The present invention relates to a method for producing a liquid hydrocarbon fuel comprising a first reaction step and a second reaction step given below: (1) a first reaction step: hydrocracking a raw material oil in the presence of a hydrocracking reaction catalyst at a feeding pressure of hydrogen of from 0.2 to 0.95 MPa, a liquid hourly space velocity of a liquid volume of the raw material oil of from 0.05 to 0.5 hr.sup.−1, and a ratio of a flow rate of the hydrogen to a flow rate of the raw material oil of from 100 to 1,000 NL of the hydrogen per 1 L of the raw material oil; and (2) a second reaction step: hydrogenating the cracked solution in the presence of a hydrogenation reaction catalyst at a feeding pressure of hydrogen of from 0.2 to 0.95 MPa, a liquid hourly space velocity of a liquid volume of the raw material oil of from 0.2 to 5 hr.sup.−1, and a ratio of a flow rate of the hydrogen to a flow rate of the raw material oil of from 100 to 1,000 NL of the hydrogen per 1 L of the raw material oil. According to the present invention, a desired liquid hydrocarbon fuel can be produced by carrying out a combination of the hydrocracking reaction and the hydrogenation reaction of a raw material oil such as fats and oils in a given composition by feeding a low-pressure hydrogen of nearly a normal pressure.

The invention relates to a catalytic cracking gasoline prehydrogenation method. Thiol etherification and double bond isomerization reactions are carried out on catalytic cracking gasoline through a prehydrogenation reactor. The reaction conditions are as follows: the reaction temperature is between 80° C. and 160° C., the reaction pressure is between 1 MPa and 5 MPa, the liquid-volume hourly space velocity is from 1 to 10 h.sup.−1, and the hydrogen-oil volume ratio is (3-8):1; a prehydrogenation catalyst comprises a carrier and active ingredients, the carrier contains an aluminium oxide composite carrier with a macroporous structure and one or more of ZSM-5, ZSM-11, ZSM-12, ZSM-35, mordenite, amorphous form aluminum silicon, SAPO-11, MCM-22, a Y molecular sieve and a beta molecular sieve, the surface of the carrier is loaded with one or more of the active ingredients cobalt, molybdenum, nickel and tungsten; based on oxides, the content of the active ingredients is between 0.1% and 15.5%.

The present invention is based on the use of a two-step hydrocracking process for the production of naphtha, comprising a step of hydrogenation placed upstream of the second hydrocracking step, the hydrogenation step treating the unconverted liquid fraction separated in the distillation step in the presence of a specific hydrogenation catalyst. Furthermore, the hydrogenation step and a second hydrocracking step are carried out under specific operating conditions and in particular under temperature conditions that are very specific with respect to one another.

A process for upgrading light cycle oil (LCO) to a high octane gasoline and a high aromatic feedstock for aromatic complex, by utilizing fluid catalytic cracking (FCC) is disclosed. FCC cracks unconverted diesel range stream from a hydrocracker to a high octane gasoline. This process further improves the quality (e.g., research octane number (RON), and Sulfur) of gasoline by utilizing FCC and hydrocracking process.

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 selectively hydrocracked for selective ring opening and dealkylation to produce a selectively hydrocracked BTX+ stream. The selectively hydrocracked BTX+ stream is 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 selective hydrocracking step, and the feed to the selective hydrogenation step comprises all or a portion of the second stream containing C10+ aromatic compounds.

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 selectively hydrocracked for selective ring opening and dealkylation to produce a selectively hydrocracked BTX+ stream. The selectively hydrocracked BTX+ stream is 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 selective hydrocracking step, and the feed to the selective hydrogenation step comprises all or a portion of the second stream containing C10+ aromatic compounds.

Systems and processes for producing olefins and aromatics. A process can include contacting a first hydrocarbon feed with a catalyst and a hydrogen source under conditions sufficient to produce a used catalyst and an intermediate stream containing olefins and aromatics, and contacting the used catalyst with the intermediate stream and a coke precursor feed to produce a spent coked catalyst and a products stream comprising additional olefins and aromatics.

The present disclosure provides an integrated method and apparatus for catalytic cracking of heavy oil and production of syngas. A cracking-gasification coupled reactor having a cracking section and a gasification section is used as a reactor in the method. A heavy oil feedstock is fed into a cracking section to contact with a bed material in a fluidized state that contains a cracking catalyst, a catalytic cracking reaction is conducted under atmospheric pressure to obtain light oil-gas and coke. The coke is carried downward by the bed material into a gasification section to conduct a gasification reaction to generate syngas; the syngas goes upward into the cracking section to merge with the light oil-gas, and is guided out from the coupled reactor and enter a gas-solid separation system. Oil-gas fractionation is performed to a purified oil-gas product output from the gas-solid separation system to collect light oil and syngas products.

Systems and methods are provided for production of renewable jet fuel and/or jet fuel blending component fractions. The systems and methods provide for formation of jet boiling range fractions via hydrodeoxygenation and catalytic dewaxing of bio-derived feeds. The systems and methods for reducing or minimizing recycle and/or forming only a jet boiling range product and a lower boiling range product can be facilitated based on selection of a suitable feedstock and/or based on selection of suitable reaction conditions and catalyst for the catalytic dewaxing.

The present invention relates to the extraction of gasoline from a gas G, with (a) a step of extracting gasoline from the gas to be treated comprising methanol GM obtained from step (d), (b) a step of separating said fluid GL1 partially condensed in step (a), producing a first aqueous liquid phase Al , a first liquid phase H1 of hydrocarbon(s) a gaseous phase G1 obtained from the gas G; (c) a step of contacting a portion of the gas G to be treated with said first aqueous liquid phase A1, producing a second aqueous liquid phase A2, a gaseous phase of gas to be treated comprising methanol GM; (d) a step of mixing said gaseous phase of gas to be treated comprising methanol GM with the remainder of the gas G to be treated, producing a gas to be treated comprising methanol GM, (e) a step of stabilizing said first liquid phase H1 of hydrocarbon(s).