Abstract: The disclosure provides processes and systems for fluid catalytic cracking of feed streams including hydrocarbons and varying amounts of mixed waste plastic oil to produce valuable petroleum products, such as light olefins and aromatics. The processes generally include providing a waste plastic pyrolysis oil, treating the waste pyrolysis oil reduce a content of one or more of silicon, chlorine, nitrogen, sulfur, and higher olefin components, providing a hydrocarbon stream, combining the hydrocarbon stream with the waste plastic pyrolysis oil to provide a combined feed stream, and feeding the combined feed stream to a fluid catalytic cracking unit having a catalytic cracking catalyst containing a mixture of HZSM-5 and USY.

Abstract: The disclosure provides processes for fluid catalytic cracking of feed streams including hydrocarbons and varying amounts of mixed waste plastic oil to produce valuable petroleum products, such as light olefins. The process generally includes providing a waste plastic pyrolysis oil; passing the waste plastic pyrolysis oil through at least one guard bed configured to adsorb chlorine components; providing a hydrocarbon stream; combining the hydrocarbon stream with the waste plastic pyrolysis oil to provide a combined feed stream; and feeding the combined feed stream, along with steam, to a fluid catalytic cracking unit.

Abstract: Methods for producing propylene by the dehydrogenation of propane are provided. Methods can include introducing a first gas mixture including propane to a dehydrogenation catalyst at a temperature of at least about 570° C., introducing a second gas mixture including steam and air to the dehydrogenation catalyst at a temperature of at least about 550° C., and allowing the second gas mixture to subsist therewith for at least about one hour. Methods can further include introducing a third gas mixture including hydrogen to the dehydrogenation catalyst at a temperature of at least about 500° C.

Abstract: Methods for producing propylene by the dehydrogenation of propane are provided. Methods can include introducing a first gas mixture including propane to a dehydrogenation catalyst at a temperature of at least about 570° C., introducing a second gas mixture including steam and air to the dehydrogenation catalyst at a temperature of at least about 550° C., and allowing the second gas mixture to subsist therewith for at least about one hour. Methods can further include introducing a third gas mixture including hydrogen to the dehydrogenation catalyst at a temperature of at least about 500° C.

Abstract: A method for recovering a product mixture from a waste stream in a diaryl carbonate manufacturing process comprising reacting the waste stream with an alkyl alcohol to form a reaction mixture, and separating the product mixture from the reaction mixture.

Abstract: A method for recovering a product mixture from a waste stream in a diaryl carbonate manufacturing process comprising reacting the waste stream with an alkyl alcohol to form a reaction mixture, and separating the product mixture from the reaction mixture.