It is also pretty much what we are having to stick with for the PFD for POX due to time constraints.
The PFD of your POX unit does not look like that of a real POX unit.
Or is this supposed to be a combination of SMR and POX? That would not make any sense.
In any case nobody uses a POX unit to produce pure hydrogen from natural gas feed as an SMR is much more economical for that.
Only if pure hydrogen is to be produced from coal or heavy oil a POX is used because steam reforming is not an option for such feeds.
A POX unit with natural gas feed only makes some sense if syngas (H2/CO = 2) is to be produced. The Shell Pearl complex in Qatar uses 18 POX units to turn natural gas into syngas for Fischer-Tropsch. The FT product is sent to a Hydrocracker which gets its hydrogen from SMR, not from POX. So although the complex has many POX units Shell also built dedicated SMR to produce pure hydrogen.
The same applies to ATR; that only makes sense for producing syngas, not to produce pure hydrogen.
In the HAZID you should also include the high amount of H2S in the NG feed and HDS effluent as H2S is very toxic. Part of the SMR unit may fall into a special classification like other parts of the refinery where H2S concentrations in the process are above a certain level.
CO in the reformer effluent is also toxic so you want to mention that as well.
I need to know a way of sizing volume (m3) based on the information available at this stage.
You should not start a new topic about the same problem, so I will ignore that other topic.
The size of a vessel depends on its service: adsorber, reactor, separator, storage vessel, ........whatever.
So to cost each vessel you first need to size it according to its service.
Edited by PingPong, 21 November 2018 - 06:05 AM.