A system and method is disclosed for efficiently sulfiding metal catalyst resident in a reactor vessel comprises a sulfiding module and a hydrogen sulfide detection module and a remote computer all arranged and configured to communicate wirelessly and to allow remote control and monitoring of the modules and sulfiding process.

Provided is a reactor device in which a fixed bed multi-tubular reactor is used to produce alkenyl acetate through a gas phase catalytic oxidation reaction of a lower olefin, acetic acid, and oxygen, and which enables accurate measurement of the temperature of a catalyst layer in a reaction tube even when a process operation has been carried out for a long time. A fixed bed multi-tubular reactor for producing alkenyl acetate, wherein the fixed bed multi-tubular reactor is equipped with a plurality of reaction tubes to which a raw material gas and a mist of an aqueous solution of an alkali metal acetate are supplied from the upper portion of the fixed bed multi-tubular reactor, a thermometer protection tube inserted into at least one of the plurality of reaction tubes from the lower portion of the fixed bed multi-tubular reactor, and a thermometer inserted into the thermometer protection tube.

Systems and methods conducive to the formation of one or more alkene hydrocarbons using a methane source and an oxidant in an oxidative coupling of methane (OCM) reaction are provided. One or more vessels each containing one or more catalyst beds containing one or more catalysts each having similar or differing chemical composition or physical form may be used. The one or more catalyst beds may be operated under a variety of conditions. At least a portion of the catalyst beds may be operated under substantially adiabatic conditions. At least a portion of the catalyst beds may be operated under substantially isothermal conditions.

A multi-tubular reactor (1) comprising a cylindrical shell (2), a plurality of reaction tubes (10) located in the shell, and a disk-and-doughnut type baffle (5), wherein the reaction tubes (10) are arranged so as to be in a triangular configuration, one or more of the reaction tubes (10) is/are a temperature-measuring reaction tube(s) provided with a thermometer (20), and a line (BL) through a central axis of the temperature-measuring reaction tube and a central axis of the shell (2) forms an angle from 0 to 15 degree with a line (CL) through the central axis of the temperature-measuring reaction tube and a central axis of at least one adjacent reaction tube next to the temperature-measuring reaction tube, in a cross section of the reactor (1) perpendicular to the central axis of the shell (2), as well as a design and production method thereof.

The present invention relates to a process for converting natural gas to higher hydrocarbon(s) including aromatic hydrocarbon(s) in n reaction zones operated in series, wherein m reaction zones are not participating in the conversion process and only (nm) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said natural gas to an effluent having said higher hydrocarbon(s). An object of the present invention is to provide a process for converting natural gas to higher hydrocarbon(s) including aromatic hydrocarbon(s) wherein a high reactant, i.e. methane, conversion can be achieved.

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 in.sup.1 to 5 in.sup.1, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr.sup.1)(gal.sup.1) to 6.0 (lb)(hr.sup.1)(gal.sup.1).

Fluidized bed reactor apparatus, comprising a cylindrical reactor chamber (10), and a rotating shaft (14) equipped with radially extending fluidization units (16) disposed in the reactor chamber (10), said rotating shaft (14) being connected to a drive unit (42). The apparatus further comprising means for feeding fluidizing bed material into the reactor chamber (10), creating a fluidized bed (28) in the reactor chamber (10), means for feeding organic material that shall be processed into the fluidized bed (28) in the reactor chamber (10), and one or more outlets (22,24) for discharge of material, gases and vapors, wherein the process in the reactor chamber (10) is controlled by a control system (40) connected to at least the drive unit (42). The invention also relates to a method for processing organic material using a fluidized bed reactor apparatus.

The invention relates to a method for decreasing the spread of the tube temperatures between tubes in a process involving the heating of at least one fluid in a furnace that comprises at least one radiation chamber with radiant walls, at least one essentially vertical row of tubes inside of which circulate the at least one fluid to be heated, and being equipped with burners that heat the tubes, where the method comprises the steps of: determining, for each of the tubes the skin temperature of the tube, selecting the 50% tubes having the lowest temperatures determined, the process being stopped, realizing on each tube selected an operation that decreases the flow of the fluid distributed to said tube while keeping the total flow rate of the fluid unchanged.

A process for operating a fuel fired reactor includes introducing fuel into the reactor and burning the fuel in the reactor by means of at least one main burner. Relevant parameters of the process are monitored. Within a predetermined critical operating range for an enforced shut down, a secondary, more stringent operating range is implemented as shut down criteria. The main burner is shut down upon one or more of the relevant parameters leaving the secondary operating range while at least one pilot burner continues to operate as long as the relevant parameters are maintained within the critical operating range.

A catalytic converter arrangement for producing phthalic anhydride by means of a gas phase oxidation of aromatic hydrocarbons, comprising a reactor with a gas inlet side for a reactant gas, a gas outlet side for a product gas, a first catalytic converter layer made of catalytic converter elements, and at least one second catalytic converter layer made of catalytic converter elements. The first catalytic converter layer is arranged on the gas inlet side, and the second catalytic converter layer is arranged downstream of the first catalytic converter layer in the gas flow direction. The catalytic converter elements have an outer layer of an active compound. The invention is characterized in that the active compound content in the first catalytic converter layer and/or in the second catalytic converter layer is below 7 wt. %, based on the total weight of the catalytic converter elements, and the ratio of the total surface of the active compound to the volume of the catalytic converter layer is preferably 10000 cm1 to 20000 cm1, in each catalytic converter layer.