A process for producing light olefins comprising thermal cracking. Hydrocracked streams are thermally cracked in a steam cracker to produce light olefins. A pyrolysis gas stream is separated into a light stream and a heavy stream. A light stream is separated into an aromatic naphtha stream and a non-aromatic naphtha stream. The aromatics can be saturated and thermally cracked. The integrated process may be employed to obtain olefin products of high value from a crude stream.

A process for producing light olefins comprising thermal cracking. Hydrocracked streams are thermally cracked in a steam cracker to produce light olefins. A pyrolysis gas stream is separated into a light stream and a heavy stream. A light stream is separated into an aromatic naphtha stream and a non-aromatic naphtha stream. The aromatics can be saturated and thermally cracked. The integrated process may be employed to obtain olefin products of high value from a crude stream.

In a method and system for treating a catalytic cracking gasoline, a catalytic cracking process, or a plant employs a fluidized reactor to carry out hydrodealkylation treatment on a catalytic cracking oil gas or catalytic cracking gasoline, so that heavy aromatics present therein can be efficiently converted into light olefins and light aromatics. The method and system can improve the yield of light olefins, allow a long-period stable operation, relieve the contradiction between supply and demand of light aromatics, and solve the problem of high content of heavy aromatics that have low value and are difficult to be utilized in aromatics present in oil gas from catalytic cracking units.

In a method and system for treating a catalytic cracking gasoline, a catalytic cracking process, or a plant employs a fluidized reactor to carry out hydrodealkylation treatment on a catalytic cracking oil gas or catalytic cracking gasoline, so that heavy aromatics present therein can be efficiently converted into light olefins and light aromatics. The method and system can improve the yield of light olefins, allow a long-period stable operation, relieve the contradiction between supply and demand of light aromatics, and solve the problem of high content of heavy aromatics that have low value and are difficult to be utilized in aromatics present in oil gas from catalytic cracking units.

The present invention concerns a process for the production of light olefins and BTX using a catalytic cracking unit, NCC, processing a naphtha type feed, and an aromatics complex. It can be used to exploit the synergies between these two units. The thermal balance of the NCC, which is intrinsically deficient in coke, is resolved by the optimal use of heat from the reforming furnaces in order to preheat the feed for the NCC, and by introducing at least a portion of the raffinate obtained from the aromatics complex as a mixture with the naphtha.

The present invention concerns a process for the production of light olefins and BTX using a catalytic cracking unit, NCC, processing a naphtha type feed, and an aromatics complex. It can be used to exploit the synergies between these two units. The thermal balance of the NCC, which is intrinsically deficient in coke, is resolved by the optimal use of heat from the reforming furnaces in order to preheat the feed for the NCC, and by introducing at least a portion of the raffinate obtained from the aromatics complex as a mixture with the naphtha.

A process for upgrading a naphtha feed includes separating the naphtha feed into at least a light naphtha fraction, contacting the light naphtha fraction with hydrogen in the presence of at least one cyclization catalyst, and contacting the cyclization effluent with at least one cracking catalyst. Contacting the light naphtha fraction with hydrogen in the presence of at least one cyclization catalyst may produce a cyclization effluent comprising a greater concentration of naphthenes compared to the light naphtha fraction. Contacting the cyclization effluent with at least one cracking catalyst under conditions sufficient to crack at least a portion of the cyclization effluent may produce a fluid catalytic cracking effluent comprising light olefins, gasoline blending components, or both. A system for upgrading a naphtha feed includes a naphtha separation unit, a cyclization unit disposed downstream of the naphtha separation unit, and a fluid catalytic cracking unit disposed downstream of the cyclization unit.

A process for upgrading a naphtha feed includes separating the naphtha feed into at least a light naphtha fraction, contacting the light naphtha fraction with hydrogen in the presence of at least one cyclization catalyst, and contacting the cyclization effluent with at least one cracking catalyst. Contacting the light naphtha fraction with hydrogen in the presence of at least one cyclization catalyst may produce a cyclization effluent comprising a greater concentration of naphthenes compared to the light naphtha fraction. Contacting the cyclization effluent with at least one cracking catalyst under conditions sufficient to crack at least a portion of the cyclization effluent may produce a fluid catalytic cracking effluent comprising light olefins, gasoline blending components, or both. A system for upgrading a naphtha feed includes a naphtha separation unit, a cyclization unit disposed downstream of the naphtha separation unit, and a fluid catalytic cracking unit disposed downstream of the cyclization unit.

A process for treatment of PFO from a steam cracking zone includes selectively hydrogenating PFO or a portion thereof for conversion of polyaromatics compounds contained in the PFO into aromatic compounds with one benzene ring to produce a selectively hydrogenated stream. The selectively hydrogenated stream is reacted in a fluid catalytic cracking reactor for selective ring opening and dealkylation to produce fluid catalytic cracking including light cycle oil. In addition, a naphtha reformer is integrated, so that light cycle oil and a reformate stream are separated into BTX compounds. Optionally the PFO is separated into a first stream containing C9+ aromatics compounds with one benzene ring, and a second stream containing C10+ aromatic compounds, whereby the first stream containing C9+ aromatics compounds with one benzene ring is passed to the fluid catalytic cracking reactor, and the feed to the selective hydrogenation step comprises all or a portion of the second stream containing C10+ aromatic compounds.

Systems and methods for processing full range naphtha to produce light olefins are disclosed. The systems and methods include separating the full range naphtha into a light naphtha stream and a heavy naphtha stream and integrating a catalytic cracking with a naphtha reforming to process the light naphtha and heavy naphtha streams.