1-Butanol, 3-methyl-, acetate (CAS 123-92-2)

Please note that you need to enable javascript to get access to all the properties. Here is how to do it for Internet Explorer and for Firefox.

Physical Properties

Property	Value	Unit	Source
ω	0.4457		Relay (1.0) Calculated Property
μ	1.80	debye	KDB
Δ_fG°	-228.30	kJ/mol	Joback Calculated Property
Δ_fH°_gas	-518.76	kJ/mol	Relay (1.0) Calculated Property
Δ_fusH°	13.15	kJ/mol	Joback Calculated Property
Δ_vapH°	46.40 ± 0.20	kJ/mol	NIST
IE	9.89	eV	Relay (1.0) Calculated Property
log₁₀WS	[-1.92; -1.92]
log₁₀WS	-1.92		Aq. Solubility Prediction
log₁₀WS	-1.92		Estimated Solubility
logP_oct/wat	1.596		Crippen Calculated Property
McVol	116.930	ml/mol	McGowan Calculated Property
NFPA Fire	3		KDB
NFPA Health	1		KDB
P_c	2760.00 ± 20.00	kPa	NIST
I_np	[836.00; 893.00]
I_np	861.32		NIST
I_np	858.00		NIST
I_np	857.80		NIST
I_np	862.00		NIST
I_np	859.70		NIST
I_np	859.00		NIST
I_np	867.00		NIST
I_np	854.00		NIST
I_np	866.00		NIST
I_np	862.00		NIST
I_np	867.00		NIST
I_np	866.00		NIST
I_np	866.00		NIST
I_np	865.00		NIST
I_np	Outlier 836.00		NIST
I_np	859.00		NIST
I_np	883.00		NIST
I_np	878.00		NIST
I_np	876.00		NIST
I_np	869.00		NIST
I_np	876.00		NIST
I_np	877.00		NIST
I_np	876.00		NIST
I_np	862.00		NIST
I_np	876.00		NIST
I_np	875.00		NIST
I_np	876.00		NIST
I_np	855.50		NIST
I_np	851.00		NIST
I_np	876.00		NIST
I_np	876.00		NIST
I_np	860.00		NIST
I_np	855.00		NIST
I_np	883.00		NIST
I_np	875.00		NIST
I_np	876.00		NIST
I_np	878.00		NIST
I_np	867.00		NIST
I_np	884.00		NIST
I_np	874.60		NIST
I_np	875.00		NIST
I_np	876.00		NIST
I_np	876.00		NIST
I_np	858.00		NIST
I_np	858.00		NIST
I_np	858.00		NIST
I_np	859.00		NIST
I_np	855.00		NIST
I_np	856.00		NIST
I_np	859.00		NIST
I_np	860.00		NIST
I_np	853.00		NIST
I_np	853.00		NIST
I_np	885.00		NIST
I_np	853.00		NIST
I_np	875.70		NIST
I_np	874.00		NIST
I_np	873.00		NIST
I_np	875.00		NIST
I_np	855.00		NIST
I_np	881.00		NIST
I_np	878.00		NIST
I_np	876.00		NIST
I_np	872.00		NIST
I_np	867.00		NIST
I_np	859.00		NIST
I_np	877.00		NIST
I_np	876.00		NIST
I_np	858.00		NIST
I_np	870.00		NIST
I_np	876.00		NIST
I_np	879.00		NIST
I_np	883.00		NIST
I_np	865.00		NIST
I_np	878.00		NIST
I_np	876.00		NIST
I_np	852.00		NIST
I_np	878.00		NIST
I_np	881.00		NIST
I_np	875.00		NIST
I_np	875.00		NIST
I_np	878.00		NIST
I_np	877.00		NIST
I_np	877.00		NIST
I_np	875.00		NIST
I_np	882.60		NIST
I_np	876.00		NIST
I_np	865.00		NIST
I_np	878.00		NIST
I_np	878.00		NIST
I_np	858.00		NIST
I_np	864.00		NIST
I_np	876.00		NIST
I_np	875.00		NIST
I_np	880.00		NIST
I_np	865.00		NIST
I_np	886.00		NIST
I_np	867.00		NIST
I_np	860.00		NIST
I_np	860.00		NIST
I_np	878.00		NIST
I_np	864.00		NIST
I_np	860.00		NIST
I_np	876.00		NIST
I_np	853.00		NIST
I_np	856.00		NIST
I_np	850.00		NIST
I_np	856.00		NIST
I_np	857.00		NIST
I_np	860.00		NIST
I_np	860.00		NIST
I_np	866.00		NIST
I_np	866.00		NIST
I_np	860.00		NIST
I_np	861.00		NIST
I_np	860.00		NIST
I_np	852.00		NIST
I_np	849.00		NIST
I_np	864.00		NIST
I_np	882.00		NIST
I_np	880.00		NIST
I_np	864.00		NIST
I_np	886.00		NIST
I_np	866.00		NIST
I_np	884.00		NIST
I_np	Outlier 893.00		NIST
I_np	884.00		NIST
I_np	851.00		NIST
I_np	876.00		NIST
I_np	875.00		NIST
I_np	852.00		NIST
I_np	876.00		NIST
I_np	851.00		NIST
I_np	871.00		NIST
I_np	878.00		NIST
I_np	859.00		NIST
I_np	867.00		NIST
I_np	Outlier 843.00		NIST
I_np	875.00		NIST
I_np	860.00		NIST
I_np	882.00		NIST
I_np	876.00		NIST
I_np	Outlier 843.00		NIST
I_np	Outlier 843.00		NIST
I_np	876.00		NIST
I_np	878.00		NIST
I_np	853.00		NIST
I_np	876.00		NIST
I_np	860.00		NIST
I_np	876.00		NIST
I_np	860.00		NIST
I_np	882.00		NIST
I_np	878.00		NIST
I_np	878.00		NIST
I_np	860.00		NIST
I_np	880.00		NIST
I_np	877.00		NIST
I_np	849.00		NIST
I_np	859.00		NIST
I_np	880.00		NIST
I_np	880.00		NIST
I_np	847.00		NIST
I_np	854.00		NIST
I_np	859.00		NIST
I_np	884.00		NIST
I_np	855.00		NIST
I_np	858.00		NIST
I_np	853.00		NIST
I	[1096.00; 1168.00]
I	1131.00		NIST
I	Outlier 1096.00		NIST
I	1135.00		NIST
I	1125.00		NIST
I	1126.00		NIST
I	1126.00		NIST
I	1124.00		NIST
I	1126.00		NIST
I	1130.00		NIST
I	1120.00		NIST
I	1102.00		NIST
I	1105.00		NIST
I	1117.00		NIST
I	1121.00		NIST
I	1126.00		NIST
I	1111.00		NIST
I	1130.00		NIST
I	1131.00		NIST
I	1101.00		NIST
I	1115.00		NIST
I	1121.00		NIST
I	1132.00		NIST
I	1143.00		NIST
I	1123.00		NIST
I	1126.00		NIST
I	1125.00		NIST
I	1112.00		NIST
I	1134.00		NIST
I	1114.00		NIST
I	1125.00		NIST
I	1139.00		NIST
I	1121.00		NIST
I	1117.00		NIST
I	1118.00		NIST
I	1115.00		NIST
I	1107.00		NIST
I	1116.00		NIST
I	1126.00		NIST
I	1126.00		NIST
I	1118.00		NIST
I	1119.00		NIST
I	1123.00		NIST
I	1127.00		NIST
I	1123.00		NIST
I	1120.00		NIST
I	1120.00		NIST
I	1115.00		NIST
I	1115.00		NIST
I	1117.00		NIST
I	1117.00		NIST
I	1116.00		NIST
I	1127.00		NIST
I	1125.00		NIST
I	1127.00		NIST
I	1137.00		NIST
I	1132.00		NIST
I	1132.00		NIST
I	1112.00		NIST
I	1118.00		NIST
I	1113.00		NIST
I	1113.00		NIST
I	1125.00		NIST
I	1132.00		NIST
I	1125.00		NIST
I	1129.00		NIST
I	1115.00		NIST
I	1132.00		NIST
I	1125.00		NIST
I	1114.00		NIST
I	1122.00		NIST
I	1128.00		NIST
I	1128.00		NIST
I	1114.00		NIST
I	1119.00		NIST
I	1122.00		NIST
I	1125.00		NIST
I	1116.00		NIST
I	1112.00		NIST
I	1140.00		NIST
I	1147.00		NIST
I	1111.00		NIST
I	1102.00		NIST
I	1137.00		NIST
I	1102.00		NIST
I	1124.00		NIST
I	1129.00		NIST
I	1105.00		NIST
I	1128.00		NIST
I	1103.00		NIST
I	1147.00		NIST
I	1110.00		NIST
I	1133.00		NIST
I	1118.00		NIST
I	1134.00		NIST
I	1120.00		NIST
I	1118.00		NIST
I	1130.00		NIST
I	1128.00		NIST
I	1132.00		NIST
I	1112.00		NIST
I	1108.00		NIST
I	1143.00		NIST
I	1128.00		NIST
I	1142.00		NIST
I	1128.00		NIST
I	1128.00		NIST
I	1101.00		NIST
I	1101.00		NIST
I	1130.00		NIST
I	1140.00		NIST
I	1110.00		NIST
I	1110.00		NIST
I	1118.00		NIST
I	1118.00		NIST
I	1122.00		NIST
I	1122.00		NIST
I	1114.00		NIST
I	1110.00		NIST
I	1127.00		NIST
I	1127.00		NIST
I	1127.00		NIST
I	1127.00		NIST
I	1129.00		NIST
I	1124.00		NIST
I	1124.00		NIST
I	Outlier 1165.00		NIST
I	Outlier 1166.00		NIST
I	Outlier 1167.00		NIST
I	1113.00		NIST
I	1132.00		NIST
I	1123.00		NIST
I	1132.00		NIST
I	1135.00		NIST
I	1122.00		NIST
I	Outlier 1098.00		NIST
I	1116.00		NIST
I	1136.00		NIST
I	1117.00		NIST
I	1130.00		NIST
I	1125.00		NIST
I	1136.00		NIST
I	1110.00		NIST
I	1111.00		NIST
I	1131.00		NIST
I	1115.00		NIST
I	1132.00		NIST
I	1143.00		NIST
I	1121.00		NIST
I	1110.00		NIST
I	1136.00		NIST
I	1126.00		NIST
I	1100.00		NIST
I	1114.00		NIST
I	1114.00		NIST
I	Outlier 1168.00		NIST
I	1110.00		NIST
I	1115.00		NIST
I	1110.00		NIST
T_boil	[415.15; 415.70]	K
T_boil	415.70	K	KDB
T_boil	415.24	K	Effect of Pressure on the Azeotrope of the Mixture Isoamyl Acetate Isoamyl Alcohol at 50.00, 101.32, 250.00, and 350.00 kPa
T_boil	415.15	K	Isobaric Vapor-Liquid Equilibrium Measurements for Separation of Azeotrope (Methanol + Methyl Acetate)
T_c	[586.10; 599.33]	K
T_c	599.00	K	KDB
T_c	586.10 ± 0.60	K	NIST
T_c	599.33 ± 6.00	K	NIST
T_fus	[189.53; 194.60]	K
T_fus	194.60	K	KDB
T_fus	189.53	K	Aq. Solubility Prediction
V_c	0.432	m³/kmol	Relay (1.0) Calculated Property

Temperature Dependent Properties

Property	Value	Unit	Temperature (K)	Source
C_p,gas	[238.73; 301.45]	J/mol×K	[435.41; 615.76]

C_p,gas	238.73	J/mol×K	435.41	Joback Calculated Property
C_p,gas	250.17	J/mol×K	465.47	Joback Calculated Property
C_p,gas	261.22	J/mol×K	495.53	Joback Calculated Property
C_p,gas	271.87	J/mol×K	525.58	Joback Calculated Property
C_p,gas	282.12	J/mol×K	555.64	Joback Calculated Property
C_p,gas	291.98	J/mol×K	585.70	Joback Calculated Property
C_p,gas	301.45	J/mol×K	615.76	Joback Calculated Property
η	[0.0004810; 0.0009400]	Pa×s	[288.15; 343.15]

η	0.0009400	Pa×s	288.15	Densities and Viscosities of Binary Mixtures of Isoamyl Acetate, Ethyl Caproate, Ethyl Benzoate, Isoamyl Butyrate, Ethyl Phenylacetate, and Ethyl Caprylate with Ethanol at T = (288.15, 298.15, 308.15, and 318.15) K
η	0.0008880	Pa×s	293.15	Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
η	0.0008270	Pa×s	298.15	Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
η	0.0008040	Pa×s	298.15	Densities and Viscosities of Binary Mixtures of Isoamyl Acetate, Ethyl Caproate, Ethyl Benzoate, Isoamyl Butyrate, Ethyl Phenylacetate, and Ethyl Caprylate with Ethanol at T = (288.15, 298.15, 308.15, and 318.15) K
η	0.0007810	Pa×s	298.15	Densities, Excess Molar Volumes, Viscosities, Speeds of Sound, Excess Isentropic Compressibilities, and Relative Permittivities for Alkyl (Methyl, Ethyl, Butyl, and Isoamyl) Acetates + Glycols at Different Temperatures
η	0.0007410	Pa×s	303.15	Thermophysical Properties of Isoamyl Acetate or Methyl Benzoate + Hydrocarbon Binary Mixtures, at (303.15 and 313.15) K
η	0.0007730	Pa×s	303.15	Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
η	0.0007470	Pa×s	308.15	Densities, Excess Molar Volumes, Viscosities, Speeds of Sound, Excess Isentropic Compressibilities, and Relative Permittivities for Alkyl (Methyl, Ethyl, Butyl, and Isoamyl) Acetates + Glycols at Different Temperatures
η	0.0007240	Pa×s	308.15	Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
η	0.0007040	Pa×s	308.15	Densities and Viscosities of Binary Mixtures of Isoamyl Acetate, Ethyl Caproate, Ethyl Benzoate, Isoamyl Butyrate, Ethyl Phenylacetate, and Ethyl Caprylate with Ethanol at T = (288.15, 298.15, 308.15, and 318.15) K
η	0.0006780	Pa×s	313.15	Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
η	0.0006490	Pa×s	313.15	Thermophysical Properties of Isoamyl Acetate or Methyl Benzoate + Hydrocarbon Binary Mixtures, at (303.15 and 313.15) K
η	0.0006270	Pa×s	318.15	Densities and Viscosities of Binary Mixtures of Isoamyl Acetate, Ethyl Caproate, Ethyl Benzoate, Isoamyl Butyrate, Ethyl Phenylacetate, and Ethyl Caprylate with Ethanol at T = (288.15, 298.15, 308.15, and 318.15) K
η	0.0006380	Pa×s	318.15	Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
η	0.0006010	Pa×s	323.15	Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
η	0.0005670	Pa×s	328.15	Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
η	0.0005360	Pa×s	333.15	Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
η	0.0005070	Pa×s	338.15	Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
η	0.0004810	Pa×s	343.15	Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
Δ_vapH	[44.30; 46.80]	kJ/mol	[291.50; 366.00]
Δ_vapH	46.80 ± 0.20	kJ/mol	291.50	NIST
Δ_vapH	46.40	kJ/mol	332.50	NIST
Δ_vapH	45.10	kJ/mol	340.50	NIST
Δ_vapH	44.30	kJ/mol	366.00	NIST
P_vap	[50.00; 100.00]	kPa	[391.07; 413.46]
P_vap	50.00	kPa	391.07	Isobaric Vapor Liquid Equilibria for Binary Mixtures of Isoamyl Acetate + Ethyl Acetate at 50 and 100 kPa
P_vap	100.00	kPa	413.46	Isobaric Vapor Liquid Equilibria for Binary Mixtures of Isoamyl Acetate + Ethyl Acetate at 50 and 100 kPa
n₀	[1.39750; 1.39893]		[293.20; 298.15]

n₀	1.39760		293.20	Experimental and Correlational Study of Phase Equilibria in Aqueous Solutions of Formic and Butyric Acids with Isoamyl Acetate and Methyl Isoamyl Ketone at T = 298.15 K
n₀	1.39750		298.15	Application of the ERAS model to volumetric properties of binary mixtures of banana oil with primary and secondary alcohols (C1- C4) at different temperatures
n₀	1.39770		298.15	Isobaric Vapor Liquid Equilibrium for Binary and Ternary Systems of Isoamyl Alcohol + Isoamyl Acetate + Dimethyl Sulfoxide at 101.33 kPa
n₀	1.39842		298.15	Vapor-Liquid Equilibrium Data for Binary Mixtures of Dimethyl Carbonate with Methyl Acetate, Ethyl Acetate, n-Propyl Acetate, Isopropyl Acetate, n-Butyl Acetate, and Isoamyl Acetate at 93.13 kPa
n₀	1.39893		298.15	Isobaric Vapor-Liquid Equilibrium for Binary Mixtures of 3-Methyl-1-butanol + 3-Methyl-1-butyl Ethanoate and 1-Pentanol + Pentyl Ethanoate at 101.3 kPa
ρ_l	[833.30; 876.00]	kg/m³	[288.00; 333.15]

ρ_l	876.00	kg/m³	288.00	KDB
ρ_l	872.90	kg/m³	293.15	Experimental High-Temperature, High-Pressure Density Measurement and Perturbed-Chain Statistical Associating Fluid Theory Modeling of Dimethyl Sulfoxide, Isoamyl Acetate, and Benzyl Alcohol
ρ_l	872.49	kg/m³	293.20	Liquid-liquid equilibrium data for ternary systems of water + acetic acid + acetate esters at 293.2 K and 303.2 K and ~ 95 kPa
ρ_l	867.36	kg/m³	298.15	Volumetric Properties of 3-Methylbutyl Ethanoate with Ethyl Acrylate, Butyl Acrylate, Methyl Methacrylate, and Styrene at 25 C
ρ_l	868.00	kg/m³	298.15	Experimental High-Temperature, High-Pressure Density Measurement and Perturbed-Chain Statistical Associating Fluid Theory Modeling of Dimethyl Sulfoxide, Isoamyl Acetate, and Benzyl Alcohol
ρ_l	867.91	kg/m³	298.15	Refractive Indices and Surface Tensions of Binary Mixtures of Isoamyl Acetate, Ethyl Caproate, Ethyl Benzoate, Isoamyl Butyrate, Ethyl Phenylacetate, and Ethyl Caprylate with Ethanol at (288.15, 298.15, 308.15, and 318.15) K
ρ_l	866.70	kg/m³	298.20	Experimental study of phase equilibria in aqueous mixtures of phosphoric acid with isoamyl acetate and methyl isoamyl ketone at T = (298.2, 308.2, and 318.2) K
ρ_l	853.30	kg/m³	313.15	Experimental High-Temperature, High-Pressure Density Measurement and Perturbed-Chain Statistical Associating Fluid Theory Modeling of Dimethyl Sulfoxide, Isoamyl Acetate, and Benzyl Alcohol
ρ_l	852.64	kg/m³	313.20	Liquid-liquid equilibrium data for ternary systems of water + acetic acid + acetate esters at 293.2 K and 303.2 K and ~ 95 kPa
ρ_l	833.30	kg/m³	333.15	Experimental High-Temperature, High-Pressure Density Measurement and Perturbed-Chain Statistical Associating Fluid Theory Modeling of Dimethyl Sulfoxide, Isoamyl Acetate, and Benzyl Alcohol
γ	[0.02; 0.03]	N/m	[288.15; 358.15]

γ	0.03	N/m	288.15	Densities, Viscosities, Refractive Indices, and Surface Tensions for 12 Flavor Esters from T ) 288.15 K to T ) 358.15 K
γ	0.02	N/m	298.15	Densities, Viscosities, Refractive Indices, and Surface Tensions for 12 Flavor Esters from T ) 288.15 K to T ) 358.15 K
γ	0.02	N/m	308.15	Densities, Viscosities, Refractive Indices, and Surface Tensions for 12 Flavor Esters from T ) 288.15 K to T ) 358.15 K
γ	0.02	N/m	318.15	Densities, Viscosities, Refractive Indices, and Surface Tensions for 12 Flavor Esters from T ) 288.15 K to T ) 358.15 K
γ	0.02	N/m	328.15	Densities, Viscosities, Refractive Indices, and Surface Tensions for 12 Flavor Esters from T ) 288.15 K to T ) 358.15 K
γ	0.02	N/m	338.15	Densities, Viscosities, Refractive Indices, and Surface Tensions for 12 Flavor Esters from T ) 288.15 K to T ) 358.15 K
γ	0.02	N/m	348.15	Densities, Viscosities, Refractive Indices, and Surface Tensions for 12 Flavor Esters from T ) 288.15 K to T ) 358.15 K
γ	0.02	N/m	358.15	Densities, Viscosities, Refractive Indices, and Surface Tensions for 12 Flavor Esters from T ) 288.15 K to T ) 358.15 K

Pressure Dependent Properties

Property	Value	Unit	Pressure (kPa)	Source
T_boil	[365.29; 431.61]	K	[20.00; 160.01]

T_boil	365.29	K	20.00	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	376.06	K	29.98	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	384.31	K	40.01	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	391.07	K	49.99	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	396.76	K	60.00	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	401.72	K	70.00	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	406.18	K	80.01	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	410.24	K	90.00	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	413.90	K	100.01	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	417.15	K	110.00	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	420.43	K	119.99	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	423.46	K	130.00	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	426.33	K	139.99	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	429.05	K	149.99	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boil	431.61	K	160.01	Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
T_boilr	415.20	K	101.00	NIST

Datasets

Mass density, kg/m3

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Mass density, kg/m3 - Liquid
298.15	100.00	867.3
Reference

Correlations

Property	Value	Unit	Temperature (K)	Source
P_vap	[1.33; 202.63]	kPa	[311.22; 438.68]	The Yaws Handbook of Vapor Pressure
Equation			ln(Pvp) = A + B/(T + C)
Coefficient A			1.53486e+01
Coefficient B			-3.83541e+03
Coefficient C			-5.65620e+01
Temperature range, min.			311.22
Temperature range, max.			438.68

P_vap	1.33	kPa	311.22	Calculated Property
P_vap	2.95	kPa	325.38	Calculated Property
P_vap	6.02	kPa	339.54	Calculated Property
P_vap	11.49	kPa	353.71	Calculated Property
P_vap	20.66	kPa	367.87	Calculated Property
P_vap	35.32	kPa	382.03	Calculated Property
P_vap	57.73	kPa	396.19	Calculated Property
P_vap	90.72	kPa	410.36	Calculated Property
P_vap	137.69	kPa	424.52	Calculated Property
P_vap	202.63	kPa	438.68	Calculated Property
P_vap	[2.06e-05; 2676.19]	kPa	[194.65; 599.00]	KDB Vapor Pressure Data
Equation			ln(Pvp) = A + B/T + Cln(T) + DT^2
Coefficient A			7.60348e+01
Coefficient B			-7.92872e+03
Coefficient C			-8.76739e+00
Coefficient D			3.24333e-06
Temperature range, min.			194.65
Temperature range, max.			599.00

P_vap	2.06e-05	kPa	194.65	Calculated Property
P_vap	7.38e-03	kPa	239.58	Calculated Property
P_vap	0.33	kPa	284.51	Calculated Property
P_vap	4.44	kPa	329.43	Calculated Property
P_vap	28.83	kPa	374.36	Calculated Property
P_vap	115.89	kPa	419.29	Calculated Property
P_vap	336.66	kPa	464.22	Calculated Property
P_vap	779.09	kPa	509.14	Calculated Property
P_vap	1532.08	kPa	554.07	Calculated Property
P_vap	2676.19	kPa	599.00	Calculated Property

Similar Compounds

Propan-1,3-dioic acid, di[3-methylbutyl] ester.

Dichloroacetic acid 3-methylbutyl ester.

Butanoic acid, 3-methyl-, 3-methylbutyl ester.

Acetic acid, dibromo, 3-methylbutyl ester.

Acetic acid, trifluoro-, 3-methylbutyl ester.

Propanoic acid, 2-methyl-, 3-methylbutyl ester.

Trichloroacetic acid 3-methylbutyl ester.

Acetic acid, tribromo, 3-methylbutyl ester.

Find more compounds similar to 1-Butanol, 3-methyl-, acetate.

Mixtures

Find more mixtures with 1-Butanol, 3-methyl-, acetate.

Sources

KDB Vapor Pressure Data
Cheméo Relay (1.0)
Crippen Method
Volumetric Properties of 3-Methylbutyl Ethanoate with Ethyl Acrylate, Butyl Acrylate, Methyl Methacrylate, and Styrene at 25 C
Experimental study of phase equilibria in aqueous mixtures of phosphoric acid with isoamyl acetate and methyl isoamyl ketone at T = (298.2, 308.2, and 318.2) K
Phase behavior of binary mixture for the isoalkyl acetate in supercritical carbon dioxide
Liquid-liquid equilibrium data for ternary systems of water + acetic acid + acetate esters at 293.2 K and 303.2 K and ~ 95 kPa
Application of the ERAS model to volumetric properties of binary mixtures of banana oil with primary and secondary alcohols (C1- C4) at different temperatures
Studies on liquid liquid interactions of some ternary mixtures by density, viscosity, ultrasonic speed and refractive index measurements
Effect of Pressure on the Azeotrope of the Mixture Isoamyl Acetate Isoamyl Alcohol at 50.00, 101.32, 250.00, and 350.00 kPa
Vapor Liquid Equilibrium for Binary Mixtures of Acetates in the Direct Esterification of Fusel Oil
Isobaric Vapor Liquid Equilibrium for Binary and Ternary Systems of Isoamyl Alcohol + Isoamyl Acetate + Dimethyl Sulfoxide at 101.33 kPa
Vapor-Liquid Equilibrium Data for Binary Mixtures of Dimethyl Carbonate with Methyl Acetate, Ethyl Acetate, n-Propyl Acetate, Isopropyl Acetate, n-Butyl Acetate, and Isoamyl Acetate at 93.13 kPa
Isobaric Vapor-Liquid Equilibrium Measurements for Separation of Azeotrope (Methanol + Methyl Acetate)
Isobaric Vapor Liquid Equilibria for Binary Mixtures of Isoamyl Acetate + Ethyl Acetate at 50 and 100 kPa
Experimental High-Temperature, High-Pressure Density Measurement and Perturbed-Chain Statistical Associating Fluid Theory Modeling of Dimethyl Sulfoxide, Isoamyl Acetate, and Benzyl Alcohol
Isobaric Vapor-Liquid Equilibria of Binary Mixtures of Diethyl Carbonate with Isopropyl Acetate, sec-Butyl Acetate, or Isoamyl Acetate at 101.3 kPa
Densities, Excess Molar Volumes, Viscosities, Speeds of Sound, Excess Isentropic Compressibilities, and Relative Permittivities for Alkyl (Methyl, Ethyl, Butyl, and Isoamyl) Acetates + Glycols at Different Temperatures
Liquid-Liquid Equilibria for the Ternary Systems of (Water + Tetrahydrofuran + Polar Solvent) at 298.15 K
Density and Viscosity Correlation for Several Common Fragrance and Flavor Esters
Densities, Viscosities, Refractive Indices, and Surface Tensions for 12 Flavor Esters from T ) 288.15 K to T ) 358.15 K
Densities and Viscosities of Binary Mixtures of Isoamyl Acetate, Ethyl Caproate, Ethyl Benzoate, Isoamyl Butyrate, Ethyl Phenylacetate, and Ethyl Caprylate with Ethanol at T = (288.15, 298.15, 308.15, and 318.15) K
Refractive Indices and Surface Tensions of Binary Mixtures of Isoamyl Acetate, Ethyl Caproate, Ethyl Benzoate, Isoamyl Butyrate, Ethyl Phenylacetate, and Ethyl Caprylate with Ethanol at (288.15, 298.15, 308.15, and 318.15) K
Vapor-Liquid Equilibrium for Carbon Dioxide + Isopropyl, Isobutyl, and Isoamyl Acetates
Experimental and Correlational Study of Phase Equilibria in Aqueous Solutions of Formic and Butyric Acids with Isoamyl Acetate and Methyl Isoamyl Ketone at T = 298.15 K
Thermophysical Properties of Isoamyl Acetate or Methyl Benzoate + Hydrocarbon Binary Mixtures, at (303.15 and 313.15) K
Isobaric Vapor-Liquid Equilibrium for Binary Mixtures of 3-Methyl-1-butanol + 3-Methyl-1-butyl Ethanoate and 1-Pentanol + Pentyl Ethanoate at 101.3 kPa
Joback Method
KDB
Aqueous Solubility Prediction Method
Estimated Solubility Method
McGowan Method
NIST Webbook
The Yaws Handbook of Vapor Pressure

Note: Cheméo is only indexing the data, follow the source links to retrieve the latest data. The source is also providing more information like the publication year, authors and more. Take the time to validate and double check the source of the data.
Outlier This icon means that the value is more than 2 standard deviations away from the property mean.

Chemical Properties of 1-Butanol, 3-methyl-, acetate (CAS 123-92-2)