62
BAB III
Pengembangan Perangkat Lunak
Untuk melakukan perhitungan analisis resiko sebuah pipeline, banyak
sekali parameter yang diperlukan. Perhitungan dilakukan dengan mengambil tabel
– tabel dan yang jumlahnya cukup banyak. Hal ini membuat kesulitan bagi kita
untuk melakukan perhitungan. Selain waktu yang dibutuhkan semakin besar,
kesalahan dalam perhitungan juga semakin besar.
Perlu sekali untuk mengembangkan perangkat lunak yang membantu
untuk melakukan perhitungan kategori resiko pipeline. Dengan adanya perangkat
lunak yang dikembangkan oleh penulis, diharapkan kemungkinan kesalahan pada
waktu perhitungan dapat diminimalkan. Selain itu diharapkan waktu untuk
melakukan perhitungan dapat diminimalkan.
Perangkat lunak yang dikembangkan adalah perhitungan kategori resiko
berdasarkan metode Muhlbauer dan API 581. Dimana perangkat lunak yang
dikembangkan menggunakan microsoft excel sebagai alat bantu. Dengan
memasukkan berbagai parameter dalam perhitungan, didapatkan calculation sheet
yang digunakan untuk perhitungan kategori resiko.
Dibawah ini akan dijelaskan tentang perangkat lunak yang telah
dikembangkan baik perhitungan kategori resiko berdasarkan metode Muhlbauer
ataupun API 581.
3.1 Pengembangan Perangkat Lunak Metode Muhlbauer
Dalam pembuatan perangkat lunak harus mengacu kepada langkah –
langkah dalam perhitungan. Setiap langkah dalam perhitungan harus dimasukkan
kedalam program untuk menghasilkan nilai sebenarnya. Dibawah ini ditunjukan
langkah – langkah yang telah dirumuskan dalam pembuatan perangkat lunak
pengkategorian resiko metode Muhlbauer.
63
3.1.1 Diagram Alir Perancangan Perangkat Lunak Metode Muhlbauer Dibawah ini ditunjukkan bagaimana aliran/langkah – langkah yang
ditempuh untuk melakukan perhitugan kategori resiko berdasarkan metode
Muhlbauer. Diagram alir perangkat lunak metode Muhlbauer ini secara umum
dapat dilihat pada gambar 3.1.
Start
End
Design, operation & environment
Data
Probability of Failure Analysis
Consequence of Failure Analysis
Design Factor
Leak Impact Factor
Risk Matrix
Third-party Damage Factor
Incorrect Operations Factor
CorrosionFactor
Gambar 3. 1 Flowchart Perangkat Lunak Metode Muhlbauer
Dari Flowchart diatas dapat kita lihat beberapa faktor yang mempengaruhi
perhitungan dalam metode Muhlbauer. Untuk mengetahui secara detail
perhitungan masing – masing faktor ditunjukkan dibawah ini.
64
1. Flowchart perhitungan third-party damage factor
Sum index
Minimum Depth of Cover
(weighting : 20%)
Activity Level(Weighting : 20%)
Aboveground Facilities
(Weighting : 10%)
Line Locating(Weighting : 15%)
Public Education Programs
(Weighting : 15%)
Right-of-Way Condition
(Weighting : 5%)
Patrol Frequency(Weighting : 15%)
- Soil Cover- Type of soil- Payment type- Warning tape or mesh- Water depth
- Population density- Stability of the area- One calls- other buried utilities- Anchoring, dregging
- Vulnerability- Threats
- Mandated- Response by owner- Well-known and used
- Methods- Frequency
- Signs- markers- Overgrowth- Undergrowth
- Ground patrol frequency- Ground patrol effectiveness- Air patrol frequency- Air patrol effectiveness
Third-party Damage Factor
Gambar 3. 2 Third-party Damage Factor Flowchart
65
2. Flowchart perhitungan corrosion factor
Gambar 3. 3 Corrosion Factor Flowchart
66
3. Flowchart perhitungan design factor
Sum index
Safety Factor(weighting : 35%)
Fatigue(weighting : 15%)
Surge Potential(weighting : 10%)
Integrity Verification
(weighting : 25%)
Land Movements (weighting : 15%)
Design Factor
- Max pressure- Normal pressure- Material strength- Pipe wall thickness- External loading- Diameter- Strength of fittings- Valves- Components
- Pressure cycle magnitude- Pressure cycle frequency- Material toughness- Diameter/wall thickness ratio
- Fluid bulk modulus- Pipe modulus of elasticity- Rate of flow stoppage- Flow rates
- Verification date- Pressure test level- In-line inspection technique- In-line inspection accuracy
- Seismic shaking- Fault movement- Subsidence- Landslide- Water bank erosion
Gambar 3. 4 Design Factor Flowchart
67
4. Flowchart perhitungan incorrect operation factor
Gambar 3. 5 Incorrect Operation Factor Flowchart
68
5. Flowchart perhitungan leak impact factor
Gambar 3. 6 Leak Impact Factor (CoF) Flowchart
69
3.1.2 Tampilan Perangkat Lunak Metode Muhlbauer Dengan memasukkan pemodelan seperti yang telah ditunjukkan pada flowchart diatas, didapatkan tampilan untuk perangkat lunak
sebagai berikut:
1. Tampilan PoF analisis
Tabel 3. 1 Tampilan Input Data Umum (Muhlbauer)
Crossing Location Handil Badak Crossing ID PK 30+350 Pipeline ID 20" Gas Pipeline Location Handil - Nilam
Tabel 3. 2 Tampilan Probability of Failure Analisis (Muhlbauer)
Probability of Failure Analysis
Corrosion Factor Comments
Atmospheric Corrosion
Pipeline existing condition :
70
Environment condition :
Coating condition based on quality
and application :
Coating condition based on quality of inspection and defect correction program :
Internal Corrosion Product Corrosivity :
Preventive Maintenance :
71
Subsurface Corrosion
Subsurface Evironment Soil resistivity :
pH
Microbial (MIC)?
Is Op. stress > 60% SMYS? 38
Is Op. temp. > 100o F?
is distance from compressor station
< 20 miles?
Is pipeline age > 10 years?
Is coating made from FBE?
72
Cathodic Protection
Is CIS polarization applied?
Is CIS on applied?
Is CIS off applied?
AC related
Is shielding situation apply?
Is there any burried metal until 500
ft?
Coating Coating Fitness :
Inspection program condition :
Defect correction program condition :
73
Design Factor Comments
Safety Factor index Actual Wall thickness (in) : 0.3154 Required wall thickness (in) : 0.3243 Rasio actual to require (t) : 0.97 Design pressure (psig) : 1453 Max Op. Pressure (psig) : 1321 Ratio Design to MOP : 1.10
Fatigue Operating pressure : 800 Ratio op. press. to MOP : 0.61 72.76 Lifetime cycles : 144
Surege Potential Potential of pressure surege :
Time since last test
Test Pressure : 1816 Ratio test pressure to MOP 1.37 Time since last test (year) 24
74
Land movement
Land movement potential
Incorrect Operations Factor Comments
Design
Which hazard identification process
is used?
Probability operation condition same
with MOP
Safety system
Is replacement process conform to
original specification?
Is design process checked and monitored carefully?
75
Construction process
Is construction process inspected?
Is material selection procedured?
are joints inspected by industry-accepted practices?
Is knowledge of good backfill/support technique applied?
12
Is there good material handling practice and storage technique?
Is Constructor care in applying and preapplied coating?
Operations are procedure quality and use exist ? are all activities monitored? Are employees tested by drug test?
76
Is there any safety program?
Maps/records system:
What are training exist? Mechanical Error Preventer Device
Maintenance
Maintenance documentation condition:
Maintenance schedule condition:
77
Maintenance procedure condition:
Third-party damage factor Comments Minimum depth of cover
buried depth from aboveground (in): 59.06
Depth below water surface (ft): 0 (no applicable) Maximum anchore depth (ft): 0 (no applicable) maximum dredge depth (ft): 0 (no applicable)
Existing condition :
Activity level Activity level :
78
Aboveground facility Aboveground condition:
36.31
Line locating
Line locating condition:
Public education Public education condition:
Right-of-way condition Right-of-way condition:
79
Patrol
Patrol condition:
Probability of Leak 159.07
2. Tampilan CoF analisis
Tabel 3. 3 Tampilan Consequence of Failure Analisis (Muhlbauer)
ID Parameter Simbol Unit Value A Product Hazard
A.1 Acute Hazard Score 8
A.1.1 Representative Fluid (most hazardous) Methane A.1.1.1 NFPA for flameable Nf
A.1.1.2 NFPA for Reactivity Nr
A.1.1.3 NFPA for Toxicity Nh
80
ID Parameter Simbol Unit Value
A.2 Chronic Hazard Score 10
A.2.1 Is the product hazardous based on CERCLA standard ? (if "Yes" Go to A.2.4)
A.2.2 Is the product hazardous by defenition AND volatile? (if "No" Go to A.2.3)
A.2.3 Is the formal cleanup required?
Reportable spill quantity (calculation) 55399.88
A.2.4 Reportable spill quantity RQ lb
A Product Hazard Score PH 18
B. Preleminiary Data & Calculation for determination Leak Volume and Dispersion
B.1 Dimension Data for Pipeline B.1.1 Nominal Diameter in 20B.1.2 Outside Diameter in 20B.1.3 Pipeline wall thickness in 0.3154B.1.4 Length of Pipe (evaluated section length) ft 27074.35B.1.5 Cross sectional area of Pipe in2 294.65B.1.6 Length of Pipe (length of upstream and downstream pipe) ft 27074.35 B.2 Fluid property inside pipeline B.2.1 Representative Fluid (most hazardous) for Gas Phase Methane B.2.2 weight density of fluid (Gas) lb/ft3 0.555
81
ID Parameter Simbol Unit Value
B.2.3 Molecular weight of fluid (Gas) lbm / mol 16.042B.2.4 Vapour Pressure of fluid (Liquid) psi B.2.5 Representative Fluid (most hazardous) for Liquid Phase B.2.6 weight density of fluid (Liquid) lb/ft3 B.2.7 Boiling Point of fluid (Liquid) oF B.3 Operating Condition B.3.1 MOP (maximum operating pressure) psi 1321B.3.2 Desain pressure psi 1453B.3.3 Desain temperature oF 100B.3.4 Normal Operating pressure psi 800B.3.5 Normal Operating temperature oF 86B.3.6 Upset pressure (if any) psi B.3.7 Ambiant Pressure psi 14.7B.3.8 Ambiant Temperatur oF 86 B.4 For Gas flow in pipeline
B.4.1 Expansion factor (0.65 until 0.95, for fluide discharge to atmosphare = 0.65) Y 0.65
B.4.2 flow coefisient ( 0.9 until 1.2) C 0.9B.4.3 Change the pressure accrose the orifice ΔP psi 785.30B.4.4 Gas flow rate q ft3/sec 4336.13B.4.5 Mass of Gas to be release per second Mq lb/sec 2406.55B.4.6 Mass of Gas released after 10 minutes lb 1443930.68
82
ID Parameter Simbol Unit Value
B.5 For Liquid flow in pipeline B.5.1 flow coefisient ( 0.9 until 1.2) C 0.9B.5.2 Change the pressure accrose the orifice ΔP psi 785.30B.5.3 Liquid flow rate q ft3/sec Not Applicable B.5.4 Mass of Liquid to be release per second Mq lb/sec Not Applicable B.5.5 Mass of Liquid released after 10 minutes lb Not Applicable B.6 For Gas & Liquid flow in pipeline (two phase fluide) B.6.1 Liquid flow rate ft3/sec Not Applicable B.6.2 Mass of Liquid to be release from 0 until 3 minute lb Not Applicable B.6.3 Gas flow rate ft3/sec Not Applicable B.6.4 Mass of Gas to be release from 3 min until 10 minute lb Not Applicable B.6.5 Total Release Mass for 10 minute lb Not Applicable C. Leak Volume Score Calculation C.1 For Gas Flow C.1.1 Spill volume by pumping flow rate (max flow rate/12) V1 ft3/sec 361.34C.1.2 Volume contributing by leak detection and response time V2 ft3 0C.1.3 Spill volume contributing length of upstream and downstrem pipe V3 ft3 55399.88C.1.4 Leak Volume for Gas Flow LV 0.44C.2 For Liquid Flow C.2.1 Spill volume by pumping flow rate (max flow rate/12) V1 ft3/sec Not Applicable C.2.2 Volume contributing by leak detection and response time V2 ft3/sec 0C.2.3 Spill volume contributing length of upstream and downstrem pipe V3 ft3/sec Not Applicable C.2.4 Leak Volume for Liquid Flow LV Not Applicable
83
ID Parameter Simbol Unit Value
D. Dispersion [D] D
D.1
For Hazardous gas/vapour release D.1.1 Product release after 10 minutes (see B.4.6) lb D.1.2 Dispersion Score gas/vapour release 6 D.2 For Hazardous Liquid release
D.2.1 Product release after 10 minutes (see B.5.5) lb
D.2.2 Dispersion Score for Liquid into air Not Applicable
D.2.3 Soil Permiability cm/sec
D.2.4 Soil Permiebability score 4 D.2.5 Dispersion Score for liquid into submerged Not Applicable D.3 For Hazardous Liquid and Gas (2 phase) release D.3.1 Gas Spill Score 8788.51
D.3.2 Liquid Spill Score
Not Applicable Maximum Spill Score
Representative Spill Score (largers from Gas or Liquid spill Score) 6
84
ID Parameter Simbol Unit Value
E. Resceptors [R] E.1 Population Density
E.1.1 Population count in one mile
E.1.2 Population type E.1.3 Population Score 9
E.2
Enviromental Consideration (only for Chronic Hazard model) E.2.1 Enviromental Sensitivity E.2.2 Enviromental Sensitivity score 0.5 E.3 High - Value Area
E.3.1 High - Value Area Description
E.3.2 High Value Area Score 0.3 E.4 Receptor Score 9.8
85
LIF Summary
Condition for Modeling 468.28
Leak Impact Factor (LIF= PH x LV x D x R) Liquid
Gas 468.28
LIF Two
Phase
86
3. Tampilan risk matrix
Tabel 3. 4 Tampilan Risk Matrix (Muhlbauer)
Risk Matrix 20" Gas [Handil - Nilam] PROBABILITY OF FAILURE
CATEGORY
5 321 - 400
4 241 - 320
3 161 - 240
2 81 - 160 X
1 0 - 80
0 - 400 401 - 800
801 - 1200
1201 - 1600
1601 - 2000
A B C D E CONSEQUENCE OF FAILURE CATEGORY
LOW RISK
MEDIUM RISK
MEDIUM-HIGH RISK
HIGH RISK
3.2 Pengembangan Perangkat Lunak Metode API 581
Perangkat lunak perhitungan kategori resiko pipeline yang kedual adalah
pengkategorian resiko metode API 581. Pembuatan perangkat lunak API 581 ini
mengacu pada langkah – langkah pada diagram alir dibawah ini.
3.2.1 Diagram Alir Perancangan Perangkat Lunak Metode API 581 Dibawah ini ditunjukkan langkah – langkah dalam pembuatan perangkat
lunak berdasarkan API 581. Secara umum, diagram alir perangkat lunak metode
API 581 ini gambar dibawah ini.
87
Start
End
Data perancangan & kondisi operasi
sistem jalur pipa
Risk Matrix
Probability of Failure Calculation
Consequences of Failure Calculation
Generic Failure Frequency
Management System Evaluation
Factor
Equipment Modification
Factor
Flammable Consequence
Environmental Consequences
Business Interruption
Consequences
Gambar 3. 7 Flowchart Perangkat Lunak Metode API 581
Dari Flowchart diatas dapat kita lihat beberapa faktor yang mempengaruhi
perhitungan dalam metode API 581. Untuk mengetahui secara detail perhitungan
masing – masing faktor ditunjukkan dibawah ini.
88
1. Flowchart perhitungan release rate
Representative Fluid Operation Temperature
Determination Heat Capacity (Cp)(Table 7.2)
Determination K
Determination Transition Pressure(Equation 7.2)
Heat Capacity (Cp)
Ptrans
K
Operation Pressure > Ptrans ?
Operation Pressure
Determination of Liquid Density (Table 7.2)
Density
Calculation of Release Rate for Each Hole(Equation 7.1)
Liquid Phase Gas Phase
Hole SizesRepresentative
Fluid
Determination Molecular Weight(Table 7.2)
Operation Pressure
Molecular Weight
Operation Temperature
Determination Sonic Release Rate for Each Hole
(Equation 7.3)
Determination Subsonic Release Rate for Each Hole
(Equation 7.4)
Release Rate for Each Hole Size
Yes No
Gambar 3. 8 Flowchart Perhitungan Release Rate
89
2. Flowchart perhitungan release tipe
Gambar 3. 9 Penentuan Release Type
3. Flowchart penentuan fasa final fluida
Representative Fluid
Determination of The Boiling Point (Table 7.2)
Determination ambient state (Table 7.5)
Boiling Point Ambient StateFluid Phase in Equipment
Determine The Fluid Phase in the case of each hole size
(Table 7.5)
Fluid Final Phase
Gambar 3. 10 Penentuan Fasa Final Fluida
90
4. Flowchart perhitungan Technical Module Subfactor
Gambar 3. 11 Flowchart Perhitungan Technical Module Subfactor (TMSF)
91
5. Flowchart perhitungan Thinning TMSF
ThicknessData
Calculation ofCorrosion Rate
ActualCorrosion
Rate
Determination ofThinning
Corrosion Rate
EstimatedCorrosion
Rate
Estimation ofCorrosion Rate (Appendix G)
Calculation ofa.r/t
MeasurementDate
a.r/t
Corrosion =Localized ?
TMSFLocalized or
General
Determine TMSF General
Determine TMSF Localized
Number of Inspections
Number of Inspections
Inspection Effectiveness Category for
Localized
Inspection Effectiveness Category for
Localized
Adjustment TMSF
OverdesignFactor
On-lineMonitoring
Factor
Adjusted TMSF
Equipment Type =Piping
Adjustment of TMSF by
Piping factor
TMSF Thinning
Y
NY
N
Gambar 3. 12 Flowchart Perhitungan Thinning TMSF
92
Gambar 3. 13 Flowchart Faktor koreksi untuk pipa/pipeline
93
6. Flowchart perhitungan Stress Corrosion Cracking SCC TMSF
Is the material ofconstruction carbon or
low alloy steel?
Screen for Caustic, Amine,SSC, HIC/SOHIC,
Carbonate Cracking
Determine Susceptibilityfor Each Potential SCC
Mechanism for Carbon andLow Alloy Steels
Have you detectedSCC in this or similarservice equipment?
Is the material ofconstruction austenitic
stainless stell?
Screen for PTA, CISCC
Determine Susceptibilityfor Each Potential SCC
Mechanism for austenitic stainless stell
Increase theSusceptibility forthat Mechanism
to High
Increase Susceptibilty
for All PotentialMechanisms to High
Do you know thecause of SCC
Determine theSeverity Index for
Each PotentialMechanism
DetermineMaximum
Severity Index
Determine TMSF
Escalation ofTMSF with Time
Modify TMSFfor On-line
Monitoring Factor
TMSF (SCC)
MAWP/OPRatio
Number of Inspections
(See Table H-5)
Highest EquivalentInspection
Effectiveness
TMSF = 1
Y
N
Y
Y
Y
N
N
N
Gambar 3. 14 Flowchart Perhitungan SCC TMSF
94
7. Flowchart perhitungan High Temperature Hydrogen Attack TMSF
Temperature
H2PP
Time
Material ofConstruction
HeatTreatment
InspectionEffectiveness
Number ofInspection
Calculate PV
DetermineSusceptibility
(Table I-3)
Determine the TMSF
(Table I-5)
Inspection Result
TMSF (HTHA)
Gambar 3. 15 Flowchart Perhitungan HTHA TMSF
95
8. Flowchart perhitungan Furnace Tube Failure TMSF
Estimate TMT
Determine ElasticMetal Temperature
from Table J-4
Is TMT? ElasticMetal Temperature
from Table J-4
Do You Have aMeasured
Corrosion Rate?
Do You Have aMeasured TMT?
Determine CurrentWall Thickness
(Tcurrent)
Calculate Stress, S
Process Outlet
Temperature
Material ofConstruction
Determine CorrosionRate from Thinning Module
Technical SupplementsNote: CRtotal = CRint + CRext
Process Outlet
Temperature
Process Outlet
Temperature
Operating Pressure
Diameter
Determine Short-TermFailure Probability
Y
Y
Y
N
N
TMSFLT = 1
Gambar 3. 16 Flowchart Perhitungan Furnace Tube Technical Module
96
Gambar 3. 17 Flowchart Penentuan Long Term TMSF
Gambar 3. 18 Flowchart Penentuan Short Term TMSF
97
9. Flowchart perhitungan Mechanical Fatigue on Piping TMSF
Gambar 3. 19 Flowchart Penentuan Piping Mechanical Fatigue TMSF
98
10. Flowchart perhitungan Brittle Fracture TMSF
Gambar 3. 20 Flowchart Perhitungan Low Temperature/Low Toughness
Failure TMSF
99
Do administrative controls Prevent pressurizing below some
temperatureTmin?
Determine Tmin, the minimum of:• Design temperature• Operating temperature• Upset temperature
Design temperature
Operating temperature
Determine appropriate wall thickness Thickness
Determine Tref from minimum of:• Impact test temperature• Impact exemption temperature• Stated MDMT
Impact temperature
Exemption temperaturefrom Figure L-1
Material specification
Stated MDMT
Calculate Tmin – (Tref + FATT)
Post-weldheat treated?Use Table L-4 Use Table L-5
Y
N
N Y
Determine FATT from:• Engineering Analysis, or• Equation L.1, or• Equation L.2, or• Assume FATT = 150� F
Gambar 3. 21 Flowchart Perhitungan Temper Embritlement TMSF
Gambar 3. 22 Flowchart Perhitungan 8850F Embritlement TMSF
100
Gambar 3. 23 Flowchart Perhitungan Sigma Phase Embritlement TMSF
101
11. Flowchart perhitungan Equipment Linings TMSF
Determine the Lining Failure Factor from Table M-5 A or B
Adjust for Lining Condition using Table M-6
Adjusted LiningFailure Factor greater
than Sum of otherTechnical Module
Subfactors?
Use Sum of otherTechnical Module
Subfactors
YN
Adjust for On-line Monitoring
Determine the Sum of the otherTechnical Module Subfactors
Use Adjusted LiningFailure Factor
Lining Type
Years Since Inspection
For Organic Coatings, Years
in Service
Qualitative Lining Condition
Thinning Subfactor,SCC Subfactor, etc.
Monitoring Program
Gambar 3. 24 Flowchart Perhitungan Lining TMSF
12. Flowchart perhitungan External Damage TMSF
Gambar 3. 25 Flowchart Penentuan External Damage
102
Gambar 3. 26 Flowchart External Corrosion untuk Carbon & Low Alloy
Steels
103
DetermineCorrosion Ratefrom Table N-9
Pipe Supportor Soil/Air Interface
Penalty?Tables N-13
and N-14
Rate 2X Rate 1X
OperatingTemperature
Driver
Y N
DetermineComplexity Factor
Table N-11Rate 0.75X Rate 1.25X
BelowAverage
DetermineInsulation Condition
Table N-12Rate 1X Rate 0.25X
Rate 1X
Rate 0.05X
TMSFEXT “B”
Date Modified
Coating Quality
Date Installed
BelowAverage
AboveAverage
AboveAverage
Average
Average
Gambar 3. 27 Flowchart CUI untuk Carbon & Low Alloy Steels
Gambar 3. 28 Flowchart External SCC untuk Austenitic Stainless Steels
104
Determine SCCSusceptibilityTable N-22
Pipe Supportor Soil/Air Interface
Penalty?Rate 2X Rate 1X
OperatingTemperature
Driver
Y N
DetermineComplexity Factor
Table N-24Rate 0.75X Rate 1.25X
BelowAverage
DetermineInsulation Condition
Rate 1X Rate 0.25X
Rate 1X
Rate 0.05X
BelowAverage
AboveAverage
AboveAverage
Average
Average
Insulation TypeTable N-26
InspectionEffectivenessTable N-27
Thickness
Modified DateTable N-23
Number ofInspections
Coating QualityTable N-23
Date Installed
Final TMSF
Gambar 3. 29 Flowchart External CUI SCC untuk Austenitic Stainless Steels
105
13. Flowchart perhitungan process subfactor TMSF
Gambar 3. 30 Flowchart Perhitungan Process Subfactor
14. Flowchart perhitungan mechanical subfactor TMSF
Gambar 3. 31 Flowchart Perhitungan Mechanical Sub Factor
106
15. Flowchart perhitungan universal subfactor TMSF dan PoF Plant
Condition(Observation)
AmbientTemperature
Seismic Zone
Determination of PlantCondition Element
(Table 8.13)
Determination ofCold Weather Element
(Table 8.14)
Determination of Seismic Activity Element
(Table 8.15)
Plant ConditionElement
Cold WeatherElement
Seismic ActivityElement
Calculation ofUniversal Sub
factor
UniversalSubfactor
MechanicalSubfactor
ProcessSubfactor
Technical Module
Subfactor
Calculation of Equipment
Modification Factor
EquipmentModification
Factor
PSM Modification
Factor
Calculation of Likelihood
Generic Failure Frequency for
Each Hole Size
LIKELIHOOD
Table 8.1
Generic PipingFailure Frequency
Determination of GenericEquipment Failure
Frequency
PipingLength
Equipment = piping ?
EquipmentType
Y
N
Gambar 3. 32 Flowchart Perhitungan Universal Subfactor dan PoF
107
16. Flowchart perhitungan Flammable Consequence
Detection Rating Isolation Rating Table 7.16
Representative Fluid
No Flammable Consequence
Release rate/mass adjusted by detection/isolation
Adjusted available mass for Release
Release rate adjusted for each hole
Available mass for release
Release Rate for Each Hole Size
Determine of the Auto Ignition Temperature
Table 7.2
Representative Fluid
Operating Temperature
Flammable Product ?
Operating Temperature >800
F + AIT ?Auto Ignition Likely Auto Ignition Not Likely
Release Type for each hole
Fluid Final Phase after Release
Table 7.10 Table 7.11 Table 7.8
Table 7.9
Calculation of the Equipment damage areas / hole size
Calculation of Personnel damage areas / hole size
Re-adjust equipment and personnel damage areas Table 7.16
Equipment affected areas
before adjustment
Mitigation System Flammable affected equipment
damage areas /hole size
Flammable affected Personnel
damage areas /hole size
Personnel affected areas
before adjustment
Gambar 3. 33 Flowchart Perhitungan Flammable Consequence
108
17. Flowchart perhitungan toxic consequence
Instantaneous Continuous
Release Type
RepresentativeMaterial
Instantaneous Release Mass
Release Rate
Release Duration
RepresentativeMaterial
Figure 7.8 Figure 7.6
Figure 7.5Determine Consequence AreaFor Release Mass
Determine Consequence Area
Consequence Area For Release Mass
Toxic Consequence Result
Consequence Area
Toxic Consequence Result
Gambar 3. 34 Flowchart Perhitungan Toxic Consequence
18. Flowchart perhitungan environmental consequence
Gambar 3. 35 Flowchart Perhitungan Environmental Consequence
109
19. Flowchart perhitungan bussiness interuption
Gambar 3. 36 Flowchart Perhitungan Bussiness Interuption Consequence
20. Flowchart perhitungan kategori CoF
Gambar 3. 37 Flowchart Perhitungan Kategori Consequence of Failure
110
3.2.2 Tampilan Perangkat Lunak Metode API 581 Dengan memasukkan pemodelan seperti yang telah ditunjukkan pada flowchart diatas, didapatkan tampilan untuk perangkat
lunak metode API 581 sebagai berikut:
1. Tampilan input data
Tabel 3. 5 Tampilan Input Data (API 581)
111
112
2. Tampilan output
Tabel 3. 6 Tampilan Output (API 581)
113
114
115