Stirrer tower top temperature, reflux rate, reflux tank level.
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There is no control point for the temperature at the top of the stripper; is it appropriate to use cascade control for the liquid level and reflux flow in the reflux tank?
In a distillation column, it is not possible to do this in order to control the temperature of the sensitive plate; however, such an operation is feasible in a stripping column
There’s nothing unreasonable about it; as long as it can be controlled, it’s fine. Sometimes, one shouldn’t be too rigid in certain procedures – innovation is needed
I feel that change is indeed necessary; we can’t be rigid. I have a distillation column here; during the design phase it was possible for the light components to be carried away by the column, but eventually it was required that none of them should be carried away. It took a long time to achieve this goal, and as a result the operating temperature rose from around 100 to around 115. After some time, it seemed wasteful to let the heavy components be discharged, so a side stream was added to the column, with the requirement that no light components be removed, only the C4 components. It was achieved in the end as well. The tower is a depropanization tower. So some operations still need to be tried.
This post was last edited by Ice-Cold Radio on 2017-1-2 at 13:37
This post was last edited by Ice-Cold Radio on 2017-1-2 at 13:37
If the pre-hydrogenation stripping tower is used only for H2S removal and is followed by a decanter tower, then the stripping tower can use level control for reflux. If it is a combined desulfurization and degassing tower, then it is not suitable.
Agree with view #8; there is a fractional distillation tower later. The stripping tower also operates in full reflux mode, so the light components are not wasted.
Generally, the tower top temperature and reflux are in cascade, while the reflux tank level and production rate are in cascade as well
As long as it can achieve control, stable production is reasonable!