Document ZpX14R0z6j0Z160d6bMDZG3d

t / UNION CARBIDE CHEMICALS COMPANY DIVISION or UNION CARBIDI CORPORATION W. O. SOX 471, TCXAS CITY, TCXAS April 25, 1962 Dr. Hans Bauer Wacker Chemie, GmbH Burghausen/OBB, Abteilung 2, West Germany ,, Suspension Polyvinyl Chloride Polyerizations At High Temperature* (Methocel-15 Recipe) Dear Dr. Bauer: This letter is being sent to you to provide you with some information about our planned operations and ask you for your comments and suggestions. As you know from the Design Report information forwarded to you early in April, our new autoclaves will be capable of operating at pressures up to 200 psig. We established this pressure rating to permit us to operate at the higher temperatures without the use of trichloroethylene or other resin viscosity degraders which are normally used when the required high temperatures cannot be achieved in equipment of lower pressure rating. In addition, operation without trichloroethylene would eliminate the cost of this raw material, increase productivity of the process, and eliminate the problems of separating this additive from recovered monomer before reuse. We are planning to use your basic recipe for the HlOO/Kf series of resins using Methocel-15 suspending agent, sodium bicarbonate buffer, and dilauroyl peroxide catalyst, but we are not certain that we can operate at the higher temperatures successfully with this recipe. The following table lists the resin viscosities we plan to make. ucc 041069 Dr. Hana Bauer April 25. 1962 2, 1. Thia ia the range of reain viacoaitiea we plan to produce without trichloroethylene degrader, and the temperaturea and preaaurea involved: RESIN SPECIFIC APPROXIMATE TEMPERATURE. AUTOCLAVE VISCOSITY.V ap* K-VALUE *C PRESSURE, pais 1) 0.110 - 0.120 2) 0.140 - 0.150 3) 0. 165 - 0. 175 4) 0.175 - 0.190 5) 0. 190 - 0.205 6) 0.205 - 0.215 50 - 51 57 61 - 62 64 - 65 65.5 66.5 68 - 69 74 64 58 56 52 50 180 145 124 115 108 100 * 0.2 gxn reain in 100 ml nitrobenzene at 20*C. 11. At the preaent time we are producing theae reaina at South Charleston according to the following recipea: Specific Viacoaity. *7 ep Monomer Operating Trichloro- Catalyat. /Water Methocel Bufferv Temp. *C Ethylene.% %-- Ratio 15. % % 1) 0.110-0.120 2) 0.140-0.150 3) 0.165-0.175 4) 0.175-0.190 5) 0. 190-0.205 6) 0.205-0.215 57.5 57 57 56 52 50 2.2 1.0 0.2 None None None 0.20 0.17 0.13 0.13 0.20 0. 32 37/63 37/63 33/67 33/67 33/67 33/67 0.15 0.15 0.15 0.15 0.15 0.15 0. 15 0. 15 0.15 0.15 0. 15 0. 15 We have experienced conaiderable foaming with the two loweat viacoaity polymeri zations. 1) and 2). and believe thia ia cauaed by the uae of trichloroethylene in the charge, aince that ia the only major change in the recipe. We would like to know whether you believe the higher temperaturea (64* and 74*C) which we plan to uae will permit ua to produce good reain with the Methocel-15. sodium bicarbonate recipe. What will be the effect of theae temperaturea n the . sua pending agent and ita ability to produce the deaired reain particlea with ut agglomeration and exceaaive fiaheye formation? Would you expect any problem of maintaining a reaaonable reaction rate with dilauroyl peroxide at theae temperaturea ? Would you expect the reaid to have good heat and light atability IJCC 041070 Dr. Hans Bauer April 25, 1962 3 or b deficient in these respects? Could you suggest ways that the c ncentrations of Methocel-15, bicarbonate, and dilauroyl peroxide could ba adjusted to make high temperature polymerisation more reliable? What is th highest temperature you would recommend for dilauroyl peroxide? Can high tempera* ture reactions be maintained properly by periodic catalyst additions) in your opinion? We are presently unable to make development scale polymerisations to determine this information because our 600-gallon experimental autoclave has been dismantled for transfer here to our Texas plant. We must know whether we need to include facilities in the new plant to store and meter trichloroethylene for these lower viscosity resins, li our pres nt plans to operate without trichloroethylene are not practical. In addition, w must make provisions for the removal of trichloroethylene from recovered monomer in the event we are forced to use this degrader to produce good resin. At this time, we would prefer not to use trichloroethylene at all. but if we must. we would prefer to duplicate our present South Charleston processes than to change to other recipes using different suspending agents or surfactants such as you now use for your H100/55D resin. What provisions do you recommend for removal of trichloroethylene from recovered vinyl chloride? Please reply to me directly at the Texas City Plant: Mr. J. F. Erdmann Building 114 Union Carbide Chemicals Company P. O. Box 471 Texas City. Texas. U. S.A. 1 will be awaiting your comments on these questions with great interest. Thank you very much for your advice and help on the questions. X send you my best personal regards. Very truly yours. JFE/des J. F. Erdmann f cc: Mr. J. A. Bruton, New York Office Dr. R. P. Kurkjy. Geneva File bcc: Mr. A. R. Anderson Mr. L. B. Dampman Mr. D. L. Engle '*r. 0. A. Holt Mr. R. W. Quarles Mr. D. E. Richardson Mr. H. H. Savage Mr. C. O. Steinmetz \ .4at M. E. Sutherland Dr. D. M. Young ucc 041071