The present invention relates to a device for treatment of material transported through the device having a specific design.

The present disclosure provides a differential hydrogenation reaction apparatus. The apparatus comprises a mixing vessel, a plurality of microreactors and a raw material conveying device, and the mixing vessel is provided with reaction product inlets; each microreactor is used as a hydrogenation reaction place and is provided with a liquid phase reaction raw material inlet and a reaction product outlet, each reaction product outlet is connected with the corresponding reaction product inlet, the plurality of microreactors are divided into one group or a plurality of groups which are arranged in parallel, and each group comprises at least one microreactor arranged in parallel; and the raw material conveying device is arranged on a feeding pipeline of the liquid phase reaction raw material inlet. The problems of high pressure unsafety and non-equilibrium in the hydrogenation reaction process can be effectively solved by adopting the reaction apparatus.

A pyrolysis reactor (12) and method for the pyrolysis of hydrocarbon gases (e.g., methane) utilizes a pyrolysis reactor (12) having a unique burner assembly (44) and pyrolysis feed assembly (56) that creates an inwardly spiraling fluid flow pattern of the feed gases to form a swirling gas mixture that passes through a burner conduit (46) with a constricted neck portion or nozzle (52). At least a portion of the swirling gas mixture forms a thin, annular mixed gas flow layer immediately adjacent to the burner conduit (46). A portion of the swirling gas mixture is combusted as the swirling gas mixture passes through the burner conduit (46) and a portion of combustion products circulates in the burner assembly (44). This provides conditions suitable for pyrolysis of hydrocarbons or light alkane gas, such as methane or natural gas.

Methods related generally to the removal of atmospheric pollutants from the gas phase, are provided. The methods involve contacting a first stream comprising NO and/or NO.sub.2 with a second stream comprising (ClO.sub.2).sup.0 to provide a third stream comprising NO and NO.sub.2 at a molar ratio of about 1:1; and contacting the third stream with a fourth stream comprising an aqueous metal hydroxide (MOH) solution to convert NO and NO.sub.2 to MNO.sub.2.

Phosgene is mixed with an organic polyamine to produce polyisocyanate compounds. A phosgene flow is established in a conduit (15), and the organic polyamine is injected into the phosgene flow. A constricted region (4) of the conduit (15) resides downstream of the point of the polyamine injection. The presence of the constricted region (4) reduces by-product formation.

A pyrolysis reactor (12) and method for the pyrolysis of hydrocarbon gases (e.g., methane) utilizes a pyrolysis reactor (12) having a unique burner assembly (44) and pyrolysis feed assembly (56) that creates an inwardly spiraling fluid flow pattern of the feed gases to form a swirling gas mixture that passes through a burner conduit (46) with a constricted neck portion or nozzle (52). At least a portion of the swirling gas mixture forms a thin, annular mixed gas flow layer immediately adjacent to the burner conduit (46). A portion of the swirling gas mixture is combusted as the swirling gas mixture passes through the burner conduit (46) and a portion of combustion products circulates in the burner assembly (44). This provides conditions suitable for pyrolysis of hydrocarbons or light alkane gas, such as methane or natural gas.

A supercritical water oxidation-flame piloted vortex reactor has a hydrothermal flame produced within the interior of the reactor fed by a fuel including a waste water stream, and has a subcritical wash stream, including water below its critical point, that creates an upward helical flow in the material within the reactor. The hydrothermal flame and upward helical flow produce within the reactor a supercritical core region, a subcritical outer region around the core region, and a transcritical intermediate region between them. The upward helical flow serves to transfer precipitated ionic compounds out of the supercritical core region, through the transcritical intermediate region, and into the subcritical outer region where they re-dissolve. A processed flow, including purified water, is removed from an upper portion of the supercritical core region by an aspirator.

An installation and method for production of nanopowders by spray pyrolysis by capture, grind, and temperature exposure of nanoparticles, wherein efficiency of particle retention in the cyclone in the suspended state is achieved.

Methods of forming crosslinked cellulose include mixing a crosslinking agent with an aqueous mixture of cellulose fibers containing little to no excess water (e.g., solids content of 25-55%), drying the resulting mixture to 85-100% solids, then curing the dried mixture to crosslink the cellulose fibers. Systems include a mixing unit to form, from an aqueous mixture of unbonded cellulose fibers having a solids content of about 25-55% and a crosslinking agent, a substantially homogenous mixture of non-crosslinked, unbonded cellulose fibers and crosslinking agent; a drying unit to dry the substantially homogenous mixture to a consistency of 85-100%; and a curing unit and to cure the crosslinking agent to form dried and cured crosslinked cellulose fibers. Intrafiber crosslinked cellulose pulp fibers produced by such methods and/or systems have a chemical on pulp level of about 2-14% and an AFAQ capacity of at least 12.0 g/g.

A fluid distribution system (208) is provided for a reactor vessel (200) defining a reaction chamber (202). The fluid distribution system (208) may include a radial distribution component (224) positionable within the reaction chamber (202) and adjacent a vessel inlet (212) at an end portion of the reactor vessel (200). The radial distribution component (224) may include one or more annular distribution conduits (230) configured to receive a fluid mixture provided to the reactor vessel (200). The fluid distribution system (208) may also include an axial distribution component (226) positionable within the reaction chamber (202) to extend from the radial distribution component (224) along a longitudinal axis of the reactor vessel (200). The axial distribution component (230) may include a plurality of helical conduits (236) fluidly coupled with the one or more annular distribution conduits (230) and configured to receive the fluid mixture from the one or more annular distribution conduits (230) and to disperse the fuel mixture uniformly within the reaction chamber (202).