- InChI
- InChI=1S/C4H8/c1-3-4-2/h3H,1,4H2,2H3
- InChI Key
- VXNZUUAINFGPBY-UHFFFAOYSA-N
- Formula
- C4H8
- SMILES
- C=CCC
- Molecular Weight1
- 56.11
- CAS
- 106-98-9
- Other Names
-
- 1-Butylene
- 1-C4H8
- BUT-1-ENE
- BUTENE-1
- ETHYLETHYLENE
- «alpha»-Butene
- «alpha»-Butylene
- «alpha»-Butene
- «alpha»-Butylene
- ω : Acentric Factor.
- Tig : Autoignition Temperature (K).
- ΔcH°gas : Standard gas 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).
- LFL : Lower Flammability Limit (% in Air).
- UFL : Upper Flammability Limit (% in Air).
- ΔfG° : Standard Gibbs free energy of formation (kJ/mol).
- Rg : Radius of Gyration.
- Δc,grossH : Heat of Combustion, Gross form (kJ/mol).
- Δc,netH : Heat of Combustion, Net Form (kJ/mol).
- ΔfH°gas : 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).
- log10WS : Log10 of Water solubility in mol/l.
- logPoct/wat : Octanol/Water partition coefficient.
- McVol : McGowan's characteristic volume (ml/mol).
- NFPA Fire : NFPA Fire Rating.
- NFPA Health : NFPA Health Rating.
- Pc : Critical Pressure (kPa).
- Pvap : Vapor pressure (kPa).
- ρc : Critical density (kg/m3).
- ρl : Liquid Density (kg/m3).
- Inp : Non-polar retention indices.
- I : 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).
- ΔvapS : Entropy of vaporization at a given temperature (J/mol×K).
- Tboil : Normal Boiling Point Temperature (K).
- Tc : Critical Temperature (K).
- Tfus : Normal melting (fusion) point (K).
- Ttriple : Triple Point Temperature (K).
- 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 | 0.1910 | KDB | |
| Tig | 658.15 | K | KDB |
| ΔcH°gas | -2716.80 ± 0.75 | kJ/mol | NIST |
| μ | 0.30 | debye | KDB |
| LFL | 1.60 | % in Air | KDB |
| UFL | 10.00 | % in Air | KDB |
| ΔfG° | 71.34 | kJ/mol | KDB |
| Rg | 2.7460 | KDB | |
| Δc,grossH | 2696.55 | kJ/mol | KDB |
| Δc,netH | 2520.483 | kJ/mol | KDB |
| ΔfH°gas | [-0.63; -0.13] | kJ/mol |
|
| ΔfH°gas | -0.13 | kJ/mol | KDB |
| ΔfH°gas | -0.63 ± 0.79 | kJ/mol | NIST |
| ΔfusH° | 4.84 | kJ/mol | Joback Calculated Property |
| ΔvapH° | [20.10; 20.88] | kJ/mol |
|
| ΔvapH° | 20.88 | kJ/mol | NIST |
| ΔvapH° | 20.10 | kJ/mol | NIST |
| IE | [9.55; 10.00] | eV |
|
| IE | 9.55 ± 0.06 | eV | NIST |
| IE | 9.55 ± 0.06 | eV | NIST |
| IE | 9.57 | eV | NIST |
| IE | 9.58 | eV | NIST |
| IE | 9.62 ± 0.05 | eV | NIST |
| IE | 9.59 ± 0.02 | eV | NIST |
| IE | 9.63 ± 0.02 | eV | NIST |
| IE | 9.62 ± 0.00 | eV | NIST |
| IE | 9.58 | eV | NIST |
| IE | 9.59 | eV | NIST |
| IE | 9.62 | eV | NIST |
| IE | 9.61 ± 0.02 | eV | NIST |
| IE | 9.58 ± 0.01 | eV | NIST |
| IE | 9.77 ± 0.01 | eV | NIST |
| IE | Outlier 10.00 | eV | NIST |
| IE | 9.72 | eV | NIST |
| log10WS | [-1.94; -1.94] |
|
|
| log10WS | -1.94 | Aq. Sol... | |
| log10WS | -1.94 | Estimat... | |
| logPoct/wat | 1.582 | Crippen Calculated Property | |
| McVol | 62.920 | ml/mol | McGowan Calculated Property |
| NFPA Fire | 4 | KDB | |
| NFPA Health | 1 | KDB | |
| Pc | [4000.00; 4020.00] | kPa |
|
| Pc | 4020.00 | kPa | KDB |
| Pc | 4005.10 | kPa | Thermod... |
| Pc | 4000.00 | kPa | Critica... |
| Pc | 4020.00 ± 50.00 | kPa | NIST |
| ρc | 232.84 ± 2.81 | kg/m3 | NIST |
| Inp | [382.00; 402.00] |
|
|
| Inp | 394.00 | NIST | |
| Inp | 394.00 | NIST | |
| Inp | 391.00 | NIST | |
| Inp | 389.00 | NIST | |
| Inp | 390.00 | NIST | |
| Inp | 388.70 | NIST | |
| Inp | 391.00 | NIST | |
| Inp | 390.00 | NIST | |
| Inp | 386.00 | NIST | |
| Inp | 384.40 | NIST | |
| Inp | 384.00 | NIST | |
| Inp | 395.00 | NIST | |
| Inp | 385.00 | NIST | |
| Inp | 385.00 | NIST | |
| Inp | 385.00 | NIST | |
| Inp | 385.00 | NIST | |
| Inp | 385.00 | NIST | |
| Inp | 393.00 | NIST | |
| Inp | 385.00 | NIST | |
| Inp | 389.20 | NIST | |
| Inp | 392.00 | NIST | |
| Inp | 386.00 | NIST | |
| Inp | Outlier 400.00 | NIST | |
| Inp | 388.00 | NIST | |
| Inp | 385.00 | NIST | |
| Inp | Outlier 402.00 | NIST | |
| Inp | Outlier 400.00 | NIST | |
| Inp | 390.00 | NIST | |
| Inp | 392.00 | NIST | |
| Inp | 382.00 | NIST | |
| Inp | 385.00 | NIST | |
| Inp | 385.00 | NIST | |
| Inp | 385.00 | NIST | |
| Inp | 388.00 | NIST | |
| Inp | 386.00 | NIST | |
| Inp | 387.00 | NIST | |
| Inp | 386.00 | NIST | |
| Inp | 390.00 | NIST | |
| Inp | 384.00 | NIST | |
| Inp | 391.00 | NIST | |
| Inp | 383.00 | NIST | |
| Inp | 387.00 | NIST | |
| Inp | 386.00 | NIST | |
| Inp | 386.00 | NIST | |
| Inp | 387.00 | NIST | |
| Inp | 387.00 | NIST | |
| Inp | 387.00 | NIST | |
| Inp | 386.00 | NIST | |
| Inp | 390.00 | NIST | |
| Inp | 390.00 | NIST | |
| Inp | 392.00 | NIST | |
| Inp | 389.20 | NIST | |
| Inp | 394.00 | NIST | |
| Inp | 388.70 | NIST | |
| Inp | 384.00 | NIST | |
| Inp | 385.00 | NIST | |
| I | [415.00; 436.00] |
|
|
| I | 436.00 | NIST | |
| I | 426.00 | NIST | |
| I | 415.00 | NIST | |
| I | 415.00 | NIST | |
| I | 436.00 | NIST | |
| S°liquid | [213.84; 229.06] | J/mol×K |
|
| S°liquid | 229.06 | J/mol×K | NIST |
| S°liquid | 227.00 | J/mol×K | NIST |
| S°liquid | 213.84 | J/mol×K | NIST |
| Tboil | 266.89 | K | KDB |
| Tc | [417.15; 419.60] | K |
|
| Tc | 419.50 | K | KDB |
| Tc | 419.50 ± 0.50 | K | NIST |
| Tc | 419.60 | K | NIST |
| Tc | 417.15 ± 2.00 | K | NIST |
| Tfus | [87.80; 87.93] | K |
|
| Tfus | 87.80 | K | KDB |
| Tfus | 87.93 | K | Aq. Sol... |
| Ttriple | [87.80; 87.83] | K |
|
| Ttriple | 87.80 ± 0.01 | K | NIST |
| Ttriple | 87.82 ± 0.02 | K | NIST |
| Ttriple | 87.80 ± 0.05 | K | NIST |
| Ttriple | 87.83 ± 0.05 | K | NIST |
| Vc | [0.241; 0.241] | m3/kmol |
|
| Vc | 0.241 | m3/kmol | KDB |
| Vc | 0.241 | m3/kmol | NIST |
| Zc | 0.2775330 | KDB | |
| Zra | 0.27 | KDB |
Temperature Dependent Properties
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [89.58; 101.21] | J/mol×K | [313.55; 363.25] |
|
| Cp,gas | 89.58 ± 0.06 | J/mol×K | 313.55 | NIST |
| Cp,gas | 101.21 ± 0.07 | J/mol×K | 363.25 | NIST |
| Cp,liquid | [118.00; 128.96] | J/mol×K | [253.40; 298.15] |
|
| Cp,liquid | 119.16 | J/mol×K | 253.40 | NIST |
| Cp,liquid | 119.45 | J/mol×K | 260.00 | NIST |
| Cp,liquid | 128.60 | J/mol×K | 294.00 | NIST |
| Cp,liquid | 128.96 | J/mol×K | 298.15 | NIST |
| Cp,liquid | 118.00 | J/mol×K | 298.15 | NIST |
| η | [0.0001647; 0.0020285] | Pa×s | [133.08; 287.60] |
|
| η | 0.0020285 | Pa×s | 133.08 | Joback Calculated Property |
| η | 0.0009508 | Pa×s | 158.83 | Joback Calculated Property |
| η | 0.0005506 | Pa×s | 184.59 | Joback Calculated Property |
| η | 0.0003645 | Pa×s | 210.34 | Joback Calculated Property |
| η | 0.0002640 | Pa×s | 236.09 | Joback Calculated Property |
| η | 0.0002038 | Pa×s | 261.85 | Joback Calculated Property |
| η | 0.0001647 | Pa×s | 287.60 | Joback Calculated Property |
| ΔfusH | [3.85; 3.96] | kJ/mol | [87.80; 87.82] |
|
| ΔfusH | 3.85 | kJ/mol | 87.80 | NIST |
| ΔfusH | 3.85 | kJ/mol | 87.80 | NIST |
| ΔfusH | 3.96 | kJ/mol | 87.81 | NIST |
| ΔfusH | 3.85 | kJ/mol | 87.82 | NIST |
| ΔfusH | 3.85 | kJ/mol | 87.82 | NIST |
| ΔvapH | [21.87; 28.30] | kJ/mol | [159.00; 376.50] |
|
| ΔvapH | 28.30 | kJ/mol | 159.00 | NIST |
| ΔvapH | 23.70 | kJ/mol | 202.00 | NIST |
| ΔvapH | 25.30 | kJ/mol | 202.00 | NIST |
| ΔvapH | 24.50 | kJ/mol | 219.00 | NIST |
| ΔvapH | 23.30 | kJ/mol | 237.00 | NIST |
| ΔvapH | 23.30 | kJ/mol | 242.00 | NIST |
| ΔvapH | 23.20 | kJ/mol | 244.50 | NIST |
| ΔvapH | 22.07 | kJ/mol | 266.90 | NIST |
| ΔvapH | 21.92 | kJ/mol | 266.90 | KDB |
| ΔvapH | 21.87 | kJ/mol | 266.91 | NIST |
| ΔvapH | 21.90 | kJ/mol | 267.00 | NIST |
| ΔvapH | 22.80 | kJ/mol | 306.00 | NIST |
| ΔvapH | 22.50 | kJ/mol | 339.00 | NIST |
| ΔvapH | 22.00 | kJ/mol | 376.50 | NIST |
| Pvap | [343.00; 1510.50] | kPa | [302.90; 364.53] |
|
| Pvap | 343.00 | kPa | 302.90 | Experim... |
| Pvap | 396.00 | kPa | 307.83 | Experim... |
| Pvap | 454.50 | kPa | 312.57 | Isother... |
| Pvap | 451.30 | kPa | 312.58 | Vapour ... |
| Pvap | 448.30 | kPa | 312.59 | Phase e... |
| Pvap | 456.00 | kPa | 312.96 | Experim... |
| Pvap | 521.00 | kPa | 318.05 | Experim... |
| Pvap | 525.20 | kPa | 318.32 | Vapor-L... |
| Pvap | 525.80 | kPa | 318.40 | Vapor-L... |
| Pvap | 525.55 | kPa | 318.42 | Vapour ... |
| Pvap | 593.00 | kPa | 322.94 | Experim... |
| Pvap | 596.14 | kPa | 323.27 | Vapor-L... |
| Pvap | 671.00 | kPa | 328.06 | Experim... |
| Pvap | 759.00 | kPa | 332.97 | Experim... |
| Pvap | 855.00 | kPa | 337.99 | Experim... |
| Pvap | 957.00 | kPa | 342.98 | Experim... |
| Pvap | 1069.00 | kPa | 347.93 | Experim... |
| Pvap | 1197.00 | kPa | 353.18 | Experim... |
| Pvap | 1510.50 | kPa | 364.51 | Vapor L... |
| Pvap | 1509.40 | kPa | 364.53 | Vapor-L... |
| ρl | 595.00 | kg/m3 | 293.00 | KDB |
| ΔfusS | [43.80; 45.09] | J/mol×K | [87.81; 87.82] |
|
| ΔfusS | 45.09 | J/mol×K | 87.81 | NIST |
| ΔfusS | 43.80 | J/mol×K | 87.82 | NIST |
| ΔfusS | 43.83 | J/mol×K | 87.82 | NIST |
| γ | 0.01 | N/m | 293.20 | KDB |
| ΔvapS | 81.92 | J/mol×K | 266.91 | NIST |
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.67] | kPa | [190.81; 285.85] |
The Yaw...
|
| Equation | ln(Pvp) = A + B/(T + C) | |||
| Coefficient A | 1.41892e+01 | |||
| Coefficient B | -2.33475e+03 | |||
| Coefficient C | -2.28580e+01 | |||
| Temperature range, min. | 190.81 | |||
| Temperature range, max. | 285.85 | |||
| Pvap | 1.33 | kPa | 190.81 | Calculated Property |
| Pvap | 3.04 | kPa | 201.37 | Calculated Property |
| Pvap | 6.30 | kPa | 211.93 | Calculated Property |
| Pvap | 12.11 | kPa | 222.49 | Calculated Property |
| Pvap | 21.79 | kPa | 233.05 | Calculated Property |
| Pvap | 37.07 | kPa | 243.61 | Calculated Property |
| Pvap | 60.08 | kPa | 254.17 | Calculated Property |
| Pvap | 93.35 | kPa | 264.73 | Calculated Property |
| Pvap | 139.80 | kPa | 275.29 | Calculated Property |
| Pvap | 202.67 | kPa | 285.85 | Calculated Property |
| Pvap | [3.40e-10; 3954.70] | kPa | [87.80; 419.59] |
KDB Vap...
|
| Equation | ln(Pvp) = A + B/T + C*ln(T) + D*T^2 | |||
| Coefficient A | 6.43474e+01 | |||
| Coefficient B | -4.50983e+03 | |||
| Coefficient C | -7.78979e+00 | |||
| Coefficient D | 9.81623e-06 | |||
| Temperature range, min. | 87.80 | |||
| Temperature range, max. | 419.59 | |||
| Pvap | 3.40e-10 | kPa | 87.80 | Calculated Property |
| Pvap | 9.46e-05 | kPa | 124.67 | Calculated Property |
| Pvap | 0.05 | kPa | 161.53 | Calculated Property |
| Pvap | 2.21 | kPa | 198.40 | Calculated Property |
| Pvap | 24.13 | kPa | 235.26 | Calculated Property |
| Pvap | 125.23 | kPa | 272.13 | Calculated Property |
| Pvap | 414.88 | kPa | 308.99 | Calculated Property |
| Pvap | 1035.55 | kPa | 345.86 | Calculated Property |
| Pvap | 2150.34 | kPa | 382.72 | Calculated Property |
| Pvap | 3954.70 | kPa | 419.59 | Calculated Property |
Similar Compounds
Find more compounds similar to 1-Butene.
Mixtures
- 1-Butene + Ethyl Acetate
- Dimethyl sulfide + 1-Butene
- 1-Butene + Diethyl sulfide
- 1-Butene + Propanenitrile
- 1-Butene + Propene, hexafluoro-
- 1-Butene + Hexafluoropropylene oxide
- 1-Butene + Difluoromethane
- 1-Butene + Butane, decafluoro-
- 1-Butene + 1-Propanol
- 1-Butene + Acetone
- 1-Butene + Isobutane
- 1-Butene + Methane + Isobutane
- 1-Butene + Carbon dioxide + Isobutane
- 1-Butene + Tetrahydropyran
- 1-Butene + 1-Butanol
- 1-Butene + Methyl Alcohol
- 1-Butene + 1-Propanol, 2-methyl-
- 2-Propanol, 2-methyl- + 1-Butene
- 1-Butene + 1-Pentanol
- 1-Butene + 2-Pentanol
Find more mixtures with 1-Butene.
Sources
- KDB Pure (Korean Thermophysical Properties Databank)
- KDB Vapor Pressure Data
- Crippen Method
- Thermodynamic properties of the butenes Part I. Experimental densities, vapor pressures, and critical points
- Vapour liquid equilibrium for the ethyl ethanoate + 1-butene, +cis-2-butene, +trans-2-butene, +2-methylpropene, +n-butane and +2-methylpropane
- Henry s law constants of 1-butene, 2-methylpropene, trans-2-butene, and 1,3-butadiene in methanol at 374 490K
- Isothermal binary vapour liquid equilibrium for butanes and butenes with dimethylsulphide
- Vapour liquid equilibrium for the systems diethyl sulphide + 1-butene, +cis-2-butene, +2-methylpropane, +2-methylpropene, +n-butane, +trans-2-butene
- Phase equilibrium measurements for systems containing propanenitrile with tert-butyl ethyl ether and C4-hydrocarbons
- Henry's constants and infinite dilution activity coefficients of propane, propene, butane, isobutene, 1-butene, isobutane, trans-2-butene and 1,3-butadiene in 1-propanol at T=(260 to 340) K
- Henry's constants and infinite dilution activity coefficients of propane, propene, butane, isobutane, 1-butene, isobutene, trans-2-butene, and 1,3-butadiene in isobutanol and tert-butanol
- Henry's constants and infinite dilution activity coefficients of propane, propene, butane, isobutane, 1-butene, isobutene, trans-2-butene, and 1,3-butadiene in 1-pentanol, 2-pentanol and 3-pentanol
- Experimental vapour liquid equilibrium data and modeling for binary mixtures of 1-butene with 1,1,2,3,3,3-hexafluoro-1-propene, 2,2,3-trifluoro-3-(trifluoromethyl)oxirane, or difluoromethane
- Experimental (vapour + liquid) equilibrium data and modelling for binary mixtures of decafluorobutane with propane and 1-butene
- Influence of a-Olefin Concentration and Length on the High-Pressure Phase Behavior of (a-Olefin + n-Hexane + LLDPE) Systems
- Henry's Constants and Infinite Dilution Activity Coefficients of Propane, Propene, Butane, Isobutane, 1-Butene, Isobutene, trans-2-Butene, and 1,3-butadiene in 2-propanol at 250-330 K
- Henry's Constants and Infinite Dilution Activity Coefficients of Propane, Propene, Butane, Isobutane, 1-Butene, Isobutene, trans-2-Butene and 1,3-Butadiene in 1-Butanol and 2-Butanol at (250 to 330) K
- Henry's law constants and infinite dilution activity coefficients of propane, propene, butane, isobutane, 1-butene, isobutene, trans-2-butene, and 1,3-butadiene in 2-methyl-1-butanol, 3-methyl-1-butanol, and 2-methyl-2-butanol
- Vapor-Liquid Equilibrium for 1-Propanol + 1-Butene, + cis-2-Butene, + 2-Methyl-propene, + trans-2-Butene, + n-Butane, and + 2-Methyl-propane
- Henry's Law Constants and Infinite Dilution Activity Coefficients of Propane, Propene, Butane, 2-Methylpropane, 1-Butene, 2-Methylpropene, trans-2-Butene, cis-2-Butene, 1,3-Butadiene, Dimethyl Ether, Chloroethane, and 1,1-Difluoroethane in 2-Propen-1-ol
- Henry s Law Constants and Infinite Dilution Activity Coefficients of Propane, Propene, Butane, 2-Methylpropane, 1-Butene, 2-Methylpropene, trans-2-Butene, cis-2-Butene, 1,3-Butadiene, Dimethyl Ether, Chloroethane, and 1,1-Difluoroethane in 2-Methyl-3-buten-2-ol and 3-Methyl-3-buten-1-ol
- Solubilities of Gases in the Ionic Liquid 1-n-Butyl-3-methylimidazolium Bis(trifluoromethylsulfonyl)imide
- Vapor Liquid Equilibrium for Six Binary Systems of C4-Hydrocarbons + 2-Propanone
- Henry's Law Constants and Infinite Dilution Activity Coefficients of Propane, Propene, Butane, 2-Methylpropane, 1-Butene, 2-Methylpropene, trans-2-Butene, cis-2-Butene, 1,3-Butadiene, Dimethyl Ether, Chloroethane, and 1,1-Difluoroethane in Benzene, Toluene, o-Xylene, m-Xylene, p-Xylene, and Styrene
- Henry's Law Constants and Infinite Dilution Activity Coefficients of Propane, Propene, Butane, 2-Methylpropane, 1-Butene, 2-Methylpropene, trans-2-Butene, cis-2-Butene, 1,3-Butadiene, Dimethyl Ether, Chloroethane, and 1,1-Difluoroethane in 2-Methylphenol, 3-Methylphenol, and 4-Methylphenol
- Critical Temperatures and Pressures of Several Binary and Ternary Mixtures Concerning the Alkylation of 2-Methylpropane with 1-Butene in the Presence of Methane or Carbon Dioxide
- Henry s Law Constants and Infinite Dilution Activity Coefficients of Propane, Propene, Butane, 2-Methylpropane, 1-Butene, 2-Methylpropene, trans-2-Butene, cis-2-Butene, 1,3-Butadiene, Dimethylether, Chloroethane, 1,1-Difluoroethane, and Hexane in Tetrahydropyran
- Vapor-Liquid Equilibrium for 1-Butene + Methanol, + 1-Propanol, + 2-Propanol, + 2-Butanol, and 2-Methyl-2-propanol (TBA) at 364.5 K
- Vapor-Liquid Equilibrium for 1-Butanol + 1-Butene at (318.4 and 364.5) K and Vapor-Liquid Equilibrium of 1-Butanol + 2-Methylpropane, + n-Butane and 1-Butene + 2-Methylpropane at 318.4 K
- Joback Method
- KDB
- Aqueous Solubility Prediction Method
- Estimated Solubility Method
- 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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