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Valve vendors specify the leakage rates for their products using ANSI standard FCI 70-2. This spec is used to determine what the Control Valve Seat Leakage is based on valve classes. The leakage rates measured in ml/min or bubbles/min an be found in the table. The higher the valve Class, the...

For typical glycol dehydration processes (without enhancements: stripping gas, lean oil (Drizo), etc)you would do well to get water levels at ~3-5 lbs/MMscf. You could probably lower that water level with stripping gas, perhaps down to 2 lbs/MM. If you went with glycol with enhanced features...

In a previous, now closed post (thread 1203-257564), the question was asked about the location of the PSV when a vessel contains a mesh pad. Although guidance was provided by several that posted, the guidance (or better yet), the regulatory requirement given in ASME Section VIII D1 was NOT...

In previous post (#) the question was asked about location of the PSV when a vessel contains a mesh pad. Although guidance was provided by several, the guidance (or better yet, the regulatory requirement given in ASME Section VIII D1 was not quoted. UG-35 discusses this requirement and states...

With the exception of a PSV downstream, is there any other application where a restriction orifice should NOT be used?? I am refering mostly to code restrictions, although best practices would also be of interest. My service is in the oil and gas business only.

Kiwi2671: NGL is a mixture of C2 through C5+ that for our operations, is a product of a cryogenic distillation process (usually thermoexpanders) in gas plants. The overhead from this tower is residue gas, mostly methane, that is used/sold as sales natural gas. The bottoms from this tower is...

Duwe6: Thank you for the response but I contend that NGL is not refrigerated methane, but rather a distillation cut that includes C2 through C5+ instead. As matter of fact, NGL may be classed as a "demethanized liquid". Also, the vapor pressures (expressed as Reid VP) follow two different specs...

What is a spec (API or other) that would define the requirements to satisfy REGAGEP (recognized and generally accepted good engineering practices) for natural gas liquid storage (NGL)? I am aware of a spec such as API 2510 (Design and Construction of LPG Installations) that is good guidance for...

thread184-114563 provides the framework for my question. It appears that each code applies to two distinct services for delaing with LPG (processing plant vs LP gas systems). In my application, I am dealing with a gas plant that stores propane used for refrigeration. According to the scope in...

A proposal has been made in a gas sweetening application using a very low L/V ratio, at 0.217. That is an 70" ID amine contactor is being proposed to treat 115 mmscfd of gas using a 25 gpm amine rate. This is the lowest L/V I have ever seen and I'm very concerned that the internals (packing)...

We operate many metal, production tanks when we produce from a well. These tanks will contain condensate (oil) that is often trucked out from a facility (E&P Operations). We are looking to prevent potential incidents caused by static buildup (we know it is not lightning in many cases) and...

In my plant design, we have full flow bypass valves around PSVs in a cryogenic hydrocarbon stream. Each PSV has two CSO valves that are closed when servicing the valve (inlet and outlet). Full flow gate bypass valve has been designed around every PSV valve. The release from these valves (PSV and...

I have a steam relief valve that failed when the inlet piping to the valve cracked. The mechanism is being investigated. Can you provide me a reference (API like code) where I can find how the discharge piping of a steam relief valve needs to be designed? The vent piping was supported.

I am looking for a design reference that would enlighten me on the proper design of a steam relief valve vent (discharge) piping. A failure resulted in the inlet piping to a steam relief valve. The valve had a sizeable vent pipe that was supported. The weight (forces) of that vent pipe is coming...

After some searching, I found the following guidance on my question. Although lengthy, will include for completeness. Bottom line, OSHA does NOT permit the storage of Class 1 and 2 liquids that are flammable or combustible. Note that there is a distinction between aboveground and belowground...

Would appreciate a steer on the use of fiberglass storage tanks in natural gas service. Background: we produce natural gas, oil condensate (light oils of API gravity 50-70), and lots of produced water. Typically, the gas patch industry uses steel tanks to store the separated oil condensate in...

Would appreciate a steer on the use of fiberglass storage tanks in natural gas service. Background: we produce natural gas, oil condensate (light oils of API gravity 50-70), and lots of produced water. Typically, the gas patch industry uses steel tanks to store the separated oil condensate in...

This was also posted in the forum for Chemical Processing Engineering (perhaps by mistake): A colleague is installing a combustion burner to combust BTEXs from a TEG glycol still. The burner has a 400F shutoff temp. For some reason, 400F seems to be low to totally combust BTEXs from htis...

A colleague is looking at installing a combustion burner to burn the BTEXs (benzene, toulene, ethylbenzene, and xylenes) from a TEG glycol still. The combustion device has a 400F temp shutoff. For some reason, this temp seems low to totally combust BTEXs. (The project team prefers combustion...

What spec do you recommend for heat exchanger tubes in amine service? Do you have shared learnings around the use of seamless CS, welded (ERW = electric resistance welded) CS vs SS tubes in amine service? What has been your experience (if any) with ERW CS failures in amines? What do you...