A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 in.sup.−1 to 5 in.sup.−1, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr.sup.−1)(gal.sup.−1) to 6.0 (lb)(hr.sup.−1)(gal.sup.−1).

Provided is a continuous reactor system for producing graphene or an inorganic 2-D compound, the reactor comprising: (a) a first body comprising an outer wall and a second body comprising an inner wall, wherein the inner wall defines a bore and the first body is configured within the bore and a motor is configured to rotate the first and/or second body; (b) a reaction chamber between the outer wall of the first body and the inner wall of the second body; (c) a first inlet and a second inlet disposed at first end of the reactor and in fluid communication with the reaction chamber; (d) a first outlet and a second outlet disposed downstream from the first inlet, the outlets being in fluid communication with the reaction chamber; and (e) a flow return conduit having two inlets/outlets in fluid communication with two ends of the reactor.

Provided is a continuous reactor system for producing graphene or an inorganic 2-D compound, the reactor comprising: (a) a rust body comprising an outer wall and a second body comprising an inner wall, wherein the inner wall defines a bore and the first body is configured within the bore and a motor is configured to rotate the first and/or second body; (b) a reaction chamber between the outer wall of the first body and the inner wall of the second body; (c) a first inlet and a second inlet disposed at first end of the reactor and in fluid communication with the reaction chamber; (d) a first outlet and a second outlet disposed downstream from the first inlet, the outlets being in fluid communication with the reaction chamber; and (e) a flow return conduit having two inlets/outlets in fluid communication with two ends of the reactor.

The present invention relates to an oligomerization process using a reaction device comprising a dispersion means. In particular, the process relates to the oligomerization of ethylene to give linear -olefins, such as 1-butene, 1-hexene or 1-octene, or a mixture of linear alpha-olefins.

A system and method for producing 1-butene and ultra-high-molecular-weight polyethylene (UHMWPE), including feeding a catalyst, an antifouling co-catalyst, and ethylene to a reactor, and dimerizing ethylene into 1-butene and polymerizing a relatively small portion of the ethylene into UHMWPE. A product slurry including 1-butene and UHMWPE is discharged from reactor and UHMWPE is removed from the product slurry as a coproduct of the product 1-butene. The coproduct UHMWPE may be a byproduct that is a relatively small amount of the product slurry. The quantity of UHMWPE produced may be small in comparison to the quantity of 1-butene produced.

The present invention provides a continuous polymerization apparatus capable of simply and efficiently separating a polymer and solid matter from a reaction mixture while having an apparatus configuration conducive to washing and maintenance, and a continuous production method for a polymer. A continuous polymerization apparatus (100) includes a plurality of reaction vessels (1a to 1c), wherein the plurality of reaction vessels are configured such that reaction mixtures (9a to 9c) successively move through each reaction vessel; in the plurality of reaction vessels, gas phase parts formed above the reaction mixture communicate with one another; and the continuous polymerization apparatus includes a washing part (5), the washing part configured to separate a solid included in the reaction mixture by sedimentation and to perform countercurrent washing.

The invention relates to a process for the production of thermoplastic moulding compounds, in particular for the production of acrylonitrile-butadiene-styrene (ABS), wherein at least a first reagent (11) and a second reagent (12) of the thermoplastic moulding compounds are fed to a loop conduit (29) which comprises a static mixer (36), wherein the reagents (11, 12) are pressed in loops through the loop conduit (29) and passing the static mixer (36), whereby the reagents (11, 12) are dispersed to form a dispersion (15) in the static mixer (36). The invention also relates to a thermoplastic moulding compound that is produced by the inventive process.

A reactor tank is provided having an enzyme inlet, a heating jacket positioned around the exterior center of the tank, a gas outlet for communicating with a vacuum apparatus to create a vacuum within the reactor tank and for communicating with a condensing unit, a first gas inlet for receiving gas from a feed tank and a first liquid outlet for recirculating the liquid from the first liquid outlet back to the feed tank. The reactor tank further includes a sparged unit and a screen positioned within the tank between the sparged unit and the first liquid outlet, where the sparged unit is connected to the first gas inlet for receiving gas from the feed tank. The reactor tank is utilized in a reactor system further including a condensing unit, vacuum pump or venturi valve, a first feed tank connected to the first gas inlet, a coalescer having at least one circulation pipe and a first circulation pump connected to the first liquid outlet for circulating a portion of the liquid dispelled from the liquid outlet to the coalescer, which after being filtered through coalescer is recirculated through circulation pipe back to the first feed tank.

Provided is a continuous production apparatus and a continuous production method capable of preventing the countercurrent of evaporation components generated at the time of polymerization so that continuous solution polymerization reactions can progress reliably. A continuous production apparatus (100) includes a housing chamber (2) configured to house a plurality of reaction vessels (1a to 1d); wherein a reaction mixture is formed by subjecting monomers to a polymerization reaction in a solvent in at least one of the reaction vessels; the reaction vessels communicate with one another via a gas phase part (4); the reaction vessels are sequentially connected; the reaction mixture successively moves to each of the reaction vessels; and the housing chamber includes a baffle (9) configured to narrow the cross-sectional area of the gas phase part at the boundary between at least one pair of adjacent reaction vessels or in the vicinity of the boundary.

A method of manufacture of high-solids hydroxide slurries from caustic calcined carbonate powder is described, whereby the properties of the slurry are its low resistance to shear thinning to facilitate transport, a high stability for transport and storage, ease of reconstitution after long periods of storage, and, as required, a high concentration of chemically reactive species at the particle surface. The method achieves these specifications by mixing caustic calcined carbonate or hydroxide powder with water in an insulated reactor vessel, and agitating the slurry sufficiently such that the hydration reaction causes the water to spontaneously boil, such that the remaining hydration proceeds spontaneously under the fixed conditions of boiling through the water loss. The mixing process is preferably carried out by a shear pump. A viscosity modifier, such as acetic acid, is used to thin the slurry to enable the mixing system to maintain uniform mixing. The reaction is terminated when the boiling has spontaneously ceased and the temperature has spontaneously dropped to a set point though the reactor heat losses, where the processing time is sufficiently long that the slurry meets the desired specifications.