A process for extracting fuel products from waste rubber, comprising the steps of subjecting the waste rubber to pyrolysis to produce a pyrolysis vapour, subjecting the pyrolysis vapour to a condensation step to produce a pyrolytic oil having a boiling point range of 45-400° C. and a flash point below 25° C., and then subjecting the pyrolytic oil to a vacuum steam stripping step so as to recover a fraction having a flash point of at least 40° C. but no higher than 55° C., a boiling point range starting at 100° C. or higher, a density at 15° C. of less than 990 kg/m.sup.3, a total acid number TAN of up to 12, a styrene content of less than 7000 ppm, and an organic halogen (as Cl) content of less than 50 ppm.

The present invention discloses a process and an apparatus for conversion of waste plastic pyrolysis oil into value added products, wherein, the pyrolysis oil is produced from waste plastics by utilizing HCGO as a preheating stream. The process and apparatus as disclosed improves the conventional DCU process in terms of liquid, gaseous yields and reduction in coke yields and without disturbing the hardware of the conventional process along with energy efficient production of pyrolysis oil. The present process and apparatus include a delayed coking process and a system for the delayed coking process which involves the integration of delayed coking system with pyrolysis section and utilization of produced pyrolysis oil by co-processing it with residual heavy hydrocarbon feedstock.

Methods and systems for producing aromatics and light olefins from a mixed plastics stream are described. The method may include feeding a plastic feedstock to a dechlorination operation to melt the plastic feedstock to release HCl and generate a liquid plastic stream; feeding the liquid plastic stream to a pyrolysis reactor, the pyrolysis reactor to generate hydrocarbon vapors; feeding the hydrocarbon vapors to an acid gas removal reactor with a solid inorganic alkali salt disposed within the reaction vessel to remove residual HCl and sulfur-containing compounds from the hydrocarbon vapors to generate a plastic derived oil; and feeding the plastic derived oil to a steam enhanced catalytic cracking reactor to generate a product stream comprising light olefins having a carbon number of C.sub.2-C.sub.4 and aromatics. The associated system for processing mixed plastics into aromatics and light olefins is also described.

A method of upgrading an overflash stream from a vacuum distillation unit comprising the steps of separating the overflash stream from an atmospheric residue stream, the overflash stream comprises an overflash fraction having a T10% between 475 and 530° C. and a T90% between 600 and 700° C.; introducing the reactor feed to a supercritical reactor at a temperature between 380° C. and 500° C. and a pressure between 25 MPa and 30 MPa; maintaining upgrading reactions in the supercritical reactor to upgrade the overflash fraction such that a reactor effluent comprises upgraded hydrocarbons relative to the overflash fraction; reducing a temperature of a reactor effluent in a cooling device to produce a cooled stream; reducing a pressure of the cooled stream in a depressurizing device to produce a discharged stream; and separating the discharged stream in a gas-liquid separator to produce a liquid phase product.

The invention relates to producing upgraded renewable oil. Renewable crude oil is provided whose oxygen content, water content, and total acid number are within predetermined ranges. Respective fractions of the oil have boiling points below 350° C. and above 450° C. After the oil is pressurized, and hydrogen is added, the mixture is heated and contacted with a heterogeneous catalyst in a first reaction zone with weight based hourly space velocity (WHSV) of 0.1 to 1 h-1. The resultant partially hydrogenated and deoxygenated oil is further heated and contacted with a heterogeneous catalyst in a second reaction zone at WHSV of 0.1 to 1.5 h-1. Low and high boiling point liquid hydrocarbon fractions of the product of the second reaction zone are sent to third and fourth reaction zones, respectively, to be contacted with hydrogen and a heterogeneous catalyst under respective heating conditions and WHSV of 0.1 to 1 h-1.

The present invention discloses an integrated process scheme for producing (i) high-octane gasoline blending stream (ii) high aromatic heavy naphtha stream which is a suitable feedstock for benzene, toluene, and xylene (BTX) production and (iii) high cetane ultra-low sulphur diesel (ULSD) stream suitable for blending in refinery diesel pool.

A process for upgrading a hydrocarbon feed includes passing the hydrocarbon feed and an aromatic bottoms stream to an FCC unit including an FCC reactor and a catalyst regenerator. The hydrocarbon feed is hydrogen-rich having at least 12 wt. % hydrogen, and the aromatic bottoms stream is a bottoms stream produced from an aromatics recovery complex for processing reformate from naphtha reforming. The hydrocarbon feed and aromatic bottoms stream are cracked over the FCC catalysts to produce an effluent and spent FCC catalysts having coke deposits. The spent FCC catalyst is regenerated through combustion of the coke deposits. The hydrogen-rich hydrocarbon feed does not produce enough coke to satisfy the heat demand of the FCC reactor. Cracking the aromatic bottoms stream increases the amount of coke so that combustion of the additional coke during regeneration produces additional heat to satisfy the heat demand of the FCC reactor.

In some examples, hydrocarbon feed and a diluent such as steam are mixed, and heated. A vapor phase product and a liquid phase product can be separated from the heated mixture. The liquid phase product can be hydroprocessed to produce a first hydroprocessed product. A pitch and one or more hydrocarbon products can be separated from the first hydroprocessed product. The pitch can be contacted with a diluent to produce a pitch-diluent mixture. The pitch-diluent mixture can be hydroprocessed to produce a second hydroprocessed product. A hydroprocessor heavy product and a utility fluid product can be separated from the second hydroprocessed product. The diluent can be or include at least a portion of the utility fluid product. The vapor phase product can be steam cracked to produce a steam cracker effluent. A tar product and a process gas that can include ethylene and propylene can be separated from the steam cracker effluent.

Systems and methods are provided for catalytically dewaxing a diesel boiling range feed. In some aspects, catalytic dewaxing can be performed at low hydrogen treat gas rates and/or low hydrogen purity conditions. In other aspects, the systems and methods can allow for distillate dewaxing while reducing or minimizing the amount of equipment required.

Catalytic conversion of ketoacids is disclosed, including methods for increasing the molecular weight of ketoacids. An exemplary method includes providing in a reactor a feedstock having at least one ketoacid. The feedstock is then subjected to one or more C—C-coupling reaction(s) in the presence of a catalyst system having a first metal oxide and a second metal oxide.