This invention relates to a polymerization process for forming polymer comprising: contacting (typically in a solution or slurry phase), a monomer and a catalyst system in a reaction zone comprising at least one spiral heat exchanger and recovering polymer, wherein the monomer, the catalyst system and the polymer flow through the at least one spiral heat exchanger in a cross-flow direction relative to spirals of the at least one spiral heat exchanger.

Disclosed are a preparation device and a preparation method of ammonia gas. The preparation device, prepares ammonia gas by reacting ammonium chloride with a particulate inorganic salt, includes one fluidized bed reactor with at least two fluidization chambers, in which one is a preheating chamber configured to preheat the particulate inorganic salt, and the other is a reaction chamber inside provided with at least one atomizing nozzle, the particulate inorganic salt forming a fluidized bed layer and reacting with an aqueous solution of ammonium chloride in the reaction chamber to generate the ammonia gas. The particulate inorganic salt can be sequentially flowed through a plurality of preheating chambers and reaction chambers under an impetus of a density difference of the particulate bed layers, finally achieving the required conversion rate.

This disclosure relates to processes for producing polyolefins in a gas phase reactor using condensing agent(s) (CAs), and real-time calculation of the ratio of one type of CA to another CA within a CA composition. This disclosure provides methods for controlling condensed phase cooling in a gas phase reactor used to polymerize olefins. The polymerization may employ one or more polymerization catalysts to polymerize one or more olefin monomers, and may include introducing a first condensing agent and a second condensing agent in a ratio of first condensing agent to second condensing agent, which ratio is calculated by ascertaining a stick limit for a first condensing agent, calculating an equivalence factor relating the first condensing agent and a second condensing agent, ascertaining a total allowable condensing agent, and calculating a first amount of the first condensing agent removed and replaced by a second amount of the second condensing agent.

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include a conventional riser reactor in combination with a mixed flow (e.g., including both counter-current and co-current catalyst flows) fluidized bed reactor designed for maximizing light olefins production. The effluents from the riser reactor and mixed flow reactor are processed in a catalyst disengagement vessel, and the catalysts used in each reactor may be regenerated in a common catalyst regeneration vessel. Further, integration of the two-reactor scheme with a catalyst cooler provides a refinery the flexibility of switching the operation between the two-reactor flow scheme, a catalyst cooler only flow scheme, or using both simultaneously.

The present invention discloses process and apparatus for the production of light olefins from their respective alkanes by catalytic dehydrogenation, where in the dehydrogenation reaction is carried out in multiple semi-continuously operated fluidized bed isothermal reactors, connected to a common regenerator and wherein the process is carried out in a sequence of steps in each cycle i.e., entry of hot regenerated catalyst, pre-treatment with reducing gas, dehydrogenation reaction, stripping, transfer of catalyst to regenerator and catalyst regeneration. Process cycle in each reactor starts at different times such that the catalyst inventory in the regenerator is invariable with time.

A process and apparatus is disclosed for gradually starting fluidization in a bed of particulate from the top down so as to avoid thrusting the entire mass of particulates upwardly in the bed at the same time which may damage internals in the bed. The particulate bed may comprise a catalyst cooler for an FCC unit containing internals such as cooling, fluidization and support equipment.

A gas replacement process and a gas replacement apparatus are employed, in the nitro compound hydrogenation reaction process. The gas replacement process at least includes a first step of subjecting a stream to be replaced to the gas replacement in presence of a first replacement gas, and then a second step of subjecting to the gas replacement in presence of the second replacement gas. Assuming the superficial velocity of the first replacement gas is V1, and the superficial velocity of the second replacement gas is V2, then V2/V1≥1.5.

A fluidized bed reactor designed for in situ gas phase impregnation. The reactor comprises a tube with an upstream zone and a downstream zone, the upstream zone and the downstream zone being separated by a separation filter. A method for a controlled-deposition of a sublimated precursor onto a fluidized solid support. The method is remarkable in that it is carried out in situ within the tube of the fluidized bed reactor in accordance with the fluidized bed reactor.

A method for processing a chemical stream includes contacting a feed stream with a catalyst in an upstream reactor section of a reactor having the upstream reactor section and a downstream reactor section, passing an intermediate product stream to the downstream reactor section, and introducing a riser quench fluid into the downstream reactor section, upstream reactor section, or transition section and into contact with the intermediate product stream and the catalyst to slow or stop the reaction. The method includes separating at least a portion of the catalyst from the product stream, passing the product stream to a product processing section, cooling the product stream, and separating a portion of the riser quench fluid from the product stream. The riser quench fluid separated from the product stream may be recycled back to the downstream reactor section, upstream reactor section, or transition section as the riser quench fluid.

The invention relates to a method for converting a gas into methane (CH4) which includes: a step of activating a catalytic material including praseodymium oxide (Pr6O11) associated with nickel oxide (NiO) and alumina (Al2O3), the respective proportions of which are, relative to the total mass of these three compounds: Pr6O11: 1 wt % to 20 wt %, NiO: 1 wt % to 20 wt %, and A12O3: 60 to 98 wt %; and a step of passing a gas including at least one carbon monoxide (CO) over the activated catalytic material.