The invention relates to a termination device of a tubular reactor comprising at least one separation element adapted for the separation of solid particles and gaseous effluents and at least one coupling element that is part of an end of said tubular reactor, said separation element being connected to said coupling element, characterized in that each element of the termination device is made of ceramic material. The invention also relates to a tubular reactor, having a vertical or substantially vertical axis, of a fluid catalytic cracking unit equipped with a termination device according to the invention and to a corresponding fluid catalytic cracking unit.

Provided herein are reactor systems and processes for producing organic acids directly from beta-lactones. Such reactor systems and processes involve the use of a heterogeneous catalyst, such as a zeolite at vapor phase conditions. The reactor systems and processes may use a fixed bed, moving bed or fluidized contacting zone as reactor configurations.

The present invention relates a steam methane reformer tube outlet assembly and a method of assembling or retrofitting same. More specifically, it relates to an exposed flanged tube outlet of a reformer designed to mitigate metal dusting corrosion, dew point condensation-related metal fatigue and cracking, and over-temperature induced metal failures such as hydrogen attack.

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.

The present invention relates to a multi-stage, single reactor and system for making methanol for synthesis gas (syngas). In particular, the reactor contains a shell and tube reactor that is divided at its top and bottom heads into a plurality vertical, isolated compartments. The associated compartments and tubes form a stage of the reactor. The raw syngas is fed to the first stage, and unreacted syngas from the first stage is fed to the second stage subsequent stages. Between each stage, the product, methanol and water, is removed from the reaction mixture before sending the unreacted syngas to the subsequent stage. The reactor allows for high conversion of synthesis gas to methanol in a once-through process, without requiring recycling of unreacted synthesis gas.

A fuel synthesis catalyst of an embodiment for hydrogenating a gas includes at least one selected from the group consisting of; carbon dioxide and carbon monoxide, the catalyst comprising, a base material containing at least one oxide selected from the group consisting of; Al.sub.2O.sub.3, MgO, TiO.sub.2, and SiO.sub.2, first metals containing at least one metal selected from the group consisting of; Ni, Co, Fe, and Cu and brought into contact with the base material, and a first oxide containing at least one selected from the group consisting of; CeO.sub.2, ZrO.sub.2, TiO.sub.2, and SiO.sub.2 and having an interface with each of the first metals and the base material. The first metals exist on an outer surface of the base material, and on a surface of the base material in fine pores having opening ends on the outer surface of the base material and inside the base material. The first metals and the first oxide exist in the fine pores. The first metals have interfaces with the base material in the fine pores. The first metals exist inside the base material.

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.

A column includes a column head, a column sump and a tube-shaped column shell disposed therebetween, two or more reaction zones lying above each other which each accommodate a catalyst bed, in which catalyst beds chlorosilanes disproportionate into low-boiling silanes, which form an ascending stream of gas, and also into high-boiling silanes which form a downwardly directed stream of liquid, within the column shell and along the column axis, two or more rectificative separation zones, the reaction zones and the separation zones alternate along the column axis, the separation zones are configured such that the stream of gas and the stream of liquid meet in the separation zones, and the reaction zones are configured such that the downwardly directed stream of liquid is led through the catalyst beds, whereas the upwardly directed stream of gas passes the catalyst beds in spatial separation from the stream of liquid.

The present disclosure provides systems and methods for hydrogen production as well as apparatuses useful in such systems and methods. Hydrogen is produced by steam reforming of a hydrocarbon in a gas heated reformer that is heated using one or more streams comprising combustion products of a fuel in an oxidant, preferably in the presence of a carbon dioxide circulating stream.

The present disclosure provides systems and methods for hydrogen production as well as apparatuses useful in such systems and methods. Hydrogen is produced by steam reforming of a hydrocarbon in a gas heated reformer that is heated using one or more streams comprising combustion products of a fuel in an oxidant, preferably in the presence of a carbon dioxide circulating stream.