Chemical Properties of Butane (CAS 106-97-8)

InChI

InChI=1S/C4H10/c1-3-4-2/h3-4H2,1-2H3

InChI Key

IJDNQMDRQITEOD-UHFFFAOYSA-N

Formula

C4H10

SMILES

CCCC

Molecular Weight¹

58.12

CAS

106-97-8

Other Names

• A 21
• Butanen
• Butani
• DIETHYL
• Freon 600
• HC 600
• HC 600 (hydrocarbon)
• LPG
• Liquefied petroleum gas
• Methylethylmethane
• R 600
• R 600 (alkane)
• UN 1011
• n-Butane
• n-C4H10

• ω : Acentric Factor.
• T_ig : Autoignition Temperature (K).
• AP : Aniline Point (K).
• 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_c,grossH : Heat of Combustion, Gross form (kJ/mol).
• Δ_c,netH : Heat of Combustion, Net Form (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_subH : Enthalpy of sublimation 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).
• 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.
• P_c : Critical Pressure (kPa).
• P_triple : Triple Point Pressure (kPa).
• P_vap : Vapor pressure (kPa).
• n₀ : Refractive Index.
• ρ_l : Liquid Density (kg/m³).
• Δ_fusS : Entropy of fusion at a given temperature (J/mol×K).
• S°_liquid : Liquid phase molar entropy at standard conditions (J/mol×K).
• c_sound,fluid : Speed of sound in fluid (m/s).
• 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).
• 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.

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	0.1990		KDB
Tig	703.71	K	KDB
AP	356.250	K	KDB
ΔcH°gas	[-2878.30; -2876.20]	kJ/mol
ΔcH°gas	-2877.50 ± 0.63	kJ/mol	NIST
ΔcH°gas	-2876.20 ± 0.63	kJ/mol	NIST
ΔcH°gas	-2878.30 ± 0.63	kJ/mol	NIST
μ	0.00	debye	KDB
LFL	1.80	% in Air	KDB
UFL	8.40	% in Air	KDB
Tflash,oc	199.82	K	KDB
ΔfG°	-16.10	kJ/mol	KDB
Rg	2.8890		KDB
Δc,grossH	2855.37	kJ/mol	KDB
Δc,netH	2635.334	kJ/mol	KDB
ΔfH°gas	[-127.10; -125.60]	kJ/mol
ΔfH°gas	-126.20	kJ/mol	KDB
ΔfH°gas	-125.60 ± 0.67	kJ/mol	NIST
ΔfH°gas	-127.10 ± 0.67	kJ/mol	NIST
ΔfusH°	6.12	kJ/mol	Joback Calculated Property
ΔvapH°	22.40	kJ/mol	NIST
IE	[10.35; 11.20]	eV
IE	10.53 ± 0.02	eV	NIST
IE	10.57	eV	NIST
IE	10.53 ± 0.10	eV	NIST
IE	10.35 ± 0.15	eV	NIST
IE	10.60 ± 0.10	eV	NIST
IE	10.61	eV	NIST
IE	10.87 ± 0.05	eV	NIST
IE	10.89	eV	NIST
IE	10.67	eV	NIST
IE	10.55 ± 0.05	eV	NIST
IE	10.50	eV	NIST
IE	10.55 ± 0.05	eV	NIST
IE	10.63 ± 0.03	eV	NIST
IE	11.09	eV	NIST
IE	11.20	eV	NIST
IE	11.20 ± 0.10	eV	NIST
log10WS	[-2.72; -2.57]
log10WS	-2.72		Aq. Solubility Prediction
log10WS	-2.57		Estimated Solubility
logPoct/wat	1.806		Crippen Calculated Property
McVol	67.220	ml/mol	McGowan Calculated Property
NFPA Fire	4		KDB
NFPA Health	1		KDB
Pc	[3787.00; 3796.00]	kPa
Pc	3796.00	kPa	KDB
Pc	3787.00	kPa	Critical Properties of Three Dimethyl Ether Binary Systems: Dimethyl Ether (RE-170) + Propane (HC-290), Butane (HC-600), and 2-Methyl Propane (HC-600A)
Ptriple	[7.00e-04; 7.00e-04]	kPa
Ptriple	7.00e-04 ± 8.00e-07	kPa	NIST
Ptriple	7.00e-04	kPa	NIST
S°liquid	[226.80; 231.00]	J/mol×K
S°liquid	231.00	J/mol×K	NIST
S°liquid	226.80	J/mol×K	NIST
S°liquid	229.70	J/mol×K	NIST
Tboil	272.60	K	KDB
Tc	[423.90; 426.35]	K
Tc	425.12	K	KDB
Tc	424.82	K	Validation of a New Apparatus Using the Dynamic Method for Determining the Critical Properties of Binary Gas/Gas Mixtures
Tc	425.10 ± 0.10	K	NIST
Tc	425.12 ± 0.20	K	NIST
Tc	425.18	K	NIST
Tc	425.16 ± 0.10	K	NIST
Tc	425.10 ± 0.10	K	NIST
Tc	424.65 ± 0.50	K	NIST
Tc	425.16 ± 0.07	K	NIST
Tc	425.16	K	NIST
Tc	425.12 ± 0.10	K	NIST
Tc	425.35 ± 0.20	K	NIST
Tc	425.40 ± 0.40	K	NIST
Tc	425.12 ± 0.20	K	NIST
Tc	425.37 ± 0.55	K	NIST
Tc	425.40 ± 1.11	K	NIST
Tc	425.16 ± 0.03	K	NIST
Tc	Outlier 423.90 ± 2.00	K	NIST
Tc	Outlier 426.35 ± 0.50	K	NIST
Tc	Outlier 424.00 ± 1.00	K	NIST
Tfus	[134.86; 135.23]	K
Tfus	134.86	K	KDB
Tfus	135.23	K	Aq. Solubility Prediction
Ttriple	134.86	K	KDB
Vc	[0.255; 0.263]	m3/kmol
Vc	0.255	m3/kmol	KDB
Vc	0.255	m3/kmol	NIST
Vc	0.263 ± 0.010	m3/kmol	NIST
Vc	0.255 ± 0.001	m3/kmol	NIST
Vc	0.258 ± 0.003	m3/kmol	NIST
Zc	0.2738530		KDB
Zra	0.27		KDB

Temperature Dependent Properties

Property	Value	Unit	Temperature (K)	Source
Cp,gas	[110.58; 185.85]	J/mol×K	[344.90; 692.60]
Cp,gas	110.58	J/mol×K	344.90	NIST
Cp,gas	114.93	J/mol×K	359.60	NIST
Cp,gas	121.75	J/mol×K	387.50	NIST
Cp,gas	137.99	J/mol×K	451.60	NIST
Cp,gas	154.01	J/mol×K	521.00	NIST
Cp,gas	162.26	J/mol×K	561.30	NIST
Cp,gas	170.33	J/mol×K	600.80	NIST
Cp,gas	185.85	J/mol×K	692.60	NIST
Cp,liquid	[129.70; 132.42]	J/mol×K	[261.80; 270.00]
Cp,liquid	129.70	J/mol×K	261.80	NIST
Cp,liquid	132.42	J/mol×K	270.00	NIST
η	[0.0001816; 0.0027951]	Pa×s	[134.84; 290.92]
η	0.0027951	Pa×s	134.84	Joback Calculated Property
η	0.0012261	Pa×s	160.85	Joback Calculated Property
η	0.0006765	Pa×s	186.87	Joback Calculated Property
η	0.0004317	Pa×s	212.88	Joback Calculated Property
η	0.0003037	Pa×s	238.89	Joback Calculated Property
η	0.0002290	Pa×s	264.91	Joback Calculated Property
η	0.0001816	Pa×s	290.92	Joback Calculated Property
ΔfusH	[2.07; 4.66]	kJ/mol	[107.60; 134.90]
ΔfusH	2.07	kJ/mol	107.60	NIST
ΔfusH	4.66	kJ/mol	134.90	NIST
ΔfusH	4.66	kJ/mol	134.90	NIST
ΔsubH	35.90	kJ/mol	107.00	NIST
ΔvapH	[21.00; 27.00]	kJ/mol	[174.00; 400.00]
ΔvapH	27.00	kJ/mol	174.00	NIST
ΔvapH	23.90	kJ/mol	234.00	NIST
ΔvapH	23.10	kJ/mol	242.50	NIST
ΔvapH	23.40	kJ/mol	243.50	NIST
ΔvapH	22.39	kJ/mol	272.05	NIST
ΔvapH	21.00 ± 0.08	kJ/mol	272.66	NIST
ΔvapH	22.44	kJ/mol	272.70	NIST
ΔvapH	22.39	kJ/mol	273.00	KDB
ΔvapH	23.20	kJ/mol	297.00	NIST
ΔvapH	22.90	kJ/mol	307.50	NIST
ΔvapH	22.60	kJ/mol	349.50	NIST
ΔvapH	22.80	kJ/mol	400.00	NIST
Pvap	[1.30e-03; 3716.90]	kPa	[135.00; 424.00]
Pvap	1.30e-03	kPa	135.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	2.10e-03	kPa	140.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	9.30e-03	kPa	150.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	0.04	kPa	160.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	0.12	kPa	170.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	0.34	kPa	180.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	0.42	kPa	182.33	Vapour pressure and excess Gibbs free energy of binary mixtures of hydrogen sulphide with ethane, propane, and n-butane at temperature of 182.33 K
Pvap	0.85	kPa	190.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	1.94	kPa	200.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	4.04	kPa	210.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	7.80	kPa	220.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	14.11	kPa	230.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	23.90	kPa	240.00	Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
Pvap	26.20	kPa	240.00	Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
Pvap	24.09	kPa	240.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	29.10	kPa	243.03	Phase Equilibria of H2S-Hydrocarbons (Propane, n-Butane, and n-Pentane) Binary Systems at Low Temperatures
Pvap	39.16	kPa	250.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	60.99	kPa	260.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	59.90	kPa	260.00	Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
Pvap	69.60	kPa	263.15	Vapor-Liquid Equilibrium for the Difluoromethane (R32) + n-Butane (R600) System
Pvap	91.50	kPa	270.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	103.00	kPa	273.15	Vapor-Liquid Equilibria for Propane (R290) + n-Butane (R600) at Various Temperatures
Pvap	104.00	kPa	273.15	Vapor-Liquid Equilibria for 1,1,1,2,3,3,3-Heptafluoropropane (HFC-227ea) + Butane (R600) at Various Temperatures
Pvap	104.00	kPa	273.15	Vapor liquid equilibria for the binary system of 1,1-difluoroethane (HFC-152a) + n-butane (R-600) at various temperatures
Pvap	104.00	kPa	273.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	103.40	kPa	273.15	Vapor-Liquid Equilibria for the 1,1,1,2-Tetrafluoroethane (HFC-134a) + n-Butane (R-600) System
Pvap	104.00	kPa	273.27	Isothermal Vapor-Liquid Equilibrium Data for the Hexafluoroethane (R116) + n-Butane System at Temperatures from 273 to 323 K
Pvap	110.67	kPa	275.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	125.10	kPa	278.15	Vapor-Liquid Equilibrium for the Difluoromethane (R32) + n-Butane (R600) System
Pvap	133.00	kPa	280.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	131.50	kPa	280.00	Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
Pvap	150.00	kPa	283.15	Vapor liquid equilibria for the binary system of 1,1-difluoroethane (HFC-152a) + n-butane (R-600) at various temperatures
Pvap	150.00	kPa	283.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	149.00	kPa	283.15	Vapor-Liquid Equilibria for the 1,1,1,2-Tetrafluoroethane (HFC-134a) + n-Butane (R-600) System
Pvap	148.10	kPa	283.15	Vapor-Liquid Equilibrium Measurements for 2,3,3,3-Tetrafluoroprop-1-ene + Butane at Temperatures from 283.15 to 323.15 K
Pvap	150.00	kPa	283.15	Vapor-Liquid Equilibria for 1,1,1,2,3,3,3-Heptafluoropropane (HFC-227ea) + Butane (R600) at Various Temperatures
Pvap	148.00	kPa	283.15	(Vapour + liquid) equilibria of the {trifluoromethane (HFC-23) + propane} and {trifluoromethane (HFC-23) + n-butane} systems
Pvap	149.00	kPa	283.15	Vapor-Liquid Equilibria for Propane (R290) + n-Butane (R600) at Various Temperatures
Pvap	158.31	kPa	285.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	177.00	kPa	288.25	Isothermal Vapor-Liquid Equilibrium Data for the Hexafluoroethane (R116) + n-Butane System at Temperatures from 273 to 323 K
Pvap	187.37	kPa	290.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	208.00	kPa	293.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	208.30	kPa	293.15	Vapor-Liquid Equilibria for the 1,1,1,2-Tetrafluoroethane (HFC-134a) + n-Butane (R-600) System
Pvap	208.00	kPa	293.15	(Vapour + liquid) equilibria of the {trifluoromethane (HFC-23) + propane} and {trifluoromethane (HFC-23) + n-butane} systems
Pvap	208.00	kPa	293.15	Vapor liquid equilibria for the binary system of 1,1-difluoroethane (HFC-152a) + n-butane (R-600) at various temperatures
Pvap	208.00	kPa	293.15	Vapor-Liquid Equilibria for 1,1,1,2,3,3,3-Heptafluoropropane (HFC-227ea) + Butane (R600) at Various Temperatures
Pvap	209.40	kPa	293.15	Vapor-Liquid Equilibrium for the Difluoromethane (R32) + n-Butane (R600) System
Pvap	207.20	kPa	293.15	Vapor-Liquid Equilibrium Measurements for 2,3,3,3-Tetrafluoroprop-1-ene + Butane at Temperatures from 283.15 to 323.15 K
Pvap	208.00	kPa	293.15	Vapor-Liquid Equilibria for Propane (R290) + n-Butane (R600) at Various Temperatures
Pvap	210.80	kPa	293.38	Phase Equilibria of H2S-Hydrocarbons (Propane, n-Butane, and n-Pentane) Binary Systems at Low Temperatures
Pvap	215.00	kPa	294.23	Isothermal Vapor-Liquid Equilibrium Data for the Hexafluoroethane (R116) + n-Butane System at Temperatures from 273 to 323 K
Pvap	231.00	kPa	296.23	Isothermal Vapor-Liquid Equilibrium Data for the Hexafluoroethane (R116) + n-Butane System at Temperatures from 273 to 323 K
Pvap	257.62	kPa	300.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	257.50	kPa	300.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	256.40	kPa	300.00	Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
Pvap	280.00	kPa	302.92	Phase equilibrium data for mixtures involving 1,1,2,3,3,3-hexafluoro-1-propene with either propane or n-butane between 312 and 343 K
Pvap	284.00	kPa	303.15	Vapor liquid equilibria for the binary system of 1,1-difluoroethane (HFC-152a) + n-butane (R-600) at various temperatures
Pvap	283.40	kPa	303.15	Vapor-Liquid Equilibrium Measurements for 2,3,3,3-Tetrafluoroprop-1-ene + Butane at Temperatures from 283.15 to 323.15 K
Pvap	283.70	kPa	303.15	Isothermal (vapour + liquid) equilibrium measurements and correlation for the {n-butane (R600) + 1,1,1,3,3-pentafluoropropane (R245fa)} system at temperatures from (303.150 to 373.150) K
Pvap	284.00	kPa	303.15	Vapor-Liquid Equilibria for the 1,1,1,2-Tetrafluoroethane (HFC-134a) + n-Butane (R-600) System
Pvap	284.00	kPa	303.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	284.00	kPa	303.15	Vapor-Liquid Equilibria for 1,1,1,2,3,3,3-Heptafluoropropane (HFC-227ea) + Butane (R600) at Various Temperatures
Pvap	284.00	kPa	303.15	Vapor-Liquid Equilibria for Propane (R290) + n-Butane (R600) at Various Temperatures
Pvap	282.00	kPa	303.15	(Vapour + liquid) equilibria of the {trifluoromethane (HFC-23) + propane} and {trifluoromethane (HFC-23) + n-butane} systems
Pvap	324.00	kPa	307.93	Phase equilibrium data for mixtures involving 1,1,2,3,3,3-hexafluoro-1-propene with either propane or n-butane between 312 and 343 K
Pvap	328.80	kPa	308.15	Vapor-Liquid Equilibrium for Thiophene + Butane, + trans-But-2-ene, + 2-Methylpropane, and + 2-Methylpropene
Pvap	332.00	kPa	308.21	Isothermal Vapor-Liquid Equilibrium Data for the Hexafluoroethane (R116) + n-Butane System at Temperatures from 273 to 323 K
Pvap	346.30	kPa	310.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	377.00	kPa	312.87	Phase equilibrium data for mixtures involving 1,1,2,3,3,3-hexafluoro-1-propene with either propane or n-butane between 312 and 343 K
Pvap	378.10	kPa	313.15	Vapor-Liquid Equilibria for the 1,1,1,2-Tetrafluoroethane (HFC-134a) + n-Butane (R-600) System
Pvap	378.00	kPa	313.15	Vapor-Liquid Equilibria for 1,1,1,2,3,3,3-Heptafluoropropane (HFC-227ea) + Butane (R600) at Various Temperatures
Pvap	378.60	kPa	313.15	Vapor-Liquid Equilibrium Measurements for 2,3,3,3-Tetrafluoroprop-1-ene + Butane at Temperatures from 283.15 to 323.15 K
Pvap	378.00	kPa	313.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	378.00	kPa	313.15	(Vapour + liquid) equilibria of the {trifluoromethane (HFC-23) + propane} and {trifluoromethane (HFC-23) + n-butane} systems
Pvap	377.00	kPa	313.15	Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane System
Pvap	378.00	kPa	313.15	Vapor-Liquid Equilibria for Propane (R290) + n-Butane (R600) at Various Temperatures
Pvap	378.00	kPa	313.15	Vapor liquid equilibria for the binary system of 1,1-difluoroethane (HFC-152a) + n-butane (R-600) at various temperatures
Pvap	378.00	kPa	313.15	Vapor-Liquid Equilibria of the Binary n-Butane (HC-600) + Difluoromethane (HFC-32), + Pentafluoroethane (HFC-125), + 1,1,1,2-Tetrafluoroethane (HFC-134a) Mixture Systems
Pvap	377.00	kPa	313.15	(Vapour + liquid) equilibria of the {1,1-difluoroethane (HFC-152a) + n-butane (HC-600)} system
Pvap	379.00	kPa	313.20	High pressure vapor-liquid equilibria measurements and modeling of butane/ethanol system and isobutane/ethanol system
Pvap	425.70	kPa	317.47	Isothermal binary vapour liquid equilibrium for butanes and butenes with dimethylsulphide
Pvap	426.80	kPa	317.60	Vapour liquid equilibrium for the systems diethyl sulphide + 1-butene, +cis-2-butene, +2-methylpropane, +2-methylpropene, +n-butane, +trans-2-butene
Pvap	432.00	kPa	317.88	Phase equilibrium data for mixtures involving 1,1,2,3,3,3-hexafluoro-1-propene with either propane or n-butane between 312 and 343 K
Pvap	436.20	kPa	318.35	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
Pvap	437.50	kPa	318.35	Vapor-Liquid Equilibrium for Tetrahydrothiophene + n-Butane, + trans-2-Butene, + 2-Methylpropane, and + 2-Methylpropene
Pvap	436.55	kPa	318.40	Vapour liquid equilibrium for the ethyl ethanoate + 1-butene, +cis-2-butene, +trans-2-butene, +2-methylpropene, +n-butane and +2-methylpropane
Pvap	456.20	kPa	320.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	454.80	kPa	320.00	Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
Pvap	456.24	kPa	320.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	479.50	kPa	322.01	Phase equilibrium measurements for systems containing propanenitrile with tert-butyl ethyl ether and C4-hydrocarbons
Pvap	491.00	kPa	322.86	Phase equilibrium data for mixtures involving 1,1,2,3,3,3-hexafluoro-1-propene with either propane or n-butane between 312 and 343 K
Pvap	495.00	kPa	323.12	Vapor Liquid Equilibrium for Butane + Methanol, + Ethanol, + 2-Propanol, + 2-Butanol, and + 2-Methyl-2-Propanol (TBA) at 323 K
Pvap	495.30	kPa	323.13	Vapor Liquid Equilibrium for Butane + Methanol, + Ethanol, + 2-Propanol, + 2-Butanol, and + 2-Methyl-2-Propanol (TBA) at 323 K
Pvap	496.00	kPa	323.15	Vapor-Liquid Equilibria of the Binary n-Butane (HC-600) + Difluoromethane (HFC-32), + Pentafluoroethane (HFC-125), + 1,1,1,2-Tetrafluoroethane (HFC-134a) Mixture Systems
Pvap	496.50	kPa	323.15	Vapor-Liquid Equilibrium Measurements for 2,3,3,3-Tetrafluoroprop-1-ene + Butane at Temperatures from 283.15 to 323.15 K
Pvap	494.00	kPa	323.15	Vapor-Liquid Equilibria for 1,1,1,2,3,3,3-Heptafluoropropane (HFC-227ea) + Butane (R600) at Various Temperatures
Pvap	494.00	kPa	323.15	Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
Pvap	495.70	kPa	323.15	Vapor Liquid Equilibrium for Butane + Methanol, + Ethanol, + 2-Propanol, + 2-Butanol, and + 2-Methyl-2-Propanol (TBA) at 323 K
Pvap	493.00	kPa	323.15	Vapor-Liquid Equilibria for Propane (R290) + n-Butane (R600) at Various Temperatures
Pvap	493.10	kPa	323.15	Vapor-Liquid Equilibria for the 1,1,1,2-Tetrafluoroethane (HFC-134a) + n-Butane (R-600) System
Pvap	495.00	kPa	323.15	Vapor liquid equilibria for the binary system of 1,1-difluoroethane (HFC-152a) + n-butane (R-600) at various temperatures
Pvap	495.60	kPa	323.15	Vapor Liquid Equilibrium for Butane + Methanol, + Ethanol, + 2-Propanol, + 2-Butanol, and + 2-Methyl-2-Propanol (TBA) at 323 K
Pvap	495.00	kPa	323.15	Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane System
Pvap	495.00	kPa	323.15	(Vapour + liquid) equilibria of the {1,1-difluoroethane (HFC-152a) + n-butane (HC-600)} system
Pvap	496.20	kPa	323.15	Isothermal (vapour + liquid) equilibrium measurements and correlation for the {n-butane (R600) + 1,1,1,3,3-pentafluoropropane (R245fa)} system at temperatures from (303.150 to 373.150) K
Pvap	498.00	kPa	323.19	Isothermal Vapor-Liquid Equilibrium Data for the Hexafluoroethane (R116) + n-Butane System at Temperatures from 273 to 323 K
Pvap	561.00	kPa	327.88	Phase equilibrium data for mixtures involving 1,1,2,3,3,3-hexafluoro-1-propene with either propane or n-butane between 312 and 343 K
Pvap	590.40	kPa	330.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	592.44	kPa	330.16	Vapor-Liquid Equilibrium for 1-Propanol + 1-Butene, + cis-2-Butene, + 2-Methyl-propene, + trans-2-Butene, + n-Butane, and + 2-Methyl-propane
Pvap	632.00	kPa	332.83	Phase equilibrium data for mixtures involving 1,1,2,3,3,3-hexafluoro-1-propene with either propane or n-butane between 312 and 343 K
Pvap	638.00	kPa	333.15	Vapor-Liquid Equilibria of the Binary n-Butane (HC-600) + Difluoromethane (HFC-32), + Pentafluoroethane (HFC-125), + 1,1,1,2-Tetrafluoroethane (HFC-134a) Mixture Systems
Pvap	639.00	kPa	333.15	Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane System
Pvap	638.00	kPa	333.15	(Vapour + liquid) equilibria of the {1,1-difluoroethane (HFC-152a) + n-butane (HC-600)} system
Pvap	645.00	kPa	333.20	High pressure vapor-liquid equilibria measurements and modeling of butane/ethanol system and isobutane/ethanol system
Pvap	677.90	kPa	335.60	Vapor-Liquid Equilibrium for Thiophene + Butane, + trans-But-2-ene, + 2-Methylpropane, and + 2-Methylpropene
Pvap	679.30	kPa	335.60	Vapor-Liquid Equilibrium for Thiophene + Butane, + trans-But-2-ene, + 2-Methylpropane, and + 2-Methylpropene
Pvap	714.00	kPa	337.82	Phase equilibrium data for mixtures involving 1,1,2,3,3,3-hexafluoro-1-propene with either propane or n-butane between 312 and 343 K
Pvap	751.90	kPa	340.00	Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
Pvap	752.00	kPa	340.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	751.00	kPa	340.00	Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
Pvap	750.50	kPa	340.00	Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
Pvap	804.00	kPa	342.82	Phase equilibrium data for mixtures involving 1,1,2,3,3,3-hexafluoro-1-propene with either propane or n-butane between 312 and 343 K
Pvap	809.80	kPa	343.15	Isothermal (vapour + liquid) equilibrium measurements and correlation for the {n-butane (R600) + 1,1,1,3,3-pentafluoropropane (R245fa)} system at temperatures from (303.150 to 373.150) K
Pvap	810.00	kPa	343.15	Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane System
Pvap	810.00	kPa	343.15	(Vapour + liquid) equilibria of the {1,1-difluoroethane (HFC-152a) + n-butane (HC-600)} system
Pvap	881.70	kPa	346.97	Vapor-Liquid Equilibrium for Tetrahydrothiophene + n-Butane, + trans-2-Butene, + 2-Methylpropane, and + 2-Methylpropene
Pvap	897.00	kPa	347.81	Phase equilibrium data for mixtures involving 1,1,2,3,3,3-hexafluoro-1-propene with either propane or n-butane between 312 and 343 K
Pvap	951.70	kPa	350.36	Vapor-Liquid Equilibrium for Dimethyl Disulfide + Butane, + trans-But-2-ene, + 2-Methylpropane, + 2-Methylpropene, + Ethanol, and 2-Ethoxy-2-methylpropane
Pvap	1012.00	kPa	353.15	Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane System
Pvap	1039.00	kPa	353.15	In Situ Determination of Phase Equilibria of Methyl Benzoate + Alkane Mixtures Using an Infrared Absorption Method. Comparison with Polar GC-SAFT Predictions
Pvap	1012.00	kPa	353.15	(Vapour + liquid) equilibria of the {1,1-difluoroethane (HFC-152a) + n-butane (HC-600)} system
Pvap	1013.00	kPa	353.20	High pressure vapor-liquid equilibria measurements and modeling of butane/ethanol system and isobutane/ethanol system
Pvap	1170.20	kPa	360.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	1168.50	kPa	360.00	Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
Pvap	1168.10	kPa	360.00	Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
Pvap	1249.80	kPa	363.15	Isothermal (vapour + liquid) equilibrium measurements and correlation for the {n-butane (R600) + 1,1,1,3,3-pentafluoropropane (R245fa)} system at temperatures from (303.150 to 373.150) K
Pvap	1250.00	kPa	363.15	Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane System
Pvap	1249.00	kPa	363.15	(Vapour + liquid) equilibria of the {1,1-difluoroethane (HFC-152a) + n-butane (HC-600)} system
Pvap	1284.50	kPa	364.51	Vapor Liquid Equilibrium for Six Binary Systems of C4-Hydrocarbons + 2-Propanone
Pvap	1434.90	kPa	370.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	1586.00	kPa	373.15	In Situ Determination of Phase Equilibria of Methyl Benzoate + Alkane Mixtures Using an Infrared Absorption Method. Comparison with Polar GC-SAFT Predictions
Pvap	1526.80	kPa	373.15	Isothermal (vapour + liquid) equilibrium measurements and correlation for the {n-butane (R600) + 1,1,1,3,3-pentafluoropropane (R245fa)} system at temperatures from (303.150 to 373.150) K
Pvap	1525.00	kPa	373.20	High pressure vapor-liquid equilibria measurements and modeling of butane/ethanol system and isobutane/ethanol system
Pvap	1739.90	kPa	380.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	1740.40	kPa	380.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	1737.40	kPa	380.00	Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
Pvap	2092.10	kPa	390.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	2265.00	kPa	393.15	In Situ Determination of Phase Equilibria of Methyl Benzoate + Alkane Mixtures Using an Infrared Absorption Method. Comparison with Polar GC-SAFT Predictions
Pvap	2494.60	kPa	400.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	2495.20	kPa	400.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	2660.00	kPa	403.20	High pressure vapor-liquid equilibria measurements and modeling of butane/ethanol system and isobutane/ethanol system
Pvap	2955.00	kPa	410.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	3156.00	kPa	413.15	In Situ Determination of Phase Equilibria of Methyl Benzoate + Alkane Mixtures Using an Infrared Absorption Method. Comparison with Polar GC-SAFT Predictions
Pvap	3482.50	kPa	420.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	3597.50	kPa	422.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
Pvap	3716.90	kPa	424.00	Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
n0	1.32920		298.15	KDB
ρl	579.00	kg/m3	293.00	KDB
ΔfusS	[19.06; 34.56]	J/mol×K	[107.60; 134.90]
ΔfusS	19.06	J/mol×K	107.60	NIST
ΔfusS	34.56	J/mol×K	134.90	NIST
γ	[3.60e-05; 0.01]	N/m	[278.15; 423.04]
γ	0.01	N/m	278.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	283.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	288.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	293.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	293.20	KDB
γ	0.01	N/m	298.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	303.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	308.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	313.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	318.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	323.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	328.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	333.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	338.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	343.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	348.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	353.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.01	N/m	358.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.00	N/m	363.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.00	N/m	368.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.00	N/m	373.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.00	N/m	378.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.00	N/m	383.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.00	N/m	388.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.00	N/m	393.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.00	N/m	398.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	0.00	N/m	403.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	9.23e-04	N/m	408.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	5.83e-04	N/m	413.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	3.41e-04	N/m	417.15	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	1.86e-04	N/m	419.75	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	1.57e-04	N/m	420.35	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	1.29e-04	N/m	420.85	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	1.18e-04	N/m	421.08	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	1.00e-04	N/m	421.48	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	8.10e-05	N/m	421.88	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	6.40e-05	N/m	422.28	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	5.10e-05	N/m	422.63	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
γ	3.60e-05	N/m	423.04	Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
ΔvapS	82.30	J/mol×K	272.05	NIST

Datasets

1. Viscosity, Pa*s (1)
2. Mass density, kg/m3 (4)
3. Speed of sound, m/s (1)

Viscosity, Pa*s

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Viscosity, Pa*s - Liquid
273.15	100.00	0.0002
273.15	10000.00	0.0002
273.15	20000.00	0.0002
273.15	30000.00	0.0003
293.15	200.00	0.0002
293.15	10000.00	0.0002
293.15	20000.00	0.0002
293.15	30000.00	0.0002
313.15	400.00	0.0001
313.15	10000.00	0.0002
313.15	20000.00	0.0002
313.15	30000.00	0.0002
333.15	600.00	0.0001
333.15	10000.00	0.0001
333.15	20000.00	0.0002
333.15	30000.00	0.0002
Reference

Mass density, kg/m3

Fixed		Measured
Temperature, K - Fluid (supercritical or subcritical phases)	Pressure, kPa - Fluid (supercritical or subcritical phases)	Mass density, kg/m3 - Fluid (supercritical or subcritical phases)
360.00	200000.00	676.57
360.00	180000.00	668.57
360.00	160000.00	659.24
360.00	140000.00	649.66
360.00	120000.00	638.57
360.00	100000.00	626.29
360.00	90000.00	619.58
360.00	80000.00	612.02
360.00	70000.00	604.19
360.00	60000.00	595.41
360.00	50000.00	585.47
400.00	200000.00	658.6
400.00	180000.00	649.69
400.00	160000.00	639.75
400.00	140000.00	629.05
400.00	120000.00	617.0
400.00	100000.00	603.28
400.00	90000.00	595.58
400.00	80000.00	587.28
400.00	70000.00	578.11
400.00	60000.00	567.8
400.00	50000.00	556.11
440.00	200000.00	641.85
440.00	180000.00	632.12
440.00	160000.00	621.49
440.00	140000.00	609.84
440.00	120000.00	596.67
440.00	100000.00	581.43
440.00	90000.00	572.93
440.00	80000.00	563.51
440.00	70000.00	552.99
440.00	60000.00	541.19
440.00	50000.00	527.49
500.00	200000.00	617.68
500.00	180000.00	607.21
500.00	160000.00	595.57
500.00	140000.00	582.51
500.00	120000.00	567.64
500.00	100000.00	550.18
500.00	90000.00	540.26
500.00	80000.00	529.24
500.00	70000.00	517.01
500.00	60000.00	502.86
500.00	50000.00	485.76
550.00	200000.00	599.35
550.00	180000.00	588.11
550.00	160000.00	575.61
550.00	140000.00	561.8
550.00	120000.00	545.49
550.00	100000.00	526.47
550.00	90000.00	515.43
550.00	80000.00	503.05
550.00	70000.00	489.04
550.00	60000.00	472.65
550.00	50000.00	452.74
600.00	200000.00	582.23
600.00	180000.00	570.23
600.00	160000.00	556.81
600.00	140000.00	541.56
600.00	120000.00	524.18
600.00	100000.00	503.41
600.00	90000.00	491.53
600.00	80000.00	477.92
600.00	70000.00	462.25
600.00	60000.00	444.04
600.00	50000.00	421.67
Reference

Fixed		Measured
Temperature, K - Fluid (supercritical or subcritical phases)	Pressure, kPa - Fluid (supercritical or subcritical phases)	Mass density, kg/m3 - Fluid (supercritical or subcritical phases)
280.00	1000.00	595.47
280.00	2000.00	596.86
280.00	3000.00	598.22
280.00	5000.00	600.88
280.00	10000.00	607.05
280.00	20000.00	617.68
280.00	30000.00	626.91
280.00	40000.00	635.29
280.00	50000.00	642.77
280.00	60000.00	649.44
280.00	70000.00	655.79
280.00	80000.00	661.73
280.00	90000.00	667.23
280.00	100000.00	672.51
280.00	120000.00	682.08
280.00	140000.00	690.89
280.00	160000.00	698.82
280.00	180000.00	706.38
280.00	200000.00	713.34
300.00	1000.00	572.94
300.00	2000.00	574.58
300.00	3000.00	576.27
300.00	5000.00	579.56
300.00	10000.00	586.77
300.00	20000.00	599.44
300.00	30000.00	610.13
300.00	40000.00	619.89
300.00	50000.00	628.14
300.00	60000.00	635.82
300.00	70000.00	642.36
300.00	80000.00	648.71
300.00	90000.00	654.83
300.00	100000.00	660.41
300.00	120000.00	670.68
300.00	140000.00	680.05
300.00	160000.00	688.48
300.00	180000.00	696.25
300.00	200000.00	703.51
320.00	1000.00	548.24
320.00	2000.00	550.53
320.00	3000.00	552.73
320.00	5000.00	556.84
320.00	10000.00	566.09
320.00	20000.00	580.87
320.00	30000.00	593.19
320.00	40000.00	603.68
320.00	50000.00	612.97
320.00	60000.00	621.23
320.00	70000.00	628.85
320.00	80000.00	635.85
320.00	90000.00	642.47
320.00	100000.00	648.38
320.00	120000.00	659.38
320.00	140000.00	669.21
320.00	160000.00	678.31
320.00	180000.00	686.49
320.00	200000.00	694.12
340.00	1000.00	521.26
340.00	2000.00	524.21
340.00	3000.00	527.06
340.00	5000.00	532.46
340.00	10000.00	544.06
340.00	20000.00	561.99
340.00	30000.00	576.2
340.00	40000.00	588.27
340.00	50000.00	598.47
340.00	60000.00	607.64
340.00	70000.00	615.81
340.00	80000.00	623.32
340.00	90000.00	630.37
340.00	100000.00	636.58
340.00	120000.00	648.45
340.00	140000.00	658.64
340.00	160000.00	668.16
340.00	180000.00	676.9
340.00	200000.00	684.85
360.00	2000.00	494.28
360.00	3000.00	498.49
360.00	5000.00	505.91
360.00	10000.00	520.98
360.00	20000.00	542.91
360.00	30000.00	559.24
360.00	40000.00	572.58
360.00	50000.00	584.17
360.00	60000.00	593.9
360.00	70000.00	602.93
360.00	80000.00	610.9
360.00	90000.00	618.47
360.00	100000.00	625.39
360.00	120000.00	637.62
360.00	140000.00	648.76
360.00	160000.00	658.47
360.00	180000.00	667.68
360.00	200000.00	676.03
380.00	2000.00	456.63
380.00	3000.00	463.53
380.00	5000.00	474.94
380.00	10000.00	495.21
380.00	20000.00	522.42
380.00	30000.00	541.49
380.00	40000.00	556.53
380.00	50000.00	569.05
380.00	60000.00	580.01
380.00	70000.00	589.59
380.00	80000.00	598.34
380.00	90000.00	606.19
380.00	100000.00	613.44
380.00	120000.00	626.58
380.00	140000.00	638.25
380.00	160000.00	648.59
380.00	180000.00	658.14
380.00	200000.00	666.86
Reference

Fixed		Measured
Pressure, kPa - Liquid	Temperature, K - Liquid	Mass density, kg/m3 - Liquid
3000.00	380.00	463.27
5000.00	380.00	474.65
5000.00	400.00	437.19
10000.00	380.00	494.93
10000.00	400.00	466.97
10000.00	420.00	436.16
10000.00	440.00	401.28
20000.00	380.00	521.9
20000.00	400.00	500.93
20000.00	420.00	479.15
20000.00	440.00	457.43
30000.00	400.00	522.83
30000.00	420.00	504.89
30000.00	440.00	487.23
40000.00	380.00	555.85
40000.00	400.00	539.73
40000.00	420.00	523.9
40000.00	440.00	508.57
50000.00	400.00	553.54
50000.00	420.00	539.08
50000.00	440.00	525.26
60000.00	380.00	579.32
60000.00	400.00	565.44
60000.00	420.00	551.8
60000.00	440.00	539.13
70000.00	400.00	575.77
70000.00	420.00	563.07
70000.00	440.00	551.03
80000.00	380.00	597.57
80000.00	400.00	585.08
80000.00	420.00	572.94
80000.00	440.00	561.56
90000.00	400.00	593.33
90000.00	420.00	581.86
90000.00	440.00	571.14
100000.00	380.00	612.79
100000.00	400.00	601.18
100000.00	420.00	589.89
100000.00	440.00	579.66
120000.00	380.00	625.93
120000.00	400.00	614.9
120000.00	420.00	604.27
120000.00	440.00	594.85
140000.00	380.00	637.29
140000.00	400.00	627.05
140000.00	420.00	617.11
140000.00	440.00	608.04
160000.00	380.00	647.82
160000.00	400.00	637.77
160000.00	420.00	628.25
160000.00	440.00	619.73
180000.00	380.00	657.28
180000.00	400.00	647.6
180000.00	420.00	638.65
180000.00	440.00	630.34
200000.00	380.00	665.98
200000.00	400.00	656.49
200000.00	420.00	647.73
200000.00	440.00	639.98
Reference

Fixed		Measured
Temperature, K - Fluid (supercritical or subcritical phases)	Pressure, kPa - Fluid (supercritical or subcritical phases)	Mass density, kg/m3 - Fluid (supercritical or subcritical phases)
298.12	221.39	5.5728
298.12	221.35	5.5716
298.14	196.75	4.9091
298.14	196.77	4.9096
298.14	175.29	4.3414
298.14	175.29	4.3415
298.11	162.81	4.0157
298.11	162.82	4.016
298.12	142.16	3.4823
298.13	142.17	3.4826
298.13	123.43	3.0049
298.13	123.44	3.0052
298.14	102.90	2.4887
298.14	102.91	2.4889
298.14	82.37	1.9794
298.14	82.38	1.9797
298.14	61.79	1.4756
298.14	61.80	1.4758
298.15	57.18	1.3635
298.15	57.18	1.3636
322.98	450.39	11.024
323.00	450.69	11.032
323.01	450.89	11.037
323.06	392.10	9.426
323.08	392.50	9.4391
323.09	392.90	9.4492
323.11	380.78	9.1236
323.11	380.74	9.1236
323.12	380.76	9.1272
323.12	330.12	7.8092
323.12	330.36	7.8164
323.13	330.63	7.8215
323.13	301.54	7.0807
323.13	303.39	7.1241
323.13	305.32	7.1762
323.13	261.18	6.0223
323.13	261.21	6.023
323.14	261.28	6.0252
323.14	215.87	4.9169
323.14	215.65	4.9111
323.14	215.63	4.9096
323.14	184.24	4.1645
323.15	184.35	4.1652
323.15	184.36	4.1667
323.15	150.03	3.3622
323.15	150.04	3.3622
323.14	132.43	2.9506
323.14	132.44	2.9492
323.14	132.46	2.9499
323.14	112.93	2.5057
323.14	112.94	2.5035
323.14	112.96	2.5057
323.14	90.51	1.9979
323.14	90.52	1.9986
323.14	66.38	1.4575
323.14	66.38	1.4567
323.14	66.39	1.4553
323.14	58.20	1.2744
323.14	58.20	1.2766
323.14	58.21	1.2766
348.03	813.99	19.581
348.03	814.13	19.586
348.03	813.85	19.576
348.13	760.25	17.999
348.13	760.34	18.002
348.12	677.52	15.682
348.12	677.82	15.691
348.14	618.24	14.097
348.14	618.34	14.099
348.15	516.76	11.497
348.15	516.69	11.497
348.15	454.98	9.9811
348.15	455.21	9.9833
348.15	340.91	7.3031
348.15	338.38	7.2445
348.15	337.86	7.2315
348.15	337.88	7.2315
348.14	293.19	6.2173
348.14	293.73	6.2296
348.14	93.82	1.9124
348.14	93.83	1.9131
348.15	63.28	1.2845
348.15	63.30	1.286
373.15	1366.40	33.46
373.15	1367.10	33.484
373.14	1262.70	30.019
373.14	1263.00	30.031
373.14	1095.40	24.953
373.14	1095.50	24.958
373.13	916.45	20.053
373.13	916.45	20.052
373.14	838.34	18.049
373.15	750.55	15.881
373.14	751.04	15.893
373.14	669.81	13.955
373.14	670.00	13.959
373.14	572.54	11.724
373.14	572.60	11.728
373.14	493.81	9.9744
373.14	493.67	9.9707
373.15	439.63	8.8018
373.15	441.23	8.8343
373.15	392.71	7.8028
373.15	344.33	6.7909
373.15	344.35	6.7909
373.14	273.38	5.3326
373.14	274.72	5.3593
373.15	210.37	4.0602
373.14	210.39	4.0609
373.14	157.75	3.0215
373.13	157.77	3.0215
373.13	106.93	2.0348
373.13	106.95	2.0363
373.13	106.98	2.037
373.14	57.69	1.0901
373.14	57.72	1.0901
373.14	57.76	1.0909
423.48	3280.80	96.642
423.47	3280.90	96.663
424.21	3176.80	88.401
424.21	3177.00	88.415
423.28	3171.40	89.266
423.20	3170.20	89.28
423.19	3006.00	79.774
423.20	3005.80	79.773
423.20	2781.60	69.058
423.20	2781.10	69.059
423.11	2532.50	59.203
423.12	2534.00	59.251
423.13	2535.60	59.303
423.17	2272.30	50.31
423.17	1490.20	29.071
423.19	1490.00	29.063
423.24	1016.10	18.65
423.25	1015.90	18.648
423.26	884.12	15.981
423.26	884.38	15.987
423.20	653.48	11.519
423.19	654.26	11.533
423.17	452.37	7.8076
423.17	450.91	7.7808
423.16	195.54	3.2893
423.16	195.59	3.2893
428.14	30023.00	498.21
428.14	30022.00	498.2
428.14	30018.00	498.2
428.21	22974.00	480.02
428.21	22974.00	480.02
428.20	22973.00	480.02
428.15	17077.00	460.12
428.15	17075.00	460.12
428.15	12773.00	440.28
428.16	12732.00	440.05
428.16	12735.00	440.06
428.16	9661.10	420.21
428.16	9662.30	420.22
428.17	7466.20	399.67
428.16	7467.10	399.68
428.16	7467.50	399.69
428.13	5948.90	378.0
428.13	5949.60	378.01
428.13	5949.60	378.02
428.09	5150.20	360.25
428.09	5149.90	360.26
428.10	4625.90	341.66
428.11	4626.60	341.66
428.11	4626.80	341.65
428.18	4312.00	322.22
428.18	4312.40	322.24
428.18	4312.40	322.25
428.14	4145.90	304.6
428.14	4146.20	304.61
428.15	4067.30	289.0
428.15	4067.50	288.98
428.20	4030.00	274.89
428.20	4030.10	274.9
428.13	3990.10	251.58
428.13	3990.10	251.63
428.12	3984.80	246.5
428.12	3984.90	246.49
428.18	3976.30	230.48
428.17	3976.10	230.45
428.12	3964.90	218.37
428.13	3964.80	218.33
428.19	3953.50	199.12
428.18	3953.30	199.18
428.19	3938.70	185.24
428.19	3939.20	185.3
428.19	3884.10	159.21
428.19	3883.80	159.22
428.34	3805.10	138.83
428.39	3806.50	138.8
428.20	3793.80	137.58
428.18	3790.90	137.62
428.13	3655.20	119.22
428.14	3655.70	119.23
428.14	3427.10	99.322
428.15	3427.20	99.316
428.16	3263.80	88.856
428.15	3263.70	88.854
428.23	3108.60	80.486
428.22	3107.80	80.455
428.14	2862.80	69.471
428.13	2862.90	69.476
428.13	2624.70	60.36
428.13	2624.60	60.353
428.12	2306.20	49.889
428.12	2306.20	49.887
428.10	1964.10	40.163
428.11	1964.30	40.167
428.21	1539.80	29.634
428.21	1540.10	29.642
428.18	1098.50	20.025
428.18	1099.10	20.038
428.15	1040.70	18.847
428.14	1041.20	18.856
428.11	904.86	16.141
428.10	904.90	16.138
428.10	796.14	14.038
428.10	796.19	14.041
428.12	685.03	11.939
428.13	684.54	11.929
428.13	578.67	9.9774
428.14	578.76	9.9803
428.13	480.91	8.2126
428.14	480.81	8.2112
428.09	194.34	3.2308
428.08	194.36	3.2322
428.11	131.61	2.1741
428.11	131.64	2.1741
428.18	62.10	1.0176
428.17	62.10	1.0183
428.16	62.10	1.0176
448.15	29472.00	478.91
448.14	29460.00	478.91
448.17	23154.00	460.09
448.16	23152.00	460.08
448.14	18184.00	440.74
448.14	18187.00	440.74
448.15	14319.00	420.46
448.17	14321.00	420.46
448.15	11528.00	400.23
448.15	11529.00	400.23
448.17	9538.60	380.13
448.17	9537.40	380.12
448.16	8140.60	359.99
448.16	8139.40	359.98
448.14	7191.00	340.37
448.13	7189.80	340.36
448.16	6551.40	321.12
448.16	6551.10	321.12
448.11	6144.80	304.18
448.11	6145.00	304.17
448.28	5785.10	281.66
448.27	5784.60	281.65
448.15	5551.90	263.05
448.15	5553.70	263.02
448.18	5346.70	240.34
448.17	5346.60	240.34
448.13	5203.20	222.02
448.13	5203.50	222.03
448.11	5054.80	201.47
448.11	5054.50	201.47
448.09	4846.20	174.16
448.13	4847.00	174.1
448.23	4727.10	160.07
448.23	4727.00	160.07
448.17	4498.30	138.72
448.18	4498.10	138.68
448.13	4161.60	114.81
448.13	4161.60	114.81
448.18	3747.80	92.905
448.19	3747.90	92.91
448.18	3433.90	79.739
448.18	3433.70	79.735
448.15	3073.30	66.943
448.16	3073.30	66.941
448.16	2511.80	50.321
448.16	2512.10	50.329
448.17	2073.00	39.287
448.16	2073.70	39.305
448.16	1662.20	30.086
448.15	1661.90	30.078
448.17	1158.40	19.932
448.17	1158.40	19.932
448.16	807.76	13.456
448.15	807.60	13.453
448.15	618.60	10.141
448.15	618.43	10.135
448.16	508.50	8.2591
448.16	509.69	8.28
448.16	430.17	6.9362
448.16	431.02	6.95
448.15	220.17	3.4915
448.16	220.38	3.4965
Reference

Speed of sound, m/s

Operational condition: Frequency, MHz = 8 (Liquid)

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Speed of sound, m/s - Liquid
200.00	1101.43	1447.79
200.00	2102.08	1453.53
200.00	3102.76	1459.25
200.00	4103.47	1464.89
200.00	5104.18	1470.49
200.00	6105.13	1476.03
200.00	7105.88	1481.53
200.00	8106.60	1486.99
200.00	9107.34	1492.39
200.00	10108.00	1497.75
200.00	12609.80	1510.92
200.00	15111.60	1523.84
200.00	17613.40	1536.5
200.00	20115.20	1548.92
200.00	25118.80	1573.08
200.00	30122.60	1596.41
200.00	35126.20	1618.97
199.99	40128.50	1640.8
199.99	45132.10	1662.03
199.99	50135.60	1682.63
200.00	60142.70	1722.21
200.00	70149.80	1759.84
200.00	80156.90	1795.79
200.00	90164.00	1830.15
200.00	100171.00	1863.22
201.00	250.62	1437.19
201.00	600.55	1439.24
201.00	1100.47	1442.14
201.00	1101.45	1442.16
201.00	2101.94	1447.96
201.00	2102.01	1447.96
201.00	3102.62	1453.68
201.00	4103.38	1459.38
201.00	5104.04	1465.01
220.00	249.98	1330.46
220.00	599.68	1332.78
220.00	1100.72	1336.09
220.00	1100.82	1336.09
220.00	10107.00	1392.58
220.00	12608.80	1407.34
220.00	15110.60	1421.75
220.00	17612.40	1435.83
220.00	2101.56	1342.65
220.00	2101.82	1342.65
220.00	2102.10	1342.65
220.00	2103.43	1342.64
220.00	3102.31	1349.14
220.00	3104.10	1349.13
220.00	4103.01	1355.55
220.00	4104.72	1355.54
220.00	5103.60	1361.88
220.00	6104.22	1368.15
220.00	7104.87	1374.34
220.00	8105.49	1380.51
220.00	9106.16	1386.56
220.00	20114.20	1449.59
220.00	25117.70	1476.25
220.00	30121.30	1501.85
220.00	35124.90	1526.52
220.00	40129.10	1550.28
220.00	45132.70	1573.31
220.00	50136.40	1595.59
220.00	60143.60	1638.17
220.00	70150.80	1678.49
220.00	80157.90	1716.78
220.00	90165.10	1753.24
220.00	100172.00	1788.2
240.00	252.21	1219.33
240.00	602.15	1222.0
240.00	1103.02	1225.8
240.00	2103.48	1233.3
240.00	2104.31	1233.3
240.00	3104.05	1240.7
240.00	3105.10	1240.7
240.00	4104.68	1248.0
240.00	4105.89	1248.0
240.00	5105.31	1255.2
240.00	5106.62	1255.2
240.00	6107.33	1262.31
240.00	12612.00	1306.37
240.00	15113.00	1322.45
240.00	17614.70	1338.08
240.00	20116.40	1353.31
240.00	25119.90	1382.68
240.00	30123.40	1410.72
240.00	35126.80	1437.56
240.00	40130.30	1463.36
240.00	45134.10	1488.2
240.00	50137.60	1512.19
240.00	60144.60	1557.82
240.00	70151.60	1600.75
240.00	7108.05	1269.32
240.00	8108.78	1276.24
240.00	9109.52	1283.08
240.00	10110.20	1289.84
240.00	80158.50	1641.41
240.00	90165.30	1680.02
240.00	100172.00	1716.86
260.00	251.45	1109.14
260.00	601.45	1112.23
260.00	1102.15	1116.62
260.00	2102.77	1125.27
260.00	2103.13	1125.31
260.00	3103.43	1133.77
260.00	3103.82	1133.82
260.00	4104.07	1142.13
260.00	4104.51	1142.17
260.00	5104.72	1150.34
260.00	5105.21	1150.38
260.00	6105.88	1158.47
260.00	7106.52	1166.42
260.00	8107.23	1174.26
260.00	9107.95	1181.97
260.00	10108.30	1189.58
259.99	12610.00	1208.12
260.00	15111.70	1226.05
260.00	17613.40	1243.41
260.00	20115.10	1260.26
260.00	25118.60	1292.53
260.00	30122.10	1323.15
260.00	35125.50	1352.3
260.00	40129.00	1380.18
260.00	45132.70	1406.9
260.00	50136.40	1432.6
260.00	60143.60	1481.28
260.00	70150.70	1526.84
259.99	80157.60	1569.77
259.99	90164.60	1610.4
260.00	100172.00	1649.05
280.00	250.96	999.47
280.00	601.00	1003.08
280.00	1101.74	1008.21
280.00	2102.38	1018.28
280.00	12609.90	1112.63
280.00	15111.50	1132.65
280.00	17613.30	1151.93
280.00	20114.90	1170.54
280.00	2102.38	1018.3
280.00	3103.03	1028.13
280.00	3103.12	1028.15
280.00	4103.63	1037.77
280.00	4103.90	1037.79
280.00	5104.07	1047.2
280.00	5104.65	1047.23
280.00	6105.39	1056.49
280.00	7106.09	1065.56
280.00	8106.82	1074.46
280.00	9107.55	1083.21
280.00	10108.20	1091.8
280.00	25118.30	1205.97
280.00	30121.70	1239.32
280.00	35125.10	1270.88
280.00	40128.50	1300.89
280.00	45132.00	1329.54
280.00	50135.30	1356.98
280.00	60142.30	1408.68
280.00	70149.30	1456.81
280.00	80158.90	1501.97
280.00	90165.90	1544.56
280.00	100173.00	1584.94
300.00	599.94	893.833
300.01	1100.40	899.926
300.00	2102.01	911.889
300.00	2104.25	911.909
300.00	3102.80	923.459
300.00	3104.95	923.478
300.00	4103.65	934.713
300.00	4105.67	934.728
300.00	5104.44	945.669
300.00	5105.89	945.676
300.00	6106.51	956.354
300.00	7107.18	966.776
300.00	8107.81	976.954
300.00	12610.50	1020.17
300.00	15112.20	1042.56
300.00	17613.90	1063.97
300.00	20115.00	1084.5
300.00	25118.50	1123.32
300.00	30121.90	1159.56
300.00	35125.40	1193.62
300.00	40128.90	1225.82
300.00	45132.40	1256.41
300.00	50135.90	1285.58
300.00	60143.00	1340.29
300.00	70150.10	1390.94
299.99	80158.10	1438.22
300.00	9108.38	986.906
300.00	10108.80	996.678
299.99	90165.20	1482.66
299.99	100172.00	1524.68
320.00	601.27	783.221
320.00	1101.18	790.665
320.00	2101.87	805.078
320.00	2104.08	805.159
320.00	3102.51	818.927
320.00	3104.80	819.008
320.00	4103.20	832.273
320.00	4105.51	832.354
320.00	5103.84	845.165
320.00	5106.14	845.242
320.00	6106.80	857.711
320.00	7107.48	869.802
320.00	8108.17	881.54
320.00	9108.89	892.953
320.00	10109.10	904.045
320.00	10109.60	904.067
320.00	12611.30	930.654
320.00	15112.90	955.743
320.00	17614.70	979.543
320.00	20116.40	1002.21
320.00	25119.90	1044.68
320.00	30123.40	1083.95
320.00	35126.90	1120.58
320.00	40130.40	1155.01
320.00	45134.00	1187.55
320.00	50137.30	1218.44
320.00	50137.50	1218.44
320.00	60144.40	1276.1
320.00	70151.60	1329.16
320.00	80158.40	1378.48
320.00	90165.50	1424.69
320.00	100173.00	1468.23
340.00	1100.43	678.122
340.00	2101.09	696.215
340.00	2103.65	696.271
340.00	3101.74	713.3
340.00	3104.31	713.359
340.00	4102.42	729.532
340.00	4105.01	729.589
340.00	5102.92	745.009
340.00	5105.58	745.066
340.00	6106.20	759.882
340.00	7106.82	774.104
340.00	8107.47	787.795
340.00	9108.12	801.008
340.00	10106.50	813.726
340.00	10108.50	813.773
340.00	12610.40	844.028
340.00	15112.20	872.222
340.00	17614.00	898.696
340.00	20115.70	923.702
340.00	25119.20	970.085
340.00	30122.60	1012.52
340.00	35126.10	1051.8
340.00	40129.60	1088.46
340.00	45133.00	1122.94
340.00	50136.50	1155.53
340.00	60144.70	1216.04
340.00	70151.80	1271.43
340.00	80158.80	1322.7
340.00	90165.80	1370.55
340.00	100173.00	1415.54
360.00	2100.75	582.292
360.00	2103.86	582.372
360.00	3101.39	604.477
360.00	3101.42	604.479
360.00	3104.59	604.562
360.00	4102.00	625.0
360.00	4102.06	624.999
360.00	4105.35	625.09
360.00	5102.59	644.168
360.00	5102.98	644.182
360.00	5106.07	644.251
360.00	6106.86	662.279
360.00	7107.63	679.33
360.00	8108.38	695.538
360.00	9109.09	711.01
360.00	10109.80	725.827
360.00	12611.50	760.445
360.00	15113.30	792.205
360.00	17615.10	821.665
360.00	20116.80	849.226
360.00	25120.40	899.751
360.00	30124.20	945.466
360.00	35127.80	987.407
360.00	40131.20	1026.3
360.00	45134.60	1062.68
360.00	50138.10	1096.92
360.00	60145.10	1160.16
360.00	70152.10	1217.74
360.00	80159.00	1270.82
360.00	90166.10	1320.23
360.00	100173.00	1366.55
380.00	2103.23	456.129
380.00	3104.16	488.076
380.00	4105.03	515.932
380.00	5105.83	540.877
380.00	6106.71	563.618
380.00	7107.52	584.618
380.00	8108.31	604.199
380.00	9109.12	622.597
380.00	10109.90	639.978
380.00	12611.10	679.849
380.00	15112.80	715.711
380.00	17614.50	748.486
380.00	20116.20	778.799
380.00	25119.70	833.691
380.00	30123.30	882.725
380.00	35126.80	927.317
380.00	40131.60	968.4
380.00	45135.10	1006.62
380.00	50138.70	1042.44
380.00	60145.70	1108.27
380.00	70152.70	1167.91
380.00	80159.70	1222.69
380.00	90166.70	1273.52
380.00	100174.00	1321.06
400.00	2704.85	329.55
400.00	3105.08	351.68
400.00	4105.76	396.177
400.00	5106.37	431.84
400.00	6107.01	462.275
400.00	7107.72	489.164
400.00	8108.42	513.443
400.00	9109.39	535.712
400.00	10110.20	556.355
400.00	12612.00	602.563
400.00	15113.90	643.081
400.00	17615.70	679.473
400.00	20117.50	712.704
400.00	25121.10	772.062
400.00	30124.70	824.409
400.00	35128.30	871.587
400.00	40131.50	914.764
400.00	45135.00	954.727
400.00	50138.40	992.039
400.00	60145.30	1060.28
400.00	70152.30	1121.82
400.00	80159.20	1178.14
400.00	90166.10	1230.27
400.00	100173.00	1278.93
420.00	4104.41	244.514
420.00	4455.16	271.524
420.00	4604.99	281.85
420.00	4955.63	302.472
420.00	5105.08	310.479
420.00	5456.11	327.761
420.00	5605.74	334.633
420.00	6105.77	355.802
420.00	6606.48	374.829
420.00	7106.50	392.204
420.00	8107.22	423.269
420.00	9107.96	450.696
420.00	10109.00	475.453
420.00	12610.80	529.119
420.00	15112.50	574.769
420.00	17614.90	614.982
420.00	20116.70	651.2
420.00	25120.20	714.992
420.00	30123.70	770.535
420.00	35127.10	820.167
420.00	40130.60	865.305
420.00	45134.00	906.887
420.00	50137.50	945.566
420.00	50138.00	945.569
420.00	55141.50	981.829
420.00	60145.00	1016.01
420.00	70152.10	1079.28
420.00	80159.20	1137.01
420.00	90166.30	1190.31
420.00	100173.00	1239.96
430.00	5105.60	236.474
430.00	5355.26	258.169
430.00	5605.96	273.029
430.00	5855.60	287.251
430.00	6106.29	300.071
430.00	6356.29	311.899
430.00	6356.31	311.9
430.00	6606.63	323.008
430.00	7106.84	343.373
430.00	7106.87	343.374
430.00	7607.19	361.852
430.00	8107.49	378.831
430.00	8607.80	394.6
430.00	9108.14	409.364
430.00	9608.49	423.279
430.00	10108.80	436.468
430.00	11109.60	461.005
430.00	12110.40	483.546
430.00	13111.40	504.468
430.00	14111.80	524.058
430.00	15112.60	542.492
430.00	17614.00	584.593
430.00	20115.70	622.274
430.00	15112.60	542.492
430.00	17614.00	584.593
430.00	20115.70	622.274
Reference

Correlations

Property	Value	Unit	Temperature (K)	Source
Pvap	[1.33; 202.65]	kPa	[195.15; 292.14]	The Yaws Handbook of Vapor Pressure
Equation			ln(Pvp) = A + B/(T + C)
Coefficient A			1.41240e+01
Coefficient B			-2.35413e+03
Coefficient C			-2.50050e+01
Temperature range, min.			195.15
Temperature range, max.			292.14
Pvap	1.33	kPa	195.15	Calculated Property
Pvap	3.04	kPa	205.93	Calculated Property
Pvap	6.32	kPa	216.70	Calculated Property
Pvap	12.15	kPa	227.48	Calculated Property
Pvap	21.86	kPa	238.26	Calculated Property
Pvap	37.18	kPa	249.03	Calculated Property
Pvap	60.23	kPa	259.81	Calculated Property
Pvap	93.51	kPa	270.59	Calculated Property
Pvap	139.92	kPa	281.36	Calculated Property
Pvap	202.65	kPa	292.14	Calculated Property
Pvap	[6.69e-04; 3779.05]	kPa	[134.86; 425.18]	KDB Vapor Pressure Data
Equation			ln(Pvp) = A + B/T + C*ln(T) + D*T^2
Coefficient A			5.87029e+01
Coefficient B			-4.34663e+03
Coefficient C			-6.92229e+00
Coefficient D			9.15271e-06
Temperature range, min.			134.86
Temperature range, max.			425.18
Pvap	6.69e-04	kPa	134.86	Calculated Property
Pvap	0.08	kPa	167.12	Calculated Property
Pvap	1.84	kPa	199.38	Calculated Property
Pvap	15.42	kPa	231.63	Calculated Property
Pvap	71.77	kPa	263.89	Calculated Property
Pvap	229.21	kPa	296.15	Calculated Property
Pvap	569.65	kPa	328.41	Calculated Property
Pvap	1192.33	kPa	360.66	Calculated Property
Pvap	2214.06	kPa	392.92	Calculated Property
Pvap	3779.05	kPa	425.18	Calculated Property

Similar Compounds

Find more compounds similar to Butane.

Mixtures

• Squalane + Butane
• Butane + Ethyl Acetate
• Butane + Methyl Alcohol
• Isopropyl Alcohol + Butane
• Butane + 1-Butanol
• 2-Propanol, 2-methyl- + Butane
• Butane + Ethane, 1,1-difluoro-
• Dimethyl sulfide + Butane
• Butane + Diethyl sulfide
• Butane + Propanenitrile
• Butane + Ethanol
• Butane + Propene, hexafluoro-
• Butane + Hydrogen sulfide
• Propane + Butane
• Butane + Fluoroform
• Butane + Propane, 1,1,1,3,3-pentafluoro
• Ethane, hexafluoro- + Butane
• Butane + Dimethyl ether
• Difluoromethane + Butane
• Ethane, pentafluoro- + Butane

Find more mixtures with Butane.

Sources

• KDB Pure (Korean Thermophysical Properties Databank)
• KDB Vapor Pressure Data
• Crippen Method
• Measurements of the Liquid Viscosities of Mixtures of n-Butane, n-Hexane, and n-Octane with Squalane to 30MPa
• Thermophysical Properties of the Refrigerant Mixtures R417A and R417B from Dynamic Light Scattering (DLS)
• Measurement of the (p, rho, T) Properties for Pure Hydrocarbons at Temperatures up to 600 K and Pressures up to 200 MPa
• Vapour liquid equilibrium for the ethyl ethanoate + 1-butene, +cis-2-butene, +trans-2-butene, +2-methylpropene, +n-butane and +2-methylpropane
• Vapour-liquid equilibrium measurements and correlation for the pentafluoroethane (R125) + n-butane (R600) system
• Viscosity, density, interfacial tension and compositional data for near critical mixtures of methane + butane and methane + decane systems at 310.95K
• Henry s law constants of propane, propene, butane, and 2-methylpropane in methanol at 374-490K
• Vapour liquid equilibrium for the systems butane + methanol, +2-propanol, +1-butanol, +2-butanol, +2-methyl-2-propanol at 364.5K
• Vapor liquid equilibria for the binary system of 1,1-difluoroethane (HFC-152a) + n-butane (R-600) at various temperatures
• Isothermal binary vapour liquid equilibrium for butanes and butenes with dimethylsulphide
• Vapor liquid equilibrium in the n-butane +methanol system, measurement and modeling from 323.2 to 443.2K
• Vapor liquid equilibrium measurements and modeling of the n-butane + ethanol system from 323 to 423K
• 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
• High pressure vapor-liquid equilibria measurements and modeling of butane/ethanol system and isobutane/ethanol system
• Effects of association with impurities in ammonia purification
• Phase equilibrium data for mixtures involving 1,1,2,3,3,3-hexafluoro-1-propene with either propane or n-butane between 312 and 343 K
• An improved static-analytic apparatus for vapor-liquid equilibrium (PTxy) measurement using modified in-situ samplers
• Capillary constant and surface tension of dimethyl ether and n-butane at temperatures from 214 K to those close to the critical point
• Measurements of activity coefficients at infinite dilution for organic solutes in two quaternary ammonium-based ionic liquids [DDA][ClO4] and [DDA][BF4]
• 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
• Measurement of the (p,.rho.,T) relation of propane, propylene, n-butane, and isobutane in the temperature range from (95 to 340) K at pressures up to 12 MPa using an accurate two-sinker densimeter
• 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
• Vapour pressure and excess Gibbs free energy of binary mixtures of hydrogen sulphide with ethane, propane, and n-butane at temperature of 182.33 K
• (pressure,density, temperature) Properties for n-butane in the temperature range from 280 K to 380 K at pressures up to 200 MPa
• Measurements of vapour pressures and saturated-liquid densities for n-butane at T = (280 to 424) K
• (Vapour + liquid) equilibria of the {1,1-difluoroethane (HFC-152a) + n-butane (HC-600)} system
• The (p,q,T,x) properties of (x1 propane + x2 n-butane) with x1 = (0.0000, 0.2729, 0.5021, and 0.7308) over the temperature range from (280 to 440) K at pressures from (1 to 200) MPa
• The (p, rho, T, x) properties for (x1 n-butane + x2 isobutane) with x1 = (0.2625, 0.4913, and 0.7508) in the temperature range from (280 to 440) K at pressures from (1 to 200) MPa
• The (p, rho, T, x) properties for (propane + n-butane + isobutane) ternary mixtures over the temperature range from (280 to 440) K at pressures from (1 to 200) MPa
• (Vapour + liquid) equilibria of the {trifluoromethane (HFC-23) + propane} and {trifluoromethane (HFC-23) + n-butane} systems
• (p, rho, T, x) properties for CO2/n-butane binary mixtures at T = (280 to 440) K and (3 to 200) MPa
• (Vapour + liquid + liquid) equilibrium measurements and correlation for the {1,1,1,2-tetrafluoroethane (R134a) + n-butane (R600)} system
• Isothermal (vapour + liquid) equilibrium measurements and correlation for the {n-butane (R600) + 1,1,1,3,3-pentafluoropropane (R245fa)} system at temperatures from (303.150 to 373.150) K
• Bubble Point Measurements of n-Butane + n-Octane and n-Butane + n-Nonane Binary Mixtures
• Reference Quality Vapor-Liquid Equilibrium Data for the Binary Systems Methane + Ethane, + Propane, + Butane and, + 2-Methylpropane, at Temperatures from (203 to 273) K and Pressures to 9 MPa
• Viscosity and dew point measurements of {xCH4 + (1- x)C4H10} for x = 0.9484 with a vibrating-wire viscometer.
• Viscosity and Density of Normal Butane Simultaneously Measured at Temperatures from (298 to 448) K and at Pressures up to 30 MPa Incorporating the Near-Critical Region
• Measurements of the Speed of Sound in Liquid n-Butane
• Isothermal Vapor-Liquid Equilibrium Data for the Hexafluoroethane (R116) + n-Butane System at Temperatures from 273 to 323 K
• Density and Compressibility of Multicomponent n-Alkane Mixtures up to 463 K and 140 MPa
• Vapor-Liquid Equilibrium Measurements for 2,3,3,3-Tetrafluoroprop-1-ene + Butane at Temperatures from 283.15 to 323.15 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 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
• Measurements of the Speed of Sound for Mixtures of Methane + Butane with a Particular Focus on the Critical State
• Critical Properties of Three Dimethyl Ether Binary Systems: Dimethyl Ether (RE-170) + Propane (HC-290), Butane (HC-600), and 2-Methyl Propane (HC-600A)
• Vapor-Liquid Equilibrium (VLE) Properties for the Binary Systems Propane (1) + n-Butane (2) and Propane (1) + Isobutane (3)
• Liquid-Phase Thermodynamic Properties for the Binary and Ternary Systems of Propane (1), n-Butane (2), and Isobutane (3)
• Liquid-Phase Thermodynamic Properties for Propane (1), n-Butane (2), and Isobutane (3)
• 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 Equilibria of the Binary n-Butane (HC-600) + Difluoromethane (HFC-32), + Pentafluoroethane (HFC-125), + 1,1,1,2-Tetrafluoroethane (HFC-134a) Mixture Systems
• Vapor-Liquid Equilibrium for the Difluoromethane (R32) + n-Butane (R600) System
• 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
• Vapor-Liquid Equilibria of the 1,1,1-Trifluoroethane + n-Butane 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 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
• Phase Behavior of the Butane + Decane Binary System
• Vapor-Liquid Equilibrium for Thiophene + Butane, + trans-But-2-ene, + 2-Methylpropane, and + 2-Methylpropene
• Vapor-Liquid Equilibrium for Dimethyl Disulfide + Butane, + trans-But-2-ene, + 2-Methylpropane, + 2-Methylpropene, + Ethanol, and 2-Ethoxy-2-methylpropane
• Phase Equilibria of H2S-Hydrocarbons (Propane, n-Butane, and n-Pentane) Binary Systems at Low Temperatures
• Experimental Study of p-.rho.-T Relationship of Compressed Liquid Phase for Octafluoropropane and Two near Azeotropic Ternary HFC/HC Mixtures
• Validation of a New Apparatus Using the Dynamic Method for Determining the Critical Properties of Binary Gas/Gas Mixtures
• Bubble-Point Measurements of Eight Binary Mixtures for Organic Rankine Cycle Applications
• Isobaric Heat Capacity Measurements of Liquid Methane + Propane, Methane + Butane, and a Mixed Refrigerant by Differential Scanning Calorimetry at High Pressures and Low Temperatures
• New Vapor Liquid Liquid Equilibrium Solubility Data for iso-Butane, n-Butane, n-Pentane, and n-Hexane in Alkanolamine Aqueous Solutions
• Vapor-Liquid Equilibria for the 1,1,1,2-Tetrafluoroethane (HFC-134a) + n-Butane (R-600) 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
• Vapor Liquid Equilibrium for Butane + Methanol, + Ethanol, + 2-Propanol, + 2-Butanol, and + 2-Methyl-2-Propanol (TBA) at 323 K
• Vapor-Liquid Equilibria for 1,1,1,2,3,3,3-Heptafluoropropane (HFC-227ea) + Butane (R600) at Various Temperatures
• Vapor-Liquid Equilibria for the Binary System of 1,1,1-Trifluoroethane (HFC-143a) + Butane (R600) at Various Temperatures
• Vapor-Liquid Equilibria for Propane (R290) + n-Butane (R600) at Various Temperatures
• 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
• In Situ Determination of Phase Equilibria of Methyl Benzoate + Alkane Mixtures Using an Infrared Absorption Method. Comparison with Polar GC-SAFT Predictions
• Vapor-Liquid Equilibrium for Tetrahydrothiophene + n-Butane, + trans-2-Butene, + 2-Methylpropane, and + 2-Methylpropene
• Isothermal Binary Vapor-Liquid Equilibrium for 2-Methylpropane and n-Butane with 1,2-Ethanedithiol and 2-Methyl-2-propanethiol
• Joback Method
• KDB
• Aqueous Solubility Prediction Method
• Estimated Solubility Method
• McGowan Method
• NIST Webbook
• The Yaws Handbook of Vapor Pressure

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Outlier This icon means that the value is more than 2 standard deviations away from the property mean.