Chemical Properties of Ethane, 1,1,1-trifluoro- (CAS 420-46-2)

InChI

InChI=1S/C2H3F3/c1-2(3,4)5/h1H3

InChI Key

UJPMYEOUBPIPHQ-UHFFFAOYSA-N

Formula

C2H3F3

SMILES

CC(F)(F)F

Molecular Weight¹

84.04

CAS

420-46-2

Other Names

• 1,1,1-Trifluoroform
• 1,1,1-trifluoroethane
• CFC 143A
• CH3CF3
• FC 143a
• FREON 143
• Fluorocarbon FC143a
• Freon 143a
• R 143a
• R-143a
• REFRIGERANT-143A
• methylfluoroform

• ω : Acentric Factor.
• Δ_cH°_gas : Standard gas enthalpy of combustion (kJ/mol).
• C_p,gas : Ideal gas heat capacity (J/mol×K).
• C_p,liquid : Liquid phase heat capacity (J/mol×K).
• μ : Dipole Moment (debye).
• η : Dynamic viscosity (Pa×s).
• Δ_fG° : Standard Gibbs free energy of formation (kJ/mol).
• Δ_fH°_gas : Enthalpy of formation at standard conditions (kJ/mol).
• Δ_fusH° : Enthalpy of fusion at standard conditions (kJ/mol).
• Δ_fusH : Enthalpy of fusion at a given temperature (kJ/mol).
• Δ_vapH° : Enthalpy of vaporization at standard conditions (kJ/mol).
• Δ_vapH : Enthalpy of vaporization at a given temperature (kJ/mol).
• IE : Ionization energy (eV).
• logP_oct/wat : Octanol/Water partition coefficient.
• McVol : McGowan's characteristic volume (ml/mol).
• P_c : Critical Pressure (kPa).
• P_vap : Vapor pressure (kPa).
• ρ_c : Critical density (kg/m³).
• ρ_g : Gas Density (kg/m³).
• I_np : Non-polar retention indices.
• Δ_fusS : Entropy of fusion at a given temperature (J/mol×K).
• S°_liquid : Liquid phase molar entropy at standard conditions (J/mol×K).
• Δ_vapS : Entropy of vaporization at a given temperature (J/mol×K).
• T_boil : Normal Boiling Point Temperature (K).
• T_c : Critical Temperature (K).
• T_fus : Normal melting (fusion) point (K).
• T_triple : Triple Point Temperature (K).
• V_c : Critical Volume (m³/kmol).
• Z_c : Critical Compressibility.
• ¹: Molecular weight from the IUPAC atomic weights tables.

Contents

1. Physical Properties
2. Temperature Dependent Properties
3. Datasets
4. Correlations
5. Similar Compounds
6. Mixtures
7. Sources

Physical Properties

Property	Value	Unit	Source
ω	0.2510		KDB
ΔcH°gas	-1008.00 ± 2.00	kJ/mol	NIST
μ	2.30	debye	KDB
ΔfG°	-679.20	kJ/mol	KDB
ΔfH°gas	[-749.00; -746.10]	kJ/mol
ΔfH°gas	-746.10	kJ/mol	KDB
ΔfH°gas	-748.70 ± 3.20	kJ/mol	NIST
ΔfH°gas	-749.00 ± 2.00	kJ/mol	NIST
ΔfusH°	2.76	kJ/mol	Joback Calculated Property
ΔvapH°	16.90	kJ/mol	Relay (1.0) Calculated Property
IE	[12.90; 13.80]	eV
IE	13.30 ± 0.10	eV	NIST
IE	13.80	eV	NIST
IE	12.90 ± 0.10	eV	NIST
logPoct/wat	1.569		Crippen Calculated Property
McVol	44.350	ml/mol	McGowan Calculated Property
Pc	[3411.60; 3769.00]	kPa
Pc	3760.00	kPa	KDB
Pc	3763.90 ± 5.00	kPa	NIST
Pc	3411.60 ± 5.00	kPa	NIST
Pc	3769.00 ± 5.00	kPa	NIST
Pc	3757.63 ± 103.42	kPa	NIST
ρc	[428.61; 433.65]	kg/m3
ρc	433.65 ± 3.36	kg/m3	NIST
ρc	433.65 ± 1.68	kg/m3	NIST
ρc	428.61 ± 3.36	kg/m3	NIST
ρc	433.65 ± 15.13	kg/m3	NIST
Inp	268.00		NIST
S°liquid	224.10	J/mol×K	NIST
Tboil	[225.60; 226.45]	K
Tboil	225.60	K	KDB
Tboil	226.00	K	NIST
Tboil	226.45 ± 0.10	K	NIST
Tc	[345.86; 346.30]	K
Tc	346.30	K	KDB
Tc	345.86 ± 0.05	K	NIST
Tc	345.86 ± 0.02	K	NIST
Tc	345.97 ± 0.20	K	NIST
Tc	346.25 ± 0.70	K	NIST
Tfus	161.80	K	KDB
Ttriple	[161.82; 161.82]	K
Ttriple	161.82 ± 0.02	K	NIST
Ttriple	161.82 ± 0.02	K	NIST
Vc	0.194	m3/kmol	KDB
Zc	0.2533380		KDB

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,gas	[63.79; 90.91]	J/mol×K	[239.74; 378.57]
Cp,gas	63.79	J/mol×K	239.74	Joback Calculated Property
Cp,gas	68.89	J/mol×K	262.88	Joback Calculated Property
Cp,gas	73.75	J/mol×K	286.02	Joback Calculated Property
Cp,gas	78.37	J/mol×K	309.15	Joback Calculated Property
Cp,gas	82.77	J/mol×K	332.29	Joback Calculated Property
Cp,gas	86.95	J/mol×K	355.43	Joback Calculated Property
Cp,gas	90.91	J/mol×K	378.57	Joback Calculated Property
Cp,liquid	[102.20; 224.39]	J/mol×K	[170.00; 350.00]
Cp,liquid	102.20	J/mol×K	170.00	Zabransky, M., Ruzicka, V., Majer, V. and Domalski, E. (1997), Heat Capacity of Liquids: Critical Review and Recommended Values - Monograph No. 6, J. Phys. & Chem. Ref. Data (JPCRD), National Institute of Standards and Technology, Gaithersburg, MD
Cp,liquid	103.40	J/mol×K	180.00	Zabransky, M., Ruzicka, V., Majer, V. and Domalski, E. (1997), Heat Capacity of Liquids: Critical Review and Recommended Values - Monograph No. 6, J. Phys. & Chem. Ref. Data (JPCRD), National Institute of Standards and Technology, Gaithersburg, MD
Cp,liquid	104.70	J/mol×K	190.00	Zabransky, M., Ruzicka, V., Majer, V. and Domalski, E. (1997), Heat Capacity of Liquids: Critical Review and Recommended Values - Monograph No. 6, J. Phys. & Chem. Ref. Data (JPCRD), National Institute of Standards and Technology, Gaithersburg, MD
Cp,liquid	106.20	J/mol×K	200.00	Zabransky, M., Ruzicka, V., Majer, V. and Domalski, E. (1997), Heat Capacity of Liquids: Critical Review and Recommended Values - Monograph No. 6, J. Phys. & Chem. Ref. Data (JPCRD), National Institute of Standards and Technology, Gaithersburg, MD
Cp,liquid	107.90	J/mol×K	210.00	Zabransky, M., Ruzicka, V., Majer, V. and Domalski, E. (1997), Heat Capacity of Liquids: Critical Review and Recommended Values - Monograph No. 6, J. Phys. & Chem. Ref. Data (JPCRD), National Institute of Standards and Technology, Gaithersburg, MD
Cp,liquid	109.66	J/mol×K	220.00	NIST
Cp,liquid	109.70	J/mol×K	220.00	Zabransky, M., Ruzicka, V., Majer, V. and Domalski, E. (1997), Heat Capacity of Liquids: Critical Review and Recommended Values - Monograph No. 6, J. Phys. & Chem. Ref. Data (JPCRD), National Institute of Standards and Technology, Gaithersburg, MD
Cp,liquid	136.15	J/mol×K	310.00	Measurements of the Isobaric Specific Heat Capacity for 1,1,1-Trifluoroethane (R143a), Pentafluoroethane (R125), and Difluoromethane (R32) in the Liquid Phase
Cp,liquid	140.35	J/mol×K	315.00	Measurements of the Isobaric Specific Heat Capacity for 1,1,1-Trifluoroethane (R143a), Pentafluoroethane (R125), and Difluoromethane (R32) in the Liquid Phase
Cp,liquid	145.39	J/mol×K	320.00	Measurements of the Isobaric Specific Heat Capacity for 1,1,1-Trifluoroethane (R143a), Pentafluoroethane (R125), and Difluoromethane (R32) in the Liquid Phase
Cp,liquid	150.43	J/mol×K	325.00	Measurements of the Isobaric Specific Heat Capacity for 1,1,1-Trifluoroethane (R143a), Pentafluoroethane (R125), and Difluoromethane (R32) in the Liquid Phase
Cp,liquid	155.47	J/mol×K	330.00	Measurements of the Isobaric Specific Heat Capacity for 1,1,1-Trifluoroethane (R143a), Pentafluoroethane (R125), and Difluoromethane (R32) in the Liquid Phase
Cp,liquid	162.20	J/mol×K	335.00	Measurements of the Isobaric Specific Heat Capacity for 1,1,1-Trifluoroethane (R143a), Pentafluoroethane (R125), and Difluoromethane (R32) in the Liquid Phase
Cp,liquid	173.96	J/mol×K	340.00	Measurements of the Isobaric Specific Heat Capacity for 1,1,1-Trifluoroethane (R143a), Pentafluoroethane (R125), and Difluoromethane (R32) in the Liquid Phase
Cp,liquid	192.45	J/mol×K	345.00	Measurements of the Isobaric Specific Heat Capacity for 1,1,1-Trifluoroethane (R143a), Pentafluoroethane (R125), and Difluoromethane (R32) in the Liquid Phase
Cp,liquid	189.93	J/mol×K	345.00	Measurements of the Isobaric Specific Heat Capacity for 1,1,1-Trifluoroethane (R143a), Pentafluoroethane (R125), and Difluoromethane (R32) in the Liquid Phase
Cp,liquid	224.39	J/mol×K	350.00	Measurements of the Isobaric Specific Heat Capacity for 1,1,1-Trifluoroethane (R143a), Pentafluoroethane (R125), and Difluoromethane (R32) in the Liquid Phase
ΔfusH	[0.30; 6.19]	kJ/mol	[156.40; 161.90]
ΔfusH	0.30	kJ/mol	156.40	NIST
ΔfusH	6.19	kJ/mol	161.80	NIST
ΔfusH	6.19	kJ/mol	161.90	NIST
ΔfusH	6.19	kJ/mol	161.90	NIST
ΔvapH	[8.70; 20.50]	kJ/mol	[200.00; 333.00]
ΔvapH	20.50	kJ/mol	200.00	NIST
ΔvapH	20.50	kJ/mol	200.00	NIST
ΔvapH	19.20 ± 0.10	kJ/mol	224.00	NIST
ΔvapH	19.20 ± 0.10	kJ/mol	224.00	NIST
ΔvapH	19.18	kJ/mol	224.40	NIST
ΔvapH	19.18	kJ/mol	224.40	NIST
ΔvapH	19.16	kJ/mol	225.70	KDB
ΔvapH	18.90	kJ/mol	233.00	NIST
ΔvapH	17.50	kJ/mol	258.00	NIST
ΔvapH	15.90	kJ/mol	258.00	NIST
ΔvapH	16.70	kJ/mol	258.00	NIST
ΔvapH	18.10	kJ/mol	258.00	NIST
ΔvapH	16.40	kJ/mol	273.00	NIST
ΔvapH	13.80	kJ/mol	303.00	NIST
ΔvapH	8.70	kJ/mol	333.00	NIST
Pvap	[529.20; 3553.00]	kPa	[268.15; 343.15]
Pvap	529.20	kPa	268.15	Measurement of vapor liquid equilibria for the binary systems of propane + 1,1,1,2-tetrafluoroethane and 1,1,1-trifluoroethane + propane at various temperatures
Pvap	626.00	kPa	273.15	(Vapour + liquid) equilibria of the {1,1,1-trifluoroethane (HFC-143a) + isobutene} system
Pvap	620.00	kPa	273.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	722.40	kPa	278.15	Measurement of vapor liquid equilibria for the binary systems of propane + 1,1,1,2-tetrafluoroethane and 1,1,1-trifluoroethane + propane at various temperatures
Pvap	837.00	kPa	283.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	838.60	kPa	283.15	Vapor-liquid equilibria for the 1,1,1,2 -tetrafluoroethane (HFC-134a) + 1,1,1,2,3,3,3-heptafluoropropane (HFC-227ea) and 1,1,1-trifluoroethane (HFC-143a) + 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) systems
Pvap	962.00	kPa	288.15	Measurement of vapor liquid equilibria for the binary systems of propane + 1,1,1,2-tetrafluoroethane and 1,1,1-trifluoroethane + propane at various temperatures
Pvap	972.00	kPa	288.15	(Vapour + liquid) equilibria of the {1,1,1-trifluoroethane (HFC-143a) + isobutene} system
Pvap	1107.90	kPa	293.15	Vapor-liquid equilibria for the 1,1,1,2 -tetrafluoroethane (HFC-134a) + 1,1,1,2,3,3,3-heptafluoropropane (HFC-227ea) and 1,1,1-trifluoroethane (HFC-143a) + 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) systems
Pvap	1104.00	kPa	293.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	1261.80	kPa	298.15	Measurement of vapor liquid equilibria for the binary systems of propane + 1,1,1,2-tetrafluoroethane and 1,1,1-trifluoroethane + propane at various temperatures
Pvap	1435.20	kPa	303.15	Vapor-liquid equilibria for the 1,1,1,2 -tetrafluoroethane (HFC-134a) + 1,1,1,2,3,3,3-heptafluoropropane (HFC-227ea) and 1,1,1-trifluoroethane (HFC-143a) + 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) systems
Pvap	1432.00	kPa	303.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	1442.00	kPa	303.15	(Vapour + liquid) equilibria of the {1,1,1-trifluoroethane (HFC-143a) + isobutene} system
Pvap	1619.80	kPa	308.15	Measurement of vapor liquid equilibria for the binary systems of propane + 1,1,1,2-tetrafluoroethane and 1,1,1-trifluoroethane + propane at various temperatures
Pvap	1831.00	kPa	313.15	Vapor liquid equilibria of the 1,1,1-trifluoroethane (HFC-143a) + dimethyl ether (DME) system
Pvap	1830.00	kPa	313.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	1831.00	kPa	313.15	Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane System
Pvap	1834.00	kPa	313.15	Vapor-liquid equilibria for the 1,1,1,2 -tetrafluoroethane (HFC-134a) + 1,1,1,2,3,3,3-heptafluoropropane (HFC-227ea) and 1,1,1-trifluoroethane (HFC-143a) + 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) systems
Pvap	1831.00	kPa	313.15	Vapor liquid equilibria of the 1,1,1-trifluoroethane (HFC-143a) + propane (HC-290) system
Pvap	2055.20	kPa	318.15	Measurement of vapor liquid equilibria for the binary systems of propane + 1,1,1,2-tetrafluoroethane and 1,1,1-trifluoroethane + propane at various temperatures
Pvap	2063.00	kPa	318.15	(Vapour + liquid) equilibria of the {1,1,1-trifluoroethane (HFC-143a) + isobutene} system
Pvap	2302.00	kPa	323.15	Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane System
Pvap	2309.70	kPa	323.15	Vapor-liquid equilibria for the 1,1,1,2 -tetrafluoroethane (HFC-134a) + 1,1,1,2,3,3,3-heptafluoropropane (HFC-227ea) and 1,1,1-trifluoroethane (HFC-143a) + 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) systems
Pvap	2302.00	kPa	323.15	Vapor liquid equilibria of the 1,1,1-trifluoroethane (HFC-143a) + dimethyl ether (DME) system
Pvap	2307.00	kPa	323.15	Vapor liquid equilibria of the 1,1,1-trifluoroethane (HFC-143a) + propane (HC-290) system
Pvap	2298.00	kPa	323.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	2875.00	kPa	333.15	(Vapour + liquid) equilibria of the {1,1,1-trifluoroethane (HFC-143a) + isobutene} system
Pvap	2874.00	kPa	333.15	Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane System
Pvap	2874.00	kPa	333.15	Vapor liquid equilibria of the 1,1,1-trifluoroethane (HFC-143a) + dimethyl ether (DME) system
Pvap	2874.00	kPa	333.15	Vapor liquid equilibria of the 1,1,1-trifluoroethane (HFC-143a) + propane (HC-290) system
Pvap	3553.00	kPa	343.15	Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane System
Pvap	3553.00	kPa	343.15	Vapor liquid equilibria of the 1,1,1-trifluoroethane (HFC-143a) + dimethyl ether (DME) system
ΔfusS	[1.90; 38.30]	J/mol×K	[156.40; 161.90]
ΔfusS	38.30	J/mol×K	156.40	NIST
ΔfusS	1.90	J/mol×K	161.90	NIST
ΔvapS	[85.45; 85.45]	J/mol×K	[224.40; 224.40]
ΔvapS	85.45	J/mol×K	224.40	NIST
ΔvapS	85.45	J/mol×K	224.40	NIST

Datasets

1. Molar heat capacity at constant pressure, J/K/mol (1)
2. Viscosity, Pa*s (1)
3. Mass density, kg/m3 (1)

Molar heat capacity at constant pressure, J/K/mol

Fixed		Measured
Temperature, K - Gas	Pressure, kPa - Gas	Molar heat capacity at constant pressure, J/K/mol - Gas
311.15	1600.00	120.18
317.15	1800.00	125.89
318.15	1600.00	111.77
318.15	2000.00	139.51
324.15	2200.00	145.31
326.15	2400.00	161.69
327.15	2400.00	160.77
338.15	2400.00	130.60
341.15	2200.00	117.24
343.15	2400.00	124.80
Reference

Viscosity, Pa*s

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Viscosity, Pa*s - Liquid
254.35	1340.00	0.0002
254.35	1350.00	0.0002
254.35	1360.00	0.0002
254.35	1410.00	0.0002
254.35	1450.00	0.0002
254.35	1960.00	0.0002
254.35	1970.00	0.0002
254.35	2010.00	0.0002
254.35	2040.00	0.0002
254.35	2070.00	0.0002
254.35	3110.00	0.0002
254.35	3160.00	0.0002
254.35	3170.00	0.0002
254.35	3210.00	0.0002
254.35	3280.00	0.0002
254.35	3320.00	0.0002
254.35	4170.00	0.0002
254.35	4190.00	0.0002
254.35	4210.00	0.0002
254.35	4940.00	0.0002
254.35	4970.00	0.0002
254.35	5000.00	0.0002
254.35	5020.00	0.0002
254.35	5050.00	0.0002
254.35	5100.00	0.0002
254.35	1350.00	0.0002
254.35	1360.00	0.0002
254.35	1960.00	0.0002
254.35	2010.00	0.0002
254.35	4210.00	0.0002
254.35	1350.00	0.0002
263.02	1300.00	0.0002
263.02	1320.00	0.0002
263.02	1330.00	0.0002
263.02	1970.00	0.0002
263.02	1980.00	0.0002
263.02	1990.00	0.0002
263.02	2010.00	0.0002
263.02	2020.00	0.0002
263.02	3420.00	0.0002
263.02	3430.00	0.0002
263.02	3450.00	0.0002
263.02	3520.00	0.0002
263.02	3560.00	0.0002
263.02	3590.00	0.0002
263.02	3640.00	0.0002
263.02	3670.00	0.0002
263.02	4800.00	0.0002
263.02	4840.00	0.0002
263.02	4870.00	0.0002
263.02	4910.00	0.0002
263.02	4950.00	0.0002
263.02	6990.00	0.0002
263.02	7090.00	0.0002
263.02	7160.00	0.0002
263.02	7200.00	0.0002
263.02	7230.00	0.0002
263.02	7310.00	0.0002
263.02	7380.00	0.0002
263.02	7390.00	0.0002
263.02	7420.00	0.0002
263.02	7460.00	0.0002
263.02	7520.00	0.0002
263.02	1320.00	0.0002
263.02	1330.00	0.0002
263.02	2020.00	0.0002
263.02	3670.00	0.0002
263.02	7310.00	0.0002
263.02	7460.00	0.0002
263.02	1330.00	0.0002
273.21	1420.00	0.0002
273.21	1430.00	0.0002
273.21	1440.00	0.0002
273.21	1450.00	0.0002
273.21	1810.00	0.0002
273.21	1820.00	0.0002
273.21	1860.00	0.0002
273.21	1890.00	0.0002
273.21	3450.00	0.0002
273.21	3460.00	0.0002
273.21	3490.00	0.0002
273.21	3500.00	0.0002
273.21	4850.00	0.0002
273.21	4860.00	0.0002
273.21	4880.00	0.0002
273.21	4910.00	0.0002
273.21	4960.00	0.0002
273.21	5010.00	0.0002
273.21	5030.00	0.0002
273.21	7780.00	0.0002
273.21	7800.00	0.0002
273.21	7810.00	0.0002
273.21	7900.00	0.0002
273.21	7960.00	0.0002
273.21	9530.00	0.0002
273.21	9540.00	0.0002
273.21	9580.00	0.0002
273.21	9610.00	0.0002
273.21	9770.00	0.0002
273.21	9880.00	0.0002
273.21	1440.00	0.0002
273.21	3450.00	0.0002
273.21	3490.00	0.0002
273.21	4880.00	0.0002
273.21	3450.00	0.0002
283.22	1240.00	0.0001
283.22	1260.00	0.0001
283.22	1470.00	0.0001
283.22	1510.00	0.0001
283.22	1530.00	0.0001
283.22	1570.00	0.0001
283.22	1900.00	0.0001
283.22	1930.00	0.0001
283.22	1950.00	0.0001
283.22	1970.00	0.0001
283.22	2000.00	0.0001
283.22	2050.00	0.0001
283.22	3700.00	0.0001
283.22	3720.00	0.0001
283.22	3850.00	0.0001
283.22	5130.00	0.0002
283.22	5220.00	0.0002
283.22	5260.00	0.0002
283.22	7400.00	0.0002
283.22	7500.00	0.0002
283.22	7540.00	0.0002
283.22	9720.00	0.0002
283.22	9780.00	0.0002
283.22	9940.00	0.0002
283.22	10050.00	0.0002
283.22	1240.00	0.0001
283.22	3700.00	0.0001
283.22	5260.00	0.0002
293.17	1370.00	0.0001
293.17	1390.00	0.0001
293.17	1400.00	0.0001
293.17	1420.00	0.0001
293.17	1430.00	0.0001
293.17	1440.00	0.0001
293.17	1850.00	0.0001
293.17	1860.00	0.0001
293.17	1890.00	0.0001
293.17	1920.00	0.0001
293.17	1940.00	0.0001
293.17	3820.00	0.0001
293.17	3830.00	0.0001
293.17	3850.00	0.0001
293.17	3860.00	0.0001
293.17	3870.00	0.0001
293.17	3890.00	0.0001
293.17	4900.00	0.0001
293.17	4920.00	0.0001
293.17	4960.00	0.0001
293.17	4970.00	0.0001
293.17	5010.00	0.0001
293.17	7450.00	0.0001
293.17	7490.00	0.0001
293.17	7520.00	0.0001
293.17	7550.00	0.0001
293.17	7560.00	0.0001
293.17	7590.00	0.0001
293.17	7620.00	0.0001
293.17	9740.00	0.0002
293.17	9770.00	0.0002
293.17	9820.00	0.0002
293.17	9880.00	0.0002
293.17	9970.00	0.0002
293.17	10070.00	0.0002
293.17	1390.00	0.0001
293.17	1430.00	0.0001
293.17	3890.00	0.0001
293.17	3890.00	0.0001
Reference

Mass density, kg/m3

Fixed		Measured
Temperature, K - Gas	Pressure, kPa - Gas	Mass density, kg/m3 - Gas
283.15	203.60	7.588
283.15	399.90	15.605
283.15	505.80	20.282
283.15	605.00	24.932
283.15	651.60	27.227
283.15	651.70	27.238
283.15	700.80	29.728
283.15	750.80	32.361
283.15	781.50	34.03
283.15	781.60	34.039
283.15	801.70	35.15
283.15	801.80	35.164
283.15	820.20	36.196
283.15	820.30	36.205
283.15	203.60	7.589
283.15	399.90	15.605
283.15	505.80	20.278
283.15	605.00	24.935
283.15	700.80	29.729
283.15	750.80	32.363
293.15	201.70	7.219
293.15	201.80	7.222
293.15	400.30	14.916
293.15	599.30	23.356
293.15	701.30	28.031
293.15	798.20	32.729
293.15	898.70	37.925
293.15	951.00	40.774
293.15	999.60	43.532
293.15	1030.90	45.365
293.15	1048.70	46.429
293.15	1048.80	46.429
293.15	1071.00	47.788
293.15	1071.10	47.784
293.15	1089.00	48.896
293.15	400.30	14.915
293.15	599.30	23.36
293.15	701.30	28.028
293.15	798.20	32.732
293.15	898.70	37.921
293.15	951.00	40.774
293.15	999.60	43.532
293.15	1030.90	45.355
293.15	1089.00	48.901
303.15	200.00	6.895
303.15	400.90	14.305
303.15	600.30	22.265
303.15	600.40	22.265
303.15	801.60	31.034
303.15	1001.00	40.662
303.15	1099.90	45.879
303.15	1197.30	51.364
303.15	1249.20	54.458
303.15	1299.50	57.578
303.15	1340.60	60.231
303.15	1369.80	62.181
303.15	1401.50	64.363
303.15	1423.70	65.925
303.15	1423.90	65.952
303.15	200.00	6.903
303.15	400.90	14.313
303.15	801.60	31.031
303.15	1001.00	40.666
303.15	1099.90	45.88
303.15	1197.30	51.363
303.15	1299.50	57.581
303.15	1340.60	60.229
303.15	1369.80	62.183
303.15	1401.50	64.364
313.15	201.50	6.696
313.15	201.80	6.718
313.15	205.10	6.831
313.15	206.20	6.869
313.15	401.60	13.776
313.15	401.70	13.775
313.15	600.30	21.275
313.15	800.30	29.41
313.15	999.10	38.197
313.15	1200.30	47.988
313.15	1400.20	58.893
313.15	1500.80	64.963
313.15	1540.90	67.443
313.15	1598.00	71.29
313.15	1598.10	71.312
313.15	1648.30	74.652
313.15	1701.30	78.498
313.15	1740.80	81.508
313.15	1771.10	83.908
313.15	1793.20	85.73
313.15	1794.40	85.811
313.15	205.10	6.828
313.15	600.30	21.282
313.15	800.30	29.413
313.15	999.10	38.204
313.15	1200.30	48.002
313.15	1400.20	58.909
313.15	1500.80	64.977
313.15	1540.90	67.442
313.15	1648.30	74.647
313.15	1701.30	78.51
313.15	1740.80	81.517
313.15	1771.10	83.916
Reference

Correlations

Property	Value	Unit	Temperature (K)	Source
Pvap	[1.19; 3729.50]	kPa	[161.82; 345.86]	The Yaws Handbook of Vapor Pressure
Equation			ln(Pvp) = A + B/(T + C)
Coefficient A			1.43786e+01
Coefficient B			-1.99833e+03
Coefficient C			-2.11680e+01
Temperature range, min.			161.82
Temperature range, max.			345.86
Pvap	1.19	kPa	161.82	Calculated Property
Pvap	7.20	kPa	182.27	Calculated Property
Pvap	29.12	kPa	202.72	Calculated Property
Pvap	88.75	kPa	223.17	Calculated Property
Pvap	220.34	kPa	243.62	Calculated Property
Pvap	469.41	kPa	264.06	Calculated Property
Pvap	889.20	kPa	284.51	Calculated Property
Pvap	1536.24	kPa	304.96	Calculated Property
Pvap	2466.04	kPa	325.41	Calculated Property
Pvap	3729.50	kPa	345.86	Calculated Property
Pvap	[1.14; 3748.81]	kPa	[161.85; 346.25]	KDB Vapor Pressure Data
Equation			ln(Pvp) = A + B/T + C*ln(T) + D*T^2
Coefficient A			6.77777e+01
Coefficient B			-3.95200e+03
Coefficient C			-8.58781e+00
Coefficient D			1.73454e-05
Temperature range, min.			161.85
Temperature range, max.			346.25
Pvap	1.14	kPa	161.85	Calculated Property
Pvap	7.20	kPa	182.34	Calculated Property
Pvap	29.53	kPa	202.83	Calculated Property
Pvap	89.83	kPa	223.32	Calculated Property
Pvap	220.81	kPa	243.81	Calculated Property
Pvap	464.76	kPa	264.29	Calculated Property
Pvap	872.40	kPa	284.78	Calculated Property
Pvap	1503.72	kPa	305.27	Calculated Property
Pvap	2431.66	kPa	325.76	Calculated Property
Pvap	3748.81	kPa	346.25	Calculated Property

Similar Compounds

Find more compounds similar to Ethane, 1,1,1-trifluoro-.

Mixtures

• Ethane, 1,1,1-trifluoro- + Dimethyl ether
• Propane + Ethane, 1,1,1-trifluoro-
• Ethane, 1,1,1-trifluoro- + Ethane, fluoro-
• Ethane, 1,1,1-trifluoro- + 1-Propene, 2-methyl-
• Ethane, 1,1,1-trifluoro- + Methane, difluoro- + Ethane, pentafluoro-
• Ethane, 1,1,1-trifluoro- + Butane
• Ethane, 1,1,1-trifluoro- + Ethane, pentafluoro-
• Ethane, 1,1,1-trifluoro- + Norflurane
• Ethane, 1,1,1-trifluoro- + Ethane, pentafluoro- + Methane, chlorodifluoro-
• Ethane, 1,1,1-trifluoro- + Ethane, pentafluoro- + Norflurane

Sources

• KDB Vapor Pressure Data
• Cheméo Relay (1.0)
• Crippen Method
• Crippen Method
• Viscosity of Alternative Refrigerants R407C and R407E in the Vapor Phase from 298.15 to 423.15K
• Measurements of Specific Heat Capacity of Gaseous R-143a Using a Flow Calorimeter
• Measurement of vapor liquid equilibria for the binary systems of propane + 1,1,1,2-tetrafluoroethane and 1,1,1-trifluoroethane + propane at various temperatures
• Vapor liquid equilibria of the 1,1,1-trifluoroethane (HFC-143a) + propane (HC-290) system
• Vapor liquid equilibria of the 1,1,1-trifluoroethane (HFC-143a) + dimethyl ether (DME) system
• Gas phase PVTx properties for binary mixtures of HFC-161 and HFC-143a
• Dielectric properties of 1,1,1-trifluoroethane (HFC-143a) in the liquid phase
• Vapor-liquid equilibria for the 1,1,1,2 -tetrafluoroethane (HFC-134a) + 1,1,1,2,3,3,3-heptafluoropropane (HFC-227ea) and 1,1,1-trifluoroethane (HFC-143a) + 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) systems
• Solubilities of R-161 and R-143a in 1-Hexyl-3-methylimidazolium bis(trifluoromethylsulfonyl)imide
• Gaseous absorption of fluorinated ethanes by ionic liquids
• (Vapour + liquid) equilibria of the {1,1,1-trifluoroethane (HFC-143a) + isobutene} system
• 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)
• Experimental Clathrate Hydrate Dissociation Data for Systems Comprising Refrigerant + CaCl2 Aqueous Solutions
• Liquid and Vapor Viscosities of Binary Refrigerant Mixtures Containing R1234yf or R1234ze(E)
• Surface Tension for the 1,1,1-Trifluoroethane (R-143a) + 1,1,1,2-Tetrafluoroethane (R-134a) System
• Acoustic Determination of Thermophysical Properties and Critical Parameters for R404A and Critical Line of xCO2 + (1 - x)R404A
• Viscosity of Compressed Liquid 1,1,1-Trifluoroethane (HFC-143a) and Pentafluoroethane (HFC-125)
• Vapor-Liquid-Liquid Equilibria of Hydrofluorocarbons + 1-Butyl-3-methylimidazolium Hexafluorophosphate
• Acoustic Determination of Thermophysical Properties and Critical Parameters for the Mixture (51 wt % R143a + 49 wt % R125) and Critical Line of xCO2 + (1 - x)(51 wt % R143a + 49 wt % R125)
• Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane System
• Isothermal Vapor-Liquid Equilibrium Data for the Binary Mixture Trifluoroethane (HFC-143a) + Ethyl Fluoride (HFC-161) over the Temperature Range (253.15 to 303.15) K
• Experimental Measurements and Thermodynamic Modeling of the Dissociation Conditions of Clathrate Hydrates for (Refrigerant + NaCl + Water) Systems
• Investigation on liquid density data at the bubble point and equations for the refrigerant HFC-404A over a wide temperature range
• Relative Permittivity Measurements of Trifluoromethyl Methyl Ether and Pentafluoroethyl Methyl Ether
• PVT Property Measurements for R143a, R125, and R32 in the Gaseous Phase
• Viscosity Measurements of Compressed Liquid Refrigerant Blend R-507A, Using a Vibrating-Wire Technique
• Relative Permittivity and Dipole Moments of Replacement Refrigerant Mixtures (R408A and R409A) in the Liquid State
• Binary Vapor Liquid and Vapor Liquid Liquid Equilibria of Hydrofluorocarbons (HFC-125 and HFC-143a) and Hydrofluoroethers (HFE-125 and HFE-143a) with Ionic Liquid [emim][Tf2N]
• Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
• Measurements of the Isobaric Specific Heat Capacity for 1,1,1-Trifluoroethane (R143a), Pentafluoroethane (R125), and Difluoromethane (R32) in the Liquid Phase
• Joback Method
• KDB
• McGowan Method
• NIST Webbook
• The Yaws Handbook of Vapor Pressure
• Zabransky, M., Ruzicka, V., Majer, V. and Domalski, E. (1997), Heat Capacity of Liquids: Critical Review and Recommended Values - Monograph No. 6, J. Phys. & Chem. Ref. Data (JPCRD), National Institute of Standards and Technology, Gaithersburg, MD

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