TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The cracking catalyst comprises a zeolite.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The temperature is greater than or equal to 450 degrees C to less than or equal to 650 degrees C (preferably greater than or equal to 480 degrees C to less than or equal to 560 degrees C). Preferred Components: The lipid-containing feedstock further comprises a hydrocarbon feedstock. The hydrocarbon feedstock comprises a vacuum gas oil, atmospheric residue or vacuum residue. The hydrocarbon feedstock comprises hydrocarbons with an initial boiling point of at least 220 degrees C as measured according to ASTM D-2887. The hydrocarbon feedstock has an initial boiling point of at least 180 degrees C as measured according to ASTM D-2887. The lipid-containing feedstock comprises 2-30 (preferably 5-20) wt.% lipids. EXAMPLE - A batch of marine microalgae of Chlorella species was partially dried and milled. Lipids were then extracted from the marine microalgae using toluene as a solvent in a solvent extraction process. The extracted lipids from Chlorella microalgae had phospholipids (4.5 wt.%), mono-glyceride (4 wt.%), di-glyceride (24 wt.%), tri-glyceride (58 wt.%) and free fatty acid (9 wt.%). A blend of 20 wt.% of these extracted lipids and 80 wt.% of mineral oil derived vacuum gas oil was formed. The metal content in a blend of 20 wt.% of extracted lipids with 80 wt.% mineral oil derived vacuum gas oil (in mg/kg) was Al (50), Ca (73), Fe (50), Mg (635), Mn (10), Na (92), P (370) and Si (52). The lipids obtained above were blended with mineral Vacuum Gas Oil (VGO) to form a first batch of the lipid-containing feedstock comprising 20 wt.% extracted lipids from microalgae and 80 wt.% VGO. The first batch was subjected to catalytic cracking in a small-scale fluidized catalytic cracking reactor. A commercial equilibrium catalyst comprising ultra stable zeolite Y (USY) in an amorphous alumina matrix was used as the cracking catalyst. The reaction temperature was kept at 500 degrees C and the pressure was maintained at 1.1 bar (0.11 MPa). For the feedstock containing 20 wt.% extracted lipids from microalgae and 80 wt.% VGO, a catalyst to oil ratio of about 8 was used. The product stream obtained was separated in a small-scale fractionator and analyzed. To establish the efficacy of the cracking process, the product stream was compared with the products obtained from the cracking of other conventionally used feedstock. VGO was used as the second batch and a blend of 20% rapeseed oil and 80% VGO was used as the third batch. The experiments were conducted in the same fluidized catalytic cracking reactor, except that a different catalyst to oil ratio was used to achieve the constant conversion rate of 67 wt.%. The product yield of each batch of cracking feedstock was calculated at 67 wt.% conversion of the cracking feedstock. The product yields at constant 67 wt.% conversion were: dry gas for first/second/third batch was 1.9/1.9/2; propylene was 2.8/3.3/3.5; LPG was 12/13/13; gasoline was 43.5/46.4/45; LCO was 25.2/26.9/24.6; HCO was 3.2/3.9/3.5; slurry oil was 1.75/2.2/2.1; and coke was 9/5.8/6.9.