Upload
jganguy2004
View
384
Download
54
Tags:
Embed Size (px)
DESCRIPTION
rbi methodoloy
Citation preview
1© Shell Global SolutionsP-B-v1.1
Shell Global SolutionsShell Global Solutions
S-RBISHELL RISK-BASED INSPECTION
- THE METHODOLOGY -
Risk and Reliability Management
Presenter: Maarten FestenBUSINESS GROUP
MAINTENANCE, INSPECTION AND RELIABILITY ENGINEERING
2© Shell Global SolutionsP-B-v1.1
S-RBI: SHELL RISK-BASED INSPECTION
• S-RBI Work flow
in the RRM software
• S-RBI methodology
part of RRM Manual, issued in 1999
3© Shell Global SolutionsP-B-v1.1
S-RBI AS PART OF RISK ANDRELIABILITY MANAGEMENT (RRM)
methodologymethodologyandand
databaseRRMRRM
database
SS--RBIRBI SS--RCMRCM IPFIPF
SHELL RSHELL ReliabilityCCentered MMaintenance
IInstrumentedPProtective FFunctions
(safeguarding systems)
4© Shell Global SolutionsP-B-v1.1
S-RBI PROCESS
ASSET INTEGRITYDATABASE
CORROSION LOOPDESCRIPTIONS
CRITICALITYASSESSMENT
CONFIDENCEASSESSMENT
INSPECTION/MONITORINGPLANNING
S-RB
I PA
CKA
GE
ANALYSIS/REVIEWFEEDBACK
TASK EXECUTION
5© Shell Global SolutionsP-B-v1.1
THE ADVANTAGES OF SINGLE RRM DATABASE FOR RBI/RCM/IPF ANALYSES
• COMMON USE OF RESOURCE DATA
pick lists for e.g. equipment types, materials etc.
Consequence of Failure analysis/data
• STANDARD CRITICALITY DEFINITION
1 Criticality Matrix
in line with HSE standard (RAM, April 1999)
• TASKS FOR EACH ITEM DEFINED ON SAME CRITERIA
tasks can be compared & optimised
6© Shell Global SolutionsP-B-v1.1
RBI STUDIES - RRM DATABASE
PREPARATION, WHERE POSSIBLE BEFORE THE STUDIES:
• Common part can be filled
or used from S-RCM or IPF, if already carried out
• Assets can be filled
or used from S-RCM or IPF, if already carried out
• Inspection information can be entered
“one liners”, giving relevant information only
7© Shell Global SolutionsP-B-v1.1
RBI STUDY - TEAM SESSIONS
• Review plant data, former and future operating conditions (where applicable)
• Discuss materials selection and inspection experience
• Develop Corrosion Loops and Operating Windows
• Do criticality analysis
• List confidence rating
• Develop inspection/monitoring scope
mainly by inspection & corrosion members, team review
8© Shell Global SolutionsP-B-v1.1
Shell Global SolutionsShell Global Solutions
S-RBI METHODOLOGY
9© Shell Global SolutionsP-B-v1.1
SIMPLIFIED S-RBI FLOW CHART (1)
NO
YES
INTOLERABLE
RECTIFY
MediumHigh
ExtremeNegligible Low
Asset Integrity Database
Review operating conditionsand Materials Selection
Corrosion Loops
LoopCriticality
Assessment
LoopCriticalityNegligible
No inspectionReview only
RCM
EquipmentItem
ItemCriticality
Inspection/Monitoring
Interval & Scope
Analysis &Feedback
1
Inspection /Monitoring
10© Shell Global SolutionsP-B-v1.1
CORROSION LOOPS
DIVIDE THE UNIT IN CORROSION LOOPS
• Discuss the process parameters
• Review materials applied
• Highlight inspection/degradation history
• Discuss Materials Engineering issues/experience (generic)
• Divide the unit in Corrosion Loops (colouring PFS schemes)
11© Shell Global SolutionsP-B-v1.1
S-RBI IS BASED ON CORROSION LOOPS
CORROSION
WHAT TYPE OF DEGRADATION CAN OCCUR AND WHERE ?
MATERIAL+
ENVIRONMENT
WHICH (PROCESS) CONTROLSARE NEEDED ?
12© Shell Global SolutionsP-B-v1.1
WHAT IS A “CORROSION LOOP”?
“A PRACTICAL WAY TO DESCRIBE, UNDERSTAND AND CHECK DEGRADATION MECHANISMS IN A UNIT”
• PART OF THE UNIT SUBJECTED TO:the same process conditionsthe same failure mechanismsthe same materials selectioncriteria
• ONE “OPERATING WINDOW”control of degradations viaprocess controlvalues agreed by team(boundary conditions for RBI)deviation should be reported
12-E-101
12-D
-101
12-G-101
12-K-1011st stage
12-E-102
to burn pit
Loop 1
Loop 2
Loop 3
CORROSION LOOP
• same process conditions• same degradation mechanisms
13© Shell Global SolutionsP-B-v1.1
CORROSION LOOPS FOR A KERO HDT
Product toStripper
Sour Water
Recycle Hydrogen
Hydrogen from Platformer
To Fuel Gas systemCTW5Cr 0.5Mo
321 SSas sscs cs cs as
Feed fromCDU
R-1201
E-1202
ABCDEF
E-1201
CSCS
CSCS
1.25Cr 0.5Mo
14© Shell Global SolutionsP-B-v1.1
EXPERIENCE WITH CORROSION LOOPS
• Applied in refineries, chemical plants and gasplants
• Good experience and part of S-RBI approach
• Useful to set operating windows
• Information on degradation mechanisms (and affected areas)
• Info on degradation available for all staff concerned with integrity!
15© Shell Global SolutionsP-B-v1.1
CRITICALITY ASSESSMENTFOR THE CORROSION LOOP:• Stop if Negligible Criticality or Negligible Consequence of Failure
is obtained (no further analysis on item by item basis)these items are analysed by S-RCM to optimise maintenance plans and in a review scheme for RBI (checking if changes occurred)
FOR INDIVIDUAL ITEMS:• Carry out the criticality rating for each item
can be grouped for similar piping items into e.g. “LP piping”can be divided into 2 loops, e.g. “Column top”,and “Column bottom”
16© Shell Global SolutionsP-B-v1.1
SIMPLIFIED S-RBI FLOW CHART (2)
NO
YES
INTOLERABLE
RECTIFY
MediumHigh
ExtremeNegligible Low
Asset Integrity Database
Review operating conditionsand Materials Selection
Corrosion Loops
LoopCriticality
Assessment
LoopCriticalityNegligible
No inspectionReview only
RCM
EquipmentItem
ItemCriticality
Inspection/Monitoring
Interval & Scope
Analysis &Feedback
1
Inspection /Monitoring
2
17© Shell Global SolutionsP-B-v1.1
CRITICALITY MATRIX
HIGHNEGLIGIBLES-RBI LOW MED
IUMEXTENSIVE
NNNEGLI-GIBLE NN LL MM HH
NNLOW LL MM HH EELLMEDIUM MM HH EE XXLLHIGH HH EE XX XX
CONSEQUENCES
PRO
BA
BIL
ITY
NEGLIGIBLENEGLIGIBLENO INSPECTIONREVIEW ONLY
INTOLERABLEINTOLERABLE
LOWLOW MEDIUMMEDIUMHIGH CRITICALITYHIGH CRITICALITY
INSPECTION PLAN
RECTIFY
EXTREMEEXTREMECRITICALITYCRITICALITY
DETAILED ANALYSIS
18© Shell Global SolutionsP-B-v1.1
SUSCEPTIBILITY TO FAILUREINSTEAD OF PROBABILITY• The Susceptibility to Failure (StF) is the worst case estimate for the
degradation under consideration, without corrective actions(no inspections, no monitoring).
• The StF will lead to the “Criticalty” of the items in combination with the Consequence of Failure (CoF).
• After implementation of monitoring & inspection, the remaining possibility that such a degradation leads to an incident is described as the Probability of Failure (PoF); together with CoF this describes the remaining “Risk” in operation.
The PoF must be As Low As Reasonably Possible (ALARP) and not exceed “Low” in general, and
“Negligible” where the CoF is Medium, High or Extreme
19© Shell Global SolutionsP-B-v1.1
CRITICALITY RATING
• Determine the Susceptibility to Failure (StF)
• Determine the Consequence of Failure (CoF)
• Combination of StF and CoF yields the Criticality
CRITICALITY = potential riskwithout preventive measures or corrections
20© Shell Global SolutionsP-B-v1.1
RBI CRITICALITY MATRIX (1)
N LL MM
E
H
XEH
HMM
MMLL
LL
N
N
XXEHLL3
2
1
4
PRO
BABI
LITY
CLA
SS
MULTIPLEFATALITIES
EXTENSIVEDAMAGE >10M
SLIGHT INJURY
SLIGHT DAMAGE<10K
SLIGHT EFFECT
MINOR INJURY
MINOR DAMAGE10-100K
MINOR EFFECT
MAJOR INJURY
LOCAL DAMAGE0.1-1M
LOCAL EFFECT
SINGLE FATALITY
MAJOR DAMAGE1-10M
MAJOR EFFECT MASSIVE EFFECT
HEALTH & SAFETY
ECONOMICS (USD)
ENVIRONMENTCON
SEQ
UEN
CECA
TEG
ORY
CONSEQUENCE CLASS NEGLIGIBLE1
LOW2
MEDIUM3
HIGH4
EXTREME5
NEGLIGIBLE
LOW
MEDIUM
HIGH
SUSCEPTIBILITY TO FAILURE RRM CRITICALITY CLASS
X = Intolerable E = ExtremeH = High M = MediumL = Low N = Negligible
21© Shell Global SolutionsP-B-v1.1
RBI CRITICALITY MATRIX (2)
N LL MM
E
H
XEH
HMM
MMLL
LL
N
N
XXEHLL3
2
1
4
PRO
BABI
LITY
CLA
SS
MULTIPLEFATALITIES
EXTENSIVEDAMAGE >10M
SLIGHT INJURY
SLIGHT DAMAGE<10K
SLIGHT EFFECT
MINOR INJURY
MINOR DAMAGE10-100K
MINOR EFFECT
MAJOR INJURY
LOCAL DAMAGE0.1-1M
LOCAL EFFECT
SINGLE FATALITY
MAJOR DAMAGE1-10M
MAJOR EFFECT MASSIVE EFFECT
HEALTH & SAFETY
ECONOMICS (USD)
ENVIRONMENTCON
SEQ
UEN
CECA
TEG
ORY
CONSEQUENCE CLASS NEGLIGIBLE1
LOW2
MEDIUM3
HIGH4
EXTREME5
NEGLIGIBLE
LOW
MEDIUM
HIGH
SUSCEPTIBILITY TO FAILURE RRM CRITICALITY CLASS
NORMAL DESIGN CASE
NEGLIGIBLE OR LOW SUSCEPTIBILITY TO FAILURE
NOTE: Medium or High StF can occure.g. as a result of changed operating conditions
22© Shell Global SolutionsP-B-v1.1
Shell Global Solutions
SUSCEPTIBILITY TO FAILURE ASSESSMENT
23© Shell Global SolutionsP-B-v1.1
SUSCEPTIBILITY TO FAILURE (STF) (1)
• Determine potential degradation mechanisms for the Loop.
• For those degradation mechanisms, identify the StF per item.
for each item since there can be differences in temperature etc..
• For each item, analyse the different degradation mechanisms separately since they may result in different failure modes.
Different inspection techniques/intervals may be required.
Monitoring scheme to be indicated for non-age realateddegradations.
24© Shell Global SolutionsP-B-v1.1
SUSCEPTIBILITY TO FAILURE (STF) (2)
• The failure mode will influence the Consequence of Failure and therefore the Criticality.
The “item criticality” will be the highest rating of all failuremodes.
25© Shell Global SolutionsP-B-v1.1
SUSCEPTIBILITY TO FAILURE (STF) (3)
• AGE RELATED DEGRADATIONStime factor (very) important in relation to degradationdegradations can be foreseen/predicted and controlled
– general corrosion (thinning)– creep
part of normal design criteria, basis for “design life”
• NON-AGE RELATED DEGRADATIONStime factor not important in relation to degradationdegradations can be fast often related to plant upsets
– e.g. stress corrosion cracking due to Cl or caustic– brittle failure ⇒ not acceptable, not in normal designs;
special precautions/controls needed
26© Shell Global SolutionsP-B-v1.1
FAILURE MODES
Time
Time
Tim
AGE-RELATED NON-AGE-RELATED
4
5
6
1
2
3
Time
Time
Time
Time
Time
PoF
PoF
PoF
PoF
PoF
PoF
⇒ internal/external corrosion⇒ creep
Random failures
Failures are mostlyrandom with only afew early-life failures
More failures occurshortly after installation,repair or overhaul
Time
PoF
?
SCC due to a Process upset
27© Shell Global SolutionsP-B-v1.1
SUSCEPTIBILITY OF FAILURESUSCEPTIBILITY OF FAILURE
DEGRADATION MODULESDEGRADATION MODULES
failure characteristic:non age-related
THINNING
- CRACKING- H-ATTACK- MECHANICALCREEP
determinefailure characteristic
failure characteristic:age-related
determine susceptibilitybased on the ratio:
actual corrosion rate/design corrosion rate
determine Susceptibilitybased on
API Technical ModulesFitness for Service study
determine susceptibilitybased on the
operating conditions
28© Shell Global SolutionsP-B-v1.1
StF - AGE-RELATED DEGRADATIONS1 Internal Corrosion The actual corrosion rate is very high (e.g. > 4 × CRd) H
General and/or localised The actual corrosion rate is high (e.g. 1 - 4 × CRd) M
The actual corrosion rate is acceptable/low (e.g. 0.5 - 1.0 × CRd) L
The actual corrosion rate is very low (e.g. < 0.5 × CRd) N
2 External Corrosion Severe external corrosion ( e.g. 60 -120 °C with high humidity and/orspray, condense, cycling conditions, damaged insulation)
H
Corrosion underinsulation
Serious external corrosion , (e.g. -5 to 60 °C or 120 - 150 °C andhumid climate, damaged insulation)
M
Minor external corrosion under normal operating conditions(0.05mm/yr) L
No foreseeable external corrosion (not insulated or >150 °C) N
3 Creep Operation in the creep range, risk of major upsets which must bequantified in terms of remnant life
H
Operation in the creep range, risk of minor upsets which must bequantified in terms of remnant life
M
Operation in the creep range at or below design conditions L
No foreseeable operation in the creep range N
29© Shell Global SolutionsP-B-v1.1
SUSCEPTIBILITY TO FAILURE INTERNAL CORROSIONgeneral & localized corrosion
0.5 - 1 x design CR
< 0.5 x design CR
Corrosion Rating for Susceptibility to Failure
RRM MATRIX
H igh
M edium
L ow
N egligible
> 4 x design CR
>1 - 4 x design CR
30© Shell Global SolutionsP-B-v1.1
StF - NON AGE-RELATED DEGRADATIONS (1)
4 Fatigue - Thermal Cyclic temperature range or delta T of two process streams greater than 250 °C H
Cyclic temperature range or delta T of two process streams between 150 and 250 °C
M
Cyclic temperature range or delta T of two process streams between 100 and 150 °C
L
All other lines or equipment N
5 Fatigue - Vibrations Vibrating in zone 1, or nominal pipe diameter less than 50 mm and in zone 2 and 3
H
Vibrating in zone 2, or nominal pipe diameter between 50 and 100 mm and in zone3
M
Vibrating in zone 3 L
No foreseeable fatigue due to vibration (zone 4 or no vibrations N
6 Stress Corrosion Cracking High susceptibility H
External or internal Medium susceptibility M
Low susceptibility L
Not susceptible N
31© Shell Global SolutionsP-B-v1.1
CAUSTIC CRACKING MODULEAPI 581 and degradation library
Start
Plot Point on NACECaustic SodaService Graph
Medium Susceptibility
Yes
No
No
Yes
Yes
Yes
No
TemperatureNaOHConcentration
Heattraced?
No
Medium Susceptibility
Not Susceptible
Yes
Steamedout?
No
Heattraced?
No
Not Susceptible
Yes
Yes
High SusceptibilityNo
H
NaOHconc<5%wt?
Plots inArea “A”?
StressRelieved?
NaOHconc<5%wt?
Steamedout?
Yes
No
M
ML
Low Susceptibility
N
32© Shell Global SolutionsP-B-v1.1
StF - NON AGE-RELATED DEGRADATIONS (2)
NAR 7 Low Temp. Embrittlement Operating or upsets outside the limits of DEP 30.10.02.31Gen.
H
(No cat. M)
Operating or upsets within the limits of DEP 30.10.02.31Gen.
L
Not susceptible under any foreseeable conditions N
NAR 8 High Temp. Embrittlement Operating in the embrittlement range and no S/Dprecautions
H
Design or upsets in the embrittlement range and no S/Dprecautions
M
Design and operation below the embrittlement range or S/Dprecautions
L
Not susceptible under any foreseeable conditions N
33© Shell Global SolutionsP-B-v1.1
StF - NON AGE-RELATED DEGRADATIONS (3)
NAR 9 High TemperatureHydrogen Attack
Operating/upset conditions above the Nelson curve limit(API 941)
H
Operating conditions between the Nelson curve limitand 20 °C below (API 941)
M
Operating conditions are 20 - 50 °C belowthe Nelson curve limit (API 941)
L
Operating conditions are > 50 °C below the Nelson curvelimit (API 941) or Material is not susceptibleunder any foreseeable conditions
N
NAR 10 Erosion Flow velocity is much higher than design and/or much largeramounts of solids/droplets present
H
(non protected system) Flow velocity is higher than design, and/or solids/dropletshigher than design
M
Flow velocity is per design or less, solids/droplets loading asper design or less
L
No foreseeable occurrence of erosion N
34© Shell Global SolutionsP-B-v1.1
StF - DEGRADATION MODULESfor further information
• Based on the API BRD 581 Technical Modules
modified where required to reflect SIOP experience
• 15 Modules available for all major degradation mechanisms (and more under development)
general corrosion – acids– water– etc.
CUI, H2S, H2 attack, SCC, etc.
35© Shell Global SolutionsP-B-v1.1
Shell Global Solutions
CONSEQUENCE OF FAILURE (CoF) ASSESSMENT
36© Shell Global SolutionsP-B-v1.1
CONSEQUENCE OF FAILURE ASSESSMENT
• PURPOSE IS TO ESTIMATE CONSEQUENCE CLASS (1 OUT OF 5)
• THREE LEVELS OF ASSESSMENT ARE AVAILABLE
1 Direct selection (using Risk Assessment Matrix - RAM)
2 “Simple” questionnaire using RAM descriptions,but split over important aspects of each category
3 “Detailed” questionnaire, using relevant processand equipment data
• USE TOP-DOWN APPROACH
Use 3 to set the levels for the loop, for main items
37© Shell Global SolutionsP-B-v1.1
DIRECT ASSESSMENT OFCONSEQUENCE OF FAILURE
>10 M$SUBSTANTIAL/TOTAL LOSS OF
OPERATION
MULTIPLEFATALITIES
MASSIVE EFFECTSEVERE DAMAGE
NUISANCE INLARGE AREA
1 - 10 M$PARTIAL
OPERATIONLOSS (2 WEEKS)
SINGLE FATALITYINCLUDING
PERMANENT TOTAL DISABILITY
MAJOR EFFECTEXTENSIVE
RESTAURATIONREQUIRED
0.1 - 1 M$PARTIAL
SHUTDOWNCAN BE RESTARTED
MAJOR INJURYINCLUDINGPERMANENT
PARTIAL DISABILITY
LOCALISED EFFECTAFFECTING
NEIGHBOURHOOD
10 - 100 k$BRIEF DISRUPTION
MINOR INJURYLOST TIMEINCLUDED
MAXIMUM 1 WEEK
MINOR EFFECTCONTAMINATION,NO PERMANENT
EFFECT
<10 k$NO DISRUPTION
NO/SLIGHT INJURYFIRST AID/MEDICAL
TREATMENT
NO/SLIGHT EFFECTLOCAL DAMAGEWITHIN FENCE
ECONOMICS
HEALTH& SAFETY
ENVIRONMENT
EXTENSIVEHIGHNEGLIGIBLE LOW MEDIUM
MAXIMUM CLASS IS GOVERNING
38© Shell Global SolutionsP-B-v1.1
ECONOMICS
• PRODUCTION LOSS
deferred income (no or downgraded product)
product wasted (flared or spilled)
• REPAIR COSTS
repair/re-install item
fixed contractor costs (lump sum)
• LABOUR
39© Shell Global SolutionsP-B-v1.1
DIRECT ASSESSMENT OFECONOMIC CONSEQUENCES
Class Potential Impact Description
N Slight damage< 10 kUSD
No disruption to operation
L Minor damage10-100 kUSD
Brief disruption
M Local damage0.1-1 MUSD
Partial shutdown that can berestarted
H Major damage1 - 10 MUSD
Partial operation loss (2 weeksshutdown)
E Extensive damage> 10 MUSD
Substantial or total loss ofoperation
definitions as given in the HSE RAM
40© Shell Global SolutionsP-B-v1.1
ECONOMIC CONSEQUENCESsimple questionnaire
1
2
3
6
COSTELEMENT
Production loss k
Repair costs k
Labour k
Total k
Economic consequence class: N
41© Shell Global SolutionsP-B-v1.1
PRODUCTION LOSS EQUATIONProduction lossesDown time 6 hr = 100 kUSD
Reduced throughput 5 hr @ 20 % = 50 kUSD
Miscellaneous = 30 kUSD
Total production losses 180 kUSD
Repair costsMaterials / Equipment = 10 kUSD
Fixed contractor costs = 4 kUSD
Miscellaneous = 0 kUSD
Total repair costs 14 kUSD
LabourCraftsmen 5 hr = 300 USD
Operator 4 min = 7.2 USD
Staff 1 hr = 80 USD
Contractor 2 hr = 100 USD
Total labour 0.487 kUSD
Total economic consequence 194.487 kUSD
Economic consequence class M
42© Shell Global SolutionsP-B-v1.1
STAGGERED PRODUCTION LOSS EQUITION
0
20
40
60
80
100
0 5 10 15Time [h]
Loss
[kU
SD]
PLE example:0 - 2 h: 2 kUSD/h2 - 8 h: 4 kUSD/h> 8h : 8 kUSD/h
t1 t2
22
88
In software 2 and 8 should be entered asthe inputs with the loss value up to that limit
5 periodscan bedefined
43© Shell Global SolutionsP-B-v1.1
HEALTH AND SAFETY• Three health and safety effects are considered:
1 Thermal effect (fire) 2 Blast and fragment (explosion)3 Toxic effect
– which can be reduced by mitigation
• Maximum of three minus mitigation is overallHealth and Safety class
• “Simple” questionnaire connects the degree of hazard toHealth and Safety descriptions
e.g. medium fire which could cause minor injuries
44© Shell Global SolutionsP-B-v1.1
HSE RAM DEFINITIONSTable 3-2 Health/Safety consequence definitions as given in the HSE RAMdocument
Class Potential Impact Description
N No/Slight injury First aid case and medical treatment case. Not affectingwork performance or causing disability.
L Minor injury Lost time injury. Affecting work performance, such asrestriction to activities or a need to take a few days to fullyrecover (maximum one week).
M Major injury Including permanent partial disability. Affecting workperformance in the longer term, such as prolonged absencefrom work. Irreversible health damage without loss of life,e.g. noise induced hearing loss, chronic back injuries.
H Single fatality Also includes the possibility of multiple fatalities (maximum3) in close succession due to the incident, e.g. explosion.
E Multiple fatalities May include 4 fatalities in close succession due to theincident, or multiple fatalities (4 or more) each at differentpoints and/or with different activities.
45© Shell Global SolutionsP-B-v1.1
HEALTH & SAFETYsimple questionnaire (1)
CONSEQUENCECLASS
CONSEQUENCE DESCRIPTION
FIREFailure mode leads to:
1 N No fire or fire which could only cause slight injuries (no LTI)2 L Fire which could cause minor injuries (LTI)3 M Fire which could cause major injuries (LTI> 1 week and/or partial disability)4 H Fire causing up to a single fatality or permanent total disability
EXPLOSIONFailure mode leads to:
1 N No explosion but just a flash fire which could only cause slight injuries (first aid)2 L No explosion but a flash fire which could cause minor injuries (LTI)3 M Explosion or flash fire which could cause major injuries (LTI>1week and/or
partial disability)4 H Explosion or flash fire which could cause a single fatality or permanent total
disability5 E Explosion which could cause multiple fatalities
46© Shell Global SolutionsP-B-v1.1
HEALTH & SAFETYsimple questionnaire (2)
CONSEQUENCECLASS
CONSEQUENCE DESCRIPTION
TOXICFailure mode leads to:
1 N No or very small toxic release which could cause only slight injuries (first aid)2 L Small toxic release which could cause minor injuries (LTI)3 M Medium toxic release which could cause major injuries (LTI>1week and/or
partial disability)4 H Large toxic release which could cause a single fatality or permanent total
di bilit5 E Very large toxic release which could cause multiple fatalities
MITIGATIONExposure near failure location and possibility to avert danger of hazardousevent could reduce possible H/S consequence class by:
0 No means or only marginally-1 One class-2 Two classes
47© Shell Global SolutionsP-B-v1.1
HEALTH & SAFETYdetailed questionnaire
Table 3-4 Common consequence matrix
4 N H E E
quantity 3 N M H E
2 N L M H
1 N N L M
1 2 3 4
property
flammability
quantityreleased
For fires
Consequenceof FailureNegligible toExtreme
48© Shell Global SolutionsP-B-v1.1
HEALTH AND SAFETYfire• Two parameters are used to estimate fire consequence:
Flammability
– NFPA (National Fire Protection Association) flammability index, 0 ≤ Nf ≤ 4 and temperature
Released quantity (instantaneous/per hour/inventory)
– three levels: < 500 kg, 0.5 - 5 ton, and > 5 ton
• Matrix to determine fire class (Max H)
49© Shell Global SolutionsP-B-v1.1
FIREdetailed H & S questionnaire
Nf Products
0 Sulphur Diox ide, SodiumChloride
1 Sulphur, Am m onia
2 Diesel Fuel, Fuel O il 1 to 6
3 Gasoline, Naphtha, EthylAlcohol, Petroleum Crude
4 Hydrogen, Methane,Hydrogen Sulphide
Table 3-6 Fire safety questionnaire
Flammability
1 Not flammable (Nf < 2) or lowflammability (Nf >1 and Tproduct < Tflash)
2 Medium flammability(Nf > 1 and Tflash < Tproduct < Tauto ign)
3 High flammability(Nf > 1 and Tproduct > Tauto ign)
Released quantity(instantaneous or per hour or inventory)
1 < 500 kg
2 0.5-5 ton
3 > 5 ton
released 3 N M H
quantity 2 N L M
1 N N L
1 2 3
flammability
50© Shell Global SolutionsP-B-v1.1
RELEASE OF LIQUID THROUGH A HOLE
1
10
1 10 100pressure [barg]
hole
dia
met
er [m
m]
505005000
5 mm
advised as theaverage case, results
in released Q=2
kg/h
51© Shell Global SolutionsP-B-v1.1
HEALTH AND SAFETYexplosions
TWO EXPLOSION/IMPACT RISKS ARE CONSIDERED:1 Vapour Cloud Explosions (VCE)
VCE possibility (flammable cloud and congested area)released vapour mass (instantaneous, per hour)matrix to determine VCE class
2 Other impact/high pressure riskshigh pressure equipmentfailure causing flying debris
⇒ MAXIMUM OF THE TWO IS EXPLOSION CLASS (MAX E)
52© Shell Global SolutionsP-B-v1.1
EXPLOSIONdetailed H & S questionnaire Table 3-7 VCE consequence questionnaire
VCE possibility
1 None; no release of anexplosive cloud
2 Low; release of an explosivecloud in an open area
3 Medium; release of an explosivecloud in a medium congestedarea (some obstacles present)
4 High; release of an explosivecloud in a heavily congestedarea (many obstacles present)
Released vapour mass(instantaneous or per hour)
1 < 50 kg
2 50 - 500 kg
3 0.5 - 5 ton
4 > 5 ton
released 4 N H E E
vapour 3 N M H E
mass 2 N L M H
1 N N L M
1 2 3 4
VCE possibility
53© Shell Global SolutionsP-B-v1.1
RELEASE OF GASthrough a 3 mm hole C1-C2 and H2
10
100
1000
0 50 100 150 200 250Pressure [bara]
Rel
ease
rate
[kg/
h]
C1-C2 (@ 50 C)H2 (@ 50 C)
54© Shell Global SolutionsP-B-v1.1
RELEASE OF LPG THROUGH A 3 MM HOLE
0
500
1000
1500
2000
2500
0 50 100 150 200 250Pressure [bara]
Rel
ease
d qu
antit
y [k
g/h]
C3 @ 50 CC3 @ 100 CC4 @ 50 CC4 @ 100 C
55© Shell Global SolutionsP-B-v1.1
EXPLOSION & HPdetailed H & S questionnaire
Table 3-8 Other explosion and high pressure equipment consequence questionnaire
N no gas present or p*V<5 bar m3
L gas present and 5 ≤ p*V ≤ 50 bar m3
M gas present and 50 < p*V < 500 bar m3
H gas present and p*V>500 bar m3 or failure causing some flying debris (solid particles)
E failure causing major flying debris (solid particles)
56© Shell Global SolutionsP-B-v1.1
HIGH PRESSURE CONSEQUENCE OF GAS PIPES
0.1
1
10
1 10 100pressure [barg]
pipe
dia
met
er [m
]
550500
P x Vbar m3
57© Shell Global SolutionsP-B-v1.1
HEALTH AND SAFETYtoxic effects
TWO PARAMETERS DETERMINE TOXIC CONSEQUENCE:Toxicity
– NFPA “health” index, 0 ≤ Nh ≤ 4 Concentration
– four levels: < 1000 ppm, …, > 10%
⇒ MATRIX TO DETERMINE TOXIC CLASS (MAX E)
58© Shell Global SolutionsP-B-v1.1
Table 3-9 Toxicity index, Nh, examples
Nh Products
0 Diesel
1 Butane, Gasoline
2 CO, benzene,Ethylene Oxide
3 H2S, chlorine, Ammonia,Sulphuric Acid, Phenol
4 Hydrogen Fluoride (HF),Hydrogen Cyanide
Table 3-10 Toxic consequence questionnaire
Toxicity
1 Not toxic (Nh≤1) or low toxicity(Nh≤3 and conc. < 100 ppm).
2 Medium toxicity (Nh=2)
3 High toxicity (Nh=3)
4 Extreme toxicity (Nh>3)
4 N H E E
Concentration (in ppm or % volume) Concentration 3 N M H E
1 < 1000 ppm 2 N L M H
2 < 10 000 ppm (or < 1%) 1 N N L M
3 1-10 % 1 2 3 4
4 > 10 % Toxicity
TOXIC RELEASESdetailed H & S questionnaire
59© Shell Global SolutionsP-B-v1.1
HEALTH AND SAFETYmitigation
TWO FACTORS DETERMINE MITIGATION:
1 Exposure
Frequency of and exposure time in hazardous zone
2 Possibility to avert the hazardous situation
Depends on: rate of development, ease of recognition, avoidance of exposure, use of ppe, experience.
⇒ MATRIX TO DETERMINE OVERALL REDUCTION(0, 1 or 2 classes)
60© Shell Global SolutionsP-B-v1.1
MITIGATIONdetailed H & S questionnaire
Possibility 3 -1 0 0
to avert 2 -1 -1 0
danger 1 -2 -1 -1
1 2 3
Exposure
Table 3-11 Mitigation questionnaire
Exposure
1 Very rare(less than 10 man-minutes per day)
2 Occasionally(less than 6 man-hours per day)
3 Frequently to continuously(more than 6 man-hours per day)
Possibility to avert danger
1 In almost all circumstances
2 In some circumstances(more than 25% of cases)
3 Not (or hardly possible)
61© Shell Global SolutionsP-B-v1.1
ENVIRONMENT
TWO EFFECTS ARE CONSIDERED:
1 Liquid spills (max E)toxicityReleased quantity (or inventory)location (within / outside fence)surface (possibility to reach surface and/or ground water
2 Gas emissions (max M)Type (volume and how harmful)Effects (complaints)
⇒ MAXIMUM OF TWO IS ENVIRONMENT CLASS
62© Shell Global SolutionsP-B-v1.1
ENVIRONMENTALsimple questionnaire
Table 3-13 Simple environment questionnaire
Severityrating
Consequence description
Liquid spillsFailure mode leads to a liquid spill with:
1 N No or negligible environmental damage2 L Minor environmental damage3 M Localised environmental damage4 H Major environmental damage5 E Massive environmental damage
Gas emissionFailure mode leads to:
1 N No or small harmful release2 L Small harmful release leading to many complaints or large3 M Large harmful release leading to many complaints
63© Shell Global SolutionsP-B-v1.1
ENVIRONMENTALdetailed questionnaire
Table 3-14 Liquid spills questionnaire
Environmental toxicity
1 Not harmful to environment (e.g.water)
2 Harmful but not toxic(e.g. most alkanes)
3 Harmful and toxic(e.g. drins)
4 N H E
Released quantity ( or inventory) 3 N M H
1 < 500 kg Quantity 2 N L M
2 0.5 - 5 ton 1 N N L
3 5 - 50 ton 1 2 3
4 > 50 ton Toxicity
Location0 Contamination remains inside fence1 (Part of) contamination is outside fence
Surface of spill0 No chance that spilled liquids will reach
outside fence surface or ground water1 There is a possibility that spilled liquids will
reach outside fence surface or ground water
64© Shell Global SolutionsP-B-v1.1
ENVIRONMENTALdetailed questionnaire
Table 3-15 Gas emission questionnaire
Type of release3 large (> 1000 normal m3 ) and harmful2 small and harmful1 other
Effect1 No or few complaints2 Many complaints or is to be reported to the Authorities.
Type of 3 L MRelease 2 N L
1 N N
1 2Effect
65© Shell Global SolutionsP-B-v1.1
DETERMINATION OF THECONSEQUENCE OF FAILURE - Summary
• DIRECT
• SIMPLE QUESTIONNAIRE
compliant with HSE descriptions
• DETAILED QUESTIONNAIRE
provide guidance and consistency
useful if limited HSE experience is available
mechanistic ⇒ keep thinking
seek specialist advice in cases of doubt or high criticality
66© Shell Global SolutionsP-B-v1.1
DETERMINE INSPECTION SCOPEDETERMINE FAILURE
CHARACTERISTIC
FAILURE CHARACTERISTIC:
AGE-RELATEDFAILURE CHARACTERISTIC:
NON AGE-RELATED
- CRACKING- H-ATTACK
- MECHANICALCREEP
MONITORING= TABLE
MAX. INSP. INTERVAL= RL X INTERVAL FACTOR
Determine Susceptibilitybased on the ratio: Actual corrosion
rate/design corrosion rate
Determine Susceptibilitybased on API Technical
Modules Fitness for Service study
Determine Susceptibilitybased on the
operating conditions
THINNING StFHMLN
CoFEHMLN
CRITICALITY
CONFIDENCERATING
ADVISED METHODS AS PER DEGRADATION MODULE,EXTENT PER CRITICALITY LEVEL
ADVISED MONITORING BASED ON DEGRADATION MODULE,EXTENT PER CRITICALITY LEVEL
67© Shell Global SolutionsP-B-v1.1
CONFIDENCE RATING
• INDICATOR FOR CONFIDENCE IN FORECAST OF DEGRADATION
• RATING - very low to very high – REFLECTS:stability/predictability of degradationnumber and quality of previous inspectionsprocess stability
⇒ BETTER CONFIDENCE YIELDS LONGER INSPECTION INTERVALS
68© Shell Global SolutionsP-B-v1.1
CALCULATION OF INSPECTION INTERVALfor age-related degradations
consequence of failure(questionnaire)
susceptibility tofailure (questionnaire)
- inspection records- experience- judgement
matrix
CONFIDENCERATING
matrix
CRITICALITY
corrosion allowancecorrosion rate
REMNANT LIFE Xmultiply
INTERVAL FACTOR
MAXIMUM INSPECTIONINTERVAL (in years)
MAXIMUM INSPECTIONINTERVAL (in years)
69© Shell Global SolutionsP-B-v1.1
AGE-RELATED DEGRADATION - inspection interval factor function of Criticality and Confidence Rating
Criticality Interval FactorE 0.2H 0.3M 0.4L 0.5N 0.6
Confidence Rating Adjustment factorVH - Very high + 0.2H - High + 0.1M - Medium 0L - Low -0.1VL - Very Low -0.2
Description ScoreYES Int. NO
Degradation mechanism is stable and properly controlled + 0.1 0 -0.1Multiple reliable inspections have been carried out + 0.1 0 -0.1Relevant process parameters are reliably monitored + 0.1 0 0
Inspection Interval Factor forMedium Confidence Rating
add orsubtract
add/subtractto/fromMEDIUMSCORE
Adjustment of interval factorbased on Confidence Rating
Scoring points for adjustment factor withmedium confidence as starting point. Maximum adjustment +/- 0.2
70© Shell Global SolutionsP-B-v1.1
INTERVAL FACTORSfor age-related degradations
CONFIDENCE RATING
CRITICALITY Very Low Low Medium High Very High
E
H
M
L
N (review only)
0 0.1 0.2 0.3 0.4
0.1 0.2 0.3 0.4 0.5
0.2 0.3 0.4 0.5 0.6
0.3 0.4 0.5 0.6 0.7
0.4 0.5 0.6 0.7 0.8
71© Shell Global SolutionsP-B-v1.1
MAXIMUM INSPECTION INTERVAL
XX
LIFETIME IN YEARS
INSPECTIONS
X
WALLTHICKNESS
MINIMUM ALLOWABLE THICKNESSt (min)
t new REMNANT LIFE
MAXIMUM INSPECTIONINTERVAL
72© Shell Global SolutionsP-B-v1.1
INSPECTION COVERAGE (PERCENTAGE)age-related degradation
CONFIDENCE RATINGCRITICALITY VERY LOW LOW MEDIUM HIGH VERY HIGH
REDESIGNINTOLERABLE80-100%EXTREME
25-100%HIGH5-25%MEDIUM
5-25%LOWNEGLIGIBLE 0-5%
SELECTION OF PROPER NDT-TECHNIQUEVIA SHELL NDT HANDBOOK
73© Shell Global SolutionsP-B-v1.1
MONITORING SCHEMEfor non age-related degradations
consequence of failure(questionnaire)
susceptibilityto failure (questionnaire)
ACCEPTABLE?
IMPLEMENTMONITORING– PROCESS
MONITORING– OPPORTUNITY
INSPECTIONS
YESmatrix
NOREDESIGN– PROCES DESIGN– MECHANICAL DESIGN
matrix
CONFIDENCERATINGCRITICALITY
74© Shell Global SolutionsP-B-v1.1
N LL MM
E
H
XEH
HMM
MMLL
LL
N
N
XXEHLL3
2
1
4
PRO
BABI
LITY
CLA
SS
MULTIPLEFATALITIES
EXT. DAMAGE>10M
SLIGHT INJURY
SLIGHT DAMAGE<10K
SLIGHTEFFECT
MINOR INJURY
MINOR DAMAGE10-100K
MINOREFFECT
MAYOR INJURY
LOCAL DAMAGE0.1-1M
LOCALISEDEFFECT
SINGLE FATALITY
MAYOR DAMAGE1-10M
MAYOREFFECT
MASSIVEEFFECT
HEALTH & SAFETY
ECONOMICS (USD)
ENVIRONMENTCON
SEQ
UEN
CECA
TEG
ORY
CONSEQUENCE CLASS NEGLIGIBLE1
LOW2
MEDIUM3
HIGH4
EXTREME5
NEGL.
LOW
MEDIUM
HIGH
RBIStF RRM CRITICALITY CLASSRRM CRITICALITY CLASSIPF
DR
> 20 y
4 - 20 y
0.5 - 4 y
0 - 0.5 y
RCMETBF
> 20 y
4 - 20 y
0.5 - 4 y
0 - 0.5 y NOT acceptable for non age-relateddegradation mechanismsAdditional
processmonitoringNOT required
RRM CRITICALITY MATRIXfor non age-related degradation
STF (RBI): Susceptibility to FailureDR (IPF): Demand RateETBF (RCM): Estimated Time Between Failures
X = Intolerable E = ExtremeH = High M = MediumL = Low N = Negligible
75© Shell Global SolutionsP-B-v1.1
CONFIDENCE RATING non-age related degradation
Confidence Rating Adjustment factorVH - Very high + 0.2H - High + 0.1M - Medium 0L - Low -0.1VL - Very Low -0.2
Description Score
YES Int. NO
Degradation mechanism can be easily controlled + 0.1 0 - 0.1
Relevant proc. parameters are reliably monitored + 0.1 0 - 0.1
Reliable inspections were carried out + 0.1 0 0
76© Shell Global SolutionsP-B-v1.1
MONITORING AND INSPECTION PLANfor non age-related degradationsMONITORING AND INSPECTION PLANfor non age-related degradations
CONFIDENCE RATINGCRITICALITY VERY LOW LOW MEDIUM HIGH VERY HIGH
NO INSPECTION/PROCESS MONITORING REQUIRED
IMPROVE MONITORING
MONITORING AND OPPORTUNITY INSPECTION
DESIGN AND/OR PROCESS CHANGE REQUIRED
INTOLERABLE
EXTREME
HIGH
MEDIUM
LOWNEGLIGIBLE
77© Shell Global SolutionsP-B-v1.1
PROCESS MONITORINGnon-age related degradations
• Parameters to be monitored, as described in the operating window.
• Frequency to be described/agreed.
• Deviations measured (outside monitoring scheme) shall be discussed in the team and actions reported;changes via Plant Change procedure if needed.
• Revise inspection plans if needed.
78© Shell Global SolutionsP-B-v1.1
INSPECTION/MONITORING TIMING?
• AGE-RELATED DEGRADATIONS - INSPECTIONS
Calculate Remnant Life
Apply Interval Factor: Max. inspection interval
– based on Confidence and Criticality Rating
• NON AGE-RELATED DEGRADATIONS - MONITORING
Apply table to check if monitoring is required/acceptable:
– monitoring scheme (+ opportunity inspections)
Based on Confidence and Criticality Rating
79© Shell Global SolutionsP-B-v1.1
CRITICALITYMATRIX
negligiblecriticality
intolerablecriticality
LOW/MEDIUM/HIGH& EXTREME CRITICALITY
‘no’ inspection rectify
INSPECTION/MONITORING TASKS
INFORMATION FROMDEGRADATIONMODULES OR
NDT HANDBOOK
CONFIDENCE RATING
NON-AGE RELATED DEGRADATIONS
INSPECTION INTERVAL
NON-INTRUSIVE/INTRUSIVE
PROCESS MONITORINGAND OPPORTUNITY INSPECTION
REMNANT LIFE
CONFIDENCE RATING
AGE RELATED DEGRADATIONS
RECTIFY IFREQUIRED
INSPECTION TASKS
80© Shell Global SolutionsP-B-v1.1
Shell Global Solutions
BACK-UPSLIDES
81© Shell Global SolutionsP-B-v1.1
NDT TECHNIQUES - see NDT Handbook• INTERNAL WALL THINNING
internal corrosion UT, RT, MFL, LRUT, PETerosion UT, RT, MFL, LRUT, PETcavitation UT, RT, MFL, LRUT, PETweld corrosion UT, RT
• EXTERNAL WALL THINNINGexternal corrosion VTcorrosion under insulation VT,RT,TT,RTR, PET
• CRACKINGfatigue UT, PT, MT, ET, TOFD, AETstress corrosion cracking UT, PT, MT, ET, TOFD, AETwet hydrogen cracking UT, PT, MT, ET, TOFD, AET
• OTHERcreep DM, R, PT, MT, UThot hydrogen damage MT, R, UThigh temperature embrittlement MT, R, UT
82© Shell Global SolutionsP-B-v1.1
FEEDBACK/REVIEW• VALIDATION AND UPDATING
OF THE PLANT INTEGRITY DATABASE:after each maintenance and inspection shutdownat the implementation of plantchangesat deviations of operating conditions
• YEARLY REVIEW BY RBI-TEAM TO ESTABLISH:actual condition and fitness for purposedegradation mechanism and -rateconfidence rating
• UPDATE INSPECTION PLAN, IF REQUIRED
83© Shell Global SolutionsP-B-v1.1
RBI METHODOLOGY• REVIEW THE OPERATING CONDITIONS OF THE PLANT
past/present/future operating conditionsprocess monitoringmain changes from design
• REVIEW MATERIALS OF CONSTRUCTIONcheck materials vs process conditions
• DEFINE CORROSION LOOPSsimilar process conditions/materials/degradations
• DO THE S-RBI STUDY FOR EACH CORROSION LOOP (following slide)
• INTEGRATE RESULTS IN AN OVERALL WORK-PLANNING
84© Shell Global SolutionsP-B-v1.1
S-RBI STUDY FOR A CORROSION LOOP• Define the Corrosion Loop• Describe process conditions• Establish the “Operating Window”• List Items in the loop
materials and corrosion allowances (design)• Agree Potential Degradation Mechanisms for the loop• Review inspection history - corrosion rates• Give a Confidence Rating for each item and degradation• Do the criticality rating per Degradation Mechanism• Establish remnant life & max. inspection interval OR
monitoring scheme • Define scope of inspections / monitoring
⇒ next stage - DEVELOP DETAILED INSPECTION PLANS
85© Shell Global SolutionsP-B-v1.1
DEGRADATION MECHANISMS
• Internal corrosion (general)Sulphur, TAN, Acids, H2S
• External corrosionCUI, ESCC
• Creep• Stress Corrosion Cracking• Embrittlement• Fatigue - thermal• Fatigue - mechanical• Erosion• Hydrogen attack
AGE - RELATED DEGRADATIONS
NON AGE - RELATED DEGRADATIONS
86© Shell Global SolutionsP-B-v1.1
AGE-RELATED DEGRADATIONS VSNON AGE-RELATED DEGRADATIONS (1)
AGE-RELATED
Deg
rada
tion
Time
87© Shell Global SolutionsP-B-v1.1
AGE-RELATED DEGRADATIONS VSNON AGE-RELATED DEGRADATIONS (2)
AGE-RELATED
NON AGE-RELATEDE.G. SCC
Deg
rada
tion
Time
88© Shell Global SolutionsP-B-v1.1
A
C
B
CAUSTIC SODA SERVICE DIAGRAM
Concentration NaOH, % weight
Tem
pera
ture
(C)
89© Shell Global SolutionsP-B-v1.1
Table S1-2A Environmental Severity - SSC H2S CONTENT OF WATER (mg/kg)
pH of water Cyanide content (mg/kg)
< 50 50 to 1000 > 1000
SEVERITY CATEGORY
< 4.0 (Note 1) Moderate High High
4.0 to 5.4 (Note 1) Low Moderate High
5.5 to 7.5 (Note 1) Low Low Moderate
7.6 to 7.9 < 50 Low Moderate High
7.6 to 7.9 ≥ 50 Moderate High High
≥ 8.0 < 20 Low Moderate High
≥ 8.0 ≥ 20 Moderate High High
NOTE 1. HCN level is not significant at pH 7.5 and below.
SUSCEPTIBILITY TO FAILURE BY SSC
Table S1-3 Susceptibility to SSCAs-welded PWHT
Environmental Max Vickers Hardness(1) Max Vickers Hardness(1)
Severity < 248 248-290 > 290 < 248 248-290 > 290
High Low Medium High Not Low Medium
Moderate Low Medium High Not Not Low
Low Low Low Medium Not Not Not(1) Actually tested as Vickers or converted from portable techniques, e.g. Equotip, Microdur etc.
90© Shell Global SolutionsP-B-v1.1
FATIGUE MONITORING (PROPOSAL)monitoring/inspection interval(s) FATIGUE MONITORING (PROPOSAL)monitoring/inspection interval(s)
NO INSPECTIONS
CONFIDENCE RATINGVERY LOW LOW MEDIUM HIGH VERY HIGHCRITICALITY
EXTREME
HIGH
MEDIUM
LOW
1 DAY 3 DAYS
1 WEEK 1 MONTH
2 MONTHS
NEGLIGIBLE
INTOLERABLE SEE NOTE
NOTE:Where Fatigue could lead to X = INTOLERABLE criticality,a full supporting system shall be designed and maintained;for criticality E, a similar approach is usually followed.
91© Shell Global SolutionsP-B-v1.1
RRM CRITICALITY MATRIX
N LL MM
E
H
XEH
HMM
MMLL
LL
N
N
XXEHLL3
2
1
4
PRO
BABI
LITY
CLA
SS
MULTIPLEFATALITIES
EXT. DAMAGE>10M
SLIGHT INJURY
SLIGHT DAMAGE<10K
SLIGHTEFFECT
MINOR INJURY
MINOR DAMAGE10-100K
MINOREFFECT
MAYOR INJURY
LOCAL DAMAGE0.1-1M
LOCALISEDEFFECT
SINGLE FATALITY
MAYOR DAMAGE1-10M
MAYOREFFECT
MASSIVEEFFECT
HEALTH & SAFETY
ECONOMICS (USD)
ENVIRONMENTCON
SEQ
UEN
CECA
TEG
ORY
CONSEQUENCE CLASS NEGLIGIBLE1
LOW2
MEDIUM3
HIGH4
EXTREME5
NEGL.
LOW
MEDIUM
HIGH
RBIStF RRM CRITICALITY CLASSRRM CRITICALITY CLASSIPF
DR
> 20 y
4 - 20 y
0.5 - 4 y
0 - 0.5 y
RCMETBF
> 20 y
4 - 20 y
0.5 - 4 y
0 - 0.5 y
STF (RBI): Susceptibility to FailureDR (IPF): Demand RateETBF (RCM): Estimated Time Between Failures
X = Intolerable E = ExtremeH = High M = MediumL = Low N = Negligible
92© Shell Global SolutionsP-B-v1.1
0.10
1.00
10.00
100.00
1,000.00
1 10 100 1000
Vibration Frequency, Hz
Vib
ratio
n A
mpl
itude
, mils
pea
k to
pea
k
Danger
Correction
Marginal
Design
Threshold of perception
SEVERITY OF VIBRATIONZONE 1
ZONE 4
23
ALLOWABLE PIPING VIBRATION LEVELS
93© Shell Global SolutionsP-B-v1.1
S-RBI AS PART OF RRMmain changes
• CONSEQUENCE OF FAILURE new questionnaire, identical for S-RBI, S-RCM and IPF
• SUSCEPTIBILITY TO FAILUREnew questionnaire
• AGE AND NON-AGE RELATED DEGRADATIONSdifferent approach
• TECHNICAL MODULESgive guidance to StF ratings
• CONFIDENCE RATING• INTERVAL FACTORS
94© Shell Global SolutionsP-B-v1.1
StF - CORROSION RATESdesign life 20 years
CA 1mm CA 3mm
CR CR
4 H >0.2 >0.6
3 M >0.05 - 0.2 >0.15 - 0.6
2 L 0.02 - 0.05 0.07 - 0.15
1 N <0.02 <0.07
95© Shell Global SolutionsP-B-v1.1
CORROSION ALLOWANCESspecial cases
• STAINLESS STEEL AND ALLOYSno corrosion allowance in designs
– use tolerances, +/–12.5% (FFP can give actual value)– or take an arbitrary small value, e.g. 0.5 mm– also take a worst case CR, e.g. 0.01 mm/yr– that results in 50 years initial lifetime
• HEAT EXCHANGER TUBESwall thickness is CA50% for inside, 50% for outside, if leaks are acceptedsometimes users want e.g. 0.5 mm minimum for pressure containment.higher minimum thickness can be agreed.
96© Shell Global SolutionsP-B-v1.1
HEAT EXCHANGER DEFINITIONS
Shell side Tube side
Shell (Sh)
Tube outside (To)
Head (He)
Tubeinside(Ti)
97© Shell Global SolutionsP-B-v1.1
SUB TAGS & TAG GROUPS
SUB - TAGS
C-20124”P10023117X
4” P1005 3117Y
“WET PIPING”tags P1002, P1003
16” P1004 3117YC-201 TOP
“DRY OH PIPING”Tags P1004, P1005, P1006
TAG GROUPSC-201 Bottom
12” P1003 3117X
98© Shell Global SolutionsP-B-v1.1
FAILURE
• TERMINATION OF THE ABILITY OFAN ITEM TO PERFORM A REQUIRED FUNCTION:
corrosion allowance lost(after FFP) below minimum required thicknessleak to outside (or internal)crack detected (beyond tolerable)deformation (beyond tolerable)extreme case: rupture
– brittle or ductile
• NORMAL DESIGNS - “LEAK BEFORE BREAK”:warns and allows to avoid hazards
99© Shell Global SolutionsP-B-v1.1
PLANTSrisk and reliability - mechanical
PLANT DEGRADATIONS INSPECTION MAINTENANCE
visualultrasonicX-rayinfraredmagnetic part.dye penetranteddy current
pHtemperaturechloride level
corrosion- general- pitting- Stress CCmechanical- fracture- fatigue- etc.
repairreplace
preventiveorbreak down
timing ofinspection/monitoring tasks
processconditions
+
DESIGNPER CODEpressure/
temperature
materials
100© Shell Global SolutionsP-B-v1.1
FAILURE CLASSIFICATION
CORROSION STRESS
SURFACE GRANULARINTER/TRANS
LOCALISEDCORROSION
GENERALCORROSION
NON-FLUCTUATING FLUCTUATING
OVERLOAD TEMPERATUREEFFECTS
BRITTLEFRACTURE
LOW HIGH
CREEPRUPTURE
THERMALFATIGUE
DUCTILEFRACTURE
THERMAL
MECHANICAL
HYDRAULIC
CAVITATIONerosion
FATIGUEWEAR
CORROSIONFATIGUE
STRESSCORROSIONCRACKING
HYDROGENEMBRITTLEMENT
OGBR MHR
- pitting- crevice- galvanic- fretting- velocity
(erosion)
101© Shell Global SolutionsP-B-v1.1
S-RBI RELATED TOOLS
Maintenanceand Inspection
Database
Electronic Drawings(VISIO)
TrendingSoftware
S-RBI ANALYSIS
S-RBI (RRM)Software
S-RBI (RRM)Manual
MEP/Corrosion ControlManual
Statistical Recipe Book
DegradationLibrary
NDTHandbook
FFPHandbook
102© Shell Global SolutionsP-B-v1.1
S-RBI IN COMPARISON WITH API STANDARDS (1) API 510 Pressure Vessel Inspection codeAPI 570 Piping Inspection codeAPI RP 580 Risk Based Inspection DRAFT
S-RBI FULLY IN LINE WITH API REQUIREMENTS
• involve various part of organisation• incorporate likelihood and consequence of failure• include HSE consequences• assess all potential degradation mechanisms• evaluate effectiveness of inspection methods• re-assessment after process change• consider design relative to operating conditions• RBI assessment should be properly documented
103© Shell Global SolutionsP-B-v1.1
S-RBI IN COMPARISON WITH API STANDARDS (2)
ADDITIONAL ADVANTAGES OF S-RBI• team effort is pre-requisite• approach is very practical, easy to apply and transparent• auditable consideration to assure integrity and define inspection plan• corrosion loop concept streamlines the analysis and adds clarity• linked to Corrosion Control Manual• definition of (integrity) operating window• comprehensive but concise report• enhanced synergy of S-RBI with S-RCM and IPF under RRM• S-RBI based on long lasting experience and applied within Shell
worldwide
104© Shell Global SolutionsP-B-v1.1
WALL THICKNESS UT MEASUREMENTS
POOR QUALITY+/– 1 mm
GOOD QUALITY+/– 0.5 mm
109 11
High quality UT measurements canobtain +/– 0.3 mm
109 11
105© Shell Global SolutionsP-B-v1.1
DEFECT SIZES UPON FAILURE• Standard hole size 3 mm for gas and 3 - 5 mm for liquids for
normal degradations leading to pitting and small holes;these sizes are detected rather quickly and precautionswill be in hand if sizes are larger:
– depressurization– evacuation– firefighting etc.
• A 1 inch hole for degradations leading to large area thinning, e.g. ammonium chloride salt attack.
• Ruptures are considered if embrittlement is encountered or large scale Stress Corrosion Cracking could occur.
• Local standards/philosophies can overrule these sizes.
106© Shell Global SolutionsP-B-v1.1
TAG NUMBERS
ADVISED DETAILS:
• PIPING (max 25 characters)sizeline code 8 PL1010 CS HI INSPmaterialinsulation codeauthority code (if applicable)
• EQUIPMENTTAG numberinsulation code V-1101 CI INSPauthority code E-302 TS Ti HI INSP
107© Shell Global SolutionsP-B-v1.1
STANDARDIZED CORROSION RATES (CR)CARBON STEEL • If no corrosion detected after about 10 years:
Assume detection limit of 0.5 mm, corrosion rate must be lower than 0.05 mm/yrUse this value as worst case CR until better information is available
STAINLESS STEEL• If no corrosion detected after about 10 years
Assume detection limit of 0.1 mm, corrosion rate must be lower than 0.01 mm/yr (after VT) or 0.03 mm/yr (if UT, good quality)Use this value as worst case CR until better information is available
108© Shell Global SolutionsP-B-v1.1
STRESS CORROSION CRACKING
START
Is the material ofconstruction austenitic
stainless steel?
Determine theseverity index for
each potentialmechanism
Have youdetected SCC in this
or similar serviceequipment?
Do you know thecause of SCC?
Increase thesusceptibility for
that mechanism tohigh
Increase susceptibilityfor all potential
mechanisms to high
No problem
No
Determine maximumseverity index
Is the material ofconstruction carbon or
low alloy steel?
Yes
No
NoYesYes Yes
Screen for Caustic, Amine,SSC, HIC/SOHIC,
Carbonate Cracking
Screen for PTA,Cl-SCC
No
Determine susceptibility foreach potential SCC
mechanism for austeniticStainless Steels
Determine susceptibilityfor each potential SCC
mechanism for Carbon andLow Alloy steels
109© Shell Global SolutionsP-B-v1.1
MAXIMUM INSPECTION INTERVAL
X
MIN. ALLOWABLE THICKNESSt(min)
t new
LIFETIME IN YEARS
Inspections
X
NLMH
20
40
< 5 ~ 5 -10
N to H CriticalityVL to VH Confidence0.1 - 0.8 Int. Factor
L to E (X) CriticalityVL to VH Confidence0.0 - 0.7 Int. Factor
StF
thic
knes
s
design life
110© Shell Global SolutionsP-B-v1.1
EFFECT OF MONITORING/INSPECTION AND/OR MITIGATIONEFFECT OF MONITORING/INSPECTION AND/OR MITIGATION
REMAINING RISK = CRITICALITY - “PREVENTIVE MEASURES”
Prob
abili
ty
LOW RISK
HIGH RISK
Criticality
monitoring/inspectioneffect
Define inspection tasksto get lowest possible riskConsequence
111© Shell Global SolutionsP-B-v1.1
“REMAINING” RISK TO BEAS LOW AS REASONABLY POSSIBLE (ALARP)
Prob
abili
ty
LOW RISK
Criticality
HIGH RISK
(ALARP)
1. Inspection interval and coverage- based on Criticality andConfidence Rating
2. Type of Inspection(s)- based on failure mode(s)
3. Location(s) to inspect- for each failure mode
4. Process Monitoring- where applicable (operating window)
Consequence
112© Shell Global SolutionsP-B-v1.1
FAILURE MODE & CONSEQUENCES
Consequence of Failureworst case & if flammable contents
Typical defect:w
Degradationw
Failure modew
Pitting Small leak Leak, no significant damage Hole, 3-5 mm dia Small fire System Inventory(Big fire or explosion)
Embrittlement Fracture Big fire or explosion System Inventory
Caustic cracking Cracks Leaks Hole, 3-5 mm dia SCC
General corrosion Leak Fire, small explosion Hole, 3-5 mm dia Rupture Big fire or explosion System Inventory
To avoid long discussions, general worst case failure modes are taken as default starting point(modified if required, after discussions)
113© Shell Global SolutionsP-B-v1.1
YEARS TO MEASURE CORROSION
0.0
0.2
0.4
0.6
0.8
1.0
1.2
1.4
1.6
0.02
0.04
0.06
0.08
0.10
0.12
0.14
Corrosion Rate, mm/yr
Mea
sure
men
t Tol
eran
ce +
/–, m
m
?
20 years
10 years
3 years
114© Shell Global SolutionsP-B-v1.1
COST REDUCTIONS
• By risk reduction• By longer inspection intervals• By lower inspection cost
N LL MM
E
H
X
EH
HMM
MMLL
LL
N
N
XXEHLL
3
2
1
4
PRO
BABI
LITY
CLA
SS
MULTIPLEFATALITIES
EXTENSIVEDAMAGE >10M
SLIGHT INJURY
SLIGHT DAMAGE<10K
SLIGHT EFFECT
MINOR INJURY
MINOR DAMAGE10-100K
MINOR EFFECT
MAJOR INJURY
LOCAL DAMAGE0.1-1M
LOCAL EFFECT
SINGLE FATALITY
MAJOR DAMAGE1-10M
MAJOR EFFECT MASSIVE EFFECT
HEALTH & SAFETY
ECONOMICS (USD)
ENVIRONMENTCON
SEQ
UEN
CECA
TEG
ORY
CONSEQUENCE CLASS NEGLIGIBLE1
LOW2
MEDIUM3
HIGH4
EXTREME5
NEGLIGIBLE
LOW
MEDIUM
HIGH
SUSCEPTIBILITY TO FAILURE RRM CRITICALITY CLASS
Risk reduction- count total if new plant- count difference if existing plant
= Freq. Reduction x CoF
from 0.1 * 5 MM to 0.001 * 5 MM⇒ reduction = 495. 000/yr
1.00.10.010.001
115© Shell Global SolutionsP-B-v1.1
FAILURE MODEWall thinning- minor loss, < 0.2 x wt- medium loss, < 0.5 x wt- serious loss, > 0.5 x wt- general or localised
Hole- small hole, < 5 mm dia- large hole, > 5 mm dia- very large hole, > 25 mm dia
Cracking- small crack, < 5 mm- medium size crack, < 25 mm- large crack, > 25 mm- through-the-wall
Rupture
DEGRADATION MECHANISM- General corrosion
- Erosion
- Hot H2-attack
- Pitting corrosion
- Fatigue
- Creep
- Stress Corrosion Cracking
- Embrittlement
DEGRADATIONS AND FAILURE MODES
116© Shell Global SolutionsP-B-v1.1
PROBABILITY OF FINDING LOCALIZED CORROSIONvia Spot Thickness measurements - with replacementPROBABILITY OF FINDING LOCALIZED CORROSIONvia Spot Thickness measurements - with replacement
4020 60 80 1000
5
10
15
Num
ber
of th
ickn
ess
read
ings
Probability of finding localized corrosion (%)
1% area
2%
5%
10%
25%
50%
75%
90%
117© Shell Global SolutionsP-B-v1.1
0
40
80
120
160
0.00 0.10 0.20
Proportion corroded
General corrosion on surface area200
50 8090 95 98% Confidence
Sam
ple
size
STATISTICAL SAMPLING
118© Shell Global SolutionsP-B-v1.1
PIPING REJECTION THICKNESSES (1)
• Piping classes have 1 or 3 mm Corrosion Allowance (CA):11010 has 1 mm CA for 150 lbs conditions11030 has 3 mm CA for 150 lbs conditions
• Pressures and temperatures are often significantly below the design conditions of the piping classes.
• Therefore EXTRA CA is often available.• Determine the minimum required wall thickness by:
spreadsheettableminimum thickness for mechanical stability
119© Shell Global SolutionsP-B-v1.1
PIPING REJECTION THICKNESSES (2)
corrosion
- Available schedule/thickness- CA, Corrosion Allowance- Plate/Pipe tolerance- DT, Design Thickness
- TminMinimum Allowable Thickness
- Tminfor single pit
120© Shell Global SolutionsP-B-v1.1
PIPING REJECTION THICKNESSES (3)PIPING REJECTION THICKNESSES (3)
corrosion wall thickness reduction
Residual wall thickness
Residual Corrosion Allowance
Fitness for Purpose (FFP) extra CAstudy
TminDESIGN
Localized pitting (FFP or Code)
121© Shell Global SolutionsP-B-v1.1
HEAT EXCHANGER TUBE - CA ?
• Internal (tube side) corrosion ?
• External (shell side) corrosion ?
• Corrosion Allowance CA ? External corrosion
CA = wt ?50/50 Int./Ext.
WT
Internal corrosion
122© Shell Global SolutionsP-B-v1.1
MINIMUM REQUIRED WALL THICKNESSmax. 250°CPipe size
1) B31.3 calculation, CS A106 Bor API 5L-B
2) Max. pipe span as per memo (check), filled with water and weight in the middle
3) Full vacuum4) NOT valid where additional stresses from
expansion etc. occur
DN 25 DN50 DN80 DN100 DN150 DN200 DN250 DN300 DN350
5 barg
10
15 2mm
20 4mm
25 4mm 4mm 5mm
30 3mm 4mm 5mm 5mm
40 4mm 5mm 6mm 7mm
50 4mm 5mm 6mm 8mm 9mm
60 5mm 6mm 8mm 9mm 10mm
75 4mm 6mm 8mm 9mm 11mm 12mm
100 4mm 5mm 8mm 10mm 12mm 14mm 16mm
125 4mm 5mm 7mm 9mm 12mm 15mm 18mm 20mm
Pres
sure
123© Shell Global SolutionsP-B-v1.1
NDT MEASUREMENTS - PLUGS
plug