The present invention relates to a method for treating a cracked stream stemming from a fluid catalytic cracker unit (FCCU) in order to improve propylene recovery. The present invention also relates to the corresponding installation to implement the method.

A plant for separating at least one purified hydrocarbon stream from at least one crude hydrocarbon feed stream. The plant comprises a vessel with a single foundation. The vessel comprises an absorber section and a first divided-wall column. The first divided-wall column comprises a dividing wall, a stripper section, and a stabilization section.

Carbon nanofiber doped alumina (Al—CNF) supported MoCo catalysts in hydrodesulfurization (HDS), and/or boron doping, e.g., up to 5 wt % of total catalyst weight, can improve catalytic efficiency. Al—CNF-supported MoCo catalysts, (Al—CNF—MoCo), can reduce the sulfur concentration in fuel, esp. liquid fuel, to below the required limit in a 6 h reaction time. Thus, Al—CNF—MoCo has a higher catalytic activity than Al—MoCo, which may be explained by higher mesoporous surface area and better dispersion of MoCo metals on the AlCNF support relative to alumina support. The BET surface area of Al—MoCo may be 75% less than Al—CNF—MoCo, e.g., 166 vs. 200 m.sup.2/g. SEM images indicate that the catalyst nanoparticles can be evenly distributed on the surface of the CNF. The surface area of the AlMoCoB5% may be 206 m.sup.2/g, which is higher than AlMoCoB0% and AlMoCoB2%, and AlMoCoB5% has the highest HDS activity, removing more than 98% sulfur and below allowed levels.

The present invention relates to debottleneck solution for delayed Coker unit. More particularly, this invention relates to bottoms of vacuum residuum routed to Coker unit through de-asphalting unit to avoid revamp of existing Coker for the processing of heavier feed stock when there is a change in crude slate. Another object of the invention, in particular, relates to improved delayed coking products, a process used in petroleum refineries to crack petroleum residue, thus converting it into gaseous and liquid product streams and leaving behind solid, carbonaceous petroleum coke.

The present invention relates to a process for the conversion of a feedstock comprising at least 50 wt % related to the total weight of the feedstock of triglycerides, fatty acid esters and/or fatty acids having at least 10 carbon atoms into hydrogen, olefins, dienes, aromatics, gasoline, diesel fuel, jet fuel, naphtha and liquefied petroleum gas comprising: a) introducing of said feedstock in a first reactor to produce linear paraffins in presence of a hydrodesulfurization catalyst and hydrogen, b) separating the effluent of said first reactor in at least three parts to produce at least a first stream comprising part of said linear paraffins and at least a second stream comprising part of said linear paraffins, and at least a third stream comprising part of said linear paraffins c) sending said first stream to a steam cracker to produce hydrogen, olefins, dienes, aromatics and gasoline, diesel fuel being further fractionated; d) introducing said second stream into a second reactor in presence of a hydrocracking or hydroisomerization catalyst to produce a mixture comprising diesel fuel, jet fuel, naphtha and liquefied petroleum gas being further fractionated e) blending said third stream with the diesel fuel obtained at said step d)
wherein said feedstock of said first reactor is diluted in order to limit the temperature increase within said first reactor; and wherein before entering the first reactor said dilution is performed with a weight ratio diluent:feedstock being 1:1, and wherein said diluent comprises at least part of said paraffins obtained at step b).

Provided in one embodiment is a continuous process for converting waste plastic into recycle for polyethylene polymerization. The process comprises selecting waste plastics containing polyethylene and/or polypropylene, and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a pyrolysis oil and optionally wax comprising a naphtha/diesel and heavy fraction, and char. The pyrolysis oil and wax is passed to a refinery FCC unit from which a liquid petroleum gas C.sub.3-C.sub.5 olefin/paraffin mixture fraction is recovered. The liquid petroleum gas C.sub.3-C.sub.5 olefin/paraffin mixture fraction is passed to a refinery alkylation unit, with a propane and butane fraction recovered from the alkylation unit. The propane and butane fraction is then passed to a steam cracker for ethylene production. In another embodiment, a naphtha fraction (C.sub.5-C.sub.8) is recovered from the alkylation unit and passed to the steam cracker. In another embodiment, a propane/propylene fraction (C.sub.3-C.sub.3.sup.=) is recovered from the FCC and passed to the steam cracker.

A continuous process for converting waste plastic into recycle for polypropylene polymerization is provided. The process integrates refinery operations to provide an effective and efficient recycle process. The process comprises selecting waste plastics containing polyethylene and polypropylene and then passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a naphtha/diesel fraction, a heavy fraction, and char. The naphtha/diesel fraction is passed to a refinery FCC unit, from which is recovered a liquid petroleum gas C.sub.3 olefin/paraffin mixture. The C.sub.3 paraffins and C.sub.3 olefins are separated into different fractions with a propane/propylene splitter. The C.sub.3 olefin fraction is passed to a propylene polymerization reactor. The C.sub.3 paraffin fraction is optionally passed to a dehydrogenation unit to produce additional propylene and then the resulting C.sub.3 olefin is passed to a propylene polymerization reactor. The heavy fraction of pyrolyzed oil is passed to an isomerization dewaxing unit to produce a lubricating base oil.

A method for the desulfurization and separation of a catalytic cracking light product includes the steps of: 1) contacting a catalytic cracking light product with a desulfurization adsorbent in an adsorption desulfurization reaction unit in the presence of hydrogen for desulfurization, and optionally, carrying out gas-liquid separation on the resulting desulfurization product, to obtain a desulfurized rich gas and a desulfurized crude gasoline, wherein the catalytic cracking light product is an overhead oil-gas fraction from a catalytic cracking fractionator, or a rich gas and a crude gasoline from a catalytic cracking fractionator; and 2) separately sending the desulfurized rich gas and the desulfurized crude gasoline obtained in the step 1) to a catalytic cracking absorption stabilization system for separation, to obtain a desulfurized dry gas, a desulfurized liquefied gas and a desulfurized stabilized gasoline.

Provided is a continuous process for converting waste plastic into recycle for polypropylene polymerization. The process comprises selecting waste plastics containing polyethylene and/or polypropylene, and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a naphtha/diesel fraction, a heavy fraction, and char. Pyrolysis oil and wax, comprising naphtha/diesel and heavy fractions, is passed to a refinery FCC unit. A liquid petroleum gas C.sub.3 olefin/paraffin mixture is recovered from the FCC unit. The C.sub.3 paraffins and C.sub.3 olefins are separated into different fractions with the C.sub.3 olefin fraction passed to a propylene polymerization reactor, and the C.sub.3 paraffin fraction passed optionally to a dehydrogenation unit to produce additional propylene.

Processes for using pyrolysis gas as a feedstock or a co-feedstock for making a variety of chemicals, for example, circular ethylene, circular ethylene polymers and copolymers, and other circular products. In these processes, pyrolysis reactor conditions can be selected to increase or optimized the production of pyrolysis gas over pyrolysis oil, and the pyrolysis gas which is usually used as fuel or flared can be fed downstream of the steam cracker furnace for economic use to form circular chemicals. Operating parameters of the pyrolysis unit may be adjusted to increase or decrease the proportion of pyrolysis gas relative to pyrolysis liquid as a function of their relative economic values.