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Welp. Looks like im dead

I have a problem with the vapor containment. It appears to me that the Inner Tank is ONLY vapor tight if the seal between Suspended Deck and the Inner Tank Shell is vapor tight - which of course it is not. Vapor will pass and be contained by the roof on the Outer Tank. It is in fact the roof on the Outer Tank - steel or steel liner and concrete that provides the vapor containment on all LNG tanks, and, all tank roofs are supported on the Outer Tank wall. If my understanding is correct then the accepted definition of Single, Double and Full Containment is not entirely accurate?

Is this a purchasable spreadsheet?

Your updates on changes to API-653 or API-650 are very much appreciated.

Great content. One minor correction. Density of LNG ranges from 0.430 to 0.47 not 0.6.

Hi, you may use vlookup function for unit change instead of nested if function.

Thanks Phil, really interesting video.

Very good summary of the Standards Process and the effort to incorporate advancing technologies. Your leadership, knowledge and contribution to the Standards effort is why you were selected for this presentation.

Thanks, finaly a serious talk about the topic.

Good stuff, thanks for sharing!

Phil this is great, love what you do!

This is really good information, not many people talk about this subject.

We've been having lots of quakes down there lately.

Thank you .. I would like to use this as an awareness presentation within my company (operator) if you wouldn’t mind .. excellent knowledge sharing with the industry much appreciated

2:54 As a spanish speaker she said: "No manches, se está abriendo bien cabrón" which could be translated as: "No way! It's opening impressively!" Great video, by the way!

The corrosion rate calculations definitely should be updated and revised with more clear language and not combining internal and external corrosion rates (assuming they line up).

😕 Promo'SM

This video was brought to my attention so I watched it and for what it's worth, have this to offer. 1st, API 653 was and is a great standard, but on several issues, it can be challenged and this is one of those areas of contention. 2nd, Mr. Myers is correct in that, depending simply on what side of the bottom plate the “same depth of pit” is located, that a person may calculate differing results in futuristic useability of the existing bottom plate. 3rd, I may slightly disagree with the assertion that topside and underside corrosion will not be located directly opposite to one other. Some believe that the possibility for alignment increases as the tank’s diameter decreases. (That’s another discussion) 4th, I would never pick an intellectual argument with Mr. Myers. Thank you.

Can you send me the excel application please

How do i get this spreadsheet ?

Can you please guide me for selecting correct size of pressure and vaccuum valves for bulk fuel storage tanks.

Glad to hear all is ok

𝚙𝚛𝚘𝚖𝚘𝚜𝚖 🌷

#sotaog is working on same concept of tank level analysis, some companies still relie on old tank level monitoring technology

Great job, Phil

woohoo-Yo. super ~

Thanks for sharing, really valuable information

Thanks for sharing, great information

Great video Phil, I’m going to show it at my next staff meeting for my safety moment!

Has anybody looked at the available seismic data to identify SA fault areas under additional stress by looking at slight variations of shockwaves thru them. Similar to when the seismo trucks vibrate and reflections are analyzed.

great!

Hi, your channel is very interesting. I write you from Ecuador. Maybe you can help me with an aclaration. For Pressure / Vaccum Relief Valves PVRV or (Breather Valves). According API 2000 (5.4.2) when you make the seat test at 75% (pressure or vacuum) the maximum allowed leak rate not shall be upper: 0.5 CFH for 2 inch to 6 inch valves; 5 CFH for 8 inch to 16 inch valves; and 20 CFH for 16 inch valves or greather. I am construting a PVRV test bench (but I dont know how to select the thermal mass low meter range appropiate); I have several alternatives: LOW FLOW 1lpm - 50 lpm SIZE 1/4 inch 4 lpm - 200 lpm SIZE 1/2 inch 8 lpm to 400 lpm SIZE 3/4 inch 4 lpm to 700 lpm SIZE 1 inch HIGH FLOW 50 lpm - 250 lpm SIZE 1/4 inch 20 lpm - 1000 lpm SIZE 1/2 inch 40 lpm - 2000 lpm SIZE 3/4 inch 70 lpm- 3500 lpm SIZE 1 inch But, I reviewed another option a mass meter too, its range is 0 - 200 ml/min SIZE 1/4 inch. Do you think, the mass meter is the adecuate? or sould I use a rotameter? Can you help me to select the adecuate flowmeter?

Very interesting - thanks for posting

How did that much flammable gas wind up In a water tank?

California warning……Exploding water tanks are known to cause cancer.

I wonder why there isn't a over pressure check valve or burst disc, filtered recirculating vent as code/regs, and if it did why didn't it work.??

kinda makes you wanta think twice about Smoking and drinking.....water at the same time......

Being a totally clueless individual I have to ask: How did a combustible gas get into a water tank?

This is basic crap. Whenever working in confined spaces, YOU MUST CHECK ENVIRONMENT. 30 years of doing this work and now retired. Never had anything like this because of procedure . Would never start work without proper screening area.

Sop should be followed

Always test the air in enclosed spaces. Especially if you’re doing open hot work. This is a great Darwin Award. It’s a shame the welder injured someone else tho.

Everybody's hopes and dreams After covid hit the second time.

I think it's worth mention that some of the newer methane meters do not power the whetstone bridge full time but rely on the last known value of the reference. If someone was to drop or jostle the meter hard enough to interrupt the battery for a split second it can re-calibrate to whatever the percentage gas is at that moment and then possibly lead the operator into thinking the % gas is a safe level, Light the torch boys, it's only 3%.... BOOM

“Who farted?” ……lights cigarette……

🤣🤣🤣🤣 I wonder if the welder made it space.....

I'm 74 and a good deal of my working years I was a welder, or worked in a Machine shop, or doing mechanical maintenance that required welding...the 'welder' always gets blamed for stuff because 'welding' scares people...and they often don't understand what it really is. I worked on those big shiny tanker trucks that bring gasoline to your neighborhood station. They often developed cracks, and we ALWAYS used a flammable gas detector before going inside and lighting up the TIG torch...

guy's really pissed about that infrastructure damage. It's almost like he's more upset about losing $ than losing life!

dang, what a way to go!

The design of the tank required adequate venting capacity or a fragile roof wall joint. Either OSHA regulation 29CFR1910.106 requires owner operators to have and maintain design information showing the adequacy of the venting system. Typically an area of incomplete documentation is the emergency venting or accumulation of hazardous materials. The loss of life is not acceptable. However as point out many details were not presented and so the comments are based on the out come and experience of the design of tank venting systems at multiple chemical manufacturers and refineries.

Hydrogen and Oxygen ??