A reclaiming method is disclosed including conducting evaporation by introducing a part of the absorbent to recover CO.sub.2 or H.sub.2S in a gas in a closed system recovery unit and separating a degraded substance contained in the absorbent from the absorbent to be introduced into an evaporator and obtain recovery steam containing an absorbent and CO.sub.2 or H.sub.2S by a heating section that is provided on a circulation line that circulates in the evaporator; and removing ionic degraded substance by cooling the concentrate obtained in the evaporation and removing an ionic degraded substance in the concentrate after the cooling, wherein a purified concentrate from which the ionic degraded substance has been removed is reused as a purified absorbent.

The present invention provides processes for removing nitrogen species from fresh water or high salinity water recirculated aquaculture systems. The processes are based on physico-chemical treatments which are performed at ambient temperatures and at low pH values thus keeping the total ammonia nitrogen concentrations below a value which is considered detrimental for the growth or survival rate of cultured fish/shrimp.

An aqueous modified acid composition for industrial activities, said composition comprising: an alkanolamine and strong acid in a molar ratio of not less than 1:15, preferably not less than 1:10; it can also further comprise a metal iodide or iodate. Said composition demonstrates advantages over known conventional acids and modified acids.

An aqueous modified acid composition for industrial activities, said composition comprising: an alkanolamine and strong acid in a molar ratio of not less than 1:15, preferably not less than 1:10; it can also further comprise a metal iodide or iodate. Said composition demonstrates advantages over known conventional acids and modified acids.

An aqueous modified acid composition for industrial activities, said composition comprising: an alkanolamine and strong acid in a molar ratio of not less than 1:15, preferably not less than 1:10; it can also further comprise a metal iodide or iodate. Said composition demonstrates advantages over known conventional acids and modified acids.

An aqueous modified acid composition for industrial activities, said composition comprising: an alkanolamine and strong acid in a molar ratio of not less than 1:15, preferably not less than 1:10; it can also further comprise a metal iodide or iodate. Said composition demonstrates advantages over known conventional acids and modified acids.

A system includes an ion exchange softener fluidly coupled to a wastewater treatment system. The first ion exchange softener may receive a first brine stream from the wastewater treatment system and to remove a plurality of minerals from the first brine stream to generate a second brine stream including the plurality of minerals and a third brine stream. The system also includes a mineral removal system disposed downstream from the ion exchange softener and that may receive the second brine stream and to generate a sodium chloride (NaCl) brine stream and an acid and caustic production system disposed downstream from and fluidly coupled to the mineral removal system. The acid and caustic production system includes a first electrodialysis (ED) system that may receive the NaCl brine stream from the mineral removal system and to generate hydrochloric acid (HCl) and sodium hydroxide (NaOH) from the NaCl brine stream. The system also includes a second ED system disposed downstream from the ion exchange softener and upstream of the acid and caustic production system. The second ED system is fluidly coupled to the ion exchange softener and to the acid and caustic production system, and the second ED may generate desalinated water from the third brine stream and an ED concentrate stream. The second ED system may direct the ED concentrate stream to the acid and caustic production system.

A system includes an ion exchange softener fluidly coupled to a wastewater treatment system. The first ion exchange softener may receive a first brine stream from the wastewater treatment system and to remove a plurality of minerals from the first brine stream to generate a second brine stream including the plurality of minerals and a third brine stream. The system also includes a mineral removal system disposed downstream from the ion exchange softener and that may receive the second brine stream and to generate a sodium chloride (NaCl) brine stream and an acid and caustic production system disposed downstream from and fluidly coupled to the mineral removal system. The acid and caustic production system includes a first electrodialysis (ED) system that may receive the NaCl brine stream from the mineral removal system and to generate hydrochloric acid (HCl) and sodium hydroxide (NaOH) from the NaCl brine stream. The system also includes a second ED system disposed downstream from the ion exchange softener and upstream of the acid and caustic production system. The second ED system is fluidly coupled to the ion exchange softener and to the acid and caustic production system, and the second ED may generate desalinated water from the third brine stream and an ED concentrate stream. The second ED system may direct the ED concentrate stream to the acid and caustic production system.

An evaporator is provided that separates, from a degraded substance, an absorbent branched off and introduced, a heating section which is interposed on a circulation line L.sub.21 that circulates the absorbent introduced into this evaporator, heats the circulating absorbent to obtain gaseous recovery steam containing a vaporized absorbent and CO.sub.2, a concentrate branch line L.sub.22 that branches off a part of the absorbent circulating through the circulation line L.sub.21 at a bottom of the evaporator from the circulation line L.sub.21 as a concentrate, a cooler that is interposed on this concentrate branch line L.sub.22 and cools the concentrate, an ionic degraded substance removal section that removes an ionic degraded substance in the cooled concentrate, and a purified absorbent discharge line L.sub.23 that reuses the concentrate as a purified absorbent from which the ionic degraded substance is removed.

An evaporator is provided that separates, from a degraded substance, an absorbent branched off and introduced, a heating section which is interposed on a circulation line L.sub.21 that circulates the absorbent introduced into this evaporator, heats the circulating absorbent to obtain gaseous recovery steam containing a vaporized absorbent and CO.sub.2, a concentrate branch line L.sub.22 that branches off a part of the absorbent circulating through the circulation line L.sub.21 at a bottom of the evaporator from the circulation line L.sub.21 as a concentrate, a cooler that is interposed on this concentrate branch line L.sub.22 and cools the concentrate, an ionic degraded substance removal section that removes an ionic degraded substance in the cooled concentrate, and a purified absorbent discharge line L.sub.23 that reuses the concentrate as a purified absorbent from which the ionic degraded substance is removed.