Hydrocarbon By Dehydrogenation TRIZ Cases

Cold sulfuric acid extracts cyclopentadiene to prevent co-dimer contamination and reduce catalyst deactivation during industrial production.

A dehydrogenation catalyst uses a platinum-tin alloy structure distributed across the alumina carrier to maintain consistent metal ratios.

A hybrid catalyst bed system maintains optimal temperatures during alkane dehydrogenation cycles through internal heat generation and active stream cooling.

A dual feed oxidative dehydrogenation reactor supplies butene and oxygen in separate streams to a catalyst fixed bed.

Counter-current flow between feedstock and particulate catalyst minimizes C4− byproduct formation while extending catalyst lifespan.

A Mo-V-Nb-Te catalyst enables ethane dehydrogenation without oxygen co-feed.

A gallium-cerium catalyst composition enables hydrocarbon dehydrogenation via sol-gel synthesis.

A NiZn alloy core encapsulated by a ZnO shell prevents reduction deactivation during propane conversion.

Homogeneous alkyl titanate catalysis converts ethylene to n-butenes with high purity, avoiding isobutene by-products and complex separation steps.

Optimized acidity and platinum ratios suppress coke formation, enabling lower hydrogen usage to improve process yield.

Segmented impregnation of a high chromium eta-alumina catalyst resolves thermal degradation issues during alkane dehydrogenation.

A composite dehydrogenation catalyst converts cyclohexane into benzene and paraffins using Group 14 and Group 6 to 10 metals.

Using hydrogen-rich supplemental fuel during catalyst regeneration prevents hydrocarbon-induced deactivation, maintaining activity and reducing inventory.

A thermal radiative catalytic system converts saturated hydrocarbons to unsaturated products using combined heat and light from a reaction furnace.

A process divides dehydrogenated LPG intermediates into two portions to produce C5 and C9 aldehydes via parallel hydroformylation.

A gallium oxide catalyst with aluminum and cerium oxides converts alkanes to alkenes.

Dehydrating renewable alcohols into olefins to produce flexible hydrocarbon streams, eliminating petroleum extraction and associated environmental damage.

Segmented gallium catalyst layers with internal heating boost aromatic yields from light hydrocarbons, overcoming low conversion rates.

A catalytic alcohol dehydrogenation heat sink absorbs thermal energy from onboard electronics through an endothermic reaction.

Dehydrogenating light paraffins to acetylene for conversion with methanol into aromatic compounds.

A model-supported predictive controller manages compressor suction pressure in acetylene production plants.

Fluorination of bound zeolite supports improves hydrocarbon conversion efficiency and selectivity for aromatic compounds.

Iron-doped alkane dehydrogenation catalysts restore activity through rapid oxygen exposure, cutting regeneration time by 10% compared to undoped systems.

Elevated reaction pressure and space velocity in a fluidized bed reactor increase light olefin yield while reducing plant size and investment costs.

Fast fluidization regime olefin production maintains catalyst activity through continuous regeneration, reducing fuel consumption by 10-15%.

Reduction pretreatment of alumina catalysts improves olefin selectivity and yield while lowering energy consumption in fluidized bed processes.

Adsorbents and membranes separate olefins from methane streams, eliminating cryogenic distillation energy costs.

A moving bed reactor uses a heat exchanger to supply delta enthalpy for hydrocarbon conversion without direct catalyst contact.

A multi-component catalyst bed mixes reaction-specific catalysts with heat-generating materials to drive endothermic hydrocarbon conversion.

A supported polymetallic oxide tandem catalyst couples direct dehydrogenation with selective hydrogen combustion at the nano-scale.

An integrated process combines propane dehydrogenation with propene epoxidation using thermally coupled rectification columns.

Independent oxygen and nitrogen introduction into the reactor enables precise ratio regulation, minimizing active component loss in purge streams.

A hydrogenation reactor design ensures uniform feed distribution across a catalyst bed to enhance reaction efficiency and selectivity.

Azeotropic vaporization recovers heat from splitter overheads to generate process steam for styrene production.

A chromium-on-alumina dehydrogenation catalyst uses ascorbic acid impregnation to reduce carcinogenic hexavalent chromium levels.

Merges dehydrogenation and alkylation units to route waste steam for heating, eliminating refrigeration needs and reducing energy costs.

A metal oxide catalyst system enables propylene production from paraffins through selective dehydrogenation reactions.

Turbine exhaust heats catalyst beds to convert acyclic C5 feedstock into cyclic compounds while minimizing byproduct formation.

A modified Pt/Kβ molecular sieve catalyst enhances aromatic hydrocarbon selectivity through controlled acidity and mesoporous structure.

A hydrocarbon mixture containing acetylene, butenyne, and dimethyl butadiyne remains stable at elevated pressures without solvent storage.

A counter-current fluidized bed reactor uses downward catalyst flow to drive endothermic dehydrogenation.

Supported metal catalyst with synergistic sites uses trinuclear transition metal-sulfur clusters to anchor active cations on large-pore alumina.

Model-supported predictive controllers regulate compressor suction pressure to prevent shutdowns from abrupt mass flow changes.

Hydrothermal synthesis produces pure M1 phase MoVNbTe mixed oxide catalysts with reduced niobium and tellurium content.