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This section covers the types of hazard found in chemical industries, including those due to high pressure and explosions, dust and vapour cloud explosions, vacuum and temperature, inflammable and toxic materials, hazardous chemicals, reactions and operations, electrostatics and ionizing radiation, noise hazards and their effects on personnel and plant operation, and fire and explosion indices and hazard analysis.
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Hazard, Risk and the Control Hierarchy • A hazard is anything with the potential to cause harm; risk is the combination of the likelihood that the harm will occur and the severity of its consequences.
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A hazard cannot be removed by a procedure — only by eliminating or substituting the substance or the operation — whereas risk can be reduced by lowering either likelihood or severity. • The hierarchy of control, in strict order of preference: • 1.
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Elimination — remove the hazard entirely; the only completely reliable measure. • 2.
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Substitution — replace with something less hazardous. • 3.
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Engineering controls — containment, ventilation, interlocks, relief systems; these protect everyone without depending on behaviour. • 4.
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Administrative controls — procedures, permits to work, training, signs, job rotation. • 5.
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Personal protective equipment — the last line of defence, protecting only the wearer, and only if it is correctly selected, fitted, worn and maintained. • Inherently safer design is the modern expression of the top of this hierarchy, and its four principles should be known: minimise (use smaller inventories of hazardous material), substitute (use a less hazardous material or route), moderate (use less severe conditions or dilute forms) and simplify (design out the complexity that causes error).
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The guiding maxim is that what you do not have cannot leak.
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Fire and Flammability • The fire triangle requires fuel, oxygen (oxidiser) and an ignition source; the fire tetrahedron adds the chemical chain reaction, which is what halon and dry powder extinguishers interrupt.
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Removing any one leg extinguishes the fire, and the three classical methods — starvation, smothering and cooling — correspond to removing fuel, oxygen and heat respectively. • The temperature definitions must be known exactly: • Flash point — the lowest temperature at which a liquid gives off sufficient vapour to form an ignitable mixture that flashes momentarily on application of a flame.
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It is the single most important property for classifying a flammable liquid. • Fire point — a few degrees above the flash point, at which burning continues once started. • Autoignition temperature — the temperature at which the material ignites spontaneously with no external ignition source; it is much higher than the flash point. • Flammability (explosive) limits: a vapour-air mixture burns only between the lower flammable limit (LFL) and the upper flammable limit (UFL).
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Below the LFL the mixture is too lean and above the UFL too rich.
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Widening limits and a low LFL mean a more dangerous material — hydrogen and acetylene have famously wide ranges. • Inerting with nitrogen reduces the oxygen below the limiting oxygen concentration, at which combustion cannot occur whatever the fuel concentration; it is the standard protection for storage tanks and reactors. • Fire classes:
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A ordinary combustibles, B flammable liquids, C flammable gases, D combustible metals, and electrical fires, with class F or K for cooking oils.
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Water must never be used on burning oil (it spreads the fire by boiling violently beneath it), on live electrical equipment or on reactive metals.
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Explosions Event Description Typical cause Deflagration Combustion front travels below the speed of sound in the unburnt gas Most ordinary vapour and dust explosions Detonation Front travels above the speed of sound, producing a shock wave and far greater damage Confined explosions, sensitive materials, deflagration-to-detonation transition in long pipes Confined vapour cloud explosion Ignition inside a vessel or building; pressure rises rapidly with nowhere to vent Leak into an enclosure Unconfined vapour cloud explosion (UVCE) A large release forms a drifting cloud that ignites in the open, producing blast overpressure Major loss of containment of a flashing liquid or gas Flash fire The same cloud burns without significant overpressure Smaller release or low congestion BLEVE Boiling liquid expanding vapour explosion: a vessel of liquid above its atmospheric boiling point fails, the contents flash instantly and, if flammable, form a fireball Fire impingement on the vapour space of an LPG vessel, weakening the shell Dust explosion Suspended combustible dust ignites; often a small primary blast raises settled dust and triggers a far larger secondary explosion Grain, flour, sugar, coal, metal powders, plastics, pharmaceuticals Runaway reaction Heat generation outruns heat removal and the reaction accelerates uncontrollably Loss of cooling, wrong charging, contamination, agitator failure • The dust explosion pentagon adds dispersion in a cloud and confinement to the three legs of the fire triangle.
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The secondary explosion is usually far more destructive than the primary, which is why good housekeeping — preventing dust accumulation on ledges and beams — is the single most effective control.
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A finer dust is more dangerous, because its surface area per unit mass is greater. • A BLEVE is a physical explosion first and a fireball second; it can occur with any liquid held above its atmospheric boiling point, flammable or not.
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Protection is by water cooling of the vessel shell, fireproof insulation, and adequate separation distances. • Pressure hazards: over-pressurisation from blocked outlets, thermal expansion of trapped liquid, external fire, utility failure or runaway reaction is guarded by relief valves and bursting discs discharging to a safe place.
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Vacuum is equally dangerous and is more often overlooked: a tank that is drained or steam-cleaned and then cooled without an adequate vacuum breaker will collapse, and vessels are far weaker in vacuum than in pressure — a favourite examination point. • Temperature hazards include thermal stress, loss of strength at high temperature, and brittle fracture at low temperature, where a steel that is ductile at ambient becomes brittle below its transition temperature — relevant wherever cryogenic or auto-refrigerating fluids are handled.
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Toxic, Electrostatic and Radiation Hazards • Routes of entry are inhalation (the principal industrial route), skin absorption and contact, ingestion, and injection through a wound. • Exposure limits:
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TLV-TWA is the time-weighted average for an eight-hour day and forty-hour week;
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TLV-STEL is a fifteen-minute short-term limit;
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TLV-C is a ceiling that must never be exceeded even momentarily; and IDLH is the concentration immediately dangerous to life or health.
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LD₅₀ and LC₅₀ are the dose and concentration lethal to half a test population — a lower value therefore means a more toxic substance, which is regularly inverted by mistake. • Acute effects appear rapidly after a single exposure; chronic effects develop slowly after repeated exposure at levels too low to cause acute symptoms, and include carcinogenic, mutagenic and teratogenic effects.
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Asphyxiants are divided into simple (displacing oxygen, such as nitrogen and carbon dioxide) and chemical (interfering with oxygen transport or use, such as carbon monoxide and hydrogen cyanide).
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Nitrogen asphyxiation in confined spaces is one of the commonest causes of industrial fatality precisely because nitrogen gives no warning at all. • The Safety Data Sheet (SDS), in its sixteen-section format, is the primary source of hazard information, and the Globally Harmonized System (GHS) standardises classification, pictograms and the signal words Danger and Warning. • Electrostatic hazards arise wherever a non-conducting liquid flows through a pipe, is splash-filled into a tank, or a powder is pneumatically conveyed or poured.
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The charge accumulates and discharges as a spark of enough energy to ignite a flammable atmosphere — and the minimum ignition energy of a vapour is only a fraction of a millijoule, far below what a person can feel.
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Control is by bonding and earthing all conductive equipment, limiting fill velocity, bottom filling rather than splash filling, using antistatic additives, and inerting.
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Note that earthing protects only conductive items; a plastic container or a non-conductive liquid cannot be earthed, which is why plastic containers are prohibited for flammable liquids. • Ionizing radiation from level and density gauges, thickness gauges and radiography is controlled on the three principles of time, distance and shielding, with distance following an inverse square law; sources are licensed, interlocked and monitored with film badges or dosimeters. • Noise hazards: prolonged exposure causes permanent, irreversible noise-induced hearing loss, which develops painlessly and is not noticed until it is well advanced; it also causes tinnitus, stress, fatigue and raised blood pressure.
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Operationally it masks alarms and speech, interferes with communication, and so becomes a cause of accidents in its own right.
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The usual industrial criterion is about 85-90 dBA for an eight-hour day, with the permissible exposure time halving for each 3 dB (or in some systems 5 dB) increase — the exact exchange rate depends on the national regulation, which must be checked.
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Control follows the hierarchy: quieter equipment, enclosure and silencers, then limiting exposure time, and hearing protection last.
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Hazard Analysis Techniques Technique Nature Use HAZOP Systematic, team based, applied line by line with guide words (no, more, less, as well as, part of, reverse, other than) against design intent The standard qualitative study for a complete process; thorough but time consuming What-if / checklist Structured brainstorming against experience Quick screening; simpler processes; early design FMEA Failure mode and effects analysis, component by component, often ranked by a risk priority number Equipment and control system reliability Fault tree analysis Deductive: starts from a defined top event and works down to root causes; quantifiable Determining the probability of a specific accident Event tree analysis Inductive: starts from an initiating event and traces forward through success and failure of each safeguard Assessing the range of possible outcomes Bow-tie Combines a fault tree and an event tree about a central loss-of-containment event Communicating barriers to management and operators LOPA Layer of protection analysis: semi-quantitative check that enough independent layers exist Deciding the required safety integrity level Dow F&EI;
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Fire and explosion index: a numerical score from material factor and penalties for general and special process hazards Ranking units by relative hazard and setting the radius of exposure • HAZOP is the technique most often named in examinations, and its distinguishing features are that it is carried out by a multidisciplinary team, applied systematically node by node, and driven by guide words combined with process parameters to generate deviations from the design intent. • The Dow Fire and Explosion Index starts from a material factor based on flammability and reactivity, applies penalties for general process hazards (exothermic reaction, material handling, enclosure, drainage) and special process hazards (operation within the flammable range, toxic materials, pressure, quantity, corrosion, leakage), and yields an index that is translated into a degree of hazard and a radius of exposure.
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The Mond index extends it to include toxicity.