CA1180849A

CA1180849A - Sulfonic acid electrolytic cell membranes

Info

Publication number: CA1180849A
Application number: CA000379463A
Authority: CA
Inventors: Bobby R. Ezzell; William P. Carl; William A. Mod
Original assignee: Dow Chemical Co
Current assignee: Dow Chemical Co
Priority date: 1980-06-11
Filing date: 1981-06-10
Publication date: 1985-01-08
Also published as: BR8103719A; KR830006472A; KR850000100B1; AU543308B2; AU7160281A; EP0041733B1; EP0041733A1; ATE11153T1; JPH0237936B2; US4358545A; ZA813906B; JPS5725331A; DE3168122D1

Abstract

ABSTRACT

An improved polymer for use as an ion ex-change membrane in an electrolytic cell wherein the polymer has pendant chains containing sulfonic acid ion exchange groups and has an equivalent weight of between about 800 and about 1500. The polymers have a hy-dration product of less than about 22,000.

The electrolytic cell and its method of operation are described when these polymers are used as ion exchange membranes.

Description

IMPROVED SULFONIC ACID
ELECTROLYTIC CELL MEMBRANES

The present invention resides in an improved polymer for use as an ion exchange membrane in an electrolytic cell. More particularly, the polymer of the invention has pendant chains containing sulfonic aci.d ion exchanye groups and has an equivalent weight of between 800 and 1500. The polymers have a hydration product of less than about 22,000. The present invention also discloses an electrolytic cell and its method of operation when these polymers are used as ion exchange membranes.

The poly~eric materials of the invention hydrate when immersed in water or electrolytes less than sulfonic acid membranes reported in the prior art.

The electrolytic production of chlorine and caustic by the electrolysis of brine has been well known for many years. ~istorically, diaphragm cells using a hydraulically~permeable asbestos diaphragm, vacuum-deposited onto foraminous steel cathodes, have been widely commercialized. Such diaphragm cells, employing permeable diaphragms, produce NaCl-containing 28,984-F -1-NaOH catholytes because NaCl passes through the diaphra~m from the anolyte to -the catholyte. Such NaCl-containing caustic generally re~u1res a de-salting process to obtain a low-salt caustic for industrial puxposes.

In recent years, the chlor-alkali industry has focused much of its attention on developing membrane cells to produce low-salt or salt-free caustic in order to improve quality and avoid the costly desalting processes. Membranes have been developed for that purpose which are substantially hydraulically-impermeable, but which will permit hydrated Na ions to be transported from the anolyte portions, while substantially preventing transport of Cl ions. Such cells are operated by flowing a brine solution into the anolyte portion and by providing salt-free water to the catholyte portion to serve as the caustic medium. The anodic reactions and cathodic reactions are the same regardless of whether a membrane cell or a diaphragm cell is employed.

Since the disclosure of fluorocarbon polymers containing sulfonic acid functional groups (U.S. Patent ~,282,875), a great deal of progress has been made in adapting the polymers for use as membrane materials in electrochemical cells. The bulk of this work has dealt with the production of chlorine and caustic soda. The membrane materials are also applicable to caustic potash and as separators for a variety of other membrane separator applications. In chlor-alkali applications, the membrane materials can be used in cells which produce hydrogen as a co-product of the cathodic reaction producing caustic soda or they may be used in chlor-alkali cells which contain depolarized cathodes (U.S. Patent 4,035,254 and U.S. Patent 4,035,255); cells where 28,984-F -2-11C 7~ 3~

caustic soda is produced without the attendent productlon of hydrogen.

In general, the polymers have found most widespread use in the above applicatiorls when the functional group is on a fluorocarbon chain which is pendant to the main polymer backbone. Fluorocarbon sulfonlc acid pol~ners and carboxylic acid polymers have been disclosed (U.S. Patent 3,041,317 and British Patent 1,497,748) which have the functional group attached direetly to the backbone, but these polymers have found seant utility. The polymer materials, whether fluoro-earbon sulfonie acids or carboxylic acids, have in general been made by copolymerizing monomers sueh as tetrafluoroethylene or ehlorotrifluoroethylene with fluoroearbon vinyl ethers whieh contain an aeid or an aeid preeursor funetional group (U.S. Patent 3,282,875 ~nd British Patent 1,513,387).

The funetion of a membrane in a ehlor-alkali eell is to separate the produet(s) produeed at the eathode, from the produets and salt in the anolyte eompartment. The membrane must effect this separation at low eleetrieal resistanee to be economical. Three faetors prevail in measuring the effieiency at which a given membrane performs: (1) eurrent efficiency is a measure of how well the membrane prevents hydroxide ion formed in the catholyte chamber from migrating to the anolyte chamber; (2) caustic eoneentration in the eatholyte ehamber is important beeause water is evaporated from the cell produet; and (3) eell voltage, which refleets the electrieal resistanee of the membrane among other things, determines the power re~uirements of operating the eell.

28, 984-F -3-A relationship between water absorption of the polymer and usefulness of the polymer as a membrane has long been recognized (W.G.F. Grot, et al, Perfluor inated Ion Exchange Membranes, 141st National Meeting The Electrochemical Society, Houston, Texas, May, 1972). Grot disclosed that the capacity of the polymer to absorb water is a function of the equivalent weight, the history of pretreatment of the polymer and the electrolytic environment of the polymer. The e~uivalent weight is the weight of polymer which will neutralize one equivalent of base. A standard method of measuring water absorption for meaningful comparisons is given in Grot's paper (above). The method consists of boiling the polymer for 30 minutes in water with the polymer lS being in the sulfonlc acid form. The water absorbed by the pol~mer under these conditions is called the "Standard Water Absorption". The sulfonic acid membranes reported on in Grot's paper are polymers disclosed in U.S.
3,282,875.

Since the original disclosure of the sulfonic acid fluoropolvmers, and particularly in recenk years, functional groups other than sulfonic acid have received considerable attention. In fact, it has been stated

2~ that, because of excessive hydration, sulfonic acid groups cannot be used for making caustic above about 18% directly in the cell (M. Seko, "Commercial Operation of the Ion ~xchange Membrane Chlor-Alkali Process", The American Chemical Society Meeting, ~pril, 1976, New York, N.Y.). While high caustic strength is desirable as a general rule, membranes capable of high current efficiency at high caustic concentration have higher electrical resistance. Thus, even though one carboxylic acid membrane is capable of producing in excess of 30%

28,984-F -4-caustic at greater than 90% current efficiency, actual operation at 21.6% caustic was found to be more economical because of excessive electrical resis-tance at the higher caustic strengths. (M. Seko, "The Asahi Chemical Membrane Chlor-Alkali Process", The Chlorine Ins~itute, Inc., 20th Chlorine Plant Managers Seminar, New Orleans, Feb., 1977 ) . II1 addition to the many efforts to achieve higher caustic strength using carboxylic acid membranes, there has been a great deal of effort to achieve the same results with sulfonamides ~U.S. 3, 784, 399 ) .
Again, higher caustic strength is achieved only at the expense of greater power consumption whiçh is caused by higher electrical resistance of the membrane. In addition, membranes capable of higher caustic strengths are more adversely effected by impurities which enter the cell with the incoming salt feed. Thus, useful operating life of these membranes is generally less than sulfonic acid membranes.
One way of correlating functional groups to performance is to measure water of hydration per func-tional group in the polymer. Carboxylic acid polymers (U.S. 4,065,366~ and sulfonamide polymers hydrate less than sulfonic acid pol~ners, (C.J. Hora, et al, Nafion~
Membranes Structured for High Efficiency Chlor-Alkali Cells, 152nd National Meeting The Electrochemical Society, Atlanta, GA., Oct., 1977) where the polymer structures are comparable. Changes in ~unctional group concentration in a given polymer structure results in changes in the hydration water per functional group.
Thus Hora disclosed that a 1500 eq. wt. sulfonic acid polymer of given structure has less water of hydration per functional group and operates at high~r current efficiency than an 1100 e~. wt. polymer of the same 28,984-F -5-general structure. In turn, the electrlcal resistance of the 1500 eq. wt. materlal is higher than the 1100 eq. wt. material because of fewer sites to transport ions and thus to conduct current. Sulfonic acids membranes which are useful in chlor-alkali cells are taught to have eq. wts. in the range of 1100 to 1500.
In practice, e~. wts. of 1500 and 1600 are considered best for preventing migration of hydroxide ions from the catholyte to the anolyte without unreasonable cell voltage penalties (C.J. Hora, ~t al, Nafion~ ~embranes Structured for High Efficiency Chlor-Alkali Cells, 152nd National Meeting The Electrochemical Society, Atlanta, GA., Oct., 1977). Extremely thin films of these materials are required to meet the voltage requireme~ts.

Data for water absorption of sul~onic acid polymers and sulfonamide polymers has been published by Hora and Maloney in the above publication. In this paper, the polymer structures axe the same except for the substitution of sulfonamide groups for sulfonic acid groups. The data shows that, for given eq. wts., the sulfonamides absorb only 35-60% as much water as do sulfonic acids. A particular case sho~,m is a comparison of 1200 eq. wt. membranes. There, the sulfonic acid membrane absorbs about 20 moles of water per equivalent of sulfonic acid, while the sulfonam1de, from methylamine, absorbs 12~3 moles of water per equivalent of sulfonamide and the sulfonamide, from ethylenediamine, absorbs only 8.1 moles of water per equivalent of sulfonamlde. From another paper (H. Ukihashi, Ion Exchange Membrane For Chlor-Alkali Process, A~stract No. 247, American Chemical Society Meeting, Philadelphia, April, 1977) it can be calculated that a carboxylic acid membrane having an 28,984~F -6 eq. wt. of 833 absorbs 8.3 moles of wa~er per equivalent of carboxylic acid and that another having an equivalent weight of 667 absorbs 9.2 moles of water per equivalent of carboxylic acid.

In addition to the work described above ~here means for increasing caustic concentration in operating cells ~by using membranes having functional groups ihat hydrate less than sulfonic acids) are used, methods for operating the cells thems~olves that lead to increased caustic concentration have been reported. Thus, series catholyte flow (U.S. 1,284,618) and series catholyte and anolyte flow (U.S. 4,197,179) can lead to i~creased caustic strength without sacrificing either current ef-ficiency, cell voltage or nlembrane life. In addition, there are numerous applications where high strengthcaustic is not needed. In the case of caustic produced by diaphragm cells, evaporation is necessary to remove the salt in the caustic. This is not neccessary with caustic produced in membrane cells. The only need for evaporation then becomes a matter of the few appli-cations requiring high strength product and cases where the product is to be shipped over long distances.
Evaporation to high strength, such as 50%, reduces the volume to be shipped and, depending on the distance of shipment, can be more economical. Thus, it can be seen that in many applications and when series flow methods of cell operation are used, sulfonic acid membranes of the prior art and certainly improved sulfonic acid membranes axe of gxeat value.

U.S. Paten-t 4,025,405 discloses electrolytic cells having a stable, hydra-ted, selectively permeable, electrically conduc-tive membrane. The men~rane is a 28,984 F -7-g~

film of fluorinated copolymer havlng pendant sulfonic acid groups containing recurring structural units of the formula:
F
C -CF,~-n and (2)CXX'-CF2 whereR is R' - CF-cF2-o(cFy-cF2o)m~
ln which R' is F or perfluoroalkyl of 1 to 10 carbon atoms; Y is F or CF3; m is 1, 2, or 3; n is 0 or 1; X
is F, Cl, H, CF3; X' and X are CF3-(CF2)z wherein Z is 0-5; the units of formula (1) being present in an amount of from 3-20 mole percent.

In addition to the development of sulfonic acid fluoropolymers for use as membranes in electrolytic cells, the acid form of the polymers have received extensive interest as solid superacids. In general these materials have been used as strong acid catalysts for organic reactions. It has been reported that the pol~mers of -the prior art are useful for alkylation of aromatics with olefins, alkyl halides, alcohols, esters, and the like as well as esterification, ketal (acetal) formation, Diels-alder reactlons, pinacol-pinacolone rearrangement and hydration of alkyner (G. A. Olah, New Synthetic Reagents and Reactions, Aldrichimica Acta, Vol. 12, No. 3, 1979).

28,984-F -8-The figure shows the hydration product, expressed as moles of water absorbed by a mer~rane per equivalent of SO3H present in the membrane, multiplied by the e~uivalent weight of the membrane vs. the equiv-alent weight of the membrane. Curve AB shows sulfonic acid membranes of the prior art and curve CD shows membranes of the present lnvention.

The general structure of the sulfonic acid lo membranes that have received extensive attention for use in chlor-alkali cells and are sold under the trade name Nafion~ by E.I. duPont Company is as follows:

~ (CF2CF2 )X~CF-CF2 )y O

O-cF2cF2so3~
It has been discover~d that polymers having a shorter chain between the functional group and the main polymer backbone absorb less water at a given concen-tration of functional group in the polymer khan do polymers having the general structure of the prior art as shown above. Concentration of functional group in the dry polymer is measured herein, and in most of the prior art, and expressed as equivalent weight. Equiv-alent weight is defined, and conveniently determined, by standard acid~base titration, as the formula weight of the polymer having the functional group in khe acid form required to neutralize one equivalent of base.
Polymer structures representative of the present invention have substantially fluorinated backbones which have recurring pendant groups attached thereto and represented by the general formula 28,984-F -9-

3~

-O(CFRf)b(CFRf~aSO3Y

where a = O - 3 a ~ b = at least 1 Rf and Rf are independently selected from the group consisting of a halogen and a substantially fluorinated alkyl group having one or more carbon atoms Y is hydrogen or an alkali metal.

Optionally, the polymers o~ the present in-~ention may also have recurring pendant groups attached thereto represented by the general formula -OR
where R is a stxaight or a branched substantially fluorinated alkyl chain which may be interrupted by oxygen atoms.

While the general structures shown above are ~5 representative of a group of polymers of the present invention, they are not intended to limit the scope of the present invention. It would become obvious to those skilled in the art, from the relationships pre-sented h~rein that other sulfonic acid functional polymers having short pendant chains, sterically hindered sulfonate groups, or the like, would absorb less water per functional group and therefore, particularly at lower equivalent weights (<1500) perform in chlor-alkali cells in a superior manner to the polymers of -the prior art.

28,984-F -10-One polymer represented by the general structures shown above -~CF2CF2 ~ CECF2~b o s03H
when made into a film with the functional groups on one side converted to sulfonamide (U.S. 3,784,399) has been taught as useful in chlor-alkali cells. The prior art does not teach the use of the sulfonic acid form of this particular polymer nor does it provide for any information that benefits are derived by having short pendant groups. In fact, this polymer has received scant attention presumably because of the difficulty in preparing the monomer, FSO2CF2CF2OCF=CF2, necessary in making the polymer (U.S. 3,560,568).

The use of polymers of lower equivalent weight (<1500) as membranes in chlor-alkali cells is particularly beneficial. Low eq. wts. are useable only when the water of hydration per functional group is low. The performance of a chlor-alkali cell is measured by two criteria; the current efficiency (the ability to prevent the migration of hydroxide ions from the catholyte to the anolyte) and the voltage at which the cell operates. One method of expressing this as a single term is to determine the power efficiency, which is the product of the theoretical voltage divided by the actual voltage multiplied by the current efficiency.
The most common method of comparing cells is to express 28,984-F -11 the operation as kilowatt hours (K~H) of power consumed per metric ton (MT) of product produced. This expression considers both voltage (higher voltage increasing the quantity KWH) and current efficiency (lower efficiency decreasing the quantity of product produced). Thus, the lower the value KWH/mT, the better the performance of the cell.

The equivalent weight and the hydration per 1~ functional group of a polymer used as a membrane in a chlor-alkali cell have a direct influence on both of the quantities, voltage and current efficiency, that determine the overall efficiency at which a cell operates.
The water of hydration per functional group, in effect, determines the size of the channels through which ions must travel to pass through the membrane. Larger channels allow more ions to penetrate into the membrane.
Successful operation of the cell only requires that sodium ions be transported from the anolyte to the catholyte. Larger channels caused by excessive hydration lead to transport of hydroxide from catholyte to anolyte and thus a loss in current efficiency. Equivalent weig~lt determines the number of sites available to transport the sodium ions from the anolyte to the catholyte. At a given applied current to the cell, a specific number of cations must be transported for cell opera-tion. Thus, the larger the number of sites for transport, the lower electrical potential required to drive the ions.

Sulfonic acid membranes of the prior art which have long pendant chains separating the polymer backbone from the functional group, hydrate to such a large degree that equivalent weights of as low as 1100 28,984-F 12-to 1200 are not practically useable in chlor alkali cells. While the voltage required (when uslng these membranes) is relativel~ good, the curren-t efficiency ls so low that the power consumed per metric ton produced is uneconomically high. E~wivalent weights of 1500 or higher are required, as demonstrated by the prior art, to arrive at a point where hydration is low enough to achieve acceptable current efficiency, but where voltage is not yet high enough to render them impractical. The 1 present invention demonstrates that, although the above materials at higher equivalent weights are useable when compared to other methods for producing chlorine and caustic, sulfonic acid membranes that hydrate l~ss are superior in cell performance. The main defining feature of the new materials are that at a given equivalent weight hydration per functional group is lower.

Particularly preferred membranes of the present invention are hydrolyzed copolymers of tetra-fluoroethylene and FSO2CF2CF20CF=CF2. These preferred materials may also contain pendant groups introduced by the addition to the polymerization of the vinyl ether monomers represented by ROCF=CF2 where R is preferrably ~5 XCF2CF2CF2- or XCF2CF2CF20CFCF2-where X = Cl or F. Equivalent weights of the membranes of the present invention are between 800 and 1500 and preferably between 800 and 1300. The preferred hydration per sulfonic acid functional group is between about 10 and 25 moles of water per e~uivalent of sulfonic acid.
More preferred is between ll and 19 moles of water per equivalent of sulfonic acid. Hydration per sulfonic 28,984-F -13-acid equivalent ls determined by measuring the water absorption of a given weight of dry polymer by the procedure described by Grot for the "Standard Water Absorption". From this, the amount of water absorbed by the weight representing one sulfonic acid equivalent is determined and thus the moles o~ water per sulfonic acid e~uivalent.

It has been found that a convenient and meaningful description of the polymer membranes that incorporates both the equivalent weight and the water absorpton is in terms of hydxation product. The hydratior product is expressed as moles of water per functional group, and the equivalent weight. Since both of these factors are critical to membrane performance it is particularly useful to combine the two into one term.
The hydration product of the polymer of the invention is below about 22,000. The sulfonic acid membranes of the present invention preferably have a hydration ~ product falling between 12,000 and 18,000 whereas the sulfonic acid membranes of the prior art have hydration products falling between 22,000 and 30,000. It is to be understood that any sulfonic acid membrane havin~
suitable mechanical and physical properties and a hydration produc-t falling between 12,000 and 22,000 would be expected to perform well in a chlor-alkali cell.

Many of the properties described above for use of the polymers of the present invention as mem-branes also apply to one of the polymers as solid superacids for acid catalyst. It is extremely important to have as high an acid concentration (low eguivalent weight) as practical in the sulfonic acid polymers used 28,984~F -14-as acid catalyst. A low equivalent weight rneans that a smaller volume (or weight) of the acid would be requlred, thus reducing the size of reactors and/or reaction time. A short pendant group and/or low hydration results in polymers with better physical properties at low equivalent weights than the polymers of the prior art having long pendant groups. Thus the polymers of the present invention having hydration products falling below about 22,000 and particularly those lC having equivalent weights of 800 to 1,300 have high acid concentration, good physical characteristics and as such should be superior solid super acids useful as acid catalyst.
Example 1 A series of ion exchange membranes were prepared and evaluated to determine the equivalent weight of each membrane and its hydration product.

2Q The wa-ter absorption was determined for each membrane by first drying the membrane in the SO3H form film for 16 hours at 110C, weighing the sample, boiling the sample for 30 minutes in wacer, blotting the surface dry with towels and then re-weighing the film. The difference in weight represents the amount of water absorbed by the film and is commonly referred to as the "Standard Water Absorption".

A sample of each film was cut into 1/16 inch to 1/8 inch wide strips and weighed. Each strip was placed into a beaker having an excess of 0.05 normal NaOH solution and heated for 30 minutes at 50C. Each film was then rinsed two times for 15 minutes in 75 ml portions of deionized wa-ter at 50C. Each strip was 28,984~F -15-removed and the rinse solutions were combined with the original caus~ic solution. l'he cornbined solution was titrated with a 0.1 normal HCl solution and the number of equivalents of NaOH consumed by the fllm ~7as determined.

The equivalent weight of each film was deter-mined by dividing the weight of the film by the number of equivalents of caustic consumed.

The water absorption per functional group was then determined by calculating the moles of water that one equivalent of the polymer absorbed. The hydration product was obtained by multiplying the equivalent weight by the moles of water absorbed by one equivalent of the polymer.

The following copolymer and terpolymer mem-branes of the present invèntion were evaluated in the manner just descrlbed and the results are shown in the following table:

28,984-F -16-water Hydration Equivalent Absorption Product Polymer ~ Moles H2O/SO3H X 1000 1 798 36.8 29.4 2 827 21.8 18.0 3 1154 18.6 21.5

4 1340 12.7 17.0 1666 8.7 14.5 6 89~ 18.4 16.4 7 1217 13.1 15.9 8 1350 11.4 15.3 Hydrolyzed copolymer of tetrafluoroethylene and FSO2CF2CF20CF = CF2 Hydrolyzed terpolymer of tetrafluoroethylene, FS02CF2CF20CF = CF2 and ClCF2CF2CF20CF = CF2 Hydrolyzed terpolymer of tetrafluoroethylene, FS02CF2CF20CF = CF2 and ClCF2CF2CF20CFCF20CF=CF2 CF2Cl These results are shown by curve CD of the drawing.

The hydration product for membranes of the prior art were calculated in a like manner from the numbers published by Gxot (see Background of the Invention) and are presented here and represented by curve AB on the drawing.

28,984-F -17-Equiva ent Weiqht Hydration Product Xl000 850 ~9.~
1000 25.4 1200 23.9 1400 23.7 1600 22.4 Example 2 A portion of the ion exchange membranes of Example 1, having a thickness of from 8 to 9 mils were individually tested in a small electrolytic cell. The cell had an anode and a cathode with the ion exchange membrane which was being evaluated positioned there-between, thus separating the cell into an anode chamber and a cathode chamber. Each electrode had a square shape and had an area of 8.63 square inches. Each electrode had a solid, metal stud welded to it. Each stud passéd through a wall of the cell and was provided with leak proof seals. Both studs were connected to a power supply. The stud connected to the anode was constructed of titanium, while the stud connected to the cathode was constructed of steel. The anode, ltself, was an expanded titanium mesh screen coated with a Ruo2-Tio2 mixture, while the cathode was con-structed from ~oven steel wires.

The anode chamber was filled with a saturated NaCl brine solution (approximately 25 weight percent NaCl) and the catholyte chamber was filled with a caustic solution having approximately 12 weight percent NaOH concentration. The cell was energized by applying a constant current of approximately 8.63 amps, to give a current density of 1.0 amps per s~uare inch of 28,984-F -18-electrode area. A satura-ted brine solution (ap-proximately 25 weight percent NaCl) was flowed lnto the anode chamber at a rate sufficient to maintain the concentration of the anolyte leaving the cell at approximately 17-20 weight percent NaCl. Deionized water was flowed into the catholyte chamber, in a similar manner, at a rate sufficient to maintain the catholyte leaving the cell at a desir~d NaOH concen-tration. During the evaluation of each membrane, the NaOH concentration was varied in order to determine the cell operation over a range of caustic concentrations.

The température of the cell was controlled throughout each evaluation at about ~0C by means of an immersion heater connected to a thermocouple inserted into the anolyte chamber. During the evaluation of each membrane the cell voltage was constantly monitored by measuring the difference in voltage potential between the anode stud and the cathode stud. For each ~ evaluation, the cell was operated for several days to reach equilibrium. Then current efficiency was determined by collecting the catholyte leaving the cell for a ~iven period of time, usually 16 hours, and determining the amount of NaOH actually produced, as compared to the amount theoretically produced at the applied current.

Before the evaluation of each membrane, the following preparatory procedures were followed:
(1) the acid form of each membrane was dried in an o~en and then e~uilibrated at ambient conditions;
(2) the membrane was soaked in a 30 weiyht % solution of triethanolamine in water for 30 minutes at 25C;

28,984-F -19-(3) the membrane was removed from the solution and air dried; and (4) the membrane was installed in the above described electrolytic cell.
s The follo~ing results were obtained:

Power Requirement (DCKWH/MT) Polymer 10% NaOH 15% NaOH

Direct current kilowatt hours per metric ton of caustic.

From the foregoing description and examples, the present invention resides in an ion exchange membrane ~5 having an equivalent weight of at least 800 and having a hydration product with 15 percent of curve CD in the figure.

It is also an object of the present invention to provide for an ion exchange me~rane having an equivalent weiyht of at least 800 and a hydration product falling within 10 percent and preferably 15 percent of the curve CD in the figure.

28,984-F -20-

Claims

-21-.

THE EMBODIMENTS OF THE INVENTION IN WHICH AN EXCLUSIVE
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:

1. A polymer comprising a fluorinated backbone structure which has pendant groups containing sulfonic acid ion exchange groups, wherein the polymer has an equivalent weight of between 800 and 1500 and a hydration product of less than about 22,000.

2. The polymer of Claim 1 wherein the polymer has a hydration product of from 12,000 to 18,000.

3. The polymer of Claims 1 or 2, wherein the polymer has an equivalent weight of between 800 and 1300.

4. The polymer of, Claim 1 which is an ion ex-change membrane having an equivalent weight of at least 800 and a hydration product falling at least 20% below the curve AB in the figure.

5. The polymer of Claim 1 which is an ion ex-change membrane having an equivalent weight of at least 800 and having a hydration product within 15% of curve CD in the figure.

6. The polymer of Claim 1, having recurring pendant groups attached thereto and represented by the formula where a = O - 3 b = O - 3 a + b = at least 1 Rf and Rf are independently selected from the group consisting Of a halogen and a substantially fluorinated alkyl group having one or more carbon atoms Y is hydrogen or an alkali metal.

7. The polymer of Claim 6 which also has recurring pendant groups attached to the backbone represented by the formula where R is a straight or branched sub-stantially fluorinated alkyl chain which may be interrupted by oxygen atoms.

8. The polymer of Claims 6 or 7 wherein the polymer has a hydration product of from 12,000 to less than 18,000.

9. The polymer of Claim 6 or 7 wherein the polymer has an equivalent weight of between 800. and 1300.

10. An electrolytic cell comprising, an anode in an anode chamber; a cathode in a cathode chamber; an ion exchange membrane separating the cathode chamber from the anode chamber; wherein the ion exchange membrane is the polymer of

Claim 1.