NAOH吸收SO2 填料塔

zzz303468126 · 发表于 1970-1-1 08:00:00

使用氢氧化钠吸收二氧化硫，填料塔，问题很多，那为大侠帮忙解决一下，不胜感谢！

飞梦101 · 发表于 1970-1-1 08:00:00

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

jinghua316 · 发表于 1970-1-1 08:00:00

这是什么啊？{:1106_368:}

zzz303468126 · 发表于 1970-1-1 08:00:00

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 ...

zzz303468126 · 发表于 1970-1-1 08:00:00

飞梦101 发表于 2011-8-11 18:51

登录/注册后可看大图

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 ...

飞梦101 · 发表于 1970-1-1 08:00:00

zzz303468126 发表于 2011-8-11 21:24

登录/注册后可看大图

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/ ...

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

co2脱除.bkp (112.88 KB, 下载次数: 838)

zzz303468126 · 发表于 1970-1-1 08:00:00

飞梦101 发表于 2011-8-12 09:42

登录/注册后可看大图

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:}

zzz303468126 · 发表于 1970-1-1 08:00:00

飞梦101 发表于 2011-8-12 09:42

登录/注册后可看大图

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

是不是你的版本太高？，打不开啊！我用的是11.1

飞梦101 · 发表于 1970-1-1 08:00:00

zzz303468126 发表于 2011-8-12 10:32

登录/注册后可看大图

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

网络营销顾问 · 发表于 1970-1-1 08:00:00

怎么不说说是什么问题啊

lcpinging · 发表于 1970-1-1 08:00:00

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

DeadHorseman · 发表于 1970-1-1 08:00:00

11.1打不开7.1的啊。。
郁闷啊

bernice · 发表于 1970-1-1 08:00:00

楼主的问题解决了吗，遇到同样的问题，求解答啊

Wake · 发表于 1970-1-1 08:00:00

分析分析什么问题啊

fengyuwuzhu68 · 发表于 1970-1-1 08:00:00

遇到同样的问题求答案

zxf824163029 · 发表于 1970-1-1 08:00:00

学习的飘过

wdh282002 · 发表于 1970-1-1 08:00:00

十分值得学习！

ecustli · 发表于 1970-1-1 08:00:00

看看能有有帮助，谢谢。

wgw1205 · 发表于 1970-1-1 08:00:00

正在研究化学吸收，学习下。

走天下看繁华 · 发表于 1970-1-1 08:00:00

结果运行不对啊

NAOH吸收SO2 填料塔

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