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Problems With Project


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#1 JArchy123

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Posted 07 January 2022 - 08:06 PM

I recently posted on this forum about 'Use Of Euler's Approach In Reaction Kinetics', and I attempted this. I had a meeting with my lecturer on Thursday and he found that the paper I used didn't have nice rate equations as the rate seemed to be inhibited by the products. I was given another catalyst and rate equation to use and found the rate of the reaction as well as the weight of catalyst. I am now attempting to find the pressure drop using the Ergun Equation. All I was told by my lecturer was to follow the paper that he sent to find the mean voidage and then use solver in Excel to find the appropriate pressure drop as we do not have a tube diameter or height of the bed (which I was told have to be in a relationship of H/D > 3). I'm having problems with finding the pressure drop within the 10% of global pressure (which I actually don't know what he means by global pressure and was wondering if he is talking about atmospheric pressure of the region), which I assume to mean 1 atm, however the dt/dpe relationship is always greater than 50 which is the maximum allowed. 

 

I have attached the excel file and also the papers below but the excel file should have everything necessary.

 

Thanks

Joel

Attached Files



#2 breizh

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Posted 07 January 2022 - 09:09 PM

Hi ,

To support your work , consider the doc attached (2 pages)

You should be able to validate your calculation .

Good luck

Breizh



#3 JArchy123

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Posted 09 January 2022 - 12:30 PM

Thanks for the help. I was also wondering now that I have the bed height and the diameter of the reactor how I would determine the height of the packed bed reactor.



#4 latexman

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Posted 09 January 2022 - 04:36 PM

If you tell us those details, maybe someone will reply with their experience.

#5 JArchy123

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Posted 10 January 2022 - 03:16 PM

The diameter of the bed and reactor is 1.15298m (5.dp) and the height of the bed is 3.45894 m (5.dp). Also where would I locate the packing support plates and what distance should these be from the packing and also from the top of the column. Also how many manways should there be, I assume just two one from above the top packing support and one just above the bottom packing support.


Edited by JArchy123, 10 January 2022 - 03:17 PM.


#6 latexman

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Posted 10 January 2022 - 03:55 PM

What does " (5.dp) " mean?



#7 JArchy123

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Posted 10 January 2022 - 04:32 PM

5 decimal places



#8 Bobby Strain

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Posted 10 January 2022 - 05:23 PM

that's 1200 mm & 3500 mm.



#9 latexman

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Posted 10 January 2022 - 05:51 PM

5 decimal places


That’s so funny!

 

It reminds me of a comment in my company's two phase flow software, "More precision is reported than is justified by the technology."



#10 breizh

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Posted 10 January 2022 - 08:36 PM

Hi,

Consider this link from Internet : https://elib.uni-stu...848/1/eig16.pdf

 

To me you should consider top and bottom heads available on the market  (hemispherical ) linked to the diameter of the reactor . 

Some adjustment may be necessary .

 

The location of the manholes (2) is based on maintenance (inspection) and to add or remove the catalyst . 

 

Note : 5 Dp is a joke , in the real world people will make fun of you .

 

Good luck

Breizh 



#11 JArchy123

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Posted 11 January 2022 - 11:14 AM

What degree to accuracy is most used in the workplace?



#12 latexman

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Posted 11 January 2022 - 11:56 AM

As Bobby indicated, two significant figures.






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