Gaurav Kumar Singh Rajput presents a methodology for assessing risks associated with liquid hydrocarbon storage tanks. The presentation outlines various tank fire accident scenarios and their potential causes, including operational errors, equipment failures, weather events, and maintenance issues. Case studies of past tank accidents in Jaipur and Kansas are examined to identify lessons learned. The methodology involves identifying potential process and non-process hazards, constructing a risk assessment flow diagram, and calculating risk through qualitative and quantitative analysis. Key aspects of the methodology include preventive maintenance, safety systems, qualitative and quantitative risk assessment, and layer of protection analysis.

1. Gaurav Kumar Singh Rajput
Roll no- 15
Gaurav Kumar Singh Rajput
Roll No- 15
HAZARD ASSESSMENT
METHODOLOGY FOR LIQUID
HYDROCARBON TANK
Gaurav Kumar Singh Rajput
Roll No- 15
S8
School Of Engineering

2. PRESENTATION OUTLINE-
1. Tank fire accident scenario
2. Failure cause of tank accident
3. Jaipur fire
4. Barton solvent chemical plant
5. Preventive and protective measure
6. potential process and non-process hazard
7. Risk assessment flow diagram
8. Risk calculation
9. Discussion of methodology
10. References

3. Tank fire accident scenarios-
 Rim seal fire
 Spill on roof fire
 Full surface fire
 Bund or dyke wall
 Pontoon explosion
 Boilover

4. Failure cause of tank accident-
1. Operational error
 Tank overfilling
 Valves left open accidently
 Vent closed during loading unloading
2. Equipment/instrument failure
 Floating roof sunk
 Level indicator
 Discharge valve rupture
 Rusted vent valve
3. Lightning
 Poor grounding

5. 4. Static electricity
 Damage seal
 Poor grounding
 Poor bonding
 Fluid transfer
5. Maintenance error
 Welding/cutting
 Circuit shortcut
 Non explosive-proof equipment used
6. Tank crack/rupture
 Poor soldering
 Corrosion
 Distortion/buckling

6. 7. Piping rupture/leak
 Valve leaking
 Pump leak
 Cut accidentally
8. Safety supporting system
 Insufficient tank cooling
 electric power loss
 Firefighter water loss
9. Miscellaneous
 Earthquake
 Arson
 Extreme weather

7. Jaipur Fire
Jaipur IOC Terminal (oct 2009)
11 people lost their life
Fire in 11 tank, fire continue for 11 days
Cause-
 Basic operation procedure was not followed
 No control room
 Delay in emergency response team
 ESD from control room was not available
Recommendations-
 Engineering related
 Operation related
 Training related
 Procurement related
 Management related
By M.B Lal committee

8. Standard operating sequence Likely sequence
1. Ensure MOV and HOV are
closed
2. Reverse the position of
hammer blind valve
3. Open the HOV
4. Open MOV
1. MOV opened first
2. Hammer blind valve opened
3. Leakage started

10. Barton Solvents Chemical Plant Accident
Barton solvent chemical plant Kansas (July 2007)
Evacuation of 6000 residents, destroyed the tank farm
Cause-
 Faulty design of level gauge.
 The tank contained an ignitable vapour-air mixture in its head
space.
 Stop-start filling, air in transfer pipe, sediment and water.
Recommendations-
 Add inert gas to the head space
 Avoid loose linkage
 Anti static additives
 Reduce fluid pumping velocity
 Require additional manufacture guidance
 By pass conductor

13. Preventive and protection measure-
1. Design
 Follow engineering standard and regulations
 Modification in design
 Dyke, Bund
2. Maintenance
 Routine inspection
 Periodic proof testing
 Use proper equipment
 Use explosion-proof tools
3. Equipment
 Follow engineering standard
 Lightning protection system
 ROSOV
 Temperature monitoring device

14. 4. Safety supporting system
 Fire detection and alarm system
 Fire fighting system
 Tank cooling system
 Emergency response plan
 CCTV equipment
5. Miscellaneous
 Safeguarding
 Good house keeping/No smoking
 Protection from DOMINO effect, areal electrical
power lines, extreme weather, mechanical stress
and vehicle bumping.

15. POTENTIAL PROCESS AND NON-PROCESS
HAZARD-

16. RISK ASSESSMENT FLOW DIAGRAM-

17. RISK CALCULATION-
 Risk due to hazard at storage tank terminal and its
surrounding is composed of summation of all risk
given no escalation of event of undesired event and
all risk given an escalation.
Risk= Risk/ No Escalation + Risk/ Escalation
The result of the quantitative risk analysis are commonly represented by
the following parameter-
1. Individual risk
2. Societal risk

18. -Individual risk is the risk that an individual remaining at a
particular spot would face from the plant facility.
The individual risk value is a frequency of fatality usually
chance per million per year and represent on ALARP
triangle.
-Societal risk is the risk on number of people who might
be affected by hazardous incident and represent on F-N
(Frequency-Number curve) curve .
Risk Analysis
Qualitative Risk
Analysis
Quantitative Risk
Analysis

19. ALARP Triangle
F-N Curve

20. DISCUSSION OF METHODOLOGY-
 All expert practitioner place great importance to an
integrated automatic system for overfilling protection.
 The protection against lightning is considered vital.
 A rim seal fire is considered as the most frequent fire
for floating roof tank.
 Venting devices placed on the top of the fixed roof
tank should be regularly checked.
 The sinking of the floating roof must be avoided.
 Reduce the all possibility of Boilover.
 Regular maintenance and inspection should be done
and their report should be maintain.

21.  Good drainage facility to avoid flooding in tank farm
area.
 High inlet temperature of the fuel is not considered
a probable accident cause.
 The non existence of specific safety measure, like
an obligatory cooling system, in the that the tank
farm have been built prior to the actually existing
regulation.
 Qualitative and quantitative risk assessment should
be conducted time to time.
 Layer of protection analysis should be done before
QRA.

22. References-
 A hazard assessment methodology for large liquid hydrocarbon fuel
tanks, C.D. Argyropoulos, M.N. Christolis, Z. Nivolianitou, N.C. Markatos.
 Barton Solvents Flammable Liquid Explosion and Fire, CSB report.
http://www.csb.gov/barton-solvents-flammable-liquid-explosion-and-fire/
 Jaipur Terminal Fire of 29.10.2009. http://www.hrdp-
idrm.in/live/hrdpmp/hrdpmaster/idrm/content/e6547/e6546/e32086/e3208
7/eventReport32415/MbLalreportonJaipurFire.Mr.Roy.ppt
 U.S. Chemical Safety Board. (2009). Cited at December, 5, 2011,
available at http://www.csb.gov/investigation/detail.aspx?SID=87
 A novel approach for Risk Assessment of Large Oil Storage Tanks Ali
Sari, Ph.D,. P.E. GenesisOilandGas.com
 A Holistic Risk Assessment Method For Storage Tank Terminals
Considering Domino Effects Triggered by Natural Hazards. ALI SARI,
PH.D,. P.E.