Channel liquid-fuel release · screening and control evidence
Confirm the actual jet-fuel / blend SDS, temperature and mist-generation potential; no product qualification, flash-point margin or ignition assessment is supplied. The former sour-gas H₂S assumptions do not represent Channel’s fuel-terminal service.
Hypothetical liquid-transfer pipe · assumptions
Defaults: 60 barg, 25 mm opening, 800 kg/m³, coefficient 0.62 and 120 seconds. The pressure is reused from the liquid-pressure DEMO; none is a measured release condition or confirmed isolation time. Product choice does not set density or composition.
Optional inventory is a user assumption about the connected, releasable volume, not full pipeline inventory or working tank stock. This cap does not model isolation performance, gravity drainage or continued pump/feed supply.
Illustrative liquid volume over assumed duration
- No inventory cap · constant pressure
This curve does not predict concentration, ignition, fire radiation, toxic exposure, affected people, evacuation distance or environmental consequence. A capped or zero result is not a safety conclusion.
Control evidence · not verified by this screen
Accountable reviewer: Process-safety / integrity engineer. Items below are review requirements, not passed checks or actual barrier states.
Product and phase
Obtain the current SDS, actual product composition, temperature, density and vapour pressure. Confirm whether flashing, mist, dissolved gas or two-phase discharge makes this simple liquid model unsuitable.
Pressure and source inventory
Identify the actual asset and connected equipment; verify pressure history, hydraulic head, isolation boundaries, feed/pump behaviour and uncertainty in releasable inventory.
Approved consequence and control basis
Use the approved loss-of-containment / fire / spill assessment, site emergency plan, consent conditions and relevant performance standards. No generic concentration or distance becomes a site limit here.
Formula, exclusions and source boundary
Q = Cd × A × √(2ΔP/ρ), where Q is m³/s, A = π(d/1,000)²/4 in m², ΔP = gauge pressure × 100,000 Pa and ρ is kg/m³. Potential liquid volume in ML = Q × seconds / 1,000. If entered, inventory-capped allowance = min(potential ML, assumed connected inventory ML). Zero pressure/opening/duration yields a mathematical zero under these assumptions, not evidence of a safe asset.
This hypothetical calculation uses browser assumptions, not sensor, leak-test or inspection records. It assumes single-phase incompressible liquid, a sharp-edged equivalent opening, constant upstream pressure and an atmospheric outlet. It excludes depressurisation, surge, hydrostatic head changes, continued supply, realistic isolation timing, pool spreading, evaporation, flashing, two-phase flow, dispersion, ignition and environmental transport. A competent engineer must establish applicability before using any result in a governed assessment.
Inputs are not saved; no control action, barrier update, notification or work order is issued.