The inventions is directed to a new design for catalyst tubes, which makes it possible to apply the concept of regenerative reforming into steam reformers having catalyst tube inlets and outlets at opposite sides of the furnace chamber. The catalyst tube comprises an inlet for process gas to enter the catalyst tube and an outlet for process gas to exit the catalyst tube, which inlet and outlet are located at opposite ends of the catalyst tube. The catalyst tube further comprises a first annular channel comprising the catalyst, a second annular channel for process gas to flow countercurrently or co-currently to the process gas flowing through the first annular channel.

Method for revamping a multi-bed ammonia converter, wherein said converter comprises a plurality of adiabatic catalytic beds including a first catalytic bed and one or more further catalytic bed(s), said catalytic beds being arranged in series so that the effluent of a bed is further reacted in the subsequent bed; at least a first inter-bed heat exchanger arranged between said first catalytic bed and a second catalytic bed to cool the effluent of said first bed before admission into said second bed, and optionally further inter-bed heat exchanger(s) arranged between consecutive beds; said method involves the conversion of said first catalytic bed into an isothermal catalytic bed.

The present invention relates to a multi tubular metal hydride reactor with integrated buffer storage. The present invention more particularly relates to metal hydride reactor with integrated buffer storage configuration with 7 tubes with metal hydride and 4 longitudinal fines attached to 5 concentric rings, the metal hydride tubes are supported by means of 4 baffles, having a total 50 kg LaNis distributed equally among the tubes and water as heat transfer fluid flows across the shell for heat transfer. The metal hydride reversibly stores 680 grams of hydrogen amounting to 1.34 wt. % of gravimetric capacity of metal hydride and equivalent energy storage of 10.4 MJ. In case of absorption, when the flow rate selected was 20 LPM the absorption time for 90% reaction completion was observed to be 1286 s (21.4 min) at 30 bar H.sub.2 supply pressure. In case of desorption studies, it was observed that the varying flow rate from 15 to 25 LPM has negligible effect on hydrogen desorption hence 15 LPM was selected as a flow rate for further desorption experiments. Further increasing HTF temperature from 60? ? C. to 80? C. improves the performance significantly.

A vertical ammonia converter with radial flow catalyst beds includes a recipient having an outer shell equipped with a dual duct inner tubular wall to route effluents in upward and downward directions, the tubular wall made of vertical tubes with gastight walls arranged in a circle on an outer periphery of an inner wall of the shell, open at their ends to route effluent to be treated in the upward direction from an injection chamber in a lower part of the shell to a distribution chamber in an upper part of the shell, which tubes are contiguous to a filtering media over a height of a catalyst bed, the filtering media open at an upper end to pass a downward-flowing effluent and closed at a lower end to route and distribute the effluent through their effluent-permeable face towards the catalyst bed retained on an outer face by the filtering media.

Systems for dehydrogenating an alkane are provided. An exemplary system includes a furnace and further includes alkane heating chambers, regeneration mixture heating chambers, and two groups of reaction chambers, all located within the furnace. The alkane heating chambers and regeneration mixture heating chambers can preheat an alkane feed and a regeneration mixture feed, respectively. The two groups of reaction chambers can be switchably coupled to an alkane feed and a regeneration mixture feed such that an alkane can flow through one group of reaction chambers while a regeneration mixture flows through the other group of reaction chambers. Processes for dehydrogenating an alkane are also provided.

The present disclosure relates to the technical field of separation of boron isotopes, in particular to a device and method for cracking a boron trifluoride complex. The device for cracking the boron trifluoride complex includes a continuous feeding system, a rising film preheater, a falling film preheater, a boron trifluoride gas circulation pipeline, a separation chamber, a cracking tower, a gas-liquid separator, an impurity removal tower, and anisole storage tank. By employing a continuous feeding method, the device for cracking boron trifluoride complex shortens retention time of anisole at a high-temperature stage while ensuring a cracking rate of a boron trifluoride-anisole complex, reduces the thermal decomposition degree of anisole, maintains the purity of anisole, and greatly improves the utilization rate and production safety of anisole, thus ensuring continuous and stable production.

A tube reactor for heterogeneous catalyzed gas phase reactions having a thermal tube with a catalyst material around which a fluid heat transfer medium, a temperature-sensitive optical waveguide surrounded by a capillary tube that extends into the catalyst material and has measuring points having a predetermined spacing between adjacent measurement points, and can be connected to a source for optical signals and to an evaluation unit (31) for optical signals reflected by the optical waveguide. The optical waveguide has measuring points having a spacing between adjacent measuring points in the axial direction of the thermal tube which is 0.8 to 5 times the shortest edge length of all imaginary cuboids which, having a minimum volume in the cases in which nominal external dimensions are associated with particles of the catalyst material.

Embodiments disclosed herein relate to the production of polypropylene. A propylene stream comprising propane is fed to a gas-phase polymerization zone. Propylene is reacted in the gas phase polymerization zone to produce a polymerization product. A recycle gas stream from the gas-phase polymerization zone is fed to a heat exchanger to remove heat of the polymerization reaction, forming a first cooled gas stream, which is recycled to the gas-phase polymerization zone, and a second cooled gas stream from the heat exchanger is fed to a first separation system, forming a propane rich stream and a second propylene stream. The first separation system is operated by a heat pump configured to compress the second propylene stream to form an at least partially condensed propylene stream. A liquid portion and optionally a vapor portion of the at least partially condensed propylene stream are fed to the gas-phase polymerization zone.

The disclosure pertains to a high pressure carbamate condensation apparatus for a urea plant, a urea plant, and a urea production method. The apparatus comprises a first U-shaped tube bundle arranged around a second U-shaped tube bundle.

A tubular waterwall structure in a fluidized bed reaction chamber includes horizontally adjacent first and second portions forming a corner structure and constituted by vertical tubes and fins centrally attached to the tubes and having a first width. The first wall portion has an outermost tube next to the corner, an upper portion defining an upper vertical plane in an upper level range and a lower portion defining a lower (outwards) vertical plane in a lower level range. The lower portion has a refractory lining. The second wall portion is vertical and has an outermost tube next to the corner. The outermost tube of the second wall portion is in the lower level region connected to the outermost tube of the first wall portion by a planar lower beveled corner fin having a refractory lining and a width that is larger than the first width.