zzz303468126 发表于 2011-8-11 17:04:24

NAOH吸收SO2 填料塔

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 2011-8-11 18:51:09

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 2011-8-11 21:15:00

这是什么啊？{:1106_368:}

zzz303468126 发表于 2011-8-11 21:22:54

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 IN25 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 IN5TRIALS. 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 OF0.10000E-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 IN5TRIALS. 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 2011-8-11 21:24:14

飞梦101 发表于 2011-8-11 18:51 static/image/common/back.gif
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 IN25 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 IN5TRIALS. 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 OF0.10000E-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 IN5TRIALS. 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 2011-8-12 09:42:11

zzz303468126 发表于 2011-8-11 21:24 static/image/common/back.gif
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


zzz303468126 发表于 2011-8-12 10:27:05

飞梦101 发表于 2011-8-12 09:42 static/image/common/back.gif
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 2011-8-12 10:32:51

飞梦101 发表于 2011-8-12 09:42 static/image/common/back.gif
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 2011-8-12 11:11:18

zzz303468126 发表于 2011-8-12 10:32 static/image/common/back.gif
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 2011-8-19 20:24:38

怎么不说说是什么问题啊

lcpinging 发表于 2011-12-14 00:05:21

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 2011-12-18 17:50:49

11.1打不开7.1的啊。。
郁闷啊

bernice 发表于 2012-3-21 23:31:24

楼主的问题解决了吗，遇到同样的问题，求解答啊

Wake 发表于 2012-6-10 08:55:10

分析分析什么问题啊

fengyuwuzhu68 发表于 2012-9-18 21:45:51

遇到同样的问题求答案

zxf824163029 发表于 2012-12-14 12:31:07

学习的飘过

wdh282002 发表于 2013-1-13 13:13:29

十分值得学习！

ecustli 发表于 2013-1-17 09:33:06

看看能有有帮助，谢谢。

wgw1205 发表于 2011-8-11 17:04:24

正在研究化学吸收，学习下。

走天下看繁华 发表于 2011-8-11 17:04:24

结果运行不对啊
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