AU604590B2

AU604590B2 - Production of chlorine dioxide in an electrolytic cell

Info

Publication number: AU604590B2
Application number: AU26977/88A
Authority: AU
Inventors: Marek Lipsztajn; James D. Mcgilvery; Zbigniew Twardowski
Original assignee: Tenneco Canada Inc
Current assignee: Sterling Canada Inc
Priority date: 1988-02-16
Filing date: 1988-12-15
Publication date: 1990-12-20
Anticipated expiration: 2008-12-15
Also published as: NO173513C; PT89221A; EP0328818A2; BR8807003A; FI87936C; AR240340A1; EP0328818B1; ATE91306T1; PL276597A1; ES2041321T3; JPH021917B2; PL160949B1; FI87936B; CA1330964C; JPH01219185A; YU46719B; DE3882220D1; FI890172L; NO885436D0; ZA889170B

Description

AUSTRALIA

Patents Act 0 COMPLETE SPECIFICATION

(ORIGINAL)

Application Number: Class Int. Class Lodged: Complete Specification Lodged: Accepted: Published: Priority S, Related Art: ft APPLICANT'S REFERENCE: MIS:eb 53-546 Name(s) of Applicant(s): Tenneco Canada Inc.

Address(es) of Applicant(s): 2 Gibbs Road Islington Ontario Canada M9B 1R1 Address for Service is:

S$,

PHILLIPS ORMONDE FITZPATRICK Patent and Trade Mark Attorneys 367 Collins Street Melbourne 3000 AUSTRALIA Complete Specification for the invention entitled: PRODUCTION OF CHLORINE DIOXIDE IN AN ELECTROLYTIC CELL Our Ref: 117028 POF Code: 1422/50647 The following statement is a full description of this invention, including the best method of performing it known to applicant(s): 1 E194/195/196 1A PRODUCTION OF CHLORINE DIOXIDE IN AN ELECTROLYTIC CELL The present invention relates to the production of chlorine dioxide in substantially pure form, i.e.

substantially free from chlorine.

Chlorine dioxide is widely used as a bleaching chemical and is known to be produced by reduction of sodium chlorate in an acid aqueous reaction medium. The reaction whereby chlorine dioxide is formed, is represented by the equation: C103 Cl- 2H+ C10 2 'C1 2

H

2 0 Generally, therefore, chlorine is co-produced with the chlorine dioxide.

S 15 Processes are known wherein the chlorine so- S. produced is reduced chemically, for example, using clot sulphur dioxide or methanol, thereby producing chloride S. ions for the process in ;itu. Such processes employ S, sulphuric acid as the acid source, resulting in sodium S, 20 sulphate by-product.

SIn addition, there have been suggestions in the art to use electrolytic procedures for the production of Stc chlorine dioxide. In this regard, the applicants are aware of U.S. Patents Nos. 3,904,495, 3,904,496, 3,9:20,801, 4,308,117, 4,324,635 and 4,456,510.

SWith the exception of the latter patent, in each instance, chlorine dioxide is produced in conjunction with chlorine from aqueous chlorate solution in the anode compartment of a multicompartment cell. In U.S.

30 No. Patent 4,456,510, an aqueous sodium chlorite solution is electrolyzed to produce chlorine dioxide.

In accordance with the present invention, there is provided an electrolytic process for the production of chlorine dioxide which is carried out in the cathode compartment of a cation-exchange membrane divided cell in which co-produced chlorine is reduced electrolytically in the cathode compartment in which is positioned a high surface area cathode having a three- 2 dimensional electroconductive surface. Chlorate ions, usually in the form of an aqueous sodium chlorate ~solution, are fed c-o the cathode compartment in which are provided hydrogen ions. The chlorate ions are reduced with the hydrogen ions and chloride ions in the cathode coxipartment to produce the chlorine dioxidee, which is vented from the cathode compartment, while an elcrtic current is applied to reduce the co-produced chlorine to chloride ions. Hydrogen ions are electrolytically formed in the anode compartment and are transferred from the anode compartment to the cathode compartment. In this way, high purity chlorine dioxide is produced electrolytically from chlorate feed.

o The chlorine dioxide is generated chemically in the cathode compartment according to the equation: NaClO 3 2H+ 2ClV C10 2 kC12 NaCl H 2 0 The chlorine co-produced with the chlorine dioxide in 'Ct the cathode compartment in accordance with this equation C f, is electrolytically reduced to chloride ions, leaving the p:'7oduct chlorine dioxide exiting from the cathode a compartment substantially free from the chlorine.

Wa~ter is fed to the anolyte compartment of the cell, an initial charge of an oxy-acid. The electrolysis carried out in the cell produces oxygen gas, which is vented from the anode compartment, and 000~ hydrogen ions, which migrate across the cation-exchange 0: membrane into the anode compartment to provide hydrogen 0 00 aions therein for the chemical reaction producing 000~chlorine dioxide therein. For each gram-atom of chlorine reduced electrochemically in the cathode compartment to cl-, one mole of H+ is transferred into the cathode compartment, thereby providing 1 mole of the two moles of hydrogen ions and chloride ions requred for continuous operation of the chlorine dioxideproducing reaction. Accordingly, the cathode compartment requires the feed of 1 mole of sodium _Z t o t 0 I J 1t 15 I te t e rI a a t a- at* chlorate, 1 mole of hydrogen ions and 1 mole of chloride ions to maintain the chlorine dioxide production as a continuous process.

Alternately, mole of chlorine may be fed to the cathode compartment along with one mole of sodium chlorate. In this case, two moles of H+ are transferred from the anode compartment to the cathode compartment to satisfy the hydrogen ion requirement of 'The process, while the k mole of chlorine fed to the cathode compartment and the mole of chlorine co-produced in the cathode compartment are electrochemicElly reduced to provide the two moles of chloride ions.

The invention is described further, by way of illustration, with reference to the accompanying drawings, in which: Figure 1 is a schematic representation of an electrolytic cell for the production of chlorine dioxide in accordance with one embodiment of the invention; Figure 2 is a schematic representation of the integration of an electrolytic cell for the production of chlorine dioxide with an electrolytic cell for the production of sodium chlorite, in accordance with another embodiment of the invention; and Figure 3 is a schematic representation of the integration of an electrolytic cell for the production of chlorine dioxide with an electrolytic cell for the production of sodium hydroxide and chlorine.

Referring first to Figure 1, there is shown therein an electrolytic cell 10 for the production of chlorine dioxide in accordance with one embodiment of the invention. Aqueous sodium chlorate solution is fed by line 12 to the cathode compartment 14 of the cell which contains a three-dimensional electrode. An acid, preferably hydrochloric acid, also is fed to the cathode compartment 14 by line 16.

I 25 a aO t 30 4 :1 15C 4 14 4 201 I t.1 251 1 66041 gag a41t 4 The aqueous sodium chlorate solution fed by line 12 has a concentration sufficient to establish, at its flow rate, a relatively high concentration of sodium chlorate in the cathode compartment 14, generally greater t'han about 5 molar, preferably about 5 to about 6.5 molar.

Usually, the sodium chlorate feed solution has a concentration in the range of about 3 to about 7 molar.

The cell 10 has a cation-exchange membrane 18 separating the cathode compartment 14 from an anode compartment 20. After an initial charge of an oxyacid, usually sulfuric acid, water is fed by line 22 to the anode compartment 20 and hydrogen ions produced by electrolysis of the anolyte migrate across the cationexchange membrane 18 to the cathode compartment 14. The anolyte sulfuric acid solution is recirculated by line 23.

The hydrogen ion migration across the cationexchange membrane 18 and the feed of hydrochloric acid by line 16 establish a total acid ncrmality in the cathode compartment 18 of at least about normal, preferably at least about 0.05 normal.

The oxygen co-produced in the electrolysis step in the anode compartment is vented by line 24 from the anode compartment In the cathode compartment 14, the sodium chlorate fed by line 12. reacts chemically with the hydrogen ions and chloride ions fed by line 16, the electrolyticallyproduced hydrogen ions transferred across the cationexchange membrane and the chloride ions electrolytically produced in the cathode compartment 14 as described below, to form chlorine dioxide and chlorine in accordance with the equation: NaClO 3 2H+ 2C1- C10 2 kC1 2 NaCl H 2 0 One half of the hydrogen ion requirement is provided by the acid fed by line 16 with the rentinder of the hydrogen ion requirement is provided by the hydrogen ions transferred from the anode compartment The co-produced chlorine is reduced under the electrochemical conditions which exist in the cathode compartment 14, selectively with respect to the chlorine dioxide present therein. The chloride ions so produced provide half the chloride ions for the chemical reduction of the chlorate, with the remainder of the chloride ions being provided by the hydrochloric acid feed in line 16, or from some othei convenient external source of chloride ions, such as sodium chloride.

Depending on the electrolytic conditions in the cathode compartment, the chloride ions may be produced i directly from the co-produced chlorine by 15 electrochemical reduction, in accordance with the 0equation: Cl 2 e C1or indirectly by reduction chemically with chlorite ion c electrolytically produced from chlorine dioxide, in accordance with the -lations: C1O 2 e ClO1 2 C V t C1 2 C10 2 C102 Cl- In this latter procedure, the chlorite ion formation is 25 controlled so as to avoid further electrolytic reduction of chlorite, which inefficiently produces chlorine.

The chlorine concentration in the product off-gas stream in line 26 may be monitored and the current applied to the cell is used to control the chlorine concentration.

The feeds of sodiun chlorate by line 12 and of chloride ions by line 16 as well as the electrochemically-produced chloride ions establish a chlorate to chloride ion ratio in the cathode compartment 14 generally at least about 1:1, preferably about 2:1 to about 4:1.

0 6 K The electrode potential which is applied to the i I cathode is more positive than -1 volt as compared with a saturated calomel electrode (SCE) and as determined at the current feeder to the cathode and more negative than the open circuit potential under the prevailing conditions, preferably about -0.2 volt.

The electrode potential of the cathode refers to the solution potential measured at the current feeder, in analogous manner to a flat plate electrode. A threedimensional electrode, such as employed herein, inherently has a distribution of potential within the structure and the actual potential will depend on the location of determination and may be more negative than 0 a -1 volt vs. SCE.

0o 15 The cathode compartment 14 preferably is maintained 0 oo0 .o at an elevated temperature to assist in the rate of chlorine dioxide formation. Usually, a temperature in excess of about 50°C is employed, preferably about 60 to 0 ,0 to about Alternatively, chlorine rn be fed to the cathode compartment 14 in place of the hydrogen ions and S" chloride ions in line 16, for selective reduction to t chloride ions along with the selective reduction of the co-produced chlorine. In this case, the anolyte feed is increased so as to provide twice as much hydrogen ion I t migration across the membrane 18 and hence provide all the hydrogen ion requirement of the cathode compartment 0 14.

The chlorine dioxide produced in the chemical reaction, substantially free from chlorine, is vented from the cathode compartment 14 as the product gas stream by line 26. This chlorine dioxide stream may be utilized further, as described, for example, with respect to the embodiment of Figure 2 below.

The by-product sodium chloQride from the chemical production of chlorine dioxide is removed from the I It 15 S a a t 20 0a 0 S00 0

I

i 1 1 2 i a o 0 00 o oo 00 0 0 0 0 00 S0 j t cathode compartment as an aqueous solution by line 28.

This aqueous sodium chloride solution may be forwarded to a chlorate cell for electrolytic conversion to aqueous sodium chlorate solution for recycle to the cathode compartment 14 to provide at least part of the sodium chlorate in line 12.

The cathode employed in the cathode compartment 14 is a high surface area electrode having a threedimensional electrolyte-contacting surface, which permits a long contact time between the reactants.

The term "high surface area" in relation to the cathode refers to an electrode of the type wherein the electrolyte is exposed to a large surface area of electrode surface in comparison to the physical dimensions of the electrode. The electrode is formed with interstices through which the electrolyte flows, and so has a three-dimensional surface of contact with the electrolyte.

The high surface area cathode may be the so-called "flow through" type, wherein the electrode is formed of electroconductive porous material, for example, layers of electroconductive cloth and the electrolyte flows through the porous structure generally parallel to the current flow while being subjected to electrolysis, and thereby is exposed to the high surface area of the mesh of the electrode.

The high surface area cathode also may be the so-called "flow by" type, wherein the electrode comprises a packed bed of individual elactroconductive particles and the electrolyte flows through the packed bed generally perpendicular to the current flow while being subjected to electrolysis, and thereby is exposed to the high surface area of the electroconductive particles in the packed bed.

The electrode may be constructed of materials having a low overpotential or preferably high t 1 z cP~' overpotential, particularly graphite, for the reaction C1 2 As is well known to those skilled in the electrochemical art, the overpotential of an electrode towards the electrochemical reaction C1 2 /C-1 refers to the relationship of the potential applied to the electrode to the equilibrium potential to sustain the electrochemical reaction at a reasonable rate. If the electrode potential is close to the equilibrium potential, then the electrode is considered to have a "low" overpotential while, if a much more negative potential is required to achieve a significant reduction rate, then the electrode is considered to have a "high" overpotential.

Materials of construction of such low overpotential electrodes are known and are employed in the so-called "Dimensionally Stable Electrodes". Such electrodes generally comprise a substrate, which is titanium, zirconium, tantalum or hafnium, having an electroconductive coating thereon, which may be a precious metal, for example, platinum; a precious metal alloy, for example, a platinum-iridium alloy; a metal oxide, for example, ruthenium oxide or titanium dioxide; a platinate, for example, lithium platinate or calcium platinate; or mixtures of two or more of such materials.

Any of these materials may be employed to provide the material of construction of a low overpotential cathode.

The cell 10 in which the electrolytic production of chlorine dioxide is effected in accordance with the present invention may have any convenient construction.

Usually, the cell is divided into anolyte and catholyte compartments 20 and 14 by an ion-exchange membrane 18, usually a cation-exchange membrane so as to promote hydrogen ion transfer and to prevent the interaction of gases produced at the anode, usually oxygen, with the chlorine dioxide and the electroreduction at the cathode. The anode of the cell may be constructed of c 25 f Z 9 any desired electroconductive material, for example, graphite or metal.

Referring now to Figure 2, there is shown the integration of the chlorine dioxide generator 10 of Figure 1 with a chlorate cell 30 and a chloritegenerating bell 32, as described in more detail below.

In this embodiment, the sodium chloride by-product in line 28 is forwarded to the chlorate cell 30, wherein the sodium chloride is electrolyzed to form sodium chlorate, which is recycled by line 12 to the chlorine dioxide generator 10. By-product hydrogen from the electrolysis in the chlorate cell 30 is vented by line 34.

o Chlorine dioxide formed in the generator 10 is 15 forwarded by line 26 to the cathode compartment 36 of t ee Vl,, the chlorite-generating cell 32. Sodium chloride is fed by line 38 to an anode compartment 40 of the chloritegenerating cell 32. Anodic electrolysis produces chlorine while sodium ions migrate across a cationexchange membrane 42 separating the anode compartment from the cathode compartment 36. In the cathode compartment, the chlorine dioxide forwarded by line 26 forms chlorite ions, resulting in a discharge of sodium chlorite solution in line 44 from the cathode compartment 36.

7' Depleted sodium chloride solution exiting the anode compartment 40 is recycled by line 46. The chlorine i' formed in the anode compartment 40 is passed by line 48 to the cathode compartment 14 of the chlorine dioxide generator 10. In comparison to Figure 1, all the hydrogen ions and chloride ions for the cathodic producti, of chlorine dioxide are produced in situ in compartment 14 from the chlorine fed by line 48 and hydrogen ion migration. This result is achieved by increasing the current supplied to the cell from 1 I Faraday to 2 Faradays per mole of chlorine dioxide produced.

The overall process between the chlorine dioxide generator 10 and the chlorite cell 32 (theoretically) requires no additional input of hydrogen ions and/or chloride ibns, since all the hydrogen ions and/or chloride ions required by the chlorine dioxide generator are provided within the system and no chlorine output requires to be handled. Further integration with the chlorate cell produces a system wherein the only inputs are sodium chloride and power and the only outputs are sodium chlorite, hydrogen and oxygen.

A modification of the procedure of Figure 2 involves forwarding sodium chloride from the anolyte 15 chamber 40 of the chlorite-generating cell 32 to the t f t chlorate cell 30. In addition, any hypochlorous acid in the hydrogen off-gas stream 34 may be condensed and recycled to cathode compartment of the chlorine dioxide generator In Figure 3, there is illustrated integration of the chlorine dioxide generator 10 with a causticchlorine cell 50. In this case, thb sodium chloride byproduct, along with unreacted sodium chlorate, is forwarded by line 28 to the anode compartment 52 of the 25 caustic-chlorine cell 50. An electrolyte is forwarded by line 54 to the cathode compartment 56 of the causticchlorine cell 50, separated from the anode compartment 52 by a cation-exchange membrane 58.

Chlorine produced in the anode compartment 52 is forwarded as an aqueous solution in the unreacted sodium chlorate, by line 60 to the cathode compartment of the chlorine dioxide generator 10. Sodium hydroxide is recovered from the cathode compartment 50 as product in line 62 and by-product hydrogen gas is vented by line 64.

The overall process for the Figure 3 embodiment is depicted by the equation:

H

2 0 NaClO 3 2e C10 2 NaOH kH 2 The input requirements are sodium chlorate and power to produce chlorine dioxide, sodium hydroxide, oxygen and hydrogen. -The sodium hydroxide is useful elsewhere in the mill and the by-product gases may be vented.

H The invention is illustrated by the following Example: An experimental cell was set up as seen in Figure 1. The cell was a conventional MP cell from Electrocell AB which had been modified to accommodate a threedimensional electrode formed by inserting a graphite Vfelt (Union Carbide Corporation) into the cathode compartment. The cell was divided into anode and cathode compartments by a cation exchange membrane (NAFION 120). The membrane area was 1 sq.dm while the area of the cathode was estimated to be approximately 100 to 1000 times the membrane area. An oxygen-evolving dimensionally-atable electrode was used as the anode.

Feed to the cathode compartment was 8.626 moles of sodium chlorate, 2.356 moles of sodium chloride and 1.536 moles of HCl. 6N H 2 S0 4 was used as the anolyte.

An electrode potential of about -0.7 volts vs. SCE was applied to the cathode at a current density og 1.97 kA/m 2 for a period of 4 hrs at 70*C. The effluent from the cathode chamber contained 7.659 moles NaClO 3 V £3.548 moles NaCi. The off-gases were analyzed and contained 0.626 moles of C10 2 and 0.068 moles Of C1 2 The chlorine dioxide had a purity of 90.2%, produced at a chemical efficiency of 82.2%.

In summary of this disclosure, the present invention provides a novel electrolyte pro~cess for the production of chlorine dioxide in substantially pure form. Modifications are possible within the scope of this invention.

Claims

1. An electrolytic process for the production of chlorine dioxide, which comprises providing an electrolytic cell having a cathode compartment with a three-dimensional high surface-area cathode therein and an anode *compartment separated from the cathode compartment by a cation-exchange membranes; feeding chlorate ions to the cathode compartment and providing hydrogen ions and chioride ions in the cathode compartment; reducing the chlorate ions with the hydrogen ions and chloride ions in the cathode compartment to form chlorine dioxide while an electric current is applied to the cathode compartment to reduce "o chlorine co-produced with the chlorine dioxide to o0 0 0Oo chloride ions; venting chlorine dioxide so produced i,,a from the cathode compartment; and electrolytically c forming hydrogen ions in the anode compartment and S transferring the hydrogen ions across an ion exchange membrane from the anode compartment to the cathode compartment.

2. A process as claimed in claim 1, in which the hydrogen ions and chloride ions in the cathode compartment are provided in part by the hydrogen ions transferred to the cathode compartment from the anode compartment and by the chloride ions produced by electrolytic reduction of the co-produced chlorine, and in part by hydrogen ions and chloride ions fed to the I *cathode compartment from external sources thereof.

3. A process as claimed in claim 2, in which the external source hydrogen ions and chloride ions are provided by hydrochloric acid.

4. A process as claimed in eic.'r claim 2 or 3, in which 1 Faraday of electrical current is applied to the cell per mole of chlorine dioxide produced. A process as claimed in claim 1, in which the hydrogen ions and chloride ions in the cathode I~- 13 compartment are provided, for hydrogen ions, wholly by the hydrogen ions transferred to the cathode compartment from the anode compartment and, for chloride ions, in part by the chloride ions produced by electrolytic reduction of the co-produced chlorine and in part by chloride ions produced by electrolytic reduction of chlorine fed to tha cathode compartment from an external source.

6. A process as claimed in claim 5, in which 2 1o Faradays of electrical current are applied to the cell per mole of chlorine dioxide produced.

7. A process as claimed in either claims 5 or 6 which is integrated with a sodium chlorite-producing electrolytic process wherein the vented chlorine dioxide is electrolytically reduced to chlorite ions and, chlorine is electrolytically formed and is forwarded to the cathode compartment to provide the chlorine feed thereto. S8. A process as claimed in claim 7 which is further integrated with a sodium chlorate-producing electrolytic Sprocess wherein by-product sodium chloride from the cathode compartment is electrolyzed to provide the sodium chlorate feed to the cathode compartment.

9. A process as claimed in either claim 5 or 6 which is integrated with a caustic-chlorine cell wherein by- product sodium chloride from the cathode compartment is Selectrolyzed to provide the chlorine feed to the cathode Scompartment. A process as claimed in any one of claims 1 to 9, in which the fatholyte in the cathode compartment has a chlorate ion concentration of at least 5 molar and a total acid normality of at least 0.01N.

11. A process as claimed in any one of claims 1 to in which the catholyte in the cathode compartment has a chlorate ion concentration of 5 to 6.5 molar, a chlorate ~e 4 14 to chloride ion ratio of 2:1 to 4:1 and a total acid normality of at least 0.05 normal.

12. A process as claimed in any one of claims 1 to 11, in which the catholyte in the cathode compartment has a temperature of at least

13. A process as claimed in claim 12, in which the temperature is 600 to :14. A process as claimed in any one of claims 1 to 13, in which the chlorate ions are provided by an aqueous solution of sodium chlorate. A process as claimed in any one of claims 1 to '4, in which an electrode potential is applied to the cathode which is more positive than -1 volt as compared S with a saturated calomel electrode and as determined at the current feeder to the three-dimensional cathode and more negative than the open circuit potential under the prevailing conditions.

16. A process as claimed in claim 15, in which the electrode potential is -0.2 volt.

17. A process as claimed in any one of claims 1 to 16, in which the cathode comprises stacked layers of electroconductive mesh material through the interstices Se of which percolates the chlorate solution generally parallel to the current flow.

18. A process as claimed in any one Pf claims 1 to 16, in which the cathode comprises a packed bed of individual electroconductive particles through which percolates the chlorate solution generally perpendicular M Tto the current flow.

19. A process as claimed in any one of claims 1 to 18, in which the catl de is constructed of a material having a high overpotential for the reaction Cl 2 Cl1. A process as claimed in claim 19, in which the nigh overpotential electrode material is graphite or other carbonaceous material.

21. A process as claimed in any one of claims 1 to which is carried out continuously by continuously feeding an aqueous sodium chlorate solution to the cathode compartment, continuously reducing the sodium chlorate in the cathode compartment with hydrogen ions and chloride ions while an electric current is applied between the anode and cathode compartments, continuously electolytically reducing chlorine co-produced with the chlorine dioxide to chloride ions, continuously to electrolytically forming hydrogen ions from an electrolyte in the anode compartment and transferring the electrolytically-formned hydrogen ions from the anode compartment to the cathode compartment, continuously providing in the cathode compartment the balance of hydrogen ions and chloride ions required in the reduction of sodium chlorate, continuously venting product chlorine dioxide and continuously removing a by- product stream of sodium chloride solution from the cathode compartment.

22. An electrolytic process for the production of i o chlorine dioxide substantially as hereinbefore described S' with reference to, and as illustrated in, Figure 1 of c the accompanying drawings. i 23. An electrolytic process for the production of chlorine dioxide integrated with an electrolytic process for the production of sodium chlorate from the V electrolytically-produced chlorine dioxide, oo substantially as hereinbefore described with reference i to, and as illustrated in, Figure 2 of the accompanying S0 drawings.

24. An electrolytic process for the production of chlorine dioxide from sodium chlorate, wherein by- product sodium chiroide results, integrated with an electrolytic process for producing sodium hydroxide and chlorine for use in the electrolytic production of chlorine dioxide from the by-product sodium chloride, 16 substantially as hereinbefore described with reference to, and as illustrated in, Figure 3 of the accompanying drawings. An electrolytic process for the production of chlorine dioxide substantially as hereinbefore described with reference to the Example.

26. Chlorine dioxide whenever prepared by a process as claimed in any one of claims 1 to DATED: 7 December 1988 PHILLIPS ORMONDE FITZPATRICK Attorneys For: TENNECO CANADA INC. -".lrhpr 1 ;A