Abstract: Embodiments of processes for producing propylene utilize a dual catalyst system comprising a mesoporous silica catalyst impregnated with metal oxide and a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm3/g, and the MFI structured silica catalyst has a total acidity of 0.001 mmol/g to 0.1 mmol/g. The propylene is produced from the butene stream via metathesis by contacting the mesoporous silica catalyst and subsequent cracking by contacting the MFI structured silica catalyst.

Abstract: Embodiments of processes for producing propylene utilize a dual catalyst system comprising a mesoporous silica catalyst impregnated with metal oxide and a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm3/g, and the MFI structured silica catalyst has a total acidity of 0.001 mmol/g to 0.1 mmol/g. The propylene is produced from the butene stream via metathesis by contacting the mesoporous silica catalyst and subsequent cracking by contacting the MFI structured silica catalyst.

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 a metathesis process for producing propylene comprise providing a metathesis catalyst comprising an amorphous mesoporous silica foam impregnated with metal oxides, where the metathesis catalyst has a pore size distribution of at least 3 nm to 40 nm and a total pore volume of at least 0.700 cm3/g. The process further involves producing a product stream comprising propylene by contacting a feed stream comprising butene with the metathesis catalyst.

Abstract: Embodiments of processes for producing propylene utilize a dual catalyst system comprising a mesoporous silica catalyst impregnated with metal oxide and a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm3/g, and the MFI structured silica catalyst has a total acidity of 0.001 mmol/g to 0.1 mmol/g. The propylene is produced from the butene stream via metathesis by contacting the mesoporous silica catalyst and subsequent cracking by contacting the MFI structured silica catalyst.

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 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 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 system and method for conversion of molecular weights of fluids includes an elongate metallic pipe. A fluid is caused to flow through the pipe. A center electrode is mounted within the pipe coaxially with the pipe axis and the flow direction, the electrode being insulated from the pipe wall. The center electrode and the pipe wall are connected to the terminals of a voltage source to create an electric field extending radially between the center electrode and the pipe wall. A source of gamma radiation positioned either within the center electrode or external to the pipe directs gamma rays transverse to the direction of fluid flow. The combined radiation and electric field disrupts chemical bonds, creating ionization zones and resulting in the formation of lower-molecular-weight compounds. Optionally, a magnetic field may be superimposed in the direction of fluid flow.

Abstract: The system and method for conversion of molecular weights of fluids includes an elongate metallic pipe. A liquid, e.g., a hydrocarbon liquid, is caused to flow through the pipe. A center electrode is mounted within the pipe coaxially with the pipe axis and the flow direction, the electrode being insulated from the pipe wall. The center electrode and the pipe wall are connected to the terminals of a voltage source to create an electric field extending radially between the center electrode and the pipe wall. A source of gamma radiation positioned either within the center electrode or external to the pipe directs gamma rays transverse to the direction of fluid flow. The combined radiation and electric field disrupts carbon-sulfur, carbon-hydrogen, and carbon-carbon bonds, creating ionization zones and resulting in the formation of lower molecular weight compounds. Optionally, a magnetic field may be superimposed in the direction of fluid flow.