Bipolar electrodialysis methods and systems

Abstract

A bipolar membrane electrodialysis method and system are described for purifying an organic acid from an aqueous solution containing the salt of the organic acid. The system includes a bipolar membrane electrodialysis stack that includes at least one three-compartment bipolar membrane electrodialysis cell and at least one two-compartment bipolar membrane electrodialysis cell. The method includes recirculating the solution of organic acid produced from the three-compartment bipolar membrane electrodialysis cell and two-compartment bipolar membrane electrodialysis cell. Cation or anion exchange resins may be included in the spacers of acid compartment to increase the conductivity of acid compartments, thereby increasing current density of the bipolar electrodialysis stack and decreasing power consumption.

Claims

1. A system for producing a purified solution that includes an organic acid from a feed solution that includes a salt of the organic acid, the system comprising: an anode; a cathode; and at least one three-compartment bipolar membrane electrodialysis cell for accepting the feed solution and for producing an organic acid containing solution; and at least one two-compartment bipolar membrane electrodialysis cell configured to accept the organic acid containing solution and for producing the purified solution containing the organic acid; wherein the purified solution containing the organic acid has a lower concentration of the organic acid salt than the organic acid containing solution does.

2. The system according to claim 1, wherein the at least one three-compartment bipolar membrane electrodialysis cell and the at least two-compartment bipolar membrane electrodialysis cell are in a single bipolar membrane electrodialysis stack.

3. The system according to claim 2, wherein the single bipolar membrane electrodialysis stack is between the anode and the cathode.

4. The system according to claim 1, wherein the system includes three-compartment bipolar membrane electrodialysis cells and two-compartment bipolar membrane electrodialysis cells in a ratio of 1:1 to 20:1.

5. The system according to claim 4, wherein the system includes three-compartment bipolar membrane electrodialysis cells and two-compartment bipolar membrane electrodialysis cells in a ratio of 5:1 to 10:1.

6. The system according to claim 1, wherein the electrodialysis cells comprise acidic-solution producing compartments that include a cation-exchange resin or an anion-exchange resin.

7. The system according to claim 6, wherein the cation-exchange resin is in H+ form, or is in Na+ form.

8. The system according to claim 6, wherein the cation-exchange resin is a strongly acidic cation-exchange resin.

9. The system according to claim 6, wherein the anion-exchange resin is in OH form.

10. The system according to claim 6, wherein the anion-exchange resin is a styrene-DVB gel with a quaternary amine functional group in OH form.

11. The system according to claim 1 further comprising a processing system adapted to transport the organic acid containing solution from the at least one three-compartment bipolar membrane electrodialysis cell to the at least one two-compartment bipolar membrane electrodialysis cell.

12. The system according to claim 1, wherein the anode is titanium coated with platinum.

13. The system according to claim 1, wherein the cathode is stainless steel.

14. A bipolar membrane electrodialysis stack comprising: at least one three-compartment bipolar membrane electrodialysis cell; and at least one two-compartment bipolar membrane electrodialysis cell.

15. The bipolar membrane electrodialysis stack according to claim 14, wherein at least some of the electrodialysis cells comprise acidic-solution producing compartments that include a strongly acidic cation-exchange resin.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) Examples of the present disclosure will now be described with reference to the attached Figures.

(2) FIG. 1 is an illustration of a bipolar membrane electrodialysis stack according to the present disclosure.

(3) FIG. 2 is a photograph of an exemplary spacer that may be used in a bipolar electrodialysis cell.

(4) FIG. 3 is a photograph of an exemplary spacer that may be used in a bipolar electrodialysis cell.

(5) FIG. 4 is a photograph of an exemplary spacer that may be used in a bipolar electrodialysis cell.

DETAILED DESCRIPTION

(6) Generally, the present disclosure provides a bipolar membrane electrodialysis method and system for recovering an organic acid from an aqueous solution containing the organic acid salt. The bipolar membrane electrodialysis system includes a bipolar membrane electrodialysis stack having at least one three-compartment bipolar electrodialysis cell, and a bipolar membrane electrodialysis stack having at least one two-compartment bipolar electrodialysis cell. The at least one three-compartment bipolar electrodialysis cell and the at least one two-compartment bipolar electrodialysis cell may be in the same electrodialysis stack.

(7) The three-compartment bipolar electrodialysis cell accepts the aqueous solution containing the organic acid salt, producing a solution containing organic acid and a solution containing a base. The solution of organic acid is also passed through the two-compartment bipolar electrodialysis cell in order to remove at least a portion of the cations that leaked across the bipolar membrane into the acid-producing compartment of the three-compartment bipolar electrodialysis cell.

(8) FIG. 1 illustrates an example of a bipolar membrane electrodialysis stack (10) according to the present disclosure. The stack includes a three-compartment bipolar membrane cell (12) and a two-compartment bipolar membrane cell (14). In the electrodialysis system of FIG. 1, the two cells (12 and 14) are located in a single stack between a cathode (16) and an anode (18). The stack (10) includes bipolar membranes (20, 20, 20), cation-exchange membranes (22, 22), and anion-exchange membrane (24).

(9) The three-compartment bipolar cell (12) accepts a feed solution containing a sodium salt of an organic acid (26). In an aqueous solution, the sodium salt of the organic acid dissociates into sodium ions (Na.sup.+) and acid anions (A.sup.). The sodium ions and acid anions in the feed solution (26) are separated under the application of an electrical current as the sodium ions migrate towards the cathode (16) and pass through the cation exchange membrane (22); and as the acid anions migrate towards the anode (18) and pass through the anion exchange membrane (24). A solution having reduced organic acid salt concentration (28) is produced.

(10) The bipolar membranes (20, 20) split water into hydronium ions (H.sub.3O.sup.+, illustrated in FIG. 1 as H.sup.+) and hydroxide ions (OH.sup.). The hydroxide ions balance the charge of the sodium ions, and result in the production of a basic sodium hydroxide solution (30). The hydronium ions balance the charge of the acid anion (A.sup.) and result in the production of an organic acid solution (32).

(11) The cation- and anion-exchange membranes (22, 24) define a compartment that accepts the organic acid salt solution and produces the solution having reduced organic acid salt concentration (28). The bipolar membrane (20) and the cation-exchange membrane (22) define a compartment that produces the basic solution (30). The anion-exchange membrane (24) and the bipolar membrane (20) define a compartment that produces the organic acid solution (32).

(12) The organic acid solution (32) also includes a portion of the sodium salt of the organic acid since sodium ions may leak through the bipolar membrane (20). These leaked sodium ions are identified in FIG. 1 as Na.sup.+ (34).

(13) The organic acid solution (32) is further purified in the two-compartment bipolar membrane cell (14) by feeding the organic acid solution (32) into the compartment defined by the cation exchange membrane (22) and the bipolar membrane (20). The sodium ion present in the organic acid solution (32) migrates through the cation exchange membrane (22) on application of the electrical current, which is balanced out by the hydronium ion (H.sub.3O.sup.+) generated at the bipolar membrane (20). This results in the production of a purified organic acid solution (34). The sodium ion that migrates through the cation exchange membrane (22) is balanced by the hydroxide ion produced at bipolar membrane (20), resulting in the production of a second basic solution (36).

(14) The organic acid solution (32) may be recycled to the bipolar membrane electrodialysis stack by being routed directly to the two-compartment bipolar membrane cell (14), or by being held in a holding tank (not shown) and subsequently passed through a two-compartment bipolar membrane cell of this or another bipolar membrane electrodialysis stack according to the present disclosure.

(15) The membranes shown in FIG. 1 may be separated by spacers, not shown. Spacers separate adjacent membranes while still allowing the solutions to flow through the system. Spacers with tortuous structure, screen structure, or spacers filled with ion exchange resins may be used. The tortuous and screen spacers may be about 1/32 thick. The resin filled spacers may be from about 1/16 to about thick. The spacers may have 4-inlets and 4-outlets. Spacers may be used in the two-compartment BPED cell, in the three-compartment BPED cell, or both.

(16) Exemplary spacers are shown in FIGS. 2-4. FIG. 2 shows an exemplary spacer, originally produced in the 1980's, having a tortuous structure. FIG. 3 shows an exemplary screen spacer, originally produced in the 2000's, having an S-type structure. FIG. 4 shows an exemplary spacer, without a screen, for filling with an ion-exchange resin.

(17) Although the stack illustrated in FIG. 1 shows only a single three-compartment bipolar membrane cell and a single two-compartment bipolar membrane cell, stacks according to the present disclosure may include a plurality of three-compartment bipolar membrane cells and a plurality of two-compartment bipolar membrane cells. For example, the stack may include from 1 to 20 three-compartment cells for every 1 two-compartment cell. The three-compartment bipolar membrane cells and the two-compartment bipolar membrane cells may be present in a ratio of 5:1 to 15:1. In specific exemplary systems, the ratio is from 5:1 to 10:1. A full size stack may include as many as 150 cell pairs, or more.

(18) The cation-exchange membranes used in the electrodialysis stacks according to the present disclosure may be homogenous membranes having an ion exchange capacity of about 2.2 to about 2.4 meq/g, a water content of about 43 to about 49%, a thickness of about 0.55 to about 0.69 mm, a resistivity of about 10 to about 12 ohm-cm.sup.2, and a Mullen burst strength of about 250 to about 350 psi. A representative example of useful cation-exchange membranes is sold under the trademark CR61CMP, available from GE Inc. The cation-exchange membranes used in an electrodialysis stack may, or may not, be all identical. The anion-exchange membranes used in the electrodialysis stacks according to the present disclosure may be homogenous membranes having an ion exchange capacity of about 2.0 to about 2.2 meq/g, a water content of about 33 to about 39%, a thickness of about 0.55 to about 0.69 mm, a resistivity of about 11 to about 14 ohm-cm.sup.2, and a Mullen burst strength of about 250 to about 350 psi. A representative example of useful anion-exchange membranes is sold under the trademark AR103QDP, available from GE Inc. The anion-exchange membranes used in an electrodialysis stack may, or may not, be all identical. The bipolar electrodialysis membranes used in the electrodialysis stacks according to the present disclosure consist of an anion exchange layer with catalyst bonded to a cation exchange layer. A representative example of useful bipolar membranes is sold under the trademark BtB BP, available from GE. The bipolar electrodialysis membranes used in an electrodialysis stack may, or may not, be all identical.

(19) Other membranes than those listed above may be used. However, the membranes are preferably stable to acid and caustic solution up to about 4 N. The membranes are preferably homogeneous membranes since homogeneous membranes have a lower resistance than heterogeneous membranes.

(20) Including a cation- or anion-exchange resin in an acid compartment of a cell may improve the conductivity of the liquid in the compartment. This is especially beneficial when purifying acids having a pKa greater than about 1.5 since aqueous solutions of such acids dissociate to generate concentrations of hydronium ions and conjugate base that result in current densities that make purification impractical. Systems according to the present disclosure may include a cation- or anion-exchange resin in at least some of the acidic solution-producing compartments, for example in the compartments that produce organic acid solution (32) and the compartments that produce purified organic acid solution (34). Including ion-exchange resins in at least some of the acidic solution-producing compartments increases the current density of the stack.

(21) The resin may be a cation-exchange resin in sodium form or H.sup.+ form, or may be an anion-exchange resin in OH.sup. form. The ion-exchange resin is preferably strongly acidic cation-exchange resin. Specific examples of resins that may be used in electrodialysis stacks according to the present disclosure include: Dowex Monosphere 650C(H) (a styrene-divinyl benzene (DVB) cation-exchange gel with a sulfonic acid functional group in H.sup.+ form) from DOW company, and Dowex Monosphere 550A(OH) (a styrene-divinyl benzene (DVB) anion-exchange gel with a quaternary amine functional group in OH.sup. form) from DOW company. Dowex Monosphere 650C(H) are spherical cation-exchange resin beads having a volume capacity of 2.0 eq/L, a harmonic mean diameter of 65050 m, an ionic conversion of 99.7%. The resin may be regenerated using 1-10% H.sub.2SO.sub.4 or 4-8% HCl. Dowex Monosphere 550A(OH) are spherical anion-exchange resin beads having a volume capacity of 1.1 eq/L, a harmonic mean diameter of 59050 m, an ionic conversion of 94% for OH.sup.. The resin may be regenerated using 4-8% NaOH.

(22) Electrodialysis devices according to the presently disclosure may include any known electrodes for the anode and cathode. The anode may include titanium/platinum, carbon, nickel, ruthenium/titanium, or iridium/titanium. The anode may be a dimensionally stable anode, such as a titanium plate or mesh coated with mixed metal oxides (MMO), such as RuO.sub.2, IrO.sub.2, TiO.sub.2 and Ta.sub.2O.sub.5. The cathode may include iron, nickel, platinum, titanium/platinum, carbon, or stainless steel. The structure of the electrodes may be any known structures. Examples of the general structure include a flat plate shaped structure, a mesh-shaped structure, and a lattice-shaped structure.

(23) A 910 bipolar electrodialysis stack according to the present disclosure, having 5 three-component bipolar electrodialysis cells and 1 two-component bipolar electrodialysis cell, may be operated with a current density of about 30 to about 100 mA/cm.sup.2 at a cell voltage from about 2 to about 4 V/cell when purifying acetic acid from a solution of sodium acetate. Stacks according to the present disclosure are preferably operated at an operation temperature of below about 50 C., a flow linear velocity of about 5 to about 20 cm/sec, and a flow pressure of about 3 to about 15 psi. Such an exemplary stack includes cation-exchange resin in the acidic-solution producing compartments. In the exemplary stack, the resin is held in place using a spacer formed from about 1/16 or about thick low-density polyethylene (LPDE), which is sandwiched between the two membranes.

(24) An electrodialysis system that included the exemplary 910 stack described above, but without resin in the acidic-solution producing compartments, was tested against an electrodialysis system that included only 6 three-compartment bipolar electrodialysis cells. The systems were used to purify a sodium acetate solution. A summary of the runs and the composition of the purified solutions are shown below:

(25) TABLE-US-00001 Run #2 Run #3 Configuration 6 3-C 5 3-C, 1 2-C Feed (equilibrium) 3.66 3.66 Acid produced (equilibrium) 2.46 2.851 Base produced (equilibrium) 2.59 2.391 Run (min) 150 180 Faraday (equilibrium) 4.63 4.60 Current efficiency %, acid 57.7 42.0 Power consumption, acid (kwh/kg) 1.795 3.155 Current efficiency %, base 56.3 52.0 Power consumption, base (kwh/kg) 2.759 3.831 Sodium (ppm) 1090 192 Acetic Acid (ppm) 79,600 80,700 Sodium (moles/L) 0.0474 0.0083 Acetic Acid (moles/L) 1.327 1.345 Sodium (mol %) 3.57 0.62 Sodium (wt %) 1.37 0.24 Final acid conductivity (mS/cm) 5.58 2.63
One can see that sodium ion is reduced from 1090 ppm in Run #2 to 192 ppm in Run #3, corresponding to a reduction in weight % of sodium from 1.37% to 0.24%.

(26) Run #2 corresponds to the purified solutions produced by the electrodialysis system that included only 6 three-compartment bipolar electrodialysis cells. Run #3 corresponds to the purified solution produced by the electrodialysis system that included 5 three-component bipolar electrodialysis cells and 1 two-component bipolar electrodialysis cell.

(27) Power consumption for purification of acetic acid from sodium acetate was compared between an electrodialysis system that included resin cation-exchange resin Dowex 650 (H.sup.+) in the acidic-solution producing compartments, and an electrodialysis system that did not include resin. Both systems had 5 three-component bipolar electrodialysis cells and 1 two-component bipolar electrodialysis cell. Run #3, as noted above, corresponds to the system without resin, while Run #9 corresponds to the system with resin. A summary of the runs and the composition of the purified solutions are shown below:

(28) TABLE-US-00002 Run #3 Run #9 Configuration 5 3-C, 1 2-C 5 3-C, 1 2-C with cation exchange resin Feed (equilibrium) 3.66 3.66 Acid produced (equilibrium) 2.851 2.46 Base produced (equilibrium) 2.391 2.59 Run (min) 180 160 Faraday (equilibrium) 4.60 4.96 Current efficiency %, acid 42.0 49.6 Power consumption, acid (kwh/kg) 3.155 2.108 Current efficiency %, base 52.0 52.2 Power consumption, base (kwh/kg) 3.831 3.001 Sodium (ppm) 192 158 Acetic Acid (ppm) 80,700 71,800 Sodium (moles/L) 0.0083 0.0069 Acetic Acid (moles/L) 1.345 1.197 Sodium (mol %) 0.62 0.58 Sodium (wt %) 0.24 0.22 Final acid conductivity (mS/cm) 2.63 2.35
One can see that power consumption is reduced from 3.155 kwh/kg of acetic acid in Run #3 to 2.108 kwh/kg in Run #9, which includes cation-exchange resin in the acidic-solution producing compartment.

(29) In the preceding description, for purposes of explanation, numerous details are set forth in order to provide a thorough understanding of the examples. However, it will be apparent to one skilled in the art that these specific details are not required. Accordingly, what has been described is merely illustrative of the application of the described examples and numerous modifications and variations are possible in light of the above teachings.

(30) Since the above description provides exemplary examples, it will be appreciated that modifications and variations can be effected to the particular examples by those of skill in the art. Accordingly, the scope of the claims should not be limited by the particular examples set forth herein, but should be construed in a manner consistent with the specification as a whole.