Chemical Properties of n-Propyl acetate (CAS 109-60-4)

InChI

InChI=1S/C5H10O2/c1-3-4-7-5(2)6/h3-4H2,1-2H3

InChI Key

YKYONYBAUNKHLG-UHFFFAOYSA-N

Formula

C5H10O2

SMILES

CCCOC(C)=O

Molecular Weight¹

102.13

CAS

109-60-4

Other Names

• 1-Acetoxypropane
• 1-Propyl acetate
• Acetate de propyle normal
• Acetic acid n-propyl ester
• Acetic acid, propyl ester
• CH3COOCH2CH2CH3
• NSC 72025
• Octan propylu
• Propyl acetate
• Propyl ester of acetic acid
• Propyl ethanoate
• Propylester kyseliny octove
• UN 1276
• ethanoic acid, propyl ester
• n-Propanol acetate
• n-Propyl ethanoate

• ω : Acentric Factor.
• PAff : Proton affinity (kJ/mol).
• BasG : Gas basicity (kJ/mol).
• C_p,gas : Ideal gas heat capacity (J/mol×K).
• C_p,liquid : Liquid phase heat capacity (J/mol×K).
• η : Dynamic viscosity (Pa×s).
• Δ_fG° : Standard Gibbs free energy of formation (kJ/mol).
• Δ_fH°_gas : Enthalpy of formation at standard conditions (kJ/mol).
• Δ_fusH° : Enthalpy of fusion at standard conditions (kJ/mol).
• Δ_vapH° : Enthalpy of vaporization at standard conditions (kJ/mol).
• Δ_vapH : Enthalpy of vaporization at a given temperature (kJ/mol).
• IE : Ionization energy (eV).
• log₁₀WS : Log10 of Water solubility in mol/l.
• logP_oct/wat : Octanol/Water partition coefficient.
• McVol : McGowan's characteristic volume (ml/mol).
• P_c : Critical Pressure (kPa).
• P_vap : Vapor pressure (kPa).
• n₀ : Refractive Index.
• ρ_c : Critical density (kg/m³).
• ρ_l : Liquid Density (kg/m³).
• I_np : Non-polar retention indices.
• I : Polar retention indices.
• γ : Surface Tension (N/m).
• T_boil : Normal Boiling Point Temperature (K).
• T_boil : Boiling point at given pressure (K).
• T_c : Critical Temperature (K).
• T_fus : Normal melting (fusion) point (K).
• V_c : Critical Volume (m³/kmol).
• ¹: Molecular weight from the IUPAC atomic weights tables.

Physical Properties

Property	Value	Unit	Source
ω	0.3910		Relay (1.0) Calculated Property
PAff	836.60	kJ/mol	NIST
BasG	805.60	kJ/mol	NIST
η	0.0005510	Pa×s	Densities and Viscosities of Ternary Mixtures of Cyclohexane + Cyclohexanone + Some Alkyl Acetates at 298.15 K
ΔfG°	-242.70	kJ/mol	Joback Calculated Property
ΔfH°gas	-475.14	kJ/mol	Relay (1.0) Calculated Property
ΔfusH°	11.49	kJ/mol	Joback Calculated Property
ΔvapH°	[34.30; 39.80]	kJ/mol
ΔvapH°	39.77	kJ/mol	NIST
ΔvapH°	37.70	kJ/mol	NIST
ΔvapH°	39.80 ± 0.10	kJ/mol	NIST
ΔvapH°	39.10 ± 0.20	kJ/mol	NIST
ΔvapH°	39.10 ± 0.20	kJ/mol	NIST
ΔvapH°	Outlier 34.30 ± 0.04	kJ/mol	NIST
IE	[9.92; 10.04]	eV
IE	10.04 ± 0.03	eV	NIST
IE	9.92	eV	NIST
log10WS	[-0.72; -0.72]
log10WS	-0.72		Aq. Solubility Prediction
log10WS	-0.72		Estimated Solubility
logPoct/wat	0.959		Crippen Calculated Property
McVol	88.750	ml/mol	McGowan Calculated Property
Pc	[3335.00; 3530.00]	kPa
Pc	3335.00 ± 81.06	kPa	NIST
Pc	3365.10 ± 40.00	kPa	NIST
Pc	3530.00 ± 101.32	kPa	NIST
ρc	[290.05; 296.39]	kg/m3
ρc	295.67 ± 5.11	kg/m3	NIST
ρc	296.39 ± 4.09	kg/m3	NIST
ρc	290.05 ± 6.13	kg/m3	NIST
Inp	[646.00; 735.00]
Inp	696.30		NIST
Inp	684.60		NIST
Inp	705.64		NIST
Inp	698.31		NIST
Inp	708.40		NIST
Inp	706.70		NIST
Inp	705.40		NIST
Inp	676.00		NIST
Inp	685.00		NIST
Inp	676.00		NIST
Inp	696.00		NIST
Inp	711.00		NIST
Inp	685.00		NIST
Inp	695.00		NIST
Inp	729.00		NIST
Inp	696.00		NIST
Inp	693.00		NIST
Inp	669.00		NIST
Inp	695.80		NIST
Inp	Outlier 653.00		NIST
Inp	Outlier 653.00		NIST
Inp	Outlier 654.00		NIST
Inp	695.00		NIST
Inp	695.00		NIST
Inp	707.00		NIST
Inp	Outlier 646.00		NIST
Inp	695.00		NIST
Inp	683.00		NIST
Inp	Outlier 648.00		NIST
Inp	Outlier 654.00		NIST
Inp	698.00		NIST
Inp	695.00		NIST
Inp	697.00		NIST
Inp	694.00		NIST
Inp	694.00		NIST
Inp	695.00		NIST
Inp	713.00		NIST
Inp	712.00		NIST
Inp	716.00		NIST
Inp	696.00		NIST
Inp	713.00		NIST
Inp	698.00		NIST
Inp	686.00		NIST
Inp	695.00		NIST
Inp	707.00		NIST
Inp	694.00		NIST
Inp	695.00		NIST
Inp	717.00		NIST
Inp	704.00		NIST
Inp	728.00		NIST
Inp	728.00		NIST
Inp	685.00		NIST
Inp	707.00		NIST
Inp	712.00		NIST
Inp	690.00		NIST
Inp	694.00		NIST
Inp	693.00		NIST
Inp	691.00		NIST
Inp	690.00		NIST
Inp	688.00		NIST
Inp	694.00		NIST
Inp	697.00		NIST
Inp	706.00		NIST
Inp	682.00		NIST
Inp	Outlier 657.00		NIST
Inp	Outlier 660.00		NIST
Inp	708.00		NIST
Inp	715.00		NIST
Inp	720.10		NIST
Inp	682.00		NIST
Inp	712.00		NIST
Inp	695.00		NIST
Inp	714.00		NIST
Inp	707.00		NIST
Inp	683.00		NIST
Inp	689.00		NIST
Inp	694.00		NIST
Inp	719.00		NIST
Inp	694.00		NIST
Inp	697.00		NIST
Inp	697.00		NIST
Inp	728.00		NIST
Inp	Outlier 735.00		NIST
Inp	713.00		NIST
Inp	Outlier 649.00		NIST
Inp	716.00		NIST
Inp	695.00		NIST
Inp	695.00		NIST
Inp	710.00		NIST
Inp	695.00		NIST
Inp	717.00		NIST
Inp	707.00		NIST
Inp	708.00		NIST
Inp	694.00		NIST
Inp	716.00		NIST
Inp	716.00		NIST
Inp	695.00		NIST
Inp	684.00		NIST
Inp	Outlier 659.00		NIST
Inp	696.00		NIST
Inp	665.00		NIST
Inp	696.00		NIST
Inp	716.00		NIST
Inp	717.00		NIST
Inp	696.00		NIST
Inp	696.00		NIST
Inp	695.00		NIST
Inp	695.00		NIST
Inp	693.00		NIST
Inp	695.00		NIST
Inp	704.00		NIST
Inp	696.00		NIST
Inp	708.00		NIST
Inp	695.00		NIST
Inp	694.00		NIST
Inp	698.00		NIST
Inp	728.00		NIST
I	[928.00; 996.00]
I	943.00		NIST
I	992.00		NIST
I	981.00		NIST
I	978.00		NIST
I	994.00		NIST
I	944.00		NIST
I	970.00		NIST
I	986.00		NIST
I	976.00		NIST
I	996.00		NIST
I	980.00		NIST
I	947.00		NIST
I	969.00		NIST
I	992.00		NIST
I	996.00		NIST
I	941.00		NIST
I	977.00		NIST
I	968.00		NIST
I	983.00		NIST
I	972.00		NIST
I	952.00		NIST
I	952.00		NIST
I	957.00		NIST
I	957.00		NIST
I	976.00		NIST
I	977.00		NIST
I	992.00		NIST
I	Outlier 935.00		NIST
I	982.00		NIST
I	939.00		NIST
I	960.00		NIST
I	970.00		NIST
I	995.00		NIST
I	969.00		NIST
I	982.00		NIST
I	Outlier 928.00		NIST
I	962.00		NIST
I	967.00		NIST
I	971.00		NIST
I	969.00		NIST
I	979.00		NIST
I	970.00		NIST
I	968.60		NIST
I	962.00		NIST
I	973.00		NIST
I	974.00		NIST
I	976.00		NIST
I	976.00		NIST
I	992.00		NIST
I	961.00		NIST
I	982.00		NIST
I	Outlier 935.00		NIST
I	Outlier 935.00		NIST
I	945.00		NIST
I	976.00		NIST
I	977.00		NIST
I	984.00		NIST
I	984.00		NIST
I	966.00		NIST
I	971.00		NIST
I	973.00		NIST
I	Outlier 932.00		NIST
I	942.00		NIST
I	984.00		NIST
I	962.00		NIST
I	984.00		NIST
I	963.00		NIST
I	990.00		NIST
I	990.00		NIST
I	990.00		NIST
I	986.00		NIST
I	975.00		NIST
I	950.00		NIST
I	995.00		NIST
I	969.00		NIST
I	968.00		NIST
I	957.00		NIST
Tboil	[370.65; 375.65]	K
Tboil	374.80	K	Heterogeneous azeotropic distillation for the separation of n-propanol + water mixture using n-propyl acetate as entrainer
Tboil	374.20	K	Experimental studies and thermodynamic analysis of isobaric vapor-liquid-liquid equilibria of 2-propanol + water system using n-propyl acetate and isopropyl acetate as entrainers
Tboil	374.62	K	Isobaric vapor-liquid equilibrium of a ternary system of ethyl acetate + propyl acetate + dimethyl sulfoxide and binary systems of ethyl acetate + dimethyl sulfoxide and propyl acetate + dimethyl sulfoxide at 101.3 kPa
Tboil	374.65	K	Isobaric Vapor-Liquid Equilibrium for the Binary Systems of 1,2-Dichloroethane + sec-Butyl Acetate, n-Propyl Acetate, and tert-Butyl Acetate at 101.3 kPa
Tboil	374.80	K	NIST
Tboil	374.00	K	NIST
Tboil	374.70	K	NIST
Tboil	374.70 ± 0.30	K	NIST
Tboil	374.28 ± 0.20	K	NIST
Tboil	374.75	K	NIST
Tboil	374.62 ± 0.50	K	NIST
Tboil	374.20 ± 2.00	K	NIST
Tboil	374.85 ± 0.50	K	NIST
Tboil	374.75 ± 0.50	K	NIST
Tboil	373.90 ± 1.00	K	NIST
Tboil	372.65 ± 1.00	K	NIST
Tboil	374.83 ± 0.30	K	NIST
Tboil	374.50 ± 1.00	K	NIST
Tboil	Outlier 370.65 ± 1.00	K	NIST
Tboil	374.75 ± 1.00	K	NIST
Tboil	374.75 ± 1.00	K	NIST
Tboil	374.69 ± 0.08	K	NIST
Tboil	375.00 ± 3.00	K	NIST
Tboil	374.75 ± 0.50	K	NIST
Tboil	374.80 ± 0.50	K	NIST
Tboil	374.80 ± 0.40	K	NIST
Tboil	374.80 ± 0.50	K	NIST
Tboil	374.75 ± 1.00	K	NIST
Tboil	374.62 ± 1.00	K	NIST
Tboil	375.15 ± 1.00	K	NIST
Tboil	373.65 ± 1.00	K	NIST
Tboil	373.95 ± 0.50	K	NIST
Tboil	374.70 ± 1.00	K	NIST
Tboil	375.30 ± 1.00	K	NIST
Tboil	374.70 ± 0.50	K	NIST
Tboil	373.00 ± 2.00	K	NIST
Tboil	375.00 ± 1.50	K	NIST
Tboil	373.95 ± 1.00	K	NIST
Tboil	375.65 ± 1.00	K	NIST
Tboil	375.20 ± 0.70	K	NIST
Tboil	Outlier 371.00 ± 3.00	K	NIST
Tboil	375.13 ± 1.00	K	NIST
Tc	540.08	K	Relay (1.0) Calculated Property
Tfus	[178.15; 179.55]	K
Tfus	179.55	K	Aq. Solubility Prediction
Tfus	178.15	K	NIST
Tfus	178.15 ± 0.60	K	NIST
Vc	0.336	m3/kmol	Relay (1.0) Calculated Property

Temperature Dependent Properties

Property	Value	Unit	Temperature (K)	Source
Cp,gas	[153.64; 178.95]	J/mol×K	[375.00; 450.00]
Cp,gas	153.64	J/mol×K	375.00	NIST
Cp,gas	162.33	J/mol×K	400.00	NIST
Cp,gas	171.19	J/mol×K	425.00	NIST
Cp,gas	178.95	J/mol×K	450.00	NIST
Cp,liquid	[194.10; 196.07]	J/mol×K	[298.00; 298.15]
Cp,liquid	194.10	J/mol×K	298.00	NIST
Cp,liquid	196.07	J/mol×K	298.15	NIST
η	[0.0004329; 0.0004878]	Pa×s	[303.15; 313.15]
η	0.0004878	Pa×s	303.15	Densities, Viscosities, and Speeds of Sound of Binary Liquid Mixtures of Sulfolane with Ethyl Acetate, n-Propyl Acetate, and n-Butyl Acetate at Temperature of (303.15, 308.15, and 313.15) K
η	0.0004595	Pa×s	308.15	Densities, Viscosities, and Speeds of Sound of Binary Liquid Mixtures of Sulfolane with Ethyl Acetate, n-Propyl Acetate, and n-Butyl Acetate at Temperature of (303.15, 308.15, and 313.15) K
η	0.0004329	Pa×s	313.15	Densities, Viscosities, and Speeds of Sound of Binary Liquid Mixtures of Sulfolane with Ethyl Acetate, n-Propyl Acetate, and n-Butyl Acetate at Temperature of (303.15, 308.15, and 313.15) K
ΔvapH	[33.90; 38.60]	kJ/mol	[313.00; 458.00]
ΔvapH	38.60 ± 0.10	kJ/mol	313.00	NIST
ΔvapH	36.70	kJ/mol	335.00	NIST
ΔvapH	36.90	kJ/mol	335.00	NIST
ΔvapH	36.90 ± 0.10	kJ/mol	336.00	NIST
ΔvapH	35.30 ± 0.10	kJ/mol	343.00	NIST
ΔvapH	38.20	kJ/mol	343.00	NIST
ΔvapH	36.40 ± 0.10	kJ/mol	344.00	NIST
ΔvapH	35.80 ± 0.10	kJ/mol	351.00	NIST
ΔvapH	38.10	kJ/mol	352.50	NIST
ΔvapH	37.00	kJ/mol	352.50	NIST
ΔvapH	34.80 ± 0.10	kJ/mol	363.00	NIST
ΔvapH	33.92	kJ/mol	374.70	NIST
ΔvapH	33.90	kJ/mol	375.00	NIST
ΔvapH	34.80	kJ/mol	458.00	NIST
Pvap	[0.50; 101.40]	kPa	[263.15; 374.80]
Pvap	0.50	kPa	263.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	1.01	kPa	273.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	1.91	kPa	283.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	3.43	kPa	293.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	4.51	kPa	298.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	4.51	kPa	298.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	5.87	kPa	303.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	9.64	kPa	313.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	9.59	kPa	313.15	Total Vapor Pressure Measurements for 2-Ethoxyethanol with Methyl Acetate, Ethyl Acetate, Propyl Acetate, and Ethyl Propionate at 313.15 K and for 2-Ethoxyethanol with Methyl Formate at 308.15 K
Pvap	9.65	kPa	313.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	15.25	kPa	323.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	15.25	kPa	323.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	16.09	kPa	323.15	Vapor-Liquid Equilibria in the Propyl Acetate + Ethanoic Acid Binary System from (323.15 to 353.15) K: Measurement with a Static Method and Modeling with the NRTL, Wilson, UNIQUAC, and COSMO-SAC Approaches
Pvap	22.20	kPa	331.70	Phase equilibria on binary systems containing diethyl sulfide
Pvap	23.33	kPa	333.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	23.33	kPa	333.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	24.01	kPa	333.15	Vapor-Liquid Equilibria in the Propyl Acetate + Ethanoic Acid Binary System from (323.15 to 353.15) K: Measurement with a Static Method and Modeling with the NRTL, Wilson, UNIQUAC, and COSMO-SAC Approaches
Pvap	31.10	kPa	340.16	Phase equilibria on binary systems containing diethyl sulfide
Pvap	34.64	kPa	343.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	34.99	kPa	343.15	Vapor-Liquid Equilibria in the Propyl Acetate + Ethanoic Acid Binary System from (323.15 to 353.15) K: Measurement with a Static Method and Modeling with the NRTL, Wilson, UNIQUAC, and COSMO-SAC Approaches
Pvap	41.80	kPa	348.06	Phase equilibria on binary systems containing diethyl sulfide
Pvap	49.92	kPa	353.15	Vapor-Liquid Equilibria in the Propyl Acetate + Ethanoic Acid Binary System from (323.15 to 353.15) K: Measurement with a Static Method and Modeling with the NRTL, Wilson, UNIQUAC, and COSMO-SAC Approaches
Pvap	50.07	kPa	353.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	50.07	kPa	353.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	50.40	kPa	353.27	Phase equilibria on binary systems containing diethyl sulfide
Pvap	62.70	kPa	359.55	Phase equilibria on binary systems containing diethyl sulfide
Pvap	70.64	kPa	363.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	70.64	kPa	363.15	Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
Pvap	71.00	kPa	363.29	Phase equilibria on binary systems containing diethyl sulfide
Pvap	81.40	kPa	367.42	Phase equilibria on binary systems containing diethyl sulfide
Pvap	91.50	kPa	371.07	Phase equilibria on binary systems containing diethyl sulfide
Pvap	101.00	kPa	374.20	Experimental studies and thermodynamic analysis of isobaric vapor-liquid-liquid equilibria of 2-propanol + water system using n-propyl acetate and isopropyl acetate as entrainers
Pvap	101.40	kPa	374.29	Phase equilibria on binary systems containing diethyl sulfide
Pvap	101.30	kPa	374.62	Isobaric vapor-liquid equilibrium of a ternary system of ethyl acetate + propyl acetate + dimethyl sulfoxide and binary systems of ethyl acetate + dimethyl sulfoxide and propyl acetate + dimethyl sulfoxide at 101.3 kPa
Pvap	101.30	kPa	374.65	Isobaric Vapor-Liquid Equilibrium for the Binary Systems of 1,2-Dichloroethane + sec-Butyl Acetate, n-Propyl Acetate, and tert-Butyl Acetate at 101.3 kPa
Pvap	101.00	kPa	374.80	Heterogeneous azeotropic distillation for the separation of n-propanol + water mixture using n-propyl acetate as entrainer
n0	[1.37170; 1.38660]		[288.20; 318.20]
n0	1.38660		288.20	Experimental and calculated liquid-liquid equilibrium data for water + furfural + solvents
n0	1.38150		298.15	Isobaric Vapor-Liquid Equilibria of Binary Mixtures of Diethyl Carbonate with Methyl Acetate, n-Propyl Acetate, or Amyl Acetate at 100.17 kPa
n0	1.38180		298.15	Multiproperty Correlation of Experimental Data of the Binaries Propyl Ethanoate + Alkanes (Pentane to Decane). New Experimental Information for Vapor Liquid Equilibrium and Mixing Properties
n0	1.38210		298.15	Isobaric (vapor+liquid) equilibrium for n-propyl acetate with 1-butanol or 2-butanol. Binary mixtures at 0.15 and 0.6 MPa
n0	1.38181		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	1.38406		298.15	Isobaric Vapor-Liquid Equilibrium Data for Binary Systems of Anisole with Methyl Acetate, Ethyl Acetate, n-Propyl Acetate, and Isopropyl Acetate at 93.9 kPa
n0	1.38280		298.20	Vapor liquid equilibria for the ternary mixture of carbon dioxide + 1-propanol + propyl acetate at elevated pressures
n0	1.38300		298.20	Experimental and correlated liquid-liquid equilibrium data for water-phosphoric acid-ester
n0	1.37920		303.15	Correlation and Prediction of Excess Quantities and Vapor-Liquid Equilibria of Alkyl Esters + tert-Butyl Alcohol: Experimental Data for Propyl Esters + tert-Butyl Alcohol
n0	1.37920		303.20	Experimental and calculated liquid-liquid equilibrium data for water + furfural + solvents
n0	1.37410		313.15	Density, refraction index and vapor-liquid equilibria of N-methyl-2-hydroxyethylammonium butyrate plus (methyl acetate or ethyl acetate or propyl acetate) at several temperatures
n0	1.37210		318.15	Thermodynamic properties of (an ester + an alkane). XVI. Experimental HEm and V Em values and a new correlation method for (an alkyl ethanoate + an n-alkane) at 318.15 K
n0	1.37200		318.15	Multiproperty Correlation of Experimental Data of the Binaries Propyl Ethanoate + Alkanes (Pentane to Decane). New Experimental Information for Vapor Liquid Equilibrium and Mixing Properties
n0	1.37170		318.20	Experimental and calculated liquid-liquid equilibrium data for water + furfural + solvents
ρl	[859.52; 893.20]	kg/m3	[288.15; 318.15]
ρl	893.20	kg/m3	288.15	Thermal and Volumetric Properties of Four Aqueous Aroma Compounds at Infinite Dilution
ρl	887.80	kg/m3	293.15	Liquid-liquid equilibria and COSMO-SAC modeling of organic solvent/ ionic liquid - hydroxyacetone - water mixtures
ρl	887.97	kg/m3	293.15	Volumetric Properties of Binary Mixtures of N-Ethylformamide with Tetrahydropyran, 2-Pentanone, and Propylacetate from (293.15 to 313.15) K
ρl	888.96	kg/m3	293.15	Volumetric and FT-IR Studies of the Binary Liquid Mixtures of Tributylamine and Alkyl Ester (C1-C5)
ρl	889.00	kg/m3	293.20	Ternary and Quaternary Liquid-Liquid Equilibria for Systems of Methyl Butyl Ketone + Water + Hydroquinone + Phenol at 313.2 K and Atmospheric Pressure
ρl	882.08	kg/m3	298.15	Thermodynamic study of (alkyl esters + a,x-alkyl dihalides) VII. HE m and VE m for 20 binary mixtures {xCu 1H2u 1CO2C3H7 + (1 x)a,x-ClCH2(CH2)v 2CH2Cl}, where u = 1 to 4, a = 1 and v = x = 2 to 6. An analysis of behavior using the COSMO-RS methodology
ρl	882.21	kg/m3	298.15	Volumetric Properties of Binary Mixtures of N-Ethylformamide with Tetrahydropyran, 2-Pentanone, and Propylacetate from (293.15 to 313.15) K
ρl	882.40	kg/m3	298.15	Experimental Determination of Vapor Liquid Equilibria. Binary Systems of Methyl Acetate, Ethyl Acetate, and Propyl Acetate with 1-Propanol at 0.6 MPa
ρl	886.00	kg/m3	298.15	Isobaric Vapor-liquid Equilibrium for Three Binary Systems of Ethyl Acetate + Propyl Acetate, Ethyl Acetate + Propylene Carbonate, and Propyl Acetate + Propylene Carbonate at 101.3 kPa
ρl	882.80	kg/m3	298.15	Isobaric Vapor Liquid Equilibria of Binary Systems (Propyl Acetate + n-Pentanol), (Propyl Acetate + 1-Methyl-1-butanol), and (Propyl Acetate + 3-Methyl-1-butanol) at 101.3 kPa
ρl	883.37	kg/m3	298.15	Volumetric and FT-IR Studies of the Binary Liquid Mixtures of Tributylamine and Alkyl Ester (C1-C5)
ρl	882.19	kg/m3	298.15	Liquid-liquid equilibria and COSMO-SAC modeling of organic solvent/ ionic liquid - hydroxyacetone - water mixtures
ρl	882.05	kg/m3	298.15	Thermal and Volumetric Properties of Four Aqueous Aroma Compounds at Infinite Dilution
ρl	881.51	kg/m3	298.20	Liquid-liquid equilibrium for methyl butyl ketone + o-, m-, p-cresol + water ternary systems and COSMO-SAC predictions
ρl	877.42	kg/m3	303.15	Volumetric and FT-IR Studies of the Binary Liquid Mixtures of Tributylamine and Alkyl Ester (C1-C5)
ρl	876.55	kg/m3	303.15	Excess Volumes and Excess Isentropic Compressibilities of Binary Liquid Mixtures of Trichloroethylene with Esters at 303.15 K
ρl	876.54	kg/m3	303.15	Volumetric Properties of Binary Mixtures of N-Ethylformamide with Tetrahydropyran, 2-Pentanone, and Propylacetate from (293.15 to 313.15) K
ρl	876.56	kg/m3	303.15	Liquid-liquid equilibria and COSMO-SAC modeling of organic solvent/ ionic liquid - hydroxyacetone - water mixtures
ρl	871.78	kg/m3	308.15	Volumetric and FT-IR Studies of the Binary Liquid Mixtures of Tributylamine and Alkyl Ester (C1-C5)
ρl	870.87	kg/m3	308.15	Thermal and Volumetric Properties of Four Aqueous Aroma Compounds at Infinite Dilution
ρl	870.81	kg/m3	308.15	Volumetric Properties of Binary Mixtures of N-Ethylformamide with Tetrahydropyran, 2-Pentanone, and Propylacetate from (293.15 to 313.15) K
ρl	870.90	kg/m3	308.15	Liquid-liquid equilibria and COSMO-SAC modeling of organic solvent/ ionic liquid - hydroxyacetone - water mixtures
ρl	866.12	kg/m3	313.15	Volumetric and FT-IR Studies of the Binary Liquid Mixtures of Tributylamine and Alkyl Ester (C1-C5)
ρl	865.21	kg/m3	313.15	Liquid-liquid equilibria and COSMO-SAC modeling of organic solvent/ ionic liquid - hydroxyacetone - water mixtures
ρl	864.95	kg/m3	313.15	Volumetric Properties of Binary Mixtures of N-Ethylformamide with Tetrahydropyran, 2-Pentanone, and Propylacetate from (293.15 to 313.15) K
ρl	859.52	kg/m3	318.15	Thermal and Volumetric Properties of Four Aqueous Aroma Compounds at Infinite Dilution
γ	[0.02; 0.02]	N/m	[298.15; 313.15]
γ	0.02	N/m	298.15	Densities, surface tensions, and derived surface thermodynamics properties of (trimethylbenzene + propyl acetate, or butyl acetate) from T = 298.15 K to 313.15 K
γ	0.02	N/m	298.15	Densities and Surface Tensions of Propyl Acetate + Xylenes or + Ethylbenzene from (298.15 to 308.15) K
γ	0.02	N/m	298.15	Surface Tension Data of Aqueous Binary Mixtures of Methyl, Ethyl, Propyl, and Butyl Acetates at 298.15 K
γ	0.02	N/m	303.15	Densities, surface tensions, and derived surface thermodynamics properties of (trimethylbenzene + propyl acetate, or butyl acetate) from T = 298.15 K to 313.15 K
γ	0.02	N/m	303.15	Densities, surface tensions, and derived surface thermodynamics properties of (trimethylbenzene + propyl acetate, or butyl acetate) from T = 298.15 K to 313.15 K
γ	0.02	N/m	303.15	Densities and Surface Tensions of Propyl Acetate + Xylenes or + Ethylbenzene from (298.15 to 308.15) K
γ	0.02	N/m	308.15	Densities, surface tensions, and derived surface thermodynamics properties of (trimethylbenzene + propyl acetate, or butyl acetate) from T = 298.15 K to 313.15 K
γ	0.02	N/m	308.15	Densities and Surface Tensions of Propyl Acetate + Xylenes or + Ethylbenzene from (298.15 to 308.15) K
γ	0.02	N/m	313.15	Densities, surface tensions, and derived surface thermodynamics properties of (trimethylbenzene + propyl acetate, or butyl acetate) from T = 298.15 K to 313.15 K

Pressure Dependent Properties

Property	Value	Unit	Pressure (kPa)	Source
Tboil	[322.62; 374.66]	K	[14.90; 101.26]
Tboil	322.62	K	14.90	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	325.01	K	16.60	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	327.77	K	18.56	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	329.58	K	20.00	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	334.71	K	24.75	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	337.78	K	27.99	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	341.96	K	33.06	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	345.55	K	37.76	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	347.21	K	40.07	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	350.05	K	44.38	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	352.73	K	48.69	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	355.66	K	54.33	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	358.60	K	60.03	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	361.80	K	66.87	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	364.80	K	73.94	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	367.13	K	79.95	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	369.07	K	85.25	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	371.41	K	91.51	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil	374.66	K	101.26	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems

Datasets

Mass density, kg/m3

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Mass density, kg/m3 - Liquid
298.15	100.00	882.0
298.15	1000.00	882.5
298.15	2000.00	883.4
298.15	3000.00	884.3
298.15	3300.00	884.6
298.15	5000.00	886.4
298.15	10000.00	890.7
298.15	15000.00	894.8
298.15	20000.00	898.7
298.15	25000.00	902.5
298.15	30000.00	906.9
298.15	35000.00	911.7
303.15	100.00	876.2
303.15	1000.00	876.8
303.15	2000.00	877.7
303.15	3000.00	878.8
303.15	3300.00	879.0
303.15	5000.00	880.8
303.15	10000.00	885.3
303.15	15000.00	889.5
303.15	20000.00	893.5
303.15	25000.00	897.4
303.15	30000.00	902.0
303.15	35000.00	906.9
308.15	100.00	870.5
308.15	1000.00	871.2
308.15	2000.00	872.2
308.15	3000.00	873.2
308.15	3300.00	873.4
308.15	5000.00	875.3
308.15	10000.00	879.9
308.15	15000.00	884.3
308.15	20000.00	888.4
308.15	25000.00	892.4
308.15	30000.00	897.2
308.15	35000.00	902.3
313.15	100.00	864.9
313.15	1000.00	865.5
313.15	2000.00	866.6
313.15	3000.00	867.6
313.15	3300.00	867.9
313.15	5000.00	869.9
313.15	10000.00	874.7
313.15	15000.00	879.2
313.15	20000.00	883.5
313.15	25000.00	887.6
313.15	30000.00	892.6
313.15	35000.00	897.7
318.15	100.00	859.3
318.15	1000.00	859.8
318.15	2000.00	860.9
318.15	3000.00	862.1
318.15	3300.00	862.4
318.15	5000.00	864.4
318.15	10000.00	869.4
318.15	15000.00	874.1
318.15	20000.00	878.5
318.15	25000.00	882.8
318.15	30000.00	887.9
318.15	35000.00	893.2
323.15	100.00	853.6
323.15	1000.00	854.8
323.15	2000.00	855.8
323.15	3000.00	856.9
323.15	3300.00	857.1
323.15	5000.00	859.0
323.15	10000.00	864.1
323.15	15000.00	869.0
323.15	20000.00	873.5
323.15	25000.00	877.9
323.15	30000.00	883.2
323.15	35000.00	888.8
328.15	100.00	848.0
328.15	1000.00	848.7
328.15	2000.00	849.9
328.15	3000.00	851.0
328.15	3300.00	851.3
328.15	5000.00	853.7
328.15	10000.00	859.0
328.15	15000.00	864.0
328.15	20000.00	868.7
328.15	25000.00	873.3
328.15	30000.00	878.8
328.15	35000.00	884.4
333.15	100.00	842.5
333.15	1000.00	843.6
333.15	2000.00	844.8
333.15	3000.00	845.9
333.15	3300.00	846.2
333.15	5000.00	848.3
333.15	10000.00	853.9
333.15	15000.00	859.0
333.15	20000.00	863.9
333.15	25000.00	868.6
333.15	30000.00	874.3
333.15	35000.00	880.1
338.15	100.00	836.7
338.15	1000.00	838.0
338.15	2000.00	839.2
338.15	3000.00	840.5
338.15	3300.00	840.8
338.15	5000.00	842.8
338.15	10000.00	848.6
338.15	15000.00	853.9
338.15	20000.00	859.0
338.15	25000.00	863.8
338.15	30000.00	869.6
338.15	35000.00	875.5
343.15	100.00	831.2
343.15	1000.00	832.3
343.15	2000.00	833.7
343.15	3000.00	834.9
343.15	3300.00	835.3
343.15	5000.00	837.6
343.15	10000.00	843.6
343.15	15000.00	849.1
343.15	20000.00	854.3
343.15	25000.00	859.2
343.15	30000.00	865.0
343.15	35000.00	871.2
348.15	100.00	825.6
348.15	1000.00	826.8
348.15	2000.00	828.1
348.15	3000.00	829.5
348.15	3300.00	829.9
348.15	5000.00	832.2
348.15	10000.00	838.3
348.15	15000.00	844.1
348.15	20000.00	849.5
348.15	25000.00	854.5
348.15	30000.00	860.6
348.15	35000.00	866.8
353.15	100.00	820.0
353.15	1000.00	821.2
353.15	2000.00	822.6
353.15	3000.00	824.0
353.15	3300.00	824.4
353.15	5000.00	826.9
353.15	10000.00	833.3
353.15	15000.00	838.8
353.15	20000.00	844.8
353.15	25000.00	850.0
353.15	30000.00	856.4
353.15	35000.00	862.7
358.15	100.00	811.6
358.15	1000.00	812.9
358.15	2000.00	814.4
358.15	3000.00	815.8
358.15	3300.00	816.3
358.15	5000.00	818.6
358.15	10000.00	825.3
358.15	15000.00	831.5
358.15	20000.00	837.2
358.15	25000.00	842.8
363.15	100.00	804.8
363.15	1000.00	806.9
363.15	2000.00	808.4
363.15	3000.00	810.0
363.15	3300.00	810.4
363.15	5000.00	812.9
363.15	10000.00	819.9
363.15	15000.00	826.2
363.15	20000.00	832.1
363.15	25000.00	837.7
363.15	30000.00	844.4
368.15	1000.00	801.0
368.15	2000.00	802.7
368.15	3000.00	804.3
368.15	3300.00	804.8
368.15	5000.00	807.4
368.15	10000.00	814.6
368.15	15000.00	821.2
368.15	20000.00	827.3
368.15	25000.00	833.1
373.15	1000.00	795.5
373.15	2000.00	797.2
373.15	3000.00	798.9
373.15	3300.00	799.5
373.15	5000.00	802.3
373.15	10000.00	809.8
373.15	15000.00	816.6
373.15	20000.00	822.9
373.15	25000.00	828.9
378.15	1000.00	789.4
378.15	2000.00	791.3
378.15	3000.00	793.0
378.15	3300.00	793.6
378.15	5000.00	796.3
378.15	10000.00	803.3
378.15	15000.00	811.3
378.15	20000.00	817.7
378.15	25000.00	824.0
378.15	30000.00	831.2
383.15	1000.00	783.6
383.15	2000.00	785.5
383.15	3000.00	787.3
383.15	3300.00	788.2
383.15	5000.00	791.2
383.15	10000.00	799.2
383.15	15000.00	806.6
383.15	20000.00	813.2
383.15	25000.00	819.7
388.15	1000.00	777.9
388.15	2000.00	779.8
388.15	3000.00	781.6
388.15	3300.00	782.1
388.15	5000.00	785.4
388.15	10000.00	793.8
388.15	15000.00	801.5
388.15	20000.00	808.5
388.15	25000.00	815.2
388.15	30000.00	823.2
393.15	1000.00	771.8
393.15	2000.00	773.9
393.15	3000.00	775.9
393.15	3300.00	776.4
393.15	5000.00	779.7
393.15	10000.00	788.6
393.15	15000.00	796.5
393.15	20000.00	803.8
393.15	25000.00	810.7
Reference

Correlations

Property	Value	Unit	Temperature (K)	Source
Pvap	[1.33; 202.64]	kPa	[276.65; 398.87]	The Yaws Handbook of Vapor Pressure
Equation			ln(Pvp) = A + B/(T + C)
Coefficient A			1.46116e+01
Coefficient B			-3.24092e+03
Coefficient C			-5.03900e+01
Temperature range, min.			276.65
Temperature range, max.			398.87
Pvap	1.33	kPa	276.65	Calculated Property
Pvap	3.00	kPa	290.23	Calculated Property
Pvap	6.19	kPa	303.81	Calculated Property
Pvap	11.86	kPa	317.39	Calculated Property
Pvap	21.35	kPa	330.97	Calculated Property
Pvap	36.38	kPa	344.55	Calculated Property
Pvap	59.16	kPa	358.13	Calculated Property
Pvap	92.33	kPa	371.71	Calculated Property
Pvap	138.98	kPa	385.29	Calculated Property
Pvap	202.64	kPa	398.87	Calculated Property
Pvap	[2.14e-05; 3330.47]	kPa	[178.15; 549.40]	KDB Vapor Pressure Data
Equation			ln(Pvp) = A + B/T + C*ln(T) + D*T^2
Coefficient A			9.54327e+01
Coefficient B			-7.93197e+03
Coefficient C			-1.19486e+01
Coefficient D			8.27424e-06
Temperature range, min.			178.15
Temperature range, max.			549.40
Pvap	2.14e-05	kPa	178.15	Calculated Property
Pvap	8.78e-03	kPa	219.40	Calculated Property
Pvap	0.40	kPa	260.65	Calculated Property
Pvap	5.40	kPa	301.90	Calculated Property
Pvap	34.25	kPa	343.15	Calculated Property
Pvap	135.12	kPa	384.40	Calculated Property
Pvap	389.33	kPa	425.65	Calculated Property
Pvap	907.07	kPa	466.90	Calculated Property
Pvap	1827.15	kPa	508.15	Calculated Property
Pvap	3330.47	kPa	549.40	Calculated Property

Similar Compounds

Find more compounds similar to n-Propyl acetate.

Mixtures

• Trichloroethylene + n-Propyl acetate
• 1-Propanol + Carbon dioxide + n-Propyl acetate
• n-Propyl acetate + Simvastatin
• n-Propyl acetate + Diethyl sulfide
• n-Propyl acetate + Water
• Furfural + n-Propyl acetate + Water
• 1-Butanol + n-Propyl acetate
• 1-Propanol + n-Propyl acetate
• 1-Propanol + n-Propyl acetate + Water
• Isopropyl Alcohol + n-Propyl acetate
• Isopropyl Alcohol + n-Propyl acetate + Water
• 2-Propanone, 1-hydroxy- + n-Propyl acetate + Water
• Heptane + n-Propyl acetate
• n-Propyl acetate + Nonane
• Undecane + n-Propyl acetate
• Tridecane + n-Propyl acetate
• Pentadecane + n-Propyl acetate
• Heptadecane + n-Propyl acetate
• n-Propyl acetate + Benzene, 1,2,4-trimethyl-
• n-Propyl acetate + Mesitylene

Find more mixtures with n-Propyl acetate.

Sources

• KDB Vapor Pressure Data
• Cheméo Relay (1.0)
• Crippen Method
• Excess Volumes and Excess Isentropic Compressibilities of Binary Liquid Mixtures of Trichloroethylene with Esters at 303.15 K
• (Liquid + liquid) equilibria of (water + 1-propanol + solvent) at T = 298.2K
• Vapor liquid equilibria for the ternary mixture of carbon dioxide + 1-propanol + propyl acetate at elevated pressures
• Solubility and limiting activity coefficient of simvastatin in different organic solvents
• Isothermal vapor-liquid equilibria and excess enthalpies of binary mixtures of propyl ethanoate + 1-hexyne, +2-hexyne, +3-hexyne
• Phase equilibria on binary systems containing diethyl sulfide
• Liquid-liquid equilibrium for the ternary systems of water + acetyl acetone + propyl acetate at several temperatures
• Investigation on isobaric vapor-liquid equilibrium for acetic acid + water + (n-propyl acetate or iso-butyl acetate)
• Vapour-liquid and chemical equilibria in the ethyl ethanoate + ethanol + propyl ethanoate + propanol system accompanied with transesterification reaction
• Experimental and calculated liquid-liquid equilibrium data for water + furfural + solvents
• Solubility, liquid-liquid equilibrium and critical states for the system acetic acid + n-propanol + n-propyl acetate + water at 293.15 K and 303.15 K
• Temperature dependence of limiting activity coefficients, Henry's law constants, and related infinite dilution properties of C4-C6 isomeric n-alkyl ethanoates/ethyl n-alkanoates in water. Measurement, critical compilation, correlation, and recommended data
• Excess molar enthalpies for binary mixtures of n-propanol, acetic acid, and n-propyl acetate at 313.15 K and atmospheric pressure
• Isobaric (vapor+liquid) equilibrium for n-propyl acetate with 1-butanol or 2-butanol. Binary mixtures at 0.15 and 0.6 MPa
• Solution thermodynamics of simvastatin in pure solvents and binary solvent mixtures
• Liquid-liquid equilibrium of the ternary system water p propargyl alcohol p n-propyl acetate
• Heterogeneous azeotropic distillation for the separation of n-propanol + water mixture using n-propyl acetate as entrainer
• Experimental studies and thermodynamic analysis of isobaric vapor-liquid-liquid equilibria of 2-propanol + water system using n-propyl acetate and isopropyl acetate as entrainers
• Liquid-liquid equilibria and COSMO-SAC modeling of organic solvent/ ionic liquid - hydroxyacetone - water mixtures
• Thermodynamic properties of (an ester + an alkane). XVI. Experimental HEm and V Em values and a new correlation method for (an alkyl ethanoate + an n-alkane) at 318.15 K
• Densities, surface tensions, and derived surface thermodynamics properties of (trimethylbenzene + propyl acetate, or butyl acetate) from T = 298.15 K to 313.15 K
• Thermodynamic study of (alkyl esters + a,x-alkyl dihalides) VII. HE m and VE m for 20 binary mixtures {xCu 1H2u 1CO2C3H7 + (1 x)a,x-ClCH2(CH2)v 2CH2Cl}, where u = 1 to 4, a = 1 and v = x = 2 to 6. An analysis of behavior using the COSMO-RS methodology
• Solubility of diosgenin in different solvents
• Density, refraction index and vapor-liquid equilibria of N-methyl-2-hydroxyethylammonium butyrate plus (methyl acetate or ethyl acetate or propyl acetate) at several temperatures
• Solid-liquid phase equilibrium and mixing properties of 2-Cyano-4'-methylbiphenyl in pure solvents
• Measurement and correlation of solubility of boscalid with thermodynamic analysis in pure and binary solvents from 288.15 K to 313.15 K
• Experimental and correlated liquid-liquid equilibrium data for water-phosphoric acid-ester
• Liquid-liquid equilibrium for methyl butyl ketone + o-, m-, p-cresol + water ternary systems and COSMO-SAC predictions
• Isobaric vapor-liquid equilibrium of a ternary system of ethyl acetate + propyl acetate + dimethyl sulfoxide and binary systems of ethyl acetate + dimethyl sulfoxide and propyl acetate + dimethyl sulfoxide at 101.3 kPa
• Studies on liquid liquid interactions of some ternary mixtures by density, viscosity, ultrasonic speed and refractive index measurements
• Ternary and Quaternary Liquid-Liquid Equilibria for Systems of Methyl Butyl Ketone + Water + Hydroquinone + Phenol at 313.2 K and Atmospheric Pressure
• Measurement and Correlation of Solubility on Reactive Crystallization of Methyl D-(-)-4-Hydroxy-phenylglycinate
• Ternary Liquid Liquid Equilibrium of Azeotropes (Ester + Alcohol) with Different Ionic Liquids at T = 298.15 K
• 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
• Solution Thermodynamics of Benzotriazole in Different Pure Solvents
• Isobaric Vapor-liquid Equilibrium for Three Binary Systems of Ethyl Acetate + Propyl Acetate, Ethyl Acetate + Propylene Carbonate, and Propyl Acetate + Propylene Carbonate at 101.3 kPa
• Liquid-Liquid Extraction of Cyclopentanone from Aqueous Solution with Methylcyclohexane or Propyl Acetate at Different Temperatures
• Isobaric Vapor-Liquid Equilibrium Data for Binary Systems of Anisole with Methyl Acetate, Ethyl Acetate, n-Propyl Acetate, and Isopropyl Acetate at 93.9 kPa
• Isobaric Vapor-Liquid Equilibrium for the Binary Systems of 1,2-Dichloroethane + sec-Butyl Acetate, n-Propyl Acetate, and tert-Butyl Acetate at 101.3 kPa
• Liquid-Liquid Equilibrium Data for the Systems n-Propyl Acetate or Isopropyl Acetate + n-Propanol or Isopropyl Alcohol + IL at 298.15 and 318.15 K and Atmospheric Pressure
• Volumetric and FT-IR Studies of the Binary Liquid Mixtures of Tributylamine and Alkyl Ester (C1-C5)
• Solubilities of 2,6-Dimethylnaphthalene in Six Pure Solvents and Two Binary Solvent Systems
• Isobaric Vapor-Liquid Equilibria of Binary Mixtures of Diethyl Carbonate with Methyl Acetate, n-Propyl Acetate, or Amyl Acetate at 100.17 kPa
• Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
• Solubility and Thermodynamic Modeling of Dimethyl Terephthalate in Pure Solvents and the Evaluation of the Mixing Properties of the Solutions
• Thermodynamic Properties of Mixtures Containing Precursors of Vitamin B5
• Total Vapor Pressure Measurements for 2-Ethoxyethanol with Methyl Acetate, Ethyl Acetate, Propyl Acetate, and Ethyl Propionate at 313.15 K and for 2-Ethoxyethanol with Methyl Formate at 308.15 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
• Liquid-Liquid Equilibria for the Ternary System Water + Acetic Acid + Propyl Acetate
• Correlation and Prediction of Excess Quantities and Vapor-Liquid Equilibria of Alkyl Esters + tert-Butyl Alcohol: Experimental Data for Propyl Esters + tert-Butyl Alcohol
• Isothermal Vapor-Liquid Equilibria and Excess Enthalpies of (Propyl Ethanoate + Heptane), (Propyl Ethanoate + Cyclohexane), and (Propyl Ethanoate + 1-Hexene)
• PVT Property Measurements for Some Aliphatic Esters from (298 to 393) K and up to 35 MPa
• Densities and Surface Tensions of Propyl Acetate + Xylenes or + Ethylbenzene from (298.15 to 308.15) K
• Vapor-Liquid Equilibria in the Propyl Acetate + Ethanoic Acid Binary System from (323.15 to 353.15) K: Measurement with a Static Method and Modeling with the NRTL, Wilson, UNIQUAC, and COSMO-SAC Approaches
• Activity Coefficients at Infinite Dilution by GLC in Alkanediamines as Stationary Phases
• Thermal and Volumetric Properties of Four Aqueous Aroma Compounds at Infinite Dilution
• Crystal Structures, Reaction Rates, and Selected Physical Properties of Halo-Boronsubphthalocyanines (Halo = Fluoride, Chloride, and Bromide)
• Volumetric Properties of Binary Mixtures of N-Ethylformamide with Tetrahydropyran, 2-Pentanone, and Propylacetate from (293.15 to 313.15) K
• Multiproperty Correlation of Experimental Data of the Binaries Propyl Ethanoate + Alkanes (Pentane to Decane). New Experimental Information for Vapor Liquid Equilibrium and Mixing Properties
• Experimental Determination of Vapor Liquid Equilibria. Binary Systems of Methyl Acetate, Ethyl Acetate, and Propyl Acetate with 1-Propanol at 0.6 MPa
• Isobaric Vapor Liquid Equilibria of Binary Systems (Propyl Acetate + n-Pentanol), (Propyl Acetate + 1-Methyl-1-butanol), and (Propyl Acetate + 3-Methyl-1-butanol) at 101.3 kPa
• Isobaric Vapor Liquid Liquid Equilibria for the Ternary Systems Ethanol + Water + Propyl Acetate and 1-Propanol + Water + Propyl acetate
• Isobaric Vapor Liquid Equilibria of Binary Systems (Propyl Acetate + 2-Methylbutan-1-ol), (Propyl Acetate + Hexan-1-ol), and (Propyl Acetate + Heptan-1-ol) at 101.3 kPa
• Solubility of Anthracene in Binary Propyl Acetate + Alcohol Solvent Mixtures at 298.15 K
• Solubility of Lovastatin in Ethyl Acetate, Propyl Acetate, Isopropyl Acetate, Butyl Acetate, sec-Butyl Acetate, Isobutyl Acetate, tert-Butyl Acetate, and 2-Butanone, between (285 and 313) K
• Ternary Liquid-Liquid Equilibria for Systems Containing Alcohol or Acetic Acid + Ester + 1-Ethyl-3-methylimidazolium Hydrogen Sulfate at 313.2 K Using Headspace Gas Chromatography
• Densities, Viscosities, and Speeds of Sound of Binary Liquid Mixtures of Sulfolane with Ethyl Acetate, n-Propyl Acetate, and n-Butyl Acetate at Temperature of (303.15, 308.15, and 313.15) K
• Densities and Viscosities of Ternary Mixtures of Cyclohexane + Cyclohexanone + Some Alkyl Acetates at 298.15 K
• Surface Tension Data of Aqueous Binary Mixtures of Methyl, Ethyl, Propyl, and Butyl Acetates at 298.15 K
• Joback Method
• Aqueous Solubility Prediction Method
• Estimated Solubility Method
• McGowan Method
• NIST Webbook
• The Yaws Handbook of Vapor Pressure

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