Chemical Properties of Ethylene (CAS 74-85-1)

InChI

InChI=1S/C2H4/c1-2/h1-2H2

InChI Key

VGGSQFUCUMXWEO-UHFFFAOYSA-N

Formula

C2H4

SMILES

C=C

Molecular Weight¹

28.05

CAS

74-85-1

Other Names

• Acetene
• Athylen
• Bicarburretted hydrogen
• C2H4
• Elayl
• Liquid ethyene
• Olefiant gas
• UN 1038
• UN 1962
• ethene

• ω : Acentric Factor.
• PAff : Proton affinity (kJ/mol).
• T_ig : Autoignition Temperature (K).
• BasG : Gas basicity (kJ/mol).
• 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).
• LFL : Lower Flammability Limit (% in Air).
• UFL : Upper Flammability Limit (% in Air).
• T_flash,oc : Flash Point (Open Cup Method) (K).
• Δ_fG° : Standard Gibbs free energy of formation (kJ/mol).
• R_g : Radius of Gyration.
• Δ_fH°_gas : Enthalpy of formation at standard conditions (kJ/mol).
• Δ_fH°_{(+) ion} : Enthalpy of formation of positive ion at standard conditions (kJ/mol).
• Δ_fH_{(+) ion,0K} : Enthalpy of formation of positive ion at 0K (kJ/mol).
• Δ_fusH° : Enthalpy of fusion at standard conditions (kJ/mol).
• Δ_fusH : Enthalpy of fusion at a given temperature (kJ/mol).
• Δ_subH : Enthalpy of sublimation at a given temperature (kJ/mol).
• Δ_vapH : Enthalpy of vaporization at a given temperature (kJ/mol).
• IE : Ionization energy (eV).
• log₁₀WS : Log10 of Water solubility in mol/l.
• logP_oct/wat : Octanol/Water partition coefficient.
• McVol : McGowan's characteristic volume (ml/mol).
• NFPA Fire : NFPA Fire Rating.
• NFPA Health : NFPA Health Rating.
• NFPA Safety : NFPA Safety Rating.
• P_c : Critical Pressure (kPa).
• P_triple : Triple Point Pressure (kPa).
• P_vap : Vapor pressure (kPa).
• ρ_c : Critical density (kg/m³).
• ρ_l : Liquid 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).
• γ : Surface Tension (N/m).
• Δ_vapS : Entropy of vaporization at a given temperature (J/mol×K).
• T_boil : Normal Boiling Point Temperature (K).
• T_c : Critical Temperature (K).
• λ : Gas thermal conductivity (W/m×K).
• T_fus : Normal melting (fusion) point (K).
• T_triple : Triple Point Temperature (K).
• V_c : Critical Volume (m³/kmol).
• Z_c : Critical Compressibility.
• Z_ra : Rackett Parameter.
• ¹: Molecular weight from the IUPAC atomic weights tables.

Physical Properties

Property	Value	Unit	Source
ω	0.0890		KDB
PAff	680.50	kJ/mol	NIST
Tig	723.15	K	KDB
BasG	651.50	kJ/mol	NIST
ΔcH°gas	-1411.20 ± 0.30	kJ/mol	NIST
μ	0.00	debye	KDB
LFL	2.70	% in Air	KDB
UFL	28.60	% in Air	KDB
Tflash,oc	137.04	K	KDB
ΔfG°	68.16	kJ/mol	KDB
Rg	1.5380		KDB
ΔfH°gas	[52.34; 52.40]	kJ/mol
ΔfH°gas	52.34	kJ/mol	KDB
ΔfH°gas	52.40 ± 0.50	kJ/mol	NIST
ΔfH°(+) ion	1067.00 ± 0.80	kJ/mol	NIST
ΔfH(+) ion,0K	1080.00	kJ/mol	NIST
ΔfusH°	-1.83	kJ/mol	Joback Calculated Property
IE	[10.50; 10.80]	eV
IE	10.51 ± 0.00	eV	NIST
IE	10.51	eV	NIST
IE	10.51 ± 0.00	eV	NIST
IE	10.51 ± 0.01	eV	NIST
IE	10.51 ± 0.01	eV	NIST
IE	10.51	eV	NIST
IE	10.50 ± 0.02	eV	NIST
IE	10.51 ± 0.01	eV	NIST
IE	10.51	eV	NIST
IE	10.51 ± 0.02	eV	NIST
IE	10.50	eV	NIST
IE	10.52 ± 0.00	eV	NIST
IE	10.52 ± 0.00	eV	NIST
IE	10.51	eV	NIST
IE	10.50	eV	NIST
IE	10.51 ± 0.00	eV	NIST
IE	10.51 ± 0.01	eV	NIST
IE	10.52 ± 0.00	eV	NIST
IE	10.51	eV	NIST
IE	10.51	eV	NIST
IE	10.51	eV	NIST
IE	10.56	eV	NIST
IE	10.51 ± 0.02	eV	NIST
IE	10.51 ± 0.05	eV	NIST
IE	10.50 ± 0.05	eV	NIST
IE	10.51	eV	NIST
IE	10.51 ± 0.01	eV	NIST
IE	10.50 ± 0.01	eV	NIST
IE	10.51 ± 0.00	eV	NIST
IE	10.50 ± 0.02	eV	NIST
IE	10.52 ± 0.01	eV	NIST
IE	10.51 ± 0.03	eV	NIST
IE	Outlier 10.80 ± 0.05	eV	NIST
IE	Outlier 10.68	eV	NIST
IE	10.50 ± 0.01	eV	NIST
IE	10.50	eV	NIST
IE	10.50	eV	NIST
log10WS	[-0.40; -0.40]
log10WS	-0.40		Aq. Solubility Prediction
log10WS	-0.40		Estimated Solubility
logPoct/wat	0.802		Crippen Calculated Property
McVol	34.740	ml/mol	McGowan Calculated Property
NFPA Fire	4		KDB
NFPA Health	1		KDB
NFPA Safety	2		KDB
Pc	[5020.00; 5119.95]	kPa
Pc	5020.00	kPa	Gas-Liquid Critical Properties of Ethylene + Hydrogen and Propylene + Hydrogen Binary Mixtures
Pc	5041.00	kPa	KDB
Pc	5041.00 ± 4.00	kPa	NIST
Pc	5055.00 ± 5.04	kPa	NIST
Pc	5040.10 ± 5.00	kPa	NIST
Pc	5055.00 ± 5.00	kPa	NIST
Pc	5040.30 ± 0.20	kPa	NIST
Pc	5040.30 ± 0.20	kPa	NIST
Pc	5042.00 ± 4.00	kPa	NIST
Pc	5076.00 ± 2.00	kPa	NIST
Pc	Outlier 5119.95 ± 20.26	kPa	NIST
Pc	5061.00 ± 101.32	kPa	NIST
Ptriple	[0.12; 0.12]	kPa
Ptriple	0.12 ± 0.01	kPa	NIST
Ptriple	0.12	kPa	NIST
ρc	[214.05; 530.04]	kg/m3
ρc	214.05 ± 0.11	kg/m3	NIST
ρc	214.14 ± 0.11	kg/m3	NIST
ρc	214.16 ± 0.02	kg/m3	NIST
ρc	530.04 ± 0.20	kg/m3	NIST
ρc	215.97 ± 0.56	kg/m3	NIST
Inp	[158.00; 188.00]
Inp	166.00		NIST
Inp	175.00		NIST
Inp	177.00		NIST
Inp	177.00		NIST
Inp	178.00		NIST
Inp	178.00		NIST
Inp	178.10		NIST
Inp	164.00		NIST
Inp	183.00		NIST
Inp	158.00		NIST
Inp	166.00		NIST
Inp	165.00		NIST
Inp	178.00		NIST
Inp	180.00		NIST
Inp	166.00		NIST
Inp	165.00		NIST
Inp	165.00		NIST
Inp	165.00		NIST
Inp	165.00		NIST
Inp	188.00		NIST
Inp	180.00		NIST
Inp	166.00		NIST
Inp	178.00		NIST
Inp	183.00		NIST
Inp	158.00		NIST
S°liquid	117.80	J/mol×K	NIST
Tboil	[168.08; 170.45]	K
Tboil	169.38	K	KDB
Tboil	169.35 ± 0.02	K	NIST
Tboil	169.30 ± 0.20	K	NIST
Tboil	Outlier 168.08 ± 2.00	K	NIST
Tboil	169.25 ± 0.50	K	NIST
Tboil	169.00 ± 0.30	K	NIST
Tboil	169.25 ± 0.50	K	NIST
Tboil	169.43 ± 0.50	K	NIST
Tboil	169.30 ± 0.50	K	NIST
Tboil	Outlier 170.45 ± 0.70	K	NIST
Tc	[282.33; 283.10]	K
Tc	282.34	K	KDB
Tc	282.34 ± 0.02	K	NIST
Tc	282.33 ± 0.02	K	NIST
Tc	282.35 ± 0.02	K	NIST
Tc	282.33 ± 0.10	K	NIST
Tc	282.34 ± 0.00	K	NIST
Tc	282.34 ± 0.00	K	NIST
Tc	282.35 ± 0.03	K	NIST
Tc	282.65 ± 0.25	K	NIST
Tc	282.69 ± 0.30	K	NIST
Tc	Outlier 283.10 ± 0.60	K	NIST
Tfus	[103.70; 104.01]	K
Tfus	104.00	K	KDB
Tfus	104.01	K	Aq. Solubility Prediction
Tfus	103.80 ± 0.20	K	NIST
Tfus	103.70 ± 0.50	K	NIST
Tfus	103.70 ± 1.00	K	NIST
Ttriple	[103.80; 104.10]	K
Ttriple	103.99 ± 0.05	K	NIST
Ttriple	103.98 ± 0.01	K	NIST
Ttriple	103.97 ± 0.02	K	NIST
Ttriple	103.97 ± 0.03	K	NIST
Ttriple	104.10 ± 0.50	K	NIST
Ttriple	103.97 ± 0.02	K	NIST
Ttriple	103.97 ± 0.15	K	NIST
Ttriple	103.95 ± 0.10	K	NIST
Ttriple	Outlier 103.80 ± 0.30	K	NIST
Vc	[0.129; 0.131]	m3/kmol
Vc	0.131	m3/kmol	KDB
Vc	0.131	m3/kmol	NIST
Vc	0.131 ± 0.000	m3/kmol	NIST
Vc	0.131 ± 0.000	m3/kmol	NIST
Vc	0.129 ± 0.000	m3/kmol	NIST
Zc	0.2815210		KDB
Zra	0.28		KDB

Cheméo can also estimate Enthalpy of vaporization at standard conditions 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	[34.66; 59.25]	J/mol×K	[178.15; 463.60]
Cp,gas	34.66 ± 0.26	J/mol×K	178.15	NIST
Cp,gas	35.30 ± 0.26	J/mol×K	192.35	NIST
Cp,gas	36.29 ± 0.27	J/mol×K	210.40	NIST
Cp,gas	37.55 ± 0.28	J/mol×K	230.90	NIST
Cp,gas	39.02 ± 0.29	J/mol×K	250.60	NIST
Cp,gas	40.75 ± 0.02	J/mol×K	270.70	NIST
Cp,gas	41.02 ± 0.31	J/mol×K	271.80	NIST
Cp,gas	42.84 ± 0.32	J/mol×K	293.45	NIST
Cp,gas	43.47 ± 0.17	J/mol×K	300.00	NIST
Cp,gas	45.98 ± 0.04	J/mol×K	320.70	NIST
Cp,gas	49.74 ± 0.37	J/mol×K	367.70	NIST
Cp,gas	59.25 ± 0.44	J/mol×K	463.60	NIST
Cp,liquid	[67.17; 68.90]	J/mol×K	[110.00; 170.00]
Cp,liquid	68.90	J/mol×K	110.00	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	68.30	J/mol×K	120.00	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	67.83	J/mol×K	130.00	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	67.48	J/mol×K	140.00	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	67.26	J/mol×K	150.00	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	67.17	J/mol×K	160.00	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	67.21	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	67.40	J/mol×K	170.00	NIST
Cp,liquid	67.24	J/mol×K	170.00	NIST
ΔfusH	[3.35; 3.35]	kJ/mol	[103.95; 104.00]
ΔfusH	3.35	kJ/mol	103.95	NIST
ΔfusH	3.35	kJ/mol	103.97	NIST
ΔfusH	3.35	kJ/mol	104.00	NIST
ΔfusH	3.35	kJ/mol	104.00	NIST
ΔsubH	[15.00; 18.40]	kJ/mol	[90.00; 91.50]
ΔsubH	15.00	kJ/mol	90.00	NIST
ΔsubH	18.40	kJ/mol	91.50	NIST
ΔvapH	[13.54; 14.40]	kJ/mol	[145.00; 267.00]
ΔvapH	14.40	kJ/mol	145.00	NIST
ΔvapH	14.40	kJ/mol	147.50	NIST
ΔvapH	14.10	kJ/mol	151.00	NIST
ΔvapH	14.30	kJ/mol	161.00	NIST
ΔvapH	13.54	kJ/mol	169.40	KDB
ΔvapH	13.54	kJ/mol	169.40	NIST
ΔvapH	14.00	kJ/mol	170.00	NIST
ΔvapH	13.70	kJ/mol	190.00	NIST
ΔvapH	13.70	kJ/mol	221.50	NIST
ΔvapH	13.60	kJ/mol	231.50	NIST
ΔvapH	14.00	kJ/mol	267.00	NIST
Pvap	[1476.00; 4891.00]	kPa	[233.73; 280.98]
Pvap	1476.00	kPa	233.73	Vapor-Liquid Equilibrium (PTxy) Measurements and Modeling for the CO-C2H4 Binary System
Pvap	1932.30	kPa	243.08	Vapor-Liquid Equilibrium (PTxy) Measurements and Modeling for the CO-C2H4 Binary System
Pvap	2534.80	kPa	253.22	Vapor-Liquid Equilibrium (PTxy) Measurements and Modeling for the CO-C2H4 Binary System
Pvap	2732.00	kPa	256.22	Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
Pvap	2903.00	kPa	258.59	Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
Pvap	3083.00	kPa	261.02	Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
Pvap	3247.50	kPa	263.22	Vapor-Liquid Equilibrium (PTxy) Measurements and Modeling for the CO-C2H4 Binary System
Pvap	3272.00	kPa	263.48	Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
Pvap	3470.00	kPa	265.94	Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
Pvap	3648.50	kPa	268.13	Vapor-liquid equilibria of ethylene (C2H4) + decafluorobutane (C4F10) at 268 to 298 K from experiment, molecular simulation and the Peng-Robinson equation of state
Pvap	3671.00	kPa	268.37	Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
Pvap	3891.00	kPa	270.85	Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
Pvap	4094.00	kPa	273.15	Phase equilibrium and critical point data for ethylene and chlorodifluoromethane binary mixtures using a new static-analytic apparatus
Pvap	4102.00	kPa	273.18	Vapor-Liquid Equilibrium (PTxy) Measurements and Modeling for the CO-C2H4 Binary System
Pvap	4113.00	kPa	273.29	Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
Pvap	4339.00	kPa	275.68	Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
Pvap	4588.00	kPa	278.16	Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
Pvap	4611.20	kPa	278.36	Vapor-liquid equilibria of ethylene (C2H4) + decafluorobutane (C4F10) at 268 to 298 K from experiment, molecular simulation and the Peng-Robinson equation of state
Pvap	4891.00	kPa	280.98	Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
ρl	577.00	kg/m3	163.00	KDB
ΔfusS	[32.23; 32.23]	J/mol×K	[103.95; 103.97]
ΔfusS	32.23	J/mol×K	103.95	NIST
ΔfusS	32.23	J/mol×K	103.97	NIST
γ	0.02	N/m	133.20	KDB
ΔvapS	79.95	J/mol×K	169.40	NIST
λ	[0.02; 0.04]	W/m×K	[283.47; 425.62]
λ	0.02	W/m×K	283.47	Measurements of the thermal conductivity of ethene in the supercritical region
λ	0.02	W/m×K	283.96	Measurements of the thermal conductivity of ethene in the supercritical region
λ	0.02	W/m×K	284.89	Measurements of the thermal conductivity of ethene in the supercritical region
λ	0.02	W/m×K	302.21	Measurements of the thermal conductivity of ethene in the supercritical region
λ	0.02	W/m×K	303.10	Measurements of the thermal conductivity of ethene in the supercritical region
λ	0.04	W/m×K	425.00	Measurements of the thermal conductivity of ethene in the supercritical region
λ	0.04	W/m×K	425.62	Measurements of the thermal conductivity of ethene in the supercritical region

Correlations

Property	Value	Unit	Temperature (K)	Source
Cp,gas	[42.84; 101.68]	J/mol×K	[298.00; 1200.00]	NIST
Equation			Y = A + B·t + C·t² + D·t³ + E/t², t = T/1000 Y is Cp,gas in J/mol×K, T in K
Coefficient A			-6.38788e+00
Coefficient B			1.84402e+02
Coefficient C			-1.12972e+02
Coefficient D			2.84959e+01
Coefficient E			3.15540e-01
Reference			Chase, 1998
Temperature range, min.			298.00
Temperature range, max.			1200.00
Cp,gas	42.84	J/mol×K	298.00	Calculated Property
Cp,gas	52.92	J/mol×K	398.22	Calculated Property
Cp,gas	62.26	J/mol×K	498.44	Calculated Property
Cp,gas	70.51	J/mol×K	598.67	Calculated Property
Cp,gas	77.68	J/mol×K	698.89	Calculated Property
Cp,gas	83.86	J/mol×K	799.11	Calculated Property
Cp,gas	89.20	J/mol×K	899.33	Calculated Property
Cp,gas	93.83	J/mol×K	999.56	Calculated Property
Cp,gas	97.94	J/mol×K	1099.78	Calculated Property
Cp,gas	101.68	J/mol×K	1200.00	Calculated Property
Cp,gas	[101.35; 131.27]	J/mol×K	[1200.00; 6000.00]	NIST
Equation			Y = A + B·t + C·t² + D·t³ + E/t², t = T/1000 Y is Cp,gas in J/mol×K, T in K
Coefficient A			1.06510e+02
Coefficient B			1.37326e+01
Coefficient C			-2.62848e+00
Coefficient D			1.74595e-01
Coefficient E			-2.61447e+01
Reference			Chase, 1998
Temperature range, min.			1200.00
Temperature range, max.			6000.00
Cp,gas	101.35	J/mol×K	1200.00	Calculated Property
Cp,gas	114.62	J/mol×K	1733.33	Calculated Property
Cp,gas	121.08	J/mol×K	2266.67	Calculated Property
Cp,gas	124.85	J/mol×K	2800.00	Calculated Property
Cp,gas	127.19	J/mol×K	3333.33	Calculated Property
Cp,gas	128.66	J/mol×K	3866.67	Calculated Property
Cp,gas	129.57	J/mol×K	4400.00	Calculated Property
Cp,gas	130.18	J/mol×K	4933.33	Calculated Property
Cp,gas	130.68	J/mol×K	5466.67	Calculated Property
Cp,gas	131.27	J/mol×K	6000.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
η	[0.0007701; 0.0001282]	Pa×s	[103.84; 197.68]	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			-1.09459e+01
Coefficient B			3.92200e+02
Coefficient C			0.00000e+00
Coefficient D			0.00000e+00
Coefficient E			0.00000e+00
Temperature range, min.			103.84
Temperature range, max.			197.68
η	0.0007701	Pa×s	103.84	Calculated Property
η	0.0005456	Pa×s	114.27	Calculated Property
η	0.0004095	Pa×s	124.70	Calculated Property
η	0.0003212	Pa×s	135.12	Calculated Property
η	0.0002609	Pa×s	145.55	Calculated Property
η	0.0002179	Pa×s	155.98	Calculated Property
η	0.0001862	Pa×s	166.40	Calculated Property
η	0.0001620	Pa×s	176.83	Calculated Property
η	0.0001432	Pa×s	187.26	Calculated Property
η	0.0001282	Pa×s	197.68	Calculated Property

Property	Value	Unit	Temperature (K)	Source
Pvap	[0.14; 5057.85]	kPa	[104.00; 282.35]	The Yaws Handbook of Vapor Pressure
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
Coefficient A			1.40310e+01
Coefficient B			-1.49623e+03
Coefficient C			-1.04200e+01
Temperature range, min.			104.00
Temperature range, max.			282.35
Pvap	0.14	kPa	104.00	Calculated Property
Pvap	2.31	kPa	123.82	Calculated Property
Pvap	16.43	kPa	143.63	Calculated Property
Pvap	70.36	kPa	163.45	Calculated Property
Pvap	215.84	kPa	183.27	Calculated Property
Pvap	525.80	kPa	203.08	Calculated Property
Pvap	1084.87	kPa	222.90	Calculated Property
Pvap	1978.17	kPa	242.72	Calculated Property
Pvap	3282.00	kPa	262.53	Calculated Property
Pvap	5057.85	kPa	282.35	Calculated Property
Pvap	[0.13; 5023.31]	kPa	[104.01; 282.36]	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			4.31991e+01
Coefficient B			-2.35577e+03
Coefficient C			-4.89843e+00
Coefficient D			1.64142e-05
Coefficient E			0.00000e+00
Temperature range, min.			104.01
Temperature range, max.			282.36
Pvap	0.13	kPa	104.01	Calculated Property
Pvap	2.27	kPa	123.83	Calculated Property
Pvap	16.54	kPa	143.64	Calculated Property
Pvap	70.85	kPa	163.46	Calculated Property
Pvap	215.10	kPa	183.28	Calculated Property
Pvap	517.00	kPa	203.09	Calculated Property
Pvap	1055.47	kPa	222.91	Calculated Property
Pvap	1917.59	kPa	242.73	Calculated Property
Pvap	3201.28	kPa	262.54	Calculated Property
Pvap	5023.31	kPa	282.36	Calculated Property
Pvap	[26.04; 276.54]	kPa	[149.37; 188.57]	NIST
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
Coefficient A			1.35222e+01
Coefficient B			-1.34505e+03
Coefficient C			-1.83070e+01
Reference			Michels and Wassenaar, 1950
Temperature range, min.			149.37
Temperature range, max.			188.57
Pvap	26.04	kPa	149.37	Calculated Property
Pvap	36.22	kPa	153.73	Calculated Property
Pvap	49.36	kPa	158.08	Calculated Property
Pvap	66.02	kPa	162.44	Calculated Property
Pvap	86.81	kPa	166.79	Calculated Property
Pvap	112.38	kPa	171.15	Calculated Property
Pvap	143.41	kPa	175.50	Calculated Property
Pvap	180.62	kPa	179.86	Calculated Property
Pvap	224.75	kPa	184.21	Calculated Property
Pvap	276.54	kPa	188.57	Calculated Property

Similar Compounds

Find more compounds similar to Ethylene.

Mixtures

• Toluene + Ethylene
• Methyl propionate + Ethylene
• 2-PROPANOL, 1,1,1,3,3,3-HEXAFLUORO- + Ethylene + Water
• Heptane, hexadecafluoro- + Ethylene
• Ethylene + nonane, eicosafluoro-
• Furan, tetrahydro-2,5-dimethyl- + Ethylene + Furan, tetrahydro-2,5-dimethyl-, cis-
• Propene, hexafluoro- + Ethylene
• Ethylene + Methyl Alcohol
• Ethylene + Methane, chlorodifluoro-
• Toluene + 2-Norbornene + Ethylene
• 2-Norbornene + Ethylene
• Methane + Ethylene + Ethanol, 2,2'-oxybis-
• Methane + Ethylene + Water
• Ethylene + Hexafluoropropylene oxide
• 2-Propenoic acid, methyl ester + Ethylene
• Ethanol, 2,2,2-trifluoro- + Ethylene + Water
• 1-Butanol + Ethylene
• Octadecafluorooctane + Ethylene
• Butane, decafluoro- + Ethylene
• Eicosane + Ethylene

Find more mixtures with Ethylene.

Sources

• KDB Vapor Pressure Data
• Crippen Method
• The experiments and correlations of the solubility of ethylene in toluene solvent
• Phase behaviour in the vicinity of the three-phase solid liquid vapour line in asymmetric nonpolar systems at high pressures
• High-pressure phase equilibrium for ethylene + 1-butanol at 283.65 K and 290.80 K
• Solubilities of several non-polar gases in mixtures water + 2,2,2-trifluoroethanol at 298.15 K and 101.33 kPa
• Phase behavior of vinyl fluoride in room-temperature ionic liquids [emim][Tf2N], [bmim][N(CN)2], [bmpy][BF4], [bmim][HFPS] and [omim][TFES]
• Vapor-liquid equilibria of ethylene (C2H4) + decafluorobutane (C4F10) at 268 to 298 K from experiment, molecular simulation and the Peng-Robinson equation of state
• Solubility of ethylene in toluene, norbornene, and toluene + norbornene mixture
• Isothermal vapor-liquid equilibrium data for the ethylene + 1,1,2,3,3,3-hexafluoro-1-propene binary system between 258 and 308 K at pressures up to 4.56 MPa
• Solubility of ethylene in methyl propionate
• Isothermal vapor liquid equilibrium data for the ethene + 2,2,3- trifluoro-3-(trifluoromethyl)oxirane binary system between 258 and 308 K at pressures up to 4.5MPa
• High-pressure phase equilibria data for mixtures involving ethene and perfluoro-n-octane from 293 to 353 K
• Separation of methane/ethylene gas mixtures efficiently by using ZIF- 67/water-ethylene glycol slurry
• Binary vapour-liquid equilibrium data for C7 and C9 straight-chain perfluorocarbons with ethylene
• Measurement and prediction of phase equilibria of ethylene + vinyl acetate + methanol + poly(ethylene-co-vinyl acetate) systems
• Phase behavior and densities of propylene + toluene and ethylene + toluene systems to 580 K and 70 MPa
• Phase equilibrium and critical point data for ethylene and chlorodifluoromethane binary mixtures using a new static-analytic apparatus
• Measurements of the thermal conductivity of ethene in the supercritical region
• Measurement and prediction of phase equilibria of ethylene + methyl acrylate + poly(ethylene-co-methyl acrylate) systems
• Mixture densities and viscosities of toluene with ethylene or propylene at temperatures to 530 K and pressures to 70 MPa
• Solubility of gases in fluoroorganic alcohols. Part III. Solubilities of several non-polar gases in water + 1,1,1,3,3,3-hexafluoropropan-2-ol at 298.15 K and 101.33 kPa
• Solubilities of gases in cycloethers. The solubility of 13 nonpolar gases in 2,5-dimethyltetrahydrofuran at 273.15 to 303.15 K and 101.32 kPa
• Solubility of Ethene in n-Hexane and n-Heptane as Common Slurry-Phase Polymerization Solvents: Experimental Measurement and Modeling
• Influence of a-Olefin Concentration and Length on the High-Pressure Phase Behavior of (a-Olefin + n-Hexane + LLDPE) Systems
• Solubilities of Nonpolar Gases in Triethylene Glycol Dimethyl Ether, Tetraethylene Glycol Dimethyl Ether, Dimethyl Carbonate, and Diethyl Carbonate at 298.15 K and 101.33 kPa Partial Pressure of Gas
• Solubilities of Nonpolar Gases in Dimethyl Carbonate and Diethyl Carbonate
• High-Pressure Phase Equilibrium for Ethylene + Ethanol at 283.65 K
• Vapor-Liquid Equilibrium Data for the Ethylene + Hexane System
• High-Pressure Phase Equilibrium for Ethylene + 2-Propanol at 283.65 K
• High-Pressure Phase Equilibrium for Ethylene + Methanol at 278.15 K and 283.65 K
• Solubility of Ethylene in 2,2,4-Trimethylpentane at Various Temperatures and Pressures
• High-Pressure Multiphase Behavior of the Ternary Systems (Ethene + Water + Acetone) and (Ethane + Water + Acetone)
• Vapor-Liquid Equilibrium (PTxy) Measurements and Modeling for the CO-C2H4 Binary System
• Solubilities of the Gaseous and Liquid Solutes and Their Thermodynamics of Solubilization in the Novel Room-Temperature Ionic Liquids at Infinite Dilution by Gas Chromatography
• High-Pressure Vapor-Liquid Equilibrium for Ethylene + 2-Methyl-1-propanol
• Gas-Liquid Critical Properties of Ethylene + Hydrogen and Propylene + Hydrogen Binary Mixtures
• Joback Method
• KDB
• Aqueous Solubility Prediction Method
• Estimated Solubility Method
• 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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