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: 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: Embodiments of the invention provide a method for the fluid catalytic cracking of a heavy hydrocarbon feedstock. According to at least one embodiment, the method includes supplying the heavy hydrocarbon feedstock to a reaction zone having a catalyst, such that both the heavy hydrocarbon feedstock and the catalyst are in contact in a down-flow mode, wherein said contact between the heavy hydrocarbon feedstock and the catalyst takes place in a fluidized catalytic cracking apparatus having a separation zone, a stripping zone, and a regeneration zone. The method further includes maintaining the reaction zone at a temperature of between 500 and 600° C., such that the hydrocarbon feedstock converts into a cracked hydrocarbon effluent comprising light olefins, gasoline, and diesel.

Abstract: Embodiments of the invention provide a method for the fluid catalytic cracking of a heavy hydrocarbon feedstock. According to at least one embodiment, the method includes supplying the heavy hydrocarbon feedstock to a reaction zone having a catalyst, such that both the heavy hydrocarbon feedstock and the catalyst are in contact in a down-flow mode, wherein said contact between the heavy hydrocarbon feedstock and the catalyst takes place in a fluidized catalytic cracking apparatus having a separation zone, a stripping zone, and a regeneration zone. The method further includes maintaining the reaction zone at a temperature of between 500 and 600° C., such that the hydrocarbon feedstock converts into a cracked hydrocarbon effluent comprising light olefins, gasoline, and diesel.

Abstract: A fluid catalytic cracking catalyst for increased production of propylene and gasoline from heavy hydrocarbon feedstock, the catalyst comprising between 10 and 20% by weight of an ultra-stable Y-type zeolite, between 10 and 20% by weight of a phosphorous modified sub-micron ZSM-5, between 20 and 30% by weight of a pseudoboehmite alumina, and between 30 and 40% by weight kaolin.

Abstract: The method of making diethylbenzene selectively produces diethylbenzene by reacting ethylbenzene and ethanol over a zeolite catalyst, such as ZSM-5. The zeolite catalyst is first heated in argon gas within a reaction chamber. The zeolite catalyst is then selectively coked with a precursor mixture of ethylbenzene and ethanol. Argon gas is then flowed over the coked zeolite catalyst, and a reaction mixture of ethylbenzene and ethanol is injected into the reaction chamber to produce diethylbenzene, which is then removed from within the reaction chamber.

Abstract: The zeolite catalyst is provided for the alkylation of toluene with methanol to selectively produce styrene and ethylbenzene. The zeolite catalyst is an X-type zeolite modified sequentially, first by ion-exchange with alkali metals, such as cesium, to replace all exchangeable sodium from the zeolite, and then by mixing the modified zeolite with borate salts of a metal such as lanthanum, zirconium, copper, zinc or the like. The initial zeolite composition has a Si to Al molar ratio of approximately 1 to 10, and is preferably either zeolite X or zeolite 13X. The zeolite composition is ion-exchanged with cesium to replace at least 50% of the exchangeable sodium in the zeolite composition. The ion-exchanged zeolite composition is then mixed with a borate salt to form the zeolite catalyst for the alkylation of toluene with methanol for the selective production of styrene and ethylbenzene.

Abstract: The method of making diethylbenzene selectively produces diethylbenzene by reacting ethyibenzene and ethanol over a zeolite catalyst, such as ZSM-5. The zeolite catalyst is first heated in argon gas within a reaction chamber. The zeolite catalyst is then selectively coked with a precursor mixture of ethylbenzene and ethanol. Argon gas is then flowed over the coked zeolite catalyst, and a reaction mixture of ethylbenzene and ethanol is injected into the reaction chamber to produce diethylbenzene, which is then removed from within the reaction chamber.

Abstract: The zeolite catalyst is provided for the alkylation of toluene with methanol to selectively produce styrene and ethylbenzene. The zeolite catalyst is an X-type zeolite modified sequentially, first by ion-exchange with alkali metals, such as cesium, to replace all exchangeable sodium from the zeolite, and then by mixing the modified zeolite with borate salts of a metal such as lanthanum, zirconium, copper, zinc or the like. The initial zeolite composition has a Si to Al molar ratio of approximately 1 to 10, and is preferably either zeolite X or zeolite 13X. The zeolite composition is ion-exchanged with cesium to replace at least 50% of the exchangeable sodium in the zeolite composition. The ion-exchanged zeolite composition is then mixed with a borate salt to form the zeolite catalyst for the alkylation of toluene with methanol for the selective production of styrene and ethylbenzene.

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: The dual-zeolite catalyst for production of ethylbenzene is formed by mixing at least two different zeolites selected from mordenite, beta, ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, MFI topology zeolite, NES topology zeolite, EU-1, SAPO-5, SAPO-34, SAPO-11 and MAPO-36 zeolites and an inactive alumina binder. The two zeolites have different topology and possess dissimilar and unique physical and chemical characteristics, including particle size, surface area, pore size and acidity. The preferred amount of the two zeolites may range from 10 to 90 wt % of the total catalyst amount in the final dried and calcined form, preferably the zeolites are in equal parts by weight.

Abstract: The dual-zeolite catalyst for production of ethylbenzene is formed by mixing at least two different zeolites selected from mordenite, beta, ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, MFI topology zeolite, NES topology zeolite, EU-1, SAPO-5, SAPO-34, SAPO-11 and MAPO-36 zeolites and an inactive alumina binder. The two zeolites have different topology and possess dissimilar and unique physical and chemical characteristics, including particle size, surface area, pore size and acidity. The preferred amount of the two zeolites may range from 10 to 90 wt % of the total catalyst amount in the final dried and calcined form, preferably the zeolites are in equal parts by weight.

Abstract: The process for conversion of alkanes to aromatics includes the steps of contacting a feedstock containing alkanes having between two and six carbon atoms per molecule with a composite catalyst to produce an aromatization reaction, and collecting aromatics produced by the reaction. The composite catalyst is a zeolite having a matrix impregnated with a noble metal and an oxide of a transition metal. The noble metal may be Pt, Pd, Rh, Ru, or Ir. The transition metal may be Fe, Co, Ni, Cu, or Zn. The zeolite may be a medium or large pore zeolite, and may have an MFI, MEL, FAU, TON, VPI, MFL, AEI, AFI, MWW, BEA, MOR, LTL, or MTT structure, preferably MFI. The zeolite framework may include silicon, aluminum, and/or gallium. The matrix may be an oxide of magnesium, aluminum, titanium, zirconium, thorium, silicon or boron, and is preferably alumina.