Dortmund Data Bank

Vapor-Liquid Equilibrium Data

The experimental data shown in these pages are freely available and have been published already in the DDB Explorer Edition. The data represent a small sub list of all available data in the Dortmund Data Bank. For more data or any further information please search the DDB or contact DDBST.

Vapor-Liquid Equilibrium Data Set 4783

Components

No. Formula Molar Mass CAS Registry Number Name
1 C4H8O2 88.106 141-78-6 Ethyl acetate
2 C2H6O 46.069 64-17-5 Ethanol
3 C4H10O 74.123 71-36-3 1-Butanol
Search the DDB for all data of this mixture

Constant Value

Pressure 96.66 kPa

Data Table

T [K] x1 [mol/mol] x2 [mol/mol] y1 [mol/mol] y2 [mol/mol]
346.15 0.21910 0.65980 0.33600 0.57630
346.05 0.23450 0.59370 0.33580 0.60180
346.95 0.30840 0.45810 0.40630 0.55230
346.15 0.38050 0.39920 0.46520 0.48770
346.85 0.55440 0.20820 0.59250 0.25510
347.15 0.68800 0.10110 0.68110 0.16260
345.35 0.47250 0.36980 0.49310 0.47400
348.65 0.07960 0.78610 0.17340 0.74180
348.65 0.39300 0.38220 0.51520 0.43590
347.95 0.41300 0.35630 0.51010 0.40380
348.15 0.42430 0.23740 0.52290 0.28820
348.85 0.50390 0.25190 0.59150 0.35140
348.65 0.61240 0.11010 0.66320 0.15080
348.55 0.71880 0.05090 0.74830 0.07410
348.15 0.80980 0.04080 0.81020 0.05150
347.35 0.80720 0.09330 0.80720 0.17460
354.95 0.14370 0.41430 0.31350 0.56090
352.95 0.20100 0.41680 0.37690 0.53190
349.45 0.24430 0.48550 0.37680 0.56510
349.65 0.67250 0.06150 0.73090 0.09490
361.15 0.10580 0.28060 0.27490 0.52660
358.65 0.11770 0.28940 0.28160 0.46730
360.05 0.10310 0.32170 0.27650 0.54840
358.55 0.12980 0.31540 0.32420 0.50210
358.45 0.17070 0.20580 0.37930 0.31050
363.35 0.17800 0.15620 0.46030 0.29070
364.95 0.11580 0.17740 0.34340 0.38450
366.75 0.11610 0.15170 0.41300 0.27810
361.55 0.10090 0.16290 0.26780 0.48640
367.25 0.08210 0.13750 0.26960 0.40090
369.65 0.09350 0.06570 0.35420 0.23550
371.25 0.06210 0.06870 0.22180 0.36670
375.85 0.03890 0.06340 0.16990 0.30170
381.05 0.01950 0.03110 0.09130 0.20970
387.90 0.00770 0.00880 0.05130 0.03100

(T - temperature, x - liquid mole fraction, y - vapor mole fraction)

Reference

Source
Mainkar S.V.; Mene P.S.: Ternary Vapor-Liquid Equilibrium Data System Ethyl Acetate Ethanol-n-Butanol. Indian Chem.Eng. 7 (1965) 47-52


Vapor-Liquid Equilibrium Data Set 10965

Components

No. Formula Molar Mass CAS Registry Number Name
1 C4H8O2 88.106 141-78-6 Ethyl acetate
2 C2H6O 46.069 64-17-5 Ethanol
3 C4H10O 74.123 71-36-3 1-Butanol
Search the DDB for all data of this mixture

Constant Value

Pressure 101.33 kPa

Data Table

T [K] x1 [mol/mol] x2 [mol/mol] y1 [mol/mol] y2 [mol/mol]
347.95 0.43900 0.46400 0.49600 0.47200
347.85 0.46100 0.44100 0.51000 0.46300
347.85 0.48000 0.41000 0.52800 0.44500
348.05 0.50200 0.40000 0.54500 0.43000
347.95 0.52900 0.37100 0.56200 0.41100
348.05 0.55600 0.34200 0.58800 0.38900
348.25 0.66100 0.24100 0.66500 0.30900
349.75 0.75600 0.14100 0.77000 0.20300
353.85 0.20300 0.51500 0.34100 0.58400
352.85 0.34000 0.39300 0.47500 0.46000
352.75 0.35200 0.38100 0.48800 0.44600
352.65 0.37800 0.36100 0.50600 0.42700
352.15 0.40200 0.34300 0.52800 0.40800
352.25 0.42200 0.32400 0.54000 0.39500
352.25 0.44100 0.30600 0.56000 0.37600
352.35 0.45500 0.29300 0.57400 0.36100
352.45 0.48700 0.26900 0.60100 0.33600
352.35 0.54300 0.22500 0.63800 0.29800
354.45 0.55600 0.13800 0.70400 0.20500
352.55 0.55900 0.20200 0.65800 0.27500
355.75 0.62100 0.06950 0.78700 0.11300
359.75 0.02960 0.58300 0.07160 0.79600
358.55 0.12800 0.45900 0.26500 0.59900
358.05 0.32400 0.24000 0.52000 0.34500
357.45 0.35800 0.21000 0.55900 0.30600
357.35 0.38200 0.19100 0.58800 0.28300
357.65 0.41100 0.18100 0.60800 0.26400
357.45 0.42400 0.15700 0.63000 0.24000
357.75 0.44600 0.13700 0.65700 0.21200
357.95 0.46600 0.11900 0.68200 0.18700
358.25 0.49900 0.08830 0.72100 0.14200
358.75 0.53000 0.06080 0.75800 0.09960
363.75 0.02330 0.47700 0.05990 0.75200
362.65 0.09750 0.38100 0.23100 0.58100
361.75 0.18800 0.26600 0.40200 0.41100
362.05 0.31200 0.13000 0.57100 0.22300
362.55 0.32500 0.10700 0.59500 0.19000
362.55 0.33900 0.10500 0.61100 0.18500
362.15 0.37400 0.09310 0.64400 0.16200
361.45 0.39600 0.08520 0.66200 0.14400
361.35 0.42800 0.05940 0.70000 0.10500
361.05 0.45900 0.03990 0.73200 0.07250
362.85 0.46900 0.01840 0.76500 0.03370
367.95 0.03680 0.34600 0.10100 0.62400
366.95 0.09690 0.24800 0.26700 0.47200
367.15 0.14400 0.18900 0.36200 0.35700
366.75 0.22100 0.10700 0.50200 0.21400
366.75 0.29200 0.05970 0.60100 0.11400
366.85 0.30100 0.04510 0.62700 0.09120
366.65 0.31700 0.03770 0.64700 0.07560
366.15 0.35200 0.02340 0.68100 0.04780
366.05 0.36600 0.01630 0.69200 0.03240
365.85 0.38200 0.00930 0.72600 0.01910
372.05 0.02750 0.25200 0.07750 0.54100
371.25 0.05300 0.22100 0.15200 0.48000
370.95 0.07990 0.19400 0.22400 0.41100
370.65 0.10200 0.16000 0.28900 0.34500
370.25 0.13400 0.12600 0.37100 0.27100
369.45 0.16100 0.11100 0.42700 0.23300
369.55 0.17500 0.09540 0.44800 0.19900
369.55 0.18700 0.07970 0.47800 0.16800
369.25 0.21200 0.06790 0.52100 0.14700
369.35 0.21600 0.04910 0.52900 0.10400
369.45 0.22900 0.03410 0.56100 0.07690
369.65 0.24000 0.02060 0.59000 0.04620
369.65 0.26500 0.00880 0.61000 0.02040
377.95 0.01480 0.13700 0.05620 0.38100
377.95 0.01550 0.14100 0.05690 0.38800
377.05 0.02850 0.13300 0.10100 0.37300
377.05 0.04610 0.12500 0.14900 0.32300
377.05 0.05740 0.10400 0.19500 0.27300
377.05 0.07330 0.08640 0.24000 0.22900
376.85 0.09180 0.06840 0.29000 0.17800
376.55 0.09490 0.05770 0.33300 0.16200
376.35 0.11600 0.05360 0.35000 0.13000
375.95 0.12100 0.04420 0.38200 0.11500
375.85 0.13400 0.03700 0.41500 0.09650
375.55 0.14900 0.02870 0.43400 0.07180
375.65 0.15100 0.01830 0.45900 0.04750
375.45 0.16600 0.00950 0.47800 0.02400
383.65 0.00910 0.07680 0.03610 0.25100
383.15 0.01900 0.07890 0.06610 0.23300
383.05 0.03080 0.04950 0.11800 0.16300
382.45 0.05010 0.03670 0.17700 0.11300
382.45 0.06610 0.01750 0.23500 0.05370
382.45 0.07340 0.00180 0.28300 0.01660
382.45 0.07610 0.00330 0.28100 0.01130
382.45 0.07610 0.00190 0.28600 0.00670

(T - temperature, x - liquid mole fraction, y - vapor mole fraction)

Reference

Source
Shono H.; Kanazawa N.; Hashitani M.; Komatsu H.; Hirata M.: Vapor-Liquid Equilibrium in Extractive Distillation of Ethyl Acetate-Ethanol System. Kogyo Kagaku Zasshi 72 (1969) 815-819


Vapor-Liquid Equilibrium Data Set 25282

Components

No. Formula Molar Mass CAS Registry Number Name
1 C4H8O2 88.106 141-78-6 Ethyl acetate
2 C2H6O 46.069 64-17-5 Ethanol
3 C4H10O 74.123 71-36-3 1-Butanol
Search the DDB for all data of this mixture

Constant Value

Pressure 101.33 kPa

Data Table

T [K] x1 [mol/mol] x2 [mol/mol]
348.90 0.38030 0.45790
352.20 0.71840 0.05100
365.70 0.10610 0.28010

(T - temperature, x - liquid mole fraction)

Reference

Source
Belousov V.P.; Gkhoneimi Kh.F.; Shulgin I.L.: Dampf-Flüssig-Gleichgewicht in binären und ternären Systemen aus n-Alkoholen und Alkylacetaten. Viniti (1986) 1-20

List of All References

Source

Vapor-Liquid Equilibrium Data Overview


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