- InChI
- InChI=1S/C2H4F2/c1-2(3)4/h2H,1H3
- InChI Key
- NPNPZTNLOVBDOC-UHFFFAOYSA-N
- Formula
- C2H4F2
- SMILES
- CC(F)F
- Molecular Weight1
- 66.05
- CAS
- 75-37-6
- Other Names
-
- 1,1-difluoroethane
- Algofrene Type 67
- CH3CHF2
- Dymel 152
- Dymel 152A
- Ethylidene difluoride
- FC 152a
- Freon 152a
- GENETRON 100
- Genetron 152a
- HFC 152a
- Halocarbon 152A
- Propellant 152a
- R 152a
- R-152a
- REFRIGERANT-152A
- UN 1030
- ethylidene fluoride
- ω : Acentric Factor.
- 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).
- 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).
- 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).
- ν : Kinematic viscosity (m2/s).
- 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).
- ρc : Critical density (kg/m3).
- ρl : Liquid Density (kg/m3).
- Inp : Non-polar retention indices.
- γ : Surface Tension (N/m).
- 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.
- 1: Molecular weight from the IUPAC atomic weights tables.
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Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ω | 0.2560 | KDB | |
| ΔcH°gas | -1220.00 ± 8.40 | kJ/mol | NIST |
| μ | 2.30 | debye | KDB |
| ΔfG° | -436.50 | kJ/mol | KDB |
| ΔfH°gas | [-497.00; -494.00] | kJ/mol |
|
| ΔfH°gas | -494.00 | kJ/mol | KDB |
| ΔfH°gas | -497.00 ± 4.00 | kJ/mol | NIST |
| ΔfusH° | 3.57 | kJ/mol | Joback Calculated Property |
| ΔvapH° | 16.15 | kJ/mol | Relay (1.0) Calculated Property |
| IE | [11.86; 12.80] | eV |
|
| IE | 11.87 ± 0.03 | eV | NIST |
| IE | 11.87 ± 0.03 | eV | NIST |
| IE | 11.86 ± 0.03 | eV | NIST |
| IE | 12.68 | eV | NIST |
| IE | 12.80 | eV | NIST |
| log10WS | -0.16 | Relay (1.0) Calculated Property | |
| logPoct/wat | 1.271 | Crippen Calculated Property | |
| McVol | 42.580 | ml/mol | McGowan Calculated Property |
| Pc | [4495.00; 4519.80] | kPa |
|
| Pc | 4500.00 | kPa | KDB |
| Pc | 4495.00 ± 10.00 | kPa | NIST |
| Pc | 4515.70 ± 3.00 | kPa | NIST |
| Pc | 4519.80 ± 1.00 | kPa | NIST |
| Pc | 4495.36 ± 103.42 | kPa | NIST |
| Ptriple | [0.06; 0.06] | kPa |
|
| Ptriple | 0.06 ± 0.01 | kPa | NIST |
| Ptriple | 0.06 ± 0.01 | kPa | NIST |
| ρc | [365.26; 369.22] | kg/m3 |
|
| ρc | 368.81 ± 0.66 | kg/m3 | NIST |
| ρc | 367.90 ± 1.32 | kg/m3 | NIST |
| ρc | 367.90 ± 1.98 | kg/m3 | NIST |
| ρc | 369.22 ± 6.61 | kg/m3 | NIST |
| ρc | 367.90 ± 1.98 | kg/m3 | NIST |
| ρc | Outlier 365.26 ± 15.19 | kg/m3 | NIST |
| Inp | [242.00; 326.00] |
|
|
| Inp | 326.00 | NIST | |
| Inp | 242.00 | NIST | |
| Inp | 326.00 | NIST | |
| Tboil | [248.20; 248.50] | K |
|
| Tboil | 248.20 | K | KDB |
| Tboil | 248.40 | K | NIST |
| Tboil | 248.50 | K | NIST |
| Tboil | 248.45 ± 0.10 | K | NIST |
| Tc | [386.30; 386.70] | K |
|
| Tc | 386.70 | K | KDB |
| Tc | 386.39 ± 0.30 | K | NIST |
| Tc | 386.65 ± 0.60 | K | NIST |
| Tc | 386.41 ± 0.20 | K | NIST |
| Tc | 386.46 ± 0.20 | K | NIST |
| Tc | 386.30 ± 0.50 | K | NIST |
| Tc | 386.44 ± 0.01 | K | NIST |
| Tc | 386.65 ± 0.80 | K | NIST |
| Tfus | 156.00 | K | KDB |
| Ttriple | [154.30; 154.56] | K |
|
| Ttriple | 154.30 | K | Solid-Liquid Equilibria for the CO2 + R152a and N2O + R152a Systems |
| Ttriple | 154.56 ± 0.01 | K | NIST |
| Ttriple | 154.56 ± 0.01 | K | NIST |
| Vc | 0.181 | m3/kmol | KDB |
| Zc | 0.2533260 | KDB |
Temperature Dependent Properties
Datasets
Molar heat capacity at constant pressure, J/K/mol
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Molar heat capacity at constant pressure, J/K/mol - Liquid |
| 305.15 | 1490.00 | 121.00 |
| 305.15 | 2070.00 | 121.14 |
| 305.15 | 2540.00 | 120.81 |
| 305.15 | 2950.00 | 120.28 |
| 305.15 | 3440.00 | 119.29 |
| 305.15 | 4010.00 | 119.55 |
| 305.15 | 4600.00 | 118.96 |
| 305.15 | 5030.00 | 118.49 |
| 310.15 | 1490.00 | 121.80 |
| 310.15 | 2070.00 | 121.53 |
| 310.15 | 2540.00 | 121.07 |
| 310.15 | 2950.00 | 120.81 |
| 310.15 | 3440.00 | 120.08 |
| 310.15 | 4010.00 | 119.75 |
| 310.15 | 4600.00 | 119.35 |
| 310.15 | 5030.00 | 119.09 |
| 315.15 | 1490.00 | 123.84 |
| 315.15 | 2070.00 | 123.25 |
| 315.15 | 2540.00 | 122.79 |
| 315.15 | 2950.00 | 122.46 |
| 315.15 | 3440.00 | 121.80 |
| 315.15 | 4010.00 | 121.20 |
| 315.15 | 4600.00 | 120.61 |
| 315.15 | 5030.00 | 120.41 |
| 320.15 | 1490.00 | 126.16 |
| 320.15 | 2070.00 | 125.23 |
| 320.15 | 2540.00 | 124.77 |
| 320.15 | 2950.00 | 124.24 |
| 320.15 | 3440.00 | 123.71 |
| 320.15 | 4010.00 | 122.99 |
| 320.15 | 4600.00 | 122.06 |
| 320.15 | 5030.00 | 121.80 |
| 325.15 | 1490.00 | 129.00 |
| 325.15 | 2070.00 | 127.61 |
| 325.15 | 2540.00 | 127.01 |
| 325.15 | 2950.00 | 126.42 |
| 325.15 | 3440.00 | 125.89 |
| 325.15 | 4010.00 | 124.97 |
| 325.15 | 4600.00 | 123.84 |
| 325.15 | 5030.00 | 123.45 |
| 330.15 | 2070.00 | 130.65 |
| 330.15 | 2540.00 | 129.79 |
| 330.15 | 2950.00 | 129.13 |
| 330.15 | 3440.00 | 128.47 |
| 330.15 | 4010.00 | 127.41 |
| 330.15 | 4600.00 | 126.09 |
| 330.15 | 5030.00 | 125.63 |
| 335.15 | 2070.00 | 134.21 |
| 335.15 | 2540.00 | 133.22 |
| 335.15 | 2950.00 | 132.36 |
| 335.15 | 3440.00 | 131.44 |
| 335.15 | 4010.00 | 130.18 |
| 335.15 | 4600.00 | 128.80 |
| 335.15 | 5030.00 | 128.27 |
| 340.15 | 2540.00 | 137.25 |
| 340.15 | 2950.00 | 136.06 |
| 340.15 | 3440.00 | 134.94 |
| 340.15 | 4010.00 | 133.49 |
| 340.15 | 4600.00 | 131.90 |
| 340.15 | 5030.00 | 131.31 |
| 345.15 | 2540.00 | 141.88 |
| 345.15 | 2950.00 | 140.36 |
| 345.15 | 3440.00 | 139.04 |
| 345.15 | 4010.00 | 137.32 |
| 345.15 | 4600.00 | 135.34 |
| 345.15 | 5030.00 | 134.61 |
| 350.15 | 2950.00 | 146.10 |
| 350.15 | 3440.00 | 144.05 |
| 350.15 | 4010.00 | 141.88 |
| 350.15 | 4600.00 | 139.43 |
| 350.15 | 5030.00 | 138.51 |
| 355.15 | 3440.00 | 150.66 |
| 355.15 | 4010.00 | 147.56 |
| 355.15 | 4600.00 | 144.45 |
| 355.15 | 5030.00 | 143.20 |
| 360.15 | 4010.00 | 155.02 |
| 360.15 | 4600.00 | 151.06 |
| 360.15 | 5030.00 | 149.14 |
| Reference | ||
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [63.99; 137.19] | J/mol×K | [273.00; 1000.00] |
Joback Predicted correlation
|
| Equation | Y = A + B·T + C·T² + D·T³ + E·T⁴ Y is Cp,gas in J/mol×K, T in K | |||
| Coefficient A | 1.15700e+01 | |||
| Coefficient B | 2.23320e-01 | |||
| Coefficient C | -1.21000e-04 | |||
| Coefficient D | 2.33000e-08 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 273.00 | |||
| Temperature range, max. | 1000.00 | |||
| Cp,gas | 63.99 | J/mol×K | 273.00 | Calculated Property |
| Cp,gas | 76.46 | J/mol×K | 353.78 | Calculated Property |
| Cp,gas | 87.68 | J/mol×K | 434.56 | Calculated Property |
| Cp,gas | 97.71 | J/mol×K | 515.33 | Calculated Property |
| Cp,gas | 106.63 | J/mol×K | 596.11 | Calculated Property |
| Cp,gas | 114.52 | J/mol×K | 676.89 | Calculated Property |
| Cp,gas | 121.45 | J/mol×K | 757.67 | Calculated Property |
| Cp,gas | 127.48 | J/mol×K | 838.44 | Calculated Property |
| Cp,gas | 132.71 | J/mol×K | 919.22 | Calculated Property |
| Cp,gas | 137.19 | J/mol×K | 1000.00 | Calculated Property |
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 4495.07] | kPa | [180.88; 386.41] |
The Yaws Handbook of Vapor Pressure
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.44412e+01 | |||
| Coefficient B | -2.15958e+03 | |||
| Coefficient C | -2.82960e+01 | |||
| Temperature range, min. | 180.88 | |||
| Temperature range, max. | 386.41 | |||
| Pvap | 1.33 | kPa | 180.88 | Calculated Property |
| Pvap | 8.42 | kPa | 203.72 | Calculated Property |
| Pvap | 34.76 | kPa | 226.55 | Calculated Property |
| Pvap | 107.07 | kPa | 249.39 | Calculated Property |
| Pvap | 267.17 | kPa | 272.23 | Calculated Property |
| Pvap | 570.09 | kPa | 295.06 | Calculated Property |
| Pvap | 1079.39 | kPa | 317.90 | Calculated Property |
| Pvap | 1861.60 | kPa | 340.74 | Calculated Property |
| Pvap | 2980.92 | kPa | 363.57 | Calculated Property |
| Pvap | 4495.07 | kPa | 386.41 | Calculated Property |
| Pvap | [0.09; 4516.09] | kPa | [156.15; 386.60] |
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 | 7.01755e+01 | |||
| Coefficient B | -4.44787e+03 | |||
| Coefficient C | -8.80272e+00 | |||
| Coefficient D | 1.46275e-05 | |||
| Coefficient E | 0.00000e+00 | |||
| Temperature range, min. | 156.15 | |||
| Temperature range, max. | 386.60 | |||
| Pvap | 0.09 | kPa | 156.15 | Calculated Property |
| Pvap | 1.48 | kPa | 181.76 | Calculated Property |
| Pvap | 10.99 | kPa | 207.36 | Calculated Property |
| Pvap | 49.13 | kPa | 232.97 | Calculated Property |
| Pvap | 156.21 | kPa | 258.57 | Calculated Property |
| Pvap | 392.77 | kPa | 284.18 | Calculated Property |
| Pvap | 837.12 | kPa | 309.78 | Calculated Property |
| Pvap | 1585.57 | kPa | 335.39 | Calculated Property |
| Pvap | 2758.83 | kPa | 360.99 | Calculated Property |
| Pvap | 4516.09 | kPa | 386.60 | Calculated Property |
| Pvap | [0.13; 101.52] | kPa | [160.70; 246.70] |
NIST
|
| Equation | ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K | |||
| Coefficient A | 1.43545e+01 | |||
| Coefficient B | -2.06351e+03 | |||
| Coefficient C | -3.47140e+01 | |||
| Reference | Stull, 1947 | |||
| Comment | Coefficents calculated by NIST from author's data. | |||
| Temperature range, min. | 160.70 | |||
| Temperature range, max. | 246.70 | |||
| Pvap | 0.13 | kPa | 160.70 | Calculated Property |
| Pvap | 0.42 | kPa | 170.26 | Calculated Property |
| Pvap | 1.14 | kPa | 179.81 | Calculated Property |
| Pvap | 2.75 | kPa | 189.37 | Calculated Property |
| Pvap | 5.98 | kPa | 198.92 | Calculated Property |
| Pvap | 11.93 | kPa | 208.48 | Calculated Property |
| Pvap | 22.16 | kPa | 218.03 | Calculated Property |
| Pvap | 38.70 | kPa | 227.59 | Calculated Property |
| Pvap | 64.12 | kPa | 237.14 | Calculated Property |
| Pvap | 101.52 | kPa | 246.70 | Calculated Property |
Similar Compounds
Find more compounds similar to Ethane, 1,1-difluoro-.
Mixtures
- Methane, trifluoroiodo- + Ethane, 1,1-difluoro-
- Butane + Ethane, 1,1-difluoro-
- Ethane, pentafluoro- + Ethane, 1,1-difluoro-
- 1,1,1,3,3-Pentafluoropropane (R245fa) + Ethane, 1,1-difluoro-
- Ethane, 1,1-difluoro- + Methyl Alcohol
- 1-Propanol + Ethane, 1,1-difluoro-
- 2-Propanol + Ethane, 1,1-difluoro-
- 1-Butanol + Ethane, 1,1-difluoro-
- 2-Propanol, 2-methyl- + Ethane, 1,1-difluoro-
- 2-Pentanol + Ethane, 1,1-difluoro-
- Ethane, 1,1-difluoro- + 1-Pentanol
- Ethane, 1,1-difluoro- + 3-Pentanol
- 2-Methyl-1-butanol + Ethane, 1,1-difluoro-
- Amylene hydrate + Ethane, 1,1-difluoro-
- 1-Butanol, 3-methyl- + Ethane, 1,1-difluoro-
- 1-Propanol, 2-methyl- + Ethane, 1,1-difluoro-
- Ethane, 1,1,2,2-tetrafluoro- + Ethane, 1,1-difluoro-
- 1-Propene, 2-methyl- + Ethane, 1,1-difluoro-
- Carbon dioxide + Ethane, 1,1-difluoro-
- Ethane, 1,1'-oxybis[2-methoxy- + Ethane, 1,1-difluoro-
Find more mixtures with Ethane, 1,1-difluoro-.
Sources
- KDB Vapor Pressure Data
- Cheméo Relay (1.0)
- Crippen Method
- Crippen Method
- Vapor liquid equilibria for the binary system of 1,1-difluoroethane (HFC-152a) + n-butane (R-600) at various temperatures
- Vapor liquid equilibria of the 1,1-difluoroethane (HFC-152a) + isobutene system
- Surface tension of pentafluoroethane + 1,1-difluoroethane from (243 to 328)K
- Vapor-liquid equilibria of difluoromethane + N,N-dimethylacetamide, difluoromethane + dimethylether diethylene glycol and 1,1-difluoroethane + dimethylether diethylene glycol systems
- Phase equilibrium for the binary mixture of {1,1-difluoroethane (R152a) + trans-1,3,3,3-tetrafluoropropene (R1234ze (E))} at various temperatures from 258.150 to 288.150 K
- Isothermal VLE measurements for the binary mixture of 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) + 1,1-difluoroethane (HFC-152a)
- Gaseous absorption of fluorinated ethanes by ionic liquids
- The investigation on the vapor + liquid equilibrium for the ternary mixture isobutene (R600a) + 1,1-difluoroethane (R152a) + 1,1,2,2-tetrafluoroethane (R134) at temperatures from 253.150 to 273.150 K
- Henry's law constants and infinite dilution activity coefficients of cis-2-butene, dimethylether, chloroethane, and 1,1-difluoroethane in methanol, 1-propanol, 2-propanol, 1-butanol, 2-butanol, isobutanol, tert-butanol, 1-pentanol, 2-pentanol, 3-pentanol, 2-methyl-1-butanol, 3-methyl-1-butanol, and 2-methyl-2-butanol
- (Vapour + liquid) equilibria of the {1,1-difluoroethane (HFC-152a) + n-butane (HC-600)} system
- (Vapor + liquid) equilibrium data for (carbon dioxide + 1,1-difluoroethane) system at temperatures from (258 to 343) K and pressures up to about 8 MPa
- (Vapour + liquid) equilibrium data for the azeotropic {1,1-difluoroethane (R152a) + 1,1,2,2-Tetrafluoroethane (R134)} system at various temperatures from (258.150 to 288.150) K
- Measurements of isothermal (vapor + liquid) phase equilibrium for {trifluoroiodomethane (R13I1) + 1,1-difluoroethane (R152a)} from T = (258.150 to 283.150) K
- (Vapour + liquid) equilibrium data for the {1,1-difluoroethane (R152a) + 1,1,1,3,3-pentafluoropropane (R245fa)} system at temperatures from (323.150 to 353.150) K
- Diffusion coefficients and Henry's constants of hydrofluorocarbons in [HMIM][Tf2N], [HMIM][TfO], and [HMIM][BF4]
- Thermal conductivity data for refrigerant mixtures containing R1234yf and R1234ze(E)
- Measurement and Correlation of Isothermal Vapor Liquid Equilibrium of Fluoroethane + Dimethyl Ether Triethylene Glycol, 1,1-Difluoroethane + Dimethyl Ether Triethylene Glycol, and 1,1-Difluoroethane + N-Methyl-2-pyrrolidone Systems
- Vapor-Liquid Equilibria for the Binary and Ternary Systems of Difluoromethane (R32), 1,1-Difluoroethane (R152a), and 2,3,3,3-Tetrafluoroprop-1-ene (R1234yf)
- Liquid and Vapor Viscosities of Binary Refrigerant Mixtures Containing R1234yf or R1234ze(E)
- Viscosity of saturated liquid dimethyl ether from ( 227 to 343 ) K
- Speeds of Sound in Dense Liquid and Vapor Pressures for 1,1-Difluoroethane.
- Experimental P-T-G Measurements of Carbon Dioxide and 1,1-Difluoroethene Mixtures
- 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
- Vapor-Liquid-Liquid Equilibria of Hydrofluorocarbons + 1-Butyl-3-methylimidazolium Hexafluorophosphate
- 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
- Vapor-Liquid Equilibria for the 1,1-Difluoroethane (HFC-152a) + Propane (R-290) System
- 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
- Vapor Liquid Equilibrium Measurements of Difluoromethane + [Emim]OTf, Difluoromethane + [Bmim]OTf, Difluoroethane + [Emim]OTf, and Difluoroethane + [Bmim]OTf Systems
- Isothermal Vapor Liquid Equilibrium Measurements of 1,1-Difluoroethane + N,N-Dimethylformamide and N,N-Dimethylacetamide
- Isobaric Heat Capacity Measurements for Dimethyl Ether and 1,1-Difluoroethane in the Liquid Phase at Temperatures from 305 K to 365 K and Pressures up to 5 MPa
- Vapor Liquid Equilibrium of Three Hydrofluorocarbons with [HMIM][Tf2N]
- Isochoric PVTx Measurements for the Carbon Dioxide + 1,1-Difluoroethane Binary System
- 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
- Solid-Liquid Equilibria for the CO2 + R152a and N2O + R152a Systems
- Isothermal Vapor-Liquid Equilibria for 1,1-Difluoroethane (R152a) + Propane (R290) at Temperatures between (254.31 and 287.94) K
- Surface Tension of Propane (R-290) + 1,1-Difluoroethane (R-152a) from (248 to 328) K
- Joback Method
- KDB
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
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