Presentation on theme: "SITING OF HAZARDOUS INDUSTRIES – ROLE OF RISK ANALYSIS 23 Oct 2010, Bengaluru, Karnataka Dr. A. Koshy 23 Oct 2010, Bengaluru, Karnataka Capacity Building."— Presentation transcript:
SITING OF HAZARDOUS INDUSTRIES – ROLE OF RISK ANALYSIS 23 Oct 2010, Bengaluru, Karnataka Dr. A. Koshy 23 Oct 2010, Bengaluru, Karnataka Capacity Building Programme on “New Techniques and Strategies in Prevention and Management of Industrial Disasters” to the Karnataka Factory Inspectorate Oct 2010 Disaster Management Institute ORGANIZERS Karnataka State Safety Institute ® Department of Factories, Boilers, Industrial Safety & Health, Bengaluru SPONSORSORGANIZERS Karnataka State Safety Institute ® Department of Factories, Boilers, Industrial Safety & Health, Bengaluru SPONSORS
Concerns and issues in Siting/ Layout Strategic Principles in the determination of safe location and layout for a new or a expansion project Key information to be considered before selecting a site location How are siting issues managed when limited space is available? How are security concerns in a new site addressed ?
An Ideal Situation A site location and layout that will minimize risk to the surrounding and community/ personnel and property while maximizing the ease of safe operation and maintenance. Appropriate siting and layout establishes a foundation for a safe and secure operation.
Hazard Management in Life Cycle of an Engineering Project PRODUCTION CONCEPT FRONT-END ENGINEERING DETAIL ENGINEERING CONSTRUCTION INSTALLATION COMMISSIONING Site Lay-out of installation
Hazard Techniques for Site evaluation Techniques of Fire Explosion Index and Toxicity Index Dow’s Index Mond’s Index Codes ( OISD) Allowing objective spacing distances to be taken into account at all stages
Major Accident Hazard Group “Major accident” means an incident involving loss of life inside or outside the site or 10 or more injuries inside and / or one or more injuries outside or release of toxic chemical or explosion or fire or spillage of hazardous chemicals resulting in ‘on-site’ or ‘off-site’ emergencies or damage to equipment leading to stoppage of process or adverse effects to the environment. THE MAJOR ACCIDENT HAZARD CONTROL RULES, 1997
Features of Well Laid out Site The potential for toxic impacts, fire escalation, and explosion damage will be low. The risk to personnel and the surrounding community will be reduced. Maintenance will be easier and safer to perform. However, these benefits do not come without associated costs. Separation distances translate to real estate that costs money.
Flixborough (6/74)28 fatalities - $167MM Seveso (7/76)Contaminated countryside Mex. City (11/84)550+ fatalities - $26MM Bhopal (12/84)3M+ fatalities - 200M affected Chernob. Nuc. Plt. (4/86)31 fatalities mi 2 evacuated Piper Alpha Plat. (7/88)165 fatalities Pasadena, Tx. (11/89)23 fatalities - $797MM Channelview, Tx. (7/90)17 fatalities - $14MM Pemex, Mexico (7/96) Multiple fatalities - $253MM, $8MMM loss to economy Petrobras, Brasil (6/2001) 10 fatalities - $300MM Toulouse, France (9/01)29 fatalities, 20,000 homes damaged * Large property damage losses (17th edition); M&M Protection Consultants; 1166 Avenue of the Americas, NY, NY Some key industrial accidents
Hazard & Risk Assessment IDENTIFY Are people exposed to harm resulting from the company’s operations? ASSESS What are the causes, consequences & effects? How likely is the loss of control? What is the risk & is it ALARP? CONTROL Can the causes be eliminated? What controls are needed & can they be effective? RECOVER Can the potential consequences & effects be mitigated? What are the recovery measures required? Are the recovery capabilities suitable & sufficient?
Explosion at Chemical facility Flixborough, England, 1974
A large quantity of cyclohexane vapor was released when a 20” “makeshift” bypass pipe ruptured The cyclohexane formed a flammable mixture and subsequently found a source of ignition. The resulting massive vapor cloud explosion killed 28 workers, injured 36. (Minimized as the office block was unoccupied)
Damages ( Onsite and Offsite) 18 fatalities occurred in the control room as a result of the windows shattering and the collapse of the roof. No one escaped from the control room. Fires burned for several days and after ten days those that still raged were hampering the rescue work. Offsite consequences reported injuries. Property in the surrounding area was damaged to a varying degree.
Contributing Factors Not following codes & operating procedures while introducing modifications design codes, management of change procedures, maintenance procedures during recommissioning Plant layout - position of occupied buildings Control Room not designed for withstanding major hazards Emergency plan not updated following modifications UK COMAH regulation was introduced
Explosion at Refinery, Pasadena, Texas 23 Oct 1989
During maintenance work on a reactor settling leg, a large release of flammable vapor occurred at the Phillips 66 chemical complex. The result -- a massive vapor cloud explosion, followed by a series of further explosions and fires. 23 fatalities and 300 people injured. Extensive damage to the plant facilities Metal & Debris as far as 4 Km
Contributing Factors Site and industry standards for maintenance not followed Training and competence Work permit system - contractors Positioning of occupied buildings
Risk Factors in Site Selection Risk to Population density around the site ( from choice hazardous material, equipment, activites) Risk from Natural disaster occurrence (earthquake, flood, etc.) Risk of non-availability of power, steam and water
Plant Siting Safety Considerations Buffer zone Location of other hazardous installations in vicinity Inventory of toxic and hazardous materials Adequacy of firefighting water supply Access to Emergency equipment Availability of emergency response support from adjacent industries and the community Weather extremes and prevailing winds Location of highways, waterways, railroad and airplane corridors Environmental and waste disposal restrictions during emergencies Draining and grade slope Maintenance and inspection
Layers of Safety in Industrial Project
Critical Radiation Levels
Damage Criteria for Explosion Over pressure (bar) Type of damage 0.30Heavy 0.20 to 0.27Rupture of Oil storage tanks Possibility of damage to eardrums (Human) 0.20Steel frame constructions distorted and pulled away from foundations 0.10Repairable damage 0.03Large & small windows usually shattered % window glass broken 0.01Crack of windows
Damage Contours from Pool fire at manifold
Damage Contours from Jetfire at tank farm
Damage Contours from VCE
Toxic Dispersion & Effects Vapor clouds may give rise to large fires, explosions or toxic effects. Other things being equal, toxic gas clouds are likely to be dangerous at much greater distances from the point of release than their flammable counterparts. Dispersion is the process through which gases can travel long distances. Two types of dispersion occur in industrial situations.
Types of Dispersion A distinction between different types of dispersion is made for the use of suitable models. It is based on the type of material Dispersions DenseNeutral
Consequences from Toxic Gas Dispersion A large toxic release may give rise to the following effects on human beings: lethal injury non-lethal injury Irritation Toxic gas releases may cause domino effects by rendering adjacent plants inoperable and injuring operators. Prevention/mitigation by provision of automatic control systems using inherently safer principles and a suitable control room
Large Toxic Release The main mode of exposure is inhalation The effects of a toxic release are estimated knowing the relationship between the concentration-time profile and the degree of injury The product C of concentration and the time of exposure t, is called dosage and is directly calculated from the dispersion equation
Exposure Limits Three agencies provide information regarding exposure limits, specifying safe levels of air borne contaminants OSHA The National Institute of Occupational Safety (NIOSH) and The American Conference of Governmental Industrial Hygienists (ACGIH) These 3 agencies have established guidelines and specific exposure levels of various contaminants
Protection from Domino/ Cascade Effects Arranging separation distances such that damage to adjacent plants will not occur even in the worst case; Provision of barriers e.g. blast walls, location in strong buildings; Protecting plant against damage; e.g. provision of thicker walls on vessels; Directing explosion relief vents away from vulnerable areas; e.g. other plants or buildings, roadways near site boundaries. However, these measures may not provide practical solutions against missiles, and risk analysis may be required to prove adequate safety.
LPG Terminal Mexico City, Mexico 1984 A major fire and a series of catastrophic explosions occurred at the PEMEX LPG Terminal. After the intial release, the first BLEVE occurred. For the next 90 minutes, a series of BLEVEs followed as other LPG vessels violently exploded. Approximetly 500 people were killed and the facility was destroyed.
Contributing Factors Plant layout - the positioning of vessels Emergency isolation Survivability of critical systems Emergency plan and site access
Guidance values for safe separation distances For prevention of Domino Effects Thermal radiation from fire (Jet/ Flash/ Pool/ Fireball) 12.5 kW/m 2 1% Fatality level 4.5 kW/m 2 Safe for firefighters Overpressure from Explosion (UVCE/ VCE/ BLEVE) 0.1 bar 1% Fatality level
The Criteria for Fatalities
Site Factors to be considered where Risks of release of flammable/ toxic materials exists Plants/Flammable storages should be sited in the open air Locating all high-volume storage of flammable / toxic material well outside process areas; Hazardous area classification (HAC) to designate areas for elimination of ignition sources. Locating hazardous plant away from main roadways through the site; Fitting remote-actuated isolation valves where high inventories of hazardous materials may be released into vulnerable areas; Provision of ditches, dykes, embankments, sloping terrain to contain and control releases & limit safety & environmental effects;
Incident at POL Depot, Jaipur, 29 th Oct 2009, 6:10 pm Liquid Motor Spirit had gushed out, when the tank was being lined up (made ready for pumping to BPCL) because MOV connecting to the tank was also open when the Hammer Blind was in the changeover position Product leaked for 75 minutes tons of MS= 20 tons TNT before explosion took After explosion, fire occurred in 9 of the 11 tanks and the fire continued till the fuel contents were totally burnt KL product burned out in 11 day 11 fatalities, many injured and 280 cr loss
LOSS OF SECONDARY CONTAINMENT Open condition of dyke valve in tank dyke drainage system is connected to storm water drain also which is open to atmosphere, Hydrocarbon entering this allows vapor to spread throughout installation. INADEQUATE MITIGATION MEASURES MOV closure from control room was malfunction Non availability of SCBA No emergency plan for the scenario No emergency responder
Critical factors to be considered in plant layout Location of control room /Protection Fire water tank and fire water pump house Congestion in the plant site because of buildings, structures, pipelines, trees etc. The emergency exit gate shall be away from the main gate and always be available for use for personnel evacuation during emergency. Evacuation routes should not be blocked by poor plant layout Extract from IOC Fire Accident Report 10.5 Plant Layout
Positioning of occupied buildings The distance between occupied buildings and plant buildings( w.r.t dangers of explosion, fire and toxicity). Locate buildings and structures in the upwind direction Congestion in the plant site because of buildings, structures, pipelines, trees etc. All buildings which are not related to terminal operation shall be located outside the plant area. (eg. canteen, ignition sources) Personnel with more general site responsibilities should usually be housed in buildings sited in a non-hazard area near the main entrance. In all cases occupied buildings should not be sited downwind of hazardous plant areas.
HPCL-Vizag refinery explosion 14th September 1997 Fire broke out at 6:15 am, following a suspected leak in the LPG pipeline from the Vizag port to the storage farm. It caused a series of explosions, and soon spread to at least six other naphtha and petrol tanks.
Damages ( HPCL Refinery Fire ) Affected the entire product terminal area, including 11 storage tanks containing naptha, petrol, diesel, kerosene and furnace oil, besides the six ''Horton spheres'' containing LPG. The refinery's administrative building, its canteen and some other buildings came crashing down like a pack of cards Even an earthquake measuring eight on the Richter scale would not have caused so much damage.
What to do in case of Restricted Space- Case study of Fire at IOC filling station (petrol bunk) Gas tanker filling underground tanks of the LPG outlet suddenly caught fire, Caused by leakage of LPG from a nozzle of a gas tanker 3 persons were killed and a dozen others injured The fire engulfed a gas tanker, an electricity transformer and three cars and spread to a nearby multi-storey apartment building. Ignition followed by Fire - spread to nearby houses and burnt trees and damaged electricity poles and wires. Estimate about 12 to 15 tonnes of fuel went up in flames with the fire raging for six hours
IOC LPG Explosion Jaipur - Oct 12,2008 Entire gas station was engulfed in flames Explosion took place in the tanker itself, destroying it completely., the impact of which was felt in the entire Shastri Nagar residential area up to a distance of three kilometres After 15 minutes of the gas that had leaked, the tanker blew off. The rear shell of the tanker had been thrown 250 feet and made a big hole into an building tanker exploded at that time and huge flames that were thrown out of it 350 feet away
Risk Analysis Need to Be Applied Helps in Forecasting any unwanted situation Estimating damage potential of such situation Decision making to assess the suitability of sites Evaluating effectiveness of control measures
IOC LPG Explosion Jaipur - Oct 12,2008
Risk The probability of suffering a harm or loss. A combination of hazard and Probability Risk = Probability of occurrence of hazard X magnitude of hazard Measurement of Risk Individual Risk Societal Risk
Risk Representation Individual Risk Contour 1.0E E E-06
ALARP – As Low As Reasonable Practicable Tolerable only if risk reduction Is impracticable or cost is grossly disproportionate to the improvement gained
Summary & Conclusion Poorly laid out site increases risk of an accident especially in MAH group of Industries Site layout factors should be considered during Plant Layout design phase Risk and Damage contours (based on consequence Analysis) helps to demarcate hazardous areas Risk analysis may be required to decide the project when there is restriction of space. Risk levels criteria as stipulated in IS should be employed to decide the case