Thermal Non-Catalytic Cracking TRIZ Cases

Amine-functionalized solid scavenger removes carbon disulfide from hydrocarbon streams, preventing catalyst deactivation and maintaining product quality.

Uses supercritical water extraction to reduce acidity, viscosity, and impurities in crude oil, preventing corrosion during transport.

An inner plate routes deposition vapor via bypass channels to prevent aperture blockage from condensation.

Hydrocracking feedstock yields liquid effluent for long-distance hydrogen movement, eliminating compression energy and vessel embrittlement.

Counterbore geometries mitigate stress concentration and coking at weld joints to enhance furnace tube durability.

Alternating heat exchangers and economizers prevent coke accumulation without increasing energy consumption.

A steam cracking process quenches cracked gas with liquid hydrocarbons to form a quenching effluent integrated into distillation.

A biomass conversion process produces lower olefins through gasification, Fischer-Tropsch synthesis, and steam cracking.

A dividing wall column fractionates alkylate reactor effluent into iso-butane, n-butane, and alkylate streams.

Ceramic sheaths surround elongated coolant channels to decouple thermal growth mismatches between ceramic and metal components, extending liner lifespan.

Mixing catalyst with feedstock in preheat zone minimizes volatile content and improves coke hardness without excessive vapor cracking.

An autothermal reactor generates steam internally to pyrolytically crack hydrocarbons into olefins.

Vacuum distillation separates pyrolysis oil into lighter and heavier fractions for further processing.

Dynamic catalyst circulation in fluidized bed reactors removes impurities from pyrolysis oils, extending catalyst cycle life and preventing unit shutdowns.

Apparatus uses supercritical water to decompose metal porphyrins, reducing hydrogen consumption and catalyst lifetime issues.

Segmented thermal conversion of vacuum resid prevents fouling in steam cracking furnaces while maintaining high olefin yields.

Hydroextraction removes metals and asphaltenes from residue feedstock, reducing coke formation during catalytic cracking.

Flue gas from a gas turbine superheats dilution steam, reducing energy consumption while generating electricity.

A fluidized bed reactor heats solid refinery residue to devolatilize and crack the feedstock into gaseous hydrocarbons.

Gas-phase thermal cracking removes sulfur and hydrogenates diolefins in C5 raffinate, preventing catalyst deterioration and lowering operational costs.

Hydroprocessing steam cracker naphtha reduces diolefin content, preventing fractionator fouling while maintaining light olefin yield.

Dearomatization separates aromatic hydrocarbons from naphthenic streams, enabling ring opening to boost ethylene yield while reducing fuel production.

Linear ceramic radiants absorb furnace heat and re-radiate it toward shadowed coil areas, improving circumferential temperature uniformity.

Hydroprocessing prepares heavy naphtha for steam cracking, resolving feedstock availability and production suitability trade-offs.

Integrating syngas waste heat recovery with olefins production reduces CO2 emissions and energy input.

Elevating steam cracker coil outlet pressure reduces compressor stages while quench towers condense and separate tar to prevent fouling.

Distilling pyrolysis fuel oil reduces sulfur content and viscosity, enabling low-emission synthesis gas production while recovering valuable aromatics.

Vertical offset between upstream and downstream screens redirects gas flow downward, preventing catalyst fluidization at the bed top.

Converts crude oil fractions into olefins and aromatics via integrated hydroprocessing, reducing feedstock costs.

Shared compressor and warm separator reduce capital costs while maintaining ultra-low sulfur diesel specifications.

Incorporating recycled heavy gas oil into the feedstock resolves the contradiction between maximizing diesel yield and minimizing heavy gas oil output.

Pre-assembling large furnace modules at a fabrication site before transport to the operating location.

Removing molecular hydrogen from pre-heaters prevents coke deposition, extending run-length and lowering maintenance costs.

A primary melting extruder and secondary mixing extruder dissolve polymer waste in fluid oil to create a polymer solution for refinery processing.

Blending aromatic gas oil with coker feed reduces fouling, extending cleaning intervals and maximizing cracked product yield.

A regenerative reactor suspends non-volatiles in liquid pyrolysis feed using a distribution device to maintain flow stability.

A hydrocarbon upgrading process converts olefinic feedstocks into xylenes and light olefins using a methylating agent and catalyst.

Hydrotreating and solvent deasphalting remove contaminants before steam pyrolysis, reducing coke formation while increasing olefin yields from heavy crude.

Converging-diverging geometry mixes superheated steam with heavy feedstock to prevent coking and reduce capital costs.

Real-time impedance monitoring detects sponge coke formation to prevent hot spots and reduce cycle times.

Merges valve assemblies with the reactor structure to reduce pressure drop and cycle time in reverse-flow applications.

Merging separate feedstocks into one processing unit reduces operational costs while maintaining high aromatic and olefin yields.

Multimodal stabilized zirconia refractory prevents stabilizer loss and thermal shock degradation in high-temperature pyrolysis reactors.

A supercritical water treatment process cracks paraffins into linear olefins.

A spirally wound electrical conductor generates magnetic fields parallel to the processing axis.

ZnxZryOz mixed oxide catalyst converts acetic and propionic acid mixtures into isobutene, propylene, and butenes using hydrogen.

An oxide-based redox catalyst converts ethane to ethylene via oxidative dehydrogenation, bypassing energy-intensive steam cracking furnaces.

A cracking furnace system preheats hydrocarbon feedstock using waste heat from cracked gas in a transfer line exchanger before the radiant section.