A method of continuously producing carbon nanotubes and hydrogencomprising: preparing a catalyst precursor, and pre-reducing the catalyst precursor; adding a height of carbon nanotubes in a reactor as a stacked bed and electrically heating the carbon nanotubes to the reaction temperature of a vapor deposition furnace in the presence of a protective gas; putting the pre-reduced catalyst or unreduced catalyst precursor into the reactor; under the condition of stirring the solid materials in the reactor, introducing a carbon source gas, reacting same by means of the vapor deposition furnace to generate new carbon nanotubes and hydrogen, continuously discharging a part of carbon nanotubes and a part of hydrogen, and repeating these steps to achieve the continuous preparation of carbon nanotubes. The device has a high utilization rate of raw materials, can manufacture a large batch of carbon nanotubes with a high purity at one time, and is suitable for large-scale industrial production.

A device for online co-production of carbon-containing precursors and high-quality oxygen-containing fuels from biomass pyrolysis gas includes a spray polymerization reactor, where a biomass pyrolysis gas inlet and a polymerization agent inlet are provided on the spray polymerization reactor, an outlet of the spray polymerization reactor is connected to an inlet of a catalytic reactor, and an outlet of the catalytic reactor is connected to an inlet of a condenser; a spray pipe is arranged at a top in the spray polymerization reactor, and a detachable collector for collecting the carbon-containing precursors is mounted at a bottom of the spray polymerization reactor; and a catalyst is arranged in the catalytic reactor, such that micromolecular pyrolysis gas is catalytically converted into the high-quality oxygen-containing fuels.

An adsorbent is in a liquid-phase hydrogenation catalyst composition. A catalyst bed containing the liquid-phase hydrogenation catalyst composition may be applicable in adsorption technology or oil liquid-phase hydrogenation technology. The adsorbent contains a porous material and a hydrogenation active metal supported on the porous material. The adsorbent has an average pore diameter of 2-15 nm, a specific surface area of 200-500 m.sup.2/g, and the hydrogenation active metal is present in an amount, calculated as metal oxide, of 2.5 wt % or less, based on the total weight of the adsorbent. The adsorbent has a high hydrogen sulfide adsorption efficiency for a long period of time, and can effectively prolong the protection period for the hydrodesulfurization catalyst.

Processes and systems for the production of heavy isoparaffinic hydrocarbons include feeding hydrogen and a mixed isoolefin stream, including C8-C12 olefins, isoolefins, and oligomers, and C8-C12+ hydrogenated hydrocarbons to a trickle-bed reactor system. The hydrogen and mixed isoolefin are reacted over a hydrogenation catalyst, producing a liquid effluent comprising hydrogenated hydrocarbons and unreacted olefins and oligomers, and a vapor effluent comprising hydrogenated hydrocarbons, hydrogen and unreacted olefins and oligomers. The liquid effluent is fed to a first heat exchanger, producing a cooled liquid effluent stream, which is combined with the vapor effluent, producing a mixed phase effluent. The mixed phase effluent is cooled in a second heat exchanger, producing a partially condensed effluent, which is fed to a drum, producing a vent stream, a hydrogenated product stream having greater than 95 wt % C8-C12 saturated hydrocarbons, and a hydrogenated recycle stream. The hydrogenated product stream may be provided to downstream blending systems.

A chemical complex to perform oxidative dehydrogenation of C2-C4 alkanes, to C2-C4 alkenes, the chemical complex involving at least one oxidative dehydrogenation reactor containing one or more mixed metal oxide catalysts and designed to accept, optionally in the presence of a heat removal diluent gas, an oxygen containing gas and a C2-C4 alkane containing gas, and to produce a product stream including a corresponding C2-C4 alkene and one or more of: an unreacted C2-C4 alkane; oxygen; heat removal diluent gas; carbon oxides, including carbon dioxide and carbon monoxide; oxygenates, including but not limited to, one or more of acetic acid, acrylic acid and maleic acid; and water; and involving a combustion chamber for combusting a product stream and at least one fuel stream and optionally at least one stream including oxygen, the combustion chamber producing a flue gas at a temperature of 850° C. to 1500° C.

Disclosed herein are systems for more efficient production of aluminum chlorohydrates, where the systems comprise a support element and/or metal catalyst, where the support element is configured to support the metal reagent in the system. Methods for efficient production of aluminum chlorohydrates are also disclosed.

Provided herein are methods of producing acrylic acid from beta-propiolactone. Such methods may involve the use of a heterogeneous catalyst, such as a zeolite.

Disclosed is a flow bypass device, a reactor system containing the flow bypass device; a method for operating a fixed bed of solid particles in which gas is re-routed to an interior of the fixed bed, for example, the flow bypass device is used to bypass a portion of the solid particles; and a method for loading solid particles and a flow bypass device into a vessel. The methods and systems can use a single flow bypass device or multiple flow bypass devices that are stacked on top of one another.

An equal flow scale catcher device, or EFSC, is designed based on a unique scale catching technology for a reactor. With multiple scale catching modules, the EFSC offers equal flows to a catalyst bed or distribution tray of the reactor, independent of each module's degree of saturation with particles of an incoming fluid during operation. Thus, the innovative EFSC system achieves substantial uniformity of fluid delivery across the distribution tray of the reactor and the static pressure field above the liquid level on the distribution tray. Further, the EFSC effectively captures solid particles in the incoming fluid to the reactor and solid particles that form at the top head of the reactor. The EFSC employs a modular structure that allows optimal configuration of the scale catching modules and scale catching units inside each scale catching module, thus efficiently facilitating simple and efficient installation, maintenance, and/or replacement of the EFSC.

A catalytic reaction unit has a plurality of catalyst bed layers arranged vertically, each of the catalyst bed layers being filled with a solid catalyst, and an inclined surface on the upper part of the corresponding solid catalyst arranged between adjacent catalyst bed layers; a liquid phase feeding subunit arranged above the topmost catalyst bed layer, and the liquid phase feed is guided by the inclined surface to sequentially enter each catalyst bed layer from top to bottom; a gas phase feeding subunit arranged between the catalyst bed layer of an upper layer and the inclined surface of the next layer, and a gas phase channel relatively isolated from the gas phase feeding subunit. The gas phase product generated after the gas-phase feed and the liquid phase feed react in the catalyst bed layer directly enters the gas phase channel.