Patent ID: 12227626

SUMMARY OF THE INVENTION

Accordingly, present invention provides a homogeneous anion-exchange membrane having repeating unit of formula 1,

In an embodiment of the present invention, the membrane has an ion-exchange capacity is in the range of 1.00 to 1.70 meq/g.

In another embodiment of the present invention, the membrane has conductivity in the range of 3.0-6.0×10−2S cm−1.

In yet another embodiment of the present invention, the membrane exhibits swelling ratio in the range of 5-10% under the treatment of hot water at temperature in the range of 60-65° C. for a time period of 24-36 hours.

In yet another embodiment of the present invention, a membrane weight, an ion-exchange capacity and a conductivity loss is less than 4% under alkaline environment) or harassed oxidative environment.

In yet another embodiment of the present invention, the alkaline environment is achieved by 2.0 M NaOH at temperature in the range of 60-65° C. for time period in the range of 120-150 hours; and the harassed oxidative environment is achieved by 3 ppm+3% H2O2at temperature of 70° C. for 1-3 hours

In yet another embodiment, the present invention provides a process for the preparation of anion-exchange membrane, comprising the steps of:i. adding 1-vinyl imidazole and N-isopropyl acrylamide to a dimethyl acetamide in a vessel under constant stiffing and nitrogen environment at a temperature in the range of 25 to 30° C. to obtain a solution;ii. charging the solution as obtained in step (i) with radical initiator azobisisobutyronitrile (AIBN) at temperature in the range of 90-95° C. for time period in the range of 24 hours with stirring to obtain isopropylacrylamide-co-vinylimidazole (IA-co-VI) copolymer solution;iii. mixing poly(vinylidene fluoride-co-hexafluoropropylene) [PVDF-co-HFP] and dimethyl acetamide (DMAc) in a ratio ranging between 1:5 (w/v) for time period in the range of 14 hours to obtain a solution;iv. mixing both the solutions as obtained in step (ii) and (iii) with stirring at temperature in the range of 75-95° C. for a period in the range of 12 hours to get a membrane forming polymer solution;v. casting of thin film membrane with the solution as obtained in step (iv) followed by drying at temperature in the range of 60-80° C. for period in the range of 24-30 hours under vacuum oven to obtain a membrane;vi. quaternizing the membrane as obtained in step (v) by dipping in 10 wt % of methyl iodide solution for time period in the range of 24-30 hours at a temperature in the range of 30-40° C. to introduce a quaternary ammonium group in a membrane matrix;vii. washing the membrane matrix as obtained in step (vi) followed by converting into hydroxide form by immersing in a sodium hydroxide solution to obtain the anion exchange membrane.

In yet another embodiment of the present invention, the weight ratios of N-isopropylacrylamide and 1-vinylimidazole is in the range of 2:0.5 to 2:1.5.

In yet another embodiment of the present invention, the dimethyl acetamide is mixed with the isopropylacrylamide-co-vinylimidazole copolymer in the ratio of 1:10 (w/v).

In yet another embodiment of the present invention, the ratio of isopropylacrylamide-co-vinylimidazole (IA-co-VI) copolymer and PVDF-co-HFP copolymer ranges from 1.0-1.5:0.5-0.7 (w/w).

In yet another embodiment of the present invention, wherein the anion-exchange membrane has 1.26 meq/g anion-exchange capacity.

In yet another embodiment of the present invention, wherein the anion-exchange membrane showed 3.66×10−2S cm−1hydroxide ion conductivity.

In yet another embodiment of the present invention, wherein the anion-exchange membrane showed about 8 to 10% swelling ratio (under treatment of hot water at 60° C. for 24 hours).

In yet another embodiment of the present invention, wherein the anion-exchange membrane exhibited good oxidative stability with about 5% loss in weight, ion-exchange capacity and conductivity after treatment under harassed oxidative environment (3 ppm FeSO4+3% H2O2at 70° C. for 3 h).

In yet another embodiment of the present invention, wherein the anion-exchange membrane showed good alkaline stability (in 2.0 M NaOH at 60° C. for 5 days) due to absence of β-hydrogen, and reduced nucleophilic substitution reaction because of steric hindrance.

In yet another embodiment of the present invention, wherein functional charged density of the anion-exchange membrane can be controlled by weight ratio of copolymer solution in the membrane forming material.

In yet another embodiment of the present invention, the interpolymerisation of isopropylacrylamide-co-vinylimidazole copolymer and poly(vinylidene fluoride-co-hexafluoropropylene) (PVDF-co-HFP), formed homogeneous dense membrane without any phase separation because of H-bonding.

In yet another embodiment of the present invention, wherein vinylimidazole-co-isopropylacrylamide copolymer was prepared in the presence of initiator (AIBN) by free radical polymerization.

In yet another embodiment of the present invention, wherein isopropylacrylamide-co-vinylimidazole copolymer provides active site for the successful attachment of quaternary amine groups.

In yet another embodiment of the present invention, wherein any anion-exchange functional group (phosphonium and sulfonium, etc.) may be grafted with isopropylacrylamide-co-vinylimidazole copolymer to achieve good conductivity.

In yet another embodiment of the present invention, wherein chemical structure of isopropylacrylamide-co-vinylimidazole copolymer is similar to formula 2.

In yet another embodiment of the present invention, wherein polymer (PVDF-co-HFP) with chemical structure similar to formula 3, provides highly stable fluorinated polymer back bone and thus stability to the anion-exchange membrane.

In yet another embodiment of the present invention, wherein anion-exchange membrane with high functional charge density exhibited reduced cell voltage and improved current efficiency during electrodialysis because of grafted functional (quaternary ammonium or phosphonium) groups with fluorinated polymer.

In yet another embodiment of the present invention, wherein anion-exchange membrane with high functional charge density exhibited improved current efficiency followed by power density during fuel cell application because of grafted functional (quaternary ammonium or phosphonium) groups with fluorinated polymer.

In yet another embodiment of the present invention, wherein anion-exchange membrane according to the present invention showed high efficiency during Cu—Cl cycle for hydrogen production by electrolysis.

In yet another embodiment of the present invention, the anion-exchange membrane exhibit high efficiency during electrodialysis, fuel cell or Cu—Cl cycle and other electro-membrane applications, followed by superior stabilities (thermal and acid). Thus, the industrial significance of the anion-exchange membrane of the present invention is extremely high.

In yet another embodiment of the present invention, wherein anion-exchange membrane with high functional charge density exhibited improved alkaline stability which is desirable condition for fuel cell application.

DETAILED DESCRIPTION OF THE INVENTION

The present invention disclosed fluorinated-aliphatic hydrocarbon based alkaline resistant anion-exchange membrane, its method of preparation and its subsequent application in various electrochemical processes.

The present invention relates to the development of polymeric anion-exchange membranes for electrodialysis to separate the inorganic salt content from water, alkaline fuel cell for energy devices and membrane electrolysis or other electrochemical applications. The anion-exchange membrane of this invention showed good thermal and chemical stabilities (oxidative and alkaline), excellent hydroxide conductivity, perm-selectivity, current efficiency, current density, power density and other physicochemical properties such as water uptake and ion-exchange capacity which are necessary condition for high performance of prepared anion-exchange membrane during diversified electro-membrane applications in different media. The methods used to produce reported anion-exchange membrane is pretty easy and less expensive in compare to the commercialized anion-exchange membrane. This less expensive part of anion-exchange membrane contribute to the overall economy of the process using these ion-exchange membranes. The invention also contains the use of the reported membrane for variety of electro-membrane applications.

In present invention, the synthetic method opted for the preparation of anion-exchange membrane includes the following steps:i. preparation of isopropylacrylamide-co-vinylimidazole copolymer via free radical polymerization in DMAc solvent and presence of AIBN initiator;ii. solution preparation of PVDF-co-HFP (known weight %);iii. Preparation of interpolymer of isopropylacrylamide-co-vinylimidazolecopolymer and PVDF-co-HFP in DMAc under constant stirring to effect the hydrogen bonding;iv. membrane thin casting, drying and quternization with methyl iodide solution.

Further the degree of quaternization i.e. the quotient of the total number of quaternary ammonium group present in membrane matrix can be controlled by adjusting the molar ratio of 1-vinylimidazole and volume of methyl iodide. This adjustment regarding degree of functionalization/quaternization will help in adjusting the lowered water uptake or swelling ratio followed by balanced conductivity which is necessary or highly preferable condition for any electrochemical applications. Moreover the reported strategy will help in homogenous formation of membrane due to strong hydrogen bonding interaction between copolymer and polymeric chain. Further the present invention is a green method to prepare the anion-exchange membrane wherein we tried to avoid the use of hazardous material in comparison to other anion-exchange membrane preparative routes. Further the manufacture of present invention anion-exchange membrane is very inexpensive which make it an ideal candidate for numerous applications in varieties of fields.

In present invention, highly basic, oxidative or alkaline stable anion-exchange membrane was prepared using isopropylacrylamide-co-vinylimidazole copolymer and PVDF-co-HFP solution in DMAc. Prepared membrane thin film was quaternized using methyl iodide, to prepare the anion-exchange membrane, according to theFIG.1.i. Known amount of 1-vinyl imidazole, and N-isopropyl acrylamide, were added to known volume of dimethyl acetamide, in a vessel under constant stirring in nitrogen enviroment at 30° C.;ii. solution obtained in step (i) was charged with radical initiator azobisisobutyronitrile (AIBN) at 90° C. and stirred vigorously for 24 h;iii. solution preparation of poly(vinylidene fluoride-co-hexafluoropropylene) in dimethyl acetamide (known weight %);iv. mixing of both solution obtained in step (ii) and (iii) under continuous stirred conditions 90-95° C. for 24 h, to get the membrane forming solution;v. casting of thin film membrane and drying at 60-80° C. for 24 h under vacuum oven;vi. quaternization of membrane by dipping in 10 wt % of methyl iodide solution for 24 h to introduce the quaternary ammonium group in membrane matrix.vii. washing of membrane and conversion to hydroxide form by immersing in 0.1 M sodium hydroxide solution.

In the preparation of anion-exchange membrane, the weight ration of isopropylacrylamide-co-vinylimidazole copolymer and PVDF-co-HFP, was 5:3, while polymeric solution weight percentage was 20%, w/v in DMAc, to achieve homogeneous membrane. Resultant polymer solution was transformed into thin film of desired thickness and dried under vacuum at 60-80° C. for 24 hours to achieve the membrane. Obtained membrane was dipped in methyl iodide (10 wt % in methanol) for 24 hours, to quaternize the vinyl imidazole moiety. Such a reaction scheme for the preparation of anion-exchange membrane is illustrated inFIG.1.

In the present invention, the process for the preparation of stable anion-exchange membrane represents a novel and simple method with several advantages over the previously reported method of lower cost, without any use of hazardous chemicals. Further, in the reported strategy, functional group (quaternary ammonium group) density can be controlled by controlling isopropylacrylamide-co-vinylimidazole copolymer content in PVDF-co-HFP matrix.

In the present invention, polymer thin film anion-exchange membrane without any fabric (woven) support has been reported. The membrane forming polymer solution possessed the thin film forming capacity and resultant membrane showed high mechanical stability and burst strength. Further, reported anion-exchange membrane can be prepared with non-woven support. Additionally, unlike radiation grafting techniques, the present composite anion-exchange membrane was prepared using interpolymer PVDF-co-HFP and isopropylacrylamide-co-vinylimidazole copolymer, in the presence of free radical initiator. Thus, membrane production technique does not involve and high-energy radiation source.

Numerous electro-membrane processes for water desalination, electro-separation, membrane electrolysis, alkaline fuel cell, and storage battery etc. were developed using anion-exchange membrane. In these applications, cost-effective nature, high permeselectivity, high conductivity and stable nature even in strong alkaline or oxidative environment of anion-exchange membranes are urgently required. Further, prepared anion-exchange membrane may be widely used for membrane electrolysis, fuel cell and battery applications in different medium. Different electrochemical processes such as desired synthesis, electro-deionization, electrodialysis for the removal of inorganic electrolyte, desalination of sea and brackish water, separation and removal of metal ions from the industrial effluent, de-acidification of fruit juice, dashing and sugar cane juice even at high temperature (70-80° C.) for better quality of sugar, purifications and amino acids, vitamins, vaccines and other biochemical purification and down-stream processing of fermentation broth, etc. can be achieved by stable anion-exchange membranes.

Optimum water content in the membrane phase governs hydration of quaternary ammonium functional groups and provide the necessary water molecules for the formation of hydrophilic ion conducting channels, which is responsible for the improved hydroxide conductivity. Further, high water content in the membrane phase causes membrane dimensional instability. Thus, to achieve the stable anion-exchange membrane, an optimized water content (20-30%, w/w) is essential. In the present invention, the proper care to balance the hydrophobic and hydrophilic segments in the membrane forming material has taken, which will enables the desired water content in the membrane matrix.

The ion-exchange capacity (IEC) represents a measure of the hydrophilic character or concentration density of fixed quaternary ammonium groups, and can be measured by meq./g or dry membrane. Density of exchangeable groups in the membrane matrix is also an important factor that controls membrane performance. However, membrane durability depends upon the environmental conditions and polymer backbone nature. All these factors were judicially considered during membrane synthesis. One skilled in the art based upon prior knowledge and description provided above should easily determine the membrane preparation procedure and parameters with specifically desired anion-exchange membrane.

The membrane perm-selectivity is a measure of the characteristic difference in the membrane permeability for counter-ions and co-ions. Counter ion transport number across the membrane was estimated by membrane potential measurement for the estimation of membrane perm-selectivity.

Membrane conductivity of anion-exchange membrane was determined in equilibration with 0.10 M NaCl solution using a potentiostat/galvanostat impedance analyzer. The membrane resistance was determined from Nyquist plots by Fit and Simulation method and considering membrane thickness and area membrane conductivity was estimated.

For these wide applications, the most desired properties required for successful development of anion-exchange membranes are: high permselectivity (close to unity)-anion-exchange membrane should be highly permeable for anion with selective impermeability to cation; high membrane conductivity-anion-exchange membrane should have high membrane conductivity responsible for low potential drop during electrodialysis or electro-membrane processes; good mechanical stability of the membrane should be mechanically strong and should have a low degree of swelling or shrinking in transition from dilute to concentrated ionic solutions; high chemical stability of the membrane should be stable in strong acidic or alkaline environment even in presence of oxidizing agents. Many previous membranes have either exhibited poor stabilities (thermal, chemical and mechanical) or have obtained it at expense of electrochemical properties. For, example cross-linking of the membrane film improves thermal and mechanical properties, but associated with deterioration in functional groups (acidic or basic) concentration thus electrochemical properties. Mechanical strength can be further increased by supporting the membrane by woven fabric (PVC, PE, glass or Teflon). But woven fabric contributes towards the non-conduction phase of the membrane matrix and reduces membrane physicochemical and electrochemical properties.

EXAMPLES

Following examples are given by way of illustration and therefore should not be construed to limit the scope of the invention.

Examples 1-3

General Procedure for the Preparation of Fluorinated-Aliphatic Hydrocarbon Based Stable Anion-Exchange Membrane

The N-isopropylacrylamide (12.5 gm) and 1-vinylimidazole (6.7 gm) (2.0:1.0 weight ratio) were added to dimethylacetamide (100 ml) under stirred conditions in nitrogen environment at 30° C., afterward 2,2′-azobis(2-methylpropionitrile) (AIBN) (2 ml) was added and reaction mixture was stirred for 24 h at 90-95° C. for the preparation of isopropylacrylamide-co-vinylimidazole (IA-co-VI) copolymer. In a separate conical flask, PVDF-co-HFP (12.5 gm) was dissolved in dimethylacetamide (60 ml) of under constant stirring for 14 h or till complete dissolution. The clear solution of isopropylacrylamide-co-vinylimidazole copolymer was mixed with PVDF-co-HFP solution, and reaction mixture was stirred for 12 h at 90-95° C. To prepare different anion-exchange membranes, weight ratios of N-isopropylacrylamide and 1-vinylimidazole was varied between 2.0:0.5-1.5, and resultant three anion-exchange membranes with 2.0:0.5; 2.0:1.0, and 2.0:1.5, were prepared. Obtained viscous solution was poured onto a clean glass plate, and a thin polymer of constant thickness (150 μm) was formed using a doctor-blade. Membrane thin film was dried at 60-80° C. in a vacuum oven.

Obtained membrane was washed with deionized water and dipped in methyl iodide solution (10 wt % in methanol) for 24 hours at 30° C. Resultant membrane was post-treated with NaOH (0.10 M) and subsequently in deionized water. The properties of three different anion-exchange membranes are included in Table 1.

TABLE 1Composition and properties of acid and oxidativeresistant anion-exchange membraneWeightratio ofIA-co-VIcopolymer:Ion-MembranePVDF-Waterexchangeconductivityco-HFPuptakecapacity(×10−2SwellingExample(w/w)*(%)(meq/g)S cm−1)ratio (%)12.0:0.511.21.023.016.222.0:1.013.71.133.427.532.0:1.515.01.353.908.4*Mechanical stability of all membranes was excellent.

Examples 4-6

General Procedure for Oxidative Stability of Anion-Exchange Membrane

Under strong oxidative water splitting environment, membrane degradation by oxy active radicals is a serious issue. Thus, oxidative stability of anion-exchange membranes was assessed under simulated oxidative conditions (3 ppm FeSO4+3% H2O2at 70° C. for 3 h).

The oxidative stability for different fluorinated-aliphatic hydrocarbon based anion-exchange membranes was confirmed by recording percentage loss in membrane weight, ion-exchange capacity, and conductivity data after the treatment and included in Table 2.

TABLE 2Oxidative stability of different anion-exchange membranes in terms ofloss in membrane weight (Wloss), ion-exchange capacity (IECloss),and membrane conductivity (κlossm) after oxidative treatment.Weight ratioof IA-co-VIcopolymer:PVDF-κlossmco-HFPWlossIECloss(×10−2Example(w/w)*(%)(meq/g)S cm−1)42.0:0.51.62.44.152.0:1.02.42.64.362.0:1.52.72.94.9

Examples 7-9

General Procedure for Alkaline Stability of Anion-Exchange Membrane

The alkaline stability of different anion-exchange membranes was tested in 2.0 M NaOH solution at 60° C. for 5 days. The membrane alkaline stability was estimated in terms of percentage loss in membrane weight, ion-exchange capacity, and conductivity after alkaline treatment and relevant data are included in Table 3 for anion-exchange membranes.

TABLE 3Alkaline stability of different anion-exchange membranes in terms ofloss in membrane weight (Wloss), ion-exchange capacity (IECloss),and membrane conductivity (κlossm) after alkaline treatment.Weight ratioof IA-co-VIcopolymer:κlossmPVDF-co-IECloss(×10−2ExampleHFP (w/w)*Wloss(%)(meq/g)S cm−1)72.0:0.52.93.63.882.0:1.03.53.94.492.0:1.53.94.34.9

Example 10

Desalination of Brackish Water Using Anion-Exchange Membrane by Electrodialysis

Brackish water may or may not be chlorine dosed is provided as drinking water (total dissolved solid: <500 ppm) after desalination by electrodialysis. The brackish water may obtained either from earth surface or from ground, passed through chlorine-dosing or other treatment and to the electrodialysis desalination unit to remove excess of salt.

An electrodialysis (ED) unit containing 10 cell pairs of anion-exchange membrane (2.0:1.5; weight ratio of IA-co-VI copolymer) and cation-exchange membrane (CEM) (AMX supplied by Tokuyama Soda Co. Ltd., Japan); structure properties: poly(styrene)/divinyl benzene; ion-exchange capacity: 1.5 meq/g; water uptake: 26%, area resistance: 3.2 Ω cm2) with 100 cm2effective membrane area was used desalination of brackish water. There was four compartments in ED unit, namely two electrodes wash (EW), concentrated stream (CS) and desalinated stream (DS) (FIG.2). Precious metal oxides (titanium-ruthenium-platinum) coated TiO2sheets of 6.0 mm thickness, obtained from Titanium Tantalum Products (TITAN, Chennai, India) were used as electrodes fitted in the ED unit. Flow arrangement of each compartments was monitored by parallel-cum-series pattern. Na2SO4solution (0.10 M) was recirculated in both interconnected EW compartments. Initially, brackish water (total dissolved solid (TDS): 2000-5000 ppm) was fed into DS (flow rate: 2.0 LPH) and CS ((flow rate: 0.6 LPH), both using peristaltic pumps. ED experiments were performed under influence of constant voltage (15.0 V) using a direct current power supply and resultant current was recoded. With progress of experiment TDS of DS was reduced to <500 ppm (drinking water as per World's Health Organization), while TDS of CS was significantly increased. The recovery of desalinated water was about 65%.

Example 11

Alkaline Fuel Cell Application Using Anion-Exchange Membrane by Electrodialysis

Suitability of prepared anion-exchange membrane (2.0:1.5; weight ratio of isopropylacrylamide-co-vinylimidazole (IA-co-VI) copolymer) for application in alkaline fuel cell was assessed. Membrane electrode assembly (MEA) was fabricated by following the technique where we consider three-layer structure, contains (anion-exchange membrane, anode/cathode catalyst layer and diffusion layers). Further the wet carbon coated with 10 wt % of IA-co-VI/PVDF-co-HFP copolymer solution by brush painting method was used. The gas diffusion layer (GDL) (25 cm2) geometric area) was fabricated by coating slurry of 0.50 mg/cm2consisting of carbon black (Vulcan XC72R) and IA-co-VI/PVDF-co-HFP copolymer dispersion on carbon paper. The Pt loading in both the anode and cathode was 0.4 mg/cm2. Thus, the developed electrode was cold pressed membrane followed by curing at 60° C. for 12 h and then hot pressed at 130° C. for 3 min at 1.2 MPa. The MEA was achieved by hot pressing an electrode/membrane/electrode sandwich at a temperature of 100° C. for 3 min at 1.0 MPa. The MEA was assembled into a single cell (FC25-01 DM fuel cell), 1.0 M MeOH in 2 M NaOH was used as a fuel at anode and air at the cathode and fed with 5 ml min-1 and 100 ml min-1 respectively to record the current-voltage polarization curves with the help of an MTS-150 manual fuel cell test station (ElectroChem Inc., USA). The single cell performance was carried with developed anion-exchange membrane at 60° C. The prepared anion-exchange membrane (2.0:1.5; weight ratio of IA-co-VI copolymer) showed 150 mA/cm2of current density and 120 mW/cm2of power density at cell voltage of 0.79 V. This suggests the potential candidature of prepared anion-exchange membrane for fuel cell application.

Example 12

Cu—Cl Cycle for Membrane Electrolysis Using Anion-Exchange Membrane

The Copper-Chlorine (Cu—Cl) cycle involving thermochemical water splitting is a promising method for large-scale hydrogen production using nuclear, solar or other thermal energy sources. It offers significant advantages over other thermochemical cycles such as relatively lower temperature operating requirements (below 550° C.) as compared to high temperature cycles that work at >750° C. and the ability to effectively utilize low-grade waste heat for endothermic processes. The performance of anion-exchange membrane (2.0:1.5; weight ratio of IA-co-VI copolymer) was evaluated in electrochemical cell, schematically presented inFIG.3. The electrochemical cell with 800 ml capacity was designed and fabricated using platinum as anode as specified above (D=5.5 cm, surface area=33.17 cm2) and dense pure copper rod (D=0.7 cm, H=6.5 cm surface area=14.29 cm2) as cathode. The anion-exchange membrane was fixed in vertical position between two flanges. The anolyte and catholyte compartments made up of acrylic were separated using anion-exchange membrane. A Masterflex peristaltic pump, L/S 600 rpm Digital Drive with two pump heads of L/S Easy-Load 3 SS was used to circulate anolyte and catholyte.

The performance of anion-exchange membrane (2.0:1.5; weight ratio of IA-co-VI copolymer) assessed under optimized conditions: (1) equal surface area ratio of anode to cathode, (2) distance between electrodes: 3.5 cm, (3) concentration of HCl: 2.36 M, (4) concentration of CuCl: 0.30 M, (5) applied voltage: 0.70 V, (6) flow rate of electrolyte: 125 ml/min for catholyte, 250 ml/min for anolyte, (7) reaction time: 5 h, (8) reaction temperature: 30° C. The experiments were repeated thrice. The data included in Table 4 represents the performance of anion-exchange membrane (2.0:1.5; weight ratio of IA-co-VI copolymer) for Cu—Cl cycle (membrane electrolysis) for hydrogen production.

TABLE 4Performance of anion-exchange membrane (2.0:1.5;weight ratio of IA-co-VI copolymer) for Cu-Cl cycle(membrane electrolysis) for hydrogen productionAvg.Avg.Avg. currentCathodicAppliedCurrentfrom threecurrentVoltageobtainedexperimentsdensityExample 12(Volt)(Amp)(Amp)(mAmp/cm2)Example 120.70.480.4557

Advantages of the Invention

Advantages of the present invention are:1. Homogenous anion exchange membrane with fluorinated polymer backbone, responsible for high membrane stability under strong oxidative, acidic and alkaline environment.2. Plenty of quaternary ammonium groups in the membrane structure, are responsible for good IEC and membrane conductivity.3. Highly stable and efficient anion exchange membrane for different electro-membrane processes such as water desalination, electro-separation, membrane electrolysis, alkaline fuel cell, and storage battery etc.4. Cost-effective anion exchange membrane with high permeselectivity, high conductivity.5. Anion-exchange membrane may be widely used for, electro-deionization, electrodialysis for the removal of inorganic electrolyte, desalination of sea and brackish water, separation and removal of metal ions from the industrial effluent, de-acidification of fruit juice, dashing and sugar cane juice even at high temperature (70-80° C.) for better quality of sugar, purifications and amino acids, vitamins, vaccines and other biochemical purification and down-stream processing of fermentation broth, etc. can be achieved by stable anion-exchange membranes.