Chemical Properties of n-Butyl ether (CAS 142-96-1)

InChI

InChI=1S/C8H18O/c1-3-5-7-9-8-6-4-2/h3-8H2,1-2H3

InChI Key

DURPTKYDGMDSBL-UHFFFAOYSA-N

Formula

C8H18O

SMILES

CCCCOCCCC

Molecular Weight¹

130.23

CAS

142-96-1

Other Names

• (n-C4H9)2O
• 1,1'-OXYBIS-BUTANE
• 1,1'-Oxybis(butane)
• 1,1'-oxybisbutane
• 1-butoxybutane
• 5-oxanonane
• Butane, 1,1'-oxybis-
• Ether butylique
• NSC 8459
• UN 1149
• butyl ether
• butyl oxide
• di-n-butyl ether
• dibutyl ether
• dibutyl oxide
• n-Dibutyl ether

• ω : Acentric Factor.
• PAff : Proton affinity (kJ/mol).
• T_ig : Autoignition Temperature (K).
• BasG : Gas basicity (kJ/mol).
• Δ_cH°_liquid : Standard liquid 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).
• ε_r : Dielectric Constant (Relative permittivity).
• T_flash,cc : Flash Point (Closed Cup Method) (K).
• Δ_fG° : Standard Gibbs free energy of formation (kJ/mol).
• Δ_fH°_gas : Enthalpy of formation at standard conditions (kJ/mol).
• Δ_fH°_liquid : Liquid phase enthalpy of formation at standard conditions (kJ/mol).
• Δ_fusH° : Enthalpy of fusion at standard conditions (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).
• ν : Kinematic viscosity (m²/s).
• 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).
• pKa : Log10 of Acid Dissociation Constant.
• P_triple : Triple Point Pressure (kPa).
• P_vap : Vapor pressure (kPa).
• n₀ : Refractive Index.
• ρ_l : Liquid Density (kg/m³).
• I_np : Non-polar retention indices.
• I_p : Polar retention indices.
• c_sound,fluid : Speed of sound in fluid (m/s).
• γ : Surface Tension (N/m).
• T_boil : Normal Boiling Point Temperature (K).
• T_c : Critical Temperature (K).
• λ_gas : Gas thermal conductivity (W/m×K).
• λ_liquid : Liquid thermal conductivity (W/m×K).
• T_fus : Normal melting (fusion) point (K).
• T_triple : Triple Point Temperature (K).
• U_Qi : UNIQUAC Qi Parameter.
• U_Ri : UNIQUAC Ri Parameter.
• 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	[0.4476; 0.5020]
ω	0.5000		PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
ω	0.4476		ChemSep v8.3 pure component data Compiled value
ω	0.5020		KDB
PAff	845.70	kJ/mol	NIST
Tig	467.15	K	NCMS SOLV-DB
BasG	[815.50; 818.30]	kJ/mol
BasG	818.30	kJ/mol	NIST
BasG	815.50 ± 0.50	kJ/mol	NIST
BasG	815.50 ± 0.50	kJ/mol	NIST
BasG	816.50	kJ/mol	NIST
ΔcH°liquid	[-5343.40; -5342.63]	kJ/mol
ΔcH°liquid	-5342.63 ± 0.92	kJ/mol	NIST
ΔcH°liquid	-5343.10 ± 2.80	kJ/mol	NIST
ΔcH°liquid	-5343.40 ± 3.30	kJ/mol	NIST
μ	[1.17; 1.20]	debye
μ	1.17	debye	ChemSep v8.3 pure component data Compiled value
μ	1.20	debye	KDB
εr	3.08		NCMS SOLV-DB
Tflash,cc	298.15	K	NCMS SOLV-DB
ΔfG°	[-88.59; -88.27]	kJ/mol
ΔfG°	-88.27	kJ/mol	ChemSep v8.3 pure component data Compiled value
ΔfG°	-88.59	kJ/mol	KDB
ΔfH°gas	[-334.10; -333.90]	kJ/mol
ΔfH°gas	-333.90	kJ/mol	ChemSep v8.3 pure component data Compiled value
ΔfH°gas	-334.10	kJ/mol	KDB
ΔfH°gas	-334.00 ± 2.00	kJ/mol	NIST
ΔfH°gas	-334.00	kJ/mol	NIST
ΔfH°liquid	[-378.00; -377.60]	kJ/mol
ΔfH°liquid	-378.00 ± 1.00	kJ/mol	NIST
ΔfH°liquid	-377.60 ± 2.80	kJ/mol	NIST
ΔfusH°	17.66	kJ/mol	Joback Calculated Property
ΔvapH°	[44.35; 45.00]	kJ/mol
ΔvapH°	44.35	kJ/mol	NCMS SOLV-DB
ΔvapH°	45.00	kJ/mol	NIST
ΔvapH°	44.70 ± 0.10	kJ/mol	NIST
ΔvapH°	44.99	kJ/mol	NIST
ΔvapH°	45.00 ± 0.10	kJ/mol	NIST
ΔvapH°	44.40	kJ/mol	NIST
IE	[9.28; 9.51]	eV
IE	9.28 ± 0.05	eV	NIST
IE	9.44	eV	NIST
IE	9.40	eV	NIST
IE	9.51 ± 0.01	eV	NIST
log10WS	[-1.85; -1.85]
log10WS	-1.85		Aq. Solubility Prediction
log10WS	-1.85		Estimated Solubility
logPoct/wat	3.080		NCMS SOLV-DB
McVol	129.450	ml/mol	McGowan Calculated Property
NFPA Fire	[%!d(float64=3); %!d(float64=3)]
NFPA Fire	3		KDB
NFPA Fire	3		NCMS SOLV-DB
NFPA Health	[%!d(float64=2); %!d(float64=2)]
NFPA Health	2		KDB
NFPA Health	2		NCMS SOLV-DB
NFPA Safety	0		NCMS SOLV-DB
Pc	[2380.00; 3010.00]	kPa
Pc	3000.00	kPa	IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value
Pc	2533.12	kPa	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Pc	2380.00	kPa	ChemSep v8.3 pure component data Compiled value
Pc	3010.00	kPa	KDB
Pc	3010.00 ± 30.07	kPa	NIST
pKa	-5.40		NCMS SOLV-DB
Ptriple	7.14e-07	kPa	ChemSep v8.3 pure component data Compiled value
Inp	[854.00; 888.00]
Inp	865.00		NIST
Inp	854.40		NIST
Inp	876.82		NIST
Inp	854.90		NIST
Inp	854.00		NIST
Inp	875.00		NIST
Inp	861.00		NIST
Inp	865.00		NIST
Inp	858.00		NIST
Inp	858.00		NIST
Inp	865.00		NIST
Inp	875.00		NIST
Inp	857.00		NIST
Inp	859.00		NIST
Inp	858.00		NIST
Inp	862.00		NIST
Inp	Outlier 888.00		NIST
Inp	880.20		NIST
Inp	876.00		NIST
Inp	872.00		NIST
Inp	875.00		NIST
Inp	876.00		NIST
Inp	858.00		NIST
Inp	875.00		NIST
Inp	873.00		NIST
Inp	876.00		NIST
Ip	[965.00; 977.00]
Ip	976.00		NIST
Ip	977.00		NIST
Ip	970.00		NIST
Ip	976.00		NIST
Ip	970.00		NIST
Ip	967.00		NIST
Ip	967.00		NIST
Ip	970.00		NIST
Ip	974.00		NIST
Ip	968.00		NIST
Ip	965.00		NIST
Ip	971.00		NIST
Ip	976.00		NIST
Ip	974.00		NIST
Tboil	[413.43; 415.60]	K
Tboil	415.35	K	ChemSep v8.3 pure component data Compiled value
Tboil	413.43	K	KDB
Tboil	413.45	K	NCMS SOLV-DB
Tboil	415.20	K	NIST
Tboil	414.00	K	NIST
Tboil	414.86 ± 0.20	K	NIST
Tboil	413.50	K	NIST
Tboil	414.65 ± 0.50	K	NIST
Tboil	415.15	K	NIST
Tboil	415.00 ± 2.00	K	NIST
Tboil	415.60 ± 0.50	K	NIST
Tboil	415.45 ± 0.30	K	NIST
Tc	[580.00; 588.10]	K
Tc	584.00	K	IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value
Tc	580.00	K	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Tc	580.15	K	ChemSep v8.3 pure component data Compiled value
Tc	584.10	K	KDB
Tc	588.10	K	NIST
Tc	584.10 ± 0.58	K	NIST
Tfus	[175.25; 177.95]	K
Tfus	176.60	K	Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value
Tfus	177.95	K	ChemSep v8.3 pure component data Compiled value
Tfus	177.90	K	KDB
Tfus	176.62	K	Aq. Solubility Prediction
Tfus	177.95	K	NCMS SOLV-DB
Tfus	177.75	K	NIST
Tfus	Outlier 175.25 ± 0.40	K	NIST
Tfus	177.78 ± 0.05	K	NIST
Ttriple	175.30	K	ChemSep v8.3 pure component data Compiled value
UQi	5.18		ChemSep v8.3 pure component data Compiled value
URi	6.09		ChemSep v8.3 pure component data Compiled value
Vc	[0.500; 0.511]	m3/kmol
Vc	0.500	m3/kmol	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Vc	0.511	m3/kmol	ChemSep v8.3 pure component data Compiled value
Zc	0.2470000		ChemSep v8.3 pure component data Compiled value
Zra	0.25		ChemSep v8.3 pure component data Compiled value

Temperature Dependent Properties

Property	Value	Unit	Temperature (K)	Source
Cp,liquid	278.16	J/mol×K	298.15	NIST
η	0.0006020	Pa×s	298.15	NCMS SOLV-DB
ΔvapH	[36.40; 46.90]	kJ/mol	[293.00; 414.30]
ΔvapH	46.90	kJ/mol	293.00	NIST
ΔvapH	41.70	kJ/mol	375.50	NIST
ΔvapH	40.90	kJ/mol	377.00	NIST
ΔvapH	40.60	kJ/mol	387.50	NIST
ΔvapH	36.40	kJ/mol	388.00	NIST
ΔvapH	39.75	kJ/mol	412.90	KDB
ΔvapH	39.40	kJ/mol	413.00	NIST
ΔvapH	36.49	kJ/mol	413.50	NIST
ΔvapH	43.93 ± 0.42	kJ/mol	414.30	NIST
ν	[0.0000007; 0.0000010]	m2/s	[283.15; 313.15]
ν	0.0000010	m2/s	283.15	Kinematic Viscosities for Ether + Alkane Mixtures: Experimental Results and UNIFAC-VISCO Parameters
ν	0.0000009	m2/s	298.15	Kinematic Viscosities for Ether + Alkane Mixtures: Experimental Results and UNIFAC-VISCO Parameters
ν	0.0000007	m2/s	313.15	Kinematic Viscosities for Ether + Alkane Mixtures: Experimental Results and UNIFAC-VISCO Parameters
Pvap	[0.08; 96.21]	kPa	[263.15; 413.15]
Pvap	0.08	kPa	263.15	Isothermal vapour liquid equilibria and excess molar enthalpies of hex-2-yne + methyl butyl ether and hex-3-yne + dibutyl ether mixtures
Pvap	0.17	kPa	273.15	Isothermal vapour liquid equilibria and excess molar enthalpies of hex-2-yne + methyl butyl ether and hex-3-yne + dibutyl ether mixtures
Pvap	0.34	kPa	283.15	Isothermal vapour liquid equilibria and excess molar enthalpies of hex-2-yne + methyl butyl ether and hex-3-yne + dibutyl ether mixtures
Pvap	0.65	kPa	293.15	Isothermal vapour liquid equilibria and excess molar enthalpies of hex-2-yne + methyl butyl ether and hex-3-yne + dibutyl ether mixtures
Pvap	0.89	kPa	298.15	Isothermal vapour liquid equilibria and excess molar enthalpies of hex-2-yne + methyl butyl ether and hex-3-yne + dibutyl ether mixtures
Pvap	0.80	kPa	298.15	NCMS SOLV-DB
Pvap	1.19	kPa	303.15	Isothermal vapour liquid equilibria and excess molar enthalpies of hex-2-yne + methyl butyl ether and hex-3-yne + dibutyl ether mixtures
Pvap	2.07	kPa	313.15	Phase equilibrium properties of the ternary mixture dibutyl ether + toluene + heptane at 313.15 K
Pvap	2.10	kPa	313.15	Isothermal vapour liquid equilibria and excess molar enthalpies of hex-2-yne + methyl butyl ether and hex-3-yne + dibutyl ether mixtures
Pvap	3.57	kPa	323.15	Isothermal vapour liquid equilibria and excess molar enthalpies of hex-2-yne + methyl butyl ether and hex-3-yne + dibutyl ether mixtures
Pvap	3.63	kPa	323.15	Vapor-Liquid Equilibrium Data, Excess Enthalpy Data, and Azeotropic Data for the Binary System Dibutyl Ether + o-Xylene
Pvap	5.86	kPa	333.15	Isothermal vapour liquid equilibria and excess molar enthalpies of hex-2-yne + methyl butyl ether and hex-3-yne + dibutyl ether mixtures
Pvap	9.33	kPa	343.15	Isothermal vapour liquid equilibria and excess molar enthalpies of hex-2-yne + methyl butyl ether and hex-3-yne + dibutyl ether mixtures
Pvap	13.90	kPa	353.15	Vapor Liquid Equilibrium and Excess Enthalpy Data for Systems Containing N,N-Dimethylacetamide
Pvap	28.40	kPa	373.15	Thermodynamics of binary mixtures containing N-methyl-2-pyrrolidinone VLE measurements for systems with ethers Comparison with the Mod. UNIFAC (Do) and DISQUAC models Predictions for VLE, GE m, HEm and SLE?
Pvap	50.60	kPa	390.80	Vapor-Liquid Equilibrium Data, Excess Enthalpy Data, and Azeotropic Data for the Binary System Dibutyl Ether + o-Xylene
Pvap	96.21	kPa	413.15	Vapor-Liquid Equilibrium Data, Excess Enthalpy Data, and Azeotropic Data for the Binary System Dibutyl Ether + o-Xylene
n0	[1.39300; 1.39920]		[293.15; 303.15]
n0	1.39780		293.15	DIELECTRIC AND REFRACTIVE INDEX MEASUREMENTS FOR THE SYSTEMS 1-PENTANOL + OCTANE, OR + DIBUTYL ETHER OR FOR DIBUTYL ETHER + OCTANE AT DIFFERENT TEMPERATURES
n0	1.39920		293.15	Isobaric Vapor-Liquid Equilibria of the Ternary System Dibutyl Ether + 1-Pentanol + Nonane
n0	1.39700		298.15	Isobaric vapor-liquid equilibria for the binary systems 1-propyl alcohol + dipropyl ether and 1-butyl alcohol + dibutyl ether at 20 and 101.3 kPa
n0	1.39646		298.15	Isothermal vapor liquid equilibrium at 333.15K and excess volumes and molar refractivity deviation at 298.15K for the ternary system di-butyl ether (1) + ethanol (2) + toluene (3) and its binary subsystems
n0	1.39668		298.15	(Liquid + liquid) equilibrium of (dibutyl ether + methanol + water) at different temperatures
n0	1.39630		298.15	Ternary (liquid + liquid) equilibria for the extraction of ethanol, or 2-propanol from aqueous solutions with 1,1'-oxybis(butane) at different temperatures
n0	1.39580		298.15	DIELECTRIC AND REFRACTIVE INDEX MEASUREMENTS FOR THE SYSTEMS 1-PENTANOL + OCTANE, OR + DIBUTYL ETHER OR FOR DIBUTYL ETHER + OCTANE AT DIFFERENT TEMPERATURES
n0	1.39700		298.15	Solubility of -Carotene in Binary Solvents Formed by Some Hydrocarbons with Dibutyl Ether and 1,2-Dimethoxyethane
n0	1.39646		298.15	Isothermal Vapor-Liquid Equilibrium at 333.15 K, Density, and Refractive Index at 298.15 K for the Ternary Mixture of Dibutyl Ether + Ethanol + Benzene and Binary Subsystems
n0	1.39700		298.15	NCMS SOLV-DB
n0	1.39300		303.15	DIELECTRIC AND REFRACTIVE INDEX MEASUREMENTS FOR THE SYSTEMS 1-PENTANOL + OCTANE, OR + DIBUTYL ETHER OR FOR DIBUTYL ETHER + OCTANE AT DIFFERENT TEMPERATURES
ρl	[710.54; 772.45]	kg/m3	[288.15; 358.15]
ρl	772.45	kg/m3	288.15	Excess Enthalpies in Binary Systems of Isomeric C8 Aliphatic Monoethers with Acetonitrile and Their Description by the COSMO-SAC Model
ρl	772.33	kg/m3	288.15	Volumetric properties of binary mixtures of ethers and acetonitrile: Experimental results and application of the Prigogine Flory Patterson theory
ρl	768.00	kg/m3	293.00	KDB
ρl	768.05	kg/m3	293.15	Excess Enthalpies in Binary Systems of Isomeric C8 Aliphatic Monoethers with Acetonitrile and Their Description by the COSMO-SAC Model
ρl	768.07	kg/m3	293.15	Volumetric properties of binary mixtures of ethers and acetonitrile: Experimental results and application of the Prigogine Flory Patterson theory
ρl	763.80	kg/m3	298.00	High-pressure vapor-liquid equilibria of the second generation biofuel blends (2-methylfuran + iso-octane) and (2-methyltetrahydrofuran + di-n-butyl ether): Experiments and PCP-SAFT modeling
ρl	763.70	kg/m3	298.15	Excess Enthalpies in Binary Systems of Isomeric C8 Aliphatic Monoethers with Acetonitrile and Their Description by the COSMO-SAC Model
ρl	763.81	kg/m3	298.15	Excess Molar Enthalpies of Dipropyl Ether + Dibutyl Ether + (1-Hexene or Tetrahydrofuran) at 298.15 K
ρl	764.23	kg/m3	298.15	Binary Liquid-Liquid Equilibrium (LLE) for Dibutyl Ether (DBE) + Water from (288.15 to 318.15) K and Ternary LLE for Systems of DBE + C1 !less thanless than C4 Alcohols + Water at 298.15 K
ρl	763.76	kg/m3	298.15	Volumetric properties of binary mixtures of ethers and acetonitrile: Experimental results and application of the Prigogine Flory Patterson theory
ρl	764.08	kg/m3	298.15	Volumetric properties of (N,N-dimethylformamide + aliphatic diethers) at Temperatures ranging from (298.15 to 358.15) K
ρl	763.81	kg/m3	298.15	Excess molar enthalpies of ternary mixtures (dibutyl ether or dipropyl ether + 2,2-dimethylbutane + 2,3-dimethylbutane) at the temperature 298.15 K
ρl	764.11	kg/m3	298.15	Excess molar enthalpies of the binary systems: (Dibutyl ether + isomers of pentanol) at T = (298.15 and 308.15) K
ρl	763.80	kg/m3	298.15	Isobaric vapor-liquid equilibrium, density and speed of sound of binary mixtures 2,2,4-trimethylpentane + 1-butanol or dibutyl ether (DBE) at 101.3 kPa
ρl	759.60	kg/m3	303.15	Density, viscosity, and speed of sound of binary liquid mixtures of vinyl acetate with butyl vinyl ether, diisopropyl ether, anisole and dibutyl ether
ρl	759.43	kg/m3	303.15	Volumetric properties of binary mixtures of ethers and acetonitrile: Experimental results and application of the Prigogine Flory Patterson theory
ρl	759.40	kg/m3	303.15	Excess Enthalpies in Binary Systems of Isomeric C8 Aliphatic Monoethers with Acetonitrile and Their Description by the COSMO-SAC Model
ρl	755.00	kg/m3	308.15	Excess Enthalpies in Binary Systems of Isomeric C8 Aliphatic Monoethers with Acetonitrile and Their Description by the COSMO-SAC Model
ρl	755.91	kg/m3	308.15	Excess molar enthalpies of the binary systems: (Dibutyl ether + isomers of pentanol) at T = (298.15 and 308.15) K
ρl	755.20	kg/m3	308.15	Density, viscosity, and speed of sound of binary liquid mixtures of vinyl acetate with butyl vinyl ether, diisopropyl ether, anisole and dibutyl ether
ρl	755.22	kg/m3	308.50	Excess Molar Enthalpies and Hydrogen Bonding in Binary Mixtures Containing Ethers and Benzyl Alcohol at 308.15 K and Atmospheric Pressure
ρl	750.80	kg/m3	313.15	Density, viscosity, and speed of sound of binary liquid mixtures of vinyl acetate with butyl vinyl ether, diisopropyl ether, anisole and dibutyl ether
ρl	750.62	kg/m3	313.15	Excess Enthalpies in Binary Systems of Isomeric C8 Aliphatic Monoethers with Acetonitrile and Their Description by the COSMO-SAC Model
ρl	750.92	kg/m3	313.15	Volumetric properties of (N,N-dimethylformamide + aliphatic diethers) at Temperatures ranging from (298.15 to 358.15) K
ρl	746.24	kg/m3	318.15	Excess Enthalpies in Binary Systems of Isomeric C8 Aliphatic Monoethers with Acetonitrile and Their Description by the COSMO-SAC Model
ρl	741.87	kg/m3	323.15	Excess Enthalpies in Binary Systems of Isomeric C8 Aliphatic Monoethers with Acetonitrile and Their Description by the COSMO-SAC Model
ρl	737.68	kg/m3	328.15	Volumetric properties of (N,N-dimethylformamide + aliphatic diethers) at Temperatures ranging from (298.15 to 358.15) K
ρl	724.25	kg/m3	343.15	Volumetric properties of (N,N-dimethylformamide + aliphatic diethers) at Temperatures ranging from (298.15 to 358.15) K
ρl	710.54	kg/m3	358.15	Volumetric properties of (N,N-dimethylformamide + aliphatic diethers) at Temperatures ranging from (298.15 to 358.15) K
csound,fluid	[1142.07; 1220.10]	m/s	[293.15; 308.15]
csound,fluid	1181.82	m/s	293.15	Thermodynamics of (1-alkanol + linear monoether) systems
csound,fluid	1181.82	m/s	293.15	Densities, Excess Molar Volumes, Speeds of Sound at (293.15, 298.15, and 303.15) K and Isentropic Compressibilities at 298.15 K for 1-Butanol, 1-Pentanol, or 1-Hexanol + Dibutylether Systems
csound,fluid	1181.82	m/s	293.15	Thermodynamics of Mixtures Containing Alkoxyethanols. Part XXVI. Densities, Excess Molar Volumes, Speeds of Sound at (293.15, 298.15, and 303.15) K, and Isentropic or Isothermal Compressibilities at 298.15 K for 2-Methoxyethanol + Alkoxyethanol or 2-Propoxyethanol + Dibutylether Systems
csound,fluid	1161.19	m/s	298.15	Thermodynamics of (1-alkanol + linear monoether) systems
csound,fluid	1220.10	m/s	298.15	Densities, Excess Molar Volumes at T = (298.15 to 313.15) K, Speeds of Sound, Excess Isentropic Compressibilities, Relative Permittivities and Deviations in Molar Polarizations at T = (298.15 and 308.15) K for Methyl Methacrylate + 2-Butoxyethanol or + Dibutyl Ether + Benzene, + Toluene and + p-Xylene
csound,fluid	1161.19	m/s	298.15	Densities, Excess Molar Volumes, Speeds of Sound at (293.15, 298.15, and 303.15) K and Isentropic Compressibilities at 298.15 K for 1-Butanol, 1-Pentanol, or 1-Hexanol + Dibutylether Systems
csound,fluid	1161.19	m/s	298.15	Thermodynamics of Mixtures Containing Alkoxyethanols. Part XXVI. Densities, Excess Molar Volumes, Speeds of Sound at (293.15, 298.15, and 303.15) K, and Isentropic or Isothermal Compressibilities at 298.15 K for 2-Methoxyethanol + Alkoxyethanol or 2-Propoxyethanol + Dibutylether Systems
csound,fluid	1142.07	m/s	303.15	Thermodynamics of (1-alkanol + linear monoether) systems
csound,fluid	1142.07	m/s	303.15	Densities, Excess Molar Volumes, Speeds of Sound at (293.15, 298.15, and 303.15) K and Isentropic Compressibilities at 298.15 K for 1-Butanol, 1-Pentanol, or 1-Hexanol + Dibutylether Systems
csound,fluid	1142.07	m/s	303.15	Thermodynamics of Mixtures Containing Alkoxyethanols. Part XXVI. Densities, Excess Molar Volumes, Speeds of Sound at (293.15, 298.15, and 303.15) K, and Isentropic or Isothermal Compressibilities at 298.15 K for 2-Methoxyethanol + Alkoxyethanol or 2-Propoxyethanol + Dibutylether Systems
csound,fluid	1179.00	m/s	308.15	Densities, Excess Molar Volumes at T = (298.15 to 313.15) K, Speeds of Sound, Excess Isentropic Compressibilities, Relative Permittivities and Deviations in Molar Polarizations at T = (298.15 and 308.15) K for Methyl Methacrylate + 2-Butoxyethanol or + Dibutyl Ether + Benzene, + Toluene and + p-Xylene
γ	[0.02; 0.03]	N/m	[263.17; 373.17]
γ	0.03	N/m	263.17	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.03	N/m	268.18	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	273.18	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	278.19	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	283.20	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	288.19	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	293.18	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	298.11	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	298.15	NCMS SOLV-DB
γ	0.02	N/m	298.20	KDB
γ	0.02	N/m	303.17	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	308.05	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	313.18	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	318.13	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	323.20	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	328.20	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	333.18	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	338.18	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	343.17	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	348.18	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	353.17	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	358.18	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	363.19	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	368.19	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	373.17	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether

Datasets

1. Viscosity, Pa*s (1)
2. Mass density, kg/m3 (3)
3. Thermal conductivity, W/m/K (1)

Viscosity, Pa*s

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Viscosity, Pa*s - Liquid
243.15	100.00	0.0017
243.15	4800.00	0.0018
243.15	10290.00	0.0020
243.15	15700.00	0.0021
243.15	21120.00	0.0022
253.15	100.00	0.0014
253.15	4550.00	0.0014
253.15	9650.00	0.0015
253.15	14760.00	0.0016
253.15	19760.00	0.0017
263.15	100.00	0.0011
263.15	4650.00	0.0012
263.15	10000.00	0.0013
263.15	15290.00	0.0013
263.15	20520.00	0.0014
273.15	100.00	0.0009
273.15	4810.00	0.0010
273.15	10200.00	0.0010
273.15	15570.00	0.0011
273.15	20870.00	0.0012
283.15	100.00	0.0008
283.15	4780.00	0.0008
283.15	10150.00	0.0009
283.15	15580.00	0.0009
283.15	20830.00	0.0010
293.15	100.00	0.0007
293.15	4750.00	0.0007
293.15	10180.00	0.0008
293.15	15470.00	0.0008
293.15	20760.00	0.0009
303.15	100.00	0.0006
303.15	4500.00	0.0006
303.15	9570.00	0.0007
303.15	14530.00	0.0007
303.15	19670.00	0.0007
313.15	100.00	0.0005
313.15	4510.00	0.0006
313.15	9600.00	0.0006
313.15	14650.00	0.0006
313.15	19640.00	0.0007
323.15	100.00	0.0005
323.15	4510.00	0.0005
323.15	9570.00	0.0005
323.15	14630.00	0.0006
323.15	19600.00	0.0006
333.15	100.00	0.0004
333.15	4490.00	0.0005
333.15	9580.00	0.0005
333.15	14630.00	0.0005
333.15	19620.00	0.0005
343.15	100.00	0.0004
343.15	4640.00	0.0004
343.15	9640.00	0.0004
343.15	14730.00	0.0005
343.15	19730.00	0.0005
353.15	100.00	0.0004
353.15	4510.00	0.0004
353.15	9570.00	0.0004
353.15	14640.00	0.0004
353.15	19630.00	0.0004
363.15	100.00	0.0003
363.15	4510.00	0.0003
363.15	9720.00	0.0004
363.15	15300.00	0.0004
363.15	21100.00	0.0004
373.15	100.00	0.0003
373.15	4900.00	0.0003
373.15	10170.00	0.0003
373.15	15630.00	0.0004
373.15	20590.00	0.0004
Reference

Mass density, kg/m3

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Mass density, kg/m3 - Liquid
283.15	100.00	777.0
288.15	100.00	772.71
293.15	100.00	768.41
298.15	100.00	764.09
303.15	100.00	759.76
308.15	100.00	755.41
318.15	100.00	746.7
323.15	100.00	742.29
328.15	100.00	737.85
333.15	100.00	733.4
283.15	5000.00	781.24
288.15	5000.00	777.03
293.15	5000.00	772.85
298.15	5000.00	768.6
303.15	5000.00	764.4
308.15	5000.00	760.14
318.15	5000.00	751.63
323.15	5000.00	747.39
328.15	5000.00	743.06
333.15	5000.00	738.78
283.15	10000.00	785.22
288.15	10000.00	781.07
293.15	10000.00	777.07
298.15	10000.00	772.95
303.15	10000.00	768.85
308.15	10000.00	764.73
318.15	10000.00	756.5
323.15	10000.00	752.4
328.15	10000.00	748.22
333.15	10000.00	744.06
283.15	15000.00	789.01
288.15	15000.00	785.0
293.15	15000.00	781.04
298.15	15000.00	777.05
303.15	15000.00	773.07
308.15	15000.00	769.04
318.15	15000.00	761.07
323.15	15000.00	757.08
328.15	15000.00	753.05
333.15	15000.00	749.04
283.15	20000.00	792.62
288.15	20000.00	788.61
293.15	20000.00	784.83
298.15	20000.00	780.93
303.15	20000.00	777.07
308.15	20000.00	773.17
318.15	20000.00	765.43
323.15	20000.00	761.57
328.15	20000.00	757.64
333.15	20000.00	753.72
283.15	25000.00	796.12
288.15	25000.00	792.26
293.15	25000.00	788.51
298.15	25000.00	784.66
303.15	25000.00	780.91
308.15	25000.00	777.08
318.15	25000.00	769.53
323.15	25000.00	765.77
328.15	25000.00	761.95
333.15	25000.00	758.2
283.15	30000.00	799.48
288.15	30000.00	795.67
293.15	30000.00	792.02
298.15	30000.00	788.29
303.15	30000.00	784.58
308.15	30000.00	780.86
318.15	30000.00	773.46
323.15	30000.00	769.82
328.15	30000.00	766.06
333.15	30000.00	762.39
283.15	35000.00	802.7
288.15	35000.00	799.01
293.15	35000.00	795.4
298.15	35000.00	791.72
303.15	35000.00	788.11
308.15	35000.00	784.45
318.15	35000.00	777.24
323.15	35000.00	773.67
328.15	35000.00	770.02
333.15	35000.00	766.45
283.15	40000.00	805.84
288.15	40000.00	802.2
293.15	40000.00	798.65
298.15	40000.00	795.05
303.15	40000.00	791.5
308.15	40000.00	787.91
318.15	40000.00	780.87
323.15	40000.00	777.34
328.15	40000.00	773.78
333.15	40000.00	770.3
283.15	45000.00	808.84
288.15	45000.00	805.31
293.15	45000.00	801.84
298.15	45000.00	798.27
303.15	45000.00	794.77
308.15	45000.00	791.25
318.15	45000.00	784.34
323.15	45000.00	780.89
328.15	45000.00	777.42
333.15	45000.00	773.98
283.15	50000.00	811.78
288.15	50000.00	808.25
293.15	50000.00	804.88
298.15	50000.00	801.34
303.15	50000.00	797.96
308.15	50000.00	794.48
318.15	50000.00	787.7
323.15	50000.00	784.31
328.15	50000.00	780.92
333.15	50000.00	777.5
283.15	55000.00	814.68
288.15	55000.00	811.16
293.15	55000.00	807.8
298.15	55000.00	804.38
303.15	55000.00	801.03
308.15	55000.00	797.62
318.15	55000.00	790.93
323.15	55000.00	787.61
328.15	55000.00	784.25
333.15	55000.00	780.96
283.15	60000.00	817.42
288.15	60000.00	814.04
293.15	60000.00	810.68
298.15	60000.00	807.34
303.15	60000.00	804.04
308.15	60000.00	800.63
318.15	60000.00	794.06
323.15	60000.00	790.8
328.15	60000.00	787.5
333.15	60000.00	784.27
283.15	65000.00	820.1
288.15	65000.00	816.76
293.15	65000.00	813.46
298.15	65000.00	810.16
303.15	65000.00	806.89
308.15	65000.00	803.58
318.15	65000.00	797.14
323.15	65000.00	793.92
328.15	65000.00	790.65
333.15	65000.00	787.49
Reference

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Mass density, kg/m3 - Liquid
298.15	100.00	763.8
298.15	1000.00	764.7
298.15	5000.00	768.2
298.15	10000.00	772.4
298.15	15000.00	776.4
298.15	20000.00	780.2
298.15	25000.00	783.7
298.15	30000.00	787.3
298.15	35000.00	790.6
298.15	40000.00	793.8
298.15	45000.00	796.9
298.15	50000.00	799.8
298.15	55000.00	802.8
298.15	60000.00	805.6
298.15	65000.00	808.3
298.15	70000.00	811.0
298.15	80000.00	816.1
298.15	90000.00	821.0
298.15	100000.00	825.5
298.15	110000.00	830.0
298.15	120000.00	834.2
298.15	130000.00	838.3
298.15	140000.00	842.1
313.15	100.00	750.7
313.15	1000.00	751.6
313.15	5000.00	755.6
313.15	10000.00	760.1
313.15	15000.00	764.5
313.15	20000.00	768.6
313.15	25000.00	772.3
313.15	30000.00	776.2
313.15	35000.00	779.7
313.15	40000.00	783.1
313.15	45000.00	786.4
313.15	50000.00	789.7
313.15	55000.00	792.7
313.15	60000.00	795.7
313.15	65000.00	798.6
313.15	70000.00	801.4
313.15	80000.00	806.7
313.15	90000.00	811.9
313.15	100000.00	816.7
313.15	110000.00	821.4
313.15	120000.00	825.7
313.15	130000.00	830.1
313.15	140000.00	834.2
333.15	100.00	733.0
333.15	1000.00	734.0
333.15	5000.00	738.5
333.15	10000.00	743.6
333.15	15000.00	748.6
333.15	20000.00	753.1
333.15	25000.00	757.5
333.15	30000.00	761.5
333.15	35000.00	765.5
333.15	40000.00	769.2
333.15	45000.00	772.7
333.15	50000.00	776.2
333.15	55000.00	779.6
333.15	60000.00	782.7
333.15	65000.00	785.8
333.15	70000.00	788.8
333.15	80000.00	794.6
333.15	90000.00	800.0
333.15	100000.00	805.2
333.15	110000.00	810.0
333.15	120000.00	814.7
333.15	130000.00	819.3
333.15	140000.00	823.5
353.15	100.00	715.0
353.15	1000.00	716.2
353.15	5000.00	721.3
353.15	10000.00	727.2
353.15	15000.00	732.7
353.15	20000.00	737.8
353.15	25000.00	742.6
353.15	30000.00	747.1
353.15	35000.00	751.4
353.15	40000.00	755.4
353.15	45000.00	759.3
353.15	50000.00	763.0
353.15	55000.00	766.6
353.15	60000.00	770.1
353.15	65000.00	773.4
353.15	70000.00	776.7
353.15	80000.00	782.7
353.15	90000.00	788.5
353.15	100000.00	794.0
353.15	110000.00	799.2
353.15	120000.00	804.0
353.15	130000.00	808.7
353.15	140000.00	813.3
373.15	1000.00	697.9
373.15	5000.00	703.8
373.15	10000.00	710.5
373.15	15000.00	716.7
373.15	20000.00	722.4
373.15	25000.00	727.7
373.15	30000.00	732.7
373.15	35000.00	737.4
373.15	40000.00	741.9
373.15	45000.00	746.1
373.15	50000.00	750.0
373.15	55000.00	754.0
373.15	60000.00	757.7
373.15	65000.00	761.2
373.15	70000.00	764.6
373.15	80000.00	771.2
373.15	90000.00	777.3
373.15	100000.00	783.0
373.15	110000.00	788.5
373.15	120000.00	793.6
373.15	130000.00	798.6
373.15	140000.00	803.3
393.15	1000.00	679.0
393.15	5000.00	685.9
393.15	10000.00	693.5
393.15	15000.00	700.6
393.15	20000.00	706.9
393.15	25000.00	712.8
393.15	30000.00	718.3
393.15	35000.00	723.5
393.15	40000.00	728.3
393.15	45000.00	732.8
393.15	50000.00	737.2
393.15	55000.00	741.4
393.15	60000.00	745.3
393.15	65000.00	749.1
393.15	70000.00	752.8
393.15	80000.00	759.7
393.15	90000.00	766.2
393.15	100000.00	772.3
393.15	110000.00	778.1
393.15	120000.00	783.4
393.15	130000.00	788.6
393.15	140000.00	793.6
Reference

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Mass density, kg/m3 - Liquid
293.15	100.00	768.0
293.15	10000.00	776.4
293.15	20000.00	783.9
293.15	30000.00	790.8
293.15	40000.00	797.2
293.15	50000.00	803.2
293.15	60000.00	808.7
293.15	70000.00	814.0
293.15	80000.00	819.1
293.15	90000.00	823.8
293.15	100000.00	828.6
293.15	110000.00	832.8
293.15	120000.00	837.0
293.15	130000.00	841.0
293.15	140000.00	844.9
313.15	100.00	750.5
313.15	10000.00	759.8
313.15	20000.00	768.1
313.15	30000.00	775.9
313.15	40000.00	782.8
313.15	50000.00	789.4
313.15	60000.00	795.4
313.15	70000.00	801.5
313.15	80000.00	806.8
313.15	90000.00	812.0
313.15	100000.00	816.7
313.15	110000.00	821.4
313.15	120000.00	825.9
313.15	130000.00	830.2
313.15	140000.00	834.3
333.15	100.00	733.5
333.15	10000.00	744.1
333.15	20000.00	753.5
333.15	30000.00	761.9
333.15	40000.00	769.5
333.15	50000.00	776.6
333.15	60000.00	783.1
333.15	70000.00	789.2
333.15	80000.00	795.0
333.15	90000.00	800.7
333.15	100000.00	805.7
333.15	110000.00	810.5
333.15	120000.00	814.7
333.15	130000.00	819.4
333.15	140000.00	823.7
353.15	100.00	715.1
353.15	10000.00	727.2
353.15	20000.00	737.8
353.15	30000.00	747.1
353.15	40000.00	755.5
353.15	50000.00	763.2
353.15	60000.00	770.2
353.15	70000.00	776.4
353.15	80000.00	782.7
353.15	90000.00	788.4
353.15	100000.00	794.0
353.15	110000.00	799.2
353.15	120000.00	804.2
353.15	130000.00	808.6
353.15	140000.00	813.3
373.15	100.00	696.4
373.15	10000.00	710.3
373.15	20000.00	722.3
373.15	30000.00	732.8
373.15	40000.00	741.8
373.15	50000.00	750.1
373.15	60000.00	757.6
373.15	70000.00	764.7
373.15	80000.00	771.1
373.15	90000.00	777.2
373.15	100000.00	783.0
373.15	110000.00	788.6
373.15	120000.00	793.5
373.15	130000.00	798.5
373.15	140000.00	803.1
393.15	100.00	677.3
393.15	10000.00	693.9
393.15	20000.00	707.3
393.15	30000.00	718.4
393.15	40000.00	728.7
393.15	50000.00	737.2
393.15	60000.00	745.3
393.15	70000.00	752.8
393.15	80000.00	759.9
393.15	90000.00	766.2
393.15	100000.00	772.2
393.15	110000.00	778.1
393.15	120000.00	783.4
393.15	130000.00	788.6
393.15	140000.00	793.5
Reference

Thermal conductivity, W/m/K

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Thermal conductivity, W/m/K - Liquid
235.96	30000.00	0.1494
236.06	20000.00	0.1463
236.17	10100.00	0.1432
236.22	200.00	0.1403
236.40	20100.00	0.1462
236.55	20100.00	0.1464
236.56	5100.00	0.1418
236.58	10000.00	0.1432
236.62	200.00	0.1406
236.87	10100.00	0.1432
236.88	30100.00	0.1491
236.95	200.00	0.1402
236.96	5000.00	0.1414
237.10	5000.00	0.1419
237.29	30000.00	0.1488
254.45	30100.00	0.1455
254.65	10000.00	0.1394
254.73	5100.00	0.1379
254.84	30000.00	0.1460
254.85	10000.00	0.1400
254.96	20000.00	0.1429
255.01	5100.00	0.1384
255.03	10000.00	0.1402
255.06	200.00	0.1367
255.11	200.00	0.1368
255.11	20000.00	0.1431
255.35	30000.00	0.1456
255.36	5100.00	0.1379
255.45	200.00	0.1364
255.78	20000.00	0.1430
274.66	200.00	0.1316
274.78	10100.00	0.1352
274.84	200.00	0.1310
274.92	5000.00	0.1323
274.96	30400.00	0.1413
275.06	10200.00	0.1352
275.08	5200.00	0.1330
275.12	30100.00	0.1413
275.27	20300.00	0.1384
275.31	20000.00	0.1384
275.38	30200.00	0.1414
275.44	200.00	0.1312
275.50	10000.00	0.1346
275.56	5100.00	0.1324
275.87	20100.00	0.1380
294.81	10200.00	0.1306
294.81	20000.00	0.1344
294.96	30000.00	0.1383
295.02	30100.00	0.1378
295.03	5100.00	0.1281
295.07	10000.00	0.1299
295.13	5200.00	0.1284
295.17	200.00	0.1260
295.17	5000.00	0.1276
295.29	20000.00	0.1351
295.37	10000.00	0.1302
295.55	30000.00	0.1384
295.56	200.00	0.1266
295.78	20000.00	0.1347
295.95	200.00	0.1262
314.68	20000.00	0.1286
314.87	200.00	0.1201
314.97	30100.00	0.1326
315.00	20000.00	0.1285
315.10	5000.00	0.1219
315.16	10100.00	0.1246
315.16	30100.00	0.1326
315.21	200.00	0.1203
315.32	20000.00	0.1289
315.45	30000.00	0.1327
315.55	200.00	0.1200
315.55	10000.00	0.1245
315.63	5100.00	0.1223
315.95	10000.00	0.1250
315.97	5000.00	0.1218
334.91	200.00	0.1145
334.94	20000.00	0.1240
335.00	9900.00	0.1191
335.18	200.00	0.1142
335.28	20000.00	0.1241
335.29	5000.00	0.1168
335.31	10100.00	0.1197
335.41	30000.00	0.1280
335.59	200.00	0.1147
335.64	30100.00	0.1286
335.69	5000.00	0.1173
335.74	10100.00	0.1191
335.74	20000.00	0.1245
335.74	30000.00	0.1288
336.14	5100.00	0.1174
354.90	20100.00	0.1196
354.98	30000.00	0.1232
355.04	200.00	0.1083
355.04	20000.00	0.1195
355.09	5200.00	0.1114
355.19	10300.00	0.1145
355.24	30000.00	0.1229
355.28	10200.00	0.1142
355.34	5300.00	0.1118
355.47	30000.00	0.1231
355.56	20000.00	0.1190
355.63	200.00	0.1081
355.69	5200.00	0.1113
355.73	10100.00	0.1147
356.48	200.00	0.1087
374.72	200.00	0.1025
374.90	30000.00	0.1186
374.98	5000.00	0.1054
374.99	30000.00	0.1183
375.00	200.00	0.1024
375.15	20000.00	0.1134
375.25	200.00	0.1024
375.25	5000.00	0.1049
375.26	10000.00	0.1088
375.52	20000.00	0.1128
375.58	10000.00	0.1082
375.70	5000.00	0.1055
375.95	30000.00	0.1198
375.97	20000.00	0.1141
376.07	10000.00	0.1085
Reference

Correlations

Property	Value	Unit	Temperature (K)	Source
Cp,gas	[166.75; 521.93]	J/mol×K	[200.00; 1500.00]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A + exp(B/T + C + D·T + E·T²) Y is Cp,gas in J/mol×K, T in K
Coefficient A			1.52990e+02
Coefficient B			-8.05710e+02
Coefficient C			6.69724e+00
Coefficient D			-2.46560e-04
Coefficient E			5.34970e-08
Temperature range, min.			200.00
Temperature range, max.			1500.00
Cp,gas	166.75	J/mol×K	200.00	Calculated Property
Cp,gas	225.19	J/mol×K	344.44	Calculated Property
Cp,gas	292.96	J/mol×K	488.89	Calculated Property
Cp,gas	351.41	J/mol×K	633.33	Calculated Property
Cp,gas	398.15	J/mol×K	777.78	Calculated Property
Cp,gas	434.93	J/mol×K	922.22	Calculated Property
Cp,gas	463.98	J/mol×K	1066.67	Calculated Property
Cp,gas	487.22	J/mol×K	1211.11	Calculated Property
Cp,gas	506.16	J/mol×K	1355.56	Calculated Property
Cp,gas	521.93	J/mol×K	1500.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
Cp,liquid	[253.33; 348.16]	J/mol×K	[175.30; 450.00]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A + exp(B/T + C + D·T + E·T²) Y is Cp,liquid in J/mol×K, T in K
Coefficient A			1.98760e+02
Coefficient B			6.54320e+01
Coefficient C			2.90454e+00
Coefficient D			3.96940e-03
Coefficient E			8.41780e-07
Temperature range, min.			175.30
Temperature range, max.			450.00
Cp,liquid	253.33	J/mol×K	175.30	Calculated Property
Cp,liquid	257.62	J/mol×K	205.82	Calculated Property
Cp,liquid	263.25	J/mol×K	236.34	Calculated Property
Cp,liquid	270.21	J/mol×K	266.87	Calculated Property
Cp,liquid	278.56	J/mol×K	297.39	Calculated Property
Cp,liquid	288.44	J/mol×K	327.91	Calculated Property
Cp,liquid	300.05	J/mol×K	358.43	Calculated Property
Cp,liquid	313.66	J/mol×K	388.96	Calculated Property
Cp,liquid	329.57	J/mol×K	419.48	Calculated Property
Cp,liquid	348.16	J/mol×K	450.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
η	[0.0059213; 0.0001305]	Pa×s	[175.30; 473.00]	ChemSep v8.3 pure component data Compiled value
Equation			Y = exp(A + B/T + C·ln(T) + D·T^E) Y is η in Pa×s, T in K
Coefficient A			2.07430e+01
Coefficient B			-8.30030e+01
Coefficient C			-4.94040e+00
Coefficient D			4.09600e-06
Coefficient E			2.00000e+00
Temperature range, min.			175.30
Temperature range, max.			473.00
η	0.0059213	Pa×s	175.30	Calculated Property
η	0.0028626	Pa×s	208.38	Calculated Property
η	0.0015517	Pa×s	241.46	Calculated Property
η	0.0009198	Pa×s	274.53	Calculated Property
η	0.0005861	Pa×s	307.61	Calculated Property
η	0.0003966	Pa×s	340.69	Calculated Property
η	0.0002825	Pa×s	373.77	Calculated Property
η	0.0002103	Pa×s	406.84	Calculated Property
η	0.0001628	Pa×s	439.92	Calculated Property
η	0.0001305	Pa×s	473.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
ΔvapH	[52.36; 15.30]	kJ/mol	[175.30; 562.58]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A·(1 − Tr)^(B + C·Tr + D·Tr² + E·Tr³), Tr = T/Tc Y is ΔvapH in kJ/mol, T in K
Coefficient A			6.48590e+01
Coefficient B			7.79920e-01
Coefficient C			-7.23830e-01
Coefficient D			3.80940e-01
Coefficient E			-2.53880e-02
Critical temperature, Tc (K)			5.80150e+02
Temperature range, min.			175.30
Temperature range, max.			562.58
ΔvapH	52.36	kJ/mol	175.30	Calculated Property
ΔvapH	49.79	kJ/mol	218.33	Calculated Property
ΔvapH	47.26	kJ/mol	261.36	Calculated Property
ΔvapH	44.67	kJ/mol	304.39	Calculated Property
ΔvapH	41.93	kJ/mol	347.42	Calculated Property
ΔvapH	38.89	kJ/mol	390.46	Calculated Property
ΔvapH	35.36	kJ/mol	433.49	Calculated Property
ΔvapH	31.01	kJ/mol	476.52	Calculated Property
ΔvapH	25.17	kJ/mol	519.55	Calculated Property
ΔvapH	15.30	kJ/mol	562.58	Calculated Property

Property	Value	Unit	Temperature (K)	Source
Pvap	[1.33; 202.65]	kPa	[311.72; 439.82]	The Yaws Handbook of Vapor Pressure
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
Coefficient A			1.53293e+01
Coefficient B			-3.84219e+03
Coefficient C			-5.62840e+01
Temperature range, min.			311.72
Temperature range, max.			439.82
Pvap	1.33	kPa	311.72	Calculated Property
Pvap	2.95	kPa	325.95	Calculated Property
Pvap	6.02	kPa	340.19	Calculated Property
Pvap	11.49	kPa	354.42	Calculated Property
Pvap	20.68	kPa	368.65	Calculated Property
Pvap	35.35	kPa	382.89	Calculated Property
Pvap	57.77	kPa	397.12	Calculated Property
Pvap	90.77	kPa	411.35	Calculated Property
Pvap	137.74	kPa	425.59	Calculated Property
Pvap	202.65	kPa	439.82	Calculated Property
Pvap	[6.66e-07; 2258.92]	kPa	[175.30; 580.15]	ChemSep v8.3 pure component data Compiled value
Equation			Y = exp(A + B/T + C·ln(T) + D·T^E) Y is Pvap in kPa, T in K
Coefficient A			8.87965e+01
Coefficient B			-8.29424e+03
Coefficient C			-1.08182e+01
Coefficient D			6.12719e-06
Coefficient E			2.00000e+00
Comment			Range stopped at Tc; ChemSep gives it to 584.1 K.
Temperature range, min.			175.30
Temperature range, max.			580.15
Pvap	6.66e-07	kPa	175.30	Calculated Property
Pvap	9.86e-04	kPa	220.28	Calculated Property
Pvap	0.09	kPa	265.27	Calculated Property
Pvap	1.79	kPa	310.25	Calculated Property
Pvap	14.70	kPa	355.23	Calculated Property
Pvap	68.77	kPa	400.22	Calculated Property
Pvap	222.61	kPa	445.20	Calculated Property
Pvap	562.06	kPa	490.18	Calculated Property
Pvap	1195.90	kPa	535.17	Calculated Property
Pvap	2258.92	kPa	580.15	Calculated Property
Pvap	[19.54; 100.69]	kPa	[362.29; 413.21]	NIST
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
Coefficient A			1.36547e+01
Coefficient B			-2.99973e+03
Coefficient C			-8.14810e+01
Reference			Cidlinský and Polák, 1969
Temperature range, min.			362.29
Temperature range, max.			413.21
Pvap	19.54	kPa	362.29	Calculated Property
Pvap	24.13	kPa	367.95	Calculated Property
Pvap	29.55	kPa	373.61	Calculated Property
Pvap	35.92	kPa	379.26	Calculated Property
Pvap	43.34	kPa	384.92	Calculated Property
Pvap	51.93	kPa	390.58	Calculated Property
Pvap	61.83	kPa	396.24	Calculated Property
Pvap	73.16	kPa	401.89	Calculated Property
Pvap	86.07	kPa	407.55	Calculated Property
Pvap	100.69	kPa	413.21	Calculated Property

Property	Value	Unit	Temperature (K)	Source
ρl	[864.19; 309.19]	kg/m3	[175.30; 580.15]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A / B^(1 + (1 − T/C)^D) Y is ρl in kg/m3, T in K
Coefficient A			2.98560e+01
Coefficient B			1.74120e-01
Coefficient C			5.84110e+02
Coefficient D			2.17640e-01
Comment			Range stopped at Tc; ChemSep gives it to 584.1 K.
Temperature range, min.			175.30
Temperature range, max.			580.15
ρl	864.19	kg/m3	175.30	Calculated Property
ρl	829.87	kg/m3	220.28	Calculated Property
ρl	793.64	kg/m3	265.27	Calculated Property
ρl	755.02	kg/m3	310.25	Calculated Property
ρl	713.35	kg/m3	355.23	Calculated Property
ρl	667.58	kg/m3	400.22	Calculated Property
ρl	615.94	kg/m3	445.20	Calculated Property
ρl	554.88	kg/m3	490.18	Calculated Property
ρl	475.06	kg/m3	535.17	Calculated Property
ρl	309.19	kg/m3	580.15	Calculated Property

Property	Value	Unit	Temperature (K)	Source
γ	[0.03; 0.01]	N/m	[178.15; 413.15]	Jasper (1972), surface tension of pure liquid compounds Compiled value
Equation			Y = A + B·T + C·T² + D·T³ + E·T⁴ Y is γ in N/m, T in K
Coefficient A			5.02922e-02
Coefficient B			-9.34000e-05
Coefficient C			0.00000e+00
Coefficient D			0.00000e+00
Coefficient E			0.00000e+00
Temperature range, min.			178.15
Temperature range, max.			413.15
γ	0.03	N/m	178.15	Calculated Property
γ	0.03	N/m	204.26	Calculated Property
γ	0.03	N/m	230.37	Calculated Property
γ	0.03	N/m	256.48	Calculated Property
γ	0.02	N/m	282.59	Calculated Property
γ	0.02	N/m	308.71	Calculated Property
γ	0.02	N/m	334.82	Calculated Property
γ	0.02	N/m	360.93	Calculated Property
γ	0.01	N/m	387.04	Calculated Property
γ	0.01	N/m	413.15	Calculated Property
γ	[0.03; 8.58e-04]	N/m	[175.30; 562.58]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A + exp(B/T + C + D·T + E·T²) Y is γ in N/m, T in K
Coefficient A			-1.16700e-02
Coefficient B			4.49060e+01
Coefficient C			-3.35670e+00
Coefficient D			9.77120e-04
Coefficient E			-5.22160e-06
Temperature range, min.			175.30
Temperature range, max.			562.58
γ	0.03	N/m	175.30	Calculated Property
γ	0.03	N/m	218.33	Calculated Property
γ	0.03	N/m	261.36	Calculated Property
γ	0.02	N/m	304.39	Calculated Property
γ	0.02	N/m	347.42	Calculated Property
γ	0.01	N/m	390.46	Calculated Property
γ	0.01	N/m	433.49	Calculated Property
γ	0.01	N/m	476.52	Calculated Property
γ	0.00	N/m	519.55	Calculated Property
γ	8.58e-04	N/m	562.58	Calculated Property

Property	Value	Unit	Temperature (K)	Source
λgas	[0.00; 0.07]	W/m×K	[175.30; 1000.00]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A·T^B / (1 + C/T + D/T²) Y is λgas in W/m×K, T in K
Coefficient A			3.60640e-03
Coefficient B			5.79180e-01
Coefficient C			1.40190e+03
Coefficient D			2.87150e+05
Temperature range, min.			175.30
Temperature range, max.			1000.00
λgas	0.00	W/m×K	175.30	Calculated Property
λgas	0.01	W/m×K	266.93	Calculated Property
λgas	0.02	W/m×K	358.57	Calculated Property
λgas	0.02	W/m×K	450.20	Calculated Property
λgas	0.03	W/m×K	541.83	Calculated Property
λgas	0.04	W/m×K	633.47	Calculated Property
λgas	0.05	W/m×K	725.10	Calculated Property
λgas	0.06	W/m×K	816.73	Calculated Property
λgas	0.06	W/m×K	908.37	Calculated Property
λgas	0.07	W/m×K	1000.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
λliquid	[0.16; 0.08]	W/m×K	[175.30; 523.15]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A + exp(B/T + C + D·T + E·T²) Y is λliquid in W/m×K, T in K
Coefficient A			-6.71280e-02
Coefficient B			2.47030e+00
Coefficient C			-1.32910e+00
Coefficient D			-1.00110e-03
Coefficient E			-2.57420e-07
Temperature range, min.			175.30
Temperature range, max.			523.15
λliquid	0.16	W/m×K	175.30	Calculated Property
λliquid	0.15	W/m×K	213.95	Calculated Property
λliquid	0.14	W/m×K	252.60	Calculated Property
λliquid	0.13	W/m×K	291.25	Calculated Property
λliquid	0.12	W/m×K	329.90	Calculated Property
λliquid	0.11	W/m×K	368.55	Calculated Property
λliquid	0.10	W/m×K	407.20	Calculated Property
λliquid	0.09	W/m×K	445.85	Calculated Property
λliquid	0.09	W/m×K	484.50	Calculated Property
λliquid	0.08	W/m×K	523.15	Calculated Property

Similar Compounds

Find more compounds similar to n-Butyl ether.

Mixtures

• n-Butyl ether + 1-Butanol
• n-Butyl ether + Pentane, 2,2,4-trimethyl-
• n-Butyl ether + 1-Butanol + Pentane, 2,2,4-trimethyl-
• 1H-Imidazole, 1-methyl- + n-Butyl ether
• n-Butyl ether + Mercury
• n-Butyl ether + Butane, 2,3-dimethyl-
• n-Butyl ether + Butane, 2,2-dimethyl-
• Toluene + n-Butyl ether
• n-Butyl ether + Cyclohexane
• Toluene + n-Butyl ether + Cyclohexane
• Benzene + n-Butyl ether
• Benzene + n-Butyl ether + 1-Butanol
• Formamide, N,N-dimethyl- + n-Butyl ether
• 1-Propanol + n-Butyl ether
• n-Butyl ether + 1-Hexanol
• 2-Propanol + n-Butyl ether
• Hexane, tetradecafluoro- + n-Butyl ether
• n-Butyl ether + Furan, tetrahydro-2-methyl-
• Acetonitrile + n-Butyl ether
• n-Butyl ether + Methane, nitro-

Find more mixtures with n-Butyl ether.

Sources

• Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) ChEDL chemicals 1.5.2, from Bradley, J.-C.; Williams, A.; Lang, A. Jean-Claude Bradley Open Melting Point Dataset. Figshare, 2014 (CC0).
• IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 ChEDL chemicals 1.5.2, from Kudchadker, A. P.; Ambrose, D.; Tsonopoulos, C. Vapor-Liquid Critical Properties of Elements and Compounds. 7. Oxygen Compounds Other Than Alkanols and Cycloalkanols. J. Chem. Eng. Data 2001, 46, 457-479.
• Jasper (1972), surface tension of pure liquid compounds ChEDL chemicals 1.5.2, from Jasper, J. J. The Surface Tension of Pure Liquid Compounds. J. Phys. Chem. Ref. Data 1972, 1, 841-1010 (as transcribed in Lange's Handbook).
• PSRK revision IV (2005), critical constants and acentric factors of 1000 components ChEDL chemicals 1.5.2, from Horstmann, S.; Jabłoniec, A.; Krafczyk, J.; Fischer, K.; Gmehling, J. PSRK Group Contribution Equation of State: Comprehensive Revision and Extension IV, Including Critical Constants and α-Function Parameters for 1000 Components. Fluid Phase Equilib. 2005, 227, 157-164.
• ChemSep v8.3 pure component data Converted from ChemSep v8.3 pure component data, H. Kooijman and R. Taylor (2021, 2022), Artistic License 2.0; see how the values differ.
• Kinematic Viscosities for Ether + Alkane Mixtures: Experimental Results and UNIFAC-VISCO Parameters
• CO2 Solubility in Physicochemical Absorbent: Dibutyl Ether/N-Methylethanolamine/Ethanol
• (Solid + liquid) phase equilibria of binary mixtures containing N-methyl-2-pyrrolidinone and ethers at atmospheric pressure
• Thermodynamics of binary mixtures containing N-methyl-2-pyrrolidinone VLE measurements for systems with ethers Comparison with the Mod. UNIFAC (Do) and DISQUAC models Predictions for VLE, GE m, HEm and SLE?
• Experimental liquid liquid equilibria of 1-methylimidazole with hydrocarbons and ethers
• Experimental investigation of the vapour-liquid equilibrium of binary and ternary mixtures containing dibutyl ether (DBE), cyclohexane and toluene at 313.15 K
• Isobaric vapor-liquid equilibria for the binary systems 1-propyl alcohol + dipropyl ether and 1-butyl alcohol + dibutyl ether at 20 and 101.3 kPa
• Isothermal vapor liquid equilibrium at 333.15K and excess volumes and molar refractivity deviation at 298.15K for the ternary system di-butyl ether (1) + ethanol (2) + toluene (3) and its binary subsystems
• Isothermal vapour liquid equilibria and excess molar enthalpies of hex-2-yne + methyl butyl ether and hex-3-yne + dibutyl ether mixtures
• Thermodynamic study of perfluorohexane + ether mixtures VLE, LLE, and HE
• Excess enthalpies of ether + alcohol + hydrocarbon mixtures: Binary and ternary mixtures containing dibutyl ether (DBE), 1-butanol and benzene at 298.15K and 313.15K
• Excess enthalpies of oxygenated compounds + hydrocarbon mixtures: Binary and ternary mixtures containing dibutyl ether (DBE), 1-butanol and 2,2,4-trimethylpentane at 298.15 K
• Ether + alcohol + hydrocarbon mixtures in fuels and bio-fuels: Excess enthalpies of binary mixtures containing dibutyl ether (DBE) or 1-butanol and 1-hexene or methylcyclohexane or toluene or cyclohexane or 2,2,4-trimethylpentane at 298.15K and 313.15K
• Phase equilibrium properties of the ternary mixture dibutyl ether + toluene + heptane at 313.15 K
• Liquid-liquid equilibrium in binary systems of isomeric C8 aliphatic monoethers with nitromethane
• (p, VE, T) Measurements of mixtures (DBE + alcohol) at temperaturesfrom (293.15 to 353.15) K and at pressures up to 140 MPa
• High-pressure vapor-liquid equilibria of the second generation biofuel blends (2-methylfuran + iso-octane) and (2-methyltetrahydrofuran + di-n-butyl ether): Experiments and PCP-SAFT modeling
• Activity coefficients at infinite dilution of organic solvents and water in 1-butyl-3-methylimidazolium dicyanamide. A literature review of hexane/hex-1-ene separation
• Experimental and modeled volumetric behavior of linear and branched ethers
• Measurement of thermal diffusivity and speed of sound of dibutyl ether from 303.15 K to 673.15 K and up to 7.5 MPa
• High selective water/butan-1-ol separation on investigation of limiting activity coefficients with [P8,8,8,8][[NTf2] ionic liquid
• Separation of binary mixtures based on limiting activity coefficients data using specific ammonium-based ionic liquid and modelling of thermodynamic functions
• Thermodynamics and activity coefficients at infinite dilution for organic solutes in the ionic liquid 1-butyl-1-methylpyrrolidinium dicyanamide
• Isobaric vapor-liquid equilibrium, density and speed of sound of binary mixtures 2,2,4-trimethylpentane + 1-butanol or dibutyl ether (DBE) at 101.3 kPa
• New ionic liquid [P4,4,4,4][NTf2] in bio-butanol extraction on investigation of limiting activity coefficients
• The behavior of mercury in water, alcohols, monoethylene glycol and triethylene glycol II. Elemental mercury solubility in alcohols, ethers and acetone; gas plant mercury distribution; and speciation in monoethylene glycol solution
• Ammonium ionic liquids in extraction of bio-butan-1-ol from water phase using activity coefficients at infinite dilution
• Measurements of activity coefficients at infinite dilution for organic solutes in two quaternary ammonium-based ionic liquids [DDA][ClO4] and [DDA][BF4]
• Density of biofuel mixtures (Dibutyl ether + Heptane) at temperatures from (298.15-393.15) K and at pressures up to 140 MPa: Experimental data and PC-SAFT modeling
• Volumetric properties of (N,N-dimethylformamide + aliphatic diethers) at Temperatures ranging from (298.15 to 358.15) K
• (Liquid + liquid) equilibrium of (dibutyl ether + methanol + water) at different temperatures
• (Liquid + liquid) phase equilibria of 1-alkyl-3-methylimidazolium methylsulfate with alcohols, or ethers, or ketones
• Volumetric properties of binary mixtures of ethers and acetonitrile: Experimental results and application of the Prigogine Flory Patterson theory
• Thermodynamics of (1-alkanol + linear monoether) systems
• Activity coefficients at infinite dilution measurements for organic solutes and water in the ionic liquid 4-methyl-N-butyl-pyridinium bis(trifluoromethylsulfonyl)-imide
• Molar excess enthalpies at T = 298.15 K for (1-alkanol + dibutylether) systems
• Excess enthalpies of binary and ternary mixtures containing dibutyl ether (DBE), 1-butanol, and heptane at T = 298.15 K and 313.15 K
• Measurements of activity coefficients at infinite dilution of organic solutes and water in 1-propyl-1-methylpiperidinium bis{(trifluoromethyl)sulfonyl}imide ionic liquid using g.l.c.
• Measurements of activity coefficients at infinite dilution of organic compounds and water in isoquinolinium-based ionic liquid [C8iQuin][NTf2] using GLC
• Activity coefficients at infinite dilution measurements for organic solutes and water in the ionic liquid 1-ethyl-3-methylimidazolium tetracyanoborate
• Excess molar enthalpies of ternary mixtures (dibutyl ether or dipropyl ether + 2,2-dimethylbutane + 2,3-dimethylbutane) at the temperature 298.15 K
• Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(3-hydroxypropyl)pyridinium bis(trifluoromethylsulfonyl)-amide
• Liquid density of biofuel mixtures: (Dibutyl ether + 1-butanol) system at pressures up to 140 MPa and temperatures from (293.15 to 393.15) K
• Thermodynamics and activity coefficients at infinite dilution measurements for organic solutes and water in the ionic liquid 1-butyl-1-methylpyrrolidinium tetracyanoborate
• Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 4-(2-methoxyethyl)-4-methylmorpholinium bis(trifluoromethylsulfonyl)-amide
• Measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-hexyl-3-methylimidazolium tetracyanoborate
• Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)-1-methylpiperidinium bis(trifluoromethylsulfonyl)-amide
• Measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-ethyl-3-methylimidazolium methanesulfonate
• Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)-1-methylpyrrolidinium bis(trifluoromethylsulfonyl)-amide
• Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 4-(2-methoxyethyl)-4-methylmorpholinium trifluorotris(perfluoroethyl)phosphate
• Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)- 1-methylpiperidinium trifluorotris(perfluoroethyl)phosphate
• Physicochemical properties and activity coefficients at infinite dilution for organic solutes and water in a novel bicyclic guanidinium superbase-derived protic ionic liquid
• Experimental and theoretical study on infinite dilution activity coefficients of various solutes in piperidinium ionic liquids
• Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)- 1-methylpyrrolidinium trifluorotris(perfluoroethyl)phosphate
• Measurements of activity coefficients at infinite dilution for organic solutes and water in N-hexylisoquinolinium thiocyanate, [HiQuin][SCN] using GLC
• Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-hydroxyethyl)- 3-methylimidazolium trifluorotris(perfluoroethyl)phosphate
• Measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-butyl-1-methylpyrrolidinium tricyanomethanide
• Thermodynamics and activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-butyl-1-methylmorpholinium tricyanomethanide
• The study of activity coefficients at infinite dilution for organic solutes and water in 1-butyl-4-methylpyridinium dicyanamide, [B4MPy][DCA] using GLC
• Thermodynamics and activity coefficients at infinite dilution for organic solutes, water and diols in the ionic liquid choline bis(trifluoromethylsulfonyl)imide
• (Liquid + liquid) equilibrium in binary systems of isomeric C8 aliphatic monoethers with acetonitrile and its interpretation by the COSMO-SAC model
• Excess enthalpies of ternary mixtures of (oxygenated additives + aromatic hydrocarbon) mixtures in fuels and bio-fuels: (Dibutyl-ether + 1-propanol + benzene), or toluene, at T = (298.15 and 313.15) K
• Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 4-(3-hydroxypropyl)-4-methylmorpholinium bis(trifluoromethylsulfonyl)-amide
• Excess molar enthalpies of the binary systems: (Dibutyl ether + isomers of pentanol) at T = (298.15 and 308.15) K
• Activity coefficients at infinite dilution for organic solutes and water in 1-ethyl-1-methylpyrrolidinium lactate
• Activity coefficients at infinite dilution, physicochemical and thermodynamic properties for organic solutes and water in the ionic liquid ethyl-dimethyl-(2-methoxyethyl)ammonium trifluorotris-(perfluoroethyl)phosphate
• Ternary (liquid + liquid) equilibria for the extraction of ethanol, or 2-propanol from aqueous solutions with 1,1'-oxybis(butane) at different temperatures
• A 1-alkylcyanopyridinium-based ionic liquid in the separation processes
• Thermodynamics and selectivity of separation based on activity coefficients at infinite dilution of various solutes in 1-allyl-3-methylimidazolium bis{(trifluoromethyl)sulfonyl}imide ionic liquid
• Separation of aliphatic from aromatic hydrocarbons and sulphur compounds from fuel based on measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid N,N-diethyl-N-methyl-N-(2-methoxy-ethyl)ammonium bis(trifluoromethylsulfonyl)imide
• Thermodynamics and limiting activity coefficients measurements for organic solutes and water in the ionic liquid 1-dodecyl-3-methylimidzolium bis(trifluoromethylsulfonyl) imide
• Excess enthalpies of ternary mixtures of (oxygenated additives + cycloalkane) in fuels and bio-fuels: (dibutyl ether + 1-propanol + cyclohexane), or methylcyclohexane, at T = (298.15 and 313.15) K
• Separation of binary mixtures hexane/hex-1-ene, cyclohexane/cyclohexene and ethylbenzene/styrene based on limiting activity coefficients
• Separation of water/butan-1-ol based on activity coefficients at infinite dilution in 1,3-didecyl-2-methylimidazolium dicyanamide ionic liquid
• Separation of binary mixtures hexane/hex-1-ene, cyclohexane/cyclohexene and ethylbenzene/styrene based on gamma infinity data measurements
• Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid trihexyl-tetradecyl-phosphonium tricyanomethanide
• Thermodynamic study of molecular interaction-selectivity in separation processes based on limiting activity coefficients
• The use of ionic liquids for separation of binary hydrocarbons mixtures based on gamma infinity data measurements
• Experimental density and PC-SAFT modeling of biofuel mixtures (DBE + 1-Heptanol) at temperatures from (298.15 to 393.15) K and at pressures up to 140 MPa
• Density, viscosity, and speed of sound of binary liquid mixtures of vinyl acetate with butyl vinyl ether, diisopropyl ether, anisole and dibutyl ether
• DIELECTRIC AND REFRACTIVE INDEX MEASUREMENTS FOR THE SYSTEMS 1-PENTANOL + OCTANE, OR + DIBUTYL ETHER OR FOR DIBUTYL ETHER + OCTANE AT DIFFERENT TEMPERATURES
• Examination of hydrogen-bonding interactions between dissolved solutes and alkylbenzene solvents based on Abraham model correlations derived from measured enthalpies of solvation
• Effect of halogen substitution on the enthalpies of solvation and hydrogen bonding of organic solutes in chlorobenzene and 1,2-dichlorobenzene derived using multi-parameter correlations
• Thermodynamic of dissolution and hydrogen bond of the pyrrole, N-methylpyrrole with proton acceptors
• Excess Enthalpies in Binary Systems of Isomeric C8 Aliphatic Monoethers with Acetonitrile and Their Description by the COSMO-SAC Model
• Activity Coefficients at Infinite Dilution of Organic Solutes and Water in Tributylethylphosphonium Diethylphosphate Using Gas Liquid Chromatography: Thermodynamic Properties of Mixtures Containing Ionic Liquids
• Vapor Liquid Equilibrium and Excess Enthalpy Data for Systems Containing N,N-Dimethylacetamide
• (r, VE, T) Measurements of the Ternary Mixture (Dibutyl Ether + 1-Heptanol + Heptane) at Temperatures up to 393.15 K and Pressures up to 140 MPa and Modeling Using the Peng-Robinson and PC-SAFT Equations of State
• Solubility of Imidazoles in Ethers
• Solubility of -Carotene in Binary Solvents Formed by Some Hydrocarbons with Dibutyl Ether and 1,2-Dimethoxyethane
• Solubilities of Some Long-Chain n-Alkanes in Dipropyl Ether, Dibutyl Ether, 1-Chlorobutane, and 1-Chlorooctane as Functions of Temperature
• Densities, Excess Molar Volumes at T = (298.15 to 313.15) K, Speeds of Sound, Excess Isentropic Compressibilities, Relative Permittivities and Deviations in Molar Polarizations at T = (298.15 and 308.15) K for Methyl Methacrylate + 2-Butoxyethanol or + Dibutyl Ether + Benzene, + Toluene and + p-Xylene
• Excess Molar Enthalpies and Hydrogen Bonding in Binary Mixtures Containing Ethers and Benzyl Alcohol at 308.15 K and Atmospheric Pressure
• Isobaric Vapor-Liquid Equilibria of the Ternary System Dibutyl Ether + 1-Pentanol + Nonane
• Vapor-Liquid Equilibrium Data, Excess Enthalpy Data, and Azeotropic Data for the Binary System Dibutyl Ether + o-Xylene
• Activity Coefficients at Infinite Dilution Measurements for Organic Solutes and Water in the Ionic Liquid 1-Butyl-3-methyl-pyridinium Trifluoromethanesulfonate
• Determination of Activity Coefficients at Infinite Dilution of 35 Solutes in the Ionic Liquid, 1-Butyl-3-methylimidazolium Tosylate, Using Gas-Liquid Chromatography
• Excess Molar Enthalpies of Dipropyl Ether + Dibutyl Ether + (1-Hexene or Tetrahydrofuran) at 298.15 K
• Measurements of Activity Coefficients at Infinite Dilution for Organic Solutes and Water in the Ionic Liquid 1-Butyl-1-methylpiperydinium Thiocyanate
• Liquid Density of Biofuel Additives: 1-Butoxybutane at Pressures up to 140 MPa and from (293.15 to 393.15) K
• Activity Coefficients at Infinite Dilution by GLC in Alkanediamines as Stationary Phases
• Biomass-Derived Platform Chemicals: Thermodynamic Studies on the Extraction of 5-Hydroxymethylfurfural from Ionic Liquids
• Measurements and Correlations of Liquid.Liquid Equilibria for Water + Ethanol + 1,1'-Oxybis(butane) + Methylbenzene or Heptane Mixtures at 298.15 K
• Oxygenated Compounds + Hydrocarbon Mixtures in Fuels and Biofuels: Excess Enthalpies of Ternary Mixtures Containing 1-Butoxybutane + Propan-1-ol +1-Hex-1-ene, or Heptane, or 2,2,4-Trimethylpentane at (298.15 and 313.15) K
• Isothermal Vapor-Liquid Equilibrium at 333.15 K, Density, and Refractive Index at 298.15 K for the Ternary Mixture of Dibutyl Ether + Ethanol + Benzene and Binary Subsystems
• Densities, Excess Molar Volumes, Speeds of Sound at (293.15, 298.15, and 303.15) K and Isentropic Compressibilities at 298.15 K for 1-Butanol, 1-Pentanol, or 1-Hexanol + Dibutylether Systems
• Phase Equilibria of (1-Ethyl-3-methylimidazolium Ethylsulfate + Hydrocarbon, + Ketone, and + Ether) Binary Systems
• Phase Equilibrium Properties of Binary and Ternary Mixtures Containing Dibutyl Ether, Cyclohexane, and Heptane or 1-Hexene at T ) 313.15 K
• Thermodynamics of Mixtures Containing Alkoxyethanols. Part XXVI. Densities, Excess Molar Volumes, Speeds of Sound at (293.15, 298.15, and 303.15) K, and Isentropic or Isothermal Compressibilities at 298.15 K for 2-Methoxyethanol + Alkoxyethanol or 2-Propoxyethanol + Dibutylether Systems
• Binary Liquid-Liquid Equilibrium (LLE) for Dibutyl Ether (DBE) + Water from (288.15 to 318.15) K and Ternary LLE for Systems of DBE + C1 !less thanless than C4 Alcohols + Water at 298.15 K
• Viscosity and Density Measurements of Diisopropyl Ether and Dibutyl Ether at Different Temperatures and Pressures
• Excess Enthalpies of Binary and Ternary Mixtures Containing Dibutyl Ether, Cyclohexane, and 1-Butanol at 298.15 K
• Measurement and Correlation of Vapor-Liquid Equilibrium for the Carbon Dioxide + 1-Butoxy Butane System
• Isothermal Vapor-Liquid Equilibrium at 333.15 K and Excess Volumes and Molar Refractivity Deviation at 298.15 K for Binary System Dibutyl Ether (DBE) + 2,2,4-Trimethylpentane and for Ternary System DBE + Ethanol + 2,2,4-Trimethylpentane
• Thermal Conductivity of Liquid Diethyl Ether, Diisopropyl Ether, and Di-n-butyl Ether from (233 to 373) K at Pressures up to 30 MPa
• Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
• Activity Coefficients at Infinite Dilution Measurements for Organic Solutes and Water in the Ionic Liquid 1-Hexyl-3-methylimidazolium Thiocyanate
• Joback Method
• KDB
• Aqueous Solubility Prediction Method
• Estimated Solubility Method
• McGowan Method
• NIST Webbook
• NCMS SOLV-DB
• The Yaws Handbook of Vapor Pressure

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