A coke control reactor, and a device and method for preparing low-carbon olefins from an oxygen-containing compound are provided. The coke control reactor includes a coke control reactor shell, a reaction zone I, and a coke controlled catalyst settling zone; a cross-sectional area at any position of the reaction zone I is less than that of the coke controlled catalyst settling zone; n baffles are arranged in a vertical direction in the reaction zone I; the n baffles divide the reaction zone I into m reaction zone I subzones; and a catalyst circulation hole is formed in each of the baffles, such that a catalyst flows in the reaction zone I in a preset manner. A catalyst charge in the present coke control reactor can be automatically adjusted, and an average residence time of a catalyst in the coke control reactor can be controlled by changing process operating conditions.

There is provided a system for energy storage comprising: a fluidized bed apparatus with an energy storage material, wherein the energy storage material is provided in volumes coated with an outer layer of solid particles of a different material, wherein the volumes have a largest size in the interval 1-1000 μm and wherein the solid particles (5) have a largest size in the interval 1-500 nm. Advantages of the system include that structural changes in the energy storage material over time are minimized so that the energy storage material can be used over many cycles without any noticeable impairment. The heat transfer to and from the energy storage material is improved. The system can further be used for CO.sub.2 capture.

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).

A system includes a standpipe for receiving a flow of solids therethrough, the standpipe having at least one inlet configured to receive a gas for decreasing a solids-to-gas ratio of the flow, a sealpot having an inlet fluidly coupled to the standpipe and an outlet fluidly coupled to a riser, the sealpot being configured to fluidize the solids received from the standpipe and to transport the solids to the riser, and a drain device fluidly coupled to an outlet in the standpipe, the outlet being located upstream from the inlet of the sealpot. The drain device is configured to remove the excess gas from the flow of solids within the standpipe to increase the solids-to-gas ratio of the flow prior to the solids entering the sealpot.

Provided herein are methods, devices and systems for processing of carbonaceous compositions. The processing may include the manufacture (or synthesis) of oxidized forms of carbonaceous compositions and/or the manufacture (or synthesis) of reduced forms of oxidized carbonaceous compositions. Some embodiments provide methods, devices and systems for the manufacture (or synthesis) of graphite oxide from graphite and/or for the manufacture (or synthesis) of reduced graphite oxide from graphite oxide.

A method for preparing a light olefin using an oxygen-containing compound, and a device for use thereof, more specifically, taking methanol and/or dimethyl ether as main starting materials, using a multi-stage (n≧2) dense phase fluidized bed reactor and a multi-stage (m≧2) catalyst regenerator, which solves the problem in the prior art of the uniformity of catalyst carbon deposition and the carbon content being difficult to control and the light olefin selectivity being low.

A process for the production of a hydrocarbon fluid includes the step of catalytically hydrogenating a hydrocarbon cut in presence of both a dearomatization catalyst and a dewaxing catalyst in a single slurry reactor. A hydrocarbon fluid is also disclosed as being obtainable by the process.

The invention relates to a process and to a unit for chemical looping oxidation-reduction combustion of a hydrocarbon feed, wherein heat exchanges are controlled through a level variation of a dense fluidized bed of active mass particles in an external heat exchanger (E1, E2), positioned on a transport line carrying particles circulating between a reduction zone (210) and an oxidation zone (200) for the particles in the chemical loop. The bed level variation is allowed through controlled application of a pressure drop on a fluidization gas outlet in the heat exchanger, said pressure drop being compensated by the level variation of an active mass particle bed in a reservoir zone provided on the particle circuit in the chemical loop.

The method for catalytic methanation of synthesis gas includes the following steps: 1) feeding the synthesis gas into the bottom of a reactor of an upward concurrent flow transporting bed so as to adequately mix and preheat with methanation catalyst entering the bottom of the reactor until the activation temperature of the catalyst is reached and then the methanation reaction begins; and 2) after the methanation reaction, immediately passing the product gas and the catalyst grains outputted from the transporting bed into a gas-solid separator to perform a rapid separation so as to obtain the product gas.

The present invention relates to an intensification of the synthetic process for the preparation of dialkyl ether from alcohol by using a conical fixed bed reactor integrated with distillation coupled conical polishing reactor.