Yes, you are right in saying that high pressure hydrotreaters do not have any block valves in recycle gas circuit. There are various reasons for that.
I would recommend a "swing elbow" at heat inlet and outlet lines. This will allow you to disconnect heater from process inlet/outlet lines and...
At present, i have set 27 Bar g because Compressor suction high pressure alarm is 26 Bar g....and i think 10% below design pressure (28 barg) i.e. 25 Bar g will be at very conservative side and additionally working range of Compressor shall also be reduced.
I hope, this 1 Bar g allowance w.r.t...
For one of our Projects, High Integrity Pressure Protection System (HIPPS) to be provided to protect down stream low pressure piping in case of failure of upstream Pressure Control Valve (Failure OPEN).
Design Pressure at upstream of Pressure Control Valve: 63.5 Bar g
Design Pressure at down...
Montemayor,
Thank you for your comments again.
Well, as far as certain basic information is concerned about the discussion, it is as follows.
Exchanger is BKU. Tube side passes = 4.
Diesel is heated and 525 oF. which is circulated through centrifugal pump.
There is a flow control valve in...
Thank you all for valuable input.
The only concern as pointed out is about the lower velocities on tube side because of large flow area.
However, with diesel as heating medium on tube side, what are the chances of scale formation with lower velocities which is in the range of 1-2 ft/sec in my...
hello to reader,
We are carrying out thermal design of De-ethaniser and De-butaniser reboilers (kettle)for one of our gas processing units using Hot oil circulation(diesel) on tube side as heating medium.
I have questions about the same.
What should be the maximum heat flux which i should...
I want to know the chemical composition of Antioxidant / Antistatic addtivites used for 'jet fuels'.
Who are the suppliers? What should an inquiry consist of, if i want to order these chemicals?
What should be the criteria for the selection of these additives from available options?
Thanks.
thnx both of u for reply.
i convinced by argument from TD2K..
Since vessel is already tested at 150% of it's design pressure, there should not be any harm to it or its piping components for comparatively smaller duratiion of exposure to pressures higher than MAWP.
any other idea ??
While designing relief valve, we consider 10% overpressure as a criteria, in general. What does it really mean?
1) Does this mean that the pressure in the system will remain at 110% value all the time during relief? (provided the cause of overpressure has not been mitigated).
2) Now consider...
One of the reasons for foaming might be the entrained heavy hydrocarbons alongwith sour gas which gradually built up inside the column.
I do not think that mere water flushing of the column will be useful. You need to 'de-grease' the tower and associated piping in order to ensure complete...
Does anyone have an experience of providing 'booster' pump in the cooling water return line?
Certain min. pressure at B/L in cooling water return line. After considering pressure drops in various exchangers, it is not possible to provide the required back pressure.
So, a pump in return line is...
Does anyone has an experience of using sealing compounds to arrest minor leakages from flanges in high pressure process plants?
how much reliable these compounds are?
Thanks,
I do not have experience of working in the cold conditions what you are referring to.
However,if insulatinos are proper, why would the steam or condensate freeze which is above 140 deg C? is it too much of heat loss due to cold climate?
regards,
nirav
In addition to cost of 150 Psig Steam, you also need to consider the cost of piping for 150 Psig Steam. The higher pound rating of materials.
Also, it will be difficult to execute steam tracing with IBR rating pipe for 150 Psig steam.
I mean to say the bends you need to provide for tracing...
Compressor manufacturer representative at site told that the conditions for nitrogen run with low suction pressure was not envisaged during design. The loading valves and internals may or may not face some adverse effect !!!
We have the following Hyrogen compressors in our Diesel Hydrotreater. The op.pressure of reactor is of the range of 115 - 120 kg/cm2g.
Compressor desing pressures are...
[1] Make-up Gas Compressor MUGC - 2 Stage Reciprocating.
With Nitrogen->
1st STAGE :: Suction P=6.0 kg/cm2 g; Disch P=14.0...
We have the following Hyrogen compressors in our Diesel Hydrotreater. The op.pressure of reactor is of the range of 115 - 120 kg/cm2g.
Compressor desing pressures are...
[1] Make-up Gas Compressor MUGC - 2 Stage Reciprocating.
With Nitrogen->
1st STAGE :: Suction P=6.0 kg/cm2 g; Disch P=14.0...
While designing safety systems we need to think about the system behaviour along with as codes & stds. No matter whether it is provided on vessel or pipe. The reason is you design PSV with a specifid 'Set Pressure'.
There should not be too much of difference between the pressure at the point...
