- InChI
- InChI=1S/C10H14/c1-3-4-10-7-5-9(2)6-8-10/h5-8H,3-4H2,1-2H3
- InChI Key
- JXFVMNFKABWTHD-UHFFFAOYSA-N
- Formula
- C10H14
- SMILES
- CCCc1ccc(C)cc1
- Molecular Weight1
- 134.22
- CAS
- 1074-55-1
- Other Names
-
- 1-Methyl-4-n-propylbenzene
- 1-Methyl-4-propylbenzene
- 4-Propyl-1-methylbenzene
- 4-n-Propyltoluene
- 4-propyltoluene
- Toluene, p-propyl-
- p-Methylpropylbenzene
- p-Propyltoluene
- p-n-Propyl toluene
- 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).
- 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 | [0.3856; 0.4134] |
|
|
| ω | 0.3856 | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value | |
| ω | 0.4134 | ChemSep v8.3 pure component data Compiled value | |
| ω | 0.4020 | KDB | |
| ΔcH°liquid | [-5860.86; -5860.40] | kJ/mol |
|
| ΔcH°liquid | -5860.86 ± 0.88 | kJ/mol | NIST |
| ΔcH°liquid | -5860.40 ± 2.20 | kJ/mol | NIST |
| μ | 0.00 | debye | ChemSep v8.3 pure component data Compiled value |
| ΔfG° | 138.20 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | -23.14 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°liquid | [-75.60; -75.10] | kJ/mol |
|
| ΔfH°liquid | -75.10 ± 1.00 | kJ/mol | NIST |
| ΔfH°liquid | -75.60 ± 2.10 | kJ/mol | NIST |
| ΔfusH° | 15.31 | kJ/mol | Joback Calculated Property |
| ΔvapH° | 51.90 | kJ/mol | NIST |
| IE | 8.34 | eV | Relay (1.0) Calculated Property |
| log10WS | -3.77 | Relay (1.0) Calculated Property | |
| logPoct/wat | 2.948 | Crippen Calculated Property | |
| McVol | 128.000 | ml/mol | McGowan Calculated Property |
| Pc | [2845.00; 2860.00] | kPa |
|
| Pc | 2845.21 | kPa | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Pc | 2860.00 | kPa | ChemSep v8.3 pure component data Compiled value |
| Pc | 2845.00 | kPa | KDB |
| Ptriple | 1.72e-05 | kPa | ChemSep v8.3 pure component data Compiled value |
| Inp | [172.80; 1070.00] |
|
|
| Inp | 1046.00 | NIST | |
| Inp | 1032.00 | NIST | |
| Inp | 1032.00 | NIST | |
| Inp | 1046.50 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1047.00 | NIST | |
| Inp | 1047.00 | NIST | |
| Inp | 1047.00 | NIST | |
| Inp | 1040.00 | NIST | |
| Inp | 1038.10 | NIST | |
| Inp | 1048.00 | NIST | |
| Inp | 1053.00 | NIST | |
| Inp | 1058.00 | NIST | |
| Inp | 1035.90 | NIST | |
| Inp | 1038.80 | NIST | |
| Inp | 1047.50 | NIST | |
| Inp | 1052.60 | NIST | |
| Inp | 1057.70 | NIST | |
| Inp | 1035.40 | NIST | |
| Inp | 1033.00 | NIST | |
| Inp | 1035.90 | NIST | |
| Inp | 1038.80 | NIST | |
| Inp | 1040.00 | NIST | |
| Inp | 1033.02 | NIST | |
| Inp | 1035.40 | NIST | |
| Inp | 1039.30 | NIST | |
| Inp | 1039.00 | NIST | |
| Inp | 1044.00 | NIST | |
| Inp | 1039.00 | NIST | |
| Inp | 1070.00 | NIST | |
| Inp | 1046.40 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1048.00 | NIST | |
| Inp | 1038.40 | NIST | |
| Inp | 1040.00 | NIST | |
| Inp | 1042.00 | NIST | |
| Inp | 1036.49 | NIST | |
| Inp | 1039.82 | NIST | |
| Inp | 1042.19 | NIST | |
| Inp | 1052.90 | NIST | |
| Inp | 1056.46 | NIST | |
| Inp | 1059.10 | NIST | |
| Inp | 1039.00 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1048.00 | NIST | |
| Inp | 1053.00 | NIST | |
| Inp | 1053.00 | NIST | |
| Inp | 1048.00 | NIST | |
| Inp | 1047.00 | NIST | |
| Inp | 1048.00 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1056.00 | NIST | |
| Inp | 1059.00 | NIST | |
| Inp | 1049.00 | NIST | |
| Inp | 1061.30 | NIST | |
| Inp | 1047.00 | NIST | |
| Inp | 1038.00 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1038.00 | NIST | |
| Inp | 1038.00 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1038.00 | NIST | |
| Inp | 1047.00 | NIST | |
| Inp | 1046.50 | NIST | |
| Inp | 1047.00 | NIST | |
| Inp | 1039.80 | NIST | |
| Inp | Outlier 172.80 | NIST | |
| Inp | 1046.00 | NIST | |
| Inp | 1047.00 | NIST | |
| Inp | 1058.00 | NIST | |
| Inp | 1057.70 | NIST | |
| Inp | 1040.00 | NIST | |
| Inp | 1044.00 | NIST | |
| Inp | Outlier 172.80 | NIST | |
| Inp | 1046.40 | NIST | |
| Ip | [1262.00; 1354.00] |
|
|
| Ip | 1262.00 | NIST | |
| Ip | 1301.00 | NIST | |
| Ip | 1279.90 | NIST | |
| Ip | 1296.00 | NIST | |
| Ip | 1279.90 | NIST | |
| Ip | 1295.00 | NIST | |
| Ip | 1297.00 | NIST | |
| Ip | 1314.00 | NIST | |
| Ip | 1315.00 | NIST | |
| Ip | 1326.00 | NIST | |
| Ip | 1338.00 | NIST | |
| Ip | Outlier 1354.00 | NIST | |
| Ip | 1302.00 | NIST | |
| Ip | 1280.00 | NIST | |
| Ip | 1301.00 | NIST | |
| Ip | 1280.00 | NIST | |
| Ip | 1287.50 | NIST | |
| Ip | 1262.00 | NIST | |
| Ip | 1295.00 | NIST | |
| Tboil | [452.90; 457.00] | K |
|
| Tboil | 456.53 | K | ChemSep v8.3 pure component data Compiled value |
| Tboil | 456.20 | K | KDB |
| Tboil | 456.60 | K | NIST |
| Tboil | 456.65 ± 0.50 | K | NIST |
| Tboil | 456.59 ± 0.20 | K | NIST |
| Tboil | 456.53 ± 0.20 | K | NIST |
| Tboil | 456.00 ± 3.00 | K | NIST |
| Tboil | 456.61 ± 0.30 | K | NIST |
| Tboil | 456.25 ± 0.20 | K | NIST |
| Tboil | 456.25 ± 0.20 | K | NIST |
| Tboil | 456.25 ± 0.20 | K | NIST |
| Tboil | 456.61 ± 0.30 | K | NIST |
| Tboil | 456.25 ± 0.30 | K | NIST |
| Tboil | 456.61 ± 0.30 | K | NIST |
| Tboil | 456.60 ± 0.30 | K | NIST |
| Tboil | 456.58 ± 0.30 | K | NIST |
| Tboil | 456.61 ± 0.30 | K | NIST |
| Tboil | 457.00 ± 3.00 | K | NIST |
| Tboil | 457.00 ± 5.00 | K | NIST |
| Tboil | 457.00 ± 4.00 | K | NIST |
| Tboil | 456.00 ± 3.00 | K | NIST |
| Tboil | Outlier 452.90 ± 3.00 | K | NIST |
| Tc | [658.00; 660.70] | K |
|
| Tc | 660.70 | K | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Tc | 658.00 | K | ChemSep v8.3 pure component data Compiled value |
| Tc | 660.70 | K | KDB |
| Tfus | [208.50; 209.55] | K |
|
| Tfus | 209.35 | K | Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value |
| Tfus | 209.46 | K | ChemSep v8.3 pure component data Compiled value |
| Tfus | 209.55 | K | KDB |
| Tfus | 209.45 ± 0.01 | K | NIST |
| Tfus | 209.38 ± 0.20 | K | NIST |
| Tfus | 208.95 ± 0.50 | K | NIST |
| Tfus | Outlier 208.50 ± 0.60 | K | NIST |
| Ttriple | 209.55 | 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 | [0.482; 0.482] | m3/kmol |
|
| Vc | 0.482 | m3/kmol | PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value |
| Vc | 0.482 | m3/kmol | ChemSep v8.3 pure component data Compiled value |
| Zc | 0.2480000 | ChemSep v8.3 pure component data Compiled value | |
| Zra | 0.25 | ChemSep v8.3 pure component data Compiled value |
Temperature Dependent Properties
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | 47.60 | kJ/mol | 411.00 | NIST |
| ρl | 859.01 | kg/m3 | 293.10 | KDB |
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [175.20; 477.28] | J/mol×K | [298.15; 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 | 9.71270e+01 | |||
| Coefficient B | -5.99110e+02 | |||
| Coefficient C | 6.36524e+00 | |||
| Coefficient D | 1.16650e-05 | |||
| Coefficient E | -1.90030e-08 | |||
| Temperature range, min. | 298.15 | |||
| Temperature range, max. | 1500.00 | |||
| Cp,gas | 175.20 | J/mol×K | 298.15 | Calculated Property |
| Cp,gas | 242.44 | J/mol×K | 431.69 | Calculated Property |
| Cp,gas | 298.63 | J/mol×K | 565.23 | Calculated Property |
| Cp,gas | 343.47 | J/mol×K | 698.77 | Calculated Property |
| Cp,gas | 379.14 | J/mol×K | 832.31 | Calculated Property |
| Cp,gas | 407.72 | J/mol×K | 965.84 | Calculated Property |
| Cp,gas | 430.80 | J/mol×K | 1099.38 | Calculated Property |
| Cp,gas | 449.54 | J/mol×K | 1232.92 | Calculated Property |
| Cp,gas | 464.83 | J/mol×K | 1366.46 | Calculated Property |
| Cp,gas | 477.28 | J/mol×K | 1500.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | [244.15; 351.17] | J/mol×K | [298.15; 492.00] |
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 | 1.28960e+02 | |||
| Coefficient B | -1.02230e+02 | |||
| Coefficient C | 4.36124e+00 | |||
| Coefficient D | 2.29130e-03 | |||
| Coefficient E | 5.07420e-07 | |||
| Temperature range, min. | 298.15 | |||
| Temperature range, max. | 492.00 | |||
| Cp,liquid | 244.15 | J/mol×K | 298.15 | Calculated Property |
| Cp,liquid | 253.65 | J/mol×K | 319.69 | Calculated Property |
| Cp,liquid | 263.60 | J/mol×K | 341.23 | Calculated Property |
| Cp,liquid | 274.06 | J/mol×K | 362.77 | Calculated Property |
| Cp,liquid | 285.10 | J/mol×K | 384.31 | Calculated Property |
| Cp,liquid | 296.77 | J/mol×K | 405.84 | Calculated Property |
| Cp,liquid | 309.15 | J/mol×K | 427.38 | Calculated Property |
| Cp,liquid | 322.29 | J/mol×K | 448.92 | Calculated Property |
| Cp,liquid | 336.27 | J/mol×K | 470.46 | Calculated Property |
| Cp,liquid | 351.17 | J/mol×K | 492.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [0.0077251; 0.0001168] | Pa×s | [209.55; 553.15] |
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 | -6.50053e+01 | |||
| Coefficient B | 3.27306e+03 | |||
| Coefficient C | 8.41308e+00 | |||
| Coefficient D | -1.01347e-05 | |||
| Coefficient E | 2.00000e+00 | |||
| Temperature range, min. | 209.55 | |||
| Temperature range, max. | 553.15 | |||
| η | 0.0077251 | Pa×s | 209.55 | Calculated Property |
| η | 0.0023833 | Pa×s | 247.73 | Calculated Property |
| η | 0.0011091 | Pa×s | 285.91 | Calculated Property |
| η | 0.0006528 | Pa×s | 324.08 | Calculated Property |
| η | 0.0004406 | Pa×s | 362.26 | Calculated Property |
| η | 0.0003220 | Pa×s | 400.44 | Calculated Property |
| η | 0.0002458 | Pa×s | 438.62 | Calculated Property |
| η | 0.0001915 | Pa×s | 476.79 | Calculated Property |
| η | 0.0001500 | Pa×s | 514.97 | Calculated Property |
| η | 0.0001168 | Pa×s | 553.15 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | [55.03; 7.44] | kJ/mol | [209.55; 656.00] |
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 | 5.96320e+01 | |||
| Coefficient B | -1.30890e-01 | |||
| Coefficient C | 1.57690e+00 | |||
| Coefficient D | -1.83250e+00 | |||
| Coefficient E | 7.46080e-01 | |||
| Critical temperature, Tc (K) | 6.58000e+02 | |||
| Temperature range, min. | 209.55 | |||
| Temperature range, max. | 656.00 | |||
| ΔvapH | 55.03 | kJ/mol | 209.55 | Calculated Property |
| ΔvapH | 52.58 | kJ/mol | 259.16 | Calculated Property |
| ΔvapH | 49.86 | kJ/mol | 308.76 | Calculated Property |
| ΔvapH | 46.92 | kJ/mol | 358.37 | Calculated Property |
| ΔvapH | 43.74 | kJ/mol | 407.97 | Calculated Property |
| ΔvapH | 40.26 | kJ/mol | 457.58 | Calculated Property |
| ΔvapH | 36.27 | kJ/mol | 507.18 | Calculated Property |
| ΔvapH | 31.36 | kJ/mol | 556.79 | Calculated Property |
| ΔvapH | 24.47 | kJ/mol | 606.39 | Calculated Property |
| ΔvapH | 7.44 | kJ/mol | 656.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.65] | kPa | [336.32; 486.18] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.45089e+01 | |||
| Coefficient B | -3.90155e+03 | |||
| Coefficient C | -6.19770e+01 | |||
| Temperature range, min. | 336.32 | |||
| Temperature range, max. | 486.18 | |||
| Pvap | 1.33 | kPa | 336.32 | Calculated Property |
| Pvap | 3.01 | kPa | 352.97 | Calculated Property |
| Pvap | 6.21 | kPa | 369.62 | Calculated Property |
| Pvap | 11.92 | kPa | 386.27 | Calculated Property |
| Pvap | 21.45 | kPa | 402.92 | Calculated Property |
| Pvap | 36.54 | kPa | 419.58 | Calculated Property |
| Pvap | 59.37 | kPa | 436.23 | Calculated Property |
| Pvap | 92.57 | kPa | 452.88 | Calculated Property |
| Pvap | 139.17 | kPa | 469.53 | Calculated Property |
| Pvap | 202.65 | kPa | 486.18 | Calculated Property |
| Pvap | [1.31e-05; 2731.75] | kPa | [209.55; 656.00] |
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 | 9.63254e+01 | |||
| Coefficient B | -9.32142e+03 | |||
| Coefficient C | -1.18535e+01 | |||
| Coefficient D | 6.22813e-06 | |||
| Coefficient E | 2.00000e+00 | |||
| Temperature range, min. | 209.55 | |||
| Temperature range, max. | 656.00 | |||
| Pvap | 1.31e-05 | kPa | 209.55 | Calculated Property |
| Pvap | 6.10e-03 | kPa | 259.16 | Calculated Property |
| Pvap | 0.29 | kPa | 308.76 | Calculated Property |
| Pvap | 4.05 | kPa | 358.37 | Calculated Property |
| Pvap | 26.06 | kPa | 407.97 | Calculated Property |
| Pvap | 104.02 | kPa | 457.58 | Calculated Property |
| Pvap | 303.40 | kPa | 507.18 | Calculated Property |
| Pvap | 717.00 | kPa | 556.79 | Calculated Property |
| Pvap | 1468.98 | kPa | 606.39 | Calculated Property |
| Pvap | 2731.75 | kPa | 656.00 | Calculated Property |
| Pvap | [1.33; 203.25] | kPa | [335.15; 487.15] |
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 | 1.04171e+02 | |||
| Coefficient B | -9.64433e+03 | |||
| Coefficient C | -1.30610e+01 | |||
| Coefficient D | 7.46048e-06 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 335.15 | |||
| Temperature range, max. | 487.15 | |||
| Pvap | 1.33 | kPa | 335.15 | Calculated Property |
| Pvap | 3.04 | kPa | 352.04 | Calculated Property |
| Pvap | 6.33 | kPa | 368.93 | Calculated Property |
| Pvap | 12.19 | kPa | 385.82 | Calculated Property |
| Pvap | 21.95 | kPa | 402.71 | Calculated Property |
| Pvap | 37.33 | kPa | 419.59 | Calculated Property |
| Pvap | 60.44 | kPa | 436.48 | Calculated Property |
| Pvap | 93.78 | kPa | 453.37 | Calculated Property |
| Pvap | 140.28 | kPa | 470.26 | Calculated Property |
| Pvap | 203.25 | kPa | 487.15 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ρl | [931.44; 436.33] | kg/m3 | [209.55; 632.50] |
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 | 6.47187e+01 | |||
| Coefficient B | 2.42590e-01 | |||
| Coefficient C | 6.58000e+02 | |||
| Coefficient D | 3.25310e-01 | |||
| Temperature range, min. | 209.55 | |||
| Temperature range, max. | 632.50 | |||
| ρl | 931.44 | kg/m3 | 209.55 | Calculated Property |
| ρl | 891.14 | kg/m3 | 256.54 | Calculated Property |
| ρl | 849.49 | kg/m3 | 303.54 | Calculated Property |
| ρl | 806.15 | kg/m3 | 350.53 | Calculated Property |
| ρl | 760.65 | kg/m3 | 397.53 | Calculated Property |
| ρl | 712.31 | kg/m3 | 444.52 | Calculated Property |
| ρl | 659.97 | kg/m3 | 491.52 | Calculated Property |
| ρl | 601.58 | kg/m3 | 538.51 | Calculated Property |
| ρl | 532.49 | kg/m3 | 585.51 | Calculated Property |
| ρl | 436.33 | kg/m3 | 632.50 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| γ | [0.04; 2.16e-05] | N/m | [209.55; 644.84] |
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 | -1.94720e-01 | |||
| Coefficient B | -2.84630e+00 | |||
| Coefficient C | -1.27260e+00 | |||
| Coefficient D | -8.55000e-04 | |||
| Coefficient E | 4.62390e-07 | |||
| Comment | Range stopped where the equation turns negative; ChemSep gives it to 656 K. | |||
| Temperature range, min. | 209.55 | |||
| Temperature range, max. | 644.84 | |||
| γ | 0.04 | N/m | 209.55 | Calculated Property |
| γ | 0.03 | N/m | 257.92 | Calculated Property |
| γ | 0.03 | N/m | 306.28 | Calculated Property |
| γ | 0.02 | N/m | 354.65 | Calculated Property |
| γ | 0.02 | N/m | 403.01 | Calculated Property |
| γ | 0.01 | N/m | 451.38 | Calculated Property |
| γ | 0.01 | N/m | 499.74 | Calculated Property |
| γ | 0.01 | N/m | 548.11 | Calculated Property |
| γ | 0.00 | N/m | 596.47 | Calculated Property |
| γ | 2.16e-05 | N/m | 644.84 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λgas | [0.01; 0.07] | W/m×K | [209.55; 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 | 8.33470e-05 | |||
| Coefficient B | 1.05170e+00 | |||
| Coefficient C | 5.73970e+02 | |||
| Coefficient D | 3.31360e+04 | |||
| Temperature range, min. | 209.55 | |||
| Temperature range, max. | 1000.00 | |||
| λgas | 0.01 | W/m×K | 209.55 | Calculated Property |
| λgas | 0.01 | W/m×K | 297.38 | Calculated Property |
| λgas | 0.02 | W/m×K | 385.21 | Calculated Property |
| λgas | 0.02 | W/m×K | 473.03 | Calculated Property |
| λgas | 0.03 | W/m×K | 560.86 | Calculated Property |
| λgas | 0.04 | W/m×K | 648.69 | Calculated Property |
| λgas | 0.05 | W/m×K | 736.52 | Calculated Property |
| λgas | 0.06 | W/m×K | 824.34 | Calculated Property |
| λgas | 0.06 | W/m×K | 912.17 | 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 | [209.55; 456.45] |
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 | -8.10490e-02 | |||
| Coefficient B | 3.27590e+00 | |||
| Coefficient C | -1.40260e+00 | |||
| Coefficient D | -4.36340e-04 | |||
| Coefficient E | -7.90350e-07 | |||
| Temperature range, min. | 209.55 | |||
| Temperature range, max. | 456.45 | |||
| λliquid | 0.14 | W/m×K | 209.55 | Calculated Property |
| λliquid | 0.13 | W/m×K | 236.98 | Calculated Property |
| λliquid | 0.13 | W/m×K | 264.42 | Calculated Property |
| λliquid | 0.12 | W/m×K | 291.85 | Calculated Property |
| λliquid | 0.12 | W/m×K | 319.28 | Calculated Property |
| λliquid | 0.11 | W/m×K | 346.72 | Calculated Property |
| λliquid | 0.11 | W/m×K | 374.15 | Calculated Property |
| λliquid | 0.10 | W/m×K | 401.58 | Calculated Property |
| λliquid | 0.10 | W/m×K | 429.02 | Calculated Property |
| λliquid | 0.09 | W/m×K | 456.45 | Calculated Property |
Similar Compounds
![Tricyclo[10.2.2.25,8]octadeca-5,7,12,14,15,17-hexaene.](data:image/png;base64,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)
Find more compounds similar to Benzene, 1-methyl-4-propyl-.
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).
- 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.
- Cheméo Relay (1.0)
- 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
- Crippen Method
- Joback Method
- KDB
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
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