An apparatus and a method for washing hydrocarbon product vapor are disclosed. The apparatus comprises housing, a first wash zone at a predefined cross-section of the housing for receiving the hydrocarbon product vapor, a plurality of injection units located within the first wash zone at predetermined intervals of the length of the housing for receiving wash oil. The injection units inject oil droplets formed from the received wash oil to contact the vapor and obtain a primary washed hydrocarbon vapor within the first wash zone. Further, a second wash zone is located above and in fluid communication with the first wash zone for receiving the primary washed hydrocarbon vapor. One or more spray headers receive wash oil and spray oil droplets formed from the received wash oil to contact with the primary washed hydrocarbon vapor, thereby forming a secondary washed hydrocarbon vapor.

A heavy hydrocarbon oil is mixed with one or more disulfide oil compounds and/or one or more oxidized disulfide oil compounds and, optionally, a homogeneous catalyst includes dissolved hydrogen, and the mixture is subjected to a delayed coking process to produce a liquid coking unit product stream for recovery and further processing, with the delayed coking being completed in a reduced residence time as compared to the delayed coking of the heavy hydrocarbon oil without the DSO and/or ODSO compounds.

Methods and systems for converting an aromatic polymer material and aromatic bottoms to needle-grade coke. An embodiment of a method includes supplying aromatic bottoms from an aromatic recovery complex; mixing the aromatic polymer material with the aromatic bottoms to obtain an aromatic polymer mixture comprising the aromatic polymer material and the aromatic bottoms; delayed coking the aromatic polymer mixture to obtain petroleum green coke and volatile components; fractionating the volatile components to obtain distillate products; and calcining the petroleum green coke to obtain needle coke.

A system includes a heat exchange system and a power generation system. The heat exchange system includes first, second, and third heat exchangers each operable as a continuous source of heat from a delayed coking plant. The first and second heat exchangers heat first and second fluid streams to produce heated first and second fluid streams, respectively. The heated second fluid stream has a lower temperature and a greater quantity of heat than the heated first fluid stream. The third heat exchanger heats a third fluid stream to produce a heated third fluid stream that includes the heated first fluid stream and a hot fluid stream. The heated third fluid stream has a lower temperature than the heated first fluid stream. The power generation system generates power using heat from the heated second and third fluid streams.

A system includes a heat exchange system and a power generation system. The heat exchange system includes first, second, and third heat exchangers each operable as a continuous source of heat from a delayed coking plant. The first and second heat exchangers heat first and second fluid streams to produce heated first and second fluid streams, respectively. The heated second fluid stream has a lower temperature and a greater quantity of heat than the heated first fluid stream. The third heat exchanger heats a third fluid stream to produce a heated third fluid stream that includes the heated first fluid stream and a hot fluid stream. The heated third fluid stream has a lower temperature than the heated first fluid stream. The power generation system generates power using heat from the heated second and third fluid streams.

A heavy hydrocarbon oil is mixed with one or more disulfide oil compounds and/or one or more oxidized disulfide oil compounds and, optionally, a homogeneous catalyst includes dissolved hydrogen, and the mixture is subjected to a delayed coking process to produce a liquid coking unit product stream for recovery and further processing, with the delayed coking being completed in a reduced residence time as compared to the delayed coking of the heavy hydrocarbon oil without the DSO and/or ODSO compounds.

Provided here are systems and methods of production of needle coke by processing an aromatic rejects stream containing long chain alkyl monoaromatics and bridged diaromatics through a delayed coking process. Various other embodiments may be disclosed and claimed.

The present invention relates to a process for production of anisotropic coke from a hydrocarbon feedstock and a system for producing the same. More particularly, the present invention relates to a thermal cracking of heavy petroleum residue producing petroleum coke and lighter hydrocarbon products. The invented process utilizes a novel scheme for production of a premium quality coke from primarily, a clarified oil feedstock. Clarified oil from fluid catalytic cracking unit is routed through a process scheme comprising a separator column, hydrotreatment section and an aromatic extraction section to create an ad-mix of effluents which form the feedstock to a thermal cracking unit. Premium quality anisotropic coke is produced in the thermal cracker reactor drums under tailor made process conditions employing the said feedstock.

Systems and methods are provided for upgrading a mixture of catalytic slurry oil and coker bottoms by hydroprocessing. Optionally, the upgrading can further include deasphalting the mixture of catalytic slurry oil and coker bottoms to form a deasphalted oil and a deasphalter residue or rock fraction. The mixture of catalytic slurry oil and coker bottoms and/or the deasphalted oil can then be hydroprocessed to form an upgraded effluent that includes fuels boiling range products. Optionally, in some aspects where the feed mixture is deasphalted prior to hydroprocessing, the feed mixture can further include a portion of a (sour) vacuum resid.

The delayed coking method includes directing a heated secondary feedstock, which contains heated primary feedstock and recirculate, from a reaction furnace to a coking chamber. Vapor-liquid coking products formed in the coking chamber are then directed to a fractionation column, which fractionates hydrocarbon gas, gasoline, light and heavy gas oils, and bottom residues. Heavy gas oil from the fractionation column is directed to a thermal cracking furnace, the products of which are cooled by cooled light gas oil and directed to an evaporator for separation. In the evaporator, gases and light boiling products are removed by evaporation and returned to the fractionation column, and the remaining distillate cracking residue is separated and used as a component of the recirculate, along with bottom residues from the fractionation column. The resulting process produces high quality and high yield needle and anode cokes.