TEMPERATURE SWING SOLVENT EXTRACTION FOR DESCALING OF FEEDSTREAMS
Systems and methods of performing temperature swing solvent extraction (TSSE) descaling of produced water and desalination of high-salinity brines, e.g., those having a total dissolved solids (TDS) greater than about 250,000 ppm are capable of producing descaled water products including less than about 5% weight percent TDS. The brine/produced water feedstreams and combined with a solvent having temperature-dependent water solubility at a temperature T L . Water is extracted from the feedstream into the solvent to form a water-in-solvent extract component and a raffinate component, from which a solid phase can be precipitated as more water is portioned in the solvent and basicity increases. Heating of the water-in-solvent extract component reduces the solubility of the water therein, producing a biphasic mixture of dewatered solvent and descaled water that can be separated. Because these systems and methods do not require a phase change of water, these products are achieved with significantly higher energy efficiencies when compared to evaporation-based thermal methods.
1 . A method of performing temperature swing solvent extraction (TSSE) desalination of high-salinity brines, comprising:
providing a feedstream having a total dissolved solids greater than about 250,000 ppm;
combining the feedstream with a solvent, wherein the solvent has temperature-dependent water solubility;
bringing the combined feedstream and solvent to a temperature T L ;
extracting a liquid from the feedstream into the solvent to form a water-in-solvent extract component and a raffinate component at temperature T L , wherein the raffinate component includes an aqueous phase, a solid phase, or combinations thereof;
separating the water-in-solvent extract component from the raffinate component;
heating the water-in-solvent extract component to a temperature T H to produce a biphasic mixture of dewatered solvent and descaled water; and
separating the dewatered solvent and the descaled water,
wherein the descaled water includes less than about 5% weight percent total dissolved solids.
2 . The method according to claim 1 , wherein the feedstream includes brine, produced water, or combinations thereof.
3 . The method according to claim 1 , further comprising:
cooling the dewatered solvent component from temperature T H ; and
combining the dewatered solvent component with the feedstream.
4 . The method according to claim 1 , further comprising:
precipitating the solid phase; and
sieving the solid phase from a liquid phase, the solid phase including one or more scalants from the feedstream.
5 . The method according to claim 4 , wherein the one or more scalants includes an alkali metal salts, Ca(OH) 2 , CaCO 3 , FeCO 3 , Mg(OH) 2 , MgCO 3 , MnCO 3 , SrCO 3 , BaSO 4 , CaSO 4 , MgSO 4 , SrSO 4 , or combinations thereof.
6 . The method according to claim 1 , wherein the solvent includes diisopropylamine (DIPA), N-ethylcyclohexylamine (ECHA), and N,N-dimethylcyclohexyl amine (DMCHA), triethylamine (TEA), N-methylcyclohexylamine (nMCHA), N,N-dimethylisopropylamine (DMIPA), or combinations thereof.
7 . The method according to claim 1 , wherein T L is below about 20° C.
8 . (canceled)
9 . The method according to claim 1 , wherein T H is between about 40° C. and about 80° C.
10 . (canceled)
11 . (canceled)
12 . The method according to claim 1 , wherein the feedstream to solvent ratio is less than about 15 mL/mol.
13 . A method of performing temperature swing solvent extraction-stepwise release (TSSE-SR) desalination of hypersaline brines, comprising:
providing a feedstream including a concentration of dissolved salts;
combining the feedstream with one or more solvents, wherein the one or more solvents has temperature-dependent water solubility;
bringing the combined feedstream and solvent to a temperature T 1 ;
extracting water from the feedstream into the solvent to form a water-in-solvent component and a raffinate component at temperature T 1 , wherein the raffinate component includes an increased concentration of dissolved salts;
separating the water-in-solvent component from the raffinate component bringing a previous water-in-solvent component produced via a previous separation step to at least one new temperature T N to produce a biphasic mixture of a subsequent water-in-solvent component and a subsequent raffinate component at temperature T N ,
separating the subsequent water-in-solvent component from the subsequent raffinate component;
bringing a subsequent water-in-solvent component to a temperature T F to produce a biphasic mixture of dewatered solvent and descaled water;
separating the dewatered solvent and the descaled water, and
recycling the dewatered solvent to the combined feedstream and solvent,
wherein the feedstream includes brines, produced waters, or combinations thereof.
14 . (canceled)
15 . (canceled)
16 . (canceled)
17 . A system of performing temperature swing solvent extraction (TSSE) desalination of high-salinity brines, comprising:
a feedstream in fluid communication with a fluid source, the fluid source including a fluid having a total dissolved solids greater than about 250,000 ppm;
a solvent source including one or more solvents with temperature-dependent water solubility;
one or more extractors in fluid communication with the feedstream and the solvent source, the extractor including at least a first outlet and a second outlet;
a water-in-solvent extract outlet stream in communication with the first outlet;
a raffinate outlet stream in communication with the second outlet, wherein the raffinate outlet stream includes an aqueous phase, a solid phase, or combinations thereof;
a separator in fluid communication with the water-in-solvent extract outlet stream, the separator including at least a third outlet and a fourth outlet;
a descaled water component outlet stream in communication with the third outlet, the descaled water component including less than about 5% weight percent total dissolved solids;
a dewatered solvent component outlet stream in communication with the fourth outlet;
a temperature controller in communication with the one or more extractors and the water-in-solvent extract outlet stream; and
a dewatered solvent recycle conduit in fluid communication with the dewatered solvent component outlet stream and the one or more extractors, the dewatered solvent recycle conduit configured to direct the dewatered solvent component outlet stream to the extractor
wherein the one or more solvents include diisopropylamine (DIPA), N-ethylcyclohexylamine (ECHA), and N,N-dimethyl cyclohexylamine (DMCHA), triethylamine (TEA), N-methylcyclohexylamine (nMCHA), N,N-dimethylisopropylamine (DMIPA), or combinations thereof.
18 . (canceled)
19 . (canceled)
20 . (canceled)
21 . The method according to claim 13 , wherein the steps of
bringing a previous water-in-solvent component produced via a previous separation step to at least one new temperature T N to produce a biphasic mixture of a subsequent water-in-solvent component and a subsequent raffinate component at temperature T N , and
separating the subsequent water-in-solvent component from the subsequent raffinate component,
is repeated 2 or more times.
22 . The method according to claim 21 , wherein the temperature swing from T 1 to T F is a continuous temperature gradient.
23 . The method according to claim 13 , wherein T 1 is below about 20° C.
24 . The method according to claim 23 , wherein T 1 is about 16° C.
25 . The method according to claim 13 , wherein T F is between about 40° C. and about 80° C.
26 . The method according to claim 25 , wherein T F is about 70° C.
27 . The method according to claim 13 , wherein the solvent includes diisopropylamine (DIPA), N-ethylcyclohexylamine (ECHA), and N,N-dimethylcyclohexylamine (DMCHA), triethylamine (TEA), N-methylcyclohexylamine (nMCHA), N,N-dimethylisopropylamine (DMIPA), or combinations thereof.
28 . The system according to claim 17 , wherein a first extractor is maintained at a temperature T L and the water-in-solvent extract outlet stream is heated to a temperature T H , wherein T L is below about 20° C. and T H is between about 40° C. and about 80° C.
29 . The system according to claim 28 , further comprising at least a second extractor in fluid communication with the first extractor via water-in-solvent extract outlet stream, wherein at least a second extractor is maintained at an intermediate temperature between T L and T H and the water-in-solvent extract outlet stream is heated to the intermediate temperature.