Recent content by andredd

no, here main stream is RO reject (8 m3) then various streams 1,5 - 2 m3 each such ad DMF backwash, neutralized effluents, etc did you have in mind different treatment for it?

well , blowdown is one of the streams to this plant, but it accounts some 2 m3 / hr on a overall of 16. yeah i m contacting evaporators suppliers, its under process, lets see what they can do with caso4 and baso4 scaling.....

thanks for your advices. The point is that the plant is already existing , so wastes are "already ready" to be discharged to my "new" WWTP (its the new WWTP to ttreat the wastes coming from the existing plant). so i can not modify that much the WT approach in the power plant but only receiving...

thanks a lot. its a power plant aiming to recover water from ro brine, effluents regeneration e dmf backwash, but they want 80 % !!

thanks for your reply very much. I do have a concern: dont the sulfates make big problems with scaling? as i know, they have inverse solubility relationship with temperature, dont they make CaSO4 / BaSO4 scaling quickly inside the evaporator? Did you not have problems such as frequent chemical...

but, would it be better evaporators or crystallizers? which is the difference exactly? is it concerning the aimed target i.e. if the scope is recovering salts (not here) or water ? my brine would enter the unit with some 62.000 TDS, mainly sulphates and calcium thanks evbody since now ! andrea

many thanx evbody for kind support ! i think i will go first to RO (45% max to have saturation 95% and be at limits of scaling) and then evaporator. yes they must recover as a) disposing outside not allowed b) paying tankers not feasible also from logistic point fo view c) evaporation pond...

ok many thanks

thank you . So at the end you are saying that the brine concentrator, working on 16 m3 / hr, in terms of CAPEX but ALSO on OPEX, would be less utility / power / overall cost consuming than RO ? thank you

ok many thanks for your quick reply ! :-) but apart from chemicals consumptions and disposal issues (also evaporator has costs, in terms of enery, and high also CAPEX cost)of sludge from clarifiers bottom, why do you say that recovering from regeneration effluents is not an application? still...

hello everybody...! i m asked by a client to recover with RO 80% of a water coming from DMF backwash + demi plant regeneration effluents (after neutralization). This water has a lot of sulphates (5000 ppm) and calcium (1250 ppm), some magnesium (550 ppm) and barium (0,5 ppm). The RO design guy...