CA1073402A - Electrolytic manufacture of chlorates using a plurality of electrolytic cells - Google Patents
Electrolytic manufacture of chlorates using a plurality of electrolytic cellsInfo
- Publication number
- CA1073402A CA1073402A CA211,588A CA211588A CA1073402A CA 1073402 A CA1073402 A CA 1073402A CA 211588 A CA211588 A CA 211588A CA 1073402 A CA1073402 A CA 1073402A
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- Canada
- Prior art keywords
- chlorate
- cell
- chloride
- chlorine
- anode
- Prior art date
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Classifications
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
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- Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Manufacture Of Macromolecular Shaped Articles (AREA)
Abstract
ELECTROLYTIC MANUFACTURE OF CHLORATES, USING A PLURALITY OF ELECTROLYTIC CELLS
ABSTRACT OF THE DISCLOSURE
A sodium chloride solution is electrolyzed to produce a high strength caustic solution and sodium chlorate solution, using two different electrolytic cells. In the first cell, a two-compartment cell in which the compartments are separated by a permselective membrane of a hydrolyzed copolymer of a per-fluorinated hydrocarbon and a fluorosulfonated perfluorovinyl ether or of a sulfostyrenated perfluorinated ethylene propylene polymer, the sodium chloride solution is electrolyzed at a pH of about 4 to 7 to produce aqueous sodium hydroxide solution in the cathode compartment and chlorine and cell liquor containing chlorate in the anode compartment. Then, the cell liquor, already containing some chlorate, is further electrolyzed in a conventional chlorate cell or equivalent apparatus to convert chloride therein to chlorate. After separation of the chlorate from chloride present with it the chloride is returned to the first cell.
ABSTRACT OF THE DISCLOSURE
A sodium chloride solution is electrolyzed to produce a high strength caustic solution and sodium chlorate solution, using two different electrolytic cells. In the first cell, a two-compartment cell in which the compartments are separated by a permselective membrane of a hydrolyzed copolymer of a per-fluorinated hydrocarbon and a fluorosulfonated perfluorovinyl ether or of a sulfostyrenated perfluorinated ethylene propylene polymer, the sodium chloride solution is electrolyzed at a pH of about 4 to 7 to produce aqueous sodium hydroxide solution in the cathode compartment and chlorine and cell liquor containing chlorate in the anode compartment. Then, the cell liquor, already containing some chlorate, is further electrolyzed in a conventional chlorate cell or equivalent apparatus to convert chloride therein to chlorate. After separation of the chlorate from chloride present with it the chloride is returned to the first cell.
Description
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. This invention relates to the electrolytic manufacture . of chlorates. More.specifically, it is of a process for making alkali metal chlorate, alkali metal hydroxide, chlorine and hydrogen from aqueous alkali me~al chloride solution by electro-, 5 lysis of the solution in a two compartment cell equipped with an effèctive cation-active permselective membrane divider, with the production of some chlorate in the anolyte, and subsequent electrolysis of the-anolyte in a chlorate cell. Polymeric material found to be effective as the membrane is a hydrolyzed '10 . polymer of a perfluorinated hydrocarbon and a fluorosulfonated perfluorovinyl ether or is a sulfostyrenated perfluorinated ethylene propylene polymer.
An advantage of this invention is that ~kali metal ~
i:~ chlorate produced by transmission of hydroxide through-the ~. -~15 membrane into the anolyte is recovered and the "contaminated" ;- ~
.: tchlorate-containing) anolyte is subsequently utilized as a feed ~ ~.
, ~ ~ to a chlorate cell. Satisfactory efficiencies are obtained under the.process conditions and little or no hydrochloric acid is - needed for the treatment of.the anolyte. , ,20 . ~n accordance with the present invention a method for ~: . -. electrolytically manufacturing hydroxide, chlorine and chlorate comprises electrolyzing an aqueous solu~Dn containing chloride .,~ .
: ions in an electrolytic chlorine cell having anode and cathode compartments, an anode, a cathode, a cation-active permselective membrane of a hydrolyzed copolymer of a perfluorinated hydrocarbon ~, . .
~ .
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and a fluorosulfonated perfluorovinyl ether, or of a sulfostyre-nated perfluorinated ethylene propylene polymer, defining a boundary between the cathode and anode compartments and between the anode and the cathode, to produce an aqueous hydroxide solu-tion and hydrogen in the cathode compartment and chlorine and chlorate in the anode compartment, removing the aqueous hydroxide solution and anolyte liquor containing chlorate and further electrolyzing the liquor in a chlorate cell to convert chloride therein to chlorate.
According to another aspect of the invention there is provided an electrolytic cell system for electrolytically manu-facturing hydroxide, chlorine and chlorate which comprises an electrolytic chlorine cell comprising a housing having an anolyte compartment, containing an anode adapted to be connected to an electrical input source; a catholyte compartment containing a cathode, a cation-active permselective membrane of a hydrolyzed copolymer of a perfluorinated hydrocarbon and a fluorosulfonated perfluorovinyl ether, or of a sulfostyrenated perfluorinated ethylene propylene polymer, defining a boundary between the catholyte and the anolyte compartments and between the anode and the cathode, outlet means from said anolyte compartment for removing anolyte liquor containing chlorate; and a chlorate cell for converting chloride to chlorate; said chlorate cell having inlet means connected to said outlet means for passage of said anolyte liquor from said anolyte compartment to said chlorate ~; cell.
The invention will be readily understood by reference to the following descriptions of embodiments thereof, taken in conjunction with the drawing in which:
The FIGURE is a schematic representation of the arrangement of cells and equipment for producing chlorate with hydroxide, chlorine and hydrogen.
. This invention relates to the electrolytic manufacture . of chlorates. More.specifically, it is of a process for making alkali metal chlorate, alkali metal hydroxide, chlorine and hydrogen from aqueous alkali me~al chloride solution by electro-, 5 lysis of the solution in a two compartment cell equipped with an effèctive cation-active permselective membrane divider, with the production of some chlorate in the anolyte, and subsequent electrolysis of the-anolyte in a chlorate cell. Polymeric material found to be effective as the membrane is a hydrolyzed '10 . polymer of a perfluorinated hydrocarbon and a fluorosulfonated perfluorovinyl ether or is a sulfostyrenated perfluorinated ethylene propylene polymer.
An advantage of this invention is that ~kali metal ~
i:~ chlorate produced by transmission of hydroxide through-the ~. -~15 membrane into the anolyte is recovered and the "contaminated" ;- ~
.: tchlorate-containing) anolyte is subsequently utilized as a feed ~ ~.
, ~ ~ to a chlorate cell. Satisfactory efficiencies are obtained under the.process conditions and little or no hydrochloric acid is - needed for the treatment of.the anolyte. , ,20 . ~n accordance with the present invention a method for ~: . -. electrolytically manufacturing hydroxide, chlorine and chlorate comprises electrolyzing an aqueous solu~Dn containing chloride .,~ .
: ions in an electrolytic chlorine cell having anode and cathode compartments, an anode, a cathode, a cation-active permselective membrane of a hydrolyzed copolymer of a perfluorinated hydrocarbon ~, . .
~ .
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and a fluorosulfonated perfluorovinyl ether, or of a sulfostyre-nated perfluorinated ethylene propylene polymer, defining a boundary between the cathode and anode compartments and between the anode and the cathode, to produce an aqueous hydroxide solu-tion and hydrogen in the cathode compartment and chlorine and chlorate in the anode compartment, removing the aqueous hydroxide solution and anolyte liquor containing chlorate and further electrolyzing the liquor in a chlorate cell to convert chloride therein to chlorate.
According to another aspect of the invention there is provided an electrolytic cell system for electrolytically manu-facturing hydroxide, chlorine and chlorate which comprises an electrolytic chlorine cell comprising a housing having an anolyte compartment, containing an anode adapted to be connected to an electrical input source; a catholyte compartment containing a cathode, a cation-active permselective membrane of a hydrolyzed copolymer of a perfluorinated hydrocarbon and a fluorosulfonated perfluorovinyl ether, or of a sulfostyrenated perfluorinated ethylene propylene polymer, defining a boundary between the catholyte and the anolyte compartments and between the anode and the cathode, outlet means from said anolyte compartment for removing anolyte liquor containing chlorate; and a chlorate cell for converting chloride to chlorate; said chlorate cell having inlet means connected to said outlet means for passage of said anolyte liquor from said anolyte compartment to said chlorate ~; cell.
The invention will be readily understood by reference to the following descriptions of embodiments thereof, taken in conjunction with the drawing in which:
The FIGURE is a schematic representation of the arrangement of cells and equipment for producing chlorate with hydroxide, chlorine and hydrogen.
- 2 -`` 107340Z
, In the FIGURE electrolytic chlorine cell 11 includes outer wall 13, anode 15, cathode 17 and conductive means 19 and 21 for connecting the anode and the cathode to sources of positive and negative electrical potentials, respectively.
Inside the walled cell cation-active permselective membrane 23 divides the volume into anode or anolyte compartment 27 and cathode or catholyte compartment 29. Alkali metal halide solu-. tion is fed to the anolyte compartment through line 33 and chloride, separated out from chlorate-chloride`solution produced in chlorate cell 35, is employed to make up halide feed to the .
.
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~ `, o lOq340~ , anode compartment, being added with other chloride to resaturator 36. Water is fed to the cathode compartment 29 through line 37.
Of course, additions of electrolyte and water should be such as to maintain the desired liquid levels in the anode and cathode ` 5 compartments and this may often be effected with feed-overflow devices and similar techniques, which are known in the art and therefore, are not illustrated.
In the pre sent cell halogen, e.g., chlorine gas, is removable from the anolyte compartment through line 39 and hydrogen is removable from the catholyte compartment through line 42. A comparatively high concentration of aqueous hydroxide solution may be taken off from the catholyte through exit 43.
Because the cation-active permselective membrane 23 allows some hydroxyl ions to migrate through it from the catholyte to the anolyte these can react to produce chlorate in the anolyte and the cell liquor resulting, a mixture of chlorate and chloride in aqueous solution, is removed at 45 and transferred through line 47 to the interior 49 of chlorate cell 35. In such cell, due to the absence of any diaphragms or separators between anode 51 and cathode 53 the products of electrolysis, chlorine and - hydroxide, interact and form chlorate, possibly also with the formation of some hypochlorite. By controlling the pH in tne chlorate cell to be within the 6 to 7.5 range the production o~
chlorate can be favored. If desired, hypochlorite may be produced in the cell and converted externally to chlorate, which . . .
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may then be processed further as described herein.
The chlorate and chloride in solution are removed from chlorate cell 35 through line 55 after the concentration of chlorate has increased sufficiently and that of chloride is lo~J
enough so as not to be salted out in the chlorate cell. Under the conditions employed the chloride is removed from the chlorate solution as a solid in separator 57 and then passes through line 59 or other suitable transfer mechanism to resaturator 36 and back to chlorine cell ll. The chlorate is crystallized out of the solution in crystallizer 61, being removed at 63. The mother liquor remaining is sent back to the chlorine cell through line 64, preferably via resaturator 36 or is recycled via line 65.
; The chlorine taken off from chlorine cell 11 may be burned in the hydrogen produced to form hydrochl~oric acid, which may be used to adjust pH in the resaturator, cell or separating ; and crystallizing apparatuses. Also, the chlorine may be reacted externally of the cell with hydroxide removed from the cell, to produce chlorate.
Various recirculations of compartment contents, pre-., "b 20 ferably intracompartmentally, may also be employed. Although ~' continuous processes such as illustrated are highly preferred, ~` once-through processes, batch method and "hybrid" processes are also useful. --~ The ~ain aspect of the present invention is in its utilization of a single permselective membrane chlorine cell to .
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.
make high purity, high strength caustic solution and at the same time produce some chlorate in the anolyte, which is subsequently made useful by processing the anolyte liquor through a chlorate cell and recycling back to the chlorine cell non-chiorate products.
s It has been found that this process can be effected at anode i efficiencies of over 85% and even over 90% and at caustic ' efficiencies over 75% and often over 80~.
- The selective ion-passing effects of cationic membranes ~ f ! : .' .
h a v e been noted in the past but the membranes of this invention have not been employed in the present processes before and the .. . .
unexpectedly beneficial effects resulting have not been previous-ly obtained or suggested. Thus, with the use of a comparatively `; thln membrane, preferably supported as described herein, several ,~ years o. opera~iûn under co~me,-cial conditions ar~ obtair,able .. ;
' lS without the need for removal or replacement of the membrane, :~, while all the time it efficiently prevents undesirable migration of chloride from the anode compartment to the cathode compartment, thus allowing production of high purity caustic. It prevents ; hydrogen formed on the cathode _ide from escaping into the halogen formed on the anode side and vice versa. In this respect the present membranes are superior to prior art membranes, being - more impervious to the passage of gases, even when the membranes are very thin, than various other polymeric materials. The prevention of hydrogen mixing with chlorine is important since these materials form explosive mixtures, especially in the Rresence , .
: - , ., : .
.
. .. .
o of oxygen, such as may be produced in the present processes. The superiority of the preferred membranes, including modified or surface treated versions thereof, over prior art membranes in the various described aspects is also evident, usually to a lesser degree, in the sulfostyrenated fluorinated ethylene propylene ; polymers.
The membranes employed are normally thin flat sheets, normally rectangular, but various other shapes and configurations may be employed. Plural membranes may be used together but usually this is of no special advanta.ge. Buffer compartments may be formed but are detrimental to the carrying out of the present processes. Instead of monopolar electrodes, bipolar electrodes may be utilized.
-, The aqueous solution containing chloride ions is ~15 normally a water solution of sodium chloride, although potassium `
and other soluble chlorides, e.g., magnesium chloride, may be utilized, at least in part. However, it is preferred to employ the alkali metal chlorides and of these, sodium chloride is -; the best. Similarly, the chlorates made will preferably be alkali metal chloratesand the hydroxides will be alkali metal hydroxides, most preferably all being sodium compounds.
The concentration of sodium chloride in a charge to the anolyte and in the anolyte will usually be as high as feasible, normally being from 200 to 320 grams per liter for sodium chloride and from 200 to 360 g./l. for potassium chloride, wi-th . - - -....... . .
10~
intermediates for mixtures thereof. The electrolyte may be acidified to a pH in the range of 2 to 6 but in many applications, as when hydrochloric acid is not readily available for acidification, instead of the addition of acid to provide a pH range of 2 to 6, the pH may be from 4 to 7, preferably about 6, and may be that resulting from generation of chlorine in the anolyte and its neutralization, at least in part, by sodium hydroxide. A most preferred concentration of sodium chloride in water is 250 to 300 9./1. Because the chlorine cell anolyte, containing chlorate made therein, is the feed to the chlorate cell, the chloride content of the chlorate cell liquor is less than that of the chlorine cell anolyte fed to it, due to conversion of some of the chloride to chlorine and thence to chlorate in the chlorate cell. After removal .~ of chloride and chlorate from the withdrawn chlorate cell liquor the chloride concentration will be still lower and the mother liquor ' which may be returned to the resaturator will normally be less than 50 or 100 g./l. concentration. It may contain a small-er quantity of chlorate, too.
The presently preferred cation permselective membrane is of a :''d 20 hydrolyzed copolymer of perfluorinated hydrocarbon and a fluoro-sulfonated perfluorovinyl ether. The perfluorinated hydrocarbon is preferably tetrafluoroethylene, although other perfluorinated ` and saturated and unsaturated hydrocarbons of 2 to 5 carbon atoms may also be utilized, of which the monoolefinic hydrocarbons are preferred, especially those of 2 to 4 carbon atoms.
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lOq3402 and most especially those of 2 to 3 carbon atoms, e.g., tetrafluoroethylene, hexafluoropropylene. The sulfonated perfluorovinyl ether which is most useful is that of the formula FS02CF2CF20CF~CF3)CF20CF=CF2. Such a material, named as perfluoro[2-(2-fluorosulfonylethoxy)-propyl vinyl ether], referred to henceforth as PSEPVE, may be modified to equivalent monomers~ as by modifying the internal per-; fluorosulfonylethoxy component to the corresponding propoxy component and by altering the propyl to ethyl or butyl, plus rearranging positions of substitution of the sulfonyl thereonand utilizing isomers of the perfluoro-lower alkyl groups, respectively. However, it is most preferred to employ PSEPVE.
The method of manufacture of the hydrolyzed copolymer - -is described in Example XVII of U.S. Patent 3,282~875 and an alternative method is mentioned in Canadian Patent 849,670, which also discloses the use of the finished membrane in fuel cells, characterized therein as electro-chemical cells. In short, the copolymer may be made by -reacting PSEPVE or equivalent with tetrafluoroethylene or equivalent in desired proportions in water at elevated temperature and pressure for over an hour, after which time the mix is cooled. It separates into a lower perfluoroether layer and an upper layer of aqueous medium with dispersed desired polymer. The molecular weight is indeterminate by the equivalent weight is about 900 to 1,600 preferably 1,100 . . . ~ . .
1073~02 to 1,400 and the percentage of PSEPVE or corresponding compound is about 10 to 30%, preferably 15 to 20% and most preferably about 17%. The unhydrolyzed copolymer may be compression molded at high temperature and pressure to produce sheets or membranes, which may vary in thickness from 0.02 to 0.5 mm. These are then further treated to hydrolyze pendant -S02F groups to -S03H groups, as by treating with 10% sulfuric acid or by the methods of the patents previously mentioned. The presence of the -S03H
groups may be verified by titration, as described in the Canadian patent. Additional details of various processing - -steps are described in Canadian Patent 752,427 and U. S.
~` Patent 3,041,317.
Because it has been found that some expansion accomp-anies hydrolysis of the copolymer it is preferred to posi-tion the copolymer membrane after hydrolysis onto a frame or other support which will hold it in place in the electro-lytic cell. Then it may be clamped or cemented in place and will be true, without sags. The membrane is preferably joined to the backing tetrafluoroethylene or other suitable filiments prior to hydrolysis, when it is still thermoplas-tic so that the film of copolymer covers each filament, penetrating into the spaces between the filaments and even around behind said filaments the films becoming slightly thinner in the process, where they cover the filaments.
The membrane described is far superior in the present processes to all other previously suggested membrane mater-- ials.
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It is more stable at elevated temperatures, e.g., about 75C.
It lasts for much longer time periods in the medium of the electrolytè and the caustic product and does not become brittle when subjected to chlorine at high cell temperatures. Considering the savings in time and fabrication costs, the present membranes are more economical. The voltage drop through the membrane is acceptable and does not become inordinately high, as it does with ; many other membrane materials, when the caustic concentration in the cathode compartment increases to above about 200 9./1. of caustic. The selectivity of the membrane and its compatibility with the electrolyte do not decrease detrimentally as the hydroxyl concentration in the catholyte liquor increases, as has been noted with other membrane materials. Furthermore, the caustic ` efficiency of the electrolysis does not diminish as significantly as it does with other membranes when the hydroxyl ion concentration in the catholyte increases. Thus, these differences in the present process make it practicable, whereas previously descrlbed processes have not attained commercial acceptance. While the more preferred copolymers are those having equivalent weights of 900 to 1,600, with 1,100 to 1,400 being most preferred, some useful resino~s membranes employable in present methods may be of equivalent weights from 500 to 4,000. The medium equivalent weight polymers are preferred because they are of satisfactory strength and stability, enable better selective ion exchange to take place and are of lower internal resistances, all of which are important to the present electrochemical cell.
- . , .
111~340Z
Improved versions of the above-described copolymers may be made by chemical treatment of surfaces thereof, as by treatments to modify the -S03H group thereon. For example, the sulfonic group may be altered on the membrane to produce a concentration gradient.
Such a change may be made in the manufacturing process or after production of the membrane. When effected as a subsequent surface treatment of a membrane the depth of treatment will usually be from 0.001 to 0.01 mm. Caustic efficiencies of the invented processes, using such modified versions of the present improved membranes can increase about 3 to 20%, often about 5 to 15%.
Exemplary of such treatments is that described in French patent publication 2,152,194 of March 26, 1973 in which one side of the membrane is treated with NH3 to form S02NH2 groups.
In addition to the copolymers previously discussed, including modifications thereof, it has been found that another type of membrane material is also superior to prior art films for applications in the present processes. Although it appears that tetrafluoroethylene (TFE) polymers which are sequentially styrenated and sulfonated are not useful for making satisfactory cation-active permselective membranes for use in the present electrolytic processes it has been established that perfluorinated ethylene propylene polymer (FEP) which is styrenated and sulfo-nated makes a useful membrane. Whereas useful lives of as much ~ as three years or more (that of the preferred copolymers) may not '~' - lZ -,`
o lOq3402 be obtained,the sulfostyrenated FEP's are surprisingly resistant to hardening and otherwise failing in use under the present process conditions.
; To manufacture the sulfostyrenated FEP membranes a standard FEP, such as manufach~edby E. I. DuPont de Nemours &
Co. Inc., is styrenated and the styrenated polymer is then sulfonated. A solution of styrene in methylene chloride or benzene at a suitable concentration in the range of about 10 to 20% is prepared and a sheet of FEP polymer having a thickness of about 0.02 to 0.5 mm., preferably 0.05 to 0.15 mm., is dipped into the solution. After removal it is subjected to radiation treatment, using a cobalt60 radiation source. The rate of appli-` cation may be in the range of about 8,000 rads/hr. and a total radiation application is about 0.9 megarad. After rinsing with water the phenyl rings of the styrene portion of the polymer are monosulfonated, preferably in ~ ~aposition, by treatment with chlorosulfonic acid, fuming sulfuric acid or SO3. Prefer-ably, chlorosulfonic acid in chloroform is utilized and the sulfonation is completed in about 1/2 hour.
- 20 Examples of useful membranes made by the described process are products of RAI Research Corporation, Hauppauge, New Yor~, identified as 18ST12S and 16ST13S, the former being 18% styrenated and having 2/3 of the phenyl groups monosulfonated ~nd the latter being 16~ styrenated and having 13/16 of the phenyl groups monosulfonated. To obtain 18% styrenation a solution of clemark D
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17 1/2X of styrene in methylene chloride is utilized and to obtain the 16X styrenation a solution of 16X of styrene in methylene chloride is employed.
The products resulting compare favorably with the ` 5 preferred copolymers previously described, giving voltage drops of about 0.2 volt each in the present cells at a current density of 2 amperes/sq. in., the same as is ob- -tained from the copolymer.
The membrane wall will nor~ally be from 0.02 to 0.5 - 10 mm. thick, preferably from 0.1 tc 0.5 mm. and most prefer-~ ably 0.1 to 0.3 mm. When the membrane is mounted on a net-`; work of material selected from the group of polytetrafluoro-ethylene, asbestos, perfluorinated ethylene, propylene polymer, polypropylene, tantalum, titanium, niobium and nob~e metals, for support, the network filaments or fibers will usually have a thickness of 0.01 to 0.5 mm., prefer-` ably 0.05 to 0.15 mm., corresponding to up to the thickness of the membrane. Often it will be preferable for the fila-menbs to be less than half the film thickness but filament thicknesses greater than that of the film may also be suc-cessfully employed, e.g., 1.1 to 5 times the film thick-ness. The networks, screens or cloths have an area per-centage of openings therein from about 8 to 80%, preferably 10 to 70X and most preferably 30 to 70X. Generally the cross-sections of the filaments will be circular but other ---shapes, such as ellipses, squares and rectangles, are also ;~ useful. The supporting network is preferably a screen or cloth and a.lthough it may be cemented to the membrane it is preferred that it be fused to it by high temperature, high pressure compression before hydrolysis of the copoly-mer. Then,the membrane-network composite can be clamped , , s~ -\~ o :10~34~;~
, ' .
or otherwise fastened in place in a holder or support.
The material of construction of the cell body may be conventional, including steel, concrete or stressed concrete lined with mastics, rubbers, e.g., neoprene, polyvinylidene chloride, FEP, chlorendic acid based polyester, polypropylene, polyvinyl chloride, TFE or other suitable plastic or may be similarly lined boxes of other structural materials. Substantial-ly self-supporting structures, such as rigid polyvinyl chloride polyvinylidene chloride,polypropylene or phenol formaldehyde resins may be employed, preferably reinforced with molded-in fibers, cloths or webs.
The migration of caustic into the anolyte compartment of the chlorine cell may be controlled by regulating the con-centration of caustic in the catholyte or by using a membrane of different thickness, more caustic being tranferred when the thick-ness is diminished. The rate of feed will determine to some ex-tent the pH in the anolyte and it is desirable to keep this in the range of 3 to 7.5, preferably 3 or 4 to 7, so as to make chlorate.
Recirculation rates may also be adjusted to help maintain the pH in the desired range and,as was mentioned previously, acids (or -~ bases) may also be utilized. On the average it is considered that a controlled proportion, from 5 to 50~ of the caustic ~! produced in the catholyte compartment, as desired, may migrate ' ~,1 .
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to the anolyte compartment and the cell design and components may ` be varied to obtain the particular proportion most preferred.
The pH of the chlorate cell may be regulated in similar manner.
In addition to controlling the pH's of the chlorine cell anolyte and the electrolyte of the chlorate cell the tempe-~ ratures of these are also usually regulated. Normally they are - maintained at less than 105C., preferably being from 20 to 95C., more preferably from 50 to 95~C. and most preferably about 60 or 65~C. to 85 or 95C. Usually `the chlorate cell is operated at about 70C. Electrolyte temperatures may be controlled by ~ recirculation of various portions thereof or by changing the -i proportions of feed. When the temperature cannot be lowered sufficiently by recirculation, refrigeration of the recirculating liquid(s) may also be utili~ed.
The processes of this invention, utilizing a single -~.!
cation-active permselective diaphragm in a two compartment chlorine cell, operate at comparatively high efficiencies. By holding the anolyte p~ in the range given, preferably at about 4.5, efficiencies of 80~ (caustic efficiency) and more an~ of 90%
(anode efficiency) and more are obtainable. Under such conditions, *
80% caustic efficiency and 90~ anode efficiency, two-compartment .. . . .
cellsof the type described, rated at a capacity of 1 ton per day of chlorine, will produce about 0.9 T/d of sodium t hydroxide, 0.8 T/d of chlorine and 0.05 T/d of sodium chlorate.
--,?t 25 The amount of chlorate produced will be increased, in accordance .:'.
- with the invention, by feeding the chlorine cell chlorate plus , .. . .
chIoride into a chlorate cell. Of course, additional chloride . ~ . ' ~ ! o .
.
.
may also be added to such cell.
The caustic made in the chlorine cell is free of chloride, normally containing as little as 0.1 to 10 g./l.
thereof. Its concentration, which is usually from 250 to 450 g./l., may be increased by feeding dilute sodium hydroxide to the cathode compartment, recirculating sodium hydroxide solution previously taken off, increasing the electrolysis time or diminishing the rate of caustic takeoff. Alternatively, more concentrated solutions may be made by evaporation of the caustic 10 produced. Of course, when more concentrated caustic is made in the catholyte the production of chlorate in the anolyte will be increased,since more caustic escapes to the anolyte and reacts.
The present-cells lend themselves to use in both large and small plants, e.g., from 5 to 1,000 tons per day of chlorine 15 or equivalent, based on the chlorine cells'production. In such cases the efficiencies described are obtainable so as to make the process economically desirable. It is highly preferred however, that the installation should be located near to and the product should be used in conjunction with a pulp bleaching 20 plant, so that chlorate made can be employed as a bleach or in the production of a bleaching agent, e.g., chlorine dioxide, and the caustic may be employed in wood pulping operations.
The following examples illustrate but do not limit the invention. Unless otherwise indicated, all parts are by 25 weight and all temperatures are in 'C.
~ 17 , ' - ' ' . . .
~ - .. ,,, .. -1073~o2 EXAMPLE i Employing the apparatus illustrated in the Figure, sodium chlorate, essentially chloride-free sodium hydroxide, chlorine and hydrogen are manufactured from an aqueous sodium chloride solution electrochemically, sequentially utilizing ~-a chlorine cell and a chlorate cell. The chlorine cell is of asbestos-filled polypropylene, equipped with a dimensionally stable anode, and a steel cathode and the anode and cathode compartments of this two-compartment cell are separated by a cation-active permselective membrane. The single anode employed is of ruthenium oxide on titanium, with the titanium base being titanium mesh, 1 mm. in diameter, of about 50%
open area~ and the coating of ruthenium oxide being about 1 mm. thick. The anode is connected to a current source through titanium-clad copper rods. The steel cathode is of mild steel wire mesh, essentially 1 mm. in equivalent -~' diameter, having about 35% open area, and it is communi-- cated with a negative electrical sink by a copper conductor.
The membrane is manufactured by E. I. DuPont de Nemours t Company, Inc. and is sold by them as their XR-type membrane.
i` It is 7 mils thick (about 0.2 mm.) and is joined to a , ..................................................................... .
backing or supporting network of polytetrafluoroethylene (Teflon~) filaments of a diameter of about 0.1 mm.~, woven .,, into a cloth which has an area percentage of openings therein of about 22%. The membrane is initially flat and is fused onto the screen or cloth of Teflon by high temperature, high .
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107:~0Z
compression pressing, with some of the membrane portions actually flowing around the filaments during a fusion process to lock onto the cloth, without thickening the membrane between the cloth filaments, although it is thinned somewhat where it is `5 pressed against the filaments.
The material of the XR-type perms~ective membrane is a hydrolyæed copolymer of a perfluorinated hydrocarbon and a fluorosulfonated perfluorovinyl ether. The copolymer is of tetrafluoroethylene and FSO2CF2CF2OCF(CF3)CF2OCF=CF2 and has an equivalent weight in the 900 to 1,600 range, about 1,250. The electrodes are each separated about 1/8 inch from the membrane although in some processes this is increased to as much as 1/4 inch (about 6 mm.), with little change in voltage drop.
In a chlorine cell OI a type described, rated for the production of 10 tons of c h l o r i n e per day and operating .~ .
~ at 90% anode efficiency, a potential drop of 4 volts, a current
, In the FIGURE electrolytic chlorine cell 11 includes outer wall 13, anode 15, cathode 17 and conductive means 19 and 21 for connecting the anode and the cathode to sources of positive and negative electrical potentials, respectively.
Inside the walled cell cation-active permselective membrane 23 divides the volume into anode or anolyte compartment 27 and cathode or catholyte compartment 29. Alkali metal halide solu-. tion is fed to the anolyte compartment through line 33 and chloride, separated out from chlorate-chloride`solution produced in chlorate cell 35, is employed to make up halide feed to the .
.
~'`.; .
` :. - - ~: :
- - .
; ~ ~
.`a ~ :
~'~
:~ :
' ~ ' ' ' ' - `' ',' ~I ' .
~ - 3 -.. . . . .
~ `, o lOq340~ , anode compartment, being added with other chloride to resaturator 36. Water is fed to the cathode compartment 29 through line 37.
Of course, additions of electrolyte and water should be such as to maintain the desired liquid levels in the anode and cathode ` 5 compartments and this may often be effected with feed-overflow devices and similar techniques, which are known in the art and therefore, are not illustrated.
In the pre sent cell halogen, e.g., chlorine gas, is removable from the anolyte compartment through line 39 and hydrogen is removable from the catholyte compartment through line 42. A comparatively high concentration of aqueous hydroxide solution may be taken off from the catholyte through exit 43.
Because the cation-active permselective membrane 23 allows some hydroxyl ions to migrate through it from the catholyte to the anolyte these can react to produce chlorate in the anolyte and the cell liquor resulting, a mixture of chlorate and chloride in aqueous solution, is removed at 45 and transferred through line 47 to the interior 49 of chlorate cell 35. In such cell, due to the absence of any diaphragms or separators between anode 51 and cathode 53 the products of electrolysis, chlorine and - hydroxide, interact and form chlorate, possibly also with the formation of some hypochlorite. By controlling the pH in tne chlorate cell to be within the 6 to 7.5 range the production o~
chlorate can be favored. If desired, hypochlorite may be produced in the cell and converted externally to chlorate, which . . .
-. :
1 0 ~ 3~
may then be processed further as described herein.
The chlorate and chloride in solution are removed from chlorate cell 35 through line 55 after the concentration of chlorate has increased sufficiently and that of chloride is lo~J
enough so as not to be salted out in the chlorate cell. Under the conditions employed the chloride is removed from the chlorate solution as a solid in separator 57 and then passes through line 59 or other suitable transfer mechanism to resaturator 36 and back to chlorine cell ll. The chlorate is crystallized out of the solution in crystallizer 61, being removed at 63. The mother liquor remaining is sent back to the chlorine cell through line 64, preferably via resaturator 36 or is recycled via line 65.
; The chlorine taken off from chlorine cell 11 may be burned in the hydrogen produced to form hydrochl~oric acid, which may be used to adjust pH in the resaturator, cell or separating ; and crystallizing apparatuses. Also, the chlorine may be reacted externally of the cell with hydroxide removed from the cell, to produce chlorate.
Various recirculations of compartment contents, pre-., "b 20 ferably intracompartmentally, may also be employed. Although ~' continuous processes such as illustrated are highly preferred, ~` once-through processes, batch method and "hybrid" processes are also useful. --~ The ~ain aspect of the present invention is in its utilization of a single permselective membrane chlorine cell to .
~ ) o ` 10~340Z
.
make high purity, high strength caustic solution and at the same time produce some chlorate in the anolyte, which is subsequently made useful by processing the anolyte liquor through a chlorate cell and recycling back to the chlorine cell non-chiorate products.
s It has been found that this process can be effected at anode i efficiencies of over 85% and even over 90% and at caustic ' efficiencies over 75% and often over 80~.
- The selective ion-passing effects of cationic membranes ~ f ! : .' .
h a v e been noted in the past but the membranes of this invention have not been employed in the present processes before and the .. . .
unexpectedly beneficial effects resulting have not been previous-ly obtained or suggested. Thus, with the use of a comparatively `; thln membrane, preferably supported as described herein, several ,~ years o. opera~iûn under co~me,-cial conditions ar~ obtair,able .. ;
' lS without the need for removal or replacement of the membrane, :~, while all the time it efficiently prevents undesirable migration of chloride from the anode compartment to the cathode compartment, thus allowing production of high purity caustic. It prevents ; hydrogen formed on the cathode _ide from escaping into the halogen formed on the anode side and vice versa. In this respect the present membranes are superior to prior art membranes, being - more impervious to the passage of gases, even when the membranes are very thin, than various other polymeric materials. The prevention of hydrogen mixing with chlorine is important since these materials form explosive mixtures, especially in the Rresence , .
: - , ., : .
.
. .. .
o of oxygen, such as may be produced in the present processes. The superiority of the preferred membranes, including modified or surface treated versions thereof, over prior art membranes in the various described aspects is also evident, usually to a lesser degree, in the sulfostyrenated fluorinated ethylene propylene ; polymers.
The membranes employed are normally thin flat sheets, normally rectangular, but various other shapes and configurations may be employed. Plural membranes may be used together but usually this is of no special advanta.ge. Buffer compartments may be formed but are detrimental to the carrying out of the present processes. Instead of monopolar electrodes, bipolar electrodes may be utilized.
-, The aqueous solution containing chloride ions is ~15 normally a water solution of sodium chloride, although potassium `
and other soluble chlorides, e.g., magnesium chloride, may be utilized, at least in part. However, it is preferred to employ the alkali metal chlorides and of these, sodium chloride is -; the best. Similarly, the chlorates made will preferably be alkali metal chloratesand the hydroxides will be alkali metal hydroxides, most preferably all being sodium compounds.
The concentration of sodium chloride in a charge to the anolyte and in the anolyte will usually be as high as feasible, normally being from 200 to 320 grams per liter for sodium chloride and from 200 to 360 g./l. for potassium chloride, wi-th . - - -....... . .
10~
intermediates for mixtures thereof. The electrolyte may be acidified to a pH in the range of 2 to 6 but in many applications, as when hydrochloric acid is not readily available for acidification, instead of the addition of acid to provide a pH range of 2 to 6, the pH may be from 4 to 7, preferably about 6, and may be that resulting from generation of chlorine in the anolyte and its neutralization, at least in part, by sodium hydroxide. A most preferred concentration of sodium chloride in water is 250 to 300 9./1. Because the chlorine cell anolyte, containing chlorate made therein, is the feed to the chlorate cell, the chloride content of the chlorate cell liquor is less than that of the chlorine cell anolyte fed to it, due to conversion of some of the chloride to chlorine and thence to chlorate in the chlorate cell. After removal .~ of chloride and chlorate from the withdrawn chlorate cell liquor the chloride concentration will be still lower and the mother liquor ' which may be returned to the resaturator will normally be less than 50 or 100 g./l. concentration. It may contain a small-er quantity of chlorate, too.
The presently preferred cation permselective membrane is of a :''d 20 hydrolyzed copolymer of perfluorinated hydrocarbon and a fluoro-sulfonated perfluorovinyl ether. The perfluorinated hydrocarbon is preferably tetrafluoroethylene, although other perfluorinated ` and saturated and unsaturated hydrocarbons of 2 to 5 carbon atoms may also be utilized, of which the monoolefinic hydrocarbons are preferred, especially those of 2 to 4 carbon atoms.
'~
..
lOq3402 and most especially those of 2 to 3 carbon atoms, e.g., tetrafluoroethylene, hexafluoropropylene. The sulfonated perfluorovinyl ether which is most useful is that of the formula FS02CF2CF20CF~CF3)CF20CF=CF2. Such a material, named as perfluoro[2-(2-fluorosulfonylethoxy)-propyl vinyl ether], referred to henceforth as PSEPVE, may be modified to equivalent monomers~ as by modifying the internal per-; fluorosulfonylethoxy component to the corresponding propoxy component and by altering the propyl to ethyl or butyl, plus rearranging positions of substitution of the sulfonyl thereonand utilizing isomers of the perfluoro-lower alkyl groups, respectively. However, it is most preferred to employ PSEPVE.
The method of manufacture of the hydrolyzed copolymer - -is described in Example XVII of U.S. Patent 3,282~875 and an alternative method is mentioned in Canadian Patent 849,670, which also discloses the use of the finished membrane in fuel cells, characterized therein as electro-chemical cells. In short, the copolymer may be made by -reacting PSEPVE or equivalent with tetrafluoroethylene or equivalent in desired proportions in water at elevated temperature and pressure for over an hour, after which time the mix is cooled. It separates into a lower perfluoroether layer and an upper layer of aqueous medium with dispersed desired polymer. The molecular weight is indeterminate by the equivalent weight is about 900 to 1,600 preferably 1,100 . . . ~ . .
1073~02 to 1,400 and the percentage of PSEPVE or corresponding compound is about 10 to 30%, preferably 15 to 20% and most preferably about 17%. The unhydrolyzed copolymer may be compression molded at high temperature and pressure to produce sheets or membranes, which may vary in thickness from 0.02 to 0.5 mm. These are then further treated to hydrolyze pendant -S02F groups to -S03H groups, as by treating with 10% sulfuric acid or by the methods of the patents previously mentioned. The presence of the -S03H
groups may be verified by titration, as described in the Canadian patent. Additional details of various processing - -steps are described in Canadian Patent 752,427 and U. S.
~` Patent 3,041,317.
Because it has been found that some expansion accomp-anies hydrolysis of the copolymer it is preferred to posi-tion the copolymer membrane after hydrolysis onto a frame or other support which will hold it in place in the electro-lytic cell. Then it may be clamped or cemented in place and will be true, without sags. The membrane is preferably joined to the backing tetrafluoroethylene or other suitable filiments prior to hydrolysis, when it is still thermoplas-tic so that the film of copolymer covers each filament, penetrating into the spaces between the filaments and even around behind said filaments the films becoming slightly thinner in the process, where they cover the filaments.
The membrane described is far superior in the present processes to all other previously suggested membrane mater-- ials.
' '' . ~ .
, lOq340Z
It is more stable at elevated temperatures, e.g., about 75C.
It lasts for much longer time periods in the medium of the electrolytè and the caustic product and does not become brittle when subjected to chlorine at high cell temperatures. Considering the savings in time and fabrication costs, the present membranes are more economical. The voltage drop through the membrane is acceptable and does not become inordinately high, as it does with ; many other membrane materials, when the caustic concentration in the cathode compartment increases to above about 200 9./1. of caustic. The selectivity of the membrane and its compatibility with the electrolyte do not decrease detrimentally as the hydroxyl concentration in the catholyte liquor increases, as has been noted with other membrane materials. Furthermore, the caustic ` efficiency of the electrolysis does not diminish as significantly as it does with other membranes when the hydroxyl ion concentration in the catholyte increases. Thus, these differences in the present process make it practicable, whereas previously descrlbed processes have not attained commercial acceptance. While the more preferred copolymers are those having equivalent weights of 900 to 1,600, with 1,100 to 1,400 being most preferred, some useful resino~s membranes employable in present methods may be of equivalent weights from 500 to 4,000. The medium equivalent weight polymers are preferred because they are of satisfactory strength and stability, enable better selective ion exchange to take place and are of lower internal resistances, all of which are important to the present electrochemical cell.
- . , .
111~340Z
Improved versions of the above-described copolymers may be made by chemical treatment of surfaces thereof, as by treatments to modify the -S03H group thereon. For example, the sulfonic group may be altered on the membrane to produce a concentration gradient.
Such a change may be made in the manufacturing process or after production of the membrane. When effected as a subsequent surface treatment of a membrane the depth of treatment will usually be from 0.001 to 0.01 mm. Caustic efficiencies of the invented processes, using such modified versions of the present improved membranes can increase about 3 to 20%, often about 5 to 15%.
Exemplary of such treatments is that described in French patent publication 2,152,194 of March 26, 1973 in which one side of the membrane is treated with NH3 to form S02NH2 groups.
In addition to the copolymers previously discussed, including modifications thereof, it has been found that another type of membrane material is also superior to prior art films for applications in the present processes. Although it appears that tetrafluoroethylene (TFE) polymers which are sequentially styrenated and sulfonated are not useful for making satisfactory cation-active permselective membranes for use in the present electrolytic processes it has been established that perfluorinated ethylene propylene polymer (FEP) which is styrenated and sulfo-nated makes a useful membrane. Whereas useful lives of as much ~ as three years or more (that of the preferred copolymers) may not '~' - lZ -,`
o lOq3402 be obtained,the sulfostyrenated FEP's are surprisingly resistant to hardening and otherwise failing in use under the present process conditions.
; To manufacture the sulfostyrenated FEP membranes a standard FEP, such as manufach~edby E. I. DuPont de Nemours &
Co. Inc., is styrenated and the styrenated polymer is then sulfonated. A solution of styrene in methylene chloride or benzene at a suitable concentration in the range of about 10 to 20% is prepared and a sheet of FEP polymer having a thickness of about 0.02 to 0.5 mm., preferably 0.05 to 0.15 mm., is dipped into the solution. After removal it is subjected to radiation treatment, using a cobalt60 radiation source. The rate of appli-` cation may be in the range of about 8,000 rads/hr. and a total radiation application is about 0.9 megarad. After rinsing with water the phenyl rings of the styrene portion of the polymer are monosulfonated, preferably in ~ ~aposition, by treatment with chlorosulfonic acid, fuming sulfuric acid or SO3. Prefer-ably, chlorosulfonic acid in chloroform is utilized and the sulfonation is completed in about 1/2 hour.
- 20 Examples of useful membranes made by the described process are products of RAI Research Corporation, Hauppauge, New Yor~, identified as 18ST12S and 16ST13S, the former being 18% styrenated and having 2/3 of the phenyl groups monosulfonated ~nd the latter being 16~ styrenated and having 13/16 of the phenyl groups monosulfonated. To obtain 18% styrenation a solution of clemark D
!, - 13 .~ . .
.
10'~3~0Z
17 1/2X of styrene in methylene chloride is utilized and to obtain the 16X styrenation a solution of 16X of styrene in methylene chloride is employed.
The products resulting compare favorably with the ` 5 preferred copolymers previously described, giving voltage drops of about 0.2 volt each in the present cells at a current density of 2 amperes/sq. in., the same as is ob- -tained from the copolymer.
The membrane wall will nor~ally be from 0.02 to 0.5 - 10 mm. thick, preferably from 0.1 tc 0.5 mm. and most prefer-~ ably 0.1 to 0.3 mm. When the membrane is mounted on a net-`; work of material selected from the group of polytetrafluoro-ethylene, asbestos, perfluorinated ethylene, propylene polymer, polypropylene, tantalum, titanium, niobium and nob~e metals, for support, the network filaments or fibers will usually have a thickness of 0.01 to 0.5 mm., prefer-` ably 0.05 to 0.15 mm., corresponding to up to the thickness of the membrane. Often it will be preferable for the fila-menbs to be less than half the film thickness but filament thicknesses greater than that of the film may also be suc-cessfully employed, e.g., 1.1 to 5 times the film thick-ness. The networks, screens or cloths have an area per-centage of openings therein from about 8 to 80%, preferably 10 to 70X and most preferably 30 to 70X. Generally the cross-sections of the filaments will be circular but other ---shapes, such as ellipses, squares and rectangles, are also ;~ useful. The supporting network is preferably a screen or cloth and a.lthough it may be cemented to the membrane it is preferred that it be fused to it by high temperature, high pressure compression before hydrolysis of the copoly-mer. Then,the membrane-network composite can be clamped , , s~ -\~ o :10~34~;~
, ' .
or otherwise fastened in place in a holder or support.
The material of construction of the cell body may be conventional, including steel, concrete or stressed concrete lined with mastics, rubbers, e.g., neoprene, polyvinylidene chloride, FEP, chlorendic acid based polyester, polypropylene, polyvinyl chloride, TFE or other suitable plastic or may be similarly lined boxes of other structural materials. Substantial-ly self-supporting structures, such as rigid polyvinyl chloride polyvinylidene chloride,polypropylene or phenol formaldehyde resins may be employed, preferably reinforced with molded-in fibers, cloths or webs.
The migration of caustic into the anolyte compartment of the chlorine cell may be controlled by regulating the con-centration of caustic in the catholyte or by using a membrane of different thickness, more caustic being tranferred when the thick-ness is diminished. The rate of feed will determine to some ex-tent the pH in the anolyte and it is desirable to keep this in the range of 3 to 7.5, preferably 3 or 4 to 7, so as to make chlorate.
Recirculation rates may also be adjusted to help maintain the pH in the desired range and,as was mentioned previously, acids (or -~ bases) may also be utilized. On the average it is considered that a controlled proportion, from 5 to 50~ of the caustic ~! produced in the catholyte compartment, as desired, may migrate ' ~,1 .
`'' . .
~-) o `
10'~3~02 . , .
to the anolyte compartment and the cell design and components may ` be varied to obtain the particular proportion most preferred.
The pH of the chlorate cell may be regulated in similar manner.
In addition to controlling the pH's of the chlorine cell anolyte and the electrolyte of the chlorate cell the tempe-~ ratures of these are also usually regulated. Normally they are - maintained at less than 105C., preferably being from 20 to 95C., more preferably from 50 to 95~C. and most preferably about 60 or 65~C. to 85 or 95C. Usually `the chlorate cell is operated at about 70C. Electrolyte temperatures may be controlled by ~ recirculation of various portions thereof or by changing the -i proportions of feed. When the temperature cannot be lowered sufficiently by recirculation, refrigeration of the recirculating liquid(s) may also be utili~ed.
The processes of this invention, utilizing a single -~.!
cation-active permselective diaphragm in a two compartment chlorine cell, operate at comparatively high efficiencies. By holding the anolyte p~ in the range given, preferably at about 4.5, efficiencies of 80~ (caustic efficiency) and more an~ of 90%
(anode efficiency) and more are obtainable. Under such conditions, *
80% caustic efficiency and 90~ anode efficiency, two-compartment .. . . .
cellsof the type described, rated at a capacity of 1 ton per day of chlorine, will produce about 0.9 T/d of sodium t hydroxide, 0.8 T/d of chlorine and 0.05 T/d of sodium chlorate.
--,?t 25 The amount of chlorate produced will be increased, in accordance .:'.
- with the invention, by feeding the chlorine cell chlorate plus , .. . .
chIoride into a chlorate cell. Of course, additional chloride . ~ . ' ~ ! o .
.
.
may also be added to such cell.
The caustic made in the chlorine cell is free of chloride, normally containing as little as 0.1 to 10 g./l.
thereof. Its concentration, which is usually from 250 to 450 g./l., may be increased by feeding dilute sodium hydroxide to the cathode compartment, recirculating sodium hydroxide solution previously taken off, increasing the electrolysis time or diminishing the rate of caustic takeoff. Alternatively, more concentrated solutions may be made by evaporation of the caustic 10 produced. Of course, when more concentrated caustic is made in the catholyte the production of chlorate in the anolyte will be increased,since more caustic escapes to the anolyte and reacts.
The present-cells lend themselves to use in both large and small plants, e.g., from 5 to 1,000 tons per day of chlorine 15 or equivalent, based on the chlorine cells'production. In such cases the efficiencies described are obtainable so as to make the process economically desirable. It is highly preferred however, that the installation should be located near to and the product should be used in conjunction with a pulp bleaching 20 plant, so that chlorate made can be employed as a bleach or in the production of a bleaching agent, e.g., chlorine dioxide, and the caustic may be employed in wood pulping operations.
The following examples illustrate but do not limit the invention. Unless otherwise indicated, all parts are by 25 weight and all temperatures are in 'C.
~ 17 , ' - ' ' . . .
~ - .. ,,, .. -1073~o2 EXAMPLE i Employing the apparatus illustrated in the Figure, sodium chlorate, essentially chloride-free sodium hydroxide, chlorine and hydrogen are manufactured from an aqueous sodium chloride solution electrochemically, sequentially utilizing ~-a chlorine cell and a chlorate cell. The chlorine cell is of asbestos-filled polypropylene, equipped with a dimensionally stable anode, and a steel cathode and the anode and cathode compartments of this two-compartment cell are separated by a cation-active permselective membrane. The single anode employed is of ruthenium oxide on titanium, with the titanium base being titanium mesh, 1 mm. in diameter, of about 50%
open area~ and the coating of ruthenium oxide being about 1 mm. thick. The anode is connected to a current source through titanium-clad copper rods. The steel cathode is of mild steel wire mesh, essentially 1 mm. in equivalent -~' diameter, having about 35% open area, and it is communi-- cated with a negative electrical sink by a copper conductor.
The membrane is manufactured by E. I. DuPont de Nemours t Company, Inc. and is sold by them as their XR-type membrane.
i` It is 7 mils thick (about 0.2 mm.) and is joined to a , ..................................................................... .
backing or supporting network of polytetrafluoroethylene (Teflon~) filaments of a diameter of about 0.1 mm.~, woven .,, into a cloth which has an area percentage of openings therein of about 22%. The membrane is initially flat and is fused onto the screen or cloth of Teflon by high temperature, high .
~ - 18 -', ~3 .. ~ . .. . .
. . . .
' ;3 ` O
107:~0Z
compression pressing, with some of the membrane portions actually flowing around the filaments during a fusion process to lock onto the cloth, without thickening the membrane between the cloth filaments, although it is thinned somewhat where it is `5 pressed against the filaments.
The material of the XR-type perms~ective membrane is a hydrolyæed copolymer of a perfluorinated hydrocarbon and a fluorosulfonated perfluorovinyl ether. The copolymer is of tetrafluoroethylene and FSO2CF2CF2OCF(CF3)CF2OCF=CF2 and has an equivalent weight in the 900 to 1,600 range, about 1,250. The electrodes are each separated about 1/8 inch from the membrane although in some processes this is increased to as much as 1/4 inch (about 6 mm.), with little change in voltage drop.
In a chlorine cell OI a type described, rated for the production of 10 tons of c h l o r i n e per day and operating .~ .
~ at 90% anode efficiency, a potential drop of 4 volts, a current
3 density of two amperes per square inch, an anolyte NaCl concentration of about 22% (25~ NaCl solution is fed to the anode compartment), an anolyte pH of about 4.5 and an electro- r lyte temperature of about 90~C., a caustic efficiency of 80%
is obtained and the chlorine cell, in a continuous operation, produces d a i 1 y 9 to~ of sodium hydroxide, 8 tons of chlorine, -~5` (containtng about 5.3~ oxygen)and 0 .5 ton of sodium chIorate.
The hydroxide i9 an aqueous solution containing 300 g.~l.
NaOH and about 0.3g./1. NaCl. The anolyte contains 250 g./l.
of NaCl and 100 g./l. of NaClO3.
The anolyte is agitated within the anode compartment, which agitation may be effected by reclrculating it to and from such compartment directly, not illustrated in the drawing, so as ~' _ 19 .
to help to combat polarization within the compartment. A proportion of the anolyte is removed and fed to a chlorate cell for conversion of chloride therein to chlorate, and for recovery of chlorate produced in the chlorine cell anolyte.
`~ 5 The chlorate cell is a monopolar single-compartment cell having steel walls which serve as the cathode. The anode is platinum-iridium or titanium mesh, like that described for the chloride cell, with the exception that the titanium is coated with a platinum-iridium mixture, containing about three times as much platinum as iridium. The cathode, of mild steel, is like that of the chloride cell. The cell cover is of a plastic or fiberglass reinforced plastic, such as an after-chlorinated polyvinyl chloride, e.g., Trovidur HT, made by Dynamit Nobel, preferably externally reinforced with a polyester resin, more preferably of the chlorendic ester type, e.g., Hetrono3 polyester, made by Hooker Chemical Corp. The chlorate ;............... cell, rated at 100 kiloamperes, operates at 4.2 volts and 4 amperes/
~ Sq. in. current density and at a temperature of 90C. 94~ Current . ~, `-~ efficiency is obtained. It produces 1.7 tons per day of sodium~i chlorate in an aqueous solution containing 430 9./l. of sodium chlorate and 120 9./1. sodium chloride. Bipolar chlorate cells are ` also used and graphite anodes can be employed. For the metal anodes preferred operating conditions used are pH: ~-6.5; temperatures:
60-80C.i preferably about 70C.; current density: 1-6 a.s.i.; and - voltage: 3-4.8 v. For graphite anodes the ranges are 6.5-7; 30-50C., preferably about 40C.; 0.5-1.5 a.s.i.; and 3.5-4~5 v.
The aqueous solution of chloride and chlorate removed from the chlorate cell is passed to a separator wherein chloride is removed, and thence to a crystallizer, from which chlorate is removed from the mother liquor. The solid chloride is returned to ~- 30 the anode compartment of the chlorine cell after f? 0 lOq340Z
being passed througll the resaturator and is used to increase the chloride concentration of the feed to the anode compartment to about 25% sodium chloride. The mother liquor remaring after p~oduction of solid sodium chlorate is recycled back to the chlorate cell and includes about l/3 of the feed of chloride to ;~ the cell. Some of the chlorine produced is burned in hydrogen to make hydrochloric acid, which is utilized to adjust the pH of the anolyte to that desired.
` -By the described process chloride-free, high strength caustic solution (containing less than l~ NaCl, on a solids basis) is made electrolytically in the chlorine cell (because the cation-active permselective membrane prevents chloride ion from entering the catholyte) and the chlorate made in the anode compartment due ~; to reaction of migrating hydroxide is not wasted, being additive ,15 to the product of the el~strol~sis of the chlorir.e c~all-anoly~e fed to the chlorate cell. The products made, chlorine, caustic il and chlorate, are subsequently utilized in the bleaching of groundwood pulps and in processing and pulping operations for-the manufacture of papers and paperboard products.
20 In variations of this process, when the sodium ~hloride 1 concentration in the chlorine cell anode compartment is varied i,, .
over the range of from 200 to 320 grams per liter, e.g., 220 g./l. -and 310 g./l., the anolyte pH of the chlorine cell is varied -over the range of 3 to 7.5, e.g., 4, 5.5 and 7, the temperatures ~25 of both cells are varied over the range of 50 to 95C., e.g., 60C., 70C. and 85C., the voltage drops of both cells are varied over the 2.3 to 6 volt range, e.g., 3 and 5 volts for each cell, and the current density is varied in the 0.5 to 6 amperes :
~:~ o 10'~340~
.
per square inch range, e.g., 1 and 3 a.s.i. for the chlorine cell ` and 2 and 6 a.s.i. for the chlorate cell, caustic, chlorine, hydrogen and chlorate are produced at satisfactory rates, with the chlorine containing less than 7.5% of oxygen, the chlorine cell operating at an anode efficiency over 85~ and a caustic efficiency over 75%, and the chlorate cell operating at a current efficiency over 90~. Such operating conditions also result when \
the anode is replaced with a noble metal, a noble metal alloy, a noble metal oxide or a mixture of noble metal oxide and valve metal oxide, e.g., platinum, platinum-ruthenium oxide, platinum-titanium oxides,any of which is a coating on a valve metal such as titanium or tantalum. The cathode is changed to be entirely ~ graphite, iron or steel or to have surfaces of platinum, iridium, ;,- ruthenium, rhodium or other noble metal on a base metal, such as copper or steel. Such c~anges in the electrodes do not adversely ~ affect the operations of the chlorine and chlorate cells or of ;1 the overall process of Example 1. Similarly, when the materials ! of construction of the cell walls are changed to polyvinylidene chloride, synthetic rubber, polypropylene-or similar useful substance or other such lining which is resistant to the ~ . , .
electrolyte and the electrochemical reaction, the processes are also successful.
, . . .
,. . .
When the cation-active permselective membrane of the chlorine cell of Example 1 is replaced with any of various modifications thereof, having equivalent weights in the 900 to .
.
.
O
`
10~3402 1,600 ran~e, e.g., 1,100, 1,400, or when the surfaces are modified to a depth of 0.002Or 0.005 mm., as by chemical reactions with pèndant groups or additional copolymerizations, utilizing products available from the manufacturer,satisfactory chloride-free caustic `~ 5 having a content of less than l~ sodium chloride on a sodium -hydroxide solids basis is made and with the modified NF membrane the current efficiency is improved by about 5~. Successful processes are also carried out, following the method of Example 1, when the backing network for the membrane is titanium mesh ~10 or polypropylene, FEP or nylon cloth of free area in the range of from 15 to 60%, e.g., 15%, 30% and 55~, with filament sizes being about 0.1 mm. Similarly, when the thickness of the membrane is varied to 4 mils or 14 mils, the processes also are operative in the same manner as in Example 1. Using the thinnest of the ~mentioned membranes, the backing network may be coated on both sides with the membrane, in a variation of this invention.
' EXAMPLE 3 ~-The process of Example 1 is repeated except for the ~- .
replacement of the membrane with 10 mil membranes identified l~ 20as 18ST12S and 16ST13S, respectively, made by RAI Research . - .
Corporation. The same efficiencies are obtained and satisfactory caustic, chlorate and chlorine production result, as reported in Example i. The former of the RAI products is a sulfostyrenated FEP in which the FEP is 18% styrenated and has 2/3 of the phenyl ~-groups thereof monosulfonated, and the latter is 16% styrenated ' .
~ o and has 13/1`6 of the phenyl groups monosulfonated. The membranes do not stand up as well under the described operating conditions as do those of Examples 1 and 2 although they are significantly better for a longer time in appearance and operating character-` 5 istics, e.g., physical appearanCe, uniformity, voltage drop, than the various other cation-active permselective membrane materials available. The membranes do not split in use but do give increased voltage drops as use continues.
..~
' The process of this example is carried out as a continuous process , like those of Example 1 and 2 but it is also operative -, as a batch or once-through process. In such latter methods, as .~` with continuous operations, circulation in the various compart-, .~
-~ ments may be obtained by recirculating the electrolyte (merely ~J removing it from the particular compartment and pumping it back into the compartment).
The invention has been described with respect to working examples and illustrative embodiments but is not to be limited to these because it is evident that one of ordinary i~ skill in the art will be able to utilize substitutes and `~ 20 equivalents without departing from the spirit of the invention or the scope of the claims.
'' ~.
.
~', , ' `
is obtained and the chlorine cell, in a continuous operation, produces d a i 1 y 9 to~ of sodium hydroxide, 8 tons of chlorine, -~5` (containtng about 5.3~ oxygen)and 0 .5 ton of sodium chIorate.
The hydroxide i9 an aqueous solution containing 300 g.~l.
NaOH and about 0.3g./1. NaCl. The anolyte contains 250 g./l.
of NaCl and 100 g./l. of NaClO3.
The anolyte is agitated within the anode compartment, which agitation may be effected by reclrculating it to and from such compartment directly, not illustrated in the drawing, so as ~' _ 19 .
to help to combat polarization within the compartment. A proportion of the anolyte is removed and fed to a chlorate cell for conversion of chloride therein to chlorate, and for recovery of chlorate produced in the chlorine cell anolyte.
`~ 5 The chlorate cell is a monopolar single-compartment cell having steel walls which serve as the cathode. The anode is platinum-iridium or titanium mesh, like that described for the chloride cell, with the exception that the titanium is coated with a platinum-iridium mixture, containing about three times as much platinum as iridium. The cathode, of mild steel, is like that of the chloride cell. The cell cover is of a plastic or fiberglass reinforced plastic, such as an after-chlorinated polyvinyl chloride, e.g., Trovidur HT, made by Dynamit Nobel, preferably externally reinforced with a polyester resin, more preferably of the chlorendic ester type, e.g., Hetrono3 polyester, made by Hooker Chemical Corp. The chlorate ;............... cell, rated at 100 kiloamperes, operates at 4.2 volts and 4 amperes/
~ Sq. in. current density and at a temperature of 90C. 94~ Current . ~, `-~ efficiency is obtained. It produces 1.7 tons per day of sodium~i chlorate in an aqueous solution containing 430 9./l. of sodium chlorate and 120 9./1. sodium chloride. Bipolar chlorate cells are ` also used and graphite anodes can be employed. For the metal anodes preferred operating conditions used are pH: ~-6.5; temperatures:
60-80C.i preferably about 70C.; current density: 1-6 a.s.i.; and - voltage: 3-4.8 v. For graphite anodes the ranges are 6.5-7; 30-50C., preferably about 40C.; 0.5-1.5 a.s.i.; and 3.5-4~5 v.
The aqueous solution of chloride and chlorate removed from the chlorate cell is passed to a separator wherein chloride is removed, and thence to a crystallizer, from which chlorate is removed from the mother liquor. The solid chloride is returned to ~- 30 the anode compartment of the chlorine cell after f? 0 lOq340Z
being passed througll the resaturator and is used to increase the chloride concentration of the feed to the anode compartment to about 25% sodium chloride. The mother liquor remaring after p~oduction of solid sodium chlorate is recycled back to the chlorate cell and includes about l/3 of the feed of chloride to ;~ the cell. Some of the chlorine produced is burned in hydrogen to make hydrochloric acid, which is utilized to adjust the pH of the anolyte to that desired.
` -By the described process chloride-free, high strength caustic solution (containing less than l~ NaCl, on a solids basis) is made electrolytically in the chlorine cell (because the cation-active permselective membrane prevents chloride ion from entering the catholyte) and the chlorate made in the anode compartment due ~; to reaction of migrating hydroxide is not wasted, being additive ,15 to the product of the el~strol~sis of the chlorir.e c~all-anoly~e fed to the chlorate cell. The products made, chlorine, caustic il and chlorate, are subsequently utilized in the bleaching of groundwood pulps and in processing and pulping operations for-the manufacture of papers and paperboard products.
20 In variations of this process, when the sodium ~hloride 1 concentration in the chlorine cell anode compartment is varied i,, .
over the range of from 200 to 320 grams per liter, e.g., 220 g./l. -and 310 g./l., the anolyte pH of the chlorine cell is varied -over the range of 3 to 7.5, e.g., 4, 5.5 and 7, the temperatures ~25 of both cells are varied over the range of 50 to 95C., e.g., 60C., 70C. and 85C., the voltage drops of both cells are varied over the 2.3 to 6 volt range, e.g., 3 and 5 volts for each cell, and the current density is varied in the 0.5 to 6 amperes :
~:~ o 10'~340~
.
per square inch range, e.g., 1 and 3 a.s.i. for the chlorine cell ` and 2 and 6 a.s.i. for the chlorate cell, caustic, chlorine, hydrogen and chlorate are produced at satisfactory rates, with the chlorine containing less than 7.5% of oxygen, the chlorine cell operating at an anode efficiency over 85~ and a caustic efficiency over 75%, and the chlorate cell operating at a current efficiency over 90~. Such operating conditions also result when \
the anode is replaced with a noble metal, a noble metal alloy, a noble metal oxide or a mixture of noble metal oxide and valve metal oxide, e.g., platinum, platinum-ruthenium oxide, platinum-titanium oxides,any of which is a coating on a valve metal such as titanium or tantalum. The cathode is changed to be entirely ~ graphite, iron or steel or to have surfaces of platinum, iridium, ;,- ruthenium, rhodium or other noble metal on a base metal, such as copper or steel. Such c~anges in the electrodes do not adversely ~ affect the operations of the chlorine and chlorate cells or of ;1 the overall process of Example 1. Similarly, when the materials ! of construction of the cell walls are changed to polyvinylidene chloride, synthetic rubber, polypropylene-or similar useful substance or other such lining which is resistant to the ~ . , .
electrolyte and the electrochemical reaction, the processes are also successful.
, . . .
,. . .
When the cation-active permselective membrane of the chlorine cell of Example 1 is replaced with any of various modifications thereof, having equivalent weights in the 900 to .
.
.
O
`
10~3402 1,600 ran~e, e.g., 1,100, 1,400, or when the surfaces are modified to a depth of 0.002Or 0.005 mm., as by chemical reactions with pèndant groups or additional copolymerizations, utilizing products available from the manufacturer,satisfactory chloride-free caustic `~ 5 having a content of less than l~ sodium chloride on a sodium -hydroxide solids basis is made and with the modified NF membrane the current efficiency is improved by about 5~. Successful processes are also carried out, following the method of Example 1, when the backing network for the membrane is titanium mesh ~10 or polypropylene, FEP or nylon cloth of free area in the range of from 15 to 60%, e.g., 15%, 30% and 55~, with filament sizes being about 0.1 mm. Similarly, when the thickness of the membrane is varied to 4 mils or 14 mils, the processes also are operative in the same manner as in Example 1. Using the thinnest of the ~mentioned membranes, the backing network may be coated on both sides with the membrane, in a variation of this invention.
' EXAMPLE 3 ~-The process of Example 1 is repeated except for the ~- .
replacement of the membrane with 10 mil membranes identified l~ 20as 18ST12S and 16ST13S, respectively, made by RAI Research . - .
Corporation. The same efficiencies are obtained and satisfactory caustic, chlorate and chlorine production result, as reported in Example i. The former of the RAI products is a sulfostyrenated FEP in which the FEP is 18% styrenated and has 2/3 of the phenyl ~-groups thereof monosulfonated, and the latter is 16% styrenated ' .
~ o and has 13/1`6 of the phenyl groups monosulfonated. The membranes do not stand up as well under the described operating conditions as do those of Examples 1 and 2 although they are significantly better for a longer time in appearance and operating character-` 5 istics, e.g., physical appearanCe, uniformity, voltage drop, than the various other cation-active permselective membrane materials available. The membranes do not split in use but do give increased voltage drops as use continues.
..~
' The process of this example is carried out as a continuous process , like those of Example 1 and 2 but it is also operative -, as a batch or once-through process. In such latter methods, as .~` with continuous operations, circulation in the various compart-, .~
-~ ments may be obtained by recirculating the electrolyte (merely ~J removing it from the particular compartment and pumping it back into the compartment).
The invention has been described with respect to working examples and illustrative embodiments but is not to be limited to these because it is evident that one of ordinary i~ skill in the art will be able to utilize substitutes and `~ 20 equivalents without departing from the spirit of the invention or the scope of the claims.
'' ~.
.
~', , ' `
Claims (10)
PRIVILEGE IS CLAIMED IS DEFINED AS FOLLOWS:
1. A method for electrolytically manufacturing hydrox-ide, chlorine and chlorate which comprises electrolyzing an aqueous solution having a pH of about 2 to 7 and containing chloride ions in an electrolytic chlorine cell having anode and cathode compartments, an anode, a cathode, a cation-active permselective membrane of a hydrolyzed copolymer of a perfluorinated hydrocarbon and a fluoro-sulfonated perfluorovinyl ether, or of a sulfostyrenated perfluor-inated ethylene propylene polymer, defining a boundary between the cathode and anode compartments and between the anode and the cathode to produce an aqueous hydroxide solution and hydrogen in the cathode compartment and chlorine and chlorate in the anode compartment, removing the aqueous hydroxide solution and anolyte liquor containing chlorate and further electrolyzing the liquor in a chlorate cell to convert chloride herein to chlorate.
2. A method according to Claim 1 wherein the chlorine cell is of two compartments, the cation-active permselective membrane is of a hydrolyzed copolymer of tetrafluoroethylene and a fluorosulfonated perfluorovinyl ether of the formula FSO2CF2CF2OCF(CF3)CF2OCF=CF2 which copolymer has an equivalent weight of about 900 to 1,600, the concentration of sodium chloride in the chlorine cell anode compartment is from about 200 to 320 grams per liter, the anolyte pH therein is about 3 to 7.5, the aqueous hydroxide solution made in the catholyte therein is at a concentration of 250 to 450 g/l., the chlorine made contains less than 7.5% of oxygen, the anode efficiency is in excess of 85% and the caustic efficiency is greater than 75%.
3. A method according to claim 2 wherein the tempe-ratures of electrolysis in both cells are less than 105°C., the voltages are from about 2.3 to 6 volts, the current densities are from about 0.5 to 4 amperes per square inch of electrode surface, the surfaces of the cathodes are of a material selected from the group consisting of platinum, iridium, ruthenium, rhodium, graphite, iron and steel and the surfaces of the anodes at of a material selected from the group consisting of noble metals, noble metal alloys, noble metal oxides, mixtures of noble metal oxides and valve metal oxides, or mixtures thereof, on a valve metal.
4. A method according to claim 3 wherein the perm-selective membrane is from about 0.02 to 0.5 mm. in thickness and is mounted on a network of material selected from the group consisting of polytetrafluoroethylene, asbestos, perfluorinated ethylene propylene polymer, polypropylene, titanium, tantalum, niobium and noble metals, having an area percentage of openings therein from about 8 to 80%.
5. A method according to claim 4 wherein the copoly-mer equivalent weight is from about 1,100 to 1,400, the cathode is of steel and the anode is of ruthenium oxide on titanium, the aqueous sodium chloride solution electrolyte in the anode compartment is at a concentration of about 250 to 300 g./l., the pH of the anolyte is about 4.5,the temperatures of the electrolytes are in the range of 65 to 95°C., the membrane wall is from 0.1 to 0.3 mm. thick and the network is a screen or cloth of polytetrafluoroethylene filaments having a thickness of 0.01 to 0.3 mm. and having an area percentage of openings therein of 10 to 70%.
6. A method according claim 5 wherein after produc-tion of chlorate in the chlorate cell, a solution thereof is withdrawn from the cell, chloride is removed from it and chlorate is crystallized out and the chloride and mother liquor are returned to the anode compartment of the chlorine cell for electrolysis.
7. An electrolytic cell system for electrolytically manu-facuring hydroxide, chlorine and chlorate which comprises an electrolytic chlorine cell comprising a housing having an anolyte compartment, containing an anode adapted to be connected to an electrical input source; a catholyte compartment containing a cathode, a cation-active permselective membrane of a hydrolyzed copolymer of a perfluorinated hydrocarbon and a fluorosulfonated perfluorovinyl ether, or of a sulfostyrenated perfluorinated ethylene propylene polymer, defining a boundary between the catholyte and the anolyte compartments and between the anode and the cathode; outlet means from said anolyte compartment for re-moving anolyte liquor containing chlorate; and a chlorate cell for converting chloride to chlorate; said chlorate cell having inlet means connected to said outlet means for passage of said anolyte liquor from said anolyte compartment to said chlorate cell.
8. A cell system according to claim 7, wherein said anolyte compartment includes inlet means connected to a source of aqueous chloride solution; said catholyte compartment in-cludes outlet means for hydroxide solution; and said anolyte and catholyte compartments include gaseous product outlets at elevated portions of said compartments; said chlorate cell including outlet means, for chlorate and chloride containing solution, communicating with a separator for separating chlorate and chloride wherein said separator includes outlet means for chloride for recycling said chloride to said source of aqueous chloride solution.
9. A cell system according to claim 7, wherein the chlorine cell is of two compartments, the cation-active perm-selective membrane is of a hydrolyzed copolymer of tetrafluoro-ethylene and a fluorosulfonated perfluorovinyl ether of the formula FSO2CF2CF2OCF(CF3)CF2OCF=CF2 which copolymer has an equivalent weight of about 900 to 1,600.
10. A cell system according to claim 7, 8 or 9, wherein the permselective membrane is from about 0.02 to 0.5 mm. in thickness and is mounted on a network of a material selected from the group consisting of polytetrafluoroethylene, asbestos, perfluorinated ethylene propylene polymer, polypropylene, titanium, tantalum, niobium and noble metals, having an area percentage of openings therein from about 8 to 80%.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US411622A US3897320A (en) | 1973-11-01 | 1973-11-01 | Electrolytic manufacture of chlorates, using a plurality of electrolytic cells |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1073402A true CA1073402A (en) | 1980-03-11 |
Family
ID=23629673
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA211,588A Expired CA1073402A (en) | 1973-11-01 | 1974-10-17 | Electrolytic manufacture of chlorates using a plurality of electrolytic cells |
Country Status (12)
| Country | Link |
|---|---|
| US (1) | US3897320A (en) |
| JP (1) | JPS5321400B2 (en) |
| BR (1) | BR7409140D0 (en) |
| CA (1) | CA1073402A (en) |
| DE (1) | DE2451845C3 (en) |
| FI (1) | FI59816C (en) |
| FR (1) | FR2249973B1 (en) |
| GB (1) | GB1482937A (en) |
| IT (1) | IT1025404B (en) |
| NL (1) | NL7414202A (en) |
| NO (1) | NO743913L (en) |
| SE (1) | SE7413729L (en) |
Families Citing this family (38)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AR205953A1 (en) * | 1975-01-22 | 1976-06-15 | Diamond Shamrock Corp | PRODUCTION OF CARBONATES FROM METALS TO CALINES IN A MEMBRANE CELL |
| JPS5227098A (en) * | 1975-08-27 | 1977-03-01 | Osaka Soda Co Ltd | Method of simultaneous process of chlorine dioxide,chlorine gas,and ca ustic alkali. |
| JPS5230295A (en) * | 1975-09-02 | 1977-03-07 | Osaka Soda Co Ltd | Electrolytic production of alkali chlorate, caustic alkali, chlorine a nd hydrogen |
| JPS5819750B2 (en) * | 1975-11-25 | 1983-04-19 | 株式会社トクヤマ | Electrolysis method |
| US4062743A (en) * | 1975-12-22 | 1977-12-13 | Ahn Byung K | Electrolytic process for potassium hydroxide |
| US4115218A (en) * | 1976-10-22 | 1978-09-19 | Basf Wyandotte Corporation | Method of electrolyzing brine |
| US4159929A (en) * | 1978-05-17 | 1979-07-03 | Hooker Chemicals & Plastics Corp. | Chemical and electro-chemical process for production of alkali metal chlorates |
| IT1113412B (en) * | 1979-02-15 | 1986-01-20 | Oronzio De Nora Impianti | ELECTROLYTIC PROCEDURE AND EQUIPMENT FOR THE PREPARATION OF ALKALINE METAL HYPOALOGENITE |
| JPS56108887A (en) * | 1980-01-30 | 1981-08-28 | Asahi Chem Ind Co Ltd | Electrolyzing method for common salt by simultaneous use of cation exchange membrane and diaphragm |
| FI71354C (en) * | 1980-03-03 | 1986-12-19 | Asahi Chemical Ind | FOERFARANDE FOER FRAMSTAELLNING AV SATRIUMKLORAT |
| FR2655061B1 (en) * | 1989-11-29 | 1993-12-10 | Atochem | MANUFACTURE OF ALKALINE METAL CHLORATE OR PERCHLORATE. |
| SE9100365L (en) * | 1991-02-05 | 1992-08-06 | Eka Nobel Ab | PROCEDURE FOR ELECTROLYTIC PREPARATION OF ALKALIMETAL CHLORATE AND ADMINISTRATIVE CHEMICALS |
| SE512388C2 (en) * | 1993-04-26 | 2000-03-13 | Eka Chemicals Ab | Process for the preparation of alkali metal chlorate by electrolysis |
| US8216443B2 (en) * | 2002-07-05 | 2012-07-10 | Akzo Nobel N.V. | Process for producing alkali metal chlorate |
| WO2006043803A1 (en) * | 2004-09-20 | 2006-04-27 | Corsa Beheer B.V. | Combination and method for the preparation of a drink |
| DE102005038970A1 (en) * | 2005-05-11 | 2006-11-16 | Over-Eloxal Gmbh | Apparatus for treating a metal in an electrolyte bath and method for reducing aerosol delivery |
| US7891046B2 (en) * | 2006-02-10 | 2011-02-22 | Tennant Company | Apparatus for generating sparged, electrochemically activated liquid |
| US8025786B2 (en) * | 2006-02-10 | 2011-09-27 | Tennant Company | Method of generating sparged, electrochemically activated liquid |
| US8012340B2 (en) * | 2006-02-10 | 2011-09-06 | Tennant Company | Method for generating electrochemically activated cleaning liquid |
| US8007654B2 (en) * | 2006-02-10 | 2011-08-30 | Tennant Company | Electrochemically activated anolyte and catholyte liquid |
| US8016996B2 (en) * | 2006-02-10 | 2011-09-13 | Tennant Company | Method of producing a sparged cleaning liquid onboard a mobile surface cleaner |
| US8156608B2 (en) * | 2006-02-10 | 2012-04-17 | Tennant Company | Cleaning apparatus having a functional generator for producing electrochemically activated cleaning liquid |
| US8025787B2 (en) * | 2006-02-10 | 2011-09-27 | Tennant Company | Method and apparatus for generating, applying and neutralizing an electrochemically activated liquid |
| US8046867B2 (en) | 2006-02-10 | 2011-11-01 | Tennant Company | Mobile surface cleaner having a sparging device |
| KR20100041773A (en) * | 2007-06-18 | 2010-04-22 | 텐난트 컴파니 | System and process for producing alcohol |
| WO2009046279A2 (en) * | 2007-10-04 | 2009-04-09 | Tennant Company | Method and apparatus for neutralizing electrochemically activated liquids |
| WO2009149327A2 (en) * | 2008-06-05 | 2009-12-10 | Global Opportunities Investment Group, Llc | Fuel combustion method and system |
| EP2291246A2 (en) * | 2008-06-10 | 2011-03-09 | Tennant Company | Steam cleaner using electrolyzed liquid and method therefor |
| US20090311137A1 (en) * | 2008-06-11 | 2009-12-17 | Tennant Company | Atomizer using electrolyzed liquid and method therefor |
| JP5670889B2 (en) * | 2008-06-19 | 2015-02-18 | テナント カンパニー | Tubular electrolysis cell including concentric electrodes and corresponding method |
| CN102112402A (en) * | 2008-06-19 | 2011-06-29 | 坦南特公司 | Electrolysis cell having electrodes with various-sized/shaped apertures |
| WO2010028031A2 (en) * | 2008-09-02 | 2010-03-11 | Tennant Company | Electrochemically-activated liquid for cosmetic removal |
| AU2009333186A1 (en) * | 2008-12-17 | 2011-07-07 | Tennant Company | Method and apparatus for applying electrical charge through a liquid to enhance sanitizing properties |
| US20110048959A1 (en) * | 2009-08-31 | 2011-03-03 | Tennant Company | Electrochemically-Activated Liquids Containing Fragrant Compounds |
| US20110219555A1 (en) * | 2010-03-10 | 2011-09-15 | Tennant Company | Cleaning head and mobile floor cleaner |
| EP2718482B1 (en) * | 2011-06-10 | 2019-10-09 | Lumetta, Michael | System and method for generating a chlorine-containing compound |
| US10227702B2 (en) | 2014-12-05 | 2019-03-12 | Westlake Vinyl Corporation | System and method for purifying depleted brine |
| CN105821436B (en) * | 2016-05-09 | 2018-07-24 | 复旦大学 | A kind of double electrolytic cell two-step method chloric alkali electrolysis method and devices based on three-electrode system |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US665426A (en) * | 1895-09-09 | 1901-01-08 | Nat Electrolytic Company | Art of obtaining chlorates by electrolysis. |
| BE466741A (en) * | 1946-01-31 | Solvay | Process and device for the production of alkaline chlorites. | |
| NL122179C (en) * | 1959-02-06 | 1966-12-15 | ||
| US3438879A (en) * | 1967-07-31 | 1969-04-15 | Hooker Chemical Corp | Protection of permselective diaphragm during electrolysis |
| US3535215A (en) * | 1967-12-04 | 1970-10-20 | Hooker Chemical Corp | Method for operating electrolytic cells |
| US3654121A (en) * | 1968-12-23 | 1972-04-04 | Engelhard Min & Chem | Electrolytic anode |
| US3784399A (en) * | 1971-09-08 | 1974-01-08 | Du Pont | Films of fluorinated polymer containing sulfonyl groups with one surface in the sulfonamide or sulfonamide salt form and a process for preparing such |
-
1973
- 1973-11-01 US US411622A patent/US3897320A/en not_active Expired - Lifetime
-
1974
- 1974-10-17 CA CA211,588A patent/CA1073402A/en not_active Expired
- 1974-10-30 NL NL7414202A patent/NL7414202A/en unknown
- 1974-10-30 NO NO743913A patent/NO743913L/no unknown
- 1974-10-30 JP JP12607674A patent/JPS5321400B2/ja not_active Expired
- 1974-10-30 FR FR7436302A patent/FR2249973B1/fr not_active Expired
- 1974-10-31 BR BR9140/74A patent/BR7409140D0/en unknown
- 1974-10-31 GB GB47168/74A patent/GB1482937A/en not_active Expired
- 1974-10-31 FI FI3194/74A patent/FI59816C/en active
- 1974-10-31 DE DE2451845A patent/DE2451845C3/en not_active Expired
- 1974-10-31 SE SE7413729A patent/SE7413729L/xx unknown
- 1974-10-31 IT IT29064/74A patent/IT1025404B/en active
Also Published As
| Publication number | Publication date |
|---|---|
| US3897320A (en) | 1975-07-29 |
| FR2249973B1 (en) | 1978-12-22 |
| FI59816C (en) | 1983-05-30 |
| FR2249973A1 (en) | 1975-05-30 |
| BR7409140D0 (en) | 1975-08-26 |
| NL7414202A (en) | 1975-05-06 |
| JPS5321400B2 (en) | 1978-07-03 |
| JPS5089300A (en) | 1975-07-17 |
| IT1025404B (en) | 1978-08-10 |
| NO743913L (en) | 1975-05-26 |
| DE2451845B2 (en) | 1978-08-31 |
| SE7413729L (en) | 1975-05-02 |
| GB1482937A (en) | 1977-08-17 |
| FI319474A (en) | 1975-05-02 |
| DE2451845A1 (en) | 1975-05-07 |
| DE2451845C3 (en) | 1979-04-26 |
| FI59816B (en) | 1981-06-30 |
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