A process for separating carbon dioxide from a feed gas comprising carbon dioxide may comprise compressing the feed gas in a feed gas compressor to produce a compressed feed gas. The process may also comprise separating the compressed feed gas by an adsorption process comprising: using a plurality of adsorbent beds to produce a carbon dioxide-enriched product stream and a carbon dioxide-depleted stream, and a blowdown step. A blowdown gas may be removed from the adsorbent bed. The process may also comprise compressing the blowdown gas in the feed gas compressor and combining the blowdown gas with the compressed feed gas.

The invention relates to dispersions of porous solids in liquids selected from deep eutectic solvents, liquid oligomers, bulky liquids, liquid polymers, silicone oils, halogenated oils, paraffin oils or triglyceride oils, as well as to their methods of preparation. In embodiments of the invention, the porous solids are metal organic framework materials (MOFs), zeolites, covalent organic frameworks (COFs), porous inorganic materials, Mobil Compositions of Matter (MCMs) or a porous carbon. The invention also relates to the use of porous materials to form dispersions, and to assemblages of such dispersions with a gas or gases. The dispersions can exhibit high gas capacities and selectivities.

The invention relates to dispersions of porous solids in liquids selected from deep eutectic solvents, liquid oligomers, bulky liquids, liquid polymers, silicone oils, halogenated oils, paraffin oils or triglyceride oils, as well as to their methods of preparation. In embodiments of the invention, the porous solids are metal organic framework materials (MOFs), zeolites, covalent organic frameworks (COFs), porous inorganic materials, Mobil Compositions of Matter (MCMs) or a porous carbon. The invention also relates to the use of porous materials to form dispersions, and to assemblages of such dispersions with a gas or gases. The dispersions can exhibit high gas capacities and selectivities.

The invention relates to an apparatus (1) for catalytic decomposition of nitrous oxide in a gas stream derived from exhalation air from a patient. The apparatus (1) comprises an inlet arrangement (2) with a gas inlet (3) for the exhalation air, an outlet arrangement (11) with a gas outlet (12) for an outlet gas, and between these arrangements a through-flow decomposition chamber (9) containing a catalyst material. According to the invention the apparatus is provided with a nitrous oxide adsorption/desorption means (4) in the inlet arrangement (2) for level out variations in the concentration of nitrous oxide fed to the decomposition chamber (9).

The invention relates to an apparatus (1) for catalytic decomposition of nitrous oxide in a gas stream derived from exhalation air from a patient. The apparatus (1) comprises an inlet arrangement (2) with a gas inlet (3) for the exhalation air, an outlet arrangement (11) with a gas outlet (12) for an outlet gas, and between these arrangements a through-flow decomposition chamber (9) containing a catalyst material. According to the invention the apparatus is provided with a nitrous oxide adsorption/desorption means (4) in the inlet arrangement (2) for level out variations in the concentration of nitrous oxide fed to the decomposition chamber (9).

The present invention relates to a specific continuous process for preparing a zeolitic material having a framework structure type selected from the group consisting of MFI, MEL, IMF, SVY, FER, SVR, and intergrowth structures of two or more thereof, preferably an MFI- and/or MEL-type framework structure, comprising Si, Ti, and O, and to a zeolitic material as obtainable and/or obtained according to said process. Further, the present invention relates to a process for preparing a molding, and to a molding obtainable and/or obtained according to said process. Yet further, the present invention relates to a use of said zeolitic material and molding.

The present invention concerns a zeolitic adsorbent agglomerate comprising at least one zeolite of faujasite type comprising sodium and/or lithium and/or calcium, and/or barium and/or potassium, of porosity between 25% and 45%, and having a standard deviation σ of crystal size distribution in said agglomerate of less than 0.30 μm. The invention also concerns the use of the zeolitic adsorbent agglomerate to separate hydrocarbon mixtures, and the process to separate hydrocarbon mixtures using said zeolitic adsorbent agglomerate.

The present invention concerns a zeolitic adsorbent agglomerate comprising at least one zeolite of faujasite type comprising sodium and/or lithium and/or calcium, and/or barium and/or potassium, of porosity between 25% and 45%, and having a standard deviation σ of crystal size distribution in said agglomerate of less than 0.30 μm. The invention also concerns the use of the zeolitic adsorbent agglomerate to separate hydrocarbon mixtures, and the process to separate hydrocarbon mixtures using said zeolitic adsorbent agglomerate.

A gas separation method includes supplying a mixed gas to a zeolite membrane complex and permeating a high permeability gas through the zeolite membrane complex to separate the high permeability gas from other gases. The mixed gas includes a high permeability gas and a trace gas that is lower in concentration than the high permeability gas. The molar concentration of a first gas included in the trace gas in the mixed gas is higher than the molar concentration of a second gas included in the trace gas in the mixed gas. The adsorption equilibrium constant of the first gas on the zeolite membrane is less than 60 times that of the high permeability gas. The adsorption equilibrium constant of the second gas on the zeolite membrane is 400 times or more that of the high permeability gas.

A gas separation method includes supplying a mixed gas to a zeolite membrane complex and permeating a high permeability gas through the zeolite membrane complex to separate the high permeability gas from other gases. The mixed gas includes a high permeability gas and a trace gas that is lower in concentration than the high permeability gas. The molar concentration of a first gas included in the trace gas in the mixed gas is higher than the molar concentration of a second gas included in the trace gas in the mixed gas. The adsorption equilibrium constant of the first gas on the zeolite membrane is less than 60 times that of the high permeability gas. The adsorption equilibrium constant of the second gas on the zeolite membrane is 400 times or more that of the high permeability gas.