Thanks JStephen,
The fact is that the tank, by specification, shall be constructed under API 650. Thus, in order to avoid further observations I'm changing to a 36 x36" connection.
Thanks again.
Hi all!
This is a simple question:
A flush type cleanout connection with the next dimensions:
Width: 24"
Height: 36"
can be allowed by API 650? That set of dimensions are not in the tables of the standard.
However, standard 650 in paragraph 3.7.7.1 states that:
'....When a size...
HI ALL!
We are about to design a flaring gas recycling system for a LPG plant. It will include a low suction pressure compressor attached to the flare header downstream KOD and upstream the flare. Also, a water seal liquid is going to be installed before flare in order to avoid backflow at very...
dcasto,
please look the diagram:
http://i3.uploadem.com/10042007/pagina.jpg
It is possible under the conditions I show you...
Need to know a scheme of the ghamsa case.
Hi ghamsa,
First of all, a question: Assuming that each of your pumps has a check valve and a shut off valve (as most of the systems have). The recycle line starts upstream or downstream of this check valve? If it starts downstream of the pump check valve I consider it is not necessary to...
Dear sgoel:
From my knowledge you should have an additional line for venting the air in a convenient way. As you explained, drying is a different operation than filtering. This new line could have an automatic valve that opens when your system is in the drying process.
Considering that such a...
Results for circumferential stress from using:
MAWP = 1126 psi (110% Pop)
t=PR/(SE+0.4P) (Based on external radius)
t= 1.155 inch, which is greater than actual w/o using corrosion allowance, that's the problem.
For ellipsoidal cup: t=1.07 inch, which is closer but w/o corrosion...
If...
Sorry I forgot to mention:
thickness for pipe = 1 inch.
thickness for cup = 1 inch.
It is possible justify this vessel by using maximum stress values other than recommended by standards?
thanks
Hi all!
I'm in a big hurry trying to verify if a vessel could be adequated for a new service. The problem is as follows:
1.- The vessel is 36 in OD 10 feet high, pipe A-106 Gr. B.
2.-Bottom ellipsoidal 2:1 cap A-516 Gr. 70.
3.- Top Flange B.16 600#.
and should be used in the following...
Hello,
Since a KOD is usually designed to separate a certain size of liquid droplets (vg 300-500 micron), besides slugs of liquid, I found redundat to install a demister.
Also, if the gas stream is expected to be dirty then demister can be plugged causing a great undesirable pressure drop...
Hello,
I've seen FRP tanks up to 80 m3 for sodium hypochlorite (3.5m diam, 8m height) , and in the same plant we had a 30 m3 32%HCl.
In other plants I've seen a group of several tanks in storage area for 32%HCl, capacity up to 20m3 each. My be this is the most common case I've seen.
But you...
Dear all,
I forgot to mention that I considered a water temperature of 5ºC as the worst condition for the system.
Well, I downloaded Mr. Montemayor's spreadsheet, it is really useful. For the system configuration I obtained an "air seepage" of 1.5 Kg/h which is within the overdesign I assumed...
Hi All!
I have designed a system for deareating 170 m3/h of river water from 13 to 0.7 ppm of oxygen. This system consists of a deoxygenation tower (Operating pressure 70 mbara) and a liquid ring pump. I've found that it is necessary to extract abt 6 Kg/h of gas/vapor from the water stream to...
weeber (Civil/Environme),
Install an overflow leg, which is an inverted "U" atacched to the bottom of your tank, and on the other side attached to the secoundary containment. It is a common solution to overflow problems like yours. The height of this leg should be calculated to evacuate stinky...
Hi Lblopez,
Try this link:
http://www.flotrend.com/flipflop.html
I do not recommend a floating skimmer device because the articulated pipe tends to clog o plugging frecuently in a dirty medium (brine is not clean water); so it is not a reliable device.
From my point of view, it is better to...
