A multi-stage process for transforming a high sulfur ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process that produces a Product Heavy Marine Fuel Oil that can be used as a feedstock for subsequent refinery process such as anode grade coking, needle coking and fluid catalytic cracking. The Product Heavy Marine Fuel Oil exhibits multiple properties desirable as a feedstock for those processes including a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process is also disclosed.

Systems, devices, and methods for a reactor feed distribution system. In some aspects, a multi-section pipe and an orifice plate. The multi-section pipe includes a first pipe section that defines a first channel and a second pipe section that defines a second channel. Second pipe section includes a first portion extending along a first longitudinal axis, a second portion extending along a second longitudinal axis that is angularly disposed relative to the first longitudinal axis, and a curved portion connecting the first portion to the second portion. The orifice plate is configured to be positioned at an inlet or a first outlet of the first pipe section. The orifice plate includes a maximum transverse dimension that is less than a minimum transverse dimension of each of the first and second channel.

A process for reducing the environmental contaminants in a ISO 8217: 2017 Table 2 compliant Feedstock Heavy Marine Fuel Oil and resulting product, the process involving: mixing a Feedstock Heavy Marine Fuel Oil with a Activating Gas to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture; separating the Product Heavy Marine Fuel Oil from the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil complies with ISO 8217:2017 Table 2 for residual marine fuel and the Environmental Contaminants, which are selected from the group consisting of: a sulfur; vanadium, nickel, iron, aluminum and silicon and combinations thereof, are less than 0.5 wt. %. The Product Heavy Marine Fuel Oil can be used as blending stock for an ISO 8217:2017 Table 2 compliant, IMO 2020 compliant, low sulfur heavy marine fuel composition.

The present disclosure discloses a continuous preparation method for a penem intermediate MAP. The continuous preparation method includes the following steps: step S1, in a column-type continuous reactor, using a rhodium-loaded catalyst to catalyze 4-nitrobenzyl(R)-2-diazo-4-((2R,3S)-3-((R)-1-hydroxyethyl)-4-oxoazetidin-2-yl)-3-oxopentanoate to generate a cyclization reaction so as to form a first intermediate, herein the rhodium-loaded catalyst is loaded in the column-type continuous reactor, and the rhodium-loaded catalyst has the following structural formula:

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step S2, performing an esterification reaction on the first intermediate, a diphenyl chlorophosphate and a diisopropylethylamine in a second continuous reactor, to obtain a product system containing the penem intermediate MAP; and step S3, performing crystallization treatment on the product system, to obtain the penem intermediate MAP.

A catalytic reactor comprises a floating particle catcher unit and a particle catching surface which extracts particles from the fluid flow stream above the catalyst bed whereby at least a part of the particles settles on the particle catching surface instead of clogging the catalyst bed.

A system for synthesizing ammonia includes a reactor including an inlet portion, an outlet portion, and an energy source arranged to deliver energy to one or more reactants receivable through the inlet portion of the reactor, and the energy source activatable to reduce nitrogen to ammonia in the presence of hydrogen, at least one hydrogen pump in fluid communication with the outlet portion of the reactor, each hydrogen pump including at least one electrochemical cell, and a recirculation circuit in fluid communication between the at least one hydrogen pump and the inlet portion of the reactor and configured to direct a respective hydrogen stream from each hydrogen pump to the inlet portion of the reactor.

The present invention relates to a plant and a process for producing propylene at least one oxygenate, comprising a reactor for converting the reactant mixture into a product mixture which comprises propylene and also aliphatic and aromatic C.sub.5+ hydrocarbons, at least one distillation column for removing a C.sub.5+ stream, the C.sub.5+ stream comprising at least 90 wt % of the aliphatic and aromatic C.sub.5+ hydrocarbons of the product mixture, an extractive distillation column for separating the C.sub.5+ stream into an aromatics stream and an aliphatics stream, the aliphatics stream comprising at least 90 wt % of the aliphatics of the C.sub.5+ stream, and the aromatics stream comprising at least 90 wt % of the aromatics of the C.sub.5+ stream, and an aliphatics recycle line for at least partial recycling of the aliphatics stream to the reactor. According to the invention, an aromatics recycle line is provided which returns the aromatics stream at least partially as extractant into the extractive distillation column.

The invention provides a support distributor for a scallop for use in a radial flow reactor. The support distributor includes an elongated sheet having a plurality of perforations extending through a thickness thereof, and at least three edges along a length thereof so as to form a member having at least three support points which engage an inner surface of the scallop.

A process and apparatus comprise a reaction chamber that includes an aspect ratio between about 0.7 and 1.3 for establishing a dense catalyst bed in the reaction chamber while minimizing hot residence time of the product gas in a range that will not deteriorate product selectivity. We have found the dense catalyst bed is necessary to ensure sufficient contact between catalyst and feed gas.

The present invention discloses a method of quickly desorbing phosgene from a catalyst in a phosgene synthesizing tower when the catalyst in the phosgene synthesizing tower is replaced. The method is carried out by first purging out easily-desorbed phosgene from the catalyst activated carbon in the phosgene synthesizing tower with nitrogen gas, then purging with ammonia gas, and the ammonia gas is reacted with the hardly-desorbed phosgene in the catalyst of the phosgene synthesizing tower. Then the phosgene synthesizing tower is rinsed with a water gun and then dried with hot gas. The phosgene content at an outlet of the phosgene synthesizing tower after purging is below 0.5 ppm, which can significantly save the time of the phosgene synthesizing tower for purging the phosgene, greatly reduce the amount of nitrogen gas consumed, and improve the safety of the process operation.