The present application generally relates to the introduction of a renewable fuel oil as a feedstock into refinery systems or field upgrading equipment. For example, the present application is directed to methods of introducing a liquid thermally produced from biomass into a petroleum conversion unit; for example, a refinery fluid catalytic cracker (FCC), a coker, a field upgrader system, a hydrocracker, and/or hydrotreating unit; for co-processing with petroleum fractions, petroleum fraction reactants, and/or petroleum fraction feedstocks and the products, e.g., fuels, and uses and value of the products resulting therefrom.

A system and method of continuous production of methanol is disclosed utilizing enriched syngas and a homogenous liquid catalyst comprising an organo-nickel compound, an ether solvent, and an organic methoxide salt. The syngas is directed into a reaction chamber in such a way as to maximize the gas-liquid interface (e.g., an eductor nozzle or bubble column) while two condensers receive tail gas and reactant fluid from the reaction chamber, the latter after undergoing flash separation. Liquid catalyst is recovered and recycled back into the system via the second condenser.

A vessel for the downflow of a preferably hydrocarbon liquid, containing solid particles: a bottom comprising a cylindrical upper part (11), a lower part (12) with a decreasing cross section and a varying angle of inclination with respect to the vertical axis (Z), and an outlet pipe (9); injections (5) and (6) of recirculated and/or of makeup liquid into the lower and upper parts respectively; injections (5) inclined with respect to the tangent to the wall of the lower part at the injection point by an angle 1 in the vertical plane (xz) and by an angle 2 in the horizontal plane (xy); injections (6) are inclined with respect to the wall of the upper part by an angle 01 in the vertical plane (xz) and by an angle 2 in the horizontal plane (xy).

A method for manufacturing a polymer by performing an anionic polymerization reaction by a flow-type reaction, including: introducing a liquid A containing an anionic polymerizable monomer, a liquid B containing an anionic polymerization initiator, and a polymerization terminator into different flow paths respectively and causing the liquids to flow in the respective flow paths; causing the liquid A and the liquid B to join together by using a multilayered cylindrical mixer; subjecting the anionic polymerizable monomer to anionic polymerization while a solution formed by the joining is flowing to downstream in the reaction flow path; and causing a polymerization reaction solution flowing in a reaction flow path and the polymerization terminator to join together such that the polymerization reaction is terminated; and a flow-type reaction system suitable for performing the manufacturing method.

Methods of adding a catalyst to a bulk polymerization process may include mixing the catalyst with propylene to form a catalyst mixture that is substantially free of any C20 or greater hydrocarbons, feeding the catalyst mixture into a polymerization reactor, activating the catalyst mixture; and performing a polymerization on the catalyst mixture in the polymerization reactor. Polymers may be formed by polymerization processes that are substantially free of any C20 or greater hydrocarbons.

Methods for determining the concentration of transition metal compounds in a solution containing more than one transition metal compound are described. Polymerization reactor systems providing real-time monitoring and control of the concentrations of the transition metal components of a multicomponent catalyst system are disclosed, as well as methods for operating such polymerization reactor systems and for improving methods of preparing the multicomponent catalyst system.

Briefly, in one aspect, a catalytic assembly described herein comprises a module comprising at least one layer of structural catalyst bodies having an inlet face for receiving a gas stream. A diffuser assembly is arranged a distance of greater than 50 mm from the inlet face, the diffuser assembly including at least one diffuser element comprising a plurality of apertures, wherein a ratio of aperture length (L) in the gas stream flow direction to aperture hydraulic diameter (D.sub.a) is less than 1.

In an embodiment, a reactor for carrying out a melt transesterification reaction at a reactor temperature of 160 to 300 C. and a reactor pressure of 5 to 200 mbar, comprises a cylindrical tank comprising a top, a side, and a bottom, wherein the bottom is convex, extending away from the top; a stirring shaft disposed within the cylindrical tank along an axis thereof so that it is rotatable from outside of the cylindrical tank; a stirring blade extending from the stirring shaft in the cylindrical tank; a reactant solution inlet located on the bottom; and a reaction solution outlet located on the bottom. The reactor can be used for the polymerization of a polycarbonate oligomer.

A process to form an ethylene-based polymer in a reactor system, said process comprising at least the following steps: a) injecting a first initiator mixture into the tubular reactor at location L along the reactor, b) injecting a compressed make-up CTA system at the location L.sub.1, at a distance (LL.sub.1) from 145*D.sub.prehehater to 1000*D.sub.preheater, upstream from L, and wherein D.sub.preheater=the inner diameter of the pre-heater in meter (m); and wherein L.sub.1 is located in the preheater, and c) optionally, injecting one or more additional compressed make-up CTA system(s) into the preheater, at one or more location: L.sub.iL.sub.i+1, L.sub.n (2i and 2n), upstream from L.sub.1, and each location is, independently, at a distance from 145*D.sub.prehehater to 1000*D.sub.preheater, and wherein n equals the total number of injection locations of the make-up CTA system(s) injected into the preheater, upstream from L.sub.1, and wherein (LL.sub.1) is less than each (LL.sub.i), (LL.sub.i+1), (LL.sub.n); and d) polymerizing a reaction mixture comprising at least ethylene, the first initiator mixture, and the compressed make-up CTA system of step b), and wherein the process has a log coefficient of variation (log(CoV.sub.1)), at L.sub.1, that meets the relationships described herein.

A withdrawal system for withdrawing particulate matter from a high-temperature unit of a high-temperature industrial process is disclosed. The withdrawal system comprises a material storage silo that comprises a vent line containing a first vent valve, one or more temperature sensors to measure temperature of the particulate matter in the material transfer line, and a controller that receives output measurements from the one or more temperature sensors to monitor and control flow of the particulate matter. The system does not contain a receiving vessel located in the material transfer line between the high-temperature unit and the material storage silo.