A pilot plant for chemical looping hydrogen generation using a single-column packed bed and hydrogen generation method. The plant has a feeding system, reaction system, tail gas treatment and analysis system, and auxiliary system. The reaction system has a packed bed reactor, inside which a thermal storage layer, oxygen carrier layer and supporting layer are arranged successively from top to bottom. The feeding system has a delivery pipe, metering pump, mass flow controller and fuel mixer. The tail gas treatment and analysis system has a cooler, gas-liquid separator, mass flow meter, gas analyzer and tail gas pipe. The packed bed reactor is subjected to fuel reduction, purge, steam oxidation, purge, air combustion and purge stages successively under control of the feeding system. The pilot plant enables evaluation for oxygen carriers and identification for technological difficulties and can generate high-purity hydrogen without using complex gas purification devices.

A catalytic reaction analysis dual reactor system and a method for measuring the catalytic activity of a catalyst by correcting for non-catalytic effects with the catalytic reaction analysis dual reactor system. The dual reactor system contains a first reactor comprising a first catalyst on a first catalyst support, and a second reactor comprising a second catalyst support, wherein the particle size and amount of the first catalyst and the second catalyst support are substantially the same, and the effect of the catalyst is isolated by correcting the result obtained from the first reactor containing the catalyst with the result obtained from the second reactor containing the catalyst support.

A flow reactor system for providing on-demand H.sub.2 evolution at pressure from a liquid organic hydrogen carrier and/or blends thereof includes a reactor that includes a reaction vessel having an inlet and outlet. The inlet is configured to introduce reactants into the reaction vessel, and the outlet is configured to release reaction products. The reaction vessel is configured to hold therein a catalyst system capable of catalyzing the evolution of molecular hydrogen from a liquid organic hydrogen carrier. Advantageously, the reaction vessel is configured to operate at pressures greater than or equal to 50 psig (e.g., from about 50 psig to about 10500 psig. The flow reactor system also includes a source of preheated liquid organic hydrogen carrier in fluid communication with the reactor and a purification system in fluid communication with the outlet that provides purified molecular hydrogen gas for on-demand applications.

A method for fluid catalytic cracking (FCC) of petroleum oil feedstock includes reacting the petroleum oil feedstock with a catalyst mixture in a reaction zone of an FCC unit to obtain a product stream including desulfurized hydrocarbon product, unreacted petroleum oil feedstock, and spent catalyst. During the reacting a process control system develops a process model based on data collected during the reacting, the process model characterizing a relationship among the feed rate of the base cracking catalyst, the feed rate of the FCC additive, the operating conditions, the composition of the product stream, and emissions from the reaction; and one or more of (i) a target feed rate of the base cracking catalyst, (ii) a target feed rate of the FCC additive, and (iii) one or more target operating conditions of the reaction in the reaction zone to reduce the emissions from the FCC unit and to increase a yield of the desulfurized hydrocarbon product in the product stream are determined.

A power generator is described that provides at least one of electrical and thermal power comprising (i) at least one reaction cell for reactions involving atomic hydrogen hydrogen products identifiable by unique analytical and spectroscopic signatures, (ii) a molten metal injection system comprising at least one pump such as an electromagnetic pump that provides a molten metal stream to the reaction cell and at least one reservoir that receives the molten metal stream, and (iii) an ignition system comprising an electrical power source that provides low-voltage, high-current electrical energy to the at least one steam of molten metal to ignite a plasma to initiate rapid kinetics of the reaction and an energy gain. In some embodiments, the power generator may comprise: (v) a source of H.sub.2 and O.sub.2 supplied to the plasma, (vi) a molten metal recovery system, and (vii) a power converter capable of (a) converting the high-power light output from a blackbody radiator of the cell into electricity using concentrator thermophotovoltaic cells or (b) converting the energetic plasma into electricity using a magnetohydrodynamic converter.

A method to stably produce trifluoroethylene with a high selectivity by reacting 1,1,1,2-tetrafluoroethane with a solid reactant and suppressing the formation of by-products such as polymer carbon is provided. In the method, a material gas containing 1,1,1,2-tetrafluoroethane passes through a layer consisting of a particulate solid reactant having an average particle size of from 1 μm to 5,000 μm to bring the solid reactant and 1,1,1,2-tetrafluoroethane into contact with each other in a state where the layer consisting of the solid reactant is fluidized.

A system for reducing dioxygen (O.sub.2) present in vapors from oil storage tanks. The system may include an inlet that receives vapors from the tanks; a heating device coupled with the inlet that heats vapors to a first temperature to form heated vapor; and a vessel coupled receiving heated vapor and containing at least one catalyst to reduce dioxygen from the heated vapor. The catalyst may include palladium, and the vessel may include zinc oxide to remove sulfur from the heated vapor. A compressor may be used to compress the vapors. A controller may be provided to monitor O.sub.2 concentration in heated vapor, and the controller directs flow of heated vapor to a gas pipeline if the O.sub.2 concentration is below a predetermined level; or if the O.sub.2 concentration is unacceptably high, the controller directs flow of vapor to be re-circulated within the system to further reduce O.sub.2 concentration therein.

A solid powder reactor includes: a reaction kettle, including a hollow kettle body and covers; an agitating device, including an agitating shaft and blades, wherein the agitating shaft is arranged in the kettle body and the blades are fixed on the agitating shaft; and a heating system, including a kettle body heater and an agitating heater, wherein the kettle body heater is fixed on the kettle body and the agitating heater is arranged on the agitating device. While the agitating device and the kettle body are driven to agitate, by a driving device fixedly arranged outside the reaction kettle, the heating system heats materials in the reactor. The present invention is applicable to solid reaction of solid powders. The materials containing attached water or not are both feasible, and the materials can directly enter the reactor and react. Compared with conventional solid reactors, the present invention increases the production efficiency.

A system and method for efficiently treating metal catalyst resident in a reactor vessel comprises a sulfiding module, a sulfur source, an ammonia source, and/or a coking source, a hydrogen sulfide detection module, a hydrogen gas detection module, a pH detection module, an ammonia gas detection module and a remote computer all arranged and configured to communicate wirelessly and to allow remote control and monitoring of the modules and process so that catalyst may be sulfided, passivated and/or soft-coked in situ.

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.