A load-following reactor system and associated facilities for improved control of a reactor under varying loads. The load-following reactor may be a tube-cooled reactor for methanol synthesis. A reactant may be controlled by at least one valve element such that a portion of the reactant is fed to the reactor through the reactor tubes, and a portion of the reactant is fed to the reactor after being heated in a heat exchanger. The heated portion of the reactant may be fed to the reactor after the tubes. The valve element may be controlled based on a temperature of the reactor and/or a flowrate of reactant feed to adapt the temperature of the reactor to the changing reactant flowrate.

A method for carrying out catalytic gas phase reactions including providing a tube bundle reactor which has a bundle of reaction tubes that are filled with a catalyst charge and are cooled by a heat transfer medium, conveying a reaction gas through the catalyst charge, the reaction gas flowing into each reaction tube divided into two part flows introduced in the axial direction of the reaction tube at different points in the catalyst charge the catalyst charge has at least two catalyst layers of different activity, wherein the activity of the first catalyst layer, in the flow direction of the reaction gas, is lower than the activity of the at least one other catalyst layer and in step a first part flow is introduced into the first catalyst layer and each further part flow is introduced past the first catalyst layer into the at least one further catalyst layer.

Fluidized-bed reactor for the gas-phase polymerization of olefins including a gas distribution grid installed in a lower part of the fluidized-bed reactor and a gas recycle line, which is equipped with a compressor and a heat exchanger and which is connected at the upper end with the top of the fluidized-bed reactor, wherein the gas recycle line splits at the lower end in at least two horizontal branches which are connected tangentially with the fluidized-bed reactor below the gas distribution grid and a process for preparing an olefin polymer carried out in the fluidized-bed reactor.

Systems and methods for isomerizing n-butane to form isobutane are disclosed. A segmented reactor system is used to isomerize n-butane. The segmented reactor system comprises a segmented reactor that includes a first catalyst bed and a second catalyst bed separated by a first heat exchanger. The catalyst in the first catalyst bed does not contact the catalyst in the second catalyst bed. During the exothermic process of isomerizing n-butane, the first heat exchanger extracts heat from an intermediate product flowing from the first catalyst bed to the second catalyst bed to improve the conversion rate of n-butane.

A reactor having a shell comprising one or more reactor tubes located within the shell, said reactor tube or tubes comprising a plurality of catalyst receptacles containing catalyst; means for providing a heat transfer fluid to the reactor shell such that the heat transfer fluid contacts the tube or tubes; an inlet for providing reactants to the reactor tubes; and an outlet for recovering products from the reactor tubes; wherein the plurality of catalyst receptacles containing catalyst within a tube comprises catalyst receptacles containing catalyst of at least two configurations.

The present application provides a high-gravity device for generating nano/micron bubble and a reaction system. In the device, the liquid phase is continuous phase and the gas phase is dispersed phase. A gas enters the interior of the device from a hollow shaft, and the gas is subjected to primary shearing under a shearing effect of aerating micropores to form bubbles; then, the bubbles rapidly disengage from the surface of a rotating shaft under the effect of the rotating shaft rotating at a high speed, and are subjected to secondary shearing under the high-gravity environment with the strong shearing force formed by the rotating shaft to form nano/micron bubbles. The device has the advantages of fastness, stability, and small average particle size. The average particle size of the formed nano/micron bubbles is between 800 nanometers and 50 microns, and the average particle size of the bubbles can be regulated in a range by adjusting the rotating speed of the rotating shaft.

A process and a device for continuous flow side-chain alkylation which relate to the technical field of organic synthesis. In this process and the device for continuous flow side-chain alkylation, an ibuprofen raw material is prepared with alkylbenzene as a raw material. This raw material alkylbenzene is easily available and has a low cost, and is suitable for scale-up production. Moreover, an entire preparation process adopts continuous chemical synthesis, and a reaction time of each stage can be precisely controlled, which is beneficial to control a total reaction time and reduce an amount of impurities produced. In this way, a purity and a yield of the ibuprofen raw material are improved. In summary, a continuous synthesis method for side-chain alkylation of alkylbenzene provided by the present disclosure shows a low cost and a high yield.

The present disclosure provides a method for preparing a transition metal lithium oxide, comprising steps of: A) mixing a lithium salt and a transition metal compound, and performing a pretreatment to obtain a precursor; wherein the pretreatment temperature is 100-300° C.; and the pretreatment time is 1-10 h; B) precalcining the precursor to obtain an intermediate; and C) continuously feeding the intermediate into a feed port of a moving bed reactor, and calcining, to obtain a transition metal lithium oxide. In the present disclosure, a pretreatment process is performed before the precalcination, and the pretreatment temperature and time are further limited, thereby solving the problem of material hardening during the calcination process of battery materials. In conjunction with using a moving bed reactor, the gas phase and the solid phase are sufficiently contacted, and at the same time the thickness of the filler is increased, the productivity is enhanced and the oxygen consumption is largely decreased at the same time. The present disclosure further provides an apparatus for preparing a transition metal lithium oxide.

Various embodiments include a reactor for carrying out a chemical equilibrium reaction between two gaseous starting materials and a gaseous product comprising: a pressure vessel including a reaction space with an inlet for the two starting materials and a first outlet for the gaseous product; a catalytic material arranged in the reaction space; a condensation area in the reaction space for the gaseous product; and a cooling duct structure cooling the condensation area. The cooling duct structure and the housing of the pressure vessel are constructed in a single piece. The reaction space includes a reaction duct running in a convoluted or helical manner between partitions within the pressure vessel. A cross section of the reaction duct extends between opposite face sides of the pressure vessel.

A multi-stage dehydrogenation process including contacting, in a first stage, a feed stream comprising a hydrocarbon and steam with a dehydrogenation catalyst under dehydrogenation conditions to yield a first stage effluent, heating the first stage effluent, and contacting, in a second stage, the heated first stage effluent with a dehydrogenation catalyst under dehydrogenation conditions to yield a second stage effluent comprising a dehydrogenation product, wherein the first stage includes a first reactor and a second reactor arranged in parallel, and wherein the second stage includes a third reactor connected in series with the first reactor and the second reactor. A multi-stage dehydrogenation system for carrying out dehydrogenation is also provided.