Disclosed is an improved process for recovering condensable components from a gas stream, in particular, hydrocarbons from a gas stream such as natural gas. The present process uses solid adsorbent media to remove said hydrocarbons wherein the adsorbent media is regenerated in a continuous fashion in a heated continuous counter-current regeneration system, wherein said heated regenerated adsorbent media is cooled prior to reuse.

A device for treating a gas laden with pollutants, includes at least one adsorption module for adsorbing the pollutants, which is utilized in an adsorption apparatus. The adsorption module includes at least one electrically conductive layer of an activated carbon fiber mat, an electric current circuit for heating the activated carbon fiber mat for the desorption of the adsorbed pollutants, and distributing conduit which is routed into the center of the adsorption module and has outlet openings for a flush gas for inertizing and rinsing the activated carbon fiber mat.

A filter medium is provided with a layer (A) provided with non-impregnated active carbon, a layer (B) with a solid carrier material that is impregnated with a permanganate salt, and a layer (C) with alkaline impregnated active carbon. The layer (B) and the layer (C) are arranged such that a gas flowing through the filter medium flows through the layer (B) before flowing through the layer (C). The layer (A) is arranged such that the gas flowing through the filter medium flows through the layer (A) before flowing through the layer (B) or the gas flowing through the filter medium flows through the layer (A) after flowing through the layer (C).

The present invention relates to an adsorbent comprising an alumina support and at least one alkali element, said adsorbent being obtained by introducing at least one alkali element, identical to or different from sodium, onto an alumina support the sodium content of which, expressed as Na.sub.2O equivalent, before the introduction of the alkali element or elements, is comprised between 1000 and 5000 ppm by weight with respect to the total weight of the support. The invention also relates to processes for the preparation of said adsorbent and use thereof in a process for the elimination of acidic molecules such as COS and/or CO.sub.2.

An air supply system for a fuel cell includes: a fuel cell stack in which multiple unit cells are stacked and that generates electricity through chemical reactions, an air channel to supply incoming air containing oxygen to the fuel cell stack and to transfer air discharged from the fuel cell stack to the outside of the air supply system, and a gas adsorption unit that is disposed on the air channel, positioned near an outlet of the fuel cell stack, and adsorbs oxygen contained in the air introduced into the air channel.

A method for producing a fluorinated carbon adsorbent which involves digesting rice husk, sulfonating the digested rice husk, and fluorinating the sulfonated rice husk. The method yields a fluorinated carbon adsorbent material having an adsorption capacity for CO.sub.2 of 1.6 to 2.5 mmol/g, an adsorption capacity for CH.sub.4 of 0.4 to 0.8 mmol/g, and an adsorption capacity for N.sub.2 of 0.1 to 0.4 mmol/g, at a temperature of 273 to 298 K and a pressure of 0.75 to 1.5 atm. Also disclosed is a method for separating a mixture of gases using the fluorinated carbon adsorbent.

The present invention relates to a method of separating and recovering NGLs from a natural gas feedstream. Specifically, the present method allows for the separation of ethane and heavier hydrocarbons and/or propane and heavier hydrocarbons from a raw natural gas feedstream to provide pipeline quality natural gas. One embodiment of this method provides for the use of a regenerable adsorbent media which is regenerated by a microwave heating system. Said regeneration step may be operated as a batch process, a semi-continuous process, or a continuous process.

A catalyst system comprising a combination of: 1) one or more catalyst compounds comprising at least one nitrogen linkage; 2) a support comprising an organosilica material, which is a mesoporous organosilica material; and 3) an optional activator. Useful catalysts include pyridyldiamido transition metal complexes, HN5 compounds, and bis(imino)pyridyl complexes. The organosilica material is a polymer of at least one monomer of Formula [Z.sup.1OZ.sup.2SiCH.sub.2].sub.3(1), where Z.sup.1 represents a hydrogen atom, a C.sub.1-C.sub.4alkyl group, or a bond to a silicon atom of another monomer and Z.sup.2 represents a hydroxyl group, a C1-C.sub.4alkoxy group, a C.sub.1-C.sub.6 alkyl group, or an oxygen atom bonded to a silicon atom of another monomer. This invention further relates to processes to polymerize olefins comprising contacting one or more olefins with the above catalyst system.

Chromatography method in which a gaseous, liquid or supercritical mobile phase containing species to be separated is circulated through a packing, said packing being characterized in that: it comprises a plurality of capillary ducts extending in the packing between an upstream face through which the mobile phase enters the packing and a downstream face through which the mobile phase leaves the packing—the material of the walls comprises a first population of connected pores, providing passages from one duct to the next enabling molecular diffusion to take place between adjacent ducts, pores having a mean diameter (d.sub.pore) of greater than 2 times the molecular diameter of at least one species to be separated—the diameter of the ducts is less than 50 μm.

An object of the present invention is to provide an adsorbent and a canister which can improve adsorption performance and purge performance. An adsorbent 10 to be packed in a canister includes: a cylindrical outer wall 10A, and a plurality of ribs 10B for partitioning along an axis of the outer wall 10A into a plurality of cells, wherein the thickness da of the outer wall 10A and the thickness dβ of the ribs 10B is less than 0.6 mm, the thickness of at least either of the outer wall 10A and the ribs 10B exceeds 0.4 mm, the outer diameter D of the outer wall 10A is 3.5 mm or more and 40 mm or less, a BWC exceeds 3.0 g/dL, and

purge efficiency((amount of butane adsorbed−amount of butane retained)/amount of butane adsorbed) is more than 0.86 or more.