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.

A reactor system for thermally treating a hydrocarbon-containing stream, that includes a pressure containment vessel comprising an interior chamber and a heat transfer medium that converts electrical current to heat and is positioned within the interior chamber of the pressure containment vessel, wherein the heat transfer medium comprises a first end face, a second end face, and channels extending between the first end face and the second end face. A process for thermally treating a hydrocarbon-containing stream includes introducing the hydrocarbon-containing stream into the reactor system, pressurizing the pressure containment vessel and the heat transfer medium without heating the pressure containment vessel or the heat transfer medium, supplying electrical current to the heat transfer medium, converting the electrical current to heat, heating the hydrocarbon-containing stream, and converting the hydrocarbon-containing stream to an effluent stream.

The present invention relates to a catalyst for preparing a light olefin, a preparation method therefor, and a method for preparing a light olefin by using same, and can provide a catalyst for preparing a light olefin, a preparation method therefor, and a method for preparing a light olefin by using same, the catalyst comprising a porous zeolite, a clay, an inorganic oxide binder, and Ag.sub.2O and P.sub.2O.sub.5 which are supported in the pores and/or on the surface of the porous zeolite.

Systems and methods for producing olefins and/or aromatics are disclosed. Methods disclosed includes aqua-processing hydro-processing of crude oils and/or heavy oils and/or residue, in an aqua-processing hydro-processing unit, to produce intermediate products, which can then be used to make valuable chemicals such as olefins and aromatics.

The invention relates to a process for producing C2 and C3 hydrocarbons, comprising a) subjecting a mixed hydrocarbon feedstream to first hydrocracking in the presence of a first hydrocracking catalyst to produce a first hydrocracking product stream; b) separating the first hydrocracking product stream to provide a light hydrocarbon stream comprising C4− hydrocarbons and c) subjecting the light hydrocarbon stream to C4 hydrocracking in the presence of a C4 hydrocracking catalyst to obtain a C4 hydrocracking product stream comprising C2 and C3 hydrocarbons.

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 present invention relates to a process for the production of butenes and butadienes from waste plastics feedstocks comprising the steps in this order of: (a) providing a hydrocarbon stream A obtained by hydrotreatment of pyrolysis oil produced from a waste plastics feedstock; (b) optionally providing a hydrocarbon stream B; (c) supplying a feed C comprising a fraction of the hydrocarbon stream A and optionally a fraction of the hydrocarbon stream B to a thermal cracker furnace comprising cracking coil(s); (d) performing a thermal cracking operation in the presence of steam to obtain a cracked hydrocarbon stream D; (e) supplying the cracked hydrocarbon stream D to one or more separation units; (f) performing a separation operation to obtain different streams of chemical products comprising ethylene, propylene, isobutene, 1-butene, 2-butene, 1,2-butadiene, 1,3-butadiene, benzene, styrene, toluene, ethylbenzene and xylenes; wherein in step (d): the coil outlet temperature is >800 and <870° C., preferably >805 and <835° C.; and the weight ratio of steam to feed C is >0.3 and <0.8, preferably >0.3 and <0.5. Such process allows for optimisation of the quantity of waste plastic material that finds its way back into products that are produced as outcome of the process. The higher that quantity is, i.e. the higher the quantity of chemical building blocks that are present in the waste plastic material that are converted to the produced products, the better the sustainability footprint of the process is. The process allows for circular utilisation of plastics.

An ethylene cracking furnace is provided. The ethylene cracking furnace includes at least one radiant section. The at least one radiant section includes bottom burners and/or sidewall burners, and at least one radiant coil arranged in the radiant section. The radiant coil includes at least an upstream pass tube and a downstream pass tube, the upstream pass tube being configured as an inner tube, and the downstream pass tube being configured as an outer tube surrounding the inner tube and having a closed end. The inner tube defines an inner space forming an upstream flow path. A gap defined between the inner tube and the outer tube forms an downstream flow path.

The invention provides a process for the preparation of an olefinic product, the comprising: (a) reacting an oxygenate to produce an effluent stream, comprising at least oxygenate, olefin, water and acidic by-products; (b) cooling the effluent stream by means of an indirect heat exchange to a temperature greater than the dew point temperature of effluent stream; (c) further rapidly cooling the effluent stream to a temperature at or lower than the dew point temperature of the reaction effluent stream by direct injection of a first aqueous liquid into the effluent stream, to form a quench effluent stream; (d) separating the first quench effluent stream into a liquid quench stream and a gaseous quench stream; and passing the gaseous quench stream into a quench tower and contacting the gaseous quench stream with a second aqueous liquid, to produce a quench tower gaseous stream comprising the olefinic product.

Distillate cracks to propylene more readily than VGO. Additionally, less branched hydrocarbons crack to propylene more readily than more branched hydrocarbons. Oligomerization to diesel range oligomers followed by catalytic cracking with less branched oligomers can provide more propylene.