Chemical Properties of Butanedioic acid, diethyl ester (CAS 123-25-1)

InChI

InChI=1S/C8H14O4/c1-3-11-7(9)5-6-8(10)12-4-2/h3-6H2,1-2H3

InChI Key

DKMROQRQHGEIOW-UHFFFAOYSA-N

Formula

C8H14O4

SMILES

CCOC(=O)CCC(=O)OCC

Molecular Weight¹

174.19

CAS

123-25-1

Other Names

• BUTANEDIOIC ACID DIETHYL ESTER
• Clorius
• Diethyl ester of butanedioic acid
• Diethylester kyseliny jantarove
• diethyl butanedioate
• diethyl succinate
• ethyl succinate
• succinic acid, diethyl ester

• ω : Acentric Factor.
• 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).
• NFPA Fire : NFPA Fire Rating.
• NFPA Health : NFPA Health Rating.
• P_c : Critical Pressure (kPa).
• P_vap : Vapor pressure (kPa).
• ρ_c : Critical density (kg/m³).
• ρ_l : Liquid Density (kg/m³).
• I_np : Non-polar retention indices.
• I_p : Polar retention indices.
• T_boil : Normal Boiling Point Temperature (K).
• T_boilr : Boiling point at reduced pressure (K).
• T_c : Critical Temperature (K).
• λ_liquid : Liquid thermal conductivity (W/m×K).
• T_fus : Normal melting (fusion) point (K).
• V_c : Critical Volume (m³/kmol).
• ¹: Molecular weight from the IUPAC atomic weights tables.

Contents

1. Physical Properties
2. Temperature Dependent Properties
3. Pressure Dependent Properties
4. Datasets
5. Correlations
6. Similar Compounds
7. Mixtures
8. Sources

Physical Properties

Property	Value	Unit	Source
ω	0.5992		Relay (1.0) Calculated Property
ΔfG°	-604.26	kJ/mol	Joback Calculated Property
ΔfH°gas	-852.35	kJ/mol	Relay (1.0) Calculated Property
ΔfusH°	25.21	kJ/mol	Joback Calculated Property
ΔvapH°	64.04	kJ/mol	Relay (1.0) Calculated Property
IE	9.75	eV	Relay (1.0) Calculated Property
log10WS	-0.96		Aq. Solubility Prediction
logPoct/wat	0.893		Crippen Calculated Property
McVol	138.460	ml/mol	McGowan Calculated Property
NFPA Fire	1		KDB
NFPA Health	1		KDB
Pc	2260.00 ± 5.00	kPa	NIST
ρc	306.58 ± 3.48	kg/m3	NIST
Inp	[1138.00; 1198.00]
Inp	1180.90		NIST
Inp	1149.00		NIST
Inp	1185.00		NIST
Inp	1193.00		NIST
Inp	1191.00		NIST
Inp	1179.00		NIST
Inp	1139.00		NIST
Inp	1180.90		NIST
Inp	1165.00		NIST
Inp	1181.00		NIST
Inp	1149.00		NIST
Inp	1148.00		NIST
Inp	1149.00		NIST
Inp	1147.00		NIST
Inp	1145.00		NIST
Inp	1191.00		NIST
Inp	1176.00		NIST
Inp	1188.00		NIST
Inp	1191.00		NIST
Inp	1176.00		NIST
Inp	1182.00		NIST
Inp	1181.00		NIST
Inp	1145.00		NIST
Inp	1172.00		NIST
Inp	1170.00		NIST
Inp	1170.00		NIST
Inp	1191.00		NIST
Inp	1183.00		NIST
Inp	1182.00		NIST
Inp	1146.00		NIST
Inp	1153.00		NIST
Inp	1153.00		NIST
Inp	1182.00		NIST
Inp	1182.00		NIST
Inp	1179.00		NIST
Inp	1166.00		NIST
Inp	1167.00		NIST
Inp	1138.00		NIST
Inp	1146.00		NIST
Inp	1198.00		NIST
Inp	1185.00		NIST
Inp	1170.00		NIST
Inp	1146.00		NIST
Inp	1179.00		NIST
Inp	1198.00		NIST
Inp	1191.00		NIST
Inp	1182.00		NIST
Ip	[1642.00; 1716.00]
Ip	1694.00		NIST
Ip	1679.00		NIST
Ip	1680.00		NIST
Ip	1687.00		NIST
Ip	1704.00		NIST
Ip	1690.00		NIST
Ip	1658.00		NIST
Ip	1677.00		NIST
Ip	1699.00		NIST
Ip	1681.20		NIST
Ip	1684.00		NIST
Ip	1681.00		NIST
Ip	1705.00		NIST
Ip	1661.00		NIST
Ip	1675.00		NIST
Ip	1690.00		NIST
Ip	1690.00		NIST
Ip	1677.00		NIST
Ip	1667.00		NIST
Ip	1690.00		NIST
Ip	1714.00		NIST
Ip	1697.00		NIST
Ip	1672.00		NIST
Ip	1672.00		NIST
Ip	1655.00		NIST
Ip	1677.00		NIST
Ip	1706.00		NIST
Ip	1668.00		NIST
Ip	1697.00		NIST
Ip	1702.00		NIST
Ip	1669.00		NIST
Ip	1675.00		NIST
Ip	1682.00		NIST
Ip	1688.00		NIST
Ip	1689.00		NIST
Ip	1689.00		NIST
Ip	1689.00		NIST
Ip	1689.00		NIST
Ip	1679.00		NIST
Ip	1686.00		NIST
Ip	1690.00		NIST
Ip	1687.00		NIST
Ip	1683.00		NIST
Ip	1700.00		NIST
Ip	1673.00		NIST
Ip	1677.00		NIST
Ip	1701.00		NIST
Ip	1664.00		NIST
Ip	1701.00		NIST
Ip	1678.00		NIST
Ip	1701.00		NIST
Ip	1668.00		NIST
Ip	1675.00		NIST
Ip	Outlier 1716.00		NIST
Ip	1662.00		NIST
Ip	1674.00		NIST
Ip	1668.00		NIST
Ip	1655.00		NIST
Ip	1683.00		NIST
Ip	1667.00		NIST
Ip	Outlier 1642.00		NIST
Ip	1668.00		NIST
Ip	1698.00		NIST
Ip	1689.00		NIST
Ip	1673.00		NIST
Ip	1680.00		NIST
Ip	1690.00		NIST
Ip	1714.00		NIST
Ip	1679.00		NIST
Ip	1700.00		NIST
Ip	1701.00		NIST
Ip	Outlier 1716.00		NIST
Ip	1683.00		NIST
Ip	1689.00		NIST
Tboil	[489.00; 490.90]	K
Tboil	490.80	K	Liquid-liquid equilibria of (water + butyric acid + diethyl succinate or diethyl glutarate or diethyl adipate) ternary systems
Tboil	490.80	K	(Liquid + liquid) equilibria of (water + propionic acid + diethyl succinate or diethyl glutarate or diethyl adipate) ternary systems
Tboil	490.85	K	Liquid-Liquid Equilibria of (Water + Acetic Acid + Diethyl Succinate or Diethyl Glutarate or Diethyl Adipate) Ternary Systems
Tboil	490.90	K	KDB
Tboil	490.90	K	NIST
Tboil	490.35	K	NIST
Tboil	Outlier 489.00 ± 8.00	K	NIST
Tboil	490.90 ± 0.60	K	NIST
Tboil	490.40 ± 0.50	K	NIST
Tboil	490.30 ± 0.25	K	NIST
Tc	[663.00; 666.00]	K
Tc	666.00	K	Critical temperatures and pressures of some dicarboxylic acid diethyl esters
Tc	663.00	K	KDB
Tc	665.00 ± 2.00	K	NIST
Tc	663.00 ± 5.00	K	NIST
Tfus	[251.20; 252.48]	K
Tfus	251.63	K	Phase Equilibrium and Physical Properties for the Purification of Propylene Carbonate (PC) and y-Butyrolactone (GBL)
Tfus	252.00	K	KDB
Tfus	252.48	K	Aq. Solubility Prediction
Tfus	252.25	K	NIST
Tfus	251.20 ± 0.50	K	NIST
Tfus	251.90 ± 0.40	K	NIST
Vc	0.544	m3/kmol	Relay (1.0) Calculated Property

Temperature Dependent Properties

Property	Value	Unit	Temperature (K)	Source
Cp,liquid	[330.50; 338.10]	J/mol×K	[292.60; 298.15]
Cp,liquid	338.10	J/mol×K	292.60	NIST
Cp,liquid	338.10	J/mol×K	292.60	NIST
Cp,liquid	330.50	J/mol×K	298.15	NIST
ΔvapH	56.50	kJ/mol	408.50	NIST
Pvap	[4.95e-03; 0.34]	kPa	[290.20; 345.50]
Pvap	4.95e-03	kPa	290.20	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	5.04e-03	kPa	290.50	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	6.78e-03	kPa	293.50	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	8.61e-03	kPa	296.40	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.01	kPa	301.40	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.02	kPa	306.40	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.03	kPa	311.40	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.04	kPa	313.40	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.05	kPa	316.40	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.05	kPa	318.40	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.07	kPa	321.40	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.08	kPa	323.50	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.09	kPa	326.50	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.10	kPa	326.50	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.11	kPa	328.50	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.13	kPa	331.40	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.14	kPa	331.60	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.15	kPa	333.60	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.19	kPa	336.50	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.22	kPa	339.40	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.27	kPa	342.40	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
Pvap	0.34	kPa	345.50	Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
ρl	[966.91; 1044.83]	kg/m3	[288.15; 363.15]
ρl	1044.83	kg/m3	288.15	Volumetric and viscometric study with FT-IR analysis of binary systems with diethyl succinate and alcohols
ρl	1039.63	kg/m3	293.15	Volumetric and viscometric study with FT-IR analysis of binary systems with diethyl succinate and alcohols
ρl	1034.44	kg/m3	298.15	Volumetric and viscometric study with FT-IR analysis of binary systems with diethyl succinate and alcohols
ρl	1035.34	kg/m3	298.20	Modeling phase equilibria of ternary systems (water + formic acid + ester or alcohol) through UNIFAC-original, SERLAS, NRTL, NRTL-modified, and three-suffix Margules: Parameter estimation using genetic algorithm
ρl	1029.59	kg/m3	303.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	1029.25	kg/m3	303.15	Volumetric and viscometric study with FT-IR analysis of binary systems with diethyl succinate and alcohols
ρl	1024.40	kg/m3	308.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	1024.08	kg/m3	308.15	Volumetric and viscometric study with FT-IR analysis of binary systems with diethyl succinate and alcohols
ρl	1019.20	kg/m3	313.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	1018.90	kg/m3	313.15	Volumetric and viscometric study with FT-IR analysis of binary systems with diethyl succinate and alcohols
ρl	1014.01	kg/m3	318.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	1013.72	kg/m3	318.15	Volumetric and viscometric study with FT-IR analysis of binary systems with diethyl succinate and alcohols
ρl	1008.81	kg/m3	323.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	1008.55	kg/m3	323.15	Volumetric and viscometric study with FT-IR analysis of binary systems with diethyl succinate and alcohols
ρl	1003.60	kg/m3	328.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	998.39	kg/m3	333.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	993.16	kg/m3	338.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	987.93	kg/m3	343.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	982.70	kg/m3	348.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	977.45	kg/m3	353.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	972.19	kg/m3	358.15	Surface tension of four oxygenated fuels: experiment and correlation
ρl	966.91	kg/m3	363.15	Surface tension of four oxygenated fuels: experiment and correlation

Pressure Dependent Properties

Property	Value	Unit	Pressure (kPa)	Source
Tboilr	378.20	K	2.00	NIST

Datasets

1. Mass density, kg/m3 (1)
2. Thermal conductivity, W/m/K (1)

Mass density, kg/m3

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Mass density, kg/m3 - Liquid
283.57	100.00	1049.61
283.57	1000.00	1050.21
283.57	3000.00	1051.56
283.57	5000.00	1052.88
283.57	10000.00	1056.11
283.57	15000.00	1059.25
283.58	20000.00	1062.29
283.58	25000.00	1065.25
283.57	30000.00	1068.16
283.57	40000.00	1073.71
283.57	50000.00	1079.0
283.57	60000.00	1084.1
283.57	70000.00	1089.01
283.57	80000.00	1093.63
283.57	90010.00	1098.12
283.56	100010.00	1102.48
293.49	100.00	1039.78
293.50	1000.00	1040.41
293.50	3000.00	1041.81
293.50	5000.00	1043.2
293.50	10000.00	1046.6
293.50	15000.00	1049.91
293.49	20000.00	1053.11
293.49	25000.00	1056.23
293.50	30000.00	1059.25
293.49	40000.00	1065.07
293.50	50000.00	1070.61
293.49	60000.00	1075.9
293.50	70000.00	1080.89
293.50	80000.00	1085.77
293.51	90000.00	1090.39
293.51	100000.00	1094.9
303.42	100.00	1028.98
303.42	1000.00	1029.62
303.43	3000.00	1031.12
303.43	5000.00	1032.59
303.44	10000.00	1036.15
303.43	15000.00	1039.61
303.42	20000.00	1042.98
303.42	25000.00	1046.26
303.43	30000.00	1049.4
303.43	40000.00	1055.5
303.43	50000.00	1061.26
303.42	60000.00	1066.78
303.42	70000.00	1072.05
303.42	80000.00	1077.09
303.43	90000.00	1081.92
303.43	100000.00	1086.58
313.33	100.00	1018.75
313.33	1000.00	1019.44
313.33	3000.00	1021.07
313.32	5000.00	1022.61
313.32	10000.00	1026.44
313.31	15000.00	1030.05
313.33	20000.00	1033.63
313.33	25000.00	1037.06
313.32	30000.00	1040.39
313.32	40000.00	1046.78
313.31	50000.00	1052.81
313.33	60000.00	1058.52
313.33	70000.00	1064.01
313.33	80000.00	1069.21
313.33	90000.00	1074.2
313.33	100000.00	1078.99
323.18	100.00	1008.44
323.18	1000.00	1009.19
323.18	3000.00	1010.86
323.19	5000.00	1012.5
323.18	10000.00	1016.52
323.18	15000.00	1020.37
323.18	20000.00	1024.08
323.18	25000.00	1027.7
323.19	30000.00	1031.17
323.19	40000.00	1037.8
323.19	50000.00	1044.06
323.19	60000.00	1050.01
323.19	70000.00	1055.67
323.19	80000.00	1061.06
323.19	90000.00	1066.22
323.19	100000.00	1071.19
333.10	100.00	998.31
333.10	1000.00	999.11
333.10	3000.00	1000.91
333.10	5000.00	1002.64
333.11	10000.00	1006.85
333.11	15000.00	1010.94
333.11	20000.00	1014.85
333.11	25000.00	1018.62
333.11	30000.00	1022.27
333.11	40000.00	1029.2
333.11	50000.00	1035.72
333.11	60000.00	1041.91
333.11	70000.00	1047.69
333.11	80000.00	1053.26
333.11	90000.00	1058.57
333.11	100000.00	1063.7
342.97	100.00	987.87
342.98	1000.00	988.73
342.98	3000.00	990.63
342.98	5000.00	992.45
342.98	10000.00	996.91
342.97	15000.00	1001.22
342.97	20000.00	1005.3
342.98	25000.00	1009.24
342.97	30000.00	1013.07
342.97	40000.00	1020.32
342.97	50000.00	1027.1
342.98	60000.00	1033.53
342.97	70000.00	1039.64
342.98	80000.00	1045.43
342.97	90000.00	1050.91
342.97	100000.00	1056.19
352.82	100.00	977.64
352.82	1000.00	978.58
352.82	3000.00	980.59
352.82	5000.00	982.53
352.82	10000.00	987.26
352.82	15000.00	991.79
352.83	20000.00	996.08
352.83	25000.00	1000.24
352.83	30000.00	1004.25
352.83	40000.00	1011.8
352.83	50000.00	1018.87
352.83	60000.00	1025.54
352.83	70000.00	1031.82
352.83	80000.00	1037.81
352.83	90000.00	1043.47
352.83	100010.00	1048.95
362.66	100.00	967.3
362.66	1000.00	968.28
362.66	3000.00	970.41
362.67	5000.00	972.48
362.67	10000.00	977.45
362.67	15000.00	982.21
362.67	20000.00	986.74
362.67	25000.00	991.07
362.67	30000.00	995.26
362.67	40000.00	1003.16
362.67	50000.00	1010.5
362.66	60000.00	1017.41
362.67	70000.00	1023.98
362.67	80000.00	1030.14
362.67	90000.00	1036.01
362.67	100000.00	1041.65
Reference

Thermal conductivity, W/m/K

Fixed		Measured
Temperature, K - Liquid	Pressure, kPa - Liquid	Thermal conductivity, W/m/K - Liquid
264.81	5000.00	0.1565
265.06	100.00	0.1559
265.23	15000.00	0.1602
265.57	15000.00	0.1596
265.83	10000.00	0.1586
265.83	20000.00	0.1615
265.94	20000.00	0.1602
266.08	15000.00	0.1594
266.13	10000.00	0.1582
266.38	100.00	0.1561
266.47	5000.00	0.1571
266.81	20000.00	0.1607
266.94	5000.00	0.1572
267.04	100.00	0.1561
267.83	10000.00	0.1589
284.87	20000.00	0.1580
285.16	10000.00	0.1556
285.41	20000.00	0.1579
285.62	5000.00	0.1539
285.63	100.00	0.1527
285.68	15000.00	0.1570
285.71	10000.00	0.1554
286.14	5000.00	0.1537
286.27	15000.00	0.1569
286.33	100.00	0.1528
286.36	10000.00	0.1555
286.56	15000.00	0.1562
286.61	5000.00	0.1538
286.76	20000.00	0.1578
287.36	15000.00	0.1563
287.43	5000.00	0.1535
287.75	100.00	0.1527
304.47	100.00	0.1484
304.53	15000.00	0.1529
304.85	20000.00	0.1551
305.64	20000.00	0.1543
305.66	100.00	0.1483
305.72	10000.00	0.1518
306.12	5000.00	0.1497
306.12	15000.00	0.1529
306.39	20000.00	0.1549
306.44	10000.00	0.1519
306.79	5000.00	0.1501
306.80	15000.00	0.1529
306.84	10000.00	0.1513
307.27	10000.00	0.1510
307.29	5000.00	0.1502
307.33	100.00	0.1482
326.02	100.00	0.1436
326.76	100.00	0.1433
327.17	10000.00	0.1466
327.21	5000.00	0.1448
327.56	100.00	0.1437
327.58	15000.00	0.1489
327.69	20000.00	0.1503
327.81	5000.00	0.1449
328.07	10000.00	0.1471
328.35	15000.00	0.1484
328.56	20000.00	0.1502
328.57	5000.00	0.1449
328.62	10000.00	0.1469
329.63	5000.00	0.1453
329.69	15000.00	0.1481
330.11	20000.00	0.1501
345.18	20000.00	0.1462
345.49	5000.00	0.1404
345.53	100.00	0.1385
345.80	10000.00	0.1422
345.99	5000.00	0.1402
346.11	5000.00	0.1404
346.18	15000.00	0.1448
346.44	10000.00	0.1423
346.52	15000.00	0.1442
346.59	20000.00	0.1462
346.63	100.00	0.1384
346.65	15000.00	0.1446
346.94	20000.00	0.1461
347.16	100.00	0.1385
347.34	10000.00	0.1419
365.09	100.00	0.1339
365.15	10000.00	0.1381
365.16	5000.00	0.1359
365.54	15000.00	0.1395
365.59	5000.00	0.1360
365.79	100.00	0.1341
366.05	20000.00	0.1409
366.11	10000.00	0.1380
366.50	100.00	0.1339
366.54	20000.00	0.1409
366.57	15000.00	0.1399
366.66	20000.00	0.1415
366.72	10000.00	0.1379
367.17	5000.00	0.1358
367.25	20000.00	0.1415
367.31	15000.00	0.1397
385.28	20000.00	0.1379
385.51	10000.00	0.1325
385.95	10000.00	0.1326
385.95	15000.00	0.1349
385.96	20000.00	0.1384
386.02	5000.00	0.1309
386.08	100.00	0.1284
386.15	5000.00	0.1301
386.36	100.00	0.1279
386.50	15000.00	0.1349
386.63	20000.00	0.1378
386.70	5000.00	0.1304
386.80	10000.00	0.1327
386.93	10000.00	0.1321
386.95	5000.00	0.1303
387.06	15000.00	0.1352
387.25	100.00	0.1278
Reference

Correlations

Property	Value	Unit	Temperature (K)	Source
Cp,gas	[207.87; 448.27]	J/mol×K	[273.00; 1000.00]	Joback Predicted correlation
Equation			Y = A + B·T + C·T² + D·T³ + E·T⁴ Y is Cp,gas in J/mol×K, T in K
Coefficient A			4.64340e+01
Coefficient B			6.54240e-01
Coefficient C			-2.22200e-04
Coefficient D			-3.02000e-08
Coefficient E			0.00000e+00
Temperature range, min.			273.00
Temperature range, max.			1000.00
Cp,gas	207.87	J/mol×K	273.00	Calculated Property
Cp,gas	248.74	J/mol×K	353.78	Calculated Property
Cp,gas	286.30	J/mol×K	434.56	Calculated Property
Cp,gas	320.44	J/mol×K	515.33	Calculated Property
Cp,gas	351.08	J/mol×K	596.11	Calculated Property
Cp,gas	378.11	J/mol×K	676.89	Calculated Property
Cp,gas	401.44	J/mol×K	757.67	Calculated Property
Cp,gas	420.97	J/mol×K	838.44	Calculated Property
Cp,gas	436.62	J/mol×K	919.22	Calculated Property
Cp,gas	448.27	J/mol×K	1000.00	Calculated Property

Property	Value	Unit	Temperature (K)	Source
η	[0.0075133; 0.0002629]	Pa×s	[251.91; 464.97]	Joback Predicted correlation
Equation			Y = exp(A + B/T + C·ln(T) + D·T^E) Y is η in Pa×s, T in K
Coefficient A			-1.22078e+01
Coefficient B			1.84316e+03
Coefficient C			0.00000e+00
Coefficient D			0.00000e+00
Coefficient E			0.00000e+00
Comment			Liquid phase. Joback/Reid (1987), valid from Tf to 0.7·Tc.
Temperature range, min.			251.91
Temperature range, max.			464.97
η	0.0075133	Pa×s	251.91	Calculated Property
η	0.0040074	Pa×s	275.58	Calculated Property
η	0.0023609	Pa×s	299.26	Calculated Property
η	0.0015031	Pa×s	322.93	Calculated Property
η	0.0010178	Pa×s	346.61	Calculated Property
η	0.0007245	Pa×s	370.28	Calculated Property
η	0.0005372	Pa×s	393.95	Calculated Property
η	0.0004120	Pa×s	417.63	Calculated Property
η	0.0003252	Pa×s	441.30	Calculated Property
η	0.0002629	Pa×s	464.97	Calculated Property

Property	Value	Unit	Temperature (K)	Source
Pvap	[1.33; 202.64]	kPa	[368.32; 518.70]	The Yaws Handbook of Vapor Pressure
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
Coefficient A			1.61345e+01
Coefficient B			-5.13395e+03
Coefficient C			-4.43450e+01
Temperature range, min.			368.32
Temperature range, max.			518.70
Pvap	1.33	kPa	368.32	Calculated Property
Pvap	2.90	kPa	385.03	Calculated Property
Pvap	5.87	kPa	401.74	Calculated Property
Pvap	11.15	kPa	418.45	Calculated Property
Pvap	20.04	kPa	435.16	Calculated Property
Pvap	34.34	kPa	451.86	Calculated Property
Pvap	56.41	kPa	468.57	Calculated Property
Pvap	89.23	kPa	485.28	Calculated Property
Pvap	136.50	kPa	501.99	Calculated Property
Pvap	202.64	kPa	518.70	Calculated Property
Pvap	[2.77e-05; 2585.44]	kPa	[252.35; 660.00]	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			1.91712e+02
Coefficient B			-1.54243e+04
Coefficient C			-2.56720e+01
Coefficient D			1.41972e-05
Coefficient E			0.00000e+00
Temperature range, min.			252.35
Temperature range, max.			660.00
Pvap	2.77e-05	kPa	252.35	Calculated Property
Pvap	6.24e-03	kPa	297.64	Calculated Property
Pvap	0.23	kPa	342.94	Calculated Property
Pvap	2.93	kPa	388.23	Calculated Property
Pvap	18.59	kPa	433.53	Calculated Property
Pvap	75.48	kPa	478.82	Calculated Property
Pvap	228.69	kPa	524.12	Calculated Property
Pvap	571.71	kPa	569.41	Calculated Property
Pvap	1262.83	kPa	614.71	Calculated Property
Pvap	2585.44	kPa	660.00	Calculated Property
Pvap	[0.13; 101.69]	kPa	[327.80; 489.70]	NIST
Equation			ln(Y) = A + B/(T + C) Y is Pvap in kPa, T in K
Coefficient A			1.74067e+01
Coefficient B			-6.05537e+03
Coefficient C			-1.60620e+01
Reference			Stull, 1947
Comment			Coefficents calculated by NIST from author's data.
Temperature range, min.			327.80
Temperature range, max.			489.70
Pvap	0.13	kPa	327.80	Calculated Property
Pvap	0.38	kPa	345.79	Calculated Property
Pvap	0.99	kPa	363.78	Calculated Property
Pvap	2.34	kPa	381.77	Calculated Property
Pvap	5.08	kPa	399.76	Calculated Property
Pvap	10.30	kPa	417.74	Calculated Property
Pvap	19.65	kPa	435.73	Calculated Property
Pvap	35.55	kPa	453.72	Calculated Property
Pvap	61.38	kPa	471.71	Calculated Property
Pvap	101.69	kPa	489.70	Calculated Property

Similar Compounds

Find more compounds similar to Butanedioic acid, diethyl ester.

Mixtures

• Formic acid + Butanedioic acid, diethyl ester + Water
• Butanedioic acid, diethyl ester + Water
• Butanedioic acid, diethyl ester + Propanoic acid + Water
• 1-Propanol, 2-methyl- + Butanedioic acid, diethyl ester
• 1-Butanol, 3-methyl- + Butanedioic acid, diethyl ester
• Butanedioic acid, diethyl ester + Ethyl Acetate
• Acetic acid + Butanedioic acid, diethyl ester
• Butanedioic acid, diethyl ester + Ethyl Acetate + Water
• Acetic acid + Butanedioic acid, diethyl ester + Water
• Ethanol + Butanedioic acid, diethyl ester
• Ethanol + Butanedioic acid, diethyl ester + Water
• Butanoic acid + Butanedioic acid, diethyl ester + Water
• 1-Propanol + Butanedioic acid, diethyl ester
• 1-Butanol + Butanedioic acid, diethyl ester
• Butanedioic acid, diethyl ester + 1-Hexanol
• Carbon dioxide + Butanedioic acid, diethyl ester
• Carbon dioxide + Ethanol + Butanedioic acid, diethyl ester
• Carbon dioxide + Butanedioic acid, diethyl ester + Ethyl Acetate
• Butanoic acid, ethyl ester + Butanedioic acid, diethyl ester
• Butanoic acid, ethyl ester + 1-Propanol, 2-methyl- + Butanedioic acid, diethyl ester

Find more mixtures with Butanedioic acid, diethyl ester.

Sources

• KDB Vapor Pressure Data
• Cheméo Relay (1.0)
• Crippen Method
• Phase equilibria for reactive distillation of diethyl succinate. Part II: Systems diethyl succinate + ethyl acetate + water and diethyl succinate + acetic acid + water
• Phase equilibria for reactive distillation of diethyl succinate Part I. System diethyl succinate + ethanol + water
• Liquid-liquid equilibria of (water + butyric acid + diethyl succinate or diethyl glutarate or diethyl adipate) ternary systems
• Critical temperatures and pressures of some dicarboxylic acid diethyl esters
• Modeling phase equilibria of ternary systems (water + formic acid + ester or alcohol) through UNIFAC-original, SERLAS, NRTL, NRTL-modified, and three-suffix Margules: Parameter estimation using genetic algorithm
• Surface tension of four oxygenated fuels: experiment and correlation
• Phase equilibrium measurements and thermodynamic modeling of {CO2 + diethyl succinate + cosolvent} systems
• (Liquid + liquid) equilibria of (water + propionic acid + diethyl succinate or diethyl glutarate or diethyl adipate) ternary systems
• Volumetric and viscometric study with FT-IR analysis of binary systems with diethyl succinate and alcohols
• Volumetric, viscometric, spectral studies and viscosity modelling of binary mixtures of esters and alcohols (diethyl succinate, or ethyl octanoate + isobutanol, or isopentanol) at varying temperatures
• Liquid Density of 2 Methoxyethyl Acetate, 2 Ethylhexyl Acetate and Diethyl Succinate at Temperatures from 283.15 K to 363.15 K and Pressures up to 100 MPa
• Density, Viscosity, and Refractive Index Data for a Ternary System of Wine Congeners (Ethyl Butyrate + Diethyl Succinate + Isobutanol) in the Temperature Range from 288.15 to 323.15 K and at Atmospheric Pressure
• Phase Behavior of Binary Mixtures Containing Succinic Acid or Its Esters
• Vapor Pressures and Enthalpies of Vaporization of a Series of the Symmetric Linear n-Alkyl Esters of Dicarboxylic Acids
• Phase Equilibrium and Physical Properties for the Purification of Propylene Carbonate (PC) and y-Butyrolactone (GBL)
• Biomass-Derived Platform Chemicals: Thermodynamic Studies on the Extraction of 5-Hydroxymethylfurfural from Ionic Liquids
• Thermal Conductivity of Liquid 2-Methoxyethyl Acetate, 2-Ethylhexyl Acetate, and Diethyl Succinate
• Vapor Liquid Phase Equilibrium Data of CO2 in Some Physical Solvents from 285.19 K to 313.26 K
• Liquid-Liquid Equilibria of (Water + Acetic Acid + Diethyl Succinate or Diethyl Glutarate or Diethyl Adipate) Ternary Systems
• Joback Method
• KDB
• Aqueous Solubility Prediction Method
• McGowan Method
• NIST Webbook
• The Yaws Handbook of Vapor Pressure

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