- InChI
- InChI=1S/C5H12S/c1-5(2,3)6-4/h1-4H3
- InChI Key
- CJFVCTVYZFTORU-UHFFFAOYSA-N
- Formula
- C5H12S
- SMILES
- CSC(C)(C)C
- Molecular Weight1
- 104.21
- CAS
- 6163-64-0
- Other Names
-
- (CH3)3CSCH3
- 2-Methyl-2-(methylthio)-propane
- 3,3-Dimethyl-2-thiabutane
- Methyl t-butyl sulfide
- Methyl tert-butyl sulfide
- NSC 97331
- Sulfide, tert-butyl methyl
- tert-Butyl methyl sulfide
- tert-Butyl methyl sulphide
- 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).
- 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).
- ρl : Liquid Density (kg/m3).
- Inp : Non-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).
- 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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Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ω | 0.1075 | ChemSep v8.3 pure component data Compiled value | |
| ΔcH°liquid | -4127.20 ± 0.63 | kJ/mol | NIST |
| μ | 1.56 | debye | ChemSep v8.3 pure component data Compiled value |
| ΔfG° | 7.40 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | [-121.00; -120.90] | kJ/mol |
|
| ΔfH°gas | -120.90 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | -121.00 ± 0.75 | kJ/mol | NIST |
| ΔfH°liquid | -156.90 ± 0.75 | kJ/mol | NIST |
| ΔfusH° | 5.42 | kJ/mol | Joback Calculated Property |
| ΔvapH° | [34.20; 35.90] | kJ/mol |
|
| ΔvapH° | 35.90 | kJ/mol | NIST |
| ΔvapH° | Outlier 34.20 | kJ/mol | NIST |
| ΔvapH° | 35.90 | kJ/mol | NIST |
| ΔvapH° | 35.80 | kJ/mol | NIST |
| ΔvapH° | 35.90 | kJ/mol | NIST |
| ΔvapH° | 35.80 | kJ/mol | NIST |
| ΔvapH° | 35.90 | kJ/mol | NIST |
| IE | 8.38 ± 0.05 | eV | NIST |
| logPoct/wat | 2.148 | Crippen Calculated Property | |
| McVol | 97.660 | ml/mol | McGowan Calculated Property |
| Pc | 3400.00 | kPa | ChemSep v8.3 pure component data Compiled value |
| Ptriple | 8.18e-04 | kPa | ChemSep v8.3 pure component data Compiled value |
| Inp | [710.00; 725.00] |
|
|
| Inp | 724.00 | NIST | |
| Inp | 724.00 | NIST | |
| Inp | 724.00 | NIST | |
| Inp | Outlier 710.00 | NIST | |
| Inp | 725.00 | NIST | |
| Inp | 724.00 | NIST | |
| S°liquid | 276.14 | J/mol×K | NIST |
| Tboil | [372.05; 375.00] | K |
|
| Tboil | 372.05 | K | ChemSep v8.3 pure component data Compiled value |
| Tboil | 374.70 | K | NIST |
| Tboil | 372.10 | K | NIST |
| Tboil | 372.05 ± 0.20 | K | NIST |
| Tboil | 372.10 ± 0.30 | K | NIST |
| Tboil | 372.20 ± 0.50 | K | NIST |
| Tboil | 375.00 ± 4.00 | K | NIST |
| Tc | [569.80; 585.00] | K |
|
| Tc | 585.00 | K | ChemSep v8.3 pure component data Compiled value |
| Tc | 569.80 | K | NIST |
| Tfus | [190.84; 190.90] | K |
|
| Tfus | 190.84 | K | ChemSep v8.3 pure component data Compiled value |
| Tfus | 190.85 ± 0.20 | K | NIST |
| Tfus | 190.90 ± 0.30 | K | NIST |
| Ttriple | [184.86; 190.85] | K |
|
| Ttriple | 190.85 | K | Staveley, Lobo and Calado (1981), triple points Compiled value |
| Ttriple | 190.84 | K | ChemSep v8.3 pure component data Compiled value |
| Ttriple | 190.84 ± 0.02 | K | NIST |
| Ttriple | 184.86 ± 0.06 | K | NIST |
| Ttriple | 190.84 ± 0.02 | K | NIST |
| Ttriple | 184.86 ± 0.06 | K | NIST |
| UQi | 3.91 | ChemSep v8.3 pure component data Compiled value | |
| URi | 4.54 | ChemSep v8.3 pure component data Compiled value | |
| Vc | 0.370 | m3/kmol | ChemSep v8.3 pure component data Compiled value |
| VCOSTALD | 0.37 | m3/kmol | Hankinson and Thomson (1979), COSTALD parameters Compiled value |
| ωSRK | 0.24 | Hankinson and Thomson (1979), COSTALD parameters Compiled value | |
| Zc | 0.2690000 | ChemSep v8.3 pure component data Compiled value | |
| Zra | [0.27; 0.27] |
|
|
| Zra | 0.27 | Hankinson and Thomson (1979), COSTALD parameters Compiled value | |
| Zra | 0.27 | 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 | 199.95 | J/mol×K | 298.15 | NIST |
| ΔfusH | [8.41; 8.41] | kJ/mol | [190.80; 190.84] |
|
| ΔfusH | 8.41 | kJ/mol | 190.80 | NIST |
| ΔfusH | 8.41 | kJ/mol | 190.80 | NIST |
| ΔfusH | 8.41 | kJ/mol | 190.84 | NIST |
| ΔfusH | 8.41 | kJ/mol | 190.84 | NIST |
| ΔvapH | [31.47; 36.50] | kJ/mol | [336.50; 372.10] |
|
| ΔvapH | 36.50 | kJ/mol | 336.50 | NIST |
| ΔvapH | 35.10 | kJ/mol | 358.00 | NIST |
| ΔvapH | 31.47 | kJ/mol | 372.10 | NIST |
| ΔfusS | [44.09; 44.09] | J/mol×K | [190.84; 190.84] |
|
| ΔfusS | 44.09 | J/mol×K | 190.84 | NIST |
| ΔfusS | 44.09 | J/mol×K | 190.84 | NIST |
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [134.81; 353.20] | J/mol×K | [273.15; 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 | 8.78620e+01 | |||
| Coefficient B | -5.73150e+02 | |||
| Coefficient C | 5.92424e+00 | |||
| Coefficient D | 9.79620e-05 | |||
| Coefficient E | -4.80380e-08 | |||
| Temperature range, min. | 273.15 | |||
| Temperature range, max. | 1500.00 | |||
| Cp,gas | 134.81 | J/mol×K | 273.15 | Calculated Property |
| Cp,gas | 183.12 | J/mol×K | 409.47 | Calculated Property |
| Cp,gas | 223.94 | J/mol×K | 545.78 | Calculated Property |
| Cp,gas | 256.62 | J/mol×K | 682.10 | Calculated Property |
| Cp,gas | 282.65 | J/mol×K | 818.42 | Calculated Property |
| Cp,gas | 303.51 | J/mol×K | 954.73 | Calculated Property |
| Cp,gas | 320.30 | J/mol×K | 1091.05 | Calculated Property |
| Cp,gas | 333.81 | J/mol×K | 1227.37 | Calculated Property |
| Cp,gas | 344.64 | J/mol×K | 1363.68 | Calculated Property |
| Cp,gas | 353.20 | J/mol×K | 1500.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | [178.02; 222.36] | J/mol×K | [189.96; 372.05] |
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 | 1.41210e+02 | |||
| Coefficient B | 1.78650e+02 | |||
| Coefficient C | 7.91645e-01 | |||
| Coefficient D | 1.13930e-02 | |||
| Coefficient E | -8.05010e-06 | |||
| Temperature range, min. | 189.96 | |||
| Temperature range, max. | 372.05 | |||
| Cp,liquid | 178.02 | J/mol×K | 189.96 | Calculated Property |
| Cp,liquid | 180.88 | J/mol×K | 210.19 | Calculated Property |
| Cp,liquid | 184.36 | J/mol×K | 230.42 | Calculated Property |
| Cp,liquid | 188.41 | J/mol×K | 250.66 | Calculated Property |
| Cp,liquid | 192.97 | J/mol×K | 270.89 | Calculated Property |
| Cp,liquid | 198.02 | J/mol×K | 291.12 | Calculated Property |
| Cp,liquid | 203.53 | J/mol×K | 311.35 | Calculated Property |
| Cp,liquid | 209.45 | J/mol×K | 331.59 | Calculated Property |
| Cp,liquid | 215.75 | J/mol×K | 351.82 | Calculated Property |
| Cp,liquid | 222.36 | J/mol×K | 372.05 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [0.0039948; 0.0001960] | Pa×s | [190.84; 452.00] |
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 | -1.07680e+01 | |||
| Coefficient B | 9.96370e+02 | |||
| Coefficient C | 4.69640e-03 | |||
| Coefficient D | -1.08650e-08 | |||
| Coefficient E | 2.00000e+00 | |||
| Temperature range, min. | 190.84 | |||
| Temperature range, max. | 452.00 | |||
| η | 0.0039948 | Pa×s | 190.84 | Calculated Property |
| η | 0.0020066 | Pa×s | 219.86 | Calculated Property |
| η | 0.0011835 | Pa×s | 248.88 | Calculated Property |
| η | 0.0007794 | Pa×s | 277.89 | Calculated Property |
| η | 0.0005555 | Pa×s | 306.91 | Calculated Property |
| η | 0.0004197 | Pa×s | 335.93 | Calculated Property |
| η | 0.0003316 | Pa×s | 364.95 | Calculated Property |
| η | 0.0002712 | Pa×s | 393.96 | Calculated Property |
| η | 0.0002280 | Pa×s | 422.98 | Calculated Property |
| η | 0.0001960 | Pa×s | 452.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | [42.31; 8.92] | kJ/mol | [190.84; 570.00] |
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 | 6.77609e+01 | |||
| Coefficient B | 2.15699e+00 | |||
| Coefficient C | -4.00915e+00 | |||
| Coefficient D | 3.63034e+00 | |||
| Coefficient E | -1.23641e+00 | |||
| Critical temperature, Tc (K) | 5.85000e+02 | |||
| Temperature range, min. | 190.84 | |||
| Temperature range, max. | 570.00 | |||
| ΔvapH | 42.31 | kJ/mol | 190.84 | Calculated Property |
| ΔvapH | 39.59 | kJ/mol | 232.97 | Calculated Property |
| ΔvapH | 37.15 | kJ/mol | 275.10 | Calculated Property |
| ΔvapH | 34.78 | kJ/mol | 317.23 | Calculated Property |
| ΔvapH | 32.31 | kJ/mol | 359.36 | Calculated Property |
| ΔvapH | 29.55 | kJ/mol | 401.48 | Calculated Property |
| ΔvapH | 26.34 | kJ/mol | 443.61 | Calculated Property |
| ΔvapH | 22.43 | kJ/mol | 485.74 | Calculated Property |
| ΔvapH | 17.30 | kJ/mol | 527.87 | Calculated Property |
| ΔvapH | 8.92 | kJ/mol | 570.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.64] | kPa | [269.89; 399.18] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.38760e+01 | |||
| Coefficient B | -2.99505e+03 | |||
| Coefficient C | -4.94790e+01 | |||
| Temperature range, min. | 269.89 | |||
| Temperature range, max. | 399.18 | |||
| Pvap | 1.33 | kPa | 269.89 | Calculated Property |
| Pvap | 3.06 | kPa | 284.26 | Calculated Property |
| Pvap | 6.39 | kPa | 298.62 | Calculated Property |
| Pvap | 12.30 | kPa | 312.99 | Calculated Property |
| Pvap | 22.14 | kPa | 327.35 | Calculated Property |
| Pvap | 37.61 | kPa | 341.72 | Calculated Property |
| Pvap | 60.80 | kPa | 356.08 | Calculated Property |
| Pvap | 94.14 | kPa | 370.45 | Calculated Property |
| Pvap | 140.40 | kPa | 384.81 | Calculated Property |
| Pvap | 202.64 | kPa | 399.18 | Calculated Property |
| Pvap | [8.18e-04; 3400.00] | kPa | [190.84; 565.29] |
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 | 7.75574e+01 | |||
| Coefficient B | -6.78659e+03 | |||
| Coefficient C | -9.39689e+00 | |||
| Coefficient D | 6.66828e-06 | |||
| Coefficient E | 2.00000e+00 | |||
| Comment | Range stopped where the equation exceeds Pc; ChemSep gives it to 570 K. | |||
| Temperature range, min. | 190.84 | |||
| Temperature range, max. | 565.29 | |||
| Pvap | 8.18e-04 | kPa | 190.84 | Calculated Property |
| Pvap | 0.08 | kPa | 232.45 | Calculated Property |
| Pvap | 1.73 | kPa | 274.05 | Calculated Property |
| Pvap | 14.10 | kPa | 315.66 | Calculated Property |
| Pvap | 64.92 | kPa | 357.26 | Calculated Property |
| Pvap | 206.27 | kPa | 398.87 | Calculated Property |
| Pvap | 511.25 | kPa | 440.48 | Calculated Property |
| Pvap | 1068.91 | kPa | 482.08 | Calculated Property |
| Pvap | 1986.22 | kPa | 523.69 | Calculated Property |
| Pvap | 3400.00 | kPa | 565.29 | Calculated Property |
| Pvap | [9.28; 269.57] | kPa | [306.15; 410.15] |
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 | 7.81918e+01 | |||
| Coefficient B | -6.79559e+03 | |||
| Coefficient C | -9.50787e+00 | |||
| Coefficient D | 7.00157e-06 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 306.15 | |||
| Temperature range, max. | 410.15 | |||
| Pvap | 9.28 | kPa | 306.15 | Calculated Property |
| Pvap | 15.38 | kPa | 317.71 | Calculated Property |
| Pvap | 24.44 | kPa | 329.26 | Calculated Property |
| Pvap | 37.42 | kPa | 340.82 | Calculated Property |
| Pvap | 55.44 | kPa | 352.37 | Calculated Property |
| Pvap | 79.74 | kPa | 363.93 | Calculated Property |
| Pvap | 111.73 | kPa | 375.48 | Calculated Property |
| Pvap | 152.92 | kPa | 387.04 | Calculated Property |
| Pvap | 204.95 | kPa | 398.59 | Calculated Property |
| Pvap | 269.57 | kPa | 410.15 | Calculated Property |
| Pvap | [9.58; 270.08] | kPa | [306.86; 410.24] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.37511e+01 | |||
| Coefficient B | -2.90050e+03 | |||
| Coefficient C | -5.44550e+01 | |||
| Reference | Scott, Good, et al., 1962, 2 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 306.86 | |||
| Temperature range, max. | 410.24 | |||
| Pvap | 9.58 | kPa | 306.86 | Calculated Property |
| Pvap | 15.80 | kPa | 318.35 | Calculated Property |
| Pvap | 24.99 | kPa | 329.83 | Calculated Property |
| Pvap | 38.10 | kPa | 341.32 | Calculated Property |
| Pvap | 56.23 | kPa | 352.81 | Calculated Property |
| Pvap | 80.62 | kPa | 364.29 | Calculated Property |
| Pvap | 112.67 | kPa | 375.78 | Calculated Property |
| Pvap | 153.85 | kPa | 387.27 | Calculated Property |
| Pvap | 205.77 | kPa | 398.75 | Calculated Property |
| Pvap | 270.08 | kPa | 410.24 | Calculated Property |
| Pvap | [9.58; 270.08] | kPa | [306.86; 410.24] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.37511e+01 | |||
| Coefficient B | -2.90050e+03 | |||
| Coefficient C | -5.44550e+01 | |||
| Reference | Scott, Good, et al., 1962 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 306.86 | |||
| Temperature range, max. | 410.24 | |||
| Pvap | 9.58 | kPa | 306.86 | Calculated Property |
| Pvap | 15.80 | kPa | 318.35 | Calculated Property |
| Pvap | 24.99 | kPa | 329.83 | Calculated Property |
| Pvap | 38.10 | kPa | 341.32 | Calculated Property |
| Pvap | 56.23 | kPa | 352.81 | Calculated Property |
| Pvap | 80.62 | kPa | 364.29 | Calculated Property |
| Pvap | 112.67 | kPa | 375.78 | Calculated Property |
| Pvap | 153.85 | kPa | 387.27 | Calculated Property |
| Pvap | 205.77 | kPa | 398.75 | Calculated Property |
| Pvap | 270.08 | kPa | 410.24 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ρl | [909.32; 359.37] | kg/m3 | [190.84; 570.00] |
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 | 2.63911e-01 | |||
| Coefficient B | 1.59670e-02 | |||
| Coefficient C | 5.85000e+02 | |||
| Coefficient D | 8.06140e-02 | |||
| Temperature range, min. | 190.84 | |||
| Temperature range, max. | 570.00 | |||
| ρl | 909.32 | kg/m3 | 190.84 | Calculated Property |
| ρl | 876.86 | kg/m3 | 232.97 | Calculated Property |
| ρl | 841.98 | kg/m3 | 275.10 | Calculated Property |
| ρl | 804.10 | kg/m3 | 317.23 | Calculated Property |
| ρl | 762.41 | kg/m3 | 359.36 | Calculated Property |
| ρl | 715.65 | kg/m3 | 401.48 | Calculated Property |
| ρl | 661.69 | kg/m3 | 443.61 | Calculated Property |
| ρl | 596.48 | kg/m3 | 485.74 | Calculated Property |
| ρl | 510.23 | kg/m3 | 527.87 | Calculated Property |
| ρl | 359.37 | kg/m3 | 570.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| γ | [0.04; 4.80e-04] | N/m | [190.84; 570.00] |
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 | -2.55310e-02 | |||
| Coefficient B | -1.78050e+01 | |||
| Coefficient C | -2.27600e+00 | |||
| Coefficient D | -2.21450e-03 | |||
| Coefficient E | -2.45440e-07 | |||
| Temperature range, min. | 190.84 | |||
| Temperature range, max. | 570.00 | |||
| γ | 0.04 | N/m | 190.84 | Calculated Property |
| γ | 0.03 | N/m | 232.97 | Calculated Property |
| γ | 0.03 | N/m | 275.10 | Calculated Property |
| γ | 0.02 | N/m | 317.23 | Calculated Property |
| γ | 0.02 | N/m | 359.36 | Calculated Property |
| γ | 0.01 | N/m | 401.48 | Calculated Property |
| γ | 0.01 | N/m | 443.61 | Calculated Property |
| γ | 0.01 | N/m | 485.74 | Calculated Property |
| γ | 0.00 | N/m | 527.87 | Calculated Property |
| γ | 4.80e-04 | N/m | 570.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λgas | [0.01; 0.08] | W/m×K | [190.84; 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 | 1.68380e-04 | |||
| Coefficient B | 9.57670e-01 | |||
| Coefficient C | 5.99310e+02 | |||
| Coefficient D | 1.29930e+04 | |||
| Temperature range, min. | 190.84 | |||
| Temperature range, max. | 1000.00 | |||
| λgas | 0.01 | W/m×K | 190.84 | Calculated Property |
| λgas | 0.01 | W/m×K | 280.75 | Calculated Property |
| λgas | 0.02 | W/m×K | 370.65 | Calculated Property |
| λgas | 0.03 | W/m×K | 460.56 | Calculated Property |
| λgas | 0.03 | W/m×K | 550.47 | Calculated Property |
| λgas | 0.04 | W/m×K | 640.37 | Calculated Property |
| λgas | 0.05 | W/m×K | 730.28 | Calculated Property |
| λgas | 0.06 | W/m×K | 820.19 | Calculated Property |
| λgas | 0.07 | W/m×K | 910.09 | Calculated Property |
| λgas | 0.08 | W/m×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λliquid | [0.15; 0.11] | W/m×K | [190.84; 372.05] |
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 | -4.93240e-02 | |||
| Coefficient B | -5.47900e+00 | |||
| Coefficient C | -1.35590e+00 | |||
| Coefficient D | -9.17060e-04 | |||
| Coefficient E | -9.50730e-07 | |||
| Temperature range, min. | 190.84 | |||
| Temperature range, max. | 372.05 | |||
| λliquid | 0.15 | W/m×K | 190.84 | Calculated Property |
| λliquid | 0.15 | W/m×K | 210.97 | Calculated Property |
| λliquid | 0.14 | W/m×K | 231.11 | Calculated Property |
| λliquid | 0.14 | W/m×K | 251.24 | Calculated Property |
| λliquid | 0.13 | W/m×K | 271.38 | Calculated Property |
| λliquid | 0.13 | W/m×K | 291.51 | Calculated Property |
| λliquid | 0.12 | W/m×K | 311.65 | Calculated Property |
| λliquid | 0.12 | W/m×K | 331.78 | Calculated Property |
| λliquid | 0.11 | W/m×K | 351.92 | Calculated Property |
| λliquid | 0.11 | W/m×K | 372.05 | Calculated Property |
Similar Compounds
![Propane, 2,2'-[methylenebis(thio)]bis[2-methyl-.](data:image/png;base64,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)
![Propane, 2-methyl-2-[(1-methylethyl)thio]-.](data:image/png;base64,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)
Find more compounds similar to Propane, 2-methyl-2-(methylthio)-.
Sources
- KDB Vapor Pressure Data
- 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.
- Staveley, Lobo and Calado (1981), triple points ChEDL chemicals 1.5.2, from Staveley, L. A. K.; Lobo, L. Q.; Calado, J. C. G. Triple-Points of Low Melting Substances and Their Use in Cryogenic Work. Cryogenics 1981, 21, 131-144.
- 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
Note: Cheméo is only indexing the data, follow the source links to retrieve the latest data. The source is also providing more information like the publication year, authors and more.
Take the time to validate and double check the source of the data.
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