Methods for sustainable membrane distillation concentration of hyper saline streams

Abstract

A novel method of producing concentrated streams or otherwise useful hypersaline brines from a source of non-potable or otherwise impaired water is provided. The method comprises feeding the source water into the feed side of a membrane distillation unit while simultaneously feeding a distillate stream through the receiving side of the distillation unit. The feed and receiving sides are separated by a hydrophobic, microporous membrane that allows water vapor to flux through the membrane to the receiving side. As the membrane becomes clogged with particulates, the unit can be subjected to stream flow reversal and/or temperature gradient reversal in order to remove those particulates and restore previous vapor flux levels, after which previous operations can be resumed.

We claim: 
     
         1 . A method of concentrating water comprising:
 (a) providing a membrane distillation unit comprising:
 a feed side having an inlet and an outlet; 
 a receiving side having an inlet and an outlet; and
 a membrane positioned between the feed and receiving sides, said membrane being in communication with both said feed side and said receiving side; 
 
   (b) passing:
 a source water having a first temperature through either said feed side or said receiving side; and 
 a distillate stream having a second temperature through the other of said feed side or said receiving side, said first temperature being higher than said second temperature, thereby creating a vapor pressure gradient across said membrane, causing a vapor flux from said source water to said distillate stream; and 
   (c) carrying out one or more of the following:
 (i) ceasing said source water and distillate stream passing and causing said distillate stream to pass through the side through which said source water was passing prior to said ceasing; 
 (ii) reversing said passing so that said source water and distillate stream pass through the opposite sides from the sides through which they were passing prior to said reversing; 
 (iii) ceasing the passing of said source water and causing a cooling stream to pass through the side through which the source water was passing prior to said ceasing, said cooling stream having a temperature that is lower than said distillate stream second temperature; and 
 (iv) ceasing the passing of said distillate stream and causing a heated water stream to pass through the side through which the distillate stream was passing prior to said ceasing, said heated water stream having a temperature that is higher than said source water first temperature. 
   
     
     
         2 . The method of  claim 1 , further comprising heating said source water prior to or during said passing (b). 
     
     
         3 . The method of  claim 1 , further comprising cooling said distillate stream prior to or during said passing (b). 
     
     
         4 . The method of  claim 1 , wherein said source water and distillate stream have respective solute concentrations, wherein the solute concentration in said source water is higher than that in said distillate stream prior to said passing (b). 
     
     
         5 . The method of  claim 1 , wherein said source water is selected from the group consisting of impaired water, chemical processing inflow, liquid foods, biological substances, treated wastewater, wastewater, saline lake water, brackish-water, runoff water, concentrated seawater, seawater, and mixtures of the foregoing. 
     
     
         6 . The method of  claim 1 , wherein the permeate/distillate stream is selected from the group consisting of distilled deionized water, potable water, and water having a low total dissolved solids. 
     
     
         7 . The method of  claim 1 , wherein the membrane is hydrophobic and microporous. 
     
     
         8 . The method of  claim 1 , wherein said membrane comprises a shape selected from the group consisting of flat sheet, spiral wound, and hollow fiber. 
     
     
         9 . The method of  claim 1 , wherein said source water is under a positive or negative pressure. 
     
     
         10 . The method of  claim 1 , wherein said distillate stream is under a positive or negative pressure. 
     
     
         11 . The method of  claim 1 , wherein during said passing (b), said source water and distillate stream are running co-currently. 
     
     
         12 . The method of  claim 1 , wherein during said passing (b), said source water and distillate stream are running counter-currently. 
     
     
         13 . The method of  claim 1 , wherein prior to said passing (b), one or both of the source water and distillate stream pass through a 4-way crossover valve. 
     
     
         14 . The method of  claim 1 , wherein a modified source stream exits the outlet of either said feed side or said receiving side, and a modified distillate stream exits the outlet of the other of said feed side or said receiving side, wherein said one or both of the modified source stream and modified distillate stream pass through a 4-way crossover valve after exiting the respective outlets. 
     
     
         15 . The method of  claim 1 , wherein during said passing (b), precipitates collect on said membrane, and during said carrying out (i) or (ii) at least some of said precipitates are removed, so as to at least partially restore membrane permeability. 
     
     
         16 . The method of  claim 1 , wherein during said carrying out (iii), the cooling stream comes from one or a plurality of source water reservoirs. 
     
     
         17 . The method of  claim 16 , wherein said fresh water reservoirs have respective temperatures that are lower than the distillate stream second temperature. 
     
     
         18 . The method of  claim 1 , where during said carrying out (iii), said vapor pressure gradient is reversed, thereby reversing said vapor flux. 
     
     
         19 . The method of  claim 18 , wherein during said passing (b), precipitates collect on said membrane, and wherein said vapor flux reversal causes at least some of said precipitates to be removed, so as to at least partially restore membrane permeability. 
     
     
         20 . The method of  claim 1 , wherein during (iv), the heated water stream comes from one or a plurality of fresh water reservoirs. 
     
     
         21 . The method of  claim 20 , wherein said fresh water reservoirs have respective temperatures that are higher than the source water first temperature. 
     
     
         22 . The method of  claim 1 , where during (iv), said vapor pressure gradient is reversed, thereby reversing said vapor flux. 
     
     
         23 . The method of  claim 22 , wherein during said passing (b), precipitates collect on said membrane, and wherein said vapor flux reversal causes at least some of said precipitates to be removed, so as to at least partially restore membrane permeability. 
     
     
         24 . The method of  claim 1 , wherein said first temperature is at least about 5° C. higher than said second temperature. 
     
     
         25 . The method of  claim 1 , wherein during said passing (b), precipitates collect on said membrane, causing a decrease in said vapor flux. 
     
     
         26 . The method of  claim 25 , wherein said carrying out (iii) is initiated upon detection of said vapor flux dropping below a predetermined level. 
     
     
         27 . The method of  claim 26 , wherein said carrying out (iii) results in the removal of at least some of said precipitates from said membrane, thereby at least partially restoring membrane permeability. 
     
     
         28 . The method of  claim 27 , further comprising resuming said passing (b) after desired membrane permeability has been restored. 
     
     
         29 . The method of  claim 1 , wherein during said carrying out (iii), said distillate second stream temperature is at least about 5° C. higher than said cooling stream temperature. 
     
     
         30 . The method of  claim 1 , where during said carrying out step (iv), said heated water stream temperature is at least about 5° C. higher than said source water first temperature.