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Hi Maddocks, I think the clients Design practice should take precedence on this. Exxonmobil, for instance, requires that you start blowing down from the maximum operating pressure. I have encounted clients to prefers PSHH set point, which can be like 90% of the MAWP. But for compressors, you...

Hi gangs, i have found the answer to my question. so you don't need to bother. Buchi

Hi DM2, it is not just about flowrate. API 521 explicitly states that the amount of steam required is primarily a function of the following; 1. flare gas composition 2. flowrate 3. steam pressure 4. tip design since tip design is a factor, that was why i suggested you touch base with your...

Hi, The HIPPS according to ASME case 2211 can replace a PRV. This is a case where an instrumented system can be used to replace a PRV. So, HIPPs when used, are proactive and can eliminate a particular relieving load scenario which could have been handled by a PRV. it cuts of the source of...

Hi DM2, One of the best ways to reduce the heat radiation on the personnel is to assist the flare tip with high pressure fluids like gas injection, water injection, steam injection etc. this is quite common in Low pressure conventional tips or so called open pipe tip which are usually subsonic...

Hi all, HYSYS reports two types of "liquid flowrates" in its conditions results tab as follows; 1. std ideal liq vol. flow in barrels/day 2. liq volume flow@std cond.in barrels/day the values assigned to these two conditions are usually close. but my question is, what is the real difference...

Hi processengineer1998, I don't imagine that you are trying to master OLGA on your own without attending the workshop in SPT group. It is a very complicated software and it seems that OLGA made that complicated to attract users to their training. actually, a trainer confided in me on that. it...

Hi all, I am trying to perform a capacity check on an existing vent header. My largest venting load has been determined. Is there some sizing criteria that one can apply to ensure a suitable vent header size. I know that relief header considers the mach number and the rhov2 criteria in...

Hi Guys, Does anyone have useful guides or reference on vent system sizing such as the sizing of the vent header and the vent scrubber? I am more farmilar with flare header sizing using flarenet and flare scrubber sizing using the API 521 criteria. thanks Buchi

Hi all, Has anyone used flaresim lately for performing flare radiation calculation? I am trying to figure how to use this software for rating an existing flare stack i.e, i already know the stack height, and would want to determine what would be the radiation on receptor points for this stack...

Hi Guys, Can someone help explain to me, in simple terms, the effect of entropy on process equipment design. thanks Buchi

In case you are getting into full blown detailed simulation of the TEG system, I am aware that HYSYS cannot be relied on for such. There are better simulators like ProMax. But like Mortena said, a simple component splitter will suffice if you are just simulating TEG in the overall...

Hi gangs, can anyone help with calculation method for determining the rate of injecting corrotion inhibitor for a give flowrate through the pipeline. best regards, Buchi Buchi

Hi Darsh73, you did not tell us whether your separator is two phase or three phase separator. It makes a whole lot of difference in the calculations algorithm. The vertical separator pretty straight forward: The calculation steps are 1. Determine the maximun superficial velocity (which uses...

Hi gangs, I need some clarification on determining the shell length for vertical separator. I am using seventh edition of API 12J, october 1, 1989. If you see page 13, Appendix C - Design and sizing calculations. There is a table c.1 titled "K factors for determining maximum allowable...

Hi Kandan, We recently had a similar situation with depressurizing a pipeline to the flare where we were going to encounter a temperature lower than the minimum design temperature. We got round this by injecting hot gas from the lean gas compressor discharge, just upstream of the compressor...

Ok Brainstorming, just to be on the same page as you; Are you looking for a standard or code that will support the argument that you can replace a PSV with HIPPS? If YES, then Guidoo has provided you with the answer: ASME VIII Division I code case 2211, approved in 1996, sets the conditions...

Hi gangs, just to help TD2K out with the reference to height above grade, API 521 fourth edition march 1997 page 14 says and i quote; " To determine the vapor generation, only that portion of the vessel that is wetted by its internal liquid and it is equal to or less than 25 feet above the...

Hi gangs, I am trying to set up a model for an Oil processing facility (FLOWSTATION) consisting of three separators stages at different conditions. I am using HYSYS. If the first stage separator is operating at 100 psig and 50 degree C (say), and the second stage is operated at 50 psig and...

Hi all, please could someone help me out with any useful tip on how to specify the flow efficiency in PIPEPHASE. i am modelling a 9km flowline and it seems the flow efficiency affects pressure drop to a large extent. thanks guys, Buchi Buchi