| Fluid Catalytic Cracking (FCC) | Fluidized zeolite catalyst with matrix engineering and attrition control | Y-type zeolite, silica-alumina matrix, kaolin, rare-earth or other stabilizing additives | Vacuum gas oil and selected residue feeds | Riser outlet commonly about 480–550°C; catalyst regeneration about 650–750°C | Converts heavy hydrocarbons into gasoline, LPG, light olefins and cycle oil | Conversion, gasoline yield, propylene yield, coke selectivity, hydrothermal stability and attrition resistance |
| Hydrodesulfurization (HDS) | Supported sulfide hydrotreating catalyst with pore-size and acidity optimization | Cobalt–molybdenum or nickel–molybdenum sulfide on alumina; nickel–tungsten for more severe service | Naphtha, kerosene, diesel, vacuum gas oil and residue streams | Approximately 300–420°C and 15–130 bar hydrogen pressure, depending on feed and product target | Removes sulfur and reduces nitrogen, metals and unstable compounds | Sulfur removal, hydrogen consumption, catalyst cycle length, pressure drop and resistance to feed contaminants |
| Hydrocracking | Bifunctional hydrocracking catalyst combining hydrogenation and acidic cracking sites | Nickel–molybdenum, nickel–tungsten or noble metals on zeolite and amorphous silica-alumina supports | Vacuum gas oil, deasphalted oil and other heavy distillates | Approximately 350–450°C and 70–200 bar hydrogen pressure | Produces high-quality diesel, jet fuel, naphtha and base-oil feedstocks | Conversion, middle-distillate selectivity, product quality, nitrogen tolerance and catalyst stability |
| Naphtha Catalytic Reforming | Bimetallic reforming catalyst with controlled acidity and metal dispersion | Platinum–rhenium or platinum–tin on chlorided alumina | Hydrotreated heavy naphtha | Approximately 480–540°C and 5–35 bar, depending on process configuration | Raises octane number and generates hydrogen and aromatics | Reformate octane, hydrogen yield, coke formation, metal dispersion and regeneration interval |
| Naphtha Isomerization | Chlorinated alumina or zeolite-based bifunctional isomerization catalyst | Platinum with chlorinated alumina, or platinum supported on zeolite | Light straight-chain C5/C6 naphtha | Approximately 120–250°C, with hydrogen co-feed in many configurations | Converts normal paraffins into higher-octane branched isomers | Octane improvement, C5/C6 conversion, chlorine or moisture tolerance and product yield |
| Alkylation | Strong-acid catalyst technology for low-vapor-pressure, high-octane blending components | Sulfuric acid or hydrofluoric acid; solid-acid alternatives are also under development | Isobutane and light olefins, mainly butenes | Sulfuric-acid units commonly operate near 0–15°C; hydrofluoric-acid units commonly operate near 20–40°C | Produces alkylate for clean, high-octane gasoline blending | Alkylate octane, acid consumption, selectivity, corrosion control and operator safety |
| Residue Upgrading and Demetallization | Guard-bed and hydrotreating catalyst systems designed for metals, asphaltenes and Conradson carbon | Nickel–molybdenum or cobalt–molybdenum sulfides on alumina with graded pore structures | Atmospheric residue, vacuum residue and heavy oil fractions | Approximately 350–430°C and 100–200 bar hydrogen pressure | Removes sulfur, nickel, vanadium and other contaminants before downstream conversion | Demetallization, desulfurization, sediment control, pressure-drop management and run length |
| Selective Catalytic Reduction of Refinery Emissions | Fixed-bed or honeycomb SCR catalyst for nitrogen-oxide abatement | Vanadium–titanium oxide or metal-exchanged zeolite formulations | Flue gas from boilers, heaters, FCC regenerators and other combustion sources | Typically about 200–450°C, depending on catalyst formulation and gas composition | Converts nitrogen oxides into nitrogen and water using ammonia or urea-derived ammonia | NOx removal efficiency, ammonia slip, sulfur tolerance, dust resistance and service life |