Six absorber types: agitated vessels (batch/continuous), bubble-cap towers (high residence time, low liquid rates), cooler absorbers (external/internal cooling for high heat of absorption), spray towers (droplet contact, entrainment tradeoffs), packed towers (most common, countercurrent gravity drainage), and venturi scrubbers (single-stage, high-solubility gases only).

36-slide design and evaluation guide — trayed vs packed selection (flow parameter Fp thresholds), structured vs random packing rules (tower diameter, liquid rate, pressure drop), packing factor Fp, flood point correlations (Sherwood-type), minimum/maximum liquid wetting rates, liquid distributor types and drip-point density, redistributor spacing, support plate weight limits, and three design methods: Kremser (lean gas), Edmister (multi-component), and HTU/NTU with mass transfer coefficient correlations.

Compression basics (pressure ratio vs capacity tradeoff, heat capacity ratio k, polytropic efficiency). Four types: centrifugal (backward-curved impellers, surge at min flow, choke at max flow), reciprocating (high pressure ratio, interstage cooling), rotary (screw, lobe, sliding vane, liquid piston), and axial (low head, high flow, gas turbines). Vacuum service and driver selection.

Compressor train sizing: pressure ratio and capacity tradeoffs across stages, interstage cooling placement, and polytropic vs isentropic efficiency calculations for driver power sizing.

Film vs dropwise condensation mechanisms and heat transfer coefficient differences. Condensation complications from non-condensable vapor accumulation. Design heuristics for contact condensers (equilibrium temperature basis), dilute isothermal service, and temperature-range service. Source: Chemical Engineers' Condensed Encyclopedia of Process Equipment.

Natural draft (hyperbolic tower, chimney effect, density differential), mechanical draft (induced vs forced fan, crossflow vs counterflow), atmospheric spray, and specialty types (deck-filled, coil-shed). Operating terminology: wet-bulb temperature, cycles of concentration, drift, blowdown, makeup water calculations, plume formation, and acceptance testing. Source: Encyclopedia of Process Equipment.

Nine flow meter types: Venturi, Dall (lower permanent pressure drop), orifice plate (sharp-edge contraction, straight-run requirements), flow nozzle (high Reynolds number), pitot tube, positive displacement (piston meters, batch/blending), mechanical (rotameters), magnetic (Faraday's law, conductive fluids), and ultrasonic/Doppler (suspended solids service). Comparison table and selection criteria.

Three distinct analysis workflows — Design (sizing new equipment from heat duty and temperature requirements to meet performance targets), Rating (predicting actual duty and pressure drop for existing equipment at off-design operating conditions), and Simulation (what-if studies, fouling buildup, startup/shutdown transients, sensitivity analysis across process changes).

Temperature crossover management: single 1-1 pass (TC-proof but velocity-limited), multi-pass shell/tube configurations, and the conditions under which each approach applies. Shell-side vs tube-side fluid assignment rules: corrosive fluids in tubes (easier bundle replacement), dirty fluids in tubes (easier cleaning), condensing fluids in shell, high-pressure service in tubes (thinner vessel walls).

Fouling mechanisms from Bott's Fouling of Heat Exchangers: particulate, crystallization/scaling (supersaturation, nucleation, normal vs. inverse solubility), corrosion, and chemical-reaction fouling, each with where it deposits, upstream prevention, and in-exchanger mitigation. Type-independent best practice (clean upstream service, separation ahead of the exchanger), deposit-growth trends (asymptotic, linear, falling-rate), and the Kern-Seaton asymptotic model R_f(t) = R_f*(1 − e^−t/τ).

Corrosion from Perry's 9th Edition: electrochemistry, Pourbaix passivation diagrams, and polarization; localized corrosion (pitting, crevice, intergranular, galvanic, dealloying); environmentally assisted cracking (SCC, hydrogen embrittlement, liquid-metal embrittlement, corrosion fatigue); high-temperature gaseous corrosion (oxidation, carburization, sulfidation, halogens, nitridation, molten salts); and prevention practice for heat exchangers, towers, tanks, and piping, plus process-environment changes (passivation promotion, deaeration, scale enhancers).

Fixed-roof tanks (flat, conical, dome roof types), floating-roof tanks (pontoon buoyancy design, rim seals for low-boiling liquids, solar boiling prevention), conservation gas holders (variable volume at fixed pressure), and open-top tanks. Tank appliances: conservation vents, hatches, mixers, and their leak exposure. Source: Encyclopedia of Process Equipment.

Souders-Brown K factor (0.15–0.25 ft/s, decreasing at higher pressure) for vessel diameter sizing, height heuristic (H = 4×D baseline), liquid residence time by service (1–3 min clean hydrocarbon, 3–5 min moderate viscosity, 5–10 min dirty/foaming), mist extractor knockdown of entrained liquid, nozzle placement, and independent PIC (vapor)/LIC (liquid) control loops — must not be coupled to avoid interaction.

Cross-equipment heuristics for fast first-pass checks: control valve authority (50–60% of system pressure drop for adequate control), PSV relief scenario selection under API 521 (including high-pressure-into-low-pressure breakthrough evaluation), pump best-efficiency-point tradeoffs (65–95% BEP range, reliability vs. energy consumption), and heat exchanger simulation methods (Dittus-Boelter, Bell-Delaware).

Decision workflow for selecting a thermodynamic property method — Classical (gamma-phi), EOS (phi-phi), or Hybrid — gated on electrolyte presence, liquid-phase ideality (UNIFAC, Kamlet-Taft/Gutmann DN-AN, and Flory-Huggins fallbacks), and pressure vs ~10 bar. Stress-tested and validated against 11 real petrochemical process families from the Meyers Handbook, with per-bucket case-study results and characterization of which systems typically land in each approach.

From GFEDPS Chapter 7 — protection layer hierarchy (ISD → control → active mitigation), electrical area classification (ANSI/NFPA 70 Class I/II/III), SIS/SIL/IPL definitions (IEC 61511), pressure relieving systems, equipment isolation and blowdown, flare systems (API 521), vapor incineration (40 CFR), fire protection modes (HC burning, pyrophoric material), deflagration/detonation arresters, explosion suppression, and dike containment design.

Safeguarding hierarchy (passive → active, decreasing reliability with increasing complexity). ISD strategies applied unit-by-unit: tank reactors (runaway prevention), continuous reactors, mass transfer columns, heat exchangers (tube leak prevention: thermal difference reduction, heat throttle), dryers (combustible dust, multicomponent LEL reduction), pumps (deadheading, cavitation), compressors, fired equipment, piping (40% of LOC incidents, ASME B.31), and utilities.

27-slide study guide from Crawley & Tyler's Guide to Best Practice — ICI origins and 6-stage Hazard Study workflow, guideword/parameter matrix construction, node definition, cause-consequence-safeguard chain evaluation, risk matrix (qualitative), HAZOP team assembly (leader, scribe, discipline members), meeting structure, recording format (dedicated PHA software, sectioned tables), auditing, and training pathways. Handoff to LOPA and MOC covered.

API 521 overpressure scenario identification (closed outlets, cooling/reflux failure, volatile material ingress, overfilling, control failure, fires, tube rupture, utility failure, hydraulic expansion, chemical reactions per DIERS methodology) → governing scenario selection. Vacuum relief evaluation, vapor depressuring design (vessel rupture pressure, failure time, brittle failure temperature), and operator response time thresholds.

From GFEDPS Chapter 8 — three PSI categories under OSHA PSM: Chemical Hazards (MSDS, reactivity, toxicity, explosive limits, heat of combustion), Process Technology (C&E matrix, P&IDs, SIS lifecycle documentation, PHA findings), and Process Equipment (equipment specs, drawings, electrical diagrams, structural analysis). Distinction between design basis, engineering design package, and EDMS-managed equipment files.

Four-step Apollo RCA — Step 1: Problem definition (what/when/significance/impact), Step 2: Reality chart construction (causal chains with action and condition causes; three evidence types: sensed, inferred, testimonial), Step 3: Effective solutions (criteria: prevent recurrence, within control, meets organizational goals; creative thinking methods), Step 4: Implement and track with profitability review to inform future decisions.

26 incident case studies from Kletz's "What Went Wrong" — compressed air oil deposits, aluminum dust explosion (Huntington IN 2003), furnace tube rupture, amine tower BLEVE (17 dead), Longford explosion (Exxon Australia 1998), Feyzin tank BLEVE (TotalEnergies 1966), nitrogen asphyxiation (Union Carbide 1998), HF Puget Sound spill, floating roof tank fire (Wales 1983), water hammer rupture (BP UK 2000), static electricity in powder, check valve backflow, and others with root cause lessons.

Chapter-by-chapter walkthrough of CCPS Guidelines for Hazard Evaluation Procedures (76 slides): incident anatomy and safeguard purpose; study preparation (scope, team, scheduling); hazard identification (inherent hazards, interaction matrices, worst-case consequence); non-scenario methods (PreHA, Safety Review, Relative Ranking, Checklist); scenario methods (What-If, What-If/Checklist, HAZOP, FMEA, Fault Tree with minimum cut sets, Event Tree, Cause-Consequence); the Chapter 6 selection flowchart and MOC hazard reviews; risk-based safeguard adequacy through LOPA; follow-up and action-item resolution; and special applications (procedures, programmable systems, reactivity, human factors, facility siting).

LOPA methodology as a semi-quantitative follow-on to HAZOP — initiating event frequency estimation, independent protection layer (IPL) identification and credit rules, enabling conditions and conditional modifiers, and comparison of mitigated event likelihood against corporate risk criteria to determine required SIL.

Profiles of fifty-nine engineers and scientists behind the methods process engineers use daily: Henry Kister (distillation, Fluor), Ernest Ludwig (Applied Process Design), Alois Kremser and Wayne Edmister (absorption), Max Peters and Ronald West (Plant Design and Economics), Donald Kern (process heat transfer), Igor Karassik (Pump Handbook), Joseph Leung (relief sizing), Thomas Bott and James Knudsen (fouling), Jürgen Gmehling (UNIFAC), Merrel Fenske, A.J.V. Underwood, Mott Souders, Sabri Ergun, Allan Colburn, Thomas Chilton, Lawrence Evans (Aspen Technology), and more, from Bernoulli and Stokes to present-day Perry's section editors.