A method for processing a hydrocarbon feed to produce olefins may comprise introducing the hydrocarbon feed to a first fluid catalytic cracking system, which may cause at least a portion of the hydrocarbon feed to undergo catalytic cracking and produce a spent first cracking catalyst and a first cracked effluent comprising one or more olefins. The method may further comprise passing the first cracked effluent to a separation system downstream of the first fluid catalytic cracking system, which may separate the first cracked effluent to produce at least a naphtha effluent comprising one or more olefins. Additionally, the method may comprise passing the naphtha effluent to a second fluid catalytic cracking system downstream of the separation system, which may cause at least a portion of the naphtha effluent to undergo catalytic cracking and produce a spent cracking catalyst mixture and a second cracked effluent comprising one or more olefins.

Supplemental heat required to raise the temperature of a regenerated catalyst to the minimum required to promote the catalyzed reaction in an FCC unit is provided by introducing adsorbent material containing HPNA compounds and HPNA precursors with the coked catalyst into the FCC catalyst regeneration unit for combustion. The HPNA compounds and HPNA precursors can be adsorbed on either a carbonaceous adsorbent, such as activated carbon, that is completely combustible and generates no ash, or on fresh or coked FCC catalyst that is recovered from an HPNA adsorption column that has treated the bottoms from a hydrocracking unit to remove the HPNA compounds and their precursors.

A fluid catalytic cracking (FCC) process for cracking multiple feedstocks in a FCC apparatus comprising a first set of feed distributors having first distributor tips and a second set of feed distributors having second distributor tips is provided. A first feed is injected into the riser from first distributor tips. A second feed is injected into the riser from second distributor tips. The first distributor tips and the second distributor tips are positioned at different radii in the riser. The first feed and the second feed are cracked in the riser in the presence of an FCC catalyst to provide a cracked effluent stream. The first distributor tips and the second distributor tips are located into a region of lower catalyst density and a region of higher catalyst density respectively in the riser.

A process is provided for the catalytic cracking of a glyceride oil feedstock with a catalyst composition containing a deactivated phosphorus-containing ZSM-5 light olefins selective additive.

The invention relates to a process for the hydrodesulfurization of a sulfur-containing olefinic gasoline cut in which said gasoline cut, hydrogen and a regenerated catalyst are brought into contact, said process being carried out at a temperature of between 200° C. and 400° C., a total pressure of between 1 and 3 MPa, an hourly space velocity, defined as being the flow rate by volume of feedstock relative to the volume of catalyst, of between 1 and 10 h.sup.−1; and a hydrogen/gasoline feedstock ratio by volume of between 100 and 1200 SI/I, said regenerated catalyst resulting from an at least partially spent catalyst resulting from a process for the hydrodesulfurization of a sulfur-containing olefinic gasoline cut and comprises at least one metal from group VIII, at least one metal from group VIb and an oxide support.

A FCC process including the steps of (a) adding a crude lignin oil (CLO) to a FCC unit, wherein the FCC unit has a FCC riser, a catalyst regenerator and a reactor/stripper, wherein CLO is a crude lignin oil composition including lignin and a polar organic solvent in 1:10 to 1:0.3 w/v ratio, (b) optionally adding a second feed including a conventional FCC feedstock to the FCC unit, (c) adding a regenerated catalyst from the regenerator to the FCC riser for catalytic cracking and upgrading the CLO and second feedstock to produce upgraded products and deactivated catalyst, (d) adding the upgraded products and deactivated catalyst from the FCC riser to the reactor/stripper and separating upgraded products from deactivated catalyst in the reactor/stripper, (e) adding the deactivated catalyst from (d) to the regenerator to regenerate the deactivated catalyst to provide regenerated catalyst; and
collecting the upgraded products.

A FCC process including the steps of (a) adding a crude lignin oil (CLO) to a FCC unit, wherein the FCC unit has a FCC riser, a catalyst regenerator and a reactor/stripper, wherein CLO is a crude lignin oil composition including lignin and a polar organic solvent in 1:10 to 1:0.3 w/v ratio, (b) optionally adding a second feed including a conventional FCC feedstock to the FCC unit, (c) adding a regenerated catalyst from the regenerator to the FCC riser for catalytic cracking and upgrading the CLO and second feedstock to produce upgraded products and deactivated catalyst, (d) adding the upgraded products and deactivated catalyst from the

FCC riser to the reactor/stripper and separating upgraded products from deactivated catalyst in the reactor/stripper, (e) adding the deactivated catalyst from (d) to the regenerator to regenerate the deactivated catalyst to provide regenerated catalyst; and collecting the upgraded products.

A system for upgrading pyrolysis oil may include a pyrolysis upgrading unit having a mixed metal oxide catalyst and a separation unit operable to separate used mixed metal oxide catalyst from a reaction effluent. A method for upgrading pyrolysis oil may include contacting the pyrolysis oil with hydrogen in the presence of the mixed metal oxide catalyst at reaction conditions to produce a reaction effluent. The pyrolysis oil may include multi-ring aromatic compounds. The mixed metal oxide catalyst may include a plurality of catalyst particles and each of the plurality of catalyst particles having a plurality of metal oxides. Contacting the pyrolysis oil with hydrogen in the presence of the mixed metal oxide catalyst at the reaction conditions may convert at least a portion of the multi-ring aromatic compounds in the pyrolysis oil to the light aromatic compounds.

A reactor system configured for efficiently removing contaminants (CCR, nickel, vanadium, nitrogen, sodium, iron, calcium, chlorine etc.) from a heavy portion of the crude oil. The products are routed to a common main fractionation section. The heavy feed with lower contaminants may then be processed in a fluid catalytic cracking (FCC) unit, the overall concept employing a fluid catalytic reaction platform with carbon rejection approach. Also disclosed is a reactor system for efficiently processing crude oil in a fluid catalytic cracking unit with a dual-reactor and dual catalyst system to maximize petrochemical building blocks such as ethylene, propylene, butylenes, BTX (benzene, toluene and xylene) rich naphtha from a variety of crude oils.

A system for upgrading pyrolysis oil may include a pyrolysis upgrading unit having a mixed metal oxide catalyst and a separation unit operable to separate used mixed metal oxide catalyst from a reaction effluent. A method for upgrading pyrolysis oil may include contacting the pyrolysis oil with hydrogen in the presence of the mixed metal oxide catalyst at reaction conditions to produce a reaction effluent. The pyrolysis oil may include multi-ring aromatic compounds. The mixed metal oxide catalyst may include a plurality of catalyst particles and each of the plurality of catalyst particles having a plurality of metal oxides. Contacting the pyrolysis oil with hydrogen in the presence of the mixed metal oxide catalyst at the reaction conditions may convert at least a portion of the multi-ring aromatic compounds in the pyrolysis oil to the light aromatic compounds.