Provided is a method for preparing synthesis gas and aromatic hydrocarbons, and more particularly, a method for preparing synthesis gas and aromatic hydrocarbons including: supplying a pyrolysis fuel oil (PFO) stream containing PFO and a pyrolysis gas oil (PGO) stream containing PGO to a distillation tower as a feed stream (S10), the PFO stream and the PGO stream being discharged from a naphtha cracking center (NCC) process; and supplying a lower discharge stream from the distillation tower to a combustion chamber for a gasification process and supplying an upper discharge stream from the distillation tower to an SM/BTX preparation process (S20).

Disclosed is an ethylene and/or propylene cracker unit that uses recycled carbon dioxide as a working fluid. A boiler may also use recycled carbon dioxide as a working fluid. In either instance, instead of releasing high-purity CO.sub.2 into the atmosphere, the bulk of the CO.sub.2 is utilized as the working fluid and the produced CO.sub.2 is captured and sent to the pipeline for utilization or storage. These systems will minimize heat loss and achieve essentially zero CO.sub.2 emission to the air.

A catalyst composition includes a metal catalyst dispersed in a molten eutectic mixture of alkali metal or alkaline earth metal carbonates or hydroxides. A process for the catalytic cracking of hydrocarbons includes contacting in a reactor system a carbon-containing feedstock with at least one catalyst in the presence of oxygen to generate olefinic and/or aromatic compounds; and collecting the olefinic and/or aromatic compounds; wherein: the at least one catalyst includes a metal catalyst dispersed in a molten eutectic mixture of alkali metal or alkaline earth metal carbonates or hydroxides. A process for preparing the catalyst includes mixing metal catalyst precursors selected from transition metal compounds and rare-earth metal compounds and a eutectic mixture of alkali metal or alkaline earth metal carbonates or hydroxides and heating it. A use of the catalyst in the catalytic cracking process of hydrocarbons.

A system for oxidative conversion of a mixed hydrocarbon feed stream to a product stream containing at least one olefin is provided. The system includes a plurality of reactors each capable of oxidatively dehydrogenating at least a portion of a hydrocarbon in the mixed hydrocarbon feed, and each reactor able to operate at different set of reaction conditions from other reactors in the plurality of reactors. All of the reactors use the same oxygen transfer agent to produce at least one olefin. In some embodiments, at least one reactor is optimized to oxidatively couple methane to produce ethylene, while other reactors are optimized to oxidatively dehydrogenate ethane to ethylene or to oxidatively dehydrogenate propane to ethylene and/or propylene. All of the reactors feed into a single regeneration unit for the oxygen transfer agent. A method of oxidatively converting the mixed hydrocarbon feed to an olefin is also provided.

Aspects of the invention relate to producing olefins and other products by oxidative dehydrogenation cracking of a hydrocarbon feed. In one embodiment, the method includes oxidative cracking a hydrocarbon feed comprised of plastic waste. Methods of the present invention employ dual functional catalyst comprising solid acids and metal oxides, which are capable of selectively oxidizing hydrogen to water rather than combustion of the hydrocarbon feeds or products. Additional aspects of the invention demonstrate catalyst synthetic methods for encapsulating metal oxides in the internal channels and cages of solid acids, thereby improving the selective oxidation of hydrogen to water and decreasing feed and product oxidation. The re-oxidation of the thus reduced metal oxide transfer agents supplies heat to drive the endothermic cracking of the feed.

According to an embodiment of the present disclosure, petrochemicals may be produced from crude oil by a process which includes passing the crude oil and hydrogen into a hydroprocessing reactor, separating the hydrotreated oil into a lesser boiling point fraction and a greater boiling point fraction, passing the lesser boiling point fraction to a pyrolysis section of a steam cracker to produce a pyrolysis effluent comprising olefins, aromatics, or both, passing the greater boiling point fraction to a gasifier, where the gasifier produces hydrogen, and passing at least a portion of the hydrogen produced by the gasifier to the hydroprocessing reactor.

Aspects of the invention relate to producing olefins by oxidative dehydrogenation cocracking of a hydrocarbon feed. In one embodiment, the method includes oxidative cocracking a hydrocarbon feed comprised of at least one alkane having a carbon chain of five or more and at least one alkane having a carbon chain of four or less by contacting the hydrocarbon feed with a metal oxide, such that the cracking of the at least one alkane having a carbon chain of four or less produces olefins and is exothermic, and the cracking of the at least one alkane having a carbon chain of five or more produces olefins and is endothermic. The method further includes utilizing the energy produced from the exothermic cracking of the alkane having a carbon chain of four or less for the endothermic cracking of the alkane having a carbon chain of five or more, and collecting the product.

Aspects of the invention relate to producing olefins by oxidative dehydrogenation cocracking of a hydrocarbon feed. In one embodiment, the method includes oxidative cocracking a hydrocarbon feed comprised of at least one alkane having a carbon chain of five or more and at least one alkane having a carbon chain of four or less by contacting the hydrocarbon feed with a metal oxide, such that the cracking of the at least one alkane having a carbon chain of four or less produces olefins and is exothermic, and the cracking of the at least one alkane having a carbon chain of five or more produces olefins and is endothermic. The method further includes utilizing the energy produced from the exothermic cracking of the alkane having a carbon chain of four or less for the endothermic cracking of the alkane having a carbon chain of five or more, and collecting the product.

A process for producing syngas and olefins includes the steps of feeding a catalytic partial oxidation (CPO) reactant mixture having oxygen, first hydrocarbons, and optionally steam to a CPO reaction zone having a CPO catalyst such that at least a portion of the CPO reactant mixture reacts, via an exothermic CPO reaction, to produce syngas having hydrogen (H.sub.2), carbon monoxide (CO), carbon dioxide (CO.sub.2), water, and unreacted first hydrocarbons. The syngas is characterized by a molar ratio M defined as (H.sub.2?CO.sub.2)/(CO+CO.sub.2). The method further includes feeding a cracking zone feed having second hydrocarbons to a cracking zone such that at least a portion of the second hydrocarbons undergoes an endothermic cracking reaction to produce a cracking zone product stream having olefins, hydrogen, and unreacted second hydrocarbons; and cooling the CPO reaction zone by heating the cracking zone while cooling the CPO reaction zone via heat transfer between the CPO reaction zone and the cracking zone.

A process for producing syngas and olefins includes the steps of feeding a catalytic partial oxidation (CPO) reactant mixture having oxygen, first hydrocarbons, and optionally steam to a CPO reaction zone having a CPO catalyst such that at least a portion of the CPO reactant mixture reacts, via an exothermic CPO reaction, to produce syngas having hydrogen (H.sub.2), carbon monoxide (CO), carbon dioxide (CO.sub.2), water, and unreacted first hydrocarbons. The syngas is characterized by a molar ratio M defined as (H.sub.2?CO.sub.2)/(CO+CO.sub.2). The method further includes feeding a cracking zone feed having second hydrocarbons to a cracking zone such that at least a portion of the second hydrocarbons undergoes an endothermic cracking reaction to produce a cracking zone product stream having olefins, hydrogen, and unreacted second hydrocarbons; and cooling the CPO reaction zone by heating the cracking zone while cooling the CPO reaction zone via heat transfer between the CPO reaction zone and the cracking zone.