |
| Inp | 1038.00 | NIST | |
| Inp | 1045.25 | NIST | |
| Inp | 1047.00 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1048.00 | NIST | |
| Inp | 1040.00 | NIST | |
| Inp | 1040.00 | NIST | |
| Inp | 1058.00 | NIST | |
| Inp | 1042.00 | NIST | |
| Inp | 1048.00 | NIST | |
| Inp | 1053.00 | NIST | |
| Inp | 1059.00 | NIST | |
| Inp | 1036.80 | NIST | |
| Inp | 1039.30 | NIST | |
| Inp | 1047.90 | NIST | |
| Inp | 1053.40 | NIST | |
| Inp | 1059.30 | NIST | |
| Inp | 1037.10 | NIST | |
| Inp | 1033.80 | NIST | |
| Inp | 1036.80 | NIST | |
| Inp | 1039.30 | NIST | |
| Inp | 1040.00 | NIST | |
| Inp | 1033.82 | NIST | |
| Inp | 1032.00 | NIST | |
| Inp | 1036.70 | NIST | |
| Inp | 1037.10 | NIST | |
| Inp | 1039.10 | NIST | |
| Inp | 1055.00 | NIST | |
| Inp | 1039.00 | NIST | |
| Inp | Outlier 1068.00 | NIST | |
| Inp | 1045.25 | NIST | |
| Inp | 1042.00 | NIST | |
| Inp | 1048.00 | NIST | |
| Inp | 1046.80 | NIST | |
| Inp | Outlier 1070.10 | NIST | |
| Inp | 1056.00 | NIST | |
| Inp | 1040.50 | NIST | |
| Inp | 1040.66 | NIST | |
| Inp | 1040.69 | NIST | |
| Inp | 1041.00 | NIST | |
| Inp | 1036.00 | NIST | |
| Inp | 1036.33 | NIST | |
| Inp | 1039.17 | NIST | |
| Inp | 1042.04 | NIST | |
| Inp | 1053.74 | NIST | |
| Inp | 1057.31 | NIST | |
| Inp | 1060.01 | NIST | |
| Inp | 1039.00 | NIST | |
| Inp | 1044.00 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1048.00 | NIST | |
| Inp | 1053.00 | NIST | |
| Inp | 1030.00 | NIST | |
| Inp | 1042.00 | NIST | |
| Inp | 1048.00 | NIST | |
| Inp | 1053.00 | NIST | |
| Inp | 1045.00 | NIST | |
| Inp | 1045.00 | NIST | |
| Inp | Outlier 1069.00 | NIST | |
| Inp | 1051.00 | NIST | |
| Inp | 1043.00 | NIST | |
| Inp | 1038.00 | NIST | |
| Inp | 1029.00 | NIST | |
| Inp | 1066.00 | NIST | |
| Inp | 1055.00 | NIST | |
| Inp | Outlier 1080.00 | NIST | |
| Inp | 1040.00 | NIST | |
| Inp | 1040.00 | NIST | |
| Inp | 1047.00 | NIST | |
| Inp | 1047.00 | NIST | |
| Inp | 1040.70 | NIST | |
| Inp | 1037.00 | NIST | |
| Inp | 1039.00 | NIST | |
| Inp | 1041.00 | NIST | |
| Inp | 1042.00 | NIST | |
| Inp | 1043.00 | NIST | |
| Inp | Outlier 1084.00 | NIST | |
| Inp | 1039.00 | NIST | |
| Ip | [1283.60; 1353.00] |
|
|
| Ip | 1305.20 | NIST | |
| Ip | 1283.60 | NIST | |
| Ip | 1289.40 | NIST | |
| Ip | 1283.60 | NIST | |
| Ip | 1293.00 | NIST | |
| Ip | 1312.00 | NIST | |
| Ip | 1320.00 | NIST | |
| Ip | 1315.00 | NIST | |
| Ip | 1300.00 | NIST | |
| Ip | 1305.00 | NIST | |
| Ip | 1306.00 | NIST | |
| Ip | 1307.00 | NIST | |
| Ip | 1284.00 | NIST | |
| Ip | Outlier 1353.00 | NIST | |
| Ip | 1305.00 | NIST | |
| Ip | 1284.00 | NIST | |
| Ip | 1305.00 | NIST | |
| Ip | 1291.50 | NIST | |
| Ip | 1305.20 | NIST | |
| Ip | 1307.00 | NIST | |
| Ip | Outlier 1353.00 | NIST | |
| Tboil | [456.00; 457.00] | K |
|
| Tboil | 456.90 | K | ChemSep v8.3 pure component data Compiled value |
| Tboil | 456.94 | K | KDB |
| Tboil | 457.00 | K | NIST |
| Tboil | Outlier 456.00 ± 2.00 | K | NIST |
| Tboil | 456.80 ± 0.20 | K | NIST |
| Tboil | 457.00 ± 2.00 | K | NIST |
| Tboil | 456.75 ± 0.30 | K | NIST |
| Tboil | 456.90 ± 1.00 | K | NIST |
| Tboil | 457.00 ± 2.00 | K | NIST |
| Tboil | 456.75 ± 0.20 | K | NIST |
| Tboil | 456.90 ± 0.03 | K | NIST |
| Tboil | Outlier 456.00 ± 2.00 | K | NIST |
| Tboil | 456.90 ± 0.15 | K | NIST |
| Tboil | 456.90 ± 0.20 | K | NIST |
| Tboil | 457.00 ± 0.60 | K | NIST |
| Tboil | 456.91 ± 0.30 | K | NIST |
| Tboil | 456.75 ± 0.20 | K | NIST |
| Tboil | 456.90 ± 0.30 | K | NIST |
| Tboil | 456.80 ± 0.50 | K | NIST |
| Tboil | 456.89 ± 0.30 | K | NIST |
| Tboil | Outlier 456.15 ± 2.00 | K | NIST |
| Tc | [657.87; 657.96] | K |
|
| Tc | 657.90 | K | IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 3 Compiled value |
| Tc | 657.88 | K | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Tc | Outlier 657.96 | K | Passut and Danner (1973), critical constants and acentric factors Compiled value |
| Tc | 657.90 | K | ChemSep v8.3 pure component data Compiled value |
| Tc | 657.90 | K | KDB |
| Tc | 657.90 ± 0.50 | K | NIST |
| Tc | 657.89 ± 0.15 | K | NIST |
| Tc | 657.87 ± 0.03 | K | NIST |
| Tfus | [229.60; 230.32] | K |
|
| Tfus | 230.15 | K | Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value |
| Tfus | 230.30 | K | ChemSep v8.3 pure component data Compiled value |
| Tfus | 230.32 | K | KDB |
| Tfus | 230.21 | K | Aq. Solubility Prediction |
| Tfus | 229.90 ± 0.20 | K | NIST |
| Tfus | 229.60 ± 0.60 | K | NIST |
| Ttriple | 230.32 | K | ChemSep v8.3 pure component data Compiled value |
| UQi | 4.62 | ChemSep v8.3 pure component data Compiled value | |
| URi | 6.01 | ChemSep v8.3 pure component data Compiled value | |
| Vc | [0.478; 0.480] | m3/kmol |
|
| Vc | 0.478 | m3/kmol | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Vc | 0.480 | m3/kmol | ChemSep v8.3 pure component data Compiled value |
| Vc | 0.480 | m3/kmol | KDB |
| Zc | [0.2462180; 0.2470000] |
|
|
| Zc | 0.2470000 | ChemSep v8.3 pure component data Compiled value | |
| Zc | 0.2462180 | KDB | |
| Zra | 0.25 | ChemSep v8.3 pure component data Compiled value |
Temperature Dependent Properties
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | [39.37; 45.80] | kJ/mol | [416.50; 456.90] |
|
| ΔvapH | 45.80 | kJ/mol | 416.50 | NIST |
| ΔvapH | 39.37 | kJ/mol | 456.90 | KDB |
| n0 | 1.49245 | 298.15 | KDB |
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [134.87; 476.45] | 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 | 1.17030e+02 | |||
| Coefficient B | -7.55240e+02 | |||
| Coefficient C | 6.72924e+00 | |||
| Coefficient D | -3.77090e-04 | |||
| Coefficient E | 9.97210e-08 | |||
| Temperature range, min. | 200.00 | |||
| Temperature range, max. | 1500.00 | |||
| Cp,gas | 134.87 | J/mol×K | 200.00 | Calculated Property |
| Cp,gas | 200.01 | J/mol×K | 344.44 | Calculated Property |
| Cp,gas | 269.04 | J/mol×K | 488.89 | Calculated Property |
| Cp,gas | 325.11 | J/mol×K | 633.33 | Calculated Property |
| Cp,gas | 367.98 | J/mol×K | 777.78 | Calculated Property |
| Cp,gas | 400.57 | J/mol×K | 922.22 | Calculated Property |
| Cp,gas | 425.75 | J/mol×K | 1066.67 | Calculated Property |
| Cp,gas | 445.76 | J/mol×K | 1211.11 | Calculated Property |
| Cp,gas | 462.25 | J/mol×K | 1355.56 | Calculated Property |
| Cp,gas | 476.45 | J/mol×K | 1500.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | [204.00; 322.35] | J/mol×K | [230.32; 456.94] |
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 | 4.27170e+01 | |||
| Coefficient B | -1.41380e+01 | |||
| Coefficient C | 4.19824e+00 | |||
| Coefficient D | 5.02340e-03 | |||
| Coefficient E | -3.97150e-06 | |||
| Temperature range, min. | 230.32 | |||
| Temperature range, max. | 456.94 | |||
| Cp,liquid | 204.00 | J/mol×K | 230.32 | Calculated Property |
| Cp,liquid | 218.13 | J/mol×K | 255.50 | Calculated Property |
| Cp,liquid | 232.33 | J/mol×K | 280.68 | Calculated Property |
| Cp,liquid | 246.48 | J/mol×K | 305.86 | Calculated Property |
| Cp,liquid | 260.45 | J/mol×K | 331.04 | Calculated Property |
| Cp,liquid | 274.09 | J/mol×K | 356.22 | Calculated Property |
| Cp,liquid | 287.26 | J/mol×K | 381.40 | Calculated Property |
| Cp,liquid | 299.79 | J/mol×K | 406.58 | Calculated Property |
| Cp,liquid | 311.54 | J/mol×K | 431.76 | Calculated Property |
| Cp,liquid | 322.35 | J/mol×K | 456.94 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [0.0036095; 0.0001321] | Pa×s | [230.32; 550.00] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = exp(A + B/T + C·ln(T) + D·T^E) Y is η in Pa×s, T in K | |||
| Coefficient A | -1.17660e+01 | |||
| Coefficient B | 1.32230e+03 | |||
| Coefficient C | 7.50760e-02 | |||
| Coefficient D | -1.45180e-07 | |||
| Coefficient E | 2.00000e+00 | |||
| Temperature range, min. | 230.32 | |||
| Temperature range, max. | 550.00 | |||
| η | 0.0036095 | Pa×s | 230.32 | Calculated Property |
| η | 0.0016899 | Pa×s | 265.84 | Calculated Property |
| η | 0.0009464 | Pa×s | 301.36 | Calculated Property |
| η | 0.0005989 | Pa×s | 336.88 | Calculated Property |
| η | 0.0004135 | Pa×s | 372.40 | Calculated Property |
| η | 0.0003044 | Pa×s | 407.92 | Calculated Property |
| η | 0.0002352 | Pa×s | 443.44 | Calculated Property |
| η | 0.0001887 | Pa×s | 478.96 | Calculated Property |
| η | 0.0001560 | Pa×s | 514.48 | Calculated Property |
| η | 0.0001321 | Pa×s | 550.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | [56.81; 0.00] | kJ/mol | [230.32; 657.90] |
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 | 5.46871e+01 | |||
| Coefficient B | -1.55122e+00 | |||
| Coefficient C | 6.62184e+00 | |||
| Coefficient D | -8.19960e+00 | |||
| Coefficient E | 3.48631e+00 | |||
| Critical temperature, Tc (K) | 6.57900e+02 | |||
| Temperature range, min. | 230.32 | |||
| Temperature range, max. | 657.90 | |||
| ΔvapH | 56.81 | kJ/mol | 230.32 | Calculated Property |
| ΔvapH | 53.34 | kJ/mol | 277.83 | Calculated Property |
| ΔvapH | 49.71 | kJ/mol | 325.34 | Calculated Property |
| ΔvapH | 46.16 | kJ/mol | 372.85 | Calculated Property |
| ΔvapH | 42.75 | kJ/mol | 420.36 | Calculated Property |
| ΔvapH | 39.35 | kJ/mol | 467.86 | Calculated Property |
| ΔvapH | 35.62 | kJ/mol | 515.37 | Calculated Property |
| ΔvapH | 30.87 | kJ/mol | 562.88 | Calculated Property |
| ΔvapH | 23.67 | kJ/mol | 610.39 | Calculated Property |
| ΔvapH | 0.00 | kJ/mol | 657.90 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.64] | kPa | [335.02; 487.02] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.45880e+01 | |||
| Coefficient B | -4.01384e+03 | |||
| Coefficient C | -5.43350e+01 | |||
| Temperature range, min. | 335.02 | |||
| Temperature range, max. | 487.02 | |||
| Pvap | 1.33 | kPa | 335.02 | Calculated Property |
| Pvap | 3.00 | kPa | 351.91 | Calculated Property |
| Pvap | 6.20 | kPa | 368.80 | Calculated Property |
| Pvap | 11.88 | kPa | 385.69 | Calculated Property |
| Pvap | 21.37 | kPa | 402.58 | Calculated Property |
| Pvap | 36.42 | kPa | 419.46 | Calculated Property |
| Pvap | 59.21 | kPa | 436.35 | Calculated Property |
| Pvap | 92.38 | kPa | 453.24 | Calculated Property |
| Pvap | 139.02 | kPa | 470.13 | Calculated Property |
| Pvap | 202.64 | kPa | 487.02 | Calculated Property |
| Pvap | [2.04e-04; 2817.26] | kPa | [230.32; 657.90] |
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 | 1.01832e+02 | |||
| Coefficient B | -9.63670e+03 | |||
| Coefficient C | -1.26560e+01 | |||
| Coefficient D | 6.66400e-06 | |||
| Coefficient E | 2.00000e+00 | |||
| Temperature range, min. | 230.32 | |||
| Temperature range, max. | 657.90 | |||
| Pvap | 2.04e-04 | kPa | 230.32 | Calculated Property |
| Pvap | 0.03 | kPa | 277.83 | Calculated Property |
| Pvap | 0.74 | kPa | 325.34 | Calculated Property |
| Pvap | 7.20 | kPa | 372.85 | Calculated Property |
| Pvap | 37.66 | kPa | 420.36 | Calculated Property |
| Pvap | 131.95 | kPa | 467.86 | Calculated Property |
| Pvap | 353.70 | kPa | 515.37 | Calculated Property |
| Pvap | 789.99 | kPa | 562.88 | Calculated Property |
| Pvap | 1556.98 | kPa | 610.39 | Calculated Property |
| Pvap | 2817.26 | kPa | 657.90 | Calculated Property |
| Pvap | [2.62e-04; 2723.59] | kPa | [230.32; 657.96] |
KDB Vapor Pressure Data
|
| Equation | ln(Y) = A + B/T + C·ln(T) + D·T² + E/T² Y is Pvap in kPa, T in K | |||
| Coefficient A | 8.43431e+01 | |||
| Coefficient B | -8.82443e+03 | |||
| Coefficient C | -1.00236e+01 | |||
| Coefficient D | 4.67268e-06 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 230.32 | |||
| Temperature range, max. | 657.96 | |||
| Pvap | 2.62e-04 | kPa | 230.32 | Calculated Property |
| Pvap | 0.03 | kPa | 277.84 | Calculated Property |
| Pvap | 0.76 | kPa | 325.35 | Calculated Property |
| Pvap | 7.20 | kPa | 372.87 | Calculated Property |
| Pvap | 37.46 | kPa | 420.38 | Calculated Property |
| Pvap | 131.48 | kPa | 467.90 | Calculated Property |
| Pvap | 352.97 | kPa | 515.41 | Calculated Property |
| Pvap | 786.06 | kPa | 562.93 | Calculated Property |
| Pvap | 1533.77 | kPa | 610.44 | Calculated Property |
| Pvap | 2723.59 | kPa | 657.96 | Calculated Property |
| Pvap | [6.42; 104.01] | kPa | [369.97; 457.97] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.41043e+01 | |||
| Coefficient B | -3.65944e+03 | |||
| Coefficient C | -7.11310e+01 | |||
| Reference | Forziati, Norris, et al., 1949, 2 | |||
| Temperature range, min. | 369.97 | |||
| Temperature range, max. | 457.97 | |||
| Pvap | 6.42 | kPa | 369.97 | Calculated Property |
| Pvap | 9.46 | kPa | 379.75 | Calculated Property |
| Pvap | 13.61 | kPa | 389.53 | Calculated Property |
| Pvap | 19.17 | kPa | 399.30 | Calculated Property |
| Pvap | 26.47 | kPa | 409.08 | Calculated Property |
| Pvap | 35.89 | kPa | 418.86 | Calculated Property |
| Pvap | 47.86 | kPa | 428.64 | Calculated Property |
| Pvap | 62.85 | kPa | 438.41 | Calculated Property |
| Pvap | 81.39 | kPa | 448.19 | Calculated Property |
| Pvap | 104.01 | kPa | 457.97 | Calculated Property |
| Pvap | [6.42; 104.01] | kPa | [369.97; 457.97] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.41043e+01 | |||
| Coefficient B | -3.65944e+03 | |||
| Coefficient C | -7.11310e+01 | |||
| Reference | Forziati, Norris, et al., 1949 | |||
| Temperature range, min. | 369.97 | |||
| Temperature range, max. | 457.97 | |||
| Pvap | 6.42 | kPa | 369.97 | Calculated Property |
| Pvap | 9.46 | kPa | 379.75 | Calculated Property |
| Pvap | 13.61 | kPa | 389.53 | Calculated Property |
| Pvap | 19.17 | kPa | 399.30 | Calculated Property |
| Pvap | 26.47 | kPa | 409.08 | Calculated Property |
| Pvap | 35.89 | kPa | 418.86 | Calculated Property |
| Pvap | 47.86 | kPa | 428.64 | Calculated Property |
| Pvap | 62.85 | kPa | 438.41 | Calculated Property |
| Pvap | 81.39 | kPa | 448.19 | Calculated Property |
| Pvap | 104.01 | kPa | 457.97 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ρl | [910.26; 268.56] | kg/m3 | [230.32; 657.90] |
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 | 6.74299e+01 | |||
| Coefficient B | 2.51080e-01 | |||
| Coefficient C | 6.57900e+02 | |||
| Coefficient D | 2.88060e-01 | |||
| Temperature range, min. | 230.32 | |||
| Temperature range, max. | 657.90 | |||
| ρl | 910.26 | kg/m3 | 230.32 | Calculated Property |
| ρl | 873.94 | kg/m3 | 277.83 | Calculated Property |
| ρl | 835.88 | kg/m3 | 325.34 | Calculated Property |
| ρl | 795.66 | kg/m3 | 372.85 | Calculated Property |
| ρl | 752.65 | kg/m3 | 420.36 | Calculated Property |
| ρl | 705.88 | kg/m3 | 467.86 | Calculated Property |
| ρl | 653.66 | kg/m3 | 515.37 | Calculated Property |
| ρl | 592.61 | kg/m3 | 562.88 | Calculated Property |
| ρl | 513.52 | kg/m3 | 610.39 | Calculated Property |
| ρl | 268.56 | kg/m3 | 657.90 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| γ | [0.04; 1.40e-06] | N/m | [230.32; 649.35] |
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 | -5.93650e-02 | |||
| Coefficient B | -4.96800e+01 | |||
| Coefficient C | -1.63760e+00 | |||
| Coefficient D | -2.43850e-03 | |||
| Coefficient E | 1.12300e-06 | |||
| Comment | Range stopped where the equation turns negative; ChemSep gives it to 657.9 K. | |||
| Temperature range, min. | 230.32 | |||
| Temperature range, max. | 649.35 | |||
| γ | 0.04 | N/m | 230.32 | Calculated Property |
| γ | 0.03 | N/m | 276.88 | Calculated Property |
| γ | 0.03 | N/m | 323.44 | Calculated Property |
| γ | 0.02 | N/m | 370.00 | Calculated Property |
| γ | 0.02 | N/m | 416.55 | Calculated Property |
| γ | 0.01 | N/m | 463.11 | Calculated Property |
| γ | 0.01 | N/m | 509.67 | Calculated Property |
| γ | 0.01 | N/m | 556.23 | Calculated Property |
| γ | 0.00 | N/m | 602.79 | Calculated Property |
| γ | 1.40e-06 | N/m | 649.35 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λgas | [0.01; 0.07] | W/m×K | [230.32; 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 | 2.39560e-05 | |||
| Coefficient B | 1.19690e+00 | |||
| Coefficient C | 2.13510e+02 | |||
| Coefficient D | 4.81270e+04 | |||
| Temperature range, min. | 230.32 | |||
| Temperature range, max. | 1000.00 | |||
| λgas | 0.01 | W/m×K | 230.32 | Calculated Property |
| λgas | 0.01 | W/m×K | 315.84 | Calculated Property |
| λgas | 0.02 | W/m×K | 401.36 | Calculated Property |
| λgas | 0.02 | W/m×K | 486.88 | Calculated Property |
| λgas | 0.03 | W/m×K | 572.40 | Calculated Property |
| λgas | 0.04 | W/m×K | 657.92 | Calculated Property |
| λgas | 0.05 | W/m×K | 743.44 | Calculated Property |
| λgas | 0.06 | W/m×K | 828.96 | Calculated Property |
| λgas | 0.06 | W/m×K | 914.48 | Calculated Property |
| λgas | 0.07 | W/m×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λliquid | [0.14; 0.09] | W/m×K | [230.32; 456.94] |
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 | -5.43230e-02 | |||
| Coefficient B | -5.91430e+00 | |||
| Coefficient C | -1.44130e+00 | |||
| Coefficient D | -6.50590e-04 | |||
| Coefficient E | -8.32550e-07 | |||
| Temperature range, min. | 230.32 | |||
| Temperature range, max. | 456.94 | |||
| λliquid | 0.14 | W/m×K | 230.32 | Calculated Property |
| λliquid | 0.13 | W/m×K | 255.50 | Calculated Property |
| λliquid | 0.13 | W/m×K | 280.68 | Calculated Property |
| λliquid | 0.12 | W/m×K | 305.86 | Calculated Property |
| λliquid | 0.12 | W/m×K | 331.04 | Calculated Property |
| λliquid | 0.11 | W/m×K | 356.22 | Calculated Property |
| λliquid | 0.11 | W/m×K | 381.40 | Calculated Property |
| λliquid | 0.10 | W/m×K | 406.58 | Calculated Property |
| λliquid | 0.10 | W/m×K | 431.76 | Calculated Property |
| λliquid | 0.09 | W/m×K | 456.94 | Calculated Property |
Similar Compounds
![Tricyclo[8.2.2.24,7]hexadeca-4,6,10,12,13,15-hexaene.](data:image/png;base64,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)
Find more compounds similar to Benzene, 1,4-diethyl-.
Mixtures
- Undecane + Benzene, 1,4-diethyl- + Thiophene, tetrahydro-, 1,1-dioxide
- Tridecane + Benzene, 1,4-diethyl- + Thiophene, tetrahydro-, 1,1-dioxide
Sources
- KDB Vapor Pressure Data
- Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) ChEDL chemicals 1.5.2, from Bradley, J.-C.; Williams, A.; Lang, A. Jean-Claude Bradley Open Melting Point Dataset. Figshare, 2014 (CC0).
- IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 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.
- 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.
- Crippen Method
- Liquid Liquid Equilibria of the Ternary Systems Undecane + 1,4-Diethylbenzene + Tetrahydrothiophene 1,1-Dioxide and Tridecane + 1,4-Diethylbenzene + Tetrahydrothiophene 1,1-Dioxide at T = (323.15, 348.15, and 373.15) K
- Joback Method
- KDB
- Aqueous Solubility Prediction Method
- Estimated Solubility Method
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
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