co2脱除.bkp

描述下问题，小版前几天给别人指导过NAOH吸收CO2，希望可以帮到你

下面是模拟结果，气相：SO2 58m3/h，N2 32226M3/H,温度 293K,压力101KPA. 液相：30%的氢氧化钠溶液150m3/h，温度 293K,压力104KPA
塔板数：15. 拉西环填料
顺便问一下，aspen能否直接计算填料高度，就像简捷法计算塔板数一样。现在用的是先估算塔板数，再根据塔板数与填料的等量高度，计算填料高度。实际中我若是能够估算准塔板数，就不用aspen计算了！
->Calculations begin ...
  

           **  ERROR
      RADFRAC NOT CONVERGED IN  25 OUTSIDE LOOP ITERATIONS.

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

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE MODEL ELECNRTL WITHOUT A SOLVENT.
      ACTIVITY COEFFICIENT OF UNITY IS USED

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE THE CLARKE AQUEOUS ELECTROLYTE DENSITY MODEL
      WITHOUT A SOLVENT. CALCULATION NOT PERFORMED.

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE THE CLARKE AQUEOUS ELECTROLYTE DENSITY MODEL
      WITHOUT A SOLVENT. CALCULATION NOT PERFORMED.

  **  ERROR
      H-LOOP DOES NOT CONVERGE IN  5  TRIALS. ENERGY BALANCE NOT SATISFIED
      WITHIN MAXIMUM NUMBER OF ITERATIONS.

  **  ERROR
      FLOODING CALCULATIONS FOR SECTION (1) FAILED TO CONVERGE.
      CALCULATED DIAMETER MAY NOT BE ACCURATE.

  **  ERROR
      PRESSURE DROP CALCULATIONS FAILED TO CONVERGE.  PRESSURE DROP
      CALCULATED FOR SECTION (1) MAY NOT BE ACCURATE.

  **  ERROR
      BLOCK ABSORBE IS NOT IN MASS BALANCE:
      MASS INLET FLOW = 0.48206959E+04, MASS OUTLET FLOW = 0.48044435E+04
      RELATIVE DIFFERENCE = 0.33827761E-02

  *   WARNING
      STREAM NAOH IS NOT IN CHARGE BALANCE:
      ANION FLOW = -.50342386E+00, CATION FLOW = 0.51602005E+00
      RELATIVE DIFFERENCE = 0.25021041E-01

  *   WARNING
      STREAM W IS NOT IN CHARGE BALANCE:
      ANION FLOW = -.67645052E+01, CATION FLOW = 0.95116797E+01
      RELATIVE DIFFERENCE = 0.40611611E+00


->Simulation calculations completed ...

  *** SEVERE ERROR
      FORTRAN OVERFLOW ENCOUNTERED.

  **  ERROR
      FLOODING CALCULATIONS FOR SECTION (1) FAILED TO CONVERGE.
      CALCULATED DIAMETER MAY NOT BE ACCURATE.

  **  ERROR
      PRESSURE DROP CALCULATIONS FAILED TO CONVERGE.  PRESSURE DROP
      CALCULATED FOR SECTION (1) MAY NOT BE ACCURATE.

  *   WARNING
      VLSTD MISSING FOR COMPONENT SODIU(S).
      CALCULATED STDVOL FLOW WILL BE INCORRECT.



      *** SEVERE ERROR
      FORTRAN INVALID OPERATION ENCOUNTERED.


       Convergence iterations:
         OL   ML   IL     Err/Tol
          1    1    1     0.24254E-09
          2    1    1     0.23979E-09
          3    1    1     0.94145E-11
  *** 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:
       13
      A LIMIT OF  0.10000E-04 * SUM OF FEEDS WAS IMPOSED ON THE FLOW RATES.

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE MODEL ELECNRTL WITHOUT A SOLVENT.
      ACTIVITY COEFFICIENT OF UNITY IS USED

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE THE CLARKE AQUEOUS ELECTROLYTE DENSITY MODEL
      WITHOUT A SOLVENT. CALCULATION NOT PERFORMED.

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE THE CLARKE AQUEOUS ELECTROLYTE DENSITY MODEL
      WITHOUT A SOLVENT. CALCULATION NOT PERFORMED.

  **  ERROR
      H-LOOP DOES NOT CONVERGE IN  5  TRIALS. ENERGY BALANCE NOT SATISFIED
      WITHIN MAXIMUM NUMBER OF ITERATIONS.

  **  ERROR
      BLOCK ABSORBE IS NOT IN MASS BALANCE:
      MASS INLET FLOW = 0.48206959E+04, MASS OUTLET FLOW = 0.12609178E+08
      RELATIVE DIFFERENCE = 0.26146345E+04

  *   WARNING
      STREAM NAOH IS NOT IN CHARGE BALANCE:
      ANION FLOW = -.50342386E+00, CATION FLOW = 0.51602005E+00
      RELATIVE DIFFERENCE = 0.25021041E-01

  *   WARNING
      STREAM W IS NOT IN CHARGE BALANCE:
      ANION FLOW = -.67644409E+01, CATION FLOW = 0.95115894E+01
      RELATIVE DIFFERENCE = 0.40611611E+00


->Simulation calculations completed ...



<< Loading Simulation Engine 20:45:55 Thu Aug 11, 2011>>

->Generating report ...

下面是模拟结果，气相：SO2 58m3/h，N2 32226M3/H,温度 293K,压力101KPA. 液相：30%的氢氧化钠溶液150m3/h，温度 293K,压力104KPA
塔板数：15. 拉西环填料
顺便问一下，aspen能否直接计算填料高度，就像简捷法计算塔板数一样。现在用的是先估算塔板数，再根据塔板数与填料的等量高度，计算填料高度。实际中我若是能够估算准塔板数，就不用aspen计算了！
->Calculations begin ...
  

           **  ERROR
      RADFRAC NOT CONVERGED IN  25 OUTSIDE LOOP ITERATIONS.

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

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE MODEL ELECNRTL WITHOUT A SOLVENT.
      ACTIVITY COEFFICIENT OF UNITY IS USED

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE THE CLARKE AQUEOUS ELECTROLYTE DENSITY MODEL
      WITHOUT A SOLVENT. CALCULATION NOT PERFORMED.

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE THE CLARKE AQUEOUS ELECTROLYTE DENSITY MODEL
      WITHOUT A SOLVENT. CALCULATION NOT PERFORMED.

  **  ERROR
      H-LOOP DOES NOT CONVERGE IN  5  TRIALS. ENERGY BALANCE NOT SATISFIED
      WITHIN MAXIMUM NUMBER OF ITERATIONS.

  **  ERROR
      FLOODING CALCULATIONS FOR SECTION (1) FAILED TO CONVERGE.
      CALCULATED DIAMETER MAY NOT BE ACCURATE.

  **  ERROR
      PRESSURE DROP CALCULATIONS FAILED TO CONVERGE.  PRESSURE DROP
      CALCULATED FOR SECTION (1) MAY NOT BE ACCURATE.

  **  ERROR
      BLOCK ABSORBE IS NOT IN MASS BALANCE:
      MASS INLET FLOW = 0.48206959E+04, MASS OUTLET FLOW = 0.48044435E+04
      RELATIVE DIFFERENCE = 0.33827761E-02

  *   WARNING
      STREAM NAOH IS NOT IN CHARGE BALANCE:
      ANION FLOW = -.50342386E+00, CATION FLOW = 0.51602005E+00
      RELATIVE DIFFERENCE = 0.25021041E-01

  *   WARNING
      STREAM W IS NOT IN CHARGE BALANCE:
      ANION FLOW = -.67645052E+01, CATION FLOW = 0.95116797E+01
      RELATIVE DIFFERENCE = 0.40611611E+00


->Simulation calculations completed ...

  *** SEVERE ERROR
      FORTRAN OVERFLOW ENCOUNTERED.

  **  ERROR
      FLOODING CALCULATIONS FOR SECTION (1) FAILED TO CONVERGE.
      CALCULATED DIAMETER MAY NOT BE ACCURATE.

  **  ERROR
      PRESSURE DROP CALCULATIONS FAILED TO CONVERGE.  PRESSURE DROP
      CALCULATED FOR SECTION (1) MAY NOT BE ACCURATE.

  *   WARNING
      VLSTD MISSING FOR COMPONENT SODIU(S).
      CALCULATED STDVOL FLOW WILL BE INCORRECT.



      *** SEVERE ERROR
      FORTRAN INVALID OPERATION ENCOUNTERED.


       Convergence iterations:
         OL   ML   IL     Err/Tol
          1    1    1     0.24254E-09
          2    1    1     0.23979E-09
          3    1    1     0.94145E-11
  *** 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:
       13
      A LIMIT OF  0.10000E-04 * SUM OF FEEDS WAS IMPOSED ON THE FLOW RATES.

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE MODEL ELECNRTL WITHOUT A SOLVENT.
      ACTIVITY COEFFICIENT OF UNITY IS USED

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE THE CLARKE AQUEOUS ELECTROLYTE DENSITY MODEL
      WITHOUT A SOLVENT. CALCULATION NOT PERFORMED.

  *   WARNING IN PHYSICAL PROPERTY SYSTEM
      ATTEMPT TO USE THE CLARKE AQUEOUS ELECTROLYTE DENSITY MODEL
      WITHOUT A SOLVENT. CALCULATION NOT PERFORMED.

  **  ERROR
      H-LOOP DOES NOT CONVERGE IN  5  TRIALS. ENERGY BALANCE NOT SATISFIED
      WITHIN MAXIMUM NUMBER OF ITERATIONS.

  **  ERROR
      BLOCK ABSORBE IS NOT IN MASS BALANCE:
      MASS INLET FLOW = 0.48206959E+04, MASS OUTLET FLOW = 0.12609178E+08
      RELATIVE DIFFERENCE = 0.26146345E+04

  *   WARNING
      STREAM NAOH IS NOT IN CHARGE BALANCE:
      ANION FLOW = -.50342386E+00, CATION FLOW = 0.51602005E+00
      RELATIVE DIFFERENCE = 0.25021041E-01

  *   WARNING
      STREAM W IS NOT IN CHARGE BALANCE:
      ANION FLOW = -.67644409E+01, CATION FLOW = 0.95115894E+01
      RELATIVE DIFFERENCE = 0.40611611E+00


->Simulation calculations completed ...

小版给你个NAOH吸收CO2的例子，自己对照着看吧，是我以前做的，就不一一给你做了

十分感谢！十分感谢{:soso_e181:}

是不是你的版本太高？，打不开啊！我用的是11.1

我的aspen是V7.1的

本帖最后由 lcpinging 于 2011-12-14 00:10 编辑

谢谢版主的例子，，，最近在学习aspen模拟填料塔的例子
非常好的例子

楼主的问题解决了吗，遇到同样的问题，求解答啊

从模型库中调用一个气体吸收的例子就可以计算了。

记得选择非平衡模型的化学吸收过程，采用平衡吸收就可能出问题。