Structured packing is highly relevant to post-combustion CO₂ capture because large near-atmospheric flue-gas flows require extensive gas-liquid contact while keeping absorber pressure drop and fan energy under control. Industrial-scale performance depends strongly on solvent distribution across large tower diameters, bed segmentation, amine condition, flue-gas cleanliness, wash and mist-control sections, temperature profile, and installation quality. Packing surface area should therefore be balanced against hydraulic capacity rather than maximized in isolation.

Pressure-swing distillation uses two different operating pressures to separate pressure-sensitive azeotropic mixtures without an added entrainer. Although both columns handle the same chemical system, their structured-packing requirements may differ because pressure changes vapor density, temperature, vapor-liquid equilibrium, reflux, recycle and hydraulic loading. Packing selection should therefore be performed for each column and packed section independently before deciding whether one packing specification can be standardized across the complete system.

Reactive distillation combines chemical reaction and vapor-liquid separation, so different sections of the same tower may require different internals. Conventional structured packing is often suitable for rectification and stripping zones, while a solid-catalyst reaction zone may require dedicated catalytic packing or catalyst-retention internals. Selection should consider reaction heat, residence time, liquid distribution, section-specific vapor and liquid loads, catalyst handling, pressure drop, fouling and maintenance access.

Structured packing can become difficult to operate in polymerizing or resin-forming service because deposits gradually narrow its ordered flow channels, increase liquid holdup and pressure drop, and create vapor and liquid maldistribution. High-specific-area packing deserves particular caution where polymer formation is known. Packing selection should consider temperature history, inhibitor control, deposit location, cleaning method, differential-pressure trend and required operating run length in addition to normal mass-transfer and hydraulic performance.

Structured packing in azeotropic distillation must be selected around the complete entrainer recycle system, not only the main feed. Overhead condensation, decanter phase separation, reflux composition, water balance and entrainer circulation can substantially change liquid loading and wetting in the packed column. Hydraulic checks should therefore use section-specific vapor and liquid loads, while retrofit projects should evaluate the condenser, decanter and recycle loop before assuming that packing is the capacity bottleneck.