bab iii pengembangan perangkat · pdf filepengembangan perangkat lunak ... - soil cover - type...

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


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


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


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


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


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


(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


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


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)

112

2. Tampilan output

Tabel 3. 6 Tampilan Output (API 581)

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