The facility (1A) includes at least two treatment devices (2) each with an exchange chamber (20) intended to contain a liquid bath in the bottom part and at least one injection line (21). An aeraulic means (4), creates by suction or by blowing, simultaneously and in parallel for each treatment device (2), an incoming gas stream (F) originating from outside the exchange chambers (2) and passes through the discharge opening of the injection line (21) by being introduced into the liquid bath contained in the bottom part of the exchange chamber (20), below the surface (S) of said liquid bath. The exchange chambers (20) communicate hydraulically with one another so that when the aeraulic means (4) are shut down, each exchange chamber (20) is suitable for containing or contains, in the bottom part, an initial volume (V.sub.initial) of liquid, with an initial liquid level (H.sub.initial) that is identical in all the exchange chambers (2).

A desulfurization gas process includes water vapor, CO.sub.2 and SO.sub.x (x=2 and/or 3). In a treatment unit, the gas contacts a cooled alkaline aqueous solution having a temperature lower than an initial gas temperature, water and a carbonate of an alkali metal, to cool the gas, condense some water vapor and absorb SO.sub.x in the carbonate-containing solution, produce an SO.sub.x-depleted gas and an acidic aqueous solution including sulfate and/or sulfite ions. The SO.sub.x-depleted gas and a portion of the acidic aqueous solution can then be withdrawn from the treatment unit. Carbonate of the alkali metal can be added to remaining acidic aqueous solution to obtain a made-up alkaline aqueous solution. This solution can be cooled and reused as the cooled alkaline aqueous solution. An SO.sub.x absorbent solution includes a bleed stream from a CO.sub.2-capture process, sodium or potassium carbonate, and an acidic aqueous solution obtained from desulfurization.

A desulfurization gas process includes water vapor, CO.sub.2 and SO.sub.x (x=2 and/or 3). In a treatment unit, the gas contacts a cooled alkaline aqueous solution having a temperature lower than an initial gas temperature, water and a carbonate of an alkali metal, to cool the gas, condense some water vapor and absorb SO.sub.x in the carbonate-containing solution, produce an SO.sub.x-depleted gas and an acidic aqueous solution including sulfate and/or sulfite ions. The SO.sub.x-depleted gas and a portion of the acidic aqueous solution can then be withdrawn from the treatment unit. Carbonate of the alkali metal can be added to remaining acidic aqueous solution to obtain a made-up alkaline aqueous solution. This solution can be cooled and reused as the cooled alkaline aqueous solution. An SO.sub.x absorbent solution includes a bleed stream from a CO.sub.2-capture process, sodium or potassium carbonate, and an acidic aqueous solution obtained from desulfurization.

A desulfurization gas process includes water vapor, CO.sub.2 and SO.sub.x (x=2 and/or 3). In a treatment unit, the gas contacts a cooled alkaline aqueous solution having a temperature lower than an initial gas temperature, water and a carbonate of an alkali metal, to cool the gas, condense some water vapor and absorb SO.sub.x in the carbonate-containing solution, produce an SO.sub.x-depleted gas and an acidic aqueous solution including sulfate and/or sulfite ions. The SO.sub.x-depleted gas and a portion of the acidic aqueous solution can then be withdrawn from the treatment unit. Carbonate of the alkali metal can be added to remaining acidic aqueous solution to obtain a made-up alkaline aqueous solution. This solution can be cooled and reused as the cooled alkaline aqueous solution. An SO.sub.x absorbent solution includes a bleed stream from a CO.sub.2-capture process, sodium or potassium carbonate, and an acidic aqueous solution obtained from desulfurization.

A desulfurization gas process includes water vapor, CO.sub.2 and SO.sub.x (x=2 and/or 3). In a treatment unit, the gas contacts a cooled alkaline aqueous solution having a temperature lower than an initial gas temperature, water and a carbonate of an alkali metal, to cool the gas, condense some water vapor and absorb SO.sub.x in the carbonate-containing solution, produce an SO.sub.x-depleted gas and an acidic aqueous solution including sulfate and/or sulfite ions. The SO.sub.x-depleted gas and a portion of the acidic aqueous solution can then be withdrawn from the treatment unit. Carbonate of the alkali metal can be added to remaining acidic aqueous solution to obtain a made-up alkaline aqueous solution. This solution can be cooled and reused as the cooled alkaline aqueous solution. An SO.sub.x absorbent solution includes a bleed stream from a CO.sub.2-capture process, sodium or potassium carbonate, and an acidic aqueous solution obtained from desulfurization.

Embodiments of the disclosure provide a method and system for sulfur recovery. A Claus tail gas stream is fed to a hydrogenation reactor to produce a hydrogenated gas stream. The hydrogenated gas stream is fed to a quench tower to produce a quenched gas stream. The quenched gas stream is fed to a first stage adsorption vessel of first stage adsorption unit to produce a first outlet gas stream. The first outlet gas stream is fed to a second stage adsorption vessel of a second stage adsorption unit to produce a second byproduct gas stream. The first stage adsorption vessel is regenerated to produce a first byproduct gas stream. The second stage adsorption vessel is regenerated to produce a second outlet gas stream including hydrogen sulfide. Optionally, a portion of the second byproduct gas stream or nitrogen can be fed to the first stage adsorption vessel or the second stage adsorption vessel for regeneration. Optionally, a sales gas can be fed to the second stage adsorption vessel for regeneration. Optionally, vacuum can be applied to the first stage adsorption vessel or the second stage adsorption vessel for regeneration.

Embodiments of the disclosure provide a method and system for sulfur recovery. A Claus tail gas stream is fed to a hydrogenation reactor to produce a hydrogenated gas stream. The hydrogenated gas stream is fed to a quench tower to produce a quenched gas stream. The quenched gas stream is fed to a first stage adsorption vessel of first stage adsorption unit to produce a first outlet gas stream. The first outlet gas stream is fed to a second stage adsorption vessel of a second stage adsorption unit to produce a second byproduct gas stream. The first stage adsorption vessel is regenerated to produce a first byproduct gas stream. The second stage adsorption vessel is regenerated to produce a second outlet gas stream including hydrogen sulfide. Optionally, a portion of the second byproduct gas stream or nitrogen can be fed to the first stage adsorption vessel or the second stage adsorption vessel for regeneration. Optionally, a sales gas can be fed to the second stage adsorption vessel for regeneration. Optionally, vacuum can be applied to the first stage adsorption vessel or the second stage adsorption vessel for regeneration.

An ammonia-based multi-zone double-loop process for ultra-low emission of multi-pollutant. From an absorption tower inlet, the flue gas successively passes through cooling concentration crystallization, sulfur oxide absorption, water washing and purifying and dust and mist removing zones, which are separated by gas permeable liquid collecting plates, forming clean flue gas and discharged from an outlet. The cooling concentration crystallization zone, the sulfur oxide absorption zone, and the water washing and purifying zone are respectively provided with a plurality of sprayers, and respectively use a concentration liquid, an absorption liquid, and a water washing liquid as spraying liquids. The absorption, concentration and water washing liquids, after converging respectively, into absorption, concentration crystallization and water washing circulation tanks, the absorption, concentration and water washing liquids, respectively, are sprayed in a circulating manner through absorption, concentration and water washing pumps.

The present invention discloses methods for extracting and recycling hydrogen in an MOCVD process by FTrPSA. Through pretreatment, fine deamination, PSA hydrogen extraction, deep dehydration and hydrogen purification procedures, ammonia-containing waste hydrogen from an MOCVD process is purified to meet the electronic-level hydrogen (the purity is greater than or equal to 99.99999% v/v) standard required by the MOCVD process, to implement resource reuse of exhaust gases, where the hydrogen yield is greater than or equal to 75-86%. The present invention solves the technical problem that atmospheric-pressure or low-pressure waste hydrogen from MOCVD processes cannot be returned to the MOCVD processes for use after being recycled, and fills the gap in green and circular economy development of the LED industry.

The present invention discloses methods for extracting and recycling hydrogen in an MOCVD process by FTrPSA. Through pretreatment, fine deamination, PSA hydrogen extraction, deep dehydration and hydrogen purification procedures, ammonia-containing waste hydrogen from an MOCVD process is purified to meet the electronic-level hydrogen (the purity is greater than or equal to 99.99999% v/v) standard required by the MOCVD process, to implement resource reuse of exhaust gases, where the hydrogen yield is greater than or equal to 75-86%. The present invention solves the technical problem that atmospheric-pressure or low-pressure waste hydrogen from MOCVD processes cannot be returned to the MOCVD processes for use after being recycled, and fills the gap in green and circular economy development of the LED industry.