This disclosure relates to the production of chemicals and plastics using pyrolysis oil from the pyrolysis of plastic waste as a co-feedstock along with a petroleum-based, fossil fuel-based, or bio-based feedstock. In an aspect, the polymers and chemicals produced according to this disclosure can be certified under International Sustainability and Carbon Certification (ISCC) provisions as circular polymers and chemicals at any point along complex chemical reaction pathways. The use of a mass balance approach which attributes the pounds of pyrolyzed plastic products derived from pyrolysis oil to any output stream of a given unit has been developed, which permits ISCC certification agency approval.

Methods for operating a system having two downflow high-severity FCC units for producing products from a hydrocarbon feed includes introducing the hydrocarbon feed to a feed separator and separating it into a lesser boiling point fraction and a greater boiling point fraction. The greater boiling point fraction is passed to the first FCC unit and cracked in the presence of a first catalyst at 500 C. to 700 C. to produce a first cracking reaction product and a spent first catalyst. The lesser boiling point fraction is passed to the second FCC unit and cracked in the presence of a second catalyst at 500 C. to 700 C. to produce a second cracking reaction product and a spent second catalyst. At least a portion of the spent first catalyst or the spent second catalyst is passed back to the first FCC unit, the second FCC unit or both.

Methods for operating a system having two downflow high-severity FCC units for producing products from a hydrocarbon feed includes introducing the hydrocarbon feed to a feed separator and separating it into a lesser boiling point fraction and a greater boiling point fraction. The greater boiling point fraction is passed to the first FCC unit and cracked in the presence of a first catalyst at 500 C. to 700 C. to produce a first cracking reaction product and a spent first catalyst. The lesser boiling point fraction is passed to the second FCC unit and cracked in the presence of a second catalyst at 500 C. to 700 C. to produce a second cracking reaction product and a spent second catalyst. At least a portion of the spent first catalyst or the spent second catalyst is passed back to the first FCC unit, the second FCC unit or both.

The present invention relates to the technical field of petroleum hydrocarbon catalytic conversion, referring to a multi-stage fluidized catalytic reaction process of petroleum hydrocarbon. In the present reaction process, multi-stage reaction takes place in the same reactor, including first order reaction and the second order reaction of FCC feedstock oil, cracking reaction process of light hydrocarbons and/or cycle oil. In the present process, catalyst replacement and two-stage relayed reaction takes place between the first and second order reaction of feedstock oil. Two-stage reaction of light hydrocarbons and/or cycle oil takes place too. These reactions take place in different region in the same one reactor. The first order reaction of light hydrocarbons and/or cycle oil takes place in independent region. In the present invention, catalytic cracking conversion of catalytic feedstock oil, light hydrocarbon and cycle oil takes place in respective reaction region and reaction condition. Multi-stage and stepped selectivity control of catalyst and reaction temperature is realized. Multi-stage reaction and stepped arrangement of temperature is realized in the same reactor. It could improve the yield and selectivity of olefin, and decrease the yield of by-products such as coke obviously.

The present invention relates to the technical field of petroleum hydrocarbon catalytic conversion, referring to a multi-stage fluidized catalytic reaction process of petroleum hydrocarbon. In the present reaction process, multi-stage reaction takes place in the same reactor, including first order reaction and the second order reaction of FCC feedstock oil, cracking reaction process of light hydrocarbons and/or cycle oil. In the present process, catalyst replacement and two-stage relayed reaction takes place between the first and second order reaction of feedstock oil. Two-stage reaction of light hydrocarbons and/or cycle oil takes place too. These reactions take place in different region in the same one reactor. The first order reaction of light hydrocarbons and/or cycle oil takes place in independent region. In the present invention, catalytic cracking conversion of catalytic feedstock oil, light hydrocarbon and cycle oil takes place in respective reaction region and reaction condition. Multi-stage and stepped selectivity control of catalyst and reaction temperature is realized. Multi-stage reaction and stepped arrangement of temperature is realized in the same reactor. It could improve the yield and selectivity of olefin, and decrease the yield of by-products such as coke obviously.

Methods for making higher-octane fuel components from a feed stream of C8+ paraffins, including catalytically cracking the C8+ paraffins using a Zeolite catalyst to produce a reaction product of mid-chain paraffins and olefins and short-chain paraffins and olefins. The reaction product comprises liquid phase paraffins having an increased Octane Value over the feed stream paraffins. The reaction product further comprises a gas phase of short-chain paraffins which are separated from the liquid phase. In embodiments, the short chain olefins are hydrogenated to form mid-chain paraffins and a gas phase containing short-chain paraffins.

Methods for operating a system having two downflow high-severity FCC units for producing products from a hydrocarbon feed includes introducing the hydrocarbon feed to a feed separator and separating it into a lesser boiling point fraction and a greater boiling point fraction. The greater boiling point fraction is passed to the first FCC unit and cracked in the presence of a first catalyst at 500 C. to 700 C. to produce a first cracking reaction product and a spent first catalyst. The lesser boiling point fraction is passed to the second FCC unit and cracked in the presence of a second catalyst at 500 C. to 700 C. to produce a second cracking reaction product and a spent second catalyst. At least a portion of the spent first catalyst or the spent second catalyst is passed back to the first FCC unit, the second FCC unit or both.

Methods for operating a system having two downflow high-severity FCC units for producing products from a hydrocarbon feed includes introducing the hydrocarbon feed to a feed separator and separating it into a lesser boiling point fraction and a greater boiling point fraction. The greater boiling point fraction is passed to the first FCC unit and cracked in the presence of a first catalyst at 500 C. to 700 C. to produce a first cracking reaction product and a spent first catalyst. The lesser boiling point fraction is passed to the second FCC unit and cracked in the presence of a second catalyst at 500 C. to 700 C. to produce a second cracking reaction product and a spent second catalyst. At least a portion of the spent first catalyst or the spent second catalyst is passed back to the first FCC unit, the second FCC unit or both.

A method for upgrading a hydrocarbon feed is disclosed. The method may be carried out in a pyrolysis furnace that may have at least two coils and at least two thermal zones. The method may include two operating or run modes that may be repeated in a cycle. In one run, upgrading may be carried out in one coil while decoking may be carried out in the other coil. After a predetermined amount of time, the streams of the two coils may be switched for a second run, such that decoking may be carried out in the coil in which upgrading was done in the first run and upgrading may be carried out in the coil in which decoking was done in the first run. The first and the second run are cyclically repeated one after the other.

The present invention relates to Delayed Coking of heavy petroleum residue producing petroleum coke and lighter hydrocarbon products. The invented process utilizes a pre-cracking reactor for mild thermal cracking of the feedstock and intermediate multistage separation system before being subjected to higher severity thermal cracking in delayed coking process, resulting in reduction in overall coke yield.