Q & A

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This face to face interactive event, features experts from leading European refineries and technology providers; engineers will have the chance to hear unparalleled knowledge through interactive discussions such as fishbowl panels, Q&A Panels and Poster Sessions. Learn more here: asktheexperts.wraconferences.com  


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Recent Questions
Date  Replies
19/09/2018 Q: Can hot naphtha at 120 deg C be transported through ICPR pipeline?  
09/09/2018 Q: What are the benefits of saturating your raw natural gas feed with water?  
08/09/2018 Q: Naphtha vapours are observed at manway lid of roof top when its opened . Mild naphtha vapours are also observed at roof drain of the storage tank when its opened. Generally roof drain of the storage tank is kept in open condition only . The storage tank is of Internal Floating Roof type . Tank safe height is 10.75m . Generally tank height is maintained at 9 m or lower. Tank outlet Temperature is between 36 to 42deg. Let me know why naphtha vapours are emanating from roof tanks and roof drains. I dont think there is swivel joint leak .
(2)
03/09/2018 Q: Coking Drum Switch Handling:
Delayed coking unit, in a strict sense, is not a continuous process. Coke drums are operated in batches and downs stream fractionators and strippers are operated continuously. Each of the events during coking cycle , such as preheating, drum switch over , drum filling cause big disturbance to the downstream process.
Advance Process Control may not be applicable for this operation.
Can automating the SOP of Drum Switching improve the coking cycle?
(1)
31/08/2018 Q: At present we face sudden increase in bromine index for benzen product in our aromatic plant. This cause our benzene product to goes to off spec as the BI exceeded the spec limit. We did several actions in order to improve the Bi level, hot clay treater for BT cut , one was isolated for replacement and only one remaining now in service and operated at higher temperatures, so is there any one has such experience. Please advise
Also the Bz losses in raffinate product from extractive column was increased to allow more lifting of heavy olefin, but still the observed effect is very minor ,so please share with us your experience if any for such case.
(2)
Recently Answered Questions
Date  Replies
11/03/2017 Q: Please tell me the normal PH limit supposed to have at the NHT Stripper Column Overhead drum water boot sample. Currently, we are getting ±1 which is very low. Please enlighten me whether it could be the effect of wet H2S alone or it could be the cause of combined effect of wet HCl and H2S which might carry over during the wash water injection from reactor effluent Separator drum to the Stripping Column Overhead Drum.
FYI- 10 wt ppm CHIMEC 1044 is being injected at the inlet of stripper overhead air cooler continuously.
(3)
08/09/2018 Q: Naphtha vapours are observed at manway lid of roof top when its opened . Mild naphtha vapours are also observed at roof drain of the storage tank when its opened. Generally roof drain of the storage tank is kept in open condition only . The storage tank is of Internal Floating Roof type . Tank safe height is 10.75m . Generally tank height is maintained at 9 m or lower. Tank outlet Temperature is between 36 to 42deg. Let me know why naphtha vapours are emanating from roof tanks and roof drains. I dont think there is swivel joint leak .
(2)
23/08/2018 Q: I am working in VGOHDT. We are facing flaring issue intermittently in Fractionator overhead drum. We are using split range controller for maintaining pressure using fuel gas and excess pressure will release in LP flare.
But we found that the overhead gas composition consist about 51% hydrogen ,23% methane and 14% nitrogen respectively which are non condensable gases. We increased HP steam in stripper column and reduce the pressure in Cold LP separator for removing it but problem persist. Kindly give suggestion to reduce H2 and methane to reduce flaring in Fractionator?
We are operating fractionator pressure at 1kg/cm2 and top temperature at 106 deg c.Overhead Finfan outlet temperature at 45 deg.
(5)
31/08/2018 Q: At present we face sudden increase in bromine index for benzen product in our aromatic plant. This cause our benzene product to goes to off spec as the BI exceeded the spec limit. We did several actions in order to improve the Bi level, hot clay treater for BT cut , one was isolated for replacement and only one remaining now in service and operated at higher temperatures, so is there any one has such experience. Please advise
Also the Bz losses in raffinate product from extractive column was increased to allow more lifting of heavy olefin, but still the observed effect is very minor ,so please share with us your experience if any for such case.
(2)
03/09/2018 Q: Coking Drum Switch Handling:
Delayed coking unit, in a strict sense, is not a continuous process. Coke drums are operated in batches and downs stream fractionators and strippers are operated continuously. Each of the events during coking cycle , such as preheating, drum switch over , drum filling cause big disturbance to the downstream process.
Advance Process Control may not be applicable for this operation.
Can automating the SOP of Drum Switching improve the coking cycle?
(1)
Post