A method of producing a cooled dry gas is provided. The method includes exposing an input gas to an aqueous saline solution having a temperature of 20 to 80° C. to produce a first intermediate gas. In addition, the method further includes exposing the first intermediate gas to freshwater having a temperature of greater than −5° C. to less than 20° C. to produce a second intermediate gas. The method also includes cooling the second intermediate gas to a temperature of −40 to −5° C. to produce a cooled gas. The method further includes exposing the cooled gas to a chemical adsorbent to produce a saturated adsorbent and the cooled dry gas.

Described herein are membrane processes for separating CO.sub.2 from flue gas. An exemplary process involves passing a fluid stream including the flue gas across a membrane permeable to CO.sub.2 and H.sub.2O, removing treated gas from a feed side of the membrane that has less CO.sub.2 than the flue gas, and removing permeate from a permeate side of the membrane comprising CO.sub.2 and H.sub.2O. Suitably, the permeate is removed at a sub-atmospheric vacuum pressure. The permeate is then cooled to remove at least some of the H.sub.2O from the permeate and form a smaller volume of H.sub.2O-depleted, CO.sub.2 enriched permeate.

Described herein are membrane processes for separating CO.sub.2 from flue gas. An exemplary process involves passing a fluid stream including the flue gas across a membrane permeable to CO.sub.2 and H.sub.2O, removing treated gas from a feed side of the membrane that has less CO.sub.2 than the flue gas, and removing permeate from a permeate side of the membrane comprising CO.sub.2 and H.sub.2O. Suitably, the permeate is removed at a sub-atmospheric vacuum pressure. The permeate is then cooled to remove at least some of the H.sub.2O from the permeate and form a smaller volume of H.sub.2O-depleted, CO.sub.2 enriched permeate.

A system for processing biogas, the system comprising: a container, a pressure swing adsorption (PSA) unit housed in the container, the PSA unit having: a plurality of beds containing adsorbent material, the adsorbent material configured to selectively adsorb gas species from the biogas to process the biogas, a rotary valve module for distributing flow of 5 the biogas within the PSA unit, an inlet for supplying the biogas to the plurality of beds from outside of the container, and an outlet for transporting the processed biogas away from the PSA unit.

A system for processing biogas, the system comprising: a container, a pressure swing adsorption (PSA) unit housed in the container, the PSA unit having: a plurality of beds containing adsorbent material, the adsorbent material configured to selectively adsorb gas species from the biogas to process the biogas, a rotary valve module for distributing flow of 5 the biogas within the PSA unit, an inlet for supplying the biogas to the plurality of beds from outside of the container, and an outlet for transporting the processed biogas away from the PSA unit.

A flue gas can be cooled for carbon capture purposes with the use of a gas-to-gas exchanger, using air as the cooling media, downstream of a heat recovery process, and optionally upstream of a quenching process; the use of an amine chilling process to reduce the required flue gas cooling duties upstream of the CO.sub.2 absorber; the use of a gas-to-gas exchanger, using the absorber overhead as the cooling media, downstream of a heat recovery process, and optionally upstream of the quenching process; and/or the use of a quenching process in which heated water and condensate is cooled by an external cooling loop utilizing treated flue gas condensate in an evaporative cooling process.

The invention relates to a method for reduction of HCl emission from a cement plant based on a treatment of a preheater (1) and/or bypass gas stream, characterized in that a cement raw meal, as a HCl absorber, is dispersed in the gas stream(s) from which HCl is to be removed; the cement raw meal is introduced from a raw mill (6) and/or a silo (8) into a pipe with a up going gas flow; the pipe being arranged in fluid communication at a point after a gas conditioning tower (7) and/or before a particle filter unit (5) and/or in a by-pass line before particle filter (4).

The invention relates to a method for reduction of HCl emission from a cement plant based on a treatment of a preheater (1) and/or bypass gas stream, characterized in that a cement raw meal, as a HCl absorber, is dispersed in the gas stream(s) from which HCl is to be removed; the cement raw meal is introduced from a raw mill (6) and/or a silo (8) into a pipe with a up going gas flow; the pipe being arranged in fluid communication at a point after a gas conditioning tower (7) and/or before a particle filter unit (5) and/or in a by-pass line before particle filter (4).

Method and installation for treating a CO.sub.2- and H.sub.2O-containing flue gas generated by an industrial process unit before CCUS, whereby the flue gas evacuated from the unit is subjected to cooling to a temperature T2 between 100 and 600° C., whereby the cooled flue gas is pretreated in one or more particle removal and/or gas cleaning and/or drying stages and the temperature of the cooled flue gas is further reduced to a temperature T3<T2, before a first part of pretreated flue gas is subjected to CCUS, a second part of the pretreated flue gas being recycled at temperature T3 as a cooling agent and mixed with the flue gas during the controlled cooling thereof, partially or fully purified CO.sub.2 from the CCUS may be recycled at temperature T4<T2 may be recycled as a cooling agent and mixed with the flue gas during the controlled cooling.

Method and installation for treating a CO.sub.2- and H.sub.2O-containing flue gas generated by an industrial process unit before CCUS, whereby the flue gas evacuated from the unit is subjected to cooling to a temperature T2 between 100 and 600° C., whereby the cooled flue gas is pretreated in one or more particle removal and/or gas cleaning and/or drying stages and the temperature of the cooled flue gas is further reduced to a temperature T3<T2, before a first part of pretreated flue gas is subjected to CCUS, a second part of the pretreated flue gas being recycled at temperature T3 as a cooling agent and mixed with the flue gas during the controlled cooling thereof, partially or fully purified CO.sub.2 from the CCUS may be recycled at temperature T4<T2 may be recycled as a cooling agent and mixed with the flue gas during the controlled cooling.