Oxidized disulfide oil (ODSO) compounds or ODSO compounds and disulfide oil (DSO) compounds are reacted with a hydrogen addition feed in a hydroprocessing complex. The hydrogen addition process can include naphtha hydrotreatment, middle distillate hydrotreatment, vacuum gas oil hydrocracking, and vacuum gas oil hydrotreatment. The ODSO or ODSO and DSO components are converted to hydrogen sulfide, water and alkanes.

A multi-bed catalytic converter comprising: a plurality of catalytic beds which are traversed in series by a process gas, sequentially from a first catalytic bed to a last catalytic bed of said plurality, and at least one inter-bed heat exchanger (7) positioned between a first catalytic bed and a second catalytic bed of said plurality, wherein at least the last catalytic bed of said plurality is adiabatic and is made of fine catalyst with a particle size not greater than 2 mm.

A method of maintaining a backpressure of a fluidic product is provided. The method includes pressurizing a first reservoir to a first predetermined pressure level using compressed air, delivering the fluidic product to the pressurized first reservoir until a current level of the fluidic product in the first reservoir reaches a first predetermined level, pressurizing a second reservoir to a second predetermined pressure level using the compressed air, delivering the fluidic product to the pressurized second reservoir until a current level of the fluidic product in the second reservoir reaches a second predetermined level, and controlling the backpressure of the fluidic product using the first reservoir and the second reservoir such that a discharge flow of the fluidic product is continuous.

A trickle bed reactor, comprising a plurality of catalyst beds connected in series and progressively increasing in catalyst mass in a direction from upstream to downstream; and a plurality of heat exchangers, wherein each of the heat exchangers is located between two of the plurality of catalyst beds, and wherein each of the heat exchangers does not exchange heat with an outer surface of a vessel that contains any of the catalyst beds.

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

A reactor for producing desired reaction products has a housing, a plurality of catalyst conduits within the housing, and a plurality of coolant conduits within the housing. The coolant conduits are interspersed among the catalyst conduits, and each catalyst conduit is positioned adjacent to at least two coolant conduits.

A load-following reactor system and associated facilities for improved control of a reactor under varying loads. The load-following reactor may be a tube-cooled reactor for methanol synthesis. A reactant may be controlled by at least one valve element such that a portion of the reactant is fed to the reactor through the reactor tubes, and a portion of the reactant is fed to the reactor after being heated in a heat exchanger. The heated portion of the reactant may be fed to the reactor after the tubes. The valve element may be controlled based on a temperature of the reactor and/or a flowrate of reactant feed to adapt the temperature of the reactor to the changing reactant flowrate.

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.

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.

An ammonia synthesis converter for small production units which provides full access for routine maintenance and catalyst replacement while providing adequate catalyst pressure drop to ensure kinetic performance and reduce heat leak from the catalyst beds. A shell has a removable top head and an annular basket is removably mounted in the shell. First and second catalyst beds are disposed in the annular zone of the basket for axial down-flow in series. A quench gas is introduced into effluent from the first catalyst bed and the resulting mixture into a top of the second catalyst bed. A feed-effluent interchanger in the inner basket zone is adapted to receive effluent from the second catalyst bed and indirectly heat a feed to the first catalyst bed. Also, methods of operating and servicing the converter.