CHLOROSULFONATION OF CHLORINATED POLYETHYLENE

Abstract: Chlorosulfonated polyethylene materials having (a) mo­ lecular weight of from about 40,000 to 300,000, (b) a chemically combined chlorine content of from 20 to 50 percent by weight of polymer, (c) a chemically combined sulfur content of from 0.8 to 2.5 percent by weight of polymer and (d) a 100 percent modulus of from 0.6 to 4.8 MPa are prepared in an anhydrous process wherein an amorphous chlorinated polyethylene start­ ing material is first fluidized and then exposed to a gaseous mixture of sulfur dioxide and chlorine having a ratio of sulfur di­ oxide to chlorine of from 1:1 to 16:1 in the presence of a chlo­ rine free radical generator such as ultraviolet light at a temper­ ature of from 25° to 100°C for a period of two hours or less.

Description: This invention relates to novel chlorosulfonated polyethylene materials and methods of preparation thereof. More particularly, the present invention relates to a finely-divided, particulate chlorosulfonated material having a weight average molecular weight of from 40,000 to 300,000 and a 100 percent modulus, measured in accordance with American Society for Testing and Materials (ASTM) Test D-412 of from 0.6 to 4.8 megapascals (MPa). Chlorosulfonated polyethylene materials in general and various processes for preparing such materials are known. chlorosulfonated polymers are manufactured commercially in an inert volatile solvent by simultaneously (a) chlorinating polyethylene to replace hydrogen by chlorine and (b) reacting the chlorinated polyethylene with a mixture of chlorine and sulfur dioxide to introduce chlorosulfonic groups into the chlorinated polymer. This procedure is described in detail in U S -A- 3,296,222 issued to Dixon et al. Chlorosulfonation of a polyethylene starting material with sulfuryl chloride in a single phase in solution is described in U S -A- 3,299,014. Chlorosulfonation in solution is not, however, a problem-free process. Solvents used in commerical processes to dissolve both polyethylene and the chlorosulfonated product are generally not volatile enough to be vaporized by the heat of reaction. Accordingly, it is necessary to heat the mixture of solvent and chlorinated product to remove the solvent. This is a slow and expensive procedure. Noeske et al., in U S -A- 2,889,259, disclose a process for the chlorosulfonation of a polyethylene starting material having a molecular weight of 80,000 to 1,400,000. The process involves fluidization of the starting material with a gaseous mixture of sulfur dioxide and chlorine at a temperature not substantially in excess of 100°C. Introduction of the gaseous mixture with ultraviolet light may enhance the chloro-sulfonation reaction. The temperature is generally within the range of 40° to 80°C. The gaseous mixture typically has a ratio of sulfur dioxide to chlorine of 1:1 to 2:1. The process provides reaction products having a sulfur content as high as 10 percent by weight and a chlorine content as high as 20 percent by weight. Noeske et al. state that treatment with gaseous chlorine before and/or after chloro-sulfonation raises the chlorine content to as high as 50 percent by weight. Chlorosulfonated materials prepared in accordance with the teachings of Noeske et al. are generally not amorphous materials. That is, the materials have sufficient residual crystallinity to render them relatively inflexible and non-elastomeric. Eckardt et al., in U S -A- 3,542,746, disclose a two-stage process for preparing high molecular weight chlorosulfonated polyethylene. In a first stage, high density, high molecular weight polyethylene is chlorinated to a chlorine content of 20 to 50 percent by weight using a procedure which reduces crystallinity of the polymer to less than one percent as determined by differential thermal analysis. In a second stage, the chlorinated polymer is treated with a mixture of sulfur dioxide and chlorine to substitute sulfonyl chloride groups on the polymer. This treatment is carried out at a temperature of 0 to 100°C, either in the dark or catalyzed with actinic light, with a ratio of sulfur dioxide to chlorine in the range of 20:1 to 1:10. The two-stage process produces polymers which are substantially amorphous and which contain 25 to 50 percent by weight of chlorine and 0.6 to 1.5 percent by weight of sulfur. By "high molecular weight" Eckardt et al. refer to weight average molecular weights in the range of 500,000 to 5,000,000, preferably 700,000 to 3,500,000. Chlorosulfonated materials prepared in accordance with the teachings of Eckardt et al. have been found to be difficult, if not impossible, to process on equipment generally used in the rubber industry such as two-roll compounding mills and high intensity mixers. In one aspect, the present invention is a novel chlorosulfonated polyethylene material which is readily processable on equipment generally used in the rubber industry. The material has several distinguishing physical properties and characteristics. First, it has a sulfur content of from 0.61 to 2.5, preferably from 0.8 to 2.5 percent by weight of polymer. Second, it has a chlorine content of from 20 to 50 percent by weight of polymer. Third, it has a weight average molecular weight of from 40,000 to 300,000. Fourth, it has a 100 percent modulus, measured in accordance with ASTM Test D-412, of from 0.6 to 4.8 mPa. Fifth, it has an ultimate tensile strength measured in accordance with ASTM Test D-412, of from 0.7 to 17.9 MPa. Sixth, it has an ultimate elongation measured in accordance with ASTM Test D-412, of from 200 to greater than 1000 percent. Finally, it has a relative crystallinity, as measured by X-ray diffraction, from 0 to 15 percent. In a second aspect, the present invention is an anhydrous process for preparing finely-divided, particulate chlorosulfonated polyethylene material. The process comprises fluidizing a finely-divided, pulverulent free-flowing chlorinated polyethylene starting material which is generally free of water and oxygen, said starting material (1) being prepared from high density polyethylene having a molecular weight of from 40,000 to 300,000 and (2) having (a) a chlorine content of from 20 to 48 percent by weight of polymer, (b) a 100 percent modulus, measured in accordance with ASTM Test D-412, of from 0.5 to 4.8 MPa, and (c) a relative crystallinity as measured by X-ray diffraction, of from 0 to 15 percent, the starting material with a gaseous mixture of sulfur dioxide and chlorine while said starting material is in the presence of chlorine free radicals, the gaseous mixture having a ratio of sulfur dioxide to chlorine of from 1:1 to 16:1, and the chlorine free radicals being generated by a ultraviolet light radiation having a wavelength sufficient to generate chlorine free radicals or by chemical free radical initiators, at a temperature within a temperature range of from 20° to 100°C and for a period of time sufficient to obtain chlorosulfonated polyethylene having a sulfur content of from 0.61 to 2.5 preferably from 0.8 to 2.5 percent by weight of polymer and a chlorine content of from 20 to 50 percent by weight of polymer. A suitable method of removing water and oxygen from the starting material is to purge the starting material with an inert gas such as nitrogen. The chlorinated polyethylene starting materials suitable for purposes of the present invention are finely-divided particles which must meet four physical property criteria. First, the materials must have a weight average molecular weight of from 40,000 to 300,000. Second, the materials must have a chemically combined chlorine content of from 20 to 48 percent by weight of polymer. Third, the materials must have a 100 percent modulus measured in accordance with ASTM Test D-412, from 0.5 to about 4.8 MPa. Fourth, the materials must have a relative crystallinity of from 0 to 15 percent. Chlorinated polyethylene materials meeting the aformentioned physical property criteria can be prepared by a chlorination procedure of the type disclosed in U S -A- 3,454,544. Satisfactory chlorinated polyethylene resins are readily obtained by practice of a chlorination procedure which comprehends suspension chlorination in an inert medium of a finely divided, essentially linear polyethylene or olefin interpolymer. The interpolymer contains at least 90 mole percent ethylene with the remainder being one or more ethylenically unsaturated monomers polymerizable therewith. The polymer is first chlorinated at a temperature below its agglomeration temperature for a period sufficient to provide a partially chlorinated polymer having a chlorine content of from 2 to 23 percent chlorine, based on the total weight of polymer. This is followed by sequential suspension chlorination of the partially chlorinated polymer, in a particulate form, at a particular temperature. The particular temperature is, with respect to the olefin interpolymer, above its agglomeration temperature but at least 2°C below its crystalline melting point. Sequential chlorination is continued for a period sufficient to provide a chemically combined Chlorine content of up to 48 percent by weight of polymer. Useful ethylenically unsaturated monomers include non-aromatic hydrocarbon olefins having 3 or more carbon atoms such as propylene, 1-butene, 1,4-hexadiene, 1,5-hexadine, 1-octene, 1,7-octadiene and 1,9-decadiene; substituted olefins such as acrylic acid and acrylic acid esters; alkenyl aromatic compounds such as styrene and its derivatives, and other known polymerizable materials. The temperature at which chlorination normally leads to agglomeration of polymer particles depends to a large extent on the nature and molecular weight of the polymer to be chlorinated. In the case of crystalline and predominantly straight chain polyethylenes having a branching of the chains of less than 1 methyl group per 100 carbon atoms and a density of at least 0.94 grams per cubic centimeter, the temperature is above 95°C, in particular above 100°C or even above 110°C. In the case of polyethylenes having a relatively marked branching of the chains and a lower density, the temperature is lower, 65°C. The temperature employed in the sequential chlorination must be greater than that employed in the initial chlorination in order to prevent (a) retention of excessive undesirable crystallinity and (b) formation of non-uniformly chlorinated polymer. The temperature employed in the sequential chlorination must also be below the crystalline melting point of the polymer being chlorinated in order to prevent accelerated particle size growth and development of undesirable agglomeration of polymer particles. After a polyolefinic material has been suspension chlorinated to a desired degree, it may easily be filtered from suspension in the inert suspending liquid and washed and dried to prepare it for subsequent use. The present invention is not restricted to chlorinated polyethylene resins prepared by suspension or slurry chlorination procedures. Solution chlorination and bulk, or fluidized bed, chlorination procedures may also be used provided the polymers produced thereby meet the aforementioned requirements with regard to chlorine content and residual crystallinity. The chlorinated polyethylene starting materials are treated with a gaseous mixture of sulfur dioxide and chlorine to substitute sulfonyl chloride groups on the polymer. This treatment is suitably carried out at a temperature of from 20° to 100°C by passing the gaseous mixture through the chlorinated polyethylene particles, as in a fluidized bed reactor, in the presence of a chlorine free-radical generator. The temperature at which the starting materials are treated is beneficially within a temperature range of from 20° to 80°C. The temperature is desirably within a temperature range of from 20° to 50°C. The temperature is preferably within a temperature range of from 20° to 45°C. A temperature of from 25° to 35°C is particularly preferred. It has been found that, with all other reaction parameters being equal, lower reaction temperatures are more conducive to increased rates of sulfonation than higher reaction temperatures. The gaseous mixture has a ratio of sulfur dioxide to chlorine which is suitably from 1:1 to 16:1, beneficially from 1:1 to 8:1, and preferably from 1:1 to 4:1. It has been found that at ratios of from 1:1 to 8:1, rates of sulfonation are greater than they are for ratios greater than 8:1. Ratios as great as 32:1 and even higher can be used if desired. They are counter-productive, however, because the rate of sulfonation is greater at lower ratios. Ratios of less than about 1:1 may be used but they are undesirable because they favor chlorination over sulfonation. If an accelerated rate of chlorosulfonation is desired, the reaction may be assisted by the employment of ultraviolet light and/or small quantities of a chlorine free-radical generating catalyst. The ultraviolet light has a wavelength suitable for generating chlorine free-radicals. Ultraviolet light alone is generally sufficient to produce satisfactory results. A catalyst, where used, must have certain characteristics in order to be suitable for purposes of the present invention. First, it must be capable of contacting or being intimately admixed with the chlorinated polyethylene starting materials. Second, it must be active over at least a portion of the temperature range used for treating the starting material with the gaseous mixture. Third, it must be sufficiently active to allow reasonable amounts thereof to be used. Various azo-type compounds and peroxides, such as tertiary butyl peroxide are suitable free-radical catalysts. Preparation of chlorosulfonated polyethylene materials is accomplished within a time period which is beneficially from 15 to 120, desirably from 15 to 70 and preferably from 15 to 35 minutes. A time period of less than 15 minutes is not sufficient to attain the desired sulfur content. A time period of greater than 120 minutes may be used. It is, however, neither necessary nor economical. The chlorosulfonated polyethylene produced in accordance with the present invention has a chlorine content which is beneficially from 20 to 50, preferably from 25 to 42 percent by weight of polymer. The chlorosulfonated polyethylene prepared in accordance with the present invention has a sulfur content which is from 0.61 to 2.5, beneficially from 0.8 to 2.5, desirably from 0.9 to 1.4 and preferably from 1.0 to 1.2 percent by weight of polymer. The chlorosulfonated polyethylene prepared in accordance with the present invention has a weight average molecular weight which is beneficially from 40,000 to 300,000, desirably from 90,000 to 250,000 and preferably from 120,000 to 180,000. When the compositions of the invention contain a vulcanizing package, the package may include magnesium oxide or lead oxide and preferably a high activity magnesium oxide for toxicological reasons, and optionally, one or more sulphur-containing accelerators such as mercaptobenzothiazole, benzothiazyl disulphide or dipentamethylene thiuram tetrasulphide. Magnesium oxide, when used, is present in an amount of from 3 to 7 parts by weight. Lead oxide, when used, is present in an amount of from 10 to 30 parts by weight. Sulphur-containing accelerators are generally used in amounts of from 0.5 up to 3 parts by weight. All parts by weight being based on 100 parts by weight of polymer. Other vulcanizing packages known by those skilled in the art to be suitable for vulcanizing chlorosulfonated polyethylene may also be used. The compositions of the invention may also contain fillers, such as carbon black, mineral fillers or carbon black-mineral filler mixtures, various processing aids and antioxidants. Illustrative fillers other than carbon black include titanium dioxide, barium sulfate, kaolin clay, diatomaceous earth, powdered talc and calcium sulfate. Suitable processing aids may include the well-known plasticizers and softeners such as low molecular weight polyethylenes, the aromatic hydrocarbon resins, polyethylene glycol and aromatic hydrocarbon oils. Antioxidants may be readily selected from among those well-known in the art. The following examples are for purposes of illustration. All parts and percentages are by weight unless otherwise stated. First Chlorosulfonation Apparatus A General Electric model RS sunlamp was spaced apart from a vertically arranged 2.5 cm diameter PYREX TM tube having an effective length of 40 cm. A porous sintered glass plate was fitted into one end (hereinafter referred to as the "bottom end") of the tube. The term "effective length", as used herein, means a length immediately above the sintered plate which is exposed to ultraviolet light. A gas supply line was connected to the bottom end of the tube. The gas supply line was connected to (a) a gaseous chlorine supply line, (b) a gaseous sulfur dioxide supply line and (c) a gaseous nitrogen supply line. The gas supply line was also fitted with an overpressure relief valve. By a suitable arrangement of check valves, a ratio of gaseous sulfur dioxide to gaseous chlorine could be established. Similarly, gaseous nitrogen rather than a mixture of sulfur dioxide and chlorine could be supplied. A cap connected to a scrubber was fitted into a second end (hereinafter referred to as the "top end") of the tube. The first chlorosulfonation apparatus had a capacity of 30 grams of polymer. A gas flow rate of 0.3 meters per second was sufficient to fluidize 30 grams of polymer. Second Chlorosulfonation Apparatus An ultraviolet light source was spaced apart from a PYREX TM tube having a diameter of 10 cm, a length of 90 cm and an effective length of 25 cm. The light source was either (a) the General Electric model RS sunlamp or (b) a Spectraline model CL100 ultraviolet spotlight having a 100 watt bulb and emitting ultraviolet light at a nominal wavelength of 3600 Angstroms. A 30-cm portion of the inside of one end (hereinafter referred to as the "bottom end") of the tube was covered with a 0.16 cm sheet of a fluorinated ethylenepropylene fluorocarbon polymer commercially available from E. I. DuPont de Nemours and Co. under the trade designation TEFLON TM . A truncated hollow right cylinder conical insert made of polytetrafluoroethylene was fitted into the bottom end of the tube. The conical insert had a large opening and a small opening. The large opening had a diameter of 10 cm. The large opening was positioned so that it was remote from rather than proximate to the bottom end of the tube. The small opening had a diameter of 3.3 cm and was positioned so that it was proximate to the bottom end of the tube. Adjacent to the conical insert and arranged so as to cover the bottom end of the tube was a screen assembly. The screen assembly had four layers arranged as follows: (a) a 200 mesh screen of polytetrafluoroethylene; (b) a woven mat made of glass fibers, commercially available from Owens-Corning Fiberglas Corporation under the trade designation FIBERGLASS TM ; (c) a 400-mesh stainless steel screen; and (d) a 20 mesh stainless steel screen. Layer (a) was placed next to the conical insert. A metal funnel having the larger opening adjacent layer (d) of the screen assembly was connected to the bottom end of the tube. The effective length was measured from the screen assembly rather than from the sintered glass plate as in the first apparatus. The stem or small opening of the funnel was connected to a gas supply line which in turn was connected to an overpressure relief valve set at 0.35 MPa, a gaseous chlorine supply line, a gaseous sulfur dioxide supply line, and a gaseous nitrogen supply line. By a suitable arrangement of check valves and blocking valves, a ratio of gaseous chlorine to gaseous sulfur dioxide could be established. Similarly, gaseous nitrogen rather than the mixture of gaseous chlorine and gaseous sulfur dioxide could be supplied via the gas supply line. One thermocouple was placed inside the tube near the screen assembly to measure powder temperature. A second thermocouple was placed inside the metal funnel to measure inlet temperature of the nitrogen gas or nitrogen/halogen gas mixture. A cap connected to a scrubber was fitted with a second end of the tube (hereinafter referred to as the "top end"). The second apparatus had a capacity of 450 grams. Blend Used to Test for Vulcanization Activity The following blend of materials was used to determine whether a polymer was suitable for use as a chlorosulfonated polyethylene material: An oscillating disk rheometer was used to check blends of materials for vulcanization activity by measuring change in torque. Torque measurements were made in accordance with ASTM Test D-2084 at a temperature of 160° and a frequency of oscillation of 1.7 Hertz with an arc of three degrees. The change in torque, or Delta T, was determined by subtracting the minimum torque from the maximum torque. Example 1 - preparation of Chlorosulfonated Polyethylene of the Present Invention The first chlorosulfonation apparatus was loaded with 30 grams of a chlorinated polyethylene starting material. The chlorinated polyethylene was made from high density polyethylene having a nominal weight average molecular weight of 240,000. The chlorinated polyethylene had a nominal chemically combined chlorine content of 36 percent of polymer weight, a 100 percent modulus of one MPa and a relative crystallinity of less than two percent. It was commercially available from The Dow Chemical Company under the trade designation CPE 3615. The chlorinated polyethylene starting material was purged with gaseous nitrogen for a period of 30 minutes. The nitrogen had a temperature of 30°C and was supplied at a rate of 0.3 meters per second which was sufficient to fluidize the starting material. The nitrogen purge was used to remove generally all oxygen and atmospheric moisture from the starting material. After the 30 minute period, the gaseous nitrogen flow was stopped. The starting material was then re-fluidized with a flow of a gaseous mixture of sulfur dioxide and chlorine having a ratio of sulfur dioxide to chlorine of 16:1. The flow was adjusted for good fluidization a flow rate of 0.3 meters per second. The sunlamp was turned on for a period of 2 hours while the starting material continued to be fluidized with the gaseous mixture at a temperature of 30°C. After the period of 2 hours, the sunlamp and the flow of the gaseous mixture was discontinued. The polymer was then fluidized again with a flow of gaseous nitrogen for a period of 30 minutes at a temperature of 40°C to remove acid gases. After the period of 30 minutes, the gaseous nitrogen flow was stopped and the polymer was recovered. The material prepared in this Example 1 was compared with the chlorinated polyethylene starting material (hereinafter referred to as "Comparative Example A") for vulcanization activity using the blend and rheometer identified hereinabove. The blend prepared with the material produced in Example 1 showed a torque gain or Delta torque of 88.1 deciNewton.Meter (dN.M) whereas that prepared with the material of Comparative Example A showed a torque gain of only 2.3 dN.M. These blends and a third blend prepared with a chloro-sulfonated polyethylene material commercially available from E. I. DuPont de Nemours & Company under the trade designation HYPALON TM 40 (hereinafter designated as "Comparative Example B") were subjected to physical property testing. Comparative Example B showed a torque gain of 86.5 dN.M. The physical property tests are set forth in Table I. The results of the testing are presented in Table II. The data presented in Table II shows that the material prepared in Example 1 responded well to a typical chlorosulfonated polyethylene vulcanization package. Chlorinated polyethylene (Comparative Example A), on the other hand, did not respond well as the data is characteristic of a non-crosslinked polymer. Similar results are obtained with other chlorosulfonated polymers prepared in accordance with the present invention. Examples 2-4 and Comparative Examples C-D - Reaction Time Study Using the second chlorosulfonation apparatus, the procedure set forth for Example 1 was duplicated except that the time interval was varied as shown in Table III. Torque gain is shown in Table III under the column headed Delta T. The data presented in Table III clearly shows two points. First, sulfonation occurred rapidly. A predominant proportion of the sulfonation occurred within the first 30 minutes. Second, straight chlorination of the starting material did not occur at a rate sufficient to significantly change the chlorine content of the polymer. Similar results are obtained with other starting materials and reaction parameters, also hereinabove specified. Examples 5-7 and Comparative Example E - Effect of Ultraviolet Light Study Using the second chlorosulfonation apparatus, the procedure set forth in Example 1 was duplicated except that the ultraviolet light source was varied. The light source used is shown in Table IV together with sulfur and chlorine content of the resultant polymers. The following code is used to represent the light source: A - The General Electric Model RS sunlamp B - The Spectraline Model CL100 spotlight The data presented in Table IV amply demonstrates that ultraviolet light enhances the sulfonation reaction. Similar results are obtained with other chlorosulfonated polyethylenes which are representative of the present invention. Examples 8-9 and Comparative Example F - Effect of Ratio of Sulfur Dioxide to Chlorine Study Using the second chlorosulfonation apparatus, the procedure set forth in Example 1 was duplicated except that the ratio of sulfur dioxide to chlorine was varied and a different chlorinated polyethylene starting material was used. The ratio is shown in Table V together with the sulfur and chlorine content of the resultant polymers. The chlorinated polyethylene starting material had (1) a nominal chemically combined chlorine content of 39 percent of polymer weight, (2) a 100 percent modulus of 2.2 MPa and (3) a relative crystallinity of less than two percent. It was prepared by chlorinating high density polyethylene having a molecular weight of 153,000. The chlorinated polyethylene was commercially available from The Dow Chemical Company under the trade designation CPE 631. The code used in Examples 5-7 above to represent the light source is also used in Table V. The data presented in Table V clearly shows the marked effect which the ratio of sulfur dioxide to chlorine has upon the final polymer product. Contrary to what might otherwise be expected, a low sulfur dioxide to chlorine ratio results in a more rapid sulfonation reaction and a higher final sulfur content than a high sulfur dioxide to chlorine ratio. Similar results are obtained with other ratios and with other starting materials as specified hereinabove in conjunction with other reaction parameters, also as specified hereinabove.

Claims: An anhydrous process for preparing finely-divided, particulate chlorosulfonated polyethylene, said process comprising fluidizing finely-divided, pulverulent, free-flowing chlorinated polyethylene starting material which is generally free of water and oxygen, said starting material (1) being prepared from high density polyethylene having a molecular weight of from 40,000 to 300,000, and (2) having (a) a chlorine content of from 20 to 48 percent by weight of polymer, (b) a 100 percent modulus of from 0.5 to 4.8 MPa and (c) a relative crystallinity of from 0 to 15 percent , as measured by X-ray diffraction, and reacting said chlorinated polyethylene starting material with a gaseous mixture of sulfur dioxide and chlorine while said starting material is in the presence of chlorine free radicals, the gaseous mixture having a ratio of sulfur dioxide to chlorine of from 1:1 to 16:1, and the chlorine free radicals being generated by ultraviolet light radiation having a wavelength sufficient to generate chlorine free radicals or by chemical free radical initiators, at a temperature within the range of from 20°C to 100°C for a period of time sufficient to obtain chlorosulfonated polyethylene having a sulfur content of from 0.61 to 2.5 percent by weight of polymer and a chlorine content of from 20 to 50 percent by weight of poylmer. The process of Claim 1 wherein the period of time is from 15 to 120 minutes. The process of Claim 1 wherein the temperature is within the range of from 20° to 80°C. The process of Claim 1 wherein the chlorosulfonated polyethylene has a sulfur content of from 0.9 to 1.4 percent by weight of polymer. The process of Claim 1 wherein the chlorosulfonated polyethylene has a chlorine content of from 25 to 42 percent by weight of polymer. The process of Claim 1 wherein the chlorosulfonated polyethylene has a molecular weight of from 90,000 to 250,000. The process of Claim 1 wherein the ratio of sulfur dioxide to chlorine is from 1:1 to 8:1. A finely-divided, particulate, chlorosulfonated polyethylene material, characterized in that the material has (1) a sulfur content of from 0.61 to 2.5 percent by weight of polymer, (2) a chlorine content of from 20 to 50 percent by weight of polymer, (3) a molecular weight from 40,000 to 300,000, (4) a 100 percent modulus (ASTM D-412) of from 0.6 to 4.8 MPa and (5) an ultimate tensile strength (ASTM D-412) of from 0.7 to 17.9 MPa and (6) an ultimate elongation (ASTM D-412) of from 200 to greater than 100 percent and (7) a relative crystallinity as measured by X-ray diffraction of from 0 to 15 percent. The chlorosulfonated polyethylene material of Claim 8 wherein the sulfur content is from 0.9 to 1.4 percent by weight of polymer. The chlorosulfonated polyethylene material of Claim 8 wherein the sulfur is from 1.0 to 1.2 percent by weight of polymer. The chlorosulfonated polyethylene material of Claim 8 wherein the chlorine is from 25 to 42 percent by weight of polymer. The chlorosulfonated polyethylene material of Claim 8 wherein the molecular weight is from 90,000 to 250,000.

Inventors: BLANCHARD, ROBERT A.
Applicants: THE DOW CHEMICAL COMPANY
Application year: 1985
Main classification: C08F8
IPC codes: C08F8