#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👇👇
@Refinerytraining

#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
https://telegram.me/joinchat/BPcqEj6oILuNjxCzl0Qhsg

💯 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.”

Follow me in Linkedin: https://www.linkedin.com/in/esmaeil-esmaeilzadeh-2216b27a?utm_source=share&utm_campaign=share_via&utm_content=profile&utm_medium=android_app

⚗️🧫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

Follow me in Linkein:
https://www.linkedin.com/in/esmaeil-esmaeilzadeh-2216b27a?utm_source=share&utm_campaign=share_via&utm_content=profile&utm_medium=android_app
Telegram link:
@Refinerytraining

https://telegram.me/joinchat/BPcqEj6oILuNjxCzl0Qhsg

🔷 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
#oilandgasindustry #oilindustry #gas #gasindustry #refinery #refineryoperations #refineries #petrochemical #oilgas #oilandgas #lng #oil #petroleum #offshore #chemicalengineering #chemicalindustry #energy #Safety #HSE
https://www.linkedin.com/posts/esmaeilesmaeilzadeh_ccr-chemicalengineering-reforming-activity-7388147677739499520---T8?utm_source=social_share_send&utm_medium=android_app&rcm=ACoAABDVMbkBXWPI6diiEmJb4W5gn6lNDAFOLFg&utm_campaign=share_via

📉🎯 Golden Rules for Selecting a Fire Pump Curve According to NFPA 20

🔴When evaluating a fire pump performance curve, focus on these critical requirements:

✅ The rated duty point should be located in the stable operating region of the curve.

✅ Prefer a relatively flat and stable pressure-flow characteristic to accommodate varying fire demand conditions.

✅ Always evaluate the complete pump curve—not just the rated duty point.

🔔✅ At 150% of rated flow, the pump shall develop at least 65% of its rated pressure.

🔔✅ At shutoff (zero flow), the pump pressure shall not exceed 140% of rated pressure.

🔔✅ The pump shall also be rated for net pressures at or above 40 pounds per square inch (psi) (276 kilopascal [kPa]).

✅ The normal system demand should fall close to the pump's Best Efficiency Point (BEP) whenever practical.

✅ Avoid excessive oversizing, which can result in operation far to the left of the curve and increase recirculation risks.

✅ Ensure sufficient pressure margin at the most hydraulically remote fire protection demand point.

✅ Verify that the available water supply curve intersects the pump curve at an acceptable operating point.

✅ Confirm adequate NPSH Available (NPSHA) throughout the entire operating range.



🔴Image 2 shows the acceptable performance characteristics of a fire pump, along with the parameters established by NFPA 20, and Image 3 displays typical pump performance characteristics when a pump is operating with a surplus of suction pressure, known as a positive pressure test, and under a 15-foot suction lift.

⚠️ A fire pump is selected for the emergency you hope never happens. The pump curve must provide reliable performance across the full range of expected fire scenarios, not only at its rated capacity.

#NFPA20 #FirePump #FireProtection #PumpCurve #FireWaterSystem #Hydraulics #ProcessSafety #MechanicalEngineering #Engineering


https://telegram.me/joinchat/BPcqEj6oILuNjxCzl0Qhsg