In accordance with one or more embodiments of the present disclosure, a process for converting diesel to products comprising light olefins, benzene-toluene-xylenes (BTX), fluid catalytically cracked naphtha, pyrolysis gasoline, and pyrolysis fuel oil includes: introducing a diesel feedstream to a diesel hydrodesulfurization unit to produce a desulfurized diesel stream; introducing the desulfurized diesel stream to a fluid catalytic cracking (FCC) unit to produce the fluid catalytically cracked naphtha, a light gas stream, and a cycle oils stream; introducing the fluid catalytically cracked naphtha to an aromatic recovery complex to produce the BTX and an aromatic bottoms stream; and introducing a paraffinic fraction of the light gas stream to a steam cracking unit to produce a light olefins stream, the pyrolysis gasoline, and the pyrolysis fuel oil.

In accordance with one or more embodiments of the present disclosure, a process for converting diesel to products comprising light olefins, benzene-toluene-xylenes (BTX), fluid catalytically cracked naphtha, pyrolysis gasoline, and pyrolysis fuel oil includes: introducing a diesel feedstream to a diesel hydrodesulfurization unit to produce a desulfurized diesel stream; introducing the desulfurized diesel stream to a fluid catalytic cracking (FCC) unit to produce the fluid catalytically cracked naphtha, a light gas stream, and a cycle oils stream; introducing the fluid catalytically cracked naphtha to an aromatic recovery complex to produce the BTX and an aromatic bottoms stream; and introducing a paraffinic fraction of the light gas stream to a steam cracking unit to produce a light olefins stream, the pyrolysis gasoline, and the pyrolysis fuel oil.

In accordance with one or more embodiments of the present disclosure, a process for converting diesel to products comprising light olefins, benzene-toluene-xylenes (BTX), fluid catalytically cracked naphtha, pyrolysis gasoline, and pyrolysis fuel oil includes: introducing a diesel feedstream to a diesel hydrodesulfurization unit to produce a desulfurized diesel stream; introducing the desulfurized diesel stream to a fluid catalytic cracking (FCC) unit to produce the fluid catalytically cracked naphtha, a light gas stream, and a cycle oils stream; introducing the fluid catalytically cracked naphtha to an aromatic recovery complex to produce the BTX and an aromatic bottoms stream; and introducing a paraffinic fraction of the light gas stream to a steam cracking unit to produce a light olefins stream, the pyrolysis gasoline, and the pyrolysis fuel oil.

In accordance with one or more embodiments of the present disclosure, a process for converting diesel to products comprising light olefins, benzene-toluene-xylenes (BTX), fluid catalytically cracked naphtha, pyrolysis gasoline, and pyrolysis fuel oil includes: introducing a diesel feedstream to a diesel hydrodesulfurization unit to produce a desulfurized diesel stream; introducing the desulfurized diesel stream to a fluid catalytic cracking (FCC) unit to produce the fluid catalytically cracked naphtha, a light gas stream, and a cycle oils stream; introducing the fluid catalytically cracked naphtha to an aromatic recovery complex to produce the BTX and an aromatic bottoms stream; and introducing a paraffinic fraction of the light gas stream to a steam cracking unit to produce a light olefins stream, the pyrolysis gasoline, and the pyrolysis fuel oil.

A process is described for reducing the level of benzene in a refinery gasoline feed containing benzene and at least one C.sub.5+ olefin, in which the refinery gasoline feed is contacted with a first alkylation catalyst under conditions effective to react at least part of the C.sub.5+ olefin and benzene in the refinery gasoline feed and produce a first alkylation effluent. The first alkylation effluent is separated into at least (i) a first fraction rich in benzene, (ii) a second fraction rich in C.sub.7 to C.sub.12 hydrocarbons and (iii) a third fraction rich in C.sub.13+ hydrocarbons. At least part of the first fraction is contacted with an alkylating agent comprising one or more C.sub.2 to C.sub.4 olefins in the presence of a second alkylation catalyst under conditions effective to produce a second alkylation effluent which has reduced benzene content as compared with the first fraction.

A process is described for reducing the level of benzene in a refinery gasoline feed containing benzene and at least one C.sub.5+ olefin, in which the refinery gasoline feed is contacted with a first alkylation catalyst under conditions effective to react at least part of the C.sub.5+ olefin and benzene in the refinery gasoline feed and produce a first alkylation effluent. The first alkylation effluent is separated into at least (i) a first fraction rich in benzene, (ii) a second fraction rich in C.sub.7 to C.sub.12 hydrocarbons and (iii) a third fraction rich in C.sub.13+ hydrocarbons. At least part of the first fraction is contacted with an alkylating agent comprising one or more C.sub.2 to C.sub.4 olefins in the presence of a second alkylation catalyst under conditions effective to produce a second alkylation effluent which has reduced benzene content as compared with the first fraction.

Optimizing power generation from waste heat in large industrial facilities such as petroleum refineries by utilizing a subset of all available hot source streams selected based, in part, on considerations for example, capital cost, ease of operation, economics of scale power generation, a number of ORC machines to be operated, operating conditions of each ORC machine, combinations of them, or other considerations are described. Recognizing that several subsets of hot sources can be identified from among the available hot sources in a large petroleum refinery, subsets of hot sources that are optimized to provide waste heat to one or more ORC machines for power generation are also described. Further, recognizing that the utilization of waste heat from all available hot sources in a mega-site such as a petroleum refinery and aromatics complex is not necessarily or not always the best option, hot source units in petroleum refineries from which waste heat can be consolidated to power the one or more ORC machines are identified.

Optimizing power generation from waste heat in large industrial facilities such as petroleum refineries by utilizing a subset of all available hot source streams selected based, in part, on considerations for example, capital cost, ease of operation, economics of scale power generation, a number of ORC machines to be operated, operating conditions of each ORC machine, combinations of them, or other considerations are described. Recognizing that several subsets of hot sources can be identified from among the available hot sources in a large petroleum refinery, subsets of hot sources that are optimized to provide waste heat to one or more ORC machines for power generation are also described. Further, recognizing that the utilization of waste heat from all available hot sources in a mega-site such as a petroleum refinery and aromatics complex is not necessarily or not always the best option, hot source units in petroleum refineries from which waste heat can be consolidated to power the one or more ORC machines are identified.

Processes for producing a gasoline blend in which C.sub.7 hydrocarbons are separated from a naphtha feed. The C.sub.7 hydrocarbons are isomerized and dehydrogenated to increase the octane value of the components therein. In order to avoid conversion of methylcyclohexane to toluene in the dehydrogenation reactor, the various processes provide flow schemes in which the methylcyclohexane bypasses the C.sub.7 dehydrogenation reaction zone.

Processes for producing a gasoline blend in which C.sub.7 hydrocarbons are separated from a naphtha feed. The C.sub.7 hydrocarbons are isomerized and dehydrogenated to increase the octane value of the components therein. In order to avoid conversion of methylcyclohexane to toluene in the dehydrogenation reactor, the various processes provide flow schemes in which the methylcyclohexane bypasses the C.sub.7 dehydrogenation reaction zone.