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Try Krohne Meters.

Have you checked the steam eductor nozzles? Once they start to wear you can lose diff P and or overwelm a condenser. Also see if large amounts of inerts may be entering the column.

The minimum schedule used for threaded connections is 40.

I've seen this often in processes where the process fluid condenses inside the normal range of ambient temperatures.

http://www.gmigasandflame.com/article_sil103.html Seem to answer your question

You basically create a aqueoua ammonia solution that get stronger until the water is saturated. Any impurities in the water could be converted to something else, most likey a salt.

Are you venting into the water or into the vapor space?

The answer to that question lies with the resolving plant requirements. Just a few off the top of my head would include; How much flow can the effluent system manage? Why are you draining the tanks? What is the cost of downtime? What type of work are you planning for? Tank entry? other...

A simple test to narrow down your problems is to test the valve with a manual input. If you can't control in manual, then it may not be the tuning parameters. It may be the valve is sized wrong, or there on transient condition upstream (or downstream) not within the control envelope.

I don't know how tightly run or well trained the operation is, but my experience is that 100% is not good practice. All it takes is one person to misunderstand that 100% means no material can ever be added above the set point and you will have a spill on your hands at some point in the future...

Does this help? http://www.woodcousa.com/about_wnf.htm

Have you checked the flow meter? As pointed out the compressor meets demand. If for some reason the flow meter was off it could account for the difference you see in perfomance.

Try this vendor. I have had good success using their products http://www.flexicraft.com/Hydropad_Accumulator/

Here is a pretty good overview of the HAZOP process http://www.ntnu.no/ross/srt/slides/hazop.pdf

The ASME BPVC code section VIII U-1 scope will provide the answer to your question. For such a high temperature application an option is to build to the code but not have it stamped. (assuming it does not need to be stamped)

One of the first things to consider is the size of the vessel. Below a specific volume and or dimensions the "vessel" is treated like a pipe.

In addition to the excellent advice posted above to hire a firm with expertise in API 510 and 570 inspections, you should get the guidelines available for the Chlorine Institute. http://www.chlorineinstitute.org/index.cfm They will include a lot of good information about pipe and equipment...

Check OSHA regulations and NFPA 101; Life Safety code

A few things come to mind 1. Operating too close to the set pressure. 2. Pipe line pulsations 3. Corrosion. (even small amounts of corrosion can adversely affect a RD) 4. Improper burst tolerance range on disc. http://www.iceweb.com.au/Technical/rupture_disk_specification.htm When you say...

IS your goal actually leak detection? That's a bit of a different animal than gasket inspection.