A plasmonic nanoparticle catalyst for producing hydrocarbon molecules by light irradiation, which comprises at least one plasmonic provider and at least one catalytic property provider, wherein the plasmonic provider and the catalytic property provider are in contact with each other or have distance less than 200 nm, and molecular composition of the hydrocarbon molecules produced by light irradiation is temperature-dependent. And a method for producing hydrocarbon molecules by light irradiation utilizing the plasmonic nanoparticle catalyst.

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and fluid catalytic cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline and FCC naphtha aromatics extraction zone within the battery limits.

A process for hydrocracking a hydrocarbon feed is provided. The process comprises hydrocracking the hydrocarbon feed to produce a first hydrocracking product stream, separating the first hydrocracking product stream to form a gas stream and a liquid stream, hydrocracking the liquid stream to produce a second hydrocracking product stream, separating the second hydrocracking product stream to form a first light stream and a first heavy stream comprising benzene, toluene, xylene, C.sub.9+ hydrocarbon, or a combination comprising at least one of the foregoing, purifying the gas stream to form a purified gas stream, and separating the purified gas stream to form at least two of a hydrogen stream, C.sub.1 stream, C.sub.2 stream, C.sub.3 stream, C.sub.4 stream, C.sub.5+ stream, or a combination comprising at least one of the foregoing.

A treatment composition for remediating for remediating H.sub.2S and other contaminant(s) in contaminated liquids, comprising: 0.1-10.0 weight % collectively of at least one hydroxide compound; 0.01-3.0 weight % collectively of at least one organic acid selected from a group consisting of fulvic acid and humic acid; 0.01-10.0 wt % of a chelating agent; and at least 75% weight of water.

The invention relates to various nonlimiting embodiments that include methods, apparatuses or systems for processing natural gas comprising a heavies removal column processing natural gas and light oil reflux. The overhead stream goes to heavies treated natural gas storage. The heavies removal column reboiler bottoms stream product is input to a debutanizer column. The debutanizer column overhead lights are input to a flash drum where the bottoms is pumped through a heat exchanger as a light oil reflux input to the heavies removal column, while the debutanizer reboiler bottoms product is stored as stabilized condensate. Alternatively, debutanizer column overhead lights are sent to heavies treated gas storage and the bottoms stream product goes to a depentanizer column, the overhead lights are pumped through a heat exchanger as a light oil reflux input to the heavies removal column, while the depentanizer reboiler bottoms product is stabilized condensate.

A method for quenching a pyrolysis product, including: supplying a discharge stream from a liquid decomposition furnace to a first quench tower; supplying an upper discharge stream from the first quench tower to a second quench tower; supplying a discharge stream from a first gas decomposition furnace to the second quench tower; and supplying a discharge stream from a second gas decomposition furnace to the second quench tower.

Provided is a method for separating normal paraffin and isoparaffin from raffinates of a benzene, toluene, and xylene (BTX) reforming process including C5 to C8 light naphtha, the method including: a liquid hydrogenation process for removing olefin by feeding raffinates in which hydrogen is dissolved into a reactor filled with a hydrogenation catalyst.

The invention relates to Process of catalytic conversion by hydrocracking of paraffinic and naphthenic hydrocarbons from a naphtha feedstock to propane, the process comprising the steps of providing a naphtha feedstock containing one or more paraffin comprising 4 to 10 carbon atoms and no olefins; and contacting said naphtha feedstock with a catalyst composition in the presence of hydrogen in a reaction zone under hydrocracking conditions; wherein the catalyst composition consists of one or more zeolite catalysts comprising acid 10-membered ring channels containing no added metals.

The invention relates to a process of catalytic conversion by hydrocracking of paraffinic and naphthenic hydrocarbons from a naphtha feedstock (1) to propylene, the process comprising the steps of providing a naphtha feedstock (1) containing one or more paraffins comprising 4 to 10 carbon atoms; and contacting said naphtha feedstock (1) with a catalyst composition in the presence of hydrogen in a reaction zone under hydrocracking conditions; wherein the catalyst composition consists of one or more zeolite catalysts comprising acid 10-membered ring channels.

A process for hydrocracking 2,4-dimethylpentane and/or 2,2,3-trimethylbutane can comprise: contacting a hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst, wherein the hydrocracking feed stream comprises at least 0.5 wt % of 2,4-dimethylpentane and/or 2,2,3-trimethylbutane, based upon a total weight of the hydrocracking feed stream; and wherein the hydrocracking catalyst comprises a medium pore zeolite having a pore size of 5-6 A and a silica to alumina molar ratio of 20-75; preferably the hydrocracking catalyst comprises a medium pore zeolite having a pore size of 5-6 A and a silica to alumina molar ratio of 20-75 and a large pore zeolite having a pore size of 6-8 A and a silica to alumina molar ratio of 10-80, wherein the hydrogenation metal is deposited on the medium pore zeolite and the large pore zeolite.