INTELLIGENT WORK FORUMS
FOR ENGINEERING PROFESSIONALS

Log In

Come Join Us!

Are you an
Engineering professional?
Join Eng-Tips Forums!
  • Talk With Other Members
  • Be Notified Of Responses
    To Your Posts
  • Keyword Search
  • One-Click Access To Your
    Favorite Forums
  • Automated Signatures
    On Your Posts
  • Best Of All, It's Free!

*Eng-Tips's functionality depends on members receiving e-mail. By joining you are opting in to receive e-mail.

Posting Guidelines

Promoting, selling, recruiting, coursework and thesis posting is forbidden.

Jobs

gas phase reactor

gas phase reactor

(OP)
in the gas phase hydrogenation reactor, is it possible to recycling the outlet of the reactor to reduce the inlet concentration of MAP (methyl acetylene & propadiene)?!

RE: gas phase reactor

Can see the benefit of this if it is possible to increase the MA and PD concentration in the recycle stream to be higher than that in the fresh feedstream to the hydrogenation reactor. This would increase the partial pressure of these components in the reactor feed, thus enabling a higher net conversion outside the recycle loop.

To concentrate these components, it would depend on the location of this reactor in the separation section, which you havent said ( is this reactor still on the bottoms exit from the de ethaniser ?)

RE: gas phase reactor

(OP)
I do not want to increase the concentration of MAPD in the inlet stream, i want to decrease it to improve the reactor run lengths.


I searched about the reason of poor run lengths of the C3 hydrogenation reactor, and I find that for Operating safety demands that the significant exotherms experienced in MAPD hydrogenation be tightly controlled. This is commonly achieved by recycling lead bed product in liquid phase two-bed systems in order to limit the MAPD content in fresh feed.

My inquiry, is it work with gas phase system?

thank you

RE: gas phase reactor

Okay, can see the reasoning for decreasing MAPD content for plants where reactor bed intercooling is a constraint.

Although the temp rise in gas phase would be much higher than that for liquid phase for a given conversion(for obvious reasons), my simple reasoning tells me the same should be possible for gas phase, assuming you have sufficient means for intercooling and with intercooling at shorter bed depths. Would guess overall net bed depth woould be more than in liquid phase in order to enable running at lower temps to allow for bigger control response margin for temperature runaway.

RE: gas phase reactor

(OP)
Thank you for your cooperation.

Red Flag This Post

Please let us know here why this post is inappropriate. Reasons such as off-topic, duplicates, flames, illegal, vulgar, or students posting their homework.

Red Flag Submitted

Thank you for helping keep Eng-Tips Forums free from inappropriate posts.
The Eng-Tips staff will check this out and take appropriate action.

Reply To This Thread

Posting in the Eng-Tips forums is a member-only feature.

Click Here to join Eng-Tips and talk with other members!


Resources


Close Box

Join Eng-Tips® Today!

Join your peers on the Internet's largest technical engineering professional community.
It's easy to join and it's free.

Here's Why Members Love Eng-Tips Forums:

Register now while it's still free!

Already a member? Close this window and log in.

Join Us             Close