We used short distance piping segment for the same purpose and similar conditions. Depressurisation of hydrogen loop in hydrotreating processes.
Positive reports were obtained from operating team.
Be sure that this segment is designed to withstand choked flow and inspected properly after each...
@kootheBUNNY
This is the brief description, not detailed one. Not enough info provided.
For your info - depending on particulate conditions I have long-term positive experience with H2SO4 and sulfate environment in contact with CS, SS, glass-lined, PTFE-lined, lead-lined, acid-proof brikcs...
Is the Aspen Plus useful for prediction of Quench system ?
I worked on Aspen Plus a year. I wouldn't recommend you to use Aspen Plus. IMHO Pro/II or Hysys would be more convenient.
I worked in a chemical plant with 10% NaOH and 94% H2SO4 for years. Some of my own advices (designers often forget about this):
1. Caustic can freeze at ambient temperature. Heat tracing (usually with steam) should be provided.
2. Caustic deposits always appear inside pipes in spite of 10% NaOH...
Yes, you are correct. But it is not so big problem. For this purpose primary oil/water separators are used. For example google API separator, parallel plate separator (cross flow or downflow), daburt separator, hydrocyclone etc.
Hi, Alexander R.
Does the drain liquids in your plant have any additional treatment stages apart the drain vessel?
Usual refinery/petrochemical wastwater treatment system.
Hi, Alexander R.
I've met an undesired emulsification in refinery and petrochemical.
1. Drains
The problem is related to closed drain system and drain vessel that is used to collect drains and separate it in 3 phases: light liquid (usually chemical or hydrocarbons), heavy liquid (usually...
to LittleInch
Q1: appreciate you're working within boundaries, but to me the pump is marginal as to whether it's "suitable"
A1: What is the specific boundaries of your "suitable"? Could you please define exact figures when pump is suitable or not (links would be appreciated)? When there are no...
Hi, guys. Sorry for delay. I was ill. Lets back to pump.
Q1: Have you got a pump curve to upload?
A1: See attached.
http://files.engineering.com/getfile.aspx?folder=570b16a6-2547-4646-9140-13e74c76bca8&file=pump_curve.pdf
Q2: From your first post, the pump min flow requirement is 40m3/hr...
to ashtree
Q1: So if excessive head is seen as your problem then fitting a VFD will solve both the flow and the head issue as Little Inch suggests.
A1: Repeat "A3: ... In my case the pump has excessive capacity but not head."
to LittleInch
Q1: For me this doesn't start well "We can do nothing with this pump ". Err yes you can, you can purchase a pump which matches the duty and doesn't need a "spill back".
A1: You are an optimist. As I sad the pumh has already bought. We are just a detailed engineering contractor and...
to georgeverghese
Q: Can we not use the steam out connection for the spillback from the product pumps? This nozzle can then be for both spillback and maintenance steamout service. Nozzle location for S1 seems to be well away (some 200mm) from pump suction exit vortex breaker top, so it should...
to georgeverghese
1. Tower has no reboiler - see sketch below
2. Pump spillback return is an issue. Can you suggest best connection for spillback? Tower feed line is not proper because of top tray flooding.
3. A process sketch see attached file...
