The present invention provides a cold-wall reactor for suspension-bed hydrogenation, comprising a reactor body, which is provided with a reaction product outlet arranged at the top thereof, a cold hydrogen gas inlet arranged on a side wall thereof and a feed inlet arranged at bottom thereof, and the reactor body comprises, in a sequence from external to internal, a housing, a surfacing layer and a thermal insulation liner, and an inner liner cylinder, which is fixedly arranged inside the reactor body and is provided with an outlet on top thereof and an inlet on bottom thereof, wherein the outlet of the inner liner cylinder is connected with the reaction product outlet in a sealing manner, and the inlet of the inner liner cylinder is communicated with the feed inlet, wherein a side wall of the inner lining cylinder and an inner side wall of the reactor body define a cavity serving as a first circulation channel, wherein a second circulation channel is arranged on the side wall of the inner lining cylinder, and wherein an interior of the inner lining cylinder is communicated with the first circulation channel through the second circulation channel; by using the cold-wall reactor for suspension-bed hydrogenation, the material temperature is more uniform and reaction efficiency is improved, materials coking is reduced. In addition the falling and damaging of the thermal insulation liner is prevented, and the temperature of the outer wall of the reactor body is lower than the temperature of the medium.

An apparatus for introducing droplets of a monomer solution for production of poly(meth)acrylate into a reactor for droplet polymerization, comprising at least one channel or a dropletizer head, the channel or the dropletizer head being sealed at its base by a dropletizer plate, the dropletizer plate having holes through which the monomer solution is introduced into the reactor, and the dropletizer plate being configured such that holes that, in an axially symmetric dropletizer plate or in an annular dropletizer plate or in one configured as a ring segment, are not on a center line of the dropletizer plate or, in the case of a circular dropletizer plate, are not at the center of the dropletizer plate are aligned such that monomer solution is introduced through the holes into the reactor at an angle to the vertical, and the holes in the case of a radial alignment of axially symmetric dropletizer plates being aligned such that the angle at which the monomer solution is introduced into the reactor decreases in the direction of the axis of the reactor and, in the case of dropletizer plates arranged parallel to one another or of concentrically arranged dropletizer plates, each being aligned on a line parallel to the center line or line running concentrically about the center, such that the angle at which the monomer solution is introduced into the reactor is constant.

The present invention relates to a process for converting natural gas to higher hydrocarbon(s) including aromatic hydrocarbon(s) in n reaction zones operated in series, wherein m reaction zones are not participating in the conversion process and only (nm) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said natural gas to an effluent having said higher hydrocarbon(s). An object of the present invention is to provide a process for converting natural gas to higher hydrocarbon(s) including aromatic hydrocarbon(s) wherein a high reactant, i.e. methane, conversion can be achieved.

A process may include shutting down a reactor in which ethylbenzene is undergoing dehydrogenation to styrene in the presence of steam and a catalyst adapted to catalyze dehydrogenation of ethylbenzene to styrene. Shutting down the reactor may include reducing a temperature of the reactor. Shutting down the reactor may include supplying a purge stream to the reactor. Supplying a purge stream may include increasing a steam-to-ethylbenzene molar ratio of an input stream to the reactor. Supplying a purge stream may include supplying steam and one or more of H.sub.2, CO.sub.2, and styrene to the reactor. The process may include stopping supply of the purge stream to the reactor and supplying an inert gas purge stream to the reactor. Shutting down the reactor may be performed without use of a steam-only purge stream.

A system and method for temperature control in an oxygen transport membrane based reactor is provided. The system and method involves introducing a specific quantity of cooling air or trim air in between stages in a multistage oxygen transport membrane based reactor or furnace to maintain generally consistent surface temperatures of the oxygen transport membrane elements and associated reactors. The associated reactors may include reforming reactors, boilers or process gas heaters.

Processes for shutting down a hydroprocessing reactor and for removing catalyst from the reactor may comprise shutting off hydrocarbon feed to the reactor, stripping hydrocarbons from the catalyst, cooling the reactor to a first threshold reactor temperature, purging the reactor with N.sub.2 gas, introducing water into the reactor, and dumping the catalyst from the reactor, wherein the first threshold reactor temperature may be substantially greater than 200 F. In an embodiment, the water may be introduced into the reactor via a quench gas distribution system when the reactor is at a second threshold reactor temperature not greater than 200 F. to cool the reactor to a third threshold reactor temperature not greater than 120 F.

A fluidized bed reactor system including a fluidized bed reactor configured to receive a heated light hydrocarbon feed stream flowing upwards and a heated regenerated catalyst at a temperature sufficient to crack the heated light hydrocarbon feed stream to produce a product effluent stream containing hydrogen and spent catalyst having coke deposits, a catalyst regeneration unit operatively connected to a bottom portion of the fluidized bed reactor, the catalyst regeneration unit being configured to receive the spent catalyst flowing downwards and combust the coke deposits to produce the heated regenerated catalyst and a heated gas effluent for generating the heated light hydrocarbon feed stream, and a riser externally attached to the fluidized bed reactor and the catalyst regeneration unit, the riser being configured to receive the heated regenerated catalyst and a gas-based stream to flow the heated regenerated catalyst upwards to the fluidized bed reactor.

A method for the reduction of a metal oxide-containing material in which a reducing gas that is obtained using ammonia (NH.sub.3) is used. The reducing gas is supplied to a reduction reactor containing the metal oxide-containing material, and a top gas is discharged from the reduction reactor. At least one sub-quantity of the top gas is used as components in the preparation of the reducing gas, optionally after the top gas is prepared. A device for the reduction of the metal oxide-containing material that includes a reduction reactor, a top gas discharge line for discharging top gas, a supply line for an ammonia contribution, a preparation system for preparing the reducing gas, a supply line for the ammonia contribution leading into the preparation system, and a feed line for feeding the reducing gas and/or a precursor of the reducing gas to the reduction reactor.

Pretreatment of biomass using targeted alkaline hydrolysis with optional alkali recovery is shown, where the biomaterial is steam exploded before an alkaline hydrolysis by a) Providing a wetted biomass, b) Flashing the wetted biomass into a pretreatment reactor at a selected pressure, c) Subjecting the biomass to thermal hydrolysis and steam explosion after holding the biomass at a temperature for 10-45 minutes, d) Subjecting the steam exploded biomass to an alkaline hydrolysis by adding an alkali component in a selected concentration obtaining an alkali reacted biomass slurry.

Apparatus is also shown having a conditioning unit (B), a feed sluice (C) configured to receive conditioned biomass and guide the biomass to the inlet of a pretreatment reactor/tank (D) for thermal hydrolysis/steam explosion, a flash tank (E), a hydrolysis tank (F) for alkaline hydrolysis, and a separation unit (G) in which the pretreated slurry can be separated into liquid and solid.

The present invention relates to a device and method for continuous recovery of ammonia nitrogen from aluminum ash. The device comprises a reaction kettle, a steam generator, and a feeder. The steam generator and the feeder are both mounted on the reaction kettle. The steam generator delivers steam into the reaction kettle, and the feeder is used to deliver aluminum ash into the reaction kettle. The device further includes an intersection dispersion assembly and a cyclic motion assembly. The intersection dispersion assembly is installed inside the reaction kettle and is used for intersecting and dispersing the steam and aluminum ash. In the present invention, operations are performed in sequence on two dispersion surfaces. Both helical surfaces of the blade are used, which improves space utilization and increases the total dispersion area. Within one cycle, aluminum ash is spread and scraped completely, effectively improving processing efficiency.