A cylindrical flow distributor (100) for performing, by means of solid reaction members, a biological or chemical transformation, or physical or chemical trapping from, or release of agents to, a fluidic media is provided. The flow distributor (100) comprises: a top wall (1); a bottom wall (2) comprising a central through going opening (13); and an outer wall (3) extending between the top wall (1) and the bottom wall (2). The top wall (1), the bottom wall (2) and an inner envelope surface (5) of said outer wall (3) together define a confinement (7) configured to contain solid reaction membersor a rigid body of a reaction member material. The outer wall (3) comprises a first plurality of longitudinally extending ribs (20) arranged side by side with longitudinal gaps (21) extending in the circumferential direction between two adjacent ribs (20), and a circumferentially extending first scaffold (22) encircling and being fixedly attached to a peripheral outer surface (29) of said plurality of longitudinally extending ribs (20). Further, a reactor using such flow distributor (100) is provided.

An inflow base which is permeable to process air and includes openings for the process air which flows thought the inflow base. The inflow base is arranged in the fluidizing apparatus in a manner rotatable about an axis Z of the fluidizing apparatus and subdivides this into a distribution chamber and into a vortex chamber. The inflow base of the fluidizing apparatus includes at least a first and a second inflow base plate, wherein one of the inflow base plates at its outer end includes or forms a sealing element.

A catalyst structure includes a porous support structure, where the support structure includes an aluminosilicate material and any two or more metals loaded in the porous support structure selected from Ga, Ag, Mo, Zn, Co and Ce. The catalyst structure is used in a hydrocarbon upgrading process that is conducted in the presence of methane, nitrogen or hydrogen.

A catalyst structure includes a porous support structure, where the support structure includes an aluminosilicate material. Any two or more metals are loaded in the porous support structure, the two or more metals selected from the group consisting of Ga, Ag, Mo, Zn, Co and Ce, where each metal loaded in the porous support structure is present in an amount from about 0.1 wt % to about 20 wt %. In example embodiments, the catalyst structure includes three or more of the metals loaded in the porous support structure. The catalyst structure is used in a hydrocarbon upgrading process that is conducted in the presence of methane, nitrogen or hydrogen.

A catalyst structure includes a porous support structure, where the support structure includes an aluminosilicate material and any two or more metals loaded in the porous support structure selected from Ga, Ag, Mo, Zn, Co and Ce. The catalyst structure is used in a hydrocarbon upgrading process that is conducted in the presence of methane, nitrogen or hydrogen.

An inflow base which is permeable to process air and includes openings for the process air which flows thought the inflow base. The inflow base is arranged in the fluidizing apparatus in a manner rotatable about an axis Z of the fluidizing apparatus and subdivides this into a distribution chamber and into a vortex chamber. The inflow base of the fluidizing apparatus includes at least a first and a second inflow base plate, wherein one of the inflow base plates at its outer end includes or forms a sealing element.

A molybdenum-vanadium bimetal oxide catalyst having a molecular formula of Mo.sub.1V.sub.y, where y represents an atomic molar ratio of vanadium and molybdenum. An oxygen support Mo.sub.1V.sub.y is prepared by an impregnation method including impregnation, drying, calcination, and tablet pressing. In the dehydrogenation reaction of a light alkane to an alkene over the supported molybdenum-vanadium bimetal oxide, the reaction temperature is 450° C.-550° C. Propane can be oxidized and dehydrogenated to produce propylene with a high activity and high selectivity. A conversion rate of propane remains at 30%-40%, and a selectivity for propylene is 80%-90%. A fresh oxygen support changes from a high-valence state to a low-valence state after reacting with propane. A low-valence state oxygen support reacts with air or oxygen to be oxidized to a high-valence state, and recovers lattice oxygen and cycles again.

A catalyst structure includes a porous support structure, where the support structure includes an aluminosilicate material. Any two or more metals are loaded in the porous support structure, the two or more metals selected from the group consisting of Ga, Ag, Mo, Zn, Co and Ce, where each metal loaded in the porous support structure is present in an amount from about 0.1 wt % to about 20 wt %. In example embodiments, the catalyst structure includes three or more of the metals loaded in the porous support structure. The catalyst structure is used in a hydrocarbon upgrading process that is conducted in the presence of methane, nitrogen or hydrogen.

A molybdenum-vanadium bimetallic oxide catalyst and its application in the chemical looping oxidative dehydrogenation of alkane. The molecular formula of molybdenum-vanadium bimetallic oxide catalyst is MoVy and y represents the atomic molar ratio of vanadium and molybdenum. The supported MoVy catalyst is prepared by impregnation method, following the drying, calcination and tablet pressing. The reaction temperature was 450-550 C., and propane could be oxidized and dehydrogenated to propylene with high activity and selectivity, with propane conversion rate remaining at 30-40% and propylene selectivity at 80-90%. The fresh catalysts were reduced to the lower valence states with the lattice oxygen diffusion to propane. After the dehydrogenation, the reduced samples were regenerated to recover to the initial state and regain the lattice oxygen. During the redox cycles, the reaction performance remains stable, which can be used in the fixed bed reactor, moving bed reactor or circulating fluidized bed.

Systems and methods employing beds of bagged and caged absorbent and adsorbent materials are disclosed. These inventions are useful in the area of solid phase extraction.