- InChI
- InChI=1S/C4H10S/c1-4(2,3)5/h5H,1-3H3
- InChI Key
- WMXCDAVJEZZYLT-UHFFFAOYSA-N
- Formula
- C4H10S
- SMILES
- CC(C)(C)S
- Molecular Weight1
- 90.19
- CAS
- 75-66-1
- Other Names
-
- 1,1-Dimethylethanethiol
- 2-Isobutanethiol
- 2-Methyl-2-propylthiol
- 2-methyl-2-propanethiol
- 2-methylpropane-2-thiol
- t-Butyl mercaptan
- tert-Butyl hydrosulfide
- tert-Butylmercaptan
- tert-Butylthiol
- tert-C4H9SH
- tert-butanethiol
- tert-butyl mercaptan
- tertiary-Butyl mercaptan
- ω : Acentric Factor.
- PAff : Proton affinity (kJ/mol).
- 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).
- 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).
- ΔfusH : Enthalpy of fusion 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).
- 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.
- ΔfusS : Entropy of fusion at a given temperature (J/mol×K).
- S°liquid : Liquid phase molar entropy at standard conditions (J/mol×K).
- 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 | 0.1914 | ChemSep v8.3 pure component data Compiled value | |
| PAff | 816.40 | kJ/mol | NIST |
| BasG | 785.10 | kJ/mol | NIST |
| ΔcH°liquid | -3465.00 ± 0.71 | kJ/mol | NIST |
| μ | 1.59 | debye | ChemSep v8.3 pure component data Compiled value |
| ΔfG° | 1.01 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | [-109.60; -108.70] | kJ/mol |
|
| ΔfH°gas | -109.60 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | -108.70 ± 0.88 | kJ/mol | NIST |
| ΔfH°liquid | -140.50 ± 0.88 | kJ/mol | NIST |
| ΔfusH° | 2.74 | kJ/mol | Joback Calculated Property |
| ΔvapH° | [30.80; 31.80] | kJ/mol |
|
| ΔvapH° | 30.93 | kJ/mol | NIST |
| ΔvapH° | 30.80 | kJ/mol | NIST |
| ΔvapH° | 30.90 ± 0.08 | kJ/mol | NIST |
| ΔvapH° | 31.80 | kJ/mol | NIST |
| ΔvapH° | 30.90 ± 0.08 | kJ/mol | NIST |
| IE | 9.03 | eV | NIST |
| logPoct/wat | 1.715 | Crippen Calculated Property | |
| McVol | 83.570 | ml/mol | McGowan Calculated Property |
| Pc | 4060.00 | kPa | ChemSep v8.3 pure component data Compiled value |
| Ptriple | 7.91 | kPa | ChemSep v8.3 pure component data Compiled value |
| Inp | [574.00; 617.00] |
|
|
| Inp | 584.00 | NIST | |
| Inp | 605.50 | NIST | |
| Inp | Outlier 617.00 | NIST | |
| Inp | 599.20 | NIST | |
| Inp | 602.50 | NIST | |
| Inp | 602.00 | NIST | |
| Inp | 586.00 | NIST | |
| Inp | Outlier 574.00 | NIST | |
| Inp | 577.00 | NIST | |
| Inp | 603.00 | NIST | |
| Inp | 602.00 | NIST | |
| Inp | 606.00 | NIST | |
| Inp | 599.00 | NIST | |
| Inp | 602.00 | NIST | |
| Inp | 584.00 | NIST | |
| Inp | 594.00 | NIST | |
| Inp | 600.00 | NIST | |
| Inp | 595.00 | NIST | |
| Inp | 587.00 | NIST | |
| Inp | 589.00 | NIST | |
| Inp | 602.00 | NIST | |
| Ip | [779.00; 779.00] |
|
|
| Ip | 779.00 | NIST | |
| Ip | 779.00 | NIST | |
| S°liquid | 246.44 | J/mol×K | NIST |
| Tboil | [334.50; 339.00] | K |
|
| Tboil | 337.37 | K | ChemSep v8.3 pure component data Compiled value |
| Tboil | 334.75 | K | KDB |
| Tboil | 337.40 | K | NIST |
| Tboil | 337.00 | K | NIST |
| Tboil | 337.40 | K | NIST |
| Tboil | 339.00 ± 2.00 | K | NIST |
| Tboil | 336.00 ± 3.00 | K | NIST |
| Tboil | 334.50 ± 0.35 | K | NIST |
| Tboil | 337.90 ± 0.60 | K | NIST |
| Tboil | 337.00 ± 2.00 | K | NIST |
| Tc | [530.00; 530.10] | K |
|
| Tc | 530.00 | K | ChemSep v8.3 pure component data Compiled value |
| Tc | 530.10 | K | NIST |
| Tfus | [273.97; 274.41] | K |
|
| Tfus | 274.26 | K | ChemSep v8.3 pure component data Compiled value |
| Tfus | 274.41 | K | KDB |
| Tfus | 273.97 ± 0.20 | K | NIST |
| Ttriple | [274.42; 274.42] | K |
|
| Ttriple | 274.42 | K | ChemSep v8.3 pure component data Compiled value |
| Ttriple | 274.42 ± 0.02 | K | NIST |
| Ttriple | 274.42 ± 0.02 | K | NIST |
| UQi | 3.91 | ChemSep v8.3 pure component data Compiled value | |
| URi | 4.35 | ChemSep v8.3 pure component data Compiled value | |
| Vc | 0.307 | m3/kmol | ChemSep v8.3 pure component data Compiled value |
| Zc | 0.2830000 | ChemSep v8.3 pure component data Compiled value | |
| Zra | 0.28 | ChemSep v8.3 pure component data Compiled value |
Cheméo can also estimate Log10 of Water solubility in mol/l for this compound, but it falls outside the models' validated range, so it is not shown here. Open the prediction tool to compute it on demand.
Temperature Dependent Properties
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | 175.06 | J/mol×K | 298.15 | NIST |
| ΔfusH | [0.65; 4.07] | kJ/mol | [151.60; 274.40] |
|
| ΔfusH | 4.07 | kJ/mol | 151.60 | NIST |
| ΔfusH | 0.65 | kJ/mol | 157.00 | NIST |
| ΔfusH | 0.97 | kJ/mol | 199.40 | NIST |
| ΔfusH | 2.48 | kJ/mol | 274.40 | NIST |
| ΔfusH | 2.48 | kJ/mol | 274.40 | NIST |
| ΔvapH | [28.45; 30.90] | kJ/mol | [284.00; 337.40] |
|
| ΔvapH | 30.10 | kJ/mol | 284.00 | NIST |
| ΔvapH | 30.90 | kJ/mol | 333.00 | NIST |
| ΔvapH | 30.90 | kJ/mol | 333.00 | NIST |
| ΔvapH | 28.45 | kJ/mol | 337.40 | NIST |
| n0 | [1.42000; 1.42000] | [293.10; 298.15] |
|
|
| n0 | 1.42000 | 293.10 | Isothermal Binary Vapor-Liquid Equilibrium for 2-Methylpropane and n-Butane with 1,2-Ethanedithiol and 2-Methyl-2-propanethiol | |
| n0 | 1.42000 | 298.15 | Vapor Liquid Equilibrium for Methoxymethane + Thiophene, + Diethylsulfide, + 2-Methyl-2-propanethiol and 1-Hexene, + 1-Propanethiol | |
| ΔfusS | [4.13; 26.83] | J/mol×K | [151.60; 274.40] |
|
| ΔfusS | 26.83 | J/mol×K | 151.60 | NIST |
| ΔfusS | 4.13 | J/mol×K | 157.00 | NIST |
| ΔfusS | 4.87 | J/mol×K | 199.40 | NIST |
| ΔfusS | 9.04 | J/mol×K | 274.40 | NIST |
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [95.07; 290.76] | 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 | 8.19890e+01 | |||
| Coefficient B | -6.77660e+02 | |||
| Coefficient C | 5.99924e+00 | |||
| Coefficient D | -2.10310e-04 | |||
| Coefficient E | 4.85430e-08 | |||
| Comment | ChemSep eq 16, IdealGasHeatCapacityCp | |||
| Temperature range, min. | 200.00 | |||
| Temperature range, max. | 1500.00 | |||
| Cp,gas | 95.07 | J/mol×K | 200.00 | Calculated Property |
| Cp,gas | 134.72 | J/mol×K | 344.44 | Calculated Property |
| Cp,gas | 174.00 | J/mol×K | 488.89 | Calculated Property |
| Cp,gas | 205.40 | J/mol×K | 633.33 | Calculated Property |
| Cp,gas | 229.48 | J/mol×K | 777.78 | Calculated Property |
| Cp,gas | 247.95 | J/mol×K | 922.22 | Calculated Property |
| Cp,gas | 262.33 | J/mol×K | 1066.67 | Calculated Property |
| Cp,gas | 273.74 | J/mol×K | 1211.11 | Calculated Property |
| Cp,gas | 283.02 | J/mol×K | 1355.56 | Calculated Property |
| Cp,gas | 290.76 | J/mol×K | 1500.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | [170.77; 221.76] | J/mol×K | [274.26; 450.00] |
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 | 1.54160e+02 | |||
| Coefficient B | 5.06030e+02 | |||
| Coefficient C | -5.05976e+00 | |||
| Coefficient D | 2.79910e-02 | |||
| Coefficient E | -2.19610e-05 | |||
| Comment | ChemSep eq 16, LiquidHeatCapacityCp | |||
| Temperature range, min. | 274.26 | |||
| Temperature range, max. | 450.00 | |||
| Cp,liquid | 170.77 | J/mol×K | 274.26 | Calculated Property |
| Cp,liquid | 174.06 | J/mol×K | 293.79 | Calculated Property |
| Cp,liquid | 177.96 | J/mol×K | 313.31 | Calculated Property |
| Cp,liquid | 182.50 | J/mol×K | 332.84 | Calculated Property |
| Cp,liquid | 187.70 | J/mol×K | 352.37 | Calculated Property |
| Cp,liquid | 193.54 | J/mol×K | 371.89 | Calculated Property |
| Cp,liquid | 199.98 | J/mol×K | 391.42 | Calculated Property |
| Cp,liquid | 206.92 | J/mol×K | 410.95 | Calculated Property |
| Cp,liquid | 214.24 | J/mol×K | 430.47 | Calculated Property |
| Cp,liquid | 221.76 | J/mol×K | 450.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [0.0008749; 0.0002172] | Pa×s | [273.15; 393.00] |
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 | -8.33370e+00 | |||
| Coefficient B | 1.21480e+03 | |||
| Coefficient C | -5.92080e-01 | |||
| Coefficient D | 2.23180e-06 | |||
| Coefficient E | 2.00000e+00 | |||
| Comment | ChemSep eq 101, LiquidViscosity | |||
| Temperature range, min. | 273.15 | |||
| Temperature range, max. | 393.00 | |||
| η | 0.0008749 | Pa×s | 273.15 | Calculated Property |
| η | 0.0007033 | Pa×s | 286.47 | Calculated Property |
| η | 0.0005771 | Pa×s | 299.78 | Calculated Property |
| η | 0.0004821 | Pa×s | 313.10 | Calculated Property |
| η | 0.0004092 | Pa×s | 326.42 | Calculated Property |
| η | 0.0003523 | Pa×s | 339.73 | Calculated Property |
| η | 0.0003072 | Pa×s | 353.05 | Calculated Property |
| η | 0.0002709 | Pa×s | 366.37 | Calculated Property |
| η | 0.0002414 | Pa×s | 379.68 | Calculated Property |
| η | 0.0002172 | Pa×s | 393.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | [32.15; 0.00] | kJ/mol | [274.26; 530.00] |
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 | 5.31370e+01 | |||
| Coefficient B | 1.45020e+00 | |||
| Coefficient C | -2.47130e+00 | |||
| Coefficient D | 2.42970e+00 | |||
| Coefficient E | -9.54580e-01 | |||
| Critical temperature, Tc (K) | 5.30000e+02 | |||
| Comment | ChemSep eq 106, HeatOfVaporization | |||
| Temperature range, min. | 274.26 | |||
| Temperature range, max. | 530.00 | |||
| ΔvapH | 32.15 | kJ/mol | 274.26 | Calculated Property |
| ΔvapH | 30.56 | kJ/mol | 302.68 | Calculated Property |
| ΔvapH | 28.89 | kJ/mol | 331.09 | Calculated Property |
| ΔvapH | 27.09 | kJ/mol | 359.51 | Calculated Property |
| ΔvapH | 25.13 | kJ/mol | 387.92 | Calculated Property |
| ΔvapH | 22.94 | kJ/mol | 416.34 | Calculated Property |
| ΔvapH | 20.42 | kJ/mol | 444.75 | Calculated Property |
| ΔvapH | 17.35 | kJ/mol | 473.17 | Calculated Property |
| ΔvapH | 13.11 | kJ/mol | 501.58 | Calculated Property |
| ΔvapH | 0.00 | kJ/mol | 530.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [7.83; 4346.40] | kPa | [274.26; 530.00] |
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 | 1.00608e+02 | |||
| Coefficient B | -7.03055e+03 | |||
| Coefficient C | -1.31586e+01 | |||
| Coefficient D | 1.27338e-05 | |||
| Coefficient E | 2.00000e+00 | |||
| Comment | ChemSep eq 101, VaporPressure | |||
| Temperature range, min. | 274.26 | |||
| Temperature range, max. | 530.00 | |||
| Pvap | 7.83 | kPa | 274.26 | Calculated Property |
| Pvap | 29.24 | kPa | 302.68 | Calculated Property |
| Pvap | 82.90 | kPa | 331.09 | Calculated Property |
| Pvap | 192.96 | kPa | 359.51 | Calculated Property |
| Pvap | 389.33 | kPa | 387.92 | Calculated Property |
| Pvap | 707.82 | kPa | 416.34 | Calculated Property |
| Pvap | 1192.60 | kPa | 444.75 | Calculated Property |
| Pvap | 1901.49 | kPa | 473.17 | Calculated Property |
| Pvap | 2914.48 | kPa | 501.58 | Calculated Property |
| Pvap | 4346.40 | kPa | 530.00 | Calculated Property |
| Pvap | [19.97; 270.09] | kPa | [293.70; 372.29] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.36145e+01 | |||
| Coefficient B | -2.56870e+03 | |||
| Coefficient C | -5.18350e+01 | |||
| Reference | McCullough, Scott, et al., 1953 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 293.70 | |||
| Temperature range, max. | 372.29 | |||
| Pvap | 19.97 | kPa | 293.70 | Calculated Property |
| Pvap | 28.91 | kPa | 302.43 | Calculated Property |
| Pvap | 40.83 | kPa | 311.16 | Calculated Property |
| Pvap | 56.38 | kPa | 319.90 | Calculated Property |
| Pvap | 76.28 | kPa | 328.63 | Calculated Property |
| Pvap | 101.31 | kPa | 337.36 | Calculated Property |
| Pvap | 132.31 | kPa | 346.09 | Calculated Property |
| Pvap | 170.16 | kPa | 354.83 | Calculated Property |
| Pvap | 215.77 | kPa | 363.56 | Calculated Property |
| Pvap | 270.09 | kPa | 372.29 | Calculated Property |
| Pvap | [19.97; 270.09] | kPa | [293.70; 372.29] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.36145e+01 | |||
| Coefficient B | -2.56870e+03 | |||
| Coefficient C | -5.18350e+01 | |||
| Reference | McCullough, Scott, et al., 1953, 2 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 293.70 | |||
| Temperature range, max. | 372.29 | |||
| Pvap | 19.97 | kPa | 293.70 | Calculated Property |
| Pvap | 28.91 | kPa | 302.43 | Calculated Property |
| Pvap | 40.83 | kPa | 311.16 | Calculated Property |
| Pvap | 56.38 | kPa | 319.90 | Calculated Property |
| Pvap | 76.28 | kPa | 328.63 | Calculated Property |
| Pvap | 101.31 | kPa | 337.36 | Calculated Property |
| Pvap | 132.31 | kPa | 346.09 | Calculated Property |
| Pvap | 170.16 | kPa | 354.83 | Calculated Property |
| Pvap | 215.77 | kPa | 363.56 | Calculated Property |
| Pvap | 270.09 | kPa | 372.29 | Calculated Property |
| Pvap | [19.97; 270.09] | kPa | [293.70; 372.29] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.36145e+01 | |||
| Coefficient B | -2.56870e+03 | |||
| Coefficient C | -5.18350e+01 | |||
| Reference | McCullough, Scott, et al., 1953, 3 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 293.70 | |||
| Temperature range, max. | 372.29 | |||
| Pvap | 19.97 | kPa | 293.70 | Calculated Property |
| Pvap | 28.91 | kPa | 302.43 | Calculated Property |
| Pvap | 40.83 | kPa | 311.16 | Calculated Property |
| Pvap | 56.38 | kPa | 319.90 | Calculated Property |
| Pvap | 76.28 | kPa | 328.63 | Calculated Property |
| Pvap | 101.31 | kPa | 337.36 | Calculated Property |
| Pvap | 132.31 | kPa | 346.09 | Calculated Property |
| Pvap | 170.16 | kPa | 354.83 | Calculated Property |
| Pvap | 215.77 | kPa | 363.56 | Calculated Property |
| Pvap | 270.09 | kPa | 372.29 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ρl | [819.48; 293.74] | kg/m3 | [274.26; 530.00] |
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 | 8.09078e+01 | |||
| Coefficient B | 2.75440e-01 | |||
| Coefficient C | 5.30000e+02 | |||
| Coefficient D | 3.13590e-01 | |||
| Comment | ChemSep eq 105, LiquidDensity | |||
| Temperature range, min. | 274.26 | |||
| Temperature range, max. | 530.00 | |||
| ρl | 819.48 | kg/m3 | 274.26 | Calculated Property |
| ρl | 789.56 | kg/m3 | 302.68 | Calculated Property |
| ρl | 758.18 | kg/m3 | 331.09 | Calculated Property |
| ρl | 725.00 | kg/m3 | 359.51 | Calculated Property |
| ρl | 689.50 | kg/m3 | 387.92 | Calculated Property |
| ρl | 650.86 | kg/m3 | 416.34 | Calculated Property |
| ρl | 607.69 | kg/m3 | 444.75 | Calculated Property |
| ρl | 557.17 | kg/m3 | 473.17 | Calculated Property |
| ρl | 491.67 | kg/m3 | 501.58 | Calculated Property |
| ρl | 293.74 | kg/m3 | 530.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| γ | [0.02; 9.45e-06] | N/m | [274.26; 526.93] |
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 | -3.17500e-03 | |||
| Coefficient B | 7.37780e+02 | |||
| Coefficient C | -1.01230e+01 | |||
| Coefficient D | 2.26980e-02 | |||
| Coefficient E | -3.23670e-05 | |||
| Comment | ChemSep eq 16, SurfaceTension, ChemSep Tmax 530 K | |||
| Temperature range, min. | 274.26 | |||
| Temperature range, max. | 526.93 | |||
| γ | 0.02 | N/m | 274.26 | Calculated Property |
| γ | 0.02 | N/m | 302.33 | Calculated Property |
| γ | 0.02 | N/m | 330.41 | Calculated Property |
| γ | 0.01 | N/m | 358.48 | Calculated Property |
| γ | 0.01 | N/m | 386.56 | Calculated Property |
| γ | 0.01 | N/m | 414.63 | Calculated Property |
| γ | 0.01 | N/m | 442.71 | Calculated Property |
| γ | 0.00 | N/m | 470.78 | Calculated Property |
| γ | 0.00 | N/m | 498.86 | Calculated Property |
| γ | 9.45e-06 | N/m | 526.93 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λgas | [0.01; 0.09] | W/m×K | [274.42; 1000.00] |
ChemSep v8.3 pure component data Compiled value
|
| Equation | Y = A·T^B / (1 + C/T + D/T²) Y is λgas in W/m×K, T in K | |||
| Coefficient A | 3.24990e-02 | |||
| Coefficient B | 3.14820e-01 | |||
| Coefficient C | 1.56230e+03 | |||
| Coefficient D | 7.75320e+05 | |||
| Comment | ChemSep eq 102, VaporThermalConductivity | |||
| Temperature range, min. | 274.42 | |||
| Temperature range, max. | 1000.00 | |||
| λgas | 0.01 | W/m×K | 274.42 | Calculated Property |
| λgas | 0.02 | W/m×K | 355.04 | Calculated Property |
| λgas | 0.03 | W/m×K | 435.66 | Calculated Property |
| λgas | 0.03 | W/m×K | 516.28 | Calculated Property |
| λgas | 0.04 | W/m×K | 596.90 | Calculated Property |
| λgas | 0.05 | W/m×K | 677.52 | Calculated Property |
| λgas | 0.06 | W/m×K | 758.14 | Calculated Property |
| λgas | 0.07 | W/m×K | 838.76 | Calculated Property |
| λgas | 0.08 | W/m×K | 919.38 | Calculated Property |
| λgas | 0.09 | W/m×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λliquid | [0.13; 0.12] | W/m×K | [274.26; 337.37] |
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 | 3.14540e-02 | |||
| Coefficient B | -2.60910e+02 | |||
| Coefficient C | 5.99000e-01 | |||
| Coefficient D | -7.90270e-03 | |||
| Coefficient E | 3.16380e-06 | |||
| Comment | ChemSep eq 16, LiquidThermalConductivity | |||
| Temperature range, min. | 274.26 | |||
| Temperature range, max. | 337.37 | |||
| λliquid | 0.13 | W/m×K | 274.26 | Calculated Property |
| λliquid | 0.13 | W/m×K | 281.27 | Calculated Property |
| λliquid | 0.13 | W/m×K | 288.28 | Calculated Property |
| λliquid | 0.13 | W/m×K | 295.30 | Calculated Property |
| λliquid | 0.13 | W/m×K | 302.31 | Calculated Property |
| λliquid | 0.12 | W/m×K | 309.32 | Calculated Property |
| λliquid | 0.12 | W/m×K | 316.33 | Calculated Property |
| λliquid | 0.12 | W/m×K | 323.35 | Calculated Property |
| λliquid | 0.12 | W/m×K | 330.36 | Calculated Property |
| λliquid | 0.12 | W/m×K | 337.37 | Calculated Property |
Similar Compounds
![Propane, 2,2'-[methylenebis(thio)]bis[2-methyl-.](data:image/png;base64,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)
Find more compounds similar to 2-Propanethiol, 2-methyl-.
Mixtures
- 2-Propanethiol, 2-methyl- + Isobutane
- Butane + 2-Propanethiol, 2-methyl-
- 1-Hexene + 2-Propanethiol, 2-methyl-
- Dimethyl ether + 2-Propanethiol, 2-methyl-
Sources
- 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
- Vapor Liquid Equilibrium for Methoxymethane + Thiophene, + Diethylsulfide, + 2-Methyl-2-propanethiol and 1-Hexene, + 1-Propanethiol
- Isothermal Binary Vapor-Liquid Equilibrium for 2-Methylpropane and n-Butane with 1,2-Ethanedithiol and 2-Methyl-2-propanethiol
- Joback Method
- KDB
- McGowan Method
- NIST Webbook
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