A process for estimating catalyst performance of catalyst used in refinery reforming processes for converting naphtha to gasoline. More in particular, the catalyst to be investigated is subjected to analysis in parallel over time at a temperature to achieve a desired RON on yield of e.g. C5+, for at least two different reaction times. The reactions are terminated after which coke deposition is determined, and relationships of coke deposition and yield, both as a function of reaction temperature for the catalyst used are established, thereby enabling comparison of catalyst performance as determined by a yield-temperature relationship at a given coke deposition degree.

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 membrane reactor includes a catalyst layer, a separation membrane, and a buffer layer. The catalyst layer contains a catalyst for promoting a conversion reaction from a feed gas containing hydrogen and carbon oxide to a liquid fuel. The separation membrane is permeable to water vapor which is a byproduct of the conversion reaction. The buffer layer is disposed between the separation membrane and the catalyst layer, and permeable to the water vapor toward the separation membrane.

A combined reforming apparatus is provided. The combined reforming apparatus includes a body, a plurality of first catalyst tubes disposed inside the body and reacting at a first temperature to reform hydrocarbons (C.sub.xH.sub.y) having two or more carbon atoms into methane (CH.sub.4), a plurality of second catalyst tubes disposed inside the body, connected to the plurality of first catalyst tubes, and reacting at a second temperature higher than the first temperature to reform methane (CH.sub.4) into synthesis gas containing hydrogen (H.sub.2) and carbon monoxide (CO), a combustion unit configured to supply heat to the plurality of first catalyst tubes and the plurality of second catalyst tubes, and a first distributor configured to connect the plurality of first catalyst tubes to each of the second catalyst tubes to distribute steam and gas discharged from the plurality of first catalyst tubes to the plurality of second catalyst tubes.

A combined reforming apparatus is provided. The combined reforming apparatus includes a body, a first catalyst tube disposed inside the body and reacting at a first temperature to reform hydrocarbons (CA) having two or more carbon atoms into methane (CH.sub.4), a second catalyst tube disposed inside the body, connected to the first catalyst tube, and reacting at a second temperature higher than the first temperature to reform methane (CH.sub.4) into synthesis gas comprising hydrogen (H.sub.2) and carbon monoxide (CO), a combustion unit configured to supply heat to the first and second catalyst tubes, a gas supply pipe configured to supply hydrocarbon gas to the first catalyst tube, a first steam supply pipe configured to supply steam to the first catalyst tube, and a second steam supply pipe configured to supply steam to the second catalyst tube.

Disclosed herein are systems and processes for the conversion of a methane feedstock to C.sub.2+ hydrocarbons.

The present disclosure generally relates to processes for preparation of n-butanol, n-octanol and n-decanol from a reaction mixture comprising ethanoi and n-hexanol by Guerbet condensation. In some aspects, the present disclosure relates to improvements in n-octanol and n-decanol yield and selectivity by the selection of process reaction conditions such as, but not limited to, mole ratio of n-hexanol to ethanol. The present disclosure further generally relates to integrated processes for preparation of n-butanol in a n-butanol reactor from a reaction mixture comprising ethanol and hydrogen to produce a n-butanol product stream by Geurbet condensation comprising n-butanol and n-hexanol and for preparation of n-octanol in a n-octanol reactor from a reaction mixture comprising ethanol, n-hexanol and hydrogen to produce a n-octanol product stream by Geurbet condensation comprising n-butanol, n-hexanol and n-octanol. A predominant proportion of the n-hexanol contained in the n-butanol and n-octanol product streams is isolated and recycled to the n-octanol reaction mixture. In some aspects, the present disclosure relates to improvements in n-octanol and n-butanol yield and selectivity by the selection of process reaction conditions such as, but not limited to, mole ratio of n-hexanol to ethanol and recovery and recycle of n-hexanol.

A distance measuring device includes a measuring member holding a length measuring instrument and at least one rail member (base member) on which the measuring member is movably disposed. When a straight line parallel to a direction in which the measuring member disposed on the base member moves is defined as a reference line, an angle formed by a straight line parallel to an axial length direction of a reaction tube and the reference line, which are on an identical plane, is constant for the plurality of reaction tubes disposed side by side along the reference line. A measurement direction of the length measuring instrument is parallel to the axial length direction of the reaction tube in a state where the measuring member is disposed on the base member. The measuring member is disposed on the base member to be able to sequentially move.

In a cooled axial flow converter, in which process gas passes from an outer annulus via a catalyst bed, wherein the process gas is converted to a product, to an inner centre tube, the catalyst bed comprises at least one module comprising at least one catalyst layer. Feed means are arranged to provide a flow of process gas from the outer annulus to an inlet part of one or more modules, and collector means are arranged to provide a flow of product stream of converted process gas, which has passed axially down the catalyst bed of one or more of the modules to the centre tube. At least one of the one or more modules comprises one or more cooling plates arranged to be cooled by a cooling fluid.

A reverse flow reactor (RFR) and process having a forward reaction feed cycle, a reverse reaction feed cycle, and a reverse regeneration cycle. The heat convected in the forward feed cycle matches the heat convected in the reverse flow cycles. Compared to an RFR without the reverse feed cycle, the three-cycle RPR substantially reduces the regeneration air flow rate, associated compression requirements, and the overall reactor volume, that are required.