aspen plusv12中甲醇精馏模拟

伸手触摸阳光 · 发表于 1970-1-1 08:00:00

甲醇精馏模拟的原料组分(进料流量92285kg/hr)中有共沸物，在预精馏的收敛选项需要选择共沸吗？丙酮(0.003%)与甲醇是共沸物，异丁醇(0.044%)与水是共沸物，正丁醇(0.048%)与水是共沸物，我选择共沸收敛之后出现了许多问题，

*** SEVERE ERROR
   FLASH CALCULATIONS FAILED TO CONVERGE IN  12  ITERATIONS. BUBBLE POINT
   CALCULATION HAS DRIVEN THE TEMPERATURE DOWN TO THE LOWER LIMIT OF
   71.1346 DEGREE K.  BUBBLE POINT TEMPERATURE MAY NOT EXIST AT THE
   SPECIFIED PRESSURE.

  * WARNING
   COMPONENT "CO" IS NOT IN PHASE EQUILIBRIUM. RELATIVE ERROR IN VL
   FUGACITY IS 0.9868 . LN FUGACITIES ARE 7.0860 FOR VAPOR AND 14.0782 FOR
   LIQUID. MOLE FRACTIONS ARE 9.1929-03 FOR VAPOR AND 9.1378-03 FOR LIQUID.
   LN FUG COEFFICIENTS ARE 0.0 FOR VAPOR AND 6.9983 FOR LIQUID.

  * WARNING
   COMPONENT "CH4" IS NOT IN PHASE EQUILIBRIUM. RELATIVE ERROR IN VL
   FUGACITY IS 6.9023 . LN FUGACITIES ARE -70.8204 FOR VAPOR AND 11.9987 FOR
   LIQUID. MOLE FRACTIONS ARE 0.0D FOR VAPOR AND 2.0282-02 FOR LIQUID. LN
   FUG COEFFICIENTS ARE 0.0 FOR VAPOR AND 4.0414 FOR LIQUID.

  * WARNING
   COMPONENT "CH4" IS NOT IN PHASE EQUILIBRIUM. RELATIVE ERROR IN VL
   FUGACITY IS 7.5370 . LN FUGACITIES ARE -71.1267 FOR VAPOR AND 10.8806 FOR
   LIQUID. MOLE FRACTIONS ARE 0.0D FOR VAPOR AND 6.8341-03 FOR LIQUID. LN
   FUG COEFFICIENTS ARE 0.0 FOR VAPOR AND 4.0052 FOR LIQUID.

  **  ERROR
   FLASH CALCULATIONS FAILED TO CONVERGE IN  60  ITERATIONS.  FAILURE TO
   SOLVE 2-PHASE FIXED VFRAC PROBLEM AS TP SUBPROBLEMS. T= 14.8411 P=
   1.4083D+05 VCALC= 1.0003D-13 VSPEC= 0.0

   Convergence iterations:
         Iter    Err/Tol
            0    0.13901E+22
            1    0.13901E+22
  *** SEVERE ERROR
   MATERIAL AND ENERGY BALANCES FAILED TO CONVERGE: CHECK COL-SPECS
   OR SUPPLY BETTER TEMPERATURE AND COMPOSITION ESTIMATES.

  *** SEVERE ERROR
   THE FOLLOWING STAGES DRIED UP:
      1 2 3 4 5 6 7 8 9 10 25
   A LIMIT OF  0.10000E-04 * SUM OF FEEDS WAS IMPOSED ON THE FLOW RATES.

  **  ERROR
   BLOCK C001 IS NOT IN MASS BALANCE:
   MASS INLET FLOW = 0.25634722E+02, MASS OUTLET FLOW = 0.22944997E+02
   RELATIVE DIFFERENCE = 0.11722492E+00

*** SEVERE ERROR
   MATERIAL AND ENERGY BALANCES FAILED TO CONVERGE: CHECK COL-SPECS
   OR SUPPLY BETTER TEMPERATURE AND COMPOSITION ESTIMATES.

  **  ERROR
   BLOCK C001 IS NOT IN MASS BALANCE:
   MASS INLET FLOW = 0.26079167E+02, MASS OUTLET FLOW = 0.25913795E+02
   RELATIVE DIFFERENCE = 0.63816208E-02

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