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 32344
Components
| No. |
Formula |
Molar Mass |
CAS Registry Number |
Name |
| 1 |
C4H10O |
74.123 |
60-29-7 |
Diethyl ether |
| 2 |
CH4O |
32.042 |
67-56-1 |
Methanol |
| 3 |
C4H10O |
74.123 |
71-36-3 |
1-Butanol |
Search the DDB for all data of this mixture
Constant Value
Data Table
| T [K] |
x1 [mol/mol] |
x2 [mol/mol] |
y1 [mol/mol] |
y2 [mol/mol] |
| 308.50 |
0.86540 |
0.09800 |
0.91840 |
0.08110 |
| 309.15 |
0.84160 |
0.09540 |
0.92260 |
0.07640 |
| 309.59 |
0.82300 |
0.09320 |
0.92540 |
0.07320 |
| 310.04 |
0.80360 |
0.09110 |
0.92780 |
0.07030 |
| 310.63 |
0.78190 |
0.08860 |
0.93000 |
0.06740 |
| 311.15 |
0.76330 |
0.08650 |
0.93140 |
0.06520 |
| 312.86 |
0.73780 |
0.08360 |
0.93300 |
0.06260 |
| 313.95 |
0.71500 |
0.08100 |
0.93390 |
0.06060 |
| 314.58 |
0.69280 |
0.07850 |
0.93430 |
0.05900 |
| 315.15 |
0.67280 |
0.07620 |
0.93450 |
0.05760 |
| 316.80 |
0.65190 |
0.07390 |
0.93430 |
0.05640 |
| 317.25 |
0.63840 |
0.07230 |
0.93400 |
0.05560 |
| 316.80 |
0.50840 |
0.25490 |
0.83270 |
0.16030 |
| 317.54 |
0.49680 |
0.24910 |
0.83120 |
0.16070 |
| 319.35 |
0.48310 |
0.24230 |
0.82930 |
0.16130 |
| 320.16 |
0.47380 |
0.23760 |
0.82790 |
0.16160 |
| 320.86 |
0.46340 |
0.23240 |
0.82620 |
0.16200 |
| 321.53 |
0.45270 |
0.22700 |
0.82430 |
0.16240 |
| 322.98 |
0.44100 |
0.22110 |
0.82210 |
0.16290 |
| 323.35 |
0.43040 |
0.21580 |
0.81990 |
0.16340 |
| 324.04 |
0.41960 |
0.21040 |
0.81740 |
0.16390 |
| 324.74 |
0.41060 |
0.20590 |
0.81530 |
0.16430 |
| 325.45 |
0.40260 |
0.20190 |
0.81320 |
0.16470 |
| 327.06 |
0.39280 |
0.19700 |
0.81060 |
0.16520 |
| 328.00 |
0.38450 |
0.19280 |
0.80820 |
0.16550 |
| 328.04 |
0.37510 |
0.18810 |
0.80530 |
0.16600 |
| 328.75 |
0.36770 |
0.18440 |
0.80290 |
0.16640 |
| 327.87 |
0.07670 |
0.92330 |
0.34930 |
0.65070 |
| 328.96 |
0.07530 |
0.90690 |
0.33900 |
0.66000 |
| 329.24 |
0.07410 |
0.89250 |
0.33040 |
0.66760 |
| 329.98 |
0.07280 |
0.87640 |
0.32130 |
0.67540 |
| 330.97 |
0.07160 |
0.86190 |
0.31340 |
0.68220 |
| 330.96 |
0.07050 |
0.84820 |
0.30630 |
0.68800 |
| 331.87 |
0.06930 |
0.83450 |
0.29920 |
0.69390 |
| 332.54 |
0.06810 |
0.82000 |
0.29210 |
0.69950 |
| 332.86 |
0.06690 |
0.80590 |
0.28530 |
0.70470 |
| 333.86 |
0.06580 |
0.79210 |
0.27920 |
0.70930 |
| 334.00 |
0.02160 |
0.97840 |
0.12700 |
0.87300 |
| 334.10 |
0.06450 |
0.77670 |
0.27230 |
0.71420 |
| 334.73 |
0.02130 |
0.96570 |
0.12310 |
0.87580 |
| 334.85 |
0.06330 |
0.76260 |
0.26620 |
0.71840 |
| 335.41 |
0.02100 |
0.95220 |
0.11930 |
0.87830 |
| 335.44 |
0.06220 |
0.74920 |
0.26070 |
0.72200 |
| 336.14 |
0.06110 |
0.73590 |
0.25540 |
0.72530 |
| 336.22 |
0.02070 |
0.93820 |
0.11560 |
0.88060 |
| 336.64 |
0.02040 |
0.92390 |
0.11210 |
0.88270 |
| 336.93 |
0.01480 |
0.95750 |
0.08660 |
0.91080 |
| 336.94 |
0.05990 |
0.72090 |
0.24970 |
0.72860 |
| 337.15 |
0.02010 |
0.91010 |
0.10880 |
0.88450 |
| 337.45 |
0.05880 |
0.70790 |
0.24480 |
0.73140 |
| 337.55 |
0.01440 |
0.93300 |
0.08170 |
0.91310 |
| 337.65 |
0.01970 |
0.89230 |
0.10470 |
0.88650 |
| 337.86 |
0.05790 |
0.69650 |
0.24070 |
0.73340 |
| 338.15 |
0.01400 |
0.90660 |
0.07710 |
0.91480 |
| 338.17 |
0.01930 |
0.87600 |
0.10110 |
0.88820 |
| 338.76 |
0.01900 |
0.86070 |
0.09810 |
0.88910 |
| 338.94 |
0.01360 |
0.87800 |
0.07270 |
0.91560 |
| 339.45 |
0.01860 |
0.84330 |
0.09470 |
0.89020 |
| 339.79 |
0.01320 |
0.85280 |
0.06900 |
0.91590 |
| 339.88 |
0.01820 |
0.82700 |
0.09160 |
0.89100 |
| 340.53 |
0.01280 |
0.83020 |
0.06570 |
0.91590 |
| 341.08 |
0.01250 |
0.80870 |
0.06320 |
0.91510 |
| 341.55 |
0.01220 |
0.78700 |
0.06080 |
0.91380 |
| 342.26 |
0.01190 |
0.77000 |
0.05880 |
0.91280 |
| 344.49 |
0.02640 |
0.63840 |
0.11870 |
0.83160 |
| 344.98 |
0.02590 |
0.62700 |
0.11640 |
0.83080 |
| 344.96 |
0.02520 |
0.60870 |
0.11320 |
0.82870 |
| 345.98 |
0.02450 |
0.59350 |
0.11020 |
0.82710 |
| 346.42 |
0.02390 |
0.57860 |
0.10760 |
0.82490 |
| 347.07 |
0.02340 |
0.56550 |
0.10550 |
0.82260 |
| 347.55 |
0.02290 |
0.55460 |
0.10340 |
0.82080 |
| 348.09 |
0.02240 |
0.54160 |
0.10140 |
0.81800 |
| 350.47 |
0.04080 |
0.45770 |
0.17740 |
0.72430 |
| 351.07 |
0.03980 |
0.44640 |
0.17410 |
0.72190 |
| 351.85 |
0.03860 |
0.43320 |
0.17020 |
0.71890 |
| 352.66 |
0.03720 |
0.41710 |
0.16570 |
0.71430 |
| 353.55 |
0.03600 |
0.40410 |
0.16170 |
0.71040 |
| 354.35 |
0.03450 |
0.38750 |
0.15680 |
0.70460 |
| 355.68 |
0.03290 |
0.36910 |
0.15160 |
0.69710 |
| 357.25 |
0.03110 |
0.34890 |
0.14560 |
0.68760 |
| 357.98 |
0.03000 |
0.33710 |
0.14180 |
0.68160 |
| 362.65 |
0.03260 |
0.24100 |
0.16360 |
0.57930 |
| 364.36 |
0.03150 |
0.23260 |
0.15980 |
0.57170 |
| 364.32 |
0.03030 |
0.22380 |
0.15550 |
0.56330 |
| 365.22 |
0.02920 |
0.21590 |
0.15150 |
0.55530 |
| 366.44 |
0.02810 |
0.20770 |
0.14740 |
0.54640 |
| 368.00 |
0.02720 |
0.20080 |
0.14410 |
0.53840 |
| 368.76 |
0.02620 |
0.19330 |
0.14030 |
0.52930 |
| 369.21 |
0.02540 |
0.18800 |
0.13710 |
0.52280 |
| 368.44 |
0.02480 |
0.18340 |
0.13470 |
0.51680 |
(T - temperature, x - liquid mole fraction, y - vapor mole fraction)
Reference
| Source |
| Gao D.; Zhang H.; Zhu D.; Sun H.; Chen H.; Shi J.; Lücking P.; Winter B.; Zhan Y.: Correlation and Prediction for Isobaric Vapor–Liquid Equilibria of the Diethyl Ether + Methanol + 1-Butanol Ternary System and the Constituent Binary Systems at 101.325 kPa. Ind.Eng.Chem.Res. 51 (2012) 567-575 |
List of All References
Vapor-Liquid Equilibrium Data Overview
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