Provided is a system for transferring reaction solution, including: a reactor that receives and reacts a feed stream to form a reaction solution; a reactor discharge pipe that is provided on a side portion of the reactor at a position corresponding to a surface height of the reaction solution in the reactor and connected to a precipitation tank to transfer the reaction solution from the reactor to the precipitation tank; and a precipitation tank that precipitates a polymer contained in the reaction solution to form a supernatant.

A synthesis reactor for producing carbon nanotubes. The reactor includes a main reactor, a feeder, a settler, an air inlet device, and a product outlet. The main reactor communicates with the settler in the form of a communicating vessel. The feeder communicates with the settler via a catalyst inlet. The air inlet device is disposed under the settler. The wall of the main reactor is provided with a heat exchanger. The product outlet is disposed at the lower part of the main reactor. A method for producing a carbon nanotube, includes: 1) drying red mud for 1 to 4 hour(s) at the temperature of between 101 C. and 109 C.; 2) smashing and sieving the red mud through a 200-mesh sieve to yield a catalyst; and 3) adding the catalyst to a synthesis reactor.

The invention relates to a process and system for the continuous polymerization of one or more -olefin monomers comprising the steps of: (a) withdrawing fluids from a reactor (b) cooling fluids comprising the withdrawn fluids with a cooling unit (c) introducing the cooled fluids to a separator to separate at least part of the liquid from these fluids to form a liquid phase and a gas/liquid phase (d) introducing the gas/liquid phase below to the reactor below a distribution plate (e) introducing the liquid phase to a settling tank to separate liquid from fines that settle down in the settling tank (f) introducing liquid from the settling tank up stream of the cooling unit.

The disclosure includes a process and a plant for separating a suspension C from a suspension A, wherein the fraction of particles P.sub.C in the suspension C, which have a diameter smaller than a defined limit grain diameter, is greater than in the suspension A by at least the factor of 2. The suspension A is introduced into a container extending from the bottom to the top and a suspension B is withdrawn from the container, whose fraction of particles with a diameter greater than the defined limit grain diameter is increased with respect to suspension A. Due to the fact that suspension C is withdrawn from the container in a second partial stream above the first partial stream, in that the flow velocity of the suspension C is greater than the sinking velocity of the particles P.sub.C contained therein, an effective separation can be achieved.

The present disclosure relates to converting equilibrium-limited reactions. Various embodiments may include methods and apparatus for such reactions, such as a method for converting equilibrium-limited reactions comprising: delivering a catalyst material to a reaction zone of a reactor; delivering starting materials into the reaction zone; reacting the materials to form a product; introducing a sorbent into the reactor; taking up the products with the sorbent; and collecting the sorbent once it is loaded with products in a collection zone of the reactor. In some embodiment, the reaction zone is separated from the collection zone in the reactor.

Aspects of the invention provide a process for upgrading a hydrocarbon feed. The process includes providing a hydrocarbon feed and a utility fluid. Then selectively extracting from the feed at least a portion of particulates to produce a raffinate and an extract. Third hydroprocessing at least a portion of the raffinate.

A system for providing Closed Loop Reformation (CLR) based synthesis gas (syngas) production processes and systems where the metal oxidation and reduction systems are decoupled from the system and process thereby avoiding the closed and coupled loop metal oxidation and reduction systems used with prior art CLR based syngas production processes and systems, and the high temperature complexities associated with prior art CLR based syngas production processes and systems.

The present invention provides a method of cooling and cycling a regenerated catalyst. The regenerated catalyst that is from the regenerator is cooled by the catalyst cooler to 200-720 C., and without being mixed with the hot regenerated catalyst directly enters a riser reactor, or mixes with another part of hot regenerated catalyst that has not been cooled to obtain a mixed regenerated catalyst with a temperature below the regenerator temperature, and enters the riser reactor. The hydrocarbon raw material performs the contact reaction with the catalyst in the riser reactor, a reactant stream enters a settler to perform a separation of the catalyst and an oil gas, the separated spent catalyst is steam stripped by a steam stripping section and enters a regenerator to be charring regenerated, and the regenerated catalyst after being cooled returns to the riser reactor to be circularly used. The bottom of each of the catalyst coolers is provided with at least one fluidized medium distributor, the range of the superficial gas velocity is 0-0.7 m/s (preferably 0.005-0.3 m/s, and most preferably 0.01-0.15 m/s), and the temperature of the cold regenerated catalyst is controlled mainly by adjusting a flow rate of the fluidized medium. The method of cooling and cycling a regenerated catalyst of the present invention has extensive application, and can be used for various fluidized catalytic cracking processes, including heavy oil catalytic cracking, wax oil catalytic cracking, gasoline catalytic conversion reforming and the like, and can also be used for other gas-solid reaction processes, including residual oil pretreating, methanol to olefin, methanol to aromatics, methanol to propylene, fluid coking, flexicoking and the like.

Systems and methods for upgrading a hydrocarbon stream to a lower boiling point hydrocarbon feed material are disclosed. The system includes a feeding device to transport a hydrocarbon stream that includes an alternative feedstock. The hydrocarbon stream is partially cracked in a first cracking unit producing a lower boiling point hydrocarbon feed material, a catalyst rich heavy hydrocarbon stream, and coke. A slurry settler receives the catalyst rich heavy hydrocarbon stream and coke and separates the catalyst from the catalyst rich heavy hydrocarbon stream thereby defining a catalyst rich stream and a heavy hydrocarbon stream. A coking vessel receives the heavy hydrocarbon stream and coke and separates the heavy hydrocarbons from the coke thereby defining a heavy hydrocarbon stream. Finally, a second cracking unit that receives the lower boiling point feed material from the first cracking unit and produces olefins and aromatics.

Vapor and liquid flow concurrently down through a vertical vessel. A horizontal scale collection and predistribution tray is located in the vessel to remove solid contaminants and to redistribute the liquid to a fine distribution tray. The scale collection and predistribution tray consists of a tray plate with a scale collection zone where the solid contaminants settle and deposit. In one embodiment, an upstanding permeable wall forms the scale collection zone, and liquid is filtered as it flows through the permeable wall, leaving the solid contaminants trapped upstream from the permeable wall. The predistribution tray has a rim provided with a slotted weir. Liquid from the scale collection zone forms a liquid level in a trough located between the permeable wall and the weir. Due to the uniform liquid level in the trough, liquid flow rates through the slots in the weir are nearly equal. Because of the polygonal shape of the tray, the liquid exits the slots in a direction along lanes defined between distribution units on the fine distribution tray, and the amount of liquid entering the vapor inlets of the distribution units is therefore small. Vapor by-passes the scale collection and pre-distribution tray through the area between the reactor wall and the permeable wall, and through the area between the reactor wall and the weir to the fine distribution tray. The scale collection and predistribution tray protects the fine distribution tray and the catalyst bed from fouling, pre-distributes liquid to the fine distribution tray to minimize level gradients on this tray, and reduces flow velocities to ensure calm flow conditions on the fine distribution tray.