Reactor rotation

Static mixing catalysts Operation Monolithic reactors Microreactors Heat exchange reactors Supersonic gas/liquid reactor Jet-impingement reactor Rotating packed-bed reactor... 

The cleaning of flue gases from stationary sources is another field in which the application of monolithic catalysts will certainly rise. There will be no versatile catalyst for cleaning all off-gases. Therefore tailor-made catalysts with zeoliths of various types for specific applications will be developed. Incorporated-type monolithic catalysts are likely to prevail in this field. Since cleaning usually requires a set of equipment items in series (e.g., converter, heat exchangers), multifunctional reactors (reverse-flow reactors, rotating monoliths) will become more common. 

Tube light reactor Multiple-tube reactor Rotating tube raector... 

Contactors in which the liquid flows as a thin film Packed columns Trickle bed reactors Thin film reactors Rotating disk reactors... 

Brief discussion of a total of over 25 reactors of all categories, such as fixed-, fluidized- and moving-bed reactors, bubble columns, sectionalized bubble columns, loop reactors, stirred-tank reactors, film reactors, rotating disk reactors, jet reactors, plunging jet reactors, spray columns, surface aerators... 

Another versatile catalyst test reactor for the investigation of multiphase reactions is shown in Figure 13-7. In such reactors, rotational velocities in excess of 750 rpm ensure very good mass transfer between the catalyst, the gas bubbles, and the liquid, and an internal circulation is generated in the reactor [4]. 

Stage including cage reactors, rotating disk reactors, wiped film reactors and extruder type reactors. 

Several tests have been carried out with a prototype laboratory-scale reactor aiming to find the best performance of the system in terms of CO2 capture rate and methane conversion using 120 g of 1.5 mm spherical particle CuO with AI2O3 (10% wt of active material) [68,69]. The operating temperature has been tested between 650 °C and 800 °C, leading to an increase in die methane conversion (up to 80%) increasing the methane flow rate (from 18 to 48 mL/min) leads to an increase in CH4 conversion but reduces the COj purity. The tests have been carried out with a reactor rotation speed ranging l rounds/min. 

An alternative method of agitation of a tubular reactor is the rotation of the reactor itself. Flow of solids is caused by mounting it in a position slightly inclined to the horizontal, and caking upon the sides is sometimes prevented by the presence of, for example, a loose H section beam or similar heavy article along the length of the tube. The powder feed can enter the end of the reactor via the hollow shaft upon which the reactor rotates. Similarly it can leave via a lower hollow shaft, gas being passed in the reverse direction. 

In most of the attractive examples of intensified process equipment (e.g. in-line mixers, spinning disc reactors, rotating packed-beds, micro-reactors, etc.) the fluid residence time is measured in seconds. Therefore, a process designer should consider the use of these devices, provided that the reactions are (or can be made to be) completed in this time frame. If this is not the case, then the fluid intensity should be detuned to match the relatively relaxed kinetic environment. In this event, with a continuous process, a simple tubular reactor with very modest flow velocities could provide adequate plug flow and residence times up to several hours. In the case of a number of biological processes, as an alternative example, substantial intensification can be achieved using a continuous oscillatory baffled reactor (COBR, see Chapter 5), where residence times may be at best minutes and could extend to hours. 

Stirred batch reactor Rotating disc contactor (RDC)... 

Figure 5. Main features of the device for formation of radial gradient of process duration in the centrifugal field (chemical reaction/exchange diffusion) on the lens surface (diametrical cross-section) 1 cylinder reactor, 2 lid 3 gasket 4 immovable pipe/air eliminator for injection/ehmination of active/inert hquids 5 reactor rotation axis 6 immovable pipe for injection/ehmination of active/inert liquids 7 lens sample (A convex, B concave) a cylinder pipe thickness of active liquid b radius of the active liquid cylinder, h height of the internal space of the reactor (1) cylinder on periphery K height of the spherical base layer of the cylinder pipe (x = a) of the active hquick K height of the spherical layer base of the cylinder pipe (x = a) of the inert liquid H height of the spherical segment R radius of the lens sample r radius of the sphere, to which the lens sample surface corresponds.

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