| Fluid Catalytic Cracking (FCC) | Rare-earth stabilized Y or ultra-stable Y zeolite in a silica–alumina matrix | USY or REY zeolite, amorphous silica–alumina, clay and alumina matrix | Regenerator: approximately 650–750°C; riser contact time: about 1–3 seconds | Gasoline yield commonly 40–55 wt% of feed; conversion often 65–80%, depending on feed quality and severity | High activity, good coke tolerance and flexible product selectivity for vacuum gas oil feeds | Metal contamination, nitrogen and heavy feeds can reduce activity and increase coke or dry-gas formation |
| Diesel and Naphtha Hydrotreating | Sulfided transition-metal catalyst on porous alumina | Co–Mo or Ni–Mo sulfide phases supported on γ-alumina | Approximately 300–380°C and 30–130 bar hydrogen pressure | Sulfur removal commonly above 90%; deep desulfurization can exceed 99% with suitable feed, pressure and space velocity | Mature technology, strong commercial availability and adaptable pore structures for different feedstocks | Feed nitrogen, high boiling-point sulfur compounds and metals can inhibit active sites and shorten cycle length |
| Residue Hydrotreating | High-pore-volume hydrotreating catalyst with metals-tolerant support | Ni–Mo or Co–Mo sulfides on alumina, alumina–silica or graded guard-bed support | Approximately 340–420°C and 100–180 bar hydrogen pressure | Sulfur reduction often 50–90%; measurable reductions in metals, Conradson carbon and nitrogen are feed-dependent | Large pores improve access to bulky molecules and help protect downstream catalysts | Rapid deactivation may occur from nickel, vanadium, asphaltenes and coke deposition |
| Hydrocracking | Bifunctional hydrocracking catalyst | Ni–W, Ni–Mo or noble-metal hydrogenation function combined with zeolite or amorphous acidic support | Approximately 350–430°C and 80–180 bar hydrogen pressure | Single-pass conversion commonly 50–95%; high-quality middle-distillate yield depends on conversion mode and feed | Strong conversion of heavy gas oils into jet fuel, diesel and naphtha with simultaneous sulfur reduction | High hydrogen consumption, strict feed pretreatment requirements and sensitivity to nitrogen and metals |
| Catalytic Reforming | Platinum-based reforming catalyst | Platinum with rhenium, tin or another promoter on chlorided alumina | Approximately 480–525°C and 5–35 bar, with continuous hydrogen recycle | Reformate typically reaches approximately 95–105 RON; hydrogen production often ranges from 1,000–2,000 Nm³ per tonne of feed | High octane uplift and valuable refinery hydrogen production | Sensitive to sulfur, nitrogen, water and chloride imbalance; catalyst cost is relatively high |
| C5/C6 Isomerization | Chlorinated alumina or zeolite-based isomerization catalyst | Platinum on chlorided alumina, or platinum on sulfated zirconia or zeolite support | Approximately 120–250°C and 15–35 bar, depending on catalyst system | Octane improvement commonly about 10–25 RON points for suitable light naphtha streams | Improves gasoline octane without increasing aromatic content or requiring substantial hydrogen consumption | Requires very low sulfur, water and benzene levels; equilibrium limits single-pass conversion |
| Selective Catalytic Cracking and Propylene Maximization | Modified Y, ZSM-5 or mixed-zeolite FCC additive | ZSM-5 or related medium-pore zeolite blended with FCC base catalyst | Approximately 500–600°C reactor temperature, depending on unit configuration and feed | Propylene yield may increase by several percentage points, while gasoline yield and octane distribution shift | Useful for adjusting refinery output toward propylene and other light olefins | Higher severity can increase dry gas and coke; results depend strongly on catalyst-to-oil ratio and feed composition |
| Sulfur Recovery | Claus reaction catalyst and tail-gas treatment catalyst | Activated alumina or titanium dioxide for Claus conversion; alumina or titania-based catalysts for tail-gas hydrogenation | Claus catalytic stages commonly operate at approximately 200–350°C | Overall sulfur recovery commonly reaches 95–99.9% when Claus and tail-gas units operate together | Supports emissions compliance and stable conversion of hydrogen sulfide to elemental sulfur | Water, hydrocarbons, ammonia and oxygenated contaminants can reduce activity or cause sulfate formation |