Use of the Taylor Series as a Convergence Technique for the Solution of Multicomponent Dew Point and...
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USE OF THE TAYLOR SERIES AS A CONVERGENCE TECHNIQUE FOR THE SOLUTION OF MULTICOMPONENT DEW POINT AND FLASH VAPORIZATION PROBLEMS A THESIS Condensed for publication Submitted on the 25 th day of January, 1962, to the Department of Chemical Engineering of the Graduate School of Tulane University
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Separation of non-electrolyte components at low pressures by distillation requires the column feed to be characterized as to the amount of each phase, composition, temperature, and pressure. For multicomponent, non-ideal solutions this requires solution of simultaneous, non-linear equations. This thesis demonstrates the use of the Taylor Series to linearize these equations while employing an outer bi-section loop to determine the temperature, pressure, or fraction flashed given one of these latter variables.
Transcript of Use of the Taylor Series as a Convergence Technique for the Solution of Multicomponent Dew Point and...
USE OF THE TAYLOR SERIES AS A
CONVERGENCE TECHNIQUE FOR
THE SOLUTION OF MULTICOMPONENT
DEW POINT AND FLASH VAPORIZATION
PROBLEMS
A THESIS
Condensed for publication
Submitted on the 25th day of January, 1962, to the Department of
Chemical Engineering of the Graduate School of Tulane University
in partial fulfillment of the requirements for the degree of Master
of Science by:
Jacob H. Lashover
Thesis Advisor: Dr. Raymond V. Bailey
FLASH VAPORIZATION CALCULATION USING DERIVATIVESSYSTEM IS MEOH, IPA, H2O AT 1 ATMFEED COMPOSITION IS 0.50, 0.15, 0.35 MOLE FRACTION OF MEOH, IPA, H2O, RESPECTIVELYFEED TEMPERATURE IS 78 CISOTHERMAL FLASH USING REDLICH-KISTER ACTIVITY COEFFICIENT MODEL AND ANTOINE VAPOR PRESSURE MODEL
(VL+VU)/2ITER. NO. VL VU V X MeOH X IPA X H2O ƩX ΔƩX
0 0 1 0.5 0.4 0.1 0.5 1 01 0 1 0.5 0.3709 0.1299 0.44 0.9408 0.05922 0.5 1 0.75 0.3138 0.1013 0.5343 0.9494 0.05063 0.75 1 0.875 0.2801 0.0781 0.616 0.9742 0.02584 0.875 1 0.9375 0.2599 0.06406 0.6733 0.9973 0.00275 0.9375 1 0.96875 0.2487 0.05662 0.7077 1.01303 -0.013036 0.9375 0.96875 0.953125 0.2543 0.06029 0.6901 1.0047 -0.00477 0.9375 0.953125 0.945313 0.2571 0.06215 0.6817 1.0009 -0.00098 0.9375 0.945313 0.941407 0.2584 0.0631 0.6775 0.9991 0.00099 0.941406 0.945313 0.94336 0.2579 0.06269 0.6794 1.000003 -3E-06
Y MEOH Y IPA Y H2O ƩY0.514535 0.15524 0.33022 0.999995
V
ITERATION NUMBER
0 1 2 3 4 5 6 7 8 9 100
0.2
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0.6
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1
1.2
Column D
