Commonly Missed Overpressure Scenarios
Transcript of Commonly Missed Overpressure Scenarios
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Commonly Missed Overpressure Scenarios
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Smith & Burgess
• Formed Smith & Burgess to have a company that providesthe highest level of customer service.
• Founders have over 25+ years of Process Safety experience each.
• Over 250 years of combined Process Safety experience.
• Members of API & participants on the 520/521 Safety Committees.
• Saved our clients an estimated $100+ million in unnecessary costs.
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Smith & Burgess
• Over 1500 completed national and international projects.
• 50+ process safety engineers on staff.
• Over 15 research papers published nationally.
• Created "Salus Solutions"- the ONLY customizable relief systems documentation tool.
• 2015 Houston Business Journal's "Best Places to Work - Top 20"
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Today’s Topics
• Reverse Flow
• Vapor Breakthrough
• Partial Power Failures
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Reverse Flow
• Historically, check valves were used to protect assets
• Contamination
• Reverse rotation – damage to bearings, seals
• Not effective means of preventing overpressure
• Check valves can leak or fail
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Reverse Flow
“Failure Modes and Causes for Swing and Lift Type Check Valves”Nuclear Industry - Oak Ridge National Laboratory
Double Disk Lift Stop-Check Swing
Significant Failure Rate*
1/114 yrs 1/63 yrs 1/438 hrs 1/87 yrs
*Significant Failure Rate: Broken/Damaged, Restricted Motion, Stuck Open, Stuck Closed, Improper Seating
Wermac.orgWermac.orgValvematic.com Babcockvalves.com
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Reverse Flow
Oak Ridge National Laboratory (Nuclear Industry), Study of failures that occurred between 1984 and 1990
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Reverse Flow
Oak Ridge National Laboratory (Nuclear Industry)
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Reverse Flow
Single Check Valve
Dual Check Valves
Single Safety Critical Check Valve
Dual Safety Critical Check Valves
Normal Leakage Yes Yes Yes Yes
Severe Leakage Yes Yes Yes Yes
Complete Failure
Yes Yes Yes No
Normal leakage: associated with normal wearSevere leakage: check valve seat damage or obstructionComplete failure: stuck wide open
RAGAGEP
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Reverse Flow
Plant #1 Plant #2 Plant #3 Plant #4
Facility Type West Coast Refinery
West Coast Refinery
Gulf Coast Refinery
Europe Refinery
Total PRV Systems Evaluated 1300 2200 600 600
# of Systems with Applicable Reverse Flow Scenario
30 35 15 20
# of Systems w/ Inadequate Overpressure Protection
10 10 11 8
% Inadequate 33% 29% 73% 40%
Average Expected Accumulation
4 X MAWP 3 X MAWP 7 X MAWP 3 X MAWP
Range of Expected Accumulation
1.4 – 18 X MAWP
1.2 – 8 X MAWP
1.5 – 15 X MAWP
1.3 – 6 X MAWP
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Reverse Flow
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Reverse Flow
Common systems where check valve failure scenario is applicable:
• Feed Surge Drums
• Deaerators
• Compressor Suction Drums
• Wash Water Drums
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Reverse Flow
Feed Surge Drums
Feed Surge Drum
Feed / Product Exchanger
DistillationSeparator
Reactors
Level Valve Reboiler
Bottoms Product
Overhead Product
Off Gas
Condenser
Feed Pumps
Tankage
Next UnitFeed Surge
Unit Boundary
FeedHeater
s
To Flare
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Reverse Flow
Reverse Flow
50 - 100 psig600 - 2000 psig
Feed may continue
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Reverse Flow
Dual Safety-Critical Check Valves
Rerate vessel
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Reverse Flow
Stops reverse flow
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Reverse Flow
Stops feed
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Reverse Flow
Relieves feed
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Reverse Flow
Summary
• Reverse flow can result in extremely high accumulation pressures if not properly mitigated
• Mitigate with:
• Higher design pressures
• Minimum dual safety critical check valves
• Instrumentation may be required
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Vapor Breakthrough
Control valve is interface between HP and LP
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Vapor Breakthrough
Liquid level drops
Liquid level rises
Control valve fails open
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Vapor Breakthrough
If downstream level sufficiently low to allow vapor-liquid disengagement
Vapor relief
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Vapor Breakthrough
If downstream level reaches point where liquid is carried over with vapor
2-phase relief
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Vapor Breakthrough
If downstream vessel overfills
Displaced liquid
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Vapor Breakthrough
• Sophisticated methods should be used to determine relief phase
• Phase quality and flow rate depend on:• High and Low P/T• Compositions• Liquid levels• Vapor velocity• Vessel orientation• Inlet nozzle elevation• Location of relief device
• But…• Generally, 14 inches of freeboard height between liquid
level and outlet nozzle may be sufficient to minimize liquid carryover
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Vapor Breakthrough
• Liquid displacement often results in substantial relief requirements
• Design options:• Increase downstream MAWP• Increase downstream vessel size
• Existing installation mitigation options:• Size PSV for liquid displacement• Credit for liquid feed• Credit for flow resistance of piping• Restrict inlet flow• Modify liquid levels• HIPS
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Reverse Flow
Summary
• Vapor breakthrough can result in high accumulation pressures if not properly mitigated
• Check effects of downstream liquid level on relief phase
• Prevent liquid displacement scenario
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Partial Power Failures
• Power failures generally belong to three different categories:• Loss of individual equipment• Total Power Failure• Partial Power Failures
• Equipment affected from partial power failures are determined using one-line drawings
• Partial power failures often result in worst-case scenarios for relief device sizing and for flare system analysis
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Partial Power Failures
Fractionator system
Feed
Heat input
Cooling
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Partial Power Failures
Individual equipment failures
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Partial Power Failures
Individual equipment failures
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Partial Power Failures
Individual equipment failures
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Partial Power Failures
Total Power Failure
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Partial Power Failures
Partial Power Failure
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Partial Power Failures
PPF-1
All “A” pumps fail during PPF-1
All “B” pumps fail during PPF-2
Assume “B” pump is spare
Assume “A” pump is spare
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Partial Power Failures
CW Failure
Steam Failure
Instrument Air Failure
TPF PPF #1 PPF #2 PPF #3
Total load (lb/hr)
650,000 1.5 MM 2 MM 2.5 MM 3.5 MM 3.5 MM 4.5 MM
# BP Concerns
2 2 3 5 13 17 21
Refinery example with ~2000 relief device systems
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Partial Power Failures
Potential Impacts of Partial Power Failures
• Larger relief requirements• Higher total flaring load• Higher backpressures• Higher header velocities• Possibly significantly larger loads in certain subheaders• Higher radiation• Higher liquid flows• Higher liquid load to flare KO drum• Slug flow in flare header
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Recap
• Reverse Flow
• Vapor Breakthrough
• Partial Power Failures
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Questions & Answers
Thank you for attending today’s presentation:
Commonly Missed Overpressure Scenarios
Please reach out to either Waheedif you would like more information:
Waheed Wakil, PE
Technical Engineering Supervisor