Chemical Properties of Diisopropyl ether (CAS 108-20-3)

InChI

InChI=1S/C6H14O/c1-5(2)7-6(3)4/h5-6H,1-4H3

InChI Key

ZAFNJMIOTHYJRJ-UHFFFAOYSA-N

Formula

C6H14O

SMILES

CC(C)OC(C)C

Molecular Weight¹

102.17

CAS

108-20-3

Other Names

• (iso-C3H7)2O
• 1,1'-Dimethyldiethyl ether
• 1-methyl-1-(1-methylethoxy)ethane
• 2,2'-OXYBIS-PROPANE
• 2,2'-Oxybispropane
• 2,4-dimethyl-3-oxapentane
• 2-isopropoxypropane
• Bis(isopropyl) ether
• Diiospropyl ether
• Diisopropyl oxide
• Ether isopropylique
• Ether, isopropyl
• Izopropylowy eter
• Propane, 2,2'-oxybis-
• UN 1159
• bis(1-methylethyl) ether
• isopropyl 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).
• C_sat : Molar heat capacity at saturation pressure (J/mol×K).
• μ : Dipole Moment (debye).
• η : Dynamic viscosity (Pa×s).
• ε_r : Dielectric Constant (Relative permittivity).
• LFL : Lower Flammability Limit (% in Air).
• UFL : Upper Flammability Limit (% in Air).
• T_flash,cc : Flash Point (Closed Cup Method) (K).
• T_flash,oc : Flash Point (Open 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_fusH : Enthalpy of fusion at a given temperature (kJ/mol).
• Δ_vapH° : Enthalpy of vaporization at standard conditions (kJ/mol).
• Δ_vapH : Enthalpy of vaporization at a given temperature (kJ/mol).
• IE : Ionization energy (eV).
• 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.
• 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).
• 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	[0.3310; 0.3400]
ω	0.3400		PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
ω	0.3387		ChemSep v8.3 pure component data Compiled value
ω	0.3310		KDB
PAff	855.50	kJ/mol	NIST
Tig	[716.15; 716.48]	K
Tig	716.48	K	KDB
Tig	716.15	K	NCMS SOLV-DB
BasG	828.10	kJ/mol	NIST
ΔcH°liquid	-4010.40 ± 1.30	kJ/mol	NIST
μ	[1.13; 1.20]	debye
μ	1.13	debye	ChemSep v8.3 pure component data Compiled value
μ	1.20	debye	KDB
εr	3.88		NCMS SOLV-DB
LFL	1.40	% in Air	KDB
UFL	7.90	% in Air	KDB
Tflash,cc	[245.15; 247.04]	K
Tflash,cc	247.04	K	KDB
Tflash,cc	245.15	K	NCMS SOLV-DB
Tflash,oc	245.37	K	KDB
ΔfG°	[-124.80; -122.00]	kJ/mol
ΔfG°	-124.80	kJ/mol	ChemSep v8.3 pure component data Compiled value
ΔfG°	-122.00	kJ/mol	KDB
ΔfH°gas	[-319.00; -318.00]	kJ/mol
ΔfH°gas	-318.99	kJ/mol	ChemSep v8.3 pure component data Compiled value
ΔfH°gas	-319.00	kJ/mol	KDB
ΔfH°gas	-318.00 ± 3.00	kJ/mol	NIST
ΔfH°liquid	-351.50 ± 1.40	kJ/mol	NIST
ΔfusH°	5.44	kJ/mol	Joback Calculated Property
ΔvapH°	[32.01; 32.70]	kJ/mol
ΔvapH°	32.01	kJ/mol	NCMS SOLV-DB
ΔvapH°	32.26	kJ/mol	NIST
ΔvapH°	32.70 ± 0.50	kJ/mol	NIST
ΔvapH°	32.12	kJ/mol	NIST
ΔvapH°	32.10 ± 0.10	kJ/mol	NIST
IE	[9.16; 9.32]	eV
IE	9.20 ± 0.05	eV	NIST
IE	9.16 ± 0.05	eV	NIST
IE	9.20 ± 0.05	eV	NIST
IE	9.32	eV	NIST
log10WS	[-1.10; -1.10]
log10WS	-1.10		Aq. Solubility Prediction
log10WS	-1.10		Estimated Solubility
logPoct/wat	1.488		NCMS SOLV-DB
McVol	101.270	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	[%!d(float64=1); %!d(float64=1)]
NFPA Safety	1		KDB
NFPA Safety	1		NCMS SOLV-DB
Pc	[2832.00; 2880.00]	kPa
Pc	2832.00	kPa	IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value
Pc	2877.63	kPa	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Pc	2880.00	kPa	ChemSep v8.3 pure component data Compiled value
Pc	2832.00	kPa	KDB
Pc	2832.00 ± 6.00	kPa	NIST
Pc	2875.10 ± 13.78	kPa	NIST
pKa	-4.30		NCMS SOLV-DB
Ptriple	6.86e-03	kPa	ChemSep v8.3 pure component data Compiled value
Inp	[563.00; 624.00]
Inp	593.00		NIST
Inp	590.00		NIST
Inp	594.00		NIST
Inp	Outlier 624.00		NIST
Inp	563.00		NIST
Inp	564.00		NIST
Inp	570.00		NIST
Inp	565.00		NIST
Inp	568.00		NIST
Inp	570.00		NIST
Inp	602.00		NIST
Inp	602.00		NIST
Inp	590.00		NIST
Inp	568.00		NIST
Inp	598.00		NIST
Inp	596.00		NIST
Inp	598.00		NIST
Inp	594.00		NIST
Inp	603.00		NIST
Inp	594.00		NIST
Inp	594.00		NIST
Inp	593.00		NIST
Inp	564.00		NIST
Ip	[649.00; 682.00]
Ip	652.00		NIST
Ip	Outlier 679.00		NIST
Ip	Outlier 682.00		NIST
Ip	670.00		NIST
Ip	667.00		NIST
Ip	659.00		NIST
Ip	658.30		NIST
Ip	657.00		NIST
Ip	655.40		NIST
Ip	651.00		NIST
Ip	649.00		NIST
Ip	662.00		NIST
Ip	657.00		NIST
Ip	658.00		NIST
Ip	659.00		NIST
Ip	651.00		NIST
Ip	649.00		NIST
S°liquid	[294.60; 304.60]	J/mol×K
S°liquid	304.60	J/mol×K	NIST
S°liquid	294.60	J/mol×K	NIST
Tboil	[340.70; 342.20]	K
Tboil	341.53	K	Vapor liquid equilibria for binary and ternary mixtures of diisopropyl ether, ethanol, and 2,2,4-trimethylpentane at 101.3 kPa
Tboil	341.35	K	Quaternary phase equilibrium of water-carboxylic acid mixture (formic-propionic acid or acetic-propionic acid)-solvent liquid systems at 298.15 K
Tboil	341.55	K	(Liquid + liquid) equilibria of (water + propionic acid + dipropyl ether or diisopropyl ether) at T = 298.2 K
Tboil	341.40	K	Isobaric (vapour + liquid + liquid) equilibrium data for (di-n-propyl ether + n-propyl alcohol + water) and (diisopropyl ether + isopropyl alcohol + water) systems at 100 kPa
Tboil	341.77	K	Vapour-liquid equilibrium and extractive distillation for separation of azeotrope isopropyl alcohol and diisopropyl ether
Tboil	341.72	K	Separation of the mixture (isopropyl alcohol + diisopropyl ether + n-propanol): Entrainer selection, interaction exploration and vapour-liquid equilibrium measurements
Tboil	341.35	K	Excess volumes, densities, speeds of sound and viscosities for the binary systems of diisopropyl ether with hydrocarbons at 303.15K
Tboil	341.35	K	Vapor-Liquid Equilibria for the Binary Systems of Dimethoxymethane with Some Fuel Oxygenates
Tboil	341.45	K	ChemSep v8.3 pure component data Compiled value
Tboil	341.66	K	KDB
Tboil	341.66	K	NCMS SOLV-DB
Tboil	341.60 ± 0.30	K	NIST
Tboil	341.40 ± 0.30	K	NIST
Tboil	341.63 ± 0.20	K	NIST
Tboil	341.20	K	NIST
Tboil	341.50	K	NIST
Tboil	341.69 ± 0.12	K	NIST
Tboil	Outlier 340.70 ± 0.50	K	NIST
Tboil	341.65	K	NIST
Tboil	341.15 ± 0.30	K	NIST
Tboil	Outlier 340.80 ± 0.60	K	NIST
Tboil	341.55 ± 1.00	K	NIST
Tboil	341.60 ± 2.00	K	NIST
Tboil	341.42 ± 0.07	K	NIST
Tboil	341.15 ± 1.00	K	NIST
Tboil	Outlier 342.20 ± 0.20	K	NIST
Tc	[499.60; 500.32]	K
Tc	500.30	K	IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value
Tc	500.00	K	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Tc	500.05	K	ChemSep v8.3 pure component data Compiled value
Tc	500.32	K	KDB
Tc	500.30	K	NIST
Tc	499.60 ± 0.30	K	NIST
Tc	499.60 ± 0.30	K	NIST
Tc	500.32 ± 0.10	K	NIST
Tc	500.10 ± 0.30	K	NIST
Tfus	[186.30; 187.65]	K
Tfus	186.75	K	Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value
Tfus	187.65	K	ChemSep v8.3 pure component data Compiled value
Tfus	186.30	K	KDB
Tfus	186.75	K	Aq. Solubility Prediction
Tfus	187.65	K	NCMS SOLV-DB
Tfus	187.65	K	NIST
Tfus	187.26 ± 0.05	K	NIST
Ttriple	[186.30; 187.77]	K
Ttriple	187.65	K	ChemSep v8.3 pure component data Compiled value
Ttriple	187.77	K	KDB
Ttriple	187.77 ± 0.06	K	NIST
Ttriple	186.30 ± 0.20	K	NIST
Ttriple	187.77 ± 0.06	K	NIST
Ttriple	186.30 ± 0.20	K	NIST
UQi	4.09		ChemSep v8.3 pure component data Compiled value
URi	4.74		ChemSep v8.3 pure component data Compiled value
Vc	[0.386; 0.386]	m3/kmol
Vc	0.386	m3/kmol	IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value
Vc	0.386	m3/kmol	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Vc	0.386	m3/kmol	ChemSep v8.3 pure component data Compiled value
Vc	0.386	m3/kmol	KDB
Vc	0.386 ± 0.005	m3/kmol	NIST
Zc	[0.2627820; 0.2670000]
Zc	0.2630000		IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value
Zc	0.2670000		ChemSep v8.3 pure component data Compiled value
Zc	0.2627820		KDB
Zra	0.27		ChemSep v8.3 pure component data Compiled value

Temperature Dependent Properties

Property	Value	Unit	Temperature (K)	Source
Cp,gas	[182.47; 219.11]	J/mol×K	[360.04; 449.98]
Cp,gas	182.47	J/mol×K	360.04	NIST
Cp,gas	191.01	J/mol×K	380.01	NIST
Cp,gas	199.33	J/mol×K	399.98	NIST
Cp,gas	209.60	J/mol×K	424.98	NIST
Cp,gas	219.11	J/mol×K	449.98	NIST
Cp,liquid	[211.50; 232.04]	J/mol×K	[290.50; 339.89]
Cp,liquid	211.50	J/mol×K	290.50	Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
Cp,liquid	216.31	J/mol×K	293.10	NIST
Cp,liquid	213.44	J/mol×K	295.44	Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
Cp,liquid	216.74	J/mol×K	298.15	NIST
Cp,liquid	216.10	J/mol×K	298.15	NIST
Cp,liquid	215.28	J/mol×K	300.38	Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
Cp,liquid	217.33	J/mol×K	305.32	Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
Cp,liquid	219.37	J/mol×K	310.26	Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
Cp,liquid	221.41	J/mol×K	315.20	Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
Cp,liquid	223.46	J/mol×K	320.13	Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
Cp,liquid	225.50	J/mol×K	325.07	Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
Cp,liquid	227.65	J/mol×K	330.01	Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
Cp,liquid	229.89	J/mol×K	334.95	Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
Cp,liquid	232.04	J/mol×K	339.89	Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
Csat	[207.70; 232.20]	J/mol×K	[277.17; 337.14]
Csat	207.70	J/mol×K	277.17	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	208.50	J/mol×K	279.16	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	209.40	J/mol×K	281.15	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	210.40	J/mol×K	283.14	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	211.30	J/mol×K	285.16	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	212.20	J/mol×K	287.16	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	213.10	J/mol×K	289.15	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	214.00	J/mol×K	291.17	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	214.80	J/mol×K	293.15	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	215.50	J/mol×K	295.16	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	216.30	J/mol×K	297.16	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	217.20	J/mol×K	299.16	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	218.00	J/mol×K	301.16	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	218.70	J/mol×K	303.15	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	219.50	J/mol×K	305.14	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	220.30	J/mol×K	307.14	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	221.00	J/mol×K	309.16	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	222.00	J/mol×K	311.15	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	222.70	J/mol×K	313.15	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	223.60	J/mol×K	315.15	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	224.40	J/mol×K	317.17	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	225.10	J/mol×K	319.16	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	225.90	J/mol×K	321.15	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	226.70	J/mol×K	323.14	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	227.40	J/mol×K	325.14	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	228.30	J/mol×K	327.13	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	229.00	J/mol×K	329.16	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	229.90	J/mol×K	331.15	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	230.50	J/mol×K	333.15	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	231.40	J/mol×K	335.14	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
Csat	232.20	J/mol×K	337.14	Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
η	[0.0002723; 0.0003790]	Pa×s	[283.15; 313.15]
η	0.0003646	Pa×s	283.15	Viscosities of Binary Mixtures Containing Isomeric Chlorobutanes and Diisopropylether: Experimental and Predicted Values
η	0.0003486	Pa×s	288.15	Viscosities of Binary Mixtures Containing Isomeric Chlorobutanes and Diisopropylether: Experimental and Predicted Values
η	0.0003340	Pa×s	293.15	Viscosities of Binary Mixtures Containing Isomeric Chlorobutanes and Diisopropylether: Experimental and Predicted Values
η	0.0003178	Pa×s	298.15	Viscosities of Binary Mixtures Containing Isomeric Chlorobutanes and Diisopropylether: Experimental and Predicted Values
η	0.0003790	Pa×s	298.15	NCMS SOLV-DB
η	0.0003001	Pa×s	303.15	Viscosities of Binary Mixtures Containing Isomeric Chlorobutanes and Diisopropylether: Experimental and Predicted Values
η	0.0002857	Pa×s	308.15	Viscosities of Binary Mixtures Containing Isomeric Chlorobutanes and Diisopropylether: Experimental and Predicted Values
η	0.0002723	Pa×s	313.15	Viscosities of Binary Mixtures Containing Isomeric Chlorobutanes and Diisopropylether: Experimental and Predicted Values
ΔfusH	[11.03; 12.05]	kJ/mol	[186.30; 187.80]
ΔfusH	11.03	kJ/mol	186.30	NIST
ΔfusH	11.03	kJ/mol	186.30	NIST
ΔfusH	12.04	kJ/mol	187.77	NIST
ΔfusH	12.04	kJ/mol	187.77	NIST
ΔfusH	12.05	kJ/mol	187.80	NIST
ΔfusH	12.05	kJ/mol	187.80	NIST
ΔfusH	12.05	kJ/mol	187.80	NIST
ΔfusH	12.05	kJ/mol	187.80	NIST
ΔvapH	[29.10; 33.20]	kJ/mol	[300.50; 468.00]
ΔvapH	33.00	kJ/mol	300.50	NIST
ΔvapH	33.20	kJ/mol	303.00	NIST
ΔvapH	32.10	kJ/mol	319.00	NIST
ΔvapH	32.60	kJ/mol	324.50	NIST
ΔvapH	29.20	kJ/mol	324.50	NIST
ΔvapH	31.10	kJ/mol	328.00	NIST
ΔvapH	30.10	kJ/mol	335.50	NIST
ΔvapH	29.33	kJ/mol	341.40	KDB
ΔvapH	29.10	kJ/mol	341.50	NIST
ΔvapH	29.90	kJ/mol	400.00	NIST
ΔvapH	29.50	kJ/mol	468.00	NIST
ν	[0.0000004; 0.0000005]	m2/s	[283.15; 313.15]
ν	0.0000005	m2/s	283.15	Kinematic Viscosities for Ether + Alkane Mixtures: Experimental Results and UNIFAC-VISCO Parameters
ν	0.0000004	m2/s	298.15	Kinematic Viscosities for Ether + Alkane Mixtures: Experimental Results and UNIFAC-VISCO Parameters
ν	0.0000004	m2/s	313.15	Kinematic Viscosities for Ether + Alkane Mixtures: Experimental Results and UNIFAC-VISCO Parameters
Pvap	[0.02; 151.82]	kPa	[263.75; 354.88]
Pvap	3.21	kPa	263.75	Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
Pvap	5.71	kPa	273.47	Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
Pvap	9.69	kPa	283.35	Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
Pvap	10.74	kPa	284.93	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	10.75	kPa	284.93	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	12.65	kPa	288.15	Isothermal vapour-liquid equilibria and excess enthalpies for the binary mixtures containing an isomeric chlorobutane and diisopropyl ether
Pvap	15.80	kPa	293.29	Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
Pvap	17.21	kPa	294.90	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	17.21	kPa	294.91	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	0.02	kPa	298.15	NCMS SOLV-DB
Pvap	20.00	kPa	298.15	Isothermal vapour-liquid equilibria and excess enthalpies for the binary mixtures containing an isomeric chlorobutane and diisopropyl ether
Pvap	24.57	kPa	303.28	Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
Pvap	26.57	kPa	304.87	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	26.58	kPa	304.89	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	30.46	kPa	308.15	Isothermal vapour-liquid equilibria and excess enthalpies for the binary mixtures containing an isomeric chlorobutane and diisopropyl ether
Pvap	30.91	kPa	308.58	The thermodynamics of vaporization of ethyl tert-butyl ether, isobutyl tert-butyl ether, and di-isopropyl ether
Pvap	37.26	kPa	313.25	The thermodynamics of vaporization of ethyl tert-butyl ether, isobutyl tert-butyl ether, and di-isopropyl ether
Pvap	36.95	kPa	313.27	Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
Pvap	39.71	kPa	314.86	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	39.72	kPa	314.87	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	45.83	kPa	318.65	The thermodynamics of vaporization of ethyl tert-butyl ether, isobutyl tert-butyl ether, and di-isopropyl ether
Pvap	53.85	kPa	323.25	Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
Pvap	56.12	kPa	324.17	The thermodynamics of vaporization of ethyl tert-butyl ether, isobutyl tert-butyl ether, and di-isopropyl ether
Pvap	57.64	kPa	324.85	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	57.65	kPa	324.87	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	67.49	kPa	329.40	The thermodynamics of vaporization of ethyl tert-butyl ether, isobutyl tert-butyl ether, and di-isopropyl ether
Pvap	76.24	kPa	333.22	Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
Pvap	81.42	kPa	334.85	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	81.41	kPa	334.85	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	81.57	kPa	334.98	The thermodynamics of vaporization of ethyl tert-butyl ether, isobutyl tert-butyl ether, and di-isopropyl ether
Pvap	93.18	kPa	339.03	The thermodynamics of vaporization of ethyl tert-butyl ether, isobutyl tert-butyl ether, and di-isopropyl ether
Pvap	95.31	kPa	339.73	The thermodynamics of vaporization of ethyl tert-butyl ether, isobutyl tert-butyl ether, and di-isopropyl ether
Pvap	97.44	kPa	340.41	The thermodynamics of vaporization of ethyl tert-butyl ether, isobutyl tert-butyl ether, and di-isopropyl ether
Pvap	104.96	kPa	343.18	Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
Pvap	112.36	kPa	344.84	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	112.39	kPa	344.85	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	151.81	kPa	354.87	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
Pvap	151.82	kPa	354.88	Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
n0	[1.35667; 1.37358]		[283.15; 313.15]
n0	1.37358		283.15	Volumetric, Acoustic, and Refractive Properties of Isomeric Chlorobutanes with Diisopropyl Ether
n0	1.37126		288.15	Densities and Viscosities for Binary and Ternary Mixtures of Diisopropyl Ether, Ethanol, and Methylcyclohexane
n0	1.37084		288.15	Volumetric, Acoustic, and Refractive Properties of Isomeric Chlorobutanes with Diisopropyl Ether
n0	1.37093		288.15	Densities, Viscosities, and Refractive Indices for Binary and Ternary Mixtures of Diisopropyl Ether, Ethanol, and 2,2,4-Trimethylpentane
n0	1.36812		293.15	Volumetric, Acoustic, and Refractive Properties of Isomeric Chlorobutanes with Diisopropyl Ether
n0	1.36537		298.15	Densities and Viscosities for Binary and Ternary Mixtures of Diisopropyl Ether, Ethanol, and Methylcyclohexane
n0	1.36510		298.15	Vapor Liquid Equilibrium for Ternary and Binary Mixtures of 2-Isopropoxypropane, 2-Propanol, and N,N-Dimethylacetamide at 101.3 kPa
n0	1.36500		298.15	NCMS SOLV-DB
n0	1.36650		298.15	Atmospheric densities and interfacial tensions for 1- alkanol (1-butanol to 1-octanol) + water and ether (MTBE, ETBE, DIPE, TAME and THP) + water demixed mixtures.
n0	1.36520		298.15	Effect of pressure and the capability of 2-methoxyethanol as a solvent in the behaviour of a diisopropyl ether isopropyl alcohol azeotropic mixture
n0	1.36524		298.15	Densities, Viscosities, and Refractive Indices for Binary and Ternary Mixtures of Diisopropyl Ether, Ethanol, and 2,2,4-Trimethylpentane
n0	1.36644		298.15	Vapor liquid equilibria and interfacial tensions for the ternary system acetone + 2,2 -oxybis[propane] + cyclohexane and its constituent binary systems
n0	1.36652		298.15	Isobaric vapor liquid equilibrium and isothermal surface tensions of 2,2 -oxybis[propane] + 2,5-Dimethylfuran
n0	1.36523		298.15	Isobaric Vapor-Liquid Equilibria at 101.32 kPa and Densities, Speeds of Sound, and Refractive Indices at 298.15 K for MTBE or DIPE or TAME + 1-Propanol Binary Systems
n0	1.36540		298.15	(Vapor + liquid) equilibrium of binary mixtures formed by N,N-dimethyl formamide with some compounds at 95.1 kPa
n0	1.36525		298.15	Volumetric, Acoustic, and Refractive Properties of Isomeric Chlorobutanes with Diisopropyl Ether
n0	1.36520		298.15	sobaric Vapor-Liquid Equilibria for Binary and Ternary Mixtures of Diisopropyl Ether, 2-Propyl Alcohol, and n-Butyl Propionate at 101.3 kPa
n0	1.36520		298.15	Isobaric Vapor-Liquid Equilibria for Binary and Ternary Mixtures of Diisopropyl Ether, 2-Propyl Alcohol, and 3-Methyl-1-Butanol
n0	1.36530		298.20	Measurement and prediction of tie-line data for mixtures of (water + 1-propanol + diisopropyl ether): LLE diagrams as a function of temperature
n0	1.36242		303.15	Volumetric, Acoustic, and Refractive Properties of Isomeric Chlorobutanes with Diisopropyl Ether
n0	1.35956		308.15	Volumetric, Acoustic, and Refractive Properties of Isomeric Chlorobutanes with Diisopropyl Ether
n0	1.35954		308.15	Densities and Viscosities for Binary and Ternary Mixtures of Diisopropyl Ether, Ethanol, and Methylcyclohexane
n0	1.35944		308.15	Densities, Viscosities, and Refractive Indices for Binary and Ternary Mixtures of Diisopropyl Ether, Ethanol, and 2,2,4-Trimethylpentane
n0	1.35667		313.15	Volumetric, Acoustic, and Refractive Properties of Isomeric Chlorobutanes with Diisopropyl Ether
ρl	[686.20; 728.82]	kg/m3	[288.15; 328.15]
ρl	728.82	kg/m3	288.15	Volumetric properties of binary mixtures of ethers and acetonitrile: Experimental results and application of the Prigogine Flory Patterson theory
ρl	724.00	kg/m3	293.00	KDB
ρl	723.67	kg/m3	293.15	Volumetric properties of binary mixtures of ethers and acetonitrile: Experimental results and application of the Prigogine Flory Patterson theory
ρl	718.30	kg/m3	298.15	Isobaric ternary vapour-liquid equilibrium of methanol(1) + diisopropyl ether(2) + isopropyl alcohol(3) along with methanol + isopropyl alcohol binary data at atmospheric and sub-atmospheric pressures
ρl	719.17	kg/m3	298.15	Volumetric properties of binary and ternary mixtures of diisopropyl ether, a,a,a-trifluorotoluene, 2,2,2-trifluoroethanol, and ethanol at a temperature 298.15 K and pressure 101 kPa
ρl	718.30	kg/m3	298.15	Experimental isobaric vapor-liquid equilibrium at atmospheric and sub-atmospheric pressures, excess molar volumes and deviations in molar refractivity from 293.15 K to 318.15 K of diisopropyl ether with methanol and isopropyl alcohol.
ρl	718.14	kg/m3	298.15	Phase equilibria for binary systems of octane boosters with 2,2,4-trimethylpentane
ρl	718.51	kg/m3	298.15	Volumetric properties of (N,N-dimethylformamide + aliphatic diethers) at Temperatures ranging from (298.15 to 358.15) K
ρl	718.38	kg/m3	298.15	Isothermal vapour liquid equilibria in the binary and ternary systems composed of 2-propanol, diisopropyl ether and 4-methyl-2-pentanone
ρl	718.24	kg/m3	298.15	Excess Volumes of Ternary Mixtures 2,2,4-Trimethylpentane + Diisopropyl Ether or Methyl tert-Butyl Ether + Methanol, Ethanol, or 1-Propanol at 298.15 K
ρl	723.80	kg/m3	298.15	Tie-Line Data for Aqueous Mixtures of Butyric Acid with Diisopropyl Ether at Various Temperatures
ρl	719.17	kg/m3	298.15	Isothermal vapor liquid equilibrium at 333.15K and excess molar volumes at 298.15K for the ternary system di-isopropyl ether + n-propyl alcohol + toluene and its binary subsystems
ρl	718.62	kg/m3	298.15	Liquid liquid equilibria for the binary system of di-isopropyl ether (DIPE) +water in between 288.15 and 323.15K and the ternary systems of DIPE +water + C1 C4 alcohols at 298.15K
ρl	718.46	kg/m3	298.15	Volumetric properties of binary mixtures of ethers and acetonitrile: Experimental results and application of the Prigogine Flory Patterson theory
ρl	718.23	kg/m3	298.15	Vapour-liquid equilibria in binary and ternary systems composed of 2,3-dimethylbutane, diisopropyl ether, and 3-methyl-2-butanone at 313.15, 323.15 and 313.15 K
ρl	718.51	kg/m3	298.15	Isothermal (vapour + liquid) equilibria for binary mixtures of diisopropyl ether with (methanol, or ethanol, or 1-butanol): Experimental data, correlations, and predictions
ρl	718.38	kg/m3	298.15	Excess Molar Volumes and Surface Tensions of Xylene with Isopropyl Ether or Methyl tert-Butyl Ether at 298.15 K
ρl	718.70	kg/m3	298.15	Excess Enthalpies of the Ternary Mixtures: Diisopropyl Ether + 3-Methylpentane + (Octane or Decane) at 298.15 K
ρl	713.21	kg/m3	303.15	Volumetric properties of binary mixtures of ethers and acetonitrile: Experimental results and application of the Prigogine Flory Patterson theory
ρl	713.10	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	713.51	kg/m3	303.15	Isothermal VLE and VE at 303.15 K for the Binary and Ternary Mixtures of Di-isopropyl Ether (DIPE) + 1-Propanol + 2,2,4-Trimethylpentane
ρl	707.90	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	702.50	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	702.59	kg/m3	313.15	Volumetric properties of (N,N-dimethylformamide + aliphatic diethers) at Temperatures ranging from (298.15 to 358.15) K
ρl	686.20	kg/m3	328.15	Volumetric properties of (N,N-dimethylformamide + aliphatic diethers) at Temperatures ranging from (298.15 to 358.15) K
ΔfusS	[59.18; 64.09]	J/mol×K	[186.30; 187.77]
ΔfusS	59.18	J/mol×K	186.30	NIST
ΔfusS	59.18	J/mol×K	186.30	NIST
ΔfusS	64.09	J/mol×K	187.77	NIST
ΔfusS	64.09	J/mol×K	187.77	NIST
csound,fluid	[135.68; 986.38]	m/s	[303.08; 492.48]
csound,fluid	986.38	m/s	303.08	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	976.00	m/s	303.15	Thermodynamic and acoustic properties of binary mixtures of ethers. III. Diisopropyl ether or oxolane with o- or m-toluidines at 303.15, 313.15 and 323.15 K
csound,fluid	976.00	m/s	303.15	Thermodynamic and acoustic properties of binary mixtures of ethers. IV. Diisopropyl ether or oxolane with N,N-dimethylaniline or N,Ndiethylaniline at 303.15, 313.15 and 323.15 K
csound,fluid	976.00	m/s	303.15	Thermodynamic and acoustic properties of binary mixtures of ethers. V. Diisopropyl ether or oxolane with 2- or 3-chloroanilines at 303.15, 313.15 and 323.15 K
csound,fluid	975.00	m/s	303.15	Thermodynamic and Acoustic Properties of Binary Mixtures of Ethers. 2. Diisopropyl Ether with Arylamines at (303.15, 313.15, and 323.15) K and Application of ERAS Model to Aniline Mixtures with Diisopropyl Ether and Oxolane
csound,fluid	932.00	m/s	313.15	Thermodynamic and acoustic properties of binary mixtures of ethers. III. Diisopropyl ether or oxolane with o- or m-toluidines at 303.15, 313.15 and 323.15 K
csound,fluid	932.00	m/s	313.15	Thermodynamic and acoustic properties of binary mixtures of ethers. IV. Diisopropyl ether or oxolane with N,N-dimethylaniline or N,Ndiethylaniline at 303.15, 313.15 and 323.15 K
csound,fluid	932.00	m/s	313.15	Thermodynamic and acoustic properties of binary mixtures of ethers. V. Diisopropyl ether or oxolane with 2- or 3-chloroanilines at 303.15, 313.15 and 323.15 K
csound,fluid	934.00	m/s	313.15	Thermodynamic and Acoustic Properties of Binary Mixtures of Ethers. 2. Diisopropyl Ether with Arylamines at (303.15, 313.15, and 323.15) K and Application of ERAS Model to Aniline Mixtures with Diisopropyl Ether and Oxolane
csound,fluid	915.66	m/s	318.27	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	891.00	m/s	323.15	Thermodynamic and Acoustic Properties of Binary Mixtures of Ethers. 2. Diisopropyl Ether with Arylamines at (303.15, 313.15, and 323.15) K and Application of ERAS Model to Aniline Mixtures with Diisopropyl Ether and Oxolane
csound,fluid	892.00	m/s	323.15	Thermodynamic and Acoustic Properties of Binary Mixtures of Ethers. 2. Diisopropyl Ether with Arylamines at (303.15, 313.15, and 323.15) K and Application of ERAS Model to Aniline Mixtures with Diisopropyl Ether and Oxolane
csound,fluid	889.00	m/s	323.15	Thermodynamic and acoustic properties of binary mixtures of ethers. V. Diisopropyl ether or oxolane with 2- or 3-chloroanilines at 303.15, 313.15 and 323.15 K
csound,fluid	889.00	m/s	323.15	Thermodynamic and acoustic properties of binary mixtures of ethers. IV. Diisopropyl ether or oxolane with N,N-dimethylaniline or N,Ndiethylaniline at 303.15, 313.15 and 323.15 K
csound,fluid	889.00	m/s	323.15	Thermodynamic and acoustic properties of binary mixtures of ethers. III. Diisopropyl ether or oxolane with o- or m-toluidines at 303.15, 313.15 and 323.15 K
csound,fluid	852.50	m/s	333.62	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	790.74	m/s	347.96	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	731.21	m/s	362.87	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	662.26	m/s	378.14	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	593.47	m/s	393.15	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	552.35	m/s	402.97	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	514.15	m/s	412.75	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	469.11	m/s	422.75	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	426.77	m/s	432.74	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	384.46	m/s	443.46	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	336.71	m/s	453.54	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	315.85	m/s	457.54	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	290.41	m/s	463.00	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	263.51	m/s	468.31	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	237.38	m/s	473.80	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	210.25	m/s	478.69	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	185.80	m/s	483.10	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	162.27	m/s	487.42	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
csound,fluid	135.68	m/s	492.48	Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
γ	[0.01; 0.02]	N/m	[248.07; 373.17]
γ	0.02	N/m	248.07	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	253.23	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	258.10	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	263.18	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	268.33	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	273.46	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	278.50	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	283.18	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	288.18	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	293.16	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	298.10	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	308.08	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	313.27	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.02	N/m	318.17	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.01	N/m	323.19	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.01	N/m	328.12	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.01	N/m	333.12	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.01	N/m	338.11	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.01	N/m	343.10	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.01	N/m	348.10	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.01	N/m	353.10	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.01	N/m	358.15	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.01	N/m	363.17	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.01	N/m	368.17	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
γ	0.01	N/m	373.17	Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether

Datasets

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

Viscosity, Pa*s

Fixed		Measured
Pressure, kPa - Liquid	Temperature, K - Liquid	Viscosity, Pa*s - Liquid
20000.00	293.15	0.0004
40000.00	293.15	0.0005
60000.00	293.15	0.0005
80000.00	293.15	0.0006
100000.00	293.15	0.0007
20000.00	313.15	0.0003
40000.00	313.15	0.0004
60000.00	313.15	0.0005
80000.00	313.15	0.0005
100000.00	313.15	0.0006
20000.00	333.15	0.0003
40000.00	333.15	0.0003
60000.00	333.15	0.0004
80000.00	333.15	0.0005
100000.00	333.15	0.0005
20000.00	353.15	0.0003
40000.00	353.15	0.0003
60000.00	353.15	0.0004
80000.00	353.15	0.0004
100000.00	353.15	0.0005
100.00	293.15	0.0003
100.00	313.15	0.0003
100.00	333.15	0.0002
Reference

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Viscosity, Pa*s - Liquid
243.15	100.00	0.0006
243.15	4660.00	0.0006
243.15	10070.00	0.0007
243.15	15370.00	0.0007
243.15	20860.00	0.0008
253.15	100.00	0.0005
253.15	4720.00	0.0006
253.15	9990.00	0.0006
253.15	15400.00	0.0006
253.15	20740.00	0.0006
263.15	100.00	0.0005
263.15	4470.00	0.0005
263.15	9490.00	0.0005
263.15	14490.00	0.0005
263.15	19640.00	0.0006
273.15	100.00	0.0004
273.15	4690.00	0.0004
273.15	10010.00	0.0005
273.15	15290.00	0.0005
273.15	20420.00	0.0005
283.15	100.00	0.0004
283.15	4700.00	0.0004
283.15	10100.00	0.0004
283.15	15460.00	0.0004
283.15	21360.00	0.0005
293.15	100.00	0.0003
293.15	4470.00	0.0003
293.15	9590.00	0.0004
293.15	14750.00	0.0004
293.15	20450.00	0.0004
303.15	100.00	0.0003
303.15	4440.00	0.0003
303.15	9500.00	0.0003
303.15	14650.00	0.0003
303.15	19650.00	0.0004
313.15	100.00	0.0003
313.15	4840.00	0.0003
313.15	10140.00	0.0003
313.15	15550.00	0.0003
313.15	21490.00	0.0003
323.15	100.00	0.0002
323.15	4760.00	0.0003
323.15	10370.00	0.0003
323.15	15480.00	0.0003
323.15	20780.00	0.0003
333.15	100.00	0.0002
333.15	4750.00	0.0002
333.15	10360.00	0.0003
333.15	15670.00	0.0003
333.15	20890.00	0.0003
343.15	130.00	0.0002
343.15	4390.00	0.0002
343.15	9530.00	0.0002
343.15	14740.00	0.0002
343.15	21230.00	0.0003
353.15	200.00	0.0002
353.15	4830.00	0.0002
353.15	10320.00	0.0002
353.15	15760.00	0.0002
353.15	21100.00	0.0002
363.15	230.00	0.0002
363.15	4730.00	0.0002
363.15	10170.00	0.0002
363.15	15830.00	0.0002
363.15	20860.00	0.0002
373.15	310.00	0.0002
373.15	4730.00	0.0002
373.15	9630.00	0.0002
373.15	15600.00	0.0002
373.15	21680.00	0.0002
Reference

Mass density, kg/m3

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Mass density, kg/m3 - Liquid
283.15	100.00	733.83
288.15	100.00	728.69
293.15	100.00	723.51
298.15	100.00	718.29
303.15	100.00	713.03
308.15	100.00	707.73
313.15	100.00	702.38
318.15	100.00	697.07
323.15	100.00	691.61
328.15	100.00	686.17
333.15	100.00	681.0
283.15	5000.00	739.6
288.15	5000.00	734.61
293.15	5000.00	729.62
298.15	5000.00	724.67
303.15	5000.00	719.61
308.15	5000.00	714.61
313.15	5000.00	709.64
318.15	5000.00	704.53
323.15	5000.00	699.42
328.15	5000.00	694.18
333.15	5000.00	688.97
283.15	10000.00	744.9
288.15	10000.00	740.14
293.15	10000.00	735.37
298.15	10000.00	730.59
303.15	10000.00	725.79
308.15	10000.00	720.99
313.15	10000.00	716.16
318.15	10000.00	711.3
323.15	10000.00	706.46
328.15	10000.00	701.52
333.15	10000.00	696.58
283.15	15000.00	749.85
288.15	15000.00	745.3
293.15	15000.00	740.69
298.15	15000.00	736.05
303.15	15000.00	731.48
308.15	15000.00	726.79
313.15	15000.00	722.17
318.15	15000.00	717.51
323.15	15000.00	712.89
328.15	15000.00	708.19
333.15	15000.00	703.52
283.15	20000.00	754.49
288.15	20000.00	750.09
293.15	20000.00	745.62
298.15	20000.00	741.13
303.15	20000.00	736.81
308.15	20000.00	732.2
313.15	20000.00	727.77
318.15	20000.00	723.27
323.15	20000.00	718.83
328.15	20000.00	714.34
333.15	20000.00	709.85
283.15	25000.00	758.89
288.15	25000.00	754.61
293.15	25000.00	750.29
298.15	25000.00	745.92
303.15	25000.00	741.76
308.15	25000.00	737.29
313.15	25000.00	732.97
318.15	25000.00	728.67
323.15	25000.00	724.38
328.15	25000.00	720.04
333.15	25000.00	715.73
283.15	30000.00	763.08
288.15	30000.00	758.9
293.15	30000.00	754.71
298.15	30000.00	750.46
303.15	30000.00	746.43
308.15	30000.00	742.07
313.15	30000.00	737.92
318.15	30000.00	733.74
323.15	30000.00	729.58
328.15	30000.00	725.37
333.15	30000.00	721.21
283.15	35000.00	767.08
288.15	35000.00	763.01
293.15	35000.00	758.91
298.15	35000.00	754.77
303.15	35000.00	750.85
308.15	35000.00	746.63
313.15	35000.00	742.55
318.15	35000.00	738.49
323.15	35000.00	734.45
328.15	35000.00	730.4
333.15	35000.00	726.36
283.15	40000.00	770.91
288.15	40000.00	766.92
293.15	40000.00	762.93
298.15	40000.00	758.89
303.15	40000.00	755.09
308.15	40000.00	750.94
313.15	40000.00	746.98
318.15	40000.00	743.01
323.15	40000.00	739.08
328.15	40000.00	735.15
333.15	40000.00	731.23
283.15	45000.00	774.59
288.15	45000.00	770.68
293.15	45000.00	766.78
298.15	45000.00	762.82
303.15	45000.00	759.12
308.15	45000.00	755.05
313.15	45000.00	751.2
318.15	45000.00	747.34
323.15	45000.00	743.5
328.15	45000.00	739.67
333.15	45000.00	735.85
283.15	50000.00	778.13
288.15	50000.00	774.31
293.15	50000.00	770.48
298.15	50000.00	766.6
303.15	50000.00	763.0
308.15	50000.00	759.01
313.15	50000.00	755.21
318.15	50000.00	751.47
323.15	50000.00	747.72
328.15	50000.00	743.94
333.15	50000.00	740.18
283.15	55000.00	781.56
288.15	55000.00	777.77
293.15	55000.00	774.06
298.15	55000.00	770.25
303.15	55000.00	766.7
308.15	55000.00	762.79
313.15	55000.00	759.09
318.15	55000.00	755.41
323.15	55000.00	751.72
328.15	55000.00	748.05
333.15	55000.00	744.38
283.15	60000.00	784.88
288.15	60000.00	781.16
293.15	60000.00	777.49
298.15	60000.00	773.75
303.15	60000.00	770.24
308.15	60000.00	766.45
313.15	60000.00	762.83
318.15	60000.00	759.21
323.15	60000.00	755.59
328.15	60000.00	751.94
333.15	60000.00	748.24
283.15	65000.00	788.07
288.15	65000.00	784.42
293.15	65000.00	780.83
298.15	65000.00	777.14
303.15	65000.00	773.7
308.15	65000.00	769.97
313.15	65000.00	766.39
318.15	65000.00	762.85
323.15	65000.00	759.26
328.15	65000.00	755.64
333.15	65000.00	752.02
Reference

Fixed		Measured
Pressure, kPa - Liquid	Temperature, K - Liquid	Mass density, kg/m3 - Liquid
100.00	293.15	723.5
1000.00	293.15	724.3
5000.00	293.15	729.1
10000.00	293.15	734.5
15000.00	293.15	739.6
20000.00	293.15	744.5
25000.00	293.15	749.0
30000.00	293.15	753.3
35000.00	293.15	757.4
40000.00	293.15	761.3
45000.00	293.15	765.0
50000.00	293.15	768.6
55000.00	293.15	772.1
60000.00	293.15	775.4
65000.00	293.15	778.6
70000.00	293.15	781.7
80000.00	293.15	787.6
90000.00	293.15	793.2
100000.00	293.15	798.5
110000.00	293.15	803.6
120000.00	293.15	808.4
130000.00	293.15	812.9
140000.00	293.15	817.3
100.00	298.15	718.3
1000.00	298.15	719.5
5000.00	298.15	724.5
10000.00	298.15	730.2
15000.00	298.15	735.6
20000.00	298.15	740.5
25000.00	298.15	745.2
30000.00	298.15	749.6
35000.00	298.15	753.7
40000.00	298.15	757.7
45000.00	298.15	761.6
50000.00	298.15	765.2
55000.00	298.15	768.7
60000.00	298.15	772.1
65000.00	298.15	775.4
70000.00	298.15	778.5
80000.00	298.15	784.5
90000.00	298.15	790.3
100000.00	298.15	795.6
110000.00	298.15	800.8
120000.00	298.15	805.6
130000.00	298.15	810.3
140000.00	298.15	814.6
100.00	313.15	702.4
1000.00	313.15	703.7
5000.00	313.15	709.3
10000.00	313.15	715.7
15000.00	313.15	721.6
20000.00	313.15	727.1
25000.00	313.15	732.0
30000.00	313.15	737.1
35000.00	313.15	741.5
40000.00	313.15	745.8
45000.00	313.15	749.9
50000.00	313.15	753.8
55000.00	313.15	757.6
60000.00	313.15	761.3
65000.00	313.15	764.8
70000.00	313.15	768.1
80000.00	313.15	774.3
90000.00	313.15	780.4
100000.00	313.15	786.0
110000.00	313.15	791.4
120000.00	313.15	796.4
130000.00	313.15	801.3
140000.00	313.15	806.0
100.00	333.15	680.4
1000.00	333.15	682.0
5000.00	333.15	688.8
10000.00	333.15	696.3
15000.00	333.15	703.1
20000.00	333.15	709.3
25000.00	333.15	715.0
30000.00	333.15	720.4
35000.00	333.15	725.5
40000.00	333.15	730.2
45000.00	333.15	734.7
50000.00	333.15	739.0
55000.00	333.15	743.1
60000.00	333.15	747.0
65000.00	333.15	750.8
70000.00	333.15	754.3
80000.00	333.15	761.2
90000.00	333.15	767.7
100000.00	333.15	773.6
110000.00	333.15	779.3
120000.00	333.15	784.6
130000.00	333.15	789.8
140000.00	333.15	794.7
1000.00	353.19	659.5
5000.00	353.19	667.5
10000.00	353.19	676.4
15000.00	353.19	684.4
20000.00	353.19	691.5
25000.00	353.19	698.0
30000.00	353.19	704.0
35000.00	353.19	709.6
40000.00	353.19	714.8
45000.00	353.19	719.7
50000.00	353.19	724.5
55000.00	353.19	728.9
60000.00	353.19	733.1
65000.00	353.19	737.2
70000.00	353.19	741.1
80000.00	353.19	748.4
90000.00	353.19	755.3
100000.00	353.19	761.6
110000.00	353.19	767.7
120000.00	353.19	773.4
130000.00	353.19	778.8
140000.00	353.19	784.0
1000.00	373.24	635.5
5000.00	373.24	645.5
10000.00	373.24	656.1
15000.00	373.24	665.3
20000.00	373.24	673.4
25000.00	373.24	680.8
30000.00	373.24	687.6
35000.00	373.24	693.8
40000.00	373.24	699.6
45000.00	373.24	705.0
50000.00	373.24	710.1
55000.00	373.24	714.9
60000.00	373.24	719.5
65000.00	373.24	723.9
70000.00	373.24	728.1
80000.00	373.24	735.9
90000.00	373.24	743.2
100000.00	373.24	750.0
110000.00	373.24	756.3
120000.00	373.24	762.3
130000.00	373.24	768.0
140000.00	373.24	773.3
1000.00	393.29	609.5
5000.00	393.29	622.1
10000.00	393.29	634.9
15000.00	393.29	645.7
20000.00	393.29	655.1
25000.00	393.29	663.4
30000.00	393.29	671.0
35000.00	393.29	677.9
40000.00	393.29	684.3
45000.00	393.29	690.2
50000.00	393.29	695.7
55000.00	393.29	701.0
60000.00	393.29	705.9
65000.00	393.29	710.6
70000.00	393.29	715.1
80000.00	393.29	723.5
90000.00	393.29	731.3
100000.00	393.29	738.3
110000.00	393.29	745.2
120000.00	393.29	751.3
130000.00	393.29	757.4
140000.00	393.29	763.0
Reference

Fixed		Measured
Pressure, kPa - Liquid	Temperature, K - Liquid	Mass density, kg/m3 - Liquid
100.00	293.15	723.5
1000.00	293.15	724.6
5000.00	293.15	729.4
10000.00	293.15	734.9
15000.00	293.15	740.0
20000.00	293.15	744.8
25000.00	293.15	749.4
30000.00	293.15	753.7
35000.00	293.15	757.7
40000.00	293.15	761.6
45000.00	293.15	765.3
50000.00	293.15	768.9
55000.00	293.15	772.4
60000.00	293.15	775.7
65000.00	293.15	778.9
70000.00	293.15	782.0
80000.00	293.15	787.9
90000.00	293.15	793.5
100000.00	293.15	798.8
110000.00	293.15	803.9
120000.00	293.15	808.7
130000.00	293.15	813.2
140000.00	293.15	817.6
100.00	298.15	718.3
1000.00	298.15	719.6
5000.00	298.15	724.5
10000.00	298.15	730.2
15000.00	298.15	735.6
20000.00	298.15	740.5
25000.00	298.15	745.2
30000.00	298.15	749.6
35000.00	298.15	753.7
40000.00	298.15	757.8
45000.00	298.15	761.6
50000.00	298.15	765.2
55000.00	298.15	768.8
60000.00	298.15	772.2
65000.00	298.15	775.4
70000.00	298.15	778.6
80000.00	298.15	784.6
90000.00	298.15	790.3
100000.00	298.15	795.7
110000.00	298.15	800.8
120000.00	298.15	805.6
130000.00	298.15	810.3
140000.00	298.15	814.6
100.00	313.15	702.4
1000.00	313.15	703.8
5000.00	313.15	709.4
10000.00	313.15	715.8
15000.00	313.15	721.7
20000.00	313.15	727.2
25000.00	313.15	732.1
30000.00	313.15	737.1
35000.00	313.15	741.6
40000.00	313.15	745.9
45000.00	313.15	750.0
50000.00	313.15	753.9
55000.00	313.15	757.7
60000.00	313.15	761.3
65000.00	313.15	764.8
70000.00	313.15	768.1
80000.00	313.15	774.4
90000.00	313.15	780.5
100000.00	313.15	786.1
110000.00	313.15	791.4
120000.00	313.15	796.5
130000.00	313.15	801.4
140000.00	313.15	806.0
100.00	333.15	680.5
1000.00	333.15	682.1
5000.00	333.15	688.9
10000.00	333.15	696.4
15000.00	333.15	703.2
20000.00	333.15	709.4
25000.00	333.15	715.1
30000.00	333.15	720.5
35000.00	333.15	725.6
40000.00	333.15	730.3
45000.00	333.15	734.8
50000.00	333.15	739.1
55000.00	333.15	743.1
60000.00	333.15	747.1
65000.00	333.15	750.9
70000.00	333.15	754.4
80000.00	333.15	761.3
90000.00	333.15	767.7
100000.00	333.15	773.7
110000.00	333.15	779.4
120000.00	333.15	784.7
130000.00	333.15	789.9
140000.00	333.15	794.8
1000.00	353.19	659.5
5000.00	353.19	667.6
10000.00	353.19	676.5
15000.00	353.19	684.4
20000.00	353.19	691.5
25000.00	353.19	698.0
30000.00	353.19	704.0
35000.00	353.19	709.7
40000.00	353.19	714.8
45000.00	353.19	719.7
50000.00	353.19	724.6
55000.00	353.19	728.9
60000.00	353.19	733.2
65000.00	353.19	737.2
70000.00	353.19	741.1
80000.00	353.19	748.4
90000.00	353.19	755.4
100000.00	353.19	761.6
110000.00	353.19	767.8
120000.00	353.19	773.4
130000.00	353.19	778.8
140000.00	353.19	784.0
1000.00	373.24	635.6
5000.00	373.24	645.5
10000.00	373.24	656.1
15000.00	373.24	665.3
20000.00	373.24	673.5
25000.00	373.24	680.8
30000.00	373.24	687.6
35000.00	373.24	693.8
40000.00	373.24	699.6
45000.00	373.24	705.0
50000.00	373.24	710.1
55000.00	373.24	714.9
60000.00	373.24	719.5
65000.00	373.24	723.9
70000.00	373.24	728.1
80000.00	373.24	735.9
90000.00	373.24	743.2
100000.00	373.24	750.0
110000.00	373.24	756.3
120000.00	373.24	762.3
130000.00	373.24	768.0
140000.00	373.24	773.3
1000.00	393.28	609.5
5000.00	393.28	622.1
10000.00	393.28	635.0
15000.00	393.28	645.8
20000.00	393.28	655.2
25000.00	393.28	663.5
30000.00	393.28	671.1
35000.00	393.28	677.9
40000.00	393.28	684.3
45000.00	393.28	690.2
50000.00	393.28	695.8
55000.00	393.28	701.1
60000.00	393.28	705.9
65000.00	393.28	710.6
70000.00	393.28	715.2
80000.00	393.28	723.5
90000.00	393.28	731.3
100000.00	393.28	738.4
110000.00	393.28	745.3
120000.00	393.28	751.4
130000.00	393.28	757.4
140000.00	393.28	763.1
Reference

Speed of sound, m/s

Operational condition: Frequency, MHz = 3 (Liquid)

Fixed		Measured
Pressure, kPa - Liquid	Temperature, K - Liquid	Speed of sound, m/s - Liquid
100.00	293.15	1019.71
20000.00	293.15	1161.24
40000.00	293.15	1274.5
60000.00	293.15	1369.29
80000.00	293.15	1454.22
100000.00	293.15	1528.73
100.00	303.15	974.32
20000.00	303.15	1122.56
40000.00	303.15	1240.38
60000.00	303.15	1337.63
80000.00	303.15	1423.43
100000.00	303.15	1501.88
100.00	313.15	930.24
20000.00	313.15	1086.83
40000.00	313.15	1207.91
60000.00	313.15	1308.13
80000.00	313.15	1396.71
100000.00	313.15	1474.97
100.00	323.15	887.83
20000.00	323.15	1051.9
40000.00	323.15	1177.1
60000.00	323.15	1278.96
80000.00	323.15	1368.68
100000.00	323.15	1448.65
100.00	333.15	847.29
20000.00	333.15	1017.78
40000.00	333.15	1146.81
60000.00	333.15	1252.38
80000.00	333.15	1343.16
100000.00	333.15	1423.5
20000.00	343.15	984.53
40000.00	343.15	1117.79
60000.00	343.15	1226.4
80000.00	343.15	1318.72
100000.00	343.15	1400.75
20000.00	353.15	953.14
40000.00	353.15	1090.71
60000.00	353.15	1200.36
80000.00	353.15	1294.59
100000.00	353.15	1378.37
Reference

Thermal conductivity, W/m/K

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Thermal conductivity, W/m/K - Liquid
235.46	100.00	0.1259
235.54	100.00	0.1258
236.06	100.00	0.1259
236.15	30600.00	0.1369
236.25	5000.00	0.1280
236.29	10100.00	0.1300
236.33	5000.00	0.1275
236.44	20200.00	0.1331
236.45	20300.00	0.1337
236.53	29900.00	0.1364
236.67	5000.00	0.1277
236.70	10200.00	0.1305
236.80	20300.00	0.1337
236.92	30000.00	0.1363
237.15	10200.00	0.1302
254.40	20400.00	0.1276
254.47	30400.00	0.1314
254.66	5100.00	0.1220
254.73	100.00	0.1201
254.74	10000.00	0.1238
254.76	29500.00	0.1312
254.86	10200.00	0.1241
254.89	5300.00	0.1223
254.90	20100.00	0.1280
255.08	100.00	0.1205
255.13	10100.00	0.1236
255.14	5100.00	0.1221
255.26	100.00	0.1199
255.58	30100.00	0.1315
255.61	19900.00	0.1285
274.60	30000.00	0.1274
274.72	10100.00	0.1177
274.86	29900.00	0.1269
274.89	20000.00	0.1220
274.95	5100.00	0.1154
275.00	100.00	0.1129
275.02	10000.00	0.1178
275.17	30100.00	0.1271
275.19	5000.00	0.1150
275.25	10000.00	0.1175
275.30	100.00	0.1135
275.51	20100.00	0.1218
275.60	5000.00	0.1152
275.91	100.00	0.1131
276.04	20100.00	0.1219
294.58	100.00	0.1073
294.64	30100.00	0.1197
294.65	10000.00	0.1118
294.95	5000.00	0.1089
294.98	10000.00	0.1115
295.03	100.00	0.1071
295.13	20100.00	0.1161
295.14	30100.00	0.1199
295.27	30000.00	0.1198
295.32	10100.00	0.1111
295.35	5000.00	0.1085
295.60	20100.00	0.1160
295.70	100.00	0.1066
295.82	5000.00	0.1087
296.18	20100.00	0.1159
314.96	30000.00	0.1145
315.03	5000.00	0.1027
315.07	20000.00	0.1105
315.13	100.00	0.0993
315.24	30000.00	0.1144
315.26	20000.00	0.1099
315.35	10000.00	0.1050
315.39	5000.00	0.1023
315.48	100.00	0.0996
315.71	10000.00	0.1054
315.73	5100.00	0.1027
315.76	20000.00	0.1104
315.88	100.00	0.0994
315.98	30000.00	0.1144
316.26	10000.00	0.1050
334.99	10100.00	0.0998
335.01	5400.00	0.0959
335.11	20000.00	0.1038
335.23	100.00	0.0935
335.29	29900.00	0.1093
335.32	10100.00	0.0995
335.46	100.00	0.0932
335.51	30200.00	0.1094
335.68	19700.00	0.1043
335.72	30000.00	0.1096
335.84	5000.00	0.0960
335.84	10100.00	0.0995
335.94	100.00	0.0931
336.31	20100.00	0.1042
336.37	5200.00	0.0959
354.72	29900.00	0.1060
354.72	29900.00	0.1051
354.85	19700.00	0.1006
354.97	5000.00	0.0913
354.97	19800.00	0.1000
355.23	10100.00	0.0944
355.29	300.00	0.0865
355.33	10100.00	0.0944
355.45	5000.00	0.0916
355.47	20100.00	0.1001
355.56	5000.00	0.0910
355.66	300.00	0.0869
355.87	10000.00	0.0940
356.04	300.00	0.0866
356.04	29900.00	0.1056
374.75	30000.00	0.1021
374.95	29800.00	0.1021
375.12	20000.00	0.0959
375.24	400.00	0.0813
375.25	10000.00	0.0893
375.40	5100.00	0.0858
375.47	400.00	0.0812
375.55	30300.00	0.1026
375.57	20000.00	0.0957
375.61	10000.00	0.0889
375.75	5100.00	0.0853
375.87	400.00	0.0816
376.05	20000.00	0.0955
376.23	10000.00	0.0890
376.26	5100.00	0.0854
Reference

Correlations

Property	Value	Unit	Temperature (K)	Source
Cp,gas	[107.03; 405.14]	J/mol×K	[187.65; 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			6.94540e+01
Coefficient B			-4.10180e+02
Coefficient C			5.73424e+00
Coefficient D			4.40850e-04
Coefficient E			-1.35950e-07
Temperature range, min.			187.65
Temperature range, max.			1500.00
Cp,gas	107.03	J/mol×K	187.65	Calculated Property
Cp,gas	172.59	J/mol×K	333.47	Calculated Property
Cp,gas	226.81	J/mol×K	479.28	Calculated Property
Cp,gas	269.89	J/mol×K	625.10	Calculated Property
Cp,gas	304.84	J/mol×K	770.92	Calculated Property
Cp,gas	333.65	J/mol×K	916.73	Calculated Property
Cp,gas	357.51	J/mol×K	1062.55	Calculated Property
Cp,gas	377.11	J/mol×K	1208.37	Calculated Property
Cp,gas	392.90	J/mol×K	1354.18	Calculated Property
Cp,gas	405.14	J/mol×K	1500.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
Cp,liquid	[184.18; 233.48]	J/mol×K	[187.65; 341.45]	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			1.61880e+02
Coefficient B			-2.88790e+00
Coefficient C			8.56045e-01
Coefficient D			1.45510e-02
Coefficient E			-1.32510e-05
Temperature range, min.			187.65
Temperature range, max.			341.45
Cp,liquid	184.18	J/mol×K	187.65	Calculated Property
Cp,liquid	188.08	J/mol×K	204.74	Calculated Property
Cp,liquid	192.41	J/mol×K	221.83	Calculated Property
Cp,liquid	197.19	J/mol×K	238.92	Calculated Property
Cp,liquid	202.39	J/mol×K	256.01	Calculated Property
Cp,liquid	207.99	J/mol×K	273.09	Calculated Property
Cp,liquid	213.96	J/mol×K	290.18	Calculated Property
Cp,liquid	220.24	J/mol×K	307.27	Calculated Property
Cp,liquid	226.78	J/mol×K	324.36	Calculated Property
Cp,liquid	233.48	J/mol×K	341.45	Calculated Property

Property	Value	Unit	Temperature (K)	Source
η	[0.0022648; 0.0001058]	Pa×s	[187.65; 450.00]	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			-9.06400e+00
Coefficient B			9.32470e+02
Coefficient C			-3.88150e-01
Coefficient D			1.03230e-06
Coefficient E			2.00000e+00
Temperature range, min.			187.65
Temperature range, max.			450.00
η	0.0022648	Pa×s	187.65	Calculated Property
η	0.0011113	Pa×s	216.80	Calculated Property
η	0.0006445	Pa×s	245.95	Calculated Property
η	0.0004194	Pa×s	275.10	Calculated Property
η	0.0002966	Pa×s	304.25	Calculated Property
η	0.0002232	Pa×s	333.40	Calculated Property
η	0.0001762	Pa×s	362.55	Calculated Property
η	0.0001445	Pa×s	391.70	Calculated Property
η	0.0001221	Pa×s	420.85	Calculated Property
η	0.0001058	Pa×s	450.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
ΔvapH	[36.20; 11.23]	kJ/mol	[187.65; 483.61]	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			5.80410e+01
Coefficient B			2.33850e+00
Coefficient C			-5.20860e+00
Coefficient D			5.03670e+00
Coefficient E			-1.69260e+00
Critical temperature, Tc (K)			5.00050e+02
Temperature range, min.			187.65
Temperature range, max.			483.61
ΔvapH	36.20	kJ/mol	187.65	Calculated Property
ΔvapH	34.87	kJ/mol	220.53	Calculated Property
ΔvapH	33.63	kJ/mol	253.42	Calculated Property
ΔvapH	32.30	kJ/mol	286.30	Calculated Property
ΔvapH	30.72	kJ/mol	319.19	Calculated Property
ΔvapH	28.74	kJ/mol	352.07	Calculated Property
ΔvapH	26.20	kJ/mol	384.96	Calculated Property
ΔvapH	22.89	kJ/mol	417.84	Calculated Property
ΔvapH	18.39	kJ/mol	450.73	Calculated Property
ΔvapH	11.23	kJ/mol	483.61	Calculated Property

Property	Value	Unit	Temperature (K)	Source
Pvap	[1.33; 202.64]	kPa	[253.56; 362.50]	The Yaws Handbook of Vapor Pressure
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
Coefficient A			1.53410e+01
Coefficient B			-3.27391e+03
Coefficient C			-3.60730e+01
Temperature range, min.			253.56
Temperature range, max.			362.50
Pvap	1.33	kPa	253.56	Calculated Property
Pvap	2.95	kPa	265.66	Calculated Property
Pvap	6.02	kPa	277.77	Calculated Property
Pvap	11.49	kPa	289.87	Calculated Property
Pvap	20.67	kPa	301.98	Calculated Property
Pvap	35.33	kPa	314.08	Calculated Property
Pvap	57.75	kPa	326.19	Calculated Property
Pvap	90.74	kPa	338.29	Calculated Property
Pvap	137.72	kPa	350.40	Calculated Property
Pvap	202.64	kPa	362.50	Calculated Property
Pvap	[3.88e-03; 2975.46]	kPa	[187.65; 500.05]	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			1.02626e+02
Coefficient B			-7.12030e+03
Coefficient C			-1.35137e+01
Coefficient D			1.43778e-05
Coefficient E			2.00000e+00
Temperature range, min.			187.65
Temperature range, max.			500.05
Pvap	3.88e-03	kPa	187.65	Calculated Property
Pvap	0.18	kPa	222.36	Calculated Property
Pvap	2.43	kPa	257.07	Calculated Property
Pvap	15.54	kPa	291.78	Calculated Property
Pvap	62.01	kPa	326.49	Calculated Property
Pvap	181.43	kPa	361.21	Calculated Property
Pvap	431.40	kPa	395.92	Calculated Property
Pvap	892.02	kPa	430.63	Calculated Property
Pvap	1679.77	kPa	465.34	Calculated Property
Pvap	2975.46	kPa	500.05	Calculated Property
Pvap	[6.74e-03; 2805.34]	kPa	[187.65; 500.05]	KDB Vapor Pressure Data
Equation			ln(Y) = A + B/T + C·ln(T) + D·T² + E/T² Y is Pvap in kPa, T in K
Coefficient A			4.13028e+01
Coefficient B			-4.89952e+03
Coefficient C			-3.87085e+00
Coefficient D			1.96241e-06
Coefficient E			0.00000e+00
Temperature range, min.			187.65
Temperature range, max.			500.05
Pvap	6.74e-03	kPa	187.65	Calculated Property
Pvap	0.21	kPa	222.36	Calculated Property
Pvap	2.44	kPa	257.07	Calculated Property
Pvap	14.99	kPa	291.78	Calculated Property
Pvap	60.31	kPa	326.49	Calculated Property
Pvap	180.79	kPa	361.21	Calculated Property
Pvap	438.33	kPa	395.92	Calculated Property
Pvap	908.22	kPa	430.63	Calculated Property
Pvap	1670.92	kPa	465.34	Calculated Property
Pvap	2805.34	kPa	500.05	Calculated Property
Pvap	[18.71; 97.74]	kPa	[296.70; 340.36]	NIST
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
Coefficient A			1.37384e+01
Coefficient B			-2.61351e+03
Coefficient C			-5.49200e+01
Reference			Cidlinský and Polák, 1969
Temperature range, min.			296.70
Temperature range, max.			340.36
Pvap	18.71	kPa	296.70	Calculated Property
Pvap	23.14	kPa	301.55	Calculated Property
Pvap	28.39	kPa	306.40	Calculated Property
Pvap	34.56	kPa	311.25	Calculated Property
Pvap	41.76	kPa	316.10	Calculated Property
Pvap	50.12	kPa	320.96	Calculated Property
Pvap	59.76	kPa	325.81	Calculated Property
Pvap	70.82	kPa	330.66	Calculated Property
Pvap	83.43	kPa	335.51	Calculated Property
Pvap	97.74	kPa	340.36	Calculated Property

Property	Value	Unit	Temperature (K)	Source
ρl	[824.06; 430.36]	kg/m3	[187.65; 483.61]	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			7.41043e+01
Coefficient B			2.75940e-01
Coefficient C			5.00050e+02
Coefficient D			2.94130e-01
Temperature range, min.			187.65
Temperature range, max.			483.61
ρl	824.06	kg/m3	187.65	Calculated Property
ρl	794.85	kg/m3	220.53	Calculated Property
ρl	764.28	kg/m3	253.42	Calculated Property
ρl	732.03	kg/m3	286.30	Calculated Property
ρl	697.67	kg/m3	319.19	Calculated Property
ρl	660.52	kg/m3	352.07	Calculated Property
ρl	619.49	kg/m3	384.96	Calculated Property
ρl	572.57	kg/m3	417.84	Calculated Property
ρl	515.18	kg/m3	450.73	Calculated Property
ρl	430.36	kg/m3	483.61	Calculated Property

Property	Value	Unit	Temperature (K)	Source
γ	[0.03; 0.01]	N/m	[186.15; 341.15]	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			4.85161e-02
Coefficient B			-1.04800e-04
Coefficient C			0.00000e+00
Coefficient D			0.00000e+00
Coefficient E			0.00000e+00
Temperature range, min.			186.15
Temperature range, max.			341.15
γ	0.03	N/m	186.15	Calculated Property
γ	0.03	N/m	203.37	Calculated Property
γ	0.03	N/m	220.59	Calculated Property
γ	0.02	N/m	237.82	Calculated Property
γ	0.02	N/m	255.04	Calculated Property
γ	0.02	N/m	272.26	Calculated Property
γ	0.02	N/m	289.48	Calculated Property
γ	0.02	N/m	306.71	Calculated Property
γ	0.01	N/m	323.93	Calculated Property
γ	0.01	N/m	341.15	Calculated Property
γ	[0.03; 6.92e-04]	N/m	[187.65; 483.61]	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			-9.26560e-03
Coefficient B			5.15620e+01
Coefficient C			-3.47630e+00
Coefficient D			1.26820e-03
Coefficient E			-7.92300e-06
Temperature range, min.			187.65
Temperature range, max.			483.61
γ	0.03	N/m	187.65	Calculated Property
γ	0.03	N/m	220.53	Calculated Property
γ	0.02	N/m	253.42	Calculated Property
γ	0.02	N/m	286.30	Calculated Property
γ	0.02	N/m	319.19	Calculated Property
γ	0.01	N/m	352.07	Calculated Property
γ	0.01	N/m	384.96	Calculated Property
γ	0.01	N/m	417.84	Calculated Property
γ	0.00	N/m	450.73	Calculated Property
γ	6.92e-04	N/m	483.61	Calculated Property

Property	Value	Unit	Temperature (K)	Source
λgas	[0.00; 0.09]	W/m×K	[187.65; 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			1.01490e-04
Coefficient B			1.02460e+00
Coefficient C			1.80970e+02
Coefficient D			9.31790e+04
Temperature range, min.			187.65
Temperature range, max.			1000.00
λgas	0.00	W/m×K	187.65	Calculated Property
λgas	0.01	W/m×K	277.91	Calculated Property
λgas	0.02	W/m×K	368.17	Calculated Property
λgas	0.03	W/m×K	458.43	Calculated Property
λgas	0.04	W/m×K	548.69	Calculated Property
λgas	0.05	W/m×K	638.96	Calculated Property
λgas	0.06	W/m×K	729.22	Calculated Property
λgas	0.07	W/m×K	819.48	Calculated Property
λgas	0.08	W/m×K	909.74	Calculated Property
λgas	0.09	W/m×K	1000.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
λliquid	[0.14; 0.08]	W/m×K	[187.65; 423.15]	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			6.77520e-02
Coefficient B			-4.62020e+02
Coefficient C			2.39970e+00
Coefficient D			-1.44530e-02
Coefficient E			2.98560e-06
Temperature range, min.			187.65
Temperature range, max.			423.15
λliquid	0.14	W/m×K	187.65	Calculated Property
λliquid	0.13	W/m×K	213.82	Calculated Property
λliquid	0.13	W/m×K	239.98	Calculated Property
λliquid	0.12	W/m×K	266.15	Calculated Property
λliquid	0.11	W/m×K	292.32	Calculated Property
λliquid	0.10	W/m×K	318.48	Calculated Property
λliquid	0.10	W/m×K	344.65	Calculated Property
λliquid	0.09	W/m×K	370.82	Calculated Property
λliquid	0.09	W/m×K	396.98	Calculated Property
λliquid	0.08	W/m×K	423.15	Calculated Property

Similar Compounds

Find more compounds similar to Diisopropyl ether.

Mixtures

• Diisopropyl ether + Acetone
• Diisopropyl ether + Cyclohexane
• Diisopropyl ether + Acetone + Cyclohexane
• Diisopropyl ether + Water
• Diisopropyl ether + Methyl Alcohol + Water
• Diisopropyl ether + Ethanol + Water
• 1-Propanol + Diisopropyl ether + Water
• Diisopropyl ether + 2-Propanol + Water
• Diisopropyl ether + 1-Butanol + Water
• Diisopropyl ether + Carbon dioxide
• Diisopropyl ether + Mercury
• Diisopropyl ether + Propanoic acid + Water
• 1-Propanol + Diisopropyl ether
• Toluene + Diisopropyl ether
• 1-Propanol + Toluene + Diisopropyl ether
• Diisopropyl ether + Furan, 2,5-dimethyl-
• Diisopropyl ether + Acetic acid, mercapto- + Water
• Diisopropyl ether + 1-Butanol
• Benzene + Diisopropyl ether
• Benzene + Diisopropyl ether + 1-Butanol

Find more mixtures with Diisopropyl ether.

Sources

• KDB Vapor Pressure Data
• 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
• Measurement of Vapor Liquid Equilibrium for the DME + Diisopropyl Ether Binary System and Correlation for the DME + CO2 + Diisopropyl Ether Ternary System
• Viscosities of Binary Mixtures Containing Isomeric Chlorobutanes and Diisopropylether: Experimental and Predicted Values
• Phase equilibria for binary systems of octane boosters with 2,2,4-trimethylpentane
• Solubility of 9-fluorenone, thianthrene and xanthene in organic solvents
• Isothermal vapour liquid equilibria in the binary and ternary systems composed of 2-propanol, diisopropyl ether and 4-methyl-2-pentanone
• Total pressure and excess Gibbs energy for the ternary mixture di-isopropyl ether + 1-propanol + benzene and its corresponding binary systems at 313.15K
• Phase equilibria properties of binary and ternary systems containing di-isopropyl ether + isobutanol + benzene at 313.15K
• Vapor liquid equilibria for binary and ternary mixtures of diisopropyl ether, ethanol, and 2,2,4-trimethylpentane at 101.3 kPa
• (Vapor + liquid) equilibrium of binary mixtures formed by N,N-dimethyl formamide with some compounds at 95.1 kPa
• Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
• Liquid liquid equilibria of ternary mixture (propargyl alcohol + diisopropyl ether +water)
• Effect of pressure and the capability of 2-methoxyethanol as a solvent in the behaviour of a diisopropyl ether isopropyl alcohol azeotropic mixture
• Measurement and correlation of vapor liquid equilibria for the system carbon dioxide diisopropyl ether
• Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
• Liquid liquid equilibria for the binary system of di-isopropyl ether (DIPE) +water in between 288.15 and 323.15K and the ternary systems of DIPE +water + C1 C4 alcohols at 298.15K
• Vapor liquid equilibria and interfacial tensions for the ternary system acetone + 2,2 -oxybis[propane] + cyclohexane and its constituent binary systems
• Isothermal vapor liquid equilibrium at 333.15K and excess molar volumes at 298.15K for the ternary system di-isopropyl ether + n-propyl alcohol + toluene and its binary subsystems
• Measurement and prediction of tie-line data for mixtures of (water + 1-propanol + diisopropyl ether): LLE diagrams as a function of temperature
• Phase equilibrium for the systems diisopropyl ether, isopropyl alcohol + 2,2,4-trimethylpentane and + n-heptane at 101.3 kPa
• Liquid + liquid equilibria for the quaternary systems of (water + acetic acid + mixed solvent) at 298.2 K and atmospheric pressure
• Experimental and predicted excess molar enthalpies of binary mixtures containing 2,2'-oxybis[propane], benzene, butan-1-ol, 2-methylpropan-1-ol, 2-methyl-2-ene-1-propanol at 303.15 K
• Liquid-liquid equilibrium for binary and ternary systems containing di-isopropyl ether (DIPE) and an imidazoliumbased ionic liquid at different temperatures
• Activity coefficients at infinite dilution of organic solutes in the ionic liquid 1-ethyl-3-methylimidazolium methanesulfonate
• Isothermal vapour-liquid equilibria and excess enthalpies for the binary mixtures containing an isomeric chlorobutane and diisopropyl ether
• Vapor-liquid equilibria at 333.15 K and excess molar volumes and deviations in molar refractivity at 298.15 K for mixtures of diisopropyl ether, ethanol and ionic liquids
• Quaternary phase equilibrium of water-carboxylic acid mixture (formic-propionic acid or acetic-propionic acid)-solvent liquid systems at 298.15 K
• Solubility of caprolactam in different organic solvents
• Vapour-liquid equilibria in binary and ternary systems composed of 2,3-dimethylbutane, diisopropyl ether, and 3-methyl-2-butanone at 313.15, 323.15 and 313.15 K
• Isobaric vapor liquid equilibrium and isothermal surface tensions of 2,2 -oxybis[propane] + 2,5-Dimethylfuran
• Experimental and theoretical study of interaction between organic compounds and 1- (4-sulfobutyl)-3-methylimidazolium based ionic liquids
• Ternary liquid-liquid equilibria of bis(trifluoromethylsulfonyl)-amidebased ionic liquids + 2-propanol + di-iso-propyl ether
• Experimental isobaric vapor-liquid equilibrium at atmospheric and sub-atmospheric pressures, excess molar volumes and deviations in molar refractivity from 293.15 K to 318.15 K of diisopropyl ether with methanol and isopropyl alcohol.
• Study of interaction between organic compounds and mono or dicationic oxygenated ionic liquids using gas chromatography
• Atmospheric densities and interfacial tensions for 1- alkanol (1-butanol to 1-octanol) + water and ether (MTBE, ETBE, DIPE, TAME and THP) + water demixed mixtures.
• Isobaric ternary vapour-liquid equilibrium of methanol(1) + diisopropyl ether(2) + isopropyl alcohol(3) along with methanol + isopropyl alcohol binary data at atmospheric and sub-atmospheric pressures
• 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
• High selective water/butan-1-ol separation on investigation of limiting activity coefficients with [P8,8,8,8][[NTf2] ionic liquid
• Speed of sound, density and derivative properties of diisopropyl ether under high pressure
• Separation of binary mixtures based on limiting activity coefficients data using specific ammonium-based ionic liquid and modelling of thermodynamic functions
• High pressure and high temperature volumetric properties of (2-propanol + diisopropyl ether) system
• Thermodynamics and activity coefficients at infinite dilution for organic solutes in the ionic liquid 1-butyl-1-methylpyrrolidinium dicyanamide
• New ionic liquid [P4,4,4,4][NTf2] in bio-butanol extraction on investigation of limiting activity coefficients
• Liquid-liquid equilibrium measurement and thermodynamics modeling for the systems water + thioglycolic acid + isopropyl ether/methyl tert-butyl ether at 298.15 and 308.15 K
• 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
• Volumetric properties of (N,N-dimethylformamide + aliphatic diethers) at Temperatures ranging from (298.15 to 358.15) K
• Quaternary (liquid + liquid) equilibria for (water + 1,1-dimethylethyl methyl ether + diisopropyl ether + toluene) at the temperature 298.15 K
• Systems with ionic liquids: Measurement of VLE and c1 data and prediction of their thermodynamic behavior using original UNIFAC, mod. UNIFAC(Do) and COSMO-RS(Ol)
• Phase equilibrium properties of binary and ternary systems containing di-isopropyl ether + 1-butanol + benzene at 313.15 K
• (Liquid + liquid) equilibria of (water + propionic acid + dipropyl ether or diisopropyl ether) at T = 298.2 K
• The thermodynamics of vaporization of ethyl tert-butyl ether, isobutyl tert-butyl ether, and di-isopropyl ether
• Volumetric properties of binary and ternary mixtures of diisopropyl ether, a,a,a-trifluorotoluene, 2,2,2-trifluoroethanol, and ethanol at a temperature 298.15 K and pressure 101 kPa
• Volumetric properties of binary mixtures of ethers and acetonitrile: Experimental results and application of the Prigogine Flory Patterson theory
• Isobaric (vapour + liquid + liquid) equilibrium data for (di-n-propyl ether + n-propyl alcohol + water) and (diisopropyl ether + isopropyl alcohol + water) systems at 100 kPa
• Thermodynamics and activity coefficients at infinite dilution measurements for organic solutes and water in the ionic liquid 1-butyl-1-methylpyrrolidinium tetracyanoborate
• Interactions of volatile organic compounds with the ionic liquid 1-ethyl-3-methylimidazolium 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
• Interactions of volatile organic compounds with the ionic liquids 1-butyl-1-methylpyrrolidinium tetracyanoborate and 1-butyl-1-methylpyrrolidinium bis(oxalato)borate
• Isothermal (vapour + liquid) equilibria for binary mixtures of diisopropyl ether with (methanol, or ethanol, or 1-butanol): Experimental data, correlations, and predictions
• 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
• Infinite dilution activity coefficients of volatile organic compounds in two ionic liquids composed of the tris(pentafluoroethyl) trifluorophosphate ([FAP]) anion and a functionalized cation
• Measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-butyl-1-methylpyrrolidinium tricyanomethanide
• Thermodynamic modeling of ternary and quaternary (liquid + liquid) systems containing water, FeCl3, HCl and diisopropyl ether
• Thermodynamics and activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-butyl-1-methylmorpholinium tricyanomethanide
• Thermodynamics and activity coefficients at infinite dilution for organic solutes, water and diols in the ionic liquid choline bis(trifluoromethylsulfonyl)imide
• (Solid + liquid) phase equilibria of tetraphenyl piperazine-1,4-diyldiphosphonate in pure solvents
• Liquid density of oxygenated additive 2,4-dimethyl-3-oxapentane at pressures up to 140 MPa and temperatures from (293.15 to 393.29) 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
• (Liquid + liquid) equilibria for (water + 1-propanol + diisopropyl ether + octane, or methylbenzene, or heptane) systems at T = 298.15 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
• 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
• Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
• Liquid densities and excess volumes of biofuel mixtures: (2-butanol + di-isopropyl ether) system at pressures up to 140 MPa and temperatures from 293.15 K to 393.28 K
• Separation of binary mixtures hexane/hex-1-ene, cyclohexane/cyclohexene and ethylbenzene/styrene based on limiting activity coefficients
• High pressure liquid densities and excess volumes of the (di-isopropyl ether + 1-hexanol) system
• 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
• Liquid-liquid equilibrium for ternary systems of water + 2,2,3,3-tetrafluoro-1-propanol + isopropyl ether/tert-butyl methyl ether at 298.2, 308.2 K
• The use of ionic liquids for separation of binary hydrocarbons mixtures based on gamma infinity data measurements
• Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
• Vapour-liquid equilibrium and extractive distillation for separation of azeotrope isopropyl alcohol and diisopropyl ether
• Separation of the mixture (isopropyl alcohol + diisopropyl ether + n-propanol): Entrainer selection, interaction exploration and vapour-liquid equilibrium measurements
• Density, viscosity, and speed of sound of binary liquid mixtures of vinyl acetate with butyl vinyl ether, diisopropyl ether, anisole and dibutyl ether
• Excess volumes, densities, speeds of sound and viscosities for the binary systems of diisopropyl ether with hydrocarbons at 303.15K
• Thermodynamic and acoustic properties of binary mixtures of ethers. III. Diisopropyl ether or oxolane with o- or m-toluidines at 303.15, 313.15 and 323.15 K
• Thermodynamic and acoustic properties of binary mixtures of ethers. IV. Diisopropyl ether or oxolane with N,N-dimethylaniline or N,Ndiethylaniline at 303.15, 313.15 and 323.15 K
• Thermodynamic and acoustic properties of binary mixtures of ethers. V. Diisopropyl ether or oxolane with 2- or 3-chloroanilines at 303.15, 313.15 and 323.15 K
• Correlation and prediction of the phase behavior and thermal properties of binary and ternary systems of 2,2 -oxybis[propane] + benzene, toluene, cyclohexane or n-heptane
• Tie-Line Data for Aqueous Mixtures of Butyric Acid with Diisopropyl Ether at Various Temperatures
• Activity Coefficients at Infinite Dilution of Organic Solutes and Water in Tributylethylphosphonium Diethylphosphate Using Gas Liquid Chromatography: Thermodynamic Properties of Mixtures Containing Ionic Liquids
• Measurement and Thermodynamic Modeling of Ternary (Liquid + Liquid) Equilibrium for Extraction of N,N-Dimethylacetamide from Aqueous Solution with Different Solvents
• High Pressure Volumetric Properties of the Binary Mixtures Di-isopropyl Ether + 2,2,4-Trimethylpentane
• High-Pressure Viscosity Measurements for the Binary Mixture HFE-7500 + Diisopropyl Ether
• Liquid-Liquid Equilibria of the System Water/Phosphoric Acid/ Diisopropyl Ether at (273.15, 283.15, and 293.15) K
• Excess Enthalpies of the Ternary Mixtures: Diisopropyl Ether + 3-Methylpentane + (Octane or Decane) at 298.15 K
• Vapor-Liquid Equilibria for the Binary Systems of Dimethoxymethane with Some Fuel Oxygenates
• Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
• Excess Molar Volumes and Surface Tensions of Xylene with Isopropyl Ether or Methyl tert-Butyl Ether at 298.15 K
• Measurement of Activity Coefficients at Infinite Dilution of Benzene, Toluene, Ethanol, Esters, Ketones, and Ethers at Various Temperatures in Water Using the Dilutor Technique
• Densities and Viscosities for Binary and Ternary Mixtures of Diisopropyl Ether, Ethanol, and Methylcyclohexane
• Ternary and Quaternary Liquid-Liquid Equilibria of Water + Methanol + Diisopropyl Ether and Water + Methanol + Diisopropyl Ether + Toluene Mixtures
• Vapor-Liquid Equilibrium of Binary and Ternary Mixtures Containing Isopropyl Ether, 2-Butanol, and Benzene at T ) 313.15 K
• Densities, Viscosities, and Refractive Indices for Binary and Ternary Mixtures of Diisopropyl Ether, Ethanol, and 2,2,4-Trimethylpentane
• Determination of Partitioning Coefficients of Numerous Organic Solutes between a Long-Chain Aliphatic Alcohol and the Gas Phase as a Function of Temperature
• Solubility of Anthracene in Binary Diisopropyl Ether + Alkane Solvent Mixtures at 298.15 K
• Liquid-Liquid Equilibria for the Ternary System Water (1) + Acetic acid (2) + Diisopropyl Ether (3) at (293.15, 303.15, and 313.15) K
• Volumetric, Acoustic, and Refractive Properties of Isomeric Chlorobutanes with Diisopropyl Ether
• Thermodynamic and Acoustic Properties of Binary Mixtures of Ethers. 2. Diisopropyl Ether with Arylamines at (303.15, 313.15, and 323.15) K and Application of ERAS Model to Aniline Mixtures with Diisopropyl Ether and Oxolane
• Activity Coefficients at Infinite Dilution of Organic Compounds in Four New Imidazolium-Based Ionic Liquids
• Measurement and Calculation of Liquid Liquid Equilibria of Ternary and Quaternary Systems Containing Water, Propan-1-ol, and 2,2,4-Trimethylpentane (TMP) with 2,2'-Oxybis(propane) (DIPE) or Dimethyl Carbonate (DMC)
• Partition Coefficients of Organic Compounds in Four New Tetraalkylammonium Bis(trifluoromethylsulfonyl)imide Ionic Liquids Using Inverse Gas Chromatography
• Interactions of Volatile Organic Compounds with the Ionic Liquid 1-Butyl-1-methylpyrrolidinium Dicyanamide
• Evaluation of the Performance of Trigeminal Tricationic Ionic Liquids for Separation Problems
• Excess Volumes of Ternary Mixtures 2,2,4-Trimethylpentane + Diisopropyl Ether or Methyl tert-Butyl Ether + Methanol, Ethanol, or 1-Propanol at 298.15 K
• Solid Liquid Phase Equilibrium and Solubility of Dibenzo[b,d]furan and 9H-Fluoren-9-one in Organic Solvents
• Activity Coefficients at Infinite Dilution for Organic Compounds Dissolved in 1-Alkyl-1-methylpyrrolidinium Bis(trifluoromethylsulfonyl)imide Ionic Liquids Having Six-, Eight-, and Ten-Carbon Alkyl Chains
• Vapor Liquid Liquid Equilibria Measurements for the Dehydration of Ethanol, Isopropanol, and n-Propanol via Azeotropic Distillation Using DIPE and Isooctane as Entrainers
• Vapor Liquid Equilibrium for Ternary and Binary Mixtures of 2-Isopropoxypropane, 2-Propanol, and N,N-Dimethylacetamide at 101.3 kPa
• Activity Coefficients at Infinite Dilution for Organic Solutes Dissolved in Three 1-Alkyl-1-methylpyrrolidinium Bis(trifluoromethylsulfonyl)imide Ionic Liquids Bearing Short Linear Alkyl Side Chains of Three to Five Carbons
• Infinite Dilution Activity Coefficients of Solutes Dissolved in Two Trihexyl(tetradecyl)phosphonium Ionic Liquids
• Deduction of Physicochemical Properties from Solubilities: 2,4-Dihydroxybenzophenone, Biotin, and Caprolactam as Examples
• Solubility of Anthracene in Binary Diisopropyl Ether + Alcohol Solvent Mixtures at 298.15 K
• Isothermal VLE and VE at 303.15 K for the Binary and Ternary Mixtures of Di-isopropyl Ether (DIPE) + 1-Propanol + 2,2,4-Trimethylpentane
• Solubilities of Adefovir Dipivoxil in Different Binary Solvents at 298.15 K
• Determination and Correlation of Excess Molar Enthalpies of the Binary Carbon Dioxide + Diisopropyl Ether (DIPE) System at Temperatures from (298.15 to 308.15) K and Pressures from (5.0 to 7.5) MPa
• Isobaric Vapor-Liquid Equilibria for Binary and Ternary Mixtures of Diisopropyl Ether, 2-Propyl Alcohol, and 3-Methyl-1-Butanol
• Viscosity and Density Measurements of Diisopropyl Ether and Dibutyl Ether at Different Temperatures and Pressures
• Activity Coefficients at Infinite Dilution of Organic Compounds in 1-Butyl-3-methylimidazolium Tetrafluoroborate Using Inverse Gas Chromatography
• Activity Coefficients at Infinite Dilution of Organic Compounds in Trihexyl(tetradecyl)phosphonium Bis(trifluoromethylsulfonyl)imide Using Inverse Gas Chromatography
• sobaric Vapor-Liquid Equilibria for Binary and Ternary Mixtures of Diisopropyl Ether, 2-Propyl Alcohol, and n-Butyl Propionate at 101.3 kPa
• Isothermal Vapor-Liquid Equilibrium at 333.15 K and Excess Molar Volumes, Refractive Indices, and Excess Molar Enthalpies at 303.15 K for the Binary and Ternary Mixtures of Di-isopropyl Ether, Ethanol, and 2,2,4-Trimethylpentane
• Isobaric Vapor-Liquid Equilibria at 101.32 kPa and Densities, Speeds of Sound, and Refractive Indices at 298.15 K for MTBE or DIPE or TAME + 1-Propanol Binary Systems
• Partition Coefficients of Organic Compounds in New Imidazolium and Tetralkylammonium Based Ionic Liquids Using Inverse Gas Chromatography
• 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
• Solubility of Avermectin B1a in Some Pure and Mixed Solvents from (278.2 to 318.2) K
• Study of Ether-, Alcohol-, or Cyano-Functionalized Ionic Liquids Using Inverse Gas Chromatography
• Thermodynamic Properties of Binary and Ternary Mixtures Containing Di-isopropyl Ether, 2-Propanol, and Benzene at T = 313.15 K
• 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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