Abstract: The presently disclosed subject matter relates to methods of producing ethylene and propylene by the catalytic steam cracking of naphtha using an HZSM-5 catalyst. An example method can include providing a naphtha feedstock, providing steam, and providing an HZSM-5 catalyst. The method can further include preparing the HZSM-5 catalyst by titanium modification or alkaline treatment, followed by phosphorus modification. The method can further include feeding the naphtha feedstock and steam to a reactor containing the catalyst and removing an effluent from the reactor having a combined yield of ethylene and propylene of greater than about 45 wt-%.

Abstract: The presently disclosed subject matter relates to methods of producing ethylene and propylene by the catalytic steam cracking of naphtha using an HZSM-5 catalyst. An example method can include providing a naphtha feedstock, providing steam, and providing an HZSM-5 catalyst. The method can further include preparing the HZSM-5 catalyst by titanium modification or alkaline treatment, followed by phosphorus modification. The method can further include feeding the naphtha feedstock and steam to a reactor containing the catalyst and removing an effluent from the reactor having a combined yield of ethylene and propylene of greater than about 45 wt-%.

Abstract: Provided here are zirconium-substituted hierarchical zeolite compositions and methods of preparing such catalytic compositions. One such method involves subjecting the zirconium-substituted zeolite to a framework modification process using a single template to produce a framework-modified zeolite, followed by subjecting the framework-modified zeolite to an ion exchange process to produce a hierarchical zeolite composition. Also provided are methods of catalytic cracking of hydrocarbon feedstocks using these zirconium-substituted hierarchical zeolite compositions.

Abstract: Provided here are zirconium-substituted hierarchical zeolite compositions and methods of preparing such catalytic compositions. One such method involves subjecting the zirconium-substituted zeolite to a framework modification process using a single template to produce a framework-modified zeolite, followed by subjecting the framework-modified zeolite to an ion exchange process to produce a hierarchical zeolite composition. Also provided are methods of catalytic cracking of hydrocarbon feedstocks using these zirconium-substituted hierarchical zeolite compositions.

Abstract: The presently disclosed subject matter relates to methods of producing ethylene and propylene by the catalytic steam cracking of naphtha using an HZSM-5 catalyst. An example method can include providing a naphtha feedstock, providing steam, and providing an HZSM-5 catalyst. The method can further include preparing the HZSM-5 catalyst by titanium modification or alkaline treatment, followed by phosphorus modification. The method can further include feeding the naphtha feedstock and steam to a reactor containing the catalyst and removing an effluent from the reactor having a combined yield of ethylene and propylene of greater than about 45 wt-%.

Abstract: The method of forming a hydrocarbon cracking catalyst provides a method of varying or tuning the mesophase MCM-41 or microporous ZSM-5 properties in biporous ZSM-5/MCM-41 composites, depending on the requirements of the intended application. The method includes the steps of performing a surfactant-mediated hydrolysis of ZSM-5 to form a solution, and then adjusting the pH of the solution to selectively tune the microporous and mesoporous properties of the final ZSM-5/MCM-41 catalyst product. Following tuning, soluble aluminosilicates are hydrothermically condensed to form a mesoporous material over the remaining ZSM-5 particles to form the ZSM-5/MCM-41 composite. The ZSM-5/MCM-41 composite may be used as a hydrocarbon cracking catalyst for cracking gas, oil or the like.

Abstract: A catalyst and a process are provided for oligomerizing ethylene. A heterogeneous catalyst system comprises: (1) a chelating ligand, preferably 2-diphenyl phosphino benzoic acid (DPPBA); (2) a nickel precursor, preferably nickel chloride hexahydrate (NiCl2.6H2O); (3) a catalyst activator, preferably sodium tetraphenylborate (NaBPh4); and (4) silica. A 1:1:1 molar ratio of Ni:DPPBA:BPh4 catalyst components are fixed on a silica support using low-temperature fixation. The catalyst components are dispersed in a diluent, preferably ethanol, and silica is added. The ethanol is evaporated using freeze-drying equipment to form a silica-supported catalyst system. The silica-supported catalyst is slurried in ethanol in a reactor, and ethylene is added. The reactor pressure and temperature are maintained at about 725 psig and 100° C., respectively, for about two hours.