ELECTROCHEMICAL PROCESS FOR PRODUCING CHLORIC ACID-ALKALI METAL CHLORATE MIXTURES

Abstract: An aqueous solution of chloric acid and alkali metal chlorate is produced in an electrolytic cell (4) having an anode compartment (10), a cathode compartment (30), and at least one ion exchange compartment (20) between the anode compartment (10) and the cathode compartment (30). The process comprises feeding an aqueous solution of an alkali metal chlorate to the ion exchange compartment (20), electrolyzing an anolyte (12) in the anode compartment (10) to generate hydrogen ions, passing the hydrogen ions from the anode compartment (10) through a cation exchange membrane (16) into the ion exchange compartment (20) to displace alkali metal ions and produce an aqueous solution of chloric acid and alkali metal chlorate, and passing alkali metal ions from the ion exchange compartment (20) into the cathode compartment (30).

Description: ELECTROCHEMICAL PROCESS FOR PRODUCING CHLORIC ACID - ALKALX METAL CHLORATE MIXTURES This invention relates to a process for electrochemically producing chloric acid - alkali metal chlorate solutions. More particularly, this invention relates to the electrochemical production of chloric acid - alkali metal chlorate solutions suitable for the generation of chlorine dioxide. Chlorine dioxide has found wide use as a disinfectant in water treatment/purification, as a bleaching agent in pulp and paper production, and a number of other uses due to its high oxidizing power. There is a variety of chlorine dioxide generator systems and processes available in the marketplace. Most of the very large scale generators employed, for example, in pulp and paper production, utilize an alkali metal chlorate salt, a reducing agent, and an acid in a chemical process for producing chlorine dioxide. These generators and the processes employed also produce by-product salts such as sodium chloride, sodium sulfate, or sodium bisulfate. In pulp and paper mills, the typical by-product is sodium sulfate (saltcake) which is converted into a sulfur salt of sodium in a high temperature boiler and used in the paper process. Boilers require energy and the paper mills have a limited boiler capacity. Increasing the production of chlorine dioxide generally means increased capital investment to provide the added boiler capacity' required to process the added amounts of saltcake by-product produced. Thus a process which reduces the amount of a by-product salt, such as sodium chloride or sodium sulfate, produced while efficiently generating chlorine dioxide is commercially desireable. U.S. Patent 3,810,969 issued May 14, 1974 to A.A. Schlumberger teaches a process for producing chloric acid by passing an aqueous solution containing from 0.2 gram mole to 11 gram moles per liter of an alkali metal chlorate such as sodium chlorate through a selected cationic exchange resin at a temperature from 5* to 40 # C. The process produces an aqueous solution containing from 0.2 gram mole to about 4.0 gram moles of HClO j . This process requires the regeneration of the cationic exchange resin with acid to remove the alkali metal ions and the treatment or disposal of the acidic salt solution. K.L. Hardee et al, in U.S. Patent No. 4,798,715 issued Jan. 17,1989, describe a process for chlorine dioxide which electrolyzes a chloric acid solution produced by passing an aqueous solution of an alkali metal chlorate through an ion exchange resin. The electrolyzed solution contains a mixture of chlorine dioxide and chloric acid which is fed to an extractor in which the chlorine dioxide is stripped off. The ion exchange resin is regenerated with hydrochloric acid and an acidic solution of an alkali metal chloride formed. In U.S. Patent No. 4,683,039, Twardowski et al describe a method for producing chlorine dioxide in which the chlorine dioxide is produced in a generator by the reaction of sodium chlorate and hydrochloric acid. After separating chlorine dioxide gas, the remaining sodium chloride solution is fed to a three-compartment cell to form sodium hydroxide and an acidified liquor which is returned to the chlorine dioxide generator. Each of the above processes produces a fixed amount and type of by-product salt. - 3 - Now a process has been discovered which permits variability in the composition of a chlorate solution used in chlorine dioxide generators. Further, the process permits a reduction in the amount of acid required and subsequently the amount of salt by-producf jproduced in the chlorine dioxide generator. Still further, the process allows for the production of an alkali metal hydroxide as a valuable by-product or acidic solutions of alkali metal salts at reduced energy costs. In addition, the process results in the reduction of process steps and process equipment required for the production of chlorine dioxide. These and other advantages are accomplished in a process for electrolytically producing an aqueous solution of chloric acid and alkali metal chlorate in an electrolytic cell having an anode compartment, a cathode compartment, and at least one ion exchange compartment between the anode compartment and the cathode compartment, characterized by feeding an aqueous solution of an alkali metal chlorate to the ion exchange compartment, electrolyzing an anolyte in the anode compartment to generate hydrogen ions, passing the hydrogen ions from the anode compartment through a cation exchange membrane into the ion exchange compartment to displace alkali metal ions and produce an aqueous solution of chloric acid and alkali metal chlorate, and passing alkali metal ions from the ion exchange compartment into the cathode compartment. More in detail, the novel process of the present invention and its application in producing chlorine dioxide ft, can be carried out in apparatus illustrated in the following FIGURES. Figure 1 is a sectional side elevational view of an electrolytic cell which can be employed in the novel i >r process of the invention; and Figure 2 is a sectional side elevational view of an additional electrolytic cell which can be employed in the novel process of the invention. Figure 3 is a diagrammatic illustration of a system which can be employed in the process of the invention. FIGURE 1 shows an electrolytic cell 4 divided into anode compartment 10, ion exchange compartment 20, and cathode compartment 30 by cation permeable ion exchange membranes 16 and 24. Anode compartment 10 includes anode 12, and anode spacer 14. Anode spacer 14 positions porous anode 12 with respect to cation permeable ion exchange membrane 16 and aids in the disengagement of anolyte gas produced. Anolyte disengager 18 completes the disengagement of anolyte gas from the spent anolyte solution. Ion exchange compartment 20 includes spacer material 22 which provides a flow channel between cation permeable ion exchange membranes 16 and 24 for the aqueous alkali metal chlorate solution. Cathode compartment 30 includes cathode 32, and cathode spacer 34. Cathode spacer 34 positions cathode 32 with respect to cation permeable ion exchange membrane 24 and aids in the disengagement of catholyte gas produced. The disengagement of catholyte gas from the spent catholyte solution is accomplished in cathode disengager 36. In FIGURE 2, electrolytic cell 4 has been expanded to include a second ion exchange compartment 40 which is positioned between anode compartment 10 and ion exchange compartment 20. Cation permeable ion exchange membrane 42 separates anode compartment 10 from ion exchange compartment 40. The sodium chlorate feed solution enters the lower part of ion exchange compartment 20, flows upward and out of ion exchange compartment 20 into the upper part of ion exchange compartment 40. The HC10 3 / NaClO- product solution is recovered from the lower part of ion exchange compartment 40. The flow direction in the ion exchange compartments can also be reversed, for example, with the solution from the top of ion exchange compartment 40 being fed to the bottom of ion exchange compartment 20. ' The product solution then exits from the top of ion exchange compartment 20. An aqueous solution of an alkali metal chlorate is fed to the single or multiple ion exchange compartments of the electrolytic cell. Suitable alkali metal chlorates include sodium chlorate, potassium chlorate and lithium chlorate. In order to simplify the disclosure, the process of the invention will be described using sodium chlorate, which is a preferred embodiment of the alkali metal chlorates. As shown in FIGURE 3, the sodium chlorate feed solution may be prepared, for example, by ' dissolving crystalline sodium chlorate in water. Commercial sodium chlorate is suitable as it has a low sodium chloride content and the formation of undesireable amounts of Chlorine dioxide in the electrolytic cell is prevented. Aqueous sodium chlorate feed solutions which may be employed contain any Suitable concentrations of sodium chlorate, for example, solutions having a concentration in the range of from about 0.1 \ by weight to those saturated with NaClO, at temperatures in the range of from about 0* to about 100 # , and preferably from about 15 # to about 80*C. The novel process of the invention utilizes an electrochemical cell to generate hydrogen ions that displace or replace a portion of the sodium ions present in the aqueous sodium chlorate solution feed stream. The generation of hydrogen ions in the process of the present invention in the anode compartment is accompanied, for example, by the oxidation of water on the anode into oxygen gas and H+ ions b the electrode reaction as follows: (4) 2H 2 0 > 0 2 + 4H + ♦ 4e " The anode compartment contains an anolyte, which can be an aqueous solution of any non-oxidizable acid electrolyte which is suitable for conducting hydrogen ions into the ion exchange compartment. Non-oxidizable acids which may be used include sulfuric acid, phosphoric acid and the like. Where a non-oxidizable acid solution is used as the anolyte, the concentration of the anolyte is preferably selected to match the osmotic concentration characteristics of the alkali metal chlorate solution fed to the ion exchange compartment to minimize water exchange between the anode compartment and the ion exchange compartment. Additionally, an alkali metal choride solution can be used as the anolyte, which results in a generation of chlorine gas at the anode. Where a chlorine generating anolyte is employed, it is necessary to select a cation exchange membrane as the separator between the anode compartment from the ion exchange compartment which is stable to chlorine gas. The anode compartment may also employ as the anolyte electrolyte a strong acid cation exchange resin in the hydrogen form and an aqueous solution such as deionized water. Any suitable anode may be employed in the anode compartment, including those which are available commercially as di ensionally stable anodes. Preferably, an anode is selected which will generate oxygen gas. These anodes include porous or high surface area anodes. As materials of construction for the anodes metals including platinum, gold, palladium, or mixtures or alloys thereof, or thin coatings of such materials on various substrates such as valve metals, i.e. titanium, can be used. Additionally oxides of iridium, rhodium or ruthenium, and alloys with other platinum group or precious metals metals could also be employed. Commercially available oxygen evolution anodes of this type include those manufactured by Englehard (PMCA 1500) or Eltech (TIR-2000) . Other suitable anode materials include graphite, graphite felt, a multiple layered graphite cloth, a graphite cloth weave, carbon, etc.. The hydrogen ions generated in the anode compartment pas through the cation exchange membrane into the sodium chlorat solution in the ion exchange compartment. As a hydrogen ion enters the solution, a sodium ion is displaced and by electrical ion mass action passes through the cation membran adjacent to the cathode compartment to maintain electrical neutrality. The novel process of the invention as operated results i the conversion of sodiu chlorate to chloric acid over a wid range, for example, from about 1 to about 99.9\, preferably from about 5 to about 95, and more preferably from about IS to about 90*. The sodium chlorate feed solution concentration, the residence time in the ion exchange compartment as well as th cell amperage are factors that affect the extent of the conversion of sodium chlorate to chloric acid. Using very dilute solutions of sodium chlorate, high percentages of conversion of NaClO. to chloric acid can be achieved, i.e. up to 99.9\ conversion. For a single pass flow through system, typical residence times in the ion exchange compartment are between about 0.1 to about 120 minutes, with a more preferred range of about 0.5 to about 60 minutes. Thus the concentration of sodium chlorate in the solutio fed to the ion exchange compartment and the flow rate of the solution through the ion exchange compartment are not critical and broad ranges can be selected for each of these parameters. The novel process of the present invention is operated a a current density of from about 0«01 KA/m to about 10 9 2 KA/m , with a more preferred range of about 0.05 KA/m to 2 about 3 KA/m . Current efficiencies during operation of the process of the invention can be increased by employing additional ion exchange compartments, as illustrated by FIGURE 2, which are adjacent and operated in a series flow pattern. Adjusting the width of the ion exchange compartment can also alter the operating cell voltage and current efficiency. The width, or space between the cation exchange membranes forming the walls of the ion exchange compartment, is in the range of from about 0.1 to about 10, and preferably from about 0.3 to about 5 centimeters. In an alternate embodiment the ion exchange compartment contains a cation exchange medium. Cation exchange mediums which can be used in the ion exchange compartment include cation exchange resins. Suitable cation exchange resins include those having substrates and backbones of polystyrene based with divinyl benzene, cellulose based, fluorocarbon based, synthetic polymeric types and the like. Where more than one ion exchange compartment is employed, inclusion of the cation exchange medium is optional for each compartment. Functional cationic groups on these mediums which may be employed include carboxylic acid, sulfonic or sulfuric acids, and acids of phosphorus such as phosphonous, phosphonic or phosphoric. The cation exchange resins are suitably ionically conductive so that a practical amount of current can be passed between the cation exchange membranes used as separators. Various percentage mixture of resins in the hydrogen form and the sodium form may be used in various sections of the ion exchange compartments on assembly to compensate for the swelling and contraction of resins during cell operation. For example, percentage ratios of hydrogen form to sodium form may include those from 50 to 100\. The use of cation exchange resins in the ion exchange compartment can serve as an active mediator which can exchange or absorb sodium ions and release hydrogen ions. The hydrogen ions generated at the anode thus regenerate the resin to the hydrogen form, releasing sodium ions to pass into the cathode compartment. Their employment is particularly beneficial when feeding dilute sodium chlorate solutions as they help reduce the cell voltage and increase conversion efficiency. Preferred as cation exchange mediums are strong acid typ cat ion exchange resins i n the hydrogen form as exempl i f ied b low cross-linked resins such as AMBERLITE* IRC- 118 (Rohm and Haas Co . ) as wel l as high -*,er cross- linked resins i . e . AMBERLITEΦ IRC-120. High surface area acro- reticular or icroporous type ion exchange resins having sufficient ionic conductivity in the ion exchange compartments are also suitable. Physical forms of the cation exchange resin which can be used are those which can be packed into compartments and include beads, rods, fibers or a cast form with internal flow channels. Bead forms of the resin are preferred. Cation exchange membranes selected as separators between compartments are those which are inert membranes, and are substantially impervious to the hydrodynamic flow of the alkali metal chlorate solution or the electrolytes and the passage of any gas products produced in the anode or cathode compartments. Cation exchange membranes are well-known to contain fixed anionic groups that permit intrusion and exchange of cations, and exclude anions from an external source. Generally the resinous membrane or diaphragm has as a matrix, a cross-linked polymer, to which are attached charged radicals such as —SOl and/or mixtures thereof with --COOH " . The resins which can be used to produce the membranes include, for example, fluorocarb ns, vinyl compounds, polyolefins, hydrocarbons, and copolymers thereof. Preferred are cation exchange membranes such as those comprised of fluorocarbon polymers or vinyl compounds such as divinyl benzene having a plurality of pendant sulfonic acid groups or carboxylic acid groups or mixtures of sulfonic acid groups and carboxylic acid groups. The terms "sulfonic acid group" and "carboxylic acid groups" are meant to include salts of sulfonic acid or salts of carboxylic acid groups by processes such as hydrolysis. Suitable cation exchange membranes are readily available, being sold commercially, for example, by Ionics, Inc., Sybron, by E.I. DuPont de Nemours & Co., Inc., under the trademark "NAFION*", by the Asahi Chemical Company under the trademark "ACIPLEX®", and by Tokuyama Soda Co., under the trademark "NEOSEPTAΦ" . Among these are the perfluorinated sulfonic acid type membranes which are resistant to oxidation and high temperatures such as DuPont NAFIONΦ types 117, 417, 423, etc., membranes from the assignee of U. S. Patent No. 4,470,888, and other polytetrafluorethylene based membranes with sulfonic acid groupings such as those sold under the RAIPORE tradename by RAI Research Corporation. The catholyte can be any suitable aqueous solution, including alkali metal chlorides, and any appropriate acids such as hydrochloric, sulfuric, phosphoric, nitric, acetic or others. In a preferred embodiment, deionized or softened water or sodium hydroxide solution is used as the catholyte in the cathode compartment to produce an alkali metal hydroxide. The water selection is dependent on the desired purity of the alkali metal hydroxide by-product. The cathode compartment may also contain a strong acid cation exchange resin in a cation form such as sodium as the electrolyte. Any suitable cathode which generates hydrogen gas may be used, including those, for example, based on nickel or its alloys, including nickel-chrome based alloys; steel, including stainless steel types 304, 316, 310, etc.; graphite, graphite felt, a multiple layered graphite cloth, a graphite cloth weave, carbon; and titanium or other valve metals as well as valve metals having coatings which can reduce the hydrogen overvoltage of the cathode. The cathode is preferably perforated to allow for suitable release of the hydrogen gas bubbles produced at the cathode particularly where the cathode is placed against the membrane. Optionally a porous spacer material such as a chemically resistant non-conductive plastic mesh or a conductive material like graphite felt can be positioned behind the anode and/or the cathode to support the electrodes and to permit the adjustment of the gap between the electrode and the cation permeable ion, exchange membrane, for example, when using high open area expanded metal electrodes. The porous spacer material preferably has large holes for ease of disengagement of the gases from the anolyte and/or catholyte. A thin protective spacer can also be placed between the anode and/or the cathode and the cation permeable ion exchange membranes. This spacer can be a non-conductive plastic or a porous conductive material like graphite felt. The cell may be operated with the electrode in contact with the thin protective spacer and the porous spacer material, or with the membrane in direct contact with the electrode and with or without the porous spacer material. It will be recognized that other configurations of the electrolytic cell can be employed in the novel process of the present invention, including bipolar cells utilizing a solid plate type anode/cathode or bipolar membranes. For example, a bipolar electrode could include a valve metal such as titanium or niobium sheet clad to stainless steel. The valve metal side could be coated with an oxygen evaluation catalyst and would serve as the anode. An alternative anode/cathode combination which is commercially available is a platinum clad layer on stainless steel or niobium or titanium and is prepared by heat/pressure bonding. The novel product solution contains chloric acid and alkali metal chlorate in a wide range of concentrations and ratios of chloric acid to alkali metal chlorate. For example, the solutions produced can provide molar ratios of chloric acid to alkali metal chlorate of from about 0.1: 1 to about 250: 1. Where the product solutions are to be used in the generation of chlorine dioxide, suitable molar ratios of chloric acid to alkali metal chlorate of from about 0.3: 1 to about 200: 1, and preferably from about 1: 1 to about 100: 1 These solutions are highly acidic and permit a reduction in the amount of acid required in the generation of chlorine dioxide in commercial processes which react a chlorate solution with an acid in the presence of a reducing agent. Further, the chloric acid - alkali metal chlorate solutions produced are substantially free of chloride, sulfate, phosphate, or other anionic groups which are present when an alkali metal chlorate is acidified with mineral or other acids used in the generation of chlorine dioxide. Where desired, the chloric acid concentrations of these novel solutions may be increased, for example, by evaporation at sub-atmospheric pressures and temperatures of about 100*C. or less. For example, in the range of from about 30 to about 90 β C. Solutions containing up to about 40\ by weight of chloric acid may be produced in this manner. As illustrated in FIGURE 3, the product solution can be fed directly from the electrolytic cell to a commercial chlorine dioxide generator. Typical commercial processes are those which use sulfuric acid or hydrochloric acid with a reducing agent such as sulfur dioxide or methanol in the presence of a salt such as sodium chloride. Commercial chlorine dioxide processes which may use the aqueous solutions of chloric acid and alkali metal chlorate of the invention include the Mathieson, Solvay, R2, R3, R8, Resting, SVP, and SVP/methanol, among others. The novel process of the present invention permits the production of solutions having a wide range of concentrations of chloric acid and sodium chlorate for use in chlorine dioxide generators. The process permits flexibility in the by-product salts produced as well as allowing the recovery of energy costs by producing, for example, an alkali metal hydroxide solution by-product. Further the process reduces operating costs by eliminating process steps and equipment from processes presently available. In addition novel solutions are procuced having a wide range of chloric acid and alkali metal chlorate concentrations which are substantially free of anionic or cationic impurities. To further illustrate the invention the following examples are provided without any intention of being limited thereby. All parts and percentages are by weight unless otherwise specified. EXΔMELE L_ An electrochemical cell of the type shown in Figure 1 consisting of three compartments machined from ultra high density polyethylene (UHDPE) including an anode compartment, a central ion exchange compartment, and a cathode compartment. The 1/2 inch (1.27 cm.) thick anode compartment contained a titanium mesh anode having an oxygen-evolving anode coating (PMCA 1500® Englehard Corporation, Edison, N.J.). The anode was supported and spaced apart from the UHDPE back wall using multiple layers of polyethylene mesh having 1/4 inch square holes and being 1/16 inch in thickness. A polyethylene mesh spacer was positioned between the anode and adjoining membrane to provide an anode-membrane gap of 0.0625 inch (0.1588 centimeters). The anode compartment was filled with a 2.0 percent by weight sulfuric acid solution. The 1/2 inch (1.27 cm.) thick cathode compartment contained a 304 stainless steel perforated plate cathode mounted flush to the surface of the cathode compartment with the polyethylene mesh spacers. The cathode was positioned in contact with the adjacent membrane providing a zero distance gap. The cathode compartment was initially filled with a sodium hydroxide solution (2\ by weight) as the catholyte. Separating the anode compartment from the ion exchange compartment, and the ion exchange compartment from the cathode compartment were a pair of perfluorosulfonic acid cation permeable membranes with a 985 equivalent weight, obtained from the assignee of U.S. Patent No. 4,470,888. The ion exchange compartment was a machined 1/4 inch (0.625 cm) thick frame with inlet and outlet and contained the polyethylene mesh spacers to distribute the chlorate solution as well as to support and separate the two membranes. An aqueous sodium chlorate solution containing 20 weight percent of NaClO- was prepared by dissolving reagent grade sodium chlorate in deionized water. During operation of the electrolytic cell, the chlorate solution was metered into the bottom of the ion exchange compartment in a single pass process at feed rates varying from 7.0 g/min. to 14.4 g/min. Electrolyte circulation in the anode and cathode compartments was by gas lift effect only. The cell was operated employing a cell current of 24.5 amperes at a current density of 1.20 2 KA/m . The cell voltage varied according to the cell operating temperature. A sample of the product solution was taken at each flow rate, the temperature measured, and the product solution analyzed for chloric acid and sodium chlorate content. The product solutions were colorless, indicating no chlorine dioxide was formed in the ion exchange compartment. The concentration of the sodium hydroxide catholyte during cell operation increased to 12 percent by weight. The results are given in Table I below. - ]6 - EXAMPLE 2 The electrochemical cell of FIGURE 2 was employed having a second ion exchange compartment adjacent to the first ion exchange compartment. The anode compartment containing the same type of anode used in Example 1 was filled with a strong acid hydrogen form cation exchange resin (AMBERLITE* IRC-120 plus, Rohm & Haas Company) as the electrolyte. A perfluorinated sulfonic acid-based membrane (Dupont NAFIONΦ 417) separated the anode compartment from the first ion exchange compartment. The two ion exchange compartments were fully filled with AMBERLITE* IRC-120 plus cation exchange resin in the hydrogen form and were separated by a Dupont NAFIONΦ 417 membrane. The same membrane was employed to separate the second ion exchange compartment from the cathode compartment. The cathode compartment contained a perforated 304 stainless steel cathode, and was filled with a sodium form AMBERLITEΦ IRC-120 plus cation exchange resin. Both the anode compartment and the cathode compartment were filled with deionized water. The sodium chlorate solution fed to the ion exchange compartments was prepared from reagent grade sodium chlorate dissolved in deionized water to form a 16 weight percent solution as sodium chlorate. The sodium chlorate solution at 20*C. was fed to the bottom of ion exchange compartment 40 adjacent to the cathode compartment at a flow rate of 6.5 grams per minute. The chloric acid - sodium chlorate solution flow from the upper part of ion exchange compartment 40 was routed into the bottom of ion exchange compartment 20 adjacent to the anode compartment and collected from the top of ion exchange compartment 20. The total residence time of the solution in the ion exchange compartments was about 42 minutes. During operation of the cell, the cell current was set at a constant 23.0 amperes for an operating current density of 1.5 KA/m 2 . The cell voltage stabilized at 9.60 volts, and the product temperature was 65 Φ C. Circulation in the anode and cathode compartments of the electrolyte was by gas lift effect and the liquid level of the gas disengagers was set at 3 inches (7.62cm) above the height of the cell. The product solution from the cell contained 11.44 weight percent as HC10 3 which represented a 90* conversion of the sodium chlorate to chloric acid. The current efficiency was determined to be 61.6% and the power consumption was 4490 KWH/Ton of HC10-. The product solution was light yellow in color, indicating the presence of some chlorine dioxide or chlorine in the chloric acid-sodium chlorate solution product.

Claims: - 19 - WHAT IS CLAIMED IS: * 1. A process for ej ctrolytically producing an aqueous solution of chloric acid and alkali metal chlorate in an electrolytic cell having an anode compartment, a cathode compartment, and at least on ion exchange compartment between the anode compartment and the cathode compartment, characterized by feeding an aqueous solution of an alkali metal chlorate to the ion exchange compartment, electrolyzing an anolyte in the anode compartment to generate hydrogen ions, passing the hydrogen ions from the anode compartment through a cation exchange membrane into the ion exchange compartment to displace alkali metal ions and produce an aqueous solution of chloric acid and alkali metal chlorate, and passing alkali metal ions from the ion exchange compartment into the cathode compartment. 2. The process of claim 1 characterized in that the alkali metal chlorate is selected from the group consisting of sodium chlorate, potassium chlorate, and lithium chlorate. 3. The process of*,claim 1 characterized in that the anolyte is a cation exchange resin in the hydrogen form and water. 4. The process of claim 1 characterized in that the anolyte is an aqueous solution of a non-oxidizable acid. 5. The process of -claim 1 characterized in that the alkali metal ions from the ion exchange compartment pass through a cation exchange membrane into the cathode compartment. 6. The process of claim 1 characterized in that the conversion of alkali metal chlorate to chloric acid is in the range of from about 1 to about 99.9 percent. 7. The process of claim 1 characterized in that the ion exchange compartment contains a cation exchange medium in the hydrogen form. 8. The process of claim 1 characterized in that the catholyte is water or an alkali metal hydroxide solution. 9. The process of claim 1 characterized in that oxygen gas is produced in the anode compartment. 10. The process of claim 1 characterized in that hydrogen gas is produced in the cathode compartment. 11. The process of claim 2 characterized in that the alkali metal chlorate is sodium chlorate. 12. The process of claim 1 characterized in that the residence time in the ion exchange compartment is from about 0.1 to about 120 minutes. 13. The process of claim 1 characterized in that the 2 current density is from about 0.1 to about 10 KA/m . 14. The process of claim 1 characterized in that the cathode compartment contains a cation exchange medium in the alkali metal form. 15. The process of claim 1 characterized in that the ion exchange compartment contains a cation exchange medium in the hydrogen and sodium form. 16. A process for producing chlorine dioxide characterized by: a) feeding an aqueous solution of an alkali metal chlorate to an ion exchange compartment of an electrolytic cell having an anode compartment, a cathode compartment, and at least one ion exchange compartment between 5 the anode compartment and the cathode compartment, b) electrolysing an anolyte in the anode compartment to generate hydrogen ions, c) passing the hydrogen ions from the anode compartment through a cation exchange membrane into a first ion lOexchange compartment to displace alkali metal ions and produce an aqueous solution of chloric acid and alkali metal chlorate, d) passing alkali metal ions from the ion exchange compartment into the cathode compartment, e) feeding, in series flow, the aqueous solution l5of chloric acid and alkali metal chlorate from the first ion exchange compartment to a second ion exchange compartment, and, f) removing the aqueous solution of chloric acid and alkali metal chlorate from the second ion exchange compartment. 17. The process of claim 16 characterized in that the aqueous solution of chloric acid and alkali metal chlorate is reacted with a mineral acid and a reducing agent to generate chlorine dioxide gas. 18. The process of claim 17 characterized in that the mineral acid is sulfuric acid or hydrochloric acid. 19. The process of claim 17 characterized in that the reducing agent is methanol or sulfur dioxide. 20 The process of claim 16 characterized in that the molar ratio of chloric acid to alkali metal chlorate in the aqueous solution of chloric acid and alkali metal chlorate is in the range of from about 0.1:1 to about 250:1. 21 The process of claim 17 characterized in that an alkali metal chloride is added to the reaction mixture. 22. A process for producing chlorine dioxide characterized by reacting an aqueous solution consisting of chloric acid and alkali metal chlorate having a molar ratio of chloric acid to alkali metal chlorate of from about 0.3: 1 to about 200: 1 with a mineral acid and a reducing agent to generate chlorine dioxide gas. 23. An aqueous solution characterized by chloric acid and an alkali metal chlorate, the solution having a molar ratio of chloric acid to alkali metal chlorate of from about 0.1:1 to about 250:1

Inventors: CAWLFIELD DAVID W, DUNCAN BUDD L, KACZUR JERRY J, WOODARD KENNETH E JR, CAWLFIELD, DAVID, W., DUNCAN, BUDD, L., KACZUR, JERRY, J., WOODARD, KENNETH, E., JR.
Applicants: OLIN CORP, OLIN CORPORATION
Application year: 1991
Main classification: C25B1
IPC codes: B01J19, C01B11, C25B1