Patent Application
20240017218
Many industries are known to produce saline effluents, such as desalination plants, gas and oil drilling rigs, energy generating plants, various food manufacturing facilities and industries that require high volumes of water, such as hydraulic fracking and the textile industry. To diminish the negative environmental impact of direct discharge of the saline effluents into water bodies (e.g., groundwater, lakes, rivers, the oceans) the high salt concentration of the effluents resulting from these processes needs to be reduced, prior to discharge into the environment.
Membrane-based processes for the treatment of the saline effluents are known in the art to include pressure retarded reverse osmosis (PRO) and reverse electrodialysis (RED), where a significant driving force in the industrial development of membranes already exists. PRO and RED utilize the electrochemical properties of solutions of differing saline concentrations (salinity) separated by semipermeable and/or charged ion-exchange membranes to accomplish Salinity Gradient Power (SGP) energy generation.
Most of the carbohydrates found in nature occur as polysaccharides, polymers of high molecular weight. Chitin is a naturally occurring biopolymer with great potential for industrial use because of its high amine content and polycationic nature. Chitin is a linear homopolymer (a polymeric carbohydrate molecule with repeating units of a single monomeric unit), containing residues of the monosaccharide N-acetyl-D-glucosamine joined by β(1→4) linkage. Chitin occurs mainly as the principal element in the hard exoskeletons, inner shell or cell wall of invertebrates, fungi and yeasts and is the second most abundant naturally occurring polymer on earth, after cellulose.
Chitin is the most abundant natural polymer in the ocean and thereby provides an enormous reservoir of organic carbon and nitrogen to draw from. Global fisheries contribute significantly to satisfying the world's need for protein. However, crustacean, and cephalopod seafood processing can generate between 35% and 75% bio-waste by weight consisting of the shell, head, and viscera. With increasing demands in both human population and protein needs, continued improvements in sustainable seafood bio-waste management, through new market development, is essential
Accordingly, what is needed in the art is an improved membrane that addresses the need for continued improvements in bio-waste management and power generation.
Chitosan membranes possess a high water flux permeability when subjected to a difference in salinity gradient concentration. In various embodiments, the present invention utilizes an asymmetric chitin/chitosan membrane as a thin film composite (TFC) membrane porous support layer for membrane filtration applications such as Reverse Osmosis (RO) desalinization, for the extraction of economically valuable materials from seawater or highly saline industrial fluids and for the reduction in the saline content of industrial and/or mining fluids for hazardous waste disposal in operations such as desalinization or hydraulic fracturing fracking. The present invention additionally proposes the use of membranes comprising chitosan and re-acetylated chitosan for salinity gradient power vapor pressure desalination (SGP-VPD).
In one embodiment, the present invention provides a thin film composite (TFC) membrane comprising a minimally hydrophilic and a substantially hydrophilic chitosan porous support layer. In particular, the minimally hydrophilic outer layer of the TFC membrane may be comprised of re-acetylated chitosan and the chitosan porous support layer may be comprised of de-acetylated chitin.
A method for performing desalination of saline water using the TFC membrane is provided. The method includes, positioning a thin film composite (TFC) membrane comprising a minimally hydrophilic re-acetylated chitosan outer layer and a substantially hydrophilic de-acetylated chitosan porous support layer, under a salinity concentration gradient. In particular, the minimally hydrophilic outer layer of the TFC membrane may be comprised of re-acetylated chitosan having pores of appropriate size and distribution to provide for liquid water separation and the substantially hydrophilic chitosan porous support layer may be comprised of de-acetylated chitin. The TFC membrane may be implemented in various desalination systems, including but not limited to, Reverse Osmosis (RO) and Electrodialysis (ED) systems for the desalination of the saline water.
In another embodiment, a multi-layer membrane is provided comprising a substantially hydrophobic re-acetylated chitosan inner layer, a substantially hydrophobic re-acetylated chitosan outer layer and a substantially hydrophilic de-acetylated chitosan porous support layer, wherein the substantially hydrophobic re-acetylated chitosan inner layer and the substantially hydrophobic re-acetylated chitosan outer layer are positioned to surround the substantially hydrophilic de-acetylated chitosan porous support layer. In particular, the substantially hydrophobic outer layer and inner layer of the membrane comprises pores of appropriate size and distribution to provide for gas separation.
The thickness of the substantially hydrophilic de-acetylated chitosan porous support layer is variable. In a specific embodiment, the thickness of the hydrophilic de-acetylated chitosan porous support layer may be essentially zero, resulting in the membrane being entirely composed of substantially hydrophobic re-acetylated chitosan.
A method for Salinity Gradient Power Vapor Pressure Desalination (SGP-VPD) generation using the multi-layer membrane is provided. The method includes, positioning the multi-layer membrane comprising a substantially hydrophobic re-acetylated chitosan inner layer, a substantially hydrophobic re-acetylated chitosan outer layer and a substantially hydrophilic de-acetylated chitosan porous support layer, under a salinity concentration gradient. The SGP-VPD method results in the extraction of both energy and drinking water from water sources having a high salinity concentration difference.
For a fuller understanding of the invention, reference should be made to the following detailed description, taken in connection with the accompanying drawings, in which:
Few biological polymers possess as high a number of amino groups as chitin, which provide for increased strength of the chitin-polymer matrix, increased hydrogen bonding between adjacent polymer layers and high adsorption properties leading to effective ion exchange capabilities. Serving as a natural structural biopolymer, chitin and its derivative chitosan, possess many interesting properties including unique crystalline structures, multidimensional properties, and nontoxicity and biodegradability in both the solution and solid-state phases Like cellulose, chitin is indigestible by vertebrate animals and forms extended fibers.
Chitin is not soluble in ordinary solvents. As shown in
Chitin exists in three different crystalline structural/polymorphic forms, referred to as α-chitin, β-chitin, and γ-chitin which differ in their degree of hydration, size of the unit cell and number of chitin chains per cell. α-chitin, the most common polymorphic form found in commercial chitin and chitosan, is frequently obtained from the large amount of available low-cost marine crustacean (e.g., lobsters, crabs, and shrimp) bio-waste. β-chitin is also available in reduced quantities from marine cephalopods (squid pen) bio-waste but can be obtained from other marine sources such as the crystalline fibrils of some microalgae (diatoms) and the tubes of vestimentiferans (giant undersea tube worms). γ-chitin is usually obtained from fungi and yeasts with the crystalline structure being a combination of the α- and β-forms. Chitin is highly acid resistant, and chitosan is highly alkaline resistant. These characteristics, that depending upon the end use application, can lend themselves well for use in separation membrane applications.
The —OH and —NH2 functional groups in chitosan facilitate an adsorbent function which has lent itself to numerous investigations as an adsorbent for the treatment of wastewater and the removal of heavy metals from liquid effluents and natural water by biosorption. The sorption capacity of chitin and chitosan materials depends on the origin of the polysaccharide, molecular weight (M), degree of N-acetylation, solution properties, and varies with crystallinity, affinity for water, and amino group content.
α-chitin has a very stable unit cell intra-chain, intra-sheet, and inter-sheet hydrogen bonds forming from antiparallel crystalline sheets, whereas the β-chitin unit cell consists of parallel sheets with weaker hydrogen bonds between two inter-sheets and reduced intra-sheet attraction. These structural changes lead to higher solubility, reactivity, and swelling ability towards solvents of β-chitin than α-chitin after alkali treatments which could alter the chitosan solution conformations and impact their antibacterial activity.
Owing to its unique crystalline structural arrangement, it has been reported that β-chitin more readily accepts intercalated water molecules than α-chitin. With the intra-crystalline swelling of β-chitin strongly anisotropic without modifications to the β-chitin sheets that are maintained by strong N-H···O═C intermolecular hydrogen bonds. Considering the reported intercalation of water molecules within its crystalline lattice and weaker intermolecular hydrogen bonding between sheets of parallel chains, β-chitin may possess differing and enhanced performance characteristics than α-chitin, with respect to diffusive water flux and ionic transport capabilities.
In various embodiments, the present invention provides a comparison of α-chitin, β-chitin to investigate and report on select physicochemical, colligative, and microstructural characteristics needed to substantiate the hypothesis of differing diffusive ion-transport and osmotic flow capabilities. The present invention additionally advances the multi-faceted synergistic goal of bio-waste management improvement and new market development by extending the consideration of possible chitosan biopolymer membrane uses to developing and sustainable technologies such as Salinity Gradient Power Vapor Pressure Desalination (VGP-SPD) and RO desalination.
Chitosan's physicochemical, rheological, and physical properties vary significantly as a function of its molecular weight characterization. The analytical technique frequently cited in the literature for the determination of chitosan's molar mass distributions; number-average molecular weight (Mn), weight-average molecular weight (Mw) distribution, and polydispersity (P D=Mw/Mn), is aqueous Gel Permeation Chromatography (GPC) Size Exclusion Chromatography (SEC). Knowledge of Mn is important for thermal properties (e.g., Glass transition, Tg), and Mw for tensile strength and impact resistance (i.e., mechanical properties).
Chitin is insoluble in water and common organic solvents and is usually converted to chitosan (deacetylated form of chitin) for use, with the extractability and degree of deacetylation (% DDA) dependent upon the conversion process used. When the % DDA approaches 50%, chitin becomes soluble in aqueous acidic solution through the protonation of the NH2 group and becomes chitosan. The presence of both amino and hydroxyl groups provides the chitosan macromolecule unique properties, which includes being easily dissolved in aqueous acetic acid of low concentrations and possessing a hydrophilic property which lends to solvent stability and water swelling.
In an exemplary embodiment, chitosan biopolymer membranes were prepared from shrimp shell (α-chitin) and squid pen (β-chitin) chitosan powder by solvent casting after which Physicochemical testing and Colligative water flux and ionic transport diffusion experiments were conducted using synthetic seawater in a side-by-side concentration test cell under differing salinity concentration gradients. Diffusion is the spontaneous, net movement of molecules of a substance from a region of high concentration to one of low concentration. Since the molecules are in thermal random motion, there will be more molecules moving from the high concentration region to the low concentration region, than in the opposite direction. There is no special force on the individual molecules and as such, diffusion is purely a consequence of statistics.
The functionality of linear polymers, such as chitosan, is highly affected by the % DDA and polymer size obtained during the conversion process. Typically, chitosan is obtained by the partial deacetylation of chitin in hot concentrated aqueous alkali (typically 40-50% NaOH for several hours) at 100° C.-160° C. for α-chitosan and at 80° C. for β-chitosan. This hydrolysis step removes some of the acetyl groups, resulting in differing amounts of acetylated units of N-acetyl-D-glucosamine (GlcNAc) and deacetylated units of D-Glucosamine (GlcN). The % DDA is defined as the molar fraction of GlcN units in the copolymer (chitosan) which is composed of GlcNAc and GlcN units. When the majority of GlcNAc units are converted to GlcN units (high % DDA), the polymer becomes highly soluble in dilute acids.
Examination of the measured FTIR (Fourier Transform Infrared) spectra can provide useful insight into the molecular characteristics as well as reveal any observed changes in the chemical bonds. % DDA was computed from the measured spectral data using Equation 1 and compared to the vendor supplied data, where A1655 and A3450 were the measured absorbance at 1,655 cm−1 (amine group) and 3,450 cm−1 (hydroxyl [OH] group), respectively.
% DDA=A1655/A3450×115 Equation 1
Using Equation 1, the computed FTIR % DDA values vs. Vendor supplied values are:
With reference to
GPC-SEC (Gel Permeation Chromatography and Size Exclusion Chromatography) is a liquid chromatography technique that separates macromolecules by their size in solution. Aqueous GPC-SEC separation is based upon differential migration between the stationary and mobile phases and governed by the hydrodynamic size and shape of the polymer chains relative to the size and shape of the porous pores within the column packing material. Summary data obtained from the aqueous GPC-SEC testing effort are presented in Table 1.
aNumber-Average molecular weight measured by gel permeation chromatography (GPC) using a mixture of 0.1M acetic acid and 0.3M sodium nitrate in HPLC grade water as the mobile phase at 35° C.
bPoly-dispersity (Mw/Mn).
c Refractive Index Increment (RII) (dn/dc) where values were calculated by assuming 100% mass injection recovery of the triplicate injections.
d Intrinsic Viscosity.
e Hydro-dynamic radius.
f Mark-Houwink.
In accordance with an exemplary procedure outlined below, α-chitosan and β-chitosan membrane test samples were made with the following casting constituents:
Resulting in a % Chitosan composition of nominally 2% (1.95%) α- and β-membranes prepared and evaluated.
Instant Oceans® Synthetic Sea Salt was used throughout this testing effort to provide a suitable medium without the deleterious effects of marine biofouling. The concentrated ionic test solution (Full Brine) was made from 300 grams of Instant Ocean® Sea Salt dissolved in enough DI water to make 1 liter of total solution. The dilute ionic test solution (1:10 Brine) was made by serially diluting 100 ml of the Full Brine solution to 1 liter with DI water. Runs consisted of either Full Brine or 1:10 Brine solution in the concentrated test cell chamber side and DI water in the dilute test cell chamber side. A summary of test configurations for each test solution type used in this analysis along with the measured electrically “loaded” cell potential voltage at osmotic equilibrium is presented in Table 2.
Samples obtained from the concentration test cell were analyzed using Inductively Coupled Plasma Mass Spectrometry (ICP-MS) instrumentation. To verify the applicability of the ICP-MS anion measurements for future use in the calculation of total osmotic pressure, a separate Cl− ion titration was done on each of the solution test samples for comparison. Discussion of both are presented herein.
Seawater contains dissolved salts at a total ionic concentration of approximately 1.12 mol L−1 (M) and a computed osmotic pressure at 25° C. of 27.2 atm. A salt is an electrically neutral ionic compound comprised of two oppositely charged ions; cations and anions. When a salt dissolves in water, it dissociates into its individual cations and anions. Seawater is nominally 86% sodium chloride (NaCl) with Na+ and Cl− almost completely dissociated. Every naturally occurring element that can be found on earth has been found dissolved in seawater. However, although present in measurable concentrations, there is a great variation in the concentration magnitudes of the ions present. According to chemical oceanographic convention, a concentration criterion of one part in a million (1 ppm or 1 mg/kg) has been established as the separation point. Elements with higher dissolved concentrations are referred to as major constituents and those below as minor constituents. These major ions are termed “conservative”, meaning that they occur in constant ratios to each other in almost all ocean (sea) water. As defined, there are 11 substances considered as major constituents: Na+, Mg2+, Ca2+, K+, Sr2+, Cl−, SO42−, HCO3−, Br−, F−, and B(OH)3. Na+, Mg2+, Ca2+, K+, Cl−, and SO42− make up >99% of the total dissolved constituents in seawater.
The ICP-MS is mainly used for elemental analysis of cations. Sulfate (SO42−) and bicarbonate (HCO3−) are polyatomic ions (not elemental) and are very difficult to measure with ICP-MS because the base elements of those ions, sulfur and carbon, along with fluorine, naturally form anions. Samples were initially run on an ICP-MS in semi-quantitative mode to identify what elements were present at concentrations that were easily measurable. The following 10 elements were mainly present: Na, Mg, Ca, K, Sr, Cl, Br, B, Li and Rb. Of these Na, Mg, Ca, K, Sr, Cl, Br, and B make up 8 of the 11 major elements found in seawater. The remaining 2 elements (Li and Rb) are considered minor constituents in seawater but were included with the other 8 in subsequent quantitative analyses because they are present at high enough concentrations to be easily measured by ICP-MS and are of frequent interest in seawater and seawater brine element recovery studies. Measured ICP-MS sample test results are presented in Table 3.
The ICP-MS is mainly used for elemental analysis of cations. Sulfate (SO42−) and Back-up concentration cell water sample Cl− ion titration testing began by serially diluting 1 ml of test sample to 100 ml with DI water and then adding it to a 250 ml beaker with magnetic stirring. Both electrodes were immersed in the solution and agitation began. Silver nitrate (AgNO3) was then added in 0.5 mL increments and both the volume of the titrant added, and the multi-meter value recorded on a spreadsheet after each addition. Using the acquired data, a second order differential potential curve was plotted to determine the titration end point and corresponding total volume of AgNO3 (VAgNO3) which was used along with the molarity (molar concentration) of the AgNO3 titrant (CAgNO3) (0.1 N for Full Brine based samples or 0.01 N for 1:10 Brine based samples or less) and the original test sample volume (VCl
CCl
Data obtained from both the Cl− ion potentiometric titration (CCl
Close examination of the results in
F
exp
=s
2
A/s
2
B Equation 3
H
o
:s
2
A
=s
2
B Equation 4
Pursuant to this, the value for: Fexp=(0.0016)2/(0.0010) 2=2.2945, and the critical value for F (0.05, 7.5) is 6.853. Because Fexp is less than F (0.05, 7, 5) we retain the null hypothesis and have no evidence for a significant difference between sA and sB, which means that the standard deviations of the 14 test samples can be pooled.
Visual examination of the corresponding measurement closeness presented in the
t
exp
=|μ−X|√n/SD Equation 5
H
o
:X=μ Equation 6
Pursuant to this, the value for: texp=(|0.0−(−0.0135)|√17)/0.0727=0.765, and the critical value for t (0.05, 16) is 2.120. Because texp is less than t (0.05, 16) we retain the null hypothesis and have no evidence for a significant difference between X=μ. Statistical based results from both two tailed F-test and the student's t-test support the use of the ICP-MS measurements for Cl− and Br− and the effectiveness of the ICP-MS methodology steps taken to minimize any carry over measurement effects.
Discussions on water and ionic transport diffusion and how it relates to osmotic pressure and osmotic equilibrium are presented herein.
The osmotic pressure, π, of a solution containing n moles of solute particles in a solution of volume V can be determined in rough approximation under dilute (ideal) conditions using the Van′t Hoff equation which obeys a form like the ideal-gas law:
ηV=nRT Equation 7
Where V is the volume of the solution, n is the number of moles of solute, R is the ideal-gas constant, and T is the temperature on the Kelvin scale. Equation 7 can be rewritten as:
π=(n/V)RT=MRT Equation 8
Where M is the molarity of the solution, expressed as the number of moles of solute per liter of solution, and the units of π are in atmospheres (atm). The ICP-MS provides individual ion concentrations in units of ppb which are converted to molarity and then summed together to determine the total solution molarity. According to the Van′t Hoff equation, an ideal solution containing 1 mole of dissolved particles per liter of solvent (1 M) at 25° C. will have an osmotic pressure of 22.2 atm.
Typical Cl− ion and water transport diffusion measurements across a casted nominal 2% β-chitosan membrane under an equalizing full brine/DI concentration gradient are presented in
Examination of
aICP-MS SD used for single measurement.
Examination of the Table 5 results reveal:
Using select data from the Table 2 run summary and Table 3 measured ICP-MS solution data, cross α-chitosan and β-chitosan membrane ion transport concentrations for Na, Cl, K, Mg, Ca, B, Br, Li, Sr, and Rb were calculated and presented in
Close examination reveals greater transport in the β-chitosan membrane over the α-chitosan membrane for monovalent Na, Cl, and K ions for both solution concentrations examined. These ions have larger crystal radii and weaker hydration shells which may enable easier detachment from their hydration layer while passing across the β-chitosan membrane with its weaker intermolecular hydrogen bonding between the sheets of parallel chains. Cross membrane ion transport also occurred for the remaining ions examined. However, with the exception of greater transport observed in the α-chitosan membrane over the β-chitosan membrane for the divalent Mg ion in the full brine solution, the closeness and SD overlap prevent an accurate prediction of any overall trend determination. Therefore, it was not possible to determine from the measured data if greater transport would also occur in the α-chitosan membrane over the β-chitosan membrane for the other divalent and trivalent ions tested. However, enough information was obtained to confirm the postulation that β-chitin may possess differing and enhanced performance characteristics than α-chitin with respect to diffusive water flux and ionic transport capabilities.
Using Equation 8 and measured ICP-MS solution data obtained from Table 3, an example calculation of the osmotic pressure and resulting osmotic equilibrium after t>20 hours is presented in Table 6.
Salinity Gradient Power (SGP) generation and/or separation process operations are possible market areas discussed herein for consideration for the chitosan-based membranes. The α-chitosan and β-chitosan membranes of the present invention possess a high water and ion flux permeability, when subjected to a difference in salinity gradient concentration that could be harnessed, as a potential thin film composite (TFC) membrane porous support layer for membrane filtration applications such as reverse osmosis (RO) desalinization, for the extraction of economically valuable materials from seawater or highly saline industrial fluids and in the reduction in the saline content of industrial and/or mining fluids for hazardous waste disposal in operations such as desalinization or hydraulic fracturing fracking.
Although numerous SGP solutions have been discussed in the literature, the most often cited technologies focus on variations of two existing water desalting membrane processes; pressure retarded osmosis (PRO) and reverse electrodialysis (RED), where a significant driving force in the industrial development of membranes already exists. PRO and RED utilize the electrochemical properties of solutions of differing saline concentrations (salinity) separated by charged semipermeable ion-exchange membranes.
In PRO, the osmotic process increases the volumetric flow of the high-pressure solution and is the energy transfer mechanism with the gross energy gain per unit membrane area equal to the product of the pressure difference multiplied by the volume flow of fresh water through the membrane. Key to PRO is the cost-effective manufacture of semi-permeable membranes with high water flux permeability and high salt retention (low salt flux).
In RED, anion exchange perm-selective membranes (AEM) and cation exchange perm-selective membranes (CEM) are alternately arranged to form a repeating unit called a cell. The basic RED stack consists of several hundred AEM/CEM cell pairs bound together between end electrodes (anode and cathode) with the driving electromotive force (EMF) in RED provided solely by the salinity concentration gradient. Voltages are generated across each membrane generated from the differences in chemical potentials of the salt ions found in the concentrated and dilute solutions with the back EMF of the transmembrane voltages' additive. Key to RED, also known as a dialytic battery, is the cost-effective manufacture of semipermeable ion-exchange membranes with high perm-selectivity (highly permeable for counter-ions but impermeable to co-ions).
In order to examine the suitability of the chitosan membranes of the present invention for PRO and/or RED operations it is necessary to examine both the water flux and ion transport characteristics from an osmotic process perspective. Examination of
Although the use of the substantially hydrophilic chitosan membranes tested herein alone would likely not be a good fit for either PRO or RED SGP operations, consideration was given for possible use in an electrochemical concentration fuel cell as part of a fuel cell membrane electrode assembly. Chitosan-based membrane electrolyte have been considered as an alternate candidate in the production of economical fuel cells. As shown in Table 3, both chitosan membranes revealed a nominal loaded membrane voltage potential of 0.6 mV under osmotic equilibrium conditions for either test solution concentration amount @ 100% relative humidity; corresponding to a power density of ˜1.5 nanoWatts/cm2 as tested. This contrasts to almost an order of magnitude lower than the ˜8.5 nanoWatts/cm2 power density previously measured by the author using Bipolar ion-exchange membranes in the same electrochemical test cell. To put these results into perspective for comparison purposes, according to the European Commission (EC) salinity power estimates, the first commercial 10 MW PRO SGP generation plants would need membranes capable of production of at least 0.6 mW/cm2.
A review of the recent literature revealed chitin films prepared with crab shell derived purified chitin using a group of enzymes obtained from Streptomyces griseus. The purified chitin slurry was dispersed in DI water with chitin sheets prepared by suction filtration. The proton conductivity of these films was examined in a traditional H2/Air fuel cell with the findings that the chitin becomes the electrolyte of the fuel cell in the humidified condition with a typical power density of 1.35 mW/cm2 at 100% relative humidity. It was deduced that the relation between the chitin hydrated structure and the proton conduction path formed by the hydrogen bond with the water molecule is significantly important and that these water molecules form hydrogen bonds between the hydroxyl and amino-acetyl groups.
It is important to mention that the electrical conduction method of the traditional Hz/Air fuel cell using proton-conducting cation permselective chitin sheets is different than that of the ˜90% DDA non-ion selective chitosan membranes in an electrochemical fuel cell considered herein. In addition, the partial deacetylation process used to convert chitin to chitosan removes some of the amino-acetyl groups which may contribute to the low energy density observed in the ˜90% DDA chitosan membranes evaluated herein. While it is possible that the energy density output of the electrochemical fuel cell will improve slightly upon using chitosan membranes with a lower % DDA value, it is unlikely that the necessary large-scale improvements in energy density from nanoWatts/cm2 to mW/cm2 for utility-scale generation purposes will be realized going solely from ˜90% DDA to the ˜50% DDA lower limits for chitin/chitosan conversion.
However, the chitosan-based membranes of the present invention having a slightly lower % DDA value may be used in energy scavenging applications including batteries, capacitors, and fuel cells for uses inside the human body where natural ion-exchange conditions are low across membrane voltages/currents exist.
Typical measurements of dry thickness and % Gel Swelling Index (GSI) for new/used membranes (using Equation 10 to follow), are presented as follows:
Examination reveals that although the dry thickness of the new β-chitosan membrane was more than for the new α-chitosan membrane, the % GSI value for the new β-chitosan membrane was less than the new α-chitosan membrane. Compare that to the used β-chitosan membranes which was lower in both dry thickness and % GSI than a used α-chitosan membrane. Owing to changes in the crystalline sheet orientation/lattice structure, degree of hydration, or the presence of any remaining intercalated water/ions. This result is also supported by visual/textual observations in which the used β-chitosan membrane physically felt thinner than and was not as stiff as when new.
SEM 10,000× (low resolution) and 50,000× (high resolution) images from a new piece of α-chitosan membrane are presented in
The 50,000× α-chitosan image with the larger cracks displayed was very unstable under the electron beam with the crack expansion occurring during observation. It is conjectured that the thinner α-membrane is breaking up under the hot electron beam as evidenced by the cracks being wider in the image center where the beam is more concentrated. This crack expansion was not observed on the 50,000× β-chitosan sample when imaged. No similar expansion was noted during observation on either of the 10,000× samples but any minor expansion would be harder to see at 10,000× vs. 50,000× so it is difficult to determine if the differences in the width of the crack between the two 10,000× images are real differences or reflect an instability problem (heating) caused by the differences in the membrane thickness.
Physicochemical and novel colligative investigations of alpha (α) and beta (β) chitosan membranes were conducted which confirmed that β-chitin may possess differing and enhanced performance characteristics than α-chitin with respect to diffusive water flux and ionic transport capabilities. The tested membranes possessed high water and ion flux permeability characteristics that could foster new market developments into separation process operations such as those used in the extraction of economically valuable materials from seawater or highly saline industrial fluids, the reduction in the saline content of mining fluids during dewatering, or during hazardous waste treatment and disposal operations.
The following paragraphs describe the experimental material and methods in accordance with various embodiments of the present invention.
Chitosan membranes were prepared from two commercially obtained sources; shrimp shells from Sigma-Aldrich Corporation, USA (CAS 9012-76-4; Sigma-Aldrich P/N C3646-25G) and squid pens from GTC Bio Corporation, Qingdao, China (SGC-2). The shrimp-based product was obtained as a white powder with a vendor supplied DDA value of 88%, and the squid-based product was obtained as a white powder with a vendor supplied DDA value of 91.7%. The viscosity of a solution of 1% chitosan (by weight) in 1% (by volume) aqueous acetic acid was provided by the vendor as 232 centipoise (cP) for the shrimp-based chitosan and <300 cP for the squid-based chitosan.
Reagent grade chemicals obtained and used include: glacial acetic acid (C2H4O2), glycerol (C3H8O3), sodium hydroxide (NaOH), nitric acid (HNO3), potassium bromide (KBr), silver nitrate (AgNO3), and sodium acetate (NaC2H3O2). Synthetic seawater was prepared using Instant Ocean® Sea Salt (Spectrum Brands, USA) dissolved in Milli-Q ultrapure (18.2 MΩ cm) water from a Millipore purification system.
Fourier-Transform Infrared (FTIR) spectrometry was used to determine the DDA and to examine any observed changes in intra-sheet or inter-sheet hydrogen bond characteristics of the α- and β-chitosan samples. % DDA results were then compared to the vendor supplied values. Chitosan powder was mixed with KBr (1:15) and pressed into a pellet. The spectrum was collected in transmission mode over a 400-4000 cm−1 range by placing the pellet in the beam path of a FTIR spectrometer (Nicolet Magna, USA). A total of 256 scans at 2 cm−1 resolution were averaged and corrected for background CO2 and water in a nitrogen purged compartment.
Aqueous GPC/SEC testing was conducted on a Viscotek TDA305 and GPCmax system, running OmniSEC 4.6.2 analysis software and configured for GPC/SEC triple detection analysis. The GPC/SEC system was equipped with a temperature-controlled oven housing four columns and three detectors: Refractive Index (RI), Right Angle and Low Angle Light Scattering (RALS/LALS), and a four-Capillary Differential Viscometer. In Triple Detection SEC/GPC, the RI detector is employed to calculate concentration, refractive index increment (dn/dc), and injection recovery. Light scattering provides absolute molecular weight while the viscometer delivers intrinsic viscosity (η), hydrodynamic radius (Rh), and conformational and structural parameters. SECs used were:
Standards at a concentration of 3 mg/ml and a 0.152 mL/g do/dc consisted of:
The mobile phase selected for use consisted of 0.1 M acetic acid and 0.3 M sodium nitrate mixture in HPLC grade water. Chitosan powder samples were dissolved in the mobile phase at a concentration of approximately 4.0 mg/mL (4.40 for Shrimp and 4.35 for Squid) and filtered through a 0.22 μm PES membrane syringe filter prior to injection. Injection parameters include: 100 μL injection, column temperature: 35° C., flow rate: 0.7 mL/min, run time: 60 minutes. Run summary consisted of triplicate runs with the verification standards injected at the end of the sample injections to verify detector calibrations.
The chitosan membrane solution was prepared by combining DI water, chitosan, and glacial acetic acid (casting solvent) in a 200 ml beaker and placed on a magnetic stirrer plate with moderate stirring for 48 hours at room temperature until thoroughly dissolved and clear. The solution was then heated to 60° C. and glycerol added as a plasticizer. After mixing for 15 minutes, the solution was removed from the heat for 30 minutes, followed by 1 hour under a 15-inch Hg vacuum to de-gas. After setting for 2 hours outside the vacuum chamber at ambient laboratory conditions (nominally 20-25° C., 40-55% RH air, standard pressure), a single membrane was cast by pouring the chitosan/glycerol solution onto a leveled 20.3×27.9 cm (8×11 inch) glass plate framed with strips of 0.635 cm (¼ inch) thick acrylic (methyl methacrylate). Water and acetic acid evaporation occurred under ambient conditions for at least 3 days under a ventilated flume hood, scored in half along the short side, and peeled from the casting surface. Since the as-cast membranes are completely soluble in water at this point, the dried membranes were placed in a 2% NaOH solution (10.05 grams of NaOH in 500 ml of DI water) for 30 minutes, and then washed extensively with DI water until neutral pH obtained. The neutralized and now insoluble membranes were stored in DI water until they were placed inside the concentration cell test fixture at the commencement of the water flux and ionic transport diffusion experiments.
The laboratory test apparatus consisted of a single, side-by-side concentration cell of cubic design with nominal outer dimensions of 10 cm×10 cm×7 cm, connected to a Vernier LabPro® sensor interface for remote data collection using Logger Pro 3 data-collection software. The test cell consists of end plates, electrodes made from #40 wire silver (Ag) mesh, two symmetrical test chambers (a concentrated solution side and a dilute solution side) and a single chitosan membrane under test, all separated by gaskets for sealing the cell and containing the liquid within. Inner test chamber nominal dimensions were 7 cm×7 cm×2.5 cm. A detailed description of the concentration test cell operation can be found in previous works by the inventor.
During each run, “loaded” cell potential voltage measurements were logged across the electrodes and a 500-ohm (nom.) resistor connected in parallel. Cumulative multi-species ion-transfer across the membrane was determined using ICP-MS analysis of samples selectively removed from the test cell at run completion. Visual evidence of the migration of water moving across the membrane from the dilute test chamber to the concentrated test chamber under direct osmotic flow was observed at ambient laboratory conditions. To accomplish this a manometer, constructed out of a piece of 0.635 cm (¼ inch) ID Tygon® tubing, was attached to the exit port of the concentrated solution side of the test chamber and secured vertically above the test cell with the other end of the tube open to ambient laboratory conditions. The exit port tube was examined for the presence of water and when observed its incremental height change recoded as it rose vertically in the tube until it stopped when isotonic (equal osmotic pressure) conditions were obtained in each chamber side.
Aqueous samples obtained from the concentration cell were diluted by a factor of 10-1000 with 2% nitric acid, except where concentrations were below the lowest calibration standard, in which case no dilution was performed. A small amount of internal standard solution containing Be, Sc, Ge, and Y was added to each sample in order to correct for instrumental drift during analysis. Prepared samples were analyzed with an Agilent 7500cx ICP-MS equipped with a concentric micro mist nebulizer, a double-pass quartz spray chamber, and a High Matrix Introduction (HMI) accessory. Samples were introduced into the ICP-MS via Tygon® tubing using an ASX-500 auto sampler. An external 6-point calibration curve was used to determine elemental concentrations. A 2% nitric acid solution was used as a blank and to rinse the instrument between samples. Samples were analyzed for Li, Na, Mg, K, Ca, Rb, and Sr at lower dilution factors (10 or 100). Because of their potential for carry over, Cl, B, and Br were analyzed separately at higher dilution factors (100 or 1000), along with an extended rinse time using both a 5% nitric acid solution and a 2% nitric acid solution. Additionally, a blank was analyzed after every standard and sample to minimize any carry over. Anions Cl− and Br− are typically not measured with the ICP-MS but because of their relative importance as major seawater constituents, Cl− 55.06% and Br− 0.173% total salt in seawater, their inclusion was important to this analysis. Evaluation of the published literature revealed the use of ICP-MS for the determination of Br− and analysis of Cl− from sweat for use in the diagnosis of cystic fibrosis. Because of the high concentrations of Cl− present in the samples, a separate Cl− ion titration was made on each test sample for ICP-MS comparison to ensure the validity of the ICP-MS measurement method and resulting values.
Chloride ion concentrations were determined by potentiometric titration with silver nitrate (AgNO3) using a converted dual electrode pH meter with agitation of the immersed electrodes achieved using a 120S Fisher Scientific magnetic stirrer. During titration a Fluke 8062A True RMS multi-meter was used to detect the change in potential between a Thermo Orion 9416BN Silver/Sulfide Half-Cell Electrode and a Thermo Orion 900200 Double Junction Reference Electrode. During the titration, the two electrodes were connected to the pH meter via the terminals used for the glass electrode and calomel electrode normally used in pH measurements.
When AgNO3 is slowly added to the Cl− ion containing synthetic seawater test sample, an insoluble precipitate of silver chloride (AgCl) forms according to Equation 9:
Ag+(aq)+Cl−(aq)→AgCl(s) Equation 9
The end point of the titration occurs when all the chloride ions are precipitated and is determined by the multi-meter reading at which the greatest change in voltage has occurred for a small and constant added increment of AgNO3.
Certain materials, including many biological membranes are semipermeable, meaning that when they come in contact with a solution, they selectively allow the passage of certain molecules or ions to cross the membrane while blocking others. Osmosis or osmotic flow refers to the net diffusional movement of solvent molecules across a semipermeable membrane under the effect of a concentration gradient toward the solution with the higher solute concentration. The only way to stop osmosis is to raise the hydrostatic pressure on the concentrated solution side of the membrane and achieve osmotic equilibrium. This can be done through the application of a suitable amount of external pressure, by letting the pressure build up via osmotic flow into an enclosed region, or in the case of our test chamber through the pressure difference resulting from the unequal vertical liquid height in the concentrated side exit port tube. The pressure required to achieve osmotic equilibrium and stop the net osmotic flow is known as the osmotic pressure.
Osmotic pressure along with boiling point elevation, freezing point depression, and vapor pressure depression are known as colligative properties that arise solely from the dilution of a solvent by non-volatile solutes. The word colligative comes from the Latin colligatus meaning to bind together. Colligative properties are physical properties of solutions that depend almost entirely on the total concentration of the dissolved species (ions or molecules) and not on the nature nor identity of the species present.
Dry membrane thickness and Gel Swelling Index (GSI) measurements were obtained from new/used pieces of the casted α- and β-chitosan membranes. Because of limited source availability, these pieces were obtained from the same manufactured batch but were not the same piece. The “used” pieces were the actual membranes used in the concentration test cell, subject to both transmembrane water and ion-transport, whereas the “new” pieces were batch remnants that were only exposed to DI water. New/used dry membrane thickness and GSI measurements were initiated by placing samples of each membrane into a desiccator and weighing them daily until there was no measurable change in weight as compared to the prior measurement. After which a final weight was recorded, as well as, a dry thickness measurement using a dial caliper. The samples were then placed in DI water for 24 hours, after which they were removed, wiped with a dry tissue, and weighed. This procedure continued until there was no measurable change in weight as compared to the prior measurement. After which a final weight was recorded and the GSI computed using Equation 10.
GSI=[(wet weight−dry weight)/(dry weight)]*100% Equation 10
Comparable visual evidence of surface deformation and overall shrinkage was present after drying, especially in the “used” pieces.
A small sample from each of the cast membranes was mounted on an aluminum stub and coated with a thin layer of gold/palladium metal. It was then imaged at two different magnifications (10,000× and 50,000×) using a Hitachi S-3500N variable pressure scanning electron microscope (SEM) with a resolution of 3 nm.
As previously described, chitin is highly hydrophobic with limited solubility in common organic solvents. Successful directly produced chitin film or fiber production and application has been limited due to finding suitable and convenient solvents and manufacturing procedures that will not dissolve or functionally degrade the polymer's molecular weight. Chitosan, the deacetylated product of chitin, is readily soluble in dilute acidic medium below a pH of 6.5, trends more hydrophilic with high % DDA and can be produced with varying pore sizes. However, chitosan's increased solubility can reduce its long-term resistance to moisture degradation and thus the overall integrity of chitosan films or fibers can be more easily compromised than chitin depending upon the conditions of use. Pursuant to this, methods have been developed to selectively reverse the moisture degradation process through re-acetylation of the chitosan films or fibers to restore them back to chitin. For example, re-acetylation of the chitosan may be accomplished with acetic anhydride or using Chitosonium acetate at elevated temperatures. The level of re-acetylation of the chitosan is dependent upon the procedure used and the time in process. This allows for its potential use as both a hydrophobic or more hydrophobic trending (but still hydrophilic) membrane layer.
In addition to the amorphous chitosan flat films previously tested and described herein, chitosan can also be used to form solid and hollow fibers through various wet-spinning processes, with all forms suitable for use in flat channel, hollow-fiber, or spiral would membrane module configurations. Chitin is hydrophobic, whereas chitosan becomes hydrophilic with high levels (greater than about 90%) of DDA. Chitosan re-acetylation enables the making of a completely amorphous chitin/chitosan TFC membrane of asymmetric structure comprising both amorphous chitin and chitosan portions. Thus, enabling chitin (re-acetylated chitosan), or other suitable hydrophobic material, as a dense outer microporous skin layer possessing suitable pore size and distribution for water vapor gas separation and chitosan (deacetylated chitin) as an interior porous support layer. The resulting re-acetylated amorphous chitosan films (or fibers) can then serve as the dense outer amorphous microporous hydrophobic chitin layer in a completely amorphous chitin/chitosan TFC membrane assembly for SGP generation.
In Salinity Gradient Power Vapor Pressure Desalination (SGP-VPD) operation, both energy and drinking water can be extracted from specially configured membrane contactors using the water vapor pressure difference between water of low salinity and high salinity. In general, a membrane contactor is a membrane separation device that allows a gas phase and a liquid phase to be in contact with each other in order to promote mass transfer between the two phases through a membrane without dispersion of one phase within another. The separation of compounds is accomplished due to a specific driving force through the membrane from one phase to the other on opposite sides. The membrane separation device can be realized through various embodiment, including, but not limited to, a series of flat channel membranes housed in a cubic or spiral wound module configuration, or a series of hollow-fiber members housed in a cylindrical axial tube module.
An embodiment of an exemplary SGP-VPD membrane contactor in accordance with the present invention is illustrated in
Low salinity water may include fresh or brackish water. High salinity water may include seawater or bine, which typically has a salt concentration about 10 times greater than seawater. SGP-VPD involves mass transfer of “gaseous” water vapor driven under a salinity gradient across a microporous membrane. Consequently, a critical prerequisite for successful SGP-VPD operation is the ability of the membrane to sustain a gas phase between the pores at the operation liquid pressures. Very important properties include the non-wettability of the membrane material (hydrophobic) as well as a suitable pore size and distribution require for water vapor gas separation.
For example, as shown in
In the amorphous chitin/chitosan SGP-VPD TFC membrane contactor arrangement of the present invention, the gaseous and liquid phases are separated by a liquid tight semipermeable membrane having a pore size and distribution suitable for water vapor gas separation which does not influence the selectivity of the process and whose only function is to provide a liquid tight barrier between the two phases. In operation, the feed flows to the membrane surface where the water is vaporized close to the surface pores and then diffuses as a gaseous vapor through the pores of the membrane. The resulting salinity gradient across the membrane conveys a partial pressure difference ensuring that the water vapor developing at the membrane surface follows the pressure drop, permeating through the membrane via the pores where it condenses and collects. Because of the existence of moisture adsorption and desorption at the membrane surfaces, heat will be transferred through the membrane, which includes not only the convection heat but also the adsorption heat due to the mass transfer, which can be assumed to be equal to the Latent Heat of Vaporization (LHV) of water.
Once through the membrane, water vapor is absorbed into the brine resulting in a release of the LHV via condensation. Sensible heat conduction will occur through the surface of the membrane. Both heat additions will elevate the temperature of the brine, raising the vapor pressure and reducing further the rate of water vapor transfer. Moreover, vapor production over the fresh water will extract LHV from the fresh water (evaporation) reducing its temperature and vapor pressure. In order to keep both liquid input streams (feed and permeate) at the same temperature, necessary for maintaining the maximum delta water vapor pressure driving force, the LHV absorbed by the water vapor condensing interface side (brine—permeate—getting warmer) must be removed from and added to the water vapor evaporating interface side (lower salinity—feed— getting cooler) to offset the LHV that was removed from the evaporating interface (lower salinity—feed) due to water vapor production. The condensed moisture on the permeate side is then collected for drinking water use.
In order to maintain near temperature equilibrium, some of the power generated by the water vapor difference will need to be fed back into the system as heat, consequently lowering the overall efficiency. To minimize this, an overall heat exchange methodology is needed to equalize the operating temperature of both input streams and to collect the moisture accompanied by the adsorption and desorption of water vapor at the permeating membrane surface. This is envisioned best configured, but allowing for other designs, as hollow fiber membrane contactors housed within a tightly packed shell with membrane and system optimization via items such as:
As such, the present invention provides for a physicochemical and colligative investigation of α-chitosan and β-chitosan membranes that was conducted with a focus on concentration gradient driven water flux and ion transport for SGP generation and separation process operations. Physicochemical and colligative comparisons are presented to provide necessary details in order to foster new market developments and continued improvements in the responsible bio-waste management of this valuable marine resource. Additionally, the present invention provides for membranes comprising re-acetylated chitosan for use in RO and SGP configurations.
The advantages set forth above, and those made apparent from the foregoing description, are efficiently attained. Since certain changes may be made in the above construction without departing from the scope of the invention, it is intended that all matters contained in the foregoing description or shown in the accompanying drawings shall be interpreted as illustrative and not in a limiting sense.
This application claims priority to and is a continuation-in-part of U.S. patent application Ser. No. 17/527,223, filed Nov. 16, 2021 and entitled, Chitosan Based Membrane and Associated Method of Use”, which claims priority to PCT International Patent Application No. PCT/US2020/034223, filed May 22, 2020 and entitled, “Chitosan Based Membrane and Associated Method of Use”, which claims priority to U.S. Provisional Patent Application No. 62/851,432, filed on May 22, 2019 and entitled, “Chitosan Based Membrane and Associated Method of Use”, the entirety of which are incorporated herein by reference.
| Number | Date | Country | |
|---|---|---|---|
| 62851432 | May 2019 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 17527223 | Nov 2021 | US |
| Child | 18473467 | US | |
| Parent | PCT/US2020/034223 | May 2020 | US |
| Child | 17527223 | US |
