- InChI
- InChI=1S/C10H10/c1-8-6-9-4-2-3-5-10(9)7-8/h2-6H,7H2,1H3
- InChI Key
- YSAXEHWHSLANOM-UHFFFAOYSA-N
- Formula
- C10H10
- SMILES
- CC1=Cc2ccccc2C1
- Molecular Weight1
- 130.19
- CAS
- 2177-47-1
- Other Names
-
- 2-Methyl-1H-indene
- 2-methylindene
- Indene, 2-methyl-
- ω : Acentric Factor.
- 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).
- 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).
- 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.
- γ : Surface Tension (N/m).
- Tboil : Normal Boiling Point Temperature (K).
- Tboilr : Boiling point at reduced pressure (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 | 0.3508 | ChemSep v8.3 pure component data Compiled value | |
| μ | 0.00 | debye | ChemSep v8.3 pure component data Compiled value |
| ΔfG° | 219.00 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfH°gas | 115.00 | kJ/mol | ChemSep v8.3 pure component data Compiled value |
| ΔfusH° | 13.21 | kJ/mol | Joback Calculated Property |
| ΔvapH° | 53.35 | kJ/mol | Relay (1.0) Calculated Property |
| IE | 8.00 | eV | Relay (1.0) Calculated Property |
| logPoct/wat | 2.646 | Crippen Calculated Property | |
| McVol | 112.840 | ml/mol | McGowan Calculated Property |
| Pc | 3460.00 | kPa | ChemSep v8.3 pure component data Compiled value |
| Ptriple | 3.02 | kPa | ChemSep v8.3 pure component data Compiled value |
| Inp | [184.40; 1057.70] |
|
|
| Inp | 1054.10 | NIST | |
| Inp | 1057.70 | NIST | |
| Inp | 1054.10 | NIST | |
| Inp | 1057.70 | NIST | |
| Inp | 1052.00 | NIST | |
| Inp | 1056.00 | NIST | |
| Inp | 184.40 | NIST | |
| Inp | 184.70 | NIST | |
| Inp | 192.61 | NIST | |
| Inp | 184.40 | NIST | |
| Tboil | 479.45 | K | ChemSep v8.3 pure component data Compiled value |
| Tc | 711.00 | K | ChemSep v8.3 pure component data Compiled value |
| Tfus | [353.15; 353.15] | K |
|
| Tfus | 353.15 | K | Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value |
| Tfus | 353.15 | K | ChemSep v8.3 pure component data Compiled value |
| Ttriple | 353.15 | K | ChemSep v8.3 pure component data Compiled value |
| UQi | 3.55 | ChemSep v8.3 pure component data Compiled value | |
| URi | 5.10 | ChemSep v8.3 pure component data Compiled value | |
| Vc | 0.436 | m3/kmol | ChemSep v8.3 pure component data Compiled value |
| Zc | 0.2550000 | ChemSep v8.3 pure component data Compiled value | |
| Zra | 0.26 | 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.
Pressure Dependent Properties
| Property | Value | Unit | Pressure (kPa) | Source |
|---|---|---|---|---|
| Tboilr | 336.70 | K | 2.70 | NIST |
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [125.39; 384.88] | J/mol×K | [273.00; 1200.00] |
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 | -1.54380e+02 | |||
| Coefficient B | -1.93880e+02 | |||
| Coefficient C | 6.29524e+00 | |||
| Coefficient D | 1.93480e-04 | |||
| Coefficient E | -5.25350e-08 | |||
| Temperature range, min. | 273.00 | |||
| Temperature range, max. | 1200.00 | |||
| Cp,gas | 125.39 | J/mol×K | 273.00 | Calculated Property |
| Cp,gas | 191.10 | J/mol×K | 376.00 | Calculated Property |
| Cp,gas | 237.56 | J/mol×K | 479.00 | Calculated Property |
| Cp,gas | 272.68 | J/mol×K | 582.00 | Calculated Property |
| Cp,gas | 300.53 | J/mol×K | 685.00 | Calculated Property |
| Cp,gas | 323.35 | J/mol×K | 788.00 | Calculated Property |
| Cp,gas | 342.49 | J/mol×K | 891.00 | Calculated Property |
| Cp,gas | 358.79 | J/mol×K | 994.00 | Calculated Property |
| Cp,gas | 372.80 | J/mol×K | 1097.00 | Calculated Property |
| Cp,gas | 384.88 | J/mol×K | 1200.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,liquid | [189.50; 219.08] | J/mol×K | [280.00; 479.45] |
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 | 1.56160e+02 | |||
| Coefficient B | -2.00070e+02 | |||
| Coefficient C | 3.60424e+00 | |||
| Coefficient D | 2.50150e-03 | |||
| Coefficient E | -1.06350e-06 | |||
| Temperature range, min. | 280.00 | |||
| Temperature range, max. | 479.45 | |||
| Cp,liquid | 189.50 | J/mol×K | 280.00 | Calculated Property |
| Cp,liquid | 192.79 | J/mol×K | 302.16 | Calculated Property |
| Cp,liquid | 196.08 | J/mol×K | 324.32 | Calculated Property |
| Cp,liquid | 199.36 | J/mol×K | 346.48 | Calculated Property |
| Cp,liquid | 202.65 | J/mol×K | 368.64 | Calculated Property |
| Cp,liquid | 205.93 | J/mol×K | 390.81 | Calculated Property |
| Cp,liquid | 209.22 | J/mol×K | 412.97 | Calculated Property |
| Cp,liquid | 212.51 | J/mol×K | 435.13 | Calculated Property |
| Cp,liquid | 215.80 | J/mol×K | 457.29 | Calculated Property |
| Cp,liquid | 219.08 | J/mol×K | 479.45 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| η | [0.0006723; 0.0003428] | Pa×s | [353.15; 497.70] |
Joback Predicted correlation
|
| Equation | Y = exp(A + B/T + C·ln(T) + D·T^E) Y is η in Pa×s, T in K | |||
| Coefficient A | -9.62401e+00 | |||
| Coefficient B | 8.19030e+02 | |||
| Coefficient C | 0.00000e+00 | |||
| Coefficient D | 0.00000e+00 | |||
| Coefficient E | 0.00000e+00 | |||
| Comment | Liquid phase. Joback/Reid (1987), valid from Tf to 0.7·Tc. | |||
| Temperature range, min. | 353.15 | |||
| Temperature range, max. | 497.70 | |||
| η | 0.0006723 | Pa×s | 353.15 | Calculated Property |
| η | 0.0006078 | Pa×s | 369.21 | Calculated Property |
| η | 0.0005541 | Pa×s | 385.27 | Calculated Property |
| η | 0.0005089 | Pa×s | 401.33 | Calculated Property |
| η | 0.0004705 | Pa×s | 417.39 | Calculated Property |
| η | 0.0004375 | Pa×s | 433.46 | Calculated Property |
| η | 0.0004089 | Pa×s | 449.52 | Calculated Property |
| η | 0.0003840 | Pa×s | 465.58 | Calculated Property |
| η | 0.0003621 | Pa×s | 481.64 | Calculated Property |
| η | 0.0003428 | Pa×s | 497.70 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ΔvapH | [55.85; 0.00] | kJ/mol | [280.00; 711.00] |
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 | 7.30307e+01 | |||
| Coefficient B | 4.33923e-01 | |||
| Coefficient C | 7.64504e-01 | |||
| Coefficient D | -1.61563e+00 | |||
| Coefficient E | 8.43055e-01 | |||
| Critical temperature, Tc (K) | 7.11000e+02 | |||
| Temperature range, min. | 280.00 | |||
| Temperature range, max. | 711.00 | |||
| ΔvapH | 55.85 | kJ/mol | 280.00 | Calculated Property |
| ΔvapH | 52.77 | kJ/mol | 327.89 | Calculated Property |
| ΔvapH | 49.73 | kJ/mol | 375.78 | Calculated Property |
| ΔvapH | 46.67 | kJ/mol | 423.67 | Calculated Property |
| ΔvapH | 43.49 | kJ/mol | 471.56 | Calculated Property |
| ΔvapH | 40.01 | kJ/mol | 519.44 | Calculated Property |
| ΔvapH | 35.93 | kJ/mol | 567.33 | Calculated Property |
| ΔvapH | 30.72 | kJ/mol | 615.22 | Calculated Property |
| ΔvapH | 23.17 | kJ/mol | 663.11 | Calculated Property |
| ΔvapH | 0.00 | kJ/mol | 711.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.64] | kPa | [353.56; 503.70] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.46511e+01 | |||
| Coefficient B | -4.00919e+03 | |||
| Coefficient C | -7.44370e+01 | |||
| Temperature range, min. | 353.56 | |||
| Temperature range, max. | 503.70 | |||
| Pvap | 1.33 | kPa | 353.56 | Calculated Property |
| Pvap | 3.00 | kPa | 370.24 | Calculated Property |
| Pvap | 6.18 | kPa | 386.92 | Calculated Property |
| Pvap | 11.84 | kPa | 403.61 | Calculated Property |
| Pvap | 21.30 | kPa | 420.29 | Calculated Property |
| Pvap | 36.32 | kPa | 436.97 | Calculated Property |
| Pvap | 59.08 | kPa | 453.65 | Calculated Property |
| Pvap | 92.23 | kPa | 470.34 | Calculated Property |
| Pvap | 138.90 | kPa | 487.02 | Calculated Property |
| Pvap | 202.64 | kPa | 503.70 | Calculated Property |
| Pvap | [0.01; 3447.59] | kPa | [280.00; 711.00] |
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 | 8.53652e+01 | |||
| Coefficient B | -9.29920e+03 | |||
| Coefficient C | -1.00970e+01 | |||
| Coefficient D | 4.27860e-06 | |||
| Coefficient E | 2.00000e+00 | |||
| Temperature range, min. | 280.00 | |||
| Temperature range, max. | 711.00 | |||
| Pvap | 0.01 | kPa | 280.00 | Calculated Property |
| Pvap | 0.36 | kPa | 327.89 | Calculated Property |
| Pvap | 3.89 | kPa | 375.78 | Calculated Property |
| Pvap | 22.37 | kPa | 423.67 | Calculated Property |
| Pvap | 84.68 | kPa | 471.56 | Calculated Property |
| Pvap | 240.66 | kPa | 519.44 | Calculated Property |
| Pvap | 559.35 | kPa | 567.33 | Calculated Property |
| Pvap | 1126.34 | kPa | 615.22 | Calculated Property |
| Pvap | 2045.49 | kPa | 663.11 | Calculated Property |
| Pvap | 3447.59 | kPa | 711.00 | Calculated Property |
| Pvap | [3.00; 3435.13] | kPa | [353.15; 684.00] |
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 | 8.50029e+01 | |||
| Coefficient B | -8.85918e+03 | |||
| Coefficient C | -1.01245e+01 | |||
| Coefficient D | 4.66607e-06 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 353.15 | |||
| Temperature range, max. | 684.00 | |||
| Pvap | 3.00 | kPa | 353.15 | Calculated Property |
| Pvap | 13.32 | kPa | 389.91 | Calculated Property |
| Pvap | 43.60 | kPa | 426.67 | Calculated Property |
| Pvap | 114.20 | kPa | 463.43 | Calculated Property |
| Pvap | 253.48 | kPa | 500.19 | Calculated Property |
| Pvap | 496.58 | kPa | 536.96 | Calculated Property |
| Pvap | 884.47 | kPa | 573.72 | Calculated Property |
| Pvap | 1464.37 | kPa | 610.48 | Calculated Property |
| Pvap | 2291.89 | kPa | 647.24 | Calculated Property |
| Pvap | 3435.13 | kPa | 684.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| ρl | [988.24; 301.34] | kg/m3 | [280.00; 711.00] |
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 | 7.63569e+01 | |||
| Coefficient B | 2.53390e-01 | |||
| Coefficient C | 7.11000e+02 | |||
| Coefficient D | 2.89410e-01 | |||
| Temperature range, min. | 280.00 | |||
| Temperature range, max. | 711.00 | |||
| ρl | 988.24 | kg/m3 | 280.00 | Calculated Property |
| ρl | 949.68 | kg/m3 | 327.89 | Calculated Property |
| ρl | 909.24 | kg/m3 | 375.78 | Calculated Property |
| ρl | 866.47 | kg/m3 | 423.67 | Calculated Property |
| ρl | 820.68 | kg/m3 | 471.56 | Calculated Property |
| ρl | 770.84 | kg/m3 | 519.44 | Calculated Property |
| ρl | 715.12 | kg/m3 | 567.33 | Calculated Property |
| ρl | 649.86 | kg/m3 | 615.22 | Calculated Property |
| ρl | 565.14 | kg/m3 | 663.11 | Calculated Property |
| ρl | 301.34 | kg/m3 | 711.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| γ | [0.04; 5.14e-06] | N/m | [280.00; 705.83] |
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 | -4.61650e-02 | |||
| Coefficient B | -7.77210e+01 | |||
| Coefficient C | -1.53110e+00 | |||
| Coefficient D | -2.72480e-03 | |||
| Coefficient E | 9.81610e-07 | |||
| Comment | Range stopped where the equation turns negative; ChemSep gives it to 711 K. | |||
| Temperature range, min. | 280.00 | |||
| Temperature range, max. | 705.83 | |||
| γ | 0.04 | N/m | 280.00 | Calculated Property |
| γ | 0.03 | N/m | 327.31 | Calculated Property |
| γ | 0.03 | N/m | 374.63 | Calculated Property |
| γ | 0.02 | N/m | 421.94 | Calculated Property |
| γ | 0.02 | N/m | 469.26 | Calculated Property |
| γ | 0.01 | N/m | 516.57 | Calculated Property |
| γ | 0.01 | N/m | 563.89 | Calculated Property |
| γ | 0.01 | N/m | 611.20 | Calculated Property |
| γ | 0.00 | N/m | 658.51 | Calculated Property |
| γ | 5.14e-06 | N/m | 705.83 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λgas | [0.01; 0.07] | W/m×K | [353.15; 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 | 9.56800e-05 | |||
| Coefficient B | 1.02680e+00 | |||
| Coefficient C | 7.01490e+02 | |||
| Coefficient D | -3.10510e+04 | |||
| Temperature range, min. | 353.15 | |||
| Temperature range, max. | 1000.00 | |||
| λgas | 0.01 | W/m×K | 353.15 | Calculated Property |
| λgas | 0.02 | W/m×K | 425.02 | Calculated Property |
| λgas | 0.02 | W/m×K | 496.89 | Calculated Property |
| λgas | 0.03 | W/m×K | 568.77 | Calculated Property |
| λgas | 0.04 | W/m×K | 640.64 | Calculated Property |
| λgas | 0.04 | W/m×K | 712.51 | Calculated Property |
| λgas | 0.05 | W/m×K | 784.38 | Calculated Property |
| λgas | 0.06 | W/m×K | 856.26 | Calculated Property |
| λgas | 0.06 | W/m×K | 928.13 | Calculated Property |
| λgas | 0.07 | W/m×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| λliquid | [0.14; 0.10] | W/m×K | [280.00; 479.45] |
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 | 5.70460e-02 | |||
| Coefficient B | -1.81520e+02 | |||
| Coefficient C | -6.33120e-01 | |||
| Coefficient D | -3.87580e-03 | |||
| Coefficient E | -8.28390e-07 | |||
| Temperature range, min. | 280.00 | |||
| Temperature range, max. | 479.45 | |||
| λliquid | 0.14 | W/m×K | 280.00 | Calculated Property |
| λliquid | 0.14 | W/m×K | 302.16 | Calculated Property |
| λliquid | 0.14 | W/m×K | 324.32 | Calculated Property |
| λliquid | 0.13 | W/m×K | 346.48 | Calculated Property |
| λliquid | 0.13 | W/m×K | 368.64 | Calculated Property |
| λliquid | 0.12 | W/m×K | 390.81 | Calculated Property |
| λliquid | 0.12 | W/m×K | 412.97 | Calculated Property |
| λliquid | 0.11 | W/m×K | 435.13 | Calculated Property |
| λliquid | 0.11 | W/m×K | 457.29 | Calculated Property |
| λliquid | 0.10 | W/m×K | 479.45 | Calculated Property |
Similar Compounds
![1H-Cyclopent[b]anthracene.](data:image/png;base64,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)
Find more compounds similar to 1H-INDENE, 2-METHYL-.
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).
- 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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