Chemical Properties of Acetic acid, propyl ester (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 ester of acetic acid
• Propylester kyseliny octove
• UN 1276
• ethanoic acid, propyl ester
• n-Propanol acetate
• n-Propyl ethanoate
• n-propyl acetate
• propyl acetate
• propyl ethanoate

• ω : Acentric Factor.
• PAff : Proton affinity (kJ/mol).
• T_ig : Autoignition Temperature (K).
• 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).
• μ : Dipole Moment (debye).
• η : Dynamic viscosity (Pa×s).
• ε_r : Dielectric Constant (Relative permittivity).
• T_flash,cc : Flash Point (Closed Cup Method) (K).
• Δ_fG° : Standard Gibbs free energy of formation (kJ/mol).
• Δ_fH°_gas : Enthalpy of formation at standard conditions (kJ/mol).
• Δ_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).
• NFPA Fire : NFPA Fire Rating.
• NFPA Health : NFPA Health Rating.
• NFPA Safety : NFPA Safety Rating.
• P_c : Critical Pressure (kPa).
• P_triple : Triple Point 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_p : Polar retention indices.
• γ : Surface Tension (N/m).
• T_boil : Normal Boiling Point Temperature (K).
• T_boil(P) : Boiling point at given pressure (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.
• ¹: Molecular weight from the IUPAC atomic weights tables.

Physical Properties

Property	Value	Unit	Source
ω	[0.3890; 0.3920]
ω	0.3920		PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
ω	0.3890		ChemSep v8.3 pure component data Compiled value
PAff	836.60	kJ/mol	NIST
Tig	723.15	K	NCMS SOLV-DB
BasG	805.60	kJ/mol	NIST
μ	1.79	debye	ChemSep v8.3 pure component data Compiled value
η	0.0005510	Pa×s	Densities and Viscosities of Ternary Mixtures of Cyclohexane + Cyclohexanone + Some Alkyl Acetates at 298.15 K
εr	6.00		NCMS SOLV-DB
Tflash,cc	286.15	K	NCMS SOLV-DB
ΔfG°	-320.40	kJ/mol	ChemSep v8.3 pure component data Compiled value
ΔfH°gas	-464.80	kJ/mol	ChemSep v8.3 pure component data Compiled value
ΔfusH°	13.07	kJ/mol	Joback Calculated Property
ΔvapH°	[34.30; 39.83]	kJ/mol
ΔvapH°	39.83	kJ/mol	NCMS SOLV-DB
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	1.240		NCMS SOLV-DB
McVol	88.750	ml/mol	McGowan Calculated Property
NFPA Fire	3		NCMS SOLV-DB
NFPA Health	1		NCMS SOLV-DB
NFPA Safety	0		NCMS SOLV-DB
Pc	[3330.00; 3530.00]	kPa
Pc	3360.00	kPa	IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value
Pc	3333.59	kPa	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Pc	3330.00	kPa	ChemSep v8.3 pure component data Compiled value
Pc	3335.00 ± 81.06	kPa	NIST
Pc	3365.10 ± 40.00	kPa	NIST
Pc	Outlier 3530.00 ± 101.32	kPa	NIST
Ptriple	1.71e-05	kPa	ChemSep v8.3 pure component data Compiled value
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	728.00		NIST
Inp	707.00		NIST
Inp	696.00		NIST
Inp	713.00		NIST
Inp	698.00		NIST
Ip	[928.00; 996.00]
Ip	943.00		NIST
Ip	992.00		NIST
Ip	981.00		NIST
Ip	978.00		NIST
Ip	994.00		NIST
Ip	944.00		NIST
Ip	970.00		NIST
Ip	986.00		NIST
Ip	976.00		NIST
Ip	996.00		NIST
Ip	980.00		NIST
Ip	947.00		NIST
Ip	969.00		NIST
Ip	992.00		NIST
Ip	996.00		NIST
Ip	941.00		NIST
Ip	977.00		NIST
Ip	968.00		NIST
Ip	983.00		NIST
Ip	972.00		NIST
Ip	952.00		NIST
Ip	952.00		NIST
Ip	957.00		NIST
Ip	957.00		NIST
Ip	976.00		NIST
Ip	977.00		NIST
Ip	992.00		NIST
Ip	935.00		NIST
Ip	982.00		NIST
Ip	939.00		NIST
Ip	960.00		NIST
Ip	970.00		NIST
Ip	995.00		NIST
Ip	969.00		NIST
Ip	982.00		NIST
Ip	Outlier 928.00		NIST
Ip	962.00		NIST
Ip	967.00		NIST
Ip	971.00		NIST
Ip	969.00		NIST
Ip	979.00		NIST
Ip	970.00		NIST
Ip	968.60		NIST
Ip	962.00		NIST
Ip	973.00		NIST
Ip	974.00		NIST
Ip	976.00		NIST
Ip	976.00		NIST
Ip	992.00		NIST
Ip	961.00		NIST
Ip	982.00		NIST
Ip	935.00		NIST
Ip	935.00		NIST
Ip	945.00		NIST
Ip	976.00		NIST
Ip	977.00		NIST
Ip	984.00		NIST
Ip	984.00		NIST
Ip	966.00		NIST
Ip	971.00		NIST
Ip	973.00		NIST
Ip	Outlier 932.00		NIST
Ip	942.00		NIST
Ip	984.00		NIST
Ip	962.00		NIST
Ip	984.00		NIST
Ip	963.00		NIST
Ip	990.00		NIST
Ip	990.00		NIST
Ip	990.00		NIST
Ip	986.00		NIST
Ip	975.00		NIST
Ip	950.00		NIST
Ip	992.00		NIST
Ip	945.00		NIST
Ip	966.00		NIST
Ip	984.00		NIST
Ip	990.00		NIST
Ip	947.00		NIST
Ip	943.00		NIST
Ip	944.00		NIST
Ip	995.00		NIST
Ip	969.00		NIST
Ip	968.00		NIST
Ip	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	374.65	K	ChemSep v8.3 pure component data Compiled value
Tboil	374.75	K	NCMS SOLV-DB
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	[537.70; 549.73]	K
Tc	549.70	K	IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value
Tc	549.40	K	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Tc	549.40	K	ChemSep v8.3 pure component data Compiled value
Tc	549.40	K	NIST
Tc	549.73 ± 0.05	K	NIST
Tc	549.40 ± 1.00	K	NIST
Tc	549.40 ± 1.00	K	NIST
Tc	Outlier 537.70 ± 10.00	K	NIST
Tc	549.50 ± 1.00	K	NIST
Tfus	[178.15; 180.15]	K
Tfus	180.15	K	Jean-Claude Bradley Open Melting Point Dataset (2014, CC0) Compiled value
Tfus	178.15	K	ChemSep v8.3 pure component data Compiled value
Tfus	179.55	K	Aq. Solubility Prediction
Tfus	178.15	K	NCMS SOLV-DB
Tfus	178.15	K	NIST
Tfus	178.15 ± 0.60	K	NIST
Ttriple	178.15	K	ChemSep v8.3 pure component data Compiled value
UQi	3.66		ChemSep v8.3 pure component data Compiled value
URi	4.15		ChemSep v8.3 pure component data Compiled value
Vc	[0.345; 0.345]	m3/kmol
Vc	0.345	m3/kmol	IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value
Vc	0.345	m3/kmol	PSRK revision IV (2005), critical constants and acentric factors of 1000 components Compiled value
Vc	0.345	m3/kmol	ChemSep v8.3 pure component data Compiled value
Zc	[0.2520000; 0.2540000]
Zc	0.2540000		IUPAC Vapor-Liquid Critical Properties of Elements and Compounds, part 7 Compiled value
Zc	0.2520000		ChemSep v8.3 pure component data Compiled value

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; 0.0005510]	Pa×s	[298.15; 313.15]
η	0.0005510	Pa×s	298.15	NCMS SOLV-DB
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	4.49	kPa	298.15	NCMS SOLV-DB
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	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	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	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	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	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	50.40	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	1.38300		298.15	NCMS SOLV-DB
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	1.38180		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	1.38181		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	1.38150		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	1.38280		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	298.15	NCMS SOLV-DB
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(P)	[322.62; 374.66]	K	[14.90; 101.26]
Tboil(P)	322.62	K	14.90	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	325.01	K	16.60	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	327.77	K	18.56	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	329.58	K	20.00	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	334.71	K	24.75	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	337.78	K	27.99	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	341.96	K	33.06	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	345.55	K	37.76	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	347.21	K	40.07	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	350.05	K	44.38	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	352.73	K	48.69	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	355.66	K	54.33	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	358.60	K	60.03	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	361.80	K	66.87	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	364.80	K	73.94	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	367.13	K	79.95	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	369.07	K	85.25	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	371.41	K	91.51	Study of Vapor-Liquid Equilibria for Acetic Acid + n-Propyl Acetate + Isopropyl Acetate Systems
Tboil(P)	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
Cp,gas	[123.02; 320.38]	J/mol×K	[246.45; 1500.00]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A + exp(B/T + C + D·T + E·T²) Y is Cp,gas in J/mol×K, T in K
Coefficient A			1.08820e+02
Coefficient B			-9.37380e+02
Coefficient C			6.60324e+00
Coefficient D			-6.29620e-04
Coefficient E			1.42490e-07
Temperature range, min.			246.45
Temperature range, max.			1500.00
Cp,gas	123.02	J/mol×K	246.45	Calculated Property
Cp,gas	160.83	J/mol×K	385.73	Calculated Property
Cp,gas	201.26	J/mol×K	525.02	Calculated Property
Cp,gas	234.88	J/mol×K	664.30	Calculated Property
Cp,gas	260.66	J/mol×K	803.58	Calculated Property
Cp,gas	279.89	J/mol×K	942.87	Calculated Property
Cp,gas	294.23	J/mol×K	1082.15	Calculated Property
Cp,gas	305.06	J/mol×K	1221.43	Calculated Property
Cp,gas	313.50	J/mol×K	1360.72	Calculated Property
Cp,gas	320.38	J/mol×K	1500.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
Cp,liquid	[163.37; 237.27]	J/mol×K	[192.29; 404.70]	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			1.24410e+02
Coefficient B			3.69320e+01
Coefficient C			1.48054e+00
Coefficient D			1.26620e-02
Coefficient E			-1.20280e-05
Temperature range, min.			192.29
Temperature range, max.			404.70
Cp,liquid	163.37	J/mol×K	192.29	Calculated Property
Cp,liquid	170.23	J/mol×K	215.89	Calculated Property
Cp,liquid	177.78	J/mol×K	239.49	Calculated Property
Cp,liquid	185.95	J/mol×K	263.09	Calculated Property
Cp,liquid	194.58	J/mol×K	286.69	Calculated Property
Cp,liquid	203.49	J/mol×K	310.30	Calculated Property
Cp,liquid	212.47	J/mol×K	333.90	Calculated Property
Cp,liquid	221.27	J/mol×K	357.50	Calculated Property
Cp,liquid	229.63	J/mol×K	381.10	Calculated Property
Cp,liquid	237.27	J/mol×K	404.70	Calculated Property

Property	Value	Unit	Temperature (K)	Source
η	[0.0010076; 0.0001050]	Pa×s	[250.00; 473.15]	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			1.54530e+01
Coefficient B			-1.57900e+02
Coefficient C			-3.93040e+00
Coefficient D			-3.21020e-07
Coefficient E			2.00000e+00
Temperature range, min.			250.00
Temperature range, max.			473.15
η	0.0010076	Pa×s	250.00	Calculated Property
η	0.0007325	Pa×s	274.79	Calculated Property
η	0.0005445	Pa×s	299.59	Calculated Property
η	0.0004127	Pa×s	324.38	Calculated Property
η	0.0003181	Pa×s	349.18	Calculated Property
η	0.0002489	Pa×s	373.97	Calculated Property
η	0.0001973	Pa×s	398.77	Calculated Property
η	0.0001583	Pa×s	423.56	Calculated Property
η	0.0001283	Pa×s	448.36	Calculated Property
η	0.0001050	Pa×s	473.15	Calculated Property

Property	Value	Unit	Temperature (K)	Source
ΔvapH	[50.48; 0.78]	kJ/mol	[178.15; 549.35]	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			8.04750e+01
Coefficient B			1.79802e+00
Coefficient C			-2.25987e+00
Coefficient D			1.29347e+00
Coefficient E			-3.33711e-01
Critical temperature, Tc (K)			5.49400e+02
Temperature range, min.			178.15
Temperature range, max.			549.35
ΔvapH	50.48	kJ/mol	178.15	Calculated Property
ΔvapH	46.39	kJ/mol	219.39	Calculated Property
ΔvapH	42.81	kJ/mol	260.64	Calculated Property
ΔvapH	39.53	kJ/mol	301.88	Calculated Property
ΔvapH	36.40	kJ/mol	343.13	Calculated Property
ΔvapH	33.21	kJ/mol	384.37	Calculated Property
ΔvapH	29.72	kJ/mol	425.62	Calculated Property
ΔvapH	25.47	kJ/mol	466.86	Calculated Property
ΔvapH	19.37	kJ/mol	508.11	Calculated Property
ΔvapH	0.78	kJ/mol	549.35	Calculated Property

Property	Value	Unit	Temperature (K)	Source
Pvap	[1.33; 202.64]	kPa	[276.65; 398.87]	The Yaws Handbook of Vapor Pressure
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
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	[2.01e-05; 3336.35]	kPa	[178.15; 549.73]	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			9.97535e+01
Coefficient B			-8.09502e+03
Coefficient C			-1.26216e+01
Coefficient D			8.99947e-06
Coefficient E			2.00000e+00
Temperature range, min.			178.15
Temperature range, max.			549.73
Pvap	2.01e-05	kPa	178.15	Calculated Property
Pvap	8.68e-03	kPa	219.44	Calculated Property
Pvap	0.41	kPa	260.72	Calculated Property
Pvap	5.45	kPa	302.01	Calculated Property
Pvap	34.52	kPa	343.30	Calculated Property
Pvap	135.63	kPa	384.58	Calculated Property
Pvap	389.40	kPa	425.87	Calculated Property
Pvap	905.48	kPa	467.16	Calculated Property
Pvap	1824.63	kPa	508.44	Calculated Property
Pvap	3336.35	kPa	549.73	Calculated Property
Pvap	[2.14e-05; 3330.47]	kPa	[178.15; 549.40]	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			9.54327e+01
Coefficient B			-7.93197e+03
Coefficient C			-1.19486e+01
Coefficient D			8.27424e-06
Coefficient E			0.00000e+00
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
Pvap	[9.20; 99.48]	kPa	[312.22; 374.03]	NIST
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
Coefficient A			1.41468e+01
Coefficient B			-2.95620e+03
Coefficient C			-6.43780e+01
Reference			Polák and Mertl, 1965
Comment			Coefficents calculated by NIST from author's data.
Temperature range, min.			312.22
Temperature range, max.			374.03
Pvap	9.20	kPa	312.22	Calculated Property
Pvap	12.69	kPa	319.09	Calculated Property
Pvap	17.21	kPa	325.96	Calculated Property
Pvap	22.98	kPa	332.82	Calculated Property
Pvap	30.24	kPa	339.69	Calculated Property
Pvap	39.27	kPa	346.56	Calculated Property
Pvap	50.37	kPa	353.43	Calculated Property
Pvap	63.87	kPa	360.29	Calculated Property
Pvap	80.11	kPa	367.16	Calculated Property
Pvap	99.48	kPa	374.03	Calculated Property

Property	Value	Unit	Temperature (K)	Source
ρl	[1004.66; 299.06]	kg/m3	[178.15; 549.35]	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			5.89821e+01
Coefficient B			2.25500e-01
Coefficient C			5.49400e+02
Coefficient D			2.58840e-01
Temperature range, min.			178.15
Temperature range, max.			549.35
ρl	1004.66	kg/m3	178.15	Calculated Property
ρl	964.88	kg/m3	219.39	Calculated Property
ρl	923.04	kg/m3	260.64	Calculated Property
ρl	878.62	kg/m3	301.88	Calculated Property
ρl	830.90	kg/m3	343.13	Calculated Property
ρl	778.73	kg/m3	384.37	Calculated Property
ρl	720.11	kg/m3	425.62	Calculated Property
ρl	651.02	kg/m3	466.86	Calculated Property
ρl	560.54	kg/m3	508.11	Calculated Property
ρl	299.06	kg/m3	549.35	Calculated Property

Property	Value	Unit	Temperature (K)	Source
γ	[0.04; 0.02]	N/m	[180.15; 374.75]	Jasper (1972), surface tension of pure liquid compounds Compiled value
Equation			Y = A + B·T + C·T² + D·T³ + E·T⁴ Y is γ in N/m, T in K
Coefficient A			5.71928e-02
Coefficient B			-1.12000e-04
Coefficient C			0.00000e+00
Coefficient D			0.00000e+00
Coefficient E			0.00000e+00
Temperature range, min.			180.15
Temperature range, max.			374.75
γ	0.04	N/m	180.15	Calculated Property
γ	0.03	N/m	201.77	Calculated Property
γ	0.03	N/m	223.39	Calculated Property
γ	0.03	N/m	245.02	Calculated Property
γ	0.03	N/m	266.64	Calculated Property
γ	0.02	N/m	288.26	Calculated Property
γ	0.02	N/m	309.88	Calculated Property
γ	0.02	N/m	331.51	Calculated Property
γ	0.02	N/m	353.13	Calculated Property
γ	0.02	N/m	374.75	Calculated Property
γ	[0.04; 9.52e-04]	N/m	[178.15; 530.17]	ChemSep v8.3 pure component data Compiled value
Equation			Y = A + exp(B/T + C + D·T + E·T²) Y is γ in N/m, T in K
Coefficient A			-1.27130e-02
Coefficient B			3.60140e+01
Coefficient C			-3.07940e+00
Coefficient D			4.25480e-04
Coefficient E			-5.36160e-06
Temperature range, min.			178.15
Temperature range, max.			530.17
γ	0.04	N/m	178.15	Calculated Property
γ	0.03	N/m	217.26	Calculated Property
γ	0.03	N/m	256.38	Calculated Property
γ	0.02	N/m	295.49	Calculated Property
γ	0.02	N/m	334.60	Calculated Property
γ	0.02	N/m	373.72	Calculated Property
γ	0.01	N/m	412.83	Calculated Property
γ	0.01	N/m	451.94	Calculated Property
γ	0.00	N/m	491.06	Calculated Property
γ	9.52e-04	N/m	530.17	Calculated Property

Property	Value	Unit	Temperature (K)	Source
λgas	[0.00; 0.11]	W/m×K	[178.15; 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			1.12850e+03
Coefficient B			1.01400e+00
Coefficient C			1.16050e+10
Coefficient D			-1.28690e+11
Temperature range, min.			178.15
Temperature range, max.			1000.00
λgas	0.00	W/m×K	178.15	Calculated Property
λgas	0.01	W/m×K	269.47	Calculated Property
λgas	0.01	W/m×K	360.78	Calculated Property
λgas	0.02	W/m×K	452.10	Calculated Property
λgas	0.03	W/m×K	543.42	Calculated Property
λgas	0.04	W/m×K	634.73	Calculated Property
λgas	0.06	W/m×K	726.05	Calculated Property
λgas	0.07	W/m×K	817.37	Calculated Property
λgas	0.09	W/m×K	908.68	Calculated Property
λgas	0.11	W/m×K	1000.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
λliquid	[0.18; 0.10]	W/m×K	[164.82; 434.82]	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			4.55130e-02
Coefficient B			-3.13280e+01
Coefficient C			-1.55720e+00
Coefficient D			-6.65380e-04
Coefficient E			-5.33340e-06
Temperature range, min.			164.82
Temperature range, max.			434.82
λliquid	0.18	W/m×K	164.82	Calculated Property
λliquid	0.17	W/m×K	194.82	Calculated Property
λliquid	0.17	W/m×K	224.82	Calculated Property
λliquid	0.16	W/m×K	254.82	Calculated Property
λliquid	0.15	W/m×K	284.82	Calculated Property
λliquid	0.14	W/m×K	314.82	Calculated Property
λliquid	0.13	W/m×K	344.82	Calculated Property
λliquid	0.12	W/m×K	374.82	Calculated Property
λliquid	0.11	W/m×K	404.82	Calculated Property
λliquid	0.10	W/m×K	434.82	Calculated Property

Similar Compounds

Find more compounds similar to Acetic acid, propyl ester.

Mixtures

• 1-Propanol + Carbon dioxide + Acetic acid, propyl ester
• Acetic acid, propyl ester + Diethyl sulfide
• 2-Propyn-1-ol + Acetic acid, propyl ester + Water
• Acetic acid, propyl ester + Water
• Furfural + Acetic acid, propyl ester + Water
• 1-Propanol + Acetic acid, propyl ester + Water
• Diosgenin + Acetic acid, propyl ester
• Acetic acid, propyl ester + 1,2,4-Trimethylbenzene
• Acetic acid, propyl ester + Mesitylene
• 1-Hexyne + Acetic acid, propyl ester
• Acetic acid, propyl ester + 2-Hexyne
• Acetic acid, propyl ester + 3-Hexyne
• Acetic acid + Acetic acid, propyl ester + Water
• Heptane + Acetic acid, propyl ester
• Acetic acid, propyl ester + Nonane
• Undecane + Acetic acid, propyl ester
• Tridecane + Acetic acid, propyl ester
• Pentadecane + Acetic acid, propyl ester
• Heptadecane + Acetic acid, propyl ester
• 2-Propanol + Acetic acid, propyl ester

Find more mixtures with Acetic acid, propyl ester.

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.
• 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
• Examination of hydrogen-bonding interactions between dissolved solutes and alkylbenzene solvents based on Abraham model correlations derived from measured enthalpies of solvation
• Effect of halogen substitution on the enthalpies of solvation and hydrogen bonding of organic solutes in chlorobenzene and 1,2-dichlorobenzene derived using multi-parameter correlations
• Enthalpies of solution and enthalpies of solvation of organic solutes in ethylene glycol at 298.15 K: Prediction and analysis of intermolecular interaction contributions
• 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
• NCMS SOLV-DB
• The Yaws Handbook of Vapor Pressure

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