A catalytic cracking process includes a step of contacting a cracking feedstock with a catalytic cracking catalyst in the presence of a radical initiator for reaction under catalytic cracking conditions. The radical initiator contains a dendritic polymer and/or a hyperbranched polymer. The dendritic polymer and the hyperbranched polymer each independently has a degree of branching of about 0.3-1, and each independently has a weight average molecular weight of greater than about 1000. The catalytic cracking process is beneficial to enhancing and accelerating the free radical cracking of petroleum hydrocarbon and promoting the regulation of cracking activity and product distribution; by using the process disclosed herein, the conversion of catalytic cracking can be improved, the yields of ethylene and propylene can be increased, and the yield of coke can be reduced.

A method of predicting the tendency of a heavy oil feed to generate coke deposits in the FCC riser under a given set of operating parameters in the unit; thus, by utilizing operating parameters appropriate to the feed, the formation of coke deposits in the riser may be minimized. The margin between the theoretical dew point of the hydrocarbon feed established from unit operating parameters and the theoretical mix zone temperature in the feed injection zone of the unit is developed by applying a regression-derived linear model from multiple rigorous model runs. The mix zone of the unit is then operated at a temperature which reduces the level of riser coking predicted from this ascertainable margin or, at least, maintains it within levels which are predictable and acceptable.

A phosphorus-modified MFI-structured molecular sieve is characterized in that the molecular sieve has a K value, satisfying: 70%≤K≤90%; for example, 75%≤K≤90%; further for example, 78%≤K≤85%. The K value is as defined in the specification. A cracking auxiliary or cracking catalyst contains the phosphorus-modified MFI molecular sieve.

The process comprises hydrocracking a hydrocarbon feed in a single stage. The catalyst comprises a base impregnated with metals from Group 6 and Groups 8 through 10 of the Periodic Table. The base of the catalyst used in the present hydrocracking process comprises alumina, an amorphous silica-alumina (ASA) material, a USY zeolite, optionally a beta zeolite, and zeolite ZSM-12.

A process for producing a base oil composition from a deasphalted oil (DAO) feed, where the DAO feed undergoes hydrotreating, hydrocracking, catalytically dewaxing, hydrofinishing, and fractionating to generate the base oil composition. The base oil composition includes a hazy-free at 0° C. heavy base oil comprising (a) a kinetic viscosity ranging from 15 to 21 cSt at 100° C., (b) a 5 viscosity index of at least 95, (c) a pour point of less than −12° C., (d) a cloud point of less than −18° C., and (e) a total aromatics content of 2 wt % or less, where the hazy-free at 0° C. heavy base oil maintains a hazy-free appearance when stored undisturbed at 0° C. during a test period.

A method may include: hydropyrolyzing a bio feedstock in a hydropyrolysis unit to produce at least a hydropyrolysis oil; introducing at least a portion of the hydropyrolysis oil with a hydrocarbon co-feed into a fluidized catalytic cracking unit; and cracking the hydropyrolysis oil in the fluidized catalytic cracking unit to produce at least fuel range hydrocarbons.

Naphthenic process oils are made by blending one or more naphthenic vacuum gas oils in one or more viscosity ranges with a high C.sub.A content distilled aromatic extract feedstock to provide at least one blended oil, and hydrotreating the at least one blended oil to provide an enhanced C.sub.A content naphthenic process oil. The order of the vacuum distillation and blending steps may be reversed.

The present disclosure relates to co-processing at least a fossil-based feed, pyrolysis liquid and a distillation residue from tall oil distillation in an oil refinery conversion process.

An extraction solvent comprised of one or more ethyleneamines having structure (I), (II), or (III): ##STR00001##
where R.sub.1-R.sub.6 can independently be H, C.sub.1-C.sub.4 linear or branched alkyl, amido (RRNC═O), or hydroxyalkyl, where each R in the amido group independently H or C.sub.1 alkyl, and where x ranges from 1 to 6, may be contacted with a hydrocarbon stream to remove or extract non-acidic contaminants, such as thiophenes, benzothiophenes, alkyl sulfides, alkyl disulfides, mercaptans, aromatics, oxygenates, metals, olefins, and combinations thereof, from the hydrocarbon stream. The extraction solvent may include co-solvents and the hydrocarbon stream may be in gas and/or liquid form.

A process and apparatus is disclosed for recovering hydrotreating effluent from a hydrotreating unit utilizing a hot stripper and a cold stripper. Only the hot hydrotreating effluent is heated in a fired heater prior to product fractionation, resulting in substantial operating and capital savings. The cold stripped stream from the cold stripper bottoms line may be passed directly to a diesel pool when VGO is hydrotreated in the hydrotreating reactor bypassing the product fractionation column.