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.

Devices and methods for controlling the properties of chemical species during time-dependent processes. A device includes a reactor for containing one or more chemical species of a time-dependent process, an extraction pump for automatically and continuously extracting an amount of the one or more chemical species from the reactor, one or more detectors for measuring property changes of the one or more extracted chemical species and generating a continuous stream of data related to the one or more property changes to the one or more chemical species during a time interval, and a process controller configured to fit the continuous stream of data to a mathematical function to predict one or more properties of the one or more chemical species at a future time point and make one or more process decisions based on the prediction of one or more properties at the future time point.

A process for the production of syngas comprising the steps of providing a feed gas comprising a hydrocarbon, carbon dioxide and optionally steam, contacting a flow of said feed gas with a metal oxide to form syngas, wherein the mole fraction of carbon dioxide or in the case the feed gas comprises steam, the sum of the mole fractions of carbon dioxide and steam, in the feed gas is between 0.3 and 0.7; and/or wherein the mole fraction of the hydrocarbon in the feed gas is between 0.3 to 0.5, wherein the feed gas is contacted with the metal oxide at a temperature of between 1050K and 1600K.

A fluidized bed reactor includes a main shell and a coke control zone shell; the main shell includes an upper shell and a lower shell; the upper shell encloses a gas-solid separation zone, and the lower shell encloses a reaction zone; the reaction zone axially communicates with the gas-solid separation zone; the coke control zone shell is circumferentially arranged on an outer wall of the main shell; the coke control zone shell and the main shell enclose an annular cavity, and the annular cavity is a coke control zone; n baffles are radially arranged in the coke control zone, and the n baffles divide the coke control zone into n coke control zone subzones, where n is an integer; the coke control zone subzones are provided with a coke control raw material inlet; and a catalyst circulation hole is formed in each of n-1 of the baffles.

The invention relates to an apparatus for analyzing heterogeneously catalyzed reactions comprising at least one reactor (3) through which a particulate catalyst flows and at least one reactant feed, wherein arranged downstream of each reactor (3) is a separation apparatus (17) for separating the particulate catalyst from a reaction product comprising condensable gases and arranged downstream of the separation apparatus (17) is a liquid separator (31) for separating liquid constituents from the reaction product, wherein the liquid separator (31) comprises a metallic tube (103) and a deflection body (119), wherein the metallic tube (103) is closed at its ends and the deflection body (119) is accommodated in the metallic tube (103) and the metallic tube (103) comprises a side feed (135) at a first end (105) and a gas outlet (113) at a second end (107) and the gas outlet (113) is connected to at least one sample vessel (37). The invention further relates to a process for analyzing heterogeneously catalyzed reactions in the apparatus.

A reactor for carrying out a chemical reaction has a reactor vessel, one or more reaction tubes and means for the electrical heating of the one or more reaction tubes. The reactor vessel has one or more discharge orifices which are permanently open or are set up to open above a preset pressure level, and gas feed means are provided, which are set up to feed an inerting gas into an interior of the reactor vessel.

This disclosure provides improved processes for converting aromatic hydrocarbons, such as benzene/toluene, alkylation, transalkylation, or isomerization. In an embodiment, a process comprises utilizing a passivated reactor to reduce deactivation of a molecular sieve catalyst. Additional measures such as the use of an auxiliary catalyst and/or an elevated reactor pressure may be used to further reduce deactivation of the molecular sieve catalyst.

A process (and a related system) for collecting samples of a polymerization catalyst or of a catalyst-containing polymer from an operation unit, having an upper end and a lower end, of a polymerization plant, including the steps of: a) extracting a prefixed amount of product from the lower end of the operation unit through a discharge valve; b) directing the product towards a filtering unit through an inlet valve; c) flushing an inert gas through the filtering unit; d) outgassing the filtering unit, through the outlet valve; and e) displacing the filtering unit, for collecting the sample.

Methods and systems for producing vinyl acetate may use flammability limit (FL) formulas with improved efficiencies at more than one location in the vinyl acetate production process. Herein, FLs can be used at one or more of four portions of the vinyl acetate production process: the reactor, the process-to-process heat exchangers, the carbon dioxide removal system, and the ethylene recovery system. Such FLs are functions of operating conditions and include at least one interaction term that represents the interrelation of two or more of the operating conditions (e.g., temperature, pressure, and component concentration) on the FL.

Process for the production of a product gas containing nitrogen and hydrogen from ammonia comprising the steps of non-catalytic partial oxidation of ammonia with an oxygen containing gas to a process gas containing nitrogen, water, amounts of nitrogen oxides and residual amounts of ammonia; cracking of at least a part of the residual amounts of ammonia to hydrogen and nitrogen in the process gas by contact with a nickel containing catalyst and simultaneously reducing the amounts of nitrogen oxides to nitrogen and water by reaction with a part of the hydrogen formed during cracking of the process gas by contact of the process gas with the nickel containing catalyst; and withdrawing the hydrogen and nitrogen containing product gas.