Patent Grant
10301198
Systems and methods in which solubilized multivalent ions are selectively retained in an aqueous stream are generally described.
Selective retention of solubilized multivalent ions in aqueous streams is generally described. Certain embodiments are related to inventive arrangements of separation membranes, which can lead to enhancements in efficiency. For example, in some embodiments, one or more osmotic membrane separators can be used to at least partially separate water from solubilized monovalent ions and/or solubilized multivalent ions. The subject matter of the present invention involves, in some cases, interrelated products, alternative solutions to a particular problem, and/or a plurality of different uses of one or more systems and/or articles.
According to certain embodiments, a method is provided. The method comprises, in some embodiments, transporting an aqueous feed stream containing solubilized monovalent ions and solubilized multivalent ions between an ion-selective membrane and an osmotic membrane, such that: the aqueous feed stream is transported across a first side of the ion-selective membrane and across a first side of the osmotic membrane; and at least a portion of the solubilized monovalent ions and the water from the aqueous feed stream is transported from the first side of the ion-selective membrane, through the ion-selective membrane, to a second side of the ion-selective membrane; and transporting at least a portion of the water from the second side of the ion-selective membrane to a second side of the osmotic membrane, such that at least a portion of the water from the second side of the osmotic membrane is transported from the second side of the osmotic membrane, through the osmotic membrane, to the first side of the osmotic membrane.
In some embodiments, the method comprises transporting an aqueous feed stream containing solubilized monovalent ions and solubilized multivalent ions into an ion-selective separator to produce a monovalent-ion-enriched stream containing at least about 75% of the solubilized monovalent ions from the aqueous feed stream and a multivalent-ion-enriched stream containing at least about 75% of the solubilized multivalent ions from the aqueous feed stream; transporting at least a portion of the monovalent-ion-enriched stream across a first side of an osmotic membrane and at least a portion of the multivalent-ion-enriched stream across a second side of the osmotic membrane such that at least a portion of the water in the monovalent-ion-enriched stream is transported through the osmotic membrane and into the multivalent-ion-enriched stream.
The method comprises, in some embodiments, exposing an ion-selective membrane to an aqueous feed stream containing solubilized monovalent ions and solubilized multivalent ions to produce a monovalent-ion-enriched stream containing water and at least about 75% of the solubilized monovalent ions from the aqueous feed stream; transporting at least a portion of the water from the monovalent-ion-enriched stream from a first side of an osmotic membrane, through the osmotic membrane, and to a second side of the osmotic membrane; and combining the portion of the water transported through the osmotic membrane with a stream on the second side of the osmotic membrane, wherein the stream on the second side of the osmotic membrane comprises at least a portion of the solubilized multivalent ions from the aqueous feed stream.
In some embodiments, a system is provided. The system comprises, in certain embodiments, a housing; an ion-selective membrane positioned at least partially within the housing, the ion-selective membrane having a first side and a second side; an osmotic membrane positioned at least partially within the housing, the osmotic membrane having a first side facing the first side of the ion-selective membrane, and a second side, wherein at least a portion of the first side of the ion-selective membrane and at least a portion of the first side of the osmotic membrane define a flow pathway between the ion-selective membrane and the osmotic membrane; and a conduit fluidically connecting the second side of the ion-selective membrane to the second side of the osmotic membrane.
In some embodiments, the system comprises an ion-selective separator configured to at least partially separate solubilized monovalent ions from solubilized multivalent ions, the ion-selective separator comprising an inlet, a first outlet configured to output a monovalent-ion-enriched stream, and a second outlet configured to output a multivalent-ion-enriched stream; and an osmotic membrane separator fluidically connected to the ion-selective separator, such that the first outlet of the ion-selective separator is fluidically connected to a first side of an osmotic membrane of the osmotic membrane separator, and the second outlet of the ion-selective separator is fluidically connected to a second side of the osmotic membrane of the osmotic membrane separator.
Other advantages and novel features of the present invention will become apparent from the following detailed description of various non-limiting embodiments of the invention when considered in conjunction with the accompanying figures. In cases where the present specification and a document incorporated by reference include conflicting and/or inconsistent disclosure, the present specification shall control.
Non-limiting embodiments of the present invention will be described by way of example with reference to the accompanying figures, which are schematic and are not intended to be drawn to scale. In the figures, each identical or nearly identical component illustrated is typically represented by a single numeral. For purposes of clarity, not every component is labeled in every figure, nor is every component of each embodiment of the invention shown where illustration is not necessary to allow those of ordinary skill in the art to understand the invention. In the figures:
Disclosed herein are systems and methods in which multivalent ions are selectively retained in an aqueous stream. According to certain embodiments, multiple separations may be used to process an aqueous feed stream containing solubilized monovalent ions and solubilized multivalent ions to produce a stream enriched in the solubilized multivalent ions. The separations may be arranged, according to certain embodiments, to enhance the overall separation process such that the product stream contains—relative to the initial aqueous feed stream—a high amount of solubilized multivalent ions, a high amount of water from the aqueous feed stream, and/or a high ratio of solubilized multivalent ions to solubilized monovalent ions.
Some embodiments are related to inventive arrangements of separation membranes. For example, according to certain embodiments, multiple separation membranes are arranged in a single housing. The membranes may be spaced apart from each other such that an aqueous stream comprising both solubilized monovalent ions and solubilized multivalent ions is transported between the membranes. According to certain embodiments, the membranes may be arranged, and the flow rates of certain streams may be configured, such that water and solubilized monovalent ions are transported out of the aqueous feed stream through the first membrane (while the transport of solubilized multivalent ions is restricted) and such that water is transported back into the aqueous feed stream through the second membrane (while the transport of solubilized monovalent ions back into the aqueous feed stream is restricted). Such arrangements can, in some instances, increase the efficiency with which the multivalent-ion enriched stream is produced. For example, in some cases, such arrangements can allow for the production of aqueous streams enriched in solubilized multivalent ions using relatively compact equipment and/or using relatively low amounts of energy.
Certain embodiments are related to inventive systems and methods for performing multiple membrane-based separation steps in an efficient manner. In some such embodiments, an ion-selective membrane can be used to produce a monovalent-ion-enriched stream (containing water and solubilized monovalent ions) from an aqueous feed stream containing solubilized monovalent ions and solubilized multivalent ions. In some such embodiments, at least a portion of the water from the monovalent-ion-enriched stream can be transported through an osmotic membrane to a stream on the permeate side of the osmotic membrane. The stream on the permeate side of the osmotic membrane can contain at least a portion of the multivalent ions from the aqueous feed stream. By performing the ion-selective separation and osmotic separation steps in this manner, according to certain embodiments, the amount of energy needed to achieve a given level of multivalent ion purity can be reduced.
Certain embodiments are related to systems for producing aqueous streams that are enriched in solubilized multivalent ions from an aqueous feed stream comprising a mixture of the solubilized multivalent ions and solubilized monovalent ions. Some embodiments are related to systems in which an ion-selective membrane and an osmotic membrane are spatially arranged and integrated with a housing to efficiently produce a multivalent-ion enriched stream from an aqueous feed stream comprising a combination of solubilized monovalent ions and solubilized multivalent ions. According to some embodiments, the system comprises a housing, an ion-selective membrane positioned at least partially within the housing, and an osmotic membrane positioned at least partially within the housing. One exemplary system is illustrated in
According to certain embodiments, the ion-selective membrane and the osmotic membrane can be positioned relative to each other such that they spatially define a flow pathway between them. For example, the ion-selective membrane can have a first side, and the osmotic membrane can have a first side facing the first side of the ion-selective membrane. Referring to
While ion-selective membrane 120 and osmotic membrane 130 are illustrated as being parallel and planar in
Suitable separation between the ion-selective membrane and the osmotic membrane (which can allow for a suitable flow pathway to be formed between the two) can be maintained via a variety of suitable methods. For example, in some embodiments, spacers can be arranged between the membranes to prevent facial contact between the first side of the ion-selective membrane and the first side of the osmotic membrane, at least in a sufficient number of regions to allow for flow of fluid between the first side of the ion-selective membrane and the first side of the osmotic membrane.
According to certain embodiments, the facial surface of the first side of the ion-selective membrane and the facial surface of the first side of the osmotic membrane can be spaced relatively close together. For example, in some embodiments, the shortest distance between the facial surface the first side of the ion-selective membrane and the facial surface of the first side of the osmotic membrane is less than about 1 cm, less than about 5 mm, less than about 1.5 mm, or less than about 1 mm. In some embodiments, the average distance between the facial surface the first side of the ion-selective membrane and the facial surface of the first side of the osmotic membrane is less than about 1 cm, less than about 5 mm, less than about 1.5 mm, or less than about 1 mm.
A variety of types of ion-selective membranes may be used, according to certain embodiments. Generally, the ion-selective membrane is chosen such that it may transmit solubilized monovalent ions while inhibiting (or completely preventing) the transmission of solubilized multivalent ions. For example, in
A variety of types of osmotic membranes may also be used, according to certain embodiments. Those of ordinary skill in the art are familiar with osmotic membranes. Generally, osmotic membranes selectively transmit water while inhibiting (or completely preventing) the transmission of ions (including both solubilized monovalent ions and solubilized multivalent ions) through the membrane. For example, in
According to certain embodiments, the system comprises a conduit fluidically connecting the second side of the ion-selective membrane to the second side of the osmotic membrane. For example, in
In some embodiments, the ion-selective membrane can be configured such that a stream (e.g., the aqueous feed stream) can be transported across the facial area of the first side of the ion-selective membrane. Such transport may be useful, for example, when the ion-selective membrane is operated as a cross-flow separator. The ion-selective membrane could also be operated, for example, as a co-flow or a counter-flow separator. For example, in some embodiments, another stream (e.g., a portion of aqueous feed stream 160 and/or another stream) could be transported across second side 124 of ion-selective membrane 120, either in a co-flow or a counter-flow configuration relative to stream 136. Transportation of a stream across the facial area of the first side of the ion-selective membrane can be achieved, for example, by arranging an inlet and an outlet such that they span at least a portion of the facial area of the first side of the ion-selective membrane. In some such embodiments, when a fluid is transported from the inlet to the outlet, it is transported across at least a portion of the facial area of the first side of the ion-selective membrane. For example, in
Unless explicitly indicated otherwise, streams that are transported “across” a side of a membrane are transported along the facial area of the membrane, while streams that are transported “through” a membrane are transported through the thickness of the membrane. For example, referring to
According to certain embodiments, the osmotic membrane can be configured such that a stream (e.g., the aqueous feed stream) can be transported across the facial area of the first side of the osmotic membrane. Such transport may be useful, for example, when the osmotic membrane is operated as a co-flow or a counter-flow osmotic membrane separator. Transportation of a stream across the facial area of the first side of the osmotic membrane can be achieved, for example, by arranging an inlet and an outlet such that they span at least a portion of the facial area of the first side of the osmotic membrane. In some such embodiments, when a fluid is transported from the inlet to the outlet, it is transported across at least a portion of the facial area of the first side of the osmotic membrane. For example, in
In some embodiments, the osmotic membrane can be configured such that a stream can be transported across the facial area of the second side of the osmotic membrane. Such transport may be useful, for example, when the osmotic membrane is operated as a co-flow or a counter-flow osmotic membrane separator. Transportation of a stream across the facial area of the second side of the osmotic membrane can be achieved, for example, by arranging an inlet and an outlet such that they span at least a portion of the facial area of the second side of the osmotic membrane. In some such embodiments, when a fluid is transported from the inlet to the outlet, it is transported across at least a portion of the facial area of the second side of the osmotic membrane. For example, in
Certain embodiments are related to methods of operating a system comprising an ion-selective membrane and an osmotic membrane to produce an aqueous stream enriched in solubilized multivalent ions from an aqueous feed stream comprising a mixture of the solubilized multivalent ions and solubilized monovalent ions.
In certain embodiments, the method comprises transporting an aqueous feed stream containing solubilized monovalent ions and solubilized multivalent ions between the ion-selective membrane and the osmotic membrane. For example, referring to
The ion-selective membrane can be configured, according to certain embodiments, such that when the first side of the ion-selective membrane is exposed to the aqueous solution containing both solubilized monovalent ions and solubilized multivalent ions (and, optionally, a hydraulic pressure is applied to the solution on the first side), at least a portion (e.g., at least about 75%, at least about 85%, at least about 90%, at least about 95%, or at least about 99%, on a molar basis) of the solubilized monovalent ions from the aqueous feed stream are transported through the ion-selective membrane from the first side to a second side. In some such embodiments, at least a portion (e.g., at least about 75%, at least about 85%, at least about 90%, at least about 95%, or at least about 99%, on a molar basis) of the solubilized multivalent ions from the aqueous feed stream are prevented from being transported through the ion-selective membrane, and remain on the first side of the ion-selective membrane. Operation in this manner can result in the creation of a multivalent-ion-enriched stream (corresponding to the retentate of the ion-selective membrane) and a monovalent-ion-enriched stream (corresponding to the permeate of the ion-selective membrane).
Certain embodiments comprise transporting the aqueous feed stream containing the solubilized monovalent ions and the solubilized multivalent ions across the ion-selective membrane to at least partially separate the solubilized monovalent ions and the solubilized multivalent ions and to produce a monovalent-ion-enriched stream and a multivalent-ion-enriched stream. According to certain embodiments, operation of the system comprises transporting at least a portion of the solubilized monovalent ions and the water from the aqueous feed stream from the first side of the ion-selective membrane, through the ion-selective membrane, to a second side of the ion-selective membrane. Solubilized multivalent ions, on the other hand, can be selectively retained by the ion-selective membrane.
For example, referring to
As noted above, certain embodiments comprise using an osmotic membrane in combination with the ion-selective membrane. In some such embodiments, the osmotic membrane can be used to separate at least a portion of the solubilized monovalent ions and the water within the monovalent-ion-enriched stream. According to certain embodiments, at least a portion of the water from the monovalent-ion-enriched stream can be added back to the aqueous stream being transported between the ion-selective membrane and the osmotic membrane, which can produce a monovalent-ion-enriched stream with a relatively high amount of water, relative to the amount of water that would be present in the monovalent-ion-enriched stream were the osmotic water addition not included.
According to certain embodiments, water can be added back to the aqueous stream by transporting at least a portion of the monovalent-ion-enriched stream across the second side of the osmotic membrane. For example, certain embodiments comprise transporting at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 85 wt %, at least about 90 wt %, at least about 95 wt %, or at least about 99 wt %) of the water from the second side of the ion-selective membrane to a second side of the osmotic membrane. Some such embodiments comprise transporting at least a portion (e.g., at least about 10%, at least about 25%, at least about 50%, at least about 75%, at least about 85%, at least about 90%, at least about 95%, or at least about 99%, on a molar basis) of the solubilized monovalent ions from the second side of the ion-selective membrane to a second side of the osmotic membrane (e.g., along with the portion of the water that is transported to the second side of the osmotic membrane). Referring to
In certain embodiments, the housing comprises an outlet on the second side of the ion-selective membrane and an inlet on the second side of the osmotic membrane. A fluidic connection can be established between the outlet on the second side of the ion-selective membrane and the inlet on the second side of the osmotic membrane, for example, via a conduit. Referring to
According to certain embodiments, water can be selectively transported through the osmotic membrane (from the second side of the osmotic membrane to the first side of the osmotic membrane), such that the aqueous stream being transported between the ion-selective membrane and the osmotic membrane is diluted while maintaining a suitable ratio of solubilized multivalent ions to solubilized monovalent ions. In some embodiments, at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 85 wt %, at least about 90 wt %, at least about 95 wt %, or at least about 99 wt %, or between about 10 wt % and about 99 wt %, or between about 10 wt % and about 90 wt %) of the water from the second side of the osmotic membrane is transported from the second side of the osmotic membrane, through the osmotic membrane, to the first side of the osmotic membrane. In
Selective transport of water (relative to solubilized species such as solubilized monovalent and/or solubilized multivalent ions) through an osmotic membrane can be achieved via a transmembrane net driving force (i.e., a net driving force through the thickness of the membrane), according to certain embodiments. Generally, the transmembrane net driving force (Δχ) is expressed as:
Δχ=ΔP−ΔΠ=(PR−PP)−(ΠR−ΠP) [1]
wherein PR is the hydraulic pressure on the retentate side of the osmotic membrane, PP is the hydraulic pressure on the permeate side of the osmotic membrane, ΠR is the osmotic pressure of the stream on the retentate side of the osmotic membrane, and ΠP is the osmotic pressure of the stream on the permeate side of the osmotic membrane. (PR−PP) can be referred to as the transmembrane hydraulic pressure gradient, and (ΠR−ΠP) can be referred to as the transmembrane osmotic pressure gradient.
Those of ordinary skill in the art are familiar with the concept of osmotic pressure. The osmotic pressure of a particular liquid is an intrinsic property of the liquid. The osmotic pressure can be determined in a number of ways, with the most efficient method depending upon the type of liquid being analyzed. For certain solutions with relatively low molar concentrations of ions, osmotic pressure can be accurately measured using an osmometer. In other cases, the osmotic pressure can simply be determined by comparison with solutions with known osmotic pressures. For example, to determine the osmotic pressure of an uncharacterized solution, one could apply a known amount of the uncharacterized solution on one side of a non-porous, semi-permeable, osmotic membrane and iteratively apply different solutions with known osmotic pressures on the other side of the osmotic membrane until the differential pressure through the thickness of the membrane is zero.
The osmotic pressure (Π) of a solution containing n solubilized species may be estimated as:
Π=Σj=1nijMjRT [2]
wherein ij is the van't Hoff factor of the jth solubilized species, Mj is the molar concentration of the jth solubilized species in the solution, R is the ideal gas constant, and T is the absolute temperature of the solution. Equation 2 generally provides an accurate estimate of osmotic pressure for liquid with low concentrations of solubilized species (e.g., concentrations at or below between about 4 wt % and about 6 wt %). For many liquid comprising solubilized species, at species concentrations above around 4-6 wt %, the increase in osmotic pressure per increase in salt concentration is greater than linear (e.g., slightly exponential).
The osmotic membrane can be used to perform, according to certain embodiments, a reverse osmosis process. Reverse osmosis generally occurs when the osmotic pressure on the retentate side of the osmotic membrane is greater than the osmotic pressure on the permeate side of the osmotic membrane, and a hydraulic pressure is applied to the retentate side of the osmotic membrane such that the hydraulic pressure on the retentate side of the osmotic membrane is sufficiently greater than the hydraulic pressure on the permeate side of the osmotic membrane to cause water to be transported from the retentate side of the osmotic membrane to the permeate side of the osmotic membrane. Generally, such situations result when the transmembrane hydraulic pressure gradient (PR−PP) is greater than the transmembrane osmotic pressure gradient (ΠR−ΠP) such that water is transported from the first side of the osmotic membrane to the second side of the osmotic membrane (rather than having water transported from the second side of the osmotic membrane to the first side of the osmotic membrane, which would be energetically favored in the absence of the pressure applied to the first side of the osmotic membrane). Operating the osmotic membrane to perform reverse osmosis can comprise applying a hydraulic pressure to the stream on the second side of the osmotic membrane, according to certain embodiments. Referring to
Arranging the system such that the monovalent-ion-enriched stream is positioned on one side of the osmotic membrane and the multivalent-ion-enriched stream is positioned on the other side of the osmotic membrane can, according to certain embodiments, enhance the efficiency with which water from the monovalent-ion-enriched stream is transported into the multivalent-ion-enriched stream via reverse osmosis, relative to the efficiency that could be achieved were water removed from the monovalent-ion-enriched stream in a standalone reverse osmosis process. In particular, according to certain embodiments, the presence of the multivalent ions on the side of the osmotic membrane opposite the monovalent-ion-enriched stream can reduce the amount of hydraulic pressure that needs to be applied to the monovalent-ion-enriched stream to achieve a desired level of separation.
In certain embodiments, the osmotic membrane can be used to perform forward osmosis. Forward osmosis generally occurs when the osmotic pressure on the permeate side of the osmotic membrane is greater than the osmotic pressure on the retentate side of the osmotic membrane such that water is transported from the retentate side of the osmotic membrane to the permeate side of the osmotic membrane. In forward osmosis systems, water generally is transported from the retentate side of the osmotic membrane to the permeate side of the osmotic membrane as long as the hydraulic pressure difference between the permeate side of the osmotic membrane and the retentate side of the osmotic membrane is not sufficiently high to overcome the osmotic pressure difference between the retentate and permeate sides of the osmotic membrane. In this way, the permeate flow and the osmotic driving force are aligned in the same direction. In certain forward osmosis arrangements, the stream on the permeate side of the osmotic membrane can initiate the transport of water from the stream on the retentate side of the osmotic membrane and through the osmotic membrane from the retentate side to the permeate side. Referring to
In some cases, hydraulic pressure may be applied to the retentate side of the osmotic membrane to enhance the forward osmosis process. For example, in some instances in which the stream on the retentate side of the osmotic membrane has a lower osmotic pressure than the stream on the permeate side of the osmotic membrane, a hydraulic pressure may be applied to the retentate side of the osmotic membrane such that the hydraulic pressure of the stream on the retentate side of the osmotic membrane is higher than the hydraulic pressure of the stream on the permeate side of the osmotic membrane. The applied pressure can increase the rate at which water is transported from the retentate side of the osmotic membrane to the permeate side of the osmotic membrane. Such arrangements are sometimes referred to herein as pressure-assisted forward osmosis (which is a particular type of forward osmosis). Referring to
Generally, whether the osmotic membrane is used to perform reverse osmosis or forward osmosis is determined by the osmotic pressures of the streams on either side of the osmotic membrane. For example, referring to
According to certain embodiments, transporting at least a portion of the water in the monovalent-ion-enriched stream through the osmotic membrane and into the aqueous feed stream produces a multivalent-ion-enriched product stream. For example, referring to
In some embodiments, a relatively large percentage of the solubilized multivalent ions from the aqueous feed stream is present in the multivalent-ion-enriched product stream. For example, in some embodiments, the multivalent-ion-enriched product stream contains at least about 75% (or at least about 85%, at least about 90%, at least about 95%, or at least about 99%, on a molar basis) of the solubilized multivalent ions from the aqueous feed stream. For example, in
Transporting at least a portion of the water in the monovalent-ion-enriched stream through the osmotic membrane and into the aqueous feed stream can also produce a monovalent-ion-enriched product stream, according to certain embodiments. For example, referring to
In some embodiments, the amount of solubilized monovalent ions within the monovalent-ion-enriched product stream is relatively high. In some embodiments, the monovalent-ion-enriched product stream contains at least about 75% (or at least about 85%, at least about 90%, at least about 95%, or at least about 99%, on a molar basis) of the solubilized monovalent ions from the aqueous feed stream. For example, in
According to certain embodiments, the multivalent-ion-enriched product stream can contain a relatively high amount of solubilized multivalent ions and a relatively low amount of solubilized monovalent ions. For example, in some embodiments, the ratio of solubilized multivalent ions within multivalent-ion-enriched product stream to solubilized monovalent ions within the multivalent-ion-enriched product stream is at least about 3:1, at least about 5:1, at least about 10:1, at least about 50:1, at least about 100:1, at least about 1000:1, at least about 10,000:1, or more. For example, in
In some embodiments, the ratio of solubilized multivalent ions within multivalent-ion-enriched product stream to solubilized multivalent ions within the monovalent-ion-enriched product stream is at least about 3:1, at least about 5:1, at least about 10:1, at least about 50:1, at least about 100:1, at least about 1000:1, at least about 10,000:1, or more. For example, in
According to certain embodiments, the monovalent-ion-enriched product stream can contain a relatively high amount of solubilized monovalent ions and a relatively low amount of solubilized multivalent ions. For example, in some embodiments, the ratio of solubilized monovalent ions within monovalent-ion-enriched product stream to solubilized multivalent ions within the monovalent-ion-enriched product stream is at least about 3:1, at least about 5:1, at least about 10:1, at least about 50:1, at least about 100:1, at least about 1000:1, at least about 10,000:1, or more. For example, in
In some embodiments, the ratio of solubilized monovalent ions within the monovalent-ion-enriched product stream to solubilized monovalent ions within the multivalent-ion-enriched product stream is at least about 3:1, at least about 5:1, at least about 10:1, at least about 50:1, at least about 100:1, at least about 1000:1, at least about 10,000:1, or more. For example, in
In some embodiments, a relatively large percentage of the water from the aqueous feed stream is present in the multivalent-ion-enriched product stream. For example, in certain embodiments, the multivalent-ion-enriched product stream contains at least about 75 wt % (or at least about 85 wt %, at least about 90 wt %, at least about 95 wt %, or at least about 99 wt %) of the water from the aqueous feed stream. For example, in
While embodiments have been described in which ion-selective separation and subsequent osmotic separation are performed using an integrated device, the ion-selective separation and osmotic separation can performed using different separators, according to certain embodiments.
In certain embodiments, the system comprises an ion-selective separator configured to at least partially separate solubilized monovalent ions from solubilized multivalent ions. For example, referring to
According to certain embodiments, the ion-selective separator comprises a first outlet configured to output a monovalent-ion-enriched stream and a second outlet configured to output a multivalent-ion-enriched stream. Referring to
According to certain embodiments, operation of the ion-selective separator comprises transporting an aqueous feed stream containing solubilized monovalent ions and solubilized multivalent ions into the ion-selective separator to at least partially separate the solubilized monovalent ions and the solubilized multivalent ions and to produce a monovalent-ion-enriched stream and a multivalent-ion-enriched stream. For example, referring to
The ion-selective separator can comprise any suitable separation apparatus capable of at least partially separating solubilized monovalent ions and solubilized multivalent ions.
According to certain embodiments, the ion-selective separator is an ion-selective membrane separator. The ion-selective membrane separator can comprise an ion-selective membrane. Examples of suitable ion-selective membranes include, for example, the ion-selective membranes described elsewhere herein with respect to
The ion-selective membrane can be configured, according to certain embodiments, such that when a first side of the membrane is exposed to an aqueous solution containing both solubilized monovalent ions and solubilized multivalent ions (and, optionally, a hydraulic pressure is applied to the solution on the first side), at least a portion (e.g., at least about 75%, at least about 85%, at least about 90%, at least about 95%, or at least about 99%, on a molar basis) of the solubilized monovalent ions from the aqueous feed stream are transported through the ion-selective membrane from the first side to a second side. In some such embodiments, at least a portion (e.g., at least about 75%, at least about 85%, at least about 90%, at least about 95%, or at least about 99%, on a molar basis) of the solubilized multivalent ions from the aqueous feed stream are prevented from being transported through the ion-selective membrane, and remain on the first side of the ion-selective membrane. Operation in this manner can result in the creation of a multivalent-ion-enriched stream (corresponding to the retentate of the ion-selective membrane separator) and a monovalent-ion-enriched stream (corresponding to the permeate of the ion-selective membrane separator).
A variety of ion-selective membranes can be used in the ion-selective membrane separator. Examples of such separators include, but are not limited to, those described above with respect to
While the use of ion-selective membrane separators may provide advantages according to certain, but not necessarily all, embodiments, the invention is not limited to the use of such separators, and in other embodiments, other ion-selective separators can be used. For example, in some embodiments, the ion-selective separator comprises an electrodialysis separator. Operation of the electrodialysis separator generally involves the transportation of salt ions from one solution through ion-exchange membranes to another solution under the influence of an applied electric potential difference. In certain embodiments, solubilized monovalent ions and solubilized multivalent ions can be transported at different rates, allowing for at least partially separation of the solubilized monovalent ions and the solubilized multivalent ions. An example of a commercially available electrodialysis separator that can be used, according to certain embodiments, is a 2020EDR system, manufactured by GE.
In some embodiments, the system comprises an osmotic membrane separator fluidically connected to the ion-selective separator. For example, in
In some such embodiments, an ion-selective separator and an osmotic membrane separator are fluidically connected such that the first outlet of the ion-selective separator is fluidically connected to a first side of the osmotic membrane of the osmotic membrane separator, and the second outlet of the ion-selective separator is fluidically connected to the second side of the osmotic membrane of the osmotic membrane separator. For example, referring to
In some embodiments, the first outlet of the ion-selective separator is directly fluidically connected to a first side of the osmotic membrane of the osmotic membrane separator. In certain embodiments, the second outlet of the ion-selective separator is directly fluidically connected to the second side of the osmotic membrane of the osmotic membrane separator. For example, in
In certain embodiments in which the ion-selective separator comprises an ion-selective membrane separator, the first side of the ion-selective membrane (which can be the retentate side) can be fluidically connected to the second side of the osmotic membrane separator (which can be the permeate side). For example, in
In some embodiments in which the ion-selective separator comprises an ion-selective membrane separator, the second side of the ion-selective membrane separator (which can be the permeate side) can be fluidically connected to the first side of the osmotic membrane separator (which can be the retentate side). For example, in
Certain embodiments comprise transporting at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the monovalent-ion-enriched stream across a first side of the osmotic membrane of the osmotic membrane separator and transporting at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the multivalent-ion-enriched stream across a second side of the osmotic membrane of the osmotic membrane separator. For example, referring to
Certain embodiments comprise transporting at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the multivalent-ion-enriched stream across a second side of the osmotic membrane of the osmotic membrane separator such that at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, or more) of the water from the monovalent-ion-enriched stream is transported through the osmotic membrane and into the multivalent-ion-enriched stream. For example, in
Arranging the system such that the monovalent-ion-enriched stream is positioned on one side of the osmotic membrane and the multivalent-ion-enriched stream is positioned on the other side of the osmotic membrane can, according to certain embodiments, enhance the efficiency with which water from the monovalent-ion-enriched stream is transported into the multivalent-ion-enriched stream, relative to the efficiency that could be achieved were water removed from the monovalent-ion-enriched stream in a standalone osmosis process. In particular, according to certain embodiments, the presence of the multivalent ions on the side of the osmotic membrane opposite the monovalent-ion-enriched stream can reduce the amount of hydraulic pressure that needs to be applied to the monovalent-ion-enriched stream to achieve a desired level of separation.
According to certain embodiments, less than about 5% (or, in some embodiments, less than about 2%, less than about 1%, or less than about 0.1%, on a molar basis) of the solubilized monovalent ions within the monovalent-ion-enriched stream are transported through the osmotic membrane during operation of the osmotic membrane separator. For example, referring to
As noted above, the osmotic membrane separator comprises an osmotic membrane, according to certain embodiments.
The osmotic membrane separator (e.g., osmotic membrane separator 245 in
In certain embodiments, the osmotic membrane separator can be used to perform forward osmosis. As noted above, forward osmosis generally occurs when the osmotic pressure on the permeate side of the osmotic membrane is greater than the osmotic pressure on the retentate side of the osmotic membrane such that water is transported from the retentate side of the osmotic membrane to the permeate side of the osmotic membrane. Referring to
In some cases, hydraulic pressure may be applied to the retentate side of the osmotic membrane separator to enhance the forward osmosis process. For example, in some instances in which the stream on the first side of the osmotic membrane has a lower osmotic pressure than the stream on the second side of the osmotic membrane, a hydraulic pressure may be applied to the first side of the osmotic membrane such that the hydraulic pressure of the stream on the first side of the osmotic membrane is higher than the hydraulic pressure of the stream on the second side of the osmotic membrane. The applied pressure can increase the rate at which water is transported from the first side of the osmotic membrane to the second side of the osmotic membrane. Such arrangements are sometimes referred to herein as pressure-assisted forward osmosis (which is a particular type of forward osmosis). Referring to
Generally, whether the osmotic membrane separator is used to perform reverse osmosis or forward osmosis is determined by the osmotic pressures of these streams on either side of the osmotic membrane of the osmotic membrane separator. For example, referring to
This osmosis process (e.g., reverse osmosis and/or forward osmosis, and involving the osmotic membrane separator (e.g., separator 245) and/or one or more intermediate osmotic membrane separators) can result, according to certain embodiments, in the production of a monovalent-ion-enriched product stream. The monovalent-ion-enriched product stream can have, according to certain embodiments, a higher osmotic pressure than the monovalent-ion-enriched stream exiting the ion-selective separator (e.g., the ion-selective membrane separator). For example, referring to
The osmosis process can also result in the production of a multivalent-ion-enriched product stream having a lower osmotic pressure than the multivalent-ion-enriched stream exiting the ion-selective separator (and/or having a lower osmotic pressure than the multivalent-ion-enriched stream fed to the osmotic membrane separator). For example, in
Certain embodiments comprise applying a hydraulic pressure to the stream on the first side of the osmotic membrane (e.g., the monovalent-ion-enriched stream in
According to certain embodiments, less than about 5% (or, in some embodiments, less than about 2%, less than about 1%, or less than about 0.1%, on a molar basis) of the solubilized monovalent ions within the monovalent-ion-enriched stream are transported through an osmotic membrane during the osmosis process. For example, referring to
According to certain embodiments, transporting at least a portion of the water in the monovalent-ion-enriched stream through the osmotic membrane and into the multivalent-ion-enriched stream produces a multivalent-ion-enriched product stream. For example, referring to
In some embodiments, a relatively large percentage of the solubilized multivalent ions from the aqueous feed stream is present in the multivalent-ion-enriched product stream. For example, in some embodiments, the multivalent-ion-enriched product stream contains at least about 75% (or at least about 85%, at least about 90%, at least about 95%, or at least about 99%, on a molar basis) of the solubilized multivalent ions from the aqueous feed stream. For example, in
Transporting at least a portion of the water in the monovalent-ion-enriched stream through the osmotic membrane and into the multivalent-ion-enriched stream can also produce a monovalent-ion-enriched product stream. For example, referring to
In some embodiments, the amount of solubilized monovalent ions within the monovalent-ion-enriched product stream is relatively high. For example, in some embodiments, the monovalent-ion-enriched product stream contains at least about 75% (or at least about 85%, at least about 90%, at least about 95%, or at least about 99%, on a molar basis) of the monovalent ions from the aqueous feed stream. For example, in
According to certain embodiments, the multivalent-ion-enriched product stream can contain a relatively high amount of solubilized multivalent ions and a relatively low amount of solubilized monovalent ions. For example, in some embodiments, the ratio of solubilized multivalent ions within multivalent-ion-enriched product stream to solubilized monovalent ions within the multivalent-ion-enriched product stream is at least about 3:1, at least about 5:1, at least about 10:1, at least about 50:1, at least about 100:1, at least about 1000:1, at least about 10,000:1, or more. For example, in
According to certain embodiments, the ratio of solubilized multivalent ions within multivalent-ion-enriched product stream to multivalent ions within the monovalent-ion-enriched product stream is at least about 3:1, at least about 5:1, at least about 10:1, at least about 50:1, at least about 100:1, at least about 1000:1, at least about 10,000:1, or more. For example, in
In certain embodiments, the total concentration of solubilized multivalent ions in the multivalent-ion-enriched product stream is at least about 60,000 ppm, at least about 80,000 ppm, or at least about 100,000 ppm (and/or, in some embodiments, up to about 500,000 ppm, or more). Multivalent-ion-enriched product streams with solubilized multivalent ion concentrations outside these ranges could also be produced. For example, in some embodiments, the total concentration of solubilized multivalent ions in the multivalent-ion-enriched product stream is as little as 10,000 ppm, 1000 ppm, 100 ppm, or less.
According to certain embodiments, the monovalent-ion-enriched product stream can contain a relatively high amount of solubilized monovalent ions and a relatively low amount of solubilized multivalent ions. For example, in some embodiments, the ratio of solubilized monovalent ions within monovalent-ion-enriched product stream to solubilized multivalent ions within the monovalent-ion-enriched product stream is at least about 3:1, at least about 5:1, at least about 10:1, at least about 50:1, at least about 100:1, at least about 1000:1, at least about 10,000:1, or more. For example, in
In certain embodiments, the total concentration of solubilized monovalent ions in the monovalent-ion-enriched product stream is at least about 60,000 ppm, at least about 80,000 ppm, or at least about 100,000 ppm (and/or, in some embodiments, up to about 500,000 ppm, or more). Monovalent-ion-enriched product streams with solubilized monovalent ion concentrations outside these ranges could also be produced. For example, in some embodiments, the total concentration of solubilized monovalent ions in the monovalent-ion-enriched product stream is as little as 10,000 ppm, 1000 ppm, 100 ppm, or less.
In some embodiments, the ratio of monovalent ions within the monovalent-ion-enriched product stream to solubilized monovalent ions within the multivalent-ion-enriched product stream is at least about 3:1, at least about 5:1, at least about 10:1, at least about 50:1, at least about 100:1, at least about 1000:1, at least about 10,000:1, or more. For example, in
In some embodiments, a relatively large percentage of the water from the aqueous feed stream is present in the multivalent-ion-enriched product stream. For example, in certain embodiments, multivalent-ion-enriched product stream contains at least about 75 wt % (or at least about 85 wt %, at least about 90 wt %, at least about 95 wt %, or at least about 99 wt %) of the water from the aqueous feed stream. For example, in
According to certain embodiments, the system comprises multiple osmotic membrane separators. The osmotic membrane separators can be arranged, according to certain embodiments, in series. The series-connected osmotic membrane separators may be arranged, according to certain embodiments, such that water and solubilized monovalent ions are separated via a plurality of successive osmotic separation steps. The use of successive separation steps can be advantageous, for example, when the concentration of solubilized monovalent ions within the monovalent-ion-enriched stream is relatively high and reverse osmosis is being used to separate water and solubilized monovalent ions. In some such cases, the use of multiple osmotic membranes can reduce the minimum amount of hydraulic pressure that needs to be applied to the membranes, resulting in more efficient overall separation. One example of a system including an intermediate osmotic membrane separator is shown in
Accordingly, while
According to certain embodiments, transporting at least a portion of the water from the monovalent-ion-enriched stream across the first (retentate) side of the osmotic membrane (and, subsequently, into at least a portion of the multivalent-ion-enriched stream) comprises transporting at least a portion of water from the monovalent-ion-enriched stream through at least one intermediate osmotic membrane separator. Examples of such processes are shown in
Accordingly, in certain embodiments, at least a portion of the monovalent-ion-enriched stream is transported to at least one intermediate osmotic membrane separator before a portion of the monovalent-ion-enriched stream is transported to the osmotic membrane separator to which a portion of the multivalent-ion-enriched stream is transported. Certain embodiments comprise transporting at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the monovalent-ion-enriched stream across a first side of the osmotic membrane of an intermediate osmotic membrane separator. For example, in
Certain embodiments comprise transporting at least a portion of a draw inlet stream across the second side of the osmotic membrane of the intermediate osmotic separator. For example, in
Certain embodiments comprise applying a hydraulic pressure to the first side of the osmotic membrane of the intermediate osmotic membrane separator such that water is transported from the first side of the intermediate osmotic separator (from the monovalent-ion-enriched stream) to the second side of the intermediate osmotic membrane separator. For example, in
Certain embodiments comprise transporting at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the draw product stream (which itself, as described above, may contain at least a portion of the monovalent-ion-enriched stream, such as at least a portion of the water from the monovalent-ion-enriched stream) across a first side of the osmotic membrane of an osmotic membrane separator and transporting at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the multivalent-ion-enriched stream across a second side of the osmotic membrane of the osmotic membrane separator. For example, referring to
In some embodiments, all or a portion of the draw product stream can be transported directly to the first side of the osmotic membrane of the osmotic membrane separator. For example, in
According to certain embodiments, at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the water in the draw product stream is transported across a first side of the osmotic membrane of the osmotic membrane separator. For example, in
In some such embodiments, at least a portion (e.g., at least about 10%, at least about 25%, at least about 50%, at least about 75%, at least about 90%, at least about 95%, at least about 98%, or more, on a molar basis) of a solubilized species (e.g., an ion or non-ion solubilized species) within the draw product stream is transported across a first side of the osmotic membrane of the osmotic membrane separator. For example, in
Certain embodiments comprise transporting at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the multivalent-ion-enriched stream across a second side of the osmotic membrane of the osmotic membrane separator such that at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, or more) of the water from the draw product stream is transported through the osmotic membrane and into the multivalent-ion-enriched stream. For example, in
In some embodiments, operation of the osmotic membrane separator within which water is added to the multivalent-ion-enriched stream generates a stream exiting the first side of the osmotic membrane and having a higher osmotic pressure than the stream fed to the first side of the osmotic membrane. For example, referring to
According to certain embodiments, less than about 5% (or, in some embodiments, less than about 2%, less than about 1%, or less than about 0.1%, on a molar basis) of the solubilized species within a draw product stream are transported through the osmotic membrane during operation of the osmotic membrane separator used to add water to the multivalent-ion-enriched stream. For example, referring to
The intermediate osmotic membrane separator can be operated as a reverse osmosis membrane separator, according to certain embodiments. That is to say, in some embodiments, water can be transported from the first side of the osmotic membrane of the intermediate osmotic membrane separator to the second side of the osmotic membrane of the intermediate osmotic membrane separator by applying a hydraulic pressure to the first side of the membrane as a driving force, such that local osmotic pressure gradients through the thickness of the membrane that would otherwise favor the transport of water from the second side of the membrane to the first side of the membrane are overcome by the applied hydraulic pressure. In some embodiments, the osmotic pressure of the stream on the first side of the osmotic membrane of the intermediate osmotic membrane separator can be higher than the osmotic pressure of the stream on the second side of the osmotic membrane of the intermediate osmotic membrane separator, such that water is transported through the osmotic membrane due to a hydraulic pressure applied to the first side of the osmotic membrane.
In certain embodiments, two or more intermediate osmotic membrane separators can be used in the system. In certain embodiments, at least a portion of the draw product stream from the first intermediate osmotic membrane separator (e.g., intermediate osmotic membrane separator 410 in
Certain embodiments comprise transporting at least a portion of a second draw inlet stream across the second side of the osmotic membrane of the second intermediate osmotic membrane separator. For example, in
The second draw inlet stream can include solubilized species (e.g., solubilized ion species) that are the same as or different from those present in the first draw inlet stream. In certain embodiments, the osmotic pressure of the first draw inlet stream can be higher than the osmotic pressure of the second draw inlet stream. For example, in some embodiments, the first draw inlet stream (e.g., stream 418) can have an osmotic pressure that is at least about 1.01 times, at least about 1.1 times, at least about 1.5 times, at least about 2 times, or at least about 5 times (and/or, in some embodiments, up to about 10 times, up to about 100 times, up to about 500 times, up to about 1000 times, up to about 5000 times, or more) the osmotic pressure of the second draw inlet stream (e.g., stream 428). In some embodiments, the total molar concentration (in units of molarity) of solubilized species (e.g., solubilized ions) in the second draw inlet stream is lower than the total molar concentration of solubilized species (e.g., solubilized ions) in the first draw inlet stream.
Certain embodiments comprise transporting at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the second draw product stream (which itself, as described above, may contain at least a portion of the first draw product stream and at least a portion of the monovalent-ion-enriched stream, such as at least a portion of the water from the first draw product stream and/or the monovalent-ion-enriched stream) across a first side of the osmotic membrane of an osmotic membrane separator and transporting at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the multivalent-ion-enriched stream across a second side of the osmotic membrane of the osmotic membrane separator. For example, referring to
In some embodiments, all or a portion of the second draw product stream can be transported directly to the first side of the osmotic membrane of the osmotic membrane separator. For example, in
According to certain embodiments, at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the water in the second draw product stream is transported across a first side of the osmotic membrane of the osmotic membrane separator. For example, in
In some such embodiments, at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50%, at least about 75%, at least about 90%, at least about 95%, at least about 98%, or more, on a molar basis) of a solubilized species (e.g., an ion or non-ion solubilized species) within the second draw product stream is transported across a first side of the osmotic membrane of the osmotic membrane separator. For example, in
Certain embodiments comprise transporting at least a portion (e.g., at least about 10 wt %, at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 98 wt %, or more) of the multivalent-ion-enriched stream across a second side of the osmotic membrane of the osmotic membrane separator such that at least a portion (e.g., at least about 25 wt %, at least about 50 wt %, at least about 75 wt %, or more) of the water from the second draw product stream is transported through the osmotic membrane and into the multivalent-ion-enriched stream. For example, in
In some embodiments, operation of the osmotic membrane separator within which water is added to the multivalent-ion-enriched stream generates a stream exiting the first side of the osmotic membrane and having a higher osmotic pressure than the stream fed to the first side of the osmotic membrane. For example, referring to
According to certain embodiments, less than about 5% (or, in some embodiments, less than about 2%, less than about 1%, or less than about 0.1%, on a molar basis) of the solubilized species within a draw product stream are transported through the osmotic membrane during operation of the osmotic membrane separator used to add water to the multivalent-ion-enriched stream. For example, referring to
The second intermediate osmotic membrane separator can be operated as a reverse osmosis membrane separator, according to certain embodiments. That is to say, in some embodiments, water can be transported from the first side of the osmotic membrane of the second intermediate osmotic membrane separator to the second side of the osmotic membrane of the second intermediate osmotic membrane separator by applying a hydraulic pressure to the first side of the membrane as a driving force, such that local osmotic pressure gradients through the thickness of the membrane that would otherwise favor the transport of water from the second side of the membrane to the first side of the membrane are overcome by the applied hydraulic pressure. In some embodiments, the osmotic pressure of the stream on the first side of the osmotic membrane of the second intermediate osmotic membrane separator can be higher than the osmotic pressure of the stream on the second side of the osmotic membrane of the second intermediate osmotic membrane separator, such that water is transported through the osmotic membrane due to a hydraulic pressure applied to the first side of the osmotic membrane.
While embodiments with a single intermediate osmotic membrane separator and two intermediate osmotic membrane separators have been described, additional intermediate osmotic membrane separators can be used, according to certain embodiments.
According to certain embodiments, streams within the system can be recycled. For example, in certain embodiments, at least a portion of the product stream from the first side of the osmotic membrane separator is recycled to the second side of the first intermediate osmotic membrane separator. For example, in
One advantage of certain, although not necessarily all, embodiments is that one or more of the osmotic-membrane-based separation steps can be performed to achieve a desired degree of separation while using relatively low transmembrane osmotic pressure gradients. Such low transmembrane osmotic pressure gradients can be advantageous, for example, in certain cases in which reverse osmosis is used to perform separations, as relatively low transmembrane osmotic pressure gradients can allow one to perform separations using relatively low applied hydraulic pressures, thus potentially reducing energy requirements and/or equipment costs compared to higher hydraulic pressure applications. In some embodiments, at at least one location on the osmotic membrane of the osmotic membrane separator, the difference between an osmotic pressure on a first side of the first osmotic membrane and an osmotic pressure on a second side of the first osmotic membrane (i.e., opposite the first side of the first osmotic membrane) is less than about 45 bar, less than about 40 bar, less than about 35 bar, less than about 30 bar, less than about 25 bar, less than about 20 bar, or less (and/or, in some embodiments, at least about 1 bar, at least about 2 bar, at least about 5 bar, at least about 10 bar, or more).
For example, in
According to certain embodiments, the transmembrane osmotic pressure gradient spatially-averaged across the facial area of one or more of the osmotic membranes (e.g., such as osmotic membrane 130 in
Achieving a relatively low spatially-averaged transmembrane osmotic pressure gradient across a facial area of an osmotic membrane can be achieved, for example, by controlling the osmotic pressure of the streams fed to either side of the osmotic membrane (e.g., by controlling salt types and/or salt concentrations within the streams). According to certain embodiments, the difference between the osmotic pressure within the monovalent-ion-enriched stream fed to the first intermediate osmotic membrane separator and the osmotic pressure within the first draw product stream is less than about 45 bar, less than about 40 bar, less than about 35 bar, less than about 30 bar, less than about 25 bar, less than about 20 bar, or less (and/or, in some embodiments, at least about 1 bar, at least about 2 bar, at least about 5 bar, at least about 10 bar, or more). In certain embodiments, the difference between the osmotic pressure of the first draw product stream and the osmotic pressure of the second draw product stream is less than about 45 bar, less than about 40 bar, less than about 35 bar, less than about 30 bar, less than about 25 bar, less than about 20 bar, or less (and/or, in some embodiments, at least about 1 bar, at least about 2 bar, at least about 5 bar, at least about 10 bar, or more).
According to certain embodiments, the streams on either side of an osmotic membrane can be operated in counter-current configuration. Operation of the osmotic membrane separators in this manner can, according to certain but not necessarily all embodiments, allow for more efficient operation of the osmotic membrane separator. An example of counter-current flow is illustrated in
It should be understood that, where a single membrane is shown or described, such single membranes could be replaced with multiple, parallel-connected osmotic membranes. The use of multiple, parallel-connected osmotic membranes can, for example, increase the capacity of the system.
In some embodiments, at least a portion of the energy used to pressurize one or more streams (e.g., for performing reverse osmosis) is recovered from the system. The recovered energy may be used, for example, to heat and/or pressurize another stream within the desalination system. Certain embodiments comprise, for example, increasing the pressure of the aqueous feed stream, before the aqueous feed stream is transported into the ion-selective separator, using at least a portion of the pressure of at least one retentate product stream from an osmotic membrane separator.
Energy from a pressurized stream can be recovered via any suitable method. For example, in some embodiments, a pressure exchange device can be used to recover energy from a pressurized stream. Those of ordinary skill in the art are familiar with pressure exchange devices, in which pressure energy from a high pressure fluid stream is transferred to a low pressure fluid stream. An exemplary type of pressure exchange device is a rotary pressure exchanger, for example, as described in U.S. Pat. No. 7,306,437. For example, in some embodiments, energy (e.g., as direct hydraulic pressure) can be recovered by directly contacting a pressurized stream with a stream at a lower pressure, such that the lower pressure stream is pressurized and the higher pressure stream is depressurized (e.g., throttled). Energy can also be recovered in the system using other devices such as, for example, a turbine (e.g., a Pelton wheel).
As noted above, certain embodiments comprise reducing the pressure of at least one retentate product stream from an osmotic membrane separator. For example, some embodiments comprise, after transporting at least a portion of the monovalent-ion-enriched stream across an osmotic membrane, reducing a pressure of the monovalent-ion-enriched product stream. For example, referring to
Certain embodiments comprise, after transporting at least a portion of a draw product stream across an osmotic membrane, reducing a pressure of the osmotic retentate stream. For example, referring to
Certain embodiments comprise recovering at least a portion of the energy released by reducing the pressure of at least one retentate product stream from an osmotic membrane separator. The recovered energy can be used, according to certain embodiments, to increase the pressure of at least one inlet stream to the retentate side of an ion-selective membrane separator and/or to increase the pressure of at least one inlet stream to the retentate side of an osmotic membrane separator. For example, in some embodiments, the recovered energy is used to increase the pressure of the aqueous feed stream before it is transported into the ion-selective separator. For example, referring to
The systems and methods described herein can be used to process a variety of aqueous feed streams. As noted above, the aqueous feed stream fed to the system generally contains both solubilized monovalent ions and solubilized multivalent ions. For example, referring to
In some embodiments, the total concentration of solubilized ions in the aqueous feed stream fed to the system (e.g., stream 160 fed to system 100 in
In certain embodiments, the total concentration of solubilized ions in the aqueous feed stream transported to the ion-selective separator is at least about 60,000 ppm, at least about 80,000 ppm, or at least about 100,000 ppm (and/or, in some embodiments, up to about 500,000 ppm, or more). Aqueous feed streams with solubilized ion concentrations outside these ranges could also be used. For example, in some embodiments, the total concentration of solubilized ions in the aqueous feed stream transported to the ion-selective separator is as little as 10,000 ppm, 1000 ppm, 100 ppm, or less.
In certain embodiments, the total concentration of solubilized monovalent ions in the aqueous feed stream transported to the ion-selective separator is at least about 60,000 ppm, at least about 80,000 ppm, or at least about 100,000 ppm (and/or, in some embodiments, up to about 500,000 ppm, or more). Aqueous feed streams with solubilized monovalent ion concentrations outside these ranges could also be used. For example, in some embodiments, the total concentration of solubilized monovalent ions in the aqueous feed stream transported to the ion-selective separator is as little as 10,000 ppm, 1000 ppm, 100 ppm, or less.
In certain embodiments, the total concentration of solubilized multivalent ions in the aqueous feed stream transported to the ion-selective separator is at least about 60,000 ppm, at least about 80,000 ppm, or at least about 100,000 ppm (and/or, in some embodiments, up to about 500,000 ppm, or more). Aqueous feed streams with solubilized multivalent ion concentrations outside these ranges could also be used. For example, in some embodiments, the total concentration of solubilized multivalent ions in the aqueous feed stream transported to the ion-selective separator is as little as 10,000 ppm, 1000 ppm, 100 ppm, or less.
In certain embodiments, the total concentration of solubilized monovalent ions in the monovalent-ion-enriched stream exiting the ion-selective separator (e.g., exiting an ion-selective membrane) is at least about 60,000 ppm, at least about 80,000 ppm, or at least about 100,000 ppm (and/or, in some embodiments, up to about 500,000 ppm, or more). Monovalent-ion-enriched streams with solubilized monovalent ion concentrations outside these ranges could also be used. For example, in some embodiments, the total concentration of solubilized monovalent ions in the monovalent-ion-enriched stream exiting the ion-selective separator (e.g., exiting an ion-selective membrane) is as little as 10,000 ppm, 1000 ppm, 100 ppm, or less.
In certain embodiments, the total concentration of solubilized multivalent ions in the multivalent-ion-enriched stream exiting the ion-selective separator (e.g., exiting an ion-selective membrane) is at least about 60,000 ppm, at least about 80,000 ppm, or at least about 100,000 ppm (and/or, in some embodiments, up to about 500,000 ppm, or more). Multivalent-ion-enriched streams with solubilized multivalent ion concentrations outside these ranges could also be used. For example, in some embodiments, the total concentration of solubilized multivalent ions in the multivalent-ion-enriched stream exiting the ion-selective separator (e.g., exiting an ion-selective membrane) is as little as 10,000 ppm, 1000 ppm, 100 ppm, or less.
In some embodiments, the aqueous feed stream can be derived from seawater, ground water, brackish water, and/or the effluent of a chemical process. In the oil and gas industry, for example, one type of aqueous feed stream that may be encountered is produced water (e.g., water that emerges from oil or gas wells along with the oil or gas). Due to the length of time produced water has spent in the ground, and due to high subterranean pressures and temperatures that may increase the solubility of certain salts and minerals, produced water often comprises relatively high concentrations of dissolved salts and minerals. For example, some produced water streams may comprise a supersaturated solution of dissolved strontium sulfate (SrSO4). In contrast, another type of aqueous feed stream that may be encountered in the oil and gas industry is flowback water (e.g., water that is injected as a fracking fluid during hydraulic fracturing operations and subsequently recovered). Flowback water often comprises a variety of constituents used in fracking, including surfactants, proppants, and viscosity reducing agents, but often has a lower salinity than produced water. In some cases, the systems and methods described herein can be used to produce multivalent-ion-enriched streams from aqueous feed streams comprising and/or derived from such process streams.
According to certain embodiments, the aqueous feed stream comprises a suspended and/or emulsified immiscible phase. Generally, a suspended and/or emulsified immiscible phase is a material that is not soluble in water to a level of more than 10% by weight at the temperature and other conditions at which the stream is operated. In some embodiments, the suspended and/or emulsified immiscible phase comprises oil and/or grease. The term “oil” generally refers to a fluid that is more hydrophobic than water and is not miscible or soluble in water, as is known in the art. Thus, the oil may be a hydrocarbon in some embodiments, but in other embodiments, the oil may comprise other hydrophobic fluids. In some embodiments, at least about 0.1 wt %, at least about 1 wt %, at least about 2 wt %, at least about 5 wt %, or at least about 10 wt % (and/or, in some embodiments, up to about 20 wt %, up to about 30 wt %, up to about 40 wt %, up to about 50 wt %, or more) of the aqueous feed stream is made up of a suspended and/or emulsified immiscible phase.
It can be undesirable, according to certain embodiments, to allow certain suspended and/or emulsified immiscible phases to enter the system. For example, in certain embodiments in which ion-selective membranes are employed, the membranes can be made of a material (e.g., polysulfones, polyethersulfone) that can be damaged when they are exposed to oil and/or other hydrocarbons. Osmotic membranes can also be damaged when exposed to such chemicals. Accordingly, removal of the oil and/or other hydrocarbons upstream of the system can be desirable.
Accordingly, certain embodiments comprise removing at least a portion of a suspended or emulsified immiscible phase from the aqueous feed stream before the aqueous feed stream is transported to an ion-selective separator and/or an ion-selective membrane. In certain embodiments, the system is configured such that little or none of the suspended and/or emulsified immiscible phase is transported to the ion-selective separator and/or an ion-selective membrane.
For example, in some embodiments, a water-immiscible phase separator can be configured to remove at least a portion of (e.g., at least about 50%, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 99 wt %, or more) of the suspended and/or emulsified immiscible phase from the aqueous feed stream before the aqueous feed stream is transported to the ion-selective membrane.
In certain embodiments, a water-immiscible phase separator can be configured to remove at least a portion of (e.g., at least about 50%, at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, at least about 99 wt %, or more) of the suspended and/or emulsified immiscible phase from the aqueous feed stream before the aqueous feed stream is transported to the ion-selective separator.
In certain embodiments, the water-immiscible phase separator can be configured to output an aqueous feed stream (e.g., to an ion-selective membrane and/or an ion-selective membrane separator) having a concentration of suspended and/or emulsified immiscible phase(s) of less than about 10 ppm, less than about 1 ppm, or less than about 0.1 ppm. In certain embodiments, the water-immiscible phase separator can be configured to output an aqueous feed stream (e.g., to an ion-selective membrane and/or an ion-selective membrane separator) having a concentration of oil of less than about 10 ppm, less than about 1 ppm, or less than about 0.1 ppm.
Optionally, the water-immiscible phase separator can produce an immiscible-phase-rich stream, which can contain at least a portion (or all) of the immiscible phase that is separated from the aqueous feed stream. For example, in
While the water-immiscible phase separator can be used to separate a suspended and/or emulsified immiscible phase from an incoming aqueous feed stream, such separation is optional. For example, in some embodiments, the aqueous feed stream transported to the system is substantially free of a suspended and/or emulsified immiscible phase, or it contains an amount of suspended and/or emulsified immiscible phase that is sufficiently low that acceptable operation of the system can be obtained without using a water-immiscible phase separator.
A variety of water-immiscible phase separators are suitable for use according to certain of the embodiments described herein. In some embodiments, the water-immiscible phase separator at least partially separates the immiscible phase from the aqueous stream via gravity, centrifugal force, adsorption, and/or using a barrier. In some embodiments, the water-immiscible phase separator comprises a hydrocyclone, such as a de-oiling hydrocyclone. In some embodiments, the hydrocyclone can be configured to remove droplets of the immiscible phase having a diameter of greater than about 10 micrometers. In certain embodiments, the water-immiscible phase separator comprises a corrugated plate interceptor. In some embodiments, the corrugated plate interceptor can be configured to remove droplets of the immiscible phase having a diameter of greater than about 50 micrometers. In some embodiments, the water-immiscible phase separator comprises an adsorption media filter. The adsorption media filter can contain an adsorption medium. The adsorption medium may comprise, for example, walnut shells. In some embodiments, the adsorption media filter can be configured to remove droplets of the immiscible phase having a diameter of greater than about 150 micrometers. The water-immiscible phase separator comprises, according to certain embodiments, a coalescing media filter. The coalescing media filter can be configured, in some embodiments, to remove droplets of the immiscible phase having a diameter of less than about 2 micrometers. In some embodiments, the water-immiscible phase separator comprises a membrane filter. In certain embodiments, the membrane filter can be configured to remove droplets of the immiscible phase having a diameter of less than about 1 micrometer. In certain embodiments, the water-immiscible phase separator comprises a settling zone in which water and the immiscible phase are at least partially physically separated. The settling zone may comprise, for example, a crystallization tank (which can be, in some embodiments, a settling tank). As one example, the water-immiscible phase separator may comprise, according to certain embodiments, an American Petroleum Institute separator, commonly referred to as API separators. In some embodiments, the API separator can be configured to remove droplets of the immiscible phase having a diameter of greater than about 150 micrometers. According to some embodiments, the water-immiscible phase separator comprises a skimmer. In some embodiments, the water-immiscible phase separator comprises a dissolved gas floatation (DGF) apparatus. In certain embodiments, the water-immiscible phase separator comprises an induced gas flotation (IGF) apparatus. In some embodiments, the DGF and/or IGF apparatus can be configured to remove droplets of the immiscible phase having a diameter of greater than about 20 micrometers.
Certain embodiments are related to producing multivalent-ion-enriched streams for use in oil recovery. Oil reservoirs generally include porous rocks, the pores of which may contain oil. In some cases, injection of water rich in solubilized multivalent ions can aid in the extraction of oil from such pores. Accordingly, some embodiments comprise injecting a multivalent-ion-enriched product stream (e.g., any of the multivalent-ion-enriched product streams described herein) into a subterranean space. The subterranean space may comprise, for example, oil contained within the pores of a porous material (e.g., porous rocks or other porous materials). In certain embodiments, the subterranean space may be part of an oil well. In certain embodiments, the multivalent-ion-enriched stream that is injected into the subterranean space can be injected under pressure (e.g., under a gauge pressure of at least about 1 bar, at least about 2 bar, at least about 5 bar, at least about 10 bar, at least about 25 bar, or more). Certain embodiments can comprise recovering at least a portion of the monovalent-ion-enriched stream from the subterranean space. In certain embodiments, the aqueous feed stream used in the system (e.g., any of the aqueous feed streams described herein) can comprise at least a portion of the monovalent-ion-enriched stream recovered from the subterranean space.
Various components are described herein as being either directly fluidically connected or indirectly fluidically connected. Generally, a direct fluidic connection exists between a first region and a second region (and the two regions are said to be directly fluidically connected to each other) when they are fluidically connected to each other and when the composition of the fluid at the second region of the fluidic connection has not substantially changed relative to the composition of the fluid at the first region of the fluidic connection (i.e., no fluid component that was present in the first region of the fluidic connection is present in a weight percentage in the second region of the fluidic connection that is more than 5% different from the weight percentage of that component in the first region of the fluidic connection). As an illustrative example, a stream that connects first and second unit operations, and in which the pressure and temperature of the fluid is adjusted but the composition of the fluid is not altered, would be said to directly fluidically connect the first and second unit operations. If, on the other hand, a separation step is performed and/or a chemical reaction is performed that substantially alters the composition of the stream contents during passage from the first component to the second component, the stream would not be said to directly fluidically connect the first and second unit operations. In some embodiments, a direct fluidic connection between a first region and a second region can be configured such that the fluid does not undergo a phase change from the first region to the second region. In some embodiments, the direct fluidic connection can be configured such that at least about 50 wt % (or at least about 75 wt %, at least about 90 wt %, at least about 95 wt %, or at least about 98 wt %) of the fluid in the first region is transported to the second region via the direct fluidic connection.
Certain components (e.g., sides of membranes) are described according to certain embodiments as facing other components (e.g., sides of other membranes). As used herein, a surface (or surface portion) is said to be “facing” an object when any line extending normal to the surface and away from the bulk of the material comprising the surface intersects the object. For example, a first surface would be facing a second surface if a line normal to the first surface and extending away from the bulk of the material comprising the first surface intersects the second surface. A surface can be facing another object when it is in contact with the other object, or when one or more intermediate materials are positioned between the surface and the other object. For example, two surfaces that are facing each other can be in contact or can include one or more intermediate materials between them.
U.S. Provisional Patent Application Ser. No. 62/205,633, filed Aug. 14, 2015 and entitled “Selective Retention of Multivalent Ions” is incorporated herein by reference in its entirety for all purposes.
While several embodiments of the present invention have been described and illustrated herein, those of ordinary skill in the art will readily envision a variety of other means and/or structures for performing the functions and/or obtaining the results and/or one or more of the advantages described herein, and each of such variations and/or modifications is deemed to be within the scope of the present invention. More generally, those skilled in the art will readily appreciate that all parameters, dimensions, materials, and configurations described herein are meant to be exemplary and that the actual parameters, dimensions, materials, and/or configurations will depend upon the specific application or applications for which the teachings of the present invention is/are used. Those skilled in the art will recognize, or be able to ascertain using no more than routine experimentation, many equivalents to the specific embodiments of the invention described herein. It is, therefore, to be understood that the foregoing embodiments are presented by way of example only and that, within the scope of the appended claims and equivalents thereto, the invention may be practiced otherwise than as specifically described and claimed. The present invention is directed to each individual feature, system, article, material, and/or method described herein. In addition, any combination of two or more such features, systems, articles, materials, and/or methods, if such features, systems, articles, materials, and/or methods are not mutually inconsistent, is included within the scope of the present invention.
The indefinite articles “a” and “an,” as used herein in the specification and in the claims, unless clearly indicated to the contrary, should be understood to mean “at least one.”
The phrase “and/or,” as used herein in the specification and in the claims, should be understood to mean “either or both” of the elements so conjoined, i.e., elements that are conjunctively present in some cases and disjunctively present in other cases. Other elements may optionally be present other than the elements specifically identified by the “and/or” clause, whether related or unrelated to those elements specifically identified unless clearly indicated to the contrary. Thus, as a non-limiting example, a reference to “A and/or B,” when used in conjunction with open-ended language such as “comprising” can refer, in one embodiment, to A without B (optionally including elements other than B); in another embodiment, to B without A (optionally including elements other than A); in yet another embodiment, to both A and B (optionally including other elements); etc.
As used herein in the specification and in the claims, “or” should be understood to have the same meaning as “and/or” as defined above. For example, when separating items in a list, “or” or “and/or” shall be interpreted as being inclusive, i.e., the inclusion of at least one, but also including more than one, of a number or list of elements, and, optionally, additional unlisted items. Only terms clearly indicated to the contrary, such as “only one of” or “exactly one of,” or, when used in the claims, “consisting of,” will refer to the inclusion of exactly one element of a number or list of elements. In general, the term “or” as used herein shall only be interpreted as indicating exclusive alternatives (i.e. “one or the other but not both”) when preceded by terms of exclusivity, such as “either,” “one of,” “only one of,” or “exactly one of.” “Consisting essentially of,” when used in the claims, shall have its ordinary meaning as used in the field of patent law.
As used herein in the specification and in the claims, the phrase “at least one,” in reference to a list of one or more elements, should be understood to mean at least one element selected from any one or more of the elements in the list of elements, but not necessarily including at least one of each and every element specifically listed within the list of elements and not excluding any combinations of elements in the list of elements. This definition also allows that elements may optionally be present other than the elements specifically identified within the list of elements to which the phrase “at least one” refers, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, “at least one of A and B” (or, equivalently, “at least one of A or B,” or, equivalently “at least one of A and/or B”) can refer, in one embodiment, to at least one, optionally including more than one, A, with no B present (and optionally including elements other than B); in another embodiment, to at least one, optionally including more than one, B, with no A present (and optionally including elements other than A); in yet another embodiment, to at least one, optionally including more than one, A, and at least one, optionally including more than one, B (and optionally including other elements); etc.
In the claims, as well as in the specification above, all transitional phrases such as “comprising,” “including,” “carrying,” “having,” “containing,” “involving,” “holding,” and the like are to be understood to be open-ended, i.e., to mean including but not limited to. Only the transitional phrases “consisting of” and “consisting essentially of” shall be closed or semi-closed transitional phrases, respectively, as set forth in the United States Patent Office Manual of Patent Examining Procedures, Section 2111.03.
This application is a U.S. National Stage patent application based on International Application PCT/US2016/046709, filed Aug. 12, 2016, which claims priority under 35 U.S.C. § 119(e) to U.S. Provisional Patent Application Ser. No. 62/205,633, filed Aug. 14, 2015 and entitled “Selective Retention of Multivalent Ions” each of which is incorporated herein by reference in its entirety for all purposes.
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/US2016/046709 | 8/12/2016 | WO | 00 |
| Publishing Document | Publishing Date | Country | Kind |
|---|---|---|---|
| WO2017/030932 | 2/23/2017 | WO | A |
| Number | Name | Date | Kind |
|---|---|---|---|
| 2151990 | Ruys | Mar 1939 | A |
| 2606820 | Viggo | Aug 1952 | A |
| 2606839 | Evans | Aug 1952 | A |
| 2640018 | Heath | May 1953 | A |
| 2997856 | Pike | Aug 1961 | A |
| 3032482 | Shoemaker | May 1962 | A |
| 3042606 | Salutsky et al. | Jul 1962 | A |
| 3080302 | Rogers et al. | Mar 1963 | A |
| 3236747 | Margiloff | Feb 1966 | A |
| 3331773 | Gunderson et al. | Jul 1967 | A |
| 3454490 | Wallace | Jul 1969 | A |
| 3489652 | Williamson | Jan 1970 | A |
| 3625761 | Tate | Dec 1971 | A |
| 3725209 | Rosa | Apr 1973 | A |
| 3906250 | Loeb | Sep 1975 | A |
| 3922154 | Kawasaki et al. | Nov 1975 | A |
| 3926739 | Izumi | Dec 1975 | A |
| 4156645 | Bray | May 1979 | A |
| 4224148 | Lindman et al. | Sep 1980 | A |
| 4251367 | Santora | Feb 1981 | A |
| 4312755 | Hwang | Jan 1982 | A |
| 4334886 | Tani et al. | Jun 1982 | A |
| 4452696 | Lopez | Jun 1984 | A |
| 4511436 | El Din et al. | Apr 1985 | A |
| 4563337 | Kim | Jan 1986 | A |
| 4576724 | Colman et al. | Mar 1986 | A |
| 4708805 | D'Muhala | Nov 1987 | A |
| 4735722 | Krepak | Apr 1988 | A |
| 4755298 | Grinstead | Jul 1988 | A |
| 4770775 | Lopez | Sep 1988 | A |
| 4806244 | Guilhem | Feb 1989 | A |
| 4832115 | Albers et al. | May 1989 | A |
| 4843828 | Gladman | Jul 1989 | A |
| 4944882 | Ray et al. | Jul 1990 | A |
| 4956157 | Nasu | Sep 1990 | A |
| 4973201 | Paul et al. | Nov 1990 | A |
| 4980077 | Morris et al. | Dec 1990 | A |
| 4981593 | Priestley et al. | Jan 1991 | A |
| 5015391 | Mohn | May 1991 | A |
| 5053132 | Sirkar | Oct 1991 | A |
| 5123481 | Albers et al. | Jun 1992 | A |
| 5167828 | Emmons et al. | Dec 1992 | A |
| 5190656 | Paul et al. | Mar 1993 | A |
| 5225087 | Kardos | Jul 1993 | A |
| 5238574 | Kawashima et al. | Aug 1993 | A |
| 5250185 | Tao et al. | Oct 1993 | A |
| 5282995 | Paul et al. | Feb 1994 | A |
| 5328616 | Martyak et al. | Jul 1994 | A |
| 5425902 | Miller et al. | Jun 1995 | A |
| 5453205 | Browne | Sep 1995 | A |
| 5464540 | Friesen et al. | Nov 1995 | A |
| 5656161 | Solomon et al. | Aug 1997 | A |
| 5840195 | Delsalle et al. | Nov 1998 | A |
| 6010631 | Delsalle et al. | Jan 2000 | A |
| 6056878 | Tessier | May 2000 | A |
| 6062070 | Maltby et al. | May 2000 | A |
| 6113797 | Al-Samadi | Sep 2000 | A |
| 6146525 | Li et al. | Nov 2000 | A |
| 6187200 | Yamamura et al. | Feb 2001 | B1 |
| 6190556 | Uhlinger | Feb 2001 | B1 |
| 6270671 | Shorr et al. | Aug 2001 | B1 |
| 6319409 | Saitou et al. | Nov 2001 | B1 |
| 6416668 | Al-Samadi et al. | Jul 2002 | B1 |
| 6423235 | Shimoi et al. | Jul 2002 | B1 |
| 6440310 | Shorr et al. | Aug 2002 | B1 |
| 6461514 | Al-Samadi | Oct 2002 | B1 |
| 6508936 | Hassan | Jan 2003 | B1 |
| 6582605 | Krulik et al. | Jun 2003 | B2 |
| 6699369 | Hartman et al. | Mar 2004 | B1 |
| 6730234 | Symens et al. | May 2004 | B2 |
| 6783682 | Awerbuch | Aug 2004 | B1 |
| 6817476 | Donnick et al. | Nov 2004 | B2 |
| 6919000 | Klausner et al. | Jul 2005 | B2 |
| 7022240 | Hart et al. | Apr 2006 | B2 |
| 7048852 | Ballard | May 2006 | B2 |
| 7115670 | Hensman et al. | Oct 2006 | B2 |
| 7141171 | Lightfoot | Nov 2006 | B2 |
| 7225620 | Klausner et al. | Jun 2007 | B2 |
| 7306437 | Hauge | Dec 2007 | B2 |
| 7316080 | Woolsey | Jan 2008 | B1 |
| 7459084 | Baig et al. | Dec 2008 | B2 |
| 7459088 | Davis | Dec 2008 | B2 |
| 7465376 | Neubert et al. | Dec 2008 | B2 |
| 7510656 | Shafer et al. | Mar 2009 | B2 |
| 7520993 | Laraway et al. | Apr 2009 | B1 |
| 7527726 | Slough et al. | May 2009 | B2 |
| 7597784 | Bednarek et al. | Oct 2009 | B2 |
| 7678235 | Deep et al. | Mar 2010 | B2 |
| 7718069 | Laraway et al. | May 2010 | B2 |
| 7726398 | Collins et al. | Jun 2010 | B2 |
| 7727400 | Flynn | Jun 2010 | B2 |
| 7731847 | Ton That | Jun 2010 | B2 |
| 7815804 | Nagghappan | Oct 2010 | B2 |
| 7824552 | Slabaugh et al. | Nov 2010 | B2 |
| 7950921 | Woolsey | May 2011 | B1 |
| 7964101 | Slough et al. | Jun 2011 | B2 |
| 8012358 | Slabaugh et al. | Sep 2011 | B2 |
| 8043509 | Thiers | Oct 2011 | B2 |
| 8119007 | Bajpayee et al. | Feb 2012 | B2 |
| 8147696 | Pandya | Apr 2012 | B1 |
| 8197693 | Al-Juil | Jun 2012 | B2 |
| 8216473 | Wohlert | Jul 2012 | B2 |
| 8252092 | Govindan et al. | Aug 2012 | B2 |
| 8292272 | Elsharqawy et al. | Oct 2012 | B2 |
| 8366924 | Vuong | Feb 2013 | B2 |
| 8469092 | Curole et al. | Jun 2013 | B2 |
| 8496234 | Govindan et al. | Jul 2013 | B1 |
| 8501007 | Bajpayee et al. | Aug 2013 | B2 |
| 8523985 | Govindan et al. | Sep 2013 | B2 |
| 8562824 | Thiers et al. | Oct 2013 | B2 |
| 8647477 | Govindan et al. | Feb 2014 | B2 |
| 8678080 | Curole et al. | Mar 2014 | B2 |
| 8679347 | Al-Samadi | Mar 2014 | B2 |
| 8695343 | Moe | Apr 2014 | B2 |
| 8727325 | Sparrow et al. | May 2014 | B2 |
| 8771477 | Thiers | Jul 2014 | B2 |
| 8778065 | Govindan et al. | Jul 2014 | B2 |
| 8794320 | Ayirala et al. | Aug 2014 | B2 |
| 8820723 | Sparrow et al. | Sep 2014 | B1 |
| 8840792 | Wohlert | Sep 2014 | B2 |
| 8857798 | Sparrow et al. | Oct 2014 | B1 |
| 8889000 | Hannemann et al. | Nov 2014 | B2 |
| 8980100 | Chidambaran | Mar 2015 | B2 |
| 8999172 | Zuback | Apr 2015 | B1 |
| 9072984 | Govindan et al. | Jul 2015 | B2 |
| 9079117 | Govindan et al. | Jul 2015 | B2 |
| 9085971 | Janssen et al. | Jul 2015 | B2 |
| 9120033 | Govindan et al. | Sep 2015 | B2 |
| 9206060 | Abusharkh | Dec 2015 | B1 |
| 9221694 | Govindan et al. | Dec 2015 | B1 |
| 9266748 | Govindan et al. | Feb 2016 | B1 |
| 9266762 | Wang et al. | Feb 2016 | B2 |
| 9427705 | Abusharkh | Aug 2016 | B1 |
| 9428404 | Bajpayee et al. | Aug 2016 | B2 |
| 9550685 | Klausner et al. | Jan 2017 | B2 |
| 9556041 | Govindan et al. | Jan 2017 | B2 |
| 9617179 | Govindan et al. | Apr 2017 | B2 |
| 9700811 | Govindan et al. | Jul 2017 | B2 |
| 9957180 | Govindan et al. | May 2018 | B2 |
| 9969638 | Govindan et al. | May 2018 | B2 |
| 20030106860 | Peloquin et al. | Jun 2003 | A1 |
| 20030132166 | Rey | Jul 2003 | A1 |
| 20040187897 | Kenowski et al. | Sep 2004 | A1 |
| 20050023222 | Baillie | Feb 2005 | A1 |
| 20060150892 | Mayer | Jul 2006 | A1 |
| 20060157409 | Hassan | Jul 2006 | A1 |
| 20060157410 | Hassan | Jul 2006 | A1 |
| 20070012556 | Lum et al. | Jan 2007 | A1 |
| 20070068791 | Thom et al. | Mar 2007 | A1 |
| 20070080113 | Vuong | Apr 2007 | A1 |
| 20070084713 | Deep et al. | Apr 2007 | A1 |
| 20070102359 | Lombardi et al. | May 2007 | A1 |
| 20070131428 | den Boestert et al. | Jun 2007 | A1 |
| 20070181480 | Lee | Aug 2007 | A1 |
| 20070235391 | Ylikangas et al. | Oct 2007 | A1 |
| 20080073200 | Godshall et al. | Mar 2008 | A1 |
| 20080102119 | Grovender | May 2008 | A1 |
| 20080116134 | Cartwright | May 2008 | A1 |
| 20080121585 | Mavis | May 2008 | A1 |
| 20080277344 | Sengupta et al. | Nov 2008 | A1 |
| 20090020289 | Sharif | Jan 2009 | A1 |
| 20090032446 | Wiemers et al. | Feb 2009 | A1 |
| 20090101490 | Thiers | Apr 2009 | A1 |
| 20090101587 | Blokker et al. | Apr 2009 | A1 |
| 20090127210 | Swisher | May 2009 | A1 |
| 20090173096 | Wohlert | Jul 2009 | A1 |
| 20090194272 | Baillie | Aug 2009 | A1 |
| 20090218210 | Demmons et al. | Sep 2009 | A1 |
| 20090277634 | Case et al. | Nov 2009 | A1 |
| 20090277640 | Thompson et al. | Nov 2009 | A1 |
| 20090277641 | Walters et al. | Nov 2009 | A1 |
| 20090308820 | Thiers et al. | Dec 2009 | A1 |
| 20100032377 | Wohlert | Feb 2010 | A1 |
| 20100163471 | Elyanow et al. | Jul 2010 | A1 |
| 20100163472 | Thiers et al. | Jul 2010 | A1 |
| 20100234795 | Wallenas | Sep 2010 | A1 |
| 20100242995 | Xiong et al. | Sep 2010 | A1 |
| 20100282675 | Sengupta et al. | Nov 2010 | A1 |
| 20100314238 | Frolov et al. | Dec 2010 | A1 |
| 20110017677 | Evans | Jan 2011 | A1 |
| 20110024354 | Xia et al. | Feb 2011 | A1 |
| 20110056822 | Elsharqawy et al. | Mar 2011 | A1 |
| 20110056878 | Matsushiro et al. | Mar 2011 | A1 |
| 20110094965 | Al-Samadi | Apr 2011 | A1 |
| 20110108484 | Liberman et al. | May 2011 | A1 |
| 20110114558 | Al-Mayahi et al. | May 2011 | A1 |
| 20110120157 | Wohlert | May 2011 | A1 |
| 20110155666 | Prakash et al. | Jun 2011 | A1 |
| 20110180479 | Cordatos et al. | Jul 2011 | A1 |
| 20110198285 | Wallace | Aug 2011 | A1 |
| 20110215039 | Acernese et al. | Sep 2011 | A1 |
| 20110233137 | Cath et al. | Sep 2011 | A1 |
| 20110257788 | Wiemers et al. | Oct 2011 | A1 |
| 20110303607 | Vora et al. | Dec 2011 | A1 |
| 20110306525 | Lighthelm | Dec 2011 | A1 |
| 20120012005 | Burke | Jan 2012 | A1 |
| 20120012511 | Kim et al. | Jan 2012 | A1 |
| 20120037568 | Karrs et al. | Feb 2012 | A1 |
| 20120067819 | McGinnis | Mar 2012 | A1 |
| 20120067820 | Henthorne et al. | Mar 2012 | A1 |
| 20120090833 | Ligthelm et al. | Apr 2012 | A1 |
| 20120091061 | Al-Jlil | Apr 2012 | A1 |
| 20120125603 | Willingham et al. | May 2012 | A1 |
| 20120125611 | Ayirala et al. | May 2012 | A1 |
| 20120125861 | Thiers | May 2012 | A1 |
| 20120145635 | Lucas, III et al. | Jun 2012 | A1 |
| 20120199524 | Bly et al. | Aug 2012 | A1 |
| 20120199534 | Holtzapple et al. | Aug 2012 | A1 |
| 20120205307 | Boudinar | Aug 2012 | A1 |
| 20120227975 | Ayirala et al. | Sep 2012 | A1 |
| 20120234664 | Nicoll | Sep 2012 | A1 |
| 20120234765 | Sengupta et al. | Sep 2012 | A1 |
| 20120267307 | McGinnis | Oct 2012 | A1 |
| 20120273417 | McGinnis et al. | Nov 2012 | A1 |
| 20120273422 | Wohlert | Nov 2012 | A1 |
| 20120279396 | Brammer et al. | Nov 2012 | A1 |
| 20120285886 | Liberman | Nov 2012 | A1 |
| 20120292259 | Marcin | Nov 2012 | A1 |
| 20120312755 | Ryan et al. | Dec 2012 | A1 |
| 20120318729 | Yip et al. | Dec 2012 | A1 |
| 20130008079 | Chung et al. | Jan 2013 | A1 |
| 20130043190 | Al-Samadi et al. | Feb 2013 | A1 |
| 20130056193 | Thiers | Mar 2013 | A1 |
| 20130074694 | Govindan et al. | Mar 2013 | A1 |
| 20130075098 | Janjua et al. | Mar 2013 | A1 |
| 20130075940 | Govindan et al. | Mar 2013 | A1 |
| 20130087501 | Moe et al. | Apr 2013 | A1 |
| 20130092622 | Kas et al. | Apr 2013 | A1 |
| 20130092626 | Zimmerman et al. | Apr 2013 | A1 |
| 20130105323 | Averbeck et al. | May 2013 | A1 |
| 20130118887 | Frolov et al. | May 2013 | A1 |
| 20130193074 | Voigt et al. | Aug 2013 | A1 |
| 20130199921 | McGovern | Aug 2013 | A1 |
| 20130213892 | Henthorne | Aug 2013 | A1 |
| 20130233786 | Posa | Sep 2013 | A1 |
| 20130240442 | Chidambaran et al. | Sep 2013 | A1 |
| 20130256228 | Bharwada et al. | Oct 2013 | A1 |
| 20130318743 | Chinta et al. | Dec 2013 | A1 |
| 20140008291 | Tang et al. | Jan 2014 | A1 |
| 20140021135 | Sawyer et al. | Jan 2014 | A1 |
| 20140041856 | Janssen et al. | Feb 2014 | A1 |
| 20140042058 | Janssen et al. | Feb 2014 | A1 |
| 20140042061 | Wallace | Feb 2014 | A1 |
| 20140061022 | Passarelli | Mar 2014 | A1 |
| 20140067958 | Bradley et al. | Mar 2014 | A1 |
| 20140069821 | Marcin et al. | Mar 2014 | A1 |
| 20140116956 | Yuan et al. | May 2014 | A1 |
| 20140151300 | Savage et al. | Jun 2014 | A1 |
| 20140197022 | Antar et al. | Jul 2014 | A1 |
| 20140197029 | Sparrow et al. | Jul 2014 | A1 |
| 20140246368 | Neubrand et al. | Sep 2014 | A1 |
| 20140263055 | Govindan et al. | Sep 2014 | A1 |
| 20140263081 | Thiers | Sep 2014 | A1 |
| 20140299462 | Thiers | Oct 2014 | A1 |
| 20140339162 | Cao et al. | Nov 2014 | A1 |
| 20140367871 | Govindan et al. | Dec 2014 | A1 |
| 20150013987 | Underwood et al. | Jan 2015 | A1 |
| 20150014248 | Herron et al. | Jan 2015 | A1 |
| 20150053619 | Cao et al. | Feb 2015 | A1 |
| 20150060286 | Govindan et al. | Mar 2015 | A1 |
| 20150060360 | Motherway et al. | Mar 2015 | A1 |
| 20150083577 | Govindan et al. | Mar 2015 | A1 |
| 20150083656 | Williams | Mar 2015 | A1 |
| 20150107840 | Ligthelm et al. | Apr 2015 | A1 |
| 20150107841 | Suijkerbuijk et al. | Apr 2015 | A1 |
| 20150129410 | Govindan et al. | May 2015 | A1 |
| 20150353397 | Cath | Dec 2015 | A1 |
| 20160001235 | Frisk | Jan 2016 | A1 |
| 20160040522 | Jacob et al. | Feb 2016 | A1 |
| 20160137526 | Govindan et al. | May 2016 | A1 |
| 20160228795 | St. John et al. | Aug 2016 | A1 |
| 20160229705 | St. John et al. | Aug 2016 | A1 |
| 20160244349 | St. John et al. | Aug 2016 | A1 |
| 20160339354 | Govindan et al. | Nov 2016 | A1 |
| 20160339356 | Govindan et al. | Nov 2016 | A1 |
| 20160339357 | Govindan et al. | Nov 2016 | A1 |
| 20160339390 | Abusharkh | Nov 2016 | A1 |
| 20170036171 | Lienhard et al. | Feb 2017 | A1 |
| 20170044033 | Lienhard et al. | Feb 2017 | A1 |
| 20170144906 | Andrews et al. | May 2017 | A1 |
| 20170174543 | Govindan et al. | Jun 2017 | A1 |
| 20180008919 | Tierney, III et al. | Jan 2018 | A1 |
| 20180036682 | Nicoll et al. | Feb 2018 | A1 |
| 20180104649 | Govindan et al. | Apr 2018 | A1 |
| 20180236372 | Govindan et al. | Aug 2018 | A1 |
| 20180236406 | St. John et al. | Aug 2018 | A1 |
| Number | Date | Country |
|---|---|---|
| 2779732 | Dec 2012 | CA |
| 2818055 | Nov 2013 | CA |
| 2821453 | Jan 2014 | CA |
| 2816746 | Apr 2014 | CA |
| 2821458 | Jul 2014 | CA |
| 1623936 | Jun 2005 | CN |
| 1856447 | Nov 2006 | CN |
| 100999364 | Jul 2007 | CN |
| 101056693 | Oct 2007 | CN |
| 101397152 | Apr 2009 | CN |
| 101636354 | Jan 2010 | CN |
| 101717161 | Jun 2010 | CN |
| 102143786 | Aug 2011 | CN |
| 102438957 | May 2012 | CN |
| 102725236 | Oct 2012 | CN |
| 102933507 | Feb 2013 | CN |
| 2145861 | Sep 1972 | DE |
| 0 207 390 | Jan 1987 | EP |
| 0 253 287 | Jan 1988 | EP |
| 0 623 561 | Nov 1994 | EP |
| 1775267 | Apr 2007 | EP |
| 1582201 | Sep 1969 | FR |
| 2561637 | Sep 1985 | FR |
| 821939 | Oct 1959 | GB |
| 1013767 | Dec 1965 | GB |
| 1036920 | Jul 1966 | GB |
| 1444241 | Jul 1976 | GB |
| 2395946 | Jun 2004 | GB |
| S55-147199 | Nov 1980 | JP |
| H05-208199 | Aug 1993 | JP |
| 2018-001111 | Jan 2018 | JP |
| 101229482 | Feb 2013 | KR |
| WO 1995027683 | Oct 1995 | WO |
| WO 2000000273 | Jan 2000 | WO |
| WO 0114256 | Mar 2001 | WO |
| WO 0232813 | Apr 2002 | WO |
| WO 2005012185 | Feb 2005 | WO |
| WO 2007128062 | Nov 2007 | WO |
| WO 2007132477 | Nov 2007 | WO |
| WO 2007138327 | Dec 2007 | WO |
| WO 2007144591 | Dec 2007 | WO |
| WO 2008137082 | Nov 2008 | WO |
| WO 2010026589 | Mar 2010 | WO |
| WO 2010118425 | Oct 2010 | WO |
| WO 2010122336 | Oct 2010 | WO |
| WO 2010131251 | Nov 2010 | WO |
| WO 2010135561 | Nov 2010 | WO |
| WO 2011159743 | Dec 2011 | WO |
| WO 2012138502 | Oct 2012 | WO |
| WO 2012142396 | Oct 2012 | WO |
| WO 2012159203 | Nov 2012 | WO |
| WO 2013012548 | Jan 2013 | WO |
| WO 2013037047 | Mar 2013 | WO |
| WO 2013078124 | May 2013 | WO |
| WO 2013158315 | Oct 2013 | WO |
| WO 2013159220 | Oct 2013 | WO |
| WO 2014058696 | Apr 2014 | WO |
| WO 2014088826 | Jun 2014 | WO |
| WO 2014121153 | Aug 2014 | WO |
| WO 2014144778 | Sep 2014 | WO |
| WO 2014150848 | Sep 2014 | WO |
| WO 2014162094 | Oct 2014 | WO |
| WO 2014188450 | Nov 2014 | WO |
| WO 2014200829 | Dec 2014 | WO |
| WO 2015021062 | Feb 2015 | WO |
| WO 2015038983 | Mar 2015 | WO |
| WO 2015042584 | Mar 2015 | WO |
| WO 2015061194 | Apr 2015 | WO |
| WO 2017019944 | Feb 2017 | WO |
| WO 2017030932 | Feb 2017 | WO |
| WO 2017030937 | Feb 2017 | WO |
| WO 2017030941 | Feb 2017 | WO |
| WO 2017044645 | Mar 2017 | WO |
| WO 2017044668 | Mar 2017 | WO |
| WO 2017127607 | Jul 2017 | WO |
| WO 2017147113 | Aug 2017 | WO |
| WO 2018075637 | Apr 2018 | WO |
| Entry |
|---|
| International Search Report and Written Opinion for PCT/US16/46709 dated Dec. 28, 2016. |
| International Preliminary Report on Patentability for PCT/US16/46709 dated Mar. 1, 2018. |
| [No Author Listed], Accepta 4360 Material Safety Data Sheet. Accepta Ltd. Manchester, UK. Jul. 19, 2011. 5 pages. |
| [No Author Listed], Caustic Soda 50% Material Safety Data Sheet. Univar. Redmond, Washington. Apr. 8, 2013. 10 pages. |
| [No Author Listed], Color Removal Using Ozone. Spartan Environmental Technologies Air and Water Treatment—Technical Bulletin. Available Jul. 21, 2006. Last accessed Mar. 2, 2017 from <http://www.spartanwatertreatment.com/ozone-color-removal.html>. |
| [No Author Listed], Everything you want to know about Coagulation & Flocculation. Chapter 1: The Electrokinetic Connection. Zeta-Meter, Inc. Staunton, VA. 4th Edition. 1993:1-8. |
| [No Author Listed], F0 Plant Completes 1-Year of Operation. Water Desalination Report Nov. 15, 2010:2 pages. |
| [No Author Listed], Hi-Cal Hydrate Material Safety Data Sheet. Chemical Lime Co. Fort Worth, Texas. May 1, 2008. 6 pages. |
| [No Author Listed], Polyaluminum Chloride Solution Material Safety Data Sheet. GEO Specialty Chemicals, Ltd. Little Rock, Arkansas Mar. 12, 2015. 11 pages. |
| [No Author Listed], Servco 1010 Material Safety Data Sheet. Servco Chemicals. Lubbock, Texas. Aug. 7, 2013. 4 pages. |
| [No Author Listed], Soda Ash Material Safety Data Sheet. Univar. Redmond, Washington. Apr. 7, 2003. 10 pages. |
| Achilli et al., Selection of inorganic-based draw solutions for forward osmosis applications. Journal of Membrane Science. 2010;364:233-41. Epub Aug. 14, 2010. |
| Akram et al., Energy Utilization of Brine from an MSF Desalination Plant by Pressure Retarded Osmosis. The International Desalination Association World Congress on Desalination and Water Reuse. Tianjin, China Oct. 2013. 12 pages. |
| Al-Hallaj et al., Solar desalination with a humidification-dehumidification cycle: performance of the unit. Desalination. 1998;120:273-80. |
| Alshakhs, Modifying Water Salinity to Improve Oil Recovery. Stanford Academic Report. Oct. 29, 2013. Last accessed on Dec. 8, 2016 at <http://large.stanford.edu/courses/2013/ph240/alshakhs1/>. 2 pages. |
| Aramco, Saudi Aramco's ‘Smart Water’ May Aid Oil Production. Rigzone. Jul. 29, 2009. <http://www.rigzone.com/news/article_pf.asp?a_id=78707> Last accessed Jul. 30, 2015. 1 page. |
| Arthur et al., Technical Summary of Oil & Gas Produced Water Treatment Technologies. All Consulting, LLC (Mar. 2005). Last accessed on Dec. 21, 2016 from <http://dvikan.no/ntnu-studentserver/reports/ALLConsulting-WaterTreatmentOptionsReport.pdf>. 53 pages. |
| Banchik et al., Thermodynamic Analysis of a Reverse Osmosis Desalination System Using Forward Osmosis for Energy Recovery. Proceedings of the ASME 2012 International Mechanical Engineering Congress & Exposition. American Society of Mechanical Engineers. Houston, Texas. Nov. 9-15, 2012. 13 pages. |
| Burk, New Technology Spotlight. CaribDA News. 2012 Fall;2(4):6-7. |
| Cath et al., A Novel Hybrid Forward Osmosis Process for Drinking Water Augmentation Using Impaired Water and Saline Water Sources. WERC and Water Research Foundation. 2009:84 pages. |
| Chung et al., Forward osmosis processes: Yesterday, today and tomorrow. Desalination. 2012;287:78-81. Epub Jan. 11, 2011. |
| El-Dessouky et al., Multiple-effect evaporation desalination systems: thermal analysis. Desalination. 1999;125:259-76. |
| Ge et al., Exploration of polyelectrolytes as draw solutes in forward osmosis processes. Water Research 2012;46:1318-26. Epub Dec. 27, 2011. |
| Global Water Intelligence, Water Desalination Report. Tom Pankratz, ed. Dec. 17, 2012;48(48):1-4. |
| Govindan, Thermal Design of Humidification Dehumidification Systems for Affordable and Small-scale Desalination. Doctoral Thesis. Massachusetts Institute of Technology. Sep. 2012 286 pages. |
| Gude, Energy consumption and recovery in reverse osmosis. Desalination and Water Treatment. 2011;36(1-3):239-60. |
| Huang et al., The bridging force between colloidal particles in a polyelectrolyte solution. Langmuir. Nov. 27, 2012;28(47):16300-5. doi:10.1021/1a303918p. |
| Khayet et al., Determination of surface and bulk pore sizes of flat-sheet and hollow-fiber membranes by atomic force microscopy, gas permeation and solute transport methods. Desalination. 2003;158:57-64. |
| Kim et al., Effect of PEG additive on membrane formation by phase inversion. Journal of Membrane Science. 1998;138:153-63. |
| Klausner et al., Evaporative heat and mass transfer for the diffusion driven desalination process. Heat Mass Transfer. 2006;42:528-36. |
| Kwak et al., New Insights on the Role of Multivalent Ions I Water-Carbonate Rock Interactions. Saudi Journal of Technology. 2014:25-38. Last accessed on Dec. 8, 2016 at <http://www.saudiaramco.com/content/dam/Publications/Journal-of-Technology/Summer2014/New_Insights.pdf>. |
| Li, Experimental Analysis of Produced Water Desalination by a Humidification-Dehumidification Process. 2009. 62 pages. |
| Li, Mineral precipitation and deposition in cooling systems using impaired waters: mechanisms, kinetics, and inhibition. Dissertation defended Jul. 27, 2010. 224 pages. |
| McGinnis et al., Pilot demonstration of the NH3/CO2 forward osmosis desalination process on high salinity brines. Desalination. Mar. 2013;312:67-74. Supporting information included. |
| Moghadasi et al., Scale deposits in porous media and their removal by EDTA injection. ECI Symposium Series. 2007. vol. RP5. Article 10. p. 57-70. |
| Narayan et al., The potential of solar-driven humidification-dehumidification desalination for small-scale decentralized water production. Renewable and Sustainable Energy Reviews. 2010;14:1187-1201. |
| Narayan et al., Thermal design of the humidification desalination system: an experimental investigation. International Journal of Heat and Mass Transfer. 2013;58:1-9. |
| Narayan et al., Thermodynamic balancing of the humidification dehumidification desalination system by mass extraction and injection. International Journal of Heat and Mass Transfer. 2013;57:756-70. |
| Sahin, A Mathematical Model for Explanation of Ion Exchange of the Boric Acid Adsorption. Jour. Chem. Soc. Pak. l998;20(1):12-8. |
| Sinex, EDTA—A molecule with a complex story. University of Bristol, School of Chemistry. <www.chm.bris.ac.uk/motm/edta/edtah.htm> (accessed Jan. 8, 2013). Aug. 1, 2007. |
| Thiel et al., Hybridization of Humidification-Dehumidification and Pressure Retarded Osmosis for Brine Concentration Applications. The International Desalination Association World Congress on Desalination and Water Reuse. San Diego, California. Aug.-Sep. 8 pages. |
| Tiraferri et al., Relating performance of thin-film composite forward osmosis membranes to support layer formation and structure. Journal of Membrane Science. 2011;367:340-52. Epub Nov. 12, 2010. |
| Zamen et al., Improvement of solar humidification-dehumidification desalination using multi-stage process. 6 pages. Accessed Jun. 6, 2014. |
| McCutcheon et al., Influence of concentrative and dilutive internal concentration polarization on flux behavior in forward osmosis. Journal of Membrane Science. Nov. 2006;284(1-2):237-47. Epub Aug. 11, 2006. |
| Number | Date | Country | |
|---|---|---|---|
| 20180244545 A1 | Aug 2018 | US |
| Number | Date | Country | |
|---|---|---|---|
| 62205633 | Aug 2015 | US |
