#storage_tank

✳️ Pilot operated valve

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🟢Can any valve be used for controlling flow rate in a pump system, and what is the effect on water hammer?
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🟢Can any valve be used for controlling flow rate in a pump system, and what is the effect on water hammer?

Not all valves are well suited for controlling system flow rate. Image 1 compares the valve characteristics of various valves. You can see that the gate valve, based on its position, increases flow rate the fastest out of any of the other valves. Of the valves presented here, the plug valve provides the most consistent flow increase versus its valve position, which is ideal for throttling. In this case, a gate valve would not be good for flow control because of the lack of linear control over the flow.

Overall, the performance and characteristics of each valve will affect the magnitude of any transients developed by valve closures and openings. It is important to consider rate of flow change versus valve position and control the closure rate of the valve such that the effects of system transients (water hammer) are reduced.
In Image 2, we have a comparison of some common valves where each valve closes over 60 seconds. The middle chart shows the pressure rising immediately upstream. The globe valve has the minimum pressure rise because the characteristics of the globe valve shown in the image above are more linear than either the butterfly or ball valve.

You can see in Image 1 that the characteristic curve of the ball valve is relatively flat coming from the bottom, with anything less than 40% open having very little effect on the flow rate. Without much change in flow until about 55 seconds, there is significant decrease in flow over the last five seconds of closure, which results in a rapid change in velocity and a high pressure change upstream. Using the ball valve would result in the greatest likeliness of a water hammer effect. This sudden rise in pressure can be damaging to equipment within the system.

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کانال تخصصی آموزش پالایشگاهی
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🔴کانال تخصصی آموزش پالایشگاهی
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Frangible Roof:
As per API 650----5.10.2.6 Frangible Roof: A roof is considered frangible ( 5.8.5 for emergency venting requirement) if the roof-to-shell joint will fail prior to the shell-to-bottom joint in the event of excessive internal pressure.

🌟کانال تخصصی آموزش پالایشگاهی:
- آموزش تجهیزات پالایشگاهی
- آموزش فرآیند و بهره برداری
- آموزش ایمنی فردی و فرآیندی
- و ...

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#Accident

🔴از حوادث درس بگیریم🔴

✳️حادثه انفجار مخزن ذخیره سازی در حین اطفا حریق به دلیل عدم رعایت استاندارد طراحی مخزن
🔴 آموزش تجهیزات صنعت نفت و ایمنی با فیلم و انیمیشن👇👇
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#Accident
✳️ دلیل فنی حادثه بالا

✅ بر اساس استاندارد API650 و API 653 بايد محل اتصال سقف مخزن با دیواره مخزن نسبت به اتصال کف مخزن با دیواره آن از جوش ضعیف تری برخوردار باشد تا در صورت وقوع انفجار داخلی سقف آن دچار پارگی شود و اگر سقف مخزن مقاومت بالایی داشته باشد مخزن از کف دچار پارگی شده و یا مخزن به پرواز در می آید و تمام محتویات آن در محیط رها می شود که میتواند بسیار خطرناک باشد...

همان طور که در این ویدئو میبینید این اصل رعایت نشده است و مخزن به هوا پرتاب شده و محتویات آن خارج می شود...
____________________________________
🔴کانال تخصصی آموزش تجهیزات صنعت نفت و ایمنی با فیلم و انیمیشن
@Refinerytraining
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💯 Refinery Micro_Theach
🟢Frangible Roof:
As per API 650----5.10.2.6 Frangible Roof: A roof is considered frangible ( 5.8.5 for emergency venting requirement) if the roof-to-shell joint will fail prior to the shell-to-bottom joint in the event of excessive internal pressure.

⚡🟢فایل درس آموزی از حادثه Failure پمپ
@Refinerytraining

🟢 Helical Strakes are aerodynamic stabilizers which are sometimes used to reduce the forces and deflections of the stack experienced due to vortex shedding.

Helical Strakes are aerodynamic stabilizers which are sometimes used to reduce the forces and deflections of the stack experienced due to vortex shedding. Strakes consist of three (3) vanes which can be wrapped in a helical pattern on the upper 1/3 of the stack. They have the appearance of a “Snake” which spirals around the stack.

If there is another stack (or tall structure) that is nearby, then the interference effects will cause the strakes to become inadequate for stopping vortex shedding. The rule of thumb is that no other tall stacks or structures within about 10 to 15 diameters of the stack. For example, if the stack was 3 m OD, then we need to make sure that we don’t have any other tall structures within 3 m x 15 = 45 m.
The one exception to this is the Euro Standard EN 1993-3-2. In Appendix B Section B.2 if the strake criteria is met, then they provide a way to calcualte the reduced the vortex shedding loads on the stack. The strakes must meet the following:
Check 1: 4.5b <= Strake Pitch <= 5b
Check 2: 0.1b <= Strake Depth <= 0.12b
Check 3: 0.3h <= Strake Length <= 0.5h
Check 4: Unstraked portion at top <= b
Check 5: Scruton Number > 8
where b = Stack Diameter, h = Stack Height
If all this criteria is met then the vortex shedding loads are multiplied by this factor:
Alpha = (1 – Ls / h)^3 , where Ls is the length of stack with strakes

The standard for fabricating strakes is as follows:
Strake Width = 0.1 * Stack Diameter
Strake Pitch = 5 * Stack Diameter
Three (3) strakes, 120 deg apart
Strake Length = 1/3 of the Stack Height
There are many instances where it is not desireable to meet all of these standards, and here are some common examples:
Don’t want strakes on a flare tip here are stiffening rings and so the strake can’t be continuous There is a conical transition in the upper 1/3 of stack Strakes interfere with ladders and platforms
The ASME STS-1 standard provides the following guidance on these issues:
“Each strake is to be aerodynamically continuous except at specific locations where cuts may be necessary to clear ring stiffeners or other attachments.”

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⚗️🧫Denitrification Reaction (or denitrogenation):

⚗️🧫Denitrification Reaction (or denitrogenation):
Nitrogen is removed in catalytic hydrotreating by the breaking of the C-N bond producing a nitrogen free aliphatic and ammonia. The breakage of the C-N bond is much more difficult to achieve than the C-S bond in desulphurization. Consequently denitrification occurs to a much lesser extent than desulphurization.
Nitrogen is typically not a significant problem in virgin naphtha. If this were the case, a nickel molybdenum catalyst at higher severity hydrotreating conditions would be required. Nitrogen compounds typically found in straight run naphthas are methylpyrrol and pyridine.
🔴The heat released by the denitrification reactions is also negligible owing to the small amount of nitrogen compound involved.
🟡Nitrogen Compounds: Pyridine, Quinoline, Acridine (Basic Nitrogen), Pyrrole, Indole, Carbazole (Non-Basic Nitrogen)
🟪 Some Point for nitrification reactions:
• 1️⃣HDN is the hydrogenation of organic nitrogen compounds yielding hydrocarbons and NH3.
• 2️⃣HDN has a two-step pathway: Hydrogenation, followed by Hydrogenolysis
• 3️⃣HDN is an exothermic reaction and is favored at high PPH2.
• 4️⃣HDN of nitrogen aromatics compounds is more difficult than of aliphatic compounds
• 5️⃣Under mild conditions HDN can be fully assigned to kinetic factors, at more severe conditions thermodynamics sets in
• 6️⃣Organic (basic) N strongly inhibits HDS and HDA reactions
• 7️⃣HDN rate decreases with increasing molecular weight and steric hindrance

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🔷 Understanding the Regeneration Loop in CCR Units

The Continuous Catalyst Regeneration (CCR) system plays a critical role in maintaining the long-term efficiency and stability of reforming units by continuously restoring the activity of the catalyst that is exposed to deactivation during the reaction process.

🎯 Objective of the Regeneration Loop: The main objectives of the regeneration section in a CCR unit include:

➡️Burning off coke deposits accumulated on the catalyst during reforming reactions.
➡️Re-adjusting chlorine levels to maintain optimal catalyst acidity and performance.
➡️Restoring metal dispersion on the catalyst surface to recover its initial activity.
➡️ Reducing catalyst metals (such as platinum) to their active state before returning to the reaction section.
➡️ Treating regeneration gases to remove contaminants and control emissions before venting or reuse.

✅ Through these steps, the regeneration loop ensures that the catalyst continuously cycles between the reaction and regeneration sections with minimal performance loss and maximum reforming efficiency.

⚙️ Main Sections of the Regeneration Loop (According to REGEN C2 Design):

1. Regenerator Reactor : The main vessel where coke combustion and catalyst reconditioning take place under controlled temperature and oxygen levels.
2. Washing Drum: Used to remove soluble impurities and residual chloride compounds from the regeneration gas stream.
3. Regeneration Loop Dryer: Eliminates moisture to protect downstream equipment and maintain stable gas composition.
4. Regeneration Loop Compressor: Circulates regeneration gas through the loop and maintains proper pressure differential across the system.
5. Air Compressor: Supplies the required combustion air to the regenerator reactor.
6. Air Dryer: Ensures the inlet air to the system is completely dry, preventing unwanted oxidation and corrosion issues.

💡Engineering Insight: A well-designed regeneration loop is vital to achieving steady-state catalyst performance, prolonged catalyst life, and optimal reformate quality. Proper control of temperature, oxygen concentration, and chlorine balance directly affects catalyst stability and unit reliability.

#CCR #chemicalengineering #Reforming #chemicalengineer
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