A reformer for production of synthesis gas may include a reformer firing space having a reformer base, reformer walls, and a reformer roof. The reformer may include a first reformer tube and a second reformer tube, with at least sections of the first reformer tube and the second reformer tube being arranged within the reformer firing space. At least one reformer burner is disposed outside the reformer firing space. A cooling duct on or beneath the reformer base is disposed between the first reformer tube and the second reformer tube. The first reformer tube and the second reformer tube can be connected to a collecting system outside the reformer firing space, with the collecting system being disposed beneath the reformer base.

Methods of sulfurizing metal containing particles in the absence of hydrogen are described. One method includes contacting a bed of metal containing particles with a gaseous stream comprising hydrogen sulfide and inert gas under reaction conditions sufficient to produce sulfided metal containing particles. The gaseous stream is introduced into a vertical reactor at an inlet positioned at the bottom portion of the reactor and any unreacted hydrogen sulfide and inert gas is removed at an outlet positioned above the inlet. The sulfided metal containing particles can be removed from the reactor and stored.

Proposed is a process for producing methanol from synthesis gas by means of multi-stage, for example two-stage, heterogeneously catalyzed methanol synthesis, wherein the methanol product formed in every synthesis stage is separated by condensation and the remaining residual gas is supplied to the downstream synthesis stage or after separation of a purge stream recycled to the first synthesis stage as a recycle stream. According to the invention after each synthesis stage the residual gas streams have separated from them a respective purge stream, from which, using one or more hydrogen recovery apparatuses, hydrogen is separated and recycled to the first synthesis stage. The ratio of the individual purge streams and their total molar flow may optionally be varied to allow better control of the reaction in the individual synthesis stages and to allow reaction to the advancing deactivation of the catalysts present therein.

A reactor vessel for high temperature catalytic reactions is provided, in which the inlet portion has a particular design. A plant comprising this reactor vessel is also provided.

In a catalytic reaction, after a reaction product leaves a catalyst bed, an inert substance with a low temperature is sprayed, and through heat absorption and vaporization processes of the inert substance, the temperature of the reaction product drops rapidly when staying in a catalyst cushion layer at a discharge end of a fixed bed reactor, or in a space formed by the catalyst cushion layer at the discharge end of the fixed bed reactor and a reactor head, or in a space formed by a tube plate at the discharge end of the fixed bed reactor and the reactor head. The residence time of the reaction product is shortened due to the entrance of the inert substance in a gaseous state.

An upflow reactor (1), includes a housing (20), a catalyst bed layer (30) and a pressing device (10). The housing (20) is internally provided with a reaction chamber (210), a reaction material inlet (220) and a reaction material outlet (230) which are in communication with the reaction chamber (210) are provided on the housing (20). The catalyst bed layer (30) is provided within the reaction chamber (210), the pressing device (10) is provided within the reaction chamber (210) and located above the catalyst bed layer (30). At least a part of the pressing device (10) is movable up and down so that the at least a part of the pressing device (10) can be pressed against the catalyst bed layer (30).

Processes for producing n-heptane from a mixture of 1-hexene and 1-octene in the presence of a suitable isomerization-metathesis catalyst followed by a hydrogenation step are disclosed. Integrated manufacturing systems for producing n-heptane with minimal waste also are disclosed.

An object of the present invention is to provide a method for producing an unsaturated carboxylic ester, wherein the risk of polymerization blockage is reduced and the required equipment cost and workload involved are kept low while maintaining a high conversion rate in an esterification reaction of unsaturated carboxylic acid. This object can be achieved by a method for producing an unsaturated carboxylic ester, which includes performing an esterification reaction using a reactor packed with a solid catalyst, wherein unsaturated carboxylic acid and alcohol are continuously fed to the reactor from an inlet thereof to form a fluid of the reaction solution in the reactor, and the vaporized organic solvent is continuously fed to the reactor from the inlet or a part near the inlet of the reactor.

An aspect of the present disclosure relates to a process for preparing a composite hydroalkylation catalyst including: (a) effecting impregnation of a hydrogenation metal on an inorganic oxide to form a metal impregnated inorganic oxide; (b) effecting calcination of the metal impregnated inorganic oxide to obtain a calcined metal impregnated inorganic oxide; (c) preparing a composite mixture comprising a molecular sieve, the calcined metal impregnated inorganic oxide and a binder; (d) preparing an extruded catalyst; and (e) effecting calcination of the extruded catalyst to obtain the composite hydroalkylation catalyst. The composite hydroalkylation catalyst prepared using this process affords dramatic improvement in conversion of mononuclear aromatic hydrocarbon and the yield of the hydroalkyled mononuclear aromatic hydrocarbon (e.g. CHB).

Systems, reactors, and processes for regenerating ionic liquid using catalyst. A plurality of tubular reactors are provided having a first end and a second end and catalyst particles disposed in the tubular reactor between the first end and the second end. A line supplies separated ionic liquid catalyst to the first end of the tubular reactor. Hydrogen is also supplied. Regenerated ionic liquid catalyst is recovered from the second end of the tubular reactor. The inner surface of the tubular reactor is preferably non-corrosive or non-reactive. A fluoropolymer lining may be used. The tubular reactors are modular, and may be changed out with the catalyst inside when the catalyst are to be replaced.